IPS-E-PR- 771(1)
FOREWORD
The Iranian Petroleum Standards (IPS) reflect
the views of the Iranian Ministry of Petroleum
and are intended for use in the oil and gas
production facilities, oil refineries, chemical and
petrochemical plants, gas handling and
processing installations and other such facilities.
IPS is based on internationally acceptable
standards and includes selections from the items
stipulated in the referenced standards. They are
also supplemented by additional requirements
and/or modifications based on the experience
acquired by the Iranian Petroleum Industry and
the local market availability. The options which
are not specified in the text of the standards are
itemized in data sheet/s, so that, the user can
select his appropriate preferences therein.
The IPS standards are therefore expected to be
sufficiently flexible so that the users can adapt
these standards to their requirements. However,
they may not cover every requirement of each
project. For such cases, an addendum to IPS
Standard shall be prepared by the user which
elaborates the particular requirements of the
user. This addendum together with the relevant
IPS shall form the job specification for the
specific project or work.
The IPS is reviewed and up-dated approximately
every five years. Each standards are subject to
amendment or withdrawal, if required, thus the
latest edition of IPS shall be applicable
The users of IPS are therefore requested to send
their views and comments, including any
addendum prepared for particular cases to the
following address. These comments and
recommendations will be reviewed by the
relevant technical committee and in case of
approval will be incorporated in the next revision
of the standard.
Standards and Research department
No.19, Street14, North kheradmand
Karimkhan Avenue, Tehran, Iran .
Postal Code- 1585886851
Tel: 88810459-60 & 66153055
Fax: 88810462
Email: Standards@nioc.org
‫ﭘﻴﺶ ﮔﻔﺘﺎر‬
‫( ﻣﻨﻌﻜﺲ ﻛﻨﻨﺪه دﻳﺪﮔﺎﻫﻬﺎي‬IPS) ‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻧﻔﺖ اﻳﺮان‬
‫وزارت ﻧﻔﺖ اﻳﺮان اﺳﺖ و ﺑﺮاي اﺳﺘﻔﺎده در ﺗﺄﺳﻴﺴﺎت ﺗﻮﻟﻴﺪ‬
‫ واﺣﺪﻫﺎي ﺷﻴﻤﻴﺎﻳﻲ و‬،‫ ﭘﺎﻻﻳﺸﮕﺎﻫﻬﺎي ﻧﻔﺖ‬،‫ﻧﻔﺖ و ﮔﺎز‬
‫ ﺗﺄﺳﻴﺴﺎت اﻧﺘﻘﺎل و ﻓﺮاورش ﮔﺎز و ﺳﺎﻳﺮ ﺗﺄﺳﻴﺴﺎت‬،‫ﭘﺘﺮوﺷﻴﻤﻲ‬
.‫ﻣﺸﺎﺑﻪ ﺗﻬﻴﻪ ﺷﺪه اﺳﺖ‬
‫ ﺑﺮاﺳﺎس اﺳﺘﺎﻧﺪاردﻫﺎي ﻗﺎﺑﻞ ﻗﺒﻮل‬،‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻧﻔﺖ‬
‫ﺑﻴﻦاﻟﻤﻠﻠﻲ ﺗﻬﻴﻪ ﺷﺪه و ﺷﺎﻣﻞ ﮔﺰﻳﺪهﻫﺎﻳﻲ از اﺳﺘﺎﻧﺪاردﻫﺎي‬
‫ ﻫﻤﭽﻨﻴﻦ ﺑﺮاﺳﺎس ﺗﺠﺮﺑﻴﺎت‬.‫ﻣﺮﺟﻊ در ﻫﺮ ﻣﻮرد ﻣﻲﺑﺎﺷﺪ‬
‫ﺻﻨﻌﺖ ﻧﻔﺖ ﻛﺸﻮر و ﻗﺎﺑﻠﻴﺖ ﺗﺄﻣﻴﻦ ﻛﺎﻻ از ﺑﺎزار داﺧﻠﻲ و ﻧﻴﺰ‬
‫ ﻣﻮاردي ﺑﻄﻮر ﺗﻜﻤﻴﻠﻲ و ﻳﺎ اﺻﻼﺣﻲ در اﻳﻦ‬،‫ﺑﺮﺣﺴﺐ ﻧﻴﺎز‬
‫ ﻣﻮاردي از ﮔﺰﻳﻨﻪﻫﺎي ﻓﻨﻲ ﻛﻪ در‬.‫اﺳﺘﺎﻧﺪارد ﻟﺤﺎظ ﺷﺪه اﺳﺖ‬
‫ﻣﺘﻦ اﺳﺘﺎﻧﺪاردﻫﺎ آورده ﻧﺸﺪه اﺳﺖ در داده ﺑﺮگﻫﺎ ﺑﺼﻮرت‬
‫ﺷﻤﺎره ﮔﺬاري ﺷﺪه ﺑﺮاي اﺳﺘﻔﺎده ﻣﻨﺎﺳﺐ ﻛﺎرﺑﺮان آورده ﺷﺪه‬
.‫اﺳﺖ‬
‫ ﺑﺸﻜﻠﻲ ﻛﺎﻣﻼً اﻧﻌﻄﺎف ﭘﺬﻳﺮ ﺗﺪوﻳﻦ ﺷﺪه‬،‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻧﻔﺖ‬
.‫اﺳﺖ ﺗﺎ ﻛﺎرﺑﺮان ﺑﺘﻮاﻧﻨﺪ ﻧﻴﺎزﻫﺎي ﺧﻮد را ﺑﺎ آﻧﻬﺎ ﻣﻨﻄﺒﻖ ﻧﻤﺎﻳﻨﺪ‬
‫ﺑﺎ اﻳﻦ ﺣﺎل ﻣﻤﻜﻦ اﺳﺖ ﺗﻤﺎم ﻧﻴﺎزﻣﻨﺪيﻫﺎي ﭘﺮوژه ﻫﺎ را‬
‫ در اﻳﻦ ﮔﻮﻧﻪ ﻣﻮارد ﺑﺎﻳﺪ اﻟﺤﺎﻗﻴﻪاي ﻛﻪ ﻧﻴﺎزﻫﺎي‬.‫ﭘﻮﺷﺶ ﻧﺪﻫﻨﺪ‬
‫ اﻳﻦ‬.‫ﺧﺎص آﻧﻬﺎ را ﺗﺄﻣﻴﻦ ﻣﻲﻧﻤﺎﻳﺪ ﺗﻬﻴﻪ و ﭘﻴﻮﺳﺖ ﻧﻤﺎﻳﻨﺪ‬
‫ ﻣﺸﺨﺼﺎت ﻓﻨﻲ آن ﭘﺮوژه‬،‫اﻟﺤﺎﻗﻴﻪ ﻫﻤﺮاه ﺑﺎ اﺳﺘﺎﻧﺪارد ﻣﺮﺑﻮﻃﻪ‬
.‫و ﻳﺎ ﻛﺎر ﺧﺎص را ﺗﺸﻜﻴﻞ ﺧﻮاﻫﻨﺪ داد‬
‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻧﻔﺖ ﺗﻘﺮﻳﺒﺎً ﻫﺮ ﭘﻨﺞ ﺳﺎل ﻳﻜﺒﺎر ﻣﻮرد ﺑﺮرﺳﻲ‬
‫ در اﻳﻦ ﺑﺮرﺳﻲﻫﺎ ﻣﻤﻜﻦ اﺳﺖ‬.‫ﻗﺮار ﮔﺮﻓﺘﻪ و روزآﻣﺪ ﻣﻲﮔﺮدﻧﺪ‬
‫اﺳﺘﺎﻧﺪاردي ﺣﺬف و ﻳﺎ اﻟﺤﺎﻗﻴﻪاي ﺑﻪ آن اﺿﺎﻓﻪ ﺷﻮد و ﺑﻨﺎﺑﺮاﻳﻦ‬
.‫ﻫﻤﻮاره آﺧﺮﻳﻦ وﻳﺮاﻳﺶ آﻧﻬﺎ ﻣﻼك ﻋﻤﻞ ﻣﻲ ﺑﺎﺷﺪ‬
‫ درﺧﻮاﺳﺖ ﻣﻲﺷﻮد ﻧﻘﻄﻪ ﻧﻈﺮﻫﺎ و‬،‫از ﻛﺎرﺑﺮان اﺳﺘﺎﻧﺪارد‬
‫ﭘﻴﺸﻨﻬﺎدات اﺻﻼﺣﻲ و ﻳﺎ ﻫﺮﮔﻮﻧﻪ اﻟﺤﺎﻗﻴﻪاي ﻛﻪ ﺑﺮاي ﻣﻮارد‬
‫ ﻧﻈﺮات و‬.‫ ﺑﻪ ﻧﺸﺎﻧﻲ زﻳﺮ ارﺳﺎل ﻧﻤﺎﻳﻨﺪ‬،‫ﺧﺎص ﺗﻬﻴﻪ ﻧﻤﻮدهاﻧﺪ‬
‫ﭘﻴﺸﻨﻬﺎدات درﻳﺎﻓﺘﻲ در ﻛﻤﻴﺘﻪﻫﺎي ﻓﻨﻲ ﻣﺮﺑﻮﻃﻪ ﺑﺮرﺳﻲ و در‬
‫ﺻﻮرت ﺗﺼﻮﻳﺐ در ﺗﺠﺪﻳﺪ ﻧﻈﺮﻫﺎي ﺑﻌﺪي اﺳﺘﺎﻧﺪارد ﻣﻨﻌﻜﺲ‬
.‫ﺧﻮاﻫﺪ ﺷﺪ‬
‫ ﻛﻮﭼﻪ‬،‫ ﺧﺮدﻣﻨﺪ ﺷﻤﺎﻟﻲ‬،‫ ﺧﻴﺎﺑﺎن ﻛﺮﻳﻤﺨﺎن زﻧﺪ‬،‫ ﺗﻬﺮان‬،‫اﻳﺮان‬
19 ‫ ﺷﻤﺎره‬،‫ﭼﻬﺎردﻫﻢ‬
‫اداره ﺗﺤﻘﻴﻘﺎت و اﺳﺘﺎﻧﺪاردﻫﺎ‬
1585886851 : ‫ﻛﺪﭘﺴﺘﻲ‬
66153055 ‫ و‬88810459 - 60 : ‫ﺗﻠﻔﻦ‬
88810462 : ‫دور ﻧﮕﺎر‬
Standards@nioc.org
:‫ﭘﺴﺖ اﻟﻜﺘﺮوﻧﻴﻜﻲ‬
: ‫ﺗﻌﺎرﻳﻒ ﻋﻤﻮﻣﻲ‬
General Definitions:
Throughout this Standard
definitions shall apply.
the
following
Company :
Refers to one of the related and/or affiliated
companies of the Iranian Ministry of Petroleum
such as National Iranian Oil Company, National
Iranian
Gas
Company,
and
National
Petrochemical Company etc.
Purchaser :
Means the "Company" Where this standard is
part of direct purchaser order by the "Company",
and the "Contractor" where this Standard is a part
of contract documents.
Vendor And Supplier:
Refers to firm or person who will supply and/or
fabricate the equipment or material.
Contractor:
Refers to the persons, firm or company whose
tender has been accepted by the company.
Executor :
Executor is the party which carries out all or part
of construction and/or commissioning for the
project.
Inspector :
The Inspector referred to in this Standard is a
person/persons or a body appointed in writing by
the company for the inspection of fabrication and
installation work
Shall:
Is used where a provision is mandatory.
Should
Is used where a provision is advisory only.
Will:
Is normally used in connection with the action
by the “Company” rather than by a contractor,
supplier or vendor.
May:
Is used where a provision is completely
discretionary.
.‫در اﻳﻦ اﺳﺘﺎﻧﺪارد ﺗﻌﺎرﻳﻒ زﻳﺮ ﺑﻪ ﻛﺎر ﻣﻲ رود‬
: ‫ﺷﺮﻛﺖ‬
‫ﺑﻪ ﺷﺮﻛﺖ ﻫﺎي اﺻﻠﻲ و واﺑﺴﺘﻪ وزارت ﻧﻔﺖ ﻣﺜﻞ ﺷﺮﻛﺖ ﻣﻠﻲ‬
‫ ﺷﺮﻛﺖ ﻣﻠﻲ ﺻﻨﺎﻳﻊ‬،‫ ﺷﺮﻛﺖ ﻣﻠﻲ ﮔﺎز اﻳﺮان‬،‫ﻧﻔﺖ اﻳﺮان‬
.‫ﭘﺘﺮوﺷﻴﻤﻲ و ﻏﻴﺮه اﻃﻼق ﻣﻴﺸﻮد‬
:‫ﺧﺮﻳﺪار‬
‫ﻳﻌﻨﻲ "ﺷﺮﻛﺘﻲ" ﻛﻪ اﻳﻦ اﺳﺘﺎﻧﺪارد ﺑﺨﺸﻲ از ﻣﺪارك ﺳﻔﺎرش‬
‫ﺧﺮﻳﺪ ﻣﺴﺘﻘﻴﻢ آن "ﺷﺮﻛﺖ" ﻣﻴﺒﺎﺷﺪ و ﻳﺎ "ﭘﻴﻤﺎﻧﻜﺎري" ﻛﻪ اﻳﻦ‬
. ‫اﺳﺘﺎﻧﺪارد ﺑﺨﺸﻲ از ﻣﺪارك ﻗﺮارداد آن اﺳﺖ‬
:‫ﻓﺮوﺷﻨﺪه و ﺗﺎﻣﻴﻦ ﻛﻨﻨﺪه‬
‫ﺑﻪ ﻣﻮﺳﺴﻪ و ﻳﺎ ﺷﺨﺼﻲ ﮔﻔﺘﻪ ﻣﻴﺸﻮد ﻛﻪ ﺗﺠﻬﻴﺰات و ﻛﺎﻻﻫﺎي‬
. ‫ﻣﻮرد ﻟﺰوم ﺻﻨﻌﺖ را ﺗﺎﻣﻴﻦ ﻣﻴﻨﻤﺎﻳﺪ‬
:‫ﭘﻴﻤﺎﻧﻜﺎر‬
‫ ﻣﻮﺳﺴﻪ و ﻳﺎ ﺷﺮﻛﺘﻲ ﮔﻔﺘﻪ ﻣﻴﺸﻮد ﻛﻪ ﭘﻴﺸﻨﻬﺎدش‬، ‫ﺑﻪ ﺷﺨﺺ‬
.‫ﺑﺮاي ﻣﻨﺎﻗﺼﻪ و ﻳﺎ ﻣﺰاﻳﺪه ﭘﺬﻳﺮﻓﺘﻪ ﺷﺪه اﺳﺖ‬
:‫ﻣﺠﺮي‬
‫ﻣﺠﺮي ﺑﻪ ﮔﺮوﻫﻲ اﻃﻼق ﻣﻲ ﺷﻮد ﻛﻪ ﺗﻤﺎم ﻳﺎ ﻗﺴﻤﺘﻲ از‬
.‫ﻛﺎرﻫﺎي اﺟﺮاﻳﻲ و ﻳﺎ راه اﻧﺪازي ﭘﺮوژه را اﻧﺠﺎم دﻫﺪ‬
:‫ﺑﺎزرس‬
‫در اﻳﻦ اﺳﺘﺎﻧﺪارد ﺑﺎزرس ﺑﻪ ﻓﺮد ﻳﺎ ﮔﺮوﻫﻲ اﻃﻼق ﻣﻲ ﺷﻮد ﻛﻪ‬
‫ﻛﺘﺒﺎً ﺗﻮﺳﻂ ﻛﺎرﻓﺮﻣﺎ ﺑﺮاي ﺑﺎزرﺳﻲ ﺳﺎﺧﺖ و ﻧﺼﺐ ﺗﺠﻬﻴﺰات‬
.‫ﻣﻌﺮﻓﻲ ﺷﺪه ﺑﺎﺷﺪ‬
:‫ﺑﺎﻳﺪ‬
.‫ﺑﺮاي ﻛﺎري ﻛﻪ اﻧﺠﺎم آن اﺟﺒﺎري اﺳﺖ اﺳﺘﻔﺎده ﻣﻴﺸﻮد‬
:‫ﺗﻮﺻﻴﻪ‬
.‫ﺑﺮاي ﻛﺎري ﻛﻪ ﺿﺮورت اﻧﺠﺎم آن ﺗﻮﺻﻴﻪ ﻣﻴﺸﻮد‬
:‫ﺗﺮﺟﻴﺢ‬
‫ﻣﻌﻤﻮﻻً در ﺟﺎﻳﻲ اﺳﺘﻔﺎده ﻣﻲﺷﻮد ﻛﻪ اﻧﺠﺎم آن ﻛﺎر ﺑﺮاﺳﺎس‬
.‫ﻧﻈﺎرت ﺷﺮﻛﺖ ﺑﺎﺷﺪ‬
: ‫ﻣﻤﻜﻦ اﺳﺖ‬
. ‫ﺑﺮاي ﻛﺎري ﻛﻪ اﻧﺠﺎم آن اﺧﺘﻴﺎري ﻣﻴﺒﺎﺷﺪ‬
IPS-E-PR- 771(1)
ENGINEERING STANDARD
FOR
PROCESS REQUIREMENTS
OF
HEAT EXCHANGING EQUIPMENT
FIRST REVISION
OCTOBER 2009
‫اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ‬
‫ﺑﺮاي‬
‫اﻟﺰاﻣﺎت ﻓﺮآﻳﻨﺪي‬
‫ﺗﺠﻬﻴﺰات ﺗﺒﺎدل ﺣﺮارت‬
‫وﻳﺮاﻳﺶ اول‬
1388 ‫ﻣﻬﺮ‬
This Standard is the property of Iranian Ministry of Petroleum.
All rights are reserved to the owner. Neither whole nor any
part of this document may be disclosed to any third party,
reproduced, stored in any retrieval system or transmitted in
any form or by any means without the prior written consent of
the Iranian Ministry of Petroleum.
‫ ﺗﻤﺎم ﺣﻘﻮق آن ﻣﺘﻌﻠﻖ ﺑﻪ‬.‫اﻳﻦ اﺳﺘﺎﻧﺪارد ﻣﺘﻌﻠﻖ ﺑﻪ وزارت ﻧﻔﺖ اﻳﺮان اﺳﺖ‬
‫ ﺗﻤﺎم ﻳﺎ‬،‫ﻣﺎﻟﻚ آن ﺑﻮده و ﻧﺒﺎﻳﺪ ﺑﺪون رﺿﺎﻳﺖ ﻛﺘﺒﻲ وزارت ﻧﻔﺖ اﻳﺮان‬
‫ ذﺧﻴﺮه‬،‫ ﺑﻪ ﻫﺮ ﺷﻜﻞ ﻳﺎ وﺳﻴﻠﻪ ازﺟﻤﻠﻪ ﺗﻜﺜﻴﺮ‬، ‫ﺑﺨﺸﻲ از اﻳﻦ اﺳﺘﺎﻧﺪارد‬
.‫ ﻳﺎ روش دﻳﮕﺮي در اﺧﺘﻴﺎر اﻓﺮاد ﺛﺎﻟﺚ ﻗﺮار ﮔﻴﺮد‬،‫ اﻧﺘﻘﺎل‬،‫ﺳﺎزي‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
CONTENTS:
Page
No
0. INTRODUCTION.....................................................3
IPS-E-PR- 771(1)
:‫ﻓﻬﺮﺳﺖ ﻣﻄﺎﻟﺐ‬
3.............................................................................. ‫ ﻣﻘﺪﻣﻪ‬-0
1. SCOPE ..........................................................................4
4.................................................................... ‫ داﻣﻨﻪ ﻛﺎرﺑﺮد‬-1
2. REFERENCES ..........................................................4
4............................................................................. ‫ ﻣﺮاﺟﻊ‬-2
3. DEFINITIONS AND TERMINOLOGY ........... 5
5................................................................. ‫ ﺗﻌﺎرﻳﻒ و واژﮔﺎن‬-3
3.1 Definitions of Different Types of Heat
Exchangers............................................................... 5
5................. ‫ ﺗﻌﺎرﻳﻒ اﻧﻮاع ﻣﺨﺘﻠﻒ ﻣﺒﺪﻟﻬﺎي ﺣﺮارﺗﻲ‬1-3
3.2 Definition of TEMA Classes............................ 10
10...................................TEMA ‫ ﺗﻌﺎرﻳﻒ ﻃﺒﻘﻪ ﺑﻨﺪي‬2-3
4. SYMBOLS & ABBREVIATIONS ......................11
11..................................................... ‫ ﻧﺸﺎﻧﻪ ﻫﺎ و اﺧﺘﺼﺎرات‬-4
5. UNITS ...........................................................................12
12............................................................................ ‫ واﺣﺪﻫﺎ‬-5
PART I PROCESS DESIGN OF SHELL AND
TUBE HEAT EXCHANGERS:
:‫ ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪﻟﻬﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬I ‫ﺑﺨﺶ‬
6. General Considerations.............................................. 13
13............................................................... ‫ ﻣﻼﺣﻈﺎت ﻋﻤﻮﻣﻲ‬- 6
7. GENERAL REQUIREMENTS ............................. 18
18...................................................................‫ اﻟﺰاﻣﺎت ﻋﻤﻮﻣﻲ‬-7
7.1 Fluid Allocation .................................................. 18
18........................................................ ‫ اﺧﺘﺼﺎص ﺳﻴﺎل‬1-7
7.2 Installation ............................................................ 19
19......................................................................... ‫ ﻧﺼﺐ‬2-7
7.3 Nozzle Location................................................... 20
20................................................................ ‫ ﻣﺤﻞ ﻧﺎزل‬3-7
7.4 Impingement Baffles and Erosion
Protection............................................................... 20
20.................. ‫ ﺻﻔﺤﺎت ﺑﺮﺧﻮردي و ﻣﺤﺎﻓﻆ ﺳﺎﻳﺸﻲ‬4-7
7.5 Geometrical .......................................................... 22
22.......................................................‫ آراﻳﺶ ﻫﻨﺪﺳﻲ‬5-7
8. BASIC RELATIONS .................................................. 30
30........................................................................... ‫ رواﺑﻂ ﭘﺎﻳﻪ‬-8
8.1 Fluid Temperature Relations ......................... 30
30......................................................‫ رواﺑﻂ دﻣﺎي ﺳﻴﺎل‬1-8
8.2 Fouling....................................................................... 30
30......................................................... ‫ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬2-8
9. THERMAL DESIGN .................................................. 36
36................................................................... ‫ ﻃﺮاﺣﻲ ﺣﺮارﺗﻲ‬-9
1
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
9.1 Pressure Drop ........................................................ 36
36.................................................................... ‫ اﻓﺖ ﻓﺸﺎر‬1-9
9.2 Design Velocities................................................... 36
36..................................................... ‫ ﺳﺮﻋﺘﻬﺎي ﻃﺮاﺣﻲ‬2-9
9.3 Exchanger Design Pressures and
Temperatures .......................................................... 36
36............................ ‫ دﻣﺎﻫﺎ و ﻓﺸﺎرﻫﺎي ﻃﺮاﺣﻲ ﻣﺒﺪل‬3-9
PART II PROCESS DESIGN OF PLATE HEAT
EXCHANGERS (PLATE FIN
EXCHANGERS):
‫ ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪﻟﻬﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻬﺎي‬II ‫ﺑﺨﺶ‬
:(‫)ﻣﺒﺪﻟﻬﺎي ﺻﻔﺤﻬﺎي ﭘﺮه دار‬
10. PLATE FIN EXCHANGERS .............................41
41........................................... ‫ ﻣﺒﺪﻟﻬﺎي ﺻﻔﺤﻬﺎي ﭘﺮه دار‬-10
11. APPLICATION .......................................................41
41........................................................................... ‫ ﻛﺎرﺑﺮد‬-11
12. MATERIAL ..............................................................44
44............................................................................. ‫ ﺟﻨﺲ‬-12
13. CONSTRUCTION..................................................44
44...........................................................................‫ ﺳﺎﺧﺖ‬-13
14. ADVANTAGES .......................................................44
44............................................................................ ‫ ﻓﻮاﻳﺪ‬-14
15. DISADVANTAGES ...............................................45
45...........................................................................‫ ﻣﻌﺎﻳﺐ‬-15
16. DESIGN CONSIDERATIONS (PLATE FIN
EXCHANGERS) .................................................45
45......... (‫ ﻣﻼﺣﻈﺎت ﻃﺮاﺣﻲ )ﻣﺒﺪﻟﻬﺎي ﺻﻔﺤﻬﺎي ﭘﺮه دار‬-16
16.1 Exchanger Geometry ................................. 45
45......................................‫ آراﻳﺶ ﻫﻨﺪﺳﻲ ﻣﺒﺪل‬1-16
APPENDICES:
:‫ﭘﻴﻮﺳﺘﻬﺎ‬
APPENDIX A....................................................................... 57
57...........................................................................‫ﭘﻴﻮﺳﺖ اﻟﻒ‬
APPENDIX B ..................................................................58
58............................................................................. ‫ﭘﻴﻮﺳﺖ ب‬
APPENDIX C TYPICAL TEMA RECOMMEND
FOULING RESISTANCES FOR
INDUSTRIAL FLUIDS..................61
TEMA ‫ﭘﻴﻮﺳﺖ ج ﻧﻤﻮﻧﻪ ﻣﻘﺎوﻣﺘﻬﺎي رﺳﻮب ﭘﻴﺸﻨﻬﺎدي‬
61.......................................... ‫ﺑﺮاي ﺳﻴﺎﻻت ﺻﻨﻌﺘﻲ‬
2
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ ﻣﻘﺪﻣﻪ‬-0
0. INTRODUCTION
"Process Design of Non-Combustion Type Heat
Exchanging Equipment" are broad and contain
variable subjects of paramount importance.
Therefore a group of process engineering
standard specifications are prepared to cover the
subject.
"‫"ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﺗﺠﻬﻴﺰات ﺗﺒﺎدل ﺣﺮارت ﻏﻴﺮ اﺣﺘﺮاﻗﻲ‬
‫ از اﻳﻦ رو‬.‫ﺑﺴﻴﺎر وﺳﻴﻊ و ﺷﺎﻣﻞ ﻣﻮﺿﻮﻋﺎت ﻣﺘﻐﻴﻴﺮ ﻣﻬﻤﻲ اﺳﺖ‬
‫ﻣﺠﻤﻮﻋﻪاي از ﻣﺸﺨﺼﺎت اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﻓﺮآﻳﻨﺪ ﺑﺮاي‬
.‫ﭘﻮﺷﺶ اﻳﻦ ﻣﻮﺿﻮع ﻣﻬﻴﺎ ﺷﺪهاﻧﺪ‬
:‫اﻳﻦ ﻣﺠﻤﻮﻋﻪ ﺷﺎﻣﻞ اﺳﺘﺎﻧﺪاردﻫﺎي زﻳﺮ ﻣﻲﺑﺎﺷﺪ‬
This group includes the following Standards:
‫ﻋﻨﻮان اﺳﺘﺎﻧﺪارد‬
STANDARD CODE STANDARD TITLE
‫ﻛﺪ اﺳﺘﺎﻧﺪارد‬
IPS-E-PR-771 "Engineering
Standard
for
Process Requirements of Heat
Exchanging Equipment"
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي اﻟﺰاﻣﺎت ﻓﺮآﻳﻨﺪي‬IPS-E-PR-771
"‫ﺗﺠﻬﻴﺰات ﺗﺒﺎدل ﺣﺮارت‬
IPS-E-PR-775 "Engineering
Standard
for
Process Design of Double Pipe
Heat Exchangers"
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي ﻃﺮاﺣﻲ‬IPS-E-PR-775
"‫ﻓﺮآﻳﻨﺪي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ دو ﻟﻮﻟﻪ‬
IPS-E-PR-785 "Engineering
Standard
for
Process Design of Air Cooled
Heat Exchangers (Air Coolers)"
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي ﻃﺮاﺣﻲ‬IPS-E-PR-785
‫ﻓﺮآﻳﻨﺪي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻫﻮاﻳﻲ )ﺧﻨﻚ‬
"(‫ﻛﻨﻨﺪه ﻫﺎي ﻫﻮاﻳﻲ‬
IPS-E-PR-790 "Engineering
Standard
for
Process Design of Cooling
Towers"
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي ﻃﺮاﺣﻲ‬IPS-E-PR-790
"‫ﻓﺮآﻳﻨﺪي ﺑﺮﺟﻬﺎي ﺧﻨﻚ ﻛﻨﻨﺪه‬
This Engineering Standard Specification covers:
:‫اﻳﻦ ﻣﺸﺨﺼﻪ اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺷﺎﻣﻞ‬
"PROCESS REQUIREMENTS OF HEAT
EXCHANGING EQUIPMENT"
"‫"اﻟﺰاﻣﺎت ﻓﺮآﻳﻨﺪي ﺗﺠﻬﻴﺰات ﺗﺒﺎدل ﺣﺮارت‬
Non-combustion type heat exchanging equipment
consist of various types from which the above
mentioned have the most application in Oil, Gas,
and Petrochemical (OGP) Industries and each
item will be discussed separately.
‫ﺗﺠﻬﻴﺰات ﺗﺒﺎدل ﺣﺮارت ﻏﻴﺮاﺣﺘﺮاﻗﻲ ﺷﺎﻣﻞ اﻧﻮاع ﻣﺘﻨﻮﻋﻲ ﻛﻪ در‬
‫ ﮔﺎز و‬،‫ داراي ﻛﺎرﺑﺮدﻫﺎي زﻳﺎدي در ﺻﻨﺎﻳﻊ ﻧﻔﺖ‬،‫ﺑﺎﻻ اﺷﺎره ﺷﺪه‬
‫( ﻫﺴﺘﻨﺪ ﻛﻪ ﻫﺮ ﺑﺨﺶ ﺑﻄﻮر ﺟﺪاﮔﺎﻧﻪ‬OGP) ‫ﭘﺘﺮوﺷﻴﻤﻲ‬
.‫ﺑﺮرﺳﻲ ﺧﻮاﻫﺪ ﺷﺪ‬
3
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ داﻣﻨﻪ ﻛﺎرﺑﺮد‬-1
1. SCOPE
This Engineering Standard Specification covers
the minimum process design requirements, for
thermal design, field of application, selection of
types and hydraulic calculations for shell and tube
heat exchangers, and plate heat exchangers (plate
fin exchangers).
‫ ﺣﺪاﻗﻞ اﻟﺰاﻣﺎت‬،‫اﻳﻦ ﻣﺸﺨﺼﺎت ﻓﻨﻲ اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ‬
،‫ رﺷﺘﻪ ﻛﺎرﺑﺮد‬،‫ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي را ﺑﺮاي ﻃﺮاﺣﻲ ﺣﺮارﺗﻲ‬
‫اﻧﺘﺨﺎب ﻧﻮع و ﻣﺤﺎﺳﺒﺎت ﻫﻴﺪروﻟﻴﻜﻲ را ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ‬
‫ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪاي و ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي )ﻣﺒﺪلﻫﺎي‬
.‫ﺻﻔﺤﻪاي ﭘﺮهدار( ﺷﺎﻣﻞ ﻣﻲﺷﻮد‬
This Engineering Standard Specification consists
of two parts as described below:
‫اﻳﻦ ﻣﺸﺨﺼﺎت ﻓﻨﻲ اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺷﺎﻣﻞ دو ﺑﺨﺶ ﻣﻄﺎﺑﻖ‬
:‫زﻳﺮ ﻣﻲﺑﺎﺷﺪ‬
Part I: Process Design of Shell and Tube Heat
Exchangers.
‫ ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و‬:I ‫ﺑﺨﺶ‬
Part II:Process Design of Plate Heat
Exchangers (Plate Fin Exchangers).
‫ ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي‬:II ‫ﺑﺨﺶ‬
.‫ﻟﻮﻟﻪاي‬
(‫)ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪاي ﭘﺮهدار‬
‫ ﺑﻪ اﺳﺘﺎﻧﺪارد ﺗﺠﻬﻴﺰات‬،I ‫ﺑﺮاي اﻟﺰاﻣﺎت ﻃﺮاﺣﻲ ﻣﻜﺎﻧﻴﻜﻲ ﺑﺨﺶ‬
.‫ ﻣﺮاﺟﻌﻪ ﺷﻮد‬IPS-G-ME-220 ‫ﻣﻜﺎﻧﻴﻜﻲ ﺛﺎﺑﺖ‬
For mechanical design requirements of Part I,
reference is made to the relevant Fixed
Mechanical Equipment Standard IPS-G-ME-220.
:1 ‫ﻳﺎدآوري‬
Note 1:
This standard specification is reviewed and
updated by the relevant technical committee on
December 2003, as amendment No. 1 by circular
No 215.
‫ ﺗﻮﺳﻂ‬1382 ‫اﻳﻦ ﻣﺸﺨﺼﺎت ﻓﻨﻲ اﺳﺘﺎﻧﺪارد در دي ﻣﺎه ﺳﺎل‬
‫ﻛﻤﻴﺘﻪ ﻓﻨﻲ ﻣﺮﺑﻮﻃﻪ ﺑﺮرﺳﻲ و ﺑﻪ روز ﺷﺪه و ﻣﻮارد ﺗﺄﻳﻴﺪ ﺷﺪه‬
‫ اﺑﻼغ‬215 ‫ ﻃﻲ ﺑﺨﺸﻨﺎﻣﻪ ﺷﻤﺎره‬1 ‫ﺑﻪ ﻋﻨﻮان اﺻﻼﺣﻴﻪ ﺷﻤﺎره‬
.‫ اﻳﻦ ﻣﻮارد در اﻳﻦ اﺳﺘﺎﻧﺪارد ﻟﺤﺎظ ﮔﺮدﻳﺪه اﺳﺖ‬.‫ﮔﺮدﻳﺪ‬
:2 ‫ﻳﺎدآوري‬
Note 2:
‫اﻳﻦ اﺳﺘﺎﻧﺪارد دو زﺑﺎﻧﻪ ﻧﺴﺨﻪ ﺑﺎزﻧﮕﺮي ﺷﺪه اﺳﺘﺎﻧﺪارد ﻣﻲﺑﺎﺷﺪ‬
‫ ﺗﻮﺳﻂ ﻛﻤﻴﺘﻪ ﻓﻨﻲ ﻣﺮﺑﻮﻃﻪ اﻧﺠﺎم و‬1388 ‫ﻛﻪ در ﻣﻬﺮ ﻣﺎه ﺳﺎل‬
(0) ‫ از اﻳﻦ ﭘﺲ وﻳﺮاﻳﺶ‬.‫( اراﻳﻪ ﻣﻲﮔﺮدد‬1) ‫ﺑﻪ ﻋﻨﻮان وﻳﺮاﻳﺶ‬
.‫اﻳﻦ اﺳﺘﺎﻧﺪارد ﻣﻨﺴﻮخ ﻣﻲﺑﺎﺷﺪ‬
This bilingual standard is a revised version of the
standard specification by the relevant technical
committee on October 2009, which is issued as
revision (1). Revision (0) of the said standard
specification is withdrawn.
:3 ‫ﻳﺎدآوري‬
Note 3:
‫ ﻣﺘﻦ اﻧﮕﻠﻴﺴﻲ‬،‫در ﺻﻮرت اﺧﺘﻼف ﺑﻴﻦ ﻣﺘﻦ ﻓﺎرﺳﻲ و اﻧﮕﻠﻴﺴﻲ‬
.‫ﻣﻼك ﻣﻲﺑﺎﺷﺪ‬
In case of conflict between Farsi and English
languages, English language shall govern.
‫ ﻣﺮاﺟﻊ‬-2
2. REFERENCES
Throughout this Standard the following dated and
undated standards/codes are referred to. These
referenced documents shall, to the extent
specified herein, form a part of this standard. For
dated references, the edition cited applies. The
applicability of changes in dated references that
occur after the cited date shall be mutually agreed
upon by the Company and the Vendor. For
undated references, the latest edition of the
referenced
documents
(including
any
‫در اﻳﻦ اﺳﺘﺎﻧﺪارد ﺑﻪ آﻳﻴﻦ ﻧﺎﻣﻪﻫﺎ و اﺳﺘﺎﻧﺪاردﻫﺎي ﺗﺎرﻳﺦ دار و‬
‫ ﺗﺎ ﺣﺪي ﻛﻪ در‬،‫ اﻳﻦ ﻣﺮاﺟﻊ‬.‫ﺑﺪون ﺗﺎرﻳﺦ زﻳﺮ اﺷﺎره ﺷﺪه اﺳﺖ‬
‫ ﺑﺨﺸﻲ از اﻳﻦ‬،‫اﻳﻦ اﺳﺘﺎﻧﺪارد ﻣﻮرد اﺳﺘﻔﺎده ﻗﺮار ﮔﺮﻓﺘﻪاﻧﺪ‬
‫ وﻳﺮاﻳﺶ‬،‫ در ﻣﺮاﺟﻊ ﺗﺎرﻳﺦ دار‬.‫اﺳﺘﺎﻧﺪارد ﻣﺤﺴﻮب ﻣﻲﺷﻮﻧﺪ‬
‫ﮔﻔﺘﻪ ﺷﺪه ﻣﻼك ﺑﻮده و ﺗﻐﻴﻴﺮاﺗﻲ ﻛﻪ ﺑﻌﺪ از ﺗﺎرﻳﺦ وﻳﺮاﻳﺶ در‬
‫ ﭘﺲ از ﺗﻮاﻓﻖ ﺑﻴﻦ ﻛﺎرﻓﺮﻣﺎ و ﻓﺮوﺷﻨﺪه ﻗﺎﺑﻞ‬،‫آﻧﻬﺎ داده ﺷﺪه اﺳﺖ‬
‫ آﺧﺮﻳﻦ وﻳﺮاﻳﺶ آﻧﻬﺎ ﺑﻪ‬،‫ در ﻣﺮاﺟﻊ ﺑﺪون ﺗﺎرﻳﺦ‬.‫اﺟﺮا ﻣﻲﺑﺎﺷﺪ‬
4
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
supplements and amendments) applies.
IPS-E-PR- 771(1)
.‫اﻧﻀﻤﺎم ﻛﻠﻴﻪ اﺻﻼﺣﺎت و ﭘﻴﻮﺳﺖﻫﺎي آن ﻣﻼك ﻋﻤﻞ ﻣﻲﺑﺎﺷﻨﺪ‬
(‫ )اﺳﺘﺎﻧﺪاردﻫﺎي ﻧﻔﺖ اﻳﺮان‬IPS
IPS (IRANIAN PETROLEUM STANDARDS)
for
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي ﻧﻤﻮدار‬IPS-E-PR-170
"‫ﺟﺮﻳﺎﻧﻲ ﻓﺮآﻳﻨﺪي‬
IPS-E-PR-230 "Engineering Standard for
Piping & Instrumentation
Diagrams (P & IDs)"
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي ﻧﻤﻮدارﻫﺎي‬IPS-E-PR-230
" ‫ﻟﻮﻟﻪﻛﺸﻲ و اﺑﺰار دﻗﻴﻖ‬
IPS-G-ME-220 "Engineering and Material
Standard for Shell & Tube
Heat Exchangers"
‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ و ﻣـﻮاد ﺑــﺮاي‬IPS-G-ME-220
"‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬
IPS-E-PR-170 "Engineering Standard
Process Flow Diagram"
IPS-E-GN-100 "Engineering
Units"
Standard
"‫ "اﺳﺘﺎﻧﺪارد ﻣﻬﻨﺪﺳﻲ ﺑﺮاي واﺣﺪﻫﺎ‬IPS-E-GN-100
for
(‫ )اﻧﺠﻤﻦ ﺳﺎزﻧﺪﮔﺎن ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ‬TEMA
TEMA(THE
TUBULAR
EXCHANGER
MANUFACTURERS ASSOCIATION)
،9 ‫"اﺳﺘﺎﻧﺪاردﻫﺎي اﻧﺠﻤﻦ ﺳﺎزﻧﺪﮔﺎن ﻣﺒﺪل ﻟﻮﻟﻪاي" وﻳﺮاﻳﺶ‬
2007 ‫ﺳﺎل‬
"Standards
of
the
Tubular
Exchanger
Manufacturers Association (TEMA)" 9th Ed.2007
(‫ )ﻣﻮﺳﺴﻪ ﻧﻔﺖ آﻣﺮﻳﻜﺎ‬API
API(AMERICAN PETROLEUM INSTITUTE)
API Std. 660, "Shell & Tube Heat Exchangers
for General Refinery Services"
7th. Ed., April 2003, Reaffirmed
Dec. 1987
‫ "ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﺑﺮاي‬API Std. 660
"‫ﻋﻤﻮﻣﻲ ﭘﺎﻻﻳﺸﮕﺎﻫﻲ‬
‫ﻛﺎرﺑﺮيﻫﺎي‬
2003 ‫ آورﻳﻞ‬7 ‫وﻳﺮاﻳﺶ‬
API Std. 662 "Plate Heat Exchanger
General Refinery Services"
for
‫ "ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﺑﺮاي‬API Std. 662
" ‫ﻛﺎرﺑﺮيﻫﺎي ﻋﻤﻮﻣﻲ ﭘﺎﻻﻳﺸﮕﺎﻫﻲ‬
Part I- Plate-and Frame Heat Exchangers
1st.Ed.Feb.2006
1 ‫ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪ و ﻗﺎﺑﻲ وﻳﺮاﻳﺶ‬:I ‫ﺑﺨﺶ‬
2006 ‫ﻓﻮرﻳﻪ‬
API Std. 662 "Plate Heat Exchanger
General Refinery Services”
for
‫ "ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﺑﺮاي‬API Std. 662
" ‫ﻛﺎرﺑﺮيﻫﺎي ﻋﻤﻮﻣﻲ ﭘﺎﻻﻳﺸﮕﺎﻫﻲ‬
Part IIBrazed Aluminum Plate –Fin Heat
Exchangers 1st.Ed.Feb.2006
‫ﭘﺮهدار ﺟﻮﺷﻜﺎري‬-‫ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪ اي‬:II ‫ﺑﺨﺶ‬
"2006 ‫ ﻓﻮرﻳﻪ‬1 ‫آﻟﻮﻣﻴﻨﻴﻮﻣﻲ وﻳﺮاﻳﺶ‬
‫ ﺗﻌﺎرﻳﻒ و واژﮔﺎن‬-3
3. DEFINITIONS AND TERMINOLOGY
3.1 Definitions of Different Types of Heat
Exchangers
‫ ﺗﻌﺎرﻳﻒ اﻧﻮاع ﻣﺨﺘﻠﻒ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ‬1-3
Heat transfer equipment can be specified either
by type of construction or by service. Generally,
they are designated by service. The following
terminology is in general use throughout the
industry.
‫ﺗﺠﻬﻴﺰات اﻧﺘﻘﺎل ﺣﺮارت ﻳﺎ از ﻧﻮع ﺳﺎﺧﺖ ﻳﺎ ﺑﺎ ﻧﻮع ﻛﺎرﺑﺮي‬
‫ ﻋﻤﻮﻣﺎً آﻧﻬﺎ ﺗﻮﺳﻂ ﻧﻮع ﻛﺎرﺑﺮي ﻣﺸﺨﺺ‬.‫ﻣﻲﺗﻮاﻧﺪ ﻣﺸﺨﺺ ﺷﻮد‬
.‫ واژهﮔﺬاري زﻳﺮ ﻛﺎرﺑﺮد ﻋﻤﻮﻣﻲ در ﻛﻞ ﺻﻨﻌﺖ دارد‬.‫ﻣﻲﺷﻮد‬
5
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ ﺳﺮدﺳﺎز‬1-1-3
3.1.1 Chiller
The chiller is a typical kettle type exchanger, and
the bundles has tubes to a height of about 60 per
cent of the diameter. The vapor space above is for
disengagement of the vapor from the liquid.
Chillers are used in refrigeration processes of the
vapor-compression type. A chiller cools a fluid
with a refrigerant to a temperature below that
obtainable using air or cooling water as the heat
sink. Common refrigerants are propane, ethylene
and propylene; chilled water or brines are less
frequently used.
‫ﺳﺮدﺳﺎز ﻳﻚ ﻣﺒﺪل ﻧﻮع ﻛﺘﺮي ﻣﻲﺑﺎﺷﺪ و دﺳﺘﻪﻫﺎي ﻟـﻮﻟـﻪﻫﺎ‬
‫ ﻓﻀﺎي ﺑﺨﺎر ﺑﺎﻻﻳﻲ‬.‫ درﺻﺪ ﻗﻄﺮ ﻣﺒﺪل اﺳﺖ‬60 ‫داراي ارﺗﻔﺎﻋﻲ ﺗﺎ‬
‫ ﺳﺮدﺳﺎزﻫﺎ در‬.‫ﻟﻮﻟﻪﻫﺎ ﺑﺮاي آزاد ﺷﺪن ﺑﺨﺎر از ﻣﺎﻳﻊ ﻣﻲﺑﺎﺷﺪ‬
.‫ﻓﺮآﻳﻨﺪﻫﺎي ﺗﺒﺮﻳﺪي از ﻧﻮع ﺗﺮاﻛﻢ – ﺑﺨﺎر اﺳﺘﻔﺎده ﻣﻲﺷﻮﻧﺪ‬
‫ ﺳﻴﺎل را ﺗﻮﺳﻂ ﻣﺎده ﻣﺒﺮد ﺑﻪ دﻣﺎﻳﻲ زﻳﺮ دﻣﺎﻳﻲ ﻛﻪ‬،‫ﺳﺮدﺳﺎز‬
‫ﺗﻮﺳﻂ ﻫﻮا ﻳﺎ آب ﺧﻨﻚ ﻛﻨﻨﺪه ﻗﺎﺑﻞ ﺣﺼﻮل اﺳﺖ ﺑﻪ ﻋﻨﻮان ﭼﺎﻟﻪ‬
‫ اﺗﻴﻠﻦ و‬،‫ ﭘﺮوﭘﺎن‬،‫ ﻣﺒﺮدﻫﺎي ﻣﺘﺪاول‬.‫ ﺳﺮد ﻣﻲﻛﻨﺪ‬،‫ﺣﺮارﺗﻲ‬
‫ آب ﺳﺮد ﺷﺪه ﻳﺎ آب ﻧﻤﻚ ﺑﻪ ﻧﺪرت اﺳﺘﻔﺎده‬،‫ﭘﺮوﭘﻴﻠﻦ ﻫﺴﺘﻨﺪ‬
.‫ﻣﻲﺷﻮﻧﺪ‬
‫ ﭼﮕﺎﻟﻨﺪه‬2-1-3
3.1.2 Condenser
A condenser is a unit in which a process vapor is
totally or partially converted to liquid. The heat
sink is ordinarily a utility, such as cooling water.
The term "surface condenser" refers specifically
to shell and tube units, used to condense the
steam from a preceding ejector stage, thus
reducing the inlet quantity of vapor mixture to the
following stage. This is a means of increasing
steam economy. They do not affect ejector
performance, but they do avoid the nuisance of
exhausting steam to the atmosphere, thus, they
allow steam to be recovered. A "direct contact
condenser" refers to a unit in which the vapor is
condensed by direct contact heat exchange with
droplets of water.
‫ﭼﮕﺎﻟﻨﺪه واﺣﺪي اﺳﺖ ﻛﻪ در آن ﺑﺨﺎر ﻓﺮآﻳﻨﺪي ﺑﻪ ﻃﻮر ﻛﺎﻣﻞ ﻳﺎ‬
‫ ﭼﺎﻟﻪ ﺣﺮارﺗﻲ ﻋﻤﻮﻣﺎً ﻳﻚ ﺳﺮوﻳﺲ‬.‫ﺟﺰﻳﻲ ﺑﻪ ﻣﺎﻳﻊ ﺗﺒﺪﻳﻞ ﻣﻲﺷﻮد‬
"‫ ﻋﺒﺎرت "ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ‬.‫ﺟﺎﻧﺒﻲ ﻣﺜﻞ آب ﺳﺮدﻛﻨﻨﺪه ﻣﻲﺑﺎﺷﺪ‬
‫ﻟﻮﻟﻪاي اﻃﻼق ﻣﻲﺷﻮد ﻛﻪ ﺑﺨﺎر ﻣﺮﺣﻠﻪ‬-‫ﻓﻘﻂ ﺑﻪ واﺣﺪﻫﺎي ﭘﻮﺳﺘﻪ‬
‫ﻣﻜﻨﺪه ﻗﺒﻠﻲ را ﻣﺎﻳﻊ ﻧﻤﺎﻳﺪ و در ﻧﺘﻴﺠﻪ ﻣﻘﺪار ﺑﺨﺎر ﻣﺨﻠﻮط ﺑﻪ‬
‫ اﻳﻦ ﻳﻚ وﺳﻴﻠﻪ ﺑﺮاي اﻓﺰاﻳﺶ ﺻﺮﻓﻪ‬.‫ﻣﺮﺣﻠﻪ ﺑﻌﺪي را ﻛﺎﻫﺶ دﻫﺪ‬
-‫ آﻧﻬﺎ ﻛﺎرآﻳﻲ ﻣﻜﻨﺪه را ﺗﺤﺖ ﺗﺄﺛﻴﺮ ﻗﺮار ﻧﻤﻲ‬.‫ﺟﻮﻳﻲ ﺑﺨﺎر اﺳﺖ‬
‫دﻫﻨﺪ ﺑﻠﻜﻪ از ﺻﺪاي آزاردﻫﻨﺪه ﺑﺨﺎر ﺧﺮوﺟﻲ ﺑﻪ ﻫﻮا ﺟﻠﻮﮔﻴﺮي‬
‫ "ﭼﮕﺎﻟﻨﺪه ﺗﻤﺎس‬.‫ﻣﻲﻛﻨﻨﺪ و ﻣﻨﺠﺮ ﺑــﻪ ﺑﺎزﻳﺎﻓﺖ ﺑﺨﺎر ﻣﻲﺷﻮﻧﺪ‬
‫ﻣﺴﺘﻘﻴﻢ" ﺑــﻪ واﺣﺪي اﻃﻼق ﻣﻲﺷﻮد ﻛﻪ ﺑﺨﺎر ﺑﺎ ﺗﺒﺎدل ﺣﺮارت‬
.‫ﻣﺴﺘﻘﻴﻢ ﺑﺎ ﻗﻄﺮات آب ﻣﺎﻳﻊ ﻣﻲ ﺷﻮد‬
‫ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ‬
3.1.2.1 Surface condenser
Surface condenser is to condense the exhaust
steam from a steam turbine to obtain maximum
efficiency and also to convert the turbine exhaust
steam into pure water (referred to as steam
condensate) so that it may be reused in the steam
generator or boiler as boiler feed water.
1-2-1-3
‫ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ ﺑﺮاي ﭼﮕﺎﻟﺶ ﺑﺨﺎر ﺧﺮوﺟﻲ از ﺗﻮرﺑﻴﻦ ﺑﺨﺎر‬
‫ﺟﻬﺖ رﺳﻴﺪن ﺑﻪ ﺣﺪاﻛﺜﺮ ﺑﺎزده و ﻫﻤﭽﻨﻴﻦ ﺗﺒﺪﻳﻞ ﺑﺨﺎر ﺧﺮوﺟﻲ‬
‫ﺗﻮرﺑﻴﻦ ﺑﻪ آب ﺧﺎﻟﺺ )اﺷﺎره ﺑﻪ ﻣﻴﻌﺎﻧﺎت ﺑﺨﺎر( ﺑﻪ ﻋﻨﻮان آب‬
‫ﺧﻮراك دﻳﮓ ﺑﺨﺎر در ﺗﻮﻟﻴﺪﻛﻨﻨﺪه ﺑﺨﺎر ﻳﺎ دﻳﮓ ﺑﺨﺎر ﺑﻜﺎر ﻣﻲ‬
.‫رود‬
‫اﻟﻒ( ﻫﺪف‬
a) Purpose
Surface condenser by condensing the steam
exhaust of a turbine at a pressure below
atmospheric pressure, the pressure drop
between the inlet and exhaust of the turbine is
increased, which increases the amount of heat
available for conversion to mechanical power.
‫در ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ ﺑﺎ ﭼﮕﺎﻟﺶ ﺑﺨﺎر ﺧﺮوﺟﻲ از ﺗﻮرﺑﻴﻦ در‬
‫ اﻓﺖ ﻓﺸﺎر ﺑﻴﻦ ورودي و ﺧﺮوﺟﻲ‬،‫ﻓﺸﺎر زﻳﺮ ﻓﺸﺎر اﺗﻤﺴﻔﺮ‬
‫ﺗﻮرﺑﻴﻦ اﻓﺰاﻳﺶ ﻣﻲﻳﺎﺑﺪ ﻛﻪ در ﻧﺘﻴﺠﻪ ﻣﻘﺪار اﻧﺮژي ﮔﺮﻣﺎﻳﻲ‬
‫ﻗﺎﺑﻞ دﺳﺘﺮس ﺑﺮاي ﺗﺒﺪﻳﻞ ﺑﻪ ﻗﺪرت ﻣﻜﺎﻧﻴﻜﻲ را اﻓﺰاﻳﺶ ﻣﻲ‬
.‫دﻫﺪ‬
‫ب ( ﻣﺎده واﺳﻄﻪ ﺳﺮدﺳﺎز‬
b) Cooling medium
Most of the heat liberated due to condensation
of the exhaust steam is carried away by the
cooling medium (water or air) used by the
‫ﺑﻴﺸﺘﺮ ﮔﺮﻣﺎﻳﻲ ﻛــﻪ در اﺛﺮ ﭼﮕﺎﻟﺶ ﺑﺨﺎر ﺧﺮوﺟﻲ آزاد‬
‫ﻣﻲﺷﻮد ﺗﻮﺳﻂ ﻣﺎده واﺳﻄﻪ ﺳﺮدﺳﺎز )آب ﻳﺎ ﻫﻮا( ﻛﻪ در‬
6
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
surface condenser.
IPS-E-PR- 771(1)
.‫ ﺟﺬب ﻣﻲﮔﺮدد‬،‫ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ اﺳﺘﻔﺎده ﻣﻲﺷﻮد‬
‫ج( ﭘﻮﺳﺘﻪ‬
c) Shell
For most water-cooled surface condensers, the
shell is under vacuum during normal operating
conditions. Surface condenser shell is
fabricated from carbon steel plates and is
stiffened as needed to provide rigidity for the
shell. When required by the selected design,
intermediate plates are installed to serve as
baffle plates that provide the desired flow path
of the condensing steam.
‫ ﭘﻮﺳﺘﻪ‬،‫ﺑﺮاي اﻏﻠﺐ ﭼﮕﺎﻟﻨﺪه ﻫﺎي ﺳﻄﺤﻲ ﺧﻨﻚ ﺷﻮﻧﺪه ﺑﺎ آب‬
‫ ﭘﻮﺳﺘﻪ‬.‫در ﺷﺮاﻳﻂ ﻣﻌﻤﻮﻟﻲ ﻋﻤﻠﻴﺎﺗﻲ ﺗﺤﺖ ﺧﻼء ﻗﺮار دارد‬
‫ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ از ﺻﻔﺤﺎت ﻓﻮﻻد ﻛﺮﺑﻨﻲ ﺳﺎﺧﺘﻪ ﺷﺪه و ﺑﻪ‬
‫ در‬.‫اﻧﺪازه ﻧﻴﺎز ﺑﺮاي ﺗﺄﻣﻴﻦ ﺳﺨﺘﻲ ﭘﻮﺳﺘﻪ ﺗﺤﻜﻴﻢ ﻳﺎﻓﺘﻪ اﺳﺖ‬
‫ ﺻﻔﺤﺎت ﻣﻴﺎﻧﻲ ﺑﻪ ﻋﻨﻮان‬،‫ﺻﻮرت ﻧﻴﺎز ﻣﻄﺎﺑﻖ اﻟﺰاﻣﺎت ﻃﺮاﺣﻲ‬
‫ ﺟﻬﺖ ﺗﻌﻴﻴﻦ ﻣﺴﻴﺮ ﻣﻄﻠﻮب ﺟﺮﻳﺎن ﺑﺨﺎر‬،‫ﻣﻤﺎﻧﻌﺖ ﻛﻨﻨﺪه‬
.‫ ﺗﻌﺒﻴﻪ ﻣﻲﺷﻮﻧﺪ‬،‫ﭼﮕﺎﻟﺶ ﺷﺪه‬
‫د( ﭼﺎﻟﻪ ﮔﺮم‬
d) Hotwell
At the bottom of the shell, where the
condensate collects, an outlet is installed. In
some designs, a sump (often referred to as the
hotwell) is provided. Condensate is pumped
from the outlet or the hotwell for reuse as
boiler feed water,
‫ ﻳﻚ‬،‫در ﭘﺎﻳﻴﻦ ﭘﻮﺳﺘﻪ ﺟﺎﻳﻲ ﻛﻪ ﻣﻴﻌﺎﻧﺎت ﺟﻤﻊ ﻣﻲﺷﻮﻧﺪ‬
‫ ﻳﻚ ﭼﺎﻟﻪ‬،‫ در ﺑﺮﺧﻲ ﻃﺮاﺣﻲﻫﺎ‬.‫ﺧﺮوﺟﻲ ﻧﺼﺐ ﺷﺪه اﺳﺖ‬
‫ ﻣﻴﻌﺎﻧﺎت از‬.‫)اﻏﻠﺐ ﻣﻨﺴﻮب ﺑﻪ ﭼﺎﻟﻪ ﮔﺮم( ﺗﻌﺒﻴﻪ ﺷﺪه اﺳﺖ‬
‫ﺧﺮوﺟﻲ ﻳﺎ ﭼﺎﻟﻪ ﮔﺮم ﺑﺮاي اﺳﺘﻔﺎده دوﺑﺎره ﺑﻪ ﻋﻨﻮان آب‬
.‫ﺧﻮراك دﻳﮓ ﺑﺨﺎر ﺗﻠﻤﺒﻪ ﻣﻲﺷﻮد‬
‫ﻫ( ﺳﻴﺴﺘﻢ ﺧﻼء‬
e)Vacuum system
For water-cooled surface condenser, the
shell’s internal vacuum is mostly commonly
supplied by and maintained by an external
steam jet ejector system. Such an ejector
system uses steam as the motive fluid to
remove any non-condensible gases that may
be present in the surface condenser.
‫ ﺧﻼء داﺧﻞ‬،‫ﺑﺮاي ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ ﺧﻨﻚ ﺷﻮﻧﺪه ﺑﺎ آب‬
‫ ﺗﺎﻣﻴﻦ و ﺣﻔﻆ‬،‫ﭘﻮﺳﺘﻪ اﻏﻠﺐ ﺗﻮﺳﻂ ﻳﻚ ﺳﺎﻣﺎﻧﻪ ﻣﻜﻨﺪه ﺑﻴﺮوﻧﻲ‬
‫ از ﺑﺨﺎر ﺑﻪ ﻋﻨﻮان ﺳﻴﺎل‬،‫ در ﭼﻨﻴﻦ ﺳﺎﻣﺎﻧﻪ ﻣﻜﻨﺪه اي‬.‫ﻣﻲﺷﻮد‬
‫ﻣﺤﺮك ﺑﺮاي ﺣﺬف ﮔﺎزﻫﺎي ﻏﻴﺮﻗﺎﺑﻞ ﭼﮕﺎﻟﺶ ﻛﻪ در ﭼﮕﺎﻟﻨﺪه‬
.‫ اﺳﺘﻔﺎده ﻣﻲ ﮔﺮدد‬،‫ﺳﻄﺤﻲ ﻣﻤﻜﻦ اﺳﺖ وﺟﻮد داﺷﺘﻪ ﺑﺎﺷﺪ‬
Motor driven mechanical vacuum pumps such
as liquid ring type vacuum pumps, are also
popular for vacuum service.
‫ﺗﻠﻤﺒﻪﻫﺎي ﺧﻼء ﻣﻜﺎﻧﻴﻜﻲ ﺑﺎ ﮔﺮداﻧﻨﺪه ﻣﻮﺗﻮري ﻧﻴﺰ ﻣﺜﻞ‬
‫ﺗﻠﻤﺒﻪﻫﺎي ﺧﻼء از ﻧﻮع ﺣﻠﻘﻪ ﻣﺎﻳﻊ در ﻛﺎرﺑﺮي ﺧﻼء ﻣﺘﺪاول‬
.‫ﻫﺴﺘﻨﺪ‬
‫و( ﺻﻔﺤﺎت ﻟﻮﻟﻪ‬
f) Tube sheets
At each end of the shell, a sheet of sufficient
thickness usually made of stainless steel is
provided, with holes for the tubes to be
inserted and rolled.
‫ ﻳﻚ ﺻﻔﺤﻪ ﺑﺎ ﺿﺨﺎﻣﺖ ﻣﻨﺎﺳﺐ ﻛﻪ‬،‫در اﻧﺘﻬﺎي ﻫﺮ ﭘﻮﺳﺘﻪ‬
‫ ﺗﻌﺒﻴﻪ ﺷﺪه اﺳﺖ ﻛﻪ‬،‫اﻏﻠﺐ از ﻓﻮﻻد زﻧﮓ ﻧﺰن ﺳﺎﺧﺘﻪ ﺷﺪه‬
‫داراي ﺳﻮراخﻫﺎﻳﻲ ﺑﺮاي داﺧﻞ ﺷﺪن و ﭼﻔﺖ ﺷﺪن ﻟﻮﻟﻪﻫﺎ‬
.‫ﻣﻲﺑﺎﺷﺪ‬
‫ز( ﻟﻮﻟﻪﻫﺎ‬
g) Tubes
‫ ﻋﻤﻮﻣﺎً ﻟﻮﻟﻪﻫﺎ از ﻓﻮﻻد زﻧﮓ‬،‫ﺑﺎ ﺗﻮﺟﻪ ﺑﻪ ﻣﻌﻴﺎرﻫﺎي اﻧﺘﺨﺎب‬
‫ ﻧﻴﻜﻞ ﻣﺴﻲ ﻳﺎ ﺗﻴﺘﺎﻧﻴﻢ‬،‫ آﻟﻴﺎژﻫﺎي ﻣﺲ ﻣﺜﻞ ﺑﺮﻧﺞ ﻳﺎ ﺑﺮﻧﺰ‬،‫ﻧﺰن‬
‫ اﺳﺘﻔﺎده از آﻟﻴﺎژﻫﺎي ﻣﺴﻲ ﻣﺜﻞ ﺑﺮﻧﺞ ﻳﺎ ﻧﻴﻜﻞ‬.‫ﺳﺎﺧﺘﻪ ﻣﻲﺷﻮد‬
‫ﻣﺴﻲ در واﺣﺪﻫﺎي ﺟﺪﻳﺪ ﺑﻪ ﺧﺎﻃﺮ ﻣﻼﺣﻈﺎت زﻳﺴﺖ ﻣﺤﻴﻄﻲ‬
‫ ﻫﻤﭽﻨﻴﻦ ﺑﺴﺘﻪ ﺑﻪ ﭼﺮﺧﻪ‬.‫ ﻧﺎدر اﺳﺖ‬،‫آﻟﻴﺎژﻫﺎي ﺳﻤﻲ ﻣﺲ‬
-‫ ﺑﻬﺘﺮ اﺳﺖ ﻛﻪ از ﻟﻮﻟﻪ‬،‫ﺑﺨﺎر و ﻓﺮآورش آب ﺑﺮاي دﻳﮓ ﺑﺨﺎر‬
‫ ﻟﻮﻟﻪﻫﺎي ﭼﮕﺎﻟﻨﺪه‬.‫ﻫﺎي ﺑﺎ ﺟﻨﺲ ﺣﺎوي ﻣﺲ اﺳﺘﻔﺎده ﻧﺸﻮد‬
Generally the tubes are made of stainless steel,
copper alloys such as brass or bronze, cupro
nickel or titanium depending on several
selection criteria. The use of copper bearing
alloys such as brass or cupro nickel is rare in
new plants, due to environmental concerns of
toxic copper alloys. Also depending on the
steam cycle water treatment for the boiler, it
7
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
may be desirable to avoid tube materials
containing copper. Titanium condenser tubes
are usually the best technical choice; however,
the use of titanium condenser tubes has been
virtually eliminated by the sharp increase in
the cost for this material.
‫ﺗﻴﺘﺎﻧﻴﻮﻣﻲ ﻣﻌﻤﻮﻻ ﺑﻬﺘﺮﻳﻦ اﻧﺘﺨﺎب ﻓﻨﻲ ﻫﺴﺘﻨﺪ ﺑﺎ اﻳﻦ وﺟﻮد‬
‫ﻟﻮﻟﻪﻫﺎي ﺗﻴﺘﺎﻧﻴﻮﻣﻲ ﭼﮕﺎﻟﻨﺪه ﺑﻪ ﺧﺎﻃﺮ اﻓﺰاﻳﺶ ﺷﺪﻳﺪ ﻗﻴﻤﺖ‬
.‫اﻳﻦ ﻣﺎده ﺑﻪ ﻃﻮر ﻃﺒﻴﻌﻲ ﺣﺬف ﺷﺪهاﻧﺪ‬
The outer diameter of condenser tubes
typically ranges from 19mm ( ¾ inch) to
32mm (1-1/4 inch), based on condenser
cooling water friction consideration and
overall condenser size.
19 ‫ﻣﺤﺪوده ﻗﻄﺮ ﺑﻴﺮوﻧﻲ ﻟﻮﻟﻪﻫــﺎي ﭼﮕﺎﻟﻨﺪه اﻏﻠﺐ ﺑﻴﻦ‬
1
‫ ﻛﻪ‬،‫اﻳﻨﭻ( اﺳﺖ‬1 ) ‫ ﻣﻴﻠﻴﻤﺘﺮ‬32 ‫ اﻳﻨﭻ( ﺗﺎ‬3 ) ‫ﻣﻴﻠﻴﻤﺘﺮ‬
4
4
‫ﺑﺴﺘﮕﻲ ﺑﻪ اﺻﻄﻜﺎك آب ﺧﻨﻚ ﻛﻦ و اﻧﺪازه ﻛﻠﻲ ﭼﮕﺎﻟﻨﺪه‬
.‫دارد‬
‫ح( ﻣﺤﻔﻈﻪ ﻫﺎي آب‬
h)Waterboxes
‫ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﻫﺎﻳﻲ ﻛﻪ در ﻫﺮ اﻧﺘﻬﺎ ﺑﺎ ﻟﻮﻟﻪﻫﺎ ﭼﻔﺖ‬،‫در ﭼﮕﺎﻟﻨﺪه‬
‫ﺷﺪهاﻧﺪ ﺑﺎ ﻳﻚ ﭘﻮﺷﺶ ﻣﺤﻔﻈﻪ ﭘﻴﺶ ﺳﺎﺧﺘﻪ ﻛﻪ ﺑﻪ اﺳﻢ‬
‫ﻣﺤﻔﻈﻪ آب ﺷﻨﺎﺧﺘﻪ ﻣﻲﺷﻮﻧﺪ و ﺑﺎ اﺗﺼﺎل ﻓﻠﻨﺠﻲ ﺑﻪ ﺻﻔﺤﻪ‬
‫ در ﻣﺤﻔﻈﻪ آب‬.‫ﻟﻮﻟــﻪ ﻳﺎ ﭘﻮﺳﺘﻪ ﭼﮕــﺎﻟﻨﺪه ﻣﺘﺼﻞ اﺳﺖ‬
‫ﻣﻌﻤﻮﻻ درﻳﭽﻪ ﻫﺎي آدم رو ﺑﺎ ﻧﮕﻬﺪارﻧﺪه ﻟﻮﻻﻳﻲ ﺑﻪ ﻣﻨﻈﻮر‬
.‫ﺑﺎزرﺳﻲ و ﺗﻤﻴﺰ ﻛﺮدن ﺗﻌﺒﻴﻪ ﻣﻲ ﺷﻮﻧﺪ‬
The tube sheet at each end with tube ends
rolled for each end of the condenser is closed
by a fabricated box cover known as waterbox,
with flanged connection to the tube sheet or
condenser shell. The waterbox is usually
provided with manholes on hinged covers to
allow inspection and cleaning.
‫ط( آﻳﻴﻦ ﻧﺎﻣﻪ ﻫﺎ‬
i) Codes
Steam surface condensers operate under a
vacuum and are, therefore, not considered
pressure vessels. The ASME Code is a
pressure vessel code and is not, Strictly
speaking, applicable to surface condensers
operating under vacuum. However, the tube
side of a surface condenser is considered a
pressure vessel, as it is subjected to the full
water pressure. When necessary, this side of
the condenser can be designed and constructed
to ASME Code requirement.
‫ ﻛﻪ در ﺷﺮاﻳﻂ ﺧﻼء ﻛﺎر‬،‫ﭼﮕﺎﻟﻨﺪه ﻫﺎي ﺳﻄﺤﻲ ﺑﺨﺎر‬
‫ آﻳﻴﻦ ﻧﺎﻣﻪ‬.‫ ﻇﺮوف ﺗﺤﺖ ﻓﺸﺎر ﻣﺤﺴﻮب ﻧﻤﻲ ﺷﻮﻧﺪ‬،‫ﻣﻲﻛﻨﻨﺪ‬
‫ ﺑﺮاي ﻇﺮف ﺗﺤﺖ ﻓﺸﺎر ﺑﻮده و ﺑﻪ ﻃﻮر ﺻﺮﻳﺢ‬ASME
‫ﻣﻲﺗﻮان ﮔﻔﺖ ﻛﻪ ﺑﺮاي ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ ﺗﺤﺖ ﺧﻼء ﺑﻪ ﻛﺎر‬
‫ ﺑﺎ اﻳﻦ وﺟﻮد ﺳﻤﺖ ﻟﻮﻟﻪ ﭼﮕﺎﻟﻨﺪه ﺳﻄﺤﻲ ﺑﻪ ﻋﻨﻮان‬.‫ﻧﻤﻲرود‬
‫ﻇﺮف ﺗﺤﺖ ﻓﺸﺎر در ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﻣﻲﺷﻮد زﻳﺮا ﺗﺤﺖ ﺗﺄﺛﻴﺮ‬
‫ اﻳﻦ ﺳﻤﺖ ﭼﮕﺎﻟﻨﺪه‬،‫ در ﺻﻮرت ﻧﻴﺎز‬.‫ﻓﺸﺎر ﻛﺎﻣﻞ آب ﻗﺮار دارد‬
.‫ ﻃﺮاﺣﻲ و ﺳﺎﺧﺘﻪ ﺷﻮد‬ASME ‫ﻣﻴﺘﻮاﻧﺪ ﺑﺮاﺳﺎس آﻳﻴﻦ ﻧﺎﻣﻪ‬
Most surface condensers are designed and
constructed in accordance with HEI Standards.
HEI ‫اﻏﻠﺐ ﭼﮕﺎﻟﻨﺪهﻫﺎي ﺳﻄﺤﻲ ﻣﻄﺎﺑﻖ ﺑﺎ اﺳﺘﺎﻧﺪاردﻫﺎي‬
.‫ﻃﺮاﺣﻲ و ﺳﺎﺧﺘﻪ ﻣﻲﺷﻮﻧﺪ‬
‫ ﺧﻨﻚ ﻛﻨﻨﺪه‬3-1-3
3.1.3 Cooler
A cooler exchanges heat between a process
stream and water or air.
‫ﻳﻚ ﺧﻨﻚ ﻛﻨﻨﺪه ﺑﻴﻦ ﺟﺮﻳﺎن ﻓﺮآﻳﻨﺪي و آب ﻳﺎ ﻫﻮا ﺗﺒﺎدل‬
.‫ﺣﺮارت اﻧﺠﺎم ﻣﻲ دﻫﺪ‬
‫ ﺗﺒﺨﻴﺮ ﻛﻨﻨﺪه‬4-1-3
3.1.4 Evaporator
Exchangers specifically designed to process fluid
by some heating medium such as steam.
‫ﻣﺒﺪلﻫﺎﻳﻲ ﻛﻪ ﻣﻨﺤﺼﺮاً ﺑﺮاي ﺳﻴﺎل ﻓﺮآﻳﻨﺪي ﻳﺎ دﻳﮕﺮ ﺳﻴﺎل‬
.‫ ﻃﺮاﺣﻲ ﻣﻲﺷﻮﻧﺪ‬،‫ﺣﺮارﺗﻲ ﻣﺜﻞ ﺑﺨﺎر‬
‫ﻳﺎ ﻣﺒﺪل ﺣﺮارﺗﻲ‬/‫ ﻣﺒﺪل و‬5-1-3
3.1.5 Exchanger and/or heat exchanger
In the broad sense, an exchanger is any item of
unfired heat transfer equipment whose function is
‫ ﻳﻚ ﻣﺒﺪل ﺑﺨﺸﻲ از ﺗﺠﻬﻴﺰ اﻧﺘﻘﺎل ﺣﺮارت ﻏﻴﺮ‬،‫از دﻳﺪﮔﺎه ﻛﻠﻲ‬
8
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
to change the total enthalpy of a stream. In the
specific (and more usual) connotation, an
exchanger transfers heat between two process
streams.
IPS-E-PR- 771(1)
.‫اﺣﺘﺮاﻗﻲ اﺳﺖ ﻛﻪ وﻇﻴﻔﻪ آن ﺗﻐﻴﻴﺮ ﻛﻞ آﻧﺘﺎﻟﭙﻲ ﺟﺮﻳﺎن ﻣﻲﺑﺎﺷﺪ‬
‫ ﻳﻚ ﻣﺒﺪل ﺑﻴﻦ دو‬،(‫ﺑﺎ ﻳﻚ ﻣﻌﻨﻲ ﻣﺸﺨﺺ )و ﺑﺴﻴﺎر ﻣﺘﺪاول‬
.‫ﺟﺮﻳﺎن ﻓﺮآﻳﻨﺪي ﺗﺒﺎدل ﺣﺮارت اﻧﺠﺎم ﻣﻲدﻫﺪ‬
‫ ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬6-1-3
3.1.6 Fouling resistance
The fouling resistance is a measure of the
ultimate additional resistance to heat transfer
caused by deposits on and corrosion of the heat
transfer material surface.
‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺷﺎﺧﺺ ﻣﻴﺰان ﻧﻬﺎﻳﻲ ﻣﻘﺎوﻣﺖ اﺿﺎﻓﻪ‬
‫ﺷﺪه در اﻧﺘﻘﺎل ﺣﺮارت ﻣﻲﺑﺎﺷﺪ ﻛﻪ ﺗﻮﺳﻂ ﺗﻪ ﻧﺸﻴﻨﻲ ذرات و‬
.‫ﺧﻮردﮔﻲ در ﺳﻄﻮح اﻧﺘﻘﺎل ﺣﺮارت اﻳﺠﺎد ﻣﻲﺷﻮد‬
:‫ﻳﺎدآوري‬
Note:
The resistance depends on the type of fluid, the
material, temperature conditions, flow velocities
and the operating period between two successive
cleaning actions.
‫ ﺳﺮﻋﺖﻫﺎي ﺟﺮﻳﺎن‬،‫ ﺷﺮاﻳﻂ دﻣﺎﻳﻲ‬،‫ ﺟﻨﺲ‬،‫ﻣﻘﺎوﻣﺖ ﺑﻪ ﻧﻮع ﺳﻴﺎل‬
‫ ﺑﺴﺘﮕﻲ‬،‫و زﻣﺎن ﻋﻤﻠﻴﺎﺗﻲ ﺑﻴﻦ دو ﻋﻤﻠﻴﺎت ﻣﺘﻮاﻟﻲ ﺗﻤﻴﺰﻛﺎري‬
.‫دارد‬
‫ ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬7-1-3
3.1.7 Fouling coefficient
The fouling coefficient is the reciprocal of the
fouling resistance.
‫ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻣﻌﻜﻮس ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬
.‫ﻣﻲﺑﺎﺷﺪ‬
:‫ﻳﺎدآوري‬
Note:
The use of the fouling coefficient has generally
been abandoned, since it tends to be confusing
that an increase in fouling results in a decrease in
fouling coefficient.
‫از آﻧﺠﺎ ﻛﻪ اﻓﺰاﻳﺶ رﺳﻮب ﻣﻨﺠﺮ ﺑﻪ ﻛﺎﻫﺶ ﺿﺮﻳﺐ رﺳﻮب‬
،‫ ﻋﻤﻮﻣﺎً اﺳﺘﻔﺎده از ﺿﺮﻳﺐ رﺳﻮب ﺑﻪ دﻟﻴﻞ اﺣﺘﻤﺎل اﺷﺘﺒﺎه‬،‫ﻣﻲﺷﺪ‬
.‫ﻣﻨﺴﻮخ ﺷﺪه اﺳﺖ‬
‫ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪه‬8-1-3
3.1.8 Reboiler
A reboiler is a vaporizer that provides latent heat
of vaporization to the bottom (generally) of a
fractionation tower.There are two general classes
of reboilers, those which send both phases to the
tower for separation of vapor from liquid and
those which return only vapor. The former
operate by either natural circulation (usually
called thermosyphon) or forced circulation.
‫ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪه ﻳﻚ ﺗﺒﺨﻴﺮﻛﻨﻨﺪه اﺳﺖ ﻛﻪ ﮔﺮﻣﺎي ﻧﻬﺎن را ﺑﺮاي‬
‫ دو ﻃﺒﻘﻪ‬.‫ﺗﺒﺨﻴﺮ در ﭘﺎﻳﻴﻦ)ﻋﻤﻮﻣﺎً( ﺑﺮج ﺟﺪاﺳﺎزي ﺗﺄﻣﻴﻦ ﻣﻲﻛﻨﺪ‬
‫ آﻧﻬﺎﻳﻲ ﻛﻪ دو‬،‫ﺑﻨﺪي ﻋﻤﻮﻣﻲ ﺑﺮاي ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪه ﻫﺎ وﺟﻮد دارد‬
‫ﻓﺎز را ﺑﺮاي ﺟﺪاﺳﺎزي ﺑﺨﺎر از ﻣﺎﻳﻊ ﺑﻪ ﺑﺮج ﻣﻲﻓﺮﺳﺘﻨﺪ و آﻧﻬﺎﻳﻲ‬
ً‫ اوﻟﻲ ﺑﺎ ﮔﺮدش ﻃﺒﻴﻌﻲ )ﻣﻌﻤﻮﻻ‬.‫ﻛﻪ ﻓﻘﻂ ﺑﺨﺎر را ﺑﺮﻣﻲﮔﺮداﻧﻨﺪ‬
.‫ﺗﺮﻣﻮﺳﻴﻔﻮن ﻧﺎﻣﻴﺪه ﻣﻲﺷﻮد( ﻳﺎ اﺟﺒﺎري ﻛﺎر ﻣﻲﻛﻨﺪ‬
3.1.8.1 Thermosyphon reboilers are by far the
common type. Horizontal thermosyphons with
vaporization on the shell side are commonly used
in the petroleum industry while vertical units with
in-tube vaporization are favored in the chemical
industry. In a thermosyphon reboiler, sufficient
liquid head is provided so that natural circulation
of the boiling medium is maintained.
.‫ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎي ﺗﺮﻣﻮﺳﻴﻔﻮن ﺑﺴﻴﺎر ﻣﺘﺪاول ﻫﺴﺘﻨﺪ‬1-8-1-3
‫ﺗﺮﻣﻮﺳﻴﻔﻮن ﻫﺎي اﻓﻘﻲ ﺑﺎ ﺗﺒﺨﻴﺮ در ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻋﻤﻮﻣﺎً در‬
‫ﺻﻨﺎﻳﻊ ﻧﻔﺖ اﺳﺘﻔﺎده ﻣﻲﺷﻮﻧﺪ در ﺻﻮرﺗﻲ ﻛﻪ واﺣﺪﻫﺎي ﻋﻤﻮدي ﺑﺎ‬
‫ در ﺑﺎز‬.‫ﺗﺒﺨﻴﺮ در ﻟﻮﻟﻪ در ﺻﻨﺎﻳﻊ ﺷﻴﻤﻴﺎﻳﻲ ﺗﺮﺟﻴﺢ داده ﻣﻲ ﺷﻮﻧﺪ‬
‫ﺟﻮﺷﺎﻧﻨﺪه ﺗﺮﻣﻮﺳﻴﻔﻮن ارﺗﻔﺎع ﻣﻨﺎﺳﺐ ﺳﻴﺎل ﺗﺄﻣﻴﻦ ﻣﻲﺷﻮد ﺗﺎ‬
.‫ﮔﺮدش ﻃﺒﻴﻌﻲ ﺳﻴﺎل ﺟﻮﺷﺎن ﻣﻤﻜﻦ ﮔﺮدد‬
3.1.8.2 Forced circulation reboilers require a
‫ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎي ﮔﺮدش اﺟﺒﺎري ﺑﺮاي اﻧﺘﻘﺎل ﺳﻴﺎل‬2-8-1-3
pump to force the boiling medium through the
‫ اﻳﻦ ﻧﻮع از ﺑﺎز‬.‫ﺟﻮﺷﺎن در ﻃﻮل ﻣﺒﺪل ﺑــﻪ ﺗﻠﻤﺒﻪ ﻧﻴـﺎز دارﻧﺪ‬
‫ﺟﻮﺷﺎﻧﻨﺪهﻫﺎ ﺑﻪ ﺧﺎﻃﺮ اﺿﺎﻓﻪ ﺷﺪن ﻫﺰﻳﻨﻪ ﺗﻠﻤﺒﻪ ﻛﺮدن ﺧﻮراك ﺑﺎز‬
‫ اﻣﺎ ﺑﺮاي ﺟﺒﺮان‬.‫ﺟﻮﺷﺎﻧﻨﺪه ﺧﻴﻠﻲ ﻛﻢ اﺳﺘﻔﺎده ﻣﻲﺷﻮﻧﺪ‬
،‫ﻣﺤﺪودﻳﺖ ارﺗﻔﺎع اﻳﺴﺘﺎﻳﻲ ﺳﻴﺎل و ﻣﺸﻜﻼت ﮔﺮدش ﺳﻴﺎل‬
exchanger. This type of reboiler is infrequently
used because of the added cost of pumping the
reboiler feed, but may be required to overcome
9
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
.‫ﻣﻤﻜﻦ اﺳﺖ ﻣﻮرد اﺳﺘﻔﺎده ﻗﺮار ﮔﻴﺮﻧﺪ‬
hydrostatic head limitations and/or circulation
problems.
3.1.8.3 Reboilers which return only vapor to the
tower are called kettle reboilers. The operation of
kettle reboilers would be best described as pool
boiling.
‫ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎﻳﻲ ﻛــــﻪ ﻓﻘﻂ ﺑﺨﺎر را ﺑـــﻪ ﺑﺮج‬3-8-1-3
‫ ﺑﻬﺘﺮﻳﻦ‬.‫ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎي ﻛﺘﺮي ﻧﺎﻣﻴﺪه ﻣﻲﺷﻮﻧﺪ‬،‫ﺑﺮﻣﻲﮔﺮداﻧﻨﺪ‬
-‫ ﺟﻮش اﺳﺘﺨﺮي ﻣﻲ‬،‫ﺗﻮﺿﻴﺢ ﺑﺮاي ﻋﻤﻠﻴﺎت ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪه ﻛﺘﺮي‬
.‫ﺑﺎﺷﺪ‬
(‫ ﻣﻮﻟﺪﻫﺎي ﺑﺨﺎر )ﺑﺨﺎرﺳﺎزﻫﺎي ﺑﺎزﻳﺎﻓﺖ ﺣﺮارﺗﻲ‬9-1-3
3.1.9 Steam generators (waste heat boilers)
Steam generators are a special type of vaporizer
used to produce steam as the vapor product.
Generally, the heat source is excess heat beyond
that which is required for process; this accounts
for the common name of "waste heat boiler" for
these Units. Like reboilers, steam generators can
be kettle, pump-through, or thermosyphon type.
‫ ﻧﻮع ﺧﺎﺻﻲ از ﺗﺒﺨﻴﺮﻛﻨﻨﺪه اﺳﺖ ﻛﻪ ﺑﺮاي ﺗﻮﻟﻴﺪ‬،‫ﻣﻮﻟﺪﻫﺎي ﺑﺨﺎر‬
‫ ﻋﻤﻮﻣﺎً ﻣﻨﺒﻊ‬.‫ﺑﺨﺎر آب ﺑﻪ ﻋﻨﻮان ﻣﺤﺼﻮل ﺗﺒﺨﻴﺮ ﺑﻪ ﻛﺎر ﻣﻲرود‬
.‫ ﺣﺮارت اﺿﺎﻓﻲ اﺳﺖ ﻛﻪ ﺑﻴﺸﺘﺮ از ﻧﻴﺎز ﻓﺮآﻳﻨﺪ ﺗﻮﻟﻴﺪ ﻣﻴﺸﻮد‬،‫ﮔﺮﻣﺎ‬
‫ﺑﻪ اﻳﻦ ﺟﻬﺖ اﻳﻦ واﺣﺪﻫﺎ ﺑﻪ اﺳﻢ ﺑﺨﺎرﺳﺎزﻫﺎي ﺑﺎزﻳﺎﻓﺖ ﺣﺮارﺗﻲ‬
‫ ﻣﻮﻟﺪﻫﺎي ﺑﺨﺎر ﻣﺜﻞ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎ ﻣﻲﺗﻮاﻧﻨﺪ از‬.‫ﻧﺎﻣﻴﺪه ﻣﻲﺷﻮﻧﺪ‬
.‫درﻣﻴﺎن ﻳﺎ ﺗﺮﻣﻮﺳﻴﻔﻮن ﺑﺎﺷﻨﺪ‬-‫ ﺗﻠﻤﺒﻪ‬،‫ﻧﻮع ﻛﺘﺮي‬
‫ ﺳﻮﭘﺮﻫﻴﺘﺮ‬10-1-3
3.1.10 Superheater
A superheater heats a vapor above its saturation
temperature.
.‫ﺳﻮﭘﺮﻫﻴﺘﺮ ﺑﺨﺎر را ﺑﺎﻻﺗﺮ از دﻣﺎي اﺷﺒﺎع ﮔﺮم ﻣﻲﻛﻨﺪ‬
‫ ﺗﺒﺨﻴﺮﻛﻨﻨﺪه‬11-1-3
3.1.11 Vaporizor
A vaporizor is an exchanger which converts
liquid into vapor. This term is sometimes limited
to units handling liquids other than water.
.‫ﺗﺒﺨﻴﺮ ﻛﻨﻨﺪه ﻳﻚ ﻣﺒﺪل اﺳﺖ ﻛﻪ ﻣﺎﻳﻊ را ﺑﻪ ﺑﺨﺎر ﺗﺒﺪﻳﻞ ﻣﻲﻛﻨﺪ‬
‫اﻳﻦ ﻋﻨﻮان ﺑﻌﻀﺎ ﺑﻪ واﺣﺪﻫﺎﻳﻲ ﻛﻪ ﺣﺎوي ﻣﺎﻳﻌﻲ ﻏﻴﺮ از آب‬
.‫ ﻣﺤﺪود ﻣﻲﺷﻮد‬،‫ﻫﺴﺘﻨﺪ‬
3.2 Definition of TEMA Classes
TEMA ‫ ﺗﻌﺎرﻳﻒ ﻃﺒﻘﻪ ﺑﻨﺪي‬2-3
3.2.1 TEMA "Class R" exchanger
TEMA "R ‫ ﻣﺒﺪل "ﻃﺒﻘﻪ‬1-2-3
The TEMA Mechanical Standards for "Class R"
heat exchanger specify design and fabrication of
unfired shell and tube heat exchangers for the
generally severe requirements of petroleum and
related process application.
‫ ﺑﺮاي ﻣﺒﺪل ﺣﺮارﺗﻲ "ﻃﺒﻘﻪ‬TEMA ‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻣﻜﺎﻧﻴﻜﻲ‬
‫ ﻋﻤﻮﻣﺎً ﻃﺮاﺣﻲ و ﺳﺎﺧﺖ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و‬،" R ‫ﺑﻨﺪي‬
‫ﻟﻮﻟﻪ ﻏﻴﺮاﺣﺘﺮاﻗﻲ در اﻟﺰاﻣﺎت ﺷﺪﻳﺪ ﻧﻔﺘﻲ و ﻛﺎرﺑﺮدﻫﺎي ﻓﺮآﻳﻨﺪي‬
.‫ﻣﺮﺑﻮﻃﻪ را ﻣﺸﺨﺺ ﻣﻲﻛﻨﺪ‬
TEMA "C ‫ ﻣﺒﺪل "ﻃﺒﻘﻪ ﺑﻨﺪي‬2-2-3
3.2.2 TEMA "Class C" exchanger
The TEMA Mechanical Standards for "Class C"
heat exchangers specify design and fabrication of
unfired shell and tube heat exchangers for the
generally moderate requirements of commercial
and general process application.
‫ ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ "ﻃﺒﻘﻪ‬TEMA ‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻣﻜﺎﻧﻴﻜﻲ‬
‫ ﻋﻤﻮﻣﺎً ﻃﺮاﺣﻲ و ﺳﺎﺧﺖ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و‬، "C ‫ﺑﻨﺪي‬
‫ﻟﻮﻟﻪ ﻏﻴﺮاﺣﺘﺮاﻗﻲ در اﻟﺰاﻣﺎت ﻣﺘﻌﺎدل ﺑﺎزرﮔﺎﻧﻲ و ﻛﺎرﺑﺮدﻫﺎي‬
.‫ﻓﺮآﻳﻨﺪي ﻣﺮﺑﻮﻃﻪ را ﻣﺸﺨﺺ ﻣﻲﻛﻨﺪ‬
‫" ﺑﺮاي ﺣﺪاﻛﺜﺮ اﻗﺘﺼﺎدي ﺑﻮدن و‬C ‫واﺣﺪﻫﺎي "ﻃﺒﻘﻪ ﺑﻨﺪي‬
"R ‫ درﺻﺪ ﻧﺴﺒﺖ ﺑﻪ "ﻃﺒﻘﻪ ﺑﻨﺪي‬5 ‫ﺻﺮﻓﻪﺟﻮﻳﻲ در ﺣﺪود‬
.‫ﻃﺮاﺣﻲ ﻣﻲ ﺷﻮﻧﺪ‬
"Class C" units are designed for maximum
economy and result in a cost saving of about 5%
over "Class R".
TEMA "B ‫ "ﻃﺒﻘﻪ ﺑﻨﺪي‬3-2-3
3.2.3 TEMA "Class B" exchanger
‫ ﺑﺮاي ﻣﺒﺪل ﺣﺮارﺗﻲ "ﻃﺒﻘﻪ‬TEMA ‫اﺳﺘﺎﻧﺪاردﻫﺎي ﻣﻜﺎﻧﻴﻜﻲ‬
The TEMA Mechanical Standards for "Class B"
10
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IPS-E-PR- 771(1)
‫ ﻋﻤﻮﻣﺎً ﻃﺮاﺣﻲ و ﺳﺎﺧﺖ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و‬،"B ‫ﺑﻨﺪي‬
‫ﻟﻮﻟﻪ ﻏﻴﺮاﺣﺘﺮاﻗﻲ را ﺑﺮاي ﻛﺎرﺑﺮيﻫﺎي ﻓﺮآﻳﻨﺪي ﺷﻴﻤﻴﺎﻳﻲ‬
.‫ﻣﺸﺨﺺ ﻣﻲﻛﻨﺪ‬
heat exchangers specify design & fabrication of
unfired shell & tube heat exchangers for chemical
process service.
‫ ﻧﺸﺎﻧﻪﻫﺎ و اﺧﺘﺼﺎرات‬-4
4. SYMBOLS & ABBREVIATIONS
(m2) ‫ﻣﺴﺎﺣﺖ ﻛﻞ ﻣﺒﺪل‬
A
(m2)‫ﺳﻄﺢ ﻣﻮﺛﺮ ﻻزم داﺧﻞ ﺳﻄﺢ اﻧﺘﻘﺎل‬
Ai
A
Total exchanger area, (m²).
Ai
Required effective inside transfer
surface, (m²).
API
American Petroleum Institute.
Btu
British Thermal Unit.
CAF
Compressed Asbestos Fiber
‫ﻓﻴﺒﺮ ﻓﺸﺮده آزﺑﺴﺖ‬
CAF
DEA
Di – Ethanol Amine.
‫دي – اﺗﺎﻧﻮل آﻣﻴﻦ‬
DEA
DGA
Di - Glycol Amine.
‫دي – ﮔﻼﻳﻜﻮل آﻣﻴﻦ‬
DGA
DN
Diameter Nominal, (mm).
DS
DS
EPDM
‫ﻣﻮﺳﺴﻪ ﻧﻔﺖ آﻣﺮﻳﻜﺎ‬
API
‫واﺣﺪ ﮔﺮﻣﺎﻳﻲ اﻧﮕﻠﻴﺴﻲ‬
Btu
(‫ﻗﻄﺮ اﺳﻤﻲ )ﻣﻴﻠﻲ ﻣﺘﺮ‬
DN
Design Pressure.
‫ﻓﺸﺎر ﻃﺮاﺣﻲ‬
DP
Diameter of shell
‫ﻗﻄﺮ ﭘﻮﺳﺘﻪ‬
DS
Ethylene Propylene Di Monomer.
F
LMTD Correction Factor
FPM
Fine Particular Matter.
h
Segment Opening Height
hf
Film coefficient of tube side
fluid, in (W/m².°C) or (W/m².K)
ID
Inside Diameter, in (mm).
LMTD
Logarithmic Mean Temperature
Difference.
MAWP
Maximum Allowable Working
Pressure.
Max.
Maximum.
MEA
mono-Ethanolamine.
Min.
Minimum.
MOP
Maximum Operating Pressure.
‫اﺗﻴﻠﻦ ﭘﺮوﭘﻴﻠﻦ دي ﻣﻨﻮﻣﺮ‬
EPDM
LMTD ‫ﺿﺮﻳﺐ ﺗﺼﺤﻴﺢ‬
F
‫ﻣﺎده رﻳﺰ ﻣﺨﺼﻮص‬
‫ارﺗﻔﺎع ﺑﺨﺶ ﺑﺎز‬
h
‫ﺿﺮﻳﺐ ﻓﻴﻠﻢ ﺳﻴﺎل ﺳﻤﺖ ﻟﻮﻟــــﻪ‬
( W/m².K) ‫( ﻳﺎ‬W/m².°C)
hf
(‫ﻗﻄﺮ داﺧﻠﻲ) ﻣﻴﻠﻲ ﻣﺘﺮ‬
ID
‫ﻣﻴﺎﻧﮕﻴﻦ ﻟﮕﺎرﻳﺘﻤﻲ اﺧﺘﻼف دﻣﺎ‬
LMTD
‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻛﺎري ﻣﺠﺎز‬
MAWP
‫ﺣﺪاﻛﺜﺮ‬
Max.
‫ﻣﻮﻧﻮ اﺗﺎﻧﻮل آﻣﻴﻦ‬
MEA
‫ﺣﺪاﻗﻞ‬
‫ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ ﺣﺪاﻛﺜﺮ‬
11
FPM
Min.
MOP
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
Operating
MOT
MOT
Maximum
Temperature.
OD
Outside Diameter, (mm).
OGP
Oil, Gas and Petrochemical.
OP
Operating Pressure
PHE
Plate Heat Exchanger.
‫ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي‬
PHE
PSV
Pressure Safety Valve.
‫ﺷﻴﺮ اﻳﻤﻨﻲ ﻓﺸﺎري‬
PSV
ri
Fouling resistance on inside
surface of tubes, (m².°C/W).
ro
Fouling resistance on outside
surface of tubes, (m².°C/W).
‫دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ ﺣﺪاﻛﺜﺮ‬
(mm) ‫ﻗﻄﺮ ﺧﺎرﺟﻲ‬
‫ ﮔﺎز و ﭘﺘﺮوﺷﻴﻤﻲ‬،‫ﻧﻔﺖ‬
‫ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ‬
‫درون‬
‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺳﻄﺢ‬
( m².°C/W) ‫ﻟﻮﻟﻪﻫﺎ‬
‫ﺳﻄﺢ ﺑﻴﺮون‬
‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬
( m².°C/W) ‫ﻟﻮﻟﻪﻫﺎ‬
OD
OGP
OP
ri
ro
‫رزﻳﻦ ﺑﻮﺗﻴﻞ ﻋﻤﻞ آورده‬
RCB
‫ﺗﺠﺮﺑﻴﺎت ﻣﻨﺎﺳﺐ ﺗﻮﺻﻴﻪ ﺷﺪه‬
RGP
RCB
Resin Cured Butyl.
RGP
Recommended Good Practice.
SS
Stainless Steel.
TEMA
Tubular Exchanger
Manufacturers Association.
V
Linear Velocity of the fluid,
(m/s).
U
The overall heat transfer
coefficient, (W/m².°C) or
(W/m².K)
WC
Water Column, (mm).
(mm) ‫ﺳﺘﻮن آب‬
WC
 (rho)
Density, (kg/m³).
( kg/m³) ‫ﭼﮕﺎﻟﻲ‬
 (rho)
‫ﻓﻮﻻد زﻧﮓ ﻧﺰن‬
‫اﻧﺠﻤﻦ ﺳﺎزﻧﺪﮔﺎن ﻣﺒﺪل ﻟﻮﻟﻪاي‬
SS
TEMA
m/s ‫ﺳﺮﻋﺖ ﺧﻄﻲ ﺳﻴﺎل‬
V
( W/m².°C) ‫ﺿﺮﻳﺐ ﻛﻠﻲ اﻧﺘﻘﺎل ﺣﺮارت‬
( W/m².K) ‫ﻳﺎ‬
U
‫ واﺣﺪﻫﺎ‬-5
5. UNITS
This standard is based on International System of
Units (SI), as per IPS-E-GN-100 except where
otherwise specified.
‫ ﻣﻨﻄﺒﻖ‬،(SI) ‫اﻳﻦ اﺳﺘﺎﻧﺪارد ﺑﺮ ﻣﺒﻨﺎي ﺳﺎﻣﺎﻧﻪ ﺑﻴﻦ اﻟﻤﻠﻠﻲ واﺣﺪﻫﺎ‬
‫ ﻣﻲ ﺑﺎﺷﺪ ﻣﮕﺮ آﻧﻜﻪ در ﻣﺘﻦ‬IPS-E-GN-100 ‫ﺑﺎ اﺳﺘﺎﻧﺪارد‬
.‫اﺳﺘﺎﻧﺪارد ﺑﻪ واﺣﺪ دﻳﮕﺮي اﺷﺎره ﺷﺪه ﺑﺎﺷﺪ‬
12
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PART I
I ‫ﺑﺨﺶ‬
PROCESS DESIGN OF SHELL AND TUBE
HEAT EXCHANGERS
‫ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ‬
‫ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬
6. General Considerations
‫ ﻣﻼﺣﻈﺎت ﻋﻤﻮﻣﻲ‬- 6
6.1 The shell and tube type exchanger is
commonly used in general petroleum processes.
It is inexpensive, easy to clean, available in many
sizes, and can be designed for moderate to high
pressures at reasonable cost. It consists of a
bundle of tubes encased in a shell.
‫ ﻣﺒﺪل ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻣﻌﻤﻮﻻً در ﻓﺮآﻳﻨﺪﻫﺎي ﻧﻔﺘﻲ‬1-6
‫ راﺣﺖ ﺑﺮاي‬،‫ ﻧﻪ ﭼﻨﺪان ﮔﺮان‬.‫ﻣﺘﺪاول اﺳﺘﻔﺎده ﻣﻲﺷﻮد‬
‫ ﻣﻮﺟﻮد در ﺗﻤﺎم اﻧﺪازهﻫﺎ و ﻗﺎﺑﻞ ﻃﺮاﺣﻲ ﺑﺮاي‬،‫ﺗﻤﻴﺰﻛﺎري‬
‫ ﺷﺎﻣﻞ ﻳﻚ‬،‫ﻓﺸﺎرﻫﺎي ﻣﺘﻮﺳﻂ ﺗﺎ ﺑﺎﻻ ﺑﺎ ﻫﺰﻳﻨﻪ ﻣﻌﻘﻮل ﻣﻲﺑﺎﺷﺪ‬
.‫دﺳﺘﻪ ﻟﻮﻟﻪﻫﺎ در درون ﻳﻚ ﭘﻮﺳﺘﻪ ﻣﻲﺑﺎﺷﺪ‬
‫ واﺣﺪﻫﺎي ﻟﻮﻟﻪاي ﻋﻤﻮﻣﺎً ﻳﻚ دﺳﺘﻪ ﻟﻮﻟﻪ ﻣﺘﺤﺮك دارﻧﺪ و‬2-6
6.2 Tubular units in general should have
removable tube bundles and should be of the
floating head type with removable shell covers.
‫ﺗﻮﺻﻴﻪ ﻣﻲ ﮔﺮدد از ﻧﻮع ﻛﻠﮕﻲ ﻣﺘﺤﺮك ﺑﺎ ﻣﺤﺎﻓﻆ ﭘﻮﺳﺘﻪ ﻣﺘﺤﺮك‬
.‫ﺑﺎﺷﺪ‬
:‫اﻧﻮاع اﺳﺘﺜﻨﺎء ﻋﺒﺎرﺗﻨﺪ از‬
Typical exceptions are:
a) Fixed tube sheet exchangers such as
refrigeration
condensers
and
vacuum
condensers.
‫اﻟﻒ( ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪ ﻟﻮﻟﻪاي ﺛﺎﺑﺖ ﻣﺜﻞ ﭼﮕﺎﻟﻨﺪهﻫﺎي ﺗﺒﺮﻳﺪ‬
In this type of
expansion of the
different operating
require the use of
packed joint.
construction, differential
shell and tubes due to
metal temperatures may
an expansion joint or a
‫ اﺧﺘﻼف اﻧﺒﺴﺎط ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪﻫﺎ ﺑﻪ‬،‫در اﻳﻦ ﻧﻮع از ﺳﺎﺧﺖ‬
‫ﺧﺎﻃﺮ دﻣﺎﻫﺎي ﻋﻤﻠﻴﺎﺗﻲ ﻣﺘﻔﺎوت ﻓﻠﺰ ﻣﻤﻜﻦ اﺳﺖ ﻧﻴﺎز ﺑﻪ‬
.‫ داﺷﺘﻪ ﺑﺎﺷﺪ‬،‫اﺳﺘﻔﺎده از اﺗﺼﺎل اﻧﺒﺴﺎﻃﻲ ﻳﺎ اﺗﺼﺎل ﻓﺸﺮده‬
b) "U" tube type for reboilers using steam in
the tube and for exchangers on hydrogen
service. Removable shell covers are not
required for this type.
‫" ﺷﻜﻞ ﺑﺮاي ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎ ﻛﻪ از ﺑﺨﺎر در‬U" ‫ب( ﻧﻮع ﻟﻮﻟﻪ‬
.‫و ﺧﻼء‬
.‫ﻟﻮﻟﻪ اﺳﺘﻔﺎده ﻣﻲﺷﻮد و ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺑﺎ ﻛﺎرﺑﺮي ﻫﻴﺪروژن‬
.‫ﻣﺤﺎﻓﻆ ﭘﻮﺳﺘﻪ ﻣﺘﺤﺮك ﺑﺮاي اﻳﻦ ﻧﻮع ﻻزم ﻧﻴﺴﺖ‬
Fluids having a fouling factor above 0.00035m².K/W(0.002 hr.ft².°F/Btu) should be
routed on the shell side of U-tube exchangers and
on the tube side for floating head type
exchangers. In all cases U-tubes should be
located in the horizontal plane.
‫ ﻣﺘﺮﻣﺮﺑﻊ‬0/00035 ‫ﺳﻴﺎﻻﺗﻲ ﻛﻪ ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺑﻴﺶ از‬
‫ درﺟﻪ ﻓﺎرﻧﻬﺎﻳﺖ ﺑﺮ ﺑﻲ‬.‫ ﻓﻮت ﻣﺮﺑﻊ‬.‫ ﺳﺎﻋﺖ‬0/002) ‫وات‬/‫در ﻛﻠﻮﻳﻦ‬
‫ و در‬U ‫ﺗﻲ ﻳﻮ(دارﻧﺪ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد در ﭘﻮﺳﺘﻪ ﻣﺒﺪلﻫﺎي ﻧﻮع‬
،‫ در ﺗﻤﺎم ﺣﺎﻟﺖﻫﺎ‬.‫ﻟﻮﻟﻪ ﻣﺒﺪلﻫﺎي ﻧﻮع ﻛﻠﮕﻲ ﺷﻨﺎور ﻗﺮار ﮔﻴﺮﻧﺪ‬
.‫" ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد در ﻣﺴﻴﺮ اﻓﻘﻲ ﻗﺮار ﮔﻴﺮﻧﺪ‬U" ‫ﻟﻮﻟﻪﻫﺎي‬
For chemical works, fixed head exchangers
should be used when the shell side fluid is nonfouling. Where the shell side fluid is fouling. Utubes or floating head type bundles should be
used and floating head type tube bundles when
both sides are fouling.
Floating head type tube bundles are to be avoided
for kettle type reboilers and chillers unless agreed
by the Company.
‫در ﺻﻮرﺗﻲ ﻛﻪ ﺳﻴﺎل ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻏﻴﺮ رﺳﻮﺑﻲ ﺑﺎﺷﺪ ﺗﻮﺻﻴﻪ‬
‫ﻣﻲﺷﻮد ﺑﺮاي ﻛﺎرﻫﺎي ﺷﻴﻤﻴﺎﻳﻲ از ﻣﺒﺪلﻫﺎي ﻛﻠﮕﻲ ﺛﺎﺑﺖ‬
‫ در ﺟﺎﻳﻲ ﻛﻪ ﺳﻴﺎل ﺳﻤﺖ ﭘﻮﺳﺘﻪ رﺳﻮب ده ﺑﺎﺷﺪ‬.‫اﺳﺘﻔﺎده ﺷﻮﻧﺪ‬
‫" ﺷﻜﻞ ﻳﺎ ﻛﻠﮕﻲ ﺷﻨﺎور ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد‬U" ‫ﻣﺒﺪلﻫﺎي ﻧﻮع ﻟﻮﻟﻪ‬
‫اﺳﺘﻔﺎده ﺷﻮﻧﺪ و دﺳﺘﻪ ﻟﻮﻟﻪﻫﺎي ﻛﻠﮕﻲ ﺷﻨﺎور زﻣﺎﻧﻲ اﺳﺘﻔﺎده‬
.‫ﻣﻲﺷﻮﻧﺪ ﻛﻪ ﻫﺮدو ﺳﻴﺎل رﺳﻮبده ﺑﺎﺷﻨﺪ‬
‫اﺳﺘﻔﺎده از دﺳﺘﻪ ﻟﻮﻟﻪﻫﺎي ﻛﻠﮕﻲ ﺷﻨﺎور ﺑﺮاي ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎي‬
.‫ ﺑﺎﻳﺪ اﺟﺘﻨﺎب ﺷﻮد‬،‫ﻧﻮع ﻛﺘﺮي و ﺳﺮد ﺳﺎزﻫﺎ ﻣﮕﺮ ﺑﺎ ﺗﻮاﻓﻖ ﺷﺮﻛﺖ‬
13
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
6.3 There are two variations of floating tube sheet
units, the pull-through and the non-pull-through.
In the pullthrough unit, the entire floating tube
sheet and cover assembly may be drawn through
the shell without disassembly. In the non-pullthrough unit, the shell cover and the floating tube
sheet cover must be removed before the bundle
can be taken out of the shell.
IPS-E-PR- 771(1)
‫ ﻗﺎﺑﻞ ﻛﺸﻴﺪن و ﻏﻴﺮ‬،‫ دو ﻧﻮع ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺷﻨﺎور وﺟﻮد دارد‬3-6
‫ ﻛﻞ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺷﻨﺎور‬،‫ در واﺣﺪﻫﺎي ﻗﺎﺑﻞ ﻛﺸﻴﺪن‬.‫ﻗﺎﺑﻞ ﻛﺸﻴﺪن‬
‫و ﻣﺤﺎﻓﻆ آن ﻣﻲﺗﻮاﻧﻨﺪ در ﭘﻮﺳﺘﻪ ﻣﺒﺪل ﺣﺮﻛﺖ ﻛﻨﻨﺪ ﺑﺪون‬
‫ در واﺣﺪﻫﺎي ﻏﻴﺮ ﻗﺎﺑﻞ ﻛﺸﻴﺪن ﻣﺤﺎﻓﻆ ﭘﻮﺳﺘﻪ و‬.‫ﺟﺪاﻛﺮدن آن‬
‫ﻣﺤﺎﻓﻆ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺷﻨﺎور ﺑﺎﻳﺪ ﻗﺒﻞ از ﺧﺎرج ﻛﺮدن دﺳﺘﻪ ﻟﻮﻟﻪ از‬
.‫ﭘﻮﺳﺘﻪ ﺟﺪا ﺷﻮﻧﺪ‬
This requirement is the greatest disadvantage of
the non-pull-through unit. However, due to the
smaller diameter tube sheet which is possible if a
split ring assembly is used to fasten the floating
head cover, the non-pull-through unit requires a
smaller shell for the same surface.
‫اﻳﻦ اﻟﺰام ﺑﺰرﮔﺘﺮﻳﻦ ﻛﺎﺳﺘﻲ واﺣﺪﻫـــﺎي ﻏﻴﺮﻗﺎﺑﻞ ﻛﺸﻴﺪن‬
‫ ﺑﺎ اﻳﻦ وﺟﻮد ﺑﻪ ﺧﺎﻃﺮ ﻗﻄﺮ ﻛﻤﺘﺮ ﺻﻔﺤﻪ ﻟﻮﻟﻪ در ﺻﻮرت‬.‫ﻣﻲﺑﺎﺷﺪ‬
،‫اﺳﺘﻔﺎده از ﻣﺠﻤﻮﻋﻪ ﺣﻠﻘﻪ دو ﺑﺨﺸﻲ ﺑﺮاي ﺑﺴﺘﻦ ﻣﺤﺎﻓﻆ ﻛﻠﮕﻲ‬
‫ ﻗﻄﺮ ﭘﻮﺳﺘﻪ ﻛﻤﺘﺮي‬،‫واﺣﺪﻫﺎي ﻏﻴﺮ ﻗﺎﺑﻞ ﻛﺸﻴﺪن ﺑﺎ ﺳﻄﺢ ﻳﻜﺴﺎن‬
.‫دارﻧﺪ‬
6.4 Listing the above variations in shell and tube
units in order of increasing cost would give the
following tabulation:
‫ ﺑﺎ ﺗﺮﺗﻴﺐ ﺑﻨﺪي ﺣﺎﻟﺖﻫﺎي ﻓﻮق در واﺣﺪﻫﺎي ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬4-6
:‫ آراﻳﺶ زﻳﺮ ﺑﻪ دﺳﺖ ﻣﻲآﻳﺪ‬،‫ﺑﻪ ﺗﺮﺗﻴﺐ اﻓﺰاﻳﺶ ﻫﺰﻳﻨﻪ‬
.‫( واﺣﺪ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﺳﺎده‬1
1) Simple fixed tube sheet unit.
.‫" ﺷﻜﻞ‬U" ‫( واﺣﺪ ﻟﻮﻟﻪ‬2
2) U-tube unit.
3) Fixed tube sheet unit with an expansion
joint or packed joint.
‫( واﺣﺪ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﺑﺎ اﺗﺼﺎل اﻧﺒﺴﺎﻃﻲ ﻳﺎ اﺗﺼﺎل‬3
4) Floating tube sheet unit (pull-through and
non-pull-through).
(‫( واﺣﺪ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺷﻨﺎور )ﻗﺎﺑﻞ و ﻏﻴﺮ ﻗﺎﺑﻞ ﻛﺸﻴﺪن‬4
Shell and tube type exchangers are usually
fabricated to conform to "Class R" of the
Standards of the Tubular Exchanger
Manufacturers Association (TEMA).
‫ﻣﺒﺪلﻫﺎي ﻧﻮع ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻫﻤﻴﺸﻪ ﻣﻄﺎﺑﻖ ﺑﺎ "ﻃﺒﻘﻪ ﺑﻨﺪي‬
‫( ﺳﺎﺧﺘﻪ‬TEMA) ‫" اﻧﺠﻤﻦ ﺳﺎزﻧﺪﮔﺎن ﻣﺒﺪل ﻟــﻮﻟــﻪاي‬R
.‫ﻣﻲﺷﻮﻧﺪ‬
.‫ﻓﺸﺮده‬
‫ ﻳﺎ "ﻃﺒﻘﻪ‬TEMA "R ‫ اﻧﺘﺨﺎب ﻣﺒﺪلﻫﺎي "ﻃﺒﻘﻪ ﺑﻨﺪي‬5-6
6.5 The selection of TEMA "Class R" or TEMA
"Class C" exchangers shall be governed by the
following:
:‫ ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ ﻣﻮارد زﻳﺮ ﺑﺎﺷﺪ‬TEMA "C ‫ﺑﻨﺪي‬
:‫ زﻣﺎﻧﻲ ﻻزم اﺳﺖ ﻛﻪ‬TEMA "R" ‫ ﻃﺒﻘﻪ ﺑﻨﺪي‬1-5-6
6.5.1 TEMA "R" is required when:
a) Tube side or shell side fouling factor is
greater than 0.00035 m².K/W; or
‫اﻟﻒ( ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺳﻤﺖ ﻟﻮﻟﻪ ﻳﺎ ﭘﻮﺳﺘﻪ ﺑﻴﺶ از‬
b) Shell side corrosion allowance is greater
than 3.175 mm (1/8 inch);
‫ ﻣﻴﻠﻴﻤﺘﺮ‬3/175 ‫ب ( ﺧﻮردﮔﻲ ﻣﺠﺎز ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﺑﻴﺶ از‬
.‫وات ؛ ﺑﺎﺷﺪ‬/ ‫ ﻣﺘﺮﻣﺮﺑﻊ ﻛﻠﻮﻳﻦ‬0/00035
1
8
.‫) اﻳﻨﭻ( ﺑﺎﺷﺪ‬
c) Shell side corrosion rate is greater than
0.254 mm/y (10 mils per year).
0/254 ‫ج( ﺷﺪت ﺧﻮردﮔﻲ ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﺑﻴﺶ از‬
.‫ ﻣﻴﻠﺰ در ﺳﺎل( ﺗﺠﺎوز ﻧﻨﻤﺎﻳﺪ‬10)‫ﺳﺎل‬/‫ﻣﻴﻠﻴﻤﺘﺮ‬
‫ ﻣﻲﺗﻮاﻧﺪ زﻣﺎﻧﻲ اﺳﺘﻔﺎده‬TEMA "C "‫ ﻃﺒﻘﻪ ﺑﻨﺪي‬2-5-6
‫ﺷﻮد ﻛﻪ ﻣﺒﺪل ﺑﺮاي ﻧﮕﻬﺪاري ﺗﻤﻴﺰﻛﺎري ﺷﻴﻤﻴﺎﻳﻲ ﻃﺮاﺣﻲ ﺷﺪه‬
‫و ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻫﻢ در ﺳﻤﺖ ﻟﻮﻟﻪ و ﻫﻢ در ﺳﻤﺖ‬
.‫وات ﺗﺠﺎوز ﻧﻨﻤﺎﻳﺪ‬/ ‫ ﻣﺘﺮ ﻣﺮﺑﻊ ﻛﻠﻮﻳﻦ‬0/00035 ‫ﭘﻮﺳﺘﻪ از‬
6.5.2 TEMA "C" may be used when exchanger is
designed for chemical cleaning maintenance and
fouling factor do not exceed 0.00035 m².K/W on
both tube side and shell side.
14
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ ﻣﺒﺪلﻫﺎي اﻓﻘﻲ و ﻋﻤﻮدي‬6-6
6.6 Horizontal and Vertical Exchangers
Heat exchangers should be of the horizontal type,
however, for process requirements and where
cleaning and other maintenance will be infrequent
and space requirements make it more attractive,
the vertical arrangement may be considered and
this should be discussed with the Company.
Centerline elevation of the top bundle of stacked
exchangers shall be limited to 3.5 m except for
large exchangers which shall be limited to two
stacked shells.
‫ ﺑﺎ اﻳﻦ‬،‫ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ از ﻧﻮع اﻓﻘﻲ ﺑﺎﺷﻨﺪ‬
‫وﺟﻮد ﺑﺮاي اﻟﺰاﻣﺎت ﻓﺮآﻳﻨﺪي و ﺟﺎﻳﻲ ﻛﻪ ﺗﻤﻴﺰﻛﺎري و ﺳﺎﻳﺮ‬
‫ آراﻳﺶ‬،‫ﺣﻔﺎﻇﺖﻫﺎ ﻧﺎدر ﺑﻮده و اﻟﺰاﻣﺎت ﺟﺎﻧﻤﺎﻳﻲ ﺿﺮوري ﺑﺎﺷﺪ‬
‫ﻋﻤﻮدي ﻣﻲ ﺗﻮاﻧﺪ ﻣﻼﺣﻈﻪ ﺷﺪه و ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺑﺎ ﺷﺮﻛﺖ‬
‫ ارﺗﻔﺎع ﺧﻂ ﻣﺮﻛﺰي دﺳﺘﻪ ﻟﻮﻟﻪ ﺑﺎﻻﻳﻲ ﻣﺒﺪلﻫﺎي روي‬.‫ﺑﺤﺚ ﺷﻮد‬
‫ ﻣﺘﺮ ﻣﺤﺪود ﺷﻮد ﺑﻪ ﺟﺰ ﻣﺒﺪلﻫﺎي ﺑﺰرگ ﻛﻪ ﺑﻪ‬3/5 ‫ﻫﻢ ﺑﺎﻳﺪ ﺑﻪ‬
.‫دو ﭘﻮﺳﺘﻪ روي ﻫﻢ ﺑﺎﻳﺪ ﻣﺤﺪود ﺷﺪهاﻧﺪ‬
When horizontal arrangements are preferred, the
stacking of exchangers should be considered to
conserve space in the structure.
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﮔﺮدد‬،‫زﻣﺎﻧﻲ ﻛﻪ آراﻳﺶ اﻓﻘﻲ ﺗﺮﺟﻴﺢ داده ﺷﻮد‬
‫اﻣﻜﺎن روي ﻫﻢ ﻗﺮار دادن ﻣﺒﺪلﻫﺎ ﺑﺮاي ﺻﺮﻓﻪﺟﻮﻳﻲ ﻓﻀﺎ در‬
.‫ﺳﺎﺧﺘﺎر در ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮد‬
6.7 The Use of Spiral Plate Heat Exchangers
May be Considered When:
‫زﻣﺎﻧﻲ اﺳﺘﻔﺎده از ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي‬
7-6
:‫ﺣﻠﺰوﻧﻲ ﻣﻤﻜﻦ اﺳﺖ ﻣﻮرد ﻣﻼﺣﻈﻪ ﻗﺮار ﮔﻴﺮد ﻛﻪ‬
a) Small overhead or vent condensers
mounted directly on process vessels are
required.
‫اﻟﻒ( ﭼﮕﺎﻟﻨﺪهﻫﺎي ﺗﺨﻠﻴﻪ ﻳﺎ ﺑﺎﻻﺳﺮي ﻛﻮﭼﻚ ﻣﺴﺘﻘﻴﻢ روي‬
b) Space limitations make use of long shell
and tube units impractical.
‫ب( ﻣﺤﺪودﻳﺖ ﻓﻀﺎ اﺳﺘﻔﺎده از واﺣﺪﻫﺎي ﻣﺒﺪلﻫﺎي ﭘﻮﺳﺘﻪ و‬
.‫ ﻧﻴﺎز ﺑﺎﺷﺪ‬،‫ﻣﺨﺎزن ﻓﺮآﻳﻨﺪي ﺗﻌﺒﻴﻪ ﺷﺪه‬
.‫ﻟﻮﻟﻪاي ﻃﻮﻳﻞ را ﻧﺸﺪﻧﻲ ﺑﻜﻨﺪ‬
6.8 Manufacturer’s standard for shell and tube
heat exchangers may be considered upon
approval of the Company and supplied as
components of other equipment such as:
‫ اﺳﺘﺎﻧﺪارد ﺳﺎزﻧﺪه ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬8-6
‫در ﺻﻮرت ﺗﺄﻳﻴﺪ ﺷﺮﻛﺖ ﻣﻤﻜﻦ اﺳﺖ ﻣﻮرد ﻣﻼﺣﻈﻪ ﻗﺮار ﮔﺮﻓﺘﻪ و‬
:‫ﺑﻪ ﻋﻨﻮان ﺑﺨﺸﻲ از ﺗﺠﻬﻴﺰات زﻳﺮ ﺗﺄﻣﻴﻦ ﮔﺮدد‬
a) Compressor inter/after coolers.
.‫ﺑﻌﺪ ﻛﻤﭙﺮﺳﻮر‬/‫اﻟﻒ( ﺧﻨﻚ ﻛﻨﻨﺪه ﻫﺎي ﻗﺒﻞ‬
b) Steam ejector inter/after condensers.
.‫ﺑﻌﺪ ﻣﻜﻨﺪه ﺑﺨﺎر‬/‫ب( ﭼﮕﺎﻟﻨﺪهﻫﺎي ﻗﺒﻞ‬
c) Machinery lube oil coolers.
. ‫ج( ﺧﻨﻚ ﻛﻨﻨﺪه ﻫﺎي روﻏﻦ روانﻛﺎري ﻣﺎﺷﻴﻦ آﻻت‬
6.8.1 Fig. A.1 in Appendix A shows different
types of shells which has been extracted from
TEMA.
‫ در ﭘﻴﻮﺳﺖ اﻟﻒ اﻧﻮاع ﻣﺨﺘﻠﻒ ﭘﻮﺳﺘﻪﻫﺎ را‬1-‫ ﺷﻜﻞ اﻟﻒ‬1-8-6
.‫ اﺳﺘﺨﺮاج ﺷﺪه ﻧﺸﺎن ﻣﻲدﻫﺪ‬TEMA ‫ﻛﻪ از‬
‫ راﻫﻨﻤﺎي اﻧﺘﺨﺎب ﺑﺮاي اﻧﻮاع ﻣﺒﺪل ﺣﺮارﺗﻲ‬9-6
6.9 Selection Guide for Heat Exchanger Types
Table B.1 in Appendix B is also selection guide
for heat exchanger types which shows significant
feature, applications best suited, limitation and
relative cost in carbon steel construction of heat
exchangers.
‫ در ﭘﻴﻮﺳﺖ )ب( ﻧﻴﺰ راﻫﻨﻤﺎي اﻧﺘﺨﺎب ﺑﺮاي اﻧﻮاع‬1-‫ﺟﺪول ب‬
،‫ ﺑﻬﺘﺮﻳﻦ ﻣﻜﺎن ﻛﺎرﺑﺮد‬،‫ﻣﺒﺪل ﺣﺮارﺗﻲ اﺳﺖ ﻛﻪ ﺧﺼﻮﺻﻴﺎت ﻣﻬﻢ‬
‫ﻣﺤﺪودﻳﺖ و ﻫﺰﻳﻨﻪ ﻣﺮﺑﻮﻃﻪ در ﺳﺎﺧﺖ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺳﺎﺧﺘﻪ‬
.‫ﺷﺪه از ﻓﻮﻻد ﻛﺮﺑﻦ دار را ﻧﺸﺎن ﻣﻲ دﻫﺪ‬
‫ اﻧﺘﺨﺎب ﻧﻮع‬10-6
6.10 Selection of Type
Fixed tube sheet heat exchangers should only be
used in services where:
‫ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﻓﻘﻂ در‬
:‫ﻛﺎرﺑﺮيﻫﺎﻳﻲ اﺳﺘﻔﺎده ﺷﻮﻧﺪ ﻛﻪ‬
- Differential expansion between the tubes
and the shell does not give rise to
unacceptable stresses;
‫ اﺧﺘﻼف اﻧﺒﺴﺎط ﺑﻴﻦ ﻟﻮﻟﻪﻫﺎ و ﭘﻮﺳﺘﻪ ﺑﻪ ﺗﻨﺶ ﻏﻴﺮﻗﺎﺑﻞ‬.‫ﻗﺒﻮل ﻣﻨﺠﺮ ﻧﺸﻮد‬
15
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
- Tube side cleaning, if required, can be done
in situ;
IPS-E-PR- 771(1)
‫ ﺗﻤﻴﺰﻛﺎري ﺑﺨﺶ ﻟﻮﻟﻪ در ﺻﻮرت ﻟﺰوم در ﻣﺤﻞ ﻣﻲﺗﻮاﻧﺪ‬.‫اﻧﺠﺎم ﺷﻮد‬
- Shell side fluid is non-fouling, or
‫ ﺳﻴﺎل ﺑﺨﺶ ﭘﻮﺳﺘﻪ ﻏﻴﺮ رﺳﻮب ده ﺑﺎﺷﺪ ﻳﺎ؛‬-
- Shell side fouling can be removed by
chemical cleaning.
‫ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺑﺨﺶ ﭘﻮﺳﺘﻪ ﺗﻮﺳﻂ ﺗﻤﻴﺰﻛﺎري ﺷﻴﻤﻴﺎﻳﻲ‬.‫ﻗﺎﺑﻞ ﺣﺬف ﺑﺎﺷﺪ‬
U-tube bundle heat exchangers shall only be
used in services where:
‫" ﺷﻜﻞ ﻓﻘﻂ در‬U" ‫ﻣﺒﺪل ﻫﺎي ﺣﺮارﺗﻲ دﺳﺘﻪ ﻟﻮﻟﻪ‬
:‫ﻛﺎرﺑﺮيﻫﺎﻳﻲ ﺑﺎﻳﺪ اﺳﺘﻔﺎده ﺷﻮد ﻛﻪ‬
0/00035 ‫ﻣﻘﺎوﻣﺖ رﺳﻮﺑﻲ ﺑﺨﺶ ﻟﻮﻟﻪ ﻛﻤﺘﺮ از‬
- Tube side fouling resistance is less than
0.00035 (m².K)/W;
-
‫( ؛‬m².K)/W
- Tube side fouling can be removed by
chemical cleaning.
‫ رﺳﻮب ﺑﺨﺶ ﻟﻮﻟﻪ ﺗﻮﺳﻂ ﺗﻤﻴﺰﻛﺎري ﺷﻴﻤﻴﺎﻳﻲ ﻗﺎﺑﻞ ﺣﺬف‬-
U-tube shall not be applied when tube side
mechanical cleaning is required.
‫" ﺷﻜﻞ زﻣﺎﻧﻲ ﻛﻪ ﺗﻤﻴﺰﻛﺎري ﻣﻜﺎﻧﻴﻜﻲ ﺑﺨﺶ ﻟﻮﻟﻪ‬U" ‫ﻟﻮﻟﻪ‬
.‫ ﻧﺒﺎﻳﺪ اﺳﺘﻔﺎده ﺷﻮد‬،‫ﻻزم ﺑﺎﺷﺪ‬
.‫ﺑﺎﺷﺪ‬
Floating head heat exchangers should be used in
all other services except as noted in item 6.1.2.
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻛﻠﮕﻲ ﺷﻨﺎور در ﺑﻘﻴﻪ ﻛﺎرﺑﺮيﻫﺎ ﺑﻪ ﻏﻴﺮ از‬
.‫ ﺑﺎﻳﺪ اﺳﺘﻔﺎده ﺷﻮد‬2-1-6 ‫ﻣﻮارد ﺑﻴﺎن ﺷﺪه در‬
‫ اﻧﺘﺨﺎب ﭘﻮﺳﺘﻪ‬11-6
6.11 Shell Selection
‫ در ﭘﻴﻮﺳﺖ‬1-‫ )ﺷﻜﻞ اﻟﻒ‬E ‫ ﻧﻮع‬،‫ ﭘﻮﺳﺘﻪ ﺗﻚ – راﻫﻪ‬1-11-6
6.11.1 The single-pass shell, Type E (see Fig. A.1
in Appendix A), has the widest application and
should be selected for general duties, except
where significant advantage can be obtained by
using one of the other shell types:
‫اﻟﻒ( داراي وﺳﻴﻌﺘﺮﻳﻦ ﻛﺎرﺑﺮد و ﺑﺮاي وﻇﺎﻳﻒ ﻋﻤﻮﻣﻲ ﺑﺎﻳﺪ اﻧﺘﺨﺎب‬
‫ ﻣﮕﺮ ﺑﺎ اﺳﺘﻔﺎده از ﻧﻮع دﻳﮕﺮ ﭘﻮﺳﺘﻪ ﻣﺰﻳﺖ ﻣﻬﻤﺘﺮي ﺣﺎﺻﻞ‬،‫ﺷﻮد‬
.‫ﺷﻮد‬
6.11.2 Where the shell side pressure drop is a
restricting factor, the divided flow shell Type J or
cross flow shell Type X or double-split flow shell
Type H, should be considered.
‫در ﺻﻮرﺗﻲ ﻛﻪ اﻓﺖ ﻓﺸﺎر ﺑﺨﺶ ﭘﻮﺳﺘﻪ ﭘﺎراﻣﺘﺮ‬
6.11.3 For horizontal shell side thermosiphon
reboilers, the split flow shell Type G or Type H
should be selected.
،‫ ﺑﺮاي ﺑﺨﺶ ﭘﻮﺳﺘﻪ اﻓﻘﻲ ﺑﺎز ﺟﻮشآورﻫﺎي ﺗﺮﻣﻮﺳﻴﻔﻮن‬3-11-6
6.11.4 The kettle type, shell Type K, should be
selected for boiling, where an almost 100%
vaporization, or where a phase separation is
required.
‫ درﺻﺪ ﺗﺒﺨﻴﺮ ﻳﺎ ﺟﺪا ﺷﺪن ﻓﺎز ﻻزم‬100 ‫ ﺟﺎﻳﻲ ﻛﻪ‬4-11-6
2-11-6
‫ ﻳﺎ ﭘﻮﺳﺘﻪ‬J ‫ ﭘﻮﺳﺘﻪ ﺟﺮﻳﺎن ﺗﻘﺴﻴﻢ ﺷﺪه ﻧﻮع‬،‫ﻣﺤﺪودﺳﺎزي ﺑﺎﺷﺪ‬
‫ ﻳﺎ ﭘﻮﺳﺘﻪ ﺟﺮﻳﺎن ﺗﻘﺴﻴﻢ ﺷﺪه دوﮔﺎﻧﻪ ﻧﻮع‬X ‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ ﻧﻮع‬
.‫ ﺑﺎﻳﺪ ﻣﻮرد ﺑﺮرﺳﻲ ﻗﺮار ﮔﻴﺮد‬H
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد‬H ‫ ﻳﺎ ﻧﻮع‬G ‫ﭘﻮﺳﺘﻪ ﺟﺮﻳﺎن ﺗﻘﺴﻴﻢ ﺷﺪه ﻧﻮع‬
.‫اﻧﺘﺨﺎب ﺷﻮد‬
‫ ﺑﺮاي ﺟﻮﺷﺶ‬.،K ‫ ﻧﻮع‬،‫ﺑﺎﺷﺪ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﭘﻮﺳﺘﻪ ﻧﻮع ﻛﺘﺮي‬
.‫اﻧﺘﺨﺎب ﺷﻮد‬
6.11.5 Use of the two-pass shell with longitudinal
baffle Type F, should be avoided.
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد اﺳﺘﻔﺎده از ﭘﻮﺳﺘﻪ دو راﻫﻪ ﺑﺎ ﺿﺨﺎﻣﺖ‬5-11-6
6.12 Front End and Rear End Selection
‫ اﻧﺘﺨﺎب اﺑﺘﺪا و اﻧﺘﻬﺎي ﻣﺒﺪل‬12-6
‫ ﻣﻌﻤﻮﻻً ﺑﺮاي ﻣﺒﺪﻟﻬﺎي ﺣﺮارﺗﻲ‬B ‫ اﺑﺘﺪاي ﻛﻼﻫﻚ ﻧﻮع‬1-12-6
‫ اﺳﺘﻔﺎده‬،‫ﻛﻪ ﺗﻤﻴﺰﻛﺎري درﺑﺨﺶ ﻟﻮﻟﻪ ﺑﻪ ﻧﺪرت اﻧﺠﺎم ﻣﻲﮔﻴﺮد‬
.‫ﺷﻮد‬
.‫ اﺟﺘﻨﺎب ﺷﻮد‬F ‫ﺟﺪا ﻛﻨﻨﺪه ﻃﻮﻟﻲ ﻧﻮع‬
6.12.1 Front end bonnet Type B is generally used
for heat exchangers where cleaning on the tube
side will be infrequent.
16
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
Rear end Type S should be used for floating head
heat exchangers.
‫ ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻛﻠﮕﻲ‬S ‫ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد اﻧﺘﻬﺎي ﻧﻮع‬
.‫ﺷﻨﺎور اﺳﺘﻔﺎده ﺷﻮد‬
6.12.2 Rear end Type M should be applied for
fixed tube sheet design.
‫ ﺑﺮاي ﻃﺮاﺣﻲ ﺻﻔﺤﻪ‬M ‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد اﻧﺘﻬﺎي ﻧﻮع‬2-12-6
6.12.3 When frequent tube side cleaning is
anticipated, and the tube design pressure is low,
the front end stationary head shall be Type A,
however, for the corresponding rear end, Type L
may be selected.
‫ زﻣﺎﻧﻲ ﻛﻪ ﺗﻤﻴﺰﻛﺎري ﺑﺨﺶ ﻟﻮﻟﻪ ﺑﻪ ﺻﻮرت ﭘﻲ در ﭘﻲ‬3-12-6
.‫ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﺑﻪ ﻛﺎر رود‬
‫ ﻛﻠﮕﻲ ﺛﺎﺑﺖ اﺑﺘﺪا‬،‫ﭘﻴﺶ ﺑﻴﻨﻲ ﺷﻮد و ﻓﺸﺎر ﻃﺮاﺣﻲ ﻟﻮﻟﻪ ﻛﻢ ﺑﺎﺷﺪ‬
"L" ‫ ﺑﺮاي ﺗﻄﺎﺑﻖ اﻧﺘﻬﺎي ﻧﻮع‬،‫ ﺑﺎ اﻳﻦ وﺟﻮد‬.‫ ﺑﺎﺷﺪ‬A ‫ﺑﺎﻳﺪ از ﻧﻮع‬
.‫ﻣﻤﻜﻦ اﺳﺖ اﺳﺘﻔﺎده ﺷﻮد‬
6.12.4 For high-pressure and/or very toxic
service, where it is desirable to limit the number
of external joints, stationary heads Type B, Type
C or Type N should be selected for the front end,
and the corresponding Type M or Type N for the
rear end.
‫ﻳﺎ‬/‫ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺑﺮاي ﻛﺎرﺑﺮيﻫـﺎي ﻓﺸﺎر ﺑﺎﻻ و‬
4-12-6
‫ﺑﺴﻴﺎر ﺳﻤﻲ ﻛـــﻪ ﻣﺤﺪود ﻛﺮدن ﺗﻌﺪاد اﺗﺼﺎﻻت ﺧﺮوﺟﻲ ﻣﻄﻠﻮب‬
‫" ﺑﺮاي اﺑﺘﺪا‬N" ‫" ﻳﺎ ﻧﻮع‬C" ‫" ﻧﻮع‬B" ‫ ﻛﻠﮕﻲﻫﺎي ﺛﺎﺑﺖ ﻧﻮع‬،‫اﺳﺖ‬
.‫ ﺑﺮاي اﻧﺘﻬﺎ اﻧﺘﺨﺎب ﺷﻮد‬N ‫ ﻳﺎ ﻧﻮع‬M ‫و ﻣﻌﺎدل آن از ﻧﻮع‬
‫ و ﺻﻔﺤﻪ ﻟﻮﻟﻪ‬P ‫ ﻛﻠﮕﻲ ﺷﻨﺎور ﻓﺸﺮده ﺧﺎرﺟﻲ ﻧﻮع‬5-12-6
6.12.5 The outside packed floating head Type P,
and externally sealed floating tubesheet type W
rear ends, are not acceptable.
.‫ اﻧﺘﻬﺎ ﻣﻮرد ﻗﺒﻮل ﻧﻴﺴﺘﻨﺪ‬W ‫ﺷﻨﺎور آب ﺑﻨﺪي ﺷﺪه ﺧﺎرﺟﻲ ﻧﻮع‬
‫ ﺧﻨﻚ ﻛﻨﻨﺪه ﻫﺎي ﺳﺮد ﻛﻦ آﺑﻲ‬13-6
6.13 Water-Cooled Coolers
The following restrictions shall apply to watercooled coolers:
‫ﻣﺤﺪودﻳﺖﻫﺎي زﻳﺮ ﺑﺎﻳﺪ ﺑﻪ ﺧﻨﻚ ﻛﻨﻨﺪهﻫﺎي ﺳﺮدﻛﻦ آﺑﻲ اﻋﻤﺎل‬
:‫ﺷﻮﻧﺪ‬
6.13.1 Cooling water shall run upwards through
the tubes in order to avoid build up of gas. The
tube side velocity shall be as specified in Table 1.
‫ آب ﺧﻨﻚ ﻛﻨﻨﺪه ﺑﺮاي ﺟﻠﻮﮔﻴﺮي از ﺗﺠﻤﻊ ﮔﺎز ﺑﺎﻳﺪ ﺑﻪ‬1-13-6
‫ ﺳﺮﻋﺖ در ﺳﻤﺖ ﻟﻮﻟﻪ ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ ﺟﺪول‬.‫ﺳﻤﺖ ﺑﺎﻻ ﺣﺮﻛﺖ ﻛﻨﺪ‬
.‫ ﺑﺎﺷﺪ‬1
6.13.2 The tube side shall be maintained at an
atmospheric over-pressure so that air cannot
separate from the water.
‫ ﺳﻤﺖ ﻟﻮﻟﻪ ﺑﺎﻳﺪ در ﻓﺸﺎر اﺿﺎﻓﻲ ﺟﻮي ﻗﺮار ﮔﻴﺮد ﺗﺎ‬2-13-6
6.13.3 In open cooling water systems, the cooling
water outlet temperature shall not be higher than
42°C, and to avoid scaling, the tube wall
temperature on the cooling water side shall not
exceed 52°C.
‫ دﻣـﺎي ﺧﺮوﺟـﻲ‬،‫ در ﺳﺎﻣﺎﻧﻪﻫﺎي ﺑﺎز آب ﺧﻨﻚ ﻛﻨﻨﺪه‬3-13-6
.‫ﻫﻮا از آب ﺟﺪا ﻧﺸﻮد‬
‫ درﺟـﻪ ﺳـﺎﻧﺘﻴﮕﺮاد ﺑﻴـﺸﺘﺮ ﺷـﻮد و‬42 ‫آب ﺧﻨﻚ ﻛﻨﻨﺪه ﻧﺒﺎﻳـﺪ از‬
‫ دﻣﺎي ﺟﺪاره ﻟﻮﻟﻪ در ﺳﻤﺖ آب ﺧﻨـﻚ‬،‫ﺑﺮاي ﺟﻠﻮﮔﻴﺮي از رﺳﻮب‬
.‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﺑﻴﺸﺘﺮ ﺷﻮد‬52 ‫ﻛﻨﻨﺪه ﻧﺒﺎﻳﺪ از‬
6.13.4 Internal bellows shall not be applied.
6.13.5 In fouling services,
additional restrictions apply:
the
.‫ ﻓﺎﻧﻮسﻫﺎي داﺧﻠﻲ ﻧﺒﺎﻳﺪ ﺑﻪ ﻛﺎر روﻧﺪ‬4-13-6
following
‫ در ﻛﺎرﺑﺮيﻫﺎي رﺳﻮبده ﻣﺤﺪودﻳﺖﻫﺎي اﺿﺎﻓﻲ زﻳﺮ‬5-13-6
:‫ﺑﺎﻳﺪ اﻋﻤﺎل ﺷﻮد‬
6.13.5.1 In cases where flow control of the water
is required, tube side velocities should not be
allowed to fall below the values specified in
Table 1, in order to avoid deposits of mud, silt or
salt.
،‫ در ﺣﺎﻟﺖﻫﺎﻳﻲ ﻛﻪ ﻛﻨﺘﺮل دﺑﻲ آب ﻻزم ﺑﺎﺷﺪ‬1-5-13-6
‫ﺳﺮﻋﺖ در ﺳﻤﺖ ﻟﻮﻟﻪ ﺗﻮﺻﻴﻪ ﻧﻤﻲ ﺷﻮد ﺑﻪ زﻳﺮ ﺳﺮﻋﺖﻫﺎي‬
‫ ﺑﻪ ﻣﻨﻈﻮر ﺟﻠﻮﮔﻴﺮي از ﺗﻪ ﻧﺸﻴﻦ ﺷﺪن‬1 ‫ﻣﺸﺨﺺ ﺷﺪه در ﺟﺪول‬
.‫ ﺑﺮﺳﺪ‬،‫ ﻻي و ﻧﻤﻚ‬،‫ﻟﺠﻦ‬
17
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
.‫" ﻧﺒﺎﻳﺪ ﺑﻪ ﻛﺎر رود‬U" ‫ ﻟﻮﻟﻪﻫﺎي ﻧﻮع‬2-5-13-6
6.13.5.2 U-tubes shall not be applied.
200 ‫ در ﺻﻮرت ﺑﺎﻻﺑﻮدن دﻣﺎي ﺳﻤﺖ ﻣﺤﺼﻮل از‬6-13-6
6.13.6 Shell and tube exchangers using water as
the cooling medium are to be avoided when
product side temperatures exceed 200°C.
‫ اﺳﺘﻔﺎده از ﻣﺒﺪلﻫﺎي ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻛﻪ در آن‬،‫درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد‬
،‫از آب ﺑﻪ ﻋﻨﻮان ﻣﺎده واﺳﻄﻪ ﺧﻨﻚ ﻛﻨﻨﺪه اﺳﺘﻔﺎده ﻣﻲﺷﻮد‬
.‫اﺟﺘﻨﺎب ﮔﺮدد‬
‫ اﻟﺰاﻣﺎت ﻋﻤﻮﻣﻲ‬-7
7. GENERAL REQUIREMENTS
‫ اﺧﺘﺼﺎص ﺳﻴﺎل‬1-7
7.1 Fluid Allocation
Fluid allocation shall be made under the
following conditions.
:‫اﺧﺘﺼﺎص ﺳﻴﺎل ﺑﺎﻳﺪ ﺗﺤﺖ ﺷﺮاﻳﻂ زﻳﺮ اﻧﺠﺎم ﺷﻮد‬
7.1.1 Dirty fluids are passed thorough the tubes
because they can be easily cleaned, particularly if
the tube bundle cannot be removed, but through
the shell if the tubes cannot be cleaned (hair pin
bundles) or if large amounts of coke or debris are
present which can be accumulated in the shell and
removed by dumping the shell.
‫ ﺳﻴﺎﻻت ﻛﺜﻴﻒ ﺑــﻪ ﺧﺎﻃﺮ ﺗﻤﻴﺰﻛﺎري آﺳﺎن از داﺧﻞ‬1-1-7
‫ﻟﻮﻟﻪﻫﺎ ﻋﺒﻮر ﻣﻲﻛﻨﻨﺪ ﻣﺨﺼﻮﺻﺎً اﮔﺮ دﺳﺘﻪ ﻟﻮﻟﻪ ﻏﻴﺮﻗﺎﺑﻞ ﺗﺤﺮك‬
‫ اﻣﺎ در ﭘﻮﺳﺘﻪ اﮔﺮ ﻟﻮﻟﻪﻫﺎ ﻏﻴﺮ ﻗﺎﺑﻞ ﺗﻤﻴﺰﻛﺎري ﺑﺎﺷﻨﺪ )دﺳﺘﻪ‬،‫ﺑﺎﺷﺪ‬
‫ﻟﻮﻟﻪﻫﺎي ﻣﻴﻠﻪ ﻣﻮﻳﻲ( ﻳﺎ ﻣﻘﺪار زﻳﺎدي از ﻛﻚ ﻳﺎ ذرات وﺟﻮد دارﻧﺪ‬
‫ﻛﻪ در داﺧﻞ ﭘﻮﺳﺘﻪ ﺟﻤﻊ ﻣﻲﺷﻮﻧﺪ و ﺑﺎ روﺑﺮداري ﭘﻮﺳﺘﻪ از ﺑﻴﻦ‬
.‫ﻣﻲروﻧﺪ‬
7.1.2 High pressure fluids, corrosive stock, and
water are sent through the tubes because the
strength of small-diameter (and thin) tube
surpasses that of the shell, because corrosionresistant tubes are relatively cheap, and because
corrosion or water scale can be easily removed.
‫ﺑﻪ ﺧﺎﻃﺮ ﺑﺎﻻ ﺑﻮدن اﺳﺘﺤﻜﺎم ﻟﻮﻟﻪ ﺑﺎ ﻗﻄﺮ ﻛﻮﭼﻚ‬
2-1-7
‫)ﺑﺎرﻳﻚ( در ﭘﻮﺳﺘﻪ و ﺑﻪ ﻋﻠﺖ ﻧﺴﺒﺘﺎً ارزان ﺑﻮدن ﻟﻮﻟﻪﻫﺎي ﻣﻘﺎوم‬
‫در ﺑﺮاﺑﺮ ﺧﻮرﻧﺪﮔﻲ و اﻳﻨﻜﻪ ﻣﻮاد ﺧﻮرﻧﺪه و رﺳﻮب آب ﺑﻪ آﺳﺎﻧﻲ‬
‫ ﺧﻮرﻧﺪه و آب را از‬،‫ ﺳﻴﺎلﻫﺎي ﺑﺎ ﻓﺸﺎر ﺑﺎﻻ‬،‫ﺑﺮﻃﺮف ﻣﻲ ﺷﻮﻧﺪ‬
.‫داﺧﻞ ﻟﻮﻟﻪﻫﺎ ﻋﺒﻮر ﻣﻲدﻫﻨﺪ‬
7.1.3 For the same pressure drop, higher heattransfer coefficients will be obtained on the tubeside than the shell-side.
‫ ﺿﺮاﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﺑﺰرﮔﺘﺮ در‬،‫ ﺑﺎ اﻓﺖ ﻓﺸﺎر ﻳﻜﺴﺎن‬3-1-7
7.1.4 Large volume fluids (vapors) are passed
through the shell because of the availability of
adequate space, but small volume fluids are also
passed through the shell where cross baffles can
be used to increase the transfer rates without
producing an excessive pressure drop.
‫ ﺳﻴﺎﻻت ﺑﺎ ﺣﺠﻢ زﻳﺎد‬،‫ ﺑﻪ ﺧﺎﻃﺮ وﺟﻮد ﻓﻀﺎي ﻣﻨﺎﺳﺐ‬4-1-7
.‫ﺑﺨﺶ ﻟﻮﻟﻪﻫﺎ ﻧﺴﺒﺖ ﺑﻪ ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻣﻲﺑﺎﺷﺪ‬
‫)ﺑﺨﺎرات( از ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻋﺒﻮر داده ﻣﻲﺷﻮﻧﺪ اﻣﺎ ﺳﻴﺎﻻت ﺑﺎ‬
‫ﺣﺠﻢ ﻛﻢ ﻧﻴﺰ در ﺻﻮرﺗﻲ ﻛﻪ از ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻋﺮﺿﻲ ﺑﺮاي‬
،‫اﻓﺰاﻳﺶ ﺷﺪت اﻧﺘﻘﺎل ﺑﺪون اﻳﺠﺎد اﻓﺖ ﻓﺸﺎر اﺿﺎﻓﻲ اﺳﺘﻔﺎده ﺷﻮد‬
.‫از ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻋﺒﻮر داده ﻣﻲﺷﻮﻧﺪ‬
7.1.5 Vapors that contain non-condensable gases
are sent through the tubes so that the
accumulation of noncondensables will be swept
out.
‫ ﺑﺨﺎرﻫﺎﻳﻲ ﻛﻪ ﺷﺎﻣﻞ ﮔﺎزﻫﺎي ﻏﻴﺮﻗﺎﺑﻞ ﭼﮕﺎﻟﺶ ﺑﺎﺷﻨﺪ ﺑﻪ‬5-1-7
‫ﺳﻤﺖ ﻟﻮﻟﻪﻫﺎ ﻓﺮﺳﺘﺎده ﻣﻲﺷﻮﻧﺪ ﻛﻪ از ﺗﺠﻤﻊ ﮔﺎزﻫﺎي ﻏﻴﺮﻗﺎﺑﻞ‬
.‫ﺗﺮاﻛﻢ ﺟﻠﻮﮔﻴﺮي ﻣﻲﺷﻮد‬
7.1.6 If the pressure drop must be low, the fluids
are sent through the shell. The same applies to
viscous or low transfer rate fluids because the
maximum transfer rates for a fixed pressure drop
can be obtained by the use of cross baffles in the
shell.
‫ ﺳﻴﺎﻻت ﺑﺎﻳﺪ ﺑﻪ‬،‫ اﮔﺮ ﻻزم ﺷﻮد ﻛﻪ اﻓﺖ ﻓﺸﺎر ﻛﻢ ﺑﺎﺷﺪ‬6-1-7
‫ و ﻛﺎر ﻣﺸﺎﺑﻪ ﻧﻴﺰ ﺑﺮاي ﺳﻴﺎﻻت ﺑﺎ‬.‫ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻓﺮﺳﺘﺎده ﺷﻮﻧﺪ‬
‫ﮔﺮاﻧﺮوي ﺑﺎﻻ ﻳﺎ ﺷﺪت اﻧﺘﻘﺎل ﻛﻢ اﻋﻤﺎل ﻣﻲﺷﻮد ﺑﻪ دﻟﻴﻞ اﻳﻨﻜﻪ‬
‫ﺣﺪاﻛﺜﺮ ﻣﻘﺪار اﻧﺘﻘﺎل ﺑﺮاي اﻓﺖ ﻓﺸﺎر ﺛﺎﺑﺖ ﺑﺎ اﺳﺘﻔﺎده از ﺻﻔﺤﺎت‬
.،‫ﺟﺪا ﻛﻨﻨﺪه ﻋﺮﺿﻲ در ﭘﻮﺳﺘﻪ ﻗﺎﺑﻞ دﺳﺘﻴﺎﺑﻲ اﺳﺖ‬
18
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
7.1.7 In fin tube equipment, high-pressure, dirty,
or corrosive stock is sent through the fin tube
because it is relatively cheap, can be easily
cleaned, and has a higher strength than the
outside tube.
IPS-E-PR- 771(1)
‫ ﻛﺜﻴﻒ ﻳﺎ‬،‫ ﺳﻴﺎل ﺑﺎ ﻓﺸﺎر ﺑﺎﻻ‬،‫ در ﺗﺠﻬﻴﺰ ﻟﻮﻟﻪ ﭘﺮه دار‬7-1-7
‫ﺧﻮرﻧﺪه ﺑﻪ ﺳﻤﺖ ﻟﻮﻟﻪ ﭘﺮه دار ﻓﺮﺳﺘﺎده ﻣﻲﺷﻮد زﻳﺮا ﻧﺴﺒﺘﺎً ارزان‬
‫ﺑﻮده و ﺑﻪ راﺣﺘﻲ ﺗﻤﻴﺰ ﺷﺪه و ﻣﻘﺎوﻣﺖ ﺑﺎﻻﺗﺮي ﻧﺴﺒﺖ ﺑﻪ ﻟﻮﻟﻪ‬
.‫ﺑﻴﺮوﻧﻲ دارد‬
7.1.8 Condensing steam is normally passed
through the tubes.
‫ ﺑﺨﺎر ﭼﮕﺎﻟﺶ ﺷﻮﻧﺪه ﺑﻪ ﺻﻮرت ﻣﺘﺪاول از ﺳﻤﺖ ﻟﻮﻟﻪﻫﺎ‬8-1-7
7.1.9 If the temperature change of one fluid is
very large (greater than approximately 145°C to
175°C), that fluid is usually passed through the
shell, rather than the tubes, if more than one tube
pass is to be used. This minimizes the
construction problems caused by thermal
expansion. Also, to avoid thermal stress
problems, fluids with greater than 175°C
temperature change cannot be passed through the
shell side of a two pass shell.
‫اﮔﺮ ﺗﻐﻴﻴﺮ دﻣﺎ در ﺳﻴﺎل ﺑﺴﻴﺎر ﺑﺰرگ ﺑﺎﺷﺪ )ﺑﻴﺸﺘﺮ از‬9-1-7
‫ ﺳﻴﺎل ﻋﻤﻮﻣﺎً در ﺳﻤﺖ‬،(‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد‬175 ‫ ﺗﺎ‬145 ً‫ﺗﻘﺮﻳﺒﺎ‬
‫ﭘﻮﺳﺘﻪ و ﻧﻪ از ﺳﻤﺖ ﻟﻮﻟﻪ ﻋﺒﻮر ﻣﻲﻛﻨﺪ اﮔﺮ ﺑﻴﺶ از ﻳﻚ راﻫﻪ ﻟﻮﻟﻪ‬
‫ اﻳﻦ ﻣﺸﻜﻼت ﺳﺎﺧﺖ را ﻛﻪ از اﻧﺒﺴﺎط دﻣﺎﻳﻲ ﻣﻨﺠﺮ‬.‫اﺳﺘﻔﺎده ﺷﻮد‬
‫ ﻫﻤﭽﻨﻴﻦ ﺑﺮاي اﺟﺘﻨﺎب از ﻣﺸﻜﻼت‬.‫ﻣﻲﺷﻮد ﻛﺎﻫﺶ ﻣﻲدﻫﺪ‬
‫ درﺟﻪ‬175 ‫ ﺳﻴﺎﻻت ﺑﺎ ﺗﻐﻴﻴﺮ دﻣﺎي ﺑﺰرﮔﺘﺮ از‬،‫ﺗﻨﺶ ﺣﺮارﺗﻲ‬
‫ﺳﺎﻧﺘﻴﮕﺮاد ﻧﺒﺎﻳﺪ در ﺳﻤﺖ ﭘﻮﺳﺘﻪ از ﻧﻮع ﭘﻮﺳﺘﻪ دو راﻫﻪ ﻋﺒﻮر‬
.‫داده ﺷﻮﻧﺪ‬
If the temperatures are high enough to require the
use of special alloys placing the higher
temperature fluid in the tubes will reduce the
overall cost. At moderate temperatures, placing
the hotter fluid in the tubes will reduce the shell
surface temperatures, and hence the need for
lagging to reduce heat loss, or for safety reasons.
‫اﮔﺮ دﻣﺎ ﺑﻪ ﺣﺪ ﻛﺎﻓﻲ ﺑﺎﻻ ﺑﺎﺷﺪ ﻛﻪ ﻧﻴﺎز ﺑﻪ اﺳﺘﻔﺎده از آﻟﻴﺎژ ﺧﺎص‬
‫ ﻫﺰﻳﻨﻪ ﻛﻠﻲ را ﻛﺎﻫﺶ‬،‫ ﺗﻌﺒﻴﻪ ﺳﻴﺎل دﻣﺎي ﺑﻴﺸﺘﺮ در ﻟﻮﻟﻪﻫﺎ‬،‫ﺑﺎﺷﺪ‬
‫ دﻣﺎي‬،‫ در دﻣﺎﻫﺎي ﻣﺘﻮﺳﻂ ﺗﻌﺒﻴﻪ ﺳﻴﺎل ﮔﺮم در ﻟﻮﻟﻪﻫﺎ‬.‫ﻣﻲدﻫﺪ‬
‫ﺳﻄﺢ ﭘﻮﺳﺘﻪ و ﻫﻤﭽﻨﻴﻦ ﻧﻴﺎز ﺑﻪ ﻋﺎﻳﻖ ﻛﺎري ﺑﺮاي ﻛﺎﻫﺶ اﺗﻼف‬
.‫ﺣﺮارﺗﻲ ﻳﺎ دﻻﻳﻞ اﻳﻤﻨﻲ را ﻛﺎﻫﺶ ﻣﻲدﻫﺪ‬
7.1.10 If one of the fluids is clean (fouling factor
0.00017 m².°C/W) and is only mildly corrosive to
the material selected this fluid is passed through
the tubes and U-tube construction is used, where
economical.
‫ اﮔﺮ ﻳﻜﻲ از ﺳﻴﺎﻻت ﺗﻤﻴﺰ ﺑﺎﺷﺪ )ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬10-1-7
.‫ﻋﺒﻮر ﻣﻲﻛﻨﺪ‬
‫ ( و ﻓﻘﻂ ﺑﺎ درﺟﻪ ﺧﻮرﻧﺪﮔﻲ ﻣﺘﻮﺳﻂ ﻓﻠﺰ‬m².°C/W0/00017
‫ اﻳﻦ ﺳﻴﺎل از ﺳﻤﺖ ﻟﻮﻟﻪﻫﺎ ﻋﺒﻮر داده ﺷﺪ و‬.‫اﻧﺘﺨﺎب ﺷﺪه ﺑﺎﺷﺪ‬
.‫" ﺷﻜﻞ اﺳﺘﻔﺎده ﻣﻲﺷﻮد ﻛﻪ اﻗﺘﺼﺎدي ﻣﻲﺑﺎﺷﺪ‬U" ‫ﺳﺎﺧﺘﺎر ﻟﻮﻟﻪ‬
‫ ﮔﺮاﻧﺮوي‬11-1-7
7.1.11 Viscosity
Generally, a higher heat-transfer coefficient will
be obtained by allocating the more viscous
material to the shell-side, providing the flow is
turbulent. The critical Reynolds number for
turbulent flow in the shell is in the region of 200.
If turbulent flow cannot be achieved in the shell it
is better to place the fluid in the tubes, as the
tube-side heat-transfer coefficient can be
predicted with more certainty.
‫ در ﺻﻮرﺗﻲ ﻛـــﻪ ﺟﺮﻳﺎن ﻣﺘﻼﻃﻢ ﺑﺎﺷﺪ ﺿﺮﻳﺐ اﻧﺘﻘﺎل‬،ً‫ﻋﻤﻮﻣﺎ‬
‫ﺣﺮارت ﺑﺰرﮔﺘﺮ ﺑﺎ اﺧﺘﺼﺎص ﻣﻮاد ﮔﺮاﻧﺮوﺗﺮ ﺑــﻪ ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﺑﻪ‬
‫ ﻋﺪد رﻳﻨﻮﻟﺪز ﺑﺤﺮاﻧﻲ ﺑﺮاي ﺟﺮﻳﺎن درﻫﻢ در ﭘﻮﺳﺘﻪ‬.‫دﺳﺖ ﻣﻲآﻳﻨﺪ‬
‫ اﮔﺮ ﺟﺮﻳﺎن ﻣﺘﻼﻃﻢ در ﺳﻤﺖ ﭘﻮﺳﺘﻪ اﻳﺠﺎد‬.‫ ﻣﻲﺑﺎﺷﺪ‬200 ‫ﺣﺪود‬
‫ ﺑﻬﺘﺮ اﺳﺖ ﻛﻪ ﺳﻴﺎل در ﻟﻮﻟﻪﻫﺎ ﻗﺮار ﮔﻴﺮد و ﺿﺮﻳﺐ اﻧﺘﻘﺎل‬،‫ﺷﻮد‬
.‫ﺣﺮارت ﺳﻤﺖ ﻟﻮﻟﻪ ﺑﺎ اﻃﻤﻴﻨﺎن ﺑﻴﺸﺘﺮي ﭘﻴﺶ ﺑﻴﻨﻲ ﺷﻮد‬
‫ ﻧﺼﺐ‬2-7
7.2 Installation
7.2.1 Vertical
‫ ﻋﻤﻮدي‬1-2-7
a)
Condensate
subcooling
may
be
accomplished more easily in a vertical unit.
‫اﻟﻒ( ﻓﻮق ﺳﺮدﻛﺮدن ﻣﻴﻌﺎﻧﺎت در واﺣﺪﻫﺎي ﻋﻤﻮدي ﺑﻪ‬
.‫راﺣﺘﻲ اﻧﺠﺎم ﻣﻲﺷﻮد‬
19
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
b) For boiling fluids, this is usually a single
tube pass type with vaporization occurring in
the tubes.
IPS-E-PR- 771(1)
‫ب ( ﺑﺮاي ﺳﻴﺎﻻت ﺟﻮﺷﺎن ﻧﻮع ﻳﻚ راﻫﻪ ﻟﻮﻟﻪ ﺑﺎ ﺗﺒﺨﻴﺮي ﻛﻪ‬
.‫ ﻣﺘﺪاول اﺳﺖ‬،‫در ﻟﻮﻟﻪﻫﺎ اﺗﻔﺎق ﻣﻲاﻓﺘﺪ‬
‫ ﻣﻮرب‬2-2-7
7.2.2 Inclined
For tube side condensing fluids, this type of heat
exchanger is sometimes employed to ensure
positive drainage of the condensate from the tube.
Even a few degrees inclination from the
horizontal prevents the accumulation of
condensate and possible redistribution, flooding,
and surging effects.
‫ اﻳﻦ ﻧﻮع از ﻣﺒﺪل ﺣﺮارﺗﻲ‬،‫ﺑﺮاي ﺳﻴﺎﻻت ﻣﺎﻳﻊ ﺷﺪه ﺳﻤﺖ ﻟﻮﻟﻪ‬
‫ﺑﺮاي اﻃﻤﻴﻨﺎن از ﺗﺄﻣﻴﻦ ﺗﺨﻠﻴﻪ ﭼﮕﺎﻟﻴﺪه از ﻟﻮﻟﻪﻫﺎ در ﺑﺮﺧﻲ ﻣﻮاﻗﻊ‬
‫ از ﺟﻤﻊ‬،‫ ﺣﺘﻲ ﭼﻨﺪ درﺟﻪ ﺗﻮرب از ﺣﺎﻟﺖ اﻓﻘﻲ‬.‫ﺑﻪ ﻛﺎر ﻣﻲرود‬
‫ ﻃﻐﻴﺎن و اﺛﺮات ﻣﻮج‬،‫ﺷﺪن ﭼﮕﺎﻟﻴﺪه و اﻣﻜﺎن ﺗﻮزﻳﻊ دوﺑﺎره‬
.‫ﻣﻤﺎﻧﻌﺖ ﻣﻲﻛﻨﺪ‬
‫ اﻓﻘﻲ‬3-2-7
7.2.3 Horizontal
Others.
.‫ﺳﺎﻳﺮ ﻣﻮارد‬
‫ ﻣﺤﻞ ﻧﺎزل‬3-7
7.3 Nozzle Location
The following rules are suggested as a guide for
locating heat exchanger nozzles:
‫ﻗﻮاﻋﺪ زﻳﺮ ﺑﺮاي ﻣﺤﻞ ﻧﺎزلﻫﺎي ﻣﺒﺪل ﺣﺮارﺗﻲ ﺑﻪ ﻋﻨﻮان راﻫﻨﻤﺎ‬
.‫ﭘﻴﺸﻨﻬﺎد ﻣﻲﺷﻮﻧﺪ‬
1) Streams being heated or vaporized should
flow from bottom to top, whether on the tube
side or the shell side.
‫( ﺟﺮﻳﺎنﻫﺎﻳﻲ ﻛﻪ ﺑﺎﻳﺪ ﮔﺮم ﺷﻮﻧﺪ ﻳﺎ ﺗﺒﺨﻴﺮ ﺷﻮﻧﺪ ﺧﻮاه ﺳﻤﺖ‬1
2) Streams being condensed should flow from
top to bottom, whether on the tube side or the
shell side.
‫( ﺗﻮﺻﻴﻪ ﻣﻲﺷﻮد ﺟﺮﻳﺎنﻫﺎﻳﻲ ﻛﻪ ﭼﮕﺎﻟﻴﺪه ﻣﻲﺷﻮﻧﺪ ﺧﻮاه‬2
3) The direction of flow of streams being
cooled should be dictated by piping
economics.
‫( ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺟﻬﺖ ﺟﺮﻳﺎنﻫﺎﻳﻲ ﻛﻪ ﺳﺮد ﻣﻲﺷﻮﻧﺪ‬3
.‫ﻟﻮﻟﻪ ﻳﺎ ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﺑﺎﻳﺪ از ﭘﺎﻳﻴﻦ ﺑﻪ ﺑﺎﻻ ﺣﺮﻛﺖ ﻛﻨﻨﺪ‬
.‫ﺳﻤﺖ ﻟﻮﻟﻪ ﻳﺎ ﺳﻤﺖ ﭘﻮﺳﺘﻪ از ﺑﺎﻻ ﺑﻪ ﭘﺎﻳﻴﻦ ﺣﺮﻛﺖ ﻛﻨﺪ‬
.‫ﺗﻮﺳﻂ اﻗﺘﺼﺎد ﻟﻮﻟﻪﻛﺸﻲ ﻣﻌﻴﻦ ﺷﻮد‬
Erosion
‫ ﺻﻔﺤﺎت ﺑﺮﺧﻮردي و ﻣﺤﺎﻓﻆ ﺳﺎﻳﺸﻲ‬4-7
The following paragraphs should provide
limitations to prevent or minimize erosion of tube
bundle components at the entrance and exit areas.
These limitations have no correlation to tube
vibration and the designer should refer to Section
6 of TEMA for information regarding this
phenomenon.
‫ﭘﺎراﮔﺮافﻫﺎي زﻳﺮ ﻣﺤﺪودﻳﺖ ﻫﺎﻳﻲ ﺟﻠﻮﮔﻴﺮي از ﺳﺎﻳﺶ اﺟﺰاء‬
‫دﺳﺘﻪ ﻟﻮﻟﻪ در ﺳﻄﻮح ورودي و ﺧﺮوﺟﻲ و ﻳﺎ ﺑﻪ ﺣﺪاﻗﻞ رﺳﺎﻧﺪن‬
‫ اﻳﻦ ﻣﺤﺪودﻳﺖ ﻫﺎ ﻫﻴﭻ ارﺗﺒﺎﻃﻲ ﺑﺎ ارﺗﻌﺎش‬.‫آﻧﺮا ﻋﺮﺿﻪ ﻣﻲ ﻧﻤﺎﻳﺪ‬
‫ ﺑﺮاي‬TEMA‫ از‬6 ‫ﻟﻮﻟﻪ ﻧﺪارد و ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﻃﺮاح ﺑﻪ ﻗﺴﻤﺖ‬
.‫اﻃﻼع از اﻳﻦ ﭘﺪﻳﺪه ﻣﺮاﺟﻌﻪ ﻧﻤﺎﻳﺪ‬
7.4 Impingement
Protection
Baffles
and
protection
‫ اﻟﺰاﻣﺎت ﺣﻔﺎﻇﺖ ﺑﺮﺧﻮردي ﺳﻤﺖ ﭘﻮﺳﺘﻪ‬1-4-7
An impingement plate, or other means to protect
the tube bundle against impinging fluids, shall be
provided when entrance line values of  V2
exceed the following: non-corrosive, nonabrasive, single phase fluids, 2230: all other
liquids, including a liquid at its boiling point,
744. For all other gases and vapors, including all
nominally saturated vapors, and for liquid vapor
mixtures, impingement protection is required. V
‫ﺻﻔﺤﻪ ﺑﺮﺧﻮردي ﻳﺎ وﺳﺎﻳﻞ دﻳﮕﺮي ﻛﻪ دﺳﺘﻪ ﻟﻮﻟﻪ را از ﺑﺮﺧﻮرد‬
‫ ورودي از‬ V2‫ در ﺻﻮرت اﻓﺰاﻳﺶ‬،‫ﺳﻴﺎل ﻣﺤﺎﻓﻈﺖ ﻣﻲﻛﻨﺪ‬
‫ ﺗﻚ‬،‫ ﻏﻴﺮﺳﺎﻳﻨﺪه‬،‫ ﺳﻴﺎﻻت ﻏﻴﺮﺧﻮرﻧﺪه‬:‫ﻣﻘﺪار زﻳﺮ ﺑﺎﻳﺪ ﺗﻌﺒﻴﻪ ﺷﻮﻧﺪ‬
744 ،‫ ﺷﺎﻣﻞ ﻣﺎﻳﻌﺎت در ﻧﻘﻄﻪ ﺟﻮش‬،‫ ﺳﺎﻳﺮ ﻣﺎﻳﻌﺎت‬:2230 ،‫ﻓﺎز‬
‫ﺑﺮاي ﺳﺎﻳﺮ ﮔﺎزﻫﺎ و ﺑﺨﺎرات ﺷﺎﻣﻞ ﺑﺨﺎرات اﺷﺒﺎع و ﺑﺮاي ﻣﺨﻠﻮط‬
‫ ﺳﺮﻋﺖ ﺧﻄﻲ ﺳﻴﺎل‬V .‫ﻣﺎﻳﻊ ﺑﺨﺎر ﺣﻔﺎﻇﺖ ﺑﺮﺧﻮردي ﻻزم اﺳﺖ‬
7.4.1 Shell side
requirements
impingement
20
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ ﭼﮕﺎﻟﻲ آن ﺑﺮ ﺣﺴﺐ ﻛﻴﻠﻮﮔﺮم ﺑﺮ ﻣﺘﺮ‬ ‫ﺑﺮ ﺣﺴﺐ ﻣﺘﺮ ﺑﺮ ﺛﺎﻧﻴﻪ و‬
‫ ﻣﻤﻜﻦ اﺳﺖ ﺑﺮاي‬،‫ ﭘﺨﺶ ﻛﻦ ﺑﺎ ﻃﺮاﺣﻲ ﻣﻨﺎﺳﺐ‬.‫ﻣﻜﻌﺐ اﺳﺖ‬
.‫ﻛﺎﻫﺶ ﺳﺮﻋﺖ ﺧﻂ در ورودي ﭘﻮﺳﺘﻪ ﺑﻪ ﻛﺎر رود‬
is the linear velocity of the fluid in meter per
second and  is its density in kg per cubic meter.
A properly designed diffuser may be used to
reduce line velocities at shell entrance.
‫ ﺳﻄﻮح ورود و ﺧﺮوج ﭘﻮﺳﺘﻪ و دﺳﺘﻪ ﻟﻮﻟﻪ‬2-4-7
7.4.2 Shell or bundle entrance and exit areas
In no case shall the shell or bundle entrance or
exit area produce a value of  V2 in excess of
5950 where V is the linear velocity of the fluid in
meter per second and  is its density in kilogram
per cubic meter.
‫ﺑﻪ ﻫﻴﭻ وﺟﻪ ﻧﺒﺎﻳﺪ ﭘﻮﺳﺘﻪ و ﻳﺎ ﺳﻄﺢ ورود و ﺧﺮوج ﭘﻮﺳﺘﻪ ﻟﻮﻟﻪ‬
‫ ﺳﺮﻋﺖ ﺧﻄﻲ‬V ‫ ﺗﻮﻟﻴﺪ ﻧﻤﺎﻳﻨﺪ ﻛﻪ‬5950 ‫ ﺑﻴﺶ از‬ V2 ‫ﻣﻘﺪار‬
‫ ﭼﮕﺎﻟﻲ آن ﺑﺮ ﺣﺴﺐ‬ ‫ﺳﻴﺎل ﺑﺮ ﺣﺴﺐ ﻣﺘﺮ ﺑﺮ ﺛﺎﻧﻴﻪ و‬
.‫ﻛﻴﻠﻮﮔﺮم ﺑﺮ ﻣﺘﺮ ﻣﻜﻌﺐ ﻣﻲﺑﺎﺷﺪ‬
7.4.2.1 Shell entrance or exit area with
impingement plate
‫ ﺳﻄﻮح ورود ﻳﺎ ﺧﺮوج ﭘﻮﺳﺘﻪ ﺑﺎ ﺻﻔﺤﻪ ﺑﺮﺧﻮرد‬1-2-4-7
When an impingement plate is provided, the flow
area shall be considered the unrestricted area
between the inside diameter of the shell at the
nozzle and the face of the impingement plate.
‫ ﺳﻄﺢ ﺟﺮﻳﺎن ﺑﺎﻳﺪ‬،‫زﻣﺎﻧﻲ ﻛﻪ ﻳﻚ ﺻﻔﺤﻪ ﺑﺮﺧﻮرد ﺑﻪ ﻛﺎر رود‬
‫ﺳﻄﺢ ﺑﺎز ﺑﻴﻦ ﻗﻄﺮ داﺧﻠﻲ ﭘﻮﺳﺘﻪ در ﻧﺎزل و ﺻﻔﺤﻪ ﺑﺮﺧﻮرد در‬
.‫ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮد‬
7.4.2.2 Shell entrance or exit area without
impingement plate
‫ ﺳﻄﻮح ورود ﻳﺎ ﺧﺮوج ﭘﻮﺳﺘﻪ ﺑﺪون ﺻﻔﺤﻪ‬2-2-4-7
‫ﺑﺮﺧﻮرد‬
For determining the area available for flow at the
entrance or exit of the shell where there is no
impingement plate, the flow area between the
tubes within the projection of the nozzle bore and
the actual unrestricted radial flow area from under
the nozzle or dome measured between the tube
bundle and shell inside diameter may be
considered.
‫ﺑﺮاي ﺗﻌﻴﻴﻦ ﺳﻄﺢ ﻣﻮﺟﻮد ﺟﺮﻳﺎن در ورود ﻳﺎ ﺧﺮوج ﭘﻮﺳﺘﻪ در‬
‫ ﺳﻄﺢ ﺟﺮﻳﺎن ﺑﻴﻦ ﻟﻮﻟﻪﻫﺎ در ﭘﻴﺶ‬،‫ﺻﻮرت ﻧﺒﻮدن ﺻﻔﺤﻪ ﺑﺮﺧﻮرد‬
‫آﻣﺪﮔﻲ داﺧﻠﻲ ﻧﺎزل و ﺳﻄﺢ ﺟﺮﻳﺎن ﺑﺎز ﺷﻌﺎﻋﻲ ﺣﻘﻴﻘﻲ ﻛﻪ از زﻳﺮ‬
‫ ﺑﻴﻦ دﺳﺘﻪ ﻟﻮﻟﻪ و ﻗﻄﺮ‬،‫ﻧﺎزل ﻳﺎ ﺑﺮآﻣﺪﮔﻲ اﻧﺪازه ﮔﺮﻓﺘﻪ ﻣﻲﺷﻮد‬
.‫داﺧﻠﻲ ﭘﻮﺳﺘﻪ ﻣﻤﻜﻦ اﺳﺖ ﻟﺤﺎظ ﺷﻮد‬
7.4.2.3 Bundle entrance or exit area with
impingement plate
‫ ﺳﻄﺢ ورود ﻳﺎ ﺧﺮوج دﺳﺘﻪ ﻟﻮﻟﻪ ﺑﺎ ﺻﻔﺤﻪ‬3-2-4-7
When an impingement plate is provided under a
nozzle, the flow area shall be the unrestricted area
between the tubes within the compartments
between baffles and/or tubesheet.
‫ ﺳﻄﺢ ﺟﺮﻳﺎن‬،‫در ﺻﻮرﺗﻲ ﻛﻪ ﺻﻔﺤﻪ ﺑﺮﺧﻮرد زﻳﺮ ﻧﺎزل ﺗﻌﺒﻴﻪ ﺷﻮد‬
‫ﻳﺎ‬/‫ﺑﺎﻳﺪ ﺳﻄﺢ ﺑﺎز ﺑﻴﻦ ﻟﻮﻟﻪﻫﺎ در ﺑﺨﺶ و ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه و‬
.‫ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺑﺎﺷﺪ‬
7.4.2.4 Bundle entrance or exit area without
impingement plate
‫ ﺳﻄﺢ ورود ﻳﺎ ﺧﺮوج دﺳﺘﻪ ﻟﻮﻟﻪ ﺑﺪون ﺻﻔﺤﻪ‬4-2-4-7
‫ﺑﺮﺧﻮرد‬
‫ﺑﺮﺧﻮرد‬
For determining the area available for flow at the
entrance or exit of the tube bundle where there is
no impingement plate, the flow area between the
tubes within the compartments between baffles
and/or tubesheet may be considered.
‫ﺑﺮاي ﺗﻌﻴﻴﻦ ﺳﻄﺢ ﻣﻮﺟﻮد ﺟﺮﻳﺎن در ورود ﻳﺎ ﺧﺮوج دﺳﺘﻪ ﻟﻮﻟﻪ‬
‫ ﺳﻄﺢ ﺟﺮﻳﺎن ﺑﻴﻦ ﻟﻮﻟﻪﻫﺎ در‬،‫در ﺻﻮرت ﻧﺒﻮدن ﺻﻔﺤﻪ ﺑﺮﺧﻮرد‬
‫ﻳﺎ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﻣﻲﺗﻮاﻧﺪ ﻟﺤﺎظ‬/‫ﺑﺨﺶ ﺑﻴﻦ ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه و‬
.‫ﺷﻮد‬
‫ ﺳﻤﺖ ﻟﻮﻟﻪ‬3-4-7
7.4.3 Tube side
Consideration shall be given to the need for
special devices to prevent erosion of the tube
ends under the following conditions:
‫ ﻧﻴﺎز ﺑﻪ وﺳﺎﻳﻞ‬،‫ﺑﺮاي ﻣﺤﺎﻓﻈﺖ از ﺳﺎﻳﺶ ﺳﺮ ﻟﻮﻟﻪ در ﺷﺮاﻳﻂ زﻳﺮ‬
:‫ﻣﺨﺼﻮص ﻣﻄﺎﺑﻖ ﻣﻮارد زﻳﺮ ﺑﺎﻳﺪ ﺗﻮﺟﻪ ﺷﻮد‬
1) Use of an axial inlet nozzle.
‫( اﺳﺘﻔﺎده از ﻧﺎزل ﻣﺤﻮري ورودي‬1
21
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ ﺳﺮﻋﺖ ﺑﺮ‬V ‫ ﺑﺎﺷﺪ ﻛﻪ‬8925 ‫ ﻣﺎﻳﻊ ﺑﻴﺶ از‬ V2 (2
2) Liquid  V2 is in excess of 8925, where V
is the linear velocity in meter per second, and
 is its density in kg per cubic meter.
‫ ﭼﮕﺎﻟﻲ ﺑﺮ ﺣﺴﺐ ﻛﻴﻠﻮﮔﺮم ﺑﺮ‬ ‫ﺣﺴﺐ ﻣﺘﺮ ﺑﺮ ﺛﺎﻧﻴﻪ و‬
.‫ﻣﺘﺮﻣﻜﻌﺐ ﺑﺎﺷﺪ‬
‫ ﺳﺮﻋﺖﻫﺎي ﺳﻴﺎل ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬1-3-4-7
7.4.3.1 Shell and tube fluid velocities
‫ﺳﺮﻋﺖﻫﺎي ﺑﺎﻻ ﻣﻨﺠﺮ ﺑﻪ ﺿﺮاﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﺑﺎﻻ اﻣﺎ ﻫﻤﭽﻨﻴﻦ‬
‫ ﺳﺮﻋﺖ ﺑﺎﻳﺪ ﺑﻪ اﻧﺪازهاي ﺑﺎﻻ ﺑﺎﺷﺪ ﻛﻪ از‬.‫اﻓﺖ ﻓﺸﺎر ﺑﺎﻻ ﻣﻲﺷﻮﻧﺪ‬
‫ﺗﻪ ﻧﺸﻴﻦ ﺷﺪن ذرات ﻣﻌﻠﻖ ﺟﻠﻮﮔﻴﺮي ﻛﻨﺪ اﻣﺎ ﻧﻪ آﻧﻘﺪر ﻛﻪ ﻣﻨﺠﺮ‬
‫ ﺗﻌﺒﻴﻪ‬.‫ ﺳﺮﻋﺖﻫﺎي ﺑﺎﻻ رﺳﻮب را ﻛﺎﻫﺶ ﻣﻲدﻫﻨﺪ‬.‫ﺑﻪ ﺳﺎﻳﺶ ﺷﻮد‬
‫ﭘﻼﺳﺘﻴﻚﻫﺎ اﻏﻠﺐ ﺑﺮاي ﻛﺎﻫﺶ ﺳﺎﻳﺶ در ورودي ﻟﻮﻟﻪ اﺳﺘﻔﺎده‬
:‫ ﺳﺮﻋﺖﻫﺎي ﻃﺮاﺣﻲ ﻧﻤﻮﻧﻪ در زﻳﺮ آﻣﺪهاﻧﺪ‬.‫ﻣﻲﺷﻮد‬
High velocities will give high heat-transfer
coefficients but also a high-pressure drop. The
velocity must be high enough to prevent any
suspended solids settling, but not so high as to
cause erosion. High velocities will reduce
fouling. Plastics inserts are sometimes used to
reduce erosion at the tube inlet. Typical design
velocities are given below:
‫ ﻣﺎﻳﻌﺎت‬2-3-4-7
7.4.3.2 Liquids
Tube-side, process fluids: 1 to 2 m/s, maximum 4
m/s if required to reduce fouling; water: 1.5 to 2.5
m/s as the following Table 1. Shell-side: 0.3 to 1
m/s.
‫ ﻣﺘﺮ‬4 ‫ ﺣﺪاﻛﺜﺮ‬،‫ ﻣﺘﺮ در ﺛﺎﻧﻴﻪ‬2 ‫ ﺗﺎ‬1 :‫ﺳﻴﺎﻻت ﻓﺮآﻳﻨﺪ ﺳﻤﺖ ﻟﻮﻟﻪ‬
‫ ﻣﺘﺮ‬2/5 ‫ ﺗﺎ‬1/5 : ‫ آب‬:‫در ﺛﺎﻧﻴﻪ در ﺻﻮرت ﻧﻴﺎز ﺑﻪ ﻛﺎﻫﺶ رﺳﻮب‬
.‫ ﻣﺘﺮ در ﺛﺎﻧﻴﻪ‬1 ‫ ﺗﺎ‬0/3 ‫ ﺳﻤﺖ ﭘﻮﺳﺘﻪ‬.1 ‫در ﺛﺎﻧﻴﻪ ﻣﻄﺎﺑﻖ ﺟﺪول‬
TABLE 1 - COOLING WATER VELOCITIES (TUBE SIDE)
(‫ ﺳﺮﻋﺖﻫﺎي آب ﺧﻨﻚ ﻛﻦ )ﺳﻤﺖ ﻟﻮﻟﻪ‬-1 ‫ﺟﺪول‬
TUBE MATERIALS
AVERAGE SPEED
‫ﺟﻨﺲﻫﺎي ﻟﻮﻟﻪ‬
‫ﺳﺮﻋﺖ ﻣﺘﻮﺳﻂ‬
(m/s)
Carbon steel
Admiralty
Aluminum brass
Aluminum bronze
Cupronickel
Aluminum
Monel
Stainless steel
‫ﻓﻮﻻد ﻛﺮﺑﻦ دار‬
‫آﻟﻴﺎژ آﻟﻮﻣﻴﻨﻤﻲ‬
‫آﻟﻮﻣﻴﻨﻴﻢ‬-‫ﺑﺮﻧﺞ‬
‫آﻟﻮﻣﻴﻨﻴﻢ‬- ‫ﺑﺮﻧﺰ‬
‫ﻣﺲ ﻧﻴﻜﻞ دار‬
‫آﻟﻮﻣﻴﻨﻴﻮم‬
‫ﻣﻮﻧﻞ‬
‫ﻓﻮﻻد زﻧﮓ ﻧﺰن‬
(ft./sec.)
min.
max.
min.
max.
‫ﺣﺪاﻗﻞ‬
‫ﺣﺪاﻛﺜﺮ‬
‫ﺣﺪاﻗﻞ‬
‫ﺣﺪاﻛﺜﺮ‬
0.9
0.9
0.9
1.5
1.5
0.9
1.8
2.4
1.8
1.8
2.4
3.1
3.1
3.1
3.6
3.6
3
3
3
5
5
3
6
8
6
6
8
10
10
10
12
12
‫ ﺑﺨﺎرات‬3-3-4-7
7.4.3.3 Vapors
For vapors, the velocity used will depend on the
operating pressure and fluid density; and
allowable pressure drop.
‫ ﺳﺮﻋﺖ ﻣﻮرد اﺳﺘﻔﺎده ﺑﻪ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ و ﭼﮕﺎﻟﻲ‬،‫ﺑﺮاي ﺑﺨﺎرات‬
.‫ﺳﻴﺎل و اﻓﺖ ﻓﺸﺎر ﻣﺠﺎز ﺑﺴﺘﮕﻲ دارد‬
‫ آراﻳﺶ ﻫﻨﺪﺳﻲ‬5-7
7.5 Geometrical
7.5.1 Tube pattern
‫ آراﻳﺶ ﻟﻮﻟﻪ‬1-5-7
Standard tube patterns are shown in Fig. 1
.‫ ﻧﺸﺎن داده ﺷﺪه اﺳﺖ‬1 ‫آراﻳﺶ اﺳﺘﺎﻧﺪارد ﻟﻮﻟﻪﻫﺎ در ﺷﻜﻞ‬
22
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
‫ﻣﺜﻠﺜﻲ‬
IPS-E-PR- 771(1)
‫ﻣﺮﺑﻌﻲ‬
‫ﻣﺜﻠﺜﻲ ﭼﺮﺧﻴﺪه‬
‫ﻣﺮﺑﻌﻲ ﭼﺮﺧﻴﺪه‬
Fig. 1
1 ‫ﺷﻜﻞ‬
Note: Flow Arrows are Perpendicular to the
Baffle Cut Edge.
‫ ﺑﺮدارﻫﺎي ﺟﺮﻳﺎن ﻋﻤﻮد ﺑﺮ ﺑﺮش ﺻﻔﺤﻪ ﺟﺪا ﻛﻨﻨﺪه‬:‫ﻳﺎدآوري‬
.‫ﻣﻲﺑﺎﺷﺪ‬
‫اﻟﻒ( آراﻳﺶ ﻣﺜﻠﺜﻲ‬
a) Triangular pattern
Most popular, generally suitable for nonfouling or fouling services of chemical
treatment processes medium to high pressure
drop; gives better coefficients than square
pitch.
‫ ﻋﻤﻮﻣﺎً ﺑﺮاي ﻛﺎرﺑﺮيﻫﺎي ﻏﻴﺮرﺳﻮبده ﻳﺎ‬،‫ﺑﺴﻴﺎر راﻳﺞ اﺳﺖ‬
‫رﺳﻮبده ﻓﺮآﻳﻨﺪﻫﺎي ﻓﺮآورش ﺷﻴﻤﻴﺎﻳﻲ ﺑﺎ اﻓﺖ ﻓﺸﺎر‬
‫ ﻧﺴﺒﺖ ﺑﻪ آراﻳﺶ ﻣﺮﺑﻌﻲ‬،‫ﻣﺘﻮﺳﻂ ﺑﻪ ﺑﺎﻻ ﻣﻨﺎﺳﺐ اﺳﺖ‬
.‫ﺿﺮاﻳﺐ ﺑﻬﺘﺮي دارد‬
‫ب( آراﻳﺶ ﻣﺜﻠﺜﻲ ﭼﺮﺧﻴﺪه‬
b) Rotated triangular pattern
Not as popular as the staggered triangular
pitch; coefficients not as high, but better than
square pitch; pressure drop about medium to
high; generally suitable for same fouling
conditions as above
‫ ﺿﺮاﻳﺐ ﭼﻨﺪان ﺑﺎﻻ ﻧﺒﻮده‬،‫ﻣﺜﻞ آراﻳﺶ ﻣﺜﻠﺜﻲ راﻳﺞ ﻧﻴﺴﺖ‬
‫ اﻓﺖ ﻓﺸﺎر ﻣﺘﻮﺳﻂ‬.‫اﻣﺎ ﻧﺴﺒﺖ ﺑﻪ آراﻳﺶ ﻣﺮﺑﻌﻲ ﺑﻬﺘﺮ اﺳﺖ‬
-‫ﺑﻪ ﺑﺎﻻ داﺷﺘﻪ و ﻋﻤﻮﻣﺎً ﺑﺮاي ﺷﺮاﻳﻂ رﺳﻮﺑﻲ ﺑﺎﻻ ﻣﻨﺎﺳﺐ ﻣﻲ‬
.‫ﺑﺎﺷﺪ‬
‫ج( آراﻳﺶ ﻣﺮﺑﻌﻲ‬
c) Square pattern
Popular for conditions requiring low pressure
drop and/or cleaning lanes for mechanical
cleaning of outside of tubes; coefficient lower
than triangular pitch.
‫ﻳﺎ ﻣﺴﻴﺮﻫﺎﻳﻲ ﺑﺮاي‬/‫ﺑﺮاي ﺷﺮاﻳﻄﻲ ﻛﻪ اﻓﺖ ﻓﺸﺎر ﻛﻢ و‬
‫ راﻳﺞ اﺳﺖ و‬،‫ﺗﻤﻴﺰﻛﺎري ﻣﻜﺎﻧﻴﻜﻲ ﺑﻴﺮون ﻟﻮﻟﻪﻫﺎ ﻻزم دارﻧﺪ‬
.‫ﺿﺮاﻳﺐ ﻛﻤﺘﺮي ﻧﺴﺒﺖ ﺑﻪ آراﻳﺶ ﻣﺜﻠﺜﻲ دارد‬
‫د( آراﻳﺶ ﻣﺮﺑﻌﻲ ﭼﺮﺧﻴﺪه‬
d) Rotated square pattern
Popular arrangement for reasonably low
pressure drop (not as low as square),
mechanical cleaning requirements, and better
coefficient than square pitch.
‫ﺑﺮاي اﻓﺖ ﻓﺸﺎرﻫﺎي ﻧﺴﺒﺘﺎ ﻛﻢ )ﻧﻪ ﺑﻪ ﻛﻤﻲ ﻣﺮﺑﻌﻲ( آراﻳﺶ‬
‫ ﻧﺴﺒﺖ ﺑﻪ آراﻳﺶ ﻣﺮﺑﻌﻲ ﻧﻴﺎز ﺑﻪ اﻟﺰاﻣﺎت‬.‫راﻳﺠﻲ اﺳﺖ‬
.‫ﺗﻤﻴﺰﻛﺎري ﻣﻜﺎﻧﻴﻜﻲ ﺑﻴﺸﺘﺮ و ﺿﺮﻳﺐ ﺑﻬﺘﺮي دارد‬
‫ ﮔﺎم ﻟﻮﻟﻪ‬2-5-7
7.5.2 Tube pitch
7.5.2.1 Tube pitch (for Class R)
(R ‫ ﮔﺎم ﻟﻮﻟﻪ )ﺑﺮاي ﻃﺒﻘﻪ ﺑﻨﺪي‬1-2-5-7
Tubes shall be spaced with a minimum center-tocenter distance of 1.25 times the outside diameter
of the tube. When mechanical cleaning of the
‫ ﺑﺮاﺑﺮ ﻗﻄﺮ‬1/25 ‫ﺣﺪاﻗﻞ ﻓﺎﺻﻠﻪ ﻣﺮﻛﺰ ﺑﻪ ﻣﺮﻛﺰ ﻟﻮﻟﻪﻫﺎ ﺑﺎﻳﺪ‬
‫ در ﺻﻮرﺗﻲ ﻛﻪ ﺗﻤﻴﺰﻛﺎري ﻣﻜﺎﻧﻴﻜﻲ ﻟﻮﻟﻪﻫﺎ‬.‫ﺧﺎرﺟﻲ ﻟﻮﻟﻪ ﺑﺎﺷﺪ‬
23
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
tubes is specified by the Company, minimum
cleaning lanes of DN6.4 (¼ inch) shall be
provided.
IPS-E-PR- 771(1)
‫ ﺣﺪاﻗﻞ ﻣﺴﻴﺮﻫﺎي ﺗﻤﻴﺰﻛﺎري ﺑﺎ ﻗﻄﺮ‬،‫ﺗﻮﺳﻂ ﺷﺮﻛﺖ ﻣﻌﻴﻦ ﺷﻮد‬
.‫اﻳﻨﭻ( ﺑﺎﻳﺪ ﺗﻌﺒﻴﻪ ﺷﻮد‬
) 6/4 ‫اﺳﻤﻲ‬
(C ‫ ﮔﺎم ﻟﻮﻟﻪ )ﺑﺮاي ﻃﺒﻘﻪ ﺑﻨﺪي‬2-2-5-7
7.5.2.2 Tube pitch (for Class C)
Tubes shall be spaced with a minimum center-tocenter distance of 1.25 times the outside diameter
of the tube. Where the tube diameters are DN 16
(5/8 inch) or less and tube-to-tubesheet joints are
expanded only, the minimum center-tocenter
distance may be reduced to 1.20 times the outside
diameter.
‫ ﺑﺮاﺑﺮ ﻗﻄﺮ‬1/25 ‫ﺣﺪاﻗﻞ ﻓﺎﺻﻠﻪ ﻣﺮﻛﺰ ﺑﻪ ﻣﺮﻛﺰ ﻟﻮﻟﻪﻫﺎ ﺑﺎﻳﺪ‬
16 ‫ ﺟﺎﻳﻲ ﻛﻪ ﻗﻄﺮﻫﺎي اﺳﻤﻲ ﻟﻮﻟﻪ‬.‫ﺧﺎرﺟﻲ ﻟﻮﻟﻪ ﺑﺎﺷﺪ‬
5
8
‫اﻳﻨﭻ( ﻳﺎ ﻛﻤﺘﺮ ﺑﺎﺷﺪ و اﺗﺼﺎل ﻟﻮﻟﻪ ﺑﻪ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺑﻪ ﺻﻮرت‬
)
1/20 ‫ ﺣﺪاﻗﻞ ﻓﺎﺻﻠﻪ ﻣﺮﻛﺰ ﺑﻪ ﻣﺮﻛﺰ ﻣﻲﺗﻮاﻧﺪ ﺗﺎ‬.‫اﻧﺒﺴﺎﻃﻲ ﺑﺎﺷﺪ‬
.‫ﺑﺮاﺑﺮ ﻗﻄﺮ ﺧﺎرﺟﻲ ﻟﻮﻟﻪ ﻛﺎﻫﺶ ﻳﺎﺑﺪ‬
(B ‫ ﮔﺎم ﻟﻮﻟﻪ )ﺑﺮاي ﻃﺒﻘﻪ ﺑﻨﺪي‬3-2-5-7
7.5.2.3 Tube pitch (for Class B)
Tubes shall be spaced with a minimum center-tocenter distance of 1.25 times the outside diameter
of the tube. When mechanical cleaning of the
tubes is specified by the Company and the
nominal shell diameter is DN300 (12 inches) or
less, minimum cleaning lanes of DN 5 (3/16 inch)
shall be provided. For shell diameters greater than
DN 300 (12 inches), minimum cleaning lanes of
DN 6.4 (¼ inch) shall be provided.
‫ ﺑﺮاﺑﺮ ﻗﻄﺮ‬1/25 ‫ﺣﺪاﻗﻞ ﻓﺎﺻﻠﻪ ﻣﺮﻛﺰ ﺑﻪ ﻣﺮﻛﺰ ﻟﻮﻟﻪﻫﺎ ﺑﺎﻳﺪ‬
‫ ﻟﻮﻟﻪﻫﺎ‬،‫ در ﺻﻮرﺗﻲ ﻛﻪ ﺗﻤﻴﺰﻛﺎري ﻣﻜﺎﻧﻴﻜﻲ‬.‫ﺧﺎرﺟﻲ ﻟﻮﻟﻪ ﺑﺎﺷﺪ‬
(‫ اﻳﻨﭻ‬12) 300 ‫ﺗﻮﺳﻂ ﺷﺮﻛﺖ ﻣﻌﻴﻦ ﺷﻮد و ﻗﻄﺮ اﺳﻤﻲ ﭘﻮﺳﺘﻪ‬
5 ‫ ﻣﺴﻴﺮﻫﺎي ﺗﻤﻴﺰﻛﺎري ﺑﺎ ﺣﺪاﻗﻞ ﻗﻄﺮ اﺳﻤﻲ‬،‫ﻳﺎ ﻛﻤﺘﺮ ﺑﺎﺷﺪ‬
‫ ﺑﺮاي ﻗﻄﺮ اﺳﻤﻲ ﭘﻮﺳﺘﻪ ﺑﻴﺸﺘﺮ از‬.‫ اﻳﻨﭻ( ﺑﺎﻳﺪ ﺗﻌﺒﻴﻪ ﺷﻮﻧﺪ‬3 )
16
‫ ﻣﺴﻴﺮﻫﺎ ﺗﻤﻴﺰﻛﺎري ﺑــﺎﻳﺪ ﺣﺪاﻗﻞ ﻗﻄﺮ‬، (‫ اﻳﻨﭻ‬12) 300
.‫اﻳﻨﭻ( ﺗﻌﺒﻴﻪ ﮔﺮدد‬
1
4
) 6/4 ‫اﺳﻤﻲ‬
‫ ﺷﻴﺮﻫﺎي ﻛﻨﺎرﮔﺬر و اﻧﺴﺪاد‬3-5-7
7.5.3 Bypasses and block valves
Bypasses and block valves are used on an
exchanger for one or more of the following
reasons:
‫ﺷﻴﺮﻫﺎي ﻛﻨﺎرﮔﺬر و اﻧﺴﺪاد در ﻣﺒﺪلﻫﺎ ﺑﺮاي ﻳﻚ ﻳﺎ ﭼﻨﺪ دﻟﻴﻞ‬
:‫زﻳﺮ ﺑﻪ ﻛﺎر ﻣﻲروﻧﺪ‬
‫ ﻛﻨﺘﺮل ﻓﺮآﻳﻨﺪ‬1-3-5-7
7.5.3.1 Process control
‫ اﺳﺘﻔﺎده‬،‫زﻣﺎﻧﻲ ﻛﻪ اﻧﺘﻘﺎل ﺣﺮارت در ﻣﺒﺪل ﻧﻴﺎز ﺑﻪ ﻛﻨﺘﺮل دارد‬
:‫ﻫﺮ ﻳﻚ از ﻣﻮارد زﻳﺮ‬
When it is necessary to control the heat transfer in
an exchanger, use either:
1) A simple bypass and 2 valves or
‫ ﺷﻴﺮ ﻳﺎ‬2 ‫( ﻳﻚ ﻛﻨﺎر ﮔﺬر ﺳﺎده ﺑﺎ‬1
‫( ﻳﻚ ﻛﻨﺎر ﮔﺬر و ﻳﻚ ﺷﻴﺮ ﺳﻪ راﻫﻪ ) ﻳــﺎ دو ﺷﻴﺮ‬2
2) A bypass and a three-way valve (or two
butterfly valves) which splits the flow between
the bypass and the exchanger.
A three-way valve is necessary
exchanger pressure drop is so
insufficient fluid diversion would
through a simple bypass in the
position.
1
4
‫ﭘﺮواﻧﻪاي( ﻛﻪ ﺟﺮﻳﺎن را ﺑﻴﻦ ﻣﺒﺪل و ﻛﻨﺎرﮔﺬر ﺗﻘﺴﻴﻢ‬
.‫ﻣﻲﻛﻨﺪ‬
when the
small that
take place
wide open
‫ﺷﻴﺮ ﺳﻪ راﻫﻪ زﻣﺎﻧﻲ ﻻزم اﺳﺖ ﻛﻪ اﻓﺖ ﻓﺸﺎر ﻣﺒﺪل آﻧﻘﺪر ﻛﻢ‬
‫اﺳﺖ ﻛﻪ اﻧﺤﺮاف ﺟﺮﻳﺎن ﻏﻴﺮﻛﺎﻓﻲ در ﻣﺴﻴﺮ ﺟﺮﻳﺎن ﻛﻨﺎرﮔﺬر در‬
.‫ﺣﺎﻟﺖ ﻛﺎﻣﻼً ﺑﺎز اﺗﻔﺎق ﻣﻲاﻓﺘﺪ‬
‫ ﻧﺸﺘﻲ‬2-3-5-7
7.5.3.2 Leakage
Where leaking of one side of a heat exchanger
would result in intolerable contamination of the
other fluid (as in an overhead vapor-feed
exchanger of a pipestill), blocks and bypasses
‫ﺟﺎﻳﻲ ﻛﻪ ﻧﺸﺘﻲ از ﻳﻚ ﺳﻤﺖ ﻣﺒﺪل ﺣﺮارﺗﻲ ﻣﻨﺠﺮ ﺑﻪ آﻟﻮدﮔﻲ‬
‫ﺷﺪﻳﺪ ﺳﻴﺎل دﻳﮕﺮ ﺷﻮد )ﻣﺜﻞ ﻣﺒﺪل ﺧﻮراك – ﺑﺨﺎر ﺑﺎﻻﺳﺮي‬
‫ ﻣﺴﺪود ﻛﻨﻨﺪهﻫﺎ و ﻛﻨﺎرﮔﺬرﻫﺎ ﺑﺮاي ﻣﺠﺰا‬،(‫دﺳﺘﮕﺎه ﺗﻘﻄﻴﺮ‬
24
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
may be installed to permit isolating the leaking
unit from the system. In addition, welded tube to
tubesheet joints or double tubesheets should be
considered.
IPS-E-PR- 771(1)
،‫ ﺑﻌﻼوه‬.‫ﻛﺮدن واﺣﺪ ﻧﺸﺘﻲدار از ﺳﺎﻣﺎﻧﻪ ﺑﺎﻳﺪ ﻧﺼﺐ ﺷﻮﻧﺪ‬
‫اﺗﺼﺎﻻت ﺟﻮﺷﻲ ﻟﻮﻟﻪ ﺑﻪ ﻣﻔﺼﻞﻫﺎي ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﻳﺎ ﺻﻔﺤﺎت ﻟﻮﻟﻪ‬
.‫دوﺗﺎﻳﻲ ﺑﺎﻳﺪ ﻟﺤﺎظ ﺷﻮﻧﺪ‬
‫ ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪهﻫﺎ‬4-5-7
7.5.4 Baffles
7.5.4.1 Types
‫ اﻧﻮاع‬1-4-5-7
The four types of cross baffles in shell and tube
type exchangers are illustrated in Fig. 2:
‫ﭼﻬﺎر ﻧﻮع از ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻋﺮﺿﻲ در ﻣﺒﺪلﻫﺎي ﭘﻮﺳﺘﻪ و‬
:‫ ﺗﺸﺮﻳﺢ ﺷﺪهاﻧﺪ‬2 ‫ﻟﻮﻟﻪ در ﺷﻜﻞ‬
‫اﻟﻒ( ﻗﻄﻌﻪاي‬
a) Segmental
This type is the most common baffles.
.‫اﻳﻦ ﻧﻮع از ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﺑﺴﻴﺎر راﻳﺞ اﺳﺖ‬
‫ب ( دو ﻗﻄﻌﻪاي‬
b) Double segmental
Double segmental baffles give one-third to
one-half the pressure drop and 60 to 90
percent of the heat transfer for the same total
flow rate compared with units with segmental
baffles having the same spacing and cut.
Therefore, if the pressure drop is a limitation
factor at the maximum allowable segmental
baffle spacing, the use of a double segmental
baffle should be investigated.
‫ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪهﻫﺎي دو ﻗﻄﻌﻪاي اﻓﺖ ﻓﺸﺎر ﻳﻚ ﺳﻮم ﺗﺎ‬
‫ درﺻﺪ ﺑﺎ دﺑﻲ ﺟﺮﻳﺎن ﻛﻞ‬90 ‫ ﺗﺎ‬60 ‫ﻧﺼﻒ و اﻧﺘﻘﺎل ﺣﺮارت‬
‫ﻳﻜﺴﺎن ﺑﻪ ﻧﺴﺒﺖ واﺣﺪﻫﺎﻳﻲ ﺑﺎ ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻗﻄﻌﻪاي‬
‫ از اﻳﻦ رو اﮔﺮ اﻓﺖ ﻓﺸﺎر‬.‫ﻛﻪ ﻓﺎﺻﻠﻪ و ﺑﺮش ﻳﻜﺴﺎن دارﻧﺪ‬
‫ﭘﺎراﻣﺘﺮ ﻣﺤﺪودﻛﻨﻨﺪه در ﺣﺪاﻛﺜﺮ ﻓﺎﺻﻠﻪ ﻣﺠﺎز ﺻﻔﺤﻪ ﺟﺪا‬
‫ اﺳﺘﻔﺎده از ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه‬،‫ﻛﻨﻨﺪهﻫﺎي ﻗﻄﻌﻪاي ﺑﺎﺷﺪ‬
.‫دو ﻗﻄﻌﻪاي ﺑﺎﻳﺪ ﺑﺮرﺳﻲ ﺷﻮد‬
‫ج( ﺳﻪ ﻗﻄﻌﻪاي‬
c) Triple segmental
Triple segmental baffles have proved very
effective in low pressure drop applications in
both laminar and turbulent flows.
‫ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪهﻫﺎي ﺳﻪ ﻗﻄﻌﻪاي ﺑﺮاي ﻛﺎرﺑﺮدﻫﺎي اﻓﺖ‬
‫ﻓﺸﺎر ﭘﺎﻳﻴﻦ در ﻫﺮ دو ﺟﺮﻳﺎن آرام و ﺗﻼﻃﻢ ﺑﺴﻴﺎر ﻛﺎرآﻣﺪ‬
.‫اﺳﺖ‬
‫د( ﺑﺪون ﻟﻮﻟﻪ در درﻳﭽﻪ‬
d) No-tubes-in-window
Support plates can be used with no-tubes-inwindow type baffles. Therefore these type
baffles can eliminate flow induced tube
vibration.
‫ﺻﻔﺤﺎت ﻧﮕﻬﺪارﻧﺪه ﻣﻲﺗﻮاﻧﻨﺪ ﺑﺎ ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﺑﺪون‬
‫ اﻳﻦ ﻧﻮع از‬،‫ ﺑـﺎ اﻳﻦ وﺟﻮد‬.‫ﻟﻮﻟﻪ در درﻳﭽﻪ اﺳﺘﻔﺎده ﺷﻮﻧﺪ‬
‫ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻟﺮزش ﻟﻮﻟﻪ ﻧﺎﺷﻲ از ﺟﺮﻳﺎن را ﺣﺬف‬
.‫ﻣﻲﻛﻨﻨﺪ‬
7.5.4.2 Cut as percentage of shell in side
diameter
‫ ﺑﺮش درﺻﺪي از ﻗﻄﺮ داﺧﻠﻲ ﭘﻮﺳﺘﻪ‬2-4-5-7
The percent baffle cut is determined at position 1
as shown in Fig. 3:
‫ ﻧﺸﺎن‬3 ‫ ﺷﻜﻞ‬1 ‫ﺑﺮش درﺻﺪي ﺻﻔﺤﻪ ﺟﺪا ﻛﻨﻨﺪه در ﻣﺤﻞ‬
:‫داده ﺷﺪه اﺳﺖ‬
‫اﻟﻒ( ﻗﻄﻌﻪاي‬
a) Segmental
‫ درﺻﺪ ﻣﻲﺑﺎﺷﺪ‬49 ‫ﺣﺪاﻛﺜﺮ ﺑﺮش ﻣﺠﺎز‬
Maximum cuts allowed are 49 percent.
b) Double, triple segmental
Normally specifies the cut of baffles in a
manner which gives equal net flow area for
each window.
‫ب ( دو ﻳﺎ ﺳﻪ ﻗﻄﻌﻪاي‬
‫ﻣﻌﻤﻮﻻً ﺑﺮش ﺻﻔﺤﻪﻫﺎي ﺟﺪا ﻛﻨﻨﺪه ﺑﻪ ﻃﺮﻳﻘﻲ اﻧﺠﺎم‬
‫ﻣﻲﺷﻮد ﻛﻪ ﺳﻄﺢ ﻋﺒﻮر ﺟﺮﻳﺎن ﺧﺎﻟﺺ ﻳﻜﺴﺎن ﺑﺮاي ﻫﺮ‬
.‫روزﻧﻪ اﻳﺠﺎد ﺷﻮد‬
25
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
c) No-tubes-in-window
The cut is extremely important because it not
only defines the window flow area but also
affects the tube count and the height under the
window.
IPS-E-PR- 771(1)
‫ج ( ﺑﺪون ﻟﻮﻟﻪ در درﻳﭽﻪ‬
‫از آﻧﺠﺎﻳﻴﻜﻪ ﺑﺮش ﻧﻪ ﺗﻨﻬﺎ ﺳﻄﺢ ﺟﺮﻳﺎن در درﻳﭽﻪ ﺑﻠﻜﻪ‬
‫ﺗﻌﺪاد ﻟﻮﻟﻪﻫﺎ و ارﺗﻔﺎع زﻳﺮ درﻳﭽﻪ را ﻧﻴﺰ ﺗﺤﺖ ﺗﺄﺛﻴﺮ ﻗﺮار‬
.‫ ﺑﺴﻴﺎر ﺣﻴﺎﺗﻲ ﻣﻲﺑﺎﺷﺪ‬،‫ﻣﻲدﻫﺪ‬
‫ ﺟﻬﺖ ﺑﺮش ﺻﻔﺤﻪ ﺟﺪا ﻛﻨﻨﺪه‬3-4-5-7
7.5.4.3 Baffle cut orientation:
a) Vertical cut
‫اﻟﻒ( ﺑﺮش ﻋﻤﻮدي‬
The baffle edge is usually vertical for service
in horizontal condensers, reboilers, vaporizers
and heat exchangers carrying suspended
matter or heavy fouling fluids. With this
arrangement non-condensable vapors and inert
gases can escape or flow along the top of the
unit and thus prevent vapor binding or vapor
lock causing a blanking-to-heat transfer of the
upper portion of the shell.
‫ ﺑﺨﺎرﺳﺎزﻫﺎ و‬،‫ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎ‬،‫در ﭼﮕﺎﻟﻨﺪهﻫﺎي اﻓﻘﻲ‬
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻛﻪ ﻣﻮاد ﻣﻌﻠﻖ ﻳﺎ ﺳﻴﺎﻻت رﺳﻮبده‬
‫ در‬.‫ﺷﺪﻳﺪ ﺑﺮش ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻫﻤﻴﺸﻪ ﻋﻤﻮدي اﺳﺖ‬
‫اﻳﻦ آراﻳﺶ ﺑﺨﺎرات ﻏﻴﺮﻗﺎﺑﻞ ﭼﮕﺎﻟﺶ و ﮔﺎزﻫﺎي ﺧﻨﺜﻲ‬
‫ﻣﻲﺗﻮاﻧﻨﺪ ﺧﺎرج ﺷﻮﻧﺪ ﻳﺎ ﺑﻪ ﺳﻤﺖ ﺑﺎﻻ ﺟﺮﻳﺎن ﻳﺎﺑﻨﺪ ﻛﻪ ﻣﺎﻧﻊ‬
‫از ﻣﺤﺪود ﺷﺪن ﻳﺎ ﺑﺴﺘﻪ ﺷﺪن ﺑﺨﺎر ﻛﻪ ﻣﻨﺠﺮ ﺑﻪ ﻛﺎﻫﺶ‬
.‫اﻧﺘﻘﺎل ﺣﺮارت ﻗﺴﻤﺖ ﺑﺎﻻﻳﻲ ﭘﻮﺳﺘﻪ ﻣﻲﺷﻮد‬
Also, equally important as the passage of
vapor, is the release of liquid from the lower
portion of the shell as it is produced.
‫ ﺧﺮوج ﻣﺎﻳﻊ ﺗﻮﻟﻴﺪ‬،‫ﻫﻤﭽﻨﻴﻦ ﺑﻪ اﻧﺪازه اﻫﻤﻴﺖ ﻋﺒﻮر ﺑﺨﺎر‬
.‫ﺷﺪه ﻧﻴﺰ از ﺑﺨﺶ ﭘﺎﻳﻴﻨﻲ ﭘﻮﺳﺘﻪ ﻣﻬﻢ اﺳﺖ‬
b) Horizontal cut
The horizontal cut baffles are good for all gas
phase or liquid phase service in the shell.
However, if there is dissolved gas in the liquid
which may be released in the exchanger, this
baffle should not be used, or else notches
should be cut at the top for the passage of gas.
Notches, will only be effective for small traces
of released gas. Liquid should be clean,
otherwise sediment will collect at the base of
every other baffle segment and blank off part
of the lower tubes to the heat transfer.
‫ب ( ﺑﺮش اﻓﻘﻲ‬
‫ﺑﺮش اﻓﻘﻲ ﺑﺮاي ﻛﺎرﺑﺮي ﻓﺎز ﮔﺎز ﻳﺎ ﻓﺎز ﻣﺎﻳﻊ در ﭘﻮﺳﺘﻪ‬
‫ ﺑﺎ اﻳﻦ وﺟﻮد اﮔﺮ ﮔﺎز ﻣﺤﻠﻮل در ﻣﺎﻳﻊ ﺑﺎﺷﺪ‬.‫ﻣﻨﺎﺳﺐ اﺳﺖ‬
‫ اﺳﺘﻔﺎده از اﻳﻦ ﺻﻔﺤﻪ‬،‫ﻛﻪ ﻣﻤﻜﻦ اﺳﺖ در ﻣﺒﺪل آزاد ﺷﻮد‬
‫ ﻳﺎ ﺑﺮاي ﻋﺒﻮر ﮔﺎزﻫﺎ در ﺑﺎﻻ‬،‫ﺟﺪا ﻛﻨﻨﺪه ﺗﻮﺻﻴﻪ ﻧﻤﻲ ﮔﺮدد‬
‫ ﺷﻜﺎفﻫﺎ‬.‫ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺷﻜﺎفﻫﺎﻳﻲ در ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮﻧﺪ‬
‫ ﺳﻴﺎل ﺑﺎﻳﺪ‬.‫ﺑﺮاي ﻣﻘﺪار ﻛﻢ ﺧﺮوج ﮔﺎز ﺛﻤﺮﺑﺨﺶ ﻫﺴﺘﻨﺪ‬
‫ﺗﻤﻴﺰ ﺑﺎﺷﺪ در ﻏﻴﺮ اﻳﻦ ﺻﻮرت ذرات در ﻛﻒ ﻫﺮ ﺑﺨﺶ‬
‫ﺻﻔﺤﻪ ﺟﺪا ﻛﻨﻨﺪه ﺟﻤﻊ ﺷﺪه و اﻧﺘﻘﺎل ﺣﺮارت ﻟﻮﻟﻪﻫــﺎي‬
.‫ﭘﺎﻳﻴﻨﻲ را از ﺑﻴﻦ ﻣﻲرود‬
26
‫)‪IPS-E-PR- 771(1‬‬
‫ﻣﻬﺮ ‪Oct. 2009 / 1388‬‬
‫دو ﻗﻄﻌﻪاي‬
‫ﻗﻄﻌﻪاي ﺑﺪون ﻟﻮﻟﻪ در درﻳﭽﻪ‬
‫ﻗﻄﻌﻪاي‬
‫ﺳﻪ ﻗﻄﻌﻪاي‬
‫‪Fig. 2-BAFFLE TYPES‬‬
‫ﺷﻜﻞ ‪ -2‬اﻧﻮاع ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه‬
‫‪27‬‬
‫ﻣﻬﺮ ‪Oct. 2009 / 1388‬‬
‫)‪IPS-E-PR- 771(1‬‬
‫ﻣﻮﻗﻌﻴﺖ‬
‫ﻣﻮﻗﻌﻴﺖ‬
‫ﻣﻮﻗﻌﻴﺖ‬
‫‪Fig. 3-BAFFLE CUT‬‬
‫ﺷﻜﻞ ‪ -3‬ﺑﺮش ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه‬
‫ﻳﺎدآوري‪:‬‬
‫درﺻﺪ ﺑﺮش ﺻﻔﺤﻪ ﺟﺪا ﻛﻨﻨﺪه = ‪× 100‬‬
‫‪Note:‬‬
‫‪% Baffle cut = h × 100‬‬
‫‪h‬‬
‫‪DS‬‬
‫‪DS‬‬
‫‪ :X‬ﻫﻢ ﭘﻮﺷﺎﻧﻲ )ﻋﻤﻮﻣﺎً دو ردﻳﻒ ﻟﻮﻟﻪ ﻫﻢ ﭘﻮش ﻣﻲ ﺷﻮﻧﺪ(‬
‫)‪X: Overlap (normally two tube rows overlap‬‬
‫‪ 5-5-7‬ﻓﺎﺻﻠﻪ ﮔﺬاري ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه و ﺻﻔﺤﺎت‬
‫‪7.5.5 Spacing of baffles and support plates‬‬
‫ﻧﮕﻬﺪارﻧﺪه‬
‫‪7.5.5.1 Minimum spacing‬‬
‫‪ 1-5-5-7‬ﺣﺪاﻗﻞ ﻓﺎﺻﻠﻪ ﮔﺬاري‬
‫ﻋﻤﻮﻣﺎ ﺗﻮﺻﻴﻪ ﻧﻤﻲ ﺷﻮد ﻓﺎﺻﻠﻪ ﮔﺬاري ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه‬
‫‪1‬‬
‫ﻗﻄﻌﻪاي ﻛﻤﺘﺮ از ﻗﻄﺮ داﺧﻠﻲ ﭘﻮﺳﺘﻪ ﻳﺎ ﻗﻄﺮ اﺳﻤﻲ ‪2) 50‬‬
‫‪5‬‬
‫اﻳﻨﭻ(‪ ،‬ﻫﺮﻛﺪام ﺑﺰرﮔﺘﺮ ﺑﺎﺷﺪ‪ ،‬اﻧﺘﺨﺎب ﺷﻮد‪ .‬ﺑﺎ اﻳﻦ وﺟﻮد‬
‫ﻣﻼﺣﻈﺎت ﻃﺮاﺣﻲ ﺧﺎص ﻣﻤﻜﻦ اﺳﺖ ﻛﻪ ﻓﺎﺻﻠﻪ ﮔﺬاري‬
‫ﻧﺰدﻳﻜﺘﺮ را ﺗﺤﻤﻴﻞ ﻧﻤﺎﻳﺪ‪.‬‬
‫‪Segmental baffles normally should not be spaced‬‬
‫‪closer than 1/5 of the shell ID or DN 50 (2‬‬
‫‪inches), whichever is greater. However, special‬‬
‫‪design considerations may dictate a closer‬‬
‫‪spacing.‬‬
‫‪ 2-5-5-7‬ﺣﺪاﻛﺜﺮ ﻓﺎﺻﻠﻪ ﮔﺬاري‬
‫‪7.5.5.2 Maximum spacing‬‬
‫ﻓﺎﺻﻠﻪ ﺻﻔﺤﺎت ﻧﮕﻬﺪارﻧﺪه ﻟﻮﻟﻪ ﺑﺎﻳﺪ آﻧﻘﺪر ﺑﺎﺷﺪ ﻛﻪ ﻃﻮل ﻟﻮﻟﻪ‬
‫ﺣﺪ ﻓﺎﺻﻞ ﺻﻔﺤﺎت) ﺑﺎ ﺗﻮﺟﻪ ﺑﻪ ﺟﻨﺲ ﻟﻮﻟﻪ( از ﻣﻘﺪار ﻣﺸﺨﺺ‬
‫ﺷﺪه در ﻣﺸﺨﺼﺎت ﻓﻨﻲ ﭘﺮوژه ﺑﻴﺸﺘﺮ ﻧﺒﺎﺷﺪ‪.‬‬
‫‪Tube support plates shall be so spaced that the‬‬
‫‪unsupported tube length does not exceed the‬‬
‫‪value indicated in the project specification for the‬‬
‫‪tube material used.‬‬
‫‪ 3-5-5-7‬ﻣﻴﻠﻪﻫﺎي راﺑﻂ و ﺟﺪاﻛﻨﻨﺪهﻫﺎ‬
‫ﺑﺎﻳﺪ ﺑﺮاي ﻧﮕﻬﺪاﺷﺘﻦ ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻋﺮﺿﻲ و ﺻﻔﺤﺎت‬
‫ﻣﺤﺎﻓﻆ ﻟﻮﻟﻪﻫﺎ ﻣﺤﻜﻢ در ﻣﻮﻗﻌﻴﺖ ﺧﻮد‪ ،‬ﻣﻴﻠﻪﻫﺎ و ﺟﺪاﻛﻨﻨﺪهﻫﺎ‬
‫ﻳﺎ ﺳﺎﻳﺮ ﺗﺠﻬﻴﺰات ﻣﻌﺎدل ﺑﺴﺘﻦ ﺳﺎﻣﺎﻧﻪ ﺻﻔﺤﻪ ﺟﺪا ﻛﻨﻨﺪه ﺑﻪ‬
‫ﻫﻤﺪﻳﮕﺮ‪ ،‬ﺗﻌﺒﻴﻪ ﺷﻮﻧﺪ‪.‬‬
‫‪7.5.5.3 Tie rods and spacers‬‬
‫‪The rods and spacers or other equivalent means‬‬
‫‪of tying the baffle system together, shall be‬‬
‫‪provided to retain all transverse baffles and tube‬‬
‫‪support plates securely in position.‬‬
‫‪28‬‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ ﻟﻮﻟﻪء ﭘﺮهدار‬6-5-7
7.5.6 Finned tube
It has been recognized for some time that the use
of integral finned tubes in shell and tube type heat
exchangers can have significant economic
advantages in certain applications. On the other
hand, there are also conditions under which these
tubes would provide no advantage over plain
tubes. In order to make proper use of their
potential, therefore, each case should be carefully
evaluated. Some of the factors which limit the use
of finned tubes are as follows:
‫در ﺑﺮﺧﻲ ﻣﻮارد واﺿﺢ اﺳﺖ ﻛﻪ اﺳﺘﻔﺎده از ﻟﻮﻟﻪﻫﺎي ﭘﺮهدار در‬
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻧﻮع ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻣﺰاﻳﺎي اﻗﺘﺼﺎدي‬
‫ از ﻃﺮف دﻳﮕﺮ‬.‫ﻣﺸﺨﺼﻲ در ﻛﺎرﺑﺮدﻫﺎي ﺑﺨﺼﻮص داﺷﺘﻪ ﺑﺎﺷﺪ‬
‫ﺷﺮاﻳﻄﻲ وﺟﻮد دارد ﻛﻪ اﻳﻦ ﻟﻮﻟﻪﻫﺎ ﻫﻴﭻ ﻣﺰاﻳﺎﻳﻲ ﻧﺴﺒﺖ ﺑﻪ‬
‫ ﺑﻪ ﻣﻨﻈﻮر اﺳﺘﻔﺎده ﻣﻨﺎﺳﺐ از ﻛﺎرآﻳﻲ آﻧﻬﺎ‬.‫ﻟﻮﻟﻪﻫﺎي ﺳﺎده ﻧﺪارﻧﺪ‬
‫ ﺑﺮﺧﻲ از ﻓﺎﻛﺘﻮرﻫﺎﻳﻲ ﻛﻪ‬.‫ﻫﺮ ﻣﻮرد ﺑﺎﻳﺪ ﺑﻪ دﻗﺖ ارزﻳﺎﺑﻲ ﺷﻮد‬
:‫ ﻋﺒﺎرﺗﻨﺪ از‬،‫اﺳﺘﻔﺎده از ﻟﻮﻟﻪﻫﺎي ﭘﺮهدار را ﻣﺤﺪود ﻣﻲﻛﻨﻨﺪ‬
‫ ﺿﺮﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﻛﻢ ﺳﻤﺖ ﻟﻮﻟﻪ‬1-6-5-7
7.5.6.1 Low tubeside heat transfer coefficient
If the tubeside resistance is a controlling factor,
the outside finned surface is almost completely
ineffective, and plain tubes should be used
instead.
‫ ﺳﻄﺢ ﭘﺮهدار‬،‫اﮔﺮ ﻣﻘﺎوﻣﺖ ﺳﻤﺖ ﻟﻮﻟﻪ ﻋﺎﻣﻞ ﻛﻨﺘﺮل ﻛﻨﻨﺪه ﺑﺎﺷﺪ‬
‫ﺑﻴﺮوﻧﻲ ﻫﻤﻴﺸﻪ ﻏﻴﺮﻣﻮﺛﺮ اﺳﺖ و ﺑﺠﺎي آﻧﻬﺎ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد از‬
.‫ﻟﻮﻟﻪﻫﺎي ﺳﺎده اﺳﺘﻔﺎده ﺷﻮد‬
‫ ﺿﺮﻳﺐ رﺳﻮب زﻳﺎد ﺳﻤﺖ ﻟﻮﻟﻪ‬2-6-5-7
7.5.6.2 High tubeside fouling factor
The additional outside area does nothing to
decrease the tubeside fouling resistance and, if
this factor is controlling, finned tubes should be
used.
‫اﻓﺰاﻳﺶ ﺳﻄﺢ ﺑﻴﺮوﻧﻲ اﺛﺮي در ﻛﺎﻫﺶ ﻣﻘﺎوﻣﺖ رﺳﻮﺑﻲ ﺳﻤﺖ‬
‫ ﺗﻮﺻﻴﻪ‬،‫ﻟﻮﻟﻪ ﻧﺪاﺷﺘﻪ و اﮔﺮ اﻳﻦ ﻋﺎﻣﻞ ﻛﻨﺘﺮل ﻛﻨﻨﺪه ﺑﺎﺷﺪ‬
.‫ﻣﻲﺷﻮد از ﻟﻮﻟﻪﻫﺎي ﭘﺮهدار اﺳﺘﻔﺎده ﺷﻮﻧﺪ‬
‫ ﺿﺮﻳﺐ رﺳﻮب زﻳﺎد ﺳﻤﺖ ﭘﻮﺳﺘﻪ‬3-6-5-7
7.5.6.3 High shell side fouling factor
The effect of fouling on the outside of finned
tubes has long been a controversial subject. It is
obvious that if fin valleys become filled with
fouling deposit, heat transfer cannot take place at
the finned surface.
‫اﺛﺮ رﺳﻮب در ﺑﻴﺮون ﻟﻮﻟﻪﻫﺎي ﭘﺮهدار ﻣﻮﺿﻮع ﺑﺤﺚاﻧﮕﻴﺰ درازي‬
‫ روﺷﻦ اﺳﺖ ﻛﻪ اﮔﺮ ﻓﻀﺎي ﺑﻴﻦ ﭘﺮهﻫﺎ ﺑﺎ ذرات‬.‫ﺑﻮده اﺳﺖ‬
‫ اﻧﺘﻘﺎل ﺣﺮارت از ﺳﻄﺢ ﭘﺮه ﻗﺎﺑﻞ اﻧﺠﺎم ﻧﺨﻮاﻫﺪ‬،‫رﺳﻮب ﭘﺮ ﺷﻮد‬
.‫ﺑﻮد‬
‫ ﺳﻄﻮح ﺗﻮﺳﻌﻪ ﻳﺎﻓﺘﻪ‬4-6-5-7
7.5.6.4 Extended surface
Extended surface exchangers are characterized by
tubes with either longitudinal or transverse helical
fins. This type of surface is best employed when
the heat transfer properties of one fluid result in a
high resistance to heat flow and those of the other
fluid have a low resistance. The fluid with the
high resistance to heat flow contacts the fin
surface.
‫ﻣﺒﺪلﻫﺎي ﺳﻄﻮح ﺗﻮﺳﻌﻪ ﻳﺎﻓﺘﻪ ﺑﺎ ﻟﻮﻟﻪﻫﺎي ﺑﺎ ﭘﺮهﻫﺎي ﻃﻮﻟﻲ ﻳﺎ‬
‫ اﻳﻦ ﻧﻮع از ﺳﻄﺢ ﺑﻬﺘﺮﻳﻦ‬.‫ﻋﺮﺿﻲ ﻣﺎرﭘﻴﭽﻲ ﺷﻨﺎﺧﺘﻪ ﻣﻲﺷﻮﻧﺪ‬
‫ﻛﺎرﺑﺮد را زﻣﺎﻧﻲ دارد ﻛﻪ ﺧﻮاص اﻧﺘﻘﺎل ﺣﺮارت ﻳﻚ ﺳﻴﺎل ﻣﻨﺠﺮ‬
‫ﺑﻪ ﻣﻘﺎوﻣﺖ ﺑﺎﻻ در اﻧﺘﻘﺎل ﮔﺮﻣﺎ و ﺳﻴﺎل دﻳﮕﺮ ﻣﻘﺎوﻣﺖ ﻛﻤﻲ‬
‫ ﺳﻴﺎل ﺑــﺎ ﻣﻘﺎوﻣﺖ ﺑﺎﻻ در اﻧﺘﻘﺎل ﮔﺮﻣﺎ ﺑﺎ ﺳﻄﺢ‬.‫داﺷﺘﻪ ﺑﺎﺷﺪ‬
.‫ﭘﺮهدار در ﺗﻤﺎس ﻗﺮار ﻣﻲﮔﻴﺮد‬
‫ ﭘﺮه ﺑﺮﻧﺠﻲ ﻟﺤﻴﻢ ﺷﺪه‬5-6-5-7
7.5.6.5 Brazed plate fin
Brazed plate fin heat exchangers are made up of a
stack of layers which consist of a corrugated fin
between plate metal sheets, sealed off on two
sides by channels or bars to form a passage for
the flow of fluid. Maximum design conditions are
about 41 bar(ga) at 38°C. Typical design
conditions are for lower pressure and sub zero
temperatures. Plate-fin type exchangers in
applicable services in some recent ethylene plant
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﺮهدار ﺑﺮﻧﺠﻲ ﻟﺤﻴﻢ ﺷﺪه از ﻣﺠﻤﻮﻋﻪاي از‬
‫ آبﺑﻨﺪي ﺷﺪه از دو‬،‫ﭘﺮهﻫﺎي ﻣﻮﺟﺪار ﺑﻴﻦ ﺻﻔﺤﺎت ﻓﻠﺰي‬
‫ﻃﺮف ﺗﻮﺳﻂ ﻛﺎﻧﺎل ﻳﺎ ﻣﻴﻠﻪﻫﺎﻳﻲ ﺑﺮاي ﺗﺸﻜﻴﻞ ﻣﺴﻴﺮ ﺟﺮﻳﺎن‬
41 ‫ ﺣﺪاﻛﺜﺮ ﺷﺮاﻳﻂ ﻃﺮاﺣــﻲ‬.‫ﺳﻴــﺎل ﺳﺎﺧﺘﻪ ﺷﺪه اﺳﺖ‬
‫ ﺷﺮاﻳﻂ ﻃﺮاﺣﻲ‬.‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﻣﻲﺑﺎﺷﺪ‬38 ‫ﺑﺎر)ﻧﺴﺒﻲ( در‬
‫ ﻣﺒﺪلﻫﺎي‬.‫ﻣﻌﻤﻮﻟﻲ ﺑﺮاي ﻓﺸﺎر ﭘﺎﻳﻴﻦ و دﻣﺎي زﻳﺮ ﺻﻔﺮ ﻣﻲﺑﺎﺷﺪ‬
‫ﻧﻮع ﺻﻔﺤﻪاي ﭘﺮهدار در ﻛﺎرﺑﺮيﻫﺎي ﻗﺎﺑﻞ اﺳﺘﻔﺎده در ﺑﺮﺧﻲ‬
29
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
designs have been used.
.‫ﻃﺮاﺣﻲ ﻫﺎي اﺧﻴﺮ واﺣﺪ اﺗﻴﻠﻦ اﺳﺘﻔﺎده ﺷﺪه اﺳﺖ‬
7.5.6.6 Spiral wound (Hampson Coil)
(Hampson ‫ ﻣﺎرﭘﻴﭽﻲ ﺷﺪه )ﻛﻮﻳﻞ‬6-6-5-7
Spiral tube heat exchangers consist of a group of
concentric spirally wound coils, which are
connected to tube sheets. Features include
countercurrent flow, elimination of differential
expansion problems, compactness, and provision
for more than two fluids exchanging heat. In
general, these units are used in cryogenic
applications where the process pressure is 45 bar
(ga) or greater.
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻟﻮﻟﻪاي دوار ﺷﺎﻣﻞ ﻣﺠﻤﻮﻋﻪاي از ﻛﻮﻳﻞﻫﺎي‬
‫ﻣﺎرﭘﻴﭽﻲ ﻫﻢ ﻣﺮﻛﺰ ﻣﻲ ﺑﺎﺷﺪ ﻛﻪ ﺑــﻪ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﻫﺎ ﻣﺘﺼﻞ‬
‫ ﺣﺬف ﻣﺸﻜﻼت‬،‫ ﻣﺰاﻳﺎي آن ﺷﺎﻣﻞ ﺟﺮﻳﺎن ﻏﻴﺮﻫﻤﺴﻮ‬.‫ﺷﺪه اﺳﺖ‬
‫ ﺗﺮاﻛﻢ ﺣﺠﻢ و ﭘﻴﺶ ﺑﻴﻨﻲ ﺗﺒﺎدل ﺣﺮارت ﺑﺮاي‬،‫اﻧﺒﺴﺎط ﻣﺘﻔﺎوت‬
‫ در ﻛﻞ اﻳﻦ واﺣﺪﻫﺎ ﺑﺮاي‬.‫ﺑﻴﺶ از دو ﺳﻴﺎل ﻣﻲ ﺑﺎﺷﺪ‬
‫ ﺑﺎر)ﻧﺴﺒﻲ( و‬45 ‫ﻛﺎرﺑﺮدﻫﺎي ﺳﺮﻣﺎﻳﺸﻲ ﺑﺎ ﻓﺸﺎر ﻓﺮآﻳﻨﺪي‬
.‫ﺑﻴﺸﺘﺮ اﺳﺘﻔﺎده ﻣﻲ ﺷﻮد‬
‫ رواﺑﻂ ﭘﺎﻳﻪ‬-8
8. BASIC RELATIONS
8.1 Fluid Temperature Relations
8.1.1
Logarithmic
difference (LMTD)
mean
‫ رواﺑﻂ دﻣﺎي ﺳﻴﺎل‬1-8
temperature
(LMTD) ‫ اﺧﺘﻼف دﻣﺎي ﻣﻴﺎﻧﮕﻴﻦ ﻟﮕﺎرﻳﺘﻤﻲ‬1-1-8
For cases of true countercurrent or cocurrent
flow, the logarithmic mean temperature
difference should be used if the following
conditions substantially apply:
‫ ﺗﻮﺻﻴﻪ‬،‫ﺑﺮاي ﺣﺎﻟﺖﻫﺎي ﺟﺮﻳﺎن ﻫﻤﺴﻮ ﻳﺎ ﻏﻴﺮﻫﻤﺴﻮ واﻗﻌﻲ‬
‫ اﮔﺮ‬،‫ﻣﻲﺷﻮد از اﺧﺘﻼف دﻣﺎي ﻣﻴﺎﻧﮕﻴﻦ ﻟﮕﺎرﻳﺘﻤﻲ اﺳﺘﻔﺎده ﺷﻮد‬
:‫ﺷﺮاﻳﻂ زﻳﺮ اﺳﺎﺳﺎً ﺑﻪ ﻛﺎر رود‬
- Constant overall heat transfer coefficient.
.‫ ﺿﺮﻳﺐ ﻛﻠﻲ اﻧﺘﻘﺎل ﺣﺮارت ﺛﺎﺑﺖ‬-
- Complete mixing within any shell cross
pass or tube pass.
.‫ اﺧﺘﻼط ﻛﺎﻣﻞ در ﻫﺮ راﻫﻪ ﻟﻮﻟﻪ ﻳﺎ راﻫﻪ ﺟﺎﻧﺒﻲ ﭘﻮﺳﺘﻪ‬-
- The number of cross baffles is large.
.‫ ﺗﻌﺪاد ﺻﻔﺤﺎت ﺟﺪا ﻛﻨﻨﺪه ﻋﺮﺿﻲ زﻳﺎد‬-
- Constant flow rate and specific heat.
.‫ دﺑﻲ ﺳﻴﺎل و ﮔﺮﻣﺎي وﻳﮋه ﺛﺎﺑﺖ‬-
- Enthalpy is a linear function of temperature.
.‫ آﻧﺘﺎﻟﭙﻲ ﺗﺎﺑﻊ ﺧﻄﻲ از دﻣﺎ‬-
- Equal surface in each shell pass or tube
pass.
.‫ ﺳﻄﺢ ﻣﺴﺎوي در ﻫﺮ راﻫﻪ ﻟﻮﻟﻪ ﻳﺎ ﭘﻮﺳﺘﻪ‬-
- Negligible heat loss to surroundings or
internally between passes.
.‫ اﺗﻼف ﻧﺎﭼﻴﺰ ﺣﺮارت ﺑﻪ ﻣﺤﻴﻂ ﻳﺎ داﺧﻠﻲ ﺑﻴﻦ راﻫﻪﻫﺎ‬‫ ﺗﺼﺤﻴﺢ ﺑﺮاي ﺟﺮﻳﺎن ﭼﻨﺪ راﻫﻪ‬2-1-8
8.1.2 Correction for multipass flow
In multipass heat exchangers, where there is a
combination of cocurrent and countercurrent flow
in alternate passes, the mean temperature
difference is less than the logarithmic mean
calculated for countercurrent flow and greater
than that based on cocurrent flow. The correct
mean temperature difference may be evaluated as
the product of the logarithmic mean for
countercurrent flow and an LMTD correction
factor,F. For these factors refer to TEMA.
‫ ﺟﺎﻳﻲ ﻛﻪ ﺗﺮﻛﻴﺒـﻲ از ﺟﺮﻳـﺎن‬،‫در ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭼﻨﺪ راﻫﻪ‬
‫ اﺧـﺘﻼف‬،‫ﻫﻤﺴﻮ و ﻏﻴﺮ ﻫﻤﺴﻮ در راﻫﻪﻫﺎي ﻣﺨﺘﻠﻒ وﺟـﻮد دارد‬
‫دﻣﺎي ﻣﻴﺎﻧﮕﻴﻦ ﻛﻤﺘﺮ از ﻣﻴﺎﻧﮕﻴﻦ ﻟﮕﺎرﻳﺘﻤﻲ ﻣﺤﺎﺳﺒﻪ ﺷﺪه ﺑـﺮاي‬
.‫ﺟﺮﻳــﺎن ﻏﻴﺮﻫﻤــﺴﻮ و ﺑﻴــﺸﺘﺮ ﺑــﺮاي ﺟﺮﻳــﺎن ﻫﻤــﺴﻮ ﻣــﻲﺑﺎﺷــﺪ‬
‫اﺧﺘﻼف دﻣﺎي ﻣﻴﺎﻧﮕﻴﻦ ﺗﺼﺤﻴﺢ ﺷﺪه از ﻣﺤﺎﺳﺒﻪ ﺣﺎﺻﻞ ﺿـﺮب‬
‫ﺑـﺮاي‬F ‫ﻣﻴﺎﻧﮕﻴﻦ ﻟﮕﺎرﻳﺘﻤﻲ ﺟﺮﻳﺎن ﻏﻴﺮﻫﻤﺴﻮ و ﺿﺮﻳﺐ ﺗﺼﺤﻴﺢ‬
TEMA ‫ ﺑـﺮاي اﻳـﻦ ﺿـﺮاﻳﺐ ﺑـﻪ‬.‫ ﺑﻪ دﺳﺖ ﻣـﻲآﻳـﺪ‬LMTD
.‫ﻣﺮاﺟﻌﻪ ﺷﻮد‬
‫ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬2-8
8.2 Fouling
‫ اﻧﻮاع رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬1-2-8
8.2.1 Types of fouling
Currently
five
different
types
of
‫اﻣﺮوزه ﭘﻨﺞ ﻧﻮع از ﻣﻜﺎﻧﻴﺰمﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺷﻨﺎﺧﺘﻪ ﺷﺪه‬
fouling
30
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
mechanisms
are
recognized.
They
are
individually
complex,
often
occurring
simultaneously, and their effects may increase
pressure drop, accelerate corrosion and decrease
the overall heat transfer coefficient. The five
different types are:
IPS-E-PR- 771(1)
‫ اﻏﻠﺐ ﻫﻤﺰﻣﺎن اﺗﻔﺎق ﻣﻲاﻓﺘﺪ و‬،‫ ﻫﺮ ﻛﺪام ذاﺗﺎ ﭘﻴﭽﻴﺪه‬.‫اﺳﺖ‬
‫ ﺧﻮردﮔﻲ را ﺷﺘﺎب‬،‫اﺛﺮات آﻧﻬﺎ اﻓﺖ ﻓﺸﺎر را اﻓﺰاﻳﺶ ﻣﻲدﻫﺪ‬
‫ ﭘﻨﺞ‬.‫ﺑﺨﺸﻴﺪه و ﺿﺮﻳﺐ ﻛﻠﻲ اﻧﺘﻘﺎل ﺣﺮارت را ﻛﺎﻫﺶ ﻣﻲدﻫﻨﺪ‬
:‫ﻧﻮع ﻋﺒﺎرﺗﻨﺪ از‬
.‫اﻟﻒ( رﺳﻮب ﺗﻪ ﻧﺸﻴﻨﻲ‬
a) Precipitation fouling.
.‫ب ( رﺳﻮب ذرات‬
b) Particular fouling.
.‫ج ( رﺳﻮب واﻛﻨﺶ ﺷﻴﻤﻴﺎﻳﻲ‬
c) Chemical reaction fouling.
d) Corrosion fouling.
.‫د ( رﺳﻮب ﺧﻮردﮔﻲ‬
e) Biological fouling
‫ﻫ( رﺳﻮب ﺑﻴﻮﻟﻮژﻳﻜﻲ‬
.‫ ﻣﺮاﺟﻌﻪ ﺷﻮد‬TEMA ‫ﺑﺮاي اﻃﻼﻋﺎت ﺑﻴﺸﺘﺮ ﺑﻪ‬
For further information refer to TEMA.
8.2.2 Considerations in evaluating fouling
resistance
‫ﻣﻼﺣﻈﺎت ﺑﺮاي ﻣﺤﺎﺳﺒﻪ ﻣﻘﺎوﻣﺖ رﺳﻮب‬
The determination of appropriate fouling
resistance values involves both physical and
economic factors, many of which vary from user
to user, even for identical services. When these
factors are known, they can be used to adjust
typical base values.
‫ﻣﺸﺨﺺ ﻛﺮدن ﻣﻘﺪار ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻣﻨﺎﺳﺐ ﺷﺎﻣﻞ‬
‫ﻋﺎﻣﻞ ﻫﺎي ﻫﻤﺰﻣﺎن ﻓﻴﺰﻳﻜﻲ و اﻗﺘﺼﺎدي ﻣﻲﺑﺎﺷﺪ ﻛﻪ از ﻫﺮ‬
‫ﻛﺎرﺑﺮ ﺑﻪ ﻛﺎرﺑﺮ دﻳﮕﺮ ﺣﺘﻲ ﺑﺮاي ﻛﺎرﺑﺮيﻫﺎي ﻳﻜﺴﺎن ﺑﺴﻴﺎر‬
‫ آﻧﻬﺎ‬،‫ زﻣﺎﻧﻲ ﻛﻪ اﻳﻦ ﻓﺎﻛﺘﻮرﻫﺎ ﺷﻨﺎﺧﺘﻪ ﺷﻮﻧﺪ‬.‫ﻣﺘﻔﺎوت اﺳﺖ‬
.‫ﻣﻲﺗﻮاﻧﻨﺪ ﺑﺮاي ﺗﻨﻈﻴﻢ ﻣﻘﺎدﻳﺮ ﭘﺎﻳﻪ واﺑﺴﺘﻪ اﺳﺘﻔﺎده ﺷﻮﻧﺪ‬
‫ﮔﺮﻓﺘﮕﻲ‬
‫ ﻣﻼﺣﻈﺎت ﻓﻴﺰﻳﻜﻲ‬1-2-2-8
8.2.2.1 Physical considerations
Typical physical factors influencing
determination of fouling resistances are:
2-2-8
the
‫ﻋﺎﻣﻞ ﻫﺎي ﻓﻴﺰﻳﻜﻲ ﻧﻤﻮﻧﻪ ﻛﻪ ﻣﺤﺎﺳﺒﻪ ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬
:‫را ﺗﺤﺖ ﺗﺄﺛﻴﺮ ﻗﺮار ﻣﻲدﻫﻨﺪ ﻋﺒﺎرﺗﻨﺪ از‬
- Fluid properties and the propensity for
fouling.
.‫ ﺧﻮاص ﺳﻴﺎل و ﺗﻤﺎﻳﻞ ﺑﻪ رﺳﻮب‬-
- Heat exchanger geometry and orientation.
‫ ﺷﻜﻞ ﻫﻨﺪﺳﻲ و ﺟﻬﺖ ﻗﺮار ﮔﺮﻓﺘﻦ ﻣﺒﺪل ﺣﺮارﺗﻲ‬-
- Surface and fluid bulk temperatures.
. ‫ دﻣﺎي ﺳﻄﺢ اﻧﺘﻘﺎل ﺣﺮارت و ﺗﻮده ﺳﻴﺎل‬-
- Local fluid velocities.
.‫ ﺳﺮﻋﺖ ﻫﺎي ﻧﻘﻄﻪ اي ﺳﻴﺎل‬-
- Heat transfer process.
.‫ ﻣﻜﺎﻧﻴﺰم اﻧﺘﻘﺎل ﺣﺮارت‬-
- Fluid treatment to prevent corrosion and
biological growth
‫ﻓﺮآورش ﺳﻴﺎل ﺑﺮاي ﻣﻤﺎﻧﻌﺖ از ﺧﻮردﮔﻲ و رﺷﺪ‬
.‫ﺑﻴﻮﻟﻮژﻳﻜﻲ‬
-
.‫ ﻓﺮآورش ﺳﻴﺎل ﺑﺮاي ﻛﺎﻫﺶ رﺳﻮب دﻫﻲ‬-
- Fluid treatment to reduce fouling
- Cathodic protection.
.‫ ﻣﺤﺎﻓﻈﺖ ﻛﺎﺗﺪﻳﻚ‬-
- Tube material, configuration and surface
finish
.‫ آراﻳﺶ و ﭘﺮدازش ﺳﻄﺢ‬،‫ ﺟﻨﺲ ﻟﻮﻟﻪ‬‫ ﻣﻼﺣﻈﺎت اﻗﺘﺼﺎدي‬2-2-2-8
8.2.2.2 Economic considerations
Typical economic factors influencing the
determination of appropriate fouling resistances
are:
‫ﻓﺎﻛﺘﻮرﻫﺎي اﻗﺘﺼﺎدي ﻧﻤﻮﻧﻪ ﻛﻪ ﻣﺤﺎﺳﺒﻪ ﻣﻘﺎوﻣﺖ رﺳﻮب‬
:‫ﮔﺮﻓﺘﮕﻲ را ﺗﺤﺖ ﺗﺄﺛﻴﺮ ﻗﺮار ﻣﻲدﻫﻨﺪ ﻋﺒﺎرﺗﻨﺪ از‬
31
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
- Frequency and amount of cleaning costs.
IPS-E-PR- 771(1)
.‫ ﺗﻮاﻟﻲ و ﻣﻘﺪار ﻫﺰﻳﻨﻪ ﺗﻤﻴﺰﻛﺎري‬-
- Maintenance costs.
‫ ﻫﺰﻳﻨﻪ ﻧﮕﻬﺪاري‬-
- Operating and production costs.
.‫ ﻫﺰﻳﻨﻪ ﻋﻤﻠﻴﺎت و ﺗﻮﻟﻴﺪ‬-
- Longer periods of time on stream.
.‫ دورهﻫﺎي ﻃﻮﻳﻞﺗﺮ زﻣﺎن ﻛﺎرﻛﺮد‬.‫ ﻫﺰﻳﻨﻪ ﺗﻠﻤﺒﻪ ﻛﺮدن ﺳﻴﺎل‬-
- Fluid pumping costs.
.‫ ﻧﺮخ اﺳﺘﻬﻼك‬-
- Depreciation rates.
.‫ ﻧﺮخ ﻣﺎﻟﻴﺎت‬-
- Tax rates.
.‫ ﻫﺰﻳﻨﻪ اوﻟﻴﻪ و ﺗﻐﻴﻴﺮات آن ﺑﺎ اﻧﺪازه‬-
- Initial cost and variation with size.
.‫ ﻫﺰﻳﻨﻪ ﺑﺴﺘﻦ‬-
- Shut down costs.
.‫ ﻫﺰﻳﻨﻪﻫﺎي ﺧﺮوج از ﻛﺎرﺑﺮي‬-
- Out-of-service costs.
8.2.2.3 Further
considerations
explanation
to
‫ ﺷﺮح ﺑﻴﺸﺘﺮ ﺑﻪ ﻣﻼﺣﻈﺎت ﻓﻴﺰﻳﻜﻲ‬3-2-2-8
physical
‫اﻟﻒ( ﺳﻄﺢ و دﻣﺎي ﺗﻮده ﺳﻴﺎل‬
a) Surface and bulk temperatures
For many kinds of fouling, as the temperatures
increase, the amount of fouling increases.
Lower temperatures produce slower fouling
build-up and deposits that often are easier to
remove.
‫ ﻣﻘﺪار رﺳﻮب‬،‫ ﺑﺎ اﻓﺰاﻳﺶ دﻣﺎ‬،‫ﺑﺮاي ﺑﻴﺸﺘﺮ اﻧﻮاع رﺳﻮب ده‬
‫ رﺳﻮب و ﺗﻪ‬،‫ دﻣﺎﻫﺎي ﻛﻤﺘﺮ‬.‫دﻫﻲ ﻧﻴﺰ اﻓﺰاﻳﺶ ﻣﻲﻳﺎﺑﺪ‬
‫ﻧﺸﻴﻨﻲ ﻛﻤﺘﺮي ﺗﻮﻟﻴﺪ ﻣﻲﻛﻨﻨﺪ ﻛﻪ اﻏﻠﺐ ﺣﺬف راﺣﺖﺗﺮي‬
.‫دارﻧﺪ‬
‫ب ( ﺳﺮﻋﺖﻫﺎي ﻧﻘﻄﻪ اي‬
b) Local velocities
Normally, keeping the velocities high reduces
the tendency to foul. Velocities on the tube
side are limited by erosion and on the shell
side by flow-induced vibration. Stagnant and
recirculation regions on the shell side lead to
heavy fouling.
‫ ﺗﻤﺎﻳﻞ ﺑﻪ رﺳﻮب را ﻛﺎﻫﺶ‬،‫ﻣﻌﻤﻮﻻً ﺑﺎﻻ ﻧﮕﻬﺪاﺷﺘﻦ ﺳﺮﻋﺖ‬
‫ ﺳﺮﻋﺖﻫﺎ در ﺳﻤﺖ ﻟﻮﻟﻪ ﺗﻮﺳﻂ ﺳﺎﻳﺶ و در ﺳﻤﺖ‬.‫ﻣﻲدﻫﺪ‬
.‫ﭘﻮﺳﺘﻪ ﺗﻮﺳﻂ ﻟﺮزش ﻧﺎﺷﻲ از ﺟﺮﻳﺎن ﻣﺤﺪود ﺷﺪهاﻧﺪ‬
‫ رﺳﻮبدﻫﻲ‬،‫ﻧﺎﺣﻴﻪﻫﺎي اﻳﺴﺘﺎ و ﭼﺮﺧﺸﻲ در ﺳﻤﺖ ﭘﻮﺳﺘﻪ‬
.‫زﻳﺎدي دارﻧﺪ‬
c) Tube material, configuration and surface
finish
‫ آراﻳﺶ و ﭘﺮدازش ﺳﻄﺢ‬،‫ج ( ﺟﻨﺲ ﻟﻮﻟﻪ‬
The selection of tube material is significant
when it comes to corrosion. Some kinds of
biological fouling can be lessened by copperbearing tube materials. There can be
differences between finned and plain tubing.
Surface finish has been shown to influence the
rate of fouling and the ease of cleaning.
‫اﻧﺘﺨﺎب ﺟﻨﺲ ﻟﻮﻟﻪ زﻣﺎﻧﻲ ﻛﻪ اﺣﺘﻤﺎل ﺧﻮردﮔﻲ وﺟﻮد‬
‫ ﺑﺮﺧﻲ اﻧﻮاع رﺳﻮب ﺑﻴﻮﻟﻮژﻳﻜﻲ‬.‫ ﻣﻬﻢ اﺳﺖ‬،‫داﺷﺘﻪ ﺑﺎﺷﺪ‬
-‫ ﺑﻴﻦ ﻟﻮﻟﻪ‬.‫ﺗﻮﺳﻂ ﻟﻮﻟﻪﻫﺎي ﺑﺎ ﺟﻨﺲ ﻣﺲ ﻛﺎﻫﺶ ﻣﻲﻳﺎﺑﻨﺪ‬
‫ ﭘﺮدازش ﺳﻄﺢ ﺑﺮ‬.‫ﻫﺎي ﺻﺎف و ﭘﺮهدار ﺗﻔﺎوت وﺟﻮد دارد‬
.‫ﺷﺪت رﺳﻮبدﻫﻲ و راﺣﺘﻲ ﺗﻤﻴﺰﻛﺎري اﺛﺮ ﻣﻲ ﮔﺬارد‬
d) Heat
orientation
exchanger
geometry
and
‫د( آراﻳﺶ ﻫﻨﺪﺳﻲ و ﺟﻬﺖ ﻣﺒﺪل ﺣﺮارﺗﻲ‬
The geometry of a particular heat exchanger
can influence the uniformity of the flows on
the tube side and the shell side. The ease of
cleaning can be greatly influenced by the
orientation of the heat exchanger.
‫ﻫﻨﺪﺳﻪ ﻳﻚ ﻣﺒﺪل ﺣﺮارﺗﻲ ﺧﺎص ﻣﻲﺗﻮاﻧﺪ ﻳﻜﻨﻮاﺧﺘﻲ‬
‫ﺟﺮﻳﺎن در ﺳﻤﺖ ﻟﻮﻟﻪ و ﺳﻤﺖ ﭘﻮﺳﺘﻪ را ﺗﺤﺖ ﺗﺄﺛﻴﺮ ﻗﺮار‬
‫ ﺳﻬﻮﻟﺖ ﺗﻤﻴﺰﻛﺎري ﺑﻪ ﻣﻘﺪار زﻳﺎدي ﺗﺤﺖ ﺗﺄﺛﻴﺮ ﺟﻬﺖ‬.‫دﻫﺪ‬
.‫ﻧﺼﺐ ﻣﺒﺪل ﺣﺮارﺗﻲ ﻗﺮار دارد‬
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Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ﻫ( ﻣﻜﺎﻧﻴﺰم اﻧﺘﻘﺎل ﺣﺮارت‬
e) Heat transfer process
The fouling resistances for the same fluid can
be considerably different depending upon
whether heat is being transferred through
sensible heating or cooling, boiling, or
condensing.
‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺑﺮاي ﻳﻚ ﺳﻴﺎل ﺑﻪ ﻣﻘﺪار ﻗﺎﺑﻞ‬
‫ﻣﻼﺣﻈﻪاي ﺑﺴﺘﻪ ﺑﻪ ﻧﺤﻮه اﻧﺘﻘﺎل ﺣﺮارت از ﮔﺮﻣﺎي‬
‫ ﻣﺘﻔﺎوت‬،‫ ﺟﻮﺷﺶ ﻳـــﺎ ﭼﮕﺎﻟﺶ‬،‫ﻣﺤﺴﻮس ﻳﺎ ﺳـﺮد ﺷﺪن‬
.‫ﻣﻲﺑﺎﺷﺪ‬
f) Place the more fouling fluid on the tube
side
‫و( ﻫﺪاﻳﺖ ﺳﻴﺎل ﺑﺎ رﺳﻮب دﻫﻲ ﺑﻴﺸﺘﺮ در ﺳﻤﺖ ﻟﻮﻟﻪ‬
There are two benefits from placing the more
fouling fluid on the tube side. There is less
danger of low velocity or stagnant flow
regions on the tube side, and, it is generally
easier to clean the tube side than the shell side.
It is often possible to clean the tube side with
the exchanger in place while it may be
necessary to remove the bundle to clean the
shell side.
‫ﻫﺪاﻳﺖ ﺳﻴﺎل ﺑﺎ رﺳﻮب دﻫﻲ ﺑﻴﺸﺘﺮ در ﺳﻤﺖ ﻟﻮﻟﻪ دو‬
‫ ﺧﻄﺮ ﺳﺮﻋﺖ ﭘﺎﻳﻴﻦ ﻳﺎ ﻧﺎﺣﻴﻪ ﺟﺮﻳﺎن اﻳﺴﺘﺎ در‬.‫ﻣﺰﻳﺖ دارد‬
‫ﺳﻤﺖ ﻟﻮﻟﻪ ﻛﻤﺘﺮ و ﻋﻤﻮﻣﺎً ﺳﻤﺖ ﻟﻮﻟﻪ ﻧﺴﺒﺖ ﺑﻪ ﺳﻤﺖ‬
‫ اﻏﻠﺐ ﺗﻤﻴﺰﻛﺮدن ﺳﻤﺖ‬.‫ﭘﻮﺳﺘﻪ راﺣﺖﺗــﺮ ﺗﻤﻴﺰ ﻣﻲﺷﻮد‬
‫ﻟﻮﻟﻪ در ﻣﺒﺪل در ﻣﺤﻞ ﺧﻮد اﻣﻜﺎنﭘﺬﻳﺮ اﺳﺖ در ﺣﺎﻟﻲ ﻛﻪ‬
‫ﺑﺮاي ﺗﻤﻴﺰ ﻛﺮدن ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻻزم اﺳﺖ دﺳﺘﻪ ﻟﻮﻟﻪ ﺧﺎرج‬
.‫ﺷﻮﻧﺪ‬
g) Cathodic protection
‫ز( ﺣﻔﺎﻇﺖ ﻛﺎﺗﺪي‬
One of the effective ways to reduce the
possibility of corrosion and corrosion fouling
is to provide cathodic protection in the design.
‫ﻳﻜﻲ از روشﻫﺎي ﻣﻮﺛﺮ در ﻛﺎﻫﺶ اﺣﺘﻤﺎل ﺧﻮردﮔﻲ و‬
‫ ﭘﻴﺶ ﺑﻴﻨﻲ ﺣﻔﺎﻇﺖ ﻛﺎﺗﺪي در ﻃﺮاﺣﻲ‬،‫رﺳﻮب ﺧﻮردﮔﻲ‬
.‫ﻣﻲﺑﺎﺷﺪ‬
h) Fouling is more severe when heating
hydrocarbons than when cooling them. In the
case of pipe stills, this is due to "salting out".
To minimize this sort of fouling, a crude
preheat train sometimes includes a desalter or
a flash drum to remove water before the crude
reaches the "salting out" temperature.
‫ح( رﺳﻮب دﻫﻲ در ﻣﻮﻗﻊ ﮔﺮم ﻛﺮدن ﻫﻴﺪروﻛﺮﺑﻦﻫﺎ ﻧﺴﺒﺖ‬
‫ در ﺣﺎﻟﺖ ﺗﻘﻄﻴﺮ‬.‫ﺑــﻪ ﺳﺮدﻛﺮدن آﻧﻬــﺎ ﺷﺪﻳﺪﺗــﺮ اﺳﺖ‬
"‫( رﺳﻮب ﮔﺬاري ﺑﻪ ﻋﻠﺖ "ﻧﻤﻚ دﻫﻲ‬Pipe Still)
‫ واﺣﺪ ﭘﻴﺶ ﮔﺮم‬،‫ ﺑﺮاي ﻛﺎﻫﺶ اﻳﻦ ﻧﻮع رﺳﻮبدﻫﻲ‬.‫ﻣﻲﺑﺎﺷﺪ‬
‫ﻛﻦ ﻧﻔﺖ ﺧﺎم در ﺑﻌﻀﻲ ﻣﻮاﻗﻊ ﺷﺎﻣﻞ ﻧﻤﻚ زدا ﻳﺎ ﻳﻚ‬
‫ﻣﺨﺰن ﺗﺒﺨﻴﺮ آﻧﻲ ﺑﺮاي ﺣﺬف آب ﻗﺒﻞ از رﺳﻴﺪن ﻧﻔﺖ ﺧﺎم‬
.‫ﺑﻪ دﻣﺎي "ﻧﻤﻚ دﻫﻲ" ﻣﻲﺑﺎﺷﺪ‬
i) Vaporization in an exchanger can cause
severe fouling.
‫ط( ﺗﺒﺨﻴﺮ در ﻣﺒﺪل ﻣﻤﻜﻦ اﺳﺖ ﻣﻮﺟﺐ رﺳﻮب دﻫﻲ‬
a) High velocities reduce fouling. This is
especially true in the case of cooling water
that contains salt.
.‫ي( ﺳﺮﻋﺖﻫﺎي ﺑﺎﻻ رﺳﻮب دﻫﻲ را ﻛﺎﻫﺶ ﻣﻲدﻫﻨﺪ‬
k) The feed to catalytic reformers and catalytic
cracking plants is sometimes severely fouled
due to organic reactions with oxygen while the
feed is in intermediate tankage. Inert gas
blanketing of the tankage is often used to
reduce this fouling.
‫ك( ﺧﻮراك واﺣﺪﻫﺎي رﻓﺮﻣﺮ ﻛﺎﺗﺎﻟﻴﺴﺘﻲ و ﻛﺮاﻛﻴﻨﮓ‬
.‫ﺷﺪﻳﺪ ﺷﻮد‬
،‫ﻣﺨﺼﻮﺻﺎً در ﺣﺎﻟﺖ آب ﺧﻨﻚ ﻛﻨﻨﺪه ﻛﻪ ﺷﺎﻣﻞ ﻧﻤﻚ اﺳﺖ‬
.‫ﺻﺤﻴﺢ ﻣﻲﺑﺎﺷﺪ‬
‫ﻛﺎﺗﺎﻟﻴﺴﺘﻲ در ﺑﻌﻀﻲ ﻣﻮاﻗﻊ ﺑﻪ ﺧﺎﻃﺮ واﻛﻨﺶ ﻣﻮاد آﻟﻲ ﺑﺎ‬
ً‫اﻛﺴﻴﮋن زﻣﺎﻧﻲ ﻛﻪ در ﻣﺨﺎزن واﺳﻄﻪ ﻫﺴﺘﻨﺪ ﺷﺪﻳﺪا‬
‫ ﮔﺎز ﭘﻮﺷﺸﻲ ﺧﻨﺜﻲ در ﻣﺨﺎزن اﻏﻠﺐ ﺑﺮاي‬.‫رﺳﻮبده ﻫﺴﺘﻨﺪ‬
.‫ﻛﺎﻫﺶ رﺳﻮب اﺳﺘﻔﺎده ﻣﻲﺷﻮد‬
‫ اﮔﺮﭼﻪ‬،‫ل(ﻣﺤﺼﻮﻻت زﻳﺮ ﺑﺮج آﺗﻤﺴﻔﺮﻳﻚ ﺗﻘﻄﻴﺮ ﻧﻔﺖ ﺧﺎم‬
l) Bottoms from a crude distillation tower,
even though heavy and at a high temperature
‫ﺳﻨﮕﻴﻦ و در دﻣﺎي ﺑﺎﻻ ﻫﺴﺘﻨﺪ ﻣﻨﺠﺮ ﺑﻪ رﺳﻮب دﻫﻲ زﻳﺎد‬
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IPS-E-PR- 771(1)
will not normally cause much fouling
(provided flash zone temperatures are not
excessive).
‫ﻧﻤﻲﺷﻮﻧﺪ )دﻣﺎﻫﺎي ﻧﺎﺣﻴﻪ ﺗﺒﺨﻴﺮ آﻧﻲ اﻳﺠﺎد ﺷﺪه زﻳﺎد‬
.(‫ﻧﻴﺴﺘﻨﺪ‬
m) Fluid treatment to provide corrosion and
biological growth. Fluid treatment is
commonly carried out to prevent corrosion
and / or biological growth. If these treatments
are neglected, rapid fouling can occur.
‫م( ﻓﺮآورش ﺳﻴﺎل ﺑﺮاي آﻣﺎده ﻛﺮدن ﺧﻮردﮔﻲ و رﺷﺪ‬
‫ﻳﺎ‬/‫ ﻓﺮآورش ﺳﻴﺎل ﺑﺮاي ﺟﻠﻮﮔﻴﺮي از ﺧﻮردﮔﻲ و‬.‫ﺑﻴﻮﻟﻮژﻳﻜﻲ‬
‫ اﮔﺮ اﻳﻦ ﻓﺮآورشﻫﺎ ﺻﺮﻓﻨﻈﺮ‬.‫رﺷﺪ ﺑﻴﻮﻟﻮژﻳﻜﻲ اﻧﺠﺎم ﻣﻲﺷﻮد‬
.‫ رﺳﻮبدﻫﻲ ﺳﺮﻳﻊ اﻣﻜﺎن وﻗﻮع دارد‬،‫ﺷﻮﻧﺪ‬
‫ن( ﻓﺮآورش ﺳﻴﺎل ﺑﺮاي ﻛﺎﻫﺶ رﺳﻮبدﻫﻲ‬
n) Fluid treatment to reduce fouling
There are additives that can disperse the
fouling material so it does not deposit.
Additives may also alter the structure of the
fouling layers that deposit so that they are
easily removed. The use of these treatments is
a product quality and economic decision.
‫اﻓﺰودﻧﻲﻫﺎﻳﻲ وﺟﻮد دارد ﻛﻪ ﻣﻲﺗﻮاﻧﺪ ﻣﻮاد رﺳﻮﺑﻲ را‬
‫ اﻓﺰودﻧﻲﻫﺎ ﻫﻤﭽﻨﻴﻦ‬.‫ﭘﺮاﻛﻨﺪه ﻛﻨﻨﺪ ﻛﻪ ﺗﻪ ﻧﺸﻴﻦ ﻧﺸﻮﻧﺪ‬
‫ﻣﻤﻜﻦ اﺳﺖ ﺳﺎﺧﺘﺎر ﻻﻳﻪﻫﺎي رﺳﻮﺑﻲ ﺗﻪ ﻧﺸﻴﻦ ﺷﺪه را‬
‫ در اﺳﺘﻔﺎده از اﻳﻦ‬.‫ﺗﻐﻴﻴﺮ دﻫﻨﺪ ﻛﻪ ﺑــﻪ راﺣﺘﻲ ﺣﺬف ﺷﻮﻧﺪ‬
.‫ﻓﺮآورشﻫـــﺎ ﻛﻴﻔﻴﺖ ﻣﺤﺼﻮل و اﻗﺘﺼﺎد ﺗﺼﻤﻴﻢﮔﻴﺮﻧﺪهاﻧﺪ‬
O) Fluid properties and the propensity for
fouling
‫س( ﺧﻮاص ﺳﻴﺎل و ﮔﺮاﻳﺶ ﺑﻪ رﺳﻮبدﻫﻲ‬
The most important consideration is the fluid
and conditions when it produces fouling. At
times, a process modification can result in
conditions that are less likely to cause fouling.
‫ﻣﻼﺣﻈﻪ ﺧﻴﻠﻲ ﻣﻬﻢ ﺳﻴﺎل و ﺷﺮاﻳﻄﻲ ﻛﻪ رﺳﻮب ﺗﻮﻟﻴﺪ‬
‫ اﺻﻼح ﻓﺮآﻳﻨﺪ ﻣﻨﺠﺮ ﺑﻪ ﺷﺮاﻳﻄﻲ‬،‫ﻣﻲﻛﻨﺪ در زﻣﺎنﻫﺎﻳﻲ‬
.‫ﻣﻲﺷﻮد ﻛﻪ ﺗﻤﺎﻳﻞ ﻛﻤﺘﺮي ﺑﻪ اﻳﺠﺎد رﺳﻮب اﻳﺠﺎد ﻣﻲﺷﻮد‬
‫ ﻛﺎرﺑﺮد ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻛﻢ‬3-2-8
8.2.3 Application of lower fouling resistances
Lower fouling resistances may be appropriate if
one or more of the circumstances described below
apply. However, such lower values may be
applied only where specifically approved by the
Company in writing.
‫ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻛﻢ ﻣﻤﻜﻦ اﺳﺖ ﻣﻨﺎﺳﺐ ﺑﺎﺷﺪ اﮔﺮ‬
‫ ﺑﺎ اﻳﻦ‬.‫ﻳﻚ ﻳﺎ ﭼﻨﺪ وﺿﻌﻴﺖ ﺗﺸﺮﻳﺢ ﺷﺪه در زﻳﺮ اﻋﻤﺎل ﺷﻮد‬
‫وﺟﻮد ﭼﻨﺎن ﻣﻘﺎدﻳﺮ ﻛﻤﻲ ﻣﻤﻜﻦ اﺳﺖ ﺑﻪ ﻛﺎر رود ﻓﻘﻂ ﺟﺎﻳﻲ‬
.‫ﻛﻪ اﺧﺘﺼﺎﺻﺎً ﺗﻮﺳﻂ ﺷﺮﻛﺖ در ﻧﺎﻣﻪ ﻧﮕﺎري ﻣﺸﺨﺺ ﺷﻮد‬
8.2.3.1 In services where the surface requirements
are significantly influenced by the magnitude of
fouling, it may be advantageous to specify a
lower resistance if a reduced period between two
successive shutdown is feasible. This can be
achieved for instance by the installation of a spare
exchanger in parallel with the one in operation,
thus enabling cleaning at any time, without plant
shut-down. This is especially important where
controllability/stability is influenced by fouling,
e.g., thermosyphon reboilers.
‫ در ﻛﺎرﺑﺮي ﻫﺎﻳﻲ ﻛﻪ اﻟﺰاﻣﺎت ﺳﻄﺢ ﺗﺤﺖ ﺗﺄﺛﻴﺮ‬1-3-2-8
‫ ﺑﻬﺘﺮ اﺳﺖ ﻳﻚ ﻣﻘﺎوﻣﺖ‬،‫ﻣﻘﺪار رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻗﺮار ﻣﻲ ﮔﻴﺮد‬
‫ﻛﻢ ﻣﺸﺨﺺ ﮔﺮدد در ﺻﻮرﺗﻴﻜﻪ ﺑﺘﻮان زﻣﺎن ﺑﻴﻦ دو ﺑﺴﺘﻦ ﭘﻲ‬
‫ اﻳﻦ ﻗﺎﺑﻞ ﺣﺼﻮل اﺳﺖ ﺑﺎ ﻧﺼﺐ ﻳﻚ‬. ‫در ﭘﻲ را ﻛﺎﻫﺶ داد‬
‫ ﺑﺎ اﻳﻦ‬.‫ﻣﺒﺪل ﻳﺪﻛﻲ ﻣﻮازي ﺑﺎ ﻣﺒﺪﻟﻲ ﻛﻪ در ﺑﻬﺮه ﺑﺮداري اﺳﺖ‬
‫ﻛﺎر اﻣﻜﺎن ﺗﻤﻴﺰ ﻛﺮدن در ﻫﺮ زﻣﺎن ﺑﺪون ﻧﻴﺎز ﺑﻪ ﺑﺴﺘﻦ ﺑﺮﻧﺎﻣﻪ‬
‫ اﻳﻦ ﺧﺼﻮﺻﺎً ﺣﺎﺋﺰ اﻫﻤﻴﺖ اﺳﺖ در‬.‫رﻳﺰي ﺷﺪه ﺧﻮاﻫﺪ ﺑﻮد‬
‫ﺛﺒﺎت ﺗﺤﺖ ﺗﺄﺛﻴﺮ رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬/ ‫ﺟﺎﺋﻴﻜﻪ ﻗﺎﺑﻠﻴﺖ ﻛﻨﺘﺮل‬
.‫ﻣﻲﺑﺎﺷﺪ ﻣﺎﻧﻨﺪ ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪهﻫﺎي ﺗﺮﻣﻮﺳﻴﻔﻮﻧﻲ‬
8.2.3.2 The maximum allowable pressure drop
generally limits the fluid velocity. This means
that for designs where low pressure drops have to
be applied fluid velocities will often become low.
If the specified fouling resistance is also high,
resulting in the installation of considerable
oversurface in clean condition, the maximum
‫ ﺣﺪاﻛﺜﺮ اﻓﺖ ﻓﺸﺎر ﻣﺠﺎز ﻋﻤﻮﻣﺎً ﺳﺮﻋﺖ ﺳﻴﺎل را‬2-3-2-8
‫ اﻳﻦ ﺑﺪان ﻣﻌﻨﻲ اﺳﺖ ﻛﻪ ﺑﺮاي ﻃﺮاﺣﻲ ﻛﻪ اﻓﺖ‬.‫ﻣﺤﺪود ﻣﻲﻛﻨﺪ‬
.‫ ﺳﺮﻋﺖﻫﺎي ﺳﻴﺎل اﻏﻠﺐ ﭘﺎﻳﻴﻦ ﻣﻲ آﻳﺪ‬،‫ﻓﺸﺎر ﻛﻢ ﺑﺎﻳﺪ ﺑﻜﺎر رود‬
،‫اﮔﺮ ﻫﻤﭽﻨﻴﻦ ﻣﻘﺎوﻣﺖ رﺳﻮﺑﻲ ﻣﺸﺨﺺ ﺷﺪه ﻧﻴﺰ ﺑﺎﻻ ﺑﺎﺷﺪ‬
‫ﻣﻨﺠﺮ ﺑﻪ ﻧﺼﺐ ﺳﻄﻮح اﺿﺎﻓﻲ ﻗﺎﺑﻞ ﻣﻼﺣﻈﻪ در ﺷﺮاﻳﻂ ﺗﻤﻴﺰ‬
34
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
attainable velocities will appreciably reduce,
which will increase the tendency to fouling. By
taking a small fouling resistance, a smaller heat
exchanger will be adequate, thus making it
possible to apply a higher velocity and still stay
within the limits of allowable pressure drop.
IPS-E-PR- 771(1)
‫ ﺣﺪاﻛﺜﺮ ﺳﺮﻋﺖﻫﺎي ﻗﺎﺑﻞ رﺳﻴﺪن ﺑﻪ ﻣﻘﺪار ﻣﺤﺴﻮﺳﻲ‬،‫ﺷﺪه‬
‫ﻛﺎﻫﺶ ﺧﻮاﻫﻨﺪ ﻳﺎﻓﺖ ﻛﻪ ﺗﻤﺎﻳﻞ ﺑﻪ رﺳﻮب دﻫﻲ را اﻓﺰاﻳﺶ‬
،‫ ﺑﺎ در ﻧﻈﺮ ﮔﺮﻓﺘﻦ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻛﻢ‬.‫ﻣﻲدﻫﺪ‬
‫ﻣﺒﺪل ﺣﺮارﺗﻲ ﻛﻮﭼﻜﺘﺮ ﻛﺎﻓﻲ ﺧﻮاﻫﺪ ﺑﻮد ﻛﻪ اﺳﺘﻔﺎده از‬
‫ﺳﺮﻋﺖﻫﺎي زﻳﺎد را ﻣﻤﻜﻦ ﻣﻲﻛﻨﺪ در ﺣﺎﻟﻴﻜﻪ ﻫﻨﻮز در ﻣﺮز اﻓﺖ‬
.‫ﻓﺸﺎر ﻣﺠﺎز ﻣﻲﺑﺎﺷﺪ‬
Though some construction materials can have a
beneficial influence on fouling, there is generally
inadequate information available. An exception
can be made for titanium in cooling water service,
where some relaxation of the specified fouling
values may be considered for each separate case.
‫اﮔﺮﭼﻪ ﺑﺮﺧﻲ ﻣﻮاد ﺳﺎﺧﺖ ﺗﺄﺛﻴﺮ ﺳﻮدﻣﻨﺪي در رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬
‫ اﺳﺘﺜﻨﺎء‬.‫ ﻋﻤﻮﻣﺎً اﻃﻼﻋﺎت ﻛﻤﻲ در دﺳﺖ ﻣﻲﺑﺎﺷﺪ‬،‫دارﻧﺪ‬
‫اﺳﺘﻔﺎده از ﺗﻴﺘﺎﻧﻴﻮم در ﻛﺎرﺑﺮي آب ﺧﻨﻚ ﻛﻨﻨﺪه ﻣﻲﺑﺎﺷﺪ ﺟﺎﻳﻲ‬
‫ﻛﻪ ﺑﺮﺧﻲ ﻣﻼﻳﻢﺳﺎزيﻫﺎ در ﻣﻘﺎدﻳﺮ رﺳﻮب ﻣﺸﺨﺺ ﺷﺪه ﺑﺮاي‬
.‫ﻫﺮ ﺣﺎﻟﺖ ﺑﻪ ﻃﻮر ﻣﺠﺰا ﻣﻤﻜﻦ اﺳﺖ در ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮﻧﺪ‬
8.2.4 The best design fouling resistances, chosen
with all physical and economic factors properly
evaluated, will result in a minimum cost based on
fixed charges of the initial investment (which
increase with added fouling resistance) and on
cleaning and down-time expenses (which
decrease with added fouling resistance). By the
very nature of the factors involved, the
manufacturer is seldom in a position to determine
optimum fouling resistances. The user, therefore,
on the basis of past experience and current or
projected costs, should specify the design fouling
resistances for his particular services and
operating conditions. In the absence of specific
data for setting proper resistances as described in
the previous paragraphs, the user may be guided
by the values tabulated in the section of TEMA
standards. In the case of inside surface fouling,
these values must be multiplied by the
outside/inside surface ratio.
‫ ﺑﺎ‬،‫ ﺑﻬﺘﺮﻳﻦ ﻃﺮاﺣﻲ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ‬4-2-8
‫ﻓﺎﻛﺘﻮرﻫﺎي ﻓﻴﺰﻳﻜﻲ و اﻗﺘﺼﺎدي ﺑﻪ دﻗﺖ ارزﻳﺎﺑﻲ ﺷﺪه ﻣﻨﺠﺮ ﺑﻪ‬
‫ﺣﺪاﻗﻞ ﻫﺰﻳﻨﻪ ﺑﺮاي ﻇﺮﻓﻴﺖ ﺛﺎﺑﺖ ﺳﺮﻣﺎﻳﻪﮔﺬاري اوﻟﻴﻪ )ﻛﻪ ﺑﺎ‬
‫اﻓﺰاﻳﺶ ﻣﻘﺎوﻣﺖ رﺳﻮب ﮔﺮﻓﺘﮕﻲ اﺿﺎﻓﻪ ﻣﻲﺷﻮد(و ﻫﺰﻳﻨﻪﻫﺎي‬
‫ﺗﻤﻴﺰ ﻛﺮدن و ﺑﺴﺘﻦ )ﻛﻪ ﺑﺎ اﺿﺎﻓﻪ ﺷﺪن ﻣﻘﺎوﻣﺖ رﺳﻮب دﻫﻲ‬
‫ ﺳﺎزﻧﺪه ﺑﻪ‬، ‫ﻛﻢ ﻣﻲ ﺷﻮد( ﺑﻪ ﺧﺎﻃﺮ ﻓﺎﻛﺘﻮرﻫﺎي ﺧﻴﻠﻲ ذاﺗﻲ‬
‫ﻧﺪرت در ﻣﻮﻗﻌﻴﺘﻲ اﺳﺖ ﻛﻪ ﻣﻘﺎوﻣﺖ رﺳﻮﺑﻲ ﺑﻬﻴﻨﻪ را ﻣﺸﺨﺺ‬
‫ ﺑﻪ ﻛﺎرﺑﺮ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺑﺮ ﭘﺎﻳﻪ ﺗﺠﺮﺑﻴﺎت ﮔﺬﺷﺘﻪ و‬.‫ﻛﻨﺪ‬
‫ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮﺑﻲ ﻃﺮاﺣﻲ را ﺑﺮاي‬،‫ﻫﺰﻳﻨﻪﻫﺎي وﻳﮋه ﻓﻌﻠﻲ‬
‫ در ﻏﻴﺎب‬.‫ﻛﺎرﺑﺮي ﻣﺨﺼﻮص و ﺷﺮاﻳﻂ ﻋﻤﻠﻴﺎﺗﻲ ﻣﺸﺨﺺ ﻛﻨﺪ‬
‫اﻃﻼﻋﺎت ﻣﺸﺨﺺ ﺑﺮاي ﺗﻌﻴﻴﻦ ﻣﻘﺎوﻣﺖ ﺻﺤﻴﺢ ﻣﻄﺎﺑﻖ آورده‬
‫ ﻛﺎرﺑﺮ ﺑﺎﻳﺪ ﺗﻮﺳﻂ ﻣﻘﺎدﻳﺮ ﻣﺸﺨﺺ ﺷﺪه‬،‫ﺷﺪه در ﭘﺎراﮔﺮاف ﻗﺒﻠﻲ‬
‫ در ﺣﺎﻟﺖ رﺳﻮب‬.‫ راﻫﻨﻤﺎﻳـــﻲ ﺷﻮد‬TEMA ‫در اﺳﺘﺎﻧﺪارد‬
‫درون‬/‫ اﻳﻦ ﻣﻘﺎدﻳﺮ ﺑﺎﻳﺪ در ﻧﺴﺒﺖ ﺳﻄﺢ ﺑﻴﺮون‬،‫ﺳﻄﺢ داﺧﻠﻲ‬
.‫ﺿﺮب ﺷﻮد‬
( m².°C/W) ‫ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮﺑﻲ ﻃﺮاﺣﻲ‬1-4-2-8
8.2.4.1 Design fouling resistances (m².°C/W)
The user should attempt to select an optimal
fouling resistance that will result in a minimum
sum of fixed shut-down and cleaning costs. The
following tabulated values of fouling resistances
allow for oversizing the heat exchanger so that it
will meet performance requirements with
reasonable intervals between shut-downs and
cleaning. These values do not recognize the time
related behavior of fouling with regard to specific
design and operational characteristics of
particular heat exchangers.
‫ﻛﺎرﺑﺮ ﺑﺎﻳﺪ ﺗﻼش ﻛﻨﺪ ﺗﺎ ﻣﻘﺎوﻣﺖ رﺳﻮﺑﻲ ﺑﻬﻴﻨﻪاي را اﻧﺘﺨﺎب‬
‫ﻛﻨﺪ ﻛﻪ ﻣﻨﺠﺮ ﺑﻪ ﺣﺪاﻗﻞ ﻣﺠﻤﻮع ﻫﺰﻳﻨﻪ ﺛﺎﺑﺖ ﺑﺴﺘﻦ و‬
‫ ﻣﻘﺎدﻳﺮ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮﺑﻲ زﻳﺮ اﺟﺎزه ﻃﺮاﺣﻲ‬.‫ﺗﻤﻴﺰﻛﺎري ﺷﻮد‬
‫ﺑﺰرﮔﺘﺮ از اﻧﺪازه ﻣﺒﺪل ﺣﺮارﺗﻲ را ﻣﻲ دﻫﺪ ﺗﺎ ﺑﺘﻮاﻧﺪ ﻛﺎرآﻳﻲ‬
‫ اﻳﻦ‬.‫ﻣﻮرد ﻧﻴﺎز را ﺑﺎ دورهﻫﺎي ﻣﻨﻄﻘﻲ ﺑﺴﺘﻦ و ﺗﻤﻴﺰﻛﺎري ﺑﺪﻫﺪ‬
‫ﻣﻘﺎدﻳﺮ رﻓﺘﺎر ﺗﺒﻌﻴﺖ زﻣﺎﻧﻲ رﺳﻮبدﻫﻲ را در رﻋﺎﻳﺖ ﻃﺮاﺣﻲ‬
‫ﻣﺸﺨﺺ و ﺧﺼﻮﺻﻴﺎت ﻋﻤﻠﻴﺎﺗﻲ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ را ﻣﺸﺨﺺ‬
.‫ﻧﻤﻲ ﻛﻨﻨﺪ‬
8.2.4.2 The normal fouling factors for a variety of
process services are recommended by TEMA.
The tabulated fouling factors are intended to
‫ﺿﺮاﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﻋﺎدي ﺑﺮاي اﻧﻮاع‬
2-4-2-8
.‫ ﭘﻴﺸﻨﻬﺎد ﺷﺪهاﻧﺪ‬TEMA ‫ﻛﺎرﺑﺮيﻫﺎي ﻓﺮآﻳﻨﺪي ﺗﻮﺳﻂ‬
35
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
prevent the exchanger from delivering less than
the required process heat load for a period of
about a year to a year and a half. That table is
only a guide, however, and if specific data is
available which can be used to determine a more
accurate fouling factor for a particular service,
that data should be used in preference to Table
C.1 of Appendix C.
‫ﻓﺎﻛﺘﻮرﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺑﻴﺎن ﺷﺪه از ﺗﻤﺎﻳﻞ ﻣﺒﺪل ﺑﻪ اﻧﺘﻘﺎل‬
‫ﻛﻤﺘﺮ ﮔﺮﻣﺎي ﻓﺮآﻳﻨﺪي ﻻزم ﺑﺮاي ﻣﺪت ﻳﻚ ﺳﺎل ﺗﺎ ﻳﻚ ﺳﺎل ﻳﺎ‬
‫ ﺟﺪول ﻓﻘﻂ ﻳﻚ راﻫﻨﻤﺎﺳﺖ ﺑﺎ اﻳﻦ‬.‫ﻧﻴﻢ ﺟﻠﻮﮔﻴﺮي ﻣﻲ ﻧﻤﺎﻳﺪ‬
‫وﺟﻮد اﮔﺮ اﻃﻼﻋﺎت ﺧﺎﺻﻲ ﻣﻮﺟﻮد ﺑﺎﺷﺪ ﻛﻪ ﻓﺎﻛﺘﻮر رﺳﻮب‬
‫ آن اﻃﻼﻋﺎت‬،‫دﻗﻴﻘﺘﺮي را ﺑﺮاي ﻛﺎرﺑﺮي ﺧﺎﺻﻲ ﻣﻲ دﻫﺪ‬
(‫ از ﭘﻴﻮﺳﺖ )ج‬1-‫رﺟﺤﺎن داﺷﺘﻪ و در ﻣﻘﺎﻳﺴﻪ ﺑﺎ ﺟﺪول ج‬
.‫ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﻣﻮرد اﺳﺘﻔﺎده ﻗﺮار ﮔﻴﺮد‬
8.2.4.3 The actual importance of the fouling
factors depends on the value of the clean
coefficient Uc, that is the better the coefficient,
the more important is the fouling factor.
‫ اﻫﻤﻴﺖ واﻗﻌﻲ ﻓﺎﻛﺘﻮرﻫﺎي رﺳﻮب ﺑﻪ ﻣﻘﺪار ﺿﺮﻳﺐ‬3-4-2-8
‫ ﻳﻌﻨﻲ ﻫﺮﭼﻪ ﺿﺮﻳﺐ ﺗﻤﻴﺰي ﺑﻬﺘﺮ ﺑﺎﺷﺪ‬،‫ ﺑﺴﺘﮕﻲ دارد‬Uc ‫ﺗﻤﻴﺰي‬
.‫اﻫﻤﻴﺖ ﺿﺮﻳﺐ رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺑﻴﺸﺘﺮ ﺧﻮاﻫﺪ ﺑﻮد‬
‫ ﺗﻌﻴﻴﻦ اﺛﺮ دوﺑﺮاﺑﺮ ﺷﺪن‬،Uc ‫ ﭘﺲ از ﻣﺤﺎﺳﺒﻪ اوﻟﻴﻪ‬4-4-2-8
8.2.4.4 After making a preliminary calculation of
Uc, it is easy to determine the effect of doubling
(or halving) the assumed fouling factors on the
size of the exchanger. If this effect is small (5%
or less), it is not worthwhile trying to determine a
more accurate fouling factor. There are many
occasions, however, when Uc is so large that the
size of the exchanger depends almost entirely on
the value of the fouling factor. For these cases, all
available plant data should be closely examined.
‫)ﻳﺎ ﻧﺼﻒ ﺷﺪن( ﻋﺎﻣﻞ ﻫﺎي رﺳﻮب ﻓﺮض ﺷﺪه روي اﻧﺪازه‬
(‫ درﺻﺪ ﻳﺎ ﻛﻤﺘﺮ‬5) ‫ اﮔﺮ اﻳﻦ اﺛﺮ ﻛﻮﭼﻚ‬.‫ﻣﺒﺪل آﺳﺎن ﺧﻮاﻫﺪ ﺑﻮد‬
‫ ارزش ﻧﺨﻮاﻫﺪ‬،‫ ﺗﻼش ﺑﺮاي ﺗﻌﻴﻴﻦ ﻓﺎﻛﺘﻮر رﺳﻮب دﻗﻴﻖﺗﺮ‬،‫ﺑﺎﺷﺪ‬
‫ آﻧﻘﺪر‬UC ‫ اﮔﺮ ﭼﻪ ﺣﺎﻟﺘﻬﺎي زﻳﺎدي وﺟﻮد دارد ﻛﻪ‬.‫داﺷﺖ‬
‫ﺑﺰرگ اﺳﺖ ﻛﻪ اﻧﺪازه ﻣﺒﺪل ﺗﻘﺮﻳﺒﺎ ﺑﻪ ﻃﻮر ﻛﺎﻣﻞ ﺑﻪ ﻣﻘﺪار ﻋﺎﻣﻞ‬
‫ ﺑﺮاي اﻳﻦ ﺣﺎﻟﺖ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺗﻤﺎم‬.‫رﺳﻮب ﺑﺴﺘﮕﻲ دارد‬
.‫اﻃﻼﻋﺎت ﻗﺎﺑﻞ دﺳﺘﺮس واﺣﺪ دﻗﻴﻘﺎً آزﻣﺎﻳﺶ ﺷﻮﻧﺪ‬
‫ ﻃﺮاﺣﻲ ﺣﺮارﺗﻲ‬-9
9. THERMAL DESIGN
‫ اﻓﺖ ﻓﺸﺎر‬1-9
9.1 Pressure Drop
Maximum acceptable pressure drops indicated in
the process data sheet shall be understood for
fouled exchangers and as inclusive of the pressure
drops through inlet and outlet nozzles. In cases of
alternate conditions these shall apply to the worst
operating condition.
‫ﺣﺪاﻛﺜﺮ اﻓﺖ ﻓﺸﺎرﻫﺎي ﻗﺎﺑﻞ ﻗﺒﻮل ﻣﺸﺨﺺ ﺷﺪه در داده‬
‫ﺑﺮﮔﻪﻫﺎي ﻓﺮآﻳﻨﺪي ﺑﺎﻳﺪ ﺑﺮاي ﻣﺒﺪلﻫﺎي رﺳﻮب ﮔﺮﻓﺘﻪ درج‬
‫ﺷﻮﻧﺪ و ﺷﺎﻣﻞ اﻓﺖ ﻓﺸﺎرﻫﺎي در ﻧﺎزلﻫﺎي ورودي و ﺧﺮوﺟﻲ‬
‫ در ﺣﺎﻟﺖ ﺷﺮاﻳﻂ ﻣﺘﻔﺎوت اﻳﻨﻬﺎ ﺑﺎﻳﺪ ﺑﻪ ﺑﺪﺗﺮﻳﻦ ﺷﺮاﻳﻂ‬.‫ﺷﻮﻧﺪ‬
.‫ﻋﻤﻠﻴﺎﺗﻲ اﻋﻤﺎل ﺷﻮﻧﺪ‬
‫ ﺳﺮﻋﺖﻫﺎي ﻃﺮاﺣﻲ‬2-9
9.2 Design Velocities
Design velocities in tubes for cooling water shall
be kept within the under mentioned operating
range (see Table 1).
9.3 Exchanger
Temperatures
Design
Pressures
‫ﺳﺮﻋﺖﻫﺎي ﻃﺮاﺣﻲ در ﻟﻮﻟﻪﻫﺎ ﺑﺮاي آب ﺧﻨﻚ ﻛﻨﻨﺪه ﺑﺎﻳﺪ زﻳﺮ‬
‫ را‬1 ‫ﻣﺤﺪوده ﻋﻤﻠﻴﺎﺗﻲ اﺷﺎره ﺷﺪه ﻧﮕﻬﺪاﺷﺘﻪ ﺷﻮﻧﺪ )ﺟﺪول‬
.(‫ﺑﺒﻴﻨﻴﺪ‬
‫ دﻣﺎﻫﺎ و ﻓﺸﺎرﻫﺎي ﻃﺮاﺣﻲ ﻣﺒﺪل‬3-9
and
‫ ﻓﺸﺎرﻫﺎي ﻃﺮاﺣﻲ‬1-3-9
9.3.1 Design pressures
9.3.1.1 Design pressures shall be as shown on the
individual process data sheet.
‫ ﻓﺸﺎرﻫﺎي ﻃﺮاﺣﻲ ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ ﺑﺎ داده ﺑﺮﮔﻪ ﻫﺎ‬1-1-3-9
9.3.1.2 Unless otherwise specified, design
pressure for heat exchangers shall be established
according to the following criteria:
‫ ﻓﺸﺎر ﻃﺮاﺣﻲ ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ‬2-1-3-9
.‫ﻓﺮآﻳﻨﺪي ﻣﺮﺑﻮﻃﻪ ﺑﺎﺷﻨﺪ‬
:‫ ﻣﮕﺮ در ﻣﻮاردي ﻛﻪ ﻣﺸﺨﺺ ﺷﻮد‬،‫ﻣﻌﻴﺎرﻫﺎي زﻳﺮ ﺑﺎﺷﺪ‬
36
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
Max. Operating Pressure (MOP)
IPS-E-PR- 771(1)
Design Pressure (DP) (See Notes 6 and 7)
(MOP) ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ‬
- Atmospheric pressure
(‫ را ﺑﺒﻴﻨﻴﺪ‬7 ‫ و‬6‫( ﻳﺎدآوري ﻫﺎي‬DP) ‫ﻓﺸﺎر ﻃﺮاﺣﻲ‬
Hydrostatic (water) pressure + 35 mm WC min.(see Note 4)
(4 ‫ ﻣﻴﻠﻴﻤﺘﺮ ارﺗﻔﺎع آب )ﻳﺎدآوري‬35 ‫ ﺣﺪاﻗﻞ‬+(‫ﻓﺸــﺎر ﻫﻴﺪرواﺳﺘﺎﺗﻴﻚ )آب‬
‫ ﻓﺸﺎر آﺗﻤﺴﻔﺮﻳﻚ‬- Vacuum (see Note 3)
Absolute vacuum and 3.5 bar (ga) min.
(3 ‫ ﺧﻼء )ﻳﺎدآوري‬- Between 0 and 1.5 bar (ga)
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬3/5 ‫ﺧﻼء ﻛﺎﻣﻞ و ﺣﺪاﻗﻞ‬
3.5 bar (ga) min.
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬1/5 ‫ ﺗﺎ‬0 ‫ ﺑﻴﻦ‬- Between 1.5 and 20 bar (ga)
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬3/5 ‫ﺣﺪاﻗﻞ‬
max. oper. pressure + 2 bar min.
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬20 ‫ ﺗﺎ‬1/5 ‫ ﺑﻴﻦ‬- Between 20 bar (ga) and 80 bar (ga)
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬2 ‫ ﺣﺪاﻗﻞ‬+ ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ‬
max. oper. press. + 10% min.
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬80 ‫ ﺗﺎ‬20 ‫ ﺑﻴﻦ‬- Between 80 bar (ga) and 140 bar (ga)
‫ درﺻﺪ‬10 ‫ ﺣﺪاﻗﻞ‬+ ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ‬
max. oper. press. + 8 bar min. (see Note 5)
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬140 ‫ ﺗﺎ‬80 ‫ ﺑﻴﻦ‬- Above 140 bar (ga)
(5 ‫ ﺑﺎر)ﻧﺴﺒﻲ()ﻳﺎدآوري‬8 ‫ ﺣﺪاﻗﻞ‬+ ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ‬
max. oper. press. + 5% min. (see Note 5)
(‫ ﺑﺎر)ﻧﺴﺒﻲ‬140 ‫ ﺑﺎﻻي‬-
(5 ‫ درﺻﺪ )ﻳﺎدآوري‬5 ‫ ﺣﺪاﻗﻞ‬+ ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ‬
:‫ﻳﺎدآوريﻫﺎ‬
Notes:
1) In defining the design temperature due
consideration shall be given to the start-up,
shutdown upset or any other condition that
could result in a temperature lower than the
normal operating. However, for all of the
above conditions, the corresponding pressure
shall be considered too.
‫( در ﺗﻌﺮﻳﻒ دﻣﺎي ﻃﺮاﺣﻲ ﻣﻼﺣﻈﺎت ﻛﺎﻓﻲ ﺑﺎﻳﺪ ﺑﺮاي‬1
2) Design temperatures lower than 85°C are
allowed only for insulated equipment for
which a design temperature of 60°C shall be
selected.
‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﻓﻘﻂ‬85 ‫( دﻣﺎﻫﺎي ﻃﺮاﺣﻲ ﻛﻤﺘﺮ از‬2
‫ﺗﻼﻃﻢ زﻣﺎن راهاﻧﺪازي و ﺗﻮﻗﻒ ﻳﺎ ﻫﺮ وﺿﻌﻴﺖ دﻳﮕﺮ ﻛﻪ‬
‫ در‬،‫ﻣﻨﺠﺮ ﺑﻪ دﻣﺎي ﻛﻤﺘﺮي از دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ ﻋﺎدي ﺷﻮد‬
‫ ﺑﺎ اﻳﻦ وﺟﻮد ﺑﺮاي ﺗﻤﺎم ﺷﺮاﻳﻂ ﺑﺎﻻ ﻓﺸﺎر‬.‫ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮد‬
.‫ﻣﺘﻨﺎﻇﺮ ﺑﺎﻳﺪ در ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮد‬
‫ﺑﺮاي ﺗﺠﻬﻴﺰات ﻋﺎﻳﻖ ﺷﺪه اي ﻣﺠﺎز اﺳﺖ ﻛﻪ ﺑﺮاي آﻧﻬﺎ‬
.‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﺑﺎﻳﺪ اﻧﺘﺨﺎب ﺷﻮد‬60 ‫دﻣﺎي ﻃﺮاﺣﻲ‬
3) Steam drums shall be designed for full
vacuum conditions.
‫( ﻣﺨﺎزن ﺑﺨﺎر ﺑﺎﻳﺪ ﺑﺮاي ﺷﺮاﻳﻂ ﺧﻼء ﻛﺎﻣﻞ ﻃــﺮاﺣــﻲ‬3
- Due consideration shall be taken to establish
external design pressure for vessels subject to
internal pressure but connected to the suction
of compressor or other evacuating equipment.
‫ ﻣﻼﺣﻈﻪ ﻛﺎﻓﻲ ﺑﺎﻳﺪ ﺑﺮاي ﻓﺸﺎر ﻃﺮاﺣﻲ ﺧﺎرﺟﻲ ﺑﺮاي‬‫ﻣﺨﺎزﻧﻲ ﻛﻪ در ﻣﻌﺮض ﻓﺸﺎر داﺧﻠﻲ ﻫﺴﺘﻨﺪ اﻣﺎ ﺑﻪ ﻣﻜﺶ‬
.‫ ﻧﻬﺎده ﺷﻮد‬،‫ﻛﻤﭙﺮﺳﻮر ﻳــﺎ ﺗﺠﻬﻴﺰ ﻣﻜﺶ دﻳﮕﺮ وﺻﻞ اﺳﺖ‬
- Vacuum design conditions shall not be
required as consequence of equipment block
in after steam out operation.
‫ ﺷﺮاﻳﻂ ﻃﺮاﺣﻲ ﺧﻼء ﺑﻪ ﺧﺎﻃﺮ ﻧﺘﻴﺠﻪ ﺑﺴﺘﻪ ﺷﺪن ﺗﺠﻬﻴﺰ‬.‫ﭘﺲ از ﻋﻤﻠﻴﺎت ﺑﺨﺎر زﻧﻲ ﻻزم ﻧﻤﻲﺑﺎﺷﺪ‬
4) Same criteria is applied for the design of
atmospheric storage tanks.
‫( ﻣﻌﻴﺎرﻫﺎي ﻳﻜﺴﺎن ﺑﺮاي ﻃﺮاﺣﻲ ﻣﺨﺎزن اﺗﻤﺴﻔﺮﻳﻚ ﺑـﻪ‬4
5) When design pressure lower than 110%
max. operating is specified, safety valves
blowdown shall be selected accordingly.
‫ درﺻﺪ ﺣﺪاﻛﺜﺮ‬110 ‫( زﻣﺎﻧﻲ ﻛﻪ ﻓﺸﺎر ﻃﺮاﺣﻲ ﻛﻤﺘﺮ از‬5
:‫ﺷﻮﻧﺪ‬
.‫ﻛﺎر ﻣﻲرود‬
‫ ﺗﺨﻠﻴﻪ ﺗﻮﺳﻂ ﺷﻴﺮ اﻃﻤﻴﻨﺎن‬.‫ﻋﻤﻠﻴﺎﺗﻲ ﻣﺸﺨﺺ ﺷﺪه ﺑﺎﺷﺪ‬
.‫ﺑﺎﻳﺪ ﺑﺮ ﻃﺒﻖ آن اﻧﺘﺨﺎب ﺷﻮد‬
37
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫( ﻣﺒﺪلﻫﺎي در ﻣﺪار ﺧﺮوﺟﻲ ﻛﻤﭙﺮﺳﻮرﻫﺎي ﺑﺎ ﻣﺤﺮك‬6
6) Exchangers in gas turbine driven
compressor discharge circuits shall have the
setting of the PSV (Pressure Safety Valve) in
that circuit. In low pressure systems (less than
20-25 bar), the relief valve setting should be
equal to the compressor’s maximum case
working pressure.
‫ )ﺷﻴﺮ اﻳﻤﻨﻲ ﻓﺸﺎر( در ﻣﺪار‬PSV ‫ﺗﻮرﺑﻴﻦ ﮔﺎزي ﺑﺎﻳﺪ ﺗﻨﻈﻴﻢ‬
‫ در ﺳﺎﻣﺎﻧﻪ ﻫﺎي ﻓﺸﺎر ﻛﻢ )ﻛﻤﺘﺮ از‬.‫را داﺷﺘﻪ ﺑﺎﺷﻨﺪ‬
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺗﻨﻈﻴﻢ ﺷﻴﺮ اﻃﻤﻴﻨﺎن ﺑﺮاﺑﺮ‬،(‫ ﺑﺎر‬20-25
.‫ﺑﺎ ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻛﺎري ﭘﻮﺳﺘﻪ ﻛﻤﭙﺮﺳﻮر ﺑﺎﺷﺪ‬
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺗﻨﻈﻴﻢ‬،‫در ﺳﺎﻣﺎﻧﻪ ﻫﺎي ﺑﺎ ﻓﺸﺎر ﺑﺎﻻﺗﺮ‬
.‫ ﺑﺮ ﻣﺒﻨﺎي ﻫﺮ ﺣﺎﻟﺖ اﻧﺘﺨﺎب ﺷﻮد‬،‫ﺷﻴﺮ اﻳﻤﻨﻲ ﻓﺸﺎر‬
In higher pressure systems, the PSV setting
should be considered on a case by case basis.
‫( ﻣﺒﺪلﻫﺎي در ﻛﺎرﺑﺮي ﻣﺒﺮد ﺑﺎﻳﺪ اﻓﺖ ﻓﺸﺎر ﺣﺪاﻗﻞ‬7
7) Exchangers in refrigerant service shall have
a minimum DP based on vapor pressure of
refrigerant maximum temperature.
،‫( ﺑﺮاﺳﺎس ﻓﺸﺎر ﺑﺨﺎر ﻣﺒﺮد در ﺣﺪاﻛﺜﺮ دﻣﺎ‬DP) ‫ﻃﺮاﺣﻲ‬
.‫داﺷﺘﻪ ﺑﺎﺷﻨﺪ‬
8) Indicate maximum sun temperature for
uninsulated exchangers. Insulated case should
be calculated.
‫( ﺑﺮاي ﻣﺒﺪلﻫﺎي ﻋﺎﻳﻖ ﻧﺸﺪه ﺣﺪاﻛﺜﺮ دﻣﺎي آﻓﺘﺎب‬8
.‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺣﺎﻟﺖ ﻋﺎﻳﻖ ﻣﺤﺎﺳﺒﻪ ﺷﻮد‬.‫ﻣﺸﺨﺺ ﺷﻮد‬
9.3.1.3 In case of equipment connected in series,
without block valves in between, the design
pressure for the upstream equipment shall be the
same as the design pressure for the downstream
equipment (equipped with safety valve) increased
by 110% of the pressure drop foreseen between
the two equipment, under safety valve discharge
conditions.
‫ در ﺣﺎﻟﺖ اﺗﺼﺎل ﺳﺮي ﺗﺠﻬﻴﺰات ﺑﺪون ﺷﻴﺮ‬3-1-3-9
‫ ﻓﺸﺎر ﻃﺮاﺣﻲ ﺑﺮاي ﺗﺠﻬﻴﺰ ﺑﺎﻻدﺳﺖ ﺑﺎﻳﺪ‬،‫اﻧﺴﺪاد در ﻣﻴﺎن آﻧﻬﺎ‬
(‫ﺑﺎ ﻓﺸﺎر ﻃﺮاﺣﻲ ﺗﺠﻬﻴﺰ ﭘﺎﻳﻴﻦ دﺳﺖ )ﻣﺠﻬﺰ ﺑﻪ ﺷﻴﺮ اﻃﻤﻴﻨﺎن‬
،‫ درﺻﺪ اﻓﺖ ﻓﺸﺎر ﭘﻴﺶ ﺑﻴﻨﻲ ﺷﺪه ﺑﻴﻦ دو ﺗﺠﻬﻴﺰ‬110 ‫ﺑﻌﻼوه‬
.‫ ﻣﺴﺎوي ﺑﺎﺷﺪ‬،‫در ﺷﺮاﻳﻂ ﺗﺨﻠﻴﻪ ﺷﻴﺮ اﻃﻤﻴﻨﺎن‬
9.3.1.4 Where the actual test pressure of the lowpressure side is less than 150 percent of the
design pressure, this lower pressure should be
used to determine whether overpressure
protection is needed. Pressure relief for tube
rupture is not required where the low-pressure
exchanger side (including upstream and
downstream systems) is designed at or above
two-thirds of high-pressre exchanger side design
pressure.
For new installations, increasing the design
pressure of the low-pressure side may reduce risk.
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد اﻳﻦ‬،‫ درﺻﺪ ﻓﺸﺎر ﻃﺮاﺣﻲ ﺑﺎﺷﺪ‬150 ‫ﻛﻤﺘﺮ از‬
‫ﻓﺸﺎر ﭘﺎﻳﻴﻦ ﺑﺮاي ﺗﻌﻴﻴﻦ ﻧﻴﺎز ﺑﻪ ﻣﺤﺎﻓﻈﺖ از ﻓﺸﺎر اﺿﺎﻓﻲ ﺑﻜﺎر‬
‫ درﺻﻮرﺗﻲ ﻛﻪ ﺳﻤﺖ ﻓﺸﺎر ﭘﺎﻳﻴﻦ ﻣﺒﺪل)ﺷﺎﻣﻞ ﭘﺎﻳﻴﻦ دﺳﺖ‬.‫رود‬
‫ﻳﺎ ﺑﺎﻻﺗﺮ از دوﺳﻮم ﻓﺸﺎر ﻃﺮاﺣﻲ ﺳﻤﺖ ﻓﺸﺎر‬/‫و ﺑﺎﻻدﺳﺖ( در‬
‫ ﺗﺨﻠﻴﻪ ﻓﺸﺎر ﺑﻪ ﺧﺎﻃﺮ ﭘﺎرﮔﻲ ﻟﻮﻟﻪ‬،‫ﺑﺎﻻي ﻣﺒﺪل ﻃﺮاﺣﻲ ﺷﻮد‬
.‫ﻻزم ﻧﻤﻲ ﺑﺎﺷﺪ‬
9.3.1.5 Exchangers operating under a vacuum
shall be designed for full vacuum.
‫ ﻣﺒﺪلﻫﺎﻳﻲ ﻛﻪ ﺗﺤﺖ ﺧﻼء ﻛﺎر ﻣﻲﻛﻨﻨﺪ ﺑﺎﻳﺪ ﺑﺮاي‬5-1-3-9
9.3.1.6 Tube plates may be required to withstand
differential pressure in high pressure exchanger
when specified on the process data sheet.
‫ ﺻﻔﺤﺎت ﻟﻮﻟﻪ ﻣﻤﻜﻦ اﺳﺖ ﺑﺮاي ﺗﺤﻤﻞ اﺧﺘﻼف‬6-1-3-9
،‫ ﺟﺎﻳﻴﻜﻪ ﻓﺸﺎر آزﻣﻮن واﻗﻌﻲ ﺳﻤﺖ ﻓﺸﺎر ﭘﺎﻳﻴﻦ‬4-1-3-9
‫ اﻓﺰاﻳﺶ ﻓﺸﺎر ﻃﺮاﺣﻲ ﺳﻤﺖ ﻓﺸﺎر‬،‫ﺑﺮاي ﺗﺎﺳﻴﺴﺎت ﺟﺪﻳﺪ‬
.‫ ﻣﻤﻜﻦ اﺳﺖ ﺧﻄﺮ را ﻛﺎﻫﺶ دﻫﺪ‬،‫ﭘﺎﻳﻴﻦ‬
.‫ﺧﻼء ﻛﺎﻣﻞ ﻃﺮاﺣﻲ ﺷﻮﻧﺪ‬
‫ زﻣﺎﻧﻲ ﻛﻪ در ﺻﻔﺤﻪ‬.‫ﻓﺸﺎر در ﻣﺒﺪل ﻓﺸﺎر ﺑﺎﻻ اﺣﺘﻴﺎج ﺑﺎﺷﻨﺪ‬
.‫اﻃﻼﻋﺎت ﻓﺮآﻳﻨﺪي ﻣﺸﺨﺺ ﺷﺪه ﺑﺎﺷﺪ‬
‫ دﻣﺎﻫﺎي ﻃﺮاﺣﻲ‬2-3-9
9.3.2 Design Temperatures
9.3.2.1 Design temperature shall be as shown on
the individual process data sheet.
‫ دﻣﺎي ﻃﺮاﺣﻲ ﺑﺎﻳﺪ در ﺻﻔﺤﻪ دادهﻫﺎي ﻓﺮآﻳﻨﺪي‬1-2-3-9
.‫ﻣﺠﺰا ﻧﺸﺎن داده ﺷﻮد‬
38
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
9.3.2.2 Unless otherwise specified, design
temperature for heat exchangers, shall be
established according to the following criteria:
IPS-E-PR- 771(1)
‫ ﻣﮕﺮ در ﻣﻮاردي ﻛﻪ ﻣﺸﺨﺺ ﺷﻮد دﻣﺎي ﻃﺮاﺣﻲ‬2-2-3-9
:‫ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ ﺑﺎ ﺿﻮاﺑﻂ زﻳﺮ ﺑﺎﺷﺪ‬
Operating Temperature (OT)
Design Temperature (DT) (See Note 4)
(OT) ‫دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ‬
(‫ را ﺑﺒﻴﻨﻴﺪ‬4 ‫( )ﻳﺎدآوري‬DT) ‫دﻣﺎي ﻃﺮاﺣﻲ‬
-100 °C ‫ ﻛﻤﺘﺮ از‬-
min. oper. temp./85°C min. (see Note 2)
(‫ را ﺑﺒﻴﻨﻴﺪ‬2 ‫ )ﻳﺎدآوري‬85°C‫ﺣﺪاﻗﻞ‬/‫ﺣﺪاﻗﻞ دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ‬
- Less than -100°C
- Between -40°C and -100°C
-100°C/85°C min. (see Note 2)
-100 °C ‫ و‬-40 °C ‫ ﺑﻴﻦ‬-
(‫ را ﺑﺒﻴﻨﻴﺪ‬2 ‫ )ﻳﺎدآوري‬85°C ‫ﺣﺪاﻗﻞ‬/-100°C -
- Between -30°C and -39°C
-45°C/85°C min. (see Note 2)
-39 °C ‫ و‬-30 °C ‫ ﺑﻴﻦ‬-
(‫ را ﺑﺒﻴﻨﻴﺪ‬2 ‫ )ﻳﺎدآوري‬85°C ‫ﺣﺪاﻗﻞ‬/-45°C -
+60 °C ‫ و‬-29 °C ‫ ﺑﻴﻦ‬-
min. oper. temp. /85°C min. (see Note 2)
(‫ را ﺑﺒﻴﻨﻴﺪ‬2 ‫ )ﻳﺎدآوري‬85°C‫ﺣﺪاﻗﻞ‬/‫ﺣﺪاﻗﻞ دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ‬
- Between -29°C and +60°C
- Between 60°C and 343°C
max. oper. temp. +25°C. (see Note 8)
343 °C ‫ و‬60 °C ‫ ﺑﻴﻦ‬-
(‫ را ﺑﺒﻴﻨﻴﺪ‬8 ‫ )ﻳﺎدآوري‬25°C + ‫ﺣﺪاﻛﺜﺮ دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ‬
- Above 343°C
To be specified according to selected material and
process requirement.
.‫ﺑﺎﻳﺪﻣﻄﺎﺑﻖ ﺑﺎ ﺟﻨﺲ اﻧﺘﺨﺎب ﺷﺪه و اﻟﺰاﻣﺎت ﻓﺮآﻳﻨﺪي ﻣﺸﺨﺺ ﺷﻮد‬
343 °C ‫ ﺑﺎﻻي‬-
Note: For note explanation see Article 9.3.1.2.
‫ را‬2-1-3-9 ‫ ﭘﺎراﮔﺮاف‬،‫ ﺑﺮاي ﺗﻮﺿﻴﺢ ﻳﺎدآوري‬:‫ﻳﺎدآوري‬
.‫ﺑﺒﻴﻨﻴﺪ‬
9.3.2.3 The design temperature is determined for
the maximum temperature coincident with the
design pressure as determined above. Indicate any
higher temperatures as alternate design
conditions.
‫ دﻣﺎي ﻃﺮاﺣﻲ ﺑﺮاي ﺣﺪاﻛﺜﺮ دﻣﺎﻳﻲ ﻛﻪ ﻣﻨﻄﺒﻖ ﺑﺎ‬3-2-3-9
‫ دﻣﺎﻫﺎي‬.‫ ﻣﺸﺨﺺ ﻣﻲﺷﻮد‬،‫ﻓﺸﺎر ﻃﺮاﺣﻲ ﻛﻪ در ﺑﺎﻻ ﺗﻌﻴﻴﻦ ﺷﺪ‬
.‫ﺑﺎﻻﺗﺮ ﺑـﻪ ﻋﻨﻮان ﺟﺎﻳﮕﺰﻳﻦ ﺷﺮاﻳﻂ ﻃﺮاﺣﻲ ﻧﺸﺎن داده ﺷﻮد‬
9.3.2.4 Exchangers which will operate at
temperatures 0°C and below shall be designed for
minimum anticipated operating temperature.
‫ ﻣﺒﺪلﻫﺎﻳﻲ ﻛـﻪ در دﻣﺎﻫﺎي ﺻﻔﺮ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد‬4-2-3-9
‫و ﭘﺎﻳﻴﻦﺗﺮ ﻛﺎر ﻣﻲﻛﻨﻨﺪ ﺑﺎﻳﺪ ﺑﺮاي ﺣﺪاﻗﻞ دﻣﺎي ﻗﺎﺑﻞ اﻧﺘﻈﺎر‬
.‫ﻋﻤﻠﻴﺎﺗﻲ ﻃﺮاﺣﻲ ﺷﻮﻧﺪ‬
9.3.2.5 Maximum water outlet temperatures on
coolers and condensers shall be based on the
water characteristics.
‫ ﺣﺪاﻛﺜﺮ دﻣﺎﻫﺎي ﺧﺮوﺟﻲ آب در ﺧﻨﻚ ﻛﻨﻨﺪهﻫﺎ‬5-2-3-9
.‫و ﭼﮕﺎﻟﻨﺪهﻫﺎ ﺑﺎﻳﺪ ﺑﺮاﺳﺎس ﺧﻮاص آب ﺑﺎﺷﺪ‬
9.3.2.6 When, due to the possible loss of flow of
the cooling medium, the tubes, tube sheets and
floating heads may be subject to the full inlet
temperature, it shall be indicated on the
individual process data sheet and these
components shall be designed for the maximum
anticipated operating temperature of the hotter
medium.
‫ زﻣﺎﻧﻲ ﻛﻪ ﺑﻪ ﺧﺎﻃﺮ ﻗﻄﻊ اﺣﺘﻤﺎﻟﻲ ﺳﻴﺎل ﺧﻨﻚ‬6-2-3-9
‫ ﺻﻔﺤﺎت ﻟﻮﻟﻪ و ﻛﻠﮕﻲﻫﺎي ﺷﻨﺎور ﻣﻤﻜﻦ اﺳﺖ‬،‫ ﻟﻮﻟﻪﻫﺎ‬،‫ﻛﻨﻨﺪه‬
‫ اﻳﻦ ﻣﺴﺌﻠﻪ ﺑﺎﻳﺪ در‬،‫در ﻣﻌﺮض دﻣﺎي ﻛﺎﻣﻞ ورودي ﻗﺮار ﮔﻴﺮﻧﺪ‬
‫داده ﺑﺮگ ﻫﺎ ﻓﺮآﻳﻨﺪي ﻣﺠﺰا ﻣﺸﺨﺺ ﺷﺪه و اﻳﻦ اﺟﺰا ﺑﺎﻳﺪ ﺑﺮاي‬
‫ﺣﺪاﻛﺜﺮ دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ ﻗﺎﺑﻞ ﭘﻴﺶ ﺑﻴﻨﻲ ﺳﻴﺎل ﮔﺮمﺗﺮ ﻃﺮاﺣﻲ‬
.‫ﺷﻮﻧﺪ‬
9.3.2.7 The design temperatures for multiple
exchangers in series shall be selected in
accordance with the maximum temperatures
likely to occur on each exchanger in both clean
and fouled condition. The design temperature
indicated on the process data sheet is the
‫ دﻣﺎﻫﺎي ﻃﺮاﺣﻲ ﺑﺮاي ﻣﺒﺪلﻫﺎي ﭼﻨﺪﺗﺎﻳﻲ ﺳﺮي‬7-2-3-9
‫ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ ﺑﺎ ﺣﺪاﻛﺜﺮ دﻣﺎﻳﻲ ﻛﻪ در ﻫﺮ ﻣﺒﺪل در ﻫﺮ دو ﺷﺮاﻳﻂ‬
‫ دﻣﺎي ﻃﺮاﺣﻲ ﻧﺸﺎن‬.‫ اﻧﺘﺨﺎب ﺷﻮد‬، ‫ﺗﻤﻴﺰ و ﻛﺜﻴﻒ اﺗﻔﺎق ﻣﻲاﻓﺘﺪ‬
‫داده ﺷﺪه در داده ﺑﺮگ ﻓﺮآﻳﻨﺪي دﻣﺎي ﮔﺮﻣﺘﺮﻳﻦ ﻣﺒﺪل‬
39
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
temperature of the hottest exchanger.
.‫ﻣﻲﺑﺎﺷﺪ‬
Intermediate design temperatures shall be
calculated assuming the highest heat transfer
coefficient with fouled surface and the lowest
heat transfer coefficient with fouled surface for
the colder and hotter sections respectively.
‫دﻣﺎﻫﺎي ﻃﺮاﺣﻲ ﻣﻴﺎﻧﻪ ﺑﺎﻳﺪ ﺑﺎ ﻓﺮض ﺑﺎﻻﺗﺮﻳﻦ ﺿﺮﻳﺐ اﻧﺘﻘﺎل‬
‫ﺣﺮارت ﺑﺎ ﺳﻄﺢ رﺳﻮبدار و ﻛﻤﺘﺮﻳﻦ ﺿﺮﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﺑﺎ‬
‫ﺳﻄﺢ رﺳﻮبدار ﺑﺮاي ﺑﺨﺶﻫﺎي ﺳﺮدﺗﺮ و ﮔﺮﻣﺘﺮ ﺑﻪ ﺗﺮﺗﻴﺐ‬
.‫ﺣﺴﺎب ﺷﻮﻧﺪ‬
If irregular heat profiles are indicated on the
process data sheet, design data will be supplied
on which the Vendor shall base all calculations,
which shall be submitted to the Company for
approval.
‫اﮔﺮ ﻧﻤﻮدارﻫﺎي ﮔﺮﻣﺎﻳﻲ ﻧﺎﻣﻨﻈﻢ در ﺻﻔﺤﻪ دادهﻫﺎي ﻓﺮآﻳﻨﺪي‬
‫ دادهﻫﺎي ﻃﺮاﺣﻲ ﺑﺮاﺳﺎس آﻧﭽﻪ ﺳﺎزﻧﺪه‬،‫ﻧﺸﺎن داده ﺷﻮد‬
‫ ﻛﻪ ﺑﺎﻳﺪ ﺑﺮاي‬،‫ ﺗﺄﻣﻴﻦ ﺷﻮد‬،‫ﻣﺤﺎﺳﺒﺎت را ﺑﺮ ﭘﺎﻳﻪ آن اﻧﺠﺎم داده‬
.‫ ﺑﺮاي ﺗﺄﻳﻴﺪ ارﺳﺎل ﺷﻮد‬،‫ﺷﺮﻛﺖ‬
9.3.2.8 For fixed tubesheet exchangers without
expansion joints, the differential between the
average shell metal temperature and the average
metal temperature of any one tube pass shall not
exceed 28°C. When temperature differentials
exceed 28°C an expansion joint shall be
furnished.
‫ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪ ﻟﻮﻟﻪاي ﺛﺎﺑﺖ ﺑﺪون‬
8-2-3-9
‫ اﺧﺘﻼف ﺑﻴﻦ دﻣﺎي ﻣﻴﺎﻧﮕﻴﻦ ﻓﻠﺰ ﭘﻮﺳﺘﻪ و‬،‫اﺗﺼﺎﻻت اﻧﺒﺴﺎﻃﻲ‬
‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﺗﺠﺎوز‬28 ‫دﻣﺎي ﻣﻴﺎﻧﮕﻴﻦ ﻫﺮ راﻫﻪ ﻟﻮﻟﻪ ﻧﺒﺎﻳﺪ‬
‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﺑﻴﺸﺘﺮ‬28 ‫ زﻣﺎﻧﻲ ﻛﻪ اﺧﺘﻼف دﻣﺎﻳﻲ از‬.‫ﻛﻨﺪ‬
.‫ اﺗﺼﺎل اﻧﺒﺴﺎﻃﻲ ﺑﺎﻳﺪ ﺑﻜﺎر رود‬،‫ﺷﻮد‬
For two-pass-shell exchangers the differential
between the inlet and the outlet temperature of
the shell side fluid shall not exceed 194°C.
‫ﺑﺮاي ﻣﺒﺪلﻫﺎي ﺑﺎ دو راﻫﻪ ﭘﻮﺳﺘﻪ اﺧﺘﻼف ﺑﻴﻦ دﻣﺎي ورودي و‬
‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد‬194 ‫ﺧﺮوﺟﻲ ﺳﻴﺎل ﺳﻤﺖ ﭘﻮﺳﺘﻪ ﻧﺒﺎﻳﺪ از‬
.‫ﺑﻴﺸﺘﺮ ﺷﻮد‬
40
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
PART II
II ‫ﺑﺨﺶ‬
PROCESS DESIGN OF PLATE HEAT
EXCHANGERS
‫ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي‬
(‫)ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪاي ﭘﺮهدار‬
(PLATE FIN EXCHANGERS)
‫ ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪاي ﭘﺮهدار‬-10
10. PLATE FIN EXCHANGERS
As the name implies, a plate-fin exchanger
consists of a series of: parallel metal (usually
aluminum) plates between which are sandwiched
corrugated metal (usually aluminum) sheets. The
corrugations act as fins providing extended
surface area for heat transfer, giving the unit
mechanical strength and forming a large number
of parallel flow channels.
‫ﻫﻤﺎﻧﻄﻮر ﻛﻪ از اﺳﻤﺶ ﭘﻴﺪاﺳﺖ ﻳﻚ ﻣﺒﺪل ﺻﻔﺤﻪاي ﭘﺮهدار‬
(‫ﺷﺎﻣﻞ ﻳﻚ ﺳﺮي از ﺻﻔﺤﺎت ﻣﻮازي ﻓﻠﺰي )ﻋﻤﻮﻣﺎً آﻟﻮﻣﻴﻨﻴﻮم‬
‫ﻛـﻪ ﺑﻴﻦ ﺻﻔﺤﺎت ﻣﻮجدار ﻓﻠﺰي )ﻋﻤﻮﻣﺎً آﻟﻮﻣﻴﻨﻴﻮم( ﻓﺸﺮده‬
‫ ﺷﻴﺎرﻫﺎي ﻣﻮاج ﻣﺎﻧﻨﺪ ﭘﺮه ﻧﻘﺶ ﺳﻄﺢ اﺿﺎﻓﻲ را ﺑﺮاي‬.‫ﺷﺪهاﻧﺪ‬
‫اﻧﺘﻘﺎل ﺣﺮارت اﻳﻔﺎ ﻣﻲﻛﻨﻨﺪ و ﺑﻪ واﺣﺪ ﻣﻘﺎوﻣﺖ ﻣﻜﺎﻧﻴﻜﻲ‬
.‫ﻣﻲدﻫﺪ و ﻣﻘﺪار زﻳﺎد ﻛﺎﻧﺎل ﺟﺮﻳﺎﻧﻲ ﻣﻮازي اﻳﺠﺎد ﻣﻲﻛﻨﺪ‬
The sides of each sandwich are sealed with metal
(usually aluminum) bars thereby forming the
overall flow passage and the entire construction is
brazed in a molten salt bath. Metal (usually
aluminum) headers are then welded to the ends of
the core.
ً‫ﻛﻨﺎرهﻫﺎي ﻫﺮ ﻓﺸﺮدﮔﻲ ﺗﻮﺳﻂ ﻣﻴﻠﻪﻫﺎي ﻓﻠﺰي )ﻋﻤﻮﻣﺎ‬
‫آﻟﻮﻣﻴﻨﻴﻮم( آبﺑﻨﺪي ﺷﺪهاﻧﺪ ﻛﻪ ﻣﺴﻴﺮ ﺟﺮﻳﺎن ﻛﻠﻲ را ﺗﺸﻜﻴﻞ‬
.‫ﻣﻲدﻫﻨﺪ و ﻛﻞ ﺳﺎﺧﺘﺎر در ﺣﻤﺎم ﻣﺬاب ﻧﻤﻚ ﺑﺮﻧﺰه ﻣﻲﺷﻮد‬
‫ﻛﻠﮕﻲ ﻓﻠﺰ )ﻋﻤﻮﻣﺎً آﻟﻮﻣﻴﻨﻴﻮم( ﺳﭙﺲ ﺑﻪ اﻧﺘﻬﺎي ﻫﺴﺘﻪ ﺟﻮش‬
.‫داده ﻣﻲﺷﻮد‬
As the subject of the standard implies, standard
gives requirement and recommendations for the
process design of fine plate exchangers.
Mechanical design of fin plate heat exchanges
which are constructed on the base of this
standard, shall be accommodated with
international standard API standard 662, 1st
edition Feb. 2006.
‫ اﺳﺘﺎﻧﺪارد اﻟﺰاﻣﺎت و‬،‫ﺑﻄﻮرﻳﻜﻪ ﻣﻮﺿﻮع اﺳﺘﺎﻧﺪارد اﺷﺎره دارد‬
‫ﺗﻮﺻﻴﻪﻫﺎﻳﻲ ﺑﺮاي ﻃﺮاﺣﻲ ﻓﺮآﻳﻨﺪي ﻣﺒﺪﻟﻬﺎي ﺻﻔﺤﻪاي ﭘﺮه دار‬
‫ ﻃﺮاﺣﻲ ﻣﻜﺎﻧﻴﻜﻲ ﻣﺒﺪﻟﻬﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي‬.‫اراﺋﻪ ﻣﻲ دﻫﺪ‬
‫ ﺑﺎﻳﺪ ﺑﺎ‬،‫ ﻛﻪ ﺑﺮ اﺳﺎس اﻳﻦ اﺳﺘﺎﻧﺪارد ﺳﺎﺧﺘﻪ ﻣﻲ ﺷﻮد‬،‫ﭘﺮه دار‬
‫ ﺗﻄﺒﻴﻖ داده‬2006 ‫ ﻓﻮرﻳﻪ‬1 ‫ وﻳﺮاﻳﺶ‬API 662 ‫اﺳﺘﺎﻧﺪارد‬
.‫ﺷﻮد‬
‫ ﻛﺎرﺑﺮد‬-11
11. APPLICATION
‫ ﻓﺮآﻳﻨﺪﻫﺎي ﭘﺘﺮوﺷﻴﻤﻲ ﻧﻤﻮﻧﻪ ﻛﻪ از ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪاي‬1-11
11.1 Typical petrochemical processes utilizing
plate-fin exchangers are:
:‫ﭘﺮهدار اﺳﺘﻔﺎده ﻣﻲﻛﻨﻨﺪ ﻋﺒﺎرﺗﻨﺪ از‬
- Air separation;
،‫ ﺟﺪاﺳﺎزي ﻫﻮا‬-
- Helium extraction from natural gas;
‫ اﺳﺘﺨﺮاج ﻫِﻠﻴﻮم از ﮔﺎز ﻃﺒﻴﻌﻲ؛‬-
- Ethylene recovery;
‫ ﺑﺎزﻳﺎﻓﺖ اﺗﻴﻠﻦ؛‬-
- Natural gas liquefaction;
‫ ﻣﻴﻌﺎن ﮔﺎز ﻃﺒﻴﻌﻲ‬-
- Hydrogen purification and liquefaction; and,
‫ ﺧﺎﻟﺺ ﺳﺎزي و ﻣﺎﻳﻊ ﺳﺎزي ﻫﻴﺪروژن و‬-
- Refrigeration systems used in conjunction
with any of these processes.
‫ ﺳﺎﻣﺎﻧﻪﻫﺎي ﺗﺒﺮﻳﺪ ﻣﻮرد اﺳﺘﻔﺎده ﻣﺮﺗﺒﻂ ﺑﺎ اﻳﻦ‬.‫ﻓﺮآﻳﻨﺪﻫﺎ‬
11.2 Suitable for fouling services and where a
high degree of sanitation is required, as in food,
dairy, brewing industries and pharmaceutical
‫ ﺑﺮاي ﻛﺎرﺑﺮيﻫﺎي رﺳﻮﺑﻲ و ﺟﺎﻳﻲ ﻛﻪ درﺟﻪ ﺑﺎﻻﻳﻲ از‬2-11
‫ ﺗﺨﻤﻴﺮي و‬،‫ ﻟﺒﻨﻴﺎﺗﻲ‬،‫ﺑﻬﺪاﺷﺖ اﺣﺘﻴﺎج ﺑﺎﺷﺪ ﻣﺜﻞ ﺻﻨﺎﻳﻊ ﻏﺬاﻳﻲ‬
41
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
processing.
IPS-E-PR- 771(1)
.‫ ﻣﻨﺎﺳﺐ اﺳﺖ‬،‫ﻓﺮآﻳﻨﺪﻫﺎي داروﻳﻲ‬
‫ ﻓﺮآورش ﻧﻔﺖﻫﺎي ﺧﺎم‬3-11
11.3 Treating Crudes
‫ )ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي( آن‬PHE ‫ﻫﺰﻳﻨﻪ ﭘﺎﻳﻴﻦ ﺗﻴﺘﺎﻧﻴﻮم در‬
‫ ﻧﻔﺖ‬.‫را ﺑﺮاي اﺳﺘﻔﺎده در ﻓﺮآورش ﻧﻔﺖ ﺧﺎم ﺟﺬاب ﻛﺮده اﺳﺖ‬
‫ آب ﻧﻤﻚ زدا و ﺷﻮر و‬،‫ آب ﺗﻮﻟﻴﺪ ﺷﺪه‬،‫ﺧﺎمﻫﺎي ﺑﺴﻴﺎر ﺧﻮرﻧﺪه‬
‫ﺧﻨﻚﻛﻦﻫﺎي آب درﻳﺎ اﺛﺮ ﻛﻤﻲ روي ﺻﻔﺤﺎت ﺗﻴﺘﺎﻧﻴﻮﻣﻲ‬
The low cost of titanium in the PHE (Plate Heat
Exchanger) has made it a favorite in treating
crudes. Highly corrosive crudes, produced water,
desalter water and brackish and sea water
coolants have little effect on the plates of a
titanium PHE. Fouling factors only 1/10 that of
shell and tube heat exchangers lend extra
reliability in these services.
‫آن در‬
1
‫ ﺿﺮاﻳﺐ رﺳﻮب ﻓﻘﻂ‬.‫ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي دارد‬
10
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ دارد ﻛﻪ اﻃﻤﻴﻨﺎن زﻳﺎدي در‬
.‫اﻳﻦ ﻛﺎرﺑﺮي ﻫﺎ دارﻧﺪ‬
‫ ﺳﻴﺴﺘﻢﻫﺎي ﺟﺬب ﮔﺎز‬4-11
11.4 Gas Absorption Systems
A number of PHEs has been installed in gas
processing absorption systems. PHE amine water
and amine amine interchangers are common.
Common amines such as MEA (mono-Ethanol
Amine) and DEA (di-Ethanol Amine) as well as
proprietary absorbents such as DGA (di-Glycol
Amine), Sulfinol and Selexol are all handled by
PHEs in gas absorption service.
‫ﺗﻌﺪادي از ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي در ﺳﺎﻣﺎﻧﻪ ﻫﺎي ﻓﺮآﻳﻨﺪي‬
‫ ﺗﺒﺎدل ﻛﻨﻨﺪهﻫﺎي ﻣﺒﺪل ﺣﺮارﺗﻲ‬.‫ﺟﺬب ﮔﺎز ﻧﺼﺐ ﺷﺪهاﻧﺪ‬
.‫ﺻﻔﺤﻪاي آﻣﻴﻦ – آب و آﻣﻴﻦ – آﻣﻴﻦ ﻣﻌﻤﻮل ﻫﺴﺘﻨﺪ‬
DEA ‫ )ﻣﻨﻮاﺗﺎﻧﻮل آﻣﻴﻦ( و‬MEA ‫آﻣﻴﻦﻫﺎي ﻣﻌﻤﻮﻟﻲ ﻣﺜﻞ‬
‫ )دي‬DGA ‫)دي – اﺗﺎﻧﻮل آﻣﻴﻦ( ﻣﺜﻞ ﺟﺎذبﻫﺎي ﺧﺎص ﻣﺜﻞ‬
‫ﮔﻼﻳﻜﻮل آﻣﻴﻦ( ﺳﻮﻟﻔﻴﻨﻮل و ﺳﻠﻜﺴﻮل ﻛــﻪ ﺗﻤﺎﻣﺎً ﺗﻮﺳﻂ‬
‫ﻣﺒﺪل ﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي در ﻛﺎرﺑﺮي ﺟﺬب ﮔﺎز ﺑﻪ ﻛﺎر‬
.‫ﻣﻲرود‬
11.5 Some of these call for very long temperature
programs. To cool Selexol from 99 to -12°C, for
example, would have required 13 two-pass shell
and tube units. Instead, two PHEs were installed.
These PHEs had nine passes on each side. Use of
brine as a coolant indicated titanium plates, which
would be impractical in conventional heat
exchangers.
‫ ﺑﺮﺧﻲ از اﻳﻨﻬﺎ ﺑﺮاي ﺑﺮﻧﺎﻣﻪﻫﺎي دﻣﺎﻳﻲ ﻃﻮﻻﻧﻲ ﺑﻪ ﻛﺎر‬5-11
‫ درﺟﻪ‬-12 ‫ ﺑﻪ‬99 ‫ ﺑﺮاي ﺳﺮد ﻛﺮدن ﺳﻠﻜﺴﻮل از‬.‫ﻣﻲروﻧﺪ‬
‫ ﻣﺒﺪل دوﭘﺎس ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ‬13 ‫ ﺑﻪ ﻋﻨﻮان ﻣﺜﺎل ﺑﻪ‬، ‫ﺳﺎﻧﺘﻴﮕﺮاد‬
9 ‫ ﻫﺎ‬PHE ‫ اﻳﻦ‬.‫ ﻧﺼﺐ ﻣﻲﺷﻮﻧﺪ‬PHE ‫ در ﻋﻮض دو‬.‫ﻧﻴﺎز دارد‬
‫ اﺳﺘﻔﺎده از آب ﻧﻤﻚ ﺑﻪ ﻋﻨﻮان ﺧﻨﻚ‬.‫ﭘﺎس در ﻫﺮ ﻃﺮف دارﻧﺪ‬
‫ﻛﻦ ﻧﺸﺎﻧﮕﺮ ﺻﻔﺤﺎت ﺗﻴﺘﺎﻧﻴﻮﻣﻲ اﺳﺖ ﻛﻪ در ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ‬
.‫ﻣﺘﺪاول ﻏﻴﺮﻋﻤﻠﻲ اﺳﺖ‬
‫ ﻓﺮآورش ﮔﺎز اﻧﺘﻬﺎﻳﻲ‬6-11
11.6 Tail Gas Treatment
Sulfidity removal from tail gas is another
increasingly common PHE application. The PHE
easily met the 35 kPa limit on pressure drop
across each side.
‫ﺣﺬف ﺳﻮﻟﻔﻮر از ﮔﺎز اﻧﺘﻬﺎﻳﻲ ﻛﺎرﺑﺮد روز اﻓﺰون ﻣﺘﺪاول دﻳﮕﺮ‬
‫ ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﺑﻪ‬.‫ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﻣﻲﺑﺎﺷﺪ‬
‫ ﻛﻴﻠﻮ ﭘﺎﺳﻜﺎل اﻓﺖ ﻓﺸﺎر در‬35 ‫راﺣﺘﻲ ﻣﻲ ﺗﻮاﻧﺪ در ﻣﺤﺪودﻳﺖ‬
.‫ﻫﺮ ﻃﺮف ﻛﺎر ﻛﻨﺪ‬
‫ آب‬- ‫ ﻛﺎرﺑﺮدﻫﺎي آب‬7-11
11.7 Water-to-Water Applications
In the refinery, water-to-water temperature
control has been the most frequent application of
the PHE. Indirect cooling, often using brackish or
natural salt water once through and discharged, is
common. Tempered water, fresh water,
condensate and process water are cooled. PHEs
also have been used for heating and cooling
‫ آب ﺑﻴﺸﺘﺮﻳﻦ ﻛﺎرﺑﺮد ﻣﻜﺮر‬- ‫ ﻛﻨﺘﺮل دﻣﺎي آب‬،‫در ﭘﺎﻻﻳﺸﮕﺎه‬
‫ ﺳﺮد ﻛﺮدن ﻏﻴﺮﻣﺴﺘﻘﻴﻢ ﻛﻪ‬.‫ﻣﺒﺪل ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﻣﻲﺑﺎﺷﺪ‬
‫اﻏﻠﺐ ﺑﺎ اﺳﺘﻔﺎده ﻳﻜﺒﺎره و ﺗﺨﻠﻴﻪ آب ﻧﻤﻚ ﻃﺒﻴﻌﻲ ﻳﺎ ﺷﻮر‬
‫ ﭼﮕﺎﻟﻴﺪه و آب ﻓﺮآﻳﻨﺪي‬،‫ آب ﺧﺎم‬،‫ آب ﻧﺮم‬.‫ﻣﺘﺪاول اﺳﺖ‬
‫ ﻣﺒﺪل ﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﻫﻤﭽﻨﻴﻦ‬.‫ﺳــﺮد ﻣــﻲﺷﻮﻧﺪ‬
42
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
glycol and glycol water in a number of refineries.
‫ﮔﻼﻳﻜﻮل در ﺗﻌﺪادي‬- ‫ﺑﺮاي ﮔﺮم ﻳﺎ ﺳﺮد ﻛﺮدن ﮔﻼﻳﻜﻮل و آب‬
.‫از ﭘﺎﻻﻳﺸﮕﺎهﻫﺎ اﺳﺘﻔﺎده ﻣﻲﺷﻮﻧﺪ‬
11.8 Most application for plate heat exchangers
are for liquid/liquid duties at operating pressure
below 2,100 kPa (ga) or 21 bar (ga) and
temperatures below 150°C, although some
models can operate at temperature up to 275°C.
‫ ﺑﻴﺸﺘﺮ ﻛﺎرﺑﺮدﻫﺎي ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﺑﺮاي‬8-11
‫ ﻛﻴﻠﻮ ﭘﺎﺳﻜﺎل‬2100 ‫ﻣﺎﻳﻊ در ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ زﻳﺮ‬/‫ﺣﺎﻟﺘﻬﺎي ﻣﺎﻳﻊ‬
‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد‬150 ‫ ﺑﺎر )ﻧﺴﺒﻲ( و دﻣﺎي زﻳﺮ‬21 ‫)ﻧﺴﺒﻲ(ﻳﺎ‬
‫ درﺟﻪ ﺳﺎﻧﺘﻴﮕﺮاد‬275 ‫ﻣﻲﺑﺎﺷﺪ اﮔﺮ ﭼﻪ ﺑﺮﺧﻲ ﻣﺪلﻫﺎ ﺗﺎ دﻣﺎي‬
.‫ﻣﻲﺗﻮاﻧﻨﺪ ﻋﻤﻞ ﻧﻤﺎﻳﻨﺪ‬
‫ ﻣﺤﺪودﻳﺖ ﻓﺸﺎر‬1-8-11
11.8.1 Pressure limitation
Maximum Allowable Working Pressure (MAWP)
may be determined by frame strength, gasket
retainment, or plate deformation resistance. It is
often the frame that limits operating pressure.
،‫( ﺗﻮﺳﻂ ﻣﻘﺎوﻣﺖ ﻗﺎب‬MAWP) ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر ﻛﺎري ﻣﺠﺎز‬
‫ﻻﻳﻲ ﻣﺤﺎﻓﻆ ﻳﺎ ﻣﻘﺎوﻣﺖ ﺗﻐﻴﻴﺮ ﺷﻜﻞ ﺻﻔﺤﻪ ﻣﻲﺗﻮاﻧﻨﺪ ﺗﻌﻴﻴﻦ‬
.‫ اﻏﻠﺐ ﻗﺎب اﺳﺖ ﻛﻪ ﻓﺸﺎر ﻋﻤﻠﻴﺎﺗﻲ را ﻣﺤﺪود ﻣﻲﻛﻨﺪ‬.‫ﺷﻮﻧﺪ‬
‫ﺗﻤﺎم ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﻛــﻪ در ﺻﻨﺎﻳﻊ ﺷﻴﻤﻴﺎﻳﻲ اﺳﺘﻔﺎده‬
6 ‫ ﻛﻴﻠﻮﭘﺎﺳﻜﺎل)ﻧﺴﺒﻲ( ﻳﺎ‬600 ‫ﻣﻲﺷﻮﻧﺪ ﻗﺎدر ﺑﻪ ﻋﻤﻠﻴﺎت در‬
10 ‫ ﻛﻴﻠﻮﭘﺎﺳﻜﺎل)ﻧﺴﺒﻲ( ﻳﺎ‬1000 ‫ ﺑﻴﺸﺘﺮ در‬،(‫ﺑﺎر)ﻧﺴﺒﻲ‬
‫ ﻛﻴﻠﻮﭘﺎﺳﻜﺎل)ﻧﺴﺒﻲ( ﻳﺎ‬1600 ‫ﺑﺎر)ﻧﺴﺒﻲ( و ﺗﻌﺪاد زﻳﺎدي در‬
21 ‫ ﻛﻴﻠﻮﭘﺎﺳﻜﺎل)ﻧﺴﺒﻲ( ﻳﺎ‬2100 ‫ ﺑﺎر)ﻧﺴﺒﻲ( و ﺑﺮﺧﻲ در‬16
.‫ﺑﺎر)ﻧﺴﺒﻲ( ﻣﻲﺑﺎﺷﺪ‬
All Plate Heat Exchanger used in chemical
industries are capable of operating at 600 kPa(g)
or 6 bar(g), most at 1000 kPa(g) or 10 bar(g),
many at 1600 kPa(g) or 16 bar(g) and some at
2100 kPa(g) or 21 bar(g).
‫ ﻣﺤﺪودﻳﺖ دﻣﺎ‬2-8-11
11.8.2 Temperature limitation
Normally it is the gasket that limit the Maximum
Operating Temperature (MOT) for Plate Heat
Exchanger.
‫( ﺑﺮاي ﻣﺒﺪل ﺣﺮارﺗﻲ‬MOT ) ‫ﻋﻤﻮﻣﺎً ﺣﺪاﻛﺜﺮ دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ‬
.‫ ﺗﻮﺳﻂ ﻗﺴﻤﺖ ﻻﻳﻲ ﻣﺤﺪود ﻣﻲﺷﻮد‬،‫ﺻﻔﺤﻪاي‬
In the absence of chemical attack, following may
serve as a rough indication guide:
‫ ﻣﻮارد زﻳﺮ ﺑﻪ ﻋﻨﻮان راﻫﻨﻤﺎﻳﻲ اوﻟﻴﻪ‬،‫در ﻏﻴﺎب ﺣﻤﻠﻪ ﺷﻴﻤﻴﺎﻳﻲ‬
:‫ﺑﻪ ﻛﺎر ﻣﻲروﻧﺪ‬
Max
‫ﺣﺪاﻛﺜﺮ‬
- Natural Rubber, Styrene Resin, Neoprene
‫ ﻧﺌﻮﭘﺮن‬،‫ رزﻳﻦ اﺳﺘﺎﻳﺮن‬،‫– ﻻﺳﺘﻴﻚ ﻃﺒﻴﻌﻲ‬
70°C
(FPM)‫ رزﻳﻦ وﻳﺘﻮن‬،‫– ﻧﻴﺘﺮﻳﻞ‬
190°C
- Nitrile, Viton (FPM) Resin*.
- Cured Butyl.
- Ethylene/Propelene, Silicone.
- Compressed Asbestos Fiber (CAF).
‫– ﺑﻮﺗﻴﻞ ﻋﻤﻞ آﻣﺪه‬
120°C
‫ ﺳﻴﻠﻴﻜﻮن‬،‫ﭘﺮوﭘﻠﻦ‬/‫– اﺳﺘﻴﻠﻦ‬
140°C
‫– ﻓﻴﺒﺮ آزﺑﺴﺖ ﻓﺸﺮده‬
200°C
Operating temperature may also be limited by
plate corrosion effect.
‫دﻣﺎي ﻋﻤﻠﻴﺎﺗﻲ ﻧﻴﺰ ﻣﻤﻜﻦ اﺳﺖ در اﺛﺮ ﺧﻮردﮔﻲ ﺻﻔﺤﻪ ﻣﺤﺪود‬
.‫ﺷﻮد‬
:‫*ﻳﺎدآوري‬
* Note:
Viton is trademark for a series of
fluoroelastomers based on the copolymers of
vinylidene fluoride and hexafluoropropylene,
with the repeating structure Possibly - CF2 - CH2
-‫وﻳﺘﻮن ﻧﺎم ﺗﺠﺎري ﻣﺠﻤﻮﻋﻪاي از ﻓﻠﻮرواﻻﺳﺘﻮﻣﺮﻫﺎ ﺑﺮ ﭘﺎﻳﻪ ﻫﻢ‬
‫ ﺑﺎ ﺳﺎﺧﺘﺎر‬،‫ﭘﻠﻴﻤﺮﻫﺎي وﻳﻨﻴﻠﻴﺪن ﻓﻠﻮرﻳﺪ و ﻫﮕﺰا ﻓﻠﻮروﭘﺮوﭘﻴﻠﻦ‬
.‫ ﻣﻲﺑﺎﺷﺪ‬-CF2-CH2-CF2-CF(CF3)‫ﺗﻜﺮاري اﺣﺘﻤﺎﻟﻲ‬
43
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
- CF2 - CF (CF3) -. It is non-flammable and
resistant to corrosive liquids and chemicals up to
315°C. Useful continuous service at 204 - 232°C.
It is further resistant to ozone, weather, flame,
oils, fuels, lubricants and many solvents. Further
has a good radiation resistance.
IPS-E-PR- 771(1)
‫وﻳﺘﻮن ﻏﻴﺮ ﻗﺎﺑﻞ اﺷﺘﻌﺎل و ﻣﻘﺎوم در ﻣﻘﺎﺑﻞ ﻣﺎﻳﻌﺎت ﺧــﻮرﻧﺪه و‬
‫ ﺑﺮاي ﻛﺎرﺑﺮد‬.‫ درﺟــﻪ ﺳﺎﻧﺘﻴﮕﺮاد ﻣﻲ ﺑــﺎﺷﺪ‬315 ‫ﺷﻴﻤﻴــﺎﻳﻲ ﺗﺎ‬
‫ ﻫﻤﭽﻨﻴﻦ ﻣﻘﺎوم در‬.‫ ﻣﻔﻴﺪ ﻣﻲﺑﺎﺷﺪ‬232 ‫ ﺗﺎ‬204 ‫ﻣﺪاوم در‬
‫ رواﻧﻜﺎرﻫﺎ و‬،‫ ﺳﻮﺧﺖﻫﺎ‬،‫ ﺷﻌﻠﻪ روﻏﻦﻫﺎ‬،‫ آب و ﻫﻮا‬،‫ﻣﻘﺎﺑﻞ ازن‬
‫ ﺑﻌﻼوه ﻣﻘﺎوﻣﺖ ﺧﻮﺑﻲ در ﻣﻘﺎﺑﻞ‬.‫ﺧﻴﻠﻲ از ﺣﻼلﻫﺎ ﻣﻲﺑﺎﺷﺪ‬
.‫ﺗﺸﻌﺸﻊ دارد‬
‫ ﺟﻨﺲ‬-12
12. MATERIAL
12.1 Plates can be pressed in many different
metals, including Aluminum, (usually) Stainless
Steel (304SS, 316SS), Titanium, Hastelloy
Alloys, Nickel, Monel, Incolloy 825, Inconel 600
and 625, Aluminum Brass and Hastelloy B & C.
‫ ﺻﻔﺤﺎت ﻣﻲﺗﻮاﻧﻨﺪ از اﻧﻮاع ﻣﺨﺘﻠﻒ زﻳﺎدي از ﻓﻠﺰات‬1-12
‫ )ﻫﻤﻴﺸﻪ( ﻓﻮﻻد زﻧﮓ ﻧﺰن‬،‫ ﺷﺎﻣﻞ آﻟﻮﻣﻴﻨﻴﻮم‬،‫ﻓﺸﺮده ﺷﻮﻧﺪ‬
، ‫ ﻧﻴﻜﻞ‬، Hastelloy ‫ آﻟﻴﺎژ‬،‫ ﺗﻴﺘﺎﻧﻴﻮم‬،(316SS ‫ و‬304SS)
‫ ﺑﺮﻧﺞ آﻟﻮﻣﻴﻨﻴﻮم و‬625 ‫ و‬600 ‫ اﻳﻨﻜﻮﻧﻞ‬،825 ‫ اﻳﻨﻜﻮﻧﻞ‬،‫ﻣﻮﻧﻞ‬
.Hastelloy B & C
12.2 Gaskets are available in nitrile, Resin Cured
Butyl (RCB), viton (FPM) resin, EPDM, silicon,
and fluorocarbon rubbers and natural rubber,
styrene resin; in addition, certain plates can be
supplied with gaskets of Compressed Asbestos
Fiber (CAF).
‫ رزﻳﻦ ﺑﻮﺗﻴﻞ ﻋﻤﻞ آورده‬،‫ ﻻﻳﻴﻬﺎ ﺑﻪ ﺻﻮرت ﻧﻴﺘﺮﻳﻞ‬2-12
‫ ﺳﻴﻠﻴﻜﻮن و‬،EPDM ،(FPM) ‫ رزﻳﻦ وﻳﺘﻮن‬،(RCB)
‫ ﺑﻪ‬،‫ رزﻳﻦ اﺳﺘﺎﻳﺮن‬،‫ﻻﺳﺘﻴﻚﻫﺎي ﻓﻠﻮروﻛﺮﺑﻦ و ﻻﺳﺘﻴﻚ ﻃﺒﻴﻌﻲ‬
‫ﻋﻼوه ﺑﺮﺧﻲ ﺻﻔﺤﺎت ﺧﺼﻮﺻﻲ ﻣﻲﺗﻮاﻧﻨﺪ از ﻻﻳﻲ ﻓﻴﺒﺮآزﺑﺴﺖ‬
.‫( ﺗﺄﻣﻴﻦ ﺷﻮﻧﺪ‬CAF)‫ﻓﺸﺮده ﺷﺪه‬
‫ ﺳﺎﺧﺖ‬-13
13. CONSTRUCTION
13.1 Unlike shell and tube units which can be
custom built to conform to virtually any capacity
and operating conditions, plates are mass
produced in thicknesses range from 0.6 to 1 mm
by complex and expensive press tools. They are
therefore available only in a limited number of
types and sizes, each of which has its own clearly
defined specification with regard to performance
and operating conditions.
‫ ﺑﺮﺧﻼف واﺣﺪﻫﺎي ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻛﻪ ﻣﺘﺪاول اﺳﺖ‬1-13
،‫ﻣﻄﺎﺑﻖ ﺑﺎ ﻇﺮﻓﻴﺖ واﻗﻌﻲ و ﺷﺮاﻳﻂ ﻋﻤﻠﻴﺎﺗﻲ ﺳﺎﺧﺘﻪ ﺷﻮﻧﺪ‬
‫ ﻣﻴﻠﻴﻤﺘﺮ ﺗﻮﺳﻂ‬1 ‫ ﺗﺎ‬0/6 ‫ﺻﻔﺤﺎت ﺑﻪ ﺻﻮرت اﻧﺒﻮه در ﺿﺨﺎﻣﺖ‬
‫ ﺑﻨﺎﺑﺮاﻳﻦ آﻧﻬﺎ در اﻧﻮاع و‬.‫اﺑﺰارﻫﺎي ﭘﻴﭽﻴﺪه و ﮔﺮان ﺗﻮﻟﻴﺪ ﺷﻮﻧﺪ‬
‫اﻧﺪازهﻫﺎي ﻣﺤﺪود وﺟﻮد دارﻧﺪ ﻛﻪ ﻫﺮﻛﺪام ﺧﻮاص ﻣﺸﺨﺺ‬
.‫ﺗﻌﺮﻳﻒ ﺷﺪه در راﺑﻄﻪ ﺑﺎ ﻛﺎرآﻳﻲ و ﺷﺮاﻳﻂ ﻋﻤﻠﻴﺎﺗﻲ دارﻧﺪ‬
‫ ﻓﻮاﻳﺪ‬-14
14. ADVANTAGES
Some of the advantages inherent in the plate-fin
construction are as follows:
:‫ﺑﺮﺧﻲ از ﻓﻮاﻳﺪ در ﺳﺎﺧﺖ ﺻﻔﺤﺎت ﭘﺮه دار ﻣﻄﺎﺑﻖ زﻳﺮ اﺳﺖ‬
14.1 A very high degree of compactness can be
achieved. Surface area to volume ratios of 1476
m²/m³ are quite common and values up to 2526
m²/m³ have been reported. In comparison,
conventional shell and tube units have ratios of
164 to 246 m²/m³.
‫ ﻧﺴﺒﺖ‬.‫ درﺟﻪ ﺑﺎﻻﻳﻲ از ﻓﺸﺮدﮔﻲ ﻗﺎﺑﻞ دﺳﺖ ﻳﺎﻓﺘﻦ اﺳﺖ‬1-14
14.2 Three or four process streams can be easily
accommodated in a single unit with the plate
spacing and fin construction optimized for each
of the streams. Such multi-stream units are ideal
for operating as reversing units for the removal of
impurities.
‫ ﺑﺎ ﺻﻔﺤﺎت ﺟﺪاﻛﻨﻨﺪه و ﺳﺎﺧﺖ ﭘﺮه ﻛﻪ ﺑﺮاي ﻫﺮﻛﺪام از‬2-14
‫ﻣﺘﺮ ﻣﻜﻌﺐ ﻛﺎﻣﻼ‬/ ‫ ﻣﺘﺮ ﻣﺮﺑﻊ‬1476 ‫ﻫﺎي ﺳﻄﺢ ﺑﻪ ﺣﺠﻢ‬
‫ﻣﺘﺮ ﻣﻜﻌﺐ ﻧﻴﺰ ﮔﺰارش‬/ ‫ ﻣﺘﺮ ﻣﺮﺑﻊ‬2526 ‫ﻣﺘﺪاول و ﻣﻘﺎدﻳﺮ ﺗﺎ‬
‫ در ﻣﻘﺎﻳﺴﻪ واﺣﺪﻫﺎي ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻣﺘﺪاول ﻧﺴﺒﺖ‬.‫ﺷﺪهاﻧﺪ‬
.‫ﻣﺘﺮ ﻣﻜﻌﺐ دارﻧﺪ‬/ ‫ ﻣﺘﺮ ﻣﺮﺑﻊ‬246 ‫ ﺗﺎ‬164
‫ ﺳﻪ ﻳﺎ ﭼﻬﺎر ﺟﺮﻳﺎن ﻓﺮآﻳﻨﺪي ﺑﻪ راﺣﺘﻲ‬،‫ﺟﺮﻳﺎنﻫﺎ ﺑﻬﻴﻨﻪ ﺷﺪهاﻧﺪ‬
‫ ﭼﻨﻴﻦ واﺣﺪﻫﺎي‬.‫در ﻳﻚ واﺣﺪ ﻣﺠﺰا ﻣﻲ ﺗﻮاﻧﻨﺪ ﺟﻤﻊ ﻣﻲﺷﻮﻧﺪ‬
‫ﭼﻨﺪﺟﺮﻳﺎﻧﻪ ﺑﺮاي ﻓﻌﺎﻟﻴﺖ در واﺣﺪﻫﺎي ﺑﺎ ﻋﻤﻠﻴﺎت ﻣﻌﻜﻮس‬
.‫ﺟﻬﺖ ﺣﺬف ﻧﺎﺧﺎﻟﺼﻲﻫﺎ ﻣﻄﻠﻮب ﻣﻲ ﺑﺎﺷﻨﺪ‬
44
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
14.3 Cores can be used individually or connected
in series and/or parallel as manifolded assemblies.
IPS-E-PR- 771(1)
‫ﻳﺎ‬/‫ ﻫﺴﺘﻪﻫﺎ ﺑﻪ ﺗﻨﻬﺎﻳﻲ ﻳﺎ ﺑﻪ ﺻﻮرت اﺗﺼﺎل ﺳﺮي و‬3-14
.‫ﻣﻮازي ﻣﺜﻞ ﻣﻮﻧﺘﺎژ ﭼﻨﺪ راﻫﻪ ﻣﻲﺗﻮاﻧﻨﺪ اﺳﺘﻔﺎده ﺷﻮﻧﺪ‬
14.4 Small size and light mass permit compact
installations with minimum foundations and
supporting structures.
‫ ﻧﺼﺐﻫﺎي ﻓﺸﺮده ﺑﺎ ﺣﺪاﻗﻞ‬،‫ اﻧﺪازه ﻛﻮﭼﻚ و وزن ﻛﻢ‬4-14
.‫ﻓﻮﻧﺪاﺳﻴﻮن و ﺳﺎزه ﻣﺤﺎﻓﻆ را اﺟﺎزه ﻣﻲدﻫﺪ‬
14.5 Pumping costs per unit of heat transfer are
said to be lower than for shell and tube
equipment.
‫ﻣﻲ ﺗﻮان ﮔﻔﺖ ﻛﻪ ﻫﺰﻳﻨﻪ ﻫﺎي ﺗﻠﻤﺒﻪ ﻛﺮدن ﺑﻪ ازاء‬
14.6 Plate heat exchangers achieve high heat
transfer rates that greatly reduce the surface area
required. Since these low surface areas are on thin
plates, plate heat exchangers need much less
material than comparable conventional units.
‫ ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﺷﺪت اﻧﺘﻘﺎل ﺣﺮارت‬6-14
5-14
.‫واﺣﺪ اﻧﺘﻘﺎل ﺣﺮارت ﺑﺮاي ﺗﺠﻬﻴﺰات ﭘﻮﺳﺘﻪ و ﻟﻮﻟﻪ ﻛﻤﺘﺮ اﺳﺖ‬
‫زﻳﺎدي دارﻧﺪ ﻛﻪ ﺑﻪ ﻣﻘﺪار زﻳﺎدي ﺳﻄﺢ ﺗﻤﺎس ﻻزم را ﻛﻢ‬
،‫ ﭼﻮن اﻳﻦ ﺳﻄﻮح روي ﺻﻔﺤﺎت ﻧﺎزك ﻣﻲ ﺑﺎﺷﻨﺪ‬.‫ﻣﻲﻛﻨﺪ‬
‫ ﻣﻮاد ﻛﻤﺘﺮي ﻧﺴﺒﺖ ﺑﻪ واﺣﺪﻫﺎي‬،‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي‬
.‫ﻣﺘﺪاول ﻗﺎﺑﻞ ﻣﻘﺎﻳﺴﻪ ﻧﻴﺎز دارﻧﺪ‬
The plate heat exchangers take less space in the
refinery and cost less even when expensive
materials are used. Noncorrosive titanium has
become a standard for plate heat exchangers in oil
and gas processing.
‫ﻣﺒﺪلﻫﺎي ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي ﻓﻀﺎي ﻛﻤﺘﺮي را در ﭘﺎﻻﻳﺸﮕﺎه‬
‫ﻣﻲﮔﻴﺮﻧﺪ ﺣﺘﻲ زﻣﺎﻧﻲ ﻛﻪ از ﻣﻮاد ﮔﺮانﺗﺮ اﺳﺘﻔﺎده ﺷﻮد ﻫﺰﻳﻨﻪ‬
‫ ﺗﻴﺘﺎﻧﻴﻮم ﻏﻴﺮﻗﺎﺑﻞ ﺧﻮرﻧﺪﮔﻲ ﺑﺮاي ﻣﺒﺪلﻫﺎي‬.‫ﭘﺎﻳﻴﻦﺗﺮي دارﻧﺪ‬
.‫ﺣﺮارﺗﻲ ﺻﻔﺤﻪاي در ﻓﺮآﻳﻨﺪ ﻧﻔﺖ و ﮔﺎز اﺳﺘﺎﻧﺪارد ﺷﺪه اﺳﺖ‬
‫ ﻣﻌﺎﻳﺐ‬-15
15. DISADVANTAGES
Against these advantages several disadvantages
and limitations must be kept in mind.
‫ ﭼﻨﺪﻳﻦ ﻣﺤﺪودﻳﺖ و ﻣﻌﺎﻳﺐ زﻳﺮ را ﺑﺎﻳﺪ‬،‫در ﻣﻘﺎﺑﻞ اﻳﻦ اﻣﺘﻴﺎزات‬
.‫در ﻧﻈﺮ داﺷﺖ‬
15.1 Maximum operating pressures are limited to
4500 kPa (ga) or 45 bar (ga) under steady
conditions and up to 2100 kPa (ga) or 21 bar (ga)
under reversing conditions.
‫ ﻛﻴﻠﻮﭘﺎﺳﻜﺎل‬4500 ‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎرﻫﺎي ﻋﻤﻠﻴﺎﺗﻲ ﺗﺎ‬
1-15
2100 ‫ ﺑﺎر )ﻧﺴﺒﻲ( در ﺷﺮاﻳﻂ ﭘـﺎﻳـﺎ و ﺗـﺎ‬45 ‫)ﻧﺴﺒﻲ( ﻳﺎ‬
‫ ﺑﺎر )ﻧﺴﺒﻲ( در ﺷﺮاﻳﻂ ﻣﻌﻜﻮس ﻣﺤﺪود‬21 ‫ﻛﻴﻠﻮﭘﺎﺳﻜﺎل ﻳـﺎ‬
.‫ﺷﺪه اﺳﺖ‬
15.2 Plate-fin exchangers cannot be used where
one or more of the process streams have a
tendency to foul.
‫ ﺟﺎﻳﻲ ﻛﻪ ﻳﻚ ﻳﺎ ﭼﻨﺪ ﺗﺎ از‬،‫ ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪاي ﭘﺮهدار‬2-15
‫ ﻧﻤﻲﺗﻮاﻧﻨﺪ اﺳﺘﻔﺎده‬،‫ﺟﺮﻳﺎﻧﻬﺎي ﻓﺮآﻳﻨﺪي ﺗﻤﺎﻳﻞ ﺑﻪ رﺳﻮب دارﻧﺪ‬
.‫ﺷﻮﻧﺪ‬
15.3 Internal leaks between passes are difficult to
locate and correct in the field. Equipment for
different alloy welding is necessary, and highly
skilled personnel are required.
‫ ﭘﻴﺪا ﻛﺮدن ﻧﺸﺘﻲ و اﺻﻼح آن در داﺧﻞ ﺑﻴﻦ راﻫﻪﻫﺎ در‬3-15
16. DESIGN CONSIDERATIONS (PLATE
FIN EXCHANGERS)
(‫ ﻣﻼﺣﻈﺎت ﻃﺮاﺣﻲ )ﻣﺒﺪﻟﻬﺎي ﺻﻔﺤﻪاي ﭘﺮهدار‬-16
‫ ﺗﺠﻬﻴﺰاﺗﻲ ﺑﺮاي ﺟﻮﺷﻜﺎري آﻟﻴﺎژﻫﺎي‬.‫ﻣﺤﻞ ﻣﺸﻜﻞ اﺳﺖ‬
.‫ﻣﺘﻔﺎوت و ﭘﺮﺳﻨﻞ ﻣﺎﻫﺮ اﺣﺘﻴﺎج اﺳﺖ‬
‫ آراﻳﺶ ﻫﻨﺪﺳﻲ ﻣﺒﺪل‬1-16
16.1 Exchanger Geometry
The core of a plate-fin exchanger is built up of a
number of elemental sandwiches of the type
shown in Fig. 4. Several types of flow patterns
are possible and with any of these patterns the
size and type of corrugation may be varied for
each stream.
‫ﻫﺴﺘﻪ ﻣﺒﺪل ﺻﻔﺤﻪاي ﭘﺮهدار از ﺗﻌﺪادي از اﺟﺰاء ﺳﺎﻧﺪوﻳﭽﻲ از‬
‫ ﭼﻨﺪﻳﻦ‬.‫ ﺳﺎﺧﺘﻪ ﺷﺪه اﺳﺖ‬4 ‫اﻧﻮاع ﻧﺸﺎن داده ﺷﺪه در ﺷﻜﻞ‬
‫ اﻧﺪازه و‬،‫ﻧﻮع از اﻟﮕﻮﻫﺎي ﺟﺮﻳﺎﻧﻲ ﻣﻤﻜﻦ ﺑﻮده ﻛﻪ ﺑﺎ ﻫﺮ آراﻳﺶ‬
‫ ﻣﻤﻜﻦ اﺳﺖ ﻣﺘﻔﺎوت‬،‫ﻧﻮع ﺻﻔﺤﺎت ﻣﻮج دار ﺑﺮاي ﻫﺮ ﺟﺮﻳﺎن‬
.‫ﺑﺎﺷﺪ‬
45
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
‫ اﻟﮕﻮﻫﺎي ﺟﺮﻳﺎن‬1-1-16
16.1.1 Flow patterns
Plate fin exchangers have two basic flow patterns,
crossflow and counterflow which are illustrated
in Fig. 4. These basic patterns are then built up to
form simple crossflow, multi-pass crossflow,
counterflow and multi-stream units by using
suitable internal seals, distributors and external
header tanks. Some typical arrangements are
illustrated in Fig. 5.
،‫ﻣﺒﺪلﻫﺎي ﺻﻔﺤﻪاي ﭘﺮهدار دو اﻟﮕﻮي ﺟﺮﻳﺎﻧﻲ ﭘﺎﻳﻪ دارﻧﺪ‬
‫ ﺗﺸﺮﻳﺢ‬4 ‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ و ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻛﻪ در ﺷﻜﻞ‬
‫ ﺟﺮﻳﺎن‬،‫ اﻳﻦ آراﻳﺶﻫﺎي ﭘﺎﻳﻪ از ﺟﺮﻳﺎن ﺳﺎده ﻣﺘﻘﺎﻃﻊ‬.‫ﺷﺪهاﻧﺪ‬
‫ ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ و واﺣﺪﻫﺎي ﭼﻨﺪ ﺟﺮﻳﺎﻧﻪ‬، ‫ﭼﻨﺪ راﻫﻪ ﻣﺘﻘﺎﻃﻊ‬
‫ ﺗﻮزﻳﻊ ﻛﻨﻨﺪهﻫﺎ و‬.‫ﺑﺎ اﺳﺘﻔﺎده از آب ﺑﻨﺪﻫﺎي داﺧﻠﻲ ﻣﻨﺎﺳﺐ‬
‫ ﺑﺮﺧﻲ از آراﻳﺶ ﻫﺎي‬.‫ﺳﺮﺷﺎﺧﻪ ﺑﻴﺮوﻧﻲ ﻣﺨﺎزن ﺗﺸﻜﻴﻞ ﺷﺪهاﻧﺪ‬
.‫ ﺗﺸﺮﻳﺢ ﺷﺪهاﻧﺪ‬5 ‫ﻧﻤﻮﻧﻪ در ﺷﻜﻞ‬
Selection of the proper flow pattern for a
particular application depends on several factors
including flow rates, pressure levels and the
temperature effectiveness of each stream.
Temperature effectiveness determines the LMTD
correction factor and therefore the size penalty
associated with flow patterns other than
counterflow.
‫اﻧﺘﺨﺎب و اﻟﮕﻮي ﺟﺮﻳﺎن ﻣﻨﺎﺳﺐ ﺑﺮاي ﻛﺎرﺑﺮد ﻣﺨﺼﻮص ﺑﻪ ﭼﻨﺪ‬
‫ ﺳﻄﺢ ﻓﺸﺎر و ﺗﺄﺛﻴﺮ دﻣﺎي ﻫﺮ ﺟﺮﻳﺎن‬،‫ﻋﺎﻣﻞ ﺷﺎﻣﻞ دﺑﻲ ﺟﺮﻳﺎن‬
‫ را ﺗﻌﻴﻴﻦ و در‬LMTD ‫ اﺛﺮ دﻣﺎ ﺿﺮﻳﺐ ﺗﺼﺤﻴﺢ‬.‫ﺑﺴﺘﮕﻲ دارد‬
‫ﻧﺘﻴﺠﻪ ﺧﻄﺎي اﻧﺪازه ﻫﻤﺮاه ﺑﺎ اﻟﮕﻮي ﺟﺮﻳﺎن ﻏﻴﺮ از ﺟﺮﻳﺎن‬
.‫ﻣﺘﻘﺎﺑﻞ اﻳﺠﺎد ﺷﺪه را ﻣﺸﺨﺺ ﻣﻲﻛﻨﺪ‬
In the simple crossflow exchanger shown in Fig.
5, the fins run throughout the full length of each
passage and no internal distributors are necessary.
This configuration is often used in liquefiers
where the warm stream is condensed, with little
temperature change, while exchanging heat with a
large throughput of a low pressure gas.
Temperature effectiveness is generally greater
than 60 percent if an excessive size penalty is to
be avoided.
،5 ‫در ﻣﺒﺪل ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ ﺳﺎده ﻧﺸﺎن داده ﺷﺪه در ﺷﻜﻞ‬
‫ﭘﺮهﻫﺎ در ﻛﻞ ﻃﻮل ﻣﺴﻴﺮ ﻗﺮار داﺷﺘﻪ و ﻫﻴﭻ ﺗﻮزﻳﻊ ﻛﻨﻨﺪه‬
‫ اﻳﻦ آراﻳﺶ اﻏﻠﺐ در ﻣﺎﻳﻊ ﻛﻨﻨﺪهﻫﺎﻳﻲ‬.‫داﺧﻠﻲ ﻻزم ﻧﻤﻲﺑﺎﺷﺪ‬
‫ زﻣﺎﻧﻲ ﻛﻪ ﺗﺒﺎدل ﺣﺮارت‬،‫ ﺑﺎ اﻧﺪك ﺗﻐﻴﻴﺮ دﻣﺎ‬، ‫ﻛﻪ ﺟﺮﻳﺎن ﮔﺮم‬
‫ ﭼﮕﺎﻟﻴﺪه‬،‫ﺑﻮﺳﻴﻠﻪ ﺣﺠﻢ اﻧﺒﻮﻫﻲ از ﮔﺎز ﻛﻢ ﻓﺸﺎر ورودي ﺑﺎﺷﺪ‬
،‫ ﺑﻪ ﻣﻨﻈﻮر اﺟﺘﻨﺎب از اﻧﺪازه ﺑﺰرگ ﻣﺒﺪل‬.‫ ﺑﻜﺎر ﻣﻲ رود‬،‫ﻣﻲﺷﻮد‬
.‫ درﺻﺪ ﻣﻲ ﺑﺎﺷﺪ‬60 ‫ﺗﺄﺛﻴﺮ دﻣﺎ ﻋﻤﻮﻣﺎً ﺑﺰرﮔﺘﺮ از‬
In the multi-pass unit shown in Fig. 5, one stream
flows straight through while the other is guided
by internal seals and external tanks to make the
required number of passes. The unit basically
consists of several crossflow sections assembled
in counterflow formation with a mean effective
temperature difference approaching that of
counterflow.
‫ ﻳﻚ‬،‫ ﻧﺸﺎن داده ﺷﺪه اﺳﺖ‬5 ‫در واﺣﺪ ﭼﻨﺪ راﻫﻪ ﻛﻪ در ﺷﻜﻞ‬
‫ﺟﺮﻳﺎن ﺑﻪ ﺻﻮرت ﻣﺴﺘﻘﻴﻢ ﺟﺮﻳﺎن ﻳﺎﻓﺘﻪ و دﻳﮕﺮي ﺗﻮﺳﻂ آب‬
‫ﺑﻨﺪﻫﺎي داﺧﻠﻲ و ﻣﺨﺎزن ﺧﺎرﺟﻲ ﻫﺪاﻳﺖ ﻣﻲﺷﻮد ﺗﺎ ﺗﻌﺪاد‬
‫ واﺣﺪ اﺳﺎﺳﺎً ﺷﺎﻣﻞ ﭼﻨﺪﻳﻦ ﺑﺨﺶ‬.‫راﻫﻪﻫﺎي ﻻزم را اﻳﺠﺎد ﻛﻨﻨﺪ‬
‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ ﻛﻪ روي ﻧﻤﻮﻧﻪ ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﺳﻮار ﺷﺪهاﻧﺪ ﺑﺎ‬
.‫ﻣﻴﺎﻧﮕﻴﻦ اﺧﺘﻼف دﻣﺎي ﻣﻮﺛﺮ ﻧﺰدﻳﻚ ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻣﻲ ﺑﺎﺷﺪ‬
In most low temperature applications counterflow
is generally specified. Header arrangements must
be matched to the type of service. The
counterflow units shown in Fig. 5 include:
‫ ﻋﻤﻮﻣﺎً ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﺗﻌﻴﻴﻦ‬،‫در اﻛﺜﺮ ﻛﺎرﺑﺮدﻫﺎ در دﻣﺎي ﭘﺎﻳﻴﻦ‬
.‫ آراﻳﺶ ﻫﺎي ﺳﺮﺷﺎﺧﻪ ﺑﺎﻳﺪ ﻣﻄﺎﺑﻖ ﺑﺎ ﻧﻮع ﻛﺎرﺑﺮد ﺑﺎﺷﺪ‬.‫ﻣﻲﺷﻮد‬
‫ ﻧﺸﺎن داده ﺷﺪهاﻧﺪ‬5 ‫واﺣﺪﻫﺎي ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻛﻪ در ﺷﻜﻞ‬
:‫ﺷﺎﻣﻞ ﻛﺎرﺑﺮي ﻫﺎي زﻳﺮ ﻣﻲ ﺑﺎﺷﺪ‬
which is mainly used in low pressure
applications;
.‫ ﻋﻤﺪﺗﺎً در ﻛﺎرﺑﺮدﻫـﺎي ﻓﺸﺎر ﭘﺎﻳﻴﻦ اﺳﺘﻔﺎده ﻣﻲﺷﻮد‬:1 ‫ﻧﻮع‬
Type 2: a symmetrical arrangement suitable
for reversing duty and for high
pressure units; and
‫ آراﻳﺶ ﻣﺘﻘﺎرن ﻣﻨﺎﺳﺐ ﺑﺮاي وﻇﺎﻳﻒ ﻣﻌﻜﻮس و‬:2 ‫ﻧﻮع‬
Type 1:
‫ و‬، ‫واﺣﺪﻫﺎي ﻓﺸﺎر ﺑﺎﻻ‬
46
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
Type 3:
which may be used for three or more
streams.
IPS-E-PR- 771(1)
.‫ ﺑﺮاي ﺳﻪ ﻳﺎ ﭼﻨﺪ ﺟﺮﻳﺎن ﻣﻤﻜﻦ اﺳﺖ اﺳﺘﻔﺎده ﺷﻮد‬:3 ‫ﻧﻮع‬
‫ ﺻﻔﺤﺎت ﻣﻮﺟﺪار‬2-1-16
16.1.2 Corrugations
To satisfy widely differing requirements, several
types of corrugations have been developed. The
more commonly used corrugations are listed as
follows along with their alternate designations:
‫ ﭼﻨﺪﻳﻦ ﻧﻮع از ﺻﻔﺤﺎت ﻣﻮجدار‬،‫ﺑﺮاي ﻧﻴﺎزﻫﺎي ﺑﺴﻴﺎر ﻣﺘﻔﺎوت‬
‫ ﺗﻌﺪادي از ﺻﻔﺤﺎت ﻣﻮجدار ﺑﺴﻴﺎر ﻣﺘﺪاول ﺑﺎ‬.‫ﺗﻮﺳﻌﻪ ﻳﺎﻓﺘﻪاﻧﺪ‬
:‫ﻣﺸﺨﺼﻪ ﻫﺎي ﻣﺘﻔﺎوت در زﻳﺮ ﻓﻬﺮﺳﺖ ﺷﺪهاﻧﺪ‬
.(‫( ﻣﺴﻄﺢ – )ﺻﺎف‬1
1) Plain - (straight).
.(‫ ورودي ﭼﻨﺪﮔﺎﻧﻪ‬،‫ دﻧﺪاﻧﻪدار‬،‫( ﻧﻴﺰهاي )ﻧﻮاري‬2
2) Lanced - (strip, serrated, multi-entry).
.(‫ ﺟﻨﺎﻗﻲ‬،‫( ﻧﺎﻫﻤﻮار – )ﻣﻮﺟﺪار‬3
3) Ruffled - (wavy, herringbone).
.‫( ﺳﻮراﺧﺪار‬4
4) Perforated.
Plain fin surfaces are characterized by long
uninterrupted flow passages with performance
similar to that obtained inside circular tubes.
Plain-fin surfaces include those with rectangular
passages, triangular passages and passages with
rounded corners. In general, the lanced, ruffled,
and perforated corrugations offer enhanced heat
transfer and pressure drop characteristics. When
compared to the plain fin, their use results in a
reduction in length with some increase in crosssectional area for a given thermal load and
pressure loss.
‫ﺳﻄﻮح ﭘﺮهدار ﻣﺴﻄﺢ ﺑﻮﺳﻴﻠﻪ ﻣﺴﻴﺮﻫﺎي ﺟﺮﻳﺎﻧﻲ ﻏﻴﺮﻣﻨﻘﻄﻊ‬
‫ﻃﻮﻻﻧﻲ ﺑﺎ ﻛﺎرآﻳﻲ ﻣﺸﺎﺑﻪ آﻧﭽﻪ در داﺧﻞ ﻟﻮﻟﻪﻫﺎي ﻣﺪور وﺟﻮد‬
‫ ﺳﻄﻮح ﭘﺮهدار ﻣﺴﻄﺢ ﺷﺎﻣﻞ ﻣﺴﻴﺮﻫﺎي‬.‫ ﻣﺸﺨﺺ ﻣﻲﺷﻮد‬،‫دارد‬
‫ ﻣﺴﻴﺮﻫﺎي ﻣﺜﻠﺜﻲ و ﻣﺴﻴﺮﻫﺎﻳﻲ ﺑﺎ ﮔﻮﺷﻪﻫﺎي ﮔﺮد‬،‫ﻣﺴﺘﻄﻴﻠﻲ‬
،‫ ﻧﺎﻫﻤﻮار و ﺳﻮراﺧﺪار‬،‫ ﻣﻮج دارﻫﺎي ﻧﻴﺰهاي‬،‫ در ﻛﻞ‬.‫ﻣﻲﺑﺎﺷﻨﺪ‬
‫ در ﻣﻘﺎﻳﺴﻪ‬.‫وﻳﮋﮔﻲ اﻧﺘﻘﺎل ﺣﺮارت و اﻓﺖ ﻓﺸﺎر ﺑﻴﺸﺘﺮي دارﻧﺪ‬
‫ اﺳﺘﻔﺎده از آﻧﻬﺎ ﺑﻪ ﻛﺎﻫﺶ ﻃﻮل و اﻓﺰاﻳﺶ‬،‫ﺑﺎ ﭘﺮهﻫﺎي ﻣﺴﻄﺢ‬
‫اﻧﺪﻛﻲ در ﺳﻄﺢ ﻣﻘﻄﻊ ﺟﺎﻧﺒﻲ ﺑﺮاي ﻳﻚ ﺑﺎر ﺣﺮارﺗﻲ و اﻓﺖ‬
.‫ ﻣﻨﺠﺮ ﻣﻲ ﮔﺮدد‬،‫ﻓﺸﺎر ﻣﺸﺨﺺ‬
Within each general category of corrugation there
are variations in specific fin geometry. For
industrial applications fin dimensions generally
lie within the following ranges:
‫ در ﺷﻜﻞ ﻫﻨﺪﺳﻲ ﭘﺮه ﻫﺎ‬،‫در ﻫﺮ ﮔﺮوه ﻛﻠﻲ از ﺻﻔﺤﺎت ﻣﻮﺟﺪار‬
،‫ ﺑﺮاي ﻛﺎرﺑﺮدﻫﺎي ﺻﻨﻌﺘﻲ‬.‫ﺗﻔﺎوتﻫﺎي ﻣﺸﺨﺼﻲ وﺟﻮد دارد‬
:‫اﺑﻌﺎد ﭘﺮه ﻋﻤﻮﻣﺎً در ﻣﺤﺪوده زﻳﺮ ﻗﺮار ﻣﻲﮔﻴﺮد‬
- height
‫ ارﺗﻔﺎع‬-
3.81
to
11.43 mm;
- thickness
‫ ﺿﺨﺎﻣﺖ‬-
0.153
to
0.635 mm;
8
to
18 fins per 25.4 mm. ‫ ﻣﻴﻠﻴﻤﺘﺮ‬25/4 ‫ ﭘﺮه در ﻫﺮ‬18
- pitch
‫ ﮔﺎم‬-
The percentage of fin surface area removed in
perforated fins generally lies between 10 and 25
percent. The resulting surface area per unit core
volume lies between 820 and 1476 m²/m³.
10 ‫ ﻋﻤﻮﻣﺎً ﺑﻴﻦ‬،‫درﺻﺪ ﺳﻄﺢ ﺣﺬف ﺷﺪه در ﭘﺮهﻫﺎي ﺳﻮراخدار‬
‫ در ﻧﺘﻴﺠﻪ ﻧﺴﺒﺖ ﺳﻄﺢ ﺑﻪ واﺣﺪ ﺣﺠﻢ‬.‫ درﺻﺪ ﻣﻲ ﺑﺎﺷﺪ‬25 ‫ﺗﺎ‬
.‫ﻣﺘﺮ ﻣﻜﻌﺐ اﺳﺖ‬/ ‫ ﻣﺘﺮ ﻣﺮﺑﻊ‬1476 ‫ ﺗﺎ‬820 ‫ﻫﺴﺘﻪ ﺑﻴﻦ‬
16.1.3 Nomenclature specific to plate-fin
exchanger geometry is given in Table 2. Also
given in Table 2 are relations for calculating the
geometrical properties of a plate-fin surface from
the fin dimensions. Note that although the
calculated geometrical properties of plain and
lanced fins having the same dimensions are the
same, their heat transfer and pressure drop
characteristics are markedly different as will be
seen later in this subsection.
‫ واژهﻫﺎﻳﻲ ﻛﻪ ﻣﺨﺼﻮص ﺷﻜﻞ ﻫﻨﺪﺳﻲ ﻣﺒﺪل‬3-1-16
‫ ﻫﻤﭽﻨﻴﻦ در‬.‫ آﻣﺪه اﺳﺖ‬2 ‫ﺻﻔﺤﻪاي ﭘﺮهدار ﻣﻲﺑﺎﺷﺪ در ﺟﺪول‬
‫ رواﺑﻂ ﻣﺤﺎﺳﺒﻪ ﺧﻮاص ﻫﻨﺪﺳﻲ ﺳﻄﺢ ﺻﻔﺤﻪاي‬2 ‫ﺟﺪول‬
‫ ﺗﻮﺟﻪ ﺷﻮد ﻛﻪ‬.‫ﭘﺮهدار ﺑﺎ اﺳﺘﻔﺎده از اﺑﻌﺎد ﭘﺮه داده ﺷﺪه اﺳﺖ‬
‫اﮔﺮ ﭼﻪ ﺧﻮاص ﻫﻨﺪﺳﻲ ﻣﺤﺎﺳﺒﻪ ﺷﺪه ﭘﺮهﻫﺎي ﻣﺴﻄﺢ و ﻧﻴﺰهاي‬
‫ﻛﻪ اﺑﻌﺎد ﻳﻜﺴﺎﻧﻲ دارﻧﺪ ﻣﺴﺎوي ﻫﺴﺘﻨﺪ وﻟﻲ ﻣﺸﺨﺼﻪ اﻧﺘﻘﺎل‬
‫ﺣﺮارت و اﻓﺖ ﻓﺸﺎر آﻧﻬﺎ ﻫﻤﺎﻧﻄﻮر ﻛﻪ در زﻳﺮﻣﺠﻤﻮﻋﻪ ﺑﻌﺪي‬
.‫ﻣﺸﺎﻫﺪه ﺧﻮاﻫﺪ ﺷﺪ ﻛﺎﻣﻼ ﻣﺘﻔﺎوت ﻣﻲ ﺑﺎﺷﺪ‬
47
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
A partial list of the many industrial corrugations
available from the principal U.S. manufacturers is
given in Table 3.
IPS-E-PR- 771(1)
‫ﻳﻚ ﻓﻬﺮﺳﺖ ﺟﺰﻳﻲ از اﻛﺜﺮ ﺻﻔﺤﺎت ﻣﻮﺟﺪار ﺻﻨﻌﺘﻲ ﻗﺎﺑﻞ‬
‫دﺳﺘﺮس ﺑﺮ اﺳﺎس اﻃﻼﻋﺎت ﺳﺎزﻧﺪﮔﺎن اﺻﻠﻲ آﻣﺮﻳﻜﺎﻳﻲ در‬
.‫ آﻣﺪه اﺳﺖ‬3 ‫ﺟﺪول‬
Included in this table are the geometrical
properties calculated using the relationships of
Table 2.
‫اﻳﻦ ﺟﺪول ﺷﺎﻣﻞ ﺧﻮاص ﻫﻨﺪﺳﻲ ﻣﺤﺎﺳﺒﻪ ﺷﺪه ﺑﺮاﺳﺎس رواﺑﻂ‬
.‫ ﻣﻲﺑﺎﺷﺪ‬2 ‫ﺟﺪول‬
‫ ﺿﻮاﺑﻂ اﻧﺘﺨﺎب ﭘﺮه‬4-1-16
16.1.4 Fin selection criteria
16.1.4.1 The selection of the optimum fins for a
particular application is at best a difficult trial
procedure due to the large number of process
variables involved and the large number of
available surfaces. However, some general
preliminary fin selection criteria can be given
based on the nature of the fluid stream and on the
working pressure.
‫ اﻧﺘﺨﺎب ﭘﺮهﻫﺎي ﺑﻬﻴﻨﻪ ﺑﺮاي ﻳﻚ ﻛﺎرﺑﺮد ﻣﺸﺨﺺ‬1-4-1-16
The most widely used fin is the lanced fin. It is
generally suitable for application in all gas, all
liquid, condensing, and vaporizing services. It is
the first fin that should be considered when
selecting surfaces for a particular application. The
use of plain fins is generally limited to special
cases of liquid and condensing flow and to cases
where the free passage of contaminating solids is
desired. Perforated fins are often used in
condensing and vaporizing service and in the
distribution sections of counterflow units.
‫ اﻳﻦ ﻧﻮع ﭘﺮه‬.‫ﭘﺮه ﻧﻴﺰهاي ﭘﺮ ﻛﺎرﺑﺮد ﺗﺮﻳﻦ ﻧﻮع ﭘﺮه ﻣﻲ ﺑﺎﺷﺪ‬
‫ ﺗﻤﺎم ﻣﺎﻳﻌﺎت؛ ﻛﺎرﺑﺮﻳﻬﺎي‬،‫ﻋﻤﻮﻣﺎً ﺑﺮاي ﻛﺎرﺑﺮد در ﺗﻤﺎم ﮔﺎزﻫﺎ‬
‫ ﺑﺮاي اﻧﺘﺘﺨﺎب ﭘﺮه در ﻳﻚ‬.‫ﭼﮕﺎﻟﺶ و ﺗﺒﺨﻴﺮ ﻣﻨﺎﺳﺐ اﺳﺖ‬
‫ﻛﺎرﺑﺮي ﺧﺎص اوﻟﻴﻦ ﻧﻮع ﭘﺮهاي اﺳﺖ ﻛﻪ ﺗﻮﺻﻴﻪ ﻣﻲ ﮔﺮدد در‬
‫ اﺳﺘﻔﺎده از ﭘﺮهﻫﺎي ﻣﺴﻄﺢ ﻋﻤﻮﻣﺎً ﺑﻪ ﻣﻮارد‬.‫ﻧﻈﺮ ﮔﺮﻓﺘﻪ ﺷﻮد‬
‫ﺧﺎﺻﻲ از ﺟﺮﻳﺎن ﻣﺎﻳﻊ و ﭼﮕﺎﻟﻴﺪه و ﺑﻪ ﺣﺎﻻﺗﻲ ﻛﻪ ﻣﺴﻴﺮآزاد‬
.‫ ﻣﺤﺪود ﺷﺪه اﺳﺖ‬،‫ﺑﺮاي ﺟﺎﻣﺪات آﻟﻮده ﻛﻨﻨﺪه ﻣﺪ ﻧﻈﺮ ﺑﺎﺷﺪ‬
‫ﭘﺮهﻫﺎي ﺳﻮراﺧﺪار اﻏﻠﺐ در ﻛﺎرﺑﺮي ﻫﺎي ﭼﮕﺎﻟﺶ و ﺗﺒﺨﻴﺮ و‬
.‫ﻗﺴﻤﺖﻫﺎي ﺗﻮزﻳﻊ واﺣﺪﻫﺎي ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ اﺳﺘﻔﺎده ﻣﻲﺷﻮﻧﺪ‬
16.1.4.2 Fin height and thickness are subject to
‫ ارﺗﻔﺎع و ﺿﺨﺎﻣﺖ ﭘﺮه ﺗﺎﺑﻌﻲ از ﻣﺤﺪودﻳﺖﻫﺎي‬2-4-1-16
working pressure limitations. The use of fins that
9/52 ‫ اﺳﺘﻔﺎده از ﭘﺮهﻫﺎﻳﻲ ﺑﺎ ارﺗﻔﺎع‬.‫ﻓﺸﺎر ﻛﺎري ﻣﻲﺑﺎﺷﺪ‬
‫ ﻣﻴﻠﻴﻤﺘﺮ ﺑﺎﺷﺪ‬0/3048 ‫ﻣﻴﻠﻴﻤﺘﺮ و ﺑﻠﻨﺪﺗﺮ و ﺑﺎ ﺿﺨﺎﻣﺖ ﻛﻤﺘﺮ از‬
‫ در‬.‫ ﺑﺎر)ﻧﺴﺒﻲ( ﻣﺤﺪود ﻣﻲ ﮔﺮدﻧﺪ‬21 ‫ﺑﻪ ﻓﺸﺎر ﻛﺎري زﻳﺮ‬
.‫ ﭘﺮهﻫﺎي ﻛﻮﺗﺎهﺗﺮ و ﺿﺨﻴﻢﺗﺮ ﻻزم اﺳﺖ‬،‫ﻓﺸﺎرﻫﺎي ﺑﺎﻻﺗﺮ‬
‫ﻣﻼﺣﻈﺎت ﻓﺸﺎري اﺟﺎزه ﻣﻲدﻫﺪ ﻛﻪ از ﺻﻔﺤﺎت ﻣﻮﺟﺪار ﺑﻠﻨﺪﺗﺮ‬
6/35 ‫ﺑﺮاي ﺟﺮﻳﺎن ﮔﺎز اﺳﺘﻔﺎده ﺷﻮد در ﺣﺎﻟﻲ ﻛﻪ ﺑﺎ ارﺗﻔﺎع‬
‫ ﭘﺮهﻫﺎي ﻣﻮجدار‬.‫ﻣﻴﻠﻴﻤﺘﺮ و ﻛﻮﭼﻜﺘﺮ ﺑﺮاي ﻣﺎﻳﻌﺎت اﺳﺘﻔﺎده ﺷﻮد‬
‫ ﻣﻴﻠﻴﻤﺘﺮ ارﺗﻔﺎع دارﻧﺪ و ﻫﻤﭽﻨﻴﻦ ﺑﺮﺧﻲ‬9/52 ‫ﻋﻤﻮﻣﺎً ﺣﺪاﻗﻞ‬
.‫اوﻗﺎت ﺑﺮاي ﺟﺮﻳﺎنﻫﺎي ﮔﺎزي ﻛﻢ ﻓﺸﺎر اﺳﺘﻔﺎده ﻣﻲﺷﻮﻧﺪ‬
‫در ﺑﻬﺘﺮﻳﻦ ﺣﺎﻟﺖ ﻳﻚ روش آزﻣﻮدﻧﻲ دﺷﻮار ﺑﻪ ﺟﻬﺖ وﺟﻮد‬
‫ ﺑﺎ‬.‫ﺗﻌﺪاد زﻳﺎد ﻣﺘﻐﻴﺮﻫﺎي ﻓﺮآﻳﻨﺪي و ﺗﻌﺪاد زﻳﺎد ﺳﻄﻮح اﺳﺖ‬
‫ ﺑﺮﺧﻲ ﻣﻌﻴﺎرﻫﺎي ﻋﻤﻮﻣﻲ اﻧﺘﺨﺎب اوﻟﻴﻪ ﭘﺮه ﻣﻴﺘﻮاﻧﺪ‬،‫اﻳﻦ وﺟﻮد‬
.‫ﺑﺮاﺳﺎس ﻣﺎﻫﻴﺖ ﺟﺮﻳﺎن ﺳﻴﺎل و ﻓﺸﺎر ﻛﺎرﻛﺮد داده ﺷﺪه ﺑﺎﺷﺪ‬
are 9.52 mm and taller and less than 0.3048 mm
thick is limited to working pressures below 21 bar
(ga). At higher pressures, shorter and thicker fins
are necessary. Pressure considerations permitting,
the taller corrugations are used for gas streams
while those with heights 6.35 mm and smaller are
used for liquids. Wavy fins are generally at least
9.52 mm high and as such are sometimes used
with low pressure gas streams.
‫ ﻣﺤﺪودﻳﺖﻫﺎي اﻧﺪازه ﻫﺴﺘﻪ‬5-1-16
16.1.5 Core size limitations
The maximum size of a single core is limited by
mechanical design considerations and by
manufacturing facilities.
‫ﺣﺪاﻛﺜﺮ اﻧﺪازه ﻫﺴﺘﻪ ﺑﻪ رﻋﺎﻳﺖ ﻣﻼﺣﻈﺎت ﻃﺮاﺣﻲ ﻣﻜﺎﻧﻴﻜﻲ و‬
.‫اﻣﻜﺎﻧﺎت ﺷﺮﻛﺖ ﺳﺎزﻧﺪه ﻣﺤﺪود ﻣﻲﺷﻮد‬
Pressure loadings limit core cross-sections to
between 0.232 and 0.836 m². The size of brazing
0/836 ‫ و‬0/232 ‫ ﺳﻄﺢ ﻣﻘﻄﻊ ﻫﺴﺘﻪ را ﺑﻴﻦ‬،‫ﺑﺎرﻫﺎي ﻓﺸﺎري‬
brazing ) ‫ اﻧﺪازه ﻛﻮره ﻟﺤﻴﻢ ﻛﺎري‬.‫ﻣﺘﺮﻣﺮﺑﻊ ﻣﺤﺪود ﻣﻲﻛﻨﺪ‬
48
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
ovens limit core lengths to about 3.048 m
although recently some 6.096 cores have become
available for low pressure operation. A list of the
maximum size cores for various non-reversing
pressure levels is given in Table 4. For reversing
operation, the maximum working pressure for
each of the cores listed should be taken as one
half the values given in the table.
IPS-E-PR- 771(1)
‫ ﻣﺘﺮ ﻣﺤﺪود ﻣﻲﻛﻨﺪ اﮔﺮ‬3/048 ‫( ﻃﻮل ﻫﺴﺘﻪ را ﺑﻪ ﺣﺪود‬ovens
‫ ﺑﺮاي ﻓﻌﺎﻟﻴﺖﻫﺎي ﻓﺸﺎر ﻛﻢ‬6/096 ‫ﭼﻪ اﺧﻴﺮاً ﺑﺮﺧﻲ ﻫﺴﺘﻪﻫﺎي‬
‫ ﻓﻬﺮﺳﺖ ﺣﺪاﻛﺜﺮ اﻧﺪازه ﻫﺴﺘﻪﻫــﺎ ﺑﺮاي‬.‫ﻗﺎﺑﻞ دﺳﺘﺮس ﺷﺪهاﻧﺪ‬
‫ داده ﺷﺪه‬4 ‫ﺳﻄﻮح ﻓﺸــﺎري ﻏﻴﺮ ﻣﻌﻜﻮس ﻣﺨﺘﻠﻒ در ﺟﺪول‬
‫ ﺗﻮﺻﻴﻪ ﻣﻲ ﺷﻮد ﺣﺪاﻛﺜﺮ ﻓﺸﺎر‬،‫ ﺑﺮاي ﻋﻤﻠﻴﺎت ﻣﻌﻜﻮس‬.‫اﺳﺖ‬
‫ﻛﺎري ﺑﺮاي ﻫﺮﻛﺪام از ﻫﺴﺘﻪﻫﺎ ﻧﺼﻒ ﻣﻘﺎدﻳﺮ ﻣﻨﺪرج در ﺟﺪول‬
.‫ﺑﺎﺷﺪ‬
Included in Table 4 are the thicknesses of the
separation sheets required at the various pressure
levels.
‫ ﺷﺎﻣﻞ ﺿﺨﺎﻣﺖﻫﺎي ﺻﻔﺤﺎت ﺟﺪاﻛﻨﻨﺪه ﻻزم در‬4 ‫ﺟﺪول‬
.‫ﺳﻄﻮح ﻓﺸﺎري ﻣﺨﺘﻠﻒ ﻣﻲ ﺑﺎﺷﺪ‬
‫ ﻣﺴﻴﺮﻫﺎي ﻛﺎذب و ﺻﻔﺤﺎت ﺑﻴﺮوﻧﻲ‬6-1-16
16.1.6 Dummy passages and outside sheets
To protect the exchanger core during shipping
and installation, dummy layers of 6.35 mm fins
and outside sheets 6.35 mm thick are brazed to
the top and bottom of the core. In some cases the
dummy passages are not necessary.
‫ ﺻﻔﺤﺎت‬،‫ﺑﺮاي ﻣﺤﺎﻓﻈﺖ ﻫﺴﺘﻪ ﻣﺒﺪل در ﻃﻮل ﺣﻤﻞ و ﻧﺼﺐ‬
‫ ﻣﻴﻠﻴﻤﺘﺮ و ﺻﻔﺤﺎت ﺑﻴﺮوﻧﻲ ﺑﺎ ﺿﺨﺎﻣﺖ‬6/35 ‫ﻛﺎذب از ﭘﺮهﻫﺎي‬
‫ در‬.‫ ﻣﻴﻠﻴﻤﺘﺮ ﺑﻪ ﺑﺎﻻ و ﭘﺎﻳﻴﻦ ﻫﺴﺘﻪ ﻟﺤﻴﻢ ﻛﺎري ﻣﻲﺷﻮد‬6/35
.‫ﺑﺮﺧﻲ ﻣﻮارد ﻣﺴﻴﺮﻫﺎي ﻛﺎذب ﻻزم ﻧﻴﺴﺖ‬
‫ ﺑﺨﺶ ﺗﻮزﻳﻊ‬7-1-16
16.1.7 Distribution section
‫ ﺑﻪ ﻗﺴﻤﺖ‬5 ‫واﺣﺪﻫﺎي ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻧﺸﺎن داده ﺷﺪه در ﺷﻜﻞ‬
‫ﺗﻮزﻳﻊ ﺑﺮاي ﮔﺴﺘﺮش ﻳﻜﻨﻮاﺧﺖ ﺟﺮﻳﺎن از ﺳﺮﺷﺎﺧﻪﻫﺎ در ﭘﻬﻨﺎي‬
‫ اﻳﻦ ﻗﺴﻤﺖﻫﺎ آراﻳﺶ ﺳﺎده اي از ﺻﻔﺤﺎت‬.‫ﻫﺴﺘﻪ ﻧﻴﺎز دارد‬
.‫ﭘﺮهدار ﻫﺴﺘﻨﺪ ﻛﻪ ﺑﺎ زاوﻳﻪ در ﺟﻬﺖ ﭘﺮه ﻫﺴﺘﻪ ﻧﺼﺐ ﺷﺪه اﺳﺖ‬
‫ﻋﻼوه ﺑﺮ آن آب ﺑﻨﺪﻫﺎي داﺧﻠﻲ ﻣﻨﺎﺳﺐ ﺑﺮاي ﻛﻤﻚ ﺑﻪ ﻫﺪاﻳﺖ‬
.‫ﺟﺮﻳﺎن وﺟﻮد دارد‬
The counterflow units shown in Fig. 5 require
distributor sections to uniformly spread the flow
from the headers over the width of the core.
These sections are simply plate-fin arrangements
installed at an angle to the core fin direction. In
addition, there are suitable internal seals to help
guide the flow.
49
‫)‪IPS-E-PR- 771(1‬‬
‫ﻣﻬﺮ ‪Oct. 2009 / 1388‬‬
‫ﻧﻤﺎي ﺑﺎز ﻳﻚ ﺟﺰء ﻣﻨﻔﺮد‬
‫آبﺑﻨﺪ ﻟﺒﻪ‬
‫ﻣﻮجدار‬
‫ﺻﻔﺤﻪ‬
‫اﺟﺰاﺋﻲ ﻛﻪ ﺑﺮاي ﺟﺮﻳﺎن‬
‫ﻣﺘﻘﺎﻃﻊ ﺳﻮار ﺷﺪهاﻧﺪ‬
‫‪Stream 2‬‬
‫‪Stream 1‬‬
‫ﺟﺮﻳﺎن ‪2‬‬
‫ﺟﺮﻳﺎن ‪1‬‬
‫اﺟﺰاﺋﻲ ﻛﻪ ﺑﺮاي ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ‬
‫ﺳﻮار ﺷﺪهاﻧﺪ‬
‫‪Stream 1‬‬
‫ﺟﺮﻳﺎن ‪1‬‬
‫‪Stream 2‬‬
‫ﺟﺮﻳﺎن ‪2‬‬
‫‪Fig. 4-PLATE FIN EXCHANGER ASSEMBLY‬‬
‫ﺷﻜﻞ ‪ -4‬ﺟﻤﻊ ﻛﺮدن ﻣﺒﺪل ﺻﻔﺤﻪاي ﭘﺮهدار‬
‫‪50‬‬
‫ﻣﻬﺮ ‪Oct. 2009 / 1388‬‬
‫)‪IPS-E-PR- 771(1‬‬
‫ﺟﺮﻳﺎن ﭼﻨﺪ راﻫﻪ‬
‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ‬
‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻧﻮع ‪1‬‬
‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻧﻮع ‪2‬‬
‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﺑﻞ ﻧﻮع ‪3‬‬
‫‪Fig. 5-PLATE FIN EXCHANGER FLOW ARRANGEMENTS‬‬
‫ﺷﻜﻞ ‪ -5‬آراﻳﺶ ﺟﺮﻳﺎﻧﻲ ﻣﺒﺪل ﺻﻔﺤﻪ اي ﭘﺮهدار‬
‫‪51‬‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
TABLE 2 - GEOMETRICAL RELATIONSHIPS OF PLATE FIN SURFACES
‫ رواﺑﻂ ﻫﻨـﺪﺳـﻲ ﺳﻄـﻮح ﭘﺮهدار ﺻﻔﺤـﻪاي‬-2 ‫ﺟﺪول‬
The following are the basic geometry data for a
plate fin surface:
‫ﻣﻮارد زﻳﺮ اﻃﻼﻋﺎت ﭘﺎﻳﻪ ﻫﻨﺪﺳﻲ ﺑﺮاي ﺳﻄﻮح ﭘﺮهدار ﺻﻔﺤﻪاي‬
:‫ﻫﺴﺘﻨﺪ‬
fin height = plate spacing
b=
25.4 mm (inch)
‫ارﺗﻔﺎع ﭘﺮه = ﻓﺎﺻﻠﻪ ﺻﻔﺤﺎت‬
fin pitch or spacing
n=
‫ﮔﺎم ﻳﺎ ﻓﺎﺻﻠﻪ ﭘﺮه‬
fins/25.4 mm (fins/inch)
fin thickness
Xf =
25.4 mm (inch)
‫ﺿﺨﺎﻣﺖ ﭘﺮه‬
fraction of fin perforated (for perforated fins only)
Y=
----
(‫ﻛﺴﺮ ﺳﻮراخ ﻛﺎري ﺷﺪه ﭘﺮه )ﻓﻘﻂ ﺑﺮاي ﭘﺮهﻫﺎي ﺳﻮراخدار‬
ratio of actual length to projected length .
K=
----
‫ﻧﺴﺒﺖ ﻃﻮل واﻗﻌﻲ ﺑﻪ ﻃﻮل ﺗﺼﻮﻳﺮ‬
From the basic fin dimensions the following
geometrical properties can be calculated for a
plate fin passage.
Ax =
AT =
L=
W=
Xp =
N=
‫ ﺧﻮاص ﻫﻨﺪﺳﻲ زﻳﺮ ﺑﺮاي ﻣﺴﻴﺮ ﭘﺮه ﻗﺎﺑﻞ‬،‫از اﺑﻌﺎد اﺻﻠﻲ ﭘﺮه‬
.‫ﻣﺤﺎﺳﺒﻪ اﺳﺖ‬
free flow area of each stream
‫ﺳﻄﺢ ﻋﺒﻮر آزاد ﻫﺮ ﺟﺮﻳﺎن‬
total heat transfer area of each stream
‫ﻛﻞ ﺳﻄﺢ اﻧﺘﻘﺎل ﺣﺮارت ﻫﺮ ﺟﺮﻳﺎن‬
effective passage length
‫ﻃﻮل ﻣﻮﺛﺮ ﻣﺴﻴﺮ‬
effective passage width
‫ﻋﺮض ﻣﻮﺛﺮ ﻣﺴﻴﺮ‬
plate thickness
‫ﺿﺨﺎﻣﺖ ﺻﻔﺤﻪ‬
number of passages of each stream .
‫ﺗﻌﺪاد ﻣﺴﻴﺮﻫﺎي ﻫﺮ ﺟﺮﻳﺎن‬
From the basic fin dimensions the following
geometrical properties can be calculated for a
plate fin passage.
m² (sq ft)
m² (sq ft)
m (ft)
25.4 mm (inch)
25.4 mm (inch)
----
‫ ﺧﻮاص ﻫﻨﺪﺳﻲ زﻳﺮ ﺑﺮاي ﻣﺴﻴﺮ ﭘﺮه ﻗﺎﺑﻞ‬،‫از اﺑﻌﺎد اﺻﻠﻲ ﭘﺮه‬
.‫ﻣﺤﺎﺳﺒﻪ اﺳﺖ‬
52
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
free flow area per passage per 25.4 mm (inch) of passage effective width
A 'x =
m²/mm (sq ft/inch)
‫ از ﻋﺮض ﻣﻮﺛﺮ ﻣﺴﻴﺮ‬25/4mm ‫ﺳﻄﺢ ﻋﺒﻮر آزاد ﺑﺮ ﻣﺴﻴﺮ ﺑﻪ ازاء‬
primary (plate) surface area per passage
Ap =
‫ﺳﻄﺢ اوﻟﻴﻪ )ﺻﻔﺤﻪ( در ﻫﺮ ﻣﺴﻴﺮ‬
m² (sq ft)
primary (plate) surface area per passage per 0.3048 m (foot) of length per
effective width
Ap" =
25.4 mm (inch) of
‫ )ﻓﻮت( از ﻃﻮل ﺑﺮ ﻋﺮض ﻣﻮﺛﺮ‬0/0348m ‫ﺳﻄﺢ اوﻟﻴﻪ )ﺻﻔﺤﻪ( در ﻫﺮ ﻣﺴﻴﺮ در ﻫﺮ‬
m²/mm (sq ft/inch)
secondary (fin) surface area per passage
Af =
‫ﺳﻄﺢ ﻛﻞ ﺛﺎﻧﻮﻳﻪ )ﭘﺮه( در ﻫﺮ ﻣﺴﻴﺮ‬
m² (sq ft)
secondary (fin) surface area per passage per 0.3048m (foot) of length per
25.4 mm (inch) of effective width
Af"=
25/4mm ‫ )ﻓﻮت( از ﻃﻮل در ﻫﺮ‬0/3048m ‫ﺳﻄﺢ ﻛﻞ ﺛﺎﻧﻮﻳﻪ )ﭘﺮه( در ﻫﺮ ﻣﺴﻴﺮ در ﻫﺮ‬
‫)اﻳﻨﭻ( از ﻋﺮض ﻣﻮﺛﺮ‬
m²/mm
(sq ft/inch)
total surface area per passage per 0.3048 m (foot) of length per 25.4 mm
(inch) of effective width
AT" =
m²/m.mm (sq ft/ft inch)
25/4mm ‫ )ﻓﻮت( از ﻃﻮل در ﻫﺮ‬0/3048m ‫ﺳﻄﺢ ﻛﻞ ﺛﺎﻧﻮﻳﻪ )ﭘﺮه( در ﻫﺮ ﻣﺴﻴﺮ در ﻫﺮ‬
‫)اﻳﻨﭻ( از ﻋﺮض ﻣﻮﺛﺮ‬
flow passage hydraulic radius, AxL/AT
rh =
A L
‫ﺷﻌﺎع ﻫﻴﺪروﻟﻴﻜﻲ ﻣﺴﻴﺮ ﺟﺮﻳﺎن‬
hydraulic diameter = 4 rh
Dh =

AT
4rh = ‫ﻗﻄﺮ ﻫﻴﺪروﻟﻴﻜﻲ‬
m (ft)
m (ft)
ratio of total transfer area on one side of the exchanger to volume between
plates on that side
=
m²/m3 (sq ft/cu ft)
‫ﻧﺴﺒﺖ ﺳﻄﺢ اﻧﺘﻘﺎل ﻛﻞ در ﻳﻚ ﻃﺮف از ﻣﺒﺪل ﺑﻪ ﺣﺠﻢ ﺑﻴﻦ ﺻﻔﺤﺎت در ﻫﻤﺎن ﻃﺮف‬
Af
=
Af "
‫= ﻧﺴﺒﺖ ﺳﻄﺢ ﭘﺮه ﺑﻪ ﺳﻄﺢ ﻛﻞ‬
= ratio of fin surface area to total
"
AT
AT
surface are (Eq. 1)
(Eq. 2)
(Eq. 3)
AP 
(Eq. 5)
AT
"
=
Af
AT
(1 ‫)ﻣﻌﺎدﻟﻪ‬
1
(bX f )(  X f ) n
A
n
A,x = Ax'  x 
W.N
144
(Eq. 4)
Af "
Af 
AP  1
n
 X f 
W .L  n
6
Af
n
 (b  X f )  K (1  Y )
W .L
6
AT 
AT
 AP  Af
N.W.L
53
(2 ‫)ﻣﻌﺎدﻟﻪ‬
(3 ‫)ﻣﻌﺎدﻟﻪ‬
(4 ‫)ﻣﻌﺎدﻟﻪ‬
(5 ‫)ﻣﻌﺎدﻟﻪ‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
(Eq. 6)
(Eq. 7)
1

(b  X f )  X f 
Ax . L AX 1
n

rh 
  
AT 24  1
AT

  X f   (b  X f )K(1Y)
n

1

24  X f   (b  X f ) K (1  Y )
n

 
1
b
n
54
IPS-E-PR- 771(1)
(6 ‫)ﻣﻌﺎدﻟﻪ‬
(7 ‫)ﻣﻌﺎدﻟﻪ‬
‫)‪IPS-E-PR- 771(1‬‬
‫ﻣﻬﺮ ‪Oct. 2009 / 1388‬‬
‫‪TABLE 3 - FIN GEOMETRY DATA‬‬
‫ﺟﺪول ‪ -3‬اﻃﻼﻋﺎت ﻫﻨﺪﺳﻲ ﭘﺮه‬
‫ﺗﻘﺮﻳﺒﻲ‬
‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر‬
‫ﺿﺨﺎﻣﺖ‬
‫ﮔﺎم‬
‫ارﺗﻔﺎع‬
‫ﻛﺎرﻓﺮﻣﺎ‬
‫ﻧﺎﻫﻤﻮار‬
‫ﻧﻴﺰهاي‬
‫ﺻﺎف‬
‫ﻣﺴﻄﺢ‬
‫ﻧﻮع‬
‫* ﻫﻤﭽﻨﻴﻦ ﺑﺼﻮرت ﺳﻮراخدار ﻧﻴﺰ در دﺳﺘﺮس ﻫﺴﺘﻨﺪ‪.‬‬
‫‪* = Also available perforated.‬‬
‫‪55‬‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
TABLE 4 - MAXIMUM CORE DIMENSIONS
‫ ﺣﺪاﻛﺜﺮ اﺑﻌﺎد ﻫﺴﺘﻪ‬-4 ‫ﺟﺪول‬
MAX. ASME
WORKING
PRESS
bar (ga), (psig)
MAX.
OVERALL
WIDTH
mm (inch)
MAX.
EFFECTIVE
WIDTH
mm (inch)
MAX.
OVERALL
HEIGHT
mm (inch)
MAX.
EFFECTIVE
LENGTH
mm (inch)
SEPARATOR
SHEET
THICKNESS
mm (inch)
‫ﺿﺨﺎﻣﺖ ﺻﻔﺤﻪ‬
‫ﺣﺪاﻛﺜﺮ ﻓﺸﺎر‬
‫ﺣﺪاﻛﺜﺮ ﻋﺮض ﻛﻠﻲ‬
‫ﺣﺪاﻛﺜﺮ ﻋﺮض ﻣﻮﺛﺮ‬
‫ﺣﺪاﻛﺜﺮ ارﺗﻔﺎع‬
‫ﺣﺪاﻛﺜﺮ ارﺗﻔﺎع‬
‫ﻛﺎري‬
(‫ﻣﻴﻠﻴﻤﺘﺮ )اﻳﻨﭻ‬
(‫ﻣﻴﻠﻴﻤﺘﺮ )اﻳﻨﭻ‬
‫ﻛﻠﻲ‬
‫ﻣﻮﺛﺮ‬
‫ﺟﺪاﻛﻨﻨﺪه‬
(‫ﻣﻴﻠﻴﻤﺘﺮ )اﻳﻨﭻ‬
(‫ﻣﻴﻠﻴﻤﺘﺮ )اﻳﻨﭻ‬
(‫ﻣﻴﻠﻴﻤﺘﺮ )اﻳﻨﭻ‬
14 (200)
914.4 (36)
885.8 (347/8)
914.4 (36)
762 (30)
0.813 (0.032)
24 (300)
914.4 (36)
885.8 (347/8)
914.4 (36)
3657.6 (144)
1.626 (0.064)
35 (500)
635 (25)
606.4 (237/8)
535 (211/16)
3048 (120)
1.626 (0.064)
49 (700)
457.2 (18)
431.8 (17)
514.4 (20¼)
3048 (120)
1.626 (0.064)
14 (200)
762 (30)
730.3 (28¾)
762 (30)
3168.7(124 ¼)
0.813 (0.032)
31 (450)
660.4 (26)
628.7 (24¾)
762 (30)
3168.7(124¾)
1.270 (0.050)
49 (700)
450 (17¾)
419.1 (16½)
762 (30)
3168.7(124¾)
1.626 (0.064)
56
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-PR- 771(1)
APPENDICES
APPENDIX A
Front end stationary head
types ‫اﻧﻮاع ﻛﻠﮕﻲ ﺛﺎﺑﺖ اﻧﺘﻬﺎي ﺟﻠﻮ‬
‫ﭘﻴﻮﺳﺖﻫﺎ‬
‫ﭘﻴﻮﺳﺖ اﻟﻒ‬
Rear end head types
‫اﻧﻮاع ﻛﻠﮕﻲ اﻧﺘﻬﺎي ﻋﻘﺐ‬
Shell types
‫اﻧﻮاع ﭘﻮﺳﺘﻪ‬
One pass shell
‫ﭘﻮﺳﺘﻪ ﻳﻚ راﻫﻪ‬
hannel
‫ﭘﻮﺷﺶ‬
Fixed tube sheet like "A" station head
"A"‫ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﺷﺒﻴﻪ ﻛﻠﮕﻲ ﺛﺎﺑﺖ‬
And removable cover ‫ﻗﺎﺑﻞ ﺣﺮﻛﺖ و ﻛﺎﻧﺎﻟﻲ‬
Tow pass shele with incngirudhal
baffle ‫ﭘﻮﺳﺘﻪ دوراه ﺑﺎ ﺑﻔﻞ‬
Bonnet (integral cover (‫ﻛﻠﮕﻲ )ﭘﻮﺷﺶ ﭘﻮﺳﺘﻪ‬
Split flow ‫ﺟﺮﻳﺎن ﺗﻔﻜﻴﻚ ﺷﺪه‬
Fixed tube sheet like "B" station head
"B"‫ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﺷﺒﻴﻪ ﻛﻠﮕﻲ ﺛﺎﺑﺖ‬
Fixed tube sheet like "N" station head
"N"‫ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ ﺷﺒﻴﻪ ﻛﻠﮕﻲ ﺛﺎﺑﺖ‬
Outside packed floating head
‫ﻛﻠﮕﻲ ﺷﻨﺎور ﻓﺸﺮده ﺑﻴﺮوﻧﻲ‬
‫ﻓﻘﻂ دﺳﺘﻪ ﻟﻮﻟﻪ ﻣﺘﺤﺮك‬
Double split flow ‫ﺟﺮﻳﺎن ﺗﻔﻜﻴﻚ ﺷﺪه دو ﺗﺎﻳﻲ‬
‫ﭘﻮﺷﺶ ﻳﻜﭙﺎره ﺑﺎ ﺻﻔﺤﻪ‬
‫ﻟﻮﻟﻪ‬
Floating head with backing device
‫ﻛﻠﮕﻲ ﺷﻨﺎور ﺑﺎ ﺗﺠﻬﻴﺰ اﻧﺘﻬﺎﻳﻲ‬
divided flow
‫ﺟﺮﻳﺎن ﺗﻘﺴﻴﻢ ﺷﺪه‬
Foll through floating head
‫ﻛﻠﮕﻲ ﺷﻨﺎور‬
‫ﭘﻮﺷﺶ ﻳﻜﭙﺎرﭼﻪ ﺑﺎ ﺻﻔﺤﻪ‬
‫ﻟﻮﻟﻪ و ﺟﻠﺪ ﻣﺘﺤﺮك‬
Kettle type reboiler
‫ﺑﺎز ﺟﻮﺷﺎن ﻛﺘﺮي‬
U tube bundle
Special high pressure closure
‫ﻣﺤﻔﻈﻪ ﻣﺨﺼﻮص ﻓﺸﺎر ﺑﺎﻻ‬
Cross flow
‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ‬
Externally sealed flooting tubesheet
‫ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺷﻨﺎور آب ﺑﻨﺪي ﺧﺎرﺟﻲ‬
Fig. A.1-TYPE DESIGNATION BY TEMA
TEMA ‫ ﺗﻌﺮﻳﻒ ﻧﻮع ﺗﻮﺳﻂ‬1-‫ﺷﻜﻞ اﻟﻒ‬
57
U ‫دﺳﺘﻪ ﻟﻮﻟﻪ‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
APPENDIX B
TABLE B.1 - SELECTION GUIDE FOR
HEAT EXCHANGER TYPES
TYPE
DESIGNATION
‫ﺗﻌﺮﻳﻒ ﻧﻮع‬
SIGNIFICANT
FEATURE
‫وﻳﮋﮔﻲ اﺻﻠﻲ‬
IPS-E-R-PR-771(0)
‫ﭘﻴﻮﺳﺖ ب‬
‫ راﻫﻨﻤﺎي اﻧﺘﺨﺎب ﺑﺮاي اﻧﻮاع ﻣﺒﺪل ﺣﺮارﺗﻲ‬1-‫ﺟﺪول ب‬
RELATIVE COST
IN CARBON
STEEL
CONSTRUCTION
‫ﻫﺰﻳﻨﻪ ﻧﺴﺒﻲ در ﺳﺎﺧﺖ ﺑﺎ‬
APPLICATIONS BEST
SUITED
‫ﺑﻬﺘﺮﻳﻦ ﻛﺎرﺑﺮد‬
LIMITATIONS
‫ﻣﺤﺪودﻳﺖﻫﺎ‬
Condensers: liquid-liquid; gas-gas; gasliquid; cooling and heating, horizontal or
vertical, reboiling
Temperature difference at extremes of about
93°C due to differential expansion
‫ ﺑﻪ ﺧﺎﻃﺮ اﻧﺒﺴﺎط‬93°C ‫ﺣﺪاﻛﺜﺮ اﺧﺘﻼف دﻣﺎ در ﺣﺪود‬
‫ﻓﻮﻻد ﻛﺮﺑﻨﻲ‬
Fixed Tube Sheet
‫ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺛﺎﺑﺖ‬
Both tube sheets fixed to shell
‫ﻫﺮدو ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﺑﻪ ﭘﻮﺳﺘﻪ ﺛﺎﺑﺖ ﺷﺪهاﻧﺪ‬
‫ ﮔـﺎز – ﻣـﺎﻳﻊ‬،‫ ﮔـﺎز – ﮔـﺎز‬،‫ ﻣﺎﻳﻊ – ﻣـﺎﻳﻊ‬:‫ﭼﮕﺎﻟﻨﺪهﻫﺎ‬
‫ ﺑﺎز ﺟﻮﺷﺎﻧﻲ‬،‫ اﻓﻘﻲ ﻳﺎ ﻋﻤﻮدي‬،‫ﮔﺮﻣﺎﻳﺶ و ﺳﺮﻣﺎﻳﺶ‬
Floating Head or
Tube Sheet
(Removable and
non-removable
bundles)
‫ﻛﻠﮕﻲ ﺷﻨﺎور ﻳﺎ ﺻﻔﺤﻪ‬
‫ﻟﻮﻟﻪ )دﺳﺘﻪ ﻟﻮﻟﻪﻫﺎي‬
(‫ﻣﺘﺤﺮك ﻳﺎ ﻏﻴﺮ ﻣﺘﺤﺮك‬
U-Tube; U-Bundle
‫ دﺳﺘﻪ‬- ‫ ﺷﻜﻞ‬U ‫ﻟﻮﻟﻪ‬
‫ ﺷﻜﻞ‬U ‫ﻟﻮﻟﻪ‬
One tube sheet "floats" in shell or with shell,
tube bundle may or may not be removable
from shell, but back cover can be removed
to expose tube ends.
.‫ﻳﻚ ﺻﻔﺤﻪ ﻟﻮﻟﻪ در ﭘﻮﺳﺘﻪ ﻳـﺎ ﺑـﺎ ﭘﻮﺳـﺘﻪ ﺷـﻨﺎور اﺳـﺖ‬
‫دﺳﺘﻪ ﻟﻮﻟﻪ ﻣﻲﺗﻮاﻧﺪ ﻳﺎ ﻧﻤﻲﺗﻮاﻧﺪ از ﭘﻮﺳﺘﻪ ﺟﺪا ﺷﻮد اﻣـﺎ‬
‫ﭘﻮﺷﺶ اﻧﺘﻬﺎﻳﻲ ﻣﻲﺗﻮاﻧﺪ ﺑﺮاي ﻧﺸﺎن دادن اﻧﺘﻬﺎي ﻟﻮﻟﻪﻫﺎ‬
.‫ﺟﺪا ﺷﻮد‬
Only one tube sheet required. Tubes bent
in U-shape. Bundle is removable.
U ‫ ﻟﻮﻟﻪﻫﺎ ﺑﻪ ﺻﻮرت‬.‫ﻓﻘﻂ ﻳﻚ ﺻﻔﺤﻪ ﻟﻮﻟﻪ ﻻزم دارﻧﺪ‬
.‫ دﺳﺘﻪ ﻟﻮﻟﻪ ﻗﺎﺑﻞ ﺣﺮﻛﺖ اﺳﺖ‬.‫ﺧﻢ ﺷﺪهاﻧﺪ‬
High temperature differentials above about
93°C extremes; dirty fluids requiring
cleaning of inside as well as outside of
shell, horizontal or vertical.
‫ ﺳﻴﺎﻻت‬،93°C ‫اﺧﺘﻼف دﻣﺎي زﻳﺎد ﺑﺎﻻ در ﺣﺪود‬
1.0
.‫ﻣﺨﺘﻠﻒ ﻣﻲﺑﺎﺷﺪ‬
Internal gaskets offer danger of leaking.
Corrosiveness of fluids on shell side floating
parts. Usually confined to horizontal units.
‫ ﺧﻮرﻧﺪه ﺑﻮدن ﺳﻴﺎل ﺳﻤﺖ‬.‫ﻻﻳﻲ ﻫﺎي داﺧﻠﻲ ﺧﻄﺮ ﻧﺸﺘﻲ دارﻧﺪ‬
.‫ ﻋﻤﻮﻣﺎ ﺑﻪ واﺣﺪﻫﺎي اﻓﻘﻲ ﻣﺤﺪود ﺷﺪه اﺳﺖ‬.‫ﭘﻮﺳﺘﻪ اﺟﺰاء ﺷﻨﺎور‬
1.28
Bends must be carefully made or
damage and danger of rupture
Tube side velocities can cause
inside of bends. Fluid should
suspended particles.
1.08
‫ﻛﺜﻴﻒ ﻛﻪ ﻧﻴﺎز ﺑﻪ ﺗﻤﻴﺰﻛﺎري داﺧﻞ ﻣﺜﻞ ﺑﻴﺮون ﭘﻮﺳﺘﻪ‬
‫ اﻓﻘﻲ ﻳﺎ ﻋﻤﻮدي‬،‫دارﻧﺪ‬
High temperature differentials which
might require provision for expansion in
fixed tube units. Clean service or easily
cleaned conditions on both tube side and
shell side. Horizontal or vertical.
‫اﺧﺘﻼف دﻣﺎي زﻳﺎد ﻛﻪ ﻣﻤﻜﻦ اﺳﺖ ﻧﻴﺎز ﺑﻪ ﻣﻼﺣﻈﺎﺗﻲ‬
.‫ﺑﺮاي اﻧﺒﺴﺎط در واﺣﺪﻫﺎي ﻟﻮﻟﻪ ﺛﺎﺑﺖ داﺷﺘﻪ ﺑﺎﺷﺪ‬
‫ﻛﺎرﺑﺮي ﺗﻤﻴﺰ ﻳﺎ راﺣﺖ ﺗﻤﻴﺰ ﺷﻮ در ﻫﺮ دو ﺳﻤﺖ ﻟﻮﻟﻪ‬
.‫ اﻓﻘﻲ ﻳﺎ ﻋﻤﻮدي‬.‫و ﭘﻮﺳﺘﻪ‬
58
mechanical
can result.
erosion of
be free of
‫ﺧﻢﻫﺎ ﺑﺎﻳﺪ ﺑﻪ دﻗﺖ ﺳﺎﺧﺘﻪ ﺷﻮﻧﺪ ﻳﺎ ﻣﻨﺠﺮ ﺑﻪ آﺳﻴﺐ‬
‫ ﺳﺮﻋﺖ ﺳﻤﺖ ﻟﻮﻟﻪ‬.‫ﻣﻜﺎﻧﻴﻜﻲ و ﺧﻄﺮ ﭘﺎرﮔﻲ ﻣﻲ ﺷﻮﻧﺪ‬
‫ ﺳﻴﺎل ﺑﺎﻳﺪ‬.‫ﻣﻤﻜﻦ اﺳﺖ ﻣﻨﺠﺮ ﺑﻪ ﺳﺎﻳﺶ در ﺧﻢﻫﺎ ﺷﻮد‬
.‫ﻋﺎري از ذرات ﻣﻌﻠﻖ ﺑﺎﺷﺪ‬
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-R-PR-771(0)
APPENDIX B (continued)
(‫ﭘﻴﻮﺳﺖ ب )اداﻣﻪ‬
TYPE
DESIGNATION
‫ﺗﻌﺮﻳﻒ ﻧﻮع‬
SIGNIFICANT
FEATURE
‫ﻣﺸﺨﺼﺎت ﻣﻬﻢ‬
APPLICATIONS BEST
SUIITED
‫ﺑﻬﺘﺮﻳﻦ ﻛﺎرﺑﺮدﻫﺎ‬
Tube bundle removable as U-type or floating
head. Shell enlarged to allow boiling and
vapor disengaging.
.‫ ﺷﻜﻞ ﻗﺎﺑﻞ ﺟﺪاﺷـﺪن ﻳـﺎ ﻛﻠﮕـﻲ ﺷـﻨﺎور‬U ‫دﺳﺘﻪ ﻟﻮﻟﻪ‬
Boiling fluid on shell side, as refrigerant,
or process fluid being vaporized. Chilling
or cooling of tube side fluid in refrigerant
evaporation on shell side.
‫ﭘﻮﺳﺘﻪ ﺑﻪ ﺧﺎﻃﺮ ﺟﻮﺷﺶ و ﺟﺪاﺷﺪن ﺑﺨﺎر ﺑـﺰرگ ﺷـﺪه‬
.‫اﺳﺖ‬
‫ ﻳﺎ‬،‫ ﻣﺜﻞ ﺳﻴﺎل ﻣﺒﺮد‬،‫ﺳﻴﺎل ﺟﻮﺷﺎن در ﺳﻤﺖ ﭘﻮﺳﺘﻪ‬
‫ ﺗﺒﺮﻳﺪ ﻳﺎ‬.‫ﺳﻴﺎل ﻓﺮآﻳﻨﺪي ﻛﻪ ﺗﺒﺨﻴﺮ ﻣﻲﺷﻮد‬
‫ﺳﺮدﻛﺮدن ﺳﻴﺎل ﺳﻤﺖ ﻟﻮﻟﻪ ﺗﺒﺨﻴﺮ ﺗﺒﺮﻳﺪي در ﺳﻤﺖ‬
‫ﭘﻮﺳﺘﻪ‬
Each tube has own shell forming annular
space for shell side fluid. Usually use
externally finned tube.
Relatively small transfer area service,
applications. Especially suitted for high
pressures in tube above 27.6 bar (ga).
‫ ﭘﻮﺳﺘﻪ ﻣﺨﺼﻮص ﺑﻪ ﺧﻮد دارد ﻛﻪ ﻓﻀﺎي‬،‫ﻫﺮ ﻟﻮﻟﻪ‬
.‫ﺣﻠﻘﻮي را ﺑﺮاي ﺳﻴﺎل ﺳﻤﺖ ﭘﻮﺳﺘﻪ اﻳﺠﺎد ﻣﻲﻛﻨﺪ‬
.‫ﻋﻤﻮﻣﺎ از ﻟﻮﻟﻪﻫﺎي ﺑﺎ ﭘﺮه ﺑﻴﺮوﻧﻲ اﺳﺘﻔﺎده ﺷﻮد‬
‫ ﻣﺨﺼﻮﺻ ًﺎ‬،‫ﻛﺎرﺑﺮﻳﻬﺎي ﺑﺎ ﺳﻄﺢ اﻧﺘﻘﺎل ﺣﺮارت ﻛﻮﭼﻚ‬
‫ ﺑﺎر ﻧﺴﺒﻲ ﻣﻨﺎﺳﺐ‬27/6 ‫ﺑﺮاي ﻟﻮﻟﻪﻫﺎﻳﻲ ﺑﺎ ﻓﺸﺎر ﺑﺎﻻي‬
.‫اﺳﺖ‬
Pipe coil for submersion in coil-box of water
or sprayed with water is simplest type of
exchanger.
Condensing, or relatively low heat loads
on sensible transfer.
Transfer coefficient is low, requires relatively
large space if heat load is high.
‫ﭼﮕﺎﻟﺶ ﻳﺎ ﺑﺎر ﺣﺮارﺗﻲ ﻧﺴﺒﻲ ﻛﻢ در اﻧﺘﻘﺎل ﺣﺮارت‬
.‫ﻣﺤﺴﻮس‬
‫ در ﺻﻮرﺗﻲ ﻛﻪ ﺑﺎر ﺣﺮارﺗﻲ‬،‫ﺿﺮﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﻛﻢ اﺳﺖ‬
.‫زﻳﺎد ﺑﺎﺷﺪ ﺑﻪ ﻓﻀﺎي ﻧﺴﺒﺘﺎ زﻳﺎدي ﻧﻴﺎز دارد‬
LIMITATIONS
‫ﻣﺤﺪودﻳﺖﻫﺎ‬
RELATIVE COST
IN CARBON
STEEL
CONSTRUCTION
‫ﻫﺰﻳﻨﻪ ﻧﺴﺒﻲ در ﺳﺎﺧﺖ ﺑﺎ‬
‫ﻓﻮﻻد ﻛﺮﺑﻨﻲ‬
Kettle
‫ﻛﺘﺮي‬
Double Pipe
‫دوﻟﻮﻟﻪاي‬
Pipe Coil
‫ﺣﻠﻘﻪ ﻟﻮﻟﻪاي‬
‫ﺣﻠﻘﻪ ﻟﻮﻟﻪ ﺑﺮاي ﻏﻮﻃﻪ ور ﺷﺪن در ﻣﺤﻔﻈﻪ ﺣﻠﻘﻪ آب ﻳﺎ‬
.‫ ﺳﺎدهﺗﺮﻳﻦ ﻧﻮع ﻣﺒﺪل اﺳﺖ‬،‫ﺗﺤﺖ ﭘﺎﺷﺶ ﺑﺎ آب‬
59
For horizontal installation.
1.2 - 1.4
.‫ﻧﺼﺐ ﺑﻪ ﺻﻮرت اﻓﻘﻲ‬
Physically large for other applications.
.‫ﺑﺮاي ﺳﺎﻳﺮ ﻛﺎرﺑﺮدﻫﺎ از ﻧﻈﺮ ﻓﻴﺰﻳﻜﻲ ﺑﺰرگ اﺳﺖ‬
Services suitable for finned tube. Piping-up a
large number often requires cost and space.
0.8 - 1.4
‫ ﻟﻮﻟﻪﻛﺸﻲ‬.‫ﺑﺮاي ﻛﺎرﺑﺮي ﻟﻮﻟﻪﻫﺎي ﭘﺮهدار ﻣﻨﺎﺳﺐ اﺳﺖ‬
.‫ﺑﺮاي ﺗﻌﺪاد زﻳﺎد اﻏﻠﺐ ﻧﻴﺎز ﺑﻪ ﻫﺰﻳﻨﻪ و ﻓﻀﺎ دارد‬
0.5 - 0.7
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-R-PR-771(0)
APPENDIX B (continued)
(‫ﭘﻴﻮﺳﺖ ب )اداﻣﻪ‬
TYPE
DESIGNATION
‫ﺗﻌﺮﻳﻒ ﻧﻮع‬
SIGNIFICANT
FEATURE
‫ﻣﺸﺨﺼﺎت ﻣﻬﻢ‬
APPLICATIONS BEST
SUITED
‫ﺑﻬﺘﺮﻳﻦ ﻛﺎرﺑﺮد‬
LIMITATIONS
‫ﻣﺤﺪودﻳﺖﻫﺎ‬
RELATIVE COST
IN CARBON
STEEL
CONSTRUCTION
‫ﻫﺰﻳﻨﻪ ﻧﺴﺒﻲ در ﺳﺎﺧﺖ ﺑﺎ‬
‫ﻓﻮﻻد ﻛﺮﺑﻨﻲ‬
Open Tube Sections
(Water Cooled)
‫ﻗﺴﻤﺖﻫﺎي ﻟﻮﻟﻪاي ﺑﺎز‬
(‫)ﺧﻨﻚ ﻛﻨﻨﺪه ﺑﺎ آب‬
Tubes require no shell, only end headers,
usually long, water sprays over surface,
sheds scales on outside tubes by expansion
and contraction. Can also be used in water
box.
Condensing, relatively low heat loads on
sensible transfer.
‫ ﺑﺎر ﻫﺎي ﺣﺮارﺗﻲ ﻧﺴﺒﺘﺎ ﻛﻢ در اﻧﺘﻘﺎل‬،‫ﭼﮕﺎﻟﺶ‬
‫ﺣﺮارت ﻣﺤﺴﻮس‬
Transfer coefficient is low, takes up less space
than pipe coil.
0.8 - 1.1
‫ ﻓﻀﺎي ﻛﻤﺘﺮي را ﻧﺴﺒﺖ‬.‫ﺿﺮﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﻛﻢ اﺳﺖ‬
.‫ﺑﻪ ﺣﻠﻘﻪ ﻟﻮﻟﻪاي ﻣﻲﮔﻴﺮد‬
‫ اﻏﻠﺐ‬،‫ ﻓﻘﻂ ﻛﻠﮕﻲ اﻧﺘﻬﺎﻳﻲ‬،‫ﻟﻮﻟﻪ ﻫﺎ ﺑﻪ ﭘﻮﺳﺘﻪ ﻧﻴﺎز ﻧﺪارﻧﺪ‬
-‫ رﺳﻮﺑﻬﺎ در ﻟﻮﻟﻪ‬،‫ آب روي ﺳﻄﺢ ﭘﺎﺷﻴﺪه ﻣﻲﺷﻮد‬،‫ﺑﻠﻨﺪ‬
‫ در‬.‫ﻫﺎي ﺑﻴﺮوﻧﻲ در اﺛﺮ اﻧﺒﺴﺎط و اﻧﻘﺒﺎض ﻣﻲرﻳﺰﻧﺪ‬
.‫ﻣﺤﻔﻈﻪ آب ﻧﻴﺰ ﻣﻲﺗﻮاﻧﺪ اﺳﺘﻔﺎده ﺷﻮﻧﺪ‬
Open Tube Sections
(Air Cooled) Plain or
finned tubes
‫ﻗﺴﻤﺖﻫﺎي ﻟﻮﻟﻪاي ﺑﺎز‬
(‫)ﺧﻨﻚ ﻛﻨﻨﺪه ﻫﻮاﻳﻲ‬
‫ﻟﻮﻟﻪﻫﺎي ﺳﺎده ﻳــﺎ ﭘﺮهدار‬
Plate and Frame
‫ﺻﻔﺤﻪ و ﻗﺎب‬
No shell required, only end headers similar
to water units.
‫ﺣﻠﺰوﻧﻲ‬
.‫ اﻧﺘﻘﺎل ﺣﺮارت زﻳﺎد‬،‫ﭼﮕﺎﻟﺶ‬
‫ ﻓﻘﻂ ﻛﻠﮕﻲ اﻧﺘﻬﺎﻳﻲ ﻣﺜﻞ ﻧﻮع‬،‫ﻧﻴﺎز ﺑﻪ ﭘﻮﺳﺘﻪ ﻧﻴﺴﺖ‬
.‫ﺧﻨﻚ ﻛﻨﻨﺪه ﺑﺎ آب‬
Composed of metal-formed thin plates
separated by gaskets. Compact, easy to
clean.
‫از ﺻﻔﺤﺎت ﻓﻠﺰي ﻧﺎزك ﺷﻜﻞ داده ﺷﺪه ﻛﻪ ﺗﻮﺳﻂ ﻻﻳﻲ‬
،‫ ﻓﺸﺮده‬.‫ﻫﺎ از ﻫﻢ ﺟﺪا ﺷﺪه اﻧﺪ ﺳﺎﺧﺘﻪ ﺷﺪه اﺳﺖ‬
.‫ﺗﻤﻴﺰﻛﺎري راﺣﺖ‬
Spiral
Condensing, high level heat transfer.
Compact, concentric plates;
no bypassing, high turbulence.
Transfer coefficient is low, if natural
convection circulation, but is improved with
forced air flow across tubes.
0.8 - 1.8
‫اﮔﺮ ﺟﺎﺑﺠﺎﻳﻲ ﮔﺮدﺷﻲ ﻃﺒﻴﻌﻲ ﺑﺎﺷﺪ ﺿﺮﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت‬
‫ اﻣﺎ ﺑﺎ ﺟﺮﻳﺎن اﺟﺒﺎري ﻫﻮا در ﻣﻘﻄﻊ ﻟﻮﻟﻪﻫﺎ‬،‫ﻛﻢ اﺳﺖ‬
.‫اﻓﺰاﻳﺶ ﻣﻲﻳﺎﺑﺪ‬
Viscous fluids, corrosive fluids slurries,
High heat transfer.
‫ اﻧﺘﻘﺎل‬، ‫ ﺳﻴﺎﻻت دوﻏﺎﺑﻲ ﺧﻮرﻧﺪه‬،‫ﺳﻴﺎﻻت ﮔﺮاﻧﺮو‬
.‫ﺣﺮارت ﺑﺎﻻ‬
Not well suited for boiling or condensing;
limit 177-260°C by gaskets. Used for LiquidLiquid only; not gas-gas.
-260°C ‫ ﺗﺎ‬.‫ﺑﺮاي ﭼﻜﺎﻟﺶ و ﺟﻮﺷﺶ ﻣﻨﺎﺳﺐ ﻧﻴﺴﺘﻨﺪ‬
Cross-flow, condensing, heating
Process corrosion, suspended materials.
‫ ﮔﺮﻣﺎﻳﺶ‬،‫ ﭼﮕﺎﻟﺶ‬،‫ﺟﺮﻳﺎن ﻣﺘﻘﺎﻃﻊ‬
0.8 – 1.5
‫ ﻓﻘﻂ ﺑﺮاي ﻣﺎﻳﻊ – ﻣﺎﻳﻊ‬،‫ ﺗﻮﺳﻂ ﻻﻳﻲ ﻣﺤﺪود ﺷﺪهاﻧﺪ‬177
.‫ ﻧﻪ ﮔﺎز – ﮔﺎز‬،‫ﺑﻪ ﻛﺎر ﻣﻲروﻧﺪ‬
0.8 - 1.5
‫ ﻣﻮاد ﻣﻌﻠﻖ‬، ‫ﺧﻮردﮔﻲ ﻓﺮآﻳﻨﺪي‬
‫ ﺗﻼﻃﻢ ﺑﺎﻻ‬،‫ ﺻﻔﺤﺎت ﻫﻢ ﻣﺮﻛﺰ ﺑﺪون ﻛﻨﺎرﮔﺬر‬،‫ﻓﺸﺮده‬
Small-tube Teflon
‫ﻟﻮﻟﻪ ﻛﻮﺗﺎه ﺗﻔﻠﻮﻧﻲ‬
Chemical resistance of tubes; no tube
fouling.
Clean fluids, condensing, cross-exchange.
.‫ ﺗﺒﺎدل ﻣﻘﻄﻌﻲ‬،‫ ﭼﮕﺎﻟﺶ‬،‫ﺳﻴﺎﻻت ﺗﻤﻴﺰ‬
‫ ﺑﺪون رﺳﻮب در ﻟﻮﻟﻪﻫﺎ‬،‫ﻣﻘﺎوﻣﺖ ﺷﻴﻤﻴﺎﻳﻲ ﻟﻮﻟﻪﻫـﺎ‬
60
Low heat transfer coefficient.
‫ﺿﺮﻳﺐ اﻧﺘﻘﺎل ﺣﺮارت ﻛﻢ‬
2.0 - 4.0
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
APPENDIX C
TYPICAL TEMA RECOMMEND FOULING
RESISTANCES FOR INDUSTRIAL FLUIDS
IPS-E-R-PR-771(0)
‫ﭘﻴﻮﺳﺖ ج‬
‫ ﺑﺮاي‬TEMA ‫ﻧﻤﻮﻧﻪ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮب ﭘﻴﺸﻨﻬﺎدي‬
‫ﺳﻴﺎﻻت ﺻﻨﻌﺘﻲ‬
TABLE C.1 - TYPICAL FOULING RESISTANCES FOR INDUSTRIAL FLUIDS
‫ ﻣﻘﺎوﻣﺖﻫﺎي رﺳﻮب ﮔﺮﻓﺘﮕﻲ ﺑﺮاي ﺳﻴﺎﻻت ﺻﻨﻌﺘﻲ‬1-‫ﺟﺪول ج‬
Oils:
:‫روﻏﻦﻫﺎ‬
# 2 ‫ﻧﻔﺖ ﻛﻮره‬
# 6 ‫ﻧﻔﺖ ﻛﻮره‬
‫روﻏﻦ ﺗﺮاﻧﺴﻔﻮرﻣﺮ‬
‫روﻏﻦ رواﻧﻜﺎري ﻣﻮﺗﻮر‬
‫روﻏﻦ ﺧﻨﻚ ﻛﻦ‬
Fuel Oil #2
Fuel Oil #6
Transformer Oil
Engine Lube Oil
Quench Oil
Gases and Vapors:
‫ﮔﺎز ﺳﺎﺧﺘﻪ ﺷﺪه‬
‫ﮔﺎز ﺧﺮوﺟﻲ ﻣﻮﺗﻮر‬
(‫ﺑﺨﺎر )ﻳﺎﺗﺎﻗﺎن ﻏﻴﺮ روﻏﻨﻲ‬
(‫ﺑﺨﺎر ﺧﺮوﺟﻲ )ﻳﺎﺗﺎﻗﺎن روﻏﻨﻲ‬
(‫ﺑﺨﺎرات ﻣﺒﺮد )ﻳﺎﺗﺎﻗﺎن روﻏﻨﻲ‬
‫ﻫﻮاي ﻓﺸﺮده‬
‫ﺑﺨﺎر آﻣﻮﻧﻴﺎك‬
CO2‫ﺑﺨﺎر‬
‫ﺑﺨﺎر ﻛﻠﺮ‬
‫ﮔﺎز ﺣﺎﺻﻞ از اﺣﺘﺮاق ذﻏﺎل‬
‫ﮔﺎز ﺣﺎﺻﻞ از اﺣﺘﺮاق ﮔﺎز ﻃﺒﻴﻌﻲ‬
Engine exhaust Gas
Steam (Non-Oil Bearing)
Exhaust Steam (Oil Bearing)
Refrigerant Vapors (Oil Bearing)
Compressed Air
Ammonia Vapor
CO2 Vapor
Chlorine Vapor
Coal Flue Gas
Natural Gas Flue Gas
Molten Heat Transfer Salts
Refrigerant Liquids
Hydraulic Fluid
Industrial Organic Heat Transfer Media
Ammonia Liquid
Ammonia Liquid (Oil Bearing)
Calcium Chloride Solutions
Sodium Chloride Solutions
CO2 Liquid
Chlorine Liquid
Methanol Solutions
Ethanol Solutions
Ethylene Glycol Solutions
0.00035
0.00085
0.00017
0.00017
0.0007
:‫ﮔﺎزﻫﺎ و ﺑﺨﺎرات‬
Manufactured Gas
Liquids:
M².°C/W
:‫ﻣﺎﻳﻌﺎت‬
‫ﻧﻤﻚﻫﺎي ﻣﺬاب اﻧﺘﻘﺎل ﺣﺮارت‬
‫ﻣﺎﻳﻌﺎت ﺗﺒﺮﻳﺪي‬
‫ﺳﻴﺎل ﻫﻴﺪروﻟﻴﻜﻲ‬
‫ﺳﻴﺎل آﻟﻲ ﺻﻨﻌﺘﻲ اﻧﺘﻘﺎل ﺣﺮارت‬
‫آﻣﻮﻧﻴﺎك ﻣﺎﻳﻊ‬
(‫آﻣﻮﻧﻴﺎك ﻣﺎﻳﻊ )ﻳﺎﺗﺎﻗﺎن روﻏﻨﻲ‬
‫ﻣﺤﻠﻮلﻫﺎي ﻛﻠﺮﻳﺪ ﻛﻠﺴﻴﻢ‬
‫ﻣﺤﻠﻮلﻫﺎي ﻛﻠﺮﻳﺪ ﺳﺪﻳﻢ‬
‫ﻣﺎﻳﻊ‬CO2
‫ﻣﺎﻳﻊ ﻛﻠﺮ‬
‫ﻣﺤﻠﻮلﻫﺎي ﻣﺘﺎﻧﻮل‬
‫ﻣﺤﻠﻮلﻫﺎي اﺗﺎﻧﻮل‬
‫ﻣﺤﻠﻮلﻫﺎي اﺗﻴﻠﻦ ﮔﻠﻴﻜﻮل‬
61
0.0017
0.0017
0.000085
0.000255 - 0.00035
0.00035
0.00017
0.00017
0.00017
0.00035
0.00017
0.00085
0.000088
0.00017
0.00017
0.00035
0.00017
0.000528
0.000528
0.000528
0.00017
0.00035
0.00035
0.00035
0.00035
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-R-PR-771(0)
FOULING RESISTANCES FOR CHEMICAL PROCESSING STREAMS
‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﺑﺮاي ﺟﺮﻳﺎنﻫﺎي ﻓﺮآﻳﻨﺪي ﺷﻴﻤﻴﺎﻳﻲ‬
Gases and Vapors:
:‫ﮔﺎزﻫﺎ و ﺑﺨﺎرﻫﺎ‬
‫ﮔﺎزﻫﺎي اﺳﻴﺪي‬
‫ﺑﺨﺎرات ﺣﻼل‬
‫ﻣﺤﺼﻮﻻت ﭘﺎﻳﺪار ﺑﺎﻻﺳﺮي‬
Acid Gases
Solvent Vapors
Stable Overhead Products
Liquids:
MEA ‫ و‬DEA ‫ﻣﺤﻠﻮلﻫﺎي‬
DEG and TEG Solutions
DEG ‫و‬TEG ‫ﻣﺤﻠﻮلﻫﺎي‬
Stable Side Draw and Bottom Product
Vegetable Oils
0.00017
0.00017
:‫ﻣﺎﻳﻌﺎت‬
MEA and DEA Solutions
Caustic Solutions
0.00035 - 0.000528
‫ﻣﺤﺼﻮل ﭘﺎﻳﺪار ﺟﺎﻧﺒﻲ و ﭘﺎﻳﻴﻨﻲ‬
‫ﻣﺤﻠﻮلﻫﺎي ﺳﻮد ﺳﻮز آور‬
‫روﻏﻦﻫﺎي ﻧﺒﺎﺗﻲ‬
0.00035
0.00035
0.00017 - 0.00035
0.00035
0.000528
FOULING RESISTANCES FOR NATURAL GAS-GASOLINE PROCESSING STREAMS
‫ ﺑﻨﺰﻳﻦ‬- ‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﺑﺮاي ﺟﺮﻳﺎنﻫﺎي ﻓﺮآﻳﻨﺪي ﮔﺎز‬
Gases and Vapors:
Natural Gas
Overhead Products
Liquids:
Lean Oil
:‫ﮔﺎزﻫﺎ و ﺑﺨﺎرﻫﺎ‬
‫ﮔﺎز ﻃﺒﻴﻌﻲ‬
‫ﻣﺤﺼﻮﻻت ﺑﺎﻻﺳﺮي‬
:‫ﻣﺎﻳﻌﺎت‬
(‫روﻏﻦ ﻋﺎري ﺷﺪه)رﻗﻴﻖ‬
‫روﻏﻦ ﻏﻨﻲ‬
Rich Oil
Natural Gasoline and Liquefied Petroleum Gases
0.00017 - 0.00035
0.00017 - 0.00035
0.00035
0.00017 - 0.00035
0.00017 - 0.00035
‫ﺑﻨﺰﻳﻦ ﻃﺒﻴﻌﻲ و ﮔﺎزﻫﺎي ﻧﻔﺘﻲ ﻣﺎﻳﻊ ﺷﺪه‬
(to be continued)
62
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-R-PR-771(0)
TABLE C.1 (continued)
TYPICAL FOULING RESISTANCES FOR OIL REFINERY STREAMS
(‫ )اداﻣﻪ‬1-‫ﺟﺪول ج‬
‫ﻧﻤﻮﻧﻪ ﻣﻘﺎوﻣﺖ رﺳﻮب ﺑﺮاي ﺟﺮﻳﺎنﻫﺎي ﭘﺎﻻﻳﺸﮕﺎه ﻧﻔﺖ‬
Crude and Vacuum Unit Gases and Vapors:
:‫ﮔﺎزﻫﺎ وﺑﺨﺎرات واﺣﺪ ﻧﻔﺖ ﺧﺎم و ﺧﻼء‬
Atmospheric Tower Overhead Vapors
‫ﺑﺨﺎرات ﺑﺎﻻﺳﺮي ﺑﺮج اﺗﻤﺴﻔﺮﻳﻚ‬
0.00017
‫ﻧﻔﺘﺎي ﺳﺒﻚ‬
0.00017
‫ﺑﺨﺎرات ﺑﺎﻻﺳﺮي ﺧﻼء‬
0.00035
Light Naphthas
Vacuum Overhead Vapors
Crude and Vacuum Liquids:
:‫ﻣﺎﻳﻌﺎت ﻧﻔﺖ ﺧﺎم و ﺧﻼء‬
Crude Oil
‫ﻧﻔﺖ ﺧﺎم‬
-17 to 121°C
Velocity (m/s)
(m/s) ‫ﺳﺮﻋﺖ‬
‫ﺧﺸﻚ‬
< 0.6
0.00053
0.6 - 1.2
0.00035
> 1.2
0.00035
< 0.6
0.00053
0.6 - 1.2
0.00035
> 1.2
0.00035
*‫ﻧﻤﻚ‬
0.00053
0.00035
0.00035
0.00088
0.000704
0.000704
Dry
Salt*
121 to 176°C
Velocity (m/s)
(m/s) ‫ﺳﺮﻋﺖ‬
0.00053
176 to 232°C
Velocity (m/s)
(m/s) ‫ﺳﺮﻋﺖ‬
232°C and over
Velocity (m/s)
(m/s) ‫ﺳﺮﻋﺖ‬
Dry
‫ﺧﺸﻚ‬
< 0.6
0.704
0.6 - 1.2
0.00053
> 1.2
0.00053
< 0.6
0.00088
0.6 - 1.2
0.000704
> 1.2
0.000704
Salt*
*‫ﻧﻤﻚ‬
1.056
0.00088
0.00088
0.00123
0.00106
0.00106
* Assumes desalting @ approx. 121°C
Gasoline
Naphtha and Light Distillates
Kerosene
Light Gas Oil
Heavy Fuel Oils
Heavy Gas Oil
Asphalt and Residuum:
Vacuum Tower Bottoms
- Atmospheric Tower Bottoms
Cracking and Coking Unit Streams:
Overhead Vapors
Light Cycle Oil
Heavy Cycle Oil
Light Coker Gas Oil
Heavy Coker Gas Oil
Bottoms Slurry Oil (1.35 m/s minimum)
Light Liquid Products
121°Cً‫* ﺑﺎ ﻓﺮض ﻧﻤﻚ زداﻳﻲ در ﺗﻘﺮﻳﺒﺎ‬
‫ﺑﻨﺰﻳﻦ‬
‫ﻧﻔﺘﺎ و ﺗﻘﻄﻴﺮﺷﺪه ﺳﺒﻚ‬
‫ﻧﻔﺖ ﺳﻔﻴﺪ‬
‫ﮔﺎزوﻳﻴﻞ ﺳﺒﻚ‬
‫ﻧﻔﺖ ﻛﻮرهﻫﺎي ﺳﻨﮕﻴﻦ‬
‫ﮔﺎزوﻳﻴﻞ ﺳﻨﮕﻴﻦ‬
:‫آﺳﻔﺎﻟﺖ و ﺗﻪ ﻣﺎﻧﺪ‬
‫ﺗﻪ ﻣﺎﻧﺪه ﺑﺮج ﺧﻼء‬
‫ﺗﻪ ﻣﺎﻧﺪه ﺑﺮج اﺗﻤﺴﻔﺮﻳﻚ‬
:‫ﺟﺮﻳﺎنﻫﺎي واﺣﺪ ﺷﻜﺴﺖ ﻣﻮﻟﻜﻮﻟﻲ و ﻛﻚ ﺳﺎزي‬
‫ﺑﺨﺎرات ﺑﺎﻻﺳﺮي‬
‫روﻏﻦ ﮔﺮدﺷﻲ ﺳﺒﻚ‬
‫روﻏﻦ ﮔﺮدﺷﻲ ﺳﻨﮕﻴﻦ‬
‫ﮔﺎزوﻳﻴﻞ ﺳﺒﻚ ﻛﻚ ﺳﺎزي‬
‫ﮔﺎزوﻳﻴﻞ ﺳﻨﮕﻴﻦ ﻛﻚ ﺳﺎزي‬
(1/35 ‫روﻏﻦ دوﻏﺎﺑﻲ ﺗﻪ ﻣﺎﻧﺪ )ﺣﺪاﻗﻞ‬
‫ﻣﺤﺼﻮﻻت ﻣﺎﻳﻊ ﺳﺒﻚ‬
0.00035
0.00035 - 0.000528
0.00035 - 0.000528
0.00035 - 0.000528
0.000528 - 0.00088
0.00088 - 0.00123
0.00017
0.00123
0.00035
0.00035 - 0.000528
0.000528 - 0.000704
0.000528 - 0.000704
0.000704 - 0.00088
0.000528
0.00035
Catalytic Reforming, Hydrocracking and Hydrodesulfurization Streams:
:‫ ﺷﻜﺴﺖ ﺑﺎ ﻫﻴﺪروژن و ﺳﻮﻟﻔﻮرزداﻳﻲ ﺑﺎ ﻫﻴﺪروژن‬،‫ﺟﺮﻳﺎنﻫﺎي ﺗﺒﺪﻳﻞ ﻛﺎﺗﺎﻟﻴﺴﺘﻲ‬
Reformer Charge
‫ﺧﻮراك واﺣﺪ ﺗﺒﺪﻳﻞ‬
Reformer Effluent
‫ﺧﺮوﺟﻲ واﺣﺪ ﺗﺒﺪﻳﻞ‬
Hydrocracker Charge and Effluent*
* ‫ورودي و ﺧﺮوﺟﻲ واﺣﺪ ﺷﻜﺴﺖ ﺑﺎ ﻫﻴﺪروژن‬
Recycle Gas
‫ﮔﺎزﻫﺎي ﺑﺎزﮔﺸﺘﻲ‬
63
0.000264
0.000264
0.00035
0.00017
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-R-PR-771(0)
TABLE C.1 (continued)
(‫ )اداﻣﻪ‬1-‫ﺟﺪول ج‬
Hydrodesulfurization Charge and Effluent*
Overhead Vapors
Liquid Product Over 50° API
Liquid Product 30 - 50° API
* ‫ورودي و ﺧﺮوﺟﻲ واﺣﺪ ﺳﻮﻟﻔﻮر زداﻳﻲ ﺑﺎ ﻫﻴﺪروژن‬
0.00035
‫ﺑﺨﺎرات ﺑﺎﻻﺳﺮي‬
50API‫ﻣﺤﺼﻮﻻت ﻣﺎﻳﻊ ﺑﺎﻻي‬
30- 50 API ‫ﻣﺤﺼﻮﻻت ﻣﺎﻳﻊ‬
0.00017
0.00017
0.00035
* Depending on charge, characteristics and storage history, charge resistance may be many times this value.
.‫ ﻣﺸﺨﺼﺎت و ﺳﺎﺑﻘﻪ اﻧﺒﺎرش ﻣﻤﻜﻦ اﺳﺖ اﻛﺜﺮ ﻣﻮاﻗﻊ اﻳﻦ ﻣﻘﺪار ﺑﺎﺷﺪ‬،‫ ﺑﺴﺘﻪ ﺑﻪ ﺧﻮراك‬،‫*ﻣﻘﺎوﻣﺖ ﺧﻮراك‬
Light Ends Processing Streams:
Overhead Vapors and Gases
Liquid Products
Absorption Oils
Alkylation Trace Acid Streams
Reboiler Streams
Lube Oil Processing Streams:
Feed Stock
Solvent Feed Mix
Solvent
Extract*
:‫ﺟﺮﻳﺎنﻫﺎي ﻓﺮآﻳﻨﺪي ﺑﺮﺷﻬﺎي ﺳﺒﻚ‬
‫ﺑﺨﺎرﻫﺎ و ﮔﺎزﻫﺎي ﺑﺎﻻﺳﺮي‬
‫ﻣﺤﺼﻮﻻت ﻣﺎﻳﻊ‬
‫روﻏﻦﻫﺎي ﺟﺎذب‬
‫ﺟﺮﻳﺎنﻫﺎي ﻛﻢ اﺳﻴﺪي آﻟﻜﻴﻼﺳﻴﻮن‬
‫ﺟﺮﻳﺎنﻫﺎي ﺑﺎز ﺟﻮﺷﺎﻧﻨﺪه‬
:‫ﺟﺮﻳﺎنﻫﺎي ﻓﺮآﻳﻨﺪي روﻏﻦ روان ﻛﺎري‬
‫ﺧﻮراك‬
‫ﻣﺨﻠﻮط ﺣﻼل و ﺧﻮراك‬
‫ﺣﻼل‬
*‫ﻋﺼﺎره‬
Raffinate
Asphalt
Wax Slurries*
Refined Lube Oil
‫ﺗﺼﻔﻴﻪ ﺷﺪه‬
‫آﺳﻔﺎﻟﺖ‬
*‫دوﻏﺎب ﻣﻮم‬
‫روﻏﻦ روان ﻛﺎري ﺗﺼﻔﻴﻪ ﺷﺪه‬
0.00017
0.00017
0.00035 - 0.000528
0.00035
0.00035 - 0.000528
0.00035
0.00035
0.00017
0.000528
0.00017
0.00088
0.000528
0.00017
*Precautions must be taken to prevent wax deposition on cold tube walls.
.‫ اﺣﺘﻴﺎط ﻻزم ﺑﺎﻳﺪ اﻧﺠﺎم ﺷﻮد‬،‫*ﺑﺮاي ﺟﻠﻮﮔﻴﺮي از ﺗﻪ ﻧﺸﻴﻨﻲ ﻣﻮم در دﻳﻮاره ﻟﻮﻟﻪ ﺳﺮد‬
Visbreaker:
Overhead Vapor
Visbreaker Bottoms
:‫واﺣﺪ ﻛﺎﻫﺶ ﮔﺮاﻧﺮوي‬
‫ﺑﺨﺎرات ﺑﺎﻻﺳﺮي‬
‫ﺗﻪ ﻣﺎﻧﺪﻫﺎي ﺑﺮج ﻛﺎﻫﺶ ﮔﺮاﻧﺮوي‬
Naphtha Hydrotreater:
:‫ﻓﺮآوري ﻫﻴﺪروژﻧﻲ ﻧﻔﺘﺎ‬
‫ﺧﻮراك‬
‫ﺧﺮوﺟﻲ‬
‫ﻧﻔﺘﺎﻫﺎ‬
‫ﺑﺨﺎرات ﺑﺎﻻﺳﺮي‬
Feed
Effluent
Naphthas
Overhead Vapors
Catalytic Hydro Desulfurizer:
Charge
Effluent
HT Sep. Overhead
Stripper Charge
Liquid Products
:‫ﺳﻮﻟﻔﻮرزداﻳﻲ ﻫﻴﺪروژﻧﻲ ﻛﺎﺗﺎﻟﻴﺴﺘﻲ‬
‫ﺧﻮراك‬
‫ﺧﻮراك ﺧﺮوﺟﻲ‬
‫ﺑﺎﻻﺳﺮي ﺟﺪاﻛﻨﻨﺪه دﻣﺎي ﺑﺎﻻ‬
‫ﺧﻮراك ﻋﺎري ﺳﺎز‬
‫ﻣﺤﺼﻮﻻت ﻣﺎﻳﻊ‬
HF Alky Unit:
Alkylate, Deprop. Bottoms, Main Fract. Overhead, Main Fract. Feed
0.0017
0.000528
0.00035
0.00035
0.000204
0.000704 - 0.00088
0.00035
0.00035
0.000528
0.00035
:HF‫واﺣﺪ آﻟﻜﺎﻟﻲ‬
‫ ﺧﻮراك ﺑﺮج ﺗﻔﻜﻴﻚ ﻛﻨﻨﺪه اﺻﻠﻲ‬،‫ ﺑﺎﻻﺳﺮي ﺑﺮج ﺗﻔﻜﻴﻚ ﻛﻨﻨﺪه اﺻﻠﻲ‬،‫ ﺗﻪ ﻣﺎﻧﺪ ﺑﺮج ﭘﺮوﭘﺎن زدا‬،‫آﻟﻜﻴﻼت‬
All Other Process Streams
‫ﺳﺎﻳﺮ ﺟﺮﻳﺎنﻫﺎي ﻓﺮآﻳﻨﺪي‬
64
0.000528
0.000528
0.00035
Oct. 2009 / 1388 ‫ﻣﻬﺮ‬
IPS-E-R-PR-771(0)
FOULING RESISTANCES FOR WATER
‫ﻣﻘﺎوﻣﺖ رﺳﻮب ﺑﺮاي آب‬
Temperature of Heating Medium*
Up to 116°C
116 to 204°C
51°C
Over 51°C
Water Velocity (m/s)
(m/s)‫ﺳﺮﻋﺖ آب‬
Water Velocity (m/s)
(m/s)‫ﺳﺮﻋﺖ آب‬
‫دﻣﺎي ﺳﻴﺎل ﮔﺮم ﻛﻨﻨﺪه‬
Temperature of Water
‫دﻣﺎي آب‬
0.9 and Less
0.000088
Over 0.9
0.000088
0.9 and Less
0.00017
Over 0.9
0.00017
0.00035
0.00017
0.000528
0.00035
‫ﺟﺒﺮاﻧﻲ ﺗﺼﻔﻴﻪ ﺷﺪه‬
0.00017
0.00017
0.00035
0.000704
‫ﺗﺼﻔﻴﻪ ﻧﺸﺪه‬
0.000528
0.000528
0.00088
0.00035
0.00017
0.00017
0.00035
0.00035
‫ﺣﺪاﻗﻞ‬
0.00035
0.00017
0.000528
0.00035
‫ﻣﻴﺎﻧﮕﻴﻦ‬
0.000528
0.00035
0.000704
0.000528
Sea Water
‫آب درﻳﺎ‬
Brackish Water
‫آب ﺷﻮر‬
Cooling Tower and Artificial Spray Pond:
:‫ﺑﺮج ﺧﻨﻚ ﻛﻨﻨﺪه و اﺳﺘﺨﺮ ﭘﺎﺷﺶ ﻣﺼﻨﻮﻋﻲ‬
Treated Make Up
Untreated
City or Well Water
River Water:
Minimum
Average
‫آب ﺷﻬﺮ ﻳﺎ ﭼﺎه‬
:‫آب رودﺧﺎﻧﻪ‬
Muddy or Silty
‫ﮔﻞ آﻟﻮد ﻳﺎ ﻟﺠﻨﻲ‬
0.000528
0.00035
0.000704
0.000528
Hard (over 258 g/m³)
(258 ‫ﺳﺨﺖ )ﺑﺎﻻي‬
0.000528
0.000528
0.00088
0.00088
‫ﺟﺪاره ﻣﻮﺗﻮر‬
0.00017
0.00017
0.00017
0.00017
0.000088
0.000088
0.000088
0.000088
0.00017
0.000088
0.00017
0.00017
Engine Jacket
Distilled or Closed Cycle
Condensate
‫ﭼﺮﺧﻪ ﺑﺴﺘﻪ ﻳﺎ آب ﻣﻘﻄﺮ‬
‫ﭼﮕﺎﻟﻴﺪه‬
Treated Boiler Feedwater ‫آب ﺗﺼﻔﻴﻪ ﺷﺪه ﺧﻮراك دﻳﮓ ﺑﺨﺎر‬
Boiler Blowdown
‫دور رﻳﺰ دﻳﮓ ﺑﺨﺎر‬
0.00035
0.00035
0.00035
0.00035
* If the heating medium temperature is over 204°C and the cooling medium is known to scale, these ratings should be modified
accordingly.
.‫ اﻳﻦ دﺳﺘﻪﺑﻨﺪي ﺑﺎﻳﺪ ﻣﺘﻨﺎﺳﺒﺎً اﺻﻼح ﺷﻮد‬،‫ و ﺳﻴﺎل ﺳﺮد ﺑﻪ ﻋﻨﻮان رﺳﻮب ﻛﻨﻨﺪه ﺷﻨﺎﺧﺘﻪ ﺷﻮد‬204°C‫*اﮔﺮ دﻣﺎ ﺳﻴﺎل ﮔﺮم ﻛﻨﻨﺪه ﺑﺎﻻﺗﺮ از‬
65