CN105457447A - Carbon dioxide trapping system based on diphase system - Google Patents
Carbon dioxide trapping system based on diphase system Download PDFInfo
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- CN105457447A CN105457447A CN201510940922.5A CN201510940922A CN105457447A CN 105457447 A CN105457447 A CN 105457447A CN 201510940922 A CN201510940922 A CN 201510940922A CN 105457447 A CN105457447 A CN 105457447A
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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
- B01D53/1475—Removing 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
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/06—Polluted air
Abstract
The invention provides a carbon dioxide trapping system based on a diphase system. The carbon dioxide trapping system comprises an absorption tower, a first gas and liquid separator, a pregnant solution pump, a first cooler, a heat exchanger, a second cooler, a second gas and liquid separator, a desorption tower, a boiling device, a barren liquor pump and a circulating pump. In the carbon dioxide trapping system based on the diphase system, a pregnant solution of the bottom of the absorption tower is divided into an upper layer and a lower layer, the pregnant solution, which is not rich in carbon dioxide, of the upper layer enters the absorption tower again through a second outlet of the absorption tower, an inlet of the circulating pump, the circulating pump, an outlet of the circulating pump, an inlet of the first cooler, the first cooler and a second inlet of the absorption tower to be recycled, and only the pregnant solution, rich in carbon dioxide, of the lower layer enters the desorption tower through a third outlet of the absorption tower, the pregnant solution pump, the heat exchanger and a first inlet of the desorption tower to be desorbed, the size of the desorption tower is reduced, energy is saved, cost is reduced, and high-purity carbon dioxide can be trapped.
Description
Technical field
The present invention relates to collecting carbonic anhydride and reclaim field, particularly relate to a kind of carbon dioxide capture system based on two-phase absorption system.
Background technology
Carbon dioxide is one of main component of the greenhouse gases causing global warming, reaches 55% to the contribution of greenhouse effects.Carbon dioxide catches purification technique technique still based on absorption tower and desorber now, uses alkanolamine solution to make absorbent, through chemical absorbing and desorb, obtains highly purified carbon dioxide.In desorption process, main energy consumption is the boiling device at the bottom of desorber, when the amount of solution in desorber is very large, at this moment the water content in solution is also a lot, then the energy required for moisture vaporization also can improve, and this is by the raising of the power consumption increase and collecting carbonic anhydride cost that directly cause whole system.Therefore the energy consumption reducing whole system has great importance.
Utilize in the system of alkanolamine solution capturing carbon dioxide original, we generally directly can import all solution after excessive alkanolamine solution and the absorption of carbon dioxide hybrid reaction in desorber and carry out desorb.We have ignored this wherein containing not carrying out the alkanolamine solution that reacts and a large amount of water does not need to carry out desorb, this is very large by what cause our desorber to do, and energy required for desorption process also will promote, therefore the installation cost of whole absorption and desorption will improve greatly.
Summary of the invention
In view of Problems existing in background technology, one object of the present invention is to provide a kind of carbon dioxide capture system based on two-phase absorption system, and it can reduce the scale of desorber, has saved the energy, reduce cost, and highly purified carbon dioxide can be trapped.
To achieve these goals, the invention provides a kind of carbon dioxide capture system based on two-phase absorption system, it comprises: absorption tower, the first gas-liquid separator, rich solution pump, the first cooler, heat exchanger, the second cooler, the second gas-liquid separator, desorber, boiling device, lean pump and circulating pump.
Absorption tower has: absorption tower first entrance, is communicated in outside CO 2 raw material gas; Absorption tower first exports, and is arranged at the top on absorption tower; Absorption tower second entrance, is positioned at the top on absorption tower; Absorption tower second exports, and is arranged at the upside of the bottom on absorption tower; Absorption tower the 3rd entrance, is positioned at the top on absorption tower; And absorption tower the 3rd exports, and is positioned at the downside of the bottom on absorption tower.
First gas-liquid separator has: the first gas-liquid separator entrance, is communicated in absorption tower first and exports; First gas-liquid separator first exports; And first gas-liquid separator second export, be communicated in absorption tower the 3rd entrance.
Rich solution pump has: rich solution pump intake, is communicated with absorption tower the 3rd and exports; And rich solution pump discharge.
First cooler has: the first cooler entrance; First cooler outlet, is communicated in absorption tower second entrance.
Heat exchanger has: heat exchanger first entrance, is communicated with rich solution pump discharge; Heat exchanger first exports; Heat exchanger second entrance; And heat exchanger second exports, be communicated in the first cooler entrance.
Second cooler has: the second cooler entrance; And second cooler outlet.
Second gas-liquid separator has: the second gas-liquid separator entrance, is communicated with the second cooler outlet; Second gas-liquid separator first exports; And second gas-liquid separator second export.
Desorber has: desorber first entrance, is positioned at the top of desorber, is communicated with heat exchanger first and exports; Desorber first exports, and is positioned at the bottom of desorber; Desorber second entrance, is positioned at the top of desorber, is communicated in the second gas-liquid separator second and exports; Desorber second exports, and is positioned at the top of desorber, is communicated in the second cooler entrance; Desorber the 3rd entrance, is positioned at the bottom of desorber; And desorber the 3rd exports, and is positioned at the bottom of desorber.
Boiling device has: boiling device entrance, is communicated in desorber the 3rd outlet; And boiling device outlet, be communicated in desorber the 3rd entrance.
Lean pump has: lean pump entrance, is communicated in desorber first and exports; And lean pump outlet, be communicated in heat exchanger second entrance.
Circulating pump has: pump entry, is communicated in absorption tower second and exports; And circulating-pump outlet, be communicated in the first cooler entrance.
Wherein, outside CO 2 raw material gas enters absorption tower via absorption tower first entrance, spray with the top from absorption tower fed via absorption tower second entrance in absorption tower and absorbent counter current contacting, carbon dioxide in absorbent absorbing carbon dioxide unstripped gas is changed to rich solution, and remaining unstripped gas exports via absorption tower first, the first gas-liquid separator entrance enters in the first gas-liquid separator and carry out gas-liquid separation.
In the first gas-liquid separator, isolated gas exports via the first gas-liquid separator first and discharges, and isolated liquid exports via the first gas-liquid separator second, absorption tower the 3rd entrance enters in absorption tower and recycles.
The rich solution being collected in the bottom on absorption tower is layered as two-layer up and down, and upper strata is not rich carbonated rich solution, and lower floor is rich carbonated rich solution.Not rich carbonated rich solution exports via absorption tower second and pump entry enters circulating pump, then enters in the first cooler via circulating-pump outlet and the first cooler entrance under the effect of circulating pump; Rich carbonated rich solution exports via absorption tower the 3rd and rich solution pump intake enters rich solution pump, then enters in heat exchanger via rich solution pump discharge and heat exchanger first entrance under the effect of rich solution pump and carries out heat exchange, with intensification of absorbing heat.
Carry out the rich solution after heat exchange to export via heat exchanger first and desorber first entrance enters desorber, export via desorber the 3rd again, boiling device entrance enters boiling device and by heating desorption, be decomposed into carbon dioxide and lean solution, carbon dioxide and lean solution enter desorber again via boiling device outlet and desorber the 3rd entrance, carbon dioxide moves upward and to export via desorber second and the second cooler entrance enters the second cooler, after cooling in the second cooler, warp is by the second cooler outlet, second gas-liquid separator entrance to enter in the second gas-liquid separator and carries out gas-liquid separation, in the second gas-liquid separator, isolated gas exports via the second gas-liquid separator first and discharges, isolated liquid exports via the second gas-liquid separator second, desorber second entrance reenters in desorber and recycles.
The lean solution of desorber congregate exports via desorber first and lean pump entrance enters lean pump, then under the effect of lean pump, enter the rich solution flowing through heat exchanger in heat exchanger with above-mentioned via lean pump outlet and heat exchanger second entrance and carry out heat exchange, lower the temperature with heat release; Carry out the lean solution after heat exchange to export via heat exchanger second and the first cooler entrance enters the first cooler, and reenter absorption tower as absorbent via the first cooler outlet and absorption tower second entrance together with the not rich carbonated rich solution entering the first cooler.
Beneficial effect of the present invention is as follows:
In the carbon dioxide capture system based on two-phase absorption system according to the present invention, the rich solution being collected in the bottom on absorption tower is divided into two-layer up and down, and the not rich carbonated rich solution in upper strata exports via absorption tower second, pump entry, circulating pump, circulating-pump outlet, the first cooler entrance, the first cooler and absorption tower second entrance reenter in absorption tower and recycle; Only have the rich carbonated rich solution of lower floor to enter in desorber via absorption tower the 3rd outlet, rich solution pump, heat exchanger and desorber first entrance and carry out desorb, thus reduce the scale of desorber, save the energy, reduced cost, and highly purified carbon dioxide can have been trapped.
Accompanying drawing explanation
Fig. 1 is the process flow diagram according to the carbon dioxide capture system based on two-phase absorption system of the present invention.
Wherein, description of reference numerals is as follows:
11 absorption towers
11A1 absorption tower first entrance
11B1 absorption tower first exports
11A2 absorption tower second entrance
11B2 absorption tower second exports
11A3 absorption tower the 3rd entrance
11B3 absorption tower the 3rd exports
12 first gas-liquid separators
12A first gas-liquid separator entrance
12B1 first gas-liquid separator first exports
12B2 first gas-liquid separator second exports
13 rich solution pumps
13A rich solution pump intake
13B rich solution pump discharge
14 first coolers
14A first cooler entrance
14B first cooler outlet
15 heat exchangers
15A1 heat exchanger first entrance
15B1 heat exchanger first exports
15A2 heat exchanger second entrance
15B2 heat exchanger second exports
16 second coolers
16A second cooler entrance
16B second cooler outlet
17 second gas-liquid separators
17A second gas-liquid separator entrance
17B1 second gas-liquid separator first exports
17B2 second gas-liquid separator second exports
18 desorbers
18A1 desorber first entrance
18B1 desorber first exports
18A2 desorber second entrance
18B2 desorber second exports
18A3 desorber the 3rd entrance
18B3 desorber the 3rd exports
19 boiling devices
19A boiling device entrance
19B boiling device exports
20 lean pumps
20A lean pump entrance
20B lean pump exports
21 circulating pumps
21A pump entry
21B circulating-pump outlet
22 liquid level display controllers
Detailed description of the invention
Describe in detail with reference to the accompanying drawings according to the carbon dioxide capture system based on two-phase absorption system of the present invention.
With reference to Fig. 1, the carbon dioxide capture system based on two-phase absorption system according to the present invention comprises: absorption tower 11, first gas-liquid separator 12, rich solution pump 13, first cooler 14, heat exchanger 15, second cooler 16, second gas-liquid separator 17, desorber 18, boiling device 19, lean pump 20 and circulating pump 21.
Absorption tower 11 has: absorption tower first entrance 11A1, is communicated in outside CO 2 raw material gas; Absorption tower first exports 11B1, is arranged at the top on absorption tower 11; Absorption tower second entrance 11A2, is positioned at the top on absorption tower 11; Absorption tower second exports 11B2, is arranged at the upside of the bottom on absorption tower 11; Absorption tower the 3rd entrance 11A3, is positioned at the top on absorption tower 11; And absorption tower the 3rd exports 11B3, is positioned at the downside of the bottom on absorption tower 11.
First gas-liquid separator 12 has: the first gas-liquid separator entrance 12A, is communicated in absorption tower first and exports 11B1; First gas-liquid separator first exports 12B1; And first gas-liquid separator second export 12B2, be communicated in absorption tower the 3rd entrance 11A3.
Rich solution pump 13 has: rich solution pump intake 13A, is communicated with absorption tower the 3rd and exports 11B3; And rich solution pump discharge 13B.
First cooler 14 has: the first cooler entrance 14A; First cooler outlet 14B, is communicated in absorption tower second entrance 11A2.
Heat exchanger 15 has: heat exchanger first entrance 15A1, is communicated with rich solution pump discharge 13B; Heat exchanger first exports 15B1; Heat exchanger second entrance 15A2; And heat exchanger second exports 15B2, be communicated in the first cooler entrance 14A.
Second cooler 16 has: the second cooler entrance 16A; And the second cooler outlet 16B.
Second gas-liquid separator 17 has: the second gas-liquid separator entrance 17A, is communicated with the second cooler outlet 16B; Second gas-liquid separator first exports 17B1; And second gas-liquid separator second export 17B2.
Desorber 18 has: desorber first entrance 18A1, is positioned at the top of desorber 18, is communicated with heat exchanger first and exports 15B1; Desorber first exports 18B1, is positioned at the bottom of desorber 18; Desorber second entrance 18A2, is positioned at the top of desorber 18, is communicated in the second gas-liquid separator second and exports 17B2; Desorber second exports 18B2, is positioned at the top of desorber 18, is communicated in the second cooler entrance 16A; Desorber the 3rd entrance 18A3, is positioned at the bottom of desorber 18; And desorber the 3rd exports 18B3, is positioned at the bottom of desorber 18.
Boiling device 19 has: boiling device entrance 19A, is communicated in desorber the 3rd and exports 18B3; And boiling device outlet 19B, be communicated in desorber the 3rd entrance 18A3.
Lean pump 20 has: lean pump entrance 20A, is communicated in desorber first and exports 18B1; And lean pump outlet 20B, be communicated in heat exchanger second entrance 15A2.
Circulating pump 21 has: pump entry 21A, is communicated in absorption tower second and exports 11B2; And circulating-pump outlet 21B, be communicated in the first cooler entrance 14A.
Wherein, outside CO 2 raw material gas enters absorption tower 11 via absorption tower first entrance 11A1, spray with the top from absorption tower 11 fed via absorption tower second entrance 11A2 in absorption tower 11 and absorbent counter current contacting, carbon dioxide in absorbent absorbing carbon dioxide unstripped gas is changed to rich solution, and remaining unstripped gas exports 11B1 via absorption tower first, the first gas-liquid separator entrance 12A enters in the first gas-liquid separator 2 and carry out gas-liquid separation.
In the first gas-liquid separator 2, isolated gas exports 12B1 discharge via the first gas-liquid separator first, and isolated liquid exports 12B2 via the first gas-liquid separator second, absorption tower the 3rd entrance 11A3 enters in absorption tower 11 and recycles.
The rich solution being collected in the bottom on absorption tower 11 is layered as two-layer up and down, and upper strata is not rich carbonated rich solution, and lower floor is rich carbonated rich solution.Not rich carbonated rich solution exports 11B2 via absorption tower second and pump entry 21A enters circulating pump 21, then enters in the first cooler 14 via circulating-pump outlet 21B and the first cooler entrance 14A under the effect of circulating pump 21; Rich carbonated rich solution exports 11B3 and rich solution pump intake 13A via absorption tower the 3rd and enters rich solution pump 13, then enter in heat exchanger 15 via rich solution pump discharge 13B and heat exchanger first entrance 15A1 under the effect of rich solution pump 13 and carry out heat exchange, with intensification of absorbing heat.
Carry out the rich solution after heat exchange and export 15B1 via heat exchanger first and desorber first entrance 18A1 enters desorber 18, 18B3 is exported again via desorber the 3rd, boiling device entrance 19A enters boiling device 19 and by heating desorption, be decomposed into carbon dioxide and lean solution, carbon dioxide and lean solution enter desorber 18 again via boiling device outlet 19B and desorber the 3rd entrance 18A3, carbon dioxide moves upward and exports 18B2 via desorber second and the second cooler entrance 16A enters the second cooler 16, after cooling in the second cooler 16, warp is by the second cooler outlet 16B, second gas-liquid separator entrance 17A to enter in the second gas-liquid separator 17 and carries out gas-liquid separation, in the second gas-liquid separator 17, isolated gas exports 17B1 discharge via the second gas-liquid separator first, isolated liquid exports 17B2 via the second gas-liquid separator second, desorber second entrance 18A2 reenters in desorber 18 and recycles.
The lean solution of desorber congregate exports 18B1 via desorber first and lean pump entrance 20A enters lean pump 20, then under the effect of lean pump 20, enter the rich solution flowing through heat exchanger 15 in heat exchanger 15 with above-mentioned via lean pump outlet 20B and heat exchanger second entrance 15A2 and carry out heat exchange, lower the temperature with heat release; Carry out the lean solution after heat exchange and export 15B2 via heat exchanger second and the first cooler entrance 14A enters the first cooler 14, and reenter absorption tower 11 as absorbent via the first cooler outlet 14B and absorption tower second entrance 11A2 together with the not rich carbonated rich solution entering the first cooler 14.
In the carbon dioxide capture system based on two-phase absorption system according to the present invention, the rich solution being collected in the bottom on absorption tower 11 is divided into two-layer up and down, and the not rich carbonated rich solution in upper strata exports 11B2, pump entry 21A, circulating pump 21, circulating-pump outlet 21B, the first cooler entrance 14A, the first cooler 14 and absorption tower second entrance 11A2 via absorption tower second and reenters in absorption tower 11 and recycle; Only have the rich carbonated rich solution of lower floor to enter in desorber 18 via absorption tower the 3rd outlet 11B3, rich solution pump 13, heat exchanger 15 and desorber first entrance 18A1 and carry out desorb, thus reduce the scale of desorber, save the energy, reduce cost, and highly purified carbon dioxide can be trapped.
Here remark additionally, the absorbent in two-phase absorption system is two-phase absorbent, and so-called two-phase absorbent refers to after absorption CO2, and absorbent is divided into the liquid phase that upper and lower two-layer CO2 load capacity difference is larger, and nearly all CO2 concentrates on lower floor.Particularly, being collected in the two-layer up and down of the rich solution of the bottom on absorption tower 11 is liquid-liquid two-phase, and lower floor obtains rich carbonated rich solution, and upper strata obtains not rich carbonated rich solution.
According to the carbon dioxide capture system based on two-phase absorption system of the present invention, in one embodiment, with reference to Fig. 1, the described carbon dioxide capture system based on two-phase absorption system also comprises: liquid level display controller 22, be communicatively coupled to circulating pump 21 and rich solution pump 13, with by the not rich carbonated rich solution bottom absorption tower 11 and the carbonated rich solution of richness two-layer between layered position carry out monitoring and the break-make of controlled circulation pump 21 and rich solution pump 13.Based on the interruption coordinating operation that liquid level display controller 22 controlled circulation pump 21 and rich solution pump 13 carry out, thus can ensure that the liquid level of two phase stratification is as far as possible constant.
In one embodiment, the first cooler 14 is water cooler, but not only for so, also can adopt the cooler of other type.
In one embodiment, the second cooler 16 is water cooler, but not only for so, also can adopt the cooler of other type.
In one embodiment, absorbent can be lipophilic class amine aqueous solution.Lipophilic class amine aqueous solution has the feature of low critical-temperature, can form organic layer-water layer two phase liquid after temperature is higher than critical-temperature, and namely the organic layer of lower floor is rich carbonated rich solution, and upper aqueous layer is not rich carbonated rich solution.Further, absorbent can be alkanolamine solution, and this is the type of the preferred absorbent of the present invention, but not only for so.What here remark additionally is, be alkanolamine solution based on the absorbent selected by the present invention, therefore the upper strata of bilevel rich solution that is divided into being collected in the bottom on absorption tower 11 is not hydroxyl amine and the solution (i.e. not rich carbonated rich solution) containing about 30% water, and lower floor is hydramine and the solution (i.e. rich carbonated rich solution) containing about 70% water.
In one embodiment, boiling device 19 can be shell-and-tube heat exchanger.
In one embodiment, outside CO 2 raw material gas can be passed through the pressurization of blower fan (not shown) before entering absorption tower 11 via absorption tower first entrance 11A1.
Claims (8)
1. based on a carbon dioxide capture system for two-phase absorption system, it is characterized in that, comprising: absorption tower (11), have:
Absorption tower first entrance (11A1), is communicated in outside CO 2 raw material gas;
Absorption tower first exports (11B1), is arranged at the top of absorption tower (11);
Absorption tower second entrance (11A2), is positioned at the top of absorption tower (11);
Absorption tower second exports (11B2), is arranged at the upside of the bottom on absorption tower (11);
Absorption tower the 3rd entrance (11A3), is positioned at the top of absorption tower (11); And
Absorption tower the 3rd exports (11B3), is positioned at the downside of the bottom on absorption tower (11);
First gas-liquid separator (12), has:
First gas-liquid separator entrance (12A), is communicated in absorption tower first and exports (11B1);
First gas-liquid separator first exports (12B1); And
First gas-liquid separator second exports (12B2), is communicated in absorption tower the 3rd entrance (11A3);
Rich solution pump (13), has:
Rich solution pump intake (13A), is communicated with absorption tower the 3rd and exports (11B3); And
Rich solution pump discharge (13B);
First cooler (14), has:
First cooler entrance (14A);
First cooler outlet (14B), is communicated in absorption tower second entrance (11A2);
Heat exchanger (15), has:
Heat exchanger first entrance (15A1), is communicated with rich solution pump discharge (13B);
Heat exchanger first exports (15B1);
Heat exchanger second entrance (15A2); And
Heat exchanger second exports (15B2), is communicated in the first cooler entrance (14A);
Second cooler (16), has:
Second cooler entrance (16A); And
Second cooler outlet (16B);
Second gas-liquid separator (17), has:
Second gas-liquid separator entrance (17A), is communicated with the second cooler outlet (16B);
Second gas-liquid separator first exports (17B1); And
Second gas-liquid separator second exports (17B2);
Desorber (18), has:
Desorber first entrance (18A1), is positioned at the top of desorber (18), is communicated with heat exchanger first and exports (15B1);
Desorber first exports (18B1), is positioned at the bottom of desorber (18);
Desorber second entrance (18A2), is positioned at the top of desorber (18), is communicated in the second gas-liquid separator second and exports (17B2);
Desorber second exports (18B2), is positioned at the top of desorber (18), is communicated in the second cooler entrance (16A);
Desorber the 3rd entrance (18A3), is positioned at the bottom of desorber (18); And
Desorber the 3rd exports (18B3), is positioned at the bottom of desorber (18);
Boiling device (19), has:
Boiling device entrance (19A), is communicated in desorber the 3rd and exports (18B3); And
Boiling device outlet (19B), is communicated in desorber the 3rd entrance (18A3);
Lean pump (20), has:
Lean pump entrance (20A), is communicated in desorber first and exports (18B1); And
Lean pump outlet (20B), is communicated in heat exchanger second entrance (15A2);
Circulating pump (21), has:
Pump entry (21A), is communicated in absorption tower second and exports (11B2); And
Circulating-pump outlet (21B), is communicated in the first cooler entrance (14A);
Wherein,
Outside CO 2 raw material gas enters absorption tower (11) via absorption tower first entrance (11A1), in absorption tower (11) with via absorption tower second entrance (11A2) feed from the top of absorption tower (11) spray and absorbent counter current contacting, carbon dioxide in absorbent absorbing carbon dioxide unstripped gas is changed to rich solution, and remaining unstripped gas exports (11B1) via absorption tower first, the first gas-liquid separator entrance (12A) enters in the first gas-liquid separator (2) and carry out gas-liquid separation;
In the first gas-liquid separator (2), isolated gas exports (12B1) discharge via the first gas-liquid separator first, and isolated liquid exports (12B2) via the first gas-liquid separator second, absorption tower the 3rd entrance (11A3) enters in absorption tower (11) and recycles;
The rich solution being collected in the bottom on absorption tower (11) is layered as two-layer up and down, and upper strata is not rich carbonated rich solution, and lower floor is rich carbonated rich solution;
Not rich carbonated rich solution exports (11B2) via absorption tower second and pump entry (21A) enters circulating pump (21), then enters in the first cooler (14) via circulating-pump outlet (21B) and the first cooler entrance (14A) under the effect of circulating pump (21);
Rich carbonated rich solution exports (11B3) via absorption tower the 3rd and rich solution pump intake (13A) enters rich solution pump (13), then enter in heat exchanger (15) via rich solution pump discharge (13B) and heat exchanger first entrance (15A1) under the effect of rich solution pump (13) and carry out heat exchange, with intensification of absorbing heat;
Carry out the rich solution after heat exchange and export (15B1) via heat exchanger first and desorber first entrance (18A1) enters desorber (18), (18B3) is exported again via desorber the 3rd, boiling device entrance (19A) enters boiling device (19) and by heating desorption, be decomposed into carbon dioxide and lean solution, carbon dioxide and lean solution enter desorber (18) again via boiling device outlet (19B) and desorber the 3rd entrance (18A3), carbon dioxide moves upward and exports (18B2) via desorber second and the second cooler entrance (16A) enters the second cooler (16), after cooling in the second cooler (16), warp is by the second cooler outlet (16B), second gas-liquid separator entrance (17A) to enter in the second gas-liquid separator (17) and carries out gas-liquid separation, in the second gas-liquid separator (17), isolated gas exports (17B1) discharge via the second gas-liquid separator first, isolated liquid exports (17B2) via the second gas-liquid separator second, desorber second entrance (18A2) reenters in desorber (18) and recycles,
The lean solution of desorber congregate exports (18B1) via desorber first and lean pump entrance (20A) enters lean pump (20), then under the effect of lean pump (20), enter the rich solution flowing through heat exchanger (15) in heat exchanger (15) with above-mentioned via lean pump outlet (20B) and heat exchanger second entrance (15A2) and carry out heat exchange, lower the temperature with heat release; Carry out the lean solution after heat exchange and export (15B2) via heat exchanger second and the first cooler entrance (14A) enters the first cooler (14), and reenter absorption tower (11) as absorbent via the first cooler outlet (14B) and absorption tower second entrance (11A2) together with the not rich carbonated rich solution entering the first cooler (14).
2. the carbon dioxide capture system based on two-phase absorption system according to claim 1, is characterized in that, the described carbon dioxide capture system based on two-phase absorption system also comprises:
Liquid level display controller (22), be communicatively coupled to circulating pump (21) and rich solution pump (13), with by the not rich carbonated rich solution of absorption tower (11) bottom and the carbonated rich solution of richness two-layer between layered position carry out monitoring and the break-make of controlled circulation pump (21) and rich solution pump (13).
3. the carbon dioxide capture system based on two-phase absorption system according to claim 1, is characterized in that, the first cooler (14) is water cooler.
4. the carbon dioxide capture system based on two-phase absorption system according to claim 1, is characterized in that, the second cooler (16) is water cooler.
5. the carbon dioxide capture system based on two-phase absorption system according to claim 1, is characterized in that, absorbent is lipophilic class amine aqueous solution.
6. the carbon dioxide capture system based on two-phase absorption system according to claim 5, is characterized in that, absorbent is alkanolamine solution.
7. the carbon dioxide capture system based on two-phase absorption system according to claim 1, is characterized in that, boiling device (19) is shell-and-tube heat exchanger.
8. the carbon dioxide capture system based on two-phase absorption system according to claim 1, it is characterized in that, outside CO 2 raw material gas pressurizes through blower fan before entering absorption tower (11) via absorption tower first entrance (11A1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510940922.5A CN105457447A (en) | 2015-12-16 | 2015-12-16 | Carbon dioxide trapping system based on diphase system |
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| CN106731600A (en) * | 2016-12-20 | 2017-05-31 | 新疆敦华石油技术股份有限公司 | A kind of collecting carbonic anhydride liquefying plant |
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