Abstract
A method for providing polyvinyl chloride (PVC) comprises the following steps: a)
providing electricity and an alkali metal chloride solution, preferably Li, K and/or Na, in a
chlor-alkali electrolysis cell (17) and obtaining Cl2 and an alkali metal hydroxide, preferably
NaOH, LiOH and/or KOH, and H2 by electrolysis; b) providing electricity and water in a
further electrolysis cell (12) and obtaining H2 and O2; c) obtaining CO2 from synthesis gas, the
CO of which has been oxidised using the O2 of step b), or by direct input of CO2 from
sustainable sources or emission sources and subsequently using the H2 obtained in step a)
and/or step b) and the CO2 in a catalytic methanol conversion process and obtaining methanol;
d) using the methanol obtained in step c) in a catalytic methanol dehydration process, resulting
in ethylene and water; e) using the ethylene obtained in step d) and the Cl2 obtained in step a)
in the direct chlorination of ethylene dichloride (EDC); f) feeding the ethylene dichloride
(EDC) into a cracking reactor to produce vinyl chloride monomer (VCM) and HCl; and h)
polymerising the vinyl chloride monomer (VCM) and obtaining polyvinyl chloride (PVC). The
aim is to provide a method for producing sustainable PVC which is based on renewable, costeffective starting materials, fulfils all the method steps, and at the same time minimises the
emission of water pollutants and air pollutants and reduces the required inputs of energy and
water.
Description
METHOD
AND
APPENDIX
FOR
PROVIDING
SUSTAINABLE
POLYVINYL
CHLORIDE (PVC)
The invention relates to a process for providing sustainable polyvinyl chloride (PVC)
and an integrated plant for the production of sustainable polyvinyl chloride
The use of renewable "green" energy sources is on the rise due to consumer interest in
renewable energy, declining wind and solar costs, climate change concerns and government
regulations around the world, especially as a result of the low cost of solar cells or solar cells
Wind turbines represent a practical alternative to conventional carbon-based energy.
Nonetheless, renewable "green" energy sources often suffer from a serious drawback,
and given the necessary environmental conditions such as solar or wind intensity, the place of
power generation is often far from the main energy consuming areas, and wind, solar, water
and tidal power become frequent These renewable energy sources often produce too much or
too little electricity (eg, based on night / day cycles or changing weather conditions) The
majority of cases are connected to the electricity grid and can deliver surplus electricity to it,
the supply of power grid with inconsistent energy is associated with economic disadvantages,
resulting in higher energy costs and additional power losses Not all battery systems are able to
buffer large amounts of energy, and batteries can store electrical power but not transport it
easily. An alternative is to store the electrical energy in a chemical carrier, e.g. As hydrogen or
methanol.
Hydrogen can store and transport energy, including RESP (Remote Excess Sustainable
Power), but requires extremely low temperatures and high pressures. Methane can store RESP,
but has a lower chemical value compared to methanol and ammonia.
The amount of RESP in the world has grown exponentially in recent years and is
projected to continue to increase until 2030. In order to achieve the goals of the Paris Climate
Decade for World Decarbonisation, it is essential to produce not only energy but also chemicals
in a sustainable way. However, there are significant problems in the production of fuels and
chemicals using purely biological processes; u. a. Typically, batch reactors and CSTR reactors
are required which are less efficient and whose scale is difficult to scale, complicated core and
extraction processes are needed, reactions take a long time, a considerable amount of water is
consumed or made unrecyclable, and it requires beautiful sources of biomaterials, such as
sugar. For example, in places with significant chemical production such as KSA, India, Texas,
Qatar and West China only limited fresh water and limited quality biomaterials available.
However, salt water, industrial water or low-quality water and sources of waste or emissions
C0 2 or syngas, low-quality biomass, wood chips, stems, leaves, sticks, garbage, animal and
human excretions leading to syngas as well as C0 2 emissions can be gasified.
Unlike PET, there is currently no sustainable PVC process. However, in many
applications of PVC, a renewable source of this important plastic would be beneficial. A
surprising technical advantage described herein is that PVC produced from RESP can be
remotely manufactured by the present innovation in the vicinity of renewable energy sources,
can be sold with an environmental friendliness premium, a reduction of the total cost of
chemical plants by using very cost-effective to free starting materials, receipt of C0 2 credits
and avoidance of C0 2 taxes and penalties based on decarbonisation contracts. Conventional
PVC synthesis methods, such as the "carbide" process, use CaC 2 as an intermediate source of
acetylene, but CaC 2 is often produced in a high-energy and high-emission process based on
lime and coke based on the quality of the carbon source Other air pollutants such as CO, C0 2 ,
hydrocarbons and SO x are emitted into the atmosphere and the adjacent landscape.
The object of the present invention is therefore to provide a process for the production
of PVC, which is based on renewable low-cost educts, covering all process steps while
minimizing the emission of water and air pollutants and reduces the required energy and water
input.
US 2011/0183143 A1 discloses a PVC resin composition with an increased content of
renewable carbon.
WO 2015/086153 A1 discloses a composite system for producing steel with a blast
furnace for pig iron production, a converter for crude steel production and a gas pipeline system
for gases, the system operating when pig iron and / or crude steel are produced. According to
the invention, the composite system also includes a chemical or biotechnological system
connected to the gas piping system and a hydrogen generating system.
US 2013/0288143 A1 discloses a fuel cell with a seawater electrolyzer, an integrated
plant and methods for producing natron, ammonia, urea and PVC. The process discloses the
use of ethylene from a cracking column. The object of the present invention is achieved by a
method according to claim 1. Preferred embodiments of the invention are the subject of the
corresponding subclaims.
Another object of the present invention is to provide a plant for producing sustainable
polyvinyl chloride (PVC) according to claim 14. Preferred embodiments of the invention are
the subject of the respective subclaims.
The process of the invention for providing polyvinyl chloride (PVC) comprises the
following steps. Step a) comprises providing electricity, preferably renewable electricity, and
an alkali metal chloride solution, preferably Li, K and / or Na, in a chloroalkali electrolysis cell
resulting in Cl 2 , alkali metal hydroxide, preferably NaOH, LiOH and / or KOH, and H 2 leads by
electrolysis. The person skilled in the art knows various types of chloralkali electrolysis cells,
eg. B. membrane cell, diaphragm cell or Castner-Kellner method (mercury cell). This creates
chlorine z. B. by
In parallel, be encompassed in a preferably alkaline or PEM electrolytic cell by
electrolysis in a step b), electricity and feed water or re- cycliertes water obtained H 2 and
0. 2 Steps a) and b) together provide H 2 , O 2 , alkali metal hydroxide, preferably NaOH, LiOH
and / or KOH, and Cl 2 . The above-mentioned water electrolysis may be necessary to provide
a sufficient amount of hydrogen in the later process steps. The method further comprises in a
first alternative variant of step c) the synthesis of C0 2 from syngas, the CO was oxidized using
the obtained in the preceding process steps 0 2, or thereafter by direct C0 2 entry from
sustainable sources or emission sources and Using H 2 obtained in the previous step b). The
C0 2 obtained is further used in a catalytic methanol conversion process leading to methanol. This
catalytic methanol conversion process can include various types of processes that are well
known in the art. Suitable catalysts are u. a. Cu, Sn, Cr, Zn and Al, preferably in the form of
the respective oxides. Exemplary process conditions may e.g. B. in the pressure range of 80
bar and temperatures in the range of 230 ° C vary.
Alternatively, the production of methanol may also be carried out, for example, by
catalytically reacting carbon monoxide with hydrogen according to the following equation (3a).
Thus, the production of methanol can also be made from synthesis gas, or alternatively
used as starting material a gas mixture of CO and C0. 2
In accordance with the present invention, methanol may also be provided in step c)
alternatively by the use of an available syngas source from an existing process and then the
above-mentioned methanol catalytic conversion process leading to methanol.
In accordance with the invention, methanol may also be provided in step c) alternatively
by a direct gasification step, preferably by a fluidized bed gasification process, e.g. For
example, the high temperature Winkler (HTW) method, in which obtained in the preceding
process step b) 0 2 for partial oxidation and temperature increase can be used and optionally in
the first process step a) obtained Al ka I i meta 11 hy d oxide , preferably NaOH, LiOH and /
or KOH, can be used. Preferably, this oxygen requires no further purification, whereby the
process according to the invention eliminates expensive production of oxygen from air. Alkali
metal hydroxides, preferably NaOH, LiOH and / or KOH, may act as catalysts in the
gasification or by providing a basic reaction medium. Thus, the by-product of the chloroalkali
electrolysis NaOH (or LiOH or KOH) and the oxygen obtained in the electrolysis of water can
surprisingly and advantageously be used directly in the carbon precursor processing steps
required to produce PVC. The methanol obtained in the above-mentioned process step c) is
then used in a catalytic methanol dehydration step d), which leads to ethylene and water.
Exemplary reaction conditions can be found, for. In S. Hussain, M. Mazhar, S. Gul, K.
Chuang, A. Sanger, Bull. Korean Chem. Soc. 2006, Vol. 27, No. 11 or by a MTO (methanolto-olefins) method, e.g. Using zeolite-based catalysts. The water can be reused as process water
or electrolysis, thereby minimizing the overall input of additional water in the process. In
addition, "polar" water can be easily separated from "polar" ethylene. The yield of ethylene
produced from methanol can be increased by a few steps including metathesis, which will be
described later in the present document. The ethylene obtained in the preceding step d) and the
Cl 2 obtained in process step a) are combined in the direct chlorination of ethylene dichloride
(EDC) in step e).
The reaction of z. B. by metal chlorides, Fe, Al, Cu Sb, more preferably
FeCl 3 catalyzed. Exemplary reaction conditions can be found in Tarrit et al., US 2011/0183143
AI, paragraph [0041] to [0052]. Nonetheless, aberrant reaction conditions can be used without
departing from the scope of the invention. The produced ethylene dichloride (EDC) is then fed
to a cracking reactor in step f) to produce vinyl chloride monomer (VCM) and HCl.
Exemplary cracking conditions can be found in Tarrit et al., US 2011/0183143 Al,
paragraph [0068], z. B. at a temperature between 400 ° C and 500 ° C and a pressure between
25 and 30 bar. Nonetheless, aberrant reaction conditions can be used without departing from
the scope of the invention. The method optionally comprises a step g). This step g) involves
recycling HCl as Cl 2 using an HCl electrolysis reactor and reusing Cl 2 in the direct
chlorination of step e). Alternatively, the process may comprise an oxychlorination step:
This step allows the further reaction of HCl from the cracking step with O 2 from the
water electrolysis and ethylene to produce additional ethylene dichloride. Exemplary
oxychlorination conditions can be found in Tarrit et al., US 2011/0183143 Al, paragraph
[0053]. Nonetheless, aberrant reaction conditions can be used without departing from the scope
of the invention. The resulting C 2 H 4 Cl 2 is fed to the cracking reactor in step f), the water
can be reused as process, cooling or electrolysis water.
The resulting vinyl chloride monomer (VCM) can be further purified, e.g. By
distillation, and in step h) to polyvinyl chloride (PVC), for example by suspension
polymerizations, emulsion polymerization and / or bulk polymerization or combinations
thereof. PVC is ideal for transportation as it has no health and safety problems under normal
conditions.
In addition, the process according to the invention makes it possible to produce PVC in
a continuous mode of operation in comparison with the discontinuous mode of operation,
avoids the use of calcium carbide, avoids market fluctuations in the price of ethylene and, in
particular, does not produce CO 2 . The manufactured PVC can be transported without safety,
health and environmental concerns and sustainably produced in locations with no or low fresh
water and bioprocessing capacity. In view of the above-mentioned reaction steps, the inventive
drive the synthesis of high quality PVC from recycled compounds such as biomass or C0 2 from
technical processes. This use of naturally occurring carbon can be verified by 1 4 C carbon
isotope analysis. In addition, in the process of this invention, numerous reaction by-products
such as water, O 2 , NaOH (or LiOH or KOH) and HCl can be recycled by direct use or reuse
in the process described above.
Table 1: Qualitative comparison of C0 2 produced by PVC process:
In accordance with the teachings of the invention, the terms "using the O" 2 "j" H " 2j Cl 2
j
H 2 O, HCl or NaOH (or LiOH and / or KOH) obtained in the preceding process steps may
include the use of additional O 2j H 2 j Cl 2 j H 2 O, HCl or NaOH (or alkali metal hydroxides,
LiOH and / or KOH) from other sources or processes.
In a preferred embodiment, the catalytic methanol dehydration in step d) comprises a
shape-selective conversion of methanol to ethylene using SAPO or similar cagecatalysts,
preferably followed by an additional process to increase the ethylene yield. These additional
steps may involve propylene self-metathesis to additional ethylene.
Preferably, the water electrolysis cell comprises an alkaline or PEM (polyelectrolyte multilayer
or proton exchange membrane) or HT (high temperature) or SO (solid oxide) water electrolysis
cell.
In another preferred embodiment, direct C0 2 input from sustainable sources or sources
of emissions includes combustion or fermentation of natural or fossil carbon sources. Including
the partial combustion of (renewable) biogas from anaerobic biodegradation for the production
of syngas and high-grade heat and use of the heat to support the energy demand of the process
according to the invention, preferably the syngas-to-methanol process. The direct introduction
of CO 2 from sustainable sources or emission sources preferably involves gasification (G) of
organic material, preferably biomass, waste, manure, lignin, biogas, bioethanol and / or wood
chips.
In a preferred embodiment, the gasification (G) comprises processes based on fluidized
bed gasification, direct quenching, high temperature Winkler (HTW) gasifier or KoppersTotzek. As described in the main process, oxygen obtained from gas electrolysis is used in
gasification (G). This oxygen preferably does not require further purification and avoids
expensive production of oxygen from air.
In another preferred embodiment, the gasification (G) is carried out with partial
oxidation (POX) or catalytic partial oxidation (CPOX).
In a further preferred embodiment, in the gasification (G), additional methanol is obtained for
use in step d).
Preferably, the water obtained in step d) is recycled and reused in the process. The reuse
of water allows the use of the method of the invention in arid areas throughout the world.
In a preferred embodiment, the electricity in step a) and / or b) is provided by a renewable
energy source, preferably solar, wind, geothermal, hydro, tidal and / or biogas.
Preferably, the electricity is stored or buffered by a battery unit, more preferably by a
redox flow battery, or stored or buffered as Cl 2 , H 2 , alkali metal hydroxide, preferably
NaOH, LiOH and / or KOH, and / or O 2 . In particular, storing as a chemical carrier Cl 2 , H 2 ,
alkali metal hydroxide, preferably NaOH, LiOH and / or KOH, and / or O 2 allows a more
flexible use of the energy provided independent of power fluctuations. The inventive chemical
energy storage can therefore overcome some of the major disadvantages of renewable energy
sources, such as variable wind power or night-day cycles of solar power.
The invention further provides a plant or integrated system for producing sustainable
polyvinyl chloride (PVC) with an electric power source or compound, a chloralkali electrolysis
cell unit, and a water electrolysis unit. The person skilled in the art knows various types of
chloralkali electrolysis cells, eg. B. membrane cell, diaphragm cell or Castner-Kellner method
(mercury cell). The plant further comprises a storage unit for a gas containing any partial
pressure mixtures of CO and C0 2 , or a gas production unit, which can be any partial pressure
mixtures of CO and C0 2 generated on. The C0 2 storage unit comprises suitable containers or
tanks for gaseous, liquid or solid carbon dioxide. The plant further comprises a methanol
synthesis unit or unit which produces methanol by gasification of biomass, as described above
in the process of the invention. In the methanol synthesis unit obtained in the above-described
storage-C0 2 or C0 2 -Herstellungseinheit for conversion of the C0 2 in methanol by a well
known in the art for a catalytic unit methanol conversion process C0 2 may be used. The plant
further comprises an ethylene synthesis unit and optionally an ethylene yield increasing unit
including a propylene self-metathesis unit. The plant further comprises an ethylene dichloride
(EDC) synthesis unit, a vinyl chloride monomer (VCM) synthesis unit and a PVC
polymerization reactor.
The system according to a further development of the invention preferably further
comprises an HCI recycling unit using HCl electrolysis to Cl 2 and / or a unit for diverting
substantially pure oxygen obtained in the process into the PVC process for carrying out
oxidations such as oxychlorination , on.
In a preferred embodiment, the gasification unit (GU) comprises fluidized-bed
gasification, direct quenching, high-temperature Winkler (HTW) gasifier or gasifier based on
Koppers-Totzek. As described in the main method, gasification (G) uses oxygen from the
electrolysis of water.
Preferably, the methanol synthesis unit has a gasification unit.
In a preferred embodiment, the gasification unit comprises a high-temperature Winkler
(HTW) gasifier for the production of additional methanol directly from biomass.
Preferably, the electrical power is provided by a sustainable and renewable energy
source, preferably solar, wind, geothermal, hydro, tidal, and / or biogas. The site may be located
in remote areas near the sustainable and renewable energy source due to the low required fresh
water supply and the high recycle rates of H 2 , 0 2 , HCl and NaOH.
In a preferred embodiment, the renewable energy source is connected directly to the
system.
Preferably, the electrical power is kept stable (buffering) despite fluctuations of the
renewable energy source, preferably by a battery unit, more preferably by a redox flow battery,
battery-backed or as Cl 2 , H 2 , alkali metal hydroxide, preferably NaOH, LiOH and / or KOH,
and / or 0 2 stored or buffered. Surprisingly, the Combining the plant according to the invention
with the renewable power source the production of high quality PVC and the storage of
otherwise unusable energy peaks.
The invention will be further described below with reference to an embodiment with
reference to the figures. The figures do not limit the scope of the invention.
FIG. 1 shows a flow chart of some partial steps of the process according to the
invention;
FIG. 2 shows a flow chart of the remaining partial steps of the method according to the
invention.
First, reference is made to Figure 1, which shows a zein schematic flow diagram of the
method according to the invention. As the first starting material, water 10 is supplied via line
11 to a first electrolysis device 12, in which hydrogen 13 is produced, and oxygen 14. As a
second starting material, a NaCl solution 15 is fed via a line 16 to a second electrolysis device
17, in which a chloroalkali Electrolysis is performed in which hydrogen 18, chlorine 19 and
NaOH 21 are produced. In the method according to the invention, the two electrolysis devices
12, 17 can be operated with renewable energy.
The other Haupteduct C0 2 can enter the inventive method via different routes. Route
A involves the gasification of biomass 20 in which the caustic soda (NaOH) 21 or, alternatively,
LiOH or KOH obtained in the saline electrolysis 17 can be used in the gasifier 22. NaOH can
serve as a catalyst or as a tool to provide basic media. Any excess NaOH 23 produced in the
chloralkali electrolysis can be removed from the system and used or sold elsewhere.
Another route B for the provision of C0 2 and then methanol is according to an
alternative variant of the invention synthesis gas 24. This contains, for example, the gases
carbon monoxide and hydrogen and next to carbon dioxide and water.
The gas obtained in Route A as well as in Route B contains not only hydrogen but also
carbon monoxide, which can be converted into carbon dioxide and hydrogen in a water gas
shift reaction 25 with steam. Subsequently, remaining CO can be eliminated by preferred
oxidation (preferential oxidation, PROX) in the device 26. Alternatively, in the inventive
method according to route C directly z. B. be used by combustion-supplied C0 2 27, which is
fed via line 28 into the plant. The gas mixture obtained in Route A as well as in Route B after
the preferred reaction contains, in addition to carbon dioxide and hydrogen, even small amounts
of water. The device 26 for the preferred oxidation of carbon monoxide can also be supplied
via the branch line 14 ' oxygen, which was generated in the first electrolyzer 12.
The carbon dioxide obtained in the manner described above can be reacted with
hydrogen either directly to sustainable ethylene or by way of methanol and subsequent
dehydration.
As can be seen from FIG. 2 in conjunction with FIG. 1, the carbon dioxide obtained
according to one of the three variants A, B or C can then be passed via the line 29 to a methanol
synthesis device 30 in which it is catalytically reacted with hydrogen to form methanol. This
methanol is then dehydrated to ethylene in the dehydrator 31 as described above. Alternatively,
in the process according to the invention it is also possible to use a further source for the
production of additional ethylene, for example by obtaining further ethylene by propylene selfmetathesis. The ethylene thus obtained is again preferably reacted with the electrolytically
recovered chlorine 19 by direct chlorination in the chlorinating apparatus 32 to yield ethylene
dichloride. Ethylene dichloride is then reacted in a cracking reactor 33 to give vinyl chloride
monomers, from which polyvinyl chloride (PVC) can then be made by polymerization in the
reactor 34. The sustainable PVC product 35 produced according to the invention is discharged
from the plant.
The above-mentioned steps thus enable the production of sustainable ethylene and PVC.
LIST OF REFERENCE NUMBERS
10 water
11 line
12 first electrolysis device
13 hydrogen
14 oxygen
14 ' branch line for oxygen
15 sodium chloride
16 line
17 second electrolysis device
18 hydrogen
19 chlorine
20 biomass
21 sodium hydroxide
22 Gasification device
23 sodium hydroxide
24 synthesis gas
25 water gas shift reaction
26 preferred oxidation
27 carbon dioxide
28 line
29 line
30 methanol synthesis device
31 Dehydration device
32 chlorinating device
33 cracking reactor
34 Polymerization reactor
35 sustainable PVC as a product
claims
A process for providing polyvinyl chloride (PVC) comprising the steps of:
a) providing electricity and an alkali metal chloride solution, preferably Li, K and / or Na, in a
chloralkali electrolysis cell (17) and obtaining Cl 2 and an alkali metal hydroxide, preferably
NaOH,
LiOH
and
/
or
KOH,
and
H 2 by
electrolysis;
b) providing electricity and water in another electrolytic cell (12) and obtaining H 2 and O 2 ;
c) obtaining C0 2 from synthesis gas whose CO has been oxidized using the O 2 from step b),
or by direct C0 2 input from sustainable sources or emission sources and then using in step a)
and / or step b) obtained H 2 and C0 2 in a catalytic methanol conversion process and obtaining
methanol;
d) using methanol obtained in step c) in a catalytic methanol dehydration, which leads to
ethylene and water;
e) using ethylene obtained in step d) and Cl 2 obtained in step a) in the direct chlorination of
ethylene dichloride (EDC);
f) feeding the ethylene dichloride (EDC) into a cracking reactor to produce vinyl chloride
monomer (VCM) and HCl;
and
h) polymerizing vinyl chloride monomer (VCM) and obtaining polyvinyl chloride (PVC).
2. The process of claim 1 wherein the HCl is recycled to Cl 2 using an HCl electrolysis reactor
and Cl 2 is used in step e) or HCl is further reacted with 0 2 obtained from step b) and obtained in
step b) Ethylene for the production of additional ethylene dichloride (EDC) by oxychlorination
for use in step f).
3. The process of claim 2 wherein the catalytic methanol dehydration in step d) comprises shape
selective conversion of methanol using SAPO or similar cagecatalysts, preferably a further step
to increase ethylene yield including propylene self metathesis.
4. The method according to any one of claims 1 to 3, wherein the further electrolytic cell (12)
comprises an alkaline, PEM, HT or SO-Wasserelektrolysezelle.
5. The method according to one or more of claims 1 to 4, wherein synthesis gas and heat by
partial oxidation of renewable biogas produced by anaerobic biodegradation, is generated.
6. The method according to one or more of claims 1 to 5, wherein the direct C0 2 entry from
sustainable sources or emission sources comprises a combustion or fermentation of natural or
fossil carbon sources.
7. The method according to one or more of claims 1 to 6, wherein the direct C0 2 entry from
sustainable sources or emission sources, a gasification (G) of organic material, preferably
biomass, waste, manure, lignin, biogas, bioethanol and / or Woodcutting, includes.
8. The method of claim 7, wherein the gasification (G) comprises processes based on fluidized
bed gasification, direct quench, high temperature Winkler (HTW) gasifier or Koppers- Totzek.
9. The method of claim 7 or 8, wherein in the gasification (G) with partial oxidation (POX) or
catalytic partial oxidation (CPOX) is used.
10. The method according to one or more of claims 7 to 9, wherein in the gasification (G)
additional methanol for use in step d) is obtained.
11. The method according to one or more of claims 1 to 10, wherein the water obtained in step
d) is recycled and reused in the process.
12. The method according to one or more of claims 1 to 11, wherein the electricity in step a)
and / or b) by a renewable energy source, preferably solar power, wind power, geothermal,
hydropower, tidal power and / or biogas, is provided.
13. The method of claim 12, wherein the electricity is stored or buffered by a battery unit, more
preferably by a redox flow battery, or as Cl 2 , H 2 , alkali metal hydroxide, preferably NaOH,
LiOH and / or KOH, and / or 0 2 is stored or buffered.
14. Plant for producing sustainable polyvinyl chloride (PVC) with:
- an electrical power source or connection;
a chlor-alkali electrolysis cell unit (17);
- Another electrolysis unit (12) for water electrolysis; a storage unit for a gas containing any
partial pressure mixtures of CO and C0 2 , or a gas production unit which generates any partial
pressure mixtures of CO and C0 2 ,
a methanol synthesis unit (30)
- or a unit that produces methanol by gasification of biomass;
an ethylene synthesis unit (31)
an ethylene dichloride (EDC) synthesis unit (32);
a vinyl chloride monomer (VCM) synthesis unit (33);
and a PVC polymerization reactor (34).
15. The system of claim 14, further comprising:
a unit for increasing the ethylene yield including a propylene self-metathesis unit and / or
Units for water recycling and water storage and / or
an HCI recycle unit using HCl electrolysis to Cl 2 and / or
Units for diverting substantially pure oxygen resulting from the process in the PVC process
for carrying out oxidations.
16. Plant according to claim 14 or 15, wherein the methanol synthesis unit comprises a
gasification unit (GU).
17. Plant according to claim 16, wherein the gasification unit comprises a high-temperature
Winkler (HTW) carburetor for producing additional methanol directly from biomass.
18. Plant according to one or more of claims 14 to 17, wherein the electrical power is provided
by a sustainable and renewable energy source, preferably solar power, wind power, geothermal,
hydropower, tidal power and / or biogas.
19. Plant according to claim 18, wherein the renewable energy source is connected directly to
the system.
20. Plant according to one of claims 18 or 19, wherein the electrical power is held despite
fluctuations of the renewable energy source as a stable output (buffers), preferably by a battery
unit, more preferably by a redox flow battery, battery-buffered or as Cl 2 , H 2 , alkali metal
hydroxide, preferably NaOH, LiOH and / or KOH, and / or 0 2 is stored or buffered.