CN102489119A - Low-temperature methanol washing and CO2 capture combined method - Google Patents

Low-temperature methanol washing and CO2 capture combined method Download PDF

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Publication number
CN102489119A
CN102489119A CN201110382640XA CN201110382640A CN102489119A CN 102489119 A CN102489119 A CN 102489119A CN 201110382640X A CN201110382640X A CN 201110382640XA CN 201110382640 A CN201110382640 A CN 201110382640A CN 102489119 A CN102489119 A CN 102489119A
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China
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gas
rich
low
tail gas
capture
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步学朋
陈强
朱豫飞
索娅
张琪
张翠清
刘潇
王涛
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China Shenhua Coal to Liquid Chemical Co Ltd
Shenhua Group Corp Ltd
Beijing Engineering Branch of China Shenhua Coal to Liquid Chemical Co Ltd
Beijing Research Institute of China Shenhua Coal To Liquid Chemical Co Ltd
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China Shenhua Coal to Liquid Chemical Co Ltd
Shenhua Group Corp Ltd
Beijing Research Institute of China Shenhua Coal To Liquid Chemical Co Ltd
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Priority to CN201110382640XA priority Critical patent/CN102489119A/en
Publication of CN102489119A publication Critical patent/CN102489119A/en
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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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • 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
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • 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

Abstract

The invention discloses a low-temperature methanol washing and CO2 capture combined method. The low-temperature methanol washing and CO2 capture combined method comprises the following steps of 1, absorbing gas, 2, desorbing the gas, 3, regenerating methanol, and 4, feeding CO2-rich tail gas into a CO2 capture device and carrying out CO2 capture and purification, or 4, carrying out part cold energy recovery of CO2-rich tail gas, then feeding the treated CO2-rich tail gas into the CO2 capture device and carrying out CO2 capture and purification. Through the low-temperature methanol washing and CO2 capture combined method, cold energy of CO2 tail gas is fully and effectively utilized; the defect that based on the prior art, tail gas discharged by a gas absorption device conducts all cold energy to other gas, enters into the CO2 capture device and then absorbs more cold energy in CO2 capture is overcome; cold energy needed by a liquefaction process in the whole CO2 capture is reduced; a process flow is shorten; CO2 capture efficiency is improved; and energy-saving effects are realized.

Description

Low-temperature rectisol and CO 2Capture coupling process
Technical field
The present invention relates to gas purification and reclaim the field, in particular to a kind of low-temperature rectisol and CO 2Capture coupling process.
Background technology
The process of utilizing of fossil energy can give off a large amount of greenhouse gases CO 2, this is one of principal element that causes global warming.Therefore, reduce CO 2Discharging just becomes the common recognition in the whole world.The country that China is is main energy sources with this high-carbon fossil fuel of coal, the clean and effective low-carbon (LC) trans-utilization of coal is imperative, and coal system oiling worker is one of main approach.As with CO 2Capture and seal up for safekeeping (Carbon Capture and Storage is called for short CCS) technology, CO 2Utilization technology (Utilization) combine with modern coal system oiling worker, just will realize the low carbonization utilization of coal resources truly.
Realize CO 2Seal up for safekeeping and utilize CO 2Capture is one of most important link.Direct burning of coal at present as generating or Industrial Boiler discharged flue gas are maximum CO 2Emission source, but CO in the general flue gas 2Content has only 4%-15%, and has plurality of impurities in the flue gas, so CO 2The capture cost very high.
In the acid gas removal workshop section of coal gasification synthetic gas production process, can discharge the high concentration CO that is rich in of some 2Tail gas, comparatively speaking, these high concentration COs 2The capture cost will be low many, therefore can be used as CO 2The important carbon source of capture, utilizing and sealing up for safekeeping (Carbon Capture, Utilization and Storage is called for short CCUS).
The low-temperature rectisol technology is widely used in the modern coal system oiling worker process dedusting cooling desulfurization and decarburization of crude synthesis gas afterwards with characteristics such as its technology maturation, degree of purification are high, operating cost is low.Through appropriate design, in low-temperature rectisol workshop section, nearly half the CO has an appointment 2Can be to contain CO 2Concentration is discharged greater than 98% mode; CO in the remainder discharging tail gas 2Concentration is roughly 70%-90%, and this part tail gas is except CO 2Mainly comprise N outward, 2And small amount of H 2, CO, sulfide, H 2O and Trace Methanol etc.In the prior art, the part low-temp methanol washing process is also arranged because of not establishing CO 2So the product tower is all CO of discharging 2CO in the tail gas 2Content all is lower than 90%.Yet CCUS empirical analysis both at home and abroad shows CO 2The CO that seals up for safekeeping and need when utilizing 2Concentration generally is greater than 95%, and what have is greater than 99.9% like food-grade, therefore that part of concentration is lower than 90% CO 2, need to increase extra technology and carry out CO 2Capture and purify.
At present, low-temp methanol washing process roughly comprises H in the crude synthesis gas 2S and CO 2Absorbing and removing, H Deng sour gas 2S and CO 2Stage such as desorb, Mathanol regenerating.Be illustrated in figure 1 as a kind of typical low-temperature rectisol part technology of the prior art and CO 2Capture the schematic flow sheet of technology; Come autopneumatolysis workshop section dedusting, remove synthesis gas behind the ammonia and spray into small amount of methanol earlier and absorb the cold cooling through first heat exchanger 61 ' again and isolate contained small amount of methanol and water subsequently; Synthesis gas gets into methanol wash tower 10 ', through removing contained H successively with the low-temp methanol counter current contacting 2S and CO 2Deng sour gas.Purified gas is discharged from cat head and after reclaiming cold, is got into follow-up workshop section; Absorbed CO 2Methyl alcohol after second heat exchanger 62 ' absorbs cold cooling and follow-up step-down flash distillation, get into H 2S concentration tower 20 ', another road has absorbed H 2The methyl alcohol of S gets into H after the 3rd heat exchanger 63 ' absorbs cold cooling and follow-up step-down flash distillation 2 S concentration tower 20 '.Be rich in H 2The methyl alcohol of S is discharged at the bottom of by tower, through the 4th heat exchanger 64 ' heat temperature raising after, gets into Mathanol regenerating device 30 ' and carries out sulphur removal dehydration regeneration, the methanol loop use after the regeneration.And by H 2S concentration tower 20 ' top discharge goes out high concentration CO 2Tail gas discharges through second heat exchanger 62 ' and first heat exchanger 61 ' and gets into gas compressor 40 ', liquefaction separator 50 ' successively after whole colds and heat absorption reach normal temperature, finally obtains CO 2Content is greater than 95% gas and be used for CO 2Seal up for safekeeping or utilize.
See H from above-mentioned technological process 2The CO of S concentration tower 20 ' discharging 2Exhaust temperature is generally about-40 ℃, after repeatedly reclaiming cold, reaches about 20 ℃ of normal temperature.As only consider from the low-temperature rectisol process, reclaim CO undoubtedly 2The contained cold of tail gas is rational; But as the follow-up CO of consideration 2Capture carry densely, subsequent process also need be reuptaked cold again and reduce temperature so that CO 2Liquefaction, so shortcoming such as there is long flow path in this technology, and energy resource consumption is many.
Summary of the invention
The present invention is providing a kind of low-temperature rectisol and CO 2Capture coupling process, to solve low-temperature rectisol and CO in the prior art 2The capture technological process is long, the technical problem that energy resource consumption is many.
To achieve these goals, according to an aspect of the present invention, a kind of low-temperature rectisol and CO are provided 2Capture coupling process, in turn include the following steps: the GAS ABSORPTION step with dedusting, remove the synthesis gas cooling behind the ammonia and be delivered to gas absorbing device, contacts to remove contained sour gas it with low-temp methanol; The gas desorption step is delivered to the gas desorption device with the low-temp methanol that removes behind the sour gas, isolates and is rich in CO 2Tail gas and be rich in H 2The low-temp methanol of S; The Mathanol regenerating step will be rich in H 2The low-temp methanol of S is delivered to the Mathanol regenerating device and carries out methyl alcohol sulphur removal dehydration regeneration; To be rich in CO 2Tail gas be delivered to CO 2Capturing device is to carry out CO 2Capture in the step of purifying, be rich in CO 2Tail gas directly be delivered to CO 2Capturing device is to carry out CO 2Capture and purify; Or be rich in CO 2Tail gas carry out being delivered to CO after the part cold recovery 2Capturing device is to carry out CO 2Capture and purify.
Further, the gas desorption device is H 2The S concentration tower.
Further, be rich in CO 2Tail gas from H 2The exhaust outlet at S concentration tower top gets into gas compressor and CO after discharging successively 2The liquefaction separator is to carry out CO 2Purifying concentrates.
Further, the gas desorption device comprises CO 2Product tower and H 2The S concentration tower.
Further, from the CO that is rich in of gas absorbing device 2Low-temp methanol after the heat exchange decrease temperature and pressure, get into CO 2The product tower is from the H that is rich in of gas absorbing device 2The low-temp methanol of S gets into H after the heat exchange decrease temperature and pressure 2The S concentration tower.
Further, from CO 2The low-temp methanol decompression back that the product tower is discharged gets into H 2The S concentration tower.
Further, be rich in CO 2Tail gas comprise CO 2Product tower tail gas and H 2S concentration tower tail gas, CO 2Product tower tail gas gets into first gas compressor and CO successively 2Liquefying plant carries out CO 2Liquefaction concentrates, H 2S concentration tower tail gas gets into second gas compressor and CO successively 2The liquefaction separator carries out CO 2Purifying concentrates.
Further, CO is rich in control 2The temperature of tail gas is-20～-50 ℃.
Further, gas compressor will be rich in CO 2Tail gas be forced into 2.0～8.0MPa.
Further, gas absorbing device is the absorption tower.
Use low-temperature rectisol of the present invention and CO 2Capture coupling process, will be rich in CO 2Tail gas directly be delivered to CO 2Capturing device is to carry out CO 2Capture and purify; Maybe will be rich in CO 2Tail gas carry out being delivered to CO after the part cold recovery 2Capturing device is to carry out CO 2Capture and purify, make CO 2The contained cold of tail gas obtains fully effectively utilizing, and having overcome the tail gas that the gas desorption device is discharged in the prior art will pass to other gas with whole colds earlier, and gets into CO 2Capturing device carries out CO 2Capture the shortcoming that to reuptake more colds when purifying again, thereby reduce whole C O 2Liquefaction step institute chilling requirement has not only shortened technological process in the capture, has improved CO 2The efficient that captures, and reached energy-conservation effect.
Description of drawings
Figure of description is used to provide further understanding of the present invention, constitutes a part of the present invention, and illustrative examples of the present invention and explanation thereof are used to explain the present invention, does not constitute improper qualification of the present invention.In the accompanying drawings:
Fig. 1 shows according to the low-temperature rectisol of prior art and CO 2Capture the sketch map of coupling process;
Fig. 2 shows according to the low-temperature rectisol of the embodiment of the invention and CO 2Capture the sketch map of coupling process;
Fig. 3 shows low-temperature rectisol and CO according to another embodiment of the present invention 2Capture the sketch map of coupling process; And
Fig. 4 shows low-temperature rectisol and CO according to yet another embodiment of the invention 2Capture the sketch map of coupling process.
The specific embodiment
Need to prove that under the situation of not conflicting, embodiment and the characteristic among the embodiment among the present invention can make up each other.Below with reference to accompanying drawing and combine embodiment to specify the present invention.
According to a kind of typical embodiment of the present invention, low-temperature rectisol and CO 2Capture coupling process, in turn include the following steps: the GAS ABSORPTION step with dedusting, remove the synthesis gas cooling behind the ammonia and be delivered to gas absorbing device, contacts to remove contained sour gas it with low-temp methanol; The gas desorption step is delivered to the gas desorption device with the low-temp methanol that removes behind the sour gas, isolates and is rich in CO 2Tail gas and be rich in H 2The low-temp methanol of S; The Mathanol regenerating step will be rich in H 2The low-temp methanol of S is delivered to the Mathanol regenerating device and carries out Mathanol regenerating; To be rich in CO 2Tail gas be delivered to CO 2Capturing device is to carry out CO 2Capture in the step of purifying, be rich in CO 2Tail gas directly be delivered to CO 2Capturing device is to carry out CO 2Capture and purify; Or be rich in CO 2Tail gas carry out being delivered to CO after the part cold recovery 2Capturing device is to carry out CO 2Capture and purify.Make CO 2The contained cold of tail gas obtains fully effectively utilizing, and having overcome the tail gas that the gas desorption device is discharged in the prior art will pass to other gas with whole colds earlier, and gets into CO 2Capturing device carries out CO 2Capture the shortcoming that to reuptake more colds when purifying again, thereby reduce whole C O 2Liquefaction step institute chilling requirement has not only shortened technological process in the capture, has improved CO 2The efficient that captures, and reached energy-conservation effect.
According to a kind of typical embodiment of the present invention, the gas desorption device is H 2The S concentration tower is at H 2The S concentration tower is through decompressional expansion and N 2The effect that gas is carried will be rich in CO 2And H 2The low-temp methanol of S carries out the selectivity desorb, isolates to be rich in CO 2Tail gas and be rich in H 2The low-temp methanol of S.Preferably, be rich in CO 2Tail gas from H 2S concentration tower top vent gets into gas compressor and CO after discharging successively 2The liquefaction separator carries out CO 2Purifying concentrates.
According to a kind of typical embodiment of the present invention, the gas desorption device is H 2The S concentration tower is at H 2The S concentration tower is through decompressional expansion and N 2The effect that gas is carried is rich in CO in inciting somebody to action 2And H 2The low-temp methanol of S carries out the selectivity desorb, isolates to be rich in CO 2Tail gas and be rich in H 2The low-temp methanol of S.Preferably, be rich in CO 2Tail gas from H 2S concentration tower top vent gets into first-class heat exchanger, gas compressor and CO after discharging successively 2The liquefaction separator carries out CO 2Purifying concentrates.
According to a kind of typical embodiment of the present invention, the gas desorption device comprises CO 2Product tower and H 2The S concentration tower is from the CO that is rich in of gas absorbing device 2Low-temp methanol after the heat exchange decrease temperature and pressure, get into CO 2The product tower is from the H that is rich in of gas absorbing device 2The low-temp methanol of S gets into H after the heat exchange decrease temperature and pressure 2The S concentration tower.That wherein, discharges from gas absorbing device middle part is rich in CO 2The most of CO that gets into of low-temp methanol 2Product tower depressurization desorption and heating, CO in the tail gas of discharge 2Concentration＞98% gets into gas compressor and CO successively 2Liquefying plant carries out CO 2Liquefaction can obtain high concentration CO 2The H that is rich in from the discharge of gas absorbing device bottom 2The methyl alcohol of S and CO 2The low-temp methanol that the product tower bottom is discharged gets into H 2The further depressurization desorption of S concentration tower separates, and discharge at the top is rich in CO 2Tail gas gets into gas compressor and CO successively 2The liquefaction separator carries out CO 2Liquefaction separates the back and obtains high concentration CO 2Preferably, from CO 2The low-temp methanol decompression back that the product tower is discharged gets into H 2The S concentration tower, and discharge from absorption tower bottom be rich in H 2The methyl alcohol of S reduces pressure after heat exchanger absorbs cold and flash distillation again and gets into H 2The S concentration tower is from the CO that is rich in of gas absorbing device middle part discharge 2Low-temp methanol partly get into H 2S concentration tower top, at this tower with the CO in the methyl alcohol 2Parse, concentrate the H that improves methyl alcohol simultaneously 2S concentration is to improve follow-up H 2The S gas concentration.Preferably, gas compressor will be rich in CO 2Tail gas be forced into 2.0～8.0MPa, be beneficial to CO 2Liquefaction and conveying.
According to a kind of typical embodiment of the present invention, gas absorbing device is the absorption tower.
To combine embodiment to specify beneficial effect of the present invention below.
Embodiment 1
Adopt low-temperature rectisol of the present invention and CO 2Capture coupling process the dedusting that comes autopneumatolysis workshop section, the synthesis gas that removes behind the ammonia are carried out low-temperature rectisol and CO 2Capture and purify.As shown in Figure 2, low-temperature rectisol and CO 2The coupled system that captures comprises low temperature washing device for methanol and CO 2Capturing device, low temperature washing device for methanol comprise methanol wash tower 10, the H that is communicated with successively 2 S concentration tower 20 and Mathanol regenerating device 30, scrubbing tower 10, H 2The arrival end of S concentration tower 20 and Mathanol regenerating device 30 is respectively arranged with first heat exchanger, 61, the second heat exchangers 62 and the 3rd heat exchanger 63, the four heat exchangers 64.CO 2Capturing device comprises gas compressor 40 and is attached thereto logical CO 2Liquefaction separator 50, H 2The gas outlet end of S concentration tower 20 is connected with the arrival end of gas compressor 40.
Dedusting, remove synthesis gas behind the ammonia and absorb outside cold cooling through first heat exchanger 61 and dewater, get into methanol wash tower 10, synthesis gas is through removing contained H with the low-temp methanol counter current contacting 2S and CO 2Deng sour gas.Purified gas is discharged from cat head and after reclaiming cold, is got into follow-up workshop section; Absorbed CO 2And H 2The methyl alcohol of S gets into H respectively respectively after second heat exchanger 62 and outside cold cooling of the 3rd heat exchanger 63 absorptions and step-down flash distillation 2 S concentration tower 20 is proposed desorb with CO at this methyl alcohol expansion gas 2Separate out, concentrate H simultaneously 2S.Be rich in H 2The methyl alcohol of S is discharged at the bottom of by tower, gets into Mathanol regenerating device 30 and carries out the sulphur removal dehydration and regenerate the methanol loop use after the regeneration through the 4th heat exchanger 64 heat exchange back of heating up.And by H 2It is-20～-50 ℃ high concentration CO that S concentration tower 20 top discharges go out temperature 2Tail gas gets into gas compressor 40 successively and boosts to 2.0～8.0MPa, a small amount of cold liquefaction of liquefaction separator 50 absorptions purification, finally obtains CO 2Content is greater than 95% liquid and be used for CO 2Seal up for safekeeping or utilize.
Embodiment 2
As shown in Figure 3, low-temperature rectisol and CO 2The coupled system that captures comprises low temperature washing device for methanol and CO 2Capturing device, low temperature washing device for methanol comprise scrubbing tower 10, the CO that is communicated with successively 2 Product tower 70, H 2 S concentration tower 20 and Mathanol regenerating device 30, scrubbing tower 10, CO 2Product tower 70, H 2The arrival end of S concentration tower 20 and Mathanol regenerating device 30 is respectively arranged with first heat exchanger, 61, the second heat exchangers 62 and the 3rd heat exchanger 63, the four heat exchangers 64.CO 2Capturing device comprises a CO 2Capturing device and the 2nd CO 2Capturing device, wherein a CO 2Capturing device comprises first gas compressor 41 and is attached thereto logical CO 2Liquefying plant 80, the first gas compressor 41 and CO 2The gas outlet end of product tower 70 is connected; The 2nd CO 2Capturing device comprises second gas compressor 42 and is attached thereto logical CO 2Liquefaction separator 50, the second gas compressor 42 and H 2The gas outlet end of S concentration tower 20 is connected.
Dedusting, remove synthesis gas behind the ammonia and absorb outside cold cooling through first heat exchanger 61 and dewater, get into scrubbing tower 10, synthesis gas is through removing contained H with the low-temp methanol counter current contacting 2S and CO 2Deng sour gas.Purified gas is discharged from cat head and after reclaiming cold, is got into follow-up workshop section; The CO that is rich in from the discharge of gas absorbing device middle part 2Low-temp methanol most of CO of entering after second heat exchanger 62 absorbs colds cooling and step-down flash distillation subsequently 2 Product tower 70 depressurization desorptions, few part gets into H 2 S concentration tower 20 tops, CO 2High concentration CO is discharged at product tower 70 tops 2Tail gas.The H that is rich in from the discharge of gas absorbing device bottom 2The methyl alcohol of S reaches CO after the 3rd heat exchanger 63 absorbs cold cooling and step-down flash distillation subsequently 2The low-temp methanol that the product tower bottom is discharged gets into H respectively 2 S concentration tower 20 further depressurization desorptions separate, and are rich in H 2The methyl alcohol of S is by H 2Discharge S concentration tower 20 bottoms, after 64 heat exchange of the 4th heat exchanger heat up, gets into Mathanol regenerating device 30 and carry out sulphur removal dehydration regeneration, and the methanol loop after the regeneration is used.By CO 2It is-20～-50 ℃ high concentration CO that product tower 70 top discharges go out temperature 2Tail gas gets into a CO 2Capturing device promptly boosts to 2.0～8.0MPa through first gas compressor 41 successively and is attached thereto the liquefying plant 80 of the logical a small amount of cold of absorption.Because from CO 2The tail gas CO of product tower 70 2Concentration＞98% then liquefies after compression again and can obtain high concentration CO 2Liquid, and need not separate.And by H 2It is-20～-50 ℃ high concentration CO that S concentration tower 20 top discharges go out temperature 2Tail gas gets into the 2nd CO 2Capturing device promptly gets into gas compressor 40 successively and boosts to 2.0～8.0MPa and a small amount of cold liquefaction of liquefaction separator 50 absorptions purification, finally obtains CO 2Content is greater than 95% liquid and be used for CO 2Seal up for safekeeping or utilize.
Embodiment 3
Adopt low-temperature rectisol of the present invention and CO 2Capture coupling process the dedusting that comes autopneumatolysis workshop section, the synthesis gas that removes behind the ammonia are carried out low-temperature rectisol and CO 2Capture and purify.As shown in Figure 4, low-temperature rectisol and CO 2The coupled system that captures comprises low temperature washing device for methanol and CO 2Capturing device, low temperature washing device for methanol comprise methanol wash tower 10, the H that is communicated with successively 2 S concentration tower 20 and Mathanol regenerating device 30, scrubbing tower 10, H 2The arrival end of S concentration tower 20 and Mathanol regenerating device 30 is respectively arranged with first heat exchanger 61, second heat exchanger 62, the 3rd heat exchanger 63 and the 4th heat exchanger 64.CO 2Capturing device comprises gas compressor 40 and is attached thereto logical CO 2Liquefaction separator 50, H 2The gas outlet end of S concentration tower 20 is connected with the arrival end of gas compressor 40.
Dedusting, remove synthesis gas behind the ammonia and absorb outside cold cooling through first heat exchanger 61 and dewater, get into methanol wash tower 10, synthesis gas is through removing contained H with the low-temp methanol counter current contacting 2S and CO 2Deng sour gas.Purified gas is discharged from cat head and after reclaiming cold, is got into follow-up workshop section; Absorbed CO 2And H 2The methyl alcohol of S gets into H respectively respectively after second heat exchanger 62 and outside cold cooling of the 3rd heat exchanger 63 absorptions and step-down flash distillation 2 S concentration tower 20 is proposed desorb with CO at this methyl alcohol expansion gas 2Separate out, concentrate H simultaneously 2S.Be rich in H 2The methyl alcohol of S is discharged at the bottom of by tower, gets into Mathanol regenerating device 30 and carries out the sulphur removal dehydration and regenerate the methanol loop use after the regeneration through the 4th heat exchanger 64 heat exchange back of heating up.And by H 2It is-40～-50 ℃ high concentration CO that S concentration tower 20 top discharges go out temperature 2Tail gas is introduced into second heat exchanger 62 temperature is increased to-20 ℃ approximately, gets into gas compressor 40 then successively and boosts to 2.0～8.0MPa, some colds liquefaction purifications of liquefaction separator 50 absorptions, finally obtains CO 2Content is greater than 95% liquid and be used for CO 2Seal up for safekeeping or utilize.
This embodiment compares with example 1, owing to get into the CO of compressor 2Temperature increases, and can reduce equipment investment relatively.
To sum up, low-temperature rectisol of the present invention and CO 2Capture coupling process, have the following advantages:
(1) CO that utilizes the low-temperature rectisol row of cells to emit 2Contained cold, thus follow-up CO reduced 2Liquefaction institute chilling requirement reaches the whole system purpose of energy saving;
(2) owing to be rich in CO 2Tail gas discharge directly entering CO of back from the gas desorption device 2Capturing device carries out CO 2Capture, make CO 2The contained cold of tail gas obtains fully effectively utilizing, and having overcome the tail gas that the gas desorption device is discharged in the prior art will pass to other gas with whole colds earlier, and gets into CO 2Capturing device carries out CO 2Capture the shortcoming that to reuptake more colds when purifying again, thereby reduce whole C O 2Liquefaction step institute chilling requirement in the capture, technology are optimized more and are compact, practice thrift to take up an area of and the reduction investment;
(3) process scale is regulated flexibly.
The above is merely the preferred embodiments of the present invention, is not limited to the present invention, and for a person skilled in the art, the present invention can have various changes and variation.All within spirit of the present invention and principle, any modification of being done, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.

Claims (10)

1. low-temperature rectisol and CO 2Capture coupling process, in turn include the following steps:
The GAS ABSORPTION step with dedusting, remove the synthesis gas cooling behind the ammonia and be delivered to gas absorbing device, contacts to remove contained sour gas it with low-temp methanol;
The gas desorption step is delivered to the gas desorption device with the said low-temp methanol that removes behind the sour gas, isolates and is rich in CO 2Tail gas and be rich in H 2The low-temp methanol of S;
The Mathanol regenerating step is with the said H that is rich in 2The low-temp methanol of S is delivered to the Mathanol regenerating device and carries out Mathanol regenerating;
It is characterized in that, with the said CO that is rich in 2Tail gas be delivered to CO 2Capturing device is to carry out CO 2Capture in the step of purifying the said CO that is rich in 2Tail gas directly be delivered to CO 2Capturing device, or the said CO that is rich in 2Tail gas carry out being delivered to CO after the part cold recovery 2Capturing device.
2. method according to claim 1 is characterized in that, said gas desorption device is H 2S concentration tower (20).
3. method according to claim 2 is characterized in that, the said CO that is rich in 2Tail gas from said H 2The exhaust outlet at S concentration tower (20) top gets into gas compressor (40) and CO after discharging successively 2Liquefaction separator (50) is to carry out CO 2Purifying concentrates.
4. method according to claim 1 is characterized in that, said gas desorption device comprises CO 2Product tower (70) and H 2S concentration tower (20).
5. method according to claim 4 is characterized in that, from the CO that is rich in of said gas absorbing device 2Low-temp methanol after the heat exchange decrease temperature and pressure, get into said CO 2Product tower (70) is from the H that is rich in of said gas absorbing device 2The low-temp methanol of S gets into said H after the heat exchange decrease temperature and pressure 2S concentration tower (20).
6. method according to claim 5 is characterized in that, from said CO 2The low-temp methanol decompression back that product tower (70) is discharged gets into said H 2S concentration tower (20).
7. method according to claim 4 is characterized in that, the said CO that is rich in 2Tail gas comprise CO 2Product tower tail gas and H 2S concentration tower tail gas, said CO 2Product tower tail gas gets into first gas compressor (41) and CO successively 2Liquefying plant (80) carries out CO 2Liquefaction concentrates, said H 2S concentration tower tail gas gets into second gas compressor (42) and CO successively 2Liquefaction separator (50) carries out CO 2Purifying concentrates.
8. method according to claim 1 is characterized in that, controls the said CO that is rich in 2The temperature of tail gas is-20～-50 ℃.
9. according to claim 3 or 7 described methods, it is characterized in that said gas compressor is with the said CO that is rich in 2Tail gas be forced into 2.0～8.0MPa.
10. method according to claim 1 is characterized in that, said gas absorbing device is absorption tower (10).
CN201110382640XA 2011-11-25 2011-11-25 Low-temperature methanol washing and CO2 capture combined method Pending CN102489119A (en)

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CN102952589A (en) * 2012-10-25 2013-03-06 李红凯 Method for removing acid gas out of raw gas or shifted gas of raw gas
CN103320176A (en) * 2013-06-20 2013-09-25 华南理工大学 Low temperature methanol washing method and device with high CO2 yield
CN103756734A (en) * 2014-01-16 2014-04-30 中石化宁波工程有限公司 Energy-saving low-temperature methanol-washing H2S concentration process
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CN107355680A (en) * 2017-07-19 2017-11-17 陕西延长石油(集团)有限责任公司研究院 A kind of CO2Trapping, conveying, using with sealing full-flow process up for safekeeping
CN107754558A (en) * 2016-08-19 2018-03-06 中国石油化工股份有限公司 A kind of NHD desulfurization concentrating method
CN105664671B (en) * 2016-03-17 2018-06-29 中石化南京工程有限公司 A kind of zero carbon emission technique gas purifying method and device
CN109954376A (en) * 2017-12-22 2019-07-02 乔治洛德方法研究和开发液化空气有限公司 For cleaning absorption tower and the method for crude synthesis gas
CN113293034A (en) * 2021-04-30 2021-08-24 南京工业大学 Green, environment-friendly and high-CO2Low temperature methanol wash process for yield
CN114963692A (en) * 2022-05-25 2022-08-30 崔静思 Low-energy-consumption carbon dioxide capturing device and method based on low-temperature methanol washing process

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CN102952589A (en) * 2012-10-25 2013-03-06 李红凯 Method for removing acid gas out of raw gas or shifted gas of raw gas
CN103320176A (en) * 2013-06-20 2013-09-25 华南理工大学 Low temperature methanol washing method and device with high CO2 yield
CN104340979A (en) * 2013-08-09 2015-02-11 陕西延长石油榆林煤化有限公司 Method for trapping and purifying CO2
CN103756734A (en) * 2014-01-16 2014-04-30 中石化宁波工程有限公司 Energy-saving low-temperature methanol-washing H2S concentration process
CN103756734B (en) * 2014-01-16 2015-03-04 中石化宁波工程有限公司 Energy-saving low-temperature methanol-washing H2S concentration process
CN105664671B (en) * 2016-03-17 2018-06-29 中石化南京工程有限公司 A kind of zero carbon emission technique gas purifying method and device
CN107754558A (en) * 2016-08-19 2018-03-06 中国石油化工股份有限公司 A kind of NHD desulfurization concentrating method
CN107754558B (en) * 2016-08-19 2020-10-20 中国石油化工股份有限公司 Desulfurization and concentration method of polyethylene glycol dimethyl ether
CN107355680A (en) * 2017-07-19 2017-11-17 陕西延长石油(集团)有限责任公司研究院 A kind of CO2Trapping, conveying, using with sealing full-flow process up for safekeeping
CN107355680B (en) * 2017-07-19 2019-06-04 陕西延长石油(集团)有限责任公司研究院 A kind of CO2Trapping, conveying, using with seal full-flow process up for safekeeping
CN109954376A (en) * 2017-12-22 2019-07-02 乔治洛德方法研究和开发液化空气有限公司 For cleaning absorption tower and the method for crude synthesis gas
CN109954376B (en) * 2017-12-22 2023-03-10 乔治洛德方法研究和开发液化空气有限公司 Absorption tower and method for cleaning raw synthesis gas
CN113293034A (en) * 2021-04-30 2021-08-24 南京工业大学 Green, environment-friendly and high-CO2Low temperature methanol wash process for yield
CN114963692A (en) * 2022-05-25 2022-08-30 崔静思 Low-energy-consumption carbon dioxide capturing device and method based on low-temperature methanol washing process

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