WO2019078156A1 - 酸性ガス除去装置及び酸性ガス除去方法 - Google Patents
酸性ガス除去装置及び酸性ガス除去方法 Download PDFInfo
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- WO2019078156A1 WO2019078156A1 PCT/JP2018/038317 JP2018038317W WO2019078156A1 WO 2019078156 A1 WO2019078156 A1 WO 2019078156A1 JP 2018038317 W JP2018038317 W JP 2018038317W WO 2019078156 A1 WO2019078156 A1 WO 2019078156A1
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- reclaimer
- water
- reclaiming
- absorbent
- lean
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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
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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
- B01D53/1412—Controlling the absorption process
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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
- B01D53/1456—Removing acid components
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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
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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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
- B01D53/18—Absorbing units; Liquid distributors therefor
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
- B01D53/526—Mixtures of hydrogen sulfide and carbon dioxide
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/608—Sulfates
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
Definitions
- the present invention relates to an acid gas removal apparatus and an acid gas removal method including a reclaiming device for removing a degraded product accumulated in an absorbing liquid that absorbs acid gas in gas.
- coal gasification gas obtained by gasifying coal, natural gas, acid gas components (for example, , CO 2 , H 2 S, etc.).
- the gas containing such an acidic component is brought into gas-liquid contact with, for example, an amine-based acid gas absorbing liquid in the absorption tower to absorb the acid gas in the acid gas absorbing liquid, thereby removing the acid gas in the gas. , To collect.
- the acid gas absorbing liquid absorbs and removes acid gas in exhaust gas, gasification gas, etc. in the absorption tower, then dissipates the acid gas absorbed in the acid gas absorbing liquid in the regeneration tower and absorbs the regenerated acid gas
- a method is used in which the liquid is again supplied to the absorption column for reuse, and the acid gas absorption liquid is circulated and used in a closed circulation system between the absorption column and the regeneration column.
- a process of recovering acid gas components for example, CO 2 , SO 2, etc.
- the amine acid-based acid gas absorbing solution used is a heat stable amine salt (Heat Stable Amine Salt: HSAS) due to degradation of the degradation product in the processing gas and the acid gas absorbing solution itself.
- HSAS Heat Stable Amine Salt
- Degraded substances generated due to the acid gas absorbing liquid are highly corrosive, so they are supplied to a reclaiming device equipped with a reclaimer to remove the deteriorated substances in the acid gas absorbing liquid, and the absorbent for the acid gas absorbing liquid is used. There is a method of entraining the recovered steam and returning it to the circulation system.
- the degraded product is concentrated and recovered as a reclaimed residue by heating the absorbent containing the extracted degraded product in the reclaimer, and the absorbent component is returned to the circulation system as recovered vapor. Therefore, it is possible to prevent the accumulation of degraded matter in the circulation system through which the acid gas absorbing liquid passes.
- a part of the absorbing liquid component may remain in the reclaiming residue without evaporating. For this reason, the absorbent is lost, and it is necessary to supply the relatively expensive absorbent that has been lost.
- the present invention is an acidic gas removal apparatus capable of promoting the recovery time of a final reclaiming operation for recovering the absorbent remaining in the reclaiming residue after the completion of the reclaiming operation for removing non-volatile substances It is an object of the present invention to provide an acid gas removal method.
- a first invention of the present invention for solving the above-mentioned problems is an acidic gas absorption tower for removing an acidic gas by bringing an acidic gas in the gas into contact with an acidic gas absorbing liquid, and a rich solution which absorbs the acidic gas Are recovered by steam from the reboiler to make a lean solution, the lean solution is drawn out, a reclaimer introducing and storing this lean drawn solution, and an alkaline agent supply supplying an alkaline agent to the inside of the reclaimer A pipe, a water supply pipe for supplying feed water into the interior of the reclaimer, a recovered vapor discharge pipe for introducing recovered vapor discharged from the reclaimer into the acid gas absorption tower or the regeneration tower, and operation for the reclaimer And a reclaimer control device for controlling, wherein the reclaimer control device introduces the lean extracted liquid to the reclaimer, and the nonvolatile substance in the lean extracted liquid is introduced.
- the initial stage of the final reclaiming to recover the absorbent in the reclaiming residue after stopping the introduction of the lean drain solution while performing the first feed water control, the reflux water, the steam condensed water, While supplying at least one of the salt water into the reclaimer as the first feed water, and supplying the washing solution containing the acid gas absorbing liquid in the washing section of the acid gas absorber as the second feed water into the reclaimer.
- the feed water control is carried out, and the second stage of the final reclaiming is to stop the supply of the second feed water, and at least one of the reflux water, the steam condensed water, and the demineralized water.
- the third water supply control for supplying a first supply water.
- a second invention switching of execution of the second feed water control and the third feed water control is carried out in such a manner that the remaining concentration of the acid gas absorbent in the reclaiming residue is in the cleaning solution.
- the present invention is the acidic gas removal apparatus characterized in that it is when the concentration of the acidic gas absorbent is reached or when the concentration of the acidic gas absorbent in the cleaning liquid is approached.
- a third invention according to the first or second invention further comprises a thermometer for measuring the temperature in the reclaimer, and a pressure gauge for measuring the pressure in the reclaimer
- the reclaimer control device further comprises: The first to third feed water control is performed, and at the time of final reclaiming to recover the absorbent in the reclaiming residue after stopping the introduction of the lean extracted solution to the reclaimer, the lean removal to the reclaimer is performed.
- An acid gas removal apparatus characterized by executing pressure control to adjust the pressure in the reclaimer so that the temperature in the reclaimer is kept at the reference temperature when the introduction of the effluent is stopped. is there.
- the reclaimer control device when the pressure in the reclaimer reaches the upper limit pressure value of the upper limit of operation of the reclaimer, the reclaimer control device is a target standard so that the temperature falls below the reference temperature.
- An acid gas removal apparatus characterized in that the temperature is changed and the pressure in the reclaimer is adjusted to maintain the changed reference temperature.
- the change of the target reference temperature is a temperature range lower than a predetermined temperature from the reference temperature in the reclaimer when the introduction of the lean extract into the reclaimer is stopped. It is in the acid gas removal device characterized by the above.
- adjusting the pressure of the reclaimer control device installs a throttling valve in the recovered vapor discharge pipe, and the throttling valve It is in the acid gas removal device characterized by adjusting.
- the pressure adjustment of the reclaimer control device is characterized by adjusting a decompression device installed in the recovered vapor discharge pipe in the case of a decompression type reclaimer. It is in the acid gas removal device to
- the eighth invention is an acid gas absorption tower for removing an acid gas by bringing acid gas in the gas into contact with an acid gas absorbing liquid, and a rich solution which absorbs the acid gas by regenerating with a reboiler vapor to obtain a lean solution
- Acid gas removal step of removing acid gas by absorbing liquid regenerator and extracting a part of the lean solution regenerated in the regenerator, and continuously introducing this lean solution into the reclaimer for storage , Introduce alkaline agent and feed water, heat, recover non-volatile components in the lean extract while recovering the absorbent remaining from the lean extract as recovered vapor, and reclaiming for removal of non-volatile components
- first feed water control to feed at least one of reflux water from the regeneration tower, steam condensed water and demineralized water into the reclaimer as the first feed water to be fed to the water feed pipe
- at least one of the reflux water, steam condensed water, and demineralized water is supplied as the first feed water into the reclaimer at the initial stage of the finish reclaiming, and the washing portion of the acid gas absorber is
- a second feed water control is performed to supply a cleaning liquid containing an acid gas absorbing solution as a second feed water into the reclaimer, and the second phase of the final reclaiming is to stop the supply of the second feed water, and to supply the reflux water
- a third aspect of the present invention is an acid gas removal method characterized in that a third feed water control is performed to supply at least one of steam condensed water and demineralized water as a first feed water.
- a ninth invention according to the eighth invention switching of execution of the second feed water control and the third feed water control is carried out in such a manner that the residual concentration of the acid gas absorbent in the reclaiming residue is in the cleaning solution.
- the present invention is the acid gas removing method characterized in that the concentration of the acid gas absorbent is reached, or the concentration of the acid gas absorbent in the cleaning liquid is approached.
- the temperature in the reclaimer when the introduction of the lean drawn liquid to the reclaimer is stopped in the finish reclaiming step is a reference temperature
- the reference temperature is a reference temperature
- the remaining absorbent after stopping the supply of the lean drawn liquid to the reclaimer is recovered, and the cleaning fluid circulated in the cleaning section of the acidic gas absorption tower for recovering the acidic gas during the final reclaiming operation Reduce the operating time required to recover the absorbent in the residue in the reclaiming equipment to the same concentration, as compared to the supply condition of only the supply water where the cleaning solution is not supplied. Can.
- the pressure in the reclaimer is controlled, and the pressure in the reclaimer is adjusted to maintain the temperature of the reclaimer at a predetermined reference temperature, thereby making the absorbent in the reclaimer residue identical. It is possible to reduce the operation time required to recover the concentration.
- FIG. 1 is a schematic view of a recovery apparatus according to a first embodiment.
- FIG. 2 is a schematic view of the reclaiming device according to the first embodiment.
- FIG. 3 is a block diagram of a control system of the reclaiming device according to the first embodiment.
- FIG. 4 is a flowchart of control of the reclaiming device according to the first embodiment.
- FIG. 5 is a view showing the relationship between the reclaimer operation time and the residual absorbent concentration.
- FIG. 6 is a schematic view of a reclaiming device according to a second embodiment.
- FIG. 7 is a schematic view of a reclaiming device according to a third embodiment.
- FIG. 8 is a block diagram of a control system of the reclaiming device according to the third embodiment.
- FIG. 10A is a diagram showing the relationship between the finish reclaiming operation time and the temperature.
- FIG. 10B is a diagram showing the relationship between the finish reclaiming operation time and the pressure.
- FIG. 10C is a diagram showing the relationship between the finish reclaiming operation time and the absorbent vapor pressure.
- FIG. 10D is a diagram showing the relationship between finish reclaiming operation time and absorbent recovery rate.
- FIG. 11 is a schematic view of another reclaiming device according to the third embodiment.
- FIG. 12 is a schematic view of a reclaiming device according to a fourth embodiment.
- FIG. 13 is a block diagram of a control system of the reclaiming device according to the fourth embodiment.
- FIG. 14 is a flowchart of control of the reclaiming device according to the fourth embodiment.
- FIG. 15 is a schematic view of another reclaiming device according to a fourth embodiment.
- FIG. 1 is a schematic view of a recovery apparatus according to a first embodiment.
- Coal gasification gas, synthesis gas, coke oven gas, petroleum gas, natural gas and the like contain an acid gas such as CO 2 (carbon dioxide) and H 2 S (hydrogen sulfide).
- a recovery device for recovering CO 2 (carbon dioxide) and H 2 S (hydrogen sulfide) and a recovery device for recovering CO 2 (carbon dioxide) from combustion exhaust gas (hereinafter referred to as exhaust gas), as shown in FIG.
- cooling tower 102 cools exhaust gas 1001 discharged from industrial equipment such as a boiler with cooling water 1002, and amine absorption liquid such as aqueous alkanolamine aqueous solution absorbing CO 2 in exhaust gas 1001 as shown in FIG.
- the exhaust gas 1001 containing CO 2 is pressurized by the exhaust gas blower 102a and then sent into the cooling tower 102, where it is cooled in countercurrent contact with the cooling water 1002 (exhaust gas cooling step) .
- the cooling water 1002 is accumulated in the lower part in the cooling tower 102, and is supplied to the upper part in the cooling tower 102 through the cooling water pipe 102c outside the cooling tower 102 by the humidified cooling water circulation pump 102b. Then, the cooling water 1002 makes countercurrent contact with the exhaust gas 1001 in the process of reaching the lower part in the cooling tower 102.
- the cooling water pipe 102c is provided with a cooler 102d for cooling the cooling water 1002.
- the cooled exhaust gas 1001 is discharged from the cooling tower 102 through the exhaust gas pipe 102 e and supplied to the absorption tower 103.
- the exhaust gas 1001 is brought into countercurrent contact with the absorption liquid 1003 (lean solution 1003a) based on the alkanolamine in the absorption section 1003A, and the CO 2 in the exhaust gas 1001 is absorbed into the absorption liquid 1003. Thereby, CO 2 is removed from the exhaust gas 1001 (CO 2 removal step).
- the exhaust gas 1001 from which the CO 2 has been removed is removed by contact between the cleaning fluid 1003 f circulating in the circulation line 1003 e and the exhaust gas 1001 in the cleaning unit 1003 B provided on the gas flow downstream side of the absorbing unit 1003 A to remove CO 2.
- the CO 2 absorbent entrained in the collected gas is recovered by the cleaning liquid 1003f.
- Reference numeral 1003g is a circulation pump for circulating the cleaning liquid 1003f
- 1003h is a cooler for cooling the cleaning liquid 1003f
- 1003i is a cleaning liquid storage part for storing the cleaning liquid.
- the absorbing solution 1003 (lean solution 1003a) is pressure-fed from the regenerator 104 by the absorbing solution supply pump 103a, and is supplied from the outside of the absorber 103 to the upper portion in the absorber 103 via the lean solution pipe 103b. Then, the absorbing liquid 1003 makes a countercurrent contact with the exhaust gas 1001 in the process of reaching the lower portion in the absorber 103.
- the lean solution pipe 103b is provided with a cooler 103c for cooling the absorbing liquid 1003 supplied to the absorption tower 103.
- Absorbent liquid 1003 (rich solution 1003b) which absorbed CO 2 is accumulated in the lower part in absorption tower 103, is discharged to the outside of absorption tower 103 through rich solution pipe 104b, and is pumped by absorption liquid discharge pump 104a while being regenerated It is supplied to the upper part in 104.
- the rich solution 1003b of the absorbing solution 1003 is a semi-lean solution in which most of the CO 2 is released by the endothermic reaction, and this semi lean solution reaches almost all of the lower portion in the regeneration tower 104.
- CO 2 is the lean solvent 1003a removed.
- the lean solution 1003a is heated and regenerated by the saturated steam 1004a in the regeneration heater 104c. Then, the regenerated lean solution 1003a is discharged to the outside of the regeneration tower 104 through the lean solution pipe 103b and supplied to the absorption tower 103 by the rich / lean heat exchanger 105 through the rich solution pipe 104b. It exchanges heat with the rich solution 1003 b in the process of being supplied to the regeneration tower 104 and is cooled (absorbed liquid regeneration step).
- the CO 2 gas separated from the rich solution 1003 b and the semi-lean solution contacts the reflux water 1005 pressure-fed from the outside of the regeneration tower 104 by the reflux water pump 104d. From the top, it is discharged to the outside of the regeneration tower 104 through the reflux pipe 104e.
- the CO 2 gas is cooled by the regenerator reflux condenser 104f, and then steam is condensed by the CO 2 separator 104g to be separated from the reflux water 1005, and the recovered CO 2 discharge pipe 104h It is led to the CO 2 recovery process.
- the reflux water 1005 separated from the CO 2 by the CO 2 separator 104 g is pressure-fed by the reflux water pump 104 d and supplied to the regeneration tower 104 through the reflux pipe 104 e.
- a part of the reflux water 1005 is introduced into the circulation line 1003 e of the washing unit 1003 B of the absorption tower 103 (* 1), and is joined to the washing solution 1003 f.
- a denitrification apparatus that carries out a denitrification step of reducing NOx (nitrogen oxide) contained in the exhaust gas 1001 and denitrifying treatment;
- a desulfurization apparatus is provided which implements a desulfurization step of desulfurizing treatment by contacting SOx (sulfur oxide) contained in the exhaust gas 1001 with calcium carbonate in the slurry.
- the alkanolamine is degraded by oxygen to generate a thermally stable salt.
- remaining NOx not removed in the NOx removal step, SOx remaining unremoved in the desulfurization step, etc. react with the alkanolamine contained in the absorbent 1003 in the CO 2 removal step to form a thermally stable salt. It occurs.
- This heat stable salt is contained in the absorbing solution 1003 as a degraded product together with solid matter such as dust contained in the exhaust gas 1001, and in the absorbing solution regeneration step of regenerating the lean solution 1003a from the rich solution 1003b, under ordinary conditions. Will not be removed.
- the recovery device 101 includes the reclaiming device 106 that reclaims the degraded material remaining in the lean solution 1003a generated in the regeneration tower 104 as a reclaimed residue (hereinafter referred to as “residue”) 1006 obtained by heating and concentrating.
- this residue is comprised by the solid component which the non-volatile component was concentrated in the lean extraction liquid 1003c, and the liquid component which is not concentrated.
- FIG. 2 is a schematic view of the reclaiming device according to the first embodiment.
- the reclaiming device 106A is a pressurized reclaiming device, and is a lean solution regenerated by the regeneration tower 104 of the recovery device 101 that recovers CO 2 of the acidic gas component in the exhaust gas 1001 by the absorbing liquid 1003.
- a reclaimer 106a that branches 1003a and extracts it as a lean extract 1003c and introduces and stores the extracted lean extract 1003c, an alkaline agent supply pipe 106d that supplies an alkaline agent 106c to the inside of the reclaimer 106a, and a reclaimer 106a Adjust the control of the water supply pipe 106g that supplies the feed water (for example, regeneration tower reflux water (reflux water), steam condensed water, demineralized water, etc.) 106f to the inside and the introduction of the feed water 106f that supplies the water supply unit 106i And a reclaimer control device 110.
- the feed water for example, regeneration tower reflux water (reflux water), steam condensed water, demineralized water, etc.
- the reclaiming device 106A extracts the lean solution 1003a from the branched portion 103d of the lean solution pipe 103b before reaching the rich / lean heat exchanger 105 from the regeneration tower 104 as the lean drain liquid 1003c and stores it in the reclaimer 106a. For example, while heating in a pressurized state of 120 ° C. to 150 ° C., the absorbent vaporized from the lean extracted liquid 1003 c is returned to the lower part of the regenerator 104 as recovered vapor 1003 d while the residue 1006 concentrated by heating is discharged Do.
- the reclaiming device 106A mainly includes an absorbent storage portion and a heating portion. As shown in FIG. 2, the absorbing liquid storage unit is used as a reclaimer 106 a of a closed container that collects CO 2 from the exhaust gas 1001 and stores a portion of the lean solution 1003 c of the lean solution 1003 a regenerated by the regeneration tower 104. It is configured.
- the reclaimer 106 a is connected to the branched portion 103 d of the lean solution pipe 103 b from the regeneration tower 104 to the rich / lean heat exchanger 105 via the extraction pipe 106 b.
- the extraction pipe 106b, the opening and closing valve V 1 and extraction pump 106o are provided.
- an alkali agent supply pipe 106d for feeding the alkali agent 106c from the alkali agent supply unit 106e is connected.
- the alkali agent supply pipe 106d, closing valve V 2 is provided.
- the reclaimer 106a is connected to a water supply pipe 106g for feeding the supply water 106f from the water supply unit 106i.
- the water supply pipe 106 g are provided on-off valve V 3.
- a residue discharge pipe 106 j for discharging the residue 1006 is connected to the reclaimer 106 a.
- the residue ⁇ extraction tube 106 j, off valve V 4 and the remaining ⁇ out pump 106k is provided.
- a recovered steam discharge pipe 106h for discharging the recovered steam 1003d connected to the connection portion 104i at the lower portion of the regeneration tower 104 is connected to the upper portion of the reclaimer 106a.
- the recovery steam discharge pipe 106h is off valve V 5 is provided.
- the feed water 106f for example, regeneration tower reflux water (reflux water), steam condensed water, and demineralized water can be mentioned.
- the heating unit is provided inside the reclaimer 106a, and is connected to the horizontal U-shaped steam pipe 106l and one end of each steam pipe 106l and is generated by heating by a heating source (not shown) outside the reclaimer 106a. It comprises a steam supply pipe 106m for supplying 1004a, and a condensed water discharge pipe 106n connected to the other end of each steam pipe 1061 and discharging the vapor condensed water 1004b to the outside of the reclaimer 106a.
- the reclaiming apparatus 106A supplies the lean extraction liquid 1003c within the reclaimer 106a by opening the on-off valve V 1, the alkaline agent supplying unit an alkaline agent 106c in the interior of the reclaimer 106a by opening the on-off valve V 2 supplied from 106e, the feed water 106f inside the reclaimer 106a by opening the on-off valve V 3 is supplied from the water supply unit 106i, and opens the on-off valve V 6 is passed through a saturated steam 1004a to the steam pipe 106l,
- the supplied lean extracted liquid 1003c and the supplied water 106f are heated, for example, in a noncontact manner at 120 to 150 ° C. by heat exchange.
- the degraded substance which is a non-volatile substance contained in the lean extracted liquid 1003c forms a salt with the alkaline agent 106c, is separated from the absorbent, and is concentrated as a residue 1006 at the bottom of the reclaimer 106a.
- the residue 1006 includes the liquid component in the reclaimer 106a (the absorbent which could not be recovered, the alkali agent, the liquid component including the supplied water, and the liquid component of the non-volatile substance) and the solid component of the non-volatile component.
- the residue 1006 is discharged to the outside of the reclaimer 106 a by opening the on-off valve V 4 and operating the residue discharge pump 106 k, and is recovered outside the recovery device 101.
- the recovered residue 1006 is treated by incineration or the like.
- the lean extracted liquid 1003 c and the feed water 106 f evaporate by heating.
- the amine absorbent which has become free by the decomposition of the alkaline agent 106c is vaporized by heating.
- the recovery steam 1003d which vaporized absorbent entrained passes through the opening and closing valve V 5 which is opened and returned to the regenerator 104 via the recovery steam discharge pipe 106 h.
- an amine-based absorbent as an absorbent and sodium hydroxide as an alkaline agent.
- An alkaline agent such as sodium hydroxide in a lean extract 1003 c containing an absorbent (including amine nitrates, amine sulfates, etc.) fixed by impurities and some impurities (including nitrates, sulfates, etc.) 106c is added and mixed, and the mixture is heated to recover the free amine absorbent as well as the water as a recovered vapor 1003d, and the non-volatile substance (impurity: containing sodium nitrate, sodium sulfate, etc.) Separately discharged out of the system as liquid, solid) 1006.
- the reclaiming device 106 ⁇ / b> A of the present embodiment is provided with a reclaimer control device 110.
- the reclaimer control device 110 manages the introduction of the feed water introduced to the water supply unit 106i, which is a supply source of the feed water 106f supplied to the reclaimer 106a, and each water supply pipe 106g-1 to 106g-3 includes
- the controller 110 c is provided with a control unit 110 c that operates the opening degree of the on-off valves V 11 to V 13 provided in each of the water supply pipes 106 g-1 to 106 g-3 according to the operating condition.
- FIG. 3 is a block diagram of a control system of the reclaiming device according to the first embodiment.
- FIG. 4 is a flowchart of control of the reclaiming device according to the first embodiment.
- the control unit 110 c is configured by a microcomputer or the like. As shown in FIG. 3, the control unit 110 c is provided with a storage unit 110 d.
- the storage unit 110 d includes a RAM, a ROM, and the like, and stores programs and data.
- the storage unit 110d includes the amount of components of non-volatile substances (impurities such as sodium nitrate and sodium sulfate) in the absorbing solution (for example, the lean solution 1003a and the lean extracted solution 1003c). Data of absorbent component amount in the stored lean extracted liquid 1003c (absorbent component amount data 1, absorbent component amount data 2) are stored.
- This setting is an index indicating how much non-volatile substance is to be removed in the circulating lean solution 1003a, and can be set arbitrarily.
- absorbent component amount data 2 is, for example, the amount of absorbent component remaining in the lean extract 1003c is set, for example, a predetermined concentration (for example, several wt%) of the absorbent, or a predetermined recovery amount of the absorbent ( Recovery rate is set.
- This setting is an index indicating how much the absorbent remaining from the lean extracted liquid 1003c stored in the reclaimer 106a is reduced, and can be set arbitrarily.
- a measurement unit 110e, on-off valves V 1 to V 4 and V 11 to V 13 , and pumps 106o and 106k are connected to the control unit 110c.
- the control unit 110c centrally controls the on-off valves V 1 to V 6 and V 11 to V 13 and the pumps 106o and 106k according to a program or data stored in advance in the storage unit 110d.
- Control unit 110c on the basis of reclaiming start command nonvolatile component removal, running an extraction pump 106o with opening the on-off valve V 1 ⁇ V 3, V 5 , V 6 (step S1 ).
- a part of the absorbing liquid 1003 is introduced from the part of the lean solution 1003a into the reclaimer 106a as the lean extracted liquid 1003c and stored, and is heated and evaporated together with the alkali agent 106c and the supplied water 106f, and the recovered vapor is discharged. It is returned to the regeneration tower 104 as a recovered vapor 1003 d through a pipe 106 h.
- a first feed water control is performed to supply either the running water 1005 (* 1) or the steam condensed water 1004b (* 2) as the feed water 106f.
- demineralized water may be separately supplied.
- step S 3 when it is determined that the non-volatile component in the liquid of the reclaimer 106 a has become equal to or less than a predetermined amount based on the non-volatile component removal information input from the measurement unit 110 e (step S 2: Yes). ), closes the on-off valve V 1 and V 2 stops extraction pump 106o, to end the reclaiming operation of the non-volatile components removed (step S3).
- the concentration of the absorbent in the reclaimer 106a at the end of this non-volatile component removal reclamation is different depending on the type of absorbent and the operating conditions of the absorber, but the concentration (for example, 30) similar to that of the lean solution 1003a circulating in the system. It is preferable from the viewpoint of absorbent recovery if the concentration is slightly lower than or equal to 60 wt%).
- the on-off valves V 3 , V 5 , V 6 , and V 11 to V 12 are kept open and the on-off valve V 13 is further opened based on a finish reclaiming start command for recovering the absorbent from the residue 1006. Furthermore, the cleaning solution 1003f (* 3) is introduced into the water supply unit 106i (step S4). As a result, the supply amount of the feed water 106f supplied into the reclaimer 106a is increased, and the second feed water control to be supplied as the feed water 106f is executed. Thereby, the amount of steam generation in the reclaimer 106a is increased.
- Step S5 since the absorbent contained in the CO 2 absorbing solution is contained in the cleaning part in the cleaning liquid 1003f, it is determined whether the concentration of the absorbent in the liquid reaches the concentration of the absorbent in the cleaning liquid 1003f. (Step S5).
- the concentration of the absorbent in the liquid in the reclaimer 106a is, when led to the concentration of the absorbent in the cleaning liquid 1003f (Step S5: Yes), by closing the on-off valve V 13, feed water
- the third feed water control to be supplied as 106f is executed, and the operation of finishing reclaiming (initial) is ended (step S6).
- the low concentration of the absorbent is contained in the washing liquid 1003f by the washing in the washing unit 1003B, so if the concentration of the absorbent in the washing liquid 1003f is reached, the absorbent is recovered even if it is introduced more than that. It is because you can not
- step S7 When the concentration of the absorbent in the liquid in the reclaimer 106a reaches a predetermined recovery target concentration (for example, several wt%) or less in the operation of finish reclaiming (late stage) (step S7: Yes), the on-off valve V 3 , V 5 and V 6 and V 11 to V 12 are closed to complete the operation of the final reclaiming (late stage) (step S 8).
- a predetermined recovery target concentration for example, several wt%) or less in the operation of finish reclaiming (late stage)
- FIG. 5 is a view showing the relationship between the reclaimer operation time and the residual absorbent concentration.
- the pressure in the reclaimer 106a is kept constant, and the relationship between the reclaimer operation time (t) and the residual absorbent concentration (%) is shown in FIG.
- time t 0 on the horizontal axis indicates the time when the lean extracted liquid 1003 c is stopped
- time t 1 to t 5 is the operation elapsed time of the finish reclaiming (initial) operation
- time t 6 to t 10 is the finish It is an operation elapsed time of the reclaiming (late stage) operation.
- t 0 previous horizontal axis shows the reclaiming operation of the non-volatile components removed.
- the concentration of the absorbent drops.
- concentration (X) of the absorbent in the residue reaches the concentration (X 2 ) of the absorbent in the washing solution 1003f, or approaches the concentration of the acidic gas absorbent, the second feed water control And the third feed water control.
- concentration (X 3 ) of the absorbent in the final cleaning fluid 1003 f of the final reclaiming (late stage) is a predetermined target concentration for recovery (eg, several wt%), and is appropriately set according to the recovery target.
- the cleaning liquid 1003f circulated in the cleaning unit 1003B when the cleaning liquid 1003f circulated in the cleaning unit 1003B is initially supplied, the supplied water not supplied with the cleaning liquid.
- the operating time required to recover the absorbent in the residue 1006 in the reclaiming apparatus 106A to the same concentration (for example, 90% recovery) compared to the supply condition of (reflux water 1005, steam condensed water 1004b) alone is approximately 5 It could be reduced by%.
- an absorption tower 103 for removing an acidic gas by bringing an acidic gas in the gas 1001 into contact with an acidic gas absorbing liquid, and a rich solution 1003b which has absorbed CO 2 is a steam of the reboiler 104c.
- the solution is continuously introduced into the reservoir and stored, the alkali agent 106c and the feed water 106f are introduced and heated, and the absorbent remaining from the lean extract 1003c is recovered as the recovered vapor 1003d, while being extracted from the lean extract 1003c.
- the first feed water control is performed to supply at least one of the reflux water 1005 from the regeneration tower 104, the vapor condensed water 1004b, and at least one of the demineralized water as water, into the reclaimer 106a. While supplying at least one of steam condensed water 1004b and demineralized water as a first feed water into the reclaimer 106a, and supplying a cleaning fluid 1003f containing the CO 2 absorbing liquid of the washing unit 1003B of the absorption tower 103 into the reclaimer 106a Execute the second feed water control to be supplied as water, and the later stage of finish reclaiming , The supply of the second feed water is stopped, reflux water 1005, the steam condensate 1004b, executes the third water supply control for supplying at least one demineralized water as a first feed water.
- this reclaiming method it is possible to reduce the operation time required for recovery of the absorbent discharged out of the system accompanying the residue of the reclaiming device, and to improve the operation efficiency of the reclaiming device.
- FIG. 6 is a schematic view of a reclaiming device according to a second embodiment.
- symbol is attached
- the reclaiming apparatus 106A shown in FIG. 2 is a pressure type reclaiming apparatus, the present invention is not limited to this, and may be a decompression type reclaiming apparatus.
- a heat exchanger 131 and a gas-liquid separator 132 are provided in a recovered steam discharge pipe 106h for discharging the recovered steam 1003d from the reclaimer 106a.
- the temperature of the recovered vapor 1003 d entrained by the absorbent discharged from the reclaimer 106 a is lowered to, for example, 50 to 100 ° C. by the cooling water 131 a of the heat exchanger 131, and then introduced into the gas-liquid separator 132 for flushing .
- the introduced recovered vapor 1003 d is separated in the gas-liquid separator 132 into a condensed liquid 1003 d-1 and a recovered vapor-condensed liquid separated gas 1003 d-2.
- the recovered vapor-condensed liquid separated gas 1003 d-2 is supplied to the absorption tower 103 by the compressor 132 b provided in the discharge line 132 a.
- the condensate 1003 d-1 is supplied to the absorber 103.
- Pressurized reclaiming devices are intended for absorbents having a boiling point of, for example, 200 ° C. or less, but some absorbents have high boiling points exceeding 200 ° C.
- it is not a pressurized type, but a pressure reducing type reclaiming device using a pressure reducing device such as a vacuum pump, for example.
- a high boiling point absorbent it becomes suitable when removing the acidic component in high pressure process gas.
- the reduced pressure type reclaiming device is used to suppress high temperature in the pressurized type, since it is necessary to use high temperature steam as well as deterioration of the absorbent and to increase the reclaiming cost.
- the supply operation of the supply water 106f is the same as that of the pressure type reclaiming device 106A.
- the absorbent recovery operation after stopping extraction of the lean extracted liquid 1003c to the reclaimer 106a when the cleaning liquid 1003f circulated in the cleaning unit 1003B is initially supplied, the supply of the cleaning liquid is not performed.
- the operating time required to recover the absorbent in the residue 1006 in the reclaiming apparatus 106B to the same concentration (for example, 90% recovery) compared to the supply condition of only the feed water (reflux water 1005, steam condensed water 1004b) It could be reduced by about 40%.
- the reduction rate is improved as compared to Example 1 because, when a high boiling point absorbent is recovered, the absorbent content is high when stopping extraction of the lean extract 1003 c, and the operation time is increased. Since the content of the remaining absorbent and the drop in vapor pressure with the passage of time are large, if the pressure of the reclaimer 106a is adjusted by the pressure reducing device 130, the recovery efficiency can be improved.
- FIG. 7 is a schematic view of a reclaiming device according to a third embodiment.
- symbol is attached
- the supply water supplied to the water supply unit 106i is controlled to reduce the operation time required to recover the absorbent in the residue 1006 in the reclaiming apparatus 106A to the same concentration.
- the pressure of the reclaiming device is further controlled to reduce the operation time.
- the reclaiming device 106C includes a thermometer 110a that measures the temperature of the liquid portion in the reclaimer 106a, a first pressure gauge 110b that measures the pressure of the gas portion in the reclaimer 106a, a thermometer 110a and and a control unit 110c for obtaining data of the first pressure gauge 110b, operates the opening degree of the on-off valve V 5 provided in recovery steam discharge pipe 106 h.
- the control unit 110 c is configured by a microcomputer or the like. As shown in FIG. 8, the control unit 110 c is provided with a storage unit 110 d.
- the storage unit 110 d includes a RAM, a ROM, and the like, and stores programs and data.
- the storage unit 110d includes the amount of components of non-volatile substances (impurities such as sodium nitrate and sodium sulfate) in the absorbing solution (for example, the lean solution 1003a and the lean extracted solution 1003c).
- Data of absorbent component amount in the stored lean extracted liquid 1003c (absorbent component amount data 1, absorbent component amount data 2) are stored.
- This setting is an index indicating how much non-volatile substance is to be removed in the circulating lean solution 1003a, and can be set arbitrarily.
- absorbent component amount data 2 is, for example, the amount of absorbent component remaining in the lean extract 1003c is set, for example, a predetermined concentration (for example, several wt%) of the absorbent, or a predetermined recovery amount of the absorbent ( Recovery rate is set.
- This setting is an index indicating how much the absorbent remaining from the lean extracted liquid 1003c stored in the reclaimer 106a is reduced, and can be set arbitrarily.
- thermometer 110a a thermometer 110a, a first pressure gauge 110b, a measuring unit 110e, on-off valves V 1 to V 6 , and pumps 106o and 106k are connected to the control unit 110c.
- the control unit 110c generally controls the on-off valves V 1 to V 6 and the pumps 106o and 106k in accordance with programs and data stored in advance in the storage unit 110d.
- Control unit 110c based on the reclaiming start command nonvolatile component removal, running an extraction pump 106o with opening the on-off valve V 1 ⁇ V 3, V 5 ⁇ V 6 (step S11 ).
- a part of the absorbing liquid 1003 is introduced from the part of the lean solution 1003a into the reclaimer 106a as the lean extracted liquid 1003c and stored, and is heated and evaporated together with the alkali agent 106c and the supplied water 106f, and the recovered vapor is discharged. It is returned to the regeneration tower 104 as a recovered vapor 1003 d through a pipe 106 h.
- step S 12 when it is determined that the non-volatile component in the liquid of the reclaimer 106 a has become equal to or less than a predetermined amount based on the non-volatile component removal information input from the measurement unit 110 e (step S 12: Yes). ), closes the on-off valve V 1 and V 2 stops extraction pump 106o, to end the non-volatile component removal reclaiming operation (step S13).
- the concentration of the absorbent in the reclaimer 106a at the end of this non-volatile component removal reclamation is different depending on the type of absorbent and the operating conditions of the absorber, but the concentration (for example, 30) similar to that of the lean solution 1003a circulating in the system. It is preferable from the viewpoint of absorbent recovery if the concentration is slightly lower than or equal to 60 wt%).
- the on-off valves V 3 , V 5 and V 6 are kept open and the extraction of the lean extract 1003 c is stopped.
- the first reference temperature T 1 of measured with a thermometer 110a the heating is continued while maintaining the first reference temperature T 1 of (step S14).
- the control unit 110c to adjust the pressure of the reclaimer in 106a on the basis of the first reference temperature T 1 of the PID (Proportional-Integral-Differential Controller ) controlled by reclaimer in 106a.
- the vapor pressure of the absorbent decreases, but in this case the vapor pressure of the absorbent decreases by increasing the pressure to maintain the first reference temperature T 1 Can be suppressed.
- the control unit 110c performed by throttling the opening and closing valve V 5 as an example.
- step S15 when the concentration of the absorbent in the liquid in the reclaimer 106a reaches a predetermined concentration (for example, several wt%) or less (step S15: Yes), the on-off valves V 3 , V 5 and V 6 are closed. Then, the final reclaiming operation is ended (step S16). Then, after completion of the finishing reclaiming operation, by operating the remaining ⁇ output pump 106k with opening the on-off valve V 4, residue 1006 it is discharged to the outside of the reclaimer 106a.
- a predetermined concentration for example, several wt%) or less
- FIG. 10 is a diagram showing the relationship between the finish reclaiming operation time and the temperature, and the vertical axis shows the temperature (° C.) in the reclaimer.
- FIG. 10B is a diagram showing the relationship between the finish reclaiming operation time and the pressure, and the vertical axis shows the pressure (Pa) in the reclaimer.
- FIG. 10C is a diagram showing the relationship between the finish reclaiming operation time and the absorbent vapor pressure, and the ordinate indicates the absorbent vapor pressure (Pa) in the reclaimer.
- FIG. 10D is a diagram showing the relationship between the finish reclaiming operation time and the absorbent recovery rate, and the vertical axis shows the absorbent recovery rate (%).
- the temperature of the reclaimer 106a is set to a predetermined value (first reference temperature T 1 ). so as to maintain the (throttle-off valve V 5, increasing the pressure from P 1 to P 2) regulating the pressure of the reclaimer 106a case of, fix the reclaimer temperature as in the prior art without the pressure regulation as an indicator
- the operating time required to recover the absorbent in the residue 1006 in the reclaiming apparatus 106A to the same concentration is reduced by about 10% compared to when the pressure condition (P 1 : constant) is used. I was able to.
- the first reference temperature T 1 of the the concentration of the absorbent remaining in the lean extraction liquid 1003c which is continuously introduced into the reclaimer in 106a but at different temperatures, for example, the first reference temperature T 1 of the of 120 ⁇ 130 ° C. It is a range.
- change of temperature drop from the first reference temperature T 1 of the second reference temperature is preferably a range within 10 ° C.. A drop exceeding 10 ° C. is not preferable because the contribution to the reduction of operating time of recovery improvement is small.
- the temperature of the saturated vapor 1004 a at this time is about 140 to 150 ° C.
- target recovery rate ⁇ target recovery rate
- ⁇ recovery rate at the start of the final reclaiming operation
- the target recovery rate ( ⁇ ) could be achieved at the operation time t 94 (solid line in FIG. 10D).
- the reclaimer controller 110 is controlled to maintain T 2 constant. In this way, stable operation can be performed without exceeding the upper limit value of the specified operating pressure of the reclaimer 106a.
- lowering of the target temperature is preferably from the first reference temperature T 1 of the temperature range within a predetermined temperature (e.g. 10 ° C.). This is because if the temperature is lower than the predetermined temperature, it does not contribute to the reduction of the recovery operation time.
- a predetermined temperature e.g. 10 ° C.
- the process of reclaiming the non-volatile substance is stopped, and the introduction of the lean extracted solution into the reclaimer is stopped, and the remaining reference temperature is maintained while removing the remaining absorbing solution. Performing a final reclaiming operation to be performed.
- the operation method of the reclaiming device 106C of Example 3 1) extracts a part of the lean solution 1003a and introduces it into the reclaimer 106a as a lean extracted solution 1003c, and supplies the alkaline agent 106c and the supply water 106f.
- control to maintain the reference temperature based on the first reference target temperature suppresses a drop in the vapor pressure of the absorbent and accelerates the recovery rate of the absorbent.
- the non-volatile substance removal reclaiming operation for removing the non-volatile substance which is the degradation product contained in the lean extracted liquid 1003c, and the introduction of the lean extracted liquid 1003c to the reclaimer 106a are stopped.
- a finish reclaiming operation to suppress a drop in the vapor pressure of the absorbent when recovering the absorbent component remaining in the non-volatile component the time for the finish reclaiming operation is shortened and the reclaiming processing cost is reduced. can do.
- the circulation is performed in the cleaning section 1003B of the absorber 103 that recovers CO 2.
- the washing liquid 1003f is initially supplied as the feed water 106f, in order to recover the absorbent in the residue in the reclaimer 106a to the same concentration as compared with the supply condition of only the feed water 106f which does not supply the washing liquid 1003f.
- the required operating time can be reduced.
- the pressure of the reduced pressure reclaiming device 106C is controlled, and the pressure of the reclaimer 106a is adjusted to maintain the temperature of the reclaimer 106a at a predetermined reference temperature. It is possible to reduce the operation time required to recover the absorbent in the 1006 to the same concentration.
- FIG. 11 is a schematic view of another reclaiming device according to the third embodiment.
- the lean extracted liquid 1003c, the alkali agent 106c, and the supply water 106f are respectively supplied to the bottom of the reclaimer 106a from the extraction pipe 106b, the alkali agent supply pipe 106d, and the water supply pipe 106g.
- the present invention is not limited to this.
- the mixer 120 is installed, and the extraction pipe 106b, the alkali agent supply pipe 106d, and the water supply pipe 106g are connected to the mixer 120, and the lean extraction liquid 1003c, alkali
- the agent 106c and the feed water 106f may be introduced into the mixer 120 once to be in a good mixing state, and then introduced from the bottom of the reclaimer 106a by the mixed liquid supply pipe 120a. Further, in order to make the mixed state more homogeneous, for example, a stirring device may be used. Thereby, when separately introducing the alkaline agent 106c, it is possible to prevent uneven distribution of the mixture and the like, and to promote separation of the amine absorbent by the alkaline agent 106c.
- FIG. 12 is a schematic view of a reclaiming device according to a fourth embodiment.
- the reclaiming apparatus 106C shown in FIG. 7 is a pressure type reclaiming apparatus, the present invention is not limited to this, and may be a decompression type reclaiming apparatus.
- the pressure reducing type reclaiming device 106E is different from the pressurized type reclaiming device 106C of the third embodiment in that a pressure reducing device 130 is provided in a recovered vapor discharge pipe 106h.
- the pressure of the recovered vapor 1003d discharged from the decompression device 130 is measured by the second pressure gauge 110f.
- the recovered vapor 1003 d discharged from the decompression device 130 is introduced into either the absorption tower 103 or the regeneration tower 104 by adjusting the degree of compression. Good.
- the compression ratio of the decompression device 130 at the time of recovering the recovered vapor 1003 d is 0.5 atm
- in order to introduce the recovered vapor 1003 d into the absorption tower 103 it is compressed to, for example, 1 atm.
- in order to introduce the recovered steam 1003d into the regeneration tower 104 for example, it is compressed to 1.5 to 2.0 atm.
- control unit 110c a thermometer 110a, the first pressure gauge 110b, a second pressure gauge 110f, measuring unit 110e, on-off valve V 1 ⁇ V 4, V 6 , and a pump 106o, 106k is connected.
- the control unit 110c generally controls the on-off valves V 1 to V 4 and V 6 and the pumps 106o and 106k according to a program or data stored in advance in the storage unit 110d.
- the control unit 110c of the reclaiming apparatus 106E opens the on-off valves V 1 to V 3 and V 6 based on the non-volatile component removing reclaiming start command and removes the extraction pump 106o. It operates (step S21). Thereby, a part of the absorbing liquid 1003 is introduced from the part of the lean solution 1003a into the reclaimer 106a as the lean extracted liquid 1003c and stored, and is heated and evaporated together with the alkali agent 106c and the supplied water 106f, and the recovered vapor is discharged. It is returned to the absorption tower 103 or the regeneration tower 104 as recovered steam 1003 d through a pipe 106 h.
- step S 22 when it is determined that the non-volatile component in the liquid of the reclaimer 106 a has become equal to or less than a predetermined amount based on the non-volatile component removal information input from the measurement unit 110 e (step S 22: Yes). ), closes the on-off valve V 1 and V 2 stops extraction pump 106o, to end the reclaiming operation of the non-volatile components removed (step S23).
- the concentration of the absorbent in the reclaimer 106a at the end of this non-volatile component removal reclamation is different depending on the type of absorbent and the operating conditions of the absorber, but the concentration (for example, 30) similar to that of the lean solution 1003a circulating in the system. It is preferable from the viewpoint of absorbent recovery if the concentration is slightly lower than or equal to 60 wt%).
- step S24 On the basis of the command for starting the finish reclaiming of absorbent recovery, the on-off valves V 3 and V 6 are kept open and the first reference temperature T 1 at the time of stopping the extraction of the lean extracted liquid 1003 c is maintained. Heating is continued (step S24).
- the control unit 110c to adjust the pressure of the reclaimer in 106a on the basis of the first reference temperature T 1 of the the reclaimer 106a.
- the degree of compression is adjusted to maintain the first reference temperature T 1 (for example, operation at 0.5 atm) If the pressure is increased by 0.6 atm, the decrease in the vapor pressure of the absorbent can be suppressed.
- the pressure is increased by changing the degree of compression of the pressure reducing device 130 according to an instruction from the control unit 110 c.
- step S25 when the concentration of the absorbent in the liquid in the reclaimer 106a reaches a predetermined concentration (for example, several wt%) or less (step S25: Yes), the on-off valves V 3 and V 6 are closed to finish The reclaiming operation is ended (step S26). Then, after completion of the finishing reclaiming operation, by operating the remaining ⁇ output pump 106k with opening the on-off valve V 4, residue 1006 it is discharged to the outside of the reclaimer 106a.
- a predetermined concentration for example, several wt%) or less
- the temperature of the reclaimer 106a is set to a predetermined value (first reference temperature T to maintain a 1), a diaphragm adjustment (on-off valve V 5 pressure reclaimer 106a, when raising) the pressure from P 1 to P 2, without pressure adjustment to the conventional reclaimer temperature as an index
- the operating time required to recover the absorbent in the residue 1006 in the reclaiming device 106C to the same concentration is reduced by 50% compared to the case where fixed pressure conditions (P 1 : constant) are used. We were able to.
- the reduction rate is improved compared to Example 3 because, in the case of recovering the high boiling point absorbent, the content ratio of the absorbent is high when stopping the extraction of the lean extract 1003 c, and the operation time is increased. Since the content of the remaining absorbent and the drop in vapor pressure with the passage of time are large, if the pressure of the reclaimer 106a is adjusted by the pressure reducing device 130, the recovery efficiency can be improved.
- FIG. 15 is a schematic view of another reclaiming device according to a fourth embodiment.
- the reclaiming device 106E shown in FIG. 12 decompresses the entire amount of the recovered steam 1003d by the decompression device 130
- the present invention is not limited to this, and the reclaiming device 106F of the present embodiment recovers the recovered steam.
- a heat exchanger 131 and a gas-liquid separator 132 are provided in a recovered vapor discharge pipe 106 h for discharging the recovered vapor 1003 d from the reclaimer 106 a when the pressure in the pressure reducing device 1003 d is reduced.
- the temperature of the recovered vapor 1003 d entrained by the absorbent discharged from the reclaimer 106 a is lowered to, for example, 50 to 100 ° C. by the cooling water 131 a of the heat exchanger 131, and then introduced into the gas-liquid separator 132 for flushing .
- the introduced recovered vapor 1003 d is separated in the gas-liquid separator 132 into a condensed liquid 1003 d-1 and a recovered vapor-condensed liquid separated gas 1003 d-2.
- a compressor 132b to a discharge line 132a of recovery steam condensate separation gas 1003d-2, the compression degree of the compressor 132b are off valve V 7 interposed in the fine adjustment line 132c to tweak provided.
- the condensed liquid 1003d-1 is discharged by the pump 132e provided in the condensed water line 132d.
- the decompressor 130 by decompressing the recovered vapor-condensed liquid separated gas 1003 d-2 from which the condensed liquid 1003 d-1 has been separated by the decompressor 130, it is not necessary to decompress a large amount of recovered vapor 1003 d.
- the power of the pressure reducing device 130 can be significantly reduced.
- the condensed liquid 1003 d-1 and the recovered vapor-condensed liquid separated gas 1003 d-2 from the recovered vapor 1003 d at the normal pressure are both introduced into the absorption tower 103.
- 1003f is initially supplied as the feed water 106f, in order to recover the absorbent in the residue 1006 in the reclaimer 106a to the same concentration as compared with the supply condition of only the feed water 106f without the supply of the washing solution 1003f.
- the required operating time can be reduced.
- the pressure of the reduced pressure reclaiming device 106E is controlled, and the pressure of the reclaimer 106a is adjusted to maintain the temperature of the reclaimer 106a at a predetermined reference temperature. It is possible to reduce the operation time required to recover the absorbent in the medium to the same concentration.
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Abstract
Description
また、吸収剤成分量データ2は、例えば、リーン抜出液1003c中に残存する吸収剤成分量が設定され、例えば吸収剤の所定濃度(例えば数wt%)、又は吸収剤の所定回収量(回収率)が設定される。この設定は、リクレーマ106aに貯留されたリーン抜出液1003cから残存する吸収剤がどれほど減ったかを示す指標であり、任意に設定することが可能である。
図8に示すように、制御部110cには、記憶部110dが設けられている。記憶部110dは、RAMやROM等から構成され、プログラムやデータが格納されている。記憶部110dには、リクレーミング装置106Aを稼働するため、吸収液(例えばリーン溶液1003a、リーン抜出液1003c)中の不揮発性物質(不純物:硝酸ナトリウム、硫酸ナトリウム等)の成分量、リクレーマ106aに貯留されたリーン抜出液1003c中での吸収剤成分量のデータ(吸収剤成分量データ1、吸収剤成分量データ2)が格納されている。
この吸収剤成分量データ1は、測定部110eにより計測されたリーン溶液1003a中の不揮発性物質の含有量が所定量(x)を超えた場合、その超えた量(x)から基準値(y)以下になる量(差分x-y=z)が設定される。
この設定は、循環するリーン溶液1003a中において、不揮発性物質をどれほど除去するかを示す指標であり、任意に設定することが可能である。
この設定は、リクレーマ106aに貯留されたリーン抜出液1003cから残存する吸収剤がどれほど減ったかを示す指標であり、任意に設定することが可能である。
制御部110cでは、PID(Proportional-Integral-Differential Controller)制御によりリクレーマ106a内の第1基準温度T1に基づいてリクレーマ106a内の圧力を調整する。
制御部110cでは、リクレーマ106a内の第1基準温度T1に基づいてリクレーマ106a内の圧力を調整する。
なお、実施例3と比べて低減率が向上するのは、高沸点の吸収剤を回収する場合、リーン抜出液1003cの抜出を停止した際の、吸収剤の含有率が高く、運転時間の経過に伴う残存吸収剤の含有率と蒸気圧の低下が大きいので、リクレーマ106aの圧力を減圧装置130で調節させると、回収効率の向上が図れるからである。
103 吸収塔
104 再生塔
106A~106F リクレーミング装置
106a リクレーマ
106b 抜出管
106c アルカリ剤
106d アルカリ剤供給管
106e アルカリ剤供給部
106f 供給水
106g 水供給管
106h 回収蒸気排出管
106i 水供給部
106j 残渣排出管
106k 残渣排出ポンプ
106l 蒸気管
106m 蒸気供給管
106n 凝縮水排出管
106o 抜出ポンプ
110a 温度計
110 リクレーマ制御装置
110b 第1圧力計
110c 制御部
110d 記憶部
110e 測定部
1001 排ガス
1003a リーン溶液
1003b リッチ溶液
1003c リーン抜出液
1003d 回収蒸気
1006 リクレーミング残渣
1004a 飽和蒸気
1004b 蒸気凝縮水
T1 第1基準温度
V1~V6、V11~V13 開閉
Claims (10)
- ガス中の酸性ガスと酸性ガス吸収液とを接触させて酸性ガスを除去する酸性ガス吸収塔と、酸性ガスを吸収したリッチ溶液をリボイラの蒸気により再生してリーン溶液とする吸収液再生塔と、
前記リーン溶液を抜出し、このリーン抜出液を導入して貯留するリクレーマと、
前記リクレーマ内部にアルカリ剤を供給するアルカリ剤供給管と、
前記リクレーマ内部に供給水を供給する水供給管と、
前記リクレーマから排出する回収蒸気を、前記酸性ガス吸収塔又は前記再生塔に導入する回収蒸気排出管と、
前記リクレーマへの運転を制御するリクレーマ制御装置と、を具備し、
前記リクレーマ制御装置は、
前記リクレーマへの前記リーン抜出液の導入を行い、該リーン抜出液中の不揮発性成分を分離する不揮発性成分除去のリクレーミングの際、前記水供給管に供給する第1供給水として、前記再生塔からの還流水、蒸気凝縮水、脱塩水のすくなくとも一つをリクレーマ内に供給する第1の供給水制御を実行すると共に、
前記リクレーマへのリーン抜出液の導入を停止した後のリクレーミング残渣中の吸収剤を回収する仕上げリクレーミングの初期は、前記還流水、蒸気凝縮水、脱塩水のすくなくとも一つをリクレーマ内に前記第1供給水として供給すると共に、前記酸性ガス吸収塔の洗浄部の前記酸性ガス吸収液を含む洗浄液をリクレーマ内に第2供給水として供給する第2の供給水制御を実行し、
前記仕上げリクレーミングの後期は、前記第2供給水の供給を停止し、前記還流水、蒸気凝縮水、脱塩水のすくなくとも一つを第1供給水として供給する第3の供給水制御を実行することを特徴とする酸性ガス除去装置。 - 請求項1において、
第2の供給水制御と第3の供給水制御との実行の切替えは、前記リクレーミング残渣中の酸性ガス吸収剤の残存濃度が、前記洗浄液中の酸性ガス吸収剤の濃度となるとき、又は前記洗浄液中の酸性ガス吸収剤の濃度に近づいたときであることを特徴とする酸性ガス除去装置。 - 請求項1又は2において、
さらに、前記リクレーマ内の温度を計測する温度計と、
前記リクレーマ内の圧力を計測する圧力計と、を具備し、
前記リクレーマ制御装置は、
第1~第3の供給水制御の実行を行うと共に、
前記リクレーマへのリーン抜出液の導入を停止した後のリクレーミング残渣中の吸収剤を回収する仕上げリクレーミングの際、
前記リクレーマへのリーン抜出液の導入を停止したときのリクレーマ内の温度を基準温度とし、該基準温度を維持するように、前記リクレーマ内の圧力を調整する圧力制御を実行することを特徴とする酸性ガス除去装置。 - 請求項3において、
前記リクレーマ内の圧力が該リクレーマの運転上限の上限圧力値に達する場合、
前記リクレーマ制御装置は、
前記基準温度を下回る温度となるように、目標基準温度を変更し、
変更した基準温度を維持するように前記リクレーマ内の圧力を調整することを特徴とする酸性ガス除去装置。 - 請求項4において、
目標基準温度の変更は、前記リクレーマへのリーン抜出液の導入を停止したときのリクレーマ内の基準温度から、所定温度以内の低い温度範囲とすることを特徴とする酸性ガス除去装置。 - 請求項3乃至5のいずれか一つにおいて、
前記リクレーマ制御装置の圧力の調整は、加圧型リクレーマの場合、
前記回収蒸気排出管に絞り弁を設置し、該絞り弁を調整することを特徴とする酸性ガス除去装置。 - 請求項3乃至5のいずれか一つにおいて、
前記リクレーマ制御装置の圧力の調整は、減圧型リクレーマの場合、
前記回収蒸気排出管に設置した減圧装置を調整することを特徴とする酸性ガス除去装置。 - ガス中の酸性ガスと酸性ガス吸収液とを接触させて酸性ガスを除去する酸性ガス吸収塔と、酸性ガスを吸収したリッチ溶液をリボイラの蒸気により再生してリーン溶液とする吸収液再生塔とにより酸性ガスを除去する酸性ガス除去工程と、
前記再生塔で再生された前記リーン溶液の一部を抜出し、このリーン抜出液をリクレーマ内に連続して導入して貯留し、アルカリ剤及び供給水を導入して加熱し、前記リーン抜出液から残存する吸収剤を回収蒸気として回収しつつ、リーン抜出液中の不揮発性成分を分離する不揮発性成分除去のリクレーミング工程と、
前記リクレーマへのリーン抜出液の導入を停止する工程と、
前記リクレーマ内の残渣中からさらに吸収剤を回収する仕上げリクレーミング工程と、を有し、
前記不揮発性成分除去のリクレーミングの際、水供給管に供給する第1供給水として、前記再生塔からの還流水、蒸気凝縮水、脱塩水のすくなくとも一つをリクレーマ内に供給する第1の供給水制御を実行すると共に、
前記仕上げリクレーミングの初期は、前記還流水、蒸気凝縮水、脱塩水の少なくとも一つをリクレーマ内に前記第1供給水として供給すると共に、前記酸性ガス吸収塔の洗浄部の前記酸性ガス吸収液を含む洗浄液をリクレーマ内に第2供給水として供給する第2の供給水制御を実行し、
前記仕上げリクレーミングの後期は、前記第2供給水の供給を停止し、前記還流水、蒸気凝縮水、脱塩水の少なくとも一つを第1供給水として供給する第3の供給水制御を実行することを特徴とする酸性ガス除去方法。 - 請求項8において、
第2の供給水制御と第3の供給水制御との実行の切替えは、リクレーミング残渣中の酸性ガス吸収剤の残存濃度が、前記洗浄液中の酸性ガス吸収剤の濃度となるとき、又は前記洗浄液中の酸性ガス吸収剤の濃度に近づいたときであることを特徴とする酸性ガス除去方法。 - 請求項8又は9において、
前記仕上げリクレーミング工程の際、
前記リクレーマへのリーン抜出液の導入を停止したときのリクレーマ内の温度を基準温度とし、該基準温度を維持するように前記リクレーマ内の圧力を調整する圧力制御を実行することを特徴とする酸性ガス除去方法。
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2020075543A1 (ja) * | 2018-10-10 | 2020-04-16 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及び方法並びにco2回収装置並びに方法 |
WO2020075541A1 (ja) * | 2018-10-10 | 2020-04-16 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及びこれを備えたco2回収装置並びにリクレーミング方法 |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP7356344B2 (ja) * | 2019-12-27 | 2023-10-04 | 三菱重工業株式会社 | ボイラープラント、及び二酸化炭素除去方法 |
US11628391B2 (en) * | 2020-04-15 | 2023-04-18 | Mitsubishi Heavy Industries Engineering, Ltd. | Carbon dioxide recovery apparatus |
JP7431708B2 (ja) * | 2020-09-11 | 2024-02-15 | 株式会社東芝 | 酸性ガス除去制御装置、酸性ガス除去制御方法、および酸性ガス除去装置 |
CN114130163B (zh) * | 2021-11-01 | 2024-05-14 | 新疆兴发化工有限公司 | 一种氧化尾气吸收制酸的环保处理工艺及装置 |
KR102556854B1 (ko) * | 2022-07-19 | 2023-07-19 | 홍원방 | 자원순환 시스템 |
KR102556853B1 (ko) * | 2022-07-19 | 2023-07-19 | 홍원방 | 배기가스로부터 이산화탄소 제거시스템 |
Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010142716A1 (en) * | 2009-06-09 | 2010-12-16 | Aker Clean Carbon As | Method for reclaiming of co2 absorbent and a reclaimer |
JP2011104580A (ja) * | 2009-10-19 | 2011-06-02 | Mitsubishi Heavy Ind Ltd | リクレーミング装置およびリクレーミング方法 |
JP2012236170A (ja) | 2011-05-13 | 2012-12-06 | Babcock Hitachi Kk | 劣化吸収液再生方法並びに劣化吸収液再生装置及びこれを用いた二酸化炭素回収システム |
JP2013099727A (ja) | 2011-11-09 | 2013-05-23 | Babcock Hitachi Kk | Co2化学吸収システムの制御方法 |
JP2015077581A (ja) * | 2013-10-18 | 2015-04-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
WO2015068576A1 (ja) * | 2013-11-05 | 2015-05-14 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
WO2015107958A1 (ja) * | 2014-01-17 | 2015-07-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
JP2017124374A (ja) * | 2016-01-14 | 2017-07-20 | 三菱重工業株式会社 | 酸性ガス回収システム及びそれに用いるリクレーミング装置 |
JP2018118203A (ja) * | 2017-01-24 | 2018-08-02 | 三菱重工業株式会社 | 排ガス処理装置及びそれを用いたco2回収装置 |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20070148068A1 (en) * | 2005-12-23 | 2007-06-28 | Burgers Kenneth L | Reclaiming amines in carbon dioxide recovery |
JP4875522B2 (ja) * | 2007-03-14 | 2012-02-15 | 三菱重工業株式会社 | Co2回収装置及び廃棄物抽出方法 |
JP5050071B2 (ja) * | 2010-03-29 | 2012-10-17 | 株式会社日立製作所 | ボイラ装置 |
WO2012067101A1 (ja) * | 2010-11-16 | 2012-05-24 | バブコック日立株式会社 | 二酸化炭素化学吸収システムの制御方法および装置 |
JP5636306B2 (ja) * | 2011-02-14 | 2014-12-03 | バブコック日立株式会社 | Co2化学吸収システムの制御方法 |
JP5812847B2 (ja) * | 2011-12-21 | 2015-11-17 | 三菱日立パワーシステムズ株式会社 | 二酸化炭素の回収装置及び方法 |
CA3056375A1 (en) * | 2017-04-12 | 2018-10-18 | Anemos Company Ltd. | Apparatus and method for recovering carbon dioxide in combustion exhaust gas |
-
2017
- 2017-10-20 JP JP2017203727A patent/JP6998174B2/ja active Active
-
2018
- 2018-10-15 AU AU2018352740A patent/AU2018352740B2/en active Active
- 2018-10-15 US US16/635,476 patent/US10874976B2/en active Active
- 2018-10-15 WO PCT/JP2018/038317 patent/WO2019078156A1/ja unknown
- 2018-10-15 CA CA3071602A patent/CA3071602C/en active Active
- 2018-10-15 EP EP18869353.5A patent/EP3646937B1/en active Active
Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2010142716A1 (en) * | 2009-06-09 | 2010-12-16 | Aker Clean Carbon As | Method for reclaiming of co2 absorbent and a reclaimer |
JP2011104580A (ja) * | 2009-10-19 | 2011-06-02 | Mitsubishi Heavy Ind Ltd | リクレーミング装置およびリクレーミング方法 |
JP2012236170A (ja) | 2011-05-13 | 2012-12-06 | Babcock Hitachi Kk | 劣化吸収液再生方法並びに劣化吸収液再生装置及びこれを用いた二酸化炭素回収システム |
JP2013099727A (ja) | 2011-11-09 | 2013-05-23 | Babcock Hitachi Kk | Co2化学吸収システムの制御方法 |
JP2015077581A (ja) * | 2013-10-18 | 2015-04-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
WO2015068576A1 (ja) * | 2013-11-05 | 2015-05-14 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
WO2015107958A1 (ja) * | 2014-01-17 | 2015-07-23 | 三菱重工業株式会社 | リクレーミング装置及び方法、co2又はh2s又はその双方の回収装置 |
JP2017124374A (ja) * | 2016-01-14 | 2017-07-20 | 三菱重工業株式会社 | 酸性ガス回収システム及びそれに用いるリクレーミング装置 |
JP2018118203A (ja) * | 2017-01-24 | 2018-08-02 | 三菱重工業株式会社 | 排ガス処理装置及びそれを用いたco2回収装置 |
Non-Patent Citations (1)
Title |
---|
See also references of EP3646937A4 |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2020075543A1 (ja) * | 2018-10-10 | 2020-04-16 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及び方法並びにco2回収装置並びに方法 |
WO2020075541A1 (ja) * | 2018-10-10 | 2020-04-16 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及びこれを備えたco2回収装置並びにリクレーミング方法 |
US11045757B2 (en) | 2018-10-10 | 2021-06-29 | Mitsubishi Heavy Industries Engineering, Ltd. | Reclaiming apparatus, CO2 recovery apparatus including the same, and reclaiming method |
JPWO2020075543A1 (ja) * | 2018-10-10 | 2021-09-02 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及び方法並びにco2回収装置並びに方法 |
JPWO2020075541A1 (ja) * | 2018-10-10 | 2021-09-24 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及びこれを備えたco2回収装置並びにリクレーミング方法 |
JP7141465B2 (ja) | 2018-10-10 | 2022-09-22 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及び方法並びにco2回収装置並びに方法 |
JP7167176B2 (ja) | 2018-10-10 | 2022-11-08 | 三菱重工エンジニアリング株式会社 | リクレーミング装置及びこれを備えたco2回収装置並びにリクレーミング方法 |
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