WO2015122050A1 - Co2回収装置及びco2回収方法 - Google Patents
Co2回収装置及びco2回収方法 Download PDFInfo
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- WO2015122050A1 WO2015122050A1 PCT/JP2014/076817 JP2014076817W WO2015122050A1 WO 2015122050 A1 WO2015122050 A1 WO 2015122050A1 JP 2014076817 W JP2014076817 W JP 2014076817W WO 2015122050 A1 WO2015122050 A1 WO 2015122050A1
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- Prior art keywords
- absorbing
- absorbent
- absorption
- solution
- gas
- Prior art date
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- 238000011084 recovery Methods 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000010521 absorption reaction Methods 0.000 claims abstract description 125
- 230000002745 absorbent Effects 0.000 claims description 86
- 239000002250 absorbent Substances 0.000 claims description 86
- 239000007788 liquid Substances 0.000 claims description 84
- 230000008929 regeneration Effects 0.000 claims description 64
- 238000011069 regeneration method Methods 0.000 claims description 64
- 239000006096 absorbing agent Substances 0.000 claims description 30
- 238000011049 filling Methods 0.000 claims description 23
- 239000000945 filler Substances 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 6
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 123
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 40
- 238000001816 cooling Methods 0.000 description 23
- 238000004140 cleaning Methods 0.000 description 12
- 230000002378 acidificating effect Effects 0.000 description 11
- 230000015572 biosynthetic process Effects 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- 238000003786 synthesis reaction Methods 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 9
- 239000003546 flue gas Substances 0.000 description 9
- 238000005406 washing Methods 0.000 description 9
- 239000000498 cooling water Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 6
- 230000001276 controlling effect Effects 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 238000000605 extraction Methods 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 239000003595 mist Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 238000009529 body temperature measurement Methods 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
Images
Classifications
-
- 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
-
- 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
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- 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
-
- 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
Definitions
- the present invention relates to a CO 2 recovery device and a CO 2 recovery method, and relates to a CO 2 recovery device and a CO 2 recovery method for recovering CO 2 in a gas to be treated using a CO 2 absorbent.
- a direct reduced iron production system including an acidic gas removing device that removes acidic components in reducing furnace exhaust gas as synthesis gas discharged from a direct reducing furnace has been proposed (see, for example, Patent Document 1).
- the reduction furnace exhaust gas having a high CO 2 partial pressure (for example, 50 kPa to 200 kPa) discharged from the direct reduction furnace is brought into contact with the acidic gas absorption liquid in the acidic gas component absorption tower to reduce the reduction furnace.
- the acidic gas absorbing solution that has absorbed the acidic gas component is heated in a regeneration tower to release the acidic gas component in the acidic gas absorbing solution to regenerate the acidic gas absorbing solution.
- an acidic gas removal facility that removes acidic components contained in natural gas has been proposed (see, for example, Non-Patent Document 1).
- CO 2 minutes is relatively low pressures (e.g., 10 kPa ⁇ 15 kPa) and CO 2 recovery apparatus is used to recover CO 2 in the combustion exhaust gas such as a boiler by CO 2 absorbing solution
- CO 2 recovery apparatus is used to recover CO 2 in the combustion exhaust gas such as a boiler by CO 2 absorbing solution
- the CO 2 from the relatively high synthesis gas is CO 2 partial pressure or when recovered by the CO 2 absorbing solution, the CO 2 from natural gas (methane) containing CO 2 at a case of recovering the CO 2 absorbing solution
- the present invention has been made in view of such circumstances, excellent absorption rate of CO 2, moreover, an object of the invention to provide a CO 2 recovery apparatus and a CO 2 recovery method that can be energy saving.
- the first CO is absorbed the contacting the gas to be treated and the CO 2 absorbing solution containing CO 2 and CO 2 contained in the gas to be treated in the CO 2 absorbing solution 2
- the first CO 2 absorbing section as an absorbing liquid, and the first CO 2 absorbing liquid and the gas to be processed containing CO 2 are brought into contact with each other to convert CO 2 contained in the gas to be processed into the first CO 2.
- the second CO and CO 2 absorption tower having two absorbing portion, the second CO 2 absorption and heating the second CO 2 absorbing solution for the second CO 2 absorbing liquid is absorbed into the absorbing solution and the CO 2 absorbing solution regeneration tower for reproducing CO 2 absorbing solution by releasing CO 2 from the liquid, measuring a temperature of the second CO 2 absorbing liquid supplied from the CO 2 absorption tower to the CO 2 absorbing solution regeneration tower a temperature measuring device for the second CO 2 adsorption measured by the temperature measuring device Characterized by comprising a control device for controlling the temperature of the first CO 2 absorbing solution supplied to the second CO 2 absorbing section based on the temperature of the liquid.
- the CO 2 recovery apparatus is excellent in CO 2 absorption rate and can save energy even when processing a synthesis gas having a high CO 2 partial pressure in the gas to be processed.
- the absorption rate is the molar amount of CO 2 absorbed per mole of the absorbing solution.
- the control device controls the temperature of the first CO 2 absorbing liquid supplied to the second CO 2 absorbing section to 50 ° C. or more and 60 ° C. or less.
- the temperature of the first CO 2 absorbing liquid supplied to the second CO 2 absorbing section is an appropriate range, to be treated in the gas in the second CO 2 absorbing section Since the absorption rate of CO 2 is further improved and the circulation rate of the CO 2 absorbent can be reduced by improving the CO 2 absorption rate, the consumption of water vapor necessary for the regeneration of the CO 2 absorbent can be reduced.
- the CO 2 absorbing solution can appropriately high temperature of the supplied CO 2 absorbing solution to the regenerator, it is also effective expected to reduce steam consumption.
- CO 2 partial pressure of the gas to be treated containing CO 2 is not less than 50 kPa.
- the CO 2 recovery device has a moderate CO 2 partial pressure in the gas to be treated, so that the CO 2 absorption rate by the first CO 2 absorbing liquid in the second CO 2 absorbing portion is further increased. improves.
- the first CO ratio of the filling height of the filling material in the filling height and the second CO 2 absorbing section of the filler in the two absorbent portion is preferably 1: 3 or more and 3: 1 or less.
- CO 2 recovery method of the present invention said CO 2 contained in the gas to be treated with the gas to be treated and the CO 2 absorbing solution by contacting with the first CO 2 absorption of the CO 2 absorber comprising CO 2
- the first CO 2 absorbing liquid is absorbed into the CO 2 absorbing liquid to make contact with the first CO 2 absorbing liquid and the gas to be treated containing CO 2 at the second CO 2 absorbing portion of the CO 2 absorbing tower.
- the CO 2 recovery method is excellent in CO 2 absorption and energy saving even when a synthesis gas having a high CO 2 partial pressure in the gas to be processed is processed.
- the temperature of the first CO 2 absorbent supplied to the second CO 2 absorber it is preferable to control the temperature of the first CO 2 absorbent supplied to the second CO 2 absorber to 50 ° C. or more and 60 ° C. or less.
- the temperature of the first CO 2 absorbing liquid supplied to the second CO 2 absorbing section is an appropriate range, to be treated in the gas in the second CO 2 absorbing section Since the absorption rate of CO 2 is further improved and the circulation rate of the CO 2 absorbent can be reduced by improving the CO 2 absorption rate, the consumption of water vapor necessary for the regeneration of the CO 2 absorbent can be reduced.
- the CO 2 absorbing solution can appropriately high temperature of the supplied CO 2 absorbing solution to the regenerator, it is also effective expected to reduce steam consumption.
- the CO 2 partial pressure of the gas to be treated containing CO 2 is not less than 50 kPa. In this way, CO 2 recovery method, since the partial pressure of CO 2 to be treated in the gas becomes a proper range, CO 2 to be treated in the gas by the first CO 2 absorbing solution in the second CO 2 absorbing section The absorptivity is further improved.
- the first CO ratio of the filling height of the filling material in the filling height and the second CO 2 absorbing section of the filler in the two absorbent portion is preferably 1: 3 or more and 3: 1 or less.
- FIG. 1 is a schematic view of a CO 2 recovery apparatus according to an embodiment of the present invention.
- FIG. 2 is a diagram showing the relationship between the temperature of the CO 2 absorbent (semi-rich solution) supplied to the lower CO 2 absorber and the ratio of the CO 2 absorption rate of the rich solution.
- Figure 3 is a diagram showing a relationship between heat ratio required regeneration temperature and CO 2 absorbing solution in the CO 2 absorbing liquid supplied to the lower CO 2 absorbing section (semi-rich solution).
- FIG. 4 is a diagram showing the relationship between the temperature of the CO 2 absorbent (semi-rich solution) supplied to the lower CO 2 absorber and the temperature of the CO 2 absorbent (rich solution) supplied to the CO 2 regeneration tower.
- FIG. 5 is a diagram showing the relationship between the packing height ratio of the filler and the ratio of the CO 2 absorption rate of the rich solution in the lower CO 2 absorption section and the upper CO 2 absorption section of the CO 2 absorption tower.
- the present inventors have found that in the conventional CO 2 recovery apparatus has a relatively low CO 2 partial pressures, such as flue gas, such as a boiler of a thermal power plant (e.g., 10 kPa ⁇ 15 kPa) and recovering the CO 2 from the gas It was noted that the CO 2 partial pressure discharged from a direct reduction furnace or the like is not premised on the recovery of CO 2 from synthesis gas having a relatively high (eg, 50 kPa to 200 kPa).
- a relatively low CO 2 partial pressures such as flue gas, such as a boiler of a thermal power plant (e.g., 10 kPa ⁇ 15 kPa) and recovering the CO 2 from the gas
- flue gas such as a boiler of a thermal power plant
- the CO 2 partial pressure discharged from a direct reduction furnace or the like is not premised on the recovery of CO 2 from synthesis gas having a relatively high (eg, 50 kPa to 200 kPa).
- the present inventors have found that in the case of recovering CO 2 from the relatively high synthesis gas is CO 2 partial pressure, the CO 2 absorption column provided with a plurality of CO 2 absorbing section, the CO 2 absorbing solution regeneration tower by controlling the temperature of the supplied CO 2 absorbing liquid to 2 absorbing section plurality of CO on the basis of the temperature of the supplied CO 2 absorbing solution in, excellent absorption rate of CO 2, moreover, capable of energy saving CO 2
- the present inventors have found that a recovery apparatus and a CO 2 recovery method can be realized, and have completed the present invention.
- FIG. 1 is a schematic view of a CO 2 recovery apparatus according to an embodiment of the present invention.
- the CO 2 recovering apparatus 1 the reducing furnace exhaust system for recovering CO 2 in (gas to be treated) 11A as a high-concentration CO 2 gas as synthesis gas discharged from the direct reduction furnace It is.
- This CO 2 recovery device 1 is provided with a cooling tower 12 that cools the exhaust gas 11A containing CO 2 discharged directly from a reduction furnace or the like, and a cooling tower 12 that is provided at the rear stage of the cooling tower 12 and absorbs the CO 2 that has been cooled.
- CO and CO 2 absorption tower 14 which is brought into contact with the liquid 13 is removed by absorbing the CO 2 in the flue gas 11A in the CO 2 absorbing liquid 13, which is provided downstream of the CO 2 absorption tower 14, it has absorbed CO 2 2 to release CO 2 from the absorbing solution 13C and includes a CO 2 absorbing solution regeneration tower 15 for reproducing the CO 2 absorbing solution 13.
- a CO 2 absorption liquid 13 is circulated between a CO 2 absorption tower 14 and a CO 2 absorption liquid regeneration tower 15.
- the CO 2 absorbing liquid 13 (lean solution) is supplied to the CO 2 absorbing liquid regeneration tower 15 as a CO 2 absorbing liquid 13C (rich solution) that has absorbed CO 2 by the CO 2 absorbing tower 14, and the CO 2 absorbing liquid.
- 13C (rich solution) is supplied to the CO 2 absorption tower 14 as a CO 2 absorption liquid 13 (lean solution) regenerated by removing CO 2 in the CO 2 absorption liquid regeneration tower 15.
- the cooling tower 12 has a cooling unit 121 that cools the exhaust gas 11A.
- a circulation line L 1 is provided between the bottom of the cooling tower 12 and the top of the cooling unit 121.
- the circulation line L 1 a heat exchanger 122 for cooling the cooling water W 1, a circulation pump 123 for circulating the cooling water W 1 in the circulation line L within 1, which is discharged separated from the circulation line L 1
- An adjustment valve 124 is provided for adjusting the amount of waste liquid.
- the exhaust gas 11 ⁇ / b> A and the cooling water W 1 are brought into countercurrent contact with each other, whereby the exhaust gas 11 ⁇ / b> A is cooled and becomes the exhaust gas 11 ⁇ / b> B after cooling.
- the heat exchanger 122 cools the cooling water W 1 which is heated by heat exchange with the exhaust gas 11A.
- the circulation pump 123 supplies the cooling water W 1 flowing down to the bottom of the cooling tower 12 via the heat exchanger 122 to the top of the cooling unit 121.
- the cooling tower 12 when the moisture in the exhaust gas 11 ⁇ / b> A is small, the liquid level of the cooling tower 12 is lowered, so that water is supplied from the top of the tower. Also, if the water in the flue gas 11A is high, the liquid level of the cooling tower 12 is increased, part of the cooling water W 1 circulating in the circulation line L 1 is being separated waste liquid treatment.
- the CO 2 absorption tower 14 is provided on the lower side of the CO 2 absorption tower 14.
- the water-washing part 142 provided in the upper part side.
- the CO 2 absorption unit 141 the lower the CO 2 absorbing section provided in the lower side of the CO 2 absorbing section 141 (second CO 2 absorbing section) 141A and an upper provided on the upper side of the CO 2 absorbing section 141 CO It has a 2 absorbing section 141B (the first CO 2 absorbing section), the.
- the lower CO 2 absorber 141A is filled so that the filling material has a filling height H1.
- the upper CO 2 absorbing portion 141B is filled so that the filling material has a filling height H2.
- the upper CO 2 absorbing section 141B, the CO 2 absorbing liquid 13 that has been reproduced by the CO 2 absorbing solution regeneration tower 15 is supplied.
- the lower CO 2 absorption part (second CO 2 absorption part) 141A is supplied with a CO 2 absorbent 13B that has absorbed CO 2 in the exhaust gas 11C by the upper CO 2 absorption part 141B.
- the CO 2 absorbing liquid that has accumulated in the bottom of the upper CO 2 absorbing section 141B flows down from the upper CO 2 absorbing section 141B (first CO 2
- the liquid storage part 143A and chimney tray 143B which store 13A of absorption liquids are provided. This is the liquid reservoir 143A, the line L 11 withdrawn supplied to lower the CO 2 absorbing section 141A is provided by extracting the CO 2 absorbing liquid 13A that is stored in the liquid storing portion 143A from the CO 2 absorber 14.
- the withdrawal line L 11 is a heat exchanger 24 and the CO 2 absorbing solution 13A to the CO 2 absorbing liquid 13B that is cooled by cooling the CO 2 absorbing solution 13A to lower the CO 2 absorbing section 141A as the CO 2 absorbing liquid 13B
- a pump 25 for supply is provided.
- the heat exchanger 24 is configured so that the supply amount of the refrigerant can be adjusted by the control device 101.
- the pump 25 is configured such that the supply amount of the CO 2 absorbent 13B to the lower CO 2 absorbent 141A can be adjusted by the control device 101.
- the control device 101 can be realized using, for example, a general-purpose or dedicated computer such as a CPU (Central Processing Unit), a ROM (Read Only Memory), a RAM (Random Access Memory), and a program operating on the computer. it can.
- the bottom of the washing section 142 the liquid reservoir 144A for storing the cleaning water W 2 for cleaning the exhaust gas 11D that CO 2 in the flue gas 11C is removed is provided.
- the circulation line L 2 a heat exchanger 21 for cooling the wash water W 2
- circulation line wash water W 2 including the CO 2 absorbing liquid 13 through the heat exchanger 21 is recovered by the liquid reservoir 144A
- a circulation pump 22 that circulates in L 2 is provided.
- the circulation line L 2 is provided with an extraction line L 3 for extracting a part of the cleaning water W 2 (cleaning water W 3 ) and supplying it to the CO 2 absorbent 13 (lean solution).
- the extraction line L 3 is provided with an adjustment valve 23 that adjusts the supply amount of the cleaning water W 3 supplied to the CO 2 absorbent 13.
- CO 2 absorber section 141 and the CO 2 absorbing solution 13, including exhaust gas 11A and alkanol amines containing CO 2 in the upper CO 2 absorbing section 141B is in contact countercurrent.
- CO 2 in the exhaust gas 11C is absorbed by the CO 2 absorbent 13 by a chemical reaction shown in the following formula.
- CO 2 in the exhaust gas 11C is removed and the exhaust gas 11C becomes the exhaust gas 11D from which the CO 2 is removed, and the CO 2 absorbent 13 becomes the CO 2 absorbent 13A.
- the lower the CO 2 absorbing section 141A, and the CO 2 absorbing solution 13B having absorbed gas 11B and CO 2 containing CO 2 is contacted countercurrent.
- the exhaust gas 11D from which the CO 2 that has passed through the upper CO 2 absorption section 141B has been removed rises via the chimney tray 144B. Then, the exhaust gas 11D is a flue gas 11E recovered by circulating the cleaning of CO 2 absorbing solution 13 accompanying the cleaning water W 2 and gas-liquid contact with flue gas 11D supplied from the top side of the washing unit 142. The exhaust gas 11E is trapped in the gas by the mist eliminator 145 and discharged from the top 14a of the CO 2 absorption tower 14 to the outside.
- the CO 2 absorption liquid 13C (rich solution) that has absorbed CO 2 by the CO 2 absorption tower 14 is CO 2 absorption liquid.
- a rich solution supply pipe 50 for supplying to the upper side of the regeneration tower 15 is provided.
- the rich solvent feed pipe 50 a thermometer for measuring the temperature of the CO 2 absorbing solution 13C (temperature measuring device) 102 and, CO 2 and CO 2 absorbing solution 13C that has absorbed CO 2 in the absorption tower 14 CO 2 absorbing solution rich heating the rich solution pump 51 supplies toward the regeneration tower 15, CO 2 absorbing solution 13C the CO 2 absorbing solution regeneration tower 15 heated by CO CO 2 has been removed 2 absorbent 13 by (lean solvent)
- a lean solution heat exchanger 52 is provided.
- the control device 101 adjusts the amount of refrigerant supplied to the heat exchanger 24 based on the temperature of the CO 2 absorbent 13C measured by the thermometer 102, and supplies CO 2 to the lower CO 2 absorber 141A by the pump 25.
- the supply amount of the absorbing liquid 13B is controlled.
- the temperature meter 102 is disposed may be provided at locations that can be controlled by the controller 101 of the CO 2 absorbing solution 13B supplies the lower the CO 2 absorbing section 141A, for example, downstream of the heat exchanger 24 of
- the central portion of the CO 2 absorbing solution regeneration tower 15, CO 2 absorbing solution supply section 151 CO 2 absorbed CO 2 absorbing solution 13C is supplied is provided.
- a regeneration heater 31 that heats the CO 2 absorbent 13 with saturated steam S
- a regulating valve 32 that adjusts the amount of saturated steam S supplied to the regeneration heater 31, and the regeneration heater 31.
- the CO 2 absorbing solution regeneration tower 15 the bottom of the CO 2 absorbing solution 13 CO 2 absorbing solution regeneration tower 15 of the CO 2 absorbing liquid circulating pump 33 for supplying the bottom of the supply unit 151 through a is provided.
- This gas discharge line L 5 represents a capacitor 42 which condenses the moisture in the CO 2 gas 41, and the separation drum 43 to separate the CO 2 gas 41 and condensed water W 5 is provided.
- the CO 2 gas 44 from which the condensed water W 5 has been separated is discharged to the outside from the upper part of the separation drum 43.
- the condensed water W 5 the CO 2 absorbing solution regeneration tower 15 the condensate line L is supplied to the upper 6 is provided.
- the condensed water line L 6 is provided with a condensed water circulation pump 45 that supplies the condensed water W 5 separated by the separation drum 43 to the upper part of the CO 2 absorbent regeneration tower 15. Between the condensed water circulation pump 45 and the CO 2 absorbent regeneration tower 15, an adjustment valve 46 for controlling the amount of the condensed water W 5 supplied to the CO 2 absorbent regeneration tower 15 is provided. Further, between the condensed water circulation pump 45 and the circulation line L 2 , a part of the condensed water W 5 supplied to the CO 2 absorbing liquid regeneration tower 15 is branched and supplied to the cleaning unit 142 of the CO 2 absorbing tower 14. return line L 12 condensed water W 5 which is provided. The reflux line L 12 is provided with an adjustment valve 47 that adjusts the amount of condensed water W 5 supplied to the cleaning unit 142.
- a lean solution supply pipe 53 that supplies the upper side of the CO 2 absorption unit 141 is provided.
- the lean solution supply pipe 53, the CO 2 absorbing solution regeneration tower 15 is heated with steam in a CO 2 absorbing solution 13 from which CO 2 has been removed (lean solution) CO 2 absorbing solution and absorbed CO 2 by @ 13 C (Rich a rich lean solution heat exchanger 52 for heating the solution), and supplies the CO 2 absorbing liquid 13 in the bottom of the CO 2 absorbing solution regeneration tower 15 to the upper part of the CO 2 absorbing section 141 lean solution pump 54, CO 2 A cooling unit 55 that cools the absorbent 13 (lean solution) to a predetermined temperature is provided.
- FIG. 2 is a diagram showing the relationship between the temperature of the CO 2 absorbent 13B (semi-rich solution) supplied to the lower CO 2 absorber and the ratio of the CO 2 absorption rate of the rich solution.
- the horizontal axis indicates the temperature of the CO 2 absorbent 13B
- the vertical axis indicates the ratio of the CO 2 absorption rate of the rich solution.
- the case where exhaust gas having a low CO 2 partial pressure (eg, about 10 kPa) such as combustion exhaust gas from a boiler is used is indicated by a dotted line, and CO 2 such as synthesis gas discharged directly from a reduction furnace or the like.
- the case where exhaust gas with a high partial pressure (for example, about 60 kPa) is used is indicated by a solid line.
- the plot is an analysis value. Further, in FIG. 2 shows coaxially relative to the maximum value of the absorption rate and each 1 in the temperature range of 40 ° C. or higher 70 ° C. or less, CO 2 partial pressure is low exhaust gas and CO 2 partial pressure The maximum absorption rate differs from that of high exhaust gas.
- the temperature of the CO 2 absorbing solution 13B supplies the lower the CO 2 absorbing section 141A as compared with the case where CO 2 partial pressure having a low exhaust gas, the lower the CO 2 absorbing thereby improving the CO 2 absorption rate in parts 141A, reduce the circulation amount of the CO 2 absorbing solution, to reduce the amount of heat of the heating of the CO 2 absorbing solution 13C in the CO 2 absorbing solution regeneration tower 15, to achieve energy saving.
- the control device 101 sets the temperature of the CO 2 absorbent 13B supplied to the lower CO 2 absorbent 141A to 50 ° C. or more and 60 ° C. or less. It is preferable to control.
- the CO 2 recovery apparatus 1 since the temperature of the CO 2 absorbent 13B supplied to the lower CO 2 absorber 141A is in an appropriate range, the CO 2 recovery apparatus 1 has the exhaust gas 11A generated by the CO 2 absorbent 13B in the lower CO 2 absorber 141A. Since the absorption rate of CO 2 is further improved and the circulation rate of the CO 2 absorbent 13B can be reduced by further improving the CO 2 absorption rate, consumption of the saturated water vapor S accompanying the regeneration of the CO 2 absorbent 13C is reduced. Is possible. Moreover, CO 2 recovering apparatus 1, the CO 2 absorbing solution can appropriately high temperature of the supplied CO 2 absorbing solution 13C to the regenerator 15, which also is effective in reducing the steam consumption.
- the CO 2 partial pressure in the exhaust gas 11B is preferably 50 kPa or more and 200 kPa or less. If the CO 2 partial pressure is 50 kPa or more, as shown by the solid line in FIG. 2, the CO 2 absorption rate in the lower CO 2 absorbing portion 141A tends to be different from that when the CO 2 partial pressure is low (for example, about 10 kPa). It becomes. Moreover, CO 2 partial pressure is not more than 200 kPa, it is possible to sufficiently reduce the CO 2 in the exhaust gas 11B in the CO 2 absorber 14.
- the CO 2 partial pressure in the exhaust gas 11B is more preferably 55 kPa or more, further preferably 60 kPa or more, more preferably 150 kPa or less, and even more preferably 100 kPa or less, from the viewpoint of further improving the above-described effects.
- the CO 2 partial pressure in the exhaust gas 13B is more preferably 55 kPa to 150 kPa, and still more preferably 60 kPa to 100 kPa.
- FIG. 3 is a diagram showing a relationship between heat ratio required regeneration temperature and CO 2 absorbing solution 13 supplied to the lower CO 2 absorbing section 141A CO 2 absorbing solution 13B (semi-rich solution).
- the horizontal axis represents the temperature of the CO 2 absorbent 13B
- the vertical axis represents the calorie ratio necessary for CO 2 regeneration.
- the ratio of the minimum heat amount required for the regeneration of the CO 2 absorbent 13B is set to 1. Yes.
- the plot is an analysis value.
- the amount of heat required for the regeneration of the CO 2 absorbing solution 13B in the CO 2 absorbing solution regeneration tower 15 becomes minimum at about 55 ° C., the 55 ° C.
- the amount of heat required to regenerate the CO 2 absorbing liquid 13C increases as the temperature deviates from. Accordingly, in the present embodiment, as shown in FIG. 2, the exhaust gas 11A by the CO 2 absorbing liquid 13B the temperature of the CO 2 absorbing solution 13B supplies the lower the CO 2 absorbing section 141A of the lower CO 2 absorbing section 141A
- the circulation amount of the CO 2 absorbent 13 can be reduced as the absorption rate is improved.
- FIG. 4 CO 2 absorbing solution 13C supplied to the temperature and the CO 2 absorbing solution regeneration tower 15 of the CO 2 absorbing liquid 13B to be supplied to the lower CO 2 absorbing section 141A (semi-rich solution) with the temperature of the (rich solution)
- FIG. 4 the vertical axis represents the temperature of the CO 2 absorbing solution 13C to be supplied to the CO 2 absorbing solution regeneration tower 15, the horizontal axis of the CO 2 absorbing solution 13B to be supplied to the lower CO 2 absorbing section 141A Indicates temperature.
- the temperature of the CO 2 absorbing solution 13C supplied to the temperature and the CO 2 absorbing solution regeneration tower 15 of the CO 2 absorbing liquid 13B to be supplied to the lower CO 2 absorbing section 141A are directly proportional to each other. Therefore, the temperature of the CO 2 absorbing solution 13C to be supplied to the CO 2 absorbing solution regeneration tower 15 which is measured by the thermometer 102 measures, so that the measured temperature reaches a predetermined range (e.g., 62 ° C. or higher 67 ° C.
- a predetermined range e.g., 62 ° C. or higher 67 ° C.
- CO of the control unit 101 by controlling the supply amount of CO 2 absorbing liquid 13B to the lower CO 2 absorbing section 141A by the refrigerant amount and the pump 25 supplied to the heat exchanger 24, the lower the CO 2 absorbing section 141A to It becomes possible to control 2 absorption liquid 13B to desired temperature.
- the high CO 2 absorption rate is obtained, it is possible to reduce the amount of heat of the heating of the CO 2 absorbing solution 13C in the CO 2 absorbing solution regeneration tower 15.
- Figure 5 is a diagram showing the relationship between the lower the CO 2 absorbing section and CO 2 absorption rate ratio of the upper CO 2 filling height ratio of the filler in the absorption section H1, H2 and the rich solution of the CO 2 absorber.
- the filling height ratio of the fillers H1 and H2 in the lower CO 2 absorber 141A and the upper CO 2 absorber 141B is 1: 3. It is shown as a ratio where the maximum value of the CO 2 absorption rate when changing in the range of ⁇ 3: 1 is 1.
- the CO 2 absorption rate is changed by changing the filling height ratio of the fillers of the lower CO 2 absorbing portion 141A and the upper CO 2 absorbing portion 141B.
- the filling height ratio (upper CO 2 absorption) between the filling height of the filler filler H2 in the upper CO 2 absorbing portion 141B and the filling height of the filler H1 in the lower CO 2 absorbing portion 141A.
- Part 141B: Lower CO 2 absorption part 141B) is preferably 1: 3 or more and 3: 1 or less.
- the filling height ratio is more preferably 1: 1 from the viewpoint of further improving the above-described effects.
- Exhaust gas 11A such as synthetic gas containing CO 2 discharged from the direct reduction furnace is cooled is cooled water W 1 and countercurrent contact is introduced into the cooling tower 12 the gas 11B to.
- the cooled exhaust gas 11B is introduced into the CO 2 absorption tower 14 via the flue 16, and the flow rate of the exhaust gas 11B introduced into the CO 2 absorption tower 14 is measured.
- Exhaust gas 11B introduced into the CO 2 absorber 14 is contact the CO 2 absorbing liquid 13 and a counter-flow, including lower CO 2 absorbing section 141A and upper CO 2 absorbing section 141B and alkanolamine in the CO 2 absorbing section 141, The CO 2 in the exhaust gas 11B is absorbed by the CO 2 absorbent 13 and becomes the exhaust gas 11D from which the CO 2 has been removed.
- the exhaust gas 11D from which the CO 2 has been removed rises via the chimney tray 144B and comes into gas-liquid contact with the cleaning water W 2 supplied from the top side of the water washing unit 142, and the CO 2 absorbing solution 13 accompanying the exhaust gas 11D
- the exhaust gas 11E recovered by the circulation cleaning is obtained.
- the exhaust gas 11E is trapped in the gas by the mist eliminator 145 and discharged from the top 14a of the CO 2 absorption tower 14 to the outside.
- the rich solvent pump 51 supplies the CO 2 absorbent regeneration tower 15 to the upper part.
- the CO 2 absorbent 13C flowing through the rich solution supply pipe 50 is measured at any time by the thermometer 102, and the measured temperature of the CO 2 absorbent 13C is transmitted to the control device 101.
- the control device 101 uses the refrigerant amount supplied to the heat exchanger 24 and the CO 2 absorption to the lower CO 2 absorption part 141A by the pump 25 so that the temperature of the CO 2 absorbent 13C measured by the thermometer 102 falls within a predetermined range.
- the supply amount of the liquid 13B is adjusted.
- This semi-lean solution is circulated through the circulation line L 4 by the circulation pump 33 and heated by the saturated steam S by the regenerative heater 31 to become the CO 2 absorbing solution 13 (lean solution).
- Saturated steam S after heating the water vapor condensed water W 4.
- CO 2 CO 2 gas 41 that is removed from the absorption liquid 13, after the moisture has been condensed by the condenser 42, condensed water W 5 is emitted to the outside as the CO 2 gas 44 separated from the top of the separation drum 43.
- the separated condensed water W 5 is supplied to the CO 2 absorption liquid regeneration tower 15 and partly branched and supplied to the cleaning unit 142 of the CO 2 absorption tower 14 through the reflux line L 12 .
- the CO 2 absorbent 13 (lean solution) at the bottom 15b of the CO 2 absorbent regeneration tower 15 is exchanged with the CO 2 absorbent 13C (rich solution) by the rich / lean solution heat exchanger 52 via the lean solution supply pipe 53.
- the lean solution pump 54 supplies the upper part of the CO 2 absorber 141 of the CO 2 absorber 14.
- the CO 2 absorbent 13 supplied to the CO 2 absorber 141 absorbs the CO 2 of the exhaust gas 11A by the upper CO 2 absorber 141A to become a CO 2 absorbent (semi-rich solution) 13A, and the upper CO 2 absorber 141A withdrawn in line L 11 withdrawn from the bottom.
- the extracted CO 2 absorbent 13A is cooled to a predetermined temperature range by the heat exchanger 24 to become a CO 2 absorbent (semi-rich solution) 13B, and then supplied to the lower CO 2 absorbent 141A by the pump 25.
- a CO 2 absorbent (semi-rich solution) 13B consisting of a lower CO 2 absorbing section 141A absorbs CO 2 in the exhaust gas 11B CO 2 absorbing solution and (rich solution) @ 13 C.
- This CO 2 absorbent (rich solution) 13C is extracted from the bottom 14b of the CO 2 absorption tower 14 and supplied to the CO 2 regeneration tower 15.
- the present invention describes CO 2 such as natural gas (methane gas). As long as it contains a gas, it can be applied to various gases.
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Abstract
Description
R-NH2+H2O+CO2→R-NH3HCO3
11A,11B,11C,11D,11E 排ガス
12 冷却塔
121 冷却部
122 熱交換器
123 循環ポンプ
124 調整弁
13 CO2吸収液(リーン溶液)
13A CO2吸収液
13B CO2吸収液(セミリッチ溶液)
13C CO2吸収液(リッチ溶液)
14 CO2吸収塔
14a 塔頂部
14b 塔底部
141 CO2吸収部
142 水洗部
143A 液貯留部
143B チムニートレイ
144A 液貯留部
144B チムニートレイ
145 ミストエリミネータ
15 CO2吸収液再生塔
15a 塔頂部
151 CO2吸収液供給部
16 煙道
21 熱交換器
22 循環ポンプ
23 調整弁
24 熱交換器
31 再生加熱器
32 調整弁
33 循環ポンプ
41,44 CO2ガス
42 コンデンサ
43 分離ドラム
45 凝縮水循環ポンプ
46,47 調整弁
50 リッチ溶液供給管
51 リッチ溶液ポンプ
52 リッチ・リーン溶液熱交換器
53 リーン溶液供給管
54 リーン溶液ポンプ
55 冷却部
101 制御装置
102 温度計(温度測定装置)
L1,L2,L4 循環ライン
L3,L11 抜き出しライン
L5 ガス排出ライン
L6 凝縮水ライン
L12 還流ライン
S 飽和水蒸気
W1 冷却水
W2,W3 洗浄水
W4 水蒸気凝縮水
W5 凝縮水
Claims (8)
- CO2を含む被処理気体とCO2吸収液とを接触させて前記被処理気体に含まれるCO2を前記CO2吸収液に吸収させて第1のCO2吸収液とする第1のCO2吸収部、及び前記第1のCO2吸収液とCO2を含む被処理気体とを接触させて前記被処理気体に含まれるCO2を前記第1のCO2吸収液に吸収させて第2のCO2吸収液とする第2のCO2吸収部を備えたCO2吸収塔と、
前記第2のCO2吸収液を加熱して前記第2のCO2吸収液からCO2を放出させてCO2吸収液を再生するCO2吸収液再生塔と、
前記CO2吸収塔から前記CO2吸収液再生塔に供給する第2のCO2吸収液の温度を測定する温度測定装置と、
前記温度測定装置によって測定された前記第2のCO2吸収液の温度に基づいて前記第2のCO2吸収部に供給する前記第1のCO2吸収液の温度を制御する制御装置とを具備することを特徴とする、CO2回収装置。 - 前記制御装置は、前記第2のCO2吸収部に供給する前記第1のCO2吸収液の温度を50℃以上60℃以下に制御する、請求項1に記載のCO2回収装置。
- CO2を含む被処理気体のCO2分圧が50kPa以上である、請求項1又は請求項2に記載のCO2回収装置。
- 前記第1のCO2吸収部における充填材の充填高さと前記第2のCO2吸収部における充填材の充填高さとの比(第1のCO2吸収部:第2のCO2吸収部)が、1:3以上3:1以下である、請求項1から請求項3のいずれか1項に記載のCO2回収装置。
- CO2を含む被処理気体とCO2吸収液とをCO2吸収塔の第1のCO2吸収部で接触させて前記被処理気体に含まれるCO2を前記CO2吸収液に吸収させて第1のCO2吸収液とし、前記第1のCO2吸収液とCO2を含む被処理気体とを前記CO2吸収塔の第2のCO2吸収部で接触させて前記被処理気体に含まれるCO2を前記第1のCO2吸収液に吸収させて第2のCO2吸収液とする工程と、
前記第2のCO2吸収液をCO2吸収液再生塔で加熱して前記CO2吸収液からCO2を放出させてCO2吸収液を再生する工程と、
前記CO2吸収塔から前記CO2吸収液再生塔に供給する第2のCO2吸収液の温度を測定し、測定した前記第2のCO2吸収液の温度に基づいて前記第2のCO2吸収部に供給する前記第1のCO2吸収液の温度を制御することを特徴とする、CO2回収方法。 - 前記第2のCO2吸収部に供給する前記第1のCO2吸収液の温度を50℃以上60℃以下に制御する、請求項5に記載のCO2回収方法。
- CO2を含む被処理気体のCO2分圧が50kPa以上である、請求項5又は請求項6に記載のCO2回収方法。
- 前記第1のCO2吸収部における充填材の充填高さと前記第2のCO2吸収部における充填材の充填高さとの比(第1のCO2吸収部:第2のCO2吸収部)が、1:3以上3:1以下である、請求項5から請求項7のいずれか1項に記載のCO2回収方法。
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US10773206B2 (en) * | 2018-10-10 | 2020-09-15 | Mitsubishi Heavy Industries Engineering, Ltd. | CO2 recovery device and CO2 recovery method |
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