CN110093191B - Recovery device and method for effective gas in low-temperature methanol washing process - Google Patents
Recovery device and method for effective gas in low-temperature methanol washing process Download PDFInfo
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- CN110093191B CN110093191B CN201910320038.XA CN201910320038A CN110093191B CN 110093191 B CN110093191 B CN 110093191B CN 201910320038 A CN201910320038 A CN 201910320038A CN 110093191 B CN110093191 B CN 110093191B
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 270
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000005406 washing Methods 0.000 title claims abstract description 23
- 238000011084 recovery Methods 0.000 title description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 117
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 66
- 239000007788 liquid Substances 0.000 claims abstract description 59
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 57
- 238000001704 evaporation Methods 0.000 claims abstract description 51
- 230000008020 evaporation Effects 0.000 claims abstract description 45
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 238000003860 storage Methods 0.000 claims abstract description 11
- 238000011143 downstream manufacturing Methods 0.000 claims description 14
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 229910052739 hydrogen Inorganic materials 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- 239000002699 waste material Substances 0.000 claims 1
- 238000003912 environmental pollution Methods 0.000 abstract description 9
- 238000001816 cooling Methods 0.000 abstract description 6
- 230000008014 freezing Effects 0.000 abstract description 4
- 238000007710 freezing Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 70
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 13
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 12
- 239000003245 coal Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
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- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
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Abstract
A device and a method for recovering effective gas in a low-temperature methanol washing process are disclosed, wherein a methanol-rich pipeline is connected with a gas-liquid separation tank, the gas-liquid separation tank is connected with a heat exchanger II through a heat exchanger I, the heat exchanger II is connected with a gas-liquid separation tank II, and the gas-liquid separation tank II is connected with a flash vapor tank. And the second gas-liquid separation tank is connected with a second heat exchanger, and the second heat exchanger is connected to a carbon dioxide storage tank. A specific process flow is set for cooling and freezing so that part of carbon dioxide in methanol flash evaporation is liquefied and separated, and therefore effective gas (H) in flash evaporation gas is increased2CO) to reduce the load of the compressor in the process of boosting the flash steam and reduce the environmental pollution of gas emission.
Description
Technical Field
The invention belongs to the field of gas purification, and particularly relates to recovery of effective gas in a low-temperature methanol washing process.
Background
The production capacity of the coal chemical industry in China is improved, the amount of flash evaporation gas is controlled by reducing the temperature of methanol or controlling the amount of flash evaporation gas by absorbing carbon dioxide in flash evaporation gas with methanol at a lower temperature in the recovery of effective gas dissolved in methanol in the low-temperature methanol washing process of gas purification, so that the load of a compressor in the pressure boosting process of the flash evaporation gas is reduced, and the environmental pollution of the gas is reduced.
Disclosure of Invention
The invention aims to provide a device and a method for recovering effective gas (H) in a low-temperature methanol washing process, which improve the effective gas (H) in flash evaporation2CO) to achieve the purposes of reducing the load of the compressor in the boosting process of flash steam and reducing the environmental pollution caused by gas emission.
The technical conception of the invention is as follows:
effective gas (H) dissolved in methanol during low-temperature methanol washing2CO) can be more thoroughly flash evaporated and analyzed only at low pressure and high temperature, and the effective gas (H) in the process can be improved2CO) utilization benefit, and environmental pollution caused by emission is reduced; the carbon dioxide dissolved in the methanol at low pressure and high temperature is also flashed correspondingly, and the load of the compressor in the pressure increasing process is increased.
The invention has the technical conception that rich methanol absorbing gas is directly subjected to low-pressure flash evaporation, and part of carbon dioxide in flash evaporation gas is separated out through cooling, freezing and liquefying, so that the load of a compressor in the boosting process is reduced, and the purpose of increasing the effective gas (H) in the process is achieved2CO), reducing the environmental pollution of emission.
The technical solution of the invention is (see the attached figure 1):
during the low-temperature methanol washing process, methanol absorbs a certain amount of effective gas (H) while absorbing carbon dioxide and hydrogen sulfide2CO), effective gas (H) is required to reduce the environmental pollution of gas emissions for increasing the process efficiency2CO) recovery. The methanol rich in the absorbed gas correspondingly flashes a certain amount of carbon dioxide in the pressure reduction and flash evaporation process, the load of a compressor in the pressure increase process of flash evaporation gas is increased, and partial carbon dioxide in the flash evaporation gas is separated by cooling, freezing and liquefying to recover the effective gas (H)2CO) while reducing the load of the compressor, increasing effective recovery and reducing the environmental pollution of discharge.
The method comprises the following specific steps:
a methanol-rich pipeline is connected with a first gas-liquid separation tank V1, the first gas-liquid separation tank V1 is connected with a second heat exchanger E2 through a first heat exchanger E1, the second heat exchanger E2 is connected with a second gas-liquid separation tank V2, and the second gas-liquid separation tank V2 is connected with a flash vapor tank.
The second gas-liquid separation tank V2 is connected with a second heat exchanger E2, and the second heat exchanger E2 is connected to a carbon dioxide storage tank.
The second heat exchanger E2 is connected to a dirty liquid storage tank through a pipeline.
The bottom of the first gas-liquid separation tank V1 is connected to a methanol-rich storage tank through a pipeline.
The other technical scheme of the invention is a method for recovering effective gas in the low-temperature methanol washing process by adopting the device, which comprises the following steps:
(1) the rich methanol absorbing the gas in the low-temperature methanol washing process is directly subjected to reduced pressure flash evaporation to separate part of the gas, and the rich methanol subjected to reduced pressure flash evaporation is sent to a downstream process for continuous regeneration treatment;
(2) the part of the flashed gas is cooled and frozen through the first heat exchanger and the second heat exchanger to liquefy part of carbon dioxide, the cooled and frozen flash steam is flashed and separated in the second gas-liquid separation tank to obtain flash steam, and the flash steam is sent to a compressor to be pressurized for reuse;
(3) and liquid carbon dioxide separated by flash evaporation in the second gas-liquid separation tank is evaporated and gasified into gas carbon dioxide through the second heat exchanger and then is sent to a downstream process for treatment, and residual foul solution after flash evaporation in the second heat exchanger is sent to the downstream process for treatment.
The rich methanol comprises methanol after carbon dioxide removal and methanol after desulfurization.
The temperature of the methanol is-20 to-12 ℃ and the pressure of the methanol is 5-7Mpa in the process of removing carbon dioxide, and the methanol gas comprises CH with the molar content of 68-75 percent3OH, CO in a molar content of 22-28%20.5-1.0% of CO and 0.2-0.6% of H20.3610% molar content of H2O; reducing the pressure to 1.0-1.5MPa in the flash evaporation process, wherein the flash evaporation gas contains H with the molar content of 7-10 percent after flash evaporation210-15% of CO by mol content and 70-80% of CO by mol content20.05-0.1% of CH by mole40.05-0.1% of CH by mole3OH。
In the process of methanol desulfurization, the temperature is minus 20 to minus 12 ℃, the pressure is 5 to 7Mpa, and the methanol gas comprises CH with the molar content of 71.371 percent3OH, 26.708% by mol CO20.6775% CO by mol, 0.4281% H by mol20.4296% molar content of H2S, H with a molar content of 0.3699%2O; reducing the pressure to 1.0-1.5MPa in the flash evaporation process, wherein the flash evaporation gas contains 5-10% of H in molar content after flash evaporation210-15% of CO by mol content and 75-85% of CO by mol content20.1-0.6% of H in molar content2S, the molar content of CH is 0.05-0.1%3OH。
In the step (2), the flash steam is liquefied and separated into carbon dioxide liquid by cooling to 50-55 ℃ and the pressure of 1.0-1.3MPa, and the carbon dioxide liquid comprises 97-99% of CO in molar content20.5-0.8% of CO and 0.2-0.3% of H2S, 0.05-0.15% of CH with molar content3OH。
In the carbon dioxide gas which is gasified by the heat exchanger in the step (3), the temperature is 50-55 ℃, the pressure is 1.0-1.3MPa, and the carbon dioxide gas comprises 50-55 percent of CO by mole content225-28% of CO and 0.1-0.2% of H2S。
Effective gas (H) absorbed in methanol in the process2CO), reducing the load of a compressor for boosting the pressure of flash steam and reducing the environmental pollution of discharged gas.
Drawings
Fig. 1 is a recovery device of effective gas in the low-temperature methanol washing process, wherein, V1: first gas-liquid separation tank, V2: second gas-liquid separation tank, E1: heat exchanger one, E2: heat exchanger two, L1: level control valve one, L2: liquid level control valve two, L3: level control valve three, P1: pressure control valve one, P2: and a second pressure control valve.
Detailed Description
The present invention will be further described with reference to fig. 1 and examples, wherein different flash pressures are set for the methanol-rich gas after low-temperature methanol washing purification of the gas in coal gasification processes of different processes, so as to resolve more effective gas (H) in methanol2CO). The temperature of the initial flash steam after temperature reduction and freezing is determined by the properties of carbon dioxide: the triple point of the carbon dioxide is-56.568 ℃, and the flash evaporation control of the liquid carbon dioxide is used for preventing the solidification of the carbon dioxide from influencing the continuity of the operationThe temperature is controlled to be-56 ℃ above the triple point of the carbon dioxide, and the temperature of flash steam can be reduced to-52 ℃.
The liquid carbon dioxide separated from the initial flash gas liquefaction contains methanol and hydrogen sulfide, and the gas carbon dioxide evaporated from the liquid carbon dioxide and the liquid remained in the evaporation process also need to be further treated by downstream processes.
And sending the methanol-rich gas after pressure reduction and flash evaporation to a downstream process for regeneration treatment.
And the initial flash evaporation gas is sent to a compressor for boosting pressure and recycling after part of carbon dioxide is separated through temperature reduction and liquefaction.
The method for recovering the effective gas in the low-temperature methanol washing process can separate part of the carbon dioxide in the initial flash evaporation gas by cooling and liquefying, and can flash more effective gas (H) in the rich methanol2CO) without increasing the load of the compressor in the boosting process of flash steam, and the environmental pollution of gas emission is reduced.
Example 1
Take the low temperature methanol washing of producing 90 ten thousand tons of methanol in a year by gasifying coal water slurry to prepare methanol
(1) The rich methanol absorbing the gas in the low-temperature methanol washing process is directly subjected to reduced pressure flash evaporation to separate part of the gas, and the rich methanol subjected to reduced pressure flash evaporation is sent to a downstream process for continuous regeneration treatment;
(2) the part of the flashed gas is cooled and frozen through the first heat exchanger and the second heat exchanger to liquefy part of carbon dioxide, the cooled and frozen flash steam is flashed and separated in the second gas-liquid separation tank to obtain flash steam, and the flash steam is sent to a compressor to be pressurized for reuse;
(3) and liquid carbon dioxide separated by flash evaporation in the second gas-liquid separation tank is evaporated and gasified into gas carbon dioxide through the second heat exchanger and then is sent to a downstream process for treatment, and residual foul solution after flash evaporation in the second heat exchanger is sent to the downstream process for treatment.
The rich methanol comprises methanol after carbon dioxide removal and methanol after desulfurization.
Decarbonized methanol 10833Kmol/H, 5.7Mpa, -16 ℃, 0.4257% H2、0.005074%N2、0.6908%CO、0.003578%Ar、0.005999%CH4、26.640%CO2、0.000100%H2S、0.00000454%COS、71.868%CH3OH、0.3610%H2Reducing the pressure of O to 1.3Mpa, and flashing off 511.368Kmol/h flash steam: 43.71222Kmol/H H20.00000699137Kmol/h of N264.62987Kmol/h CO, 0.3237219Kmol/h Ar, 0.4661208Kmol/h CH4401.8661208Kmol/h CO20.000467086Kmol/H of H2S, 0.0000000119054Kmol/h COS, 0.3652255Kmol/h CH3OH, 0.000537869Kmol/H of H2And O. 2.403866Kmol/H of H remained in methanol210.20449Kmol/h CO.
Desulfurized methanol 10030Kmol/H, 5.6Mpa, -13 ℃, 0.4281% H2、0.005032%N2、0.6775%CO、0.003505%Ar、0.005792 %CH4、26.708 %CO2、0.4296 %H2S、0.000992%COS、71.371%CH3OH、0.3699%H2Reducing the pressure of O to 1.3Mpa, and flashing off 543.0724Kmol/h flash steam: 40.99477Kmol/H H20.00000851361Kmol/h of N259.87315Kmol/h CO, 0.2940462Kmol/h Ar, 0.4347023Kmol/h CH4439.7033Kmol/h CO22.212422Kmol/H of H2S, 0.00527699Kmol/h COS, 0.4380453Kmol/h CH3OH, 0.000676451Kmol/H of H2And O. 1.94366Kmol/H of H remained in methanol28.0801Kmol/h CO.
Combining the carbon dioxide-removed flash steam and the desulfurized methanol flash steam: 1055.3227Kmol/H, 1.3MPa, -21.4 deg.C, 84.70699Kmol/H H20.000015505Kmol/h of N2124.50304Kmol/h CO, 0.6177682Kmol/h Ar, 0.9008233Kmol/h CH4841.5714Kmol/h CO22.212889Kmol/H of H2S, 0.005277Kmol/h COS, 0.8032727Kmol/h CH3OH, 0.001214323Kmol/H of H2And O. Cooling to-52 ℃, liquefying and separating out liquid: 611.7564Kmol/H, 1.26MPa, -52 ℃ and 0.5275026Kmol/H of H20.0000142124Kmol/h of N24.724741Kmol/h CO, 0.031536Kmol/h Ar, 0.0630994Kmol/h CH4604.018Kmol/h CO2、1.589226KmolH of/H2S, 0.00495008Kmol/h COS, 0.796218Kmol/h CH3OH, 0.00110411Kmol/H of H2O; flash evaporated gas phase: 443.5663Kmol/H, 1.26MPa, -52 ℃ and 84.17949Kmol/H of H20.0000012926Kmol/h of N2119.7783Kmol/h CO, 0.5862321Kmol/h Ar, 0.8377238Kmol/h CH4237.5534Kmol/h CO20.6236633Kmol/H of H2S, 0.000326923Kmol/h COS, 0.00705466Kmol/h CH3OH, 0.000110223Kmol/H of H2O。
Residual effective gas 27.88435Kmol/H, 4.8750256Kmol/H H in methanol and liquid carbon dioxide223.009321Kmol/h CO.
Example 2
(1) The rich methanol absorbing the gas in the low-temperature methanol washing process is directly subjected to reduced pressure flash evaporation to separate part of the gas, and the rich methanol subjected to reduced pressure flash evaporation is sent to a downstream process for continuous regeneration treatment;
(2) the part of the flashed gas is cooled and frozen through the first heat exchanger and the second heat exchanger to liquefy part of carbon dioxide, the cooled and frozen flash steam is flashed and separated in the second gas-liquid separation tank to obtain flash steam, and the flash steam is sent to a compressor to be pressurized for reuse;
(3) and liquid carbon dioxide separated by flash evaporation in the second gas-liquid separation tank is evaporated and gasified into gas carbon dioxide through the second heat exchanger and then is sent to a downstream process for treatment, and residual foul solution after flash evaporation in the second heat exchanger is sent to the downstream process for treatment.
The rich methanol comprises methanol after carbon dioxide removal and methanol after desulfurization.
The temperature of the methanol is-18 ℃ and the pressure of the methanol is 5Mpa in the process of removing carbon dioxide, and the methanol gas comprises CH with the molar content of 72 percent3OH, 28 mol% CO20.7 mol% CO and 0.55 mol% H20.3610% molar content of H2O; reducing the pressure to 1.2MPa in the flash evaporation process, wherein the flash evaporation gas contains 8 percent of H in molar content after flash evaporation 212% by mole of CO and 75% by mole of CO2Molar content of 0.1%CH40.1% by mole of CH3OH。
In the process of methanol desulfurization, the temperature is-18 ℃, the pressure is 6Mpa, and the methanol gas comprises CH with the molar content of 71.371%3OH, 26.708% by mol CO20.6775% CO by mol, 0.4281% H by mol20.4296% molar content of H2S, H with a molar content of 0.3699%2O; reducing the pressure to 1.2MPa in the flash evaporation process, wherein the flash evaporation gas contains H with the molar content of 6.5 percent after flash evaporation211.5% by mole of CO and 80% by mole of CO20.3% H by mole2S, mole content of 0.1% CH3OH。
Cooling the flash steam to 53 ℃, liquefying and separating carbon dioxide liquid at the pressure of 1.2MPa, wherein the carbon dioxide liquid comprises 98.5 percent of CO in molar content20.72% CO by mol, 0.25% H by mol2S, 0.15% CH by mole3OH。
The temperature of the carbon dioxide gas gasified by the heat exchanger is 52 ℃, the pressure is 1.2MPa, and the carbon dioxide gas comprises 54 percent of CO in molar content227.2% CO by mol, 0.15% H by mol2S。
Example 3
An apparatus for recovering effective gas in a low-temperature methanol washing process, comprising: v1: first gas-liquid separation tank, V2: second gas-liquid separation tank, E1: heat exchanger one, E2: heat exchanger two, L1: level control valve one, L2: liquid level control valve two, L3: level control valve three, P1: pressure control valve one, P2: and a second pressure control valve.
A pipeline of the rich methanol (01) is connected with a gas-liquid separation tank V1, and a pipeline of the flash evaporation gas (02) is connected with a first heat exchanger E1;
the pipeline of the rich methanol (03) is connected with a liquid level control valve L1 and then is connected with a rich methanol storage tank;
a pipeline of flash steam (05) is connected with a heat exchanger E1, a pipeline of flash steam (06) is connected with a gas-liquid separation tank V2, a pipeline of flash steam (07) is connected with a pressure control valve P1, and a pipeline of flash steam (08) is connected with a flash steam storage tank;
the pipeline of the liquid carbon dioxide (09) is connected with a liquid level control valve L2, the pipeline of the liquid carbon dioxide (10) is connected with a heat exchanger E2, the pipeline of the gas carbon dioxide (11) is connected with a pressure control valve P2, and the pipeline of the gas carbon dioxide (12) is connected with a carbon dioxide storage tank;
the pipeline of residual dirty liquid (13) of the heat exchanger E2 is connected with a liquid level control valve L3, and the pipeline of dirty liquid (14) is connected to a dirty liquid storage tank.
Wherein the heat exchanger E2 is provided with a blowdown conduit (13).
Claims (4)
1. The method for recovering the effective gas in the low-temperature methanol washing process is characterized by comprising the following steps of:
(1) the rich methanol absorbing the gas in the low-temperature methanol washing process is directly subjected to reduced pressure flash evaporation to separate part of the gas, and the rich methanol subjected to reduced pressure flash evaporation is sent to a downstream process for continuous regeneration treatment, wherein the rich methanol comprises methanol subjected to carbon dioxide removal and methanol subjected to desulfurization;
in the process of removing carbon dioxide, the temperature of methanol is minus 20 to minus 12 ℃, the pressure is 5 to 7Mpa, and the methanol gas comprises CH with the molar content of 68 to 75 percent3OH, CO in a molar content of 22-28%20.5-1.0% of CO and 0.2-0.6% of H20.3610% molar content of H2O; reducing the pressure to 1.0-1.5MPa in the flash evaporation process, wherein the flash evaporation steam contains H with the molar content of 7-10 percent after flash evaporation210-15% of CO by mol content and 70-80% of CO by mol content20.05-0.1% of CH by mole40.05-0.1% of CH by mole3OH；
In the process of methanol desulfurization, the temperature is minus 20 ℃ to minus 12 ℃, the pressure is 5MPa to 7MPa, and the methanol gas contains 71.371 percent of CH3OH, 26.708% by mol CO20.6775% CO by mol, 0.4281% H by mol20.4296% molar content of H2S, H with a molar content of 0.3699%2O; reducing the pressure to 1.0-1.5MPa in the flash evaporation process, wherein the flash evaporation steam contains the molar content of5-10% H210-15% of CO by mol content and 75-85% of CO by mol content20.1-0.6% of H in molar content2S, the molar content of CH is 0.05-0.1%3OH；
(2) Part of the flashed gas is cooled and frozen through a heat exchanger I and a heat exchanger II to liquefy part of carbon dioxide, the cooled and frozen flash steam is flashed and separated in a gas-liquid separation tank II, the flash steam is sent to a compressor to be pressurized and reused, the flash steam is cooled to minus 50 ℃ to minus 55 ℃ and the pressure is 1.0 MPa to 1.3MPa to liquefy and separate carbon dioxide liquid, and the carbon dioxide liquid comprises 97 percent to 99 percent of CO in molar content20.5-0.8% of CO and 0.2-0.3% of H2S, 0.05-0.15% of CH with molar content3OH；
(3) Liquid carbon dioxide separated by flash evaporation in the gas-liquid separation tank II is evaporated and gasified into gas carbon dioxide through the heat exchanger II and then is sent to a downstream process for treatment, and residual foul solution after flash evaporation in the heat exchanger II is sent to the downstream process for treatment;
in the process of the method for recovering the effective gas in the low-temperature methanol washing process, a methanol-rich pipeline is connected with a first gas-liquid separation tank (V1), the first gas-liquid separation tank (V1) is connected with a second heat exchanger (E2) through the first heat exchanger (E1), the second heat exchanger (E2) is connected with a second gas-liquid separation tank (V2), the second gas-liquid separation tank (V2) is connected with a flash vapor tank, the second gas-liquid separation tank (V2) is connected with the second heat exchanger (E2), and the second heat exchanger (E2) is connected with a carbon dioxide storage tank.
2. The method for recovering the working gas in the low-temperature methanol washing process as claimed in claim 1, wherein the second heat exchanger (E2) is connected to a waste liquid storage tank through a pipeline.
3. The method for recovering working gas in a low-temperature methanol washing process as claimed in claim 1, wherein the bottom of the first gas-liquid separation tank (V1) is connected to a methanol-rich storage tank through a pipeline.
4. The method for recovering working gas in a low-temperature methanol washing process as claimed in claim 1, wherein in the step (3), heat exchange is carried outThe temperature and pressure of the carbon dioxide gas gasified in the secondary gasifier are 50-55 ℃ and 1.0-1.3MPa, and the carbon dioxide gas contains 50-55% of CO by mole content225-28% of CO and 0.1-0.2% of H2S。
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| CN106000000B (en) * | 2016-06-29 | 2019-03-08 | 中山大学 | A kind of the multistage flash distillation parsing separator and method of synthesis ammonia decarburization absorption tower bottom rich solution |
| CN207662249U (en) * | 2017-11-13 | 2018-07-27 | 中国石油化工股份有限公司 | A kind of strange low-temp methanol in Shandong washes low temperature cold recovery system |
| CN109321285B (en) * | 2018-10-31 | 2020-10-09 | 崔静思 | Energy-saving low-temperature methanol washing device and method |
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