CN113731117A - Novel process for high-efficiency low-temperature methanol elution and pure recovery of carbon dioxide - Google Patents
Novel process for high-efficiency low-temperature methanol elution and pure recovery of carbon dioxide Download PDFInfo
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- CN113731117A CN113731117A CN202111054429.5A CN202111054429A CN113731117A CN 113731117 A CN113731117 A CN 113731117A CN 202111054429 A CN202111054429 A CN 202111054429A CN 113731117 A CN113731117 A CN 113731117A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 233
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000011084 recovery Methods 0.000 title claims abstract description 18
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 7
- 238000010828 elution Methods 0.000 title claims abstract description 4
- 239000007788 liquid Substances 0.000 claims abstract description 42
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 20
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 20
- 239000011593 sulfur Substances 0.000 claims abstract description 19
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 239000002253 acid Substances 0.000 claims abstract description 16
- 230000008020 evaporation Effects 0.000 claims abstract description 14
- 239000002994 raw material Substances 0.000 claims abstract description 9
- 238000005406 washing Methods 0.000 claims description 33
- 238000010521 absorption reaction Methods 0.000 claims description 16
- 238000003795 desorption Methods 0.000 claims description 13
- 238000005516 engineering process Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 238000004064 recycling Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 58
- 239000000243 solution Substances 0.000 description 19
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 230000008929 regeneration Effects 0.000 description 10
- 238000011069 regeneration method Methods 0.000 description 10
- 238000000926 separation method Methods 0.000 description 8
- 229910021529 ammonia Inorganic materials 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 7
- 238000003786 synthesis reaction Methods 0.000 description 7
- 238000001816 cooling Methods 0.000 description 5
- 239000002912 waste gas Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 238000007599 discharging Methods 0.000 description 3
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 description 2
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 235000012538 ammonium bicarbonate Nutrition 0.000 description 2
- 239000001099 ammonium carbonate Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000002151 riboflavin Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2021—Methanol
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
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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
- 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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Abstract
The invention relates to a new process for high-efficiency low-temperature methanol elution and pure recovery of carbon dioxide, which is characterized in that methanol is used for absorbing and removing the carbon dioxide, and a flash evaporation process is added after sulfur-containing rich liquid and sulfur-free rich liquid are subjected to flash evaporation at medium pressure, wherein flash evaporation gas obtained by flash evaporation of the sulfur-containing rich liquid is recycled into raw material gas, and flash evaporation gas obtained by flash evaporation of the sulfur-free rich liquid is discharged after the cold energy of the flash evaporation gas is recovered; the temperature of the rich liquid is increased in two steps by a heating flash mode through a heat exchange network to increase CO2Recovery rate; CO 22The rich liquid at the bottom of the flash tower is continuously flashed, so that CO can be further improved2The recovery rate can be increased, and the H content in the acid gas can be increased2The concentration of S. CO of the invention2Basically all the components are recycled, the energy consumption of the recycling is low, and simultaneously, the H can be improved2Method of S concentrationThe method is carried out.
Description
Technical Field
The invention relates to the field of mixed gas purification, and acid gas (CO) is absorbed and recovered by using low-temperature methanol2，H2S, COS). The method is suitable for the fields of synthesis of methanol, ammonia and the like by purifying synthesis gas.
Background
Low temperature methanol washing (Rectisol) is a physical absorption method for removing acid gas by using cold methanol as a solvent, and is an effective gas purification process developed by Linde (Linde) company and Lurgi (Lurgi) company in Germany in the 50 th century. The process is widely applied to purification processes of production devices such as ammonia synthesis plants, methanol synthesis, oxo synthesis, industrial hydrogen production, city gas and natural gas desulfurization and the like.
The low-temperature methanol washing process mainly utilizes methanol to absorb acid gas (CO) at low temperature and high pressure2，H2S, COS) and the methanol rich solution are subjected to flash evaporation, gas stripping and heating to separate acid gas, so that the aim of separation and recovery is fulfilled. Relevant patents for the recovery of acid gases are US 4050909(1997), US4324567(1982), CN1113824A (1995), CN1107382A (1995), etc. Wherein:
US4609384(1986) provides two CO related physical absorption processes2A regeneration process, the first process being the use of N at two different temperatures2Stripping of CO2Desorbing and stripping CO2All are lost. The second process flow is to realize CO by using a flash evaporation mode2Desorption, in which most of the CO is recovered by vacuum flash evaporation2And the energy consumption of the process is higher.
CN1113824A (1995) the main objective of this technology was to recover all CO2And increase H2The concentration of S. In the recovery of CO from sulfur-containing pregnant solution2When in use, the CO is firstly stripped by utilizing medium pressure gas2The sulfur-free rich solution is used for stripping CO2Absorbed and then enters CO2The desorption system can desorb and recover, so that the technical process is more complicated.
The low-temperature methanol washing process adopted in the prior art is shown as the attached figure 1:
generally speaking, the low-temperature methanol washing process is mainly divided into the following parts, namely adding water to remove ammonia (not shown in the figure), cooling and dehydrating, removing acid gas at low temperature and high pressure, recovering effective gas and H by medium-pressure flash evaporation2S gas stripping enrichment and heat regeneration H recovery2S, methanol-water separation and tail gas washing and emptying (not shown in the figure). The basic process is as follows: washing raw material gas with water to remove ammonia below 1ppm to prevent ammonia and CO2The reaction generates ammonium bicarbonate at low temperature, thereby blocking pipelines and equipment. Injecting a small amount of A into the raw material gasAlcohol to prevent freezing of water vapor in the feed in subsequent cryogenic systems. The raw material gas enters a cooler E101, and is mixed with purified gas and CO from the top of a methanol washing tower2Product gas and H2And (4) carrying out heat exchange and cooling on the waste gas at the top of the S concentration tower, and allowing the waste gas to enter a gas-liquid separator S101 to separate methanol water. The raw material gas enters a methanol washing tower D101, and H which is easier to be absorbed by methanol is arranged at the lower section of the methanol washing tower2S is first treated with CO from the upper section of the column2CO is removed to below 0.1ppm by the methanol absorbent2Is removed at the upper section of the washing tower, the absorbed methanol comes from the cooled methanol at the bottom of the thermal regeneration tower, and the methanol absorbs CO2The temperature is increased, and a certain amount of CO is absorbed2After the methanol liquid is pumped out from the tower for heat exchange and temperature reduction, the methanol liquid returns to the washing tower for continuously removing CO2. The purified gas enters a cooler from the top of the tower for heat exchange and then goes to the next synthesis section. The methanol without sulfur and the methanol containing sulfur from the middle section of absorption and the tower bottom respectively enter a flash tank S102 and a flash tank S103 to release effective gas H2CO and a portion of CO2And the gas is compressed by a recycle gas compressor and recycled into the feed gas. Continuous flash evaporation of sulfur-free rich solution to recover CO2. Two streams of methanol liquid enter H from different positions respectively2S concentration column D102, low pressure nitrogen to CO2And H2S is stripped from methanol solution, H2S is absorbed again by the sulfur-free methanol at the top of the concentration tower, and the waste gas (CO)2And N2) And (4) discharging from the tower top, entering a tail gas washing tower before emptying, and removing trace methanol in tail gas by using brine. The rich methanol solution in the middle section of the concentration tower is used as a low-temperature source of the system, exchanges heat with the barren solution and the absorption solution entering the methanol washing tower and is recycled back to the H2S. condensation column from H2Exchanging heat between the rich methanol solution and the lean solution at the bottom of the S concentration tower, and then feeding the rich methanol solution and the lean solution into a thermal regeneration tower D103 to separate H2S and residual CO2Desorbing, cooling most of the methanol at the bottom of the tower, circulating the methanol to the methanol washing tower, allowing the small part of the methanol to enter the alcohol-water separation tower D104, circulating the gaseous methanol liquid at the top of the tower back to the heat regeneration tower, discharging the wastewater from the bottom of the tower, and ensuring that the content of the methanol in the wastewater is lower than 1 wt%.
The prior art has the following defects:
existing process CO2The recovery rate is very low, and is only about 35 percent. H in acid gas2The concentration of S is lower, 10-15%.
Disclosure of Invention
The invention aims to provide a novel low-temperature methanol washing process by improvement on the basis of the existing process, so as to improve CO2The purpose of recovery rate is to increase the content of H in the acid gas2The concentration of S.
The purpose of the invention is realized by the following technical scheme:
based on CO2Different applications of the product to CO2And (3) performing further flash evaporation on the sulfur-free rich liquid and the sulfur-containing rich liquid from the medium-pressure flash tanks S102 and S103 according to different purity requirements, wherein the gas desorbed from the sulfur-free rich liquid is discharged after cold energy is recovered, and the gas desorbed from the sulfur-containing rich liquid and the gas flashed from the medium pressure are compressed and circulated back to the feed gas. CO 22The product concentration is increased. And controlling the pressure of the flash tank S104 without the sulfur-containing rich liquid to be 500-1200 kpa, and controlling the pressure of the flash tank S105 with the sulfur-containing rich liquid to be 600-1200 kpa.
From CO with rich liquid containing no sulphur2The top of the desorption tower enters a flash tower, and sulfur-containing rich liquid is separated from CO2The lower part of the desorption tower enters. Characterized by CO2The operating pressure of the desorption tower is 150-240 kpa. The methanol rich liquid which is led out from the lower part of the flash tower for the first time is further flashed to reduce the temperature of the solution so as to cool the lean liquid to-50 ℃ and absorb the methanol. The flash tank S106 is operated at a pressure of 70kpa to 150 kpa. Meanwhile, the purpose of heating the rich liquid is achieved. The rich liquid is led out from the flash tower for the second time and exchanges heat with the lean liquid at the bottom of the desorption tower to 30 ℃. The liquid from the bottom of the flash tower is flashed to normal pressure or vacuum state. The flash tank S108 is operated at a pressure of 40kpa to 150 kpa.
The invention can achieve the following effects:
(1) increase CO2And (4) recovering rate. CO of original process2The recovery was very low, about 35%. The invention realizes the temperature rise flash evaporation of the rich solution by fully utilizing heat recovery through a heat exchange network. CO of the invention2The recovery rate is improved to 90 percentLeft and right.
(2) Saving gas and lifting gas. CO of original process2The regeneration is largely by N2And (4) gas stripping is realized. The invention can recover all CO basically by heating and flash evaporation2Completely replaces the prior gas stripping flash evaporation mode, saves N2。
(3) Can increase H content in acid gas2The concentration of S. Consider H2The influence of the concentration of S on the energy consumption of the subsequent Claus sulfur recovery process (the lower the concentration, the higher the energy consumption), the invention provides the method which can improve the H content2S concentration by adjusting the operating pressure of the flash tank S1082The concentration range of S is between 15% and 33%.
Drawings
FIG. 1 shows a low-temperature methanol washing process in the prior art
Wherein D101 absorption column, D102H2S concentration tower, D103 thermal regeneration tower and D104 alcohol-water separation tower as shown in figure 2 are the low-temperature methanol washing process flow of the invention
Wherein D101 absorption column, D102 CO2The invention is further detailed by a desorption tower, a D103 thermal regeneration tower and a D104 alcohol-water separation tower in combination with the attached figure 2:
FIG. 2 shows a low temperature methanol washing process, which comprises the following steps: washing raw material gas with water to remove ammonia below 1ppm (not shown in figure) to prevent ammonia and CO2The reaction generates ammonium bicarbonate at low temperature, thereby blocking pipelines and equipment. A small amount of methanol is then injected into the feed gas to prevent freezing of water vapor in the feed in subsequent cryogenic systems. The raw material gas enters a cooler and is mixed with purified gas and CO from the top of a methanol washing tower2And (3) performing heat exchange and cooling on the product gas and the tail gas, enabling the product gas and the tail gas to enter a gas-liquid separator, separating out methanol and water, enabling the separated methanol water solution to enter a D104 alcohol-water separation tower, and recovering the methanol. The raw material gas enters a methanol washing tower, and H which is easier to be absorbed by methanol is arranged at the lower section of the methanol washing tower2S is first treated with CO from the upper section of the column2CO is removed to below 0.1ppm by the methanol absorbent2Is removed in the upper section of the washing tower, absorbs poor methanol which is cooled from the bottom of the thermal regeneration tower and divides the decarbonization section into rough washing from bottom to top in sequenceSection, main washing section, fine washing section, methanol absorption of CO2The temperature is increased, and a certain amount of CO is absorbed2After the methanol liquid is pumped out from the tower for heat exchange and temperature reduction, the methanol liquid returns to the washing tower for continuously removing CO2. The purified gas enters a cooler from the top of the tower for heat exchange and then goes to the next synthesis section. The methanol without sulfur and the methanol containing sulfur from the middle section and the bottom of the absorption tower respectively enter a flash tank S102 and a flash tank S103, and effective gas H is released2CO and a portion of CO2And the gas is compressed by a recycle gas compressor and then recycled into the feed gas. The two methanol rich solutions are further flashed, the gas desorbed from the flash tank S104 can be directly discharged as waste gas after cold energy is recovered, and the gas desorbed from the flash tank S105 is recycled into the feed gas. Two streams of methanol liquid enter CO from different positions after coming out of the flash tank2Desorption column D102, H2S is absorbed again by methanol without sulfur at the upper part of the concentration tower, and CO is obtained2The product gas is discharged from the top of the tower. The methanol liquid is led out for the first time at the lower part of D102 and enters a flash tank S106 to reduce the temperature of the rich methanol liquid, and the lean liquid can be cooled to-50 ℃. The absorption liquid continues to be cooled and returns to D102. The absorption liquid is led out from the D102 for the second time to exchange heat with the barren solution, and is returned to the tower after the temperature is raised to 30 ℃. The absorption liquid from the bottom of the column is desorbed to atmospheric pressure (or vacuum state), and the flash gas from S108 and the gas from the top of S106 are simultaneously recycled to D102. The rich methanol solution enters a thermal regeneration tower after exchanging heat with the lean solution to remove H2S and residual CO2Desorbing, cooling most of the methanol at the bottom of the tower, circulating the cooled methanol back to the methanol washing tower, allowing the small part of the methanol to enter into the alcohol-water separation tower, circulating the gaseous methanol liquid at the top of the alcohol-water separation tower back to the regenerative tower, discharging the wastewater from the bottom of the tower, and ensuring that the content of the methanol in the wastewater is lower than 1 wt%.
Selecting CO in the invention2Purity of 99.0%, H2Compared with the original flow, the two states of 15.49 percent and 33.25 percent of S concentration are respectively compared, the recovery rate of carbon dioxide is greatly increased, and the energy consumption of carbon dioxide per unit is greatly reduced.
Claims (6)
1. A new technology for high-efficiency low-temperature methanol elution and pure recovery of carbon dioxide is characterized in that:
a is to increase CO2The product gas purity is obtained by further flashing the sulfur-free rich liquid and the sulfur-containing rich liquid after flashing from the medium-pressure flash tanks S102 and S103, wherein the flash vapor flashed from the sulfur-containing rich liquid is recycled to the raw material gas, and the flash vapor flashed from the sulfur-free rich liquid is discharged after the cold energy of the flash vapor is recovered;
b, respectively introducing the sulfur-free rich solution and the sulfur-containing rich solution into CO2A desorption tower for recovering cold energy and CO by gradually increasing the temperature of a heat exchange network2And (4) flash evaporation desorption.
c CO2The rich liquid at the bottom of the desorption tower is continuously flashed to further improve CO2The recovery rate is increased, and the H content in the acid gas is also increased2The concentration of S.
2. The method for recovering the acid gas by the low-temperature methanol washing absorption as claimed in claim 1, wherein the pressure of the flash tank S104 without the sulfur-rich liquid is 500 kPa-1200 kPa.
3. The method for recovering the acid gas by the low-temperature methanol washing absorption as claimed in claim 1, wherein the pressure of a flash tank S105 of the sulfur-containing rich solution is 600kPa to 1200 kPa.
4. The method for recovering acid gas by low-temperature methanol washing absorption as claimed in claim 1, wherein CO is recovered2The operating pressure of the desorption tower is 150kPa to 240 kPa.
5. The method for recovering acid gas by low-temperature methanol washing absorption as claimed in claim 1, wherein the operating pressure of the flash tank S106 is 70kPa to 150 kPa.
6. The method for recovering acid gas by low-temperature methanol washing absorption as claimed in claim 1, wherein CO is recovered2The operation pressure of the flash tank S108 at the bottom of the desorption tower is 40 kPa-150 kPa.
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| CN104208978A (en) * | 2014-08-28 | 2014-12-17 | 崔静思 | Equipment and method for gas purification |
| CN104293398A (en) * | 2014-10-27 | 2015-01-21 | 上海国际化建工程咨询公司 | Energy-saving and production-increasing method and device adopting low temperature methanol cleaning technology |
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2021
- 2021-09-09 CN CN202111054429.5A patent/CN113731117A/en active Pending
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|---|---|---|---|---|
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