CN102261811A - Device for cryogenically separating carbon monoxide from hydrogen - Google Patents

Device for cryogenically separating carbon monoxide from hydrogen Download PDF

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Publication number
CN102261811A
CN102261811A CN2011101691022A CN201110169102A CN102261811A CN 102261811 A CN102261811 A CN 102261811A CN 2011101691022 A CN2011101691022 A CN 2011101691022A CN 201110169102 A CN201110169102 A CN 201110169102A CN 102261811 A CN102261811 A CN 102261811A
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CN
China
Prior art keywords
carbon monoxide
heat exchanger
communicated
hydrogen
outlet
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Application number
CN2011101691022A
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Chinese (zh)
Inventor
陈环琴
苟文广
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杭州中泰深冷技术股份有限公司
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Priority to CN2011101691022A priority Critical patent/CN102261811A/en
Publication of CN102261811A publication Critical patent/CN102261811A/en

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0223—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0261—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/90—Hot gas waste turbine of an indirect heated gas for power generation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle

Abstract

The invention discloses a device for cryogenically separating carbon monoxide from hydrogen. The device comprises a pre-treatment unit and a cryogenic separation cold box. The cryogenic separation cold box comprises a heat exchanger, a gas-liquid separation tank and a carbon monoxide purification unit. Mixed gas of carbon monoxide and hydrogen is purified through the pre-treatment unit and then enters the inlet in the middle of the gas-liquid separation tank through the heat exchanger. The outlet at the upper end of the gas-liquid separation tank is communicated with a hydrogen collection system through the heat exchanger. The outlet at the lower end of the gas-liquid separation tank is communicated with the inlet in the middle of the carbon monoxide purification unit through a throttle decompressing valve J1. The carbon monoxide purification unit is a rectification tower. The rectification tower comprises a condenser arranged on the top of the tower and a reboiler arranged at the bottom of the tower. The outlet on the top of the rectification tower is communicated with a corresponding outer collection system through the heat exchanger. The outlet at the bottom of the rectification tower is communicated with the carbon monoxide collection system through a throttle decompressing valve J2 and the heat exchanger. When the treatment amount of the mixed gas of CO and H2 is higher, the process flow can be simplified by adopting the device disclosed by the invention; and the operation cost and the equipment investment cost can be reduced.

Description

The device of cryogenic separation carbon monoxide and hydrogen

Technical field

The present invention relates to separate carbon monoxide (CO) and hydrogen (H 2) device, the device of especially a kind of cryogenic separation carbon monoxide and hydrogen.

Background technology

CO and H 2It is important basic chemical industry raw material, be widely used in chemical processes such as carbonyl synthesizes, for example carbonylation of methanol system acetic acid, aceticanhydride, formic acid, oxalic acid and dimethyl formamide etc., and phosgene synthetic, produce Merlon, polyurethane, synthetic metal carbonyl etc.Present CO and H 2Separate and mainly contain Deep Cooling Method, absorption process and pressure swing adsorption method etc.Deep Cooling Method is to utilize the difference of gas component boiling point, realizes separation of gaseous mixture by cryogenic rectification.Thereby stop up heat exchanger and pipeline in order to prevent that various impurity compositions from solidifying at low temperatures, therefore with Deep Cooling Method separation of C O and H 2Just need unstripped gas before entering ice chest, to carry out preliminary treatment, remove the component that can solidify at low temperatures that contains in the component.Pressure swing adsorption method is the composition requirement according to product gas, select suitable adsorbent and technical process, utilize adsorbent to some component high adsorption capacity and to the characteristic (adsorptive selectivity) a little less than other component adsorption capacity, process by continuous repetition high pressure absorption and low pressure desorb is separated admixture of gas and is made required product.Absorption process is a kind of solution absorption and separation method, and it is to utilize the complex compound lyosoption to select to absorb CO, obtains CO product gas through heating desorption again, and this method requires very strict to raw material gas purifying.

CO and H 2The gaseous mixture treatment scale hour adopts pressure swing adsorption method to have superiority, as CO and H 2The gaseous mixture treatment scale adopts pressure swing adsorption method can cause equipment investment and operating cost higher when big.And absorption process operating cost height first, moreover there is environmental issue, present less employing.Therefore at CO and H 2Usually adopt separation by deep refrigeration when treatment scale is big.Chinese patent (publication number CN 1860338A) has been put down in writing a kind of separation and has been contained CO, H 2And N 2Process.The defective that this method exists is: its separation of C O and H 2The flow process more complicated, and energy consumption is higher.

Summary of the invention

The objective of the invention is to: provide the device of a kind of cryogenic separation carbon monoxide and hydrogen, as CO and H 2When the gaseous mixture treating capacity is big, adopt this device can simplify technological process, reduce operating cost and equipment investment cost.

For achieving the above object, the present invention can take following technical proposals:

The device of a kind of cryogenic separation carbon monoxide of the present invention and hydrogen, comprise the pretreatment unit and the cryogenic separation ice chest that are used to remove foreign gas, described cryogenic separation ice chest comprises heat exchanger, knockout drum and carbon monoxide purifier units, carbon monoxide and hydrogen mixed gas input channel G1 are communicated with the inlet of described pretreatment unit, the mixed gas outlet that removes impurity of pretreatment unit is communicated with the centre entrance of described knockout drum through described heat exchanger by pipeline G2, the upper end outlet of knockout drum is communicated with hydrogen collection through heat exchanger by pipeline, the lower end outlet of knockout drum is communicated with the centre entrance of carbon monoxide purifier units through expenditure and pressure valve J1 by pipeline G5, described carbon monoxide purifier units is a rectifying column, reboiler at the bottom of this rectifying column comprises the condenser that is arranged at cat head and is arranged at tower, its top outlet is communicated with outside corresponding gathering system through heat exchanger by pipeline G10, and its bottom exports by pipeline G2 successively through expenditure and pressure valve J2, heat exchanger is communicated with the carbon monoxide gathering system.

As preferably, described condenser is a segregation and fractionation formula condenser, and described reboiler is inner thermosyphon reboiler.

As preferably, also comprise the nitrogen cooling cycle system that is used to described segregation and fractionation formula condenser that institute's chilling requirement is provided and institute's calorific requirement is provided for described inner thermosyphon reboiler.

As preferably, the outlet of described rectifying column bottom also is connected with pipeline G3, and described pipeline G3 is communicated with described carbon monoxide gathering system successively through heat exchanger, carbon monoxide decompressor, return heat exchanger more at last.

Compared with prior art the invention has the beneficial effects as follows: owing to adopt technique scheme, described carbon monoxide purifier units is a rectifying column, reboiler at the bottom of this rectifying column comprises the condenser that is arranged at cat head and is arranged at tower, its top outlet is communicated with outside corresponding gathering system through heat exchanger by pipeline G10, its bottom outlet is communicated with the carbon monoxide gathering system through expenditure and pressure valve J2, heat exchanger successively by pipeline G2, this structure, can obtain the CO product that purity is 96-99.9% in the bottom of rectifying column, cat head obtains rich H 2Product.

The further beneficial effect of the present invention is: described condenser is a segregation and fractionation formula condenser, described reboiler is inner thermosyphon reboiler, rectifying column overhead condenser and tower bottom reboiler adopt segregation and fractionation formula condenser and inner thermosyphon reboiler respectively, overhead condenser has improved separating effect, reduced the layout difficulty of ice chest equipment, for the device of big specification is provided convenience, thermal siphon formula evaporimeter is placed on heat exchanger the outside of rectifying column, cut down the consumption of energy, improve heat exchanger efficiency, also reduced simultaneously the layout difficulty of ice chest equipment, making progress for the big specification of device provides convenience.

Description of drawings

Fig. 1 is a syndeton schematic diagram of the present invention.

The specific embodiment

As shown in Figure 1, the device of a kind of cryogenic separation carbon monoxide of the present invention and hydrogen, comprise the pretreatment unit 1 and the cryogenic separation ice chest 2 that are used to remove foreign gas, described cryogenic separation ice chest 2 comprises plate-fin heat exchanger B1 12, plate-fin heat exchanger B2 13, knockout drum 3, is used for the rectifying column 6 that carbon monoxide is purified, inside thermosyphon reboiler 10 at the bottom of described rectifying column 6 comprises the segregation and fractionation formula condenser 9 that is arranged at cat head and is arranged at tower contains N 2Argon gas 0.02%(volume) and micro-H the 0.67%(volume), 2S, CO 2CO and H 2Gaseous mixture enters in the described pretreatment unit 1 by pipeline G1 101, adopts the technology of low-temperature rectisol and molecular sieve adsorption in pretreatment unit 1, and methanol-eluted fractions is removed sour gas H 2S and CO 2, molecular sieve removes methyl alcohol, the CO of the one-step removal trace of going forward side by side 2Through pretreatment unit 1 remove impurity satisfy carbon monoxide that cryogenic separation requires and hydrogen gas mixture by pipeline G2 102 through plate-fin heat exchanger B1 12 and the cooling of plate-fin heat exchanger B2 13 two-stages, be cooled to about-182 ℃, enter the centre entrance of knockout drum 3, in knockout drum 3, be divided into two bursts of logistics of gas-liquid, after tank deck hydrogen goes out tank deck, return plate-fin heat exchanger B2 13 re-heats by pipeline G4 103 adverse currents, again through plate-fin heat exchanger B1 12 re-heats, go out cryogenic separation ice chest 2, enter hydrogen collection 4 then, can be used as product hydrogen as required or further purify by technologies such as PSA; The liquid stream of the lower end of knockout drum 3 outlet enters the centre entrance of rectifying column 6 by pipeline G5 105 after expenditure and pressure valve J1 5 decompressions, in rectifying column with H 2, N 2Separate from cat head,, enter hydrogen collection 4, obtain purity at the bottom of the tower and be 99.9% CO product through plate-fin heat exchanger B1 12 and plate-fin heat exchanger B2 13 twice re-heat; Operating pressure 0.5 MPaG at the bottom of the tower, purity is that 99.9% CO is divided into two-way from the outlet of rectifying column 6 bottoms, lead up to pipeline G2 201 successively through expenditure and pressure valve J2 7(throttling to 0.15MPaG), through plate-fin heat exchanger B2 13 and plate-fin heat exchanger B1 12 two-stage re-heats, enter carbon monoxide gathering system 8, pressure behind the expenditure and pressure valve J2 7 and flow are by plate-fin heat exchanger B2 13 cold junctions required cold and temperature decision, another road is by pipeline G3 301, successively through plate-fin heat exchanger B2 13(evaporation re-heat), plate-fin heat exchanger B1 12(evaporates about re-heat to 0 ℃ once more), carbon monoxide decompressor 11(is expanded to 0.17MPaG), return plate-fin heat exchanger B2 13 re-heats again, enter described carbon monoxide gathering system 8 at last; The heat that the cold that the described segregation and fractionation formula condenser 9 of rectifying column 6 cats head is required and the described inner thermosyphon reboiler at the bottom of the tower 10 are required, provide by the nitrogen cooling cycle system, nitrogen passes through nitrogen compressor 14 successively, nitrogen heat exchanger 15, plate-fin heat exchanger B1 12(is cooled to-152 ℃), inner thermosyphon reboiler 10, expenditure and pressure valve J3 16(is decompressed to 0.25MPa), segregation and fractionation formula condenser 9, plate-fin heat exchanger B2 13(re-heat), return re-heat once more) through plate-fin heat exchanger B1 12(, be back to described nitrogen compressor 14 at last, constitute the nitrogen refrigeration cycle.

The foregoing description is a preferred implementation of the present invention.For this CO and H 2Cryogenic separation device can be made multiple combination that is equal to or variation, all belongs to protection scope of the present invention.

Claims (4)

1. the device of cryogenic separation carbon monoxide and hydrogen, comprise the pretreatment unit (1) and the cryogenic separation ice chest (2) that are used to remove foreign gas, described cryogenic separation ice chest (2) comprises heat exchanger, knockout drum (3) and carbon monoxide purifier units, carbon monoxide and hydrogen mixed gas input channel G1(101) be communicated with the inlet of described pretreatment unit (1), the mixed gas outlet that removes impurity of pretreatment unit (1) is by pipeline G2(102) be communicated with through the centre entrance of described heat exchanger with described knockout drum (3), the upper end outlet of knockout drum (3) is communicated with hydrogen collection (4) through heat exchanger by pipeline, the lower end outlet of knockout drum (3) is by pipeline G5(105) through expenditure and pressure valve J1(5) be communicated with the centre entrance of carbon monoxide purifier units, it is characterized in that: described carbon monoxide purifier units is rectifying column (6), reboiler at the bottom of this rectifying column (6) comprises the condenser that is arranged at cat head and is arranged at tower, its top outlet is by pipeline G10(110) be communicated with outside corresponding gathering system through heat exchanger, its bottom outlet is by pipeline G2(201) successively through expenditure and pressure valve J2(7), heat exchanger is communicated with carbon monoxide gathering system (8).
2. the device of cryogenic separation carbon monoxide according to claim 1 and hydrogen is characterized in that: described condenser is a segregation and fractionation formula condenser (9), and described reboiler is inner thermosyphon reboiler (10).
3. the device of cryogenic separation carbon monoxide according to claim 2 and hydrogen is characterized in that: also comprise the nitrogen cooling cycle system that is used to described segregation and fractionation formula condenser (9) that institute's chilling requirement is provided and institute's calorific requirement is provided for described inner thermosyphon reboiler (10).
4. the device of cryogenic separation carbon monoxide according to claim 3 and hydrogen, it is characterized in that: the outlet of described rectifying column (6) bottom also is connected with pipeline G3(301), described pipeline G3(301) successively through heat exchanger, carbon monoxide decompressor (11), return heat exchanger again, is communicated with described carbon monoxide gathering system (8) at last.
CN2011101691022A 2011-06-22 2011-06-22 Device for cryogenically separating carbon monoxide from hydrogen CN102261811A (en)

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102721264A (en) * 2012-07-04 2012-10-10 开封空分集团有限公司 Carbon monoxide mixture purification system and purification method
CN103523751A (en) * 2013-09-29 2014-01-22 开封空分集团有限公司 Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen
CN104236253A (en) * 2014-07-01 2014-12-24 开封空分集团有限公司 Device and method for extracting pure carbon monoxide and oxygen-rich gas by aid of cryogenic technology
CN105865146A (en) * 2016-04-25 2016-08-17 重庆耐德能源装备集成有限公司 Copious cooling liquefying system and cold box

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Publication number Priority date Publication date Assignee Title
CN1117129A (en) * 1994-04-13 1996-02-21 乔治·克劳德方法的研究开发空气股份有限公司 Process and installation for the separation of a gaseous mixture
EP0928936A2 (en) * 1998-01-13 1999-07-14 Air Products And Chemicals, Inc. Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures
CN1860338A (en) * 2003-09-30 2006-11-08 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 Method and installation for producing carbon monoxide by cryogenic distillation
CN1907849A (en) * 2005-05-10 2007-02-07 林德股份公司 Process and device for the recovery of products from synthesis gas
CN101617189A (en) * 2007-01-16 2009-12-30 乔治洛德方法研究和开发液化空气有限公司 Produce the method and apparatus of carbon monoxide by low temperature distillation
CN202133230U (en) * 2011-06-22 2012-02-01 杭州中泰深冷技术股份有限公司 Carbonic oxide and hydrogen cryogenic separation device

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1117129A (en) * 1994-04-13 1996-02-21 乔治·克劳德方法的研究开发空气股份有限公司 Process and installation for the separation of a gaseous mixture
EP0928936A2 (en) * 1998-01-13 1999-07-14 Air Products And Chemicals, Inc. Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures
CN1860338A (en) * 2003-09-30 2006-11-08 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 Method and installation for producing carbon monoxide by cryogenic distillation
CN1907849A (en) * 2005-05-10 2007-02-07 林德股份公司 Process and device for the recovery of products from synthesis gas
CN101617189A (en) * 2007-01-16 2009-12-30 乔治洛德方法研究和开发液化空气有限公司 Produce the method and apparatus of carbon monoxide by low temperature distillation
CN202133230U (en) * 2011-06-22 2012-02-01 杭州中泰深冷技术股份有限公司 Carbonic oxide and hydrogen cryogenic separation device

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102721264A (en) * 2012-07-04 2012-10-10 开封空分集团有限公司 Carbon monoxide mixture purification system and purification method
CN103523751A (en) * 2013-09-29 2014-01-22 开封空分集团有限公司 Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen
CN103523751B (en) * 2013-09-29 2015-03-11 开封空分集团有限公司 Device and method for performing cryogenic separation and purification on carbon monoxide and hydrogen
CN104236253A (en) * 2014-07-01 2014-12-24 开封空分集团有限公司 Device and method for extracting pure carbon monoxide and oxygen-rich gas by aid of cryogenic technology
CN105865146A (en) * 2016-04-25 2016-08-17 重庆耐德能源装备集成有限公司 Copious cooling liquefying system and cold box

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Application publication date: 20111130