WO2015014527A1 - Process for producing high purity co by membrane purification of soec-produced co - Google Patents

Process for producing high purity co by membrane purification of soec-produced co Download PDF

Info

Publication number
WO2015014527A1
WO2015014527A1 PCT/EP2014/062362 EP2014062362W WO2015014527A1 WO 2015014527 A1 WO2015014527 A1 WO 2015014527A1 EP 2014062362 W EP2014062362 W EP 2014062362W WO 2015014527 A1 WO2015014527 A1 WO 2015014527A1
Authority
WO
WIPO (PCT)
Prior art keywords
bar
membrane
soec
retentate
permeate
Prior art date
Application number
PCT/EP2014/062362
Other languages
French (fr)
Inventor
Niklas Bengt Jakobsson
Claus FRIIS PEDERSEN
Original Assignee
Haldor Topsøe A/S
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Haldor Topsøe A/S filed Critical Haldor Topsøe A/S
Priority to CA2916959A priority Critical patent/CA2916959A1/en
Priority to CN201480043120.8A priority patent/CN105431221A/en
Priority to US14/903,186 priority patent/US20160151739A1/en
Publication of WO2015014527A1 publication Critical patent/WO2015014527A1/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/06—Tubular membrane modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/08—Flat membrane modules
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/20—Carbon monoxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0208—Other waste gases from fuel cells
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B01D2311/251—Recirculation of permeate
    • B01D2311/2512—Recirculation of permeate to feed side
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a process for producing high purity carbon monoxide (CO) by membrane purification of CO produced in a solid oxide electrolysis cell (SOEC) .
  • CO carbon monoxide
  • a solid oxide electrolysis cell is a solid oxide fuel cell (SOFC) run in reverse mode, which uses a solid oxide or ce- ramie electrolyte to produce e.g. oxygen and hydrogen gas by electrolysis of water. It can also be used to produce CO from carbon dioxide (C0 2 ) , which is led to the fuel side of the SOEC or SOEC stack with an applied current. Excess oxy ⁇ gen is transported to the oxygen side of the SOEC, option- ally using air, nitrogen or CO 2 to flush the oxygen side, and afterwards the product stream from the SOEC, containing CO mixed with CO 2 , is subjected to a separation process.
  • SOFC solid oxide fuel cell
  • Carbon monoxide of high purity is an important raw material for the synthesis of chemicals. Most reactions for the syn ⁇ thesis of chemicals require high temperatures as well as high pressures, and therefore the CO used should have the lowest possible content of carbon dioxide (C0 2 ) which cor ⁇ rodes the reactor by oxidation. Additionally, CO 2 may limit the equilibrium conversion of the reaction in which the produced CO takes part. CO 2 may also inhibit the kinetics of the reaction where CO is used.
  • US 6,787,118 is related to selective removal of CO. More specifically it deals with catalyst compositions useful for destruction of volatile organic carbon compounds (VOCs) in an oxygen-containing gas stream at low temperatures and for selective oxidation of carbon monoxide from a hydrogen- containing gas. This patent is not related to any use of membranes.
  • VOCs volatile organic carbon compounds
  • EP 0 129 444 and US 4,539,020 concern high- purity CO obtained by pressure swing adsorption (PSA) .
  • PSA pressure swing adsorption
  • PSA pressure swing adsorption
  • SOEC is an attractive alternative to PSA, mainly due to its simplicity, because a membrane separation unit operates without any moving parts, but also due to a reduced capital expenditure (CAPEX) because of its modular nature.
  • Gas separation membranes are presently used for the removal of CO2 from natural gas and syngas.
  • Such membranes can be based on polymers or zeolites coated on alumina tubes, and they generally have a selectivity towards transporting CO2 through the membrane, whereas hydrocarbons, 3 ⁇ 4 and CO are held back on the retentate side.
  • Typical selectivity con ⁇ stants for CO/ CO2 are between 5 and 20, and fluxes may vary from 20 to 200 Nm 3 /h per m 2 membrane area.
  • Membrane separation is driven by the difference in partial pressure, and thus it is most suitable for removing the bulk of an impurity, such as CO2 , whereas an extensive mem ⁇ brane area is required to reach a high purity when the driving force for separation decreases.
  • the mem ⁇ branes may be of planar or tubular shape, and they may be used in a single membrane unit or in multiple membrane units in series or in parallel.
  • the driving force for separation can be boosted by applying a high absolute pressure on the retentate side of the mem- brane and applying an approximate vacuum on the permeate side of the membrane.
  • a CAPEX limitation for installing a multi-stage compressor to reach a high pressure and the power required to drive the compressor.
  • the maximum pressure difference is also limited by the mechanical strength of the membrane and of the mem ⁇ brane module.
  • the present invention relates to a selective separation of CO from a mixture of CO and CO 2 , especially in relation to small scale production of CO by SOEC electrolysis.
  • the principle is quite similar to a reflux column within dis ⁇ tillation.
  • the invention concerns a process for pro- ducing high purity carbon monoxide (CO) by membrane purifi ⁇ cation of CO produced in a solid oxide electrolysis cell (SOEC), said process comprising the following steps:
  • the driving force for CO2 flux through the membrane is increased.
  • the driving force for transportation of CO through the membrane is decreased, and thus the yield of CO can be increased when high purities of CO are targeted.
  • the outlet permeate stream is fully or partly recycled back to the SOEC as a feed gas together with fresh CO2 in the above step (7), whereby the CO2 yield is increased.
  • the moderate pressure on the retentate side of the membrane can be from 250 bar g down to 3 bar g, preferably from 175 bar g down to 3 bar g, more preferably from 40 bar g down to 3 bar g and most preferably from 20 bar g down to 5 bar g.
  • the lower pressure on the permeate side of the membrane can be between -0.8 bar g and 50 bar g, preferably between -0.8 bar g and 10 bar g, more preferably between -0.8 bar g and 3 bar g, even more preferably between -0.8 and 2 bar g and most preferably between -0.3 bar g and 0.5 bar g, especial- ly between 0 and 0.3 bar g.
  • the splitting of the retentate stream into two separate parts also has analogy to the reflux at the top of a dis- tillation column.
  • the SOEC unit has a function similar to the reboiler in a distillation unit; see the appended fig 1.
  • the membrane unit is preferably designed with a tubular membrane or multiple planar membranes connected in series where the retentate and permeate streams are operated in counter-current mode. This implies that the enriched CO re ⁇ flux stream from the retentate side enters (after expan ⁇ sion) the permeate side of the membrane unit in the oppo- site end from the feed gas entering the membrane unit from the SOEC unit.
  • the process according to the invention can be further outlined with reference to fig. 1, which shows a solid oxide electrolysis cell (SOEC) unit with the oxygen side at the top, the electrolyte in the middle and the fuel side at the bottom.
  • SOEC solid oxide electrolysis cell
  • CO 2 is led to the fuel side of the SOEC unit with an applied current to convert CO 2 to CO and transport any oxygen surplus to the oxygen side of the SOEC unit.
  • CO 2 is also led to the oxygen side to flush this side, but air or nitrogen may also be used for this purpose.
  • Flushing the oxygen side of the SOEC unit has two advantages, more spe ⁇ cifically (1) to reduce the oxygen concentration and relat ⁇ ed corrosive effects and (2) to provide means for feeding energy into the SOEC unit, operating it endothermic.
  • the product stream from the SOEC contains mixed CO and CO 2 , which is led to a compressor C, which serves to establish a high absolute pressure on the retentate side of the mem ⁇ brane.
  • a lower pressure is applied on the permeate side of the membrane by leading part of the CO product stream through a pressure reduction valve P and into the permeate side of the membrane.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Electrochemistry (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

A process for producing high purity carbon monoxide (CO) by membrane purification of CO produced in a solid oxide electrolysis cell (SOEC) comprises the steps of generating a gaseous mixture of CO and CO2 by SOEC electrolysis of CO2, applying a moderate pressure on the retentate side of the membrane in one or more membrane units connected to the exit of the SOEC via a compressor or an ejector, applying a lower pressure than the moderate pressure on the permeate side of the membrane, splitting the retentate stream, which is now enriched in CO, into two separate parts, expanding the first part of the retentate stream to reach the permeate low pressure conditions, leading the above-mentioned part of the retentate to the permeate side of the membrane to lower the partial pressure of CO2 on this side, and recycling the outlet permeate stream back to the SOEC as a feed gas together with fresh CO2. Preferably the membrane unit is designed with a tubular membrane or multiple planar membranes connected in series, and the retentate and permeate streams are operated in counter-current mode.

Description

Title: Process for producing high purity CO by membrane pu¬ rification of SOEC-produced CO
The present invention relates to a process for producing high purity carbon monoxide (CO) by membrane purification of CO produced in a solid oxide electrolysis cell (SOEC) .
A solid oxide electrolysis cell is a solid oxide fuel cell (SOFC) run in reverse mode, which uses a solid oxide or ce- ramie electrolyte to produce e.g. oxygen and hydrogen gas by electrolysis of water. It can also be used to produce CO from carbon dioxide (C02) , which is led to the fuel side of the SOEC or SOEC stack with an applied current. Excess oxy¬ gen is transported to the oxygen side of the SOEC, option- ally using air, nitrogen or CO2 to flush the oxygen side, and afterwards the product stream from the SOEC, containing CO mixed with CO2, is subjected to a separation process.
Carbon monoxide of high purity is an important raw material for the synthesis of chemicals. Most reactions for the syn¬ thesis of chemicals require high temperatures as well as high pressures, and therefore the CO used should have the lowest possible content of carbon dioxide (C02) which cor¬ rodes the reactor by oxidation. Additionally, CO2 may limit the equilibrium conversion of the reaction in which the produced CO takes part. CO2 may also inhibit the kinetics of the reaction where CO is used.
Production of high purity CO is described in a number of patent publications. Thus, US 5,482,539 describes a multi¬ ple stage semi-permeable membrane process and apparatus for gas separation. This patent, however, does not deal with CO produced in electrolysis cells.
US 6,787,118 is related to selective removal of CO. More specifically it deals with catalyst compositions useful for destruction of volatile organic carbon compounds (VOCs) in an oxygen-containing gas stream at low temperatures and for selective oxidation of carbon monoxide from a hydrogen- containing gas. This patent is not related to any use of membranes.
US 2009/0014336 concerns electrolysis of carbon dioxide in aqueous media to carbon monoxide and hydrogen for produc¬ tion of methanol. However, this patent application is nei- ther related to CO production using SOECs nor to the use of membranes .
A system wherein a membrane unit is coupled to the exit of an electrolysis cell is disclosed in US 5,814,127. This pa- tent concerns the production of aluminum in an aluminum electrolysis cell and the subsequent removal of inorganic fluorides from the vent gas in the membrane unit, where the gas is split into a retentate stream rich in fluorides and a permeate stream depleted in fluorides. This has nothing to do with purification of CO, but the system resembles the one used in the present invention.
Finally, both EP 0 129 444 and US 4,539,020 concern high- purity CO obtained by pressure swing adsorption (PSA) .
In fact, pressure swing adsorption (PSA) is the only known technology, which in an economically feasible way is able to purify CO to a purity of 95 % and above from a mixture of CO and CO2 in the scale applicable to "small scale CO", i.e. a CO production of 1 to 200 Nm3/h. Only a very limited number of producers can supply PSA units in this scale. Be- sides, the PSA unit adds a significant complexity and cost to the smaller units. For these reasons it would be desira¬ ble to find a feasible alternative to PSA for the purifica¬ tion of CO produced in small scale. Installing a membrane separation unit downstream from the
SOEC is an attractive alternative to PSA, mainly due to its simplicity, because a membrane separation unit operates without any moving parts, but also due to a reduced capital expenditure (CAPEX) because of its modular nature.
Gas separation membranes are presently used for the removal of CO2 from natural gas and syngas. Such membranes can be based on polymers or zeolites coated on alumina tubes, and they generally have a selectivity towards transporting CO2 through the membrane, whereas hydrocarbons, ¾ and CO are held back on the retentate side. Typical selectivity con¬ stants for CO/ CO2 are between 5 and 20, and fluxes may vary from 20 to 200 Nm3/h per m2 membrane area. Membrane separation is driven by the difference in partial pressure, and thus it is most suitable for removing the bulk of an impurity, such as CO2 , whereas an extensive mem¬ brane area is required to reach a high purity when the driving force for separation decreases.
All membranes that have a difference in permeability for CO and for CO2 , where the permeability of the membrane is higher for CO2 than that for CO, can be used in the present invention. These criteria are met with ceramic membranes, coated ceramic membranes and polymeric membranes. The mem¬ branes may be of planar or tubular shape, and they may be used in a single membrane unit or in multiple membrane units in series or in parallel.
The driving force for separation can be boosted by applying a high absolute pressure on the retentate side of the mem- brane and applying an approximate vacuum on the permeate side of the membrane. In practice, however, there is a CAPEX limitation for installing a multi-stage compressor to reach a high pressure and the power required to drive the compressor. The maximum pressure difference is also limited by the mechanical strength of the membrane and of the mem¬ brane module.
The present invention relates to a selective separation of CO from a mixture of CO and CO2, especially in relation to small scale production of CO by SOEC electrolysis. The principle is quite similar to a reflux column within dis¬ tillation.
More specifically the invention concerns a process for pro- ducing high purity carbon monoxide (CO) by membrane purifi¬ cation of CO produced in a solid oxide electrolysis cell (SOEC), said process comprising the following steps:
(1) generating a gaseous mixture of CO and CO2 by SOEC electrolysis of CO2, (2) applying a moderate pressure on the retentate side of the membrane in a membrane unit connected to the exit of the SOEC via a compressor or an ejector, (3) applying a lower pressure than the pressure in step (2) on the permeate side of the membrane,
(4) splitting the retentate stream, which is now enriched in CO, into two separate parts,
(5) expanding the first part of the retentate stream to reach the permeate low pressure conditions,
(6) leading the above-mentioned part of the retentate to the permeate side of the membrane to lower the partial pressure of CO2 on this side, and
(7) recycling the outlet permeate stream back to the SOEC as a feed gas together with fresh CO2 .
By lowering the partial pressure of CO2 on the permeate side of the membrane in the above step (6), the driving force for CO2 flux through the membrane is increased. In addition, the driving force for transportation of CO through the membrane is decreased, and thus the yield of CO can be increased when high purities of CO are targeted. The outlet permeate stream is fully or partly recycled back to the SOEC as a feed gas together with fresh CO2 in the above step (7), whereby the CO2 yield is increased.
Regarding the moderate pressure on the retentate side of the membrane, it can be from 250 bar g down to 3 bar g, preferably from 175 bar g down to 3 bar g, more preferably from 40 bar g down to 3 bar g and most preferably from 20 bar g down to 5 bar g. The lower pressure on the permeate side of the membrane can be between -0.8 bar g and 50 bar g, preferably between -0.8 bar g and 10 bar g, more preferably between -0.8 bar g and 3 bar g, even more preferably between -0.8 and 2 bar g and most preferably between -0.3 bar g and 0.5 bar g, especial- ly between 0 and 0.3 bar g.
Regarding the analogy to distillation as mentioned above, the splitting of the retentate stream into two separate parts also has analogy to the reflux at the top of a dis- tillation column. Furthermore, the SOEC unit has a function similar to the reboiler in a distillation unit; see the appended fig 1.
The membrane unit is preferably designed with a tubular membrane or multiple planar membranes connected in series where the retentate and permeate streams are operated in counter-current mode. This implies that the enriched CO re¬ flux stream from the retentate side enters (after expan¬ sion) the permeate side of the membrane unit in the oppo- site end from the feed gas entering the membrane unit from the SOEC unit.
The process according to the invention can be further outlined with reference to fig. 1, which shows a solid oxide electrolysis cell (SOEC) unit with the oxygen side at the top, the electrolyte in the middle and the fuel side at the bottom. CO2 is led to the fuel side of the SOEC unit with an applied current to convert CO2 to CO and transport any oxygen surplus to the oxygen side of the SOEC unit. CO2 is also led to the oxygen side to flush this side, but air or nitrogen may also be used for this purpose. Flushing the oxygen side of the SOEC unit has two advantages, more spe¬ cifically (1) to reduce the oxygen concentration and relat¬ ed corrosive effects and (2) to provide means for feeding energy into the SOEC unit, operating it endothermic.
The product stream from the SOEC contains mixed CO and CO2, which is led to a compressor C, which serves to establish a high absolute pressure on the retentate side of the mem¬ brane. A lower pressure is applied on the permeate side of the membrane by leading part of the CO product stream through a pressure reduction valve P and into the permeate side of the membrane.

Claims

Claims :
1. A process for producing high purity carbon monoxide (CO) by membrane purification of CO produced in a solid ox- ide electrolysis cell (SOEC) , said process comprising the following steps:
(1) generating a gaseous mixture of CO and CO2 by SOEC electrolysis of CO2,
(2) applying a moderate pressure on the retentate side of the membrane in one or more membrane units connected to the exit of the SOEC via a compressor or an ejector, (3) applying a lower pressure than the pressure in step (2) on the permeate side of the membrane,
(4) splitting the retentate stream, which is now enriched in CO, into two separate parts,
(5) expanding the first part of the retentate stream to reach the permeate low pressure conditions,
(6) leading the above-mentioned part of the retentate to the permeate side of the membrane to lower the partial pressure of CO2 on this side, and
(7) recycling the outlet permeate stream back to the SOEC as a feed gas together with fresh CO2.
2. The process according to claim 1, wherein the membrane is selected from the group consisting of ceramic membranes, coated ceramic membranes, such as zeolite coated membranes, and polymeric membranes.
3. The process according to claim 1 or 2, wherein the membrane unit is designed with a tubular membrane or multi¬ ple planar membranes connected in series, and wherein the retentate and permeate streams are operated in counter- current mode.
4. The process according to any of claims 1 - 3, wherein the moderate pressure in step (2) is from 250 bar g down to 3 bar g, preferably from 175 bar g down to 3 bar g.
5. The process according to claim 4, wherein the moderate pressure in step (2) is from 40 bar g down to 3 bar g and preferably from 20 bar g down to 5 bar g.
6. The process according to any of claims 1 - 3, wherein the lower pressure in step (3) is between -0.8 bar g and 50 bar g, preferably between -0.8 bar g and 10 bar g.
7. The process according to claim 6, wherein the lower pressure in step (3) is between -0.8 bar g and 3 bar g, preferably between -0.8 and 2 bar g.
8. The process according to claim 7, wherein the lower pressure in step (3) is between -0.3 bar g and 0.5 bar g, preferably between 0 and 0.3 bar g.
PCT/EP2014/062362 2013-07-30 2014-06-13 Process for producing high purity co by membrane purification of soec-produced co WO2015014527A1 (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CA2916959A CA2916959A1 (en) 2013-07-30 2014-06-13 Process for producing high purity co by membrane purification of soec-produced co
CN201480043120.8A CN105431221A (en) 2013-07-30 2014-06-13 Process for producing high purity co by membrane purification of soec-produced co
US14/903,186 US20160151739A1 (en) 2013-07-30 2014-06-13 Process for producing high purity co by membrane purification of soec-produced co

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP13178475.3 2013-07-30
EP13178475.3A EP2832421B1 (en) 2013-07-30 2013-07-30 Process for producing high purity co by membrane purification of soec-produced co

Publications (1)

Publication Number Publication Date
WO2015014527A1 true WO2015014527A1 (en) 2015-02-05

Family

ID=48900819

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2014/062362 WO2015014527A1 (en) 2013-07-30 2014-06-13 Process for producing high purity co by membrane purification of soec-produced co

Country Status (8)

Country Link
US (1) US20160151739A1 (en)
EP (1) EP2832421B1 (en)
CN (1) CN105431221A (en)
AR (1) AR097092A1 (en)
CA (1) CA2916959A1 (en)
ES (1) ES2583903T3 (en)
TW (1) TW201516184A (en)
WO (1) WO2015014527A1 (en)

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015202789A1 (en) * 2015-02-17 2016-08-18 Robert Bosch Gmbh Product gas treatment apparatus and method for processing a product gas
WO2018228718A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Method and system for producing a gas product containing carbon monoxide
WO2018228716A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Method and system for producing a gas product containing carbon monoxide
DE102017005678A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Process and plant for producing a carbon monoxide-containing gas product
EP3511442A1 (en) 2018-01-12 2019-07-17 Linde Aktiengesellschaft Production of a gas product containing carbon monoxide
EP3511441A1 (en) 2018-01-12 2019-07-17 Linde Aktiengesellschaft Production of a gas product containing carbon monoxide
WO2019158307A1 (en) 2018-02-15 2019-08-22 Siemens Aktiengesellschaft Electrochemical production of a gas comprising co with intermediate cooling of the electrolyte flow
WO2019158308A1 (en) 2018-02-15 2019-08-22 Siemens Aktiengesellschaft Method for the electrochemical production of a gas product containing co
WO2019158305A1 (en) 2018-02-15 2019-08-22 Siemens Aktiengesellschaft Electrochemical production of carbon monoxide and/or syngas
DE102018003332A1 (en) 2018-04-24 2019-10-24 Linde Aktiengesellschaft Preparation of a synthesis product
DE102018003343A1 (en) 2018-04-24 2019-10-24 Linde Aktiengesellschaft Process and plant for the production of ethanol
DE102018003342A1 (en) 2018-04-24 2019-10-24 Linde Aktiengesellschaft Production of a gas product containing at least carbon monoxide
WO2021073769A1 (en) 2019-10-18 2021-04-22 Linde Gmbh Method and plant for producing a carbon-monoxide-rich gas product
DE102020000476A1 (en) 2020-01-27 2021-07-29 Linde Gmbh Process and plant for the production of hydrogen
DE102020000937A1 (en) 2020-02-14 2021-08-19 Linde Gmbh Method and system for providing an industrial product using oxygen
WO2022136025A1 (en) 2020-12-22 2022-06-30 Topsoe A/S An improved method for operation of a solid oxide electrolysis cell in carbon dioxide electrolysis
US11905173B2 (en) 2018-05-31 2024-02-20 Haldor Topsøe A/S Steam reforming heated by resistance heating
EP4324957A1 (en) 2022-08-19 2024-02-21 Linde GmbH Method and installation for the production of a product containing hydrocarbon
EP4345086A1 (en) 2022-09-30 2024-04-03 Linde GmbH Method and system for producing methanol
EP4345191A1 (en) 2022-09-30 2024-04-03 Linde GmbH Method and system for producing a hydrogen-containing product using electrolysis

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015202117A1 (en) * 2015-02-06 2016-08-11 Siemens Aktiengesellschaft Process and electrolysis system for carbon dioxide recovery
ITUA20163761A1 (en) * 2016-05-24 2017-11-24 Microprogel S R L Gas dryer
FR3063437B1 (en) * 2017-03-02 2019-03-29 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude APPARATUS AND METHOD FOR MEMBRANE PERMEATION TREATMENT OF A GAS SUPPLY FLOW COMPRISING METHANE AND CARBON DIOXIDE
DE102018009198A1 (en) * 2018-11-22 2020-05-28 Linde Aktiengesellschaft Process for changing the operating mode of an electrolysis plant and electrolysis plant
AU2021288580A1 (en) * 2020-06-09 2023-02-02 Twelve Benefit Corporation System and method for high concentration of multielectron products or CO in electrolyzer output

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5306427A (en) * 1992-12-18 1994-04-26 Permea, Inc. Low pressure feed membrane separation process
WO2000068146A1 (en) * 1999-05-06 2000-11-16 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude On site carbon monoxide generator
US20110253551A1 (en) * 2010-04-19 2011-10-20 Jonathan Andrew Lane Electrochemical carbon monoxide production

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0129444B2 (en) 1983-06-20 1995-04-19 Kawasaki Steel Corporation Methods for obtaining high-purity carbon monoxide
US4539020A (en) 1983-07-10 1985-09-03 Kawasaki Steel Corporation Methods for obtaining high-purity carbon monoxide
US5482539A (en) 1993-09-22 1996-01-09 Enerfex, Inc. Multiple stage semi-permeable membrane process and apparatus for gas separation
US5814127A (en) 1996-12-23 1998-09-29 American Air Liquide Inc. Process for recovering CF4 and C2 F6 from a gas
EP1246691A4 (en) 1999-12-20 2004-11-10 Eltron Research Inc CATALYSTS AND METHODS FOR LOW-TEMPERATURE DESTRUCTION OF VOCs IN AIR AND SELECTIVE REMOVAL OF CO
JP5144755B2 (en) * 2007-07-13 2013-02-13 ユニバーシティ オブ サザン カリフォルニア Electrolysis of carbon dioxide to carbon monoxide and hydrogen in aqueous media for methanol production

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5306427A (en) * 1992-12-18 1994-04-26 Permea, Inc. Low pressure feed membrane separation process
WO2000068146A1 (en) * 1999-05-06 2000-11-16 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude On site carbon monoxide generator
US20110253551A1 (en) * 2010-04-19 2011-10-20 Jonathan Andrew Lane Electrochemical carbon monoxide production

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
EBBESEN S D ET AL: "Electrolysis of carbon dioxide in Solid Oxide Electrolysis Cells", JOURNAL OF POWER SOURCES, ELSEVIER SA, CH, vol. 193, no. 1, 1 August 2009 (2009-08-01), pages 349 - 358, XP026150424, ISSN: 0378-7753, [retrieved on 20090319], DOI: 10.1016/J.JPOWSOUR.2009.02.093 *

Cited By (36)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102015202789A1 (en) * 2015-02-17 2016-08-18 Robert Bosch Gmbh Product gas treatment apparatus and method for processing a product gas
CN105887119A (en) * 2015-02-17 2016-08-24 罗伯特·博世有限公司 Product Gas Purifying Device And Method For Purifying Product Gas
WO2018228718A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Method and system for producing a gas product containing carbon monoxide
DE102017005681A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Process and plant for producing a carbon monoxide-containing gas product
WO2018228716A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Method and system for producing a gas product containing carbon monoxide
DE102017005680A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Process and plant for producing a carbon monoxide-containing gas product
DE102017005678A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Process and plant for producing a carbon monoxide-containing gas product
WO2018228717A1 (en) 2017-06-14 2018-12-20 Linde Aktiengesellschaft Method and system for producing a gas product containing carbon monoxide
EP3511442A1 (en) 2018-01-12 2019-07-17 Linde Aktiengesellschaft Production of a gas product containing carbon monoxide
EP3511441A1 (en) 2018-01-12 2019-07-17 Linde Aktiengesellschaft Production of a gas product containing carbon monoxide
WO2019137827A1 (en) 2018-01-12 2019-07-18 Linde Aktiengesellschaft Production of a gas product containing carbon monoxide
DE102018000214A1 (en) 2018-01-12 2019-07-18 Linde Aktiengesellschaft Production of a gas product containing at least carbon monoxide
DE102018000213A1 (en) 2018-01-12 2019-07-18 Linde Aktiengesellschaft Production of a gas product containing at least carbon monoxide
US11105007B2 (en) 2018-02-15 2021-08-31 Siemens Aktiengesellschaft Method for the electrochemical production of a gas product containing CO
WO2019158307A1 (en) 2018-02-15 2019-08-22 Siemens Aktiengesellschaft Electrochemical production of a gas comprising co with intermediate cooling of the electrolyte flow
DE102018202337A1 (en) 2018-02-15 2019-08-22 Linde Aktiengesellschaft Electrochemical production of a gas comprising CO with intercooling of the electrolyte flow
WO2019158305A1 (en) 2018-02-15 2019-08-22 Siemens Aktiengesellschaft Electrochemical production of carbon monoxide and/or syngas
DE102018202335A1 (en) * 2018-02-15 2019-08-22 Linde Aktiengesellschaft Plant for the electrochemical production of a CO-containing gas product
US11560633B2 (en) 2018-02-15 2023-01-24 Siemens Energy Global GmbH & Co. KG Electrochemical production of carbon monoxide and/or syngas
WO2019158308A1 (en) 2018-02-15 2019-08-22 Siemens Aktiengesellschaft Method for the electrochemical production of a gas product containing co
DE102018003343A1 (en) 2018-04-24 2019-10-24 Linde Aktiengesellschaft Process and plant for the production of ethanol
DE102018003342A1 (en) 2018-04-24 2019-10-24 Linde Aktiengesellschaft Production of a gas product containing at least carbon monoxide
WO2019206451A1 (en) 2018-04-24 2019-10-31 Linde Aktiengesellschaft Production of a gas product which contains at least carbon monoxide
WO2019206450A1 (en) 2018-04-24 2019-10-31 Linde Aktiengesellschaft Producing a synthesis product
DE102018003332A1 (en) 2018-04-24 2019-10-24 Linde Aktiengesellschaft Preparation of a synthesis product
US11905173B2 (en) 2018-05-31 2024-02-20 Haldor Topsøe A/S Steam reforming heated by resistance heating
WO2021073769A1 (en) 2019-10-18 2021-04-22 Linde Gmbh Method and plant for producing a carbon-monoxide-rich gas product
WO2021151453A1 (en) 2020-01-27 2021-08-05 Linde Gmbh Method and plant for producing hydrogen
DE102020000476A1 (en) 2020-01-27 2021-07-29 Linde Gmbh Process and plant for the production of hydrogen
DE102020000937A1 (en) 2020-02-14 2021-08-19 Linde Gmbh Method and system for providing an industrial product using oxygen
WO2022136025A1 (en) 2020-12-22 2022-06-30 Topsoe A/S An improved method for operation of a solid oxide electrolysis cell in carbon dioxide electrolysis
EP4324957A1 (en) 2022-08-19 2024-02-21 Linde GmbH Method and installation for the production of a product containing hydrocarbon
EP4345086A1 (en) 2022-09-30 2024-04-03 Linde GmbH Method and system for producing methanol
EP4345191A1 (en) 2022-09-30 2024-04-03 Linde GmbH Method and system for producing a hydrogen-containing product using electrolysis
WO2024068047A1 (en) 2022-09-30 2024-04-04 Linde Gmbh Process and system for preparing methanol
WO2024068048A2 (en) 2022-09-30 2024-04-04 Linde Gmbh Method and system for producing a hydrogen-containing product using electrolysis

Also Published As

Publication number Publication date
CA2916959A1 (en) 2015-02-05
CN105431221A (en) 2016-03-23
AR097092A1 (en) 2016-02-17
EP2832421A1 (en) 2015-02-04
ES2583903T3 (en) 2016-09-22
EP2832421B1 (en) 2016-05-25
TW201516184A (en) 2015-05-01
US20160151739A1 (en) 2016-06-02

Similar Documents

Publication Publication Date Title
EP2832421B1 (en) Process for producing high purity co by membrane purification of soec-produced co
US11370658B2 (en) Method for the preparation of ammonia synthesis gas
AU2012361210B2 (en) Method for separating gases
US8114192B2 (en) Gas separation processes using membrane with permeate sweep to recover reaction feedstocks
US10258921B2 (en) Gas separation system and enriched gas production method
WO2013119465A1 (en) Gas separation process for production of hydrogen by autothermal reforming of natural gas, with carbon dioxide recovery
US20170088419A1 (en) Membrane-Based Gas Separation Processes to Produce Synthesis Gas With a High CO Content
AU2019250452B2 (en) A method for generating gas mixtures comprising carbon monoxide and carbon dioxide for use in synthesis reactions
CN113784941B (en) Method of
WO2011138809A8 (en) Process for the production of syngas and hydrogen starting from reagents comprising liquid hydrocarbons, gaseous hydrocarbons, and/or oxygenated compounds, also deriving from biomasses, by means of a non- integrated membrane reactor
US9919982B2 (en) Method and device for gas processing
JP6464881B2 (en) Gas separation system and method for producing enriched gas
US8568510B2 (en) Gas-separation processes using membranes with permeate sweep to recover reaction feedstocks
CA3096322A1 (en) A method for generating synthesis gas for use in hydroformylation reactions
JP6511912B2 (en) Gas separation system and method for producing enriched gas
US20220135402A1 (en) Method and device for producing synthesis gas with carbon dioxide return
WO2024014493A1 (en) Gas separation system and method for producing methane-enriched gas
WO2024048673A1 (en) Method for producing liquid fuel and liquid fuel synthesis system
AU2022303845A1 (en) Method for highly purifying condensable product in membrane reactor
CA3214550A1 (en) Membrane process and system for high recovery of a nonpermeating gas utilizing a sweep gas
JP2022176139A (en) gas separation process
Harasimowicz et al. Methane enrichment of CH4+ CO2 mixture on 2-stage GS membrane module system with circulation stream and chemical final purification
TH81550A (en) Carbon production process Better monoxides
RU2006133433A (en) METHOD FOR PRODUCING CARBON OXIDE

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 201480043120.8

Country of ref document: CN

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14729906

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2916959

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 14903186

Country of ref document: US

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 14729906

Country of ref document: EP

Kind code of ref document: A1