CN104236253B - The device and method of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas - Google Patents

The device and method of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas Download PDF

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Publication number
CN104236253B
CN104236253B CN201410305908.3A CN201410305908A CN104236253B CN 104236253 B CN104236253 B CN 104236253B CN 201410305908 A CN201410305908 A CN 201410305908A CN 104236253 B CN104236253 B CN 104236253B
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China
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gas
pipeline
heat exchanger
carbon monoxide
liquid separator
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CN201410305908.3A
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Chinese (zh)
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CN104236253A (en
Inventor
卓跃光
王剑锋
王庆波
韦向攀
孙宇
翟彦邦
李美玲
黄磊
张苏宁
苏建龙
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开封空分集团有限公司
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    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/0228Processes 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
    • F25J3/0252Processes 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/0204Processes 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
    • F25J3/0223H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02Processes 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
    • F25J3/0228Processes 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
    • F25J3/0261Processes 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/40Features relating to the provision of boil-up in the bottom of a column
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00Processes or apparatus using separation by rectification
    • F25J2200/70Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/02Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00Processes or apparatus using other separation and/or other processing means
    • F25J2205/02Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • F25J2205/04Processes 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
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00Processes characterised by the type or other details of the feed stream
    • F25J2210/42Nitrogen
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/32Compression of the product stream
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02Recycle of a stream in general, e.g. a by-pass stream
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25JLIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00Refrigeration techniques used
    • F25J2270/90External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

Abstract

The present invention relates to the device and method of a kind of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, this device comprises front end pretreatment unit and cryogenic separation purifier units, described cryogenic separation purifier units comprises the first main heat exchanger, the second main heat exchanger and rectifying column, described rectifying column comprises the evaporimeter bottom tower body and tower body, and described cryogenic separation purifier units also comprises the first gas-liquid separator, the second gas-liquid separator, the 3rd gas-liquid separator and the 4th gas-liquid separator; The present invention by Joule-Thomson effect for whole device provide that the energy consumption of cold is low, good effect of heat exchange, technological process be simple.The device and method heat transfer effect of Deep Cooling Method making pure carbon monoxide disclosed by the invention and hydrogen rich gas is more desirable, and supplements without the need to nitrogen circulation refrigeration and a large amount of liquid nitrogen, reduces equipment, reduces energy consumption.

Description

The device and method of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas

Technical field

The invention belongs to synthesis gas cryogenic purification separation field, particularly relate to and produced with CO and (or) H by synthesis gas (by obtaining with the gasification of biomass such as coal or oil) 2for the technique of the chemical products of raw material, the particularly device and method of a kind of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas.

Background technology

CO and H 2be important basic chemical industry raw material, be widely used in the chemical processes such as carbonylation synthesis, especially C 1chemical is growing, CO has become the important source material of a series of basic organic chemical industry product and intermediate, such as Production of Acetic Acid by Methanol Carbonylation, aceticanhydride, formic acid, oxalic acid and dimethyl formamide etc., and optical self-encoding, production Merlon, polyurethane, synthetic metals carbonyls etc.Cheap and the CO isolation technics of CO that quantity is enriched source and advanced person, can promote the further growth of CO chemical process product technology widely.No matter be the CO synthesis gas obtained by coal, oil, natural gas, or the various industrial off-gas comprising CO, all CO sources are substantially all containing a certain amount of CO 2, H 2, N 2, CH 4, O 2deng admixture of gas, in order to obtain high-purity CO, should select low energy consumption, low cost, high efficiency separate mode, and deep cooling separating method being wherein applicable to large-scale industrial production, effectively can obtaining highly purified CO, effect is very good.

Cryogenic separation purification CO is a kind of physical separation method of high pressure low temperature, its general principle is Joule-Thomson throttling refrigeration effect, the process gas of certain pressure is by decompression, throttling, lower temperature can be produced, cold is reclaimed by heat exchange, can by the CO condensation separation in unstripped gas, the cold of whole system is then transformed by the pressure energy of technique.The core of separation by deep refrigeration is the difference utilizing each component boiling point in mist, realizes being separated of admixture of gas in gas-liquid separator with rectifying column.Solidify at low temperatures to prevent impurity contained in composite gas component thus block heat exchanger and pipeline, therefore using Deep Cooling Method separation of C O and H 2just need unstripped gas to carry out pretreatment before entering cryogenic separation purifier units, remove the component can solidified at low temperatures contained in component, as CO 2, methyl alcohol and H 2s etc.

In CO cryogenic separation method of purification disclosed in China, device technique flow process is relatively simple, but each period all needs N in separating-purifying process 2circularly cooling, use machine more, energy consumption is higher, and effect is not very desirable in heat exchanger matching process, heat exchanger be manufactured with larger difficulty.

Summary of the invention

The object of the invention is to overcome the energy consumption existed in above-mentioned prior art is high, machine is many and heat exchanger effect is undesirable shortcoming and provide that a kind of the energy consumption of cold is low, the device and method of good effect of heat exchange, technological process simple Deep Cooling Method making pure carbon monoxide and hydrogen rich gas for whole device provides by Joule-Thomson effect.

Technical scheme of the present invention is achieved in that the device of a kind of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, this device comprises front end pretreatment unit and cryogenic separation purifier units, described cryogenic separation purifier units comprises the first main heat exchanger, the second main heat exchanger and rectifying column, described rectifying column comprises the evaporimeter bottom tower body and tower body, and described cryogenic separation purifier units also comprises the first gas-liquid separator, the second gas-liquid separator, the 3rd gas-liquid separator and the 4th gas-liquid separator; The porch of described front end pretreatment unit connects the first pipeline of input material synthesis gas, the gas vent of described front end pretreatment unit is connected with described rectifying column bottom evaporator inlet through the first main heat exchanger and the 3rd choke valve by second pipe, described evaporator outlet is connected with described first gas-liquid separator centre entrance through the second main heat exchanger by the 3rd pipeline, and described first gas-liquid separator upper gas outlet is connected with Hydrogen collection unit through the second main heat exchanger, the first main heat exchanger successively by the 4th pipeline; The lower part outlet of described first gas-liquid separator is communicated with the 5th pipeline and the 6th pipeline respectively, described 5th pipeline is connected with described rectifier entrance through first throttle valve, described 6th pipeline is connected with described rectifying column centre entrance through second throttle, the second main heat exchanger, and the carbon monoxide liquid outlet of described rectifier bottoms is connected with described second gas-liquid separator centre entrance through the 4th choke valve by the 8th pipeline; Described second gas-liquid separator upper gas outlet is connected with the 19 pipeline through the second main heat exchanger, the first main heat exchanger successively by the 9th pipeline, described second gas-liquid separator lower liquid outlet connects two pipelines: the tenth pipeline and the 11 pipeline, described tenth pipeline after the second main heat exchanger with the 9th pipeline communication, described 11 pipeline is connected with described 3rd gas-liquid separator centre entrance through the 5th choke valve; Described 3rd gas-liquid separator upper gas outlet is connected with carbon monoxide compressor entrance through the second main heat exchanger, the first main heat exchanger successively by the 12 pipeline, the gas vent of described carbon monoxide compressor connects the 19 pipeline, described 3rd gas-liquid separator lower liquid outlet connects two pipelines: the 13 pipeline and the 14 pipeline, described 13 pipeline is connected with the 12 pipeline after the second main heat exchanger, and described 14 pipeline is connected with described 4th gas-liquid separator centre entrance through the 6th choke valve; Described 4th gas-liquid separator upper gas outlet is connected with carbon monoxide compressor through the second main heat exchanger, the first main heat exchanger successively by the 15 pipeline; Described 4th gas-liquid separator lower liquid outlet connects the 16 pipeline, and described 16 pipeline is connected with the 15 pipeline after the second main heat exchanger, and described 19 pipeline is connected to the gas access place of carbon monoxide collector unit.

Described first main heat exchanger and the second main heat exchanger are vacuum brazing aluminum plate fin heat exchanger, and described rectifying column is plate column or is packed tower, and described evaporimeter is vacuum brazing formula aluminum plate-fin heat exchanger.

The exit of described carbon monoxide compressor connects the 17 pipeline, and described 17 pipeline docks with the 19 pipeline, and described 19 pipeline is connected to described carbon monoxide collector unit porch, and described 9th pipeline docks with described 19 pipeline.

Described carbon monoxide compressor is a two-part carbon monoxide compressor: carbon monoxide compressor one section and carbon monoxide compressor two sections, the porch of described carbon monoxide compressor one section connects described 15 pipeline, the porch of described carbon monoxide compressor two sections connects the 12 pipeline, the gas vent of described carbon monoxide compressor one section connects the 18 pipeline, and described 18 pipeline docks with described 12 pipeline; Normal pressure CO gas enters carbon monoxide compressor one section successively through the 15 pipeline, carbon monoxide compressor two sections carries out two second compression, and low pressure CO gas directly enters carbon monoxide compressor two sections through the 12 pipeline carries out one section of compression.

Described rectifier arranges a flashed vapour outlet, described flashed vapour exit connects one the 7th pipeline, described 7th pipeline is connected with the second main heat exchanger, the first main heat exchanger, and described 7th pipeline stretches out described cryogenic separation unit outside and is connected with flashed vapour collector unit.

A method for Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, the method comprises:

1) material synthesis gas enters front end pretreatment unit through the first pipeline, by the molecular sieve adsorption in the pretreatment unit of front end by the Trace Methanol that contains in material synthesis gas and carbon dioxide eliminating, after decontaminating syngas after imurity-removal to enter in the first main heat exchanger cooling by second pipe, the evaporimeter entered in described rectifying column is cooled again as thermal source, decontaminating syngas after cooled is entered in the second main heat exchanger by the 3rd pipeline and continues to be cooled to design temperature 85 ~ 100K, the decontaminating syngas of design temperature is cooled to enter in the first gas-liquid separator by the 3rd pipeline through the entrance of the first gas-liquid separator,

2) the first gas-liquid separator carries out initial gross separation to cooled mist, the gas produced after being separated is hydrogen rich gas, hydrogen rich gas enters the second main heat exchanger, the first main heat exchanger re-heat reclaim cold from the gas vent on gas-liquid separator top successively by the 4th pipeline, and the hydrogen rich gas after re-heat is admitted to the Hydrogen collection unit of cryogenic separation unit outside by the 4th pipeline; The liquid part gone out by gas-liquid separator separates directly enters rectifying column from rectifier liquid inlet by the 5th pipeline by gas-liquid separator bottom liquid outlet after the throttling of first throttle valve, participates in rectifying as phegma; Another part liquid gone out by gas-liquid separator separates is introduced into the second heat exchanger re-heat pervaporation by gas-liquid separator bottom liquid outlet by the 6th pipeline after second throttle throttling, and after to enter described rectifying column middle and lower part through the liquid inlet of rectifying column bottom as rising gas and participate in rectifying;

3) after rectifying column rectifying, rectifier bottoms isolates aqueous carbon monoxide, the aqueous carbon monoxide of rectifier bottoms is sent by the 8th pipeline by the liquid outlet bottom it, after three throttling, send into the first main heat exchanger and the second main heat exchanger re-heat reclaim cold, after send cryogenic separation purifier units.

Described 3) described in, three throttling methods are as follows:

The aqueous carbon monoxide sent through the 8th pipeline provides cold through the 4th choke valve throttling for system, enters the second gas-liquid separator after throttling, and this is first time throttling; Second gas-liquid separator top gas enters the second main heat exchanger, the first main heat exchanger re-heat reclaim cold successively by the 9th pipeline, and the CO gas after re-heat is admitted to the carbon monoxide gas collector unit of cryogenic separation purifier units outside by the 19 pipeline; The liquid part gone out by the second gas-liquid separator separates enters the second main heat exchanger by gas-liquid separator bottom liquid outlet by the tenth pipeline, imports the 9th pipeline and enter First Heat Exchanger after re-heat;

Another part liquid gone out by the second gas-liquid separator separates by the 11 pipeline through the 5th choke valve throttling for system provides cold, enter the 3rd gas-liquid separator after throttling, this be second time throttling; 3rd gas-liquid separator top gas enters the second main heat exchanger, the first main heat exchanger re-heat reclaim cold successively by the 12 pipeline, CO gas after re-heat enters carbon monoxide compressor two sections and compresses, import the 19 pipeline by the 17 pipeline, send into the carbon monoxide gas collector unit of cryogenic separation purifier units outside; The liquid part gone out by the 3rd gas-liquid separator separates enters the second main heat exchanger by gas-liquid separator bottom liquid outlet by the 13 pipeline, imports the 12 pipeline and enter First Heat Exchanger after re-heat;

Another part liquid gone out by the 3rd gas-liquid separator separates by the 14 pipeline through the 6th choke valve throttling for system provides cold, enter the 4th gas-liquid separator after throttling, this be third time throttling; 4th gas-liquid separator top gas enters the second main heat exchanger, the first main heat exchanger re-heat reclaim cold successively by the 15 pipeline, CO gas after re-heat enters carbon monoxide compressor one section successively, carbon monoxide compressor one section carries out two second compression, carbon monoxide compressor second stage exit imports the 19 pipeline by the 17 pipeline, sends into the carbon monoxide gas collector unit of cryogenic separation purifier units outside; The liquid gone out by the 4th gas-liquid separator separates enters the second main heat exchanger by gas-liquid separator bottom liquid outlet by the 16 pipeline, imports the 15 pipeline and enter First Heat Exchanger after re-heat.

After described rectifying column rectifying, its top produces flashed vapour, flashed vapour enters described second main heat exchanger by the gas vent of rectifier successively by the 7th pipeline, the first main heat exchanger carries out re-heat and reclaims cold, send the flashed vapour collector unit outside described cryogenic separation purifier units through the 7th pipeline after cold recovery, described flashed vapour can be burning after collecting and provides heat.

After described 4th choke valve first time throttling, pressure is all 0.6MPa(G mutually with gas product pressure); After described 5th choke valve second time throttling, pressure and carbon monoxide compressor two sections of pressure at inlet are all 0.2MPa (G) mutually, and after described 6th choke valve third time throttling, pressure is normal pressure.

Pressure when material synthesis gas enters described first pipeline is 2.0MPa ~ 8.0Mpa, and described carbon monoxide compressor second stage exit pressure is 0.5MPa ~ 2.0MPa.

The good effect that technical scheme of the present invention produces is as follows: hydrogen rich gas is purified and can be completed in the first gas-liquid separator 5, after first separation, in liquid bottom first gas-liquid separator 5, CO purity can reach more than 90%, carry out rectification and purification entering described rectifying column 6, this rectifying column 6 comprises tower body and is arranged at the evaporimeter at the bottom of tower, and obtaining aqueous carbon monoxide purity in rectifier bottoms is more than 98.5%; Liquid CO product is sent by re-heat after three throttling refrigerations, through carbon monoxide compressor one section 71 or (with) after carbon monoxide compressor two section 72 compression, send and do product; Further, send cryogenic separation unit 2 after cold is reclaimed in the flashed vapour re-heat that rectifying column 6 top obtains to burn.

Described three throttling refrigerations, for main heat exchange, especially the thermal source in described second heat exchanger 4 provides the low-temperature receiver of three kinds of different pressures grades, better for thermal source carries out heat exchange coupling, thermal source is made to have suitable low-temperature receiver to mate with it in the diverse location section of heat exchanger, as shown in Figure 2, better play heat transfer effect, improve heat exchanger performance.

Described rectifying column 6 adopts plate column or packed tower, and rectification effect is good, and operating flexibility is large, is applicable to Off-design operation, and can adapts to the larger operating mode of liquid-gas ratio; Corresponding device is single tower process simultaneously, and the equipment of cryogenic separation purifier units is fewer, and ice chest is less, saves equipment investment; And this device also has the high advantage of carbon monoxide recovery rate, recovery rate can reach more than 90%.

The cold of described first main heat exchanger 3, second main heat exchanger 4 is provided by three throttlings of aqueous carbon monoxide product, hydrogen rich gas and flashed vapour re-heat, and without the need to nitrogen circulation refrigeration, reduce equipment, reduce energy consumption, the second heat exchanger 4 heat exchange property is better.

Accompanying drawing explanation

Fig. 1 is the schematic flow sheet of the device of Deep Cooling Method making pure carbon monoxide of the present invention and hydrogen rich gas.

Fig. 2 is the heat exchange property curve map of the second heat exchanger 4 in the method for Deep Cooling Method making pure carbon monoxide of the present invention and hydrogen rich gas.

Detailed description of the invention

Embodiment one

The device of a kind of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, as shown in Figure 1, this device comprises front end pretreatment unit 1 and cryogenic separation purifier units 2, described cryogenic separation purifier units 2 comprises the first main heat exchanger 3, second main heat exchanger 4, first gas-liquid separator 5, second gas-liquid separator 11, the 3rd gas-liquid separator 12, the 4th gas-liquid separator 13 and rectifying column 6, and described rectifying column 6 comprises the evaporimeter 61 bottom tower body itself and tower body.The unstripped gas of separating-purifying is for containing N 2, Ar, CH 4and micro-H 2s, CO 2cO and H 2gaseous mixture, described front end pretreatment unit 1 connects the first pipeline 101 of an input unstripped gas, the gas outlet of described front end pretreatment unit 1 connects second pipe 102, described second pipe 102 is connected with the bottom evaporator inlet of described rectifying column 6 through described first main heat exchanger 3 and the 3rd choke valve 16, described rectifying column 6 bottom evaporator outlet is connected through the centre entrance of the second main heat exchanger 4 with described first gas-liquid separator 5 by the 3rd pipeline 103, described first gas-liquid separator 5 upper gas exports by the 4th pipeline 104 through the second main heat exchanger 4, first main heat exchanger 3 is connected with Hydrogen collection unit 8, described first gas-liquid separator 5 lower liquid outlet connects two pipelines: the 5th pipeline 105 and the 6th pipeline 106, described 5th pipeline 105 is connected with described rectifying column 6 upper liquid entrance through first throttle valve 14, described 6th pipeline 106 is connected with described rectifying column 6 central gas entrance after the second main heat exchanger 4 re-heat through second throttle 15, carbon monoxide liquid outlet bottom described rectifying column 6 is connected with described second gas-liquid separator 11 through the 4th choke valve 17 by the 8th pipeline 108, described second gas-liquid separator 11 upper gas outlet is docked with the 19 pipeline 119 successively by the 9th pipeline 109 after the second main heat exchanger 4, first main heat exchanger 3 heat exchange, described second gas-liquid separator 11 lower liquid outlet connects two pipelines: the tenth pipeline the 110 and the 11 pipeline 111, described tenth pipeline 110 imports the 9th pipeline 109 after the second main heat exchanger 4 re-heat, and described 11 pipeline 111 is connected with described 3rd gas-liquid separator 12 through the 5th choke valve 18, described 3rd gas-liquid separator 12 upper gas exports by the 12 pipeline 112 successively through the second main heat exchanger 4, first main heat exchanger 3 is connected with carbon monoxide compressor 7 entrance, the gas vent of described carbon monoxide compressor 7 connects the 19 pipeline 119, described 3rd gas-liquid separator 12 lower liquid outlet connects two pipelines: the 13 pipeline the 113 and the 14 pipeline 114, described 13 pipeline 113 imports the 12 pipeline 112 after the second main heat exchanger 4 re-heat, described 14 pipeline 114 is connected with described 4th gas-liquid separator 13 through the 6th choke valve 19, described 4th gas-liquid separator 13 upper gas outlet is connected with carbon monoxide compressor 7 entrance through the second main heat exchanger 4, first main heat exchanger 3 successively by the 15 pipeline 115, described 16 pipeline 116 is connected with the second main heat exchanger 4, imports the 15 pipeline 115 after re-heat.Described 19 pipeline 119 is connected with carbon monoxide collector unit 9.

The exit of described carbon monoxide compressor 7 connects the 17 pipeline 117, described 17 pipeline 117 docks with the 19 pipeline 119, described 19 pipeline 119 is connected to described carbon monoxide collector unit 9 porch, and described 9th pipeline 109 docks with described 19 pipeline 119.

Described carbon monoxide compressor is a two-part carbon monoxide compressor: carbon monoxide compressor one section 71 and carbon monoxide compressor two section 72, the porch that described carbon monoxide compressor is one section 71 connects described 15 pipeline 115, the porch that described carbon monoxide compressor is two section 72 connects the 12 pipeline 112, the gas vent that described carbon monoxide compressor is one section 71 connects the 18 pipeline 118, and described 18 pipeline docks with described 12 pipeline 112; Normal pressure CO gas enters carbon monoxide compressor one section 71 successively through the 15 pipeline 115, carbon monoxide compressor carries out two second compression for two section 72, and low pressure CO gas directly enters carbon monoxide compressor through the 12 pipeline 112 carries out first compression for two section 72.

Described rectifying column 6 top arranges a flashed vapour outlet, described flashed vapour exit connects one the 7th pipeline 107, described 7th pipeline 107 is connected with the second main heat exchanger 4, first main heat exchanger 3, and it is outside that described 7th pipeline 107 stretches out described cryogenic separation purifier units 2.

Described first main heat exchanger 3 and the second main heat exchanger 4 are vacuum brazing aluminum plate fin heat exchanger, and described rectifying column 6 is plate column or is packed tower, and described evaporimeter is vacuum brazing aluminum plate fin heat exchanger.

Material synthesis atmospheric pressure in the first pipeline 101 described in input is 2.0MPa ~ 8.0MPa, and the CO gas pressure in described carbon monoxide compressor two section of 72 exit is 0.5MPa ~ 1.0MPa.

To reclaim after cold through heat exchanger re-heat from described rectifying column 6 top flashed vapour out and go out described cryogenic separation purifier units 2, if the pressure of unstripped gas is not high, whole system is except J-T effect (J-T effect: Joule-Thomson (Joule-Thomson) effect, be adiabatic throttling effect) refrigeration outside, supplementary liquid nitrogen is needed to provide the amount of cold little, even if be reserved with liquid nitrogen passage in heat exchanger, structural manufacturing process is still very simply smooth and easy, when driving to run, in order to whole cryogenic separation purifier units 2 being cooled down fast, a small amount of liquid nitrogen can be supplemented.

Embodiment two

A method for Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, the Deep Cooling Method making pure carbon monoxide wherein used in the method and the device of hydrogen rich gas are a kind of described device of embodiment, and this is no longer going to repeat them, and the method comprises:

1) material synthesis gas (CO+H 2content>=90%(mol%)) enter front end pretreatment unit 1 through the first pipeline 101, by the molecular sieve adsorption in front end pretreatment unit 1 by the Trace Methanol that contains in material synthesis gas and carbon dioxide eliminating, decontaminating syngas after imurity-removal is entered in the first main heat exchanger 3 by second pipe 102 and is cooled to uniform temperature (about 140K, different according to operating mode different set), the evaporimeter 61 entered in described rectifying column 6 through second pipe 102 is again cooled (gas saturation point) as thermal source, decontaminating syngas after cooled is entered in the second main heat exchanger 4 by the 3rd pipeline 103 and continues to be cooled to design temperature (85K ~ 100K, different according to operating mode different set), the decontaminating syngas of design temperature is cooled to enter in the first gas-liquid separator 5 by the 3rd pipeline 103 through the centre entrance of the first gas-liquid separator 5,

2) the first gas-liquid separator 5 carries out initial gross separation to cooled decontaminating syngas, the gas produced after being separated is hydrogen rich gas, hydrogen rich gas enters the second main heat exchanger 4, first main heat exchanger 3 re-heat from the gas vent on gas-liquid separator 5 top successively by the 4th pipeline 104 and reclaims cold, and the hydrogen rich gas after re-heat is admitted to the Hydrogen collection unit 8 of cryogenic separation purifier units 2 outside by the 4th pipeline 104; Directly enter rectifying column 6 from rectifying column 6 upper liquid entrance by the 5th pipeline 105 by gas-liquid separator bottom liquid outlet after first throttle valve 14 throttling by the isolated liquid part of the first gas-liquid separator 5, participate in rectifying as phegma; After second throttle 15 throttling, be introduced into the second heat exchanger re-heat pervaporation by the isolated another part liquid of gas-liquid separator 5 by the 6th pipeline 106, and after to enter described rectifying column 6 middle and lower part through the gas access of rectifying column 6 bottom as rising gas and participate in rectifying;

3) after rectifying column 6 rectifying, rectifying column 6 bottom part is from going out aqueous carbon monoxide, aqueous carbon monoxide bottom rectifying column 6 is sent by the 8th pipeline 108 by the liquid outlet bottom it, after three throttling, send into the first main heat exchanger 3 and the second main heat exchanger 4 re-heat reclaim cold, after send cryogenic separation purifier units 2.Described three throttling methods are specific as follows:

The aqueous carbon monoxide sent through the 8th pipeline 108 provides cold through the 4th choke valve 17 throttling for system, enters the second gas-liquid separator 11 after throttling, and this is first time throttling, and throttling downstream pressure is required product atmospheric pressure.Second gas-liquid separator 11 top gas enters the second main heat exchanger 4, first main heat exchanger 3 re-heat successively by the 9th pipeline 109 and reclaims cold, and the CO gas after re-heat is admitted to the carbon monoxide gas collector unit 9 of cryogenic separation purifier units 2 outside by the 19 pipeline 119; Enter second main heat exchanger 4 by gas-liquid separator bottom liquid outlet by the tenth pipeline 110 by the isolated liquid part of the second gas-liquid separator 11, import the 9th pipeline 109 after re-heat and enter First Heat Exchanger 3;

By the isolated another part liquid of the second gas-liquid separator 11 by the 11 pipeline 111 through the 5th choke valve 18 throttling for system provides cold, the 3rd gas-liquid separator 12 is entered after throttling, this is second time throttling, and throttling downstream pressure is carbon monoxide compressor two section of 72 inlet pressure.3rd gas-liquid separator 12 top gas enters the second main heat exchanger 4, first main heat exchanger 3 re-heat successively by the 12 pipeline 112 and reclaims cold, CO gas after re-heat enters carbon monoxide compressor two section of 72 entrance and compresses, import the 19 pipeline 119 by the 17 pipeline 117, send into the carbon monoxide gas collector unit 9 of cryogenic separation purifier units 2 outside; Enter second main heat exchanger 4 by gas-liquid separator 12 bottom liquid outlet by the 13 pipeline 113 by the isolated liquid part of the 3rd gas-liquid separator 12, import the 12 pipeline 112 after re-heat and enter First Heat Exchanger 3.

There is provided cold through the 6th choke valve 19 throttling for system by the 14 pipeline 114 by the isolated another part liquid of the 3rd gas-liquid separator 12, enter the 4th gas-liquid separator 13 after throttling, this is third time throttling, and throttling downstream pressure is normal pressure.4th gas-liquid separator 13 top gas enters the second main heat exchanger 4, first main heat exchanger 3 re-heat successively by the 15 pipeline 115 and reclaims cold, CO gas after re-heat enters carbon monoxide compressor one section of 71 entrance and carries out two second compression, carbon monoxide compressor one section 71 outlet is connected by the entrance of the 18 pipeline 118 and carbon monoxide compressor two section 72, then import the 19 pipeline 119 by the 17 pipeline 117, send into the carbon monoxide gas collector unit 9 of cryogenic separation purifier units 2 outside; The liquid gone out by the 4th gas-liquid separator separates 13 enters the second main heat exchanger 4 by gas-liquid separator 13 bottom liquid outlet by the 16 pipeline 116, imports the 15 pipeline 115 and enter First Heat Exchanger 3 after re-heat.

Described carbon monoxide compressor 7 outlet pressure is 0.5MPa ~ 2.0MPa, can according to different operating mode, adjustment compression number of times.

After the rectifying of described rectifying column 6, rectifying column 6 top produces flashed vapour, flashed vapour enters described second main heat exchanger 4, first main heat exchanger 3 by the gas vent on rectifying column 6 top successively by the 7th pipeline 107 and carries out re-heat recovery cold, send the flashed vapour collector unit 10 of described cryogenic separation purifier units 2 after cold recovery through the 7th pipeline 107, flashed vapour can provide heat for burning after collecting.

After described 4th choke valve 17 first time throttling, pressure is all 0.6MPa(G mutually with gas product pressure); After described 5th choke valve 18 second time throttling, pressure and carbon monoxide compressor two sections of pressure at inlet are all 0.2MPa (G) mutually, and after described 6th choke valve 19 third time throttling, pressure is normal pressure.

Described aqueous carbon monoxide by three throttling refrigerations through the 4th choke valve 17, the 5th choke valve 18 and the 6th choke valve 19, is not only technical process and provides most of cold, and better mates with thermal source in heat exchanger, and heat transfer effect is more desirable; The thermal source of described evaporimeter provided by the decontaminating syngas body tentatively cooled through First Heat Exchanger 3.

The cold of described first main heat exchanger 3, second main heat exchanger 4 is provided by three throttlings of aqueous carbon monoxide product, hydrogen rich gas and flashed vapour re-heat, without the need to nitrogen circulation refrigeration, reduces equipment, reduces energy consumption.And three throttling refrigerations, for the thermal source in First Heat Exchanger 3 and especially described second heat exchanger 4 of the second heat exchanger 4 provides the low-temperature receiver of three kinds of different pressures grades, better for thermal source carries out heat exchange coupling, thermal source is made to have suitable low-temperature receiver to mate with it in the diverse location section of the second heat exchanger 4, better performance heat transfer effect, improves heat exchanger performance.

As seen in Fig. 2, adopt three throttling technologies, can reduce, and warm end temperature difference also has corresponding reduction at cold junction heat transfer temperature difference, the mean logarithmic temperature difference of this heat exchanger can accomplish about 6, and maximum temperature difference only has 14k; Although there is temperature difference major part to occur in heat exchanger, heat transfer effect has obtained higher embodiment, reaches energy-conservation object.

Claims (10)

1. the device of a Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, this device comprises front end pretreatment unit (1) and cryogenic separation purifier units (2), described cryogenic separation purifier units (2) comprises the first main heat exchanger (3), second main heat exchanger (4) and rectifying column (6), described rectifying column (6) comprises the evaporimeter (61) bottom tower body and tower body, it is characterized in that: described cryogenic separation purifier units (2) also comprises the first gas-liquid separator (5), second gas-liquid separator (11), 3rd gas-liquid separator (12) and the 4th gas-liquid separator (13), the porch of described front end pretreatment unit (1) connects first pipeline (101) of input material synthesis gas, the gas vent of described front end pretreatment unit (1) is connected with described rectifying column (6) bottom evaporimeter (61) entrance through the first main heat exchanger (3) and the 3rd choke valve (16) by second pipe (102), described evaporimeter (61) outlet is connected with described first gas-liquid separator (5) centre entrance through the second main heat exchanger (4) by the 3rd pipeline (103), described first gas-liquid separator (5) upper gas exports by the 4th pipeline (104) successively through the second main heat exchanger (4), first main heat exchanger (3) is connected with Hydrogen collection unit (8), the lower part outlet of described first gas-liquid separator (5) is communicated with the 5th pipeline (105) and the 6th pipeline (106) respectively, described 5th pipeline (105) is connected with described rectifying column (6) upper entrance through first throttle valve (14), described 6th pipeline (106) is through second throttle (14), second main heat exchanger (4) is connected with described rectifying column (6) centre entrance, the carbon monoxide liquid outlet of described rectifying column (6) bottom is connected with described second gas-liquid separator (11) centre entrance through the 4th choke valve (17) by the 8th pipeline (108), described second gas-liquid separator (11) upper gas exports by the 9th pipeline (109) successively through the second main heat exchanger (4), first main heat exchanger (3) is connected with the 19 pipeline (119), described second gas-liquid separator (11) lower liquid outlet connects two pipelines: the tenth pipeline (110) and the 11 pipeline (111), described tenth pipeline (110) is communicated with the 9th pipeline (109) after the second main heat exchanger (4), described 11 pipeline (111) is connected with described 3rd gas-liquid separator (12) centre entrance through the 5th choke valve (18), described 3rd gas-liquid separator (12) upper gas exports by the 12 pipeline (112) successively through the second main heat exchanger (4), first main heat exchanger (3) is connected with carbon monoxide compressor (7) entrance, the gas vent of described carbon monoxide compressor (7) connects the 19 pipeline (119), described 3rd gas-liquid separator (12) lower liquid outlet connects two pipelines: the 13 pipeline (113) and the 14 pipeline (114), described 13 pipeline (113) is connected with the 12 pipeline (112) after the second main heat exchanger (4), described 14 pipeline (114) is connected with described 4th gas-liquid separator (13) centre entrance through the 6th choke valve (19), described 4th gas-liquid separator (13) upper gas outlet is connected with carbon monoxide compressor (7) through the second main heat exchanger (4), the first main heat exchanger (3) successively by the 15 pipeline (115), described 4th gas-liquid separator (13) lower liquid outlet connects the 16 pipeline (116), described 16 pipeline (116) is connected with the 15 pipeline (115) after the second main heat exchanger (4), and described 19 pipeline (119) is connected to the gas access place of carbon monoxide collector unit (9).
2. the device of Deep Cooling Method making pure carbon monoxide according to claim 1 and hydrogen rich gas, it is characterized in that: described first main heat exchanger (3) and the second main heat exchanger (4) are vacuum brazing aluminum plate fin heat exchanger, described rectifying column (6) is for plate column or be packed tower, and described evaporimeter is vacuum brazing formula aluminum plate-fin heat exchanger.
3. the device of Deep Cooling Method making pure carbon monoxide according to claim 1 and hydrogen rich gas, it is characterized in that: the exit of described carbon monoxide compressor (7) connects the 17 pipeline (117), described 17 pipeline (117) docks with the 19 pipeline (119), described 19 pipeline (119) is connected to described carbon monoxide collector unit (9) porch, and described 9th pipeline (109) docks with described 19 pipeline (119).
4. the device of Deep Cooling Method making pure carbon monoxide according to claim 1 and hydrogen rich gas, it is characterized in that: described carbon monoxide compressor is a two-part carbon monoxide compressor: carbon monoxide compressor one section (71) and carbon monoxide compressor two sections (72), the porch of described carbon monoxide compressor one section (71) connects described 15 pipeline (115), the porch of described carbon monoxide compressor two sections (72) connects the 12 pipeline (112), the gas vent of described carbon monoxide compressor one section (71) connects the 18 pipeline (118), described 18 pipeline docks with described 12 pipeline (112), normal pressure CO gas enters carbon monoxide compressor one section (71) successively through the 15 pipeline (115), carbon monoxide compressor two sections (72) carries out two second compression, and low pressure CO gas directly enters carbon monoxide compressor two sections (72) through the 12 pipeline (112) carries out one section of compression.
5. the device of Deep Cooling Method making pure carbon monoxide according to claim 1 and hydrogen rich gas, it is characterized in that: described rectifying column (6) top arranges a flashed vapour outlet, described flashed vapour exit connects one the 7th pipeline (107), described 7th pipeline (107) is connected with the second main heat exchanger (4), the first main heat exchanger (3), and described 7th pipeline (107) stretches out described cryogenic separation unit (2) outside and is connected with flashed vapour collector unit (10).
6. utilize device described in claim 1 to carry out a method for Deep Cooling Method making pure carbon monoxide and hydrogen rich gas, it is characterized in that: the method comprises:
1) material synthesis gas enters front end pretreatment unit (1) through the first pipeline (101), by the molecular sieve adsorption in front end pretreatment unit (1) by the Trace Methanol that contains in material synthesis gas and carbon dioxide eliminating, after decontaminating syngas after imurity-removal enters the interior cooling of the first main heat exchanger (3) by second pipe (102), the evaporimeter (61) entered in described rectifying column (6) is cooled again as thermal source, decontaminating syngas after cooled is entered in the second main heat exchanger (4) by the 3rd pipeline (103) and continues to be cooled to design temperature 85 ~ 100K, the decontaminating syngas of design temperature is cooled to enter in the first gas-liquid separator (5) by the 3rd pipeline (103) through the entrance of the first gas-liquid separator (5),
2) the first gas-liquid separator (5) carries out initial gross separation to cooled mist, the gas produced after being separated is hydrogen rich gas, hydrogen rich gas enters the second main heat exchanger (4), the first main heat exchanger (3) re-heat reclaim cold from the gas vent on gas-liquid separator (5) top successively by the 4th pipeline (104), and the hydrogen rich gas after re-heat is admitted to the outside Hydrogen collection unit (8) of cryogenic separation unit (2) by the 4th pipeline (104); Directly enter rectifying column (6) from rectifying column (6) upper liquid entrance by the 5th pipeline (105) by gas-liquid separator (5) bottom liquid outlet after first throttle valve (14) throttling by the isolated liquid part of gas-liquid separator (5), participate in rectifying as phegma; Through second throttle (15) throttling after be introduced into second heat exchanger (4) re-heat pervaporation by gas-liquid separator (5) bottom liquid outlet by the 6th pipeline (106) by the isolated another part liquid of gas-liquid separator (5), and after enter described rectifying column (6) middle and lower part through the liquid inlet of rectifying column (6) bottom as rising gas and participate in rectifying;
3) after rectifying column (6) rectifying, rectifying column (6) bottom part is from going out aqueous carbon monoxide, the aqueous carbon monoxide of rectifying column (6) bottom is sent by the 8th pipeline (108) by the liquid outlet bottom it, after three throttling, send into the first main heat exchanger (3) and the second main heat exchanger (4) re-heat reclaim cold, after send cryogenic separation purifier units (2).
7. the method for Deep Cooling Method making pure carbon monoxide according to claim 6 and hydrogen rich gas, is characterized in that: described 3), three throttling methods are as follows:
The aqueous carbon monoxide sent through the 8th pipeline (108) provides cold through the 4th choke valve (17) throttling for system, enters the second gas-liquid separator (11) after throttling, and this is first time throttling; Second gas-liquid separator (11) top gas enters the second main heat exchanger (4), the first main heat exchanger (3) re-heat reclaim cold successively by the 9th pipeline (109), and the CO gas after re-heat is admitted to the outside carbon monoxide gas collector unit (9) of cryogenic separation purifier units (2) by the 19 pipeline (119); Enter second main heat exchanger (4) by gas-liquid separator bottom liquid outlet by the tenth pipeline (110) by the isolated liquid part of the second gas-liquid separator (11), import the 9th pipeline (109) after re-heat and enter First Heat Exchanger (3);
There is provided cold through the 5th choke valve (18) throttling for system by the 11 pipeline (111) by the isolated another part liquid of the second gas-liquid separator (11), enter the 3rd gas-liquid separator (12) after throttling, this is second time throttling; 3rd gas-liquid separator (12) top gas enters the second main heat exchanger (4), the first main heat exchanger (3) re-heat reclaim cold successively by the 12 pipeline (112), CO gas after re-heat enters carbon monoxide compressor two sections (72) and compresses, import the 19 pipeline (119) by the 17 pipeline (117), send into the carbon monoxide gas collector unit (9) that cryogenic separation purifier units (2) is outside; Enter second main heat exchanger (4) by gas-liquid separator (12) bottom liquid outlet by the 13 pipeline (113) by the isolated liquid part of the 3rd gas-liquid separator (12), import the 12 pipeline (112) after re-heat and enter First Heat Exchanger (3);
There is provided cold through the 6th choke valve (19) throttling for system by the 14 pipeline (114) by the isolated another part liquid of the 3rd gas-liquid separator (12), enter the 4th gas-liquid separator (13) after throttling, this is third time throttling; 4th gas-liquid separator (13) top gas enters the second main heat exchanger (4), the first main heat exchanger (3) re-heat reclaim cold successively by the 15 pipeline (115), CO gas after re-heat enters carbon monoxide compressor one section (71) successively, carbon monoxide compressor two sections (72) carries out two second compression, carbon monoxide compressor two sections (72) outlet imports the 19 pipeline (119) by the 17 pipeline (117), sends into the carbon monoxide gas collector unit (9) that cryogenic separation purifier units (2) is outside; Enter second main heat exchanger (4) by gas-liquid separator bottom liquid outlet by the 16 pipeline (116) by the 4th gas-liquid separator (13) isolated liquid, import the 15 pipeline (115) after re-heat and enter First Heat Exchanger (3).
8. the method for Deep Cooling Method making pure carbon monoxide according to claim 6 and hydrogen rich gas, it is characterized in that: after described rectifying column (6) rectifying, its top produces flashed vapour, flashed vapour enters described second main heat exchanger (4) by the gas vent on rectifying column (6) top successively by the 7th pipeline (107), the first main heat exchanger (3) carries out re-heat and reclaims cold, send described cryogenic separation purifier units (2) flashed vapour collector unit (10) outward through the 7th pipeline (107) after cold recovery, described flashed vapour can be burning after collecting and provides heat.
9. the method for Deep Cooling Method making pure carbon monoxide according to claim 7 and hydrogen rich gas, is characterized in that: after described 4th choke valve (17) first time throttling, pressure is all 0.6MPa(G mutually with gas product pressure); After described 5th choke valve (18) second time throttling, pressure and carbon monoxide compressor two sections of pressure at inlet are all 0.2MPa (G) mutually, and after described 6th choke valve (19) third time throttling, pressure is normal pressure.
10. the method for Deep Cooling Method making pure carbon monoxide according to claim 7 and hydrogen rich gas, it is characterized in that: pressure when material synthesis gas enters described first pipeline (101) is 2.0MPa ~ 8.0Mpa, and described carbon monoxide compressor two sections of (72) outlet pressures are 0.5MPa ~ 2.0MPa.
CN201410305908.3A 2014-07-01 2014-07-01 The device and method of Deep Cooling Method making pure carbon monoxide and hydrogen rich gas CN104236253B (en)

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CN105716370B (en) * 2016-04-07 2018-05-11 开封空分集团有限公司 A kind of system and method that hydrogen rich gas and carbon monoxide are produced from synthesis gas
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