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CN101627273A - Method and device for obtaining products from synthesis gas - Google Patents

Method and device for obtaining products from synthesis gas Download PDF

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Publication number
CN101627273A
CN101627273A CN200780043967A CN200780043967A CN101627273A CN 101627273 A CN101627273 A CN 101627273A CN 200780043967 A CN200780043967 A CN 200780043967A CN 200780043967 A CN200780043967 A CN 200780043967A CN 101627273 A CN101627273 A CN 101627273A
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Prior art keywords
carbon monoxide
gas
condensation
nitrogen
hydrogen
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Chinese (zh)
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M·朗
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Linde GmbH
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Linde GmbH
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    • 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
    • C—CHEMISTRY; METALLURGY
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
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    • 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
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    • 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
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    • 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
    • F25J3/04—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 for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04527—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general
    • F25J3/04539—Integration with an oxygen consuming unit, e.g. glass facility, waste incineration or oxygen based processes in general for the H2/CO synthesis by partial oxidation or oxygen consuming reforming processes of fuels
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    • 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
    • F25J3/04—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 for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
    • F25J3/04587—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating for the NH3 synthesis, e.g. for adjusting the H2/N2 ratio
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
    • 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
    • F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead 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
    • 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
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    • 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
    • F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
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    • 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/42—Nitrogen
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    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2270/02—Internal refrigeration with liquid vaporising loop
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    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
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Abstract

The invention relates to a method for obtaining a carbon monoxide (37) and a hydrogen product (16) by cryogenically decomposing a feed gas (1) predominantly composed of hydrogen (H2) and carbon monoxide (CO) in a two-stage condensation process, maximum coldness for the second condensation stage being generated by mixing an H2-rich fraction (43) with liquid nitrogen (M-N2) (38, 42). The invention also relates to a device for carrying out said method. At least some (G-N2) (42) of the M-N2 is produced from nitrogen (39) that is externally fed to the two-stage condensation process as a gas, by cooling, condensing, and, preferably, supercooling the same within the two-stage condensation process against process flows that are to be heated.

Description

Obtain the method and apparatus of product by synthesis gas
Technical field
The present invention relates to by mainly by hydrogen (H 2) and the feed gas formed of carbon monoxide (CO) in the condensed in two stages process cryogenic separation and obtain the method for carbon monoxide product and hydrogen production, wherein by being rich in H 2Fraction and liquid nitrogen (M-N 2) mix and produce the maximum cold of second condensation stage.The invention still further relates to the equipment that is used to implement this method.
Background technology
By different production methods, for example catalytic steam reforming or partial oxidation (POX), the raw material by such as the hydrocarbonaceous of natural gas, liquefied gas, naphtha, heavy oil or coal produces the overwhelming majority by H 2With CO form but also comprise methane (CH 4), water (H 2O), carbon dioxide (CO 2) and such as the so-called synthesis gas of other components of nitrogen and argon.Particularly obtain CO and H by purifying with separating by synthesis gas 2As product, they have various purposes industrial.
Depend on the composition of feed gas to be separated, desired product line and the product purity of making every effort to reach, particularly adopt two kinds of low temperature processings, condensation process and methane washes with the extensive synthesis gas that separates.
More outmoded and fairly simple condensation process in two kinds of low temperature processings is particularly suitable for separating the synthesis gas that produces by partial oxidation, because this type of gas exists with high pressure usually, has high CO content and low methane content simultaneously.In condensation process, feed gas cools off in the indirect heat exchange relative with process flow to be heated, thereby makes it that partial condensation take place, and is rich in CO in this formation, contains H 2Liquid fraction and be rich in H 2, contain the gas fraction of CO, in phase-splitter, separate subsequently.(H then purifies 2Stripping, methane separation) wherein still is dissolved with H 2Reach the liquid fraction that is rich in CO of other materials, and discharge as the CO product.In the method, only can obtain contained CO in the feed gas with about 90% productive rate.In addition, produce the H that contains that purity only is about 90 moles of % 2Material flow, therefore can't discharge as product.
For fear of above-mentioned shortcoming, and with higher productive rate acquisition CO product, and/or production purity is greater than the H of 95 moles of % 2Product, according to prior art, condensation process is launched (condensed in two stages process) around film unit or around condensation stage.In these two processes, further handle the H that is rich in by the condensation acquisition 2, contain the gas fraction of CO, wherein isolate carbon monoxide basically, and import in the CO product; After isolating carbon monoxide, be rich in H 2The gas fraction have desired purity greater than 95 moles of %, can omit subsequent purification thus in some cases by transformation absorption.
In the condensed in two stages process, at the H that is rich in of first condensation stage acquisition 2, contain gas fraction and the process flow to be heated further cooling relatively of CO, wherein produce and be rich in CO, contain H 2Second liquid fraction and be rich in H 2, contain the second gas fraction of CO, in second phase-splitter, separate subsequently.By being mixed with the gas fraction of mainly being made up of hydrogen, liquid nitrogen produces the required maximum cold of this second condensation stage according to prior art, for this reason from the outside, for example,, in this Cryogenic air separation machine, obtain the required oxygen of POX to chilling process input liquid nitrogen from the Cryogenic air separation machine.In order to reach enough low temperature at the second seperator place, must be to a large amount of relatively liquid nitrogen of condensed in two stages process input, thus the cold that makes introducing is greater than satisfying the required cold of this process cold balancing.Superfluous at present cold is not utilized and loses.Because prepare liquid nitrogen with sizable equipment complexity and particularly energy consumption, so unemployed cold damages the economy of condensed in two stages process significantly.
Summary of the invention
Therefore, the objective of the invention is to the equipment that proposes the method for aforementioned type and implement this method, it can produce hydrogen production and carbon monoxide product by synthesis gas with the operating cost that is lower than prior art.
Aspect method, realize this purpose as follows according to the present invention, by in the condensed in two stages process, relatively cool off with process flow to be heated, condensation and preferred cold excessively, produce M-N by the nitrogen that imports the condensed in two stages process with gaseous state from the outside 2At least a portion (G-N 2).
The present invention is based on following experience, compare, can produce gaseous nitrogen by significantly lower cost with liquid nitrogen.By adopting the method according to this invention, in the deaerator scope, realize the corresponding reduction of operating cost and cost of investment.
If the condensed in two stages process for example is used for separating the synthesis gas that produces by partial oxidation (POX), and in deaerator, obtains the required oxygen of POX, then obtain liquid nitrogen from this deaerator pointedly by low temperature air separating.
If showing in the condensed in two stages process, cold balancing can't produce enough G-N 2, reach desired temperature with seperator place in second condensation stage, then, import the nitrogen amount (L-N that is lacked from the outside with liquid form according to an embodiment of the inventive method 2).Regulate G-N pointedly 2With L-N 2The ratio of amount, thereby produce carbon monoxide product and produce hydrogen production with desired productive rate with desired degree of purity, but the cold surplus can not take place.
According to another embodiment of the inventive method, suggestion obtains G-N from deaerator 2And/or L-N 2, produce oxygen contains hydrogen and carbon monoxide with generation feed gas (for example in POX) therein.G-N 2Preferably discharge from deaerator, thereby the overall energy requirement of this process is minimized with medium or low stress level.
In addition, the invention still further relates to the equipment (gas seperator) that is used to implement the condensed in two stages process, therein can be with mainly by hydrogen (H 2) and the feed gas formed of carbon monoxide (CO) be separated into carbon monoxide product and hydrogen production, wherein by being rich in H 2Fraction and liquid nitrogen (M-N 2) mix and produce the maximum cold of second condensation stage of this gas seperator.
Realizing as follows aspect equipment according to the present invention that the purpose that proposed, gas seperator comprise is used to make M-N 2At least a portion (G-N 2) device, will implement condensation and preferred cold excessively from the nitrogen of outside input by relatively cooling off with gaseous state therein with process flow to be heated.
According to prior art, the gas seperator has the heat exchanger of two series connection mostly, and wherein heat exchanger is a heat-exchangers of the plate type, and the cold side of first heat exchanger is also warmmer than the hot side of second heat exchanger.The hot side of first heat exchanger is connected with the source of gaseous nitrogen via pipeline pointedly, can import nitrogen to first heat exchanger by gaseous state via this pipeline.Subsequently in heat exchanger with process flow to be heated relatively to nitrogen cool off, condensation and optional cold excessively.
There are not enough colds in gas seperator inside to produce required M-N from gaseous nitrogen 2The situation of total amount under, according to an embodiment of present device, this gas seperator is equipped with a device, can be from the outside with liquid nitrogen (L-N via this device 2) form to the M-N of gas seperator input a part of amount 2
According to an embodiment preferred of present device, obtain gaseous nitrogen to produce G-N from deaerator 2And/or L-N 2, produce oxygen contains hydrogen and carbon monoxide with generation feed gas (for example in POX) therein.
Gaseous nitrogen from deaerator preferably has medium or low stress level.
By replacing liquid nitrogen with gaseous nitrogen, the method according to this invention can reduce the cost that is used for producing the maximum cold of condensed in two stages process, and improves the economy of this partition method.
Set forth the present invention in more detail according to two embodiment below, both all relate to the schematic diagram in the accompanying drawing.
Description of drawings
Figure 1 shows that according to embodiment of the present invention.
The specific embodiment
This embodiment is the method for being produced hydrogen production and carbon monoxide product by the charging of hydrocarbonaceous.
The charging 1 of hydrocarbonaceous is imported the POX reactor P with the oxygen flow 2 that obtains from deaerator LZ, be converted into by partial oxidation at this and mainly contain hydrogen (H 2) and the synthetic raw gas 3 of carbon monoxide (CO).In gas purification device R, obtain the feed gas 4 mainly formed from synthetic raw gas 3, subsequently with its importing cryogenic separation unit Z by hydrogen and carbon monoxide by further removing such as the material of the non-expectation of water and carbon dioxide.At this,, it is separated in phase-splitter D1 is rich in H by in two main heat exchanger E1 and E2, relatively cooling off with partial condensation and from feed gas 4 generations first two-phase mixture 5 with process flow to be heated 2, contain first gas phase 6 of CO and be rich in CO, contain H 2First liquid phase 7.In heat exchanger E3, further cool off this and be rich in H 2, contain first gas phase 6 of CO, the part of wherein contained carbon monoxide is condensed out, and produces second two-phase mixture 8, it is separated in phase-splitter D2 is rich in H 2, contain second gas phase 9 of CO and be rich in CO, contain H 2Second liquid phase 10.Be rich in CO, contain H 2Second liquid phase 10 in heat exchanger E3, relatively heat with process flow to be cooled after, further guide via pipeline 11, via throttling arrangement a decompression, with being rich in CO, containing H via throttling arrangement b decompression 2First liquid phase 7 guide to H via pipeline 12 together 2Stripper T1, and add at cat head.This H 2Stripper T1 is used for removing the hydrogen that is dissolved in the material flow 12 that is rich in CO.Use is integrated in the natural-circulation evaporator (reboiler) among the heat exchanger E2, with heating H 2Stripper T1.From H 2At the bottom of the tower of stripper T1 material flow 13 is imported reboiler, in this part evaporation, and via pipeline 14 backflows.From H 2Stripper T1's is rich in H 2, the cat head fraction 15 that contains CO heats in heat exchanger E2 and E1, and is back to this process as so-called flash gas 16 via gas purification device R.If this gas purification device R is a low-temp methanol to be washed (
Figure G2007800439676D00051
), then preferably will be used for this backflow at the recycle compressor (not shown) of this installation.
From H 2Fraction at the bottom of the tower of stripper T1 promptly mainly contains carbon monoxide and nitrogen (N 2) mixture, discharge via pipeline 17, via throttling arrangement c decompression, and send into N 2In/CO the knockout tower.N 2/ CO knockout tower T2 is stream 18 heating of the carbon monoxide 19 by having product purity directly, it is discharged from CO compressor V in intermediate pressure section V2 downstream, in heat exchanger E1, relatively cool off,, and directly send at the bottom of the tower subsequently via throttling arrangement d decompression with process flow to be heated.
Will be from N 2The carbon monoxide fraction 27 with product purity at the bottom of the tower of/CO knockout tower T2 is divided into two parts and measures 28 and 29, and wherein part measures 28 via throttling arrangement g decompression, and importing is integrated in N 2Overhead condenser E5 among the/CO knockout tower T2 to be cooling off it, and part measure 29 after via throttling arrangement h decompression with in cat head cooler E5, evaporate and from N 2The CO fraction 30 that the cat head of/CO knockout tower T2 is discharged is heated and discharges thus via pipeline 32 together via pipeline 31 inflow heat exchanger E2.For to the cold budget of cryogenic gas separation process (
Figure G2007800439676D00052
) carry out meticulous adjusting, distribute little part amount 33 from CO fraction 32, and in the bypass of heat exchanger E1, guide, wherein pass through the size of adjusting device i adjusting portion component 33.The rest parts amount 34 of CO fraction 32 heats in heat exchanger E1, further guides via pipeline 35, and deliver to CO compressor V via pipeline 36 as intermediate feed with the part amount 33 that guides after converging in bypass.
From N 2The part of the liquid carbon monoxide of/CO knockout tower T2 cat head is discharged via pipeline 20.After being decompressed to the low pressure level via throttling arrangement e, heat exchanger E2 provides maximum cold, subsequently evaporation therein.Via pipeline 21 delivery heat exchanger E1, heat at this, and import the suction side of first section V1 of CO compressor V via pipeline 22.
From N 2The cat head fraction 23 of/CO knockout tower T2, i.e. N 2/ CO mixture via throttling arrangement f decompression, and imports in the residual gas, and it is via among pipeline 24 and 25 delivery heat exchanger E1 and the E2, and in this heating, derives from this process via pipeline 26 then.
Two kinds of carbon monoxide fractions 22 and 36 with product quality are compressed to product pressure in compressor section V1 to V4, and discharge at the device end place as CO product 37.
Use two strands of nitrogen streams 38 and 39 to be created in maximum cold required in the condensed in two stages process and compensation cold balancing, wherein obtain one nitrogen stream 38 with liquid state, and obtain another strand nitrogen stream 39 with gaseous state from deaerator LZ.The gaseous nitrogen stream 39 that also is used for reclaiming cold is at first in heat exchanger E1 and E2 cooling and condensation, and is cold via carrying out among the pipeline 41 delivery heat exchanger E3 subsequently.Discharged cold nitrogen via pipeline 42 from heat exchanger E3, be decompressed to via throttling arrangement j after the pressure of residual gas, with H from seperator D2 2The part amount 43 of fraction 9 and liquid nitrogen stream 38 mixing that import via throttling arrangement k.By being mixed with hydrogen, liquid nitrogen makes N 2/ H 2Mixture 44 is to be lower than N 2The temperature of dew point (78K) is in cold side delivery heat exchanger E3.Thus can be in seperator D2 with high-purity (greater than 95 moles of %H 2) isolate and be rich in H 2, contain operation seperator D2 under the temperature of second gas phase 9 of CO.Be rich in H 2, the main amount 46 that contains second gas phase 9 of CO heats in heat exchanger E3 and heat in two heat exchanger E2 that it is imported via pipeline 47 and 48 and E1 subsequently, and discharge in the device end place as hydrogen production 49.The N that will in heat exchanger E3, heat 2/ H 2Mixture 50 with from N 2The cat head fraction 23 of/CO knockout tower T2 imports in the residual gas 26 together.
In a second embodiment, the nitrogen stream 41 of part condensation in heat exchanger E1 and E2 is as H 2The backflow of stripper T1 is rich in H with reduction 2The cat head fraction in CO content.In this structure, can omit from H 2The backflow of the cat head fraction 16 of stripper T1.Instead, cat head fraction 15 is entered in the residual gas stream 24, perhaps if require extra high H 2Productive rate, then in heat exchanger E3, cross cold after, replace the H that is rich in from seperator D2 2 Fraction 9 part stream 43 and mix with two bursts of liquid nitrogen stream 38 and 42.

Claims (6)

1, by in the condensed in two stages process cryogenic separation mainly by hydrogen (H 2) and the feed gas (1) formed of carbon monoxide (CO) to obtain the method for carbon monoxide product (37) and hydrogen production (16), wherein by being rich in H 2Fraction (43) and liquid nitrogen (M-N 2) (38,42) mixed and produced the maximum cold of second condensation stage, it is characterized in that, by the nitrogen (39) of importing described condensed in two stages process with gaseous state from the outside by described condensed in two stages process, relatively cool off with process flow to be heated, condensation and the cold M-N of generation of preferred mistake 2At least a portion (G-N 2) (42).
2, according to the method for claim 1, it is characterized in that M-N 2A part by G-N 2Form, and another part (L-N 2) import described condensation process from the outside with liquid state.
3, according to the method for claim 1 or 2, it is characterized in that, obtain G-N by deaerator 2And/or L-N 2, in this deaerator, produce oxygen contains hydrogen and carbon monoxide with generation feed gas.
4, be used to implement the equipment (gas seperator) of condensed in two stages process, therein will be mainly by hydrogen (H 2) and the feed gas formed of carbon monoxide (CO) be separated into carbon monoxide product and hydrogen production, wherein by being rich in H 2Fraction and liquid nitrogen (M-N 2) mix and produce the maximum cold of second condensation stage of described gas seperator, it is characterized in that described gas seperator comprises and is used to make M-N 2At least a portion (G-N 2) device, will implement condensation and preferred cold excessively from the nitrogen of outside input by relatively cooling off with gaseous state therein with process flow to be heated.
According to the equipment of claim 4, it is characterized in that 5, described gas seperator is equipped with a device, install from the outside with liquid nitrogen (L-N via this 2) form to the M-N of described gas seperator input part amount 2
6, according to the equipment of claim 4 or 5, it is characterized in that, obtain G-N by a deaerator 2And/or L-N 2, produce oxygen contains hydrogen and carbon monoxide with generation feed gas therein.
CN200780043967A 2006-11-30 2007-11-06 Method and device for obtaining products from synthesis gas Pending CN101627273A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103438666A (en) * 2013-08-21 2013-12-11 张周卫 Multi-strand winding pipe type main back heating and heat exchange device for low-temperature liquid nitrogen
CN110044133A (en) * 2019-05-17 2019-07-23 成都赛普瑞兴科技有限公司 The apparatus and method for of separating-purifying carbon monoxide

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3018599B1 (en) * 2014-03-17 2019-06-28 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude METHOD AND APPARATUS FOR CRYOGENIC SEPARATION OF A SYNTHESIS GAS CONTAINING CARBON MONOXIDE, METHANE AND HYDROGEN
DE102014015160A1 (en) 2014-10-14 2016-04-14 Linde Aktiengesellschaft Process and apparatus for recovering carbon monoxide and hydrogen from synthesis gas
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Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1515926A (en) * 1966-09-30 1968-03-08 Air Liquide Process for the production of oxygen and pure nitrogen under high pressure from air for the manufacture and purification at low temperature of a mixture of hydrogen and nitrogen
IN160585B (en) * 1983-02-14 1987-07-18 Exxon Research Engineering Co
DE3802552A1 (en) * 1988-01-28 1989-08-10 Linde Ag PROCESS FOR CLEANING A GAS MIXTURE
GB9802231D0 (en) * 1998-02-02 1998-04-01 Air Prod & Chem Separation of carbon monoxide from nitrogen-contaminated gaseous mixtures also containing hydrogen
EP1215458B1 (en) * 2000-12-18 2005-02-09 Air Products And Chemicals, Inc. Process and apparatus for the separation of carbon monoxide and hydrogen from a gaseous mixture thereof
DE10226209B4 (en) * 2002-06-13 2008-04-03 Lurgi Ag Plant and process for the production and decomposition of synthesis gases from natural gas
DE10226210A1 (en) * 2002-06-13 2004-01-08 Lurgi Ag Plant part for the disassembly and cleaning of synthesis gas
DE102005046790A1 (en) * 2005-09-29 2007-04-05 Linde Ag Method for cleaning of gas mixture, involves obtaining part of washing column of supplied nitrogen liquid and deep-frozen from a cryogenic air decomposer

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103438666A (en) * 2013-08-21 2013-12-11 张周卫 Multi-strand winding pipe type main back heating and heat exchange device for low-temperature liquid nitrogen
CN110044133A (en) * 2019-05-17 2019-07-23 成都赛普瑞兴科技有限公司 The apparatus and method for of separating-purifying carbon monoxide
CN110044133B (en) * 2019-05-17 2024-03-22 成都赛普瑞兴科技有限公司 Apparatus and method for separating and purifying carbon monoxide

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