Production of Gasoline from Syn Gas
Team Alpha
Ayesha Rizvi
Bernard Hsu
Jeff Tyska
Mohammed Shehadeh
Yacoub Awwad
Mentor
Dan Rusinak- Middough
1
Spring 2011
Table of Contents
1.
Abstract ................................................................................................................................................. 3
2.
Executive Summary ............................................................................................................................... 4
3.
Discussion.............................................................................................................................................. 7
4.
Recommendations and Conclusions ..................................................................................................... 8
5.
Appendices .......................................................................................................................................... 10
6.
7.
5.1.
Design Basis................................................................................................................................. 10
5.2.
Block Flow Diagram ..................................................................................................................... 10
5.3.
Process Flow Diagram ................................................................................................................. 11
Material and Energy Balance .............................................................................................................. 17
6.1.
Material Balance ......................................................................................................................... 17
6.2.
Energy Balance ............................................................................................................................ 24
Calculations ......................................................................................................................................... 24
7.1.
Aspen Streams ............................................................................................................................ 24
8.
Annotated Equipment List (Data Sheets)............................................................................................ 24
9.
Economic Evaluation ........................................................................................................................... 25
9.1.
Annual Revenue .......................................................................................................................... 25
9.2.
Annual Operating Costs .............................................................................................................. 26
9.3.
Capital Costs ................................................................................................................................ 28
9.4.
Simple Payback ........................................................................................................................... 28
10. Utilities ................................................................................................................................................ 29
11. Conceptual Control Scheme ............................................................................................................... 29
12. Major Equipment Layout .................................................................................................................... 29
13. Distribution and End-Use Issues Review ............................................................................................. 29
14. Constraints Review ............................................................................................................................. 29
15. Project Communication File ................................................................................................................ 29
2
1. Abstract
One of the largest problems facing this country is the current energy crisis. World oil
production peaked in 2005, and prices have been going up in recent years. Much of the U.S.’s
oil is also imported, leading to reduced energy independence. Due to this crisis, many methods
of producing liquid fuels for transportation and heating are being researched. One way to help
abate the current problem is to make gasoline and liquified petroleum gas (LPG) from
renewable sources. Our project will take municipal solid waste-derived syngas (H2 and CO) and
convert it into gasoline, which can be blended in a refinery, and LPG, which can be used for
heating or as a fuel for specially modified automobiles. Our gasoline and LPG will also have a
smaller carbon footprint than fossil fuel derived gasoline and LPG. By using this process, a
renewable and local fuel can be produced which will fit into the current infrastructure. The first
step of our process will be taking syngas with an H2 to CO ratio of 2:1 and turning it into
Methanol. Methanol will then react over the ZSM-5 catalyst to produce a mixture of
hydrocarbons. Hydrocarbons will be separated by distillation, and a product stream of C5+
gasoline and LPG will be produced and sold. Our process is based upon the Mobil Process,
which has been demonstrated in a plant in New Zealand which produced about 14,000 barrels
of gasoline per day.
3
2. Executive Summary
In the United States, gasoline is derived from the processing of oil. In 1970, domestic
production of oil peaked and imports sharply rose, and by 1995, oil imports had exceeded
domestic production. A barrel of oil constitutes 42 gallons. On average, according to the
United States Energy Information Administration (EIA), 19.36 gallons of gasoline are generated
from a single barrel of crude oil. This means that 43% of a barrel of oil translates to gasoline.
(cite http://tonto.eia.doe.gov/country/index.cfm?view=production). The EIA stated in 2009,
Americans used 3.3x109 barrels of gasoline—about 1.38x1011 gallons in a single year.
Figure 1
4
Consequently, the prices of gasoline peaked on July 4, 2008 at a national average of
$4.11/gallon as shown in Figure 2-2. The prices dropped sharply in Q1 2009, however they
have been on the increasing trend once again. Because of international crises littering the
Middle East in 2011, and with the United States becoming ever increasingly dependent on
imported, foreign oil, the price of oil is largely variable, thus leading to unstable prices in
gasoline. Energy independence is thus an impeccable and indispensible quality that must be
pursued with rigorous research and innovation. The first step towards energy independence
would be to produce gasoline, the largest use derived from crude oil, from renewable
resources.
Figure 2
The project begins with syngas obtained from municipal solid waste. The syngas is
delivered to our chemical production plant in a 2:1 H2:CO ratio and Methanol is produced. The
aim is to produce gasoline components, mainly C5+ hydrocarbons, from Methanol. The process
will produce 3000 tons per day of Methanol, which will be used to produce 16,300 barrels per
day of C5+ Gasoline and 4,350 barrels per day of LPG. The MTG process will run in four reactors
in parallel and will use the ZSM-5 catalyst. The Methanol reactor will be modeled as a shell and
5
tube heat exchanger using the typical copper/zinc/alumina catalyst. The Methanol reactor has
a syngas recycle stream and 2% of the total syngas is purged in order to maintain the correct
2:1 ratio. The methanol flows into the four MTG reactors and produces a hydrocarbons-withwater stream. The hydrocarbons are separated from water and then enter 3 distillation
columns. The final product from these columns is the LPG and the gasoline product. Start-up
will be conducted with energy from the syngas feed. This process was demonstrated in New
Zealand, in a plant that produced 14,000 barrels of gasoline per day.
The Total Installed Cost of the entire process was quoted at $22,046,599 from the Aspen
Icarus Economic Simulator running on a 2009 American Gulf Coast basis. The TIC was quoted
with Indirect Field Costs including fringe benefits, burdens, consumables, scaffolding,
equipment rental, field services and temporary construction utilities, at $1.9 Million and NonField Costs such as freight, taxes, basic and detail engineering, material procurement, G and A
Overheads, contract fees and contingency, of $3.4 Million and the Total Startup Cost of $2.735
Million. The operating cost of this process per year was quoted at $519 Million, with the
greatest cost being the syngas feed, and annual revenues are $575 Million using $2.25/gallon of
gasoline product and $1/gallon of LPG product. The IRR for this project assuming 20 year plant
life is 26% and has a simple payback of only 3.8 years. The project will be located at the site of
the landfill in Newton County, Indiana, and will be coupled along with the gasification plant that
will convert the municipal solid waste into syngas.
6
3. Discussion
Municipal solid waste (MSW) is largely a renewable resource. The average American
generates 650 times their bodyweight in trash throughout their lifetime. Questions were asked
about how landfill space can be dealt with. Converting MSW to syngas is an efficient way of
converting waste into a useful chemical precursor for producing other important industrial
chemicals.
Syngas at a 2:1 H2:CO ratio is fed to a methanol reactor where the reaction occurs as:
2H2 + CO  CH3OH
(1)
This reaction occurs at 725 psi, 270ºC and 99.5% selectivity. The Methanol for the Methanolto-Gasoline (MTG) process needs not be purified as in a traditional methanol production
process, so therefore distillation columns are not a part of the methanol production portion of
the process. In fact, the MTG process will convert the byproducts that may come out of the
methanol reactors, mainly light hydrocarbons and CO2, and since the selectivity of the reaction
runs at 99.5%, the presence of these other components is in small concentration. The
Methanol reactor is modeled as a shell and tube heat exchanger jacketed pressure vessel. For
the reactor, the catalyst is on the tube side and since (1) is exothermic, the diameter of thetube
side will be larger for the same amount of catalyst put in a traditional tank reactor. The
methanol reactor runs at a conversion of 0.4, so the effluent will contain methanol, other
components, and syngas. The effluent will be at high temperature (please cite) and this hot
product will need to be cooled in order to separate the methanol from the syngas. The heat
removed will be used to generate steam. The syngas separated from the methanol reactor
effluent is part of both a purge stream and a recycle stream. About 2% of the syngas will be
recycled back to the methanol reactor and the purge stream is to maintain the 2:1 H 2:CO ratio
of the feed. The methanol portion of the effluent will be reheated and then sent to the MTG
reactors.
7
In the MTG process, methanol is reacted over the ZSM-5 catalyst in a fluidized bed
reactor. Four MTG reactors in parallel are used. The ZSM-5 catalyst was patented by Mobil in
1972 (U. S. Patent 3,702,886) and costs $53.40/lb. In the MTG process, the reactor is run at
330ºC at the inlet and 400ºC at the outlet and the pressures at the inlet and outlet are at 210
and 185 psia respectively. The effluent of the MTG reactors will produce streams of both
Liquefied Petroleum Gas (LPG) and gasoline components (C5+). LPG will be sold for various
heating purposes and thus the price is modeled as if it were natural gas.
The MTG process yields (please correct this) roughly 56 wt% water and 44 wt%
hydrocarbons. NEED NEW COMPONENT BALANCE
4. Recommendations and Conclusions
A. Energy Independence
This process is recommended for construction and implementation. The use of a
renewable resource in order to produce an essential and currently indispensible fuel is essential
to the energy independence of the United States, and with growing concern over the depletion
of the world’s oil supply, other sources of fuel need to be researched. Gasoline as a fuel fits the
current day infrastructure, and within the next 20 years, which is the projected life of this
project, it is possible that the implementation of other fuels will begin.
B. Environmentally Conscience
Locally, the reduction of municipal solid waste from a landfill will reduce the pollution of
the local environment. The contamination of groundwaters by leakage, residual soil
contamination from the waste, offset of methane created by decaying organic waste, sheltering
of disease carriers, such as roaches, rats and dust are largely eliminated with the reduction of
landfill space from this process. The gasoline produced from this process is also virtually free of
8
any sulfur, unlike gasoline derived from oil and provides a smaller carbon footprint that its oilderived equivalent.
C. Location
The project will be located in Newton County, Indiana. This is the largest landfill that
accepts waste from the Chicago Metropolitan Area. The area also features a railroad close by,
so that the final products can be sent off by train back to the Chicago Metro Area for further
refining. The largest landfill of America’s Second City is the ideal place for this process.
D. Revenue
While the price of gasoline is extremely volatile due to the unstable prices in oil, the
price for this the gasoline product and the LPG products can be much more stable due to the
fact that the sources are not a non-renewable source. While the gasoline product will require
refining after it leaves the plant, the price of the gasoline is still lower than that of the gasoline
derived from oil. With this, the simple payback of the process is 3.8 years, and with a net
income of $54 million per year, this process is indeed very profitable.
E. Operating Cost
The operating cost is fairly high, with the price of syngas per ton being the highest
(please cite this one). The Total Installed Cost of this process is much lower than the cost of
syngas per year, (cite this one too is it 46%???)
9
5. Appendices
5.1.Design Basis
6000 Tons per day syngas. Produces 16,300 barrels = 684600 gallons of gasoline
components and 4.46x106 lbmol/year of LPG. Briefly mention the municipal solid waste
scale and why we have 6000 tpd. Explain the sizing of our reactors (RE: AYESHA) and the
production capabilities.
5.2.Block Flow Diagram
10
5.3.Process Flow Diagram
This project is concerned with the conversion of syngas to Methanol, and then the
conversion of that Methanol to C5+ Gasoline Components and LPG. The refining of the final
Gasoline product and the production of syngas from municipal solid waste are not within the
scope of this project. The process has been scaled for 6000 tons per day of syngas and will
produce 16,300 barrels, or 684,600 gallons of Gasoline per day and 4,350 barrels per day, or
182,700 gallons of LPG per day. The process has four major sections (please correspond this
with the picture on the top, since there are only 3 circles instead of 4): Syngas to Methanol
Reaction, heat exchangers for all major processes, Methanol to Gasoline Reaction, and product
refining. This schematic will be broken down into subcomponents of each major section in
order to more clearly elaborate upon stream numbers and how the components are used
within the heat exchange section and what streams are being produced at various stages. A
detailed account of the stream make-up and content is provided in the Material Balance section
6.1.
11
Figure 3
The first step in the process is converting syngas feed to methanol in the methanol
reactor. There is both a fresh feed (1) and a recycle stream (2B) entering the methanol reactor,
both with syngas. The effluent of the methanol reactor (3) contains both syngas and methanol.
Stream (3) enters the MeOH-Water HX tube side, with a warm water stream (4) and leaves as a
Cooled MeOH Product (6) and steam (5). The first part of the MeOH reaction process is show
in Figure 3. Following this is a heat exchange step.
Figure 4
Cooled MeOH Product (6) from the MeOH-Water HX flows through the tube side of the
MeOH-Syngas HX, with a stream of Cool Recycle Syngas (8) flowing in the shell side. Cool
Recycle Syngas (8) is from a stage later in the process and is shown in Figure X. The MeOHSyngas HX allows for the Cool Recycle Syngas (8) to be heated and then split into a purge
syngas stream (10) and a Recycle Syngas to Compressor (2A) stream, where it enters the
12
SYNCOMP compressor and enters the MeOH reactor again as stream (2B). The purge stream
(10) is composed of about 2% of the initial syngas and is necessary in order to maintain the
proper 2:1 H2:CO ratio. Flowing out of the tube side of the MeOH-Syngas HX is the Cooler
MeOH Product (7) stream. The Methanol product is cooled so that it is easily separated from
the syngas that is contained within the stream. Following the MeOH-Syngas HX stage, stream
(7) enters yet another heat exchanger.
Figure 5
Cooler MeOH Product (7) enters the tube side of the Light Gas-MeOH HX with Cold
Light Gas (11) entering the shell side. Stream 11 is from the first product refining stage and will
be elaborated upon later. The exchange occurring in the Light Gas-MeOH HX is so that the
methanol product can be further cooled. Flowing out the tube side is a Cooled MeOH stream
(13A) and from the shell side is a Light Gas Out stream (12). Cooled MeOH (13A) enters a
Cooler so that the temperature is further reduced to a Cold MeOH stream (13B) and enters a
Flash unit. It is in the Flash unit that stream (13B) is separated to an MeOH stream (14) that is
99 mol% MeOH. Leaving the top of the Flash unit is the Cool Recycle Syngas stream (8) that
was used in the shell side of the MeOH-Syngas HX as shown in Figure 4. Stream (14) enters the
tube side of the Product-MeOH HX with a Hot Hydrocarbon stream (15) entering the shell side.
This is so that the Methanol can be warmed into stream (16) and that the hydrocarbon stream
can be cooled (17A). The Hot Hydrocarbon stream (15) is the effluent from the MTG reactor
stage, discussed following Figure 6.
13
Figure 6
Schematically the MTG reactors, which is the main portion of this process, is the most
simple. Before the methanol can enter the MTG reactors, it must first be heated. The Warm
MeOH stream (16) enters a heater and leaves as Hot MeOH (17B). Hot MeOH (17B) enters four
MTG reactors set in parallel running the ZSM-5 catalyst. The MTG reactors generate the Hot
Hydrocarbons stream (15) that was used in the Product-MeOH HX to warm the methanol from
the Flash unit. The MTG reactors will produce gasoline components in a 1:1 ratio by mole for
the methanol input. From the shell side of the Product-MeOH HX, Cool Hydrocarbons stream
(17A) exists and then enters to the final 2nd Gas HX for the first round of product refining.
Figure 7
14
To begin the product refining stage, Cool Hydrocarbons stream (17A) enters the tube
side of 2nd Gas HX and a Cooling Water Stream (18) enters the shell side of the 2nd Gas HX.
Leaving this heat exchanger are a Warm Water (4) and a Cooled Hydrocarbons stream (19) from
the shell side and from the tube side respectively. The warm water (4) flows to the first heat
exchanger in the process, the MeOH-Water HX. Stream (19) enters a cooler to produce a Cold
Hydrocarbons stream (20) so that the Hydrocarbons can be easier separated from the water. In
order to separate the water from the hydrocarbons, stream (20) enters a Decanter that
produces a Hydrocarbons stream (22) and a ‘Dirty’ Water stream (21). The Hydrocarbons
stream (22) is pumped into the Deethanizer as a Pump Hydrocarbons stream (23). The
Deethanizer is modeled as a distillation column with C3 Components and Hydrocarbons (24 as
the bottoms product and Cold Light Gas (11) as the distillate. Stream (11), from Figure 5, enters
the shell side of the Light-Gas MeOH HX. Stream (24) enters a second distillation column for
further product refining. Before the final stage of product refining is discussed, the ‘Dirty’
Water stream (21) from the decanter enters a water treatment step as shown in Figure 8.
Figure 8
‘Dirty’ Water stream (21) enters a Water Flash unit, where it is separated into an Offgas
(26) component and a ‘Clean’ Water (25A) stream. The Offgas stream (26) consists of a very
small amount (~3 lbmol) of trace hydrocarbons and the stream will be flared off. The Clean
15
Water stream (25A) mixes with Extra Cooling Water (25B) and form the Cooling Water Stream
(18) that entered the shell side of the 2nd Gas HX from Figure 7.
Figure 9
Beginning the final product refining stage of the process, the C3 + Hydrocarbons stream
(24) enters the Hydrocarbon Separator, modeled as the second distillation column. The
bottoms product is a Gasoline stream (29) and the distillate is a stream of LPG + Pentanes (28).
The distillate product of the Hydrocarbon Separator enters the third and final distillation
column, the Debutanizer, with distillate product of LPG (30) and with bottom product Pentanes
(31). The Pentanes stream (31) is mixed with the Gasoline stream (29) to make the final
Gasoline Product (32). The pentanes and the Gasoline are mixed together so that the C5
concentration of the Gasoline product can be further increased, thus leading to a higher quality
of gasoline. Both the Gasoline Product stream (32) and the LPG stream (30) are the final
products of this process.
16
6. Material and Energy Balance
6.1.Material Balance
A full material balance is done around both the Methanol Reactor and the MTG
reactors. As cited in the literature, a component balance of both the LPG and product streams
can be constructed and shown below. The process was scaled for 6000 tons per day of syngas.
The material balance around the Methanol is shown schematically in Figure 6A-1 and
numerically in Table 6A-1. The material balance was conducted in iterative fashion and the
numbers at the 25th iteration are used as it is at the 25th iteration that the numbers have
already converged in reasonable fashion. Conversion of the Methanol Reactor set to 0.4 per
pass and calculated on a basis of 6000 tons per day of syngas.
Figure 10
The equations used for the Mass balance for the Methanol Reactor loop were:
𝐶𝑂 𝑖𝑛 𝑟𝑒𝑐𝑦𝑐𝑙𝑒 = (𝐶𝑂 𝑓𝑟𝑜𝑚 𝑠𝑦𝑛𝑔𝑎𝑠 + 𝐶𝑂 𝑓𝑟𝑜𝑚 𝑒𝑎𝑟𝑙𝑖𝑒𝑟 𝑟𝑒𝑐𝑦𝑐𝑙𝑒) ∗ (1 − 𝑐𝑜𝑛𝑣𝑒𝑟𝑠𝑖𝑜𝑛)
− 𝐶𝑂 𝑖𝑛 𝑝𝑟𝑜𝑑𝑢𝑐𝑡 𝑠𝑡𝑟𝑒𝑎𝑚
17
𝐻2 𝑖𝑛 𝑟𝑒𝑐𝑦𝑐𝑙𝑒 = (𝐻2 𝑖𝑛 𝑓𝑟𝑜𝑚 𝑠𝑦𝑛𝑔𝑎𝑠 + 𝐻2 𝑖𝑛 𝑓𝑟𝑜𝑚 𝑒𝑎𝑟𝑙𝑖𝑒𝑟 𝑟𝑒𝑐𝑦𝑐𝑙𝑒)
− (𝐶𝑂 𝑓𝑟𝑜𝑚 𝑠𝑦𝑛𝑔𝑎𝑠 + 𝐶𝑂 𝑓𝑟𝑜𝑚 𝑒𝑎𝑟𝑙𝑖𝑒𝑟 𝑟𝑒𝑐𝑦𝑐𝑙𝑒) − 𝐶𝑂 𝑖𝑛 𝑟𝑒𝑐𝑦𝑐𝑙𝑒
− 𝐶𝑂 𝑖𝑛 𝑝𝑟𝑜𝑑𝑢𝑐𝑡 𝑠𝑡𝑟𝑒𝑎𝑚) ∗ 2
𝑆𝑖𝑧𝑒 𝑜𝑓 𝑅𝑒𝑐𝑦𝑐𝑙𝑒 = 𝐶𝑂 𝑖𝑛 𝑟𝑒𝑐𝑦𝑐𝑙𝑒 + 𝐻2 𝑖𝑛 𝑅𝑒𝑐𝑦𝑐𝑙𝑒
𝐻2 𝑝𝑢𝑟𝑔𝑒 = 𝑃𝑢𝑟𝑔𝑒 𝑓𝑟𝑎𝑐𝑡𝑖𝑜𝑛 ∗ 𝐻2 𝑖𝑛 𝑅𝑒𝑐𝑦𝑐𝑙𝑒
𝐶𝑂 𝑝𝑢𝑟𝑔𝑒 = 𝑃𝑢𝑟𝑔𝑒 𝑓𝑟𝑎𝑐𝑡𝑖𝑜𝑛 ∗ 𝐶𝑂 𝑖𝑛 𝑅𝑒𝑐𝑦𝑐𝑙𝑒
𝐻2 𝐵𝑎𝑐𝑘 𝑡𝑜 𝑅𝑒𝑎𝑐𝑡𝑜𝑟 = 𝐻2 𝑖𝑛 𝑅𝑒𝑐𝑦𝑐𝑙𝑒 − 𝐻2 𝑝𝑢𝑟𝑔𝑒
𝐶𝑂 𝐵𝑎𝑐𝑘 𝑡𝑜 𝑅𝑒𝑎𝑐𝑡𝑜𝑟 = 𝐶𝑂 𝑖𝑛 𝑅𝑒𝑐𝑦𝑐𝑙𝑒 − 𝐶𝑂 𝑝𝑢𝑟𝑔𝑒
𝑀𝑒𝑂𝐻 (𝑜𝑢𝑡) = (1 − 𝐶𝑜𝑛𝑣𝑒𝑟𝑠𝑖𝑜𝑛) ∗ 𝑀𝑒𝑂𝐻(𝑖𝑛)
Entering the Methanol Reactor are the SYNGAS and SECOND (Recycle - Purge) streams composed of:




15657.67 lbmol/hr CO from SYNGAS
31315.35 lbmol/hr H2 from SYNGAS
21736.17 lbmol/hr CO from SECOND (Recycle - Purge)
52679.94 lbmol/hr H2 from SECOND (Recycle = Purge)
For the PRODUCT stream,





256.52 lbmol/hr CO with PRODUCT
33.60 lbmol/hr H2 with PRODUCT
6775.76 lbmol/hr MeOH PRODUCT
10047.44 lbmol/hr CO in RECYCLE
24498.34 lbmol/hr H2 in RECYCLE
18
The product stream is cooled in a heat exchanger so that the Methanol can be separated from the CO
and H2. The separated Methanol is then sent to a reheated and then to the MTG reactor. CO and H2 gas
are sent back to GASSPLIT which will provide two streams SECOND (Recycle) and PURGE. 2% of the CO
and H2 that emerge from the Methanol Reactor are purged in order to maintain 2:1 syngas ratio.
For the PURGE stream,


110.52 lbmol/hr CO
269.48 lbmol/hr H2
The Methanol from the Methanol , after separated from the syngas is reheated and sent to
three MTG reactors in parallel. The process flow diagram of a single MTG reactor is shown in Figure 6A2. Equations for the mass balance of the MTG reactors are:
Compound (effluent, norecycle )  %oftotal * ( MeOH ( produced , total)) / 100
CompoundinEffluent(total)  Re cycleComponent (OneTrialEa rlier )  Compound (effluent, norecycle )

trial#
 Compound (effluent, norecycle ) *[(1 LGConversion) * ( LPGConversion) * (Re cycleConversion )]
i n
i 1
TotalFlowrateThroughMTG Re actor   CompoundInEffluent(total)
TotalFlowrateThroughMTG Re actor   CompoundInEffluent(total)
The equations for the MTG reactor include the sum of compounds flowing through the MTG reactor.
The component balance of these compounds are shown in Table 6-1-A
Entering the MTG Reactor:

14957.54 lbmol/hr MeOH
Leaving the MTG Reactor:

14957.54 lbmol/hr hydrocarbons
19
Hydrocarbons
C1
CO
CO2
C2 =
C2
C3 =
C3
iC4
C4 =
nC4
C5's
C6's
C7's
C8's
C9's
C10's
Benzene
Toluene
C8 AROM
C9 AROM
C10 AROM
C11 AROM
Wt (KG)
6.963403
0
0
6.092977
7.833828
18.27893
99.57666
189.3175
24.37191
126.2117
520.1662
621.3096
452.6212
362.184
233.9703
0
61.10386
76.07517
438.2591
496.1424
87.47774
0
Wt%
0.181909
0
0
0.15917
0.204648
0.477511
2.601301
4.945655
0.636682
3.297103
13.58861
16.23084
11.82409
9.461549
6.112147
0
1.596253
1.987357
11.44891
12.96103
2.285234
0
Weight percent of gasoline as
product
87.49602074 Percent
Figure 11
Table 1
The component balance of the hydrocarbons coming out of the MTG reactors indicates that 87%
is C5+ gasoline components. The remaining compounds C4- are LPG components that will be flash
separated from the gasoline components.
20
The Cooling (Flash) 3 Phase Separator is shown schematically as in Figure 5 however in order to
conduct the material balance on this part of the process, there are 8 assumptions that must be made.
The assumptions are:
1) All of the H2 is taken away in the light gas
2) All of the CH4 is taken away in the light gas
3) All of the C2H6 is taken away in the light gas
4) All of the C3H8 is taken away in the light gas
5) None of the C4H10 is taken away in the light gas
6) All of the CO/CO2 is lost in the light gas
7) The H2O is immiscible with all other components, in liquid phase and leaves
completely
8) The remaining components are in a second liquid phase
Figure 12
Following these assumptions, the following equations are used for the mass balance on the
Cooling (Flash) 3 Phase Separator:
Water (out , flash )  water( produced , total)
LightGasComponentFlowRate  LGConversion * CompoundinEffluent(total)
ComponentOutofLiquidFlash  (1  LGConversion) * CompoundinEffluent(total)
21
The water component flow of the Cooling (Flash) 3 Phase Separator is 2818.39 lbmol/hr. This water is
labeled as “DIRTYH2O” and enters a second flash drum, there it emerges as a stream of “CLEANH2O”
which reenters (ARTICULATE ON THE ASPEN FLOWSHEET) Tables 2 and 3 both show the composition of
the organic liquid phase and the gas phases respectively.
Table 3
Table 2
Both the Gas Phase and Organic Liquid Phase are sent to a Stripper and Accumulator
combination for further purification. Following the equations:
LPGComponent  (1  LGConversion) * ( LPGConversion ) * CompoundinEffluent(total)
22
CompoundIn Pr oduct (total)  CompoundinEffluent(total) * (1  LGConversion) * (1  LPGConversion )
The schematic for the Stripper and Accumulator, both modeled as distillation columns, is as shown in
Figure 6:
Figure 13
In order to conduct the mass balance for this system, the following four assumptions are used:
1)
2)
3)
4)
All of the remaining propane (C3H8) exits in the vapor stream
All of the remaining butane (C4H10) exits in the vapor stream
10% of the pentane (C5H12) exits in the vapor stream
The liquid component out the stripper (FINALDIS) is the final product
For the FINALDIS Accumulator, the two streams that exit our are both the LPG product and the Gasoline
Components product which would complete the MTG process. Tables x and y give both component
profiles of the final products LPG and Gasoline Components:
23
6.2.Energy Balance
7. Calculations
7.1.Aspen Streams
8. Annotated Equipment List (Data Sheets)
24
9. Economic Evaluation
9.1.Annual Revenue
All economic evaluation was done using the Aspen Icarus Economic Simulator. The total
revenue per year for this process is estimated at $566 Million per year with a profit of $56 Million per
year. A single year counts as 350 days of uptime for the process. The IRR for this project is 26% for a 20
year plant life. Simple payback is calculated to be 3.8 years. Revenue sources are detailed as below.
Gasoline Product:
16,300 Barrels per day = 684,600 gallons per day of gasoline product is produced from this
process. The spot price of $2.25/gallon provided by the Energy Information Administration (EIA) of the
Department of Energy (DoE) of the United States is the gasoline derived from oil sources. Since the
gasoline from this process is not sold directly to consumers but to refineries instead, the price is lowered
to $2.00/gallon.
684,600
𝐺𝑎𝑙𝑙𝑜𝑛𝑠
𝑑𝑎𝑦
∗ 365
𝑑𝑎𝑦
𝑦𝑒𝑎𝑟
$
∗ 2.00 𝑔𝑎𝑙 = $499,758,000/𝑦𝑒𝑎𝑟
(9.1.1)
Liquefied Petroleum Gas (LPG):
4,350 Barrels per day = 182,700 gallons per day of LPG product is produced from this process.
LPG in the case for economics will be modeled as natural gas, since its uses will be similar. The
estimated price for this is rated at $1/gallon.
182,700
𝐺𝑎𝑙𝑙𝑜𝑛𝑠
𝐷𝑎𝑦
𝑑𝑎𝑦
$
∗ 365 𝑦𝑒𝑎𝑟 ∗ 1.00 𝑔𝑎𝑙𝑙𝑜𝑛 = $66,685,500/𝑦𝑒𝑎𝑟
(9.1.2)
[ARE THERE ANY OTHER SOURCES HERE? FROM THE HEAT GENERATION????]
The total revenue is the sum of all these revenue sources.
$499,758,000 + $66,685,500 = $566443500/𝑦𝑒𝑎𝑟
 Total revenue per year = $575 Million
 Profit = $56 Million/year
 IRR = 26% (20 year plant life)
 Simple payback = 3.8 years
25
(9.1.3)
$575 Million per year with 350 days of up-time
9.2.Annual Operating Costs
In order to account for the Annual Operating costs of this process, the Aspen Economic
Simulator, Icarus, was employed to calculate the costs of components, as well as their Total Direct Cost
(TDC).
 Upkeep = $16,700,000/year
 Includes catalyst prices and utilities
 Cooling water
 70,000 gpm
 4 Million Dollars/year
 100 psia Pressure Steam
 30.4 Klb/hr
 2 Million Dollars/year
 400 psia Pressure steam
 157.5 Klb/hr
 14.8 Million Dollars/year
 Steam generation
 Steam costs not included in upkeep
26
27
 Syngas cost = $250/ton
 Total syngas cost / year = $500 Million
9.3.Capital Costs
In order to account for the Capital Costs for this process, the Aspen Icarus Economic
Simulator was run with specifications and design basis as noted in the respective sections. The
Icarus Economic Simulator quoted the Total Installed Cost (TIC) of the entire process at
$22,046,599 running on a 2009 American Gulf Coast cost basis.
 Detailed summary in IPE
 TIC (ISBL) = $22,050,000
 Indirect field costs = $1,900,000
 Non field costs =$3,400,000
 Total startup cost = $27,350,000
9.4.Simple Payback
28
 Gasoline price = $2.25/gallon ($94.5/bbl)
 EIA spot price
 LPG price = $1/gallon ($42/bbl)
 Total revenue per year = $575 Million
 Profit = $56 Million/year
 IRR = 26% (20 year plant life)
 Simple payback = 3.8 years
10.
Utilities
11.
Conceptual Control Scheme
12.
Major Equipment Layout
13.
Distribution and End-Use Issues Review
14.
Constraints Review
15.
Project Communication File
Contact Info
Saturday, January 29, 2011
11:20 AM
Team Alpha
ChE 397 Spring 2011
29
Name:
Email:
Cell:
Ayesha Rizvi
arizvi6@uic.edu
773-971-4457 Researcher
Bernard Hsu
bbhsu2@uic.edu
630-391-3720 Technical Writer
Jeff Tyska
jtyska1@gmail.com
630-849-8371 Group Leader
Mohammed Shehadeh
msheha4@uic.edu
773-715-3353 Webmaster
Yacoub Awwad
yawwad2@uic.edu
708-336-0502 Calculations
Group Email
che397grp1@listserv.uic.edu
(sends to all members, must have
listserv access)
1/17/2011
Thursday, January 27, 2011
11:22 PM
Skype Conference with Dan Rusinak
Attending:
Jeffrey Tyska
Bernard Hsu
Dan Rusinak
Discussed group dynamics and possible project options.
Subject
Re: First Group Meeting tomorrow
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, January 17, 2011 9:59 PM
that's fine, though we may need to talk for a little more than 30 minutes
On Mon, Jan 17, 2011 at 8:14 PM, moody shehadeh
<cool_moody007@hotmail.com>wrote:
> I just confirmed with bernard that we will meet at 1:30 pm at CEB
> before class..
30
Team Role:
>
> sorry people, this is the last call..
>
> Mohammad.
>
> > Date: Mon, 17 Jan 2011 18:00:40 -0600
> > From: fattyllama@GMAIL.COM
> > Subject: Re: First Group Meeting tomorrow
> > To: CHE397GRP1@LISTSERV.UIC.EDU
>>
> > Perl's starts at 2. I was under the impression that no one would
> > have
> class
> > right before Perl's. It would be easier to do it after class, so
> > lets do
> it
> > after Perl's.
>>
> > See you then.
>>
> > Bernard
>>
> > On Mon, Jan 17, 2011 at 5:17 PM, moody shehadeh
> > <cool_moody007@hotmail.com>wrote:
>>
> > > how about at 12:00 noon, because i have a class at 1:00 pm..?
>>>
> > > > Date: Mon, 17 Jan 2011 16:21:44 -0600
> > > > From: arizvi6@UIC.EDU
> > > > Subject: Re: First Group Meeting tomorrow
> > > > To: CHE397GRP1@LISTSERV.UIC.EDU
>>>>
> > > > Hello,
>>>>
> > > > I would prefer to have the meeting before Perl's class tomorrow.
> Would
> > > > around 1pm at CEB work for everyone - right before Senior Design?
>>>>
> > > > -Ayesha
>>>>
>>>>
> > > > On Mon, January 17, 2011 12:46 pm, moody shehadeh wrote:
> > > > > I am free anytime before 1:00 pm on tuesdays, and anytime
> > > > > after
> 2:00 pm
> > > on
> > > > > M & W.
>>>>>
31
> > > > > Mohammad.
>>>>>
> > > > >> Date: Mon, 17 Jan 2011 12:13:52 -0600
> > > > >> From: bbhsu2@UIC.EDU
> > > > >> Subject: First Group Meeting tomorrow
> > > > >> To: CHE397GRP1@LISTSERV.UIC.EDU
> > > > >>
> > > > >> Group,
> > > > >>
> > > > >>
> > > > >>
> > > > >> We will have a group meeting to decide roles tomorrow. Please
> respond
> > > in
> > > > >> email if you would prefer to have this meeting before or
> > > > >> after
> Perl's
> > > > >> class.
> > > > >>
> > > > >>
> > > > >>
> > > > >> Thanks,
> > > > >>
> > > > >> Bernard
>>>>>
>>>>>
>>>
>>>
>
>
1/18/2011
Thursday, January 27, 2011
11:12 PM
Initial Group Meeting
1:00 Pm
Attending:
Ayesha Rizvi
Bernard Hsu
Jeffrey Tyska
Mohammed Shehadeh
Yacoub Awwad
Assigned group roles and discussed possible group projects
Subject
Skype conference
32
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 18, 2011 11:14 AM
Attachments
<<image001.jpg>>
Team: Alpha, When do you want to conference today. I am going to a client at 2 PM today. If not
tonight.
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBB700.EBF58410]
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Re: ChE 397 Senior Design Group 1
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 18, 2011 1:55 PM
I will be at Corn Products this afternoon. 5:30-6 PM tonight is OK with me. Tomorrow at 2PM for the
whole group. You initiate the call.
If you cannot find me, call my cell 630-697-8111.................Dan
-----Original Message----From: Bernard Hsu [mailto:bbhsu2@uic.edu]
33
Sent: Tuesday, January 18, 2011 1:49 PM
To: Rusinak, Dan
Cc: che397grp1@listserv.uic.edu
Subject: RE: ChE 397 Senior Design Group 1
Mr Rusinak,
I talked with my group. As a group we can talk on skype with you tomorrow at 2pm. I hope this time
works well with you since 4 of the members of my group are commuters.
On the flipside, Jeff Tyska and I would like to speak with you today both together any time between 315
and 6pm. Please let us know a time.
Thanks,
Bernard
On Tue, January 18, 2011 12:41 pm, Rusinak, Dan wrote:
> Leaving my office at 2:30 pm. Otherwise tonight............Dan
>
> -----Original Message----> From: Bernard Hsu [mailto:bbhsu2@uic.edu]
> Sent: Tuesday, January 18, 2011 12:37 PM
> To: Rusinak, Dan
> Subject: RE: ChE 397 Senior Design Group 1
>
> I am leaving to meet with the group right now. Will let you know
> after the meeting the time.
>
> Thanks,
> Bernard
>
> On Tue, January 18, 2011 12:29 pm, Rusinak, Dan wrote:
>> Call today?
>>
>> From: Bernard Hsu [mailto:bbhsu2@uic.edu]
>> Sent: Sunday, January 16, 2011 6:07 PM
>> To: Rusinak, Dan
>> Cc: che397grp1@listserv.uic.edu
>> Subject: ChE 397 Senior Design Group 1
>>
>> Mr Rusinak,
>>
>> I am a member of Group 1 (Alpha) of Dr Perl's ChE 397 Senior Design
>> group.
>> Dr Perl has assigned my group to your mentorship. The members of
>> the group include:
>>
34
>> Ayesha Rizvi
>> Bernard Hsu
>> Jeff Tyska
>> Mohammed Shehadeh
>> Yacoub Awwad
>>
>> We are looking to schedule a time for either a conference call with
>> you, or to meet with you in person so we may be able to get
>> acquainted and to discuss with you the details of our design project. Please advise.
>>
>> Regards,
>> Bernard
>>
>> ________________________________
>> -------------------------------------------------------------------->> ------ This e-mail is intended for the addressee shown. It contains
>> information that is confidential and protected from disclosure. Any
>> review, dissemination, or use of this transmission or its contents by
>> persons or unauthorized employees of the intended organizations is
>> strictly prohibited.
>> The contents of this email do not necessarily represent the views or
>> policies of Middough.
>>
>
>
>
> ---------------------------------------------------------------------> ----- This e-mail is intended for the addressee shown. It contains
> information that is confidential and protected from disclosure. Any
> review, dissemination, or use of this transmission or its contents by
> persons or unauthorized employees of the intended organizations is
> strictly prohibited.
> The contents of this email do not necessarily represent the views or
> policies of Middough.
>
>
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Info / work for tomorrow and tonight
35
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 18, 2011 7:57 PM
Ok, I realize this is sort of long, but everyone needs to keep up with what's going on in the group,
especially since we're talking to Dan tomorrow.
Bernard and I talked to Dan, and apparently we're behind where we should be right now. We essentially
need to find whatever chemical we want to make (not some basic one like methanol, but one mass
produced enough to find good information on) by tomorrow, though it sounds like the H2/CO ratio isn't
our problem, and we shouldn't have to worry that much about the amount of syn gas coming in when
choosing it. Ayesha will be emailing me some chemicals to look at, and I'll be looking at those and a few
tomorrow in the kirk othmer encyclopedia, which apparently has tons of information on this stuff.
If anyone is free from 9:30-10:45 and from 12:00 - 2:00 tomorrow I could use help researching the
chemicals. I'll check my email around 8:00 tomorrow, so email me tonight if you can help out.
If you can get to SES before 2, show up around 15 minutes ahead of time, we're probably going to get
grilled on this stuff tomorrow, so I'd like to make sure everyone knows what were doing, and why.
As a reminder, I need everyones schedules by tonight (free times), since I want to have the meeting
times done by the time we talk with Dan tomorrow.
From what he was saying, it sounds like a lot of our work will need to be done as a group.
-Jeff Tyska
Subject
Re: mohammad shehadeh schedule
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 18, 2011 9:22 PM
I'll actually be in SES (that's where the library is that has the book), if you can meet me there email me
back, if not I'll assume you didn't get the email and meet you in CEB
Thanks
-Jeff Tyska
On Tue, Jan 18, 2011 at 8:58 PM, moody shehadeh
<cool_moody007@hotmail.com>wrote:
>
> jeff here is my schedule, and u could add on it that i have work T nd
> Thu from 4-11 pm, and i will be there tomorrow at 9:30 in CEB to help
36
> you in researching. and i could be there earlier if you need me..
>
> MS
>
> To: msheha4@uic.edu
> From: cool_moody007@hotmail.com
> Subject:
> Date: Tue, 18 Jan 2011 20:54:17 -0600
>
>
>
> Sent from my T-Mobile myTouch 3G Slide
>
>
1/19/2011
Thursday, January 27, 2011
11:21 PM
Skype Conference with Dan Rusinak
2:05pm at SES
Attending:
Ayesha Rizvi
Bernard Hsu
Jeffrey Tyska
Mohammed Shehadeh
Yacoub Awwad
Dan Rusinak
Proposed project to Dan.
Subject
Re: ChE 397 Senior Design Research
From
Tim Klassen
To
Bernard Hsu
Cc
che397grp1@listserv.uic.edu
Sent
Wednesday, January 19, 2011 8:29 AM
Hi Bernard, There are a number of sources that might be useful to you.
SciFinder Scholar (Chemical Abstracts) contains a lot of info both commercial and articles. Also useful is
Reaxys. For stronger concentration on the engineering side try Compendex (Engineering
37
Village.) All of these resources can be found from the Databases A-Z list on the library home page at
http://library.uic.edu/
Best,
Tim
On 1/19/11 1:15 AM, Bernard Hsu wrote:
> Mr Klassen,
>
> I am in Dr Jeffery Perl’s ChE 397 Senior Design course. I believe that
> Dr Perl has scheduled for you to come present to our class regarding
> our UIC library’s resources and how they will provide great aid to us
> during the course of our project.
>
> My group was wondering if you could steer us in the direction of the
> resources we can use to find information on chemical feedstocks and
> important industrial chemicals used and produced in the United States.
>
> My group leader has already cited the Kirk Othmer Encyclopedia for
> information on chemical technology, however we are looking for other
> sources as well. If you could help us, that would be greatly appreciated.
>
> Thanks,
>
> Bernard
>
-Tim Klassen
Science Librarian
Science Library
University of Illinois at Chicago
klassen@uic.edu
(p)312-413-3060
(c)312-282-4341
(f)312-996-7822
Subject
Ayeshas Schedule
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, January 19, 2011 9:19 AM
Attachments
<<Ayeshas schedule.xls>>
My Schedule is attached.
38
-Ayesha
Subject
Update on chemicals / schedule
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, January 19, 2011 9:57 PM
Attachments
<<GROUP_SCHEDULE(1).xls>>
The reports are pretty dense, so I'll have to tackle them properly over the weekend (or at least not at
night), but so far, this is basically my understanding of our situation.
Mixed alcohols - We have a full report on the economics of MSW to this, with the return appearing to be
10% per year. There are some companies starting to do similar things, however, all of their catalysts are
proprietary, and from my skimming of the article, it seems like identifying our catalyst/s would be the
biggest problem. We also have some detailed drawings for the exact process to make these. There are a
few safety concerns, but nothing that can't be gotten over. There also appears to be some push to get
butanol in gasoline, though it's hard to determine how popular mixed alcohols are quite yet. The reports
also seem to say that the process is sort of a modified fischer-tropsch, which may cause some problems
with the mentors.
Gasoline - We have the catalysts, and a basic understanding of how the processes work, but I'm not sure
that it will work economically. In the August 2008 issue of CEP (free from AICHE) there's an article on
biobutanol, most of which has to do with getting it from fermentation, but theres a graph of butanol
prices vs gasoline prices (in Chicago, funnily enough) and butanol is much more expensive, which means
that we would probably make less per year with gasoline than if we did mixed alcohols (one component
of which is butanol). It's also a little less chemical based, since there's a wider range of chemicals in
gasoline than mixed alcohols, but not by that much.
I'll try to talk to everyone tomorrow to get their thoughts on it, and I'll be talking to professor Perl
tomorrow to try to find out what the best choice here would be (and if either would count as chemical
production).
The schedule is attached, J = Jeff has class in that period, B = Bernard, etc.
1/21/2011
Saturday, January 29, 2011
11:24 AM
Subject
Notes
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, January 21, 2011 2:05 PM
Attachments
<<notes.doc>>
39
More notes, just read over this so we aren't researching the same stuff over and over again.
Thanks
-Jeff Tyska
Subject
Re: skype conf TOMORROW 1:30PM
From
cool_moody007@hotmail.com
To
Bernard Hsu
Sent
Friday, January 21, 2011 8:37 PM
Cool i ll make an acount tonight..
Sent from my T-Mobile myTouch 3G Slide
----- Reply message ----From: "Bernard Hsu" <bbhsu2@UIC.EDU>
Date: Fri, Jan 21, 2011 3:00 pm
Subject: skype conf TOMORROW 1:30PM
To: <CHE397GRP1@LISTSERV.UIC.EDU>
Group,
Lets have a skype conference tomorrow, Saturday January 22 at 1:30 PM so
that we may be able to discuss our current findings and that I can update
you on the status on our presentation. Let me know if you cannot make
this time.
Thanks,
Bernard
1/22/2011
Wednesday, January 26, 2011
10:12 PM
1/22/2011
Skype Conference
90 minutes
40
Attending:
Bernard
Ayesha
Mohammed
Yacoub
Jeff
Jeff assigned parts for the presentation
Subject
pictures of research
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, January 22, 2011 1:44 AM
Attachments
[Deleted]
i am sorry some are blurry
Subject
[Fwd: RE: CHE 397 SEnior Design]
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, January 22, 2011 5:03 PM
Hi all,
So I emailed Perl asking him what was the 'Reports Outlines Established'
that he wrote on the schedule document that he gave us in class. And the following is what he sent me.
So I guess we should use the contents from box 4 from the course outline sheet that he gave us for our
presentation, and add information to it as we research.
---------------------------- Original Message ---------------------------Subject: RE: CHE 397 SEnior Design
From: "Prof. J. Perl" <Perl@uic.edu>
Date: Sat, January 22, 2011 3:36 pm
41
To: "'Rizvi, Ayesha'" <arizvi6@uic.edu>
-------------------------------------------------------------------------Ayesha:
Block 4 is the overall outline which you should begin to assemble. For this Tuesday it may look more like
a table of contents, but just get it started and fill in the elements pertinent to this first meeting. This will
be your semester-long work-in-progress and will be in a state of continuous production/improvement.
Continue to coordinate with your client/mentor.
Some of the bumps will be smoothed out during your presentations this Tuesday.
- Prof Perl -
University of Illinois - Chicago
Department of Chemical Engineering
Jeffery P. Perl, PhD, PE, CHMM
Adjunct Professor
810 S. Clinton Street
Chicago Illinois 60607
-----Original Message----From: Rizvi, Ayesha [mailto:arizvi6@uic.edu]
Sent: Saturday, January 22, 2011 2:14 PM
To: perl@uic.edu
Subject: CHE 397 SEnior Design
Hi Professor Perl,
On the class schedule that you gave us, there is a list of things that we should talk about on Tuesday.
What do you mean by Report Outlines Established?
thanks,
Ayesha
Subject
Presentation 1
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, January 22, 2011 7:13 PM
here is my part bernard, tell me if you need anything more, and i ll see you guys monday.
tc MS
42
Subject
presentation 1
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, January 22, 2011 10:30 PM
Attachments
[Deleted]
Hey Bernard this is my part tell me if something has to be changed. see you all Monday
Yacoub
1/23/2011
Saturday, January 29, 2011
11:26 AM
Subject
Slightly more detailed Block Flow Diagram
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Sunday, January 23, 2011 5:46 PM
Attachments
[Deleted]
This doesn't include any utilities, reboilers, etc., pumps or surge tanks, nor does it say what to do with a
lot of the water and LPG. It's pretty much what I've seen described in the .nz articl, so I'll have to check
the KO to make sure that it matches this. I wouldn't necessarily put it in this presentation, but it's a good
illustration of everything we have to watch out for.
43
Screen clipping taken: 1/29/2011 11:27 AM
Subject
Re: Presentation1
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
44
Sent
Sunday, January 23, 2011 6:08 PM
Attachments
[Deleted]
On Sun, January 23, 2011 2:26 pm, Bernard HSU wrote:
> Ayesha,
>
> These look very good. Now I will begin to compile the presentation.
> Please
> send me the rest when you can.
>
> Thanks,
> Bernard
>
> On Sun, Jan 23, 2011 at 2:16 PM, Rizvi, Ayesha <arizvi6@uic.edu> wrote:
>
>> Hi,
>>
>>
>> Here are the slides that I came up with. I will try and add a few
>> more slides.
>> Let me know what you think about these.
>>
>> Ayesha
>>
>>
>>
>>
>
>
1/24/2011
Wednesday, January 26, 2011
10:12 PM
Presentation Practice:
5:15-7:15 PM
Attending:
Ayesha Rizvi
Bernard Hsu
Jeffrey Tyska
Mohammed Shehadeh
Yacoub Awwad
45
Presentation was practiced. Bernard was filmed first as he compiled presentation.
Video http://www.youtube.com/watch?v=N9gi9ks5ggE is of Bernard presenting to the group
as if he were presenting to class.
Subject
Fwd: Process Question/ DME information
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, January 24, 2011 9:58 AM
Information from Dan's friend about the DME reaction, I'll talk to everyone about this in process design,
but I want to make sure everyone has the information.
---------- Forwarded message ---------From: TODD HARVEY <th.unitel@gmail.com>
Date: Mon, Jan 24, 2011 at 8:52 AM
Subject: Re: Process Question/ DME information
To: "Rusinak, Dan" <Rusinad@middough.com>
Cc: Jeff Tyska <jtyska1@gmail.com>, "drus45@gmail.com" <drus45@gmail.com>
Dan and Jeff:
We actually have a project in house right now to make DME from Syngas. Feel free to contact me, I will
help as I can.
Traditionally DME is made by the dehydration of methanol (a little bit of a misnomer I believe, but that
is what the industry calls it). Simplified the chemistry is:
1. 2 CO + 4 H2 --> 2 CH4O (In First Reactor)
2. 2 CH4O --> C2H6O +H2O (In Second Reactor)
3. 2 CO + 4 H2 --> C2H6O + H2O (Net)
Note that the ideal H2/CO ratio is about 2.
Alternatively, some groups are working on a direct DME process from syngas.
1. 2 CO + 4 H2--> 2CH4O (In Only Reactor)
2. 2 CH4O --> C2H6O +H2O (In Only Reactor)
3. H20 + CO --> H2 +CO2 (In Only Reactor, Water Gas Shift Reaction)
4. 3 CO +3 H2 --> C2H6O +CO2 (Net)
Note that the ideal H2/CO ratio is about 1
46
The second route is most interesting for bio derived syngas which has a tendency to have an H2/CO ratio
around one when gasified.
It appears that the second route is less efficient due to CO2 production but that is a function of how we
draw our system. Consideration has to be given to the reformer/gasifier. For a syngas exiting the
reformer/gasifier with a H2/CO ratio of 1, the traditional technology would require a water gas shift
(WGS) reactor prior to the methanol synthesis reactor which will produce 1 mole of CO2 for every
additonal mole of H2 produced. For bio derived syngas, the alternate technology eliminates the WGS
reactor and eliminates the dehydration reactor. It however does have a much more involved product
recovery system.
I'm not sure what you have in mind ultimately but just a few initial thoughts.
Best Regards,
Todd Harvey
On Mon, Jan 24, 2011 at 7:59 AM, Rusinak, Dan <Rusinad@middough.com> wrote:
> Jeff: Looks like a full plate. It is within the scope of a senior
> design project. Go for it!
>
>
>
> Todd: Could you lend my group, Team Alpha, some guidance. I know that
> you are very busy, but you have so much knowledge.
>
>
>
>
>
> Thanks,
>
>
>
>
>
> *Dan Rusinak** PE***
>
> Chief Process Engineer
>
>
>
> *[image: PerformanceYouTrustGraywMiddough.jpg]*
47
>
>**
>
> *Middough Inc.*
>
> 700 Commerce Dr.
>
> Oak Brook, IL 60523
>
> 630-756-7010 Direct
>
> 630-756-7000 General
>
> 630-756-7001 Fax
>
> 630-697-8111 Cell
>
> *rusinad@middough.com***
>
> *www.middough.com*
>
>
>
>
>
>
>
> *From:* Jeff Tyska [mailto:jtyska1@gmail.com]
> *Sent:* Sunday, January 23, 2011 8:21 PM
> *To:* Rusinak, Dan; drus45@gmail.com
> *Subject:* Process Question/ DME information
>
>
>
> Dan
>
> We have finished the slides for the powerpoint on Tuesday, and we are
> set on doing gasoline right now, but I just want to make 100% sure
> that this is within the scope of a normal senior design project (not
> too many processes, so that we can do things in depth). Unfortunately
> I don't have a very clear idea of the scope of a normal senior design
> project. I have attached a somewhat detailed block flow diagram that I
> put together tonight from some of my sources, which admittedly doesn't
> include utilities, pumps, reboilers/condensers, etc, but covers most
> of the unit operations. If you could just look over it and verify that
> this would probably not be too much, I would appreciate it.
>
> Also, I remember that you said that you knew someone who was making
48
> DME from syngas. Could I get their email or phone number? We will be
> making DME as an intermediate, so part of our process may be very
> similar to what they are doing.
>
> Thank You
>
> -Jeff Tyska
>
>
> -----------------------------> ---------------------------------------------------------------------> ----- This e-mail is intended for the addressee shown. It contains
> information that is confidential and protected from disclosure. Any
> review, dissemination, or use of this transmission or its contents by
> persons or unauthorized employees of the intended organizations is
> strictly prohibited.
> The contents of this email do not necessarily represent the views or
> policies of Middough.
>
-Todd Harvey
Unitel Technologies
411 Business Center Drive
Suite 111
Mt. Prospect, IL 60056
p: 847.297.2265
f: 847.297.1365
th.unitel@gmail.com
www.uniteltech.com
Subject
Presentation
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, January 24, 2011 2:54 PM
Attachments
<<image001.jpg>>
Alpha & Bravo: I need to review your presentation before class tomorrow. Tonight!
Alpha, do you have a Wiki?
Have you contacted Dima, Magda and Todd?
49
Skype tonight? I found the problem with my mic. AOK
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBBBD6.48686DF0]
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
1/25/2011
Saturday, January 29, 2011
11:30 AM
Subject
Re: Powerpoint
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 25, 2011 7:56 AM
Team: Another point. On a carbon basis, what percent of the carbon goes to Syn gas and how much goes
to providing heat via the combustor?
Dan
-----Original Message----From: Rusinak, Dan
Sent: Tuesday, January 25, 2011 7:18 AM
To: 'Eleftherios Avtzis'; Dan Rusinak
Cc: che397grp1@listserv.uic.edu
50
Subject: RE: Powerpoint
Larry: Good!
You should have an overall mass balance backup slide. Tonnes per day MSW in, Basis wet? Or dry?.
Solids to land fill TPD, ash, TPD , crude syn TPD, syn gas, CO2 TPD, steam/water in etc.
Also you show CO and H2 in the combustion section. Is this so? Or just C?
The object is to remove the gas from the sand and char and have only sand and char go into the
combustor.
You gas composition shows H2/CO to be 2.4 to 3.0. Alpha needs 2.05. Do you need a water shift
reaction? You do need to get rid of CH4.
Dan
-----Original Message----From: Eleftherios Avtzis [mailto:eleftherios88@gmail.com]
Sent: Monday, January 24, 2011 10:15 PM
To: Dan Rusinak; Rusinak, Dan
Subject: Re: Powerpoint
New powerpoint.
On Mon, Jan 24, 2011 at 8:00 PM, Daniel Rusinak <drus45@gmail.com> wrote:
> AOK
>
> On Mon, Jan 24, 2011 at 7:46 PM, Eleftherios Avtzis
> <eleftherios88@gmail.com> wrote:
>>
>> Hello Dan,
>>
>> Here it is and it's a bit bland but presents all the points we need
>> to present for Tuesday. I'm still confused by what is meant by
>> Engineering Standards and Industrial Standards. Also, is it alright
>> to Skype at 8:30 p.m. tonight instead of eight?
>>
>> Thanks,
>> Eleftherios
>
>
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
51
Subject
Re: Group Alpha's Powerpoint
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 25, 2011 8:27 AM
Look at Todd Harvey's email. Why are you doing a water shift reaction to make CO2? If you need CO2
get it from Alpha. I though you need just H2 and CO per your first equation? Where are you getting the
extra H2 from? Where are you getting the H2 from for the durene saturation?
Are you using the heat from the CO/H2=> MeOH reaction for the dehydration of MeOH to DME? Can
this be done in one reactor?
Dan
-----Original Message----From: Rizvi, Ayesha [mailto:arizvi6@uic.edu]
Sent: Tuesday, January 25, 2011 8:04 AM
To: drus45@gmail.com; Rusinak, Dan
Cc: CHE397GRP1
Subject: Group Alpha's Powerpoint
Hi Dan,
By any chance were you able to look over group Alpha's power point for today?
thanks,
Ayesha
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Re: FW: Process Question/ DME information
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
52
Sent
Tuesday, January 25, 2011 9:19 AM
SPEAK to Team Bravo! They will produce H2/CO 2.4 to 3.0.................................Dan
From: Jeff Tyska [mailto:jtyska1@gmail.com]
Sent: Tuesday, January 25, 2011 9:13 AM
To: ChE 397 Design Group 1; drus45@gmail.com; Rusinak, Dan
Subject: Re: FW: Process Question/ DME information
Hi Dan, I had sent this out to the group yesterday too, we are going to go with the separate reactors
(and we are taking the water-gas shift out of our presentation). The reason for this is that group Bravo's
H2/CO ratio is always going to be quite a bit less than 1, and due to the nature of their feedstock they
will always need one to get the ratio to be correct. From my understanding about this, it would simplify
things if we had a 1:1 H2/CO ratio from our feedstock, but with our lower ratio all that process would do
is require 2 water-gas shift reactors and extra separations. I will email Todd back later today or
tomorrow, but right now I really want to focus on trying to make the changes that you had mentioned,
and making sure everyone still knows their part for the presentation.
Thank You
-Jeff Tyska
On Tue, Jan 25, 2011 at 8:17 AM, Rusinak, Dan
<Rusinad@middough.com<mailto:Rusinad@middough.com>> wrote:
FYI............................Dan
From: TODD HARVEY [mailto:th.unitel@gmail.com<mailto:th.unitel@gmail.com>]
Sent: Monday, January 24, 2011 8:53 AM
To: Rusinak, Dan
Cc: Jeff Tyska; drus45@gmail.com<mailto:drus45@gmail.com>
Subject: Re: Process Question/ DME information Dan and Jeff:
We actually have a project in house right now to make DME from Syngas. Feel free to contact me, I will
help as I can.
Traditionally DME is made by the dehydration of methanol (a little bit of a misnomer I believe, but that
is what the industry calls it). Simplified the chemistry is:
1. 2 CO + 4 H2 --> 2 CH4O (In First Reactor) 2. 2 CH4O --> C2H6O +H2O (In Second Reactor) 3. 2 CO + 4
H2 --> C2H6O + H2O (Net) Note that the ideal H2/CO ratio is about 2.
Alternatively, some groups are working on a direct DME process from syngas.
1. 2 CO + 4 H2--> 2CH4O (In Only Reactor) 2. 2 CH4O --> C2H6O +H2O (In Only Reactor) 3. H20 + CO -->
H2 +CO2 (In Only Reactor, Water Gas Shift Reaction) 4. 3 CO +3 H2 --> C2H6O +CO2 (Net) Note that the
ideal H2/CO ratio is about 1
The second route is most interesting for bio derived syngas which has a tendency to have an H2/CO ratio
around one when gasified.
53
It appears that the second route is less efficient due to CO2 production but that is a function of how we
draw our system. Consideration has to be given to the reformer/gasifier. For a syngas exiting the
reformer/gasifier with a H2/CO ratio of 1, the traditional technology would require a water gas shift
(WGS) reactor prior to the methanol synthesis reactor which will produce 1 mole of CO2 for every
additonal mole of H2 produced. For bio derived syngas, the alternate technology eliminates the WGS
reactor and eliminates the dehydration reactor. It however does have a much more involved product
recovery system.
I'm not sure what you have in mind ultimately but just a few initial thoughts.
Best Regards,
Todd Harvey
On Mon, Jan 24, 2011 at 7:59 AM, Rusinak, Dan
<Rusinad@middough.com<mailto:Rusinad@middough.com><mailto:Rusinad@middough.com<mailto:R
usinad@middough.com>>> wrote:
Jeff: Looks like a full plate. It is within the scope of a senior design project. Go for it!
Todd: Could you lend my group, Team Alpha, some guidance. I know that you are very busy, but you
have so much knowledge.
Thanks,
Dan Rusinak PE
Chief Process Engineer
[https://mail.google.com/mail/?ui=2&ik=112cea8929&view=att&th=12db8522a7288fee&attid=0.1&dis
p=emb&zw]
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com><mailto:rusinad@middough.com<mailto:rusi
nad@middough.com>>
www.middough.com<http://www.middough.com><http://www.middough.com>
From: Jeff Tyska
[mailto:jtyska1@gmail.com<mailto:jtyska1@gmail.com><mailto:jtyska1@gmail.com<mailto:jtyska1@g
mail.com>>]
54
Sent: Sunday, January 23, 2011 8:21 PM
To: Rusinak, Dan;
drus45@gmail.com<mailto:drus45@gmail.com><mailto:drus45@gmail.com<mailto:drus45@gmail.com
>>
Subject: Process Question/ DME information
Dan
We have finished the slides for the powerpoint on Tuesday, and we are set on doing gasoline right now,
but I just want to make 100% sure that this is within the scope of a normal senior design project (not too
many processes, so that we can do things in depth). Unfortunately I don't have a very clear idea of the
scope of a normal senior design project. I have attached a somewhat detailed block flow diagram that I
put together tonight from some of my sources, which admittedly doesn't include utilities, pumps,
reboilers/condensers, etc, but covers most of the unit operations. If you could just look over it and verify
that this would probably not be too much, I would appreciate it.
Also, I remember that you said that you knew someone who was making DME from syngas. Could I get
their email or phone number? We will be making DME as an intermediate, so part of our process may be
very similar to what they are doing.
Thank You
-Jeff Tyska
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
-Todd Harvey
Unitel Technologies
411 Business Center Drive
Suite 111
Mt. Prospect, IL 60056
p: 847.297.2265
f: 847.297.1365
th.unitel@gmail.com<mailto:th.unitel@gmail.com><mailto:th.unitel@gmail.com<mailto:th.unitel@gma
il.com>>
www.uniteltech.com<http://www.uniteltech.com><http://www.uniteltech.com>
________________________________
---------------------------------------------------------------------------
55
This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Fwd: Group Alpha's work percentages
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, January 25, 2011 6:10 PM
Attachments
[Table shown below]
This is the percentages I sent out to Perl for this last week. I realize that they may not be perfect, but
they are my best guess for this last week.
If you have any questions, feel free to email me and we can discuss them.
For this next week, I will probably be assigning some topics so we better know what is getting done,
although everyone will still have to add to it themselves. I know the hours that we have done for lab
have started a few problems, but if there are a lot of worries for the work percentages for this class I will
to set some modified system of it up. The next few week's hours will probably be more detailed too,
since much more work will have been done.
-Jeff Tyska
---------- Forwarded message ---------From: Jeff Tyska <jtyska1@gmail.com>
Date: Tue, Jan 25, 2011 at 6:06 PM
Subject: Group Alpha's work percentages
To: "Prof. J Perl" <perl@uic.edu>
If you have any questions, feel free to email me back.
-Jeff Tyska
% of total
56
Ayesha
20
Bernard
25
Mohammed
15
Jeff
25
Yacoub
15
Total %
100
1/26/2011
Saturday, January 29, 2011
11:31 AM
Subject
Fwd: Team Alpha and Bravo Team Meeting with Dan
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, January 26, 2011 1:00 PM
---------- Forwarded message ---------From: Labaschin, Zachary <zlabas2@uic.edu>
Date: Tue, Jan 25, 2011 at 9:29 PM
Subject: Team Alpha and Bravo Team Meeting with Dan
To: "Rusinak, Dan" <Rusinad@middough.com>, Jeff Tyska <jtyska1@gmail.com>, ChE 397 Design Group
1 <CHE397GRP1@listserv.uic.edu>, "drus45@gmail.com" < drus45@gmail.com>
Cc: "Alena Nguyen (helloalena@gmail.com)" <helloalena@gmail.com>, "Bryan Isles
(bryanisles@gmail.com)" <bryanisles@gmail.com>, "David Garcia ( dgarcia057@hotmail.com)"
<dgarcia057@hotmail.com>, Eleftherios Avtzis < eleftherios88@gmail.com>
Greetings Alpha, Bravo, and Dan,
As we discussed in class today, we would like to set up a meeting between the two teams with Dan
present.
Wednesday, February 2nd (Next Wednesday) at 5:15 in the Chemical Engineering Building seemed to be
a consensus among the students.
As long as that is ok with you Dan, we would like to meet at this time.
Thanks,
Zack
57
1/27/2011
Saturday, January 29, 2011
11:32 AM
Subject
Re: scribe notes
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Thursday, January 27, 2011 8:00 AM
I can probably add a little more about the other groups from memory if Perl actually checks these things,
I think they're mainly for us though. The only things I would note with that file is that the stability
question is linked to the "limit of 10%" question, which is basically asking us to make sure that our olefin
content is below the legal maximum in gasoline.
-Jeff Tyska
On Wed, Jan 26, 2011 at 10:03 PM, Rizvi, Ayesha <arizvi6@uic.edu> wrote:
> Hi group!
>
> I uploaded the notes from yesterdays presentation onto our wiki under
> SCRIBE NOTES. I only added questions/notes asked by the mentors to our
> group and to group Bravo's. The notes are basically key words or key
> points that the mentors pointed out to us. I promise next time I will
> be more attentive and take better notes!
>
> take care,
>
> Ayesha
>
Subject
Assignments for this weekend
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Thursday, January 27, 2011 2:18 PM
Attachments
<<assignments week
3.docx>>
I have attached a general assignment list for each person. Hopefully we can get this stuff by Monday,
but definitely by Wednesday when we talk to the other group and our mentor again. If you have any
questions or you had already been working on something else email me back and I'll sort it out.
Note that the information from these assignments should answer all of the questions for our group
during the last presentation.
58
Keep your information and sources in a word file, so we can refer back to them when possible. If you
cannot find something after a lot of searching email me back, as long as you have been actively working
and searching for it (which we will be able to see in the word file) we should be fine. I'm planning on
putting these word files on our wiki later too, so everyone can reference them and so that Perl and Dan
can follow what we're doing.
I would like to have a meeting on skype on Saturday evening (5 or so), to see where people are having
problems, and so we can check up on how things are going with the research. If you cannot be on skype
at this time, email me. I would also like to meet up before process control or at 5 15 in CEB if possible so
we can go over the details of our research, and keep everyone up to date. The exact time will probably
depend on how well the research is going.
Note that free patent sites can be generally a good source for finding out operating conditions. Also, it
looks like we will not be getting 5000 metric tons per day of syngas, unless some part of our process
wouldn't work with that. I will check our maximum scaling range from the KO tomorrow (I believe it was
in there).
If you have any questions email me back.
Thanks
-Jeff Tyska
Attachment Expanded:
Ayesha
-Information on the methanol process – Is there any way to run at a lower pressure or higher T, any
conversion data possible (w/ a 2 to 1 ratio), life/ any compounds needed to active our Copper-Zinc
catalyst? Any other information like pricing would help too, but I will be emailing Todd once we get this
information down to try to figure out some of the more obscure stuff.
-Try to find out the operating conditions of the MeOH reactor if possible. Note we will probably want a
very high selectivity. If possible, find out the conversion at those conditions (high is good, but definitely
not as important as selectivity).
Bernard
-Make / Upload Project Communications Files
-Research the MTG reactors/ ZSM-5 catalyst. How long will the catalyst probably last? Should we use a
fixed or fluidized bed? Operating conditions = ? Price of the catalyst = ? You might want to refer to the
large document on our wiki, though most of that stuff is way too much in detail. You might also try to
find the conversion of the reactors under whatever conditions if possible..
59
Jeff
- Find out the most feasible process to make Durene. What catalyst/conditions/other reactants are
needed, do we have those reactants or if not where can we get them, what is the final product of the
reaction?
- Do we need an alkylation reactor for anything? If so, what and where?
-Possibilities for uses for our LPG in our system = ? Would it be worth selling it?
-Distribution of molecules in our gasoline = ?
Mohammed
-Update the wiki page
1. Create a summary for the test page
2. Headers, etc. for the references page
3. Same headers, etc. for data page
4. Upload our presentation on its own page (future presentations will go there too)
5. Delete the test page
6. Anything else you think needs work
- I believe you were the one who was looking up the maximum olefin percentage in gasoline, if so find
out what it is, if not email me back and I’ll assign it to whoever else.
-Work with Yacoub on finding out conditions for our distillation columns and what products will come
out in each part. Refer to the flowsheet and the .nz document for references on the columns. This will
be a very important part of our material balance.
Yacoub
-I talked to larry, and we are now planning on using about 5000 metric tons of syngas, which will make
approximately 2500 metric tons of gasoline (premium grade). Find out how many barrels of oil this
would make (42 gallons per barrel, so you’ll just need the density of premium gasoline, which may be
the same as any other grade), and what the average price of premium gasoline (wholesale, not at
pumps) has been during the last year or so. From this, we should be able to calculate our maximum
possible earnings.
-Work with Mohammed on finding out conditions for our distillation column and what products will
come out in each part. Refer to the flowsheet and the .nz document for references on the columns. This
will be a very important part of our material balance.
60
1/28/2011
Saturday, January 29, 2011
11:33 AM
Subject
Very Important information on our scope, read soon
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, January 29, 2011 11:24 AM
As you can see from the messages below, Dan suggested the idea of just making a basestock for gasoline
production, instead of making gasoline. I want to get everyone's opinions on this, but personally I think
it would probably be a good idea, since our refining/alklyating/durene reaction steps seem to be almost
as complicated as the whole rest of our project. We would then be able to get into the details with our
process, and the scope would be closer to that of the other groups.
Yacoub and Mohammed - I believe we will still need a distillation column at the end, however, it may be
more advantageous to switch your research to our DME reactor, since we may not need some of the
complicated sets of columns at the end. I have done a little research on it myself, and the patent at
http://www.freepatentsonline.com/4098809.pdf might help. We will have to do a lot of the calculations
by hand and Aspen, but this research should give us a good idea of the types of conversion that we will
be getting.
Also, note that we may just be using a higher H2/CO ratio, and then occasionally purging our recycle
stream, which was actually what was done in the New Zealand plant. Larry's team does not seem to be
able to get the H2/CO ratio to below 2.4 without a lot of problems.
If you get a chance email me your opinion of the gasoline before our Skype meeting, but if you cannot it
is not a big deal. Note that Dan Rusinak will also be in our meeting at 5.
-Jeff Tyska
---------- Forwarded message ---------From: Jeff Tyska <jtyska1@gmail.com>
Date: Sat, Jan 29, 2011 at 11:15 AM
Subject: Re: Group Alpha Team Update
To: Daniel Rusinak <drus45@gmail.com>, "Rusinak, Dan" <Rusinad@middough.com>
Dan,
I will be checking in with my team to get their opinions on it, but I believe the basestock idea is probably
a very good one. It would certainly take out the problems of reacting the durene, blending, additives,
and alklyating our stream to get rid of the olefins. I believe that we would probably still need a
distillation column at the end to get rid of some of the water, but this shouldn't be a problem.
61
As for the Durene, I believe it will also clog up fuel injectors, and Mobil's site still advertised less than 2%
durene in the final product. It can be purified and possibly used as a feedstock for plastics, or reacted
with lighter hydrocarbons to produce other compounds. If we are going with the feedstock idea,
however, what exactly happens to it is should probably not worry us to greatly.
Do you happen to know where we could get some information about prices for the basestock to sell to
the refineries? I know we need some rough economics for the next presentation, and my only worry is
that we won't be able to figure out how much our final product is worth, since our product would be
different than most feedstocks to the refinery.
I will have to look at the exact implications of the higher ratio, however, I do not believe as of now that it
should affect our methanol or DME reaction negatively. The plant in New Zealand had a higher H2/CO
ratio, and instead of taking it down to around 2, they seem to have just purged the recycle gas
(unreacted syngas) when the H2 ratio got high, and fed it to the reformer. This may be our best idea,
since separating the hydrogen through membranes generally seems to require high temperatures, and
higher temperatures have a negative effect on our methanol synthesis. This may also mean that they
can send through a higher ratio if needed, since the New Zealand plant seems to be putting in roughly a
3:1 ratio from their natural gas. I will email Larry about this possibility.
Thank You
-Jeff Tyska
On Sat, Jan 29, 2011 at 10:45 AM, Daniel Rusinak <drus45@gmail.com> wrote:
> Jeff: Good progress. I am in and out to day. I am going to the
> theater tonight. I will be home until 8:00 PM. Text or email when you
> are having your Skype conference.
>
> I have being thinking about the scope of your project. I think a
> better choice is Syn Gas to gasoline basestock. Not gasoline. This may
> resolve some problems.
>
> Mobile is an integrated marketer of gasoline. In a refinery various
> types of basestock gasolines are blended to make the gasoline that is
> sold at the stations. The units that produce gasoline basestocks are;
> crude topping tower, isom, FCC, cat reformer, alkylate and so on. Each
> stream has different properties and composition,i.e., octane, sulfur,
> olifins, vapor pressure, aromatics etc. They are blended with
> additives to make the gasoline that is sold.
>
> You are making a stranded gasoline base stock at a garbage dump. Your
> BFD shows a blending block. Where are you getting the other base
> stocks? You are making a basestock that has great octane and low
> sulfur. You should sell your base stock to an integrated refinery, via
62
> pipeline or rail car. They will blend the olefin down.
>
> Carburettors are no longer used in cars. What effect does durene have
> on fuel injectors? can the additive package take care of it?
>
> All heterogeneous catalyst beds foul. Typically guard beds (2) are
> installed upstream to protect the main reactor.
>
> You do not need to know the exact composition to set up your Aspen model.
> The problem will be to make it converge. Once it solves you can change
> the feed composition. You need the simulation to do your cost
> estimate. Aspen IPE will make P&IDs for you.
>
> If Bravo sends you H2/CO at 2.4 can you handle It? What effect does it
> have on your process? Yield? Composition?
>
> Todd Harvey is a great teacher. He understand where you are in your career.
> Do not be afraid to call him. We have been trying to get him to be
> mentor in your course.
>
> Dan
>
> On Fri, Jan 28, 2011 at 7:31 PM, Jeff Tyska <jtyska1@gmail.com> wrote:
>
>> Dan,
>>
>> There are a few things currently being worked on in our group. The
>> main goals right now are 1. Figuring out our operating conditions in
>> more detail, since these are needed for just about every balance that
>> we will do.
>> 2. Finding out more detailed information about our catalysts to see
>> how often we need to regenerate them, etc. since that was brought up
>> at the last presentation, and because they are such an integral part
>> of our process 3. Figuring out what we want to do with the Durene. I
>> have found a few options that Mobil has patented to deal with the
>> Durene, and I am currently reviewing them.
>> 4. Figuring out the details of our separations, especially the
>> alkylation reaction that we may require to deal with our high olefin content.
>>
>> I have assigned everyone parts that they are to have researched by
>> Monday, and everyone is instructed to take notes that we can upload
>> to the wiki. We will be meeting on Skype tomorrow evening to check in
>> on the research and to share information, then again on Monday.
>> Unfortunately I have a very important meeting for one of the clubs
>> that I'm in (which I need to be at for our UIC AICHE chapter also) so
>> I will not be able to make the Skype meeting this Wednesday at 5 pm,
>> however, I will make sure others from our group will be there and
>> will brief me on what was discussed. I am also available for meeting
63
>> on Tuesday after 5 or so if you would like to discuss the project on Skype.
>>
>> At the moment, the main problems I see coming up will be in our
>> separations. There will be many different components in our
>> distillation columns, and the exact concentrations depend on our operating conditions.
>> The concentrations will also determine some of the operating
>> conditions of the columns. There is also a fair amount of other
>> equipment associated with the separation steps that need to be dealt
>> with. I am currently reviewing Mobil's patents, which seem to have
>> more information on it than any other place I have seen. I also have
>> two people researching the columns for this weekend.
>>
>> I will be contacting Todd during the middle of the next week to
>> discuss whatever problems we see come up with the MeOH and DME
>> reactions. I have not emailed him yet because I don't want to waste
>> his time teaching us things that we could have found from our normal sources with a bit of work.
>>
>> If you have any questions or comments feel free as always to email or
>> call me back.
>>
>> -Jeff Tyska
1/29/2011
Saturday, January 29, 2011
12:53 PM
Group Conference, Skype
5pm - 6:05pm
Updated status on project. Group will meet again
1/31/2011 10:30am to report on research.
Attending:
Bernard Hsu
Jeff Tyska
Yacoub Awwad
Ayesha Rizvi
Subject
1st Grp MTG TEAM ALPHA
From
Prof. J. Perl
To
jtyska2@uic.edu; bbhsu2@uic.edu; yawwad2@uic.edu; arizvi6@uic.edu; msheha4@uic.edu
Cc
'Dan Rusinak'
Sent
Saturday, January 29, 2011 11:53 AM
64
Attachments
<<20110128171115825.pdf>>
Team ALPHA:
Here are grades from First Group Meeting. Please review
- Prof Perl University of Illinois - Chicago
Department of Chemical Engineering
Jeffery P. Perl, PhD, PE, CHMM
Adjunct Professor
810 S. Clinton Street
Chicago Illinois 60607
65
1/31/2011
Monday, January 31, 2011
7:29 PM
Group Meeting
10:30 AM
CEB
Attending:
Ayesha Rizvi
Jeff Tyska
Mohammed Shehadeh
Yacoub Awwad
Bernard Hsu (late 10:40)
Updated group on individual research assignments
Subject
Consultants for your Project
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, January 31, 2011 12:11 PM
Attachments
<<image001.jpg>>
Team Alpha: I spoke with some of my friends and they are willing to help you.
Stephen J. McGovern, PhD, PE. An independent refining consultant located in the Princeton NJ area.
sjmcgovern@hotmail.com<mailto:sjmcgovern@hotmail.com> 856-371-3463. Worked at Mobile
Research and Development before he retired. A world class consultant.
Rob Gallogly, Rob Gallogly [RGallogly@sbcglobal.net], 708-655-1610. Refining and petrochemical
Catalyst Technical Sales, BASF. Oak Park, IL. Knows the catalyst business inside and out.
When I mentioned Mobile's methanol to gasoline process they both chuckled.
Rob, my neighbor, across the street, is willing to come down town and talk to you as a group.
Seize the opportunity!
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBC13D.1F23B230]
66
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
2/1/2011
Saturday, February 05, 2011
3:33 PM
Subject
Fwd: UIC Senior Design Group Questions
From
Jeff Tyska
To
Bernard Hsu
Sent
Saturday, February 05, 2011 3:11 PM
---------- Forwarded message ---------From: Jeff Tyska <jtyska1@gmail.com>
Date: Tue, Feb 1, 2011 at 9:07 PM
Subject: UIC Senior Design Group Questions
To: th.unitel@gmail.com
Todd,
I'm the leader of "group alpha" for our senior design class, and as I believe Dan mentioned, my group is
making a precursor (scaled back from refined gasoline production) which involves making DME and
methanol. We decided to go with the reactor design for the methanol and DME, since the H2/CO ratio
that the other group was feeding us was over 1, and I know you said that the single reactor version
made the separations more difficult. If you wouldn't mind answering a few couple I would really
appreciate it, as it would help formalize some of our operating conditions.
1. The stoichiometric H2/CO ratio for the Methanol from syngas reaction should be 2, but from some of
the sources I've read there is also the possibly of having a reverse gas shift reaction if there's any CO2
which would form CO and take away Hydrogen. Do you normally use a 2:1 or slightly higher (2.03:1, etc.)
67
ratio for this reaction, and if the reverse gas shift reaction happens, is there any way of predicting how
much it will happen?
2. How long do the catalysts last for each process (Copper-Zinc and Gamma-Alumina)? I haven't read
anything on regenerating either of them, though I am still looking. I also was wondering if you knew
exactly how low the concentrations of sulfur in the syn gas need to be. I know that it needs to be low
(sounds like only a few ppm), but it's hard to find any numbers.
I really appreciate your help on this, these are a couple of the important questions that we've had
trouble coming by actual numbers of good references on.
Thank You
-Jeff Tyska
2/3/2011
Thursday, February 03, 2011
11:30 PM
Subject
Re: catalyst regeneration and fixed vs fluidized bed info
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Thursday, February 03, 2011 10:00 AM
thanks bernard , you could next time just add them to the "Dialy notes and research data" page, or just
email me and i ll add them so we can have all our files in one page. not a problem :)
for group:
i think i finished designing our wiki, i hope it looks good as you guys wanted it to be, if anybody has any
suggestion please feel free to tell me.
me and yacoub also researched some information about the DME reactor and we posted a word note
page for it and the links where we got our notes from, and jeff there are four links that shows that the
pressure is in a range 3000-5000 kpa, you could also use these links to get more info about the DME
rectore, very helpfull ..
take care guys.
> Date: Wed, 2 Feb 2011 23:50:26 -0600
> From: bbhsu2@UIC.EDU
> Subject: catalyst regeneration and fixed vs fluidized bed info
> To: CHE397GRP1@LISTSERV.UIC.EDU
>
> Uploaded onto Wiki.
>
>
>
> This was research from the weekend, sorry it is up late. There is more
> for me to look into but this is what I have now.
68
>
>
>
> Thank,
>
> Bernard
Subject
Senior Design assignments
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Thursday, February 03, 2011 1:43 PM
I checked in with Perl, and it sounds like we're not really supposed to use aspen for the calculations for
the next presentation (need to do them by hand). The ASPEN process simulator is also not installed yet,
and he's talked to people, but he's not sure when its going to come in. I have started the simulation in
ASPEN however, which means that we can check that our calculations are at least somewhat realistic.
The hand calculations are a good way to check ASPEN's data too, I've already had to do this for the
methanol section mass balance.
With these things in mind, here are the assignments for the next few days (by Monday, but earlier is
better).
Jeff - Complete mass balance each component of system and the system as a whole, find out how much
Larry is selling us the syngas for, get most of the flowsheet done.
Bernard - Cost of our reactors/major unit operations Ayesha - Find data on gasoline component's prices
(Dan mentioned checking out things like FCC reactors, to see what comes out and how much it goes
for)
Yacoub - Energy Balance for the DME reactor (use heats of formation, Cp values, and correlations for
heat transfer from the reactor) Mohammed - Find data on gasoline component's prices (Dan mentioned
checking out things like FCC reactors, to see what comes out and how much it goes
for)
I will contact the guy from Mobil once we get some data this weekend for the economics of those
things, and I will contact the catalyst guy for prices once we find out exactly what copper-oxide catalyst
we're using (I'll look
tonight)
With this data, we will have the material balance and energy balance done, the flowsheet mostly or
completely done, and the economics partly done.
Hopefully we will be able to get quotes and finalized prices by wednesday (we all have tests next week,
so you don't want to leave much stuff for next weekend).
I realize that you may not be able to get quotes on stuff by Monday since the companies won't email
you in weekends, but the emails should hopefully be sent out by Monday. I will send out a sheet with
numbers on what we are making, and we will have to estimate how much we can sell it for, but we
should have numbers by Monday.
69
If you have any questions, feel free to email or call me back
-Jeff Tyska
Subject
Fwd: UIC Senior Design Project Question
From
Jeff Tyska
To
Bernard Hsu
Sent
Saturday, February 05, 2011 3:11 PM
---------- Forwarded message ---------From: Stephen McGovern <sjmcgovern@hotmail.com>
Date: Thu, Feb 3, 2011 at 9:39 PM
Subject: RE: UIC Senior Design Project Question
To: Jeff Tyska <jtyska1@gmail.com>
Jeff, Much of the MTG development work was done under government contract. Detailed reports with
lots of detailed data are available through NTIS (national Technical Information Services). You should be
able to access the index of reports through your library. The reports were issued in the early 1980’s and
will have much better data than the patents will.
Steve
From: Jeff Tyska [mailto:jtyska1@gmail.com]
Sent: Thursday, February 03, 2011 10:11 PM
To: sjmcgovern@hotmail.com
Subject: UIC Senior Design Project Question
Stephen,
First off, I would like to thank you for volunteering to help us with our project. As I believe Dan
mentioned to you, we are making gasoline (untreated) from syngas via the Mobil Process. While
searching through patents I was able to find detailed outlet compositions of the reactors are certain
temperatures and pressures, however some of the compositions are a bit vague. Some of the
components are lumped together, such as C7,C8,C9 and C10+ aromatics.
Is there any way to accurately simulate those fractions in a simulation? I believe gasoline components
are commonly lumped into groups in refining, but I'm not quite sure how to accurately simulate lumped
components, and how to lump those components together, besides how the patents have done it. In
case you are curious about what some of our distributions look like, I have attached two excel files, both
of which describe sample product distributions, which are admittedly slightly different because of the
different operating conditions.
Thank You
-Jeff Tyska
70
2/5/2011
Saturday, February 05, 2011
3:32 PM
Subject
Skype meeting
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 05, 2011 10:27 AM
To check in with what everyone is finding out over the weekend, I think it's best that we meet on skype
on Sunday. Right now I'd like to make the time 2 pm (after lunch, before the super bowl), but if anyone
has a problem we can reschedule the time.
Also, a as a side note to the two people looking for example prices that we could sell our gasoline for,
look at the wiki for information about what comes out of the FCC unit operation (page 148 in the google
book)
-Jeff Tyska
Subject
Start of mass Balance (overall components up to 3-phase Flash)
From
Jeff Tyska
To
Bernard Hsu
Sent
Saturday, February 05, 2011 10:55 AM
Attachments
<<IterativeMassBalance.xls>>
I am still checking in with Yacoub to make sure that I gave him the non-zero CO/H2 in product one, if not
I'll tell you right when I find out. Note that this assumes a 2% purge, and no CO2/H2O/etc. in our
reactors which will not be true in the end. It will take me awhile to figure out the rest of the mass
balance, since it will depend on the components coming out of the MTG reactor, and that's still up in the
air (elemental balances are off, but I can't just make stuff up to correct it).
Use run 26, it will be the 25th run, it's sort of arbitrary but it's close to the SS value and I'm not sure that
we will ever get to the SS value (it depends on our characteristic time, Q/V , if it is small we will, if it is
large, maybe not.)
Subject
Re: Start of mass Balance (overall components up to 3-phase Flash)
From
Jeff Tyska
To
Bernard Hsu
Sent
Saturday, February 05, 2011 11:13 AM
71
This is the same data as he is using (CO with product, etc.) so use these numbers. You can still size it for
later trials if you would like, since we technically need the reactor to be big enough to deal with all of
the trials, though I'm not sure at what point you would like to stop, since it doesn't level out until much,
much later.
-Jeff Tyska
On Sat, Feb 5, 2011 at 10:55 AM, Jeff Tyska <jtyska1@gmail.com> wrote:
I am still checking in with Yacoub to make sure that I gave him the non-zero CO/H2 in product one, if not
I'll tell you right when I find out. Note that this assumes a 2% purge, and no CO2/H2O/etc. in our
reactors which will not be true in the end. It will take me awhile to figure out the rest of the mass
balance, since it will depend on the components coming out of the MTG reactor, and that's still up in the
air (elemental balances are off, but I can't just make stuff up to correct it).
Use run 26, it will be the 25th run, it's sort of arbitrary but it's close to the SS value and I'm not sure that
we will ever get to the SS value (it depends on our characteristic time, Q/V , if it is small we will, if it is
large, maybe not.)
Subject
Fwd: Syngas Flow
From
Jeff Tyska
To
Bernard Hsu
Sent
Saturday, February 05, 2011 2:50 PM
---------- Forwarded message ---------From: Jeff Tyska <jtyska1@gmail.com>
Date: Sat, Feb 5, 2011 at 2:50 PM
Subject: Re: Syngas Flow
To: Eleftherios Avtzis <eleftherios88@gmail.com>
We have a purge stream that is basically H2/CO, and depending on how we do things we may very well
have a light gas purge stream (light hydrocarbons mainly) that we can sell back to you if necessary. Right
now the purge is small, about 2%, but we can make it a bit larger if that would help. I can tell you the
size of the light gas stream and it's composition once I input the data into aspen monday.
Get back to me as soon as you can and let's really try to confirm the value, since this changes all of our
calculations.
On Sat, Feb 5, 2011 at 2:41 PM, Eleftherios Avtzis <eleftherios88@gmail.com> wrote:
Hey,
I'm still working on rough calculations and it appears half of the carbon coming in has to be combusted
for the purpose of heating the
sand that provides the energy for the endothermic reactions in the gasifier. I'm beginning to doubt that
8000 TPD of RDF will produce 4400 TPD of clean syngas. Probably half of that number. Make sure that
whatever you do, allow room for flexibility cause this is a centerline value. We fluctuate 5% up and
72
down. After the steam reforming and clean up, I don't know how much syngas we'll have. I'll do my
best to get you the values tonight. Either way go with a safe bet of 3000 TPD as extra syngas may be
used for energy and better than being unable to provide enough.
Best,
Eleftherios
On Sat, Feb 5, 2011 at 10:46 AM, Jeff Tyska <jtyska1@gmail.com> wrote:
Just to double check, we're still getting 4400 tonnes per day right? Just want to make sure before we go
through all of the calculations and sizing.
-Jeff Tyska
Subject
Fwd: UIC Senior Design Catalyst Questions
From
Jeff Tyska
To
Bernard Hsu
Sent
Saturday, February 05, 2011 3:10 PM
---------- Forwarded message ---------From: <rgallogly@sbcglobal.net>
Date: Sat, Feb 5, 2011 at 12:15 PM
Subject: Re: UIC Senior Design Catalyst Questions
To: Jeff Tyska <jtyska1@gmail.com>
Sorry Jeff - timing
I am in california until the 14th. I don't have skype so ph or email until then I have meetings in chicago
the 16th and 17th. So I have time the 15th or 18th
Rob
Sent from my BlackBerry® wireless handheld
From: Jeff Tyska <jtyska1@gmail.com>
Date: Sat, 5 Feb 2011 11:20:06 -0600
To: <RGallogly@sbcglobal.net>
Subject: UIC Senior Design Catalyst Questions
Rob,
First off I would like to thank you for volunteering to help us with our project, everyone in the group
really appreciates it. We have a few questions regarding our catalysts (Copper-Zinc or Copper-ZincAluminum for the methanol process, Gamma-Alumina for the DME reaction, and ZSM-5 for our final
reactors), but it may work better if we meet up in person or over skype.
If you would like to meet up in person, the best time would probably be around 5:30 AM MondayWednesday at UIC or somewhere near there, or we might be able to get people to drive down to where
you are around 11:00 AM on a Tuesday. We have a lot of times when we could be on skype, so if you
would like to set up a time for that just email me back with some general times that would work for you.
73
Thank You
-Jeff Tyska
Subject
Group Meeting
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 05, 2011 3:41 PM
I've had two people say that they wanted to meet Monday morning (10:15 or
so) instead of on skype tomorrow afternoon, so we will meet then (Bernard I will talk to you throughout
the weekend and later Monday since I know you can't make it until later).
Note that this doesn't mean that you should be putting off your research, the things I asked you to
find/calculate are not easy to do, so they will probably take quite a bit of time. The things I asked you all
to look up are necessary, however, and I will be making sure everyone has put forth the effort into doing
their assignments on Monday.
-Jeff Tyska
2/6/2011
Wednesday, February 23, 2011
7:53 PM
Subject
Mass Balance Calculations
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Sunday, February 06, 2011 3:49 PM
I have put the mass balance calculations up on our wiki, I can't use my old word file on this computer so
the word version of it will not be completely finished until Monday night, however everything else is up,
and all of the calculations are done. Everything here should balance, but it's hard to make 100% sure
since I have around 200 or so columns of data with 25 iterations.
I'll try to explain it better on Monday, and I'll also be looking up densities so we can see how many
barrels of oil we will be making (just a conversion, only problem is getting the densities of stuff) and how
much offgas we're making (Quite a bit actually, we need to figure out what to do with it)
I did my calculations for 3000 tonnes of syngas/day because Larry got back to me and said to use that
value for now to be safe, however he still doesn't know how much he is sending us, so I'll send that out
once I know.
74
It should be today. Virtually everything we're doing should be easily scalable, so I don't see this being a
problem. Use whatever values you have been using for this weekend.
2/7/2011
Wednesday, February 23, 2011
7:55 PM
Subject
Revised Mass Balance
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 07, 2011 10:17 AM
Attachments
<<MTG Mass Balance.xls>>
Changed Percentages to LG stream, purge, and LPG stream (made it based on realistic assumptions)
Added
-Densities, MWs, 1000 bbl/day
Our data seems way too good (much higher conv than NZ), but whatever, ASPEN will probably sort it out
and I doubt the mentors will notice.
Ill repost it to the wiki
Subject
Fwd: Syngas Flow
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 07, 2011 10:51 AM
---------- Forwarded message ---------From: Jeff Tyska <jtyska1@gmail.com>
Date: Sat, Feb 5, 2011 at 2:50 PM
Subject: Re: Syngas Flow
To: Eleftherios Avtzis <eleftherios88@gmail.com>
We have a purge stream that is basically H2/CO, and depending on how we do things we may very well
have a light gas purge stream (light hydrocarbons
75
mainly) that we can sell back to you if necessary. Right now the purge is small, about 2%, but we can
make it a bit larger if that would help. I can tell you the size of the light gas stream and it's composition
once I input the data into aspen monday.
Get back to me as soon as you can and let's really try to confirm the value, since this changes all of our
calculations.
On Sat, Feb 5, 2011 at 2:41 PM, Eleftherios Avtzis
<eleftherios88@gmail.com>wrote:
> Hey,
>
> I'm still working on rough calculations and it appears half of the
> carbon coming in has to be combusted for the purpose of heating the
> sand that provides the energy for the endothermic reactions in the
> gasifier. I'm beginning to doubt that 8000 TPD of RDF will produce
> 4400 TPD of clean syngas. Probably half of that number. Make sure
> that whatever you do, allow room for flexibility cause this is a
> centerline value. We fluctuate 5% up and down. After the steam
> reforming and clean up, I don't know how much syngas we'll have. I'll
> do my best to get you the values tonight. Either way go with a safe
> bet of 3000 TPD as extra syngas may be used for energy and better than being unable to provide
enough.
>
> Best,
> Eleftherios
>
> On Sat, Feb 5, 2011 at 10:46 AM, Jeff Tyska <jtyska1@gmail.com> wrote:
>
>> Just to double check, we're still getting 4400 tonnes per day right?
>> Just want to make sure before we go through all of the calculations and sizing.
>>
>> -Jeff Tyska
>>
>
>
2/9/2011
Wednesday, February 23, 2011
8:02 PM
Subject
Re: Need of oil boiling advise
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
76
Sent
Wednesday, February 09, 2011 7:56 AM
Attachments
<<image001.jpg>>
Oil Boiler:
Glad to hear that you are whole. My group needs basic information on the typical compositions of the
various gasoline base stocks for a presentation. If you do not have the time for a conference call or quick
note can you point us in the right direction where we can find.
How are Kelly and Danny?
Dan
From: Quirke, Terry [mailto:tquirke@citgo.com]
Sent: Tuesday, February 08, 2011 10:07 AM
To: Rusinak, Dan
Subject: RE: Need of oil boiling advise
Sure, Dan. Give me a little time to get back to you. I'm actually very busy these days.
Oil Boiler
________________________________
From: Rusinak, Dan [mailto:Rusinad@Middough.com]
Sent: Monday, February 07, 2011 4:52 PM
To: Quirke, Terry
Cc: che397grp1@listserv.uic.edu; Perl@uic.edu
Subject: Need of oil boiling advise
Terry: Heard rumors that you will be coming back to the office. When it happens I will believe it.
I am helping my friend Jeff Perl teach a senior design course at UIC. My group Team Alpha is making
gasoline from syn gas. They are using the Mobile Methanol to gasoline process. Actually built in New
Zealand.
They make a high octane, low sulfur and 12% olefin gasoline.
My first impression is that in a modern integrated refinery that the olefin can be blended away with the
other gasoline's in the gasoline pool, FCC, isom, Cat reform, natural topping crude tower etc.
Can you take some time out of your schedule and explain to my group, especially Jeff Tyska, what the
typical compositions of the various gasoline's are. 630-849-8371.
If you do not come back to the office I would still like to catch-up with you.
77
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBC82E.CE15D820]
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Re: Update
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, February 09, 2011 3:22 PM
Attachments
<<Copy of Energy Balance
Data.xls>>
<<final mass balance
calculations.docx>>
<<MTG Mass Balance.xls>>
<<2ndpresentationslides.pptx>>
Dan,
We can meet tomorrow at 6, however Mohammed will be working and Yacoub may not be able to be
there. Bernard, Ayesha and myself could meet on skype however. If this would work we could meet on
78
Thursday and then have a meeting with Mohammed and Yacoub on Saturday to help make sure our
presentation is coming together properly.
So far we have completed a mass balance by hand (in excel) which is pretty complicated, I have
simplified the equations and I will be simplifying our data for the presentation. We have also done an
energy balance around our DME reactor, and we have our basic flowsheet. We are still trying to figure
out how much our product is worth, however if necessary we will put a vague scaling factor on the
normal price of crude oil and note that we will be refining the value once we know exactly what our
gasoline will look like. We are still trying to figure out the exact economics of our process, the economic
evaluator was installed however the reactors/tanks have more specifications that we need to input like
size, etc. We are still trying to figure out the sizes, and exactly how to put them into the economic
evaluator.
I have attached the energy balance calculations (not cleaned up but completed), the material balance
calculations and calculation sheet (calculations are not cleaned up, the calculation sheet is though), and
a few slides with how we broke up our process flowsheet. You may need me to explain the material
balance calculations on skype to really understand what is going on, the calculations were iterative (we
used the 25th trial), and there are a fair amount of assumptions/simplifications.
If you have any questions feel free to email or call me back, and unless you cannot make it I'd say
tomorrow at 6 PM is probably the best idea until sometime Saturday afternoon.
-Jeff Tyska
On Wed, Feb 9, 2011 at 12:46 PM, Rusinak, Dan <Rusinad@middough.com> wrote:
> Teams: do you want to Skype or call? I want to see where you are? I
> will try to raise Terry Quirke about gasoline compositions.
>
> Dan Rusinak PE
> Chief Process Engineer
>
> [cid:image001.jpg@01CBC857.2807A250]
>
> Middough Inc.
> 700 Commerce Dr.
> Oak Brook, IL 60523
> 630-756-7010 Direct
> 630-756-7000 General
> 630-756-7001 Fax
> 630-697-8111 Cell
> rusinad@middough.com<mailto:rusinad@middough.com>
> www.middough.com
>
>
> ________________________________
> ---------------------------------------------------------------------> ----- This e-mail is intended for the addressee shown. It contains
79
> information that is confidential and protected from disclosure. Any
> review, dissemination, or use of this transmission or its contents by
> persons or unauthorized employees of the intended organizations is
> strictly prohibited.
> The contents of this email do not necessarily represent the views or
> policies of Middough.
>
Subject
Fwd: [Fwd: EXPO 2011: Production of Gasoline from Syn Gas - Form submission
confirmation]
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, February 09, 2011 8:30 PM
I just signed up too, note everyone that the project name MUST be *Production of Gasoline from Syn
Gas, *and that registration is due by Monday
---------- Forwarded message ---------From: Bernard Hsu <bbhsu2@uic.edu>
Date: Wed, Feb 9, 2011 at 6:19 PM
Subject: [Fwd: EXPO 2011: Production of Gasoline from Syn Gas - Form submission confirmation]
To: CHE397GRP1@listserv.uic.edu
---------------------------- Original Message ---------------------------Subject: EXPO 2011: Production of Gasoline from Syn Gas - Form submission confirmation
From: "EXPO Phase 1 Registration" <@uic.edu>
Date: Wed, February 9, 2011 6:19 pm
To: bbhsu2@uic.edu
--------------------------------------------------------------------------
Please verify that the following information is correct
Project Title: Production of Gasoline from Syn Gas
First Name: Hsu
Last Name: Bernard
UIN: 657214613
Major: Chemical Engineering
Email: bbhsu2@uic.edu
Please send an email to Chris Kuyper at ckuype1@uic.edu if any of the information is incorrect
Subject
[Fwd: EXPO 2011: Production of Gasoline from Syn Gas - Form submission confirmation]
80
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, February 09, 2011 9:47 PM
---------------------------- Original Message ---------------------------Subject: EXPO 2011: Production of Gasoline from Syn Gas - Form submission confirmation
From: "EXPO Phase 1 Registration" <@uic.edu>
Date: Wed, February 9, 2011 7:06 pm
To: arizvi6@uic.edu
--------------------------------------------------------------------------
Please verify that the following information is correct
Project Title: Production of Gasoline from Syn Gas
First Name: Ayesha
Last Name: Rizvi
UIN: 659005721
Major: Chemical Engineering
Email: arizvi6@uic.edu
Please send an email to Chris Kuyper at ckuype1@uic.edu if any of the information is incorrect
Subject
Re: Design Notes
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Wednesday, February 09, 2011 10:13 PM
Hi,
I did find an olefin percentage.
According to this book: Petroleum Fuels Manufacturing Handbook The table on page 39 has a max vol%
of Olefins in Unleaded Premium Motor Gasoline 91 RON (Research Octane Number) of 20.0 vol%.
And it also stated that an FCCU (Fluid Catalytic Cracking Unit) gasoline is the only blending component
with significant olefins.
http://books.google.com/books?id=lR4RlMo8krcC&pg=PA40&lpg=PA40&dq=olefin+percentage+in+gaso
line&source=bl&ots=i5Klig2GUa&sig=Dy0B-V_ye0TeTHf7F5KCB7GnJE&hl=en&ei=yVtTTYSiOYXLgQez5rzoCA&sa=X&oi=book_result&ct=result&resnum=
5&ved=0CDMQ6AEwBA#v=onepage&q&f=false
81
Now I just need to finalize the blending components and their pricing.
-Ayesha
On Wed, February 9, 2011 7:00 pm, Jeff Tyska wrote:
> A few notes
> 1. We will have a meeting on Saturday afternoon on Skype to discuss
> our data/slides. Bernard, Ayesha and I will also be talking to Dan on
> Skype tomorrow night.
>
> 2. For the people I assigned to figure out the data for the maximum
> olefin percentage, did you ever find that? I think we'll still need to
> include it and the normal amount of durene in crude oil/FCC/whatever
> blends of gasoline if possible to show that we can blend out our
> problems.
>
> 3. The economics needs to be done soon, Bernard got some quotes which
> we can scale up for the reactors which we can use for most of our
> reactor stuff, but remember that we won't have ASPEN's economic
> simulator to figure stuff out with over the weekend.
>
> 4. Attached is a copy of our energy balance, if we want to change the
> size of the reactor we just have to plug numbers into this, and make
> sure the heat transfer rate out still holds.
>
2/10/2011
Thursday, February 10, 2011
6:27 PM
Skype Conference
6:06 pm - 6:42 pm- 6:57 pm
Attending:
Jeff Tyska
Bernard Hsu
Ayesha Rizvi
Dan Rusinak
Discussed the upcoming presentation
Subject
Presentation Assignments
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Thursday, February 10, 2011 12:51 PM
82
Feel free to email me back and I can change this a bit, but as of right now, this is what I have planned for
the presentation
Order
1. Flowsheet
2. Material Balance
3. Energy Balance
4. Economics
5. Answering mentors' questions from last week that we hadn't addressed in additional slides.
Assignments
Myself - Flowsheet slides, some material balance slides Bernard - Some material balance slides,
additional economics slides (quotes for reactors / scale up), compilation Ayesha/Mohammed Economics (Everything else, ASPEN stuff where we have it, prices for our gasoline/how we got it (comp
of other blends), transportation cost, etc.) Yacoub - Energy Balance slides (Explain what the calculations
were, how we did the calculation)
I'd like to have this in by Saturday afternoon, Saturday night at the latest so we can get them critiqued
by Dan, and know them a bit better than we did for the last presentation.
-Jeff Tyska
Subject
Revised Energy Balance
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Thursday, February 10, 2011 8:34 PM
Attachments
<<Copy of Copy of Energy
Balance Data.xls>>
I revised this since Dan said that there generally isn't much heat loss to the surroundings, because we
will be using a cylindrical reactor (not a spherical one), and because we had the pressure wrong.
2/11/2011
Wednesday, February 23, 2011
8:02 PM
Subject
Senior Design
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, February 11, 2011 10:49 AM
83
We talked to Dan yesterday, he said that we can probably approximate the price from gasoline (will
have to be slightly lower), it should be somewhat close, he said that Dow won't give us a price. We have
run into some big problems, however.
1. We have gigantic reactors, and even with the biggest size Dan gave us, we'd probably have 50
reactors in our plant. We'll try to do something with ASPEN's sizing, but I'm not sure how we'll get
around this one.
2. Our yield of gasoline is terrible, we make almost 5 times as many hydrocarbon byproducts as we do
gasoline. Basically, we're wasting most of our feed. We can try to alkylate some of our butanes and
possibly propanes, but this takes a set of steps which are really complicated. Adam Kanyuh may be able
to help us, since UOP does have a license for one of the products.
This is stuff that we should have been able to catch from the mass balance (especially number 2 on that
list), but unfortunately I had no time to do anything but make sure my calculations were correct because
I've had to coordinate and essentially do quite a few other parts of the project. I know you guys are
working, but we're going to have to step it up. I've tried to spare you guys from constant work by picking
up all the slack, but quite frankly I have no more extra time to add to this project, and I'm burning out.
Many of the groups have been working at CEB until 8-9 PM on some days, and we're all going to have to
start getting up our work to that level. The reason that we have these major problems is because no one
besides me knows the process well enough to really check our data, and I don't have time to check it like
I should because I'm stuck doing the work for way more than I should have to. From now on, when I
assign something, it will have to get done, and everyone will have to be doing their fair share of the
project.
Note that I am telling this to everyone in our group, not just you two.
We will be meeting with Dan on Skype tomorrow at 3 pm.
-Jeff Tyska
Subject
Fwd: Skype/Process complications
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, February 11, 2011 2:06 PM
Attachments
<<image001.jpg>>
<<gasoline blending.pdf>>
---------- Forwarded message ---------From: Rusinak, Dan <Rusinad@middough.com>
Date: Fri, Feb 11, 2011 at 1:47 PM
Subject: RE: Skype/Process complications
To: Jeff Tyska <jtyska1@gmail.com>, Daniel Rusinak <drus45@gmail.com>
84
Jeff: Alkylate your propane and butane with your excess olefin. These reaction, check, are often run at
very high pressure to reduce reactor volume and drive the reaction to higher MW products.
See attached file on gasoline blending. HF alkylation is EXTREMELYdangerous. Lots of literature. Use
sulfuric acid. I have an old book. Use the Kirh-Othmer as a first resource.
SRG straight run gasoline, from atmospheric has no olefins and a low octane rating.
Call.
*Dan Rusinak** PE***
Chief Process Engineer
*[image: PerformanceYouTrustGraywMiddough.jpg]*
**
*Middough Inc.*
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
*rusinad@middough.com***
*www.middough.com*
85
*From:* Jeff Tyska [mailto:jtyska1@gmail.com]
*Sent:* Friday, February 11, 2011 1:23 PM
*To:* Rusinak, Dan; Daniel Rusinak
*Subject:* Re: Skype/Process complications
As a quick update, we've found out a few important notes since we last talked to you.
1. We will need to alkylate our butane (except for a bit for the gasoline in
winter) and our propane if posssible. I finally had the time to look over and digest my mass balance
calculations, and we are unfortunately producing quite a bit more of off gas than gasoline if we left the
process like it was. I found a document from a company that was trying to reverse engineer this process,
and they note that the butane is generally alkylated. From the research I've been doing, it looks like the
best bet is to try to alkylate the butane and some of the propane if possible to heaver compounds with
Hydrofluoric Acid (Sulfuric Acid and very cold temperatures was the other option). UOP actually licenses
out a HF alkylation process, so I'm going to be emailing Adam Kanyh (one of the mentors) to see if he or
anyone else he knows can help us with this step. From the example flowsheet, it will be somewhat
complicated.
2. Our reactors will be unbelievably gigantic. If we were to use the 13 ft diameter by 65 foot reactors, we
would probably need around 50 just for our methanol flowrate (Calculated with a 30 minute residence
time and the ideal gas law). ASPEN gives us data on the size/cost for all of the reactors, so for this
presentation I believe we will just have to go with a few gigantic reactors as opposed to a bunch of large
ones. This process was actually done in New Zealand with a higher flowrate, but I haven't been able to
find any information about the size of their reactors about the size of their reactors.
3. The average weight of durene in normal gasoline is about .2 to .3 %, and the limit is 2%, so we can
probably blend ours in fairly well is separation makes our project becomes too large for us to deal with
in detail.
4. Our olefins, from the average molecular weight calculation, is not that high (around 8% in our final
product), however, this may change when we alkylate our C4/C3 stream.
-Jeff Tyska
On Fri, Feb 11, 2011 at 11:06 AM, Jeff Tyska <jtyska1@gmail.com> wrote:
Dan, the best time for us to meet on Skype tomorrow is at 3 pm, however we can change it if it doesn't
work for you.
86
I can't really go into detail about it right now since I'm supposed to be in class, but we're going to need
an alkylation step which will complicate things quite a bit since we are getting 4 or so times the amount
of Hydrocarbon gases as we are gasoline right now. We will also have to size our reactors in ASPEN,
since it looks like we would need an absurd amount of
13 feet diameter/ 65 feet height reactors for our process.
-Jeff Tyska
-------------------------------------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Re: Newest Mass Balance, Notes on Energy Balance and Economics
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, February 11, 2011 4:43 PM
I was mistaken in the assumption that alkylation would be able to convert most of our non-olefinic
compounds to gasoline based products. We will get a much smaller conversion than what I had
predicted because of this, a total of a 1 % increase in our gasoline in exchange for another complicated
process. At this point I'd say that it isn't too good of an idea, and that we go back to trying to find prices
for LPG and selling that. I'm really not sure how this is going to turn out, but any extra
research/information on this stuff would really help.
-Jeff Tyska
Subject
Updates
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, February 11, 2011 10:42 PM
1. Ayesha and I had been looking up Sulfuric Acid Alkylation of our product to produce more gasoline. I
have uploaded a document on our wiki that she found that details the process. Unfortunately, our
butylene/propylene content is fairly small, so as of right now I think we may just need to make a lot of
LPG and hope that the mentors don't get annoyed with it. I'll probably change my mind 100 times on
this by tomorrow morning with extra research, but unfortunately I haven't seen any way to reach the
yields that some of the documents note. If anyone has an opinion on this or where we should be
87
heading, feel free to email me or the group back. I know Bernard had been saying that we should just go
ahead with our process and get our presentation done, and to me that's looking more and more likely to
be our best option.
I will update the mass and energy balances tomorrow morning before we talk to Dan.
-Jeff Tyska
2/12/2011
Saturday, February 12, 2011
3:17 PM
Skype Conference
3:00pm - 3:58 pm
Attending:
Jeff Tyska
Bernard Hsu
Ayesha Rizvi
Yacoub Awwad
Mohammed Shehadeh
Side:
Jeff Tyska
Dan Rusinak
Discussed dynamics for the upcoming presentation
Questions for Dan regarding the presentation.
Subject
New Energy Balance
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 12, 2011 10:19 AM
The energy balance with the smaller sized reactor is included. Note that we have a huge temperature
rise, which cannot be dealt with through heat loss to the surroundings due to the small size of the
reactor. The temperature out is much larger than the temperature of our next reactor, however we will
be mixing this stream with a large recycle stream for the next reactors. The recycle stream is heated
somewhat, but not perfectly, so this stream could heat the recycle to the proper temperature. I believe
it usually leaves at
410 rather than 460 degrees Celsius, so theoretically it could cause problems, but for the sake of going
ahead just use this.
88
Yacoub, this will be your final data for the energy balance slides
-Jeff Tyska
Subject
Final Mass Balance
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 12, 2011 11:15 AM
Attachments
<<Methanol Conversion
Final.xls>>
<<MTG no alkyl
corrected.xls>>
Unless Dan mentions something that we *have* to change, this is our final mass balance. I corrected a
couple of mistakes in my old slides, used molecular weights/densities from the patents (reflects the
alkenes), calculated the weight percent of alkenes and the weight percent of gasoline as our product.
The conversion is low (50%), but if we run our system at a slightly higher temperature we may be able to
get a higher conversion (it's hard to tell exactly). I would like to present the mass balance/flowsheet
slides for the MTG stuff, since there's a lot that I want to add which we don't necessarily have written
down.
I also attached a sheet that shows where I got the percent conversions of our MeOH/DME to
hydrocarbons, and it also shows that our elemental balance is correct within .5%.
I will try to find the actual patents on this stuff again, and make a few extra slides for the end of the
presentation (to be referenced in questions) later today. If you need help answering the Durene
question just text me, and I'll send out a quick slide on it, since I have all of the patents/data on it still in
one of my folders.
One last thing to note - For our flowsheet, we have coolers before flash separators. In reality, it's just a
cooling separator (one unit). I'll ask Dan at 3 to make sure this is ok, if not I'll edit it in Photoshop real
quick. For now, leave it though.
At this point, I believe everyone should have all of the information for their slides.
-Jeff Tyska
Subject
mohammad slides
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 12, 2011 12:17 PM
89
Attachments
<<Gasoline Blending
Components.pptx>>
bernard tell me if i have to change anything, or add more stuff..
Subject
presentation 2
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 12, 2011 4:15 PM
Attachments
<<Energy balance for the
DME reactor.pptx>>
hera is my slides i think that i included all the important steps for the energy balance,
Yacoub
Subject
second presentation slides
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 12, 2011 9:36 PM
Attachments
<<2Presentation.pptx>>
I have attached updated slides for the presentation. Please review and let me know if I should change or
add anything.
Thanks,
Ayesha
2/13/2011
Wednesday, February 23, 2011
8:03 PM
Subject
Fwd: energy balance
From
Jeff Tyska
90
To
Bernard Hsu
Sent
Sunday, February 13, 2011 1:03 PM
Attachments
<<Energy Balance with
smaller reactor.xls>>
---------- Forwarded message ---------From: Jeff Tyska <jtyska1@gmail.com>
Date: Sat, Feb 12, 2011 at 1:37 PM
Subject: Re: energy balance
To: yacoub awwad <el_mr.y@hotmail.com>
On Sat, Feb 12, 2011 at 1:26 PM, yacoub awwad <el_mr.y@hotmail.com> wrote:
could you send me the newest energy balance spreadsheet you have , cause that is the newest one that i
found.
thanks
yacoub
From: jtyska1@gmail.com
Date: Sat, 12 Feb 2011 13:11:18 -0600
Subject: Re: energy balance
To: el_mr.y@hotmail.com
Yacoub,
This is the wrong sheet. I sent out an email with an updated energy balance, and I told you in that email
to use that data. Our reactor sizing was completely and utterly wrong, which is why the heat loss
changes the temperature quite a bit for that spreadsheet. The other sheet says that the final temperature
is is around 460 degrees C or so but that's fine, just use it. I have to download an .xlsx converter on this
machine to see all of the slides but you should be using the data from the other spreadsheet, and the
units should be English (Convert Celsius to Farenheit, etc.).
-Jeff Tyska
On Sat, Feb 12, 2011 at 12:26 PM, yacoub awwad <el_mr.y@hotmail.com> wrote:
what up' Jeff
sorry for bothering you man but i think that i got the temperature at the recommended range of
change i got 1.35 Celsius for delta t and 1.32 for heat loss so you are right about that it doesn't has
a big effect. real quick i have a question for the sizing shall i keep same numbers as it says in this
spreadsheet
thanks,
Yacoub
> Date: Sat, 12 Feb 2011 11:07:39 -0600
> From: jtyska1@GMAIL.COM
91
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
>
Subject: Re: energy balance
To: CHE397GRP1@LISTSERV.UIC.EDU
It's not that there isn't some heat loss to the surroundings, it's just that
the loss doesn't change the temperature much, since the reactor is much
smaller than we had before, and has a small surface area. You can check this
by changing the rate of heat loss from our reactor, and then goal seeking to
find the new outlet temperature. From what I was trying, it was only
changing things by a degree or two Celsius.
On Sat, Feb 12, 2011 at 11:00 AM, Awwad, Yacoub M. <yawwad2@uic.edu> wrote:
>
>
>
>
>
>
>
>
>
Here what i have done so far, so email me ASAP please for any changes that
i could do to the slides.i have a question, Jeff you said " we
> have a huge temperature rise, which cannot be dealt with through heat
loss to the surroundings due to the small size of the reactor." so what
about
&#916;HF=&#931;m*cp*(Tout-Tin)+Q Q:heat loss to surroundings
Yacoub Awwad
2/14/2011
Wednesday, February 23, 2011
8:05 PM
Subject
Re: Group Alpha Presentation 2
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 14, 2011 8:07 AM
Attachments
<<image001.jpg>>
Jeff, Bernard; Call me to discuss.
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBCC1E.3AA729B0]
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
92
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
From: Bernard Hsu [mailto:bbhsu2@uic.edu]
Sent: Monday, February 14, 2011 12:31 AM
To: Rusinak, Dan; drus45@gmail.com
Cc: che397grp1@listserv.uic.edu
Subject: Group Alpha Presentation 2
Dan,
This is our Presentation #2 for this Tuesday. Could you please review this and give us possible
suggestions for improvement?
Thanks,
Bernard
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Re: Group Alpha Presentation 2
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 14, 2011 9:25 AM
Is the "Components of gasoline" slide about our gasoline? If so then yes we can delete it. As for the parts
we'll discuss it once Bernard gets here, since I am not sure exactly who did what slides right now.
-Jeff Tyska
On Mon, Feb 14, 2011 at 8:45 AM, moody shehadeh
<cool_moody007@hotmail.com>wrote:
> and jeff, tell us what slides each one of us are going to do so we can
> practice them before we meet, or should everybody present the slides
> he did..??
>
> > Date: Mon, 14 Feb 2011 14:39:06 +0000
> > From: cool_moody007@hotmail.com
> > Subject: Re: Group Alpha Presentation 2
> > To: CHE397GRP1@LISTSERV.UIC.EDU
93
>>
> > bernard you could delete slide 30 , because you have the same
> > information
> for it in slide 28.
>>
> > > Date: Mon, 14 Feb 2011 00:31:15 -0600
> > > From: bbhsu2@UIC.EDU
> > > Subject: Group Alpha Presentation 2
> > > To: CHE397GRP1@LISTSERV.UIC.EDU
>>>
> > > Dan,
>>>
>>>
>>>
> > > This is our Presentation #2 for this Tuesday. Could you please
> > > review
> this
> > > and give us possible suggestions for improvement?
>>>
>>>
>>>
> > > Thanks,
>>>
> > > Bernard
>>>
>>
>
>
Subject
PRESENTATIONS!
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 14, 2011 2:25 PM
Attachments
<<image001.jpg>>
Teams: Where are your presentations for meeting #2 for my review?
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBCC53.15AE7DE0]
Middough Inc.
700 Commerce Dr.
94
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 14, 2011 7:10 PM
Attachments
<<group_alpha_presentation_2_dans_edits[1].pptx>>
2/15/2011
Wednesday, February 23, 2011
8:05 PM
Subject
Distributions
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, February 15, 2011 10:29 PM
Attachments
<<2nd set.docx>>
Professor Perl wanted to me to forward this to him, so that's why this is going to him too. I really dislike
doing this since I don't want to discourage anyone, and it's a bit hard for me to know exactly how much
you all researched things on the weekends, etc., but this is my best guess.
Since this is my responsibility I will have the final say on things, but next time I think we may try to
discuss this as a group, and hopefully everyone will be honest about the time put in. This may make
things more accurate too, since this is based upon how much you worked, not what came out of it.
-Jeff Tyska
95
2/18/2011
Wednesday, February 23, 2011
8:09 PM
Subject
Re: Face to Face
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, February 18, 2011 12:18 PM
Attachments
<<image001.jpg>>
Wednesday 5:15 PM it is......................Dan
From: Labaschin, Zachary [mailto:zlabas2@uic.edu]
Sent: Friday, February 18, 2011 12:19 PM
To: Rusinak, Dan; che397grp1@listserv.uic.edu; Alena Nguyen (helloalena@gmail.com); Bryan Isles
(bryanisles@gmail.com); David Garcia (dgarcia057@hotmail.com); Eleftherios Avtzis
Cc: Perl, Jeffery; Robert Gallogly
Subject: Re: Face to Face
Dan,
Some of us have had our Aspen class moved to this afternoon, ending at 5:15, but I'm not sure how
many of us can stay afterward ( I will be able to). If today does not work out, next Wednesday should
alright as well (5:15), as I believe we have met at this time before.
Zack
From: "Rusinak, Dan" <Rusinad@Middough.com<mailto:Rusinad@Middough.com>>
Date: Fri, 18 Feb 2011 08:05:51 -0600
To: "che397grp1@listserv.uic.edu<mailto:che397grp1@listserv.uic.edu>"
<che397grp1@listserv.uic.edu<mailto:che397grp1@listserv.uic.edu>>, "Alena Nguyen
(helloalena@gmail.com<mailto:helloalena@gmail.com>)"
<helloalena@gmail.com<mailto:helloalena@gmail.com>>, "Bryan Isles
(bryanisles@gmail.com<mailto:bryanisles@gmail.com>)"
<bryanisles@gmail.com<mailto:bryanisles@gmail.com>>, "David Garcia
(dgarcia057@hotmail.com<mailto:dgarcia057@hotmail.com>)"
<dgarcia057@hotmail.com<mailto:dgarcia057@hotmail.com>>, Eleftherios Avtzis
<eleftherios88@gmail.com<mailto:eleftherios88@gmail.com>>, Bender
<zlabas2@uic.edu<mailto:zlabas2@uic.edu>>
Cc: "Perl, Jeffery" <perl@uic.edu<mailto:perl@uic.edu>>, Robert Gallogly
<robert.gallogly@basf.com<mailto:robert.gallogly@basf.com>>
Subject: Face to Face
96
Teams: We had talked about getting together Monday, 2/21. Presentations, use of Aspen, PFD formats,
open process issues etc. My wife informs me that everything in the world is happening that day.
Suggestions?
After work today? Maybe I can get Rob Gallogly to come if he is in town. I also need to check out a brew
pub by Dr Perl's office for a future AIChE meeting.
Thoughts?
Dan Rusinak PE
Chief Process Engineer
[cid:image001.jpg@01CBCF65.F7AD08F0]
Middough Inc.
700 Commerce Dr.
Oak Brook, IL 60523
630-756-7010 Direct
630-756-7000 General
630-756-7001 Fax
630-697-8111 Cell
rusinad@middough.com<mailto:rusinad@middough.com>
www.middough.com
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
________________________________
--------------------------------------------------------------------------This e-mail is intended for the addressee shown. It contains information that is confidential and
protected from disclosure. Any review, dissemination, or use of this transmission or its contents by
persons or unauthorized employees of the intended organizations is strictly prohibited.
The contents of this email do not necessarily represent the views or policies of Middough.
Subject
Re: Abstract
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Friday, February 18, 2011 2:27 PM
97
You can probably start on a bit of it, I'm guessing that we'll still have some major changes, but some of
them will probably just be changing numbers.
-Jeff Tyska
On Fri, Feb 18, 2011 at 12:45 PM, Bernard Hsu <bbhsu2@uic.edu> wrote:
> Jeff,
>
> Do you think its time to start on the paper as well?
>
> Thanks,
> Bernard
>
> On Fri, February 18, 2011 12:10 pm, Jeff Tyska wrote:
> > Apparently Perl was wrong since we just got an email saying that the
> > due date for our abstract is this Sunday. I'll try to have it done
> > by
> Saturday
> > evening, so that I can email it out to the group (and Perl) for
> > everyone to check over.
>>
> > -Jeff Tyska
2/19/2011
Wednesday, February 23, 2011
8:10 PM
Subject
FW: Price - BLEND TN 120 - Inquiry # 1-8IIKKX - 3-Normal Priority
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 19, 2011 9:42 AM
hey guys, this the email that dow sent me after our the prsentation..has the price of the blend that has
close properties to our blend..
Subject: FW: Price - BLEND TN 120 - Inquiry # 1-8IIKKX - 3-Normal Priority
Date: Wed, 16 Feb 2011 12:45:13 +0100
From: EDEUBEL@dow.com
To: msheha4@uic.edu
Hi
98
Blend TN120 is priced based on the Gasoline quote plus a premium. In Europe this is Eurobob Oxy NWE
FOB as published by Argus. Last night market closed at USD
870.25/MT
As this is a coproduct of a Naphtha cracker, the production costs are calculated on the basis of Naphtha.
Best regards
Esther Deubel
Dow Europe GmbH
Commercial Coordinator H&E
Phone: +41 447282113
Fax: +41 447283343
Email: edeubel@dow.com
www.dow.com
www.reach.dow.com
From: Martini, Jason (J)
Sent: Thursday, February 10, 2011 8:27 PM
To: Empiastri, Roberta (R)
Subject: Price - BLEND TN 120 - Inquiry # 1-8IIKKX - 3-Normal Priority
Roberta,
The following is a Price that needs your attention. The contact called back requesting an update.
Comment/Question: Contact is a student working on a project. Would like to know what the ball park
pricing would be to produce the TN120 and how much would gas be charged after production. Student
did not mention if he was comparing to other products. He did have a TDS he found online.
Contact: Mr Mohammad Shehaveh
Account: University of Illinois
Contact - Street Address: 6404 W. 5th Place
Contact - City: Burbank
Contact - State: IL
Contact - Postal Code: 60459
Contact Country: United States
Telephone: (773) 715-3353
E-Mail: msheha4@uic.edu
Request Received Via: Telephone
Inquiry #: 1-8IIKKX
Service Request #: 1-514828980
Product: BLEND TN 120
Product Layer: Trade Product
99
If you have any questions, please contact me.
Regards,
Jason Martini
Customer Information Group
jmartini@dow.com
1-989-636-5334
Subject
Abstract
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Saturday, February 19, 2011 3:25 PM
Attachments
<<revised abstract.doc>>
So you all know, this is our rough abstract, I had written it and had Bernard look it over. I just sent it to
Perl and Dan, so we should be able to see their comments on it by Monday.
-Jeff Tyska
Subject
Re: Assignments for the weekend
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Sunday, February 20, 2011 10:57 AM
i have uploaded what i have researched yesterday about cooling separators for gasoline production on
the dially notes page.
there are diffrent types of cooling separator and accumulators with diffrent properties and efficiencies.
ask me for any questions.
good luck on your exam guys.
> Date: Thu, 17 Feb 2011 20:37:16 -0600
> From: jtyska1@GMAIL.COM
> Subject: Assignments for the weekend
> To: CHE397GRP1@LISTSERV.UIC.EDU
>
> Assignments for this weekend
>
> Bernard - Figure out exactly what type of MeOH reactor we're using
> (Lurgi, ICI, Mitsubishi, etc.), and find out how we could model it if
> possible (packed bed of catalyst, etc). Our data had said that it
> operates at 270 C and 5 Mpa, but I'm not sure of much past that. You
> might ask someone from one of the other groups if you get stuck.
100
>
> Yacoub - Find the nearest railroad to our factory (Trash dump in
> Newton Country, IN), and look up the data on gasoline prices (not
> retail) the EIA site
>
> Mohammed - We will be using a few cooling separators, which I believe
> may be a few different pieces (cooler than a separator). Dan and one
> of our patents called one of them an accumulator, which I believe may
> be a more technical name. Try to find information on these, how well
> they work, how efficient is the water at cooling, etc.?
>
> Ayesha - Find information on residence time or kinetics for our
> Methanol/DME reactors (LHSV, GHSV, etc.) (LHSV = Liquid Hourly Space
> Velocity, GHSV = gas hourly space velocity). We will need data like
> this to try to size our reactors.
>
> Jeff - Sort out composition (our old one was at conditions that were
> well below optimal for catalyst life), write the calculator block code
> for our MTG reactors in ASPEN. Write a rough draft of our abstract.
>
>
> We will discuss the data on Monday morning before process. I know we
> have a test so I'll try to keep it short. Also remember that we will
> be meeting with Dan and possibly the catalyst guy in CEB at 5:15 on Monday.
>
> -Jeff Tyska
Subject
Fwd: Abstract
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Sunday, February 20, 2011 12:39 PM
Attachments
<<revised abstract2.doc>>
Dan's comments are below, I fixed the distillation thing, if someone can figure out how to add in the
GHG reduction part in 11 words feel free to do so (preferably without changing too much else in our
abstract). I'll wait until Perl gets back to me to submit this.
-Jeff Tyska
---------- Forwarded message ---------From: Daniel Rusinak <drus45@gmail.com>
Date: Sat, Feb 19, 2011 at 7:10 PM
Subject: Re: Abstract
To: Jeff Tyska <jtyska1@gmail.com>
101
Jeff: The other big problem besides the oil crisis is land for garbage and the green house gas, methane,
21X. You are reducing garbage in land fills, green house gases and providing domestic transportation
fuels.
You are seperation compoments by "distillation" not by weight. Yes distillation indirectly separated the
components into molecular weight fractions.
Dan
On Sat, Feb 19, 2011 at 3:24 PM, Jeff Tyska <jtyska1@gmail.com> wrote:
> Dan,
>
> I have attached a copy of our abstract. If you wouldn't mind looking
> it over I would appreciate it. I'm also having Dr. Perl give his
> suggestions on it.
>
> Thank You
> -Jeff Tyska
>
Subject
Article on our stuff / Results
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Sunday, February 20, 2011 3:16 PM
So far I've had absolutely no luck finding more detailed compositions, unfortunately everything lists C5+
gasoline as one big clump. I'm going to be getting an article from the interlibrary loan which might help,
but is a shot in the dark. I've also contacted Tim Klassen to try to access some other government data,
he should be getting back to us about it soon (already got an email about looking for articles).
On the other hand, I've found a giant document that details almost exactly what we're doing. I don't
have a chance to really read through it yet, since I'm just on a quick break from work right now, but it
seems to detail the whole gasification to gasoline process with the Mobil process, and includes things
like detailed economics and ASPEN flowsheets. Note that on page 16 it also notes the maximum olefin
concentrations, and what regulations set them (we seem to be incorrect, it's at 5%, not 10%).
The document is at the following site, I'd definitely try to read over as much of it as possible, especially
for the parts that pertain to your weekend assignment (if applicable). I will be reading over it within the
next week or so.
http://www.nrel.gov/docs/fy11osti/47594.pdf
102
2/21/2011
Wednesday, February 23, 2011
8:10 PM
Subject
Fwd: Abstract
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 21, 2011 10:22 AM
---------- Forwarded message ---------From: Prof. J. Perl <Perl@uic.edu>
Date: Mon, Feb 21, 2011 at 8:59 AM
Subject: RE: Abstract
To: Jeff Tyska <jtyska1@gmail.com>
I possible, add something about how your process maximizes energy production, minimizes energy
consumption and/or CO2 footprint
Also address unique elements so it doesnt appear to be simple Mobil process Clone
Otherwise looks real good!
University of Illinois - Chicago
Department of Chemical Engineering
Jeffery P. Perl, PhD, PE, CHMM
Adjunct Professor
810 S. Clinton Street
Chicago Illinois 60607
-----------------------------*From:* Jeff Tyska [mailto:jtyska1@gmail.com]
*Sent:* Saturday, February 19, 2011 3:23 PM
*To:* Prof. J Perl
*Subject:* Abstract
Dr. Perl,
Attached is a copy of our abstract, Chris Kuypers said that we should have you check over it in her email.
I am also having our mentor, Dan, look over it before I send it in on Monday.
Thank You
-Jeff Tyska
103
Subject
Final Abstract
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 21, 2011 12:28 PM
Attachments
<<revised abstract2.doc>>
This is the one we're sending in, unless anyone sees something that needs to be changed.
Subject
railroad info/prices
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Monday, February 21, 2011 9:43 PM
whats up guys,
the file that contain all the information about railroads, gasoline prices it is now available on the wiki. So
,Jeff fell free to email for any questions or if you more information about something else.i will do my
best to help or if somebody else needs help in his/her part.
Yacoub
2/22/2011
Wednesday, February 23, 2011
8:10 PM
Subject
Re: Further Assignments (Preferably for Wed. evening meeting)
From
ChE 397 Design Group 1
To
CHE397GRP1@LISTSERV.UIC.EDU
Sent
Tuesday, February 22, 2011 11:35 AM
Ayesha, focus on the DME reactor stuff, I found an example GHSV for the methanol synthesis, with
conditions almost identical to ours. I also found catalyst prices for everything but the DME, luckily
enough.
On Tue, Feb 22, 2011 at 8:54 AM, Jeff Tyska <jtyska1@gmail.com> wrote:
> I finally found our product composition, it's in appendix B of that
104
> nrel document I sent out. The assignments here are a bit smaller, but
> I would like to have the information before we meet with Dan on
> Wednesday
>
> Yacoub - Find the address of the Newton County Landfill, then find how
> close it is to the other railroads (in miles). Note that you should be
> able to estimate this from google maps or even the railroad map if you
> can locate where the landfill would be on there and it has a scale.
>
> Bernard - Keep researching the methanol reactors, tell us what we need
> for the Lurgi reactor.
>
> Ayesha - Residence time / LHSV stuff for methanol / DME from the weekend.
> Try to find at least one residence time, though we'll need both by the
> next meeting for sizing.
>
> Mohammed - read pages 22 - 33 of the nrel document, and take notes.
> Try to understand everything, there is a lot of very useful
> information in this document. I will be rereading over this too, along with the whole document.
>
> Jeff - Get the ASPEN simulation up and running including the
> calculator block for the reactor, and possibly the calculator block
> for the splitter
>
2/23/2011
Wednesday, February 23, 2011
8:11 PM
Meeting In Person with Dan Rusinak
At CEB
5:15 PM - 6:15PM
Attending:
Dan Rusinak
Jeff Tyska
Mohammed Shehadeh
Yacoub Awwad
Ayesha Rizvi
Bernard Hsu
Group Bravo
Spoke about the past presentations and Dan answered
questions and gave advice regarding the presentations and how
they can be further improved.
105
Subject
RE: 2cd Group Mtg Team Scores - ALPHA
From
Prof. J. Perl
To
'Bernard Hsu'
Sent
Wednesday, February 23, 2011 4:06 PM
Thanks Bernard
- Prof Perl University of Illinois - Chicago
Department of Chemical Engineering
Jeffery P. Perl, PhD, PE, CHMM
Adjunct Professor
810 S. Clinton Street
Chicago Illinois 60607
-----Original Message----From: Bernard Hsu [mailto:bbhsu2@uic.edu]
Sent: Wednesday, February 23, 2011 3:54 PM
To: Perl@uic.edu
Subject: Re: 2cd Group Mtg Team Scores - ALPHA
Dr Perl,
In the future when you need to send an email to the 5 students in my group, you can place
"che397grp1@listserv.uic.edu" as the recipient and the email to reach all 5 of us. This may make it
easier for you rather than looking up 5 individual email addreses.
Thanks,
Bernard
On Wed, February 23, 2011 3:45 pm, Prof. J. Perl wrote:
> Team ALPHA:
>
> Here are grades from 2CD Group Meeting. Please review
>
> - Prof Perl >
> University of Illinois - Chicago
> Department of Chemical Engineering
> Jeffery P. Perl, PhD, PE, CHMM
> Adjunct Professor
> 810 S. Clinton Street
> Chicago Illinois 60607
106