WO2011122525A1 - 二酸化炭素ガス回収装置 - Google Patents
二酸化炭素ガス回収装置 Download PDFInfo
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- WO2011122525A1 WO2011122525A1 PCT/JP2011/057549 JP2011057549W WO2011122525A1 WO 2011122525 A1 WO2011122525 A1 WO 2011122525A1 JP 2011057549 W JP2011057549 W JP 2011057549W WO 2011122525 A1 WO2011122525 A1 WO 2011122525A1
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- WIPO (PCT)
- Prior art keywords
- heat
- carbon dioxide
- rich
- tower
- dioxide gas
- Prior art date
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 364
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 182
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 182
- 238000011084 recovery Methods 0.000 title claims abstract description 88
- 238000010521 absorption reaction Methods 0.000 claims abstract description 316
- 230000008929 regeneration Effects 0.000 claims abstract description 169
- 238000011069 regeneration method Methods 0.000 claims abstract description 169
- 238000001816 cooling Methods 0.000 claims abstract description 105
- 238000006243 chemical reaction Methods 0.000 claims abstract description 65
- 239000002904 solvent Substances 0.000 claims abstract description 38
- 239000007788 liquid Substances 0.000 claims description 251
- 230000002745 absorbent Effects 0.000 claims description 121
- 239000002250 absorbent Substances 0.000 claims description 121
- 230000000630 rising effect Effects 0.000 claims description 56
- 238000004140 cleaning Methods 0.000 claims description 38
- 238000010438 heat treatment Methods 0.000 claims description 32
- 238000012856 packing Methods 0.000 claims description 24
- 230000003247 decreasing effect Effects 0.000 claims description 8
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000006096 absorbing agent Substances 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 abstract description 7
- 239000000203 mixture Substances 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 350
- 150000001412 amines Chemical class 0.000 description 124
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 35
- 238000009833 condensation Methods 0.000 description 17
- 230000005494 condensation Effects 0.000 description 17
- 238000005406 washing Methods 0.000 description 16
- 238000011144 upstream manufacturing Methods 0.000 description 9
- 239000012530 fluid Substances 0.000 description 7
- 239000000498 cooling water Substances 0.000 description 4
- 238000006114 decarboxylation reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 230000006837 decompression Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 206010037660 Pyrexia Diseases 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 239000011874 heated mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
Images
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
- B01D53/1425—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
-
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
-
- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall 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
- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- 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
Definitions
- the present invention relates to a carbon dioxide gas recovery apparatus that recovers carbon dioxide gas using a CO 2 chemical absorption separation method.
- the carbon dioxide gas recovery apparatus 1000 brings a carbon dioxide-containing gas containing carbon dioxide gas into contact with a lean absorbent, and absorbs the carbon dioxide gas in the carbon dioxide-containing gas into the absorbent.
- a tower 1002 that generates the rich absorption liquid
- the regeneration that regenerates the rich absorption liquid into the lean absorption liquid by heating the rich absorption liquid supplied from the absorption tower 1001 and separating the carbon dioxide gas from the rich absorption liquid
- a tower 1002 that generates the rich absorption liquid
- the regeneration tower 1002 includes a reboiler system 1003 that draws a lean absorption liquid from the regeneration tower 1002, heats it, and reintroduces it into the regeneration tower 1002, and a solute and solvent (for example, water) of carbon dioxide gas and the absorption liquid.
- a solute and solvent for example, water
- the mixed gas with the vapor component is led out from the regeneration tower 1002 and cooled, the vapor components of the solute and the solvent in the mixed gas are condensed and reintroduced into the regeneration tower 1002, and uncondensed carbon dioxide gas is discharged.
- heat that is a heat source for heating the rich absorbent in the regeneration tower 1002 is supplied via the absorbent that is heated by the reboiler system 1003 and reintroduced into the regeneration tower 1002.
- the reboiler system 1003 includes a reboiler body 1005 that heats the absorbing liquid using heat supplied from the outside as a heat source.
- the heat supplied from the reboiler body 1005 of the reboiler system 1003 is mainly consumed when the absorbing solution is heated and regenerated in the regeneration tower 1002. Further, the heat supplied from the reboiler main body 1005 leaks to the outside when the mixed gas cooling system 1004 cools the mixed gas or when the mixed gas cooling system 1004 discharges the carbon dioxide gas.
- the conventional carbon dioxide gas recovery apparatus 1000 it is desired that the amount of heat input from the outside in the reboiler system 1003 is suppressed to further save energy.
- the present invention has been made in view of the above-described circumstances, and an object of the present invention is to provide a carbon dioxide gas recovery apparatus capable of saving energy by suppressing the amount of heat input from the outside.
- the carbon dioxide gas recovery device introduces and contacts a carbon dioxide-containing gas containing carbon dioxide gas and a lean absorbent, and the carbon dioxide gas in the carbon dioxide-containing gas is used as the absorbent.
- the mixed gas with the vapor of the solvent is led out from the regeneration tower and cooled, the vapor of the solute and the solvent is condensed, and the condensate is reintroduced into the regeneration tower.
- a mixed gas cooling system for discharging gas, and transferring heat generated by an exothermic reaction when the absorption liquid absorbs the carbon dioxide gas in the absorption tower through a heat medium, and in the regeneration tower A heat pump used as a heat source for an endothermic reaction when the carbon dioxide gas is separated from the rich absorbent is provided.
- the absorption liquid means a lean absorption liquid, a rich absorption liquid, or a mixed liquid of a lean absorption liquid and a rich absorption liquid.
- the heat generated by the exothermic reaction in the absorption tower can be used as a heat source for the endothermic reaction in the regeneration tower. Since the heat generated by the exothermic reaction is equal to the heat of the endothermic reaction, it is possible to cancel the reaction heat by exchanging it internally. Conventionally, the endothermic reaction is heated from the outside, and the reaction exotherm is discarded in the cooling water. Although it was heated, the reaction heat generated by such water cooling can be used as a heat source for the endothermic reaction necessary for regeneration, and the amount of heat input from the outside can be suppressed to save energy. it can.
- the heat pump exchanges heat between the heat medium which is interposed in the absorption tower packing disposed in the absorption tower and expands to lower the temperature, and the absorption liquid in the absorption tower.
- a first heat exchanger may be further provided.
- the heat pump since the heat pump includes the first heat exchanger, the heat generated by the exothermic reaction in the absorption tower can be received by the heat medium with high loss and high efficiency. As a result, the heat generated by the exothermic reaction in the absorption tower can be effectively used as a heat source for the endothermic reaction in the regeneration tower, and further energy saving can be achieved. Further, in this case, the absorption rate is improved due to a decrease in the temperature of the absorbing solution, so that the device efficiency can be further improved.
- the heat pump is interposed between the regenerative tower packing disposed in the regeneration tower and heated by the heat medium that has been compressed to raise the temperature, and the rich absorbing liquid in the regeneration tower. You may provide the 2nd heat exchanger to exchange.
- the heat pump since the heat pump includes the second heat exchanger, the heat generated by the exothermic reaction moved by the heat medium can be used with high efficiency as a heat source for the endothermic reaction in the regeneration tower with little loss. it can. As a result, the heat generated by the exothermic reaction in the absorption tower can be effectively used as a heat source for the endothermic reaction in the regeneration tower, and further energy saving can be achieved.
- the absorption tower may be provided with a lead-out path for deriving decarbonation gas obtained by separating the carbon dioxide gas from the carbon dioxide-containing gas, and between the lead-out path and the heat pump.
- a third heat exchanger for exchanging heat between the decarbonation gas and the heat medium expanded to lower the temperature may be interposed.
- the third heat exchanger is interposed between the lead-out path and the heat pump, the heat is exchanged between the decarbonized gas in the lead-out path and the heat medium of the heat pump, so that the lead is derived from the absorption tower.
- the heat generated by the decarboxylation gas can be received by the heat medium to heat the heat medium.
- the absorption tower is provided with a decarbonation gas cleaning system in which the cleaning liquid stored at the top of the absorption tower is led out from the absorption tower, cooled, and then reintroduced from the top of the absorption tower.
- a fourth heat exchanger for exchanging heat between the cleaning liquid and the expanded heat-reduced heat medium is interposed between the decarbonation gas cleaning system and the heat pump. Also good.
- the decarbonation gas cleaning system is provided in the absorption tower, when the decarbonation gas obtained by separating the carbon dioxide gas from the carbon dioxide-containing gas rises inside the absorption tower, the decarbonation gas It is possible to suppress the solute of the absorption liquid accompanying the flow out from the top of the absorption tower to the outside. Further, since the fourth heat exchanger is interposed between the decarbonation gas cleaning system and the heat pump, the cleaning liquid can be obtained by exchanging heat between the cleaning liquid of the decarbonation gas cleaning system and the heat medium of the heat pump. The heating medium can be heated while cooling. As a result, it is possible to suppress the heat generated by the exothermic reaction of the absorption tower and transferred to the cleaning liquid from leaking to the outside, and further energy saving can be achieved.
- a rich supply path for supplying the rich absorbent from the absorption tower to the regeneration tower may be provided, and the rich absorbent is expanded between the rich supply path and the heat pump.
- a fifth heat exchanger that exchanges heat with the lowered heat medium may be interposed.
- the absorption tower is obtained by exchanging heat between the rich absorption liquid in the rich supply path and the heat medium of the heat pump.
- the heat of the rich absorbent that is generated by the exothermic reaction and delivered to the rich absorbent can be received by the heat medium to heat the heat medium.
- the carbon dioxide gas recovery device includes a lean supply path for supplying a lean absorbent from the regeneration tower to the absorption tower, and heat is generated between the lean absorbent and the rich absorbent between the lean supply path and the rich supply path.
- the rich heat absorption liquid passing through the amine heat exchange is passed through the fifth heat exchanger. It can be cooled with. This makes it possible to increase the amount of heat exchange between the rich absorption liquid in the rich supply path and the lean absorption liquid in the lean supply path in the amine heat exchange, and the lean absorption liquid in the lean supply path is effective. The amount of heat recovered as viewed from the regeneration tower can be increased.
- a lean amine cooler that cools the lean absorbent is provided downstream of the amine heat exchange in the lean supply path, and the lean absorbent that is supplied to the absorption tower is cooled before being supplied to the absorption tower. Even if it exists, the heat loss to the exterior by this cooling can be reduced.
- the absorption tower is provided with an intercooler system in which the absorption liquid is led out from the tower intermediate section between the tower top and tower bottom in the absorption tower and cooled, and then reintroduced from the tower intermediate section.
- a sixth heat exchanger that exchanges heat between the absorbing liquid and the expanded heat-reduced heat medium may be interposed between the intercooler system and the heat pump. .
- the intercooler system since the intercooler system is provided in the absorption tower, the absorption liquid in the middle of the tower can be cooled and reintroduced, and the absorption of carbon dioxide gas by the absorption liquid in the absorption tower is promoted. be able to. Further, since the sixth heat exchanger is interposed between the intercooler system and the heat pump, the heat is exchanged between the absorption liquid of the intercooler system and the heat medium of the heat pump, thereby cooling the absorption liquid. The heating medium can be heated. Thereby, it is possible to suppress the heat generated by the exothermic reaction of the absorption tower and transferred to the absorbing solution from leaking to the outside, and further energy saving can be achieved.
- a lean supply path for supplying the lean absorbing liquid from the regeneration tower to the absorption tower is provided, and the lean absorbing liquid and the heat pump are expanded between the lean supplying path and the heat pump to reduce the temperature.
- a seventh heat exchanger that exchanges heat with the heat medium may be interposed.
- the lean absorption is achieved by exchanging heat between the lean absorbing liquid in the lean supply path and the heat medium of the heat pump.
- the heating medium can be heated while cooling the liquid.
- an eighth heat exchanger for exchanging heat between the absorbent and the heat medium that has been compressed and raised in temperature may be interposed between the reboiler system and the heat pump.
- the eighth heat exchanger is interposed between the reboiler system and the heat pump, the heat of the heat medium is reduced by exchanging heat between the reboiler system absorption liquid and the heat medium of the heat pump.
- the absorbent can be heated by receiving it in the absorbent. As a result, the amount of heat input from the outside in the reboiler system can be further suppressed, and further energy saving can be achieved.
- a rich supply path for supplying the rich absorption liquid from the absorption tower to the regeneration tower is provided, and the rich absorption liquid is compressed between the rich supply path and the heat pump to raise the temperature.
- a ninth heat exchanger for exchanging heat with the heat medium may be interposed.
- the ninth heat exchanger is interposed between the rich supply path and the heat pump, heat exchange is performed between the rich absorbent in the rich supply path and the heat medium of the heat pump. Can be received by the rich absorbent supplied to the regeneration tower to heat the rich absorbent.
- the rich absorption liquid supplied to the regeneration tower can be preheated, the amount of heat that the rich absorption liquid needs to receive in the regeneration tower can be suppressed. Therefore, the amount of heat input from the outside in the reboiler system can be further suppressed, and further energy saving can be achieved.
- the carbon dioxide gas recovery device includes a lean supply path for supplying a lean absorbent from the regeneration tower to the absorption tower, and heat is generated between the lean absorbent and the rich absorbent between the lean supply path and the rich supply path.
- amine heat exchange to be exchanged When amine heat exchange to be exchanged is present, the amount of heat in the 13th heat exchanger is added to the amount of heat in the amine heat exchange, resulting in an increase in the preheat amount of the rich absorbent and absorption by the reboiler system.
- the amount of heat to be given to the liquid can be further suppressed. Therefore, the amount of heat input from the outside in the reboiler system can be further suppressed, and further energy saving can be achieved.
- the mixed gas cooling system may include a mixed gas compressor that compresses the mixed gas to raise the temperature to obtain a temperature-increased mixed gas, and is provided between the reboiler system and the mixed gas cooling system. May include a tenth heat exchanger for exchanging heat between the absorbing liquid and the temperature rising mixed gas.
- the mixed gas cooling system includes the mixed gas compressor, the heated mixed gas can be obtained by applying a small amount of external power without heating from the outside. Furthermore, since the tenth heat exchanger is interposed between the reboiler system and the mixed gas cooling system, heat exchange is performed between the reboiler system absorption liquid and the temperature rising mixed gas of the mixed gas cooling system. Thus, the temperature rising mixed gas can be cooled while heating the absorbing liquid. As a result, the amount of heat input from the outside in the reboiler system can be reliably suppressed, and energy saving can be effectively achieved.
- a rich supply path for supplying the rich absorbent from the absorption tower to the regeneration tower may be provided, and the tenth heat exchanger may be provided between the mixed gas cooling system and the rich supply path.
- An eleventh heat exchanger that exchanges heat between the temperature rising mixed gas after passing through and the rich absorbent may be interposed.
- the eleventh heat exchanger is interposed between the mixed gas cooling system and the rich supply path, the temperature rising mixed gas of the mixed gas cooling system and the rich absorbing liquid of the rich supply path are By performing heat exchange, the temperature rising mixed gas can be cooled while heating the rich absorbent supplied to the regeneration tower.
- the rich absorption liquid supplied to the regeneration tower can be preheated by the amount of heat of the mixed gas flowing out of the regeneration tower, so that the amount of heat that the rich absorption liquid needs to receive in the regeneration tower is suppressed. Can do. Therefore, the amount of heat input from outside in the reboiler system can be further suppressed, and further energy saving can be achieved.
- the temperature rising mixed gas of the mixed gas cooling system passes through the eleventh heat exchanger after passing through the tenth heat exchanger, for example, the latent heat of the vapor of the solute and the solvent in the temperature rising mixed gas is reduced.
- the sensible heat and the remaining latent heat of the remaining temperature rising mixed gas composed of the vapors of the uncondensed solute and solvent and carbon dioxide gas can be recovered by the 11th heat exchanger.
- a rich supply path for supplying the rich absorbent from the absorption tower to the regeneration tower may be provided, and the mixed gas cooling system compresses the mixed gas to increase a temperature to increase the temperature of the mixed gas. Even if a twelfth heat exchanger for exchanging heat between the temperature rising mixed gas and the rich absorbing liquid is interposed between the mixed gas cooling system and the rich supply path. good.
- the mixed gas cooling system is provided with the mixed gas compressor, the heated mixed gas can be obtained without heating from the outside by applying a small amount of external power.
- the regeneration tower is obtained by exchanging heat between the temperature rising mixed gas of the mixed gas cooling system and the rich absorbent in the rich supply path.
- the temperature rising mixed gas can be cooled while heating the rich absorbing liquid supplied to.
- the rich absorption liquid supplied to the regeneration tower can be preheated by the amount of heat of the mixed gas flowing out of the regeneration tower, so that the amount of heat that the rich absorption liquid needs to receive in the regeneration tower is suppressed. Can do. Therefore, the amount of heat input from the outside in the reboiler system can be reliably suppressed, and energy saving can be effectively achieved.
- a 13th heat exchanger for exchanging heat between the temperature rising mixed gas after passing through the 12th heat exchanger and the rich absorbent is provided between the mixed gas cooling system and the rich supply path. It may be interposed.
- the regeneration tower is determined by the amount of heat of the mixed gas flowing out of the regeneration tower. It is possible to effectively preheat the rich absorbent supplied to the refrigeration, and the amount of heat that the rich absorbent must receive in the regeneration tower can be further suppressed. Therefore, the amount of heat input from outside in the reboiler system can be further suppressed, and further energy saving can be achieved.
- the temperature rising mixed gas of the mixed gas cooling system passes through the thirteenth heat exchanger after passing through the twelfth heat exchanger, for example, the latent heat of the vapor of the solute and the solvent in the temperature rising mixed gas is reduced.
- the sensible heat and the remaining latent heat of the remaining heated mixed gas consisting of the vapors of the uncondensed solute and solvent and carbon dioxide gas can be recovered by the 13th heat exchanger.
- the carbon dioxide gas recovery apparatus can save energy by suppressing the amount of heat input from the outside.
- FIG. 1 is a schematic view of a carbon dioxide gas recovery device according to a first embodiment of the present invention. It is the schematic of the carbon dioxide gas recovery device concerning a 2nd embodiment of the present invention. It is the schematic of the carbon dioxide gas recovery device concerning a 3rd embodiment of the present invention. It is the schematic of the carbon dioxide gas recovery device concerning a 4th embodiment of the present invention. It is the schematic of the carbon dioxide gas recovery device concerning a 5th embodiment of the present invention. It is the schematic of the carbon dioxide gas recovery device concerning a 6th embodiment of the present invention. It is the schematic of the carbon dioxide gas recovery device concerning a 7th embodiment of the present invention. It is the schematic of the conventional carbon dioxide gas recovery apparatus.
- This carbon dioxide gas recovery device recovers carbon dioxide gas from carbon dioxide containing gas by absorbing and separating the carbon dioxide gas by a CO 2 chemical absorption separation method, and the carbon dioxide gas is separated from the carbon dioxide containing gas.
- a CO 2 chemical absorption separation method an absorbing solution capable of absorbing carbon dioxide gas is used.
- an absorbing solution for example, an amine absorbing solution using monoethanolamine (MEA), diethanolamine (DEA) or the like as a solute and water as a solvent can be used.
- energy saving of the carbon dioxide gas recovery device is achieved by so-called self-heat regeneration.
- the carbon dioxide gas recovery apparatus 1 includes an absorption tower 2, a regeneration tower 3, a rich supply path 4, a lean supply path 5, and a heat pump 6.
- the absorption tower 2 brings a carbon dioxide-containing gas into contact with a lean absorbent that can absorb the carbon dioxide gas, and absorbs the carbon dioxide gas in the carbon dioxide-containing gas into the lean absorbent to produce a rich absorbent.
- the regeneration tower 3 regenerates the lean absorbent by heating the rich absorbent supplied from the absorber 2 and separating the carbon dioxide gas from the rich absorbent.
- the rich supply path 4 supplies the rich absorbent from the absorption tower 2 to the regeneration tower 3.
- the lean supply path 5 supplies the lean absorbent to the absorption tower 2 from the regeneration tower 3.
- the heat pump 6 moves heat generated by an exothermic reaction when the lean absorbing liquid absorbs the carbon dioxide gas in the absorption tower 2 through the heat medium, and when the carbon dioxide gas is separated from the rich absorbing liquid in the regeneration tower 3. It is used as a heat source for the endothermic reaction.
- An introduction path 2 d for introducing a carbon dioxide-containing gas is provided in the tower bottom 2 a of the absorption tower 2.
- a first nozzle 7 for supplying a lean absorbent into the tower downward is disposed in the tower top 2b of the absorption tower 2.
- an absorption tower packing 8 for bringing the lean absorbent and carbon dioxide-containing gas into contact with each other is disposed.
- the absorption tower 2 is connected to a lead-out path 9 through which the decarbonized gas is led out from the tower top 2 b of the absorption tower 2, and washing water (washing liquid) stored in the tower top 2 b of the absorption tower 2 is led out from the absorption tower 2.
- a decarbonation gas cleaning system 10 that is reintroduced from the tower top 2b of the absorption tower 2 after cooling is provided.
- the decarbonation gas cleaning system 10 includes a liquid receiving tray 11 disposed above the first nozzle 7 and storing cleaning water, and disposed above the liquid receiving tray 11 and supplying cleaning water downward.
- a second nozzle 12 to be supplied and a pipe 13 for connecting the liquid receiving tray 11 and the second nozzle 12 are provided.
- the piping 13 includes a cleaning water circulation pump 13a that transfers cleaning water from the liquid receiving tray 11 to the second nozzle 12 through the piping 13, and a water-cooled cleaning water cooler 15 that cools the cleaning water downstream of the cleaning water circulation pump 13a.
- the washing water is preferably the same as the solute of the absorbing solution (for example, water).
- the absorption liquid means a lean absorption liquid, a rich absorption liquid, or a mixed liquid of a lean absorption liquid and a rich absorption liquid.
- the rich supply path 4 connects the tower bottom 2a of the absorption tower 2 and a third nozzle 16 which is disposed in the tower top 3b of the regeneration tower 3 and supplies a rich absorbent liquid downward.
- the rich supply path 4 is provided with an absorption tower bottom pump 17 for transferring the rich absorption liquid from the tower bottom 2a of the absorption tower 2 to the third nozzle 16 through the rich supply path 4.
- a regeneration tower packing 18 is disposed in the tower intermediate part 3c between the tower top part 3b and the tower bottom part 3a in the regeneration tower 3.
- the absorption liquid flowing down the surface of the regeneration tower packing 18 includes the solute of the absorption liquid rising in the regeneration tower 3 and the vapor content of the solvent (for example, water), and the mixed gas of the vapor content and carbon dioxide gas. Gas-liquid contact.
- regenerator 3 draws the absorbing liquid from the regenerator 3 and heats it, reboiler system 19 is reintroduced into the regenerator 3, and the mixed gas is led out from the regenerator 3 and is cooled.
- a mixed gas cooling system 20 is provided that condenses the vapor and reintroduces the condensate into the regeneration tower 3 and discharges uncondensed carbon dioxide gas.
- the reboiler system 19 reintroduces the absorbent from the tower bottom 3 a of the regeneration tower 3 after heating the absorbent. At this time, a part of the heated absorption liquid is flushed, and a part of each of the solute and the solvent of the absorption liquid becomes vapor.
- the reboiler system 19 includes a liquid receiving tray 21 that is disposed in the bottom 3a of the regeneration tower 3 and stores an absorption liquid, and a steam that is located below the liquid receiving tray 21 in the liquid receiving tray 21 and the tower bottom 3a. And a pipe 23 for connecting the generation portion 22.
- the piping 23 is provided with a reboiler pump 24 and a reboiler body 25.
- the reboiler pump 24 transfers the absorbing liquid from the liquid receiving tray 21 to the steam generating portion 22 through the pipe 23.
- the reboiler body 25 heats the absorption liquid using heat supplied from the outside downstream of the reboiler pump 24 as a heat source.
- the reboiler body 25 is configured by a heat exchanger that exchanges heat between the reboiler system 19 and a reboiler pipe 26 through which a high-temperature fluid (for example, saturated steam) supplied from the outside flows.
- the reboiler pipe 26 is provided with a steam trap 27 downstream of the reboiler body 25.
- the mixed gas cooling system 20 is disposed above the third nozzle 16, and supplies the condensate, which is the vapor content of the condensed solute and solvent, downward, and the regeneration tower 3. And a pipe 29 for connecting the top of the tower and the fourth nozzle 28 to each other.
- a mixed gas compressor 30, a pressure reduction / expansion valve 31, a gas / liquid separator 32, and a condensate circulation pump 29 a are arranged in this order between the top of the regeneration tower 3 and the fourth nozzle 28. Is provided.
- the mixed gas compressor 30 increases the temperature by compressing the mixed gas to obtain a heated mixed gas.
- the decompression / expansion valve 31 reduces the temperature by expanding the temperature rising mixed gas.
- the gas-liquid separator 32 separates the condensate and carbon dioxide gas.
- the condensate circulation pump 29 a transfers the condensate from the gas-liquid separator 32 to the fourth nozzle 28 through the pipe 29.
- the gas-liquid separator 32 is provided with a discharge path 33 for discharging the carbon dioxide gas separated from the mixed gas by the gas-liquid separator 32.
- a condensing heat exchanger (tenth heat exchanger) 34 for exchanging heat between the absorbent and the temperature rising mixed gas is interposed between the reboiler system 19 and the mixed gas cooling system 20.
- the absorption liquid before being heated by the reboiler body 25 passes through the condensation heat exchanger 34.
- the condensing heat exchanger 34 is interposed between the reboiler pump 24 and the reboiler body 25 in the pipe 23 of the reboiler system 19, and the mixed gas compressor 30 and the pressure reducing / expansion valve in the pipe 29 of the mixed gas cooling system 20. 31 is interposed.
- the lean supply path 5 connects the tower bottom 3 a of the regeneration tower 3 and the first nozzle 7 in the absorption tower 2, and the lean supply path 5 is connected to the second bottom from the tower bottom 3 a of the regeneration tower 3.
- a regeneration tower bottom pump 35 for transferring the lean absorption liquid to the one nozzle 7 through the lean supply path 5 is provided.
- an amine heat exchanger 36 that exchanges heat between the lean absorbent and the rich absorbent.
- the heat pump 6 is interposed in the absorption tower internal heat exchange (first heat exchanger) 37 interposed in the absorption tower packing 8 in the absorption tower 2 and in the regeneration tower packing 18 in the regeneration tower 3. And a pair of pipes 39 and 40 for connecting the absorption tower internal heat exchange 37 and the regeneration tower internal heat exchange 38.
- the heat exchange 37 inside the absorption tower is interposed so as to cut through the absorption tower packing 8, and exchanges heat between the heat medium whose temperature has decreased due to expansion and the absorption liquid in the absorption tower 2.
- the regeneration tower internal heat exchange 38 is interposed so as to run vertically through the regeneration tower packing 18, and exchanges heat between the heat medium whose temperature has been increased by compression and the absorbent in the regeneration tower 3.
- one pipe 39 connects the upper part of the regeneration tower internal heat exchange 38 and the lower part of the absorption tower internal heat exchange 37.
- the pipe 39 is provided with a heat medium expansion valve 41 that lowers the temperature by expanding the heat medium.
- the other pipe 40 connects the upper part of the absorption tower internal heat exchange 37 and the lower part of the regeneration tower internal heat exchange 38.
- the pipe 40 is provided with a heat medium compressor 42 that raises the temperature by compressing the heat medium.
- the heat generated by the exothermic reaction in the absorption tower 2 is recovered as latent heat of evaporation by evaporating in the heat exchange 37 inside the absorption tower and condensed in the heat exchange 38 inside the regeneration tower.
- a fluid capable of generating heat of condensation and using the heat of condensation as a heat source for the endothermic reaction in the regeneration tower 3 is preferable. Examples of such fluid include pentane and water.
- the operation of the carbon dioxide gas recovery apparatus 1 configured as described above will be described.
- the flow of the absorption liquid will be described starting from the absorption tower 2.
- the carbon dioxide-containing gas supplied to the tower bottom 2a rises inside, and the lean absorbent supplied from the first nozzle 7 in the tower top 2b falls inside.
- the carbon dioxide-containing gas and the lean absorbing liquid come into contact with each other, and the carbon dioxide gas in the carbon dioxide-containing gas is absorbed by the lean absorbing liquid to cause an exothermic reaction.
- the absorption tower packing 8 is disposed in the tower middle part 2c of the absorption tower 2.
- the absorption tower packing 8 has, for example, a fin configuration having a large number of narrow gaps, a large fin surface area per volume, and the gap is configured so that the angle of the flow path changes regularly. The turbulence of the flow occurs.
- the absorption liquid flows down on the fins while forming a wet wall, and is brought into gas-liquid contact with the carbon dioxide-containing gas rising in the absorption tower 2.
- the absorption tower packing 8 has a structure in which the gap between the wetting walls is narrow and the traveling angle changes at a constant pitch, thereby disturbing the flow of gas and liquid and improving the efficiency of gas-liquid contact. Therefore, on the surface of the absorption tower packing 8, the rising carbon dioxide-containing gas and the falling absorption liquid are easily in contact with each other, and the absorption of the carbon dioxide gas by the absorption liquid is promoted.
- the decarbonation gas cleaning system 10 since the decarbonation gas cleaning system 10 is provided in the absorption tower 2, the inside of the tower top 2b of the absorption tower 2 is cooled by the cleaning water cooled and re-introduced by the water-cooled cleaning water cooler 15. can do. Therefore, for example, even if the solute in the absorption liquid scatters or evaporates and rises accompanying the decarbonation gas, the solute is supplied to the decarbonation gas cleaning system 10 before reaching the lead-out path 9. Thereby, it is possible to prevent the solute in the absorption liquid from flowing out from the tower top 2 b of the absorption tower 2 through the outlet path 9.
- the rich absorbent produced together with the decarbonation gas descends in the absorption tower 2 and is stored in the tower bottom 2a, and then passes through the rich supply path 4 to the third nozzle 16 in the tower top 3b of the regeneration tower 3.
- the amine heat exchange 36 is interposed between the lean supply path 5 and the rich supply path 4, and the rich absorption liquid exchanges heat with the lean absorption liquid in the lean supply path 5. Heated while cooling the lean absorbent.
- the rich absorbent supplied from the third nozzle 16 descends and the absorbent heated by the reboiler system 19 is reintroduced from the tower bottom 3a.
- a part of the heated absorption liquid is flushed in the vapor generation part 22, a part of each of the solute and the solvent of the absorption liquid becomes a vapor, and the regenerated carbon dioxide becomes a gas, To rise.
- the rich absorption liquid and the vapors of the solute and solvent come into contact with each other, and an endothermic reaction of desorption regeneration takes place using the heat of condensation of the vapors of the solute and solvent as a heat source. Are separated.
- the regenerative tower packing 18 is disposed in the middle part 3c of the regenerative tower 3.
- the regeneration tower packing 18 has, for example, a fin configuration having a large number of narrow gaps, a large fin surface area per volume, and the gap is configured so that the angle of the flow path changes regularly. The turbulence of the flow occurs.
- the absorbing solution flows down on the fins while forming a wet wall, contacts the vapor of the solute and the solvent rising in the regenerator 3, and is efficient due to the size of the surface area and flow disturbance. Gas-liquid contact is made and the separation and release of carbon dioxide is promoted.
- the rich absorbent is separated into the lean absorbent and the carbon dioxide gas.
- the carbon dioxide gas is mixed with the solute and the vapor of the solvent to become a mixed gas, and rises in the regeneration tower 3.
- This mixed gas is introduced into the pipe 29 of the mixed gas cooling system 20 from the top of the regeneration tower 3, and is then compressed by the mixed gas compressor 30 in the process of passing through this pipe 29 so that the temperature rises and the temperature rises. It becomes a mixed gas. Thereafter, the temperature rising mixed gas is cooled while heating the absorption liquid by exchanging heat with the absorption liquid of the reboiler system 19 in the condensation heat exchanger 34. Thereafter, the temperature rising mixed gas is expanded by the pressure reduction / expansion valve 31 and the temperature is lowered.
- steam part of the said solute and solvent in temperature rising mixed gas is condensed, and it becomes a condensate
- This condensate and the non-condensed carbon dioxide main gas (temperature rising mixed gas) which mainly consisted of carbon dioxide gas Are separated by the gas-liquid separator 32.
- the condensate is reintroduced into the regeneration tower 3 from the fourth nozzle 28, and uncondensed carbon dioxide main gas is discharged to the outside through the discharge path 33.
- the absorption liquid descending in the regeneration tower 3 is stored in the tower bottom 3 a and then led out from the regeneration tower 3 a as a separated and regenerated lean absorption liquid, and passes through the lean supply path 5 in the tower top 2 b of the absorption tower 2.
- the lean absorption liquid is cooled while preheating the rich absorption liquid by exchanging heat with the rich absorption liquid in the rich supply path 4 by the amine heat exchanger 36.
- the heat that the lean absorbing solution brings out can be recovered as the preheating of the rich absorbing solution supplied from the outside.
- the heat medium expansion valve 41 As a starting point.
- the heat medium whose temperature has been lowered by the heat medium expansion valve 41 passes through the one pipe 39 and then moves from the lower part to the upper part of the heat exchange 37 inside the absorption tower to exchange heat with the absorbing liquid. While cooling the absorbing liquid, it absorbs and evaporates the heat of the exothermic reaction that occurs when the absorbing liquid chemically absorbs carbon dioxide. Thereafter, the heat medium moves to the lower part of the regeneration tower internal heat exchange 38 through the other pipe 40. At this time, the heat medium is compressed by the heat medium compressor 42 and the temperature rises.
- the heat medium is cooled by exchanging heat with the absorbing liquid while moving from the lower part to the upper part of the heat exchanger 38 inside the regeneration tower, thereby heating the absorbing liquid and consuming the heat as a heat source for the endothermic reaction. ⁇ Condensed. Thereafter, the heat medium moves toward the lower part of the heat exchange 37 inside the absorption tower through the one pipe 39. At this time, the pressure of the heat medium is lowered by the heat medium expansion valve 41, and the temperature is lowered again to become a gas / liquid mixed fluid.
- the heat pump 6 since the heat pump 6 is provided, it is generated by an exothermic reaction in the absorption tower 2 as a heat source for the endothermic reaction in the regeneration tower 3. Heat can be used. Since the heat generated by the exothermic reaction is equal to the heat of the endothermic reaction, it becomes possible to cancel the reaction heat by exchanging it internally. Conventionally, while heat is applied from the outside for endothermic reaction, the reaction exotherm was wasted in the cooling water, but this waste heat generated from the reaction can be used as a heat source for the endothermic reaction required for regeneration. become. As a result, it is possible to save energy by suppressing the amount of heat input from the outside.
- the heat pump 6 since the heat pump 6 includes the absorption tower internal heat exchange 37, the heat medium can receive the heat generated by the exothermic reaction in the absorption tower 2 with high loss and high efficiency. Furthermore, since the heat pump 6 includes the regeneration tower internal heat exchange 38, the heat generated by the exothermic reaction moved by the heat medium can be used with high efficiency as a heat source for the endothermic reaction in the regeneration tower 3 with little loss. it can. As described above, the heat generated by the exothermic reaction in which the absorption liquid chemically absorbs carbon dioxide in the absorption tower 2 is absorbed in the regeneration tower 3 without consuming the energy of waste heat to the cooling water while being externally heated. It can be effectively used as a heat source for an endothermic reaction for separating and regenerating carbon dioxide from the carbon dioxide, and further energy saving can be achieved.
- the mixed gas cooling system 20 includes a mixed gas compressor 30. Therefore, by applying a slight amount of external power, a temperature rising mixed gas can be obtained without heating from the outside. Further, the condensing heat exchanger 34 is interposed between the reboiler system 19 and the mixed gas cooling system 20. Therefore, by performing heat exchange between the absorption liquid of the reboiler system 19 and the temperature rising mixed gas of the mixed gas cooling system 20, the temperature rising mixed gas can be cooled while heating the absorption liquid. In this way, the rich absorbent supplied to the regeneration tower 3 can be preheated by the amount of heat of the mixed gas flowing out of the regeneration tower 3. As a result, the amount of heat input from the outside in the reboiler system 19 can be reliably suppressed, and energy saving can be effectively achieved.
- reaction heat generation amount in the absorption tower 2 is equal to the reaction heat absorption amount in the regeneration tower 3. Therefore, the reaction heat conventionally applied by heating from the outside with a small amount of power required for the heat pump 6 can be covered by the transfer of heat inside the process, and the transfer of heat from the outside can be eliminated. As a result, the amount of external heat applied in the reboiler system 19 of the regeneration tower 3 is reduced as compared with the conventional case.
- the amount of heat to be applied is the amount of recovery leakage heat in the amine heat exchanger 36 (the sensible heat amount of the lean absorbing liquid flowing out from the amine heat exchanger 36 and the sensible heat amount of the rich absorbing liquid flowing into the amine heat exchanger 36).
- the amount of heat is commensurate with the sum of the amount of heat dissipated around the regeneration tower 3.
- the pressure reduction / expansion valve 31 of the mixed gas cooling system 20 is provided in the discharge passage 33 and the gas in the pipe 29 of the mixed gas cooling system 20
- a level control valve 101 is provided between the liquid separator 32 and the fourth nozzle 28 instead of the condensate circulation pump 29a.
- the heat pump 6 does not include the absorption tower internal heat exchange 37.
- a decarbonation gas cooler (third heat exchanger) 102 that exchanges heat between the decarbonization gas and the heat medium that has expanded and reduced in temperature is provided between the outlet path 9 and the heat pump 6. Is intervening.
- a cleaning water cooler (fourth heat exchanger) 103 for exchanging heat between the cleaning water and the heat medium whose temperature has decreased due to expansion.
- a rich amine heat exchanger (fifth heat exchanger) 104 is provided between the rich supply path 4 and the heat pump 6 to exchange heat between the rich absorbing liquid and the heat medium whose temperature has decreased due to expansion. is doing.
- the decarbonation gas cooler 102, the washing water cooler 103, and the rich amine heat exchanger 104 pass through the heat medium whose temperature is lowered by the heat medium expansion valve 41 in the heat pump 6, and the heat recovery in which the heat medium receives heat. Is on the side.
- the heat pump 6 includes a plurality of pipes 105, 106, 107, and 108, and a heat medium distributor 109 and a heat medium collector 110 that connect the pipes 105, 106, 107, and 108.
- the plurality of pipes 105, 106, 107, 108 connect the first pipe 105 that connects the upper part of the heat exchanger 38 inside the regeneration tower and the heat medium distributor 109, and the heat medium distributor 109 and the heat medium collector 110.
- Two branch pipes 106 and 107, and a second pipe 108 that connects the heat medium collector 110 and the lower part of the heat exchange 38 inside the regeneration tower.
- one of the branch pipes 106 is provided with a decarboxylation gas cooler 102 and a washing water cooler 103 in this order from the heat medium distributor 109 to the heat medium collector 110.
- a rich amine heat exchanger 104 is interposed in the other branch pipe 107.
- the first pipe 105 is provided with the heat medium expansion valve 41, and the second pipe 108 is provided with the heat medium compressor 42.
- a cleaning water cooler 103 is interposed between the cleaning water circulation pump 13a and the second nozzle 12 in the pipe 13, The water-cooled washing water cooler 15 is not provided.
- a rich amine heat exchanger 104 is interposed in the rich supply path 4 downstream of the absorption tower bottom pump 17 and upstream of the amine heat exchanger 36.
- the operation of the carbon dioxide gas recovery apparatus 100 configured as described above will be described.
- the flow of the heat medium of the heat pump 6 will be described with the heat medium expansion valve 41 as a starting point.
- the heat medium whose temperature has been lowered by the heat medium expansion valve 41 passes through the first pipe 105 and then passes through the two branch pipes 106 and 107 branched by the heat medium distributor 109.
- the heat medium passing through the one branch pipe 106 receives heat of the decarbonized gas derived from the absorption tower 2 by exchanging heat with the decarbonized gas in the outlet channel 9 in the decarbonized gas cooler 102. Heated. Thereafter, the heat medium is further heated while cooling the washing water by exchanging heat with the washing water of the decarbonation gas washing system 10 in the washing water cooler 103.
- the heat medium passing through the other branch pipe 107 receives the heat of the rich absorbent flowing out from the absorption tower 2 in the rich amine heat exchanger 104 and is heated.
- the heat medium that has passed through both branch pipes 106 and 107 merges at the heat medium collector 110.
- the heat medium merged in the heat medium collector 110 moves to the lower part of the regenerator internal heat exchange 38 through the second pipe 108.
- the temperature of the heat medium rises by the heat medium compressor 42.
- the heat medium is cooled by exchanging heat with the absorbing liquid while moving from the lower part to the upper part of the heat exchange 38 inside the regeneration tower, thereby heating the absorbing liquid and consuming the heat with the heat source of the endothermic reaction.
- it moves toward the heat medium distributor 109 through the first pipe 105.
- the temperature of the heat medium is lowered again by the heat medium expansion valve 41.
- the decarbonation gas cooler 102 is interposed between the outlet path 9 and the heat pump 6. Therefore, heat exchange is performed between the decarbonation gas in the outlet passage 9 and the heat medium of the heat pump 6, so that the heat medium receives heat of the decarbonation gas derived from the absorption tower 2 and heats the heat medium. be able to. Thereby, it is possible to suppress the heat generated by the exothermic reaction of the absorption tower 2 and transferred to the decarbonized gas from leaking to the outside, and further energy saving can be achieved.
- the cleaning water cooler 103 is interposed between the decarbonation gas cleaning system 10 and the heat pump 6, heat is exchanged between the cleaning water of the decarbonation gas cleaning system 10 and the heat medium of the heat pump 6.
- the heat medium can be heated while cooling the washing water.
- the rich amine heat exchanger 104 is interposed between the rich supply path 4 and the heat pump 6. Therefore, by exchanging heat between the rich absorption liquid in the rich supply path 4 and the heat medium of the heat pump 6, the heat of the rich absorption liquid generated by the exothermic reaction of the absorption tower 2 and transferred to the rich absorption liquid is obtained.
- the heat medium can be heated by being received by the heat medium.
- the rich amine heat exchanger 104 is interposed upstream of the amine heat exchanger 36 in the rich supply path 4, so that the rich absorbent that passes through the amine heat exchanger 36 is passed through the rich amine heat exchanger 36. It can be cooled by the vessel 104.
- the amine heat exchanger 36 it becomes possible to increase the amount of heat exchange between the rich absorption liquid in the rich supply path 4 and the lean absorption liquid in the lean supply path 5, and the lean absorption in the lean supply path 5
- the liquid can be cooled effectively, and the amount of heat recovered as viewed from the regeneration tower can be increased. Therefore, for example, a lean amine cooler (not shown) that cools the lean absorbent is provided downstream of the amine heat exchanger 36 in the lean supply path 5, and before the lean absorbent that is supplied to the absorption tower 2 is supplied to the absorption tower 2. Even in the case of cooling in advance, heat loss to the outside due to this cooling can be reduced.
- the heat of decarboxylation gas and absorption liquid led out from the inside of the absorption tower 2 is received by the decarbonation gas cooler 102, the washing water cooler 103, and the rich amine heat exchanger 104. Yes. Therefore, the heat generated by the exothermic reaction in the absorption tower 2 can be received by the heat medium without providing the absorption tower internal heat exchange 37. Thereby, for example, the carbon dioxide gas recovery apparatus 100 can be simplified.
- the heat pump 6 does not include the absorption tower internal heat exchange 37, but may include this.
- the absorption tower packing 8 is divided into two vertically divided in the tower middle part 2 c of the absorption tower 2, and the absorption tower 2.
- the intercooler system 201 is disposed between the divided absorption tower packings 8 and has a liquid receiving tray 202 in which the absorbing liquid is stored, and is disposed below the liquid receiving tray 202 and supplies the absorbing liquid downward. And a pipe 204 that connects the liquid receiving tray 202 and the fifth nozzle 203 to each other.
- the pipe 204 is provided with an intercooler pump 205 that transfers the absorption liquid from the liquid receiving tray 202 to the fifth nozzle 203 through the pipe 204.
- a heat-medium cooling type intercooler (sixth heat exchanger) 206 that exchanges heat between the absorbing liquid and the heat medium that has expanded and the temperature has decreased. Is intervening.
- a heat-medium cooling type lean amine cooler (seventh heat exchanger) 207 that exchanges heat between the lean absorbing liquid and the heat medium that has expanded and the temperature has decreased. Is intervening.
- the heat pump 6 includes five branch pipes 208, and each of the branch pipes 208 includes the decarbonation gas cooler 102, the washing water cooler 103, the rich amine heat exchanger 104, and the heat medium cooling. Either a type intercooler 206 or a heat medium cooling type lean amine cooler 207 is interposed.
- a heat medium cooling type intercooler 206 is interposed between the intercooler pump 205 and the fifth nozzle 203 in the pipe 204.
- a heat medium cooling type lean amine cooler 207 is interposed in the lean supply path 5 downstream of the amine heat exchanger 36.
- the operation of the carbon dioxide gas recovery device 200 configured as described above will be described.
- the flow of the heat medium of the heat pump 6 will be described from the heat medium expansion valve 41 as a starting point until the heat medium collector 110 is reached.
- the heat medium whose temperature has been lowered by the heat medium expansion valve 41 passes through the five branch pipes 208 branched by the heat medium distributor 109 after passing through the second pipe 108.
- the heat medium passing through the branch pipe 208 provided with the heat medium cooling intercooler 206 is heated while cooling the absorption liquid by exchanging heat with the absorption liquid in the heat medium cooling intercooler 206. Further, the heat medium passing through the branch pipe 208 in which the heat medium cooling type lean amine cooler 207 is interposed is heated in the heat medium cooling type lean amine cooler 207 while cooling the lean absorbent. Then, the heat medium that has passed through each branch pipe 208 joins in the heat medium collector 110.
- the heat medium cooling type lean amine cooler 207 is interposed between the lean supply path 5 and the heat pump 6. Therefore, the heat medium can be heated while cooling the lean absorbent by heat exchange between the lean absorbent in the lean supply path 5 and the heat medium in the heat pump 6. Thereby, the heat
- the intercooler system 201 is provided in the absorption tower 2, it becomes possible to re-introduce the absorption liquid in the tower intermediate part 2 c and to absorb carbon dioxide gas by the absorption liquid in the absorption tower 2. Can be promoted more.
- the heat medium cooling type intercooler 206 is interposed between the intercooler system 201 and the heat pump 6, absorption is achieved by exchanging heat between the absorbing liquid of the intercooler system 201 and the heat medium of the heat pump 6.
- the heating medium can be heated while cooling the liquid.
- the flow of the rich absorbent is branched to a portion located between the absorption tower bottom pump 17 and the amine heat exchanger 36 in the rich supply path 4.
- first rich amine heat exchanger 305 that exchanges heat between the rich absorbent and the lean absorbent.
- the first rich amine heat exchanger 305 is interposed downstream of the amine heat exchanger 36 in the lean supply path 5.
- the first rich amine heat exchanger 305 exchanges heat between the rich absorbent in the one rich branch 302 and the lean absorbent in the lean supply path 5.
- a reboiler distributor 306 is provided between the reboiler pump 24 and the condensation heat exchanger 34 in the pipe 23 of the reboiler system 19 provided in the regeneration tower 3.
- a branch pipe 307 connected to the tower bottom 3a of the tower 3 is branched.
- a heat medium reboiler heater (eighth heat exchanger) 308 that exchanges heat between the absorbing liquid and the heat medium that has been compressed and increased in temperature. Is intervening.
- a second rich amine heat exchanger (9th heat exchanger) 309 that exchanges heat between the rich absorbent and the heat medium that has been compressed and increased in temperature.
- the heat medium reboiler heater 308, the second rich amine heat exchanger 309, and the regeneration tower internal heat exchanger 38 pass through the heat medium whose temperature is increased by being compressed by the heat medium compressor 42 in the heat pump 6, and the heat medium is heated. Intervenes in the heat supply that delivers the heat.
- the heat pump 6 includes a plurality of pipes 310, 311, 312, 313, and 314, and a heat medium distributor 315 and a heat medium collector 316 that connect the pipes.
- the plurality of pipes 310, 311, 312, 313, and 314 include three branch pipes 310, 311, and 312 that connect the heat medium distributor 315 and the heat medium collector 316, the heat medium collector 316, and the absorption tower internal heat. It consists of a first pipe 313 connecting the lower part of the cross 37 and a second pipe 314 connecting the upper part of the heat exchange 37 inside the absorption tower and the heat medium distributor 315.
- the regeneration tower internal heat exchanger 38 is provided at an intermediate portion of the first branch pipe 310, and a heat medium reboiler heater 308 is provided in the second branch pipe 311. Is installed, and a second rich amine heat exchanger 309 is interposed in the third branch pipe 312.
- the first pipe 313 is provided with the heat medium expansion valve 41
- the second pipe 314 is provided with the heat medium compressor 42.
- a heating medium reboiler heater 308 is interposed in the branch pipe 307, and in the rich supply path 4, one of the rich branch paths 302, 303 is the one rich branch.
- a second rich amine heat exchanger 309 is interposed in the other rich branch path 303 different from the path 302.
- the second rich amine heat exchanger 309 is interposed upstream of the amine heat exchanger 36 in the rich supply path 4.
- the heat medium whose temperature has been lowered by the heat medium expansion valve 41 passes through the first pipe 313 and is then absorbed by exchanging heat with the absorbing liquid while moving from the lower part to the upper part of the heat exchange 37 inside the absorption tower.
- the heat of the exothermic reaction is received while cooling the liquid, and then moves to the heat medium distributor 315 through the second pipe 314.
- the temperature of the heat medium rises by the heat medium compressor 42.
- the heat medium is branched by the heat medium distributor 315 and passes through the branch pipes 310, 311, and 312.
- the heat medium passing through the first branch pipe 310 is rich in the heat exchange as the heat source of the endothermic reaction by exchanging heat with the absorption liquid while moving from the lower part to the upper part of the heat exchange 38 inside the regeneration tower. Transfer to absorbent and heat.
- the heat medium passing through the second branch pipe 311 exchanges heat with the absorption liquid of the reboiler system 19 in the heat medium reboiler heater 308, thereby transferring the heat to the absorption liquid and heating it.
- the heat medium passing through the third branch pipe 312 exchanges heat with the rich absorption liquid in the rich supply path 4 to transfer the heat to the rich absorption liquid and heat it.
- the heat medium reboiler heater 308 is interposed between the reboiler system 19 and the heat pump 6. Therefore, by performing heat exchange between the absorption liquid of the reboiler system 19 and the heat medium of the heat pump 6, the heat of the heat medium can be received by the absorption liquid and the absorption liquid can be heated. As a result, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the second rich amine heat exchange 309 is interposed between the rich supply path 4 and the heat pump 6, heat exchange is performed between the rich absorbent in the rich supply path 4 and the heat medium of the heat pump 6.
- the rich absorption liquid supplied to the regeneration tower 3 can be received by the heat of the heat medium so that the rich absorption liquid can be heated.
- the rich absorption liquid supplied to the regeneration tower 3 can be preheated, the amount of heat that the rich absorption liquid needs to receive in the regeneration tower 3 can be suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the second rich amine heat exchanger is included in the heating amount in the amine heat exchanger 36.
- the preheating amount of the rich absorption liquid increases, and the amount of heat to be given to the absorption liquid by the reboiler system 19 can be further suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the reboiler is disposed between the reboiler pump 24 and the condensation heat exchanger 34 in the pipe 23 of the reboiler system 19 provided in the regeneration tower 3.
- a distributor 401 is provided.
- a branch pipe 402 connected to the tower bottom 3 a of the regeneration tower 3 is branched from the reboiler distributor 401.
- the heat pump 6 does not include the regeneration tower internal heat exchange 38.
- a heat medium reboiler heater (eighth heat exchanger) 403 that exchanges heat between the absorbing liquid and the heat medium that has been compressed and increased in temperature. Is intervening.
- the plurality of pipes 404 and 405 of the heat pump 6 are connected to the heat medium collector 110 and the heat medium distributor 109 and the main pipe 404 provided with the heat medium compressor 42 and the heat medium distributor. 109 and three branch pipes 405 connecting the heat medium collector 110.
- the main pipe 404 is provided with a heat medium expansion turbine 406 that reduces the temperature by expanding the heat medium.
- the heat medium expansion turbine 406 obtains rotational power when the heat medium is expanded.
- the heat medium reboiler heater 403 is interposed between the heat medium compressor 42 and the heat medium expansion turbine 406 in the main pipe 404.
- Each of the branch pipes 405 is provided with any one of a heat medium cooling type decarboxylation gas cooler 102, a heat medium cooling type washing water cooler 103, and a heat medium cooling type rich amine heat exchanger 104. .
- the heat medium whose temperature has been lowered by the heat medium expansion turbine 406 passes through the main pipe 404 and then is branched by the heat medium distributor 109 and is heated in each heat exchanger through the three branch pipes 405. Merge at the aggregator 110.
- the heat medium merged in the heat medium collector 110 passes through the main pipe 404 and is heated by the heat medium compressor 42, and then is heat-exchanged with the absorption liquid of the reboiler system 19 in the heat medium type reboiler heater 403.
- the heat of the heat medium is transferred to the absorption liquid and heated. Then, it moves toward the heat medium distributor 109 through the main pipe 404. At this time, the temperature of the heat medium is lowered again by the heat medium expansion turbine 406.
- the heat medium reboiler heater 403 is interposed between the reboiler system 19 and the heat pump 6. Therefore, by performing heat exchange between the absorption liquid of the reboiler system 19 and the heat medium of the heat pump 6, the heat of the heat medium can be received by the absorption liquid and the absorption liquid can be heated. As a result, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the heat pump 6 is not provided with the regeneration tower internal heat exchange 38, it may be provided with this.
- the absorption tower packing 8 is divided into two vertically divided in the tower middle part 2 c of the absorption tower 2 and Is provided with an intercooler system 501 for deriving the lean absorbing liquid from the tower intermediate part 2c of the absorption tower 2 and cooling it, and then reintroducing it from the tower intermediate part 2c.
- a lean amine cooler 502 that cools the lean absorbent is provided in the lean supply path 5 downstream of the amine heat exchanger 36.
- the piping 29 of the mixed gas cooling system 20 is not provided with the decompression / expansion valve 31, and the condensate circulation is provided between the gas-liquid separator 32 and the fourth nozzle 28 in the piping 29.
- a level adjustment valve 503 is provided instead of the pump 29a.
- the gas-liquid separator 32 includes a condensate that is the vapor of the solute and the solvent condensed by the condensation heat exchanger 34, and the remaining uncondensed gas that is composed of the vapor of the solute and the solvent and the carbon dioxide gas. The temperature rising mixed gas is separated.
- the gas-liquid separator 32 is provided with a residual gas flow passage 504 connected to the tower top 3 b of the regeneration tower 3 through another gas-liquid separator 505 described later, instead of the discharge passage 33.
- the remaining non-condensed heated mixture gas separated by the gas-liquid separator 32 passes.
- a third rich amine heat exchanger (an eleventh heat exchanger) 514, the decompression / expansion valve 31, a condensate of vapor of the solute and the solvent, and uncondensed carbon dioxide are provided.
- Another gas-liquid separator 505 for separating gas and a level control valve 506 are arranged in this order from the gas-liquid separator 32 to the top 3b of the regeneration tower 3.
- the other gas-liquid separator 505 is provided with the discharge path 33.
- a rich amine distributor 507 for branching the flow of the rich absorbent liquid and a branched rich absorbent liquid circulate in a portion located between the absorption tower bottom pump 17 and the amine heat exchanger 36 in the rich supply path 4.
- the first rich amine heat exchange that exchanges heat between the rich absorbent and the lean absorbent. 512 is interposed.
- the first rich amine heat exchanger 512 is interposed downstream of the amine heat exchanger 36 in the lean supply path 5.
- the second rich branch 509 of the three rich branches 508, 509, and 510 and the reboiler pipe 26 the second rich amine heat that exchanges heat between the rich absorbent and the high-temperature fluid.
- Intersection 513 is interposed.
- the second rich amine heat exchanger 513 is interposed downstream of the steam trap 27 in the reboiler pipe 26.
- Intersection 514 is interposed.
- the third rich amine heat exchanger 514 is interposed in the third rich branch 510 of the three rich branches 508, 509, 510, and upstream of the pressure reducing / expansion valve 31 in the residual gas flow passage 504. Is intervened.
- the rich absorbent passing through the rich supply path 4 reaches the rich amine distributor 507 and then branches into three branch paths 508, 509, and 510.
- the rich absorption liquid passing through the first rich branch 508 is heated while cooling the lean absorption liquid by exchanging heat with the lean absorption liquid in the lean supply path 5 in the first rich amine heat exchange 512.
- the rich absorbent passing through the second rich branch 509 is heated by receiving heat from the high-temperature fluid by exchanging heat with the high-temperature fluid in the reboiler pipe 26 in the second rich amine heat exchange 513.
- the rich absorbing liquid passing through the third rich branch 510 is exchanged with the remaining temperature rising mixed gas flowing through the remaining gas flow passage 504 in the third rich amine heat exchange 514, whereby the remaining rising temperature is increased.
- the hot mixed gas is heated while cooling.
- the rich absorbent heated through the rich branch paths 508, 509, and 510 is joined by the rich amine collector 511 and then supplied to the third nozzle 16.
- the mixed gas that has risen in the regeneration tower 3 passes through the pipe 29 of the mixed gas cooling system 20 and is first compressed by the mixed gas compressor 30 to rise in temperature and become a heated mixed gas. Thereafter, the condensation heat exchanger 34 performs heat exchange with the absorption liquid of the reboiler system 19 to recover the latent heat of the solute and solvent vapor, and at least a part of the solute and solvent vapor is condensed. It becomes a condensate. Next, the condensate is separated from the remaining non-condensed temperature rising mixed gas by the gas-liquid separator 32, and among these, the condensate passes through the pipe 29 to the tower top 3 b of the regeneration tower 3. Supplied from the fourth nozzle 28.
- the remaining non-condensed temperature rising mixed gas passes through the residual gas flow passage 504 and exchanges heat with the rich absorption liquid passing through the third rich branch 510 in the third rich amine heat exchanger 514,
- the sensible heat and the latent heat of the remaining steam are recovered. That is, the latent heat of the vapor of the solute and the solvent is recovered to condense the vapor of the solute and the solvent in the remaining temperature rising mixed gas, and the carbon dioxide gas in the remaining temperature rising mixed gas Sensible heat is recovered.
- the remaining temperature rising mixed gas is expanded by the pressure reducing / expansion valve 31 and the temperature is lowered, so that all the vapors of the solute and the solvent in the remaining temperature rising mixed gas are condensed to become a condensate. .
- the other liquid-liquid separator 505 separates the condensate from uncondensed carbon dioxide gas.
- the condensate is supplied to the top 3 b of the regeneration tower 3 through the residual gas flow passage 504, and the carbon dioxide gas is discharged through the discharge path 33.
- the third rich amine heat exchanger 514 is interposed between the mixed gas cooling system 20 and the rich supply path 4. Therefore, by heat exchange between the remaining temperature rising mixed gas of the mixed gas cooling system 20 and the rich absorbent in the rich supply path 4, while heating the rich absorbent supplied to the regeneration tower 3, The remaining temperature rising mixed gas can be cooled.
- the rich absorption liquid supplied to the regeneration tower 3 can be preheated by the amount of heat of the mixed gas flowing out of the regeneration tower 3, so the amount of heat that the rich absorption liquid needs to receive in the regeneration tower 3. Can be suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the temperature rising mixed gas of the mixed gas cooling system 20 passes through the condensation heat exchanger 34 and then passes through the third rich amine heat exchanger 514, the latent heat of vapor of the solute and the solvent in the temperature rising mixed gas. After being recovered by the condensation heat exchanger 34, the sensible heat and the remaining latent heat of the remaining unheated mixed gas mixture can be recovered by the third rich amine heat exchanger 514.
- the amount of heat to be applied is the amount of recovery leakage heat in the amine heat exchanger 36 (the sensible heat amount of the lean absorbing liquid flowing out of the amine heat exchanger 36 and the sensible heat amount of the rich absorbing liquid flowing in the amine heat exchanger 36).
- the amount of heat to be applied from the outside in the reboiler system 19 is the amount of heat that only corresponds to the amount of heat released around the regeneration tower 3. Reduce to. Since heat radiation can be controlled by the degree of heat retention, the amount of heat to be finally applied from the outside in the reboiler system 19 can be made near zero.
- heat is exchanged between the remaining temperature rising mixed gas in the mixed gas cooling system 20 and the rich absorbent in the rich supply path 4. It is not limited to.
- heat exchange may be performed between the carbon dioxide gas and the rich absorbing solution, and sensible heat recovery of the carbon dioxide gas may be performed.
- the temperature rises upstream of the gas-liquid separator 32 so that all the vapors of the solute and the solvent in the temperature rise mixed gas are separated from the carbon dioxide gas.
- the mixed gas cooling system 20 may be configured such that all of the vapors of the solute and the solvent in the mixed gas are condensed.
- a rich amine distributor that branches the flow of the rich absorption liquid to a portion located downstream of the absorption tower bottom pump 17 in the rich supply path 4.
- 601 two rich branch paths 602 and 603 through which the branched rich absorbing liquid flows, and a rich amine collector 604 in which the rich branch paths 602 and 603 merge.
- the amine heat exchanger 36 is interposed between one rich branch path 602 and the lean supply path 5.
- the heat pump 6 does not have the heat exchange 38 inside the regeneration tower.
- the first rich amine heat exchange (the ninth heat exchange) that exchanges heat between the rich absorbent and the heat medium that has been compressed and increased in temperature. ) Is interposed.
- the heat pump 6 includes a heat pump pipe 607 that connects the lower part and the upper part of the heat exchange 37 inside the absorption tower.
- the heat pump pipe 607 is provided with the heat medium compressor 42, and a heat medium expansion turbine 608 that lowers the temperature by expanding the heat medium is provided downstream of the heat medium compressor 42 in the heat pump pipe 607. ing.
- the heat medium expansion turbine 608 obtains rotational power when the heat medium is expanded.
- the first rich amine heat exchanger 605 is interposed in the heat pump pipe 607 downstream of the heat medium compressor 42 and upstream of the heat medium expansion turbine 608, and in the rich supply path 4 It is interposed downstream from the container 604.
- the pressure reducing / expansion valve 31 of the mixed gas cooling system 20 is provided in the discharge passage 33, and condensate is provided between the gas-liquid separator 32 and the fourth nozzle 28 in the pipe 29 of the mixed gas cooling system 20.
- a level adjustment valve 609 is provided instead of the circulation pump 29a. Further, in the illustrated example, the condensation heat exchanger 34 is not provided.
- a second rich amine heat exchanger (a twelfth heat exchanger) 610 that performs heat exchange between the temperature rising mixed gas and the rich absorbent is provided between the mixed gas cooling system 20 and the rich supply path 4. Intervene. Furthermore, between the mixed gas cooling system 20 and the rich supply path 4, a third rich amine heat exchange (which exchanges heat between the temperature-increased mixed gas and the rich absorbent after passing through the second rich amine heat exchange 610 ( (13th heat exchanger) 611 is interposed.
- the second rich amine heat exchanger 610 is interposed downstream of the mixed gas compressor 30 and upstream of the gas-liquid separator 32 in the piping 29 of the mixed gas cooling system 20, and is richly supplied. In the path 4, it is interposed downstream from the first rich amine heat exchanger 605.
- the third rich amine heat exchanger 611 is interposed upstream of the pressure reducing / expansion valve 31 in the discharge passage 33 of the mixed gas cooling system 20, and the two rich branch passages 602 and 603 in the rich supply passage 4. Of these, the other branch 603 different from one rich branch 602 is interposed.
- the rich absorption liquid passing through one rich branch path 602 is heated while cooling the lean absorption liquid by exchanging heat with the lean absorption liquid in the lean supply path 5 by the amine heat exchange 36. Further, the rich absorbing liquid passing through the other rich branch 603 is exchanged with the carbon dioxide main gas in the discharge passage 33 of the mixed gas cooling system 20 by the third rich amine heat exchange 611, thereby Receives heat and is heated.
- the rich absorbent heated through the rich branch paths 602 and 603 merges in the rich amine collector 604, and then exchanges heat with the heat medium of the heat pump 6 in the first rich amine heat exchanger 605. Heat is received from the heat medium and heated. Thereafter, the rich absorbent is further heated by cooling the heated mixed gas by exchanging heat with the heated mixed gas in the discharge passage 33 of the mixed gas cooling system 20 in the second rich amine heat exchanger 610. The rich absorbent heated as described above is then supplied to the third nozzle 16.
- the mixed gas that has risen in the regeneration tower 3 passes through the pipe 29 of the mixed gas cooling system 20 and is first compressed by the mixed gas compressor 30 to rise in temperature and become a heated mixed gas. Thereafter, in the second rich amine heat exchanger 610, heat exchange with the rich absorbing liquid in the rich supply path 4 is performed to recover the latent heat of the solute and solvent vapor, and the solute and solvent vapor are condensed. To condensate.
- the condensate and the non-condensed carbon dioxide main gas mainly composed of carbon dioxide gas are separated by the gas-liquid separator 32, and among these, the condensate passes through the pipe 29 and enters the regeneration tower 3.
- the fourth nozzle 28 is supplied to the tower top 3b.
- the uncondensed carbon dioxide main gas passes through the discharge path 33, and in the third rich amine heat exchange 611, exchanges heat with the rich absorption liquid that passes through the one rich branch path 602, so that the sensible heat of the gas and After the latent heat of a part of the remaining steam is recovered, the steam is expanded by the pressure reduction / expansion valve 31 and is discharged at a reduced temperature. At this time, the latent heat of the vapor of the solute and the solvent is recovered to condense the vapor of the solute and the solvent in the carbon dioxide main gas, and the sensible heat of the carbon dioxide gas in the carbon dioxide main gas Collected.
- the heat medium whose temperature has been lowered by the heat medium expansion turbine 608 passes through the heat pump pipe 607 and then exchanges heat with the absorption liquid while moving from the lower part to the upper part of the heat exchange 37 inside the absorption tower.
- the heat of the exothermic reaction is received while cooling.
- the heat medium is compressed by the heat medium compressor 42 through the heat pump pipe 607, and after the temperature rises, heat exchange with the rich absorption liquid is performed in the first rich amine heat exchanger 605 to heat the rich absorption liquid.
- it is cooled.
- the heat medium moves through the heat pump pipe 607 toward the lower part of the heat exchange 37 inside the absorption tower. At this time, the temperature of the heat medium is lowered again by the heat medium expansion turbine 608.
- the mixed gas cooling system 20 includes the mixed gas compressor 30. Therefore, by applying a slight amount of external power, a temperature rising mixed gas can be obtained without heating from the outside. Further, the second rich amine heat exchanger 610 is interposed between the mixed gas cooling system 20 and the rich supply path 4. Therefore, heat exchange is performed between the temperature-increased mixed gas of the mixed gas cooling system 20 and the rich absorbent in the rich supply path 4, so that the heat supplied by the mixed gas flowing out of the regeneration tower 3 is supplied to the regeneration tower 3. The temperature rising mixed gas can be cooled while heating the rich absorbent.
- the rich absorption liquid supplied to the regeneration tower 3 can be preheated, the amount of heat that the rich absorption liquid needs to receive in the regeneration tower 3 can be suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be suppressed, and energy saving can be effectively achieved.
- the second rich amine heat exchange 610 and the third rich amine heat exchange 611 are interposed between the mixed gas cooling system 20 and the rich supply path 4. Therefore, it is possible to effectively preheat the rich absorption liquid supplied to the regeneration tower 3, and the amount of heat that the rich absorption liquid needs to receive in the regeneration tower 3 can be further suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the temperature rising mixed gas of the mixed gas cooling system 20 passes through the third rich amine heat exchange 611 after passing through the second rich amine heat exchange 610. Therefore, for example, after the latent heat of the vapors of the solute and the solvent in the temperature rising mixed gas is recovered by the second rich amine heat exchanger 610, the sensible heat of the non-condensed carbon dioxide main gas and the remaining latent heat are third rich. It can be recovered by amine heat exchanger 611.
- the first rich amine heat exchange 605 is interposed between the rich supply path 4 and the heat pump 6, heat exchange is performed between the rich absorbent in the rich supply path 4 and the heat medium of the heat pump 6.
- the rich absorption liquid supplied to the regeneration tower 3 can be received by the heat of the heat medium so that the rich absorption liquid can be heated.
- the rich absorption liquid supplied to the regeneration tower 3 can be preheated, the amount of heat that the rich absorption liquid needs to receive in the regeneration tower 3 can be suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the amine heat exchange 36 when the amine heat exchange 36 is interposed between the lean supply path 5 and the rich supply path 4, the amount of heat for heating the rich absorbent is reduced by the amine heat exchange 36, The amount of heat to be given to the absorbent by the reboiler system 19 can be further suppressed. Therefore, the amount of heat input from the outside in the reboiler system 19 can be further suppressed, and further energy saving can be achieved.
- the heat pump 6 is not provided with the regeneration tower internal heat exchange 38, but may be provided.
- the condensation heat exchanger 34 is not provided, but this may be provided.
- the third rich amine heat exchanger 611 is provided, but this may not be provided.
- the technical scope of the present invention is not limited to the above embodiment, and various modifications can be made without departing from the spirit of the present invention.
- the temperature of the temperature rising mixed gas is decreased by the pressure reducing / expansion valve 31, but an expansion turbine may be adopted instead. In this case, rotational power can be obtained when the temperature rising mixed gas is expanded.
- the second rich amine heat exchanger 610 shown in the seventh embodiment is not provided. However, this may be provided. Furthermore, in the first to sixth embodiments, the condensation heat exchanger 34 is provided, and in the seventh embodiment, the second rich amine heat exchanger 610 is provided. However, these may be omitted.
- the carbon dioxide gas recovery apparatus can save energy by suppressing the amount of heat input from the outside.
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Abstract
Description
本願は、2010年03月31日に日本出願された特願2010-080237に基づいて優先権を主張し、その内容をここに援用する。
また、再生塔1002には、再生塔1002からリーン吸収液を導出して加熱し、再生塔1002に再導入するリボイラー系統1003と、二酸化炭素ガスと吸収液の溶質および溶媒(例えば、水)の蒸気分との混合ガスを再生塔1002から導出して冷却し、混合ガス中の前記溶質および溶媒の蒸気分を凝縮させて再生塔1002に再導入するとともに、未凝縮の二酸化炭素ガスを排出する混合ガス冷却系統1004と、が設けられている。
ここで、前記従来の二酸化炭素ガス回収装置1000では、リボイラー系統1003での外部からの入熱量を抑え、更なる省エネルギー化を図ることが望まれている。
本発明に係る二酸化炭素ガス回収装置は、二酸化炭素ガスを含有する二酸化炭素含有ガスと、リーン吸収液と、を導入して接触させ、前記二酸化炭素含有ガス中の前記二酸化炭素ガスを吸収液に吸収させてリッチ吸収液を生成する吸収塔と、前記吸収塔から供給された前記リッチ吸収液を加熱して前記二酸化炭素ガスを分離させることにより前記リーン吸収液に再生する再生塔と、を備えた二酸化炭素ガス回収装置であって、前記再生塔には、前記再生塔から吸収液を導出して加熱し、前記再生塔に再導入するリボイラー系統と、前記二酸化炭素ガスと前記吸収液の溶質および溶媒の蒸気分との混合ガスを前記再生塔から導出して冷却し、前記溶質および溶媒の蒸気分を凝縮させて、凝縮液を前記再生塔に再導入するとともに、前記二酸化炭素ガスを排出する混合ガス冷却系統とが設けられ、前記吸収塔で前記吸収液が前記二酸化炭素ガスを吸収するときの発熱反応で生じた熱を熱媒体を介して移動させ、前記再生塔で前記リッチ吸収液から前記二酸化炭素ガスが分離するときの吸熱反応の熱源として利用するヒートポンプを備えている。
ここで吸収液とは、リーン吸収液、リッチ吸収液、もしくはリーン吸収液とリッチ吸収液との混合液を意味する。
これにより、吸収塔での発熱反応で生じた熱を、再生塔での吸熱反応の熱源として効果的に利用することが可能になり、更なる省エネルギー化を図ることができる。さらにこの場合、吸収液の温度の低下による吸収速度の向上も起こるので、さらなる装置効率の向上も図れる。
これにより、吸収塔での発熱反応で生じた熱を、再生塔での吸熱反応の熱源として効果的に利用することが可能になり、更なる省エネルギー化を図ることができる。
これにより、吸収塔の発熱反応で生じて脱炭酸ガスに受け渡された熱が外部に漏出するのを抑制することが可能になり、更なる省エネルギー化を図ることができる。
また、脱炭酸ガス洗浄系統とヒートポンプとの間に、前記第4熱交換器が介在しているので、脱炭酸ガス洗浄系統の洗浄液と、ヒートポンプの熱媒体と、で熱交換することで、洗浄液を冷却しつつ、熱媒体を加熱することができる。
これにより、吸収塔の発熱反応で生じて洗浄液に受け渡された熱が、外部に漏出するのを抑制することが可能になり、更なる省エネルギー化を図ることができる。
なお、当該二酸化炭素ガス回収装置が、再生塔から吸収塔にリーン吸収液を供給するリーン供給路を備え、リーン供給路とリッチ供給路との間に、リーン吸収液とリッチ吸収液とで熱交換するアミン熱交が介在し、第5熱交換器が、リッチ供給路においてアミン熱交よりも上流に介装されている場合、アミン熱交を通るリッチ吸収液を、前記第5熱交換器で冷却しておくことができる。これにより、アミン熱交において、リッチ供給路のリッチ吸収液と、リーン供給路のリーン吸収液と、での熱交換量を増加することが可能になり、リーン供給路のリーン吸収液を効果的に冷却することができ、再生塔から見た熱回収量を増やすことができる。したがって、例えば、リーン供給路においてアミン熱交よりも下流に、リーン吸収液を冷却するリーンアミンクーラーを設け、吸収塔に供給されるリーン吸収液を吸収塔に供給する前に予め冷却する場合であっても、この冷却による外部への熱ロスを低減することができる。
また、インタークーラー系統とヒートポンプとの間に、前記第6熱交換器が介在しているので、インタークーラー系統の吸収液と、ヒートポンプの熱媒体と、で熱交換することで、吸収液を冷却しつつ、熱媒体を加熱することができる。
これにより、吸収塔の発熱反応で生じて吸収液に受け渡された熱が、外部に漏出するのを抑制することが可能になり、更なる省エネルギー化を図ることができる。
これにより、吸収塔に供給されるリーン吸収液を冷却することが可能になり、吸収塔でのリーン吸収液による二酸化炭素ガスの吸収を促進することができる。
これにより、リボイラー系統での外部からの入熱量をより抑えることが可能になり、更なる省エネルギー化を図ることができる。
このように、再生塔に供給されるリッチ吸収液を予熱しておくことができるので、再生塔でリッチ吸収液が受け取る必要がある熱量を抑えることができる。したがって、リボイラー系統での外部からの入熱量をより抑えることが可能になり、更なる省エネルギー化を図ることができる。
なお、当該二酸化炭素ガス回収装置が、再生塔から吸収塔にリーン吸収液を供給するリーン供給路を備え、リーン供給路とリッチ供給路との間に、リーン吸収液とリッチ吸収液とで熱交換するアミン熱交が介在している場合、アミン熱交での加熱量に、第13熱交換器での加熱量が加算される結果、リッチ吸収液の予熱量が増大し、リボイラー系統によって吸収液に与えるべき熱量を更に抑えることができる。したがって、リボイラー系統での外部からの入熱量をより一層抑えることが可能になり、一層更なる省エネルギー化を図ることができる。
これにより、リボイラー系統での外部からの入熱量を確実に抑えることが可能になり、効果的に省エネルギー化を図ることができる。
このように、再生塔を流出する混合ガスの持つ熱量により、再生塔に供給されるリッチ吸収液を予熱しておくことができるので、再生塔でリッチ吸収液が受け取る必要がある熱量を抑えることができる。したがって、リボイラー系統での外部からの入熱量をより抑えることが可能になり、一層の省エネルギー化を図ることができる。
このように、再生塔を流出する混合ガスの持つ熱量により、再生塔に供給されるリッチ吸収液を予熱しておくことができるので、再生塔でリッチ吸収液が受け取る必要がある熱量を抑えることができる。したがって、リボイラー系統での外部からの入熱量を確実に抑えることが可能になり、効果的に省エネルギー化を図ることができる。
以下、図面を参照し、本発明の第1実施形態に係る二酸化炭素ガス回収装置を説明する。この二酸化炭素ガス回収装置は、二酸化炭素ガスを含有する二酸化炭素含有ガスから二酸化炭素ガスをCO2化学吸収分離法によって吸収分離することで回収し、二酸化炭素含有ガスから二酸化炭素ガスが分離されてなる脱炭酸ガスを生成する。このCO2化学吸収分離法には、二酸化炭素ガスを吸収可能な吸収液を用いる。この吸収液としては、例えば、溶質としてモノエタノールアミン(MEA)やジエタノールアミン(DEA)等を採用し、溶媒として水を採用したアミン吸収液などを採用することができる。
なお本実施形態では、以下に示すようにいわゆる自己熱再生により二酸化炭素ガス回収装置の省エネルギー化を図る。
また吸収塔2には、吸収塔2の塔頂部2bから脱炭酸ガスを導出する導出路9と、吸収塔2の塔頂部2bに貯留された洗浄水(洗浄液)を吸収塔2から導出して冷却した後、吸収塔2の塔頂部2bから再導入する脱炭酸ガス洗浄系統10と、が設けられている。
配管13には、液受けトレー11から第2ノズル12に配管13を通して洗浄水を移送する洗浄水循環ポンプ13aと、この洗浄水循環ポンプ13aの下流において洗浄水を冷却する水冷式洗浄水クーラー15とが設けられている。
なお洗浄水は、吸収液の溶質と同一(例えば、水)であることが好ましい。ここで吸収液とは、リーン吸収液、リッチ吸収液、もしくはリーン吸収液とリッチ吸収液との混合液を意味する。
このとき、加熱された吸収液の一部がフラッシュし、吸収液の溶質および溶媒それぞれの一部が蒸気となる。このリボイラー系統19は、再生塔3の塔底部3a内に配設され吸収液が貯留された液受けトレー21と、液受けトレー21と塔底部3aにおいて液受けトレー21よりも下方に位置する蒸気発生部分22とを接続する配管23と、備えている。
配管23には、リボイラーポンプ24と、リボイラー本体25とが設けられている。リボイラーポンプ24は、液受けトレー21から前記蒸気発生部分22に配管23を通して吸収液を移送する。リボイラー本体25は、このリボイラーポンプ24の下流において外部から供給される熱を熱源として吸収液を加熱する。
図示の例では、リボイラー本体25は、リボイラー系統19と、外部から供給される高温流体(例えば、飽和蒸気)が流通するリボイラー配管26との間で熱交換する熱交換器で構成されている。リボイラー配管26には、リボイラー本体25よりも下流にスチームトラップ27が設けられている。
配管29には、混合ガスコンプレッサー30と、減圧・膨張弁31と、気液分離器32と、凝縮液循環ポンプ29aとが、再生塔3の塔頂から第4ノズル28までの間においてこの順に設けられている。混合ガスコンプレッサー30は、混合ガスを圧縮することで温度を上昇させ昇温混合ガスとする。減圧・膨張弁31は、昇温混合ガスを膨張させることで温度を低下させる。気液分離器32は、凝縮液と二酸化炭素ガスとを分離する。凝縮液循環ポンプ29aは、凝縮液を気液分離器32から第4ノズル28に配管29を通して移送する。
気液分離器32には、この気液分離器32により混合ガスから分離された二酸化炭素ガスを排出する排出路33が設けられている。
図示の例では、凝縮熱交換器34には、リボイラー本体25によって加熱される前の吸収液が通る。この凝縮熱交換器34は、リボイラー系統19の配管23においてリボイラーポンプ24とリボイラー本体25との間に介装されるとともに、混合ガス冷却系統20の配管29において混合ガスコンプレッサー30と減圧・膨張弁31との間に介装されている。
また、リーン供給路5とリッチ供給路4との間には、リーン吸収液とリッチ吸収液とで熱交換するアミン熱交36が介在している。
また、再生塔内部熱交38は、再生塔充填物18を縦断するように介装され、圧縮されて温度が上昇した熱媒体と、再生塔3内の吸収液と、で熱交換する。
はじめに、吸収液の流れについて、吸収塔2を起点として説明する。
まず吸収塔2では、塔底部2aに供給された二酸化炭素含有ガスが内部を上昇するとともに、塔頂部2b内の第1ノズル7から供給されたリーン吸収液が内部を下降する。この過程で、二酸化炭素含有ガスとリーン吸収液とが接触し、二酸化炭素含有ガス中の二酸化炭素ガスが、リーン吸収液に吸収されて発熱反応が生じる。
なお本実施形態では、吸収塔2に前記脱炭酸ガス洗浄系統10が設けられているので、水冷式洗浄水クーラー15で冷却され再導入された洗浄水によって吸収塔2の塔頂部2b内を冷却することができる。したがって、例えば、吸収液中の溶質が飛散もしくは蒸発して脱炭酸ガスに随伴して上昇したとしても、導出路9に到達する前に溶質は脱炭酸ガス洗浄系統10に供給される。これにより、吸収液中の溶質が吸収塔2の塔頂部2bから導出路9を通して外部に流出することを抑制することができる。
熱媒膨張弁41で温度が低下した熱媒体は、前記一方の配管39を通った後、吸収塔内部熱交37の下部から上部に向けて移動しながら、吸収液と熱交換することで、吸収液を冷却しつつ、吸収液が二酸化炭素を化学吸収する際に発生する発熱反応の熱を受け取り蒸発して気化する。その後、熱媒体は前記他方の配管40を通って再生塔内部熱交38の下部に移動する。このとき、熱媒体は熱媒コンプレッサー42によって圧縮され、温度が上昇する。
さらに、ヒートポンプ6が前記再生塔内部熱交38を備えているので、熱媒体により移動した発熱反応で生じた熱を、再生塔3での吸熱反応の熱源として損失少なく高効率に利用することができる。
以上により、外部加熱する一方で冷却水に廃熱するというエネルギーの消費をすることなく、吸収塔2で吸収液が二酸化炭素を化学吸収する発熱反応で生じた熱を、再生塔3で吸収液から二酸化炭素を分離再生する吸熱反応の熱源として効果的に利用することが可能になり、更なる省エネルギー化を図ることができる。
このように、再生塔3を流出する混合ガスの持つ熱量により、再生塔3に供給されるリッチ吸収液を予熱しておくことができる。その結果、リボイラー系統19での外部からの入熱量を確実に抑えることが可能になり、効果的に省エネルギー化を図ることができる。
(1)反応熱の自己熱再生効果
吸収塔2での反応発熱量は、再生塔3での反応吸熱量に等しい。よって、ヒートポンプ6に要する僅かな動力で、従来外部から加熱により与えていた反応熱は、プロセス内部の熱の授受で賄い、外部との熱の授受を無くすことができる。その結果、再生塔3のリボイラー系統19で加えていた外部熱量が従来に比べて低減される。
(2)塔操作に要する潜熱の自己熱再生
再生塔3の塔頂部3bから流出する混合ガスの熱量は、リボイラー系統19で外部から加熱し、吸収液の溶質および溶媒を蒸発させるために消費した熱量から吸収液再生のために要する反応吸熱量を引いたものに等しい。よって混合ガスを圧縮する僅かな動力で、昇温混合ガスを得て、凝縮熱交換器34で、前記混合ガスの熱をリボイラー系統19に与えることができれば、リボイラー系統19で外部から加えるべき熱量は低減する。さらに厳密に言えば、加えるべき熱量は、アミン熱交36での回収漏れ熱量(アミン熱交36から流出するリーン吸収液の顕熱量とアミン熱交36に流入するリッチ吸収液の顕熱熱量との差違)と再生塔3廻りの放熱量の和に見合う熱量になる。
次に、本発明に係る第2実施形態の二酸化炭素ガス回収装置を説明する。
なお、この第2実施形態においては、第1実施形態における構成要素と同一の部分については同一の符号を付し、その説明を省略し、異なる点についてのみ説明する。
これらの脱炭酸ガスクーラー102、洗浄水クーラー103およびリッチアミン熱交換器104は、ヒートポンプ6において熱媒膨張弁41によって膨張して温度が低下した熱媒体が通り、熱媒体が熱を受け取る熱回収側に介在している。
またリッチ供給路4には、吸収塔底ポンプ17よりも下流で、かつアミン熱交36よりも上流にリッチアミン熱交換器104が介装されている。
熱媒膨張弁41により温度が低下した熱媒体は、第1配管105を通った後、熱媒分配器109で分岐された2つの分岐配管106、107を通る。
また、前記他方の分岐配管107を通る熱媒体は、リッチアミン熱交換器104において、吸収塔2から流出するリッチ吸収液の熱を受け取って加熱される。
これにより、吸収塔2の発熱反応で生じて脱炭酸ガスに受け渡された熱が外部に漏出するのを抑制することが可能になり、更なる省エネルギー化を図ることができる。
これにより、吸収塔2の発熱反応で生じて脱炭酸ガスから洗浄水に受け渡された熱が、外部に漏出するのを抑制することが可能になり、更なる省エネルギー化を図ることができる。
また本実施形態では、リッチアミン熱交換器104が、リッチ供給路4においてアミン熱交36よりも上流に介装されているので、アミン熱交36を通るリッチ吸収液を、前記リッチアミン熱交換器104で冷却しておくことができる。これにより、アミン熱交36において、リッチ供給路4のリッチ吸収液と、リーン供給路5のリーン吸収液と、での熱交換量を増加することが可能になり、リーン供給路5のリーン吸収液を効果的に冷却することができ、再生塔から見た熱回収量を増やすことができる。したがって、例えば、リーン供給路5においてアミン熱交36よりも下流に、リーン吸収液を冷却する図示しないリーンアミンクーラーを設け、吸収塔2に供給されるリーン吸収液を吸収塔2に供給する前に予め冷却する場合であっても、この冷却による外部への熱ロスを低減することができる。
なお本実施形態では、ヒートポンプ6は、吸収塔内部熱交37を備えていないものとしたが、これを備えていても良い。
次に、本発明に係る第3実施形態の二酸化炭素ガス回収装置を説明する。
なお、この第3実施形態においては、第2実施形態における構成要素と同一の部分については同一の符号を付し、その説明を省略し、異なる点についてのみ説明する。また図3では、図面の見易さのため、第2実施形態における構成要素と同一の部分については一部、図示を省略している。
配管204には、液受けトレー202から第5ノズル203に配管204を通して吸収液を移送するインタークーラーポンプ205が設けられている。
またリーン供給路5には、アミン熱交36よりも下流に熱媒冷却式リーンアミンクーラー207が介装されている。
熱媒膨張弁41により温度が低下した熱媒体は、第2配管108を通った後、熱媒分配器109で分岐された5つの分岐配管208を通る。
また、熱媒冷却式リーンアミンクーラー207が介装された分岐配管208を通る熱媒体は、熱媒冷却式リーンアミンクーラー207において、リーン吸収液を冷却しつつ加熱される。
そして、各分岐配管208を通った熱媒体は熱媒集合器110で合流する。
これにより、従来は冷却水に廃熱していたリーン吸収液の熱を、廃熱することなく熱媒体の熱として回収することができる。また、吸収塔2に供給されるリーン吸収液を冷却することが可能になり、吸収塔2での吸収液による二酸化炭素ガスの吸収を促進することができる。
これにより、吸収塔2の発熱反応で生じて吸収液に受け渡された熱が、外部に漏出するのを抑制することが可能になり、更なる省エネルギー化を図ることができる。
次に、本発明に係る第4実施形態の二酸化炭素ガス回収装置を説明する。
なお、この第4実施形態においては、第1実施形態における構成要素と同一の部分については同一の符号を付し、その説明を省略し、異なる点についてのみ説明する。
また、再生塔3に設けられた前記リボイラー系統19の配管23におけるリボイラーポンプ24と凝縮熱交換器34との間にはリボイラー分配器306が設けられており、このリボイラー分配器306からは、再生塔3の塔底部3aに接続される枝配管307が分岐されている。
これらの熱媒式リボイラーヒーター308、第2リッチアミン熱交309および前記再生塔内部熱交38は、ヒートポンプ6において熱媒コンプレッサー42によって圧縮されて温度が上昇した熱媒体が通り、熱媒体が熱を受け渡す熱供給に介在している。
なお図示の例では、リボイラー系統19では、枝配管307に熱媒式リボイラーヒーター308が介装されるとともに、リッチ供給路4では、2つのリッチ分岐路302、303のうち、前記一方のリッチ分岐路302とは異なる他方のリッチ分岐路303に第2リッチアミン熱交309が介装されている。第2リッチアミン熱交309は、リッチ供給路4においてアミン熱交36よりも上流に介装されている。
また、第2の分岐配管311を通る熱媒体は、熱媒式リボイラーヒーター308において、リボイラー系統19の吸収液と熱交換することで、その熱を吸収液に受け渡して加熱する。
さらに、第3の分岐配管312を通る熱媒体は、リッチ供給路4のリッチ吸収液と熱交換することで、その熱をリッチ吸収液に受け渡して加熱する。
これにより、リボイラー系統19での外部からの入熱量をより抑えることが可能になり、更なる省エネルギー化を図ることができる。
このように、再生塔3に供給されるリッチ吸収液を予熱しておくことができるので、再生塔3でリッチ吸収液が受け取る必要がある熱量を抑えることができる。したがって、リボイラー系統19での外部からの入熱量をより抑えることが可能になり、更なる省エネルギー化を図ることができる。
また本実施形態のように、リーン供給路5とリッチ供給路4との間に前記アミン熱交36が介在している場合、アミン熱交36での加熱量に、前記第2リッチアミン熱交309での加熱量が加算される結果、リッチ吸収液の予熱量が増大し、リボイラー系統19によって吸収液に与えるべき熱量を更に抑えることができる。したがって、リボイラー系統19での外部からの入熱量をより一層抑えることが可能になり、一層更なる省エネルギー化を図ることができる。
次に、本発明に係る第5実施形態の二酸化炭素ガス回収装置を説明する。
なお、この第5実施形態においては、第2実施形態における構成要素と同一の部分については同一の符号を付し、その説明を省略し、異なる点についてのみ説明する。
図示の例では、ヒートポンプ6の複数の配管404、405は、熱媒集合器110と熱媒分配器109とを接続するとともに前記熱媒コンプレッサー42が設けられた主配管404と、熱媒分配器109と熱媒集合器110とを接続する3つの分岐配管405と、からなる。
また、各分岐配管405には、熱媒冷却式の脱炭酸ガスクーラー102、熱媒冷却式の洗浄水クーラー103および熱媒冷却式のリッチアミン熱交換器104のいずれかが介装されている。
これにより、リボイラー系統19での外部からの入熱量をより抑えることが可能になり、更なる省エネルギー化を図ることができる。
なお、ヒートポンプ6は、前記再生塔内部熱交38を備えていないものとしたが、これを備えていても良い。
次に、本発明に係る第6実施形態の二酸化炭素ガス回収装置を説明する。
なお、この第6実施形態においては、第1実施形態における構成要素と同一の部分については同一の符号を付し、その説明を省略し、異なる点についてのみ説明する。また図6では、図面の見易さのためにヒートポンプ6の図示を省略している。
また、リーン供給路5には、リーン吸収液を冷却するリーンアミンクーラー502がアミン熱交36よりも下流に設けられている。
気液分離器32は、凝縮熱交換器34で凝縮された前記溶質および溶媒の蒸気分である凝縮液と、未凝縮の前記溶質および溶媒の蒸気分および二酸化炭素ガスからなる未凝縮の残りの昇温混合ガスと、を分離する。この気液分離器32には、排出路33に代えて、後述する他の気液分離器505を経て再生塔3の塔頂部3bに接続された残ガス流通路504が設けられている。
他の気液分離器505には、前記排出路33が設けられている。
また、3つのリッチ分岐路508、509、510のうちの第2リッチ分岐路509と、前記リボイラー配管26と、の間には、リッチ吸収液と高温流体とで熱交換する第2リッチアミン熱交513が介在している。第2リッチアミン熱交513は、リボイラー配管26においてスチームトラップ27よりも下流に介装されている。
第3リッチアミン熱交514は、3つのリッチ分岐路508、509、510のうちの第3リッチ分岐路510に介装されているとともに、残ガス流通路504において減圧・膨張弁31よりも上流に介装されている。
はじめに、リッチ供給路4でのリッチ吸収液の流れについて説明する。
リッチ供給路4を通るリッチ吸収液は、リッチアミン分配器507に到達した後、3つの分岐路508、509、510に分岐される。
また、第2リッチ分岐路509を通るリッチ吸収液は、第2リッチアミン熱交513で、リボイラー配管26の高温流体と熱交換することで、高温流体から熱を受け取り加熱される。
さらに、第3リッチ分岐路510を通るリッチ吸収液は、第3リッチアミン熱交514で、残ガス流通路504を流通する前記残りの昇温混合ガスと熱交換することで、前記残りの昇温混合ガスを冷却しつつ加熱される。
再生塔3内を上昇した混合ガスは、混合ガス冷却系統20の配管29を通り、まず混合ガスコンプレッサー30によって圧縮され温度が上昇して昇温混合ガスとなる。その後、凝縮熱交換器34で、リボイラー系統19の吸収液と熱交換することで、前記溶質および溶媒の蒸気分が持つ潜熱が回収され、前記溶質および溶媒の蒸気分の少なくとも一部が凝縮されて、凝縮液となる。
次いで、気液分離器32により、前記凝縮液と、未凝縮の前記残りの昇温混合ガスと、が分離され、これらのうち、凝縮液は、配管29を通り再生塔3の塔頂部3bに前記第4ノズル28から供給される。
(3)塔操作に要する顕熱の自己熱再生
再生塔3に流入するリッチ吸収液に含まれる二酸化炭素に相当する顕熱量は、前記残りの昇温混合ガスのガス顕熱に等しい。よって混合ガスを圧縮する僅かな動力で昇温混合ガスを得て、第3リッチアミン熱交514により、その顕熱を回収すれば、再生塔に導入されるリッチ吸収液の予熱量が増加して、リボイラー系統19で外部から加えるべき熱量は低減する。さらに厳密に言えば、加えるべき熱量は、アミン熱交36での回収漏れ熱量(アミン熱交36を流出するリーン吸収液の顕熱量とアミン熱交36に流入するリッチ吸収液の顕熱量との差違)からリッチ吸収液に含まれる二酸化炭素の顕熱相当熱量を除いた熱量と、再生塔3廻りの放熱量に見合う熱量と、の和になる。
さらにアミン熱交36の伝熱面積を大きく設定し、アミン熱交36での回収漏れ熱量をゼロに近づけると、リボイラー系統19で外部から加えるべき熱量は再生塔3廻りの放熱量だけに見合う熱量にまで低減する。放熱は保温の程度で制御できることから、最終的にリボイラー系統19で外部から加えるべき熱量は、ゼロ近傍とすることが可能となる。
この場合、例えば、気液分離器32で、昇温混合ガス中の前記溶質および溶媒の蒸気分の全てが二酸化炭素ガスから分離されるように、気液分離器32よりも上流で、昇温混合ガス中の前記溶質および溶媒の蒸気分の全てが凝縮されるように、混合ガス冷却系統20を構成しても良い。
次に、本発明に係る第7実施形態の二酸化炭素ガス回収装置を説明する。
なお、この第7実施形態においては、第1実施形態における構成要素と同一の部分については同一の符号を付し、その説明を省略し、異なる点についてのみ説明する。
2つのリッチ分岐路602、603のうち、一方のリッチ分岐路602とリーン供給路5との間には、前記アミン熱交36が介在している。
また第3リッチアミン熱交611は、混合ガス冷却系統20の排出路33において減圧・膨張弁31よりも上流に介装されるとともに、リッチ供給路4において、2つのリッチ分岐路602、603のうち、一方のリッチ分岐路602と異なる他方の分岐路603に介装されている。
はじめに、リッチ供給路4でのリッチ吸収液の流れについて説明する。
リッチ供給路4を通るリッチ吸収液は、リッチアミン分配器601に到達した後、2つのリッチ分岐路602、603に分岐される。
また、他方のリッチ分岐路603を通るリッチ吸収液は、第3リッチアミン熱交611で、混合ガス冷却系統20の排出路33の二酸化炭素主体ガスと熱交換することで、二酸化炭素主体ガスから熱を受け取り加熱される。
以上のようにして加熱されたリッチ吸収液は、その後、前記第3ノズル16に供給される。
再生塔3内を上昇した混合ガスは、混合ガス冷却系統20の配管29を通り、まず混合ガスコンプレッサー30によって圧縮され温度が上昇して昇温混合ガスとなる。その後、第2リッチアミン熱交610で、リッチ供給路4のリッチ吸収液と熱交換することで、前記溶質および溶媒の蒸気分が持つ潜熱が回収され、前記溶質および溶媒の蒸気分が凝縮されて凝縮液となる。
熱媒膨張タービン608で温度が低下した熱媒体は、ヒートポンプ配管607を通った後、吸収塔内部熱交37の下部から上部に向けて移動しながら、吸収液と熱交換することで、吸収液を冷却しつつ発熱反応の熱を受け取る。
そして熱媒体は、ヒートポンプ配管607を通って、熱媒コンプレッサー42によって圧縮され、温度が上昇した後、第1リッチアミン熱交605で、リッチ吸収液と熱交換することで、リッチ吸収液を加熱しつつ冷却される。その後、熱媒体は、ヒートポンプ配管607を通って、吸収塔内部熱交37の下部に向けて移動する。このとき、熱媒体は熱媒膨張タービン608により再び温度が低下する。
例えば、前記各実施形態では、混合ガス冷却系統20では、減圧・膨張弁31で昇温混合ガスの温度を低下させたが、これに代えて膨張タービンを採用しても良い。この場合、昇温混合ガスを膨張させるときに回転動力を得ることができる。
2 吸収塔
2a 塔底部
2b 塔頂部
2c 塔中間部
3 再生塔
4 リッチ供給路
5 リーン供給路
6 ヒートポンプ
8 吸収塔充填物
9 導出路
10 脱炭酸ガス洗浄系統
18 再生塔充填物
19 リボイラー系統
20 混合ガス冷却系統
26 リボイラー配管
30 混合ガスコンプレッサー(混合ガス圧縮機)
34 凝縮熱交換器(第10熱交換器)
37 吸収塔内部熱交(第1熱交換器)
38 再生塔内部熱交(第2熱交換器)
102 脱炭酸ガスクーラー(第3熱交換器)
103 洗浄水クーラー(第4熱交換器)
104 リッチアミン熱交換器(第5熱交換器)
201、501 インタークーラー系統
206 熱媒冷却式インタークーラー(第6熱交換器)
207 熱媒冷却式リーンアミンクーラー(第7熱交換器)
308、403 熱媒式リボイラーヒーター(第8熱交換器)
309 第2リッチアミン熱交(第9熱交換器)
514 第3リッチアミン熱交(第11熱交換器)
605 第1リッチアミン熱交(第9熱交換器)
610 第2リッチアミン熱交(第12熱交換器)
611 第3リッチアミン熱交(第13熱交換器)
Claims (14)
- 二酸化炭素ガスを含有する二酸化炭素含有ガスと、リーン吸収液と、を導入して接触させ、前記二酸化炭素含有ガス中の前記二酸化炭素ガスを吸収液に吸収させてリッチ吸収液を生成する吸収塔と、
前記吸収塔から供給された前記リッチ吸収液を加熱して前記二酸化炭素ガスを分離させることにより前記リーン吸収液を再生する再生塔と、を備えた二酸化炭素ガス回収装置であって、
前記再生塔には、
前記再生塔から吸収液を導出して加熱し、前記再生塔に再導入するリボイラー系統と、
前記二酸化炭素ガスと前記吸収液の溶質および溶媒の蒸気分との混合ガスを前記再生塔から導出して冷却し、前記溶質および溶媒の蒸気分を凝縮させて前記再生塔に再導入するとともに、前記二酸化炭素ガスを排出する混合ガス冷却系統と、
が設けられ、
前記吸収塔で前記吸収液が前記二酸化炭素ガスを吸収するときの発熱反応で生じた熱を熱媒体を介して移動させ、前記再生塔で前記リッチ吸収液から前記二酸化炭素ガスが分離するときの吸熱反応の熱源として利用するヒートポンプを備えている二酸化炭素ガス回収装置。 - 請求項1記載の二酸化炭素ガス回収装置であって、
前記ヒートポンプは、前記吸収塔内に配設された吸収塔充填物に介装され、膨張して温度が低下した前記熱媒体と、前記吸収塔内の前記吸収液と、で熱交換する第1熱交換器を備えている二酸化炭素ガス回収装置。 - 請求項1又は2に記載の二酸化炭素ガス回収装置であって、
前記ヒートポンプは、前記再生塔内に配設された再生塔充填物に介装され、圧縮され温度が上昇した前記熱媒体と、前記再生塔内の前記リッチ吸収液と、で熱交換する第2熱交換器を備えている二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記吸収塔には、前記二酸化炭素含有ガスから前記二酸化炭素ガスが分離されてなる脱炭酸ガスを導出する導出路が設けられ、
前記導出路と前記ヒートポンプとの間には、前記脱炭酸ガスと、膨張して温度が低下した前記熱媒体と、で熱交換する第3熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記吸収塔には、前記吸収塔の塔頂部に貯留された洗浄液を前記吸収塔から導出して冷却した後、前記吸収塔の塔頂部から再導入する脱炭酸ガス洗浄系統が設けられ、
前記脱炭酸ガス洗浄系統と前記ヒートポンプとの間には、前記洗浄液と、膨張して温度が低下した前記熱媒体と、で熱交換する第4熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記吸収塔から前記再生塔に前記リッチ吸収液を供給するリッチ供給路を備え、
前記リッチ供給路と前記ヒートポンプとの間には、前記リッチ吸収液と、膨張して温度が低下した前記熱媒体と、で熱交換する第5熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記吸収塔には、前記吸収塔における塔頂部と塔底部との間の塔中間部から前記吸収液を導出して冷却した後、前記塔中間部から再導入するインタークーラー系統が設けられ、
前記インタークーラー系統と前記ヒートポンプとの間には、前記吸収液と、膨張して温度が低下した前記熱媒体と、で熱交換する第6熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記再生塔から前記吸収塔に前記リーン吸収液を供給するリーン供給路を備え、
前記リーン供給路と前記ヒートポンプとの間には、前記リーン吸収液と、膨張して温度が低下した前記熱媒体と、で熱交換する第7熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記リボイラー系統と前記ヒートポンプとの間には、前記吸収液と、圧縮され温度が上昇した前記熱媒体と、で熱交換する第8熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記吸収塔から前記再生塔に前記リッチ吸収液を供給するリッチ供給路を備え、
前記リッチ供給路と前記ヒートポンプとの間には、前記リッチ吸収液と、圧縮して温度が上昇した前記熱媒体と、で熱交換する第9熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記混合ガス冷却系統は、前記混合ガスを圧縮して温度を上昇させ昇温混合ガスとする混合ガス圧縮機を備え、
前記リボイラー系統と前記混合ガス冷却系統との間には、前記吸収液と前記昇温混合ガスとで熱交換する第10熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項11記載の二酸化炭素ガス回収装置であって、
前記吸収塔から前記再生塔に前記リッチ吸収液を供給するリッチ供給路を備え、
前記混合ガス冷却系統と前記リッチ供給路との間には、前記第10熱交換器を通った後の前記昇温混合ガスと前記リッチ吸収液とで熱交換する第11熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項1に記載の二酸化炭素ガス回収装置であって、
前記吸収塔から前記再生塔に前記リッチ吸収液を供給するリッチ供給路を備え、
前記混合ガス冷却系統は、前記混合ガスを圧縮して温度を上昇させ昇温混合ガスとする混合ガス圧縮機を備え、
前記混合ガス冷却系統と前記リッチ供給路との間には、前記昇温混合ガスと前記リッチ吸収液とで熱交換する第12熱交換器が介在している二酸化炭素ガス回収装置。 - 請求項13記載の二酸化炭素ガス回収装置であって、
前記混合ガス冷却系統と前記リッチ供給路との間には、前記第12熱交換器を通った後の前記昇温混合ガスと前記リッチ吸収液とで熱交換する第13熱交換器が介在している二酸化炭素ガス回収装置。
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US9492783B2 (en) | 2016-11-15 |
US20130055756A1 (en) | 2013-03-07 |
JP2011212510A (ja) | 2011-10-27 |
TW201208758A (en) | 2012-03-01 |
CA2795028A1 (en) | 2011-10-06 |
JP5665022B2 (ja) | 2015-02-04 |
CA2795028C (en) | 2015-07-07 |
CN102869426A (zh) | 2013-01-09 |
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