CN106000009A - Twin-tower MEDA landfill treating gas system - Google Patents
Twin-tower MEDA landfill treating gas system Download PDFInfo
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- CN106000009A CN106000009A CN201610571782.3A CN201610571782A CN106000009A CN 106000009 A CN106000009 A CN 106000009A CN 201610571782 A CN201610571782 A CN 201610571782A CN 106000009 A CN106000009 A CN 106000009A
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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
- B01D53/14—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
- B01D53/1456—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
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
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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
- B01D2252/60—Additives
- B01D2252/602—Activators, promoting agents, catalytic agents or enzymes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention belongs to the technical field of environmental engineering protection and gas purification treatment, and particularly relates to a twin-tower MEDA landfill gas treating system which can effectively treat harmful gas like CO2 and H2S in landfill gas. The twin-tower MEDA landfill treating gas system comprises a raw material gas tank, a raw material gas pressurizing pump, an absorbing tower, a sleeve-type microreactor, an activator piperazine inlet, a gas-liquid separator, a hydraulic turbine, a circulating pump, a flash evaporator, a rich-lean liquid heat exchanger, a semi-lean liquid heat exchanger, a regeneration tower, a reboiler, a cooling water tank, a heat pump, a separator, an acid water backflow pump, an acid gas recycling tank, a semi-lean liquid aftercooler, a lean liquid aftercooler, an MDEA circulating pump, a washing tank backflow pump, a water washing tank and a treated gas collection tank. The twin-tower MEDA landfill gas treating system is structurally characterized in that the sleeve-type microreactor is arranged in a cavity on one side in the absorbing cavity.
Description
Technical field
The invention belongs to environmental project protection and gas purification processes technical field, particularly relate to a kind of double-tower type MEDA and process landfill gas system.
Background technology
Solvent absorption trapping CO2And H2S is the method being most widely used at present, with methyl diethanolamine (MDEA) as absorbing liquid, adds activator piperazine and can be effectively improved its absorbability in MDEA.MEDA compares that other regeneration of absorption solution is easy, energy consumption is low, at the bottom of MEDA vapour pressure, absorbs acid gas solvent loss few, and solvent is to CO2And H2S load capacity is big, and degree of purification is high, is the acid gas removal agent of the high-efficiency low energy consumption that a kind of chemical method purifies.But for single absorption CO2Or H2The removal efficiency of S, MDEA can be the highest, especially to CO2More than 95% can be reached.
So problem is just at MDEA and H2S、CO2Response difference there are differences, cause MDEA solution absorb H2S and CO2Speed different, so that MDEA can be containing H2S and CO2System in selective absorbing H2S.Therefore, make great efforts to improve to accelerate CO2Speed be so that MDEA solution absorbs CO simultaneously2And H2S is crucial.
Summary of the invention
The present invention is aiming at the problems referred to above, it is provided that a kind of can effectively process the CO in landfill gas2And H2The double-tower type MEDA of the harm therein gas such as S processes landfill gas system.
For achieving the above object, the present invention adopts the following technical scheme that, the present invention includes raw material gas tank, unstripped gas booster pump, absorption tower, bushing type microreactor, activator piperazine entrance, gas-liquid separator, hydraulic turbine, circulating pump, flash vessel, poor rich liquid heat exchanger, semi lean solution heat exchanger, regenerator, reboiler, cooling water tank, heat pump, separator, sour water reflux pump, acid gas collection box, semi lean solution aftercooler, lean solution aftercooler, MDEA circulating pump, sink reflux pump, water washing groove, regulate the flow of vital energy collecting box in place, its structural feature bushing type microreactor is arranged in absorption tower in the cavity of side, activator piperazine entrance connects with bushing type microreactor outboard chambers and is arranged on cavity bottom, the lower end import of bushing type microreactor is connected with raw material gas tank by unstripped gas booster pump.
Cavity upper end above bushing type microreactor upper end outlet is provided with vertical exit, vertical exit is connected with the gas-liquid separator entrance of upper end in absorption tower, gas-liquid separator upper end gas outlet is connected with water washing groove, the gas outlet of water washing groove collecting box of regulating the flow of vital energy with place is connected, and the liquid outlet of water washing groove is connected with the centre inlet of vertical regenerator by sink reflux pump；Gas-liquid separator is provided with downward liquid outlet away from cavity side lower end, in liquid outlet absorption tower outer with cavity, space connects, lower end, absorption tower is provided with the horizontal rich solution outlet connected with space in absorption tower outside cavity, rich solution outlet is connected with the import of hydraulic turbine, the outlet of hydraulic turbine by flash vessel respectively the first heat exchanger channels entrance with poor rich liquid heat exchanger, semi lean solution heat exchanger be connected, poor rich liquid heat exchanger, the first heat exchanger channels of semi lean solution heat exchanger export and are connected with the rich solution import of reboiler.
The drive output of hydraulic turbine is connected with the driving input of circulating pump, circulation delivery side of pump is connected with the semi lean solution import being arranged on cavity bottom with the connection of bushing type microreactor outboard chambers, the import of circulating pump is connected with the second heat exchanger channels outlet of semi lean solution heat exchanger by semi lean solution aftercooler, and the second heat exchanger channels entrance of semi lean solution heat exchanger is connected with semi lean solution outlet in the middle part of regenerator.
Second heat exchanger channels entrance of poor rich liquid heat exchanger is connected with the outlet of regenerator lower end lean solution, and the second heat exchanger channels outlet of poor rich liquid heat exchanger passes sequentially through lean solution aftercooler, MDEA circulating pump is connected with the lean solution import being arranged on cavity top with the connection of bushing type microreactor outboard chambers.
The gas outlet of reboiler is connected with the gas access of regenerator bottom, and the semi lean solution outlet of reboiler is connected with the liquid inlet of regenerator bottom；The semi lean solution outlet of regenerator lower end is connected with semi lean solution entrance, the heat pump semi lean solution heating gate of reboiler respectively.
The condensation-water drain of reboiler is connected with the condensing water inlet of cooling water tank, and the condensation-water drain of cooling water tank is connected with the heat exchanging liquid import of heat pump, and the heat exchanging liquid outlet of heat pump is connected with condensing water inlet after the heat exchange of cooling water tank；The recuperated gas entrance of heat pump is connected with the sour moisture outlet of the heat of regenerator upper end, export the entrance with separator after the heat exchange of heat pump to be connected, the acid gas outlet of separator is connected with acid gas collection box, and the sour water outlet of separator is connected with the sour water refluxing opening of regenerator upper end by sour water reflux pump.
It is provided with valve as between the second heat exchanger channels outlet of a kind of preferred version, semi lean solution aftercooler of the present invention and semi lean solution heat exchanger.
As another kind of preferred version, between the second heat exchanger channels entrance of poor rich liquid heat exchanger of the present invention and the outlet of regenerator lower end lean solution, it is provided with valve.
Secondly, it is provided with valve between MDEA circulating pump of the present invention and lean solution import.
It addition, flashed vapour outlet in flash vessel top of the present invention is connected with regenerator or acid gas collection box.
Beneficial effect of the present invention.
The present invention with the addition of hydraulic turbine installation and the fluid pressure of rich solution can be utilized to be converted into the mechanical energy of circulating pump.The heat energy that with the addition of heat pump reclaiming tower acid water provides reboiler heater.With the addition of bushing type microreactor and coordinate CO2And H2The absorption of S so that the maximization of absorption efficiency.Maximum feature can utilize semi lean solution to flow back into absorption tower, reduces reboiler section and reheats.The tank washing that finally with the addition of absorption tower dampness absorbs the harmful gas that can be dissolved in water further.This flow path device can be accomplished almost without pollution, the maximized re-using of the energy, and can accomplish CO simultaneously2And H2S maximizes advantages such as coordinating absorption.
It is generally acknowledged that MEDA removes CO2Efficiency be up to more than 95%, if process H simultaneously2S, then remove H2The efficiency of S can be the lowest.This is because speed different during reaction, MEDA and CO2During reaction partially slow and and H2S is the most fast.So using a kind of bushing type microreactor and activator piperazine then can accelerate MEDA and CO2Reaction allows itself and H2The reaction of S reaches to synchronize.The heat energy using the pressure of hydraulic turbine and heat pump withdrawal liquid to reclaim sour water to circulating pump supply mechanical energy and heat pump in terms of energy recovery supplies the semi lean solution boiled again.And be additionally arranged again rich or poor/half poor rich liquid heat exchanger can with MDEA rich solution carry out heat exchange reclaim heat energy.After arranging two, refrigerator is respectively half lean/lean solution aftercooler.Reduce the remaining temperature after lean/semi lean solution heat exchange rapidly, it is ensured that reach the condition of absorption tower internal-response.Prevent the temperature within regenerator from MDEA turning lean impact.Employing reboiler, the semi lean solution entrance reboiler bottom regenerator, then semi lean solution and the reboiler upper steam after boiling return again regenerator.The produced water that condenses of reboiler can be delivered directly to cooling water tank, so can make full use of and saving water resource.
It is generally acknowledged that condensation water is that comparison totally and is cleaned.On the top of regenerator, out sour water gas carries out gas-liquid separation with separator after heat pump, and sour water is reclaimed by sour water reflux pump and enters regenerator, and acid gas acid gas collection box reclaims.On absorption tower, purification gas out is through water washing groove, H2S is dissolved in water and CO2It is slightly soluble in water and the harmful gas not absorbed in time can be retrieved washing, can directly connect regenerator after washing and be further processed.Major part uses transport pump to carry out the process of gas purification step by step in this process.
The present invention adds a bushing type microreactor and adds activator piperazine quickening MDEA and CO2Reaction, so can meet MDEA and H2S and CO2Coordination absorb.It is uneconomic for also having traditional double-tower type to process landfill gas, such as from absorption tower, rich solution out through pressurization, is therefore added to hydraulic turbine installation in view of withdrawal liquid pressure and reclaims to not waste the energy and can be recycled into absorption tower to circulating pump energy supply for semi lean solution.This technique adds semi lean solution and lean solution two cooling line and enters absorption tower, reduce semi lean solution and save the energy through reboiler process of boiling the most again.
Use heat pump that the heat energy heat exchange of cooling water and acid gas is connect boiling again of reboiler supply semi lean solution the heat energy after heat exchange again when reclaiming the heat energy of acid gas.The condensation water of acid gas is discharged through separator acid gas after heat pump and is collected, and sour water flows back into regenerator.In order to absorption tower can not absorb CO efficiently2And H2S, allows wet purification gas wash through water washing groove, and after washing, cleaning mixture returns regenerator by CO2And H2S separates out.Whole device technique absorbs CO to accelerate absorption tower2It is main for efficiently utilizing hydraulic pressure heat energy, can be substantially reduced the cost purifying technique.Crucial whole technique will not produce secondary pollution, protects environment, removes CO2And H2The advantages such as the efficiency of S.
Accompanying drawing explanation
The present invention will be further described with detailed description of the invention below in conjunction with the accompanying drawings.Scope is not only limited to the statement of herein below.
Fig. 1 is present configuration schematic diagram.
In figure, 1 is raw material gas tank, 2 is unstripped gas booster pump, 3 is absorption tower, 4 is bushing type microreactor, 5 is activator piperazine entrance, 6 is gas-liquid separator, 7 is hydraulic turbine, 8 is circulating pump, 9 is flash vessel, 10 is poor rich liquid heat exchanger, 11 is semi lean solution heat exchanger, 12 is regenerator, 13 is reboiler, 14 is cooling water tank, 15 is heat pump, 16 is separator, 17 is sour water reflux pump, 18 is acid gas collection box, 19 is cold air after semi lean solution, 20 is lean solution aftercooler, 21 is MDEA circulating pump, 22 is sink reflux pump, 23 is water washing groove, 24 regulate the flow of vital energy collecting box for place.
Detailed description of the invention
nullAs shown in the figure，The present invention includes raw material gas tank (1)、Unstripped gas booster pump (2)、Absorption tower (3)、Bushing type microreactor (4)、Activator piperazine entrance (5)、Gas-liquid separator (6)、Hydraulic turbine (7)、Circulating pump (8)、Flash vessel (9)、Poor rich liquid heat exchanger (10)、Semi lean solution heat exchanger (11)、Regenerator (12)、Reboiler (13)、Cooling water tank (14)、Heat pump (15)、Separator (16)、Sour water reflux pump (17)、Acid gas collection box (18)、Semi lean solution aftercooler (19)、Lean solution aftercooler (20)、MDEA circulating pump (21)、Sink reflux pump (22)、Water washing groove (23)、Regulate the flow of vital energy collecting box (24) in place，Bushing type microreactor (4) is arranged in the cavity of absorption tower (3) interior side，Activator piperazine entrance (5) connects with bushing type microreactor (4) outboard chambers and is arranged on cavity bottom，Bushing type microreactor (4) lower end import is connected with raw material gas tank (1) by unstripped gas booster pump (2).
Cavity upper end above bushing type microreactor (4) upper end outlet is provided with vertical exit, vertical exit is connected with gas-liquid separator (6) entrance of absorption tower (3) interior upper end, gas-liquid separator (6) upper end gas outlet is connected with water washing groove (23), the gas outlet of water washing groove (23) collecting box (24) of regulating the flow of vital energy with place is connected, and the liquid outlet of water washing groove (23) is connected with the centre inlet of vertical regenerator (12) by sink reflux pump (22)；Gas-liquid separator (6) is provided with downward liquid outlet away from cavity side lower end, liquid outlet absorption tower (3) interior space outer with cavity connects, absorption tower (3) lower end is provided with the horizontal rich solution outlet that absorption tower (3) interior space outer with cavity connects, rich solution outlet is connected with the import of hydraulic turbine (7), the outlet of hydraulic turbine (7) by flash vessel (9) respectively with poor rich liquid heat exchanger (10), first heat exchanger channels entrance of semi lean solution heat exchanger (11) is connected, poor rich liquid heat exchanger (10), first heat exchanger channels outlet of semi lean solution heat exchanger (11) is connected with the rich solution import of reboiler (13).
The drive output of hydraulic turbine (7) is connected with the driving input of circulating pump (8), the outlet of circulating pump (8) is connected with the semi lean solution import being arranged on cavity bottom with the connection of bushing type microreactor (4) outboard chambers, the import of circulating pump (8) is connected with the second heat exchanger channels outlet of semi lean solution heat exchanger (11) by semi lean solution aftercooler (19), and the second heat exchanger channels entrance of semi lean solution heat exchanger (11) is connected with the semi lean solution outlet of regenerator (12) middle part.
Second heat exchanger channels entrance of poor rich liquid heat exchanger (10) is connected with the outlet of regenerator (12) lower end lean solution, and the second heat exchanger channels outlet of poor rich liquid heat exchanger (10) passes sequentially through lean solution aftercooler (20), MDEA circulating pump (21) is connected with the lean solution import being arranged on cavity top with the connection of bushing type microreactor (4) outboard chambers.
The gas outlet of reboiler (13) is connected with the gas access of regenerator (12) bottom, and the semi lean solution outlet of reboiler (13) is connected with the liquid inlet of regenerator (12) bottom；The semi lean solution outlet of regenerator (12) lower end is connected with semi lean solution entrance, heat pump (15) the semi lean solution heating gate of reboiler (13) respectively.
The condensation-water drain of reboiler (13) is connected with the condensing water inlet of cooling water tank (14), the condensation-water drain of cooling water tank (14) is connected with the heat exchanging liquid import of heat pump (15), and the heat exchanging liquid outlet of heat pump (15) is connected with condensing water inlet after the heat exchange of cooling water tank (14)；The recuperated gas entrance of heat pump (15) is connected with the sour moisture outlet of the heat of regenerator (12) upper end, after the heat exchange of heat pump (15), outlet is connected with the entrance of separator (16), the acid gas outlet of separator (16) is connected with acid gas collection box (18), and the sour water outlet of separator (16) is connected by the sour water refluxing opening of sour water reflux pump (17) with regenerator (12) upper end.
Wherein raw material gas tank (1), acid gas collection box (18), place collecting box (24) of regulating the flow of vital energy belongs to collection system.Unstripped gas booster pump (2), circulating pump (8), sour water reflux pump (17), MDEA circulating pump (21), sink reflux pump (22) belong to gas-liquid induction system.Bushing type microreactor (4), activator piperazine entrance (5) belong to promotion reaction and accelerate absorption system.Gas-liquid separator (6), separator (16) belong to Separate System of Water-jet.Hydraulic turbine (7), poor rich liquid heat exchanger (10), semi lean solution heat exchanger (11), heat pump (15) belong to fluid pressure and air heat energy recovery system.Flash vessel (9), reboiler (13) belong to blood pressure lowering and aid system of boiling again.
It is provided with valve between described semi lean solution aftercooler (19) and the second heat exchanger channels outlet of semi lean solution heat exchanger (11).
It is provided with valve between second heat exchanger channels entrance of described poor rich liquid heat exchanger (10) and the outlet of regenerator (12) lower end lean solution.
It is provided with valve between described MDEA circulating pump (21) and lean solution import.
The flashed vapour outlet of described flash vessel (9) top is connected with regenerator (12) or acid gas collection box (18).
This process unit meeting scale is built according to actual landfill yard operation conditions.When assembly, can first do and mainly partially absorb tower (3) and regenerator (12).Miniature double tube reactor (4) and gas-liquid separator (6) is arranged therein when doing absorption tower (3).Then according to the major part such as cold air (20), separator (16) after art work sheet layout hydraulic turbine (7), flash vessel (9), poor rich liquid heat exchanger (10), semi lean solution heat exchanger (11), reboiler (13), lean solution.Some circulating pumps and heat pump are installed the most again.Finally arrange water washing groove (23) and gas loading attachment.
Described regenerator can use contains precious sbhb type regenerator.
Described heat pump can use the CWW type heat pump of section's Lay Tyke.
The work process of the present invention is described below in conjunction with the accompanying drawings.
Hydraulic turbine (7) top lead-in wire supply circulating pump (8) energy is converted by rich solution pressure.After flash vessel (9) top egress line is flash distillation rich solution, after the reduction of rich solution pressure, the flashed vapour of gained resolves gained from rich solution, and flash gas can be directly accessed regenerator (12), it is also possible to is directly accessed acid gas collection box (18).Rich solution behind heat exchanger (10), (11) directly enters from reboiler (13) bottom, and heat exchanger (10), the outlet of (11) top are semi lean solution, and lean solution heat exchange exports.Reboiler (13) left side has two imports to enter regenerator (12), and upper inlet line is some gases separated out after reboiler (13) heats up, and lower inlet line is that semi lean solution is heated to reflux into regenerator (12).Reboiler 13 upper right import is the low-pressure steam work for reboiler (13), and being connected into cooling water tank (14) from reboiler (13) is condensed water, the product of reboiler work gained.Cooling water tank (14) left side is (14) natural cooling after the condensed water acid gas heat exchange with heat in heat pump (15) flows back into cooling water tank again after major part heat setting in heat pump (15) absorption condensation water.Heat pump (15) lower-left lead-in wire and the semi lean solution to boil again are connected to after heat pump 15 absorbs heat energy enter back into reboiler (13) to the heating of semi lean solution temperature.Heat pump (15) left side is acid gas import, exports after being arranged above heat exchange.Right side, absorption tower (3) upper inlet is lean solution import, and lower right-hand side is semi lean solution import.Just process gas collecting box (24) from absorption tower (3) gas entrance after water washing groove (23) washs out again to collect.After water washing groove (23) dissolves remainder harmful gas, fetch regenerator (12) through pumping and process.
It is understandable that, above with respect to the specific descriptions of the present invention, it is merely to illustrate the present invention and is not limited to the technical scheme described by the embodiment of the present invention, it will be understood by those within the art that, still the present invention can be modified or equivalent, to reach identical technique effect；Needs are used, all within protection scope of the present invention as long as meeting.
Claims (5)
1. a double-tower type MEDA processes landfill gas system, including raw material gas tank, unstripped gas booster pump, absorption tower, bushing type microreactor, activator piperazine entrance, gas-liquid separator, hydraulic turbine, circulating pump, flash vessel, poor rich liquid heat exchanger, semi lean solution heat exchanger, regenerator, reboiler, cooling water tank, heat pump, separator, sour water reflux pump, acid gas collection box, semi lean solution aftercooler, lean solution aftercooler, MDEA circulating pump, sink reflux pump, water washing groove, regulate the flow of vital energy collecting box in place, it is characterized in that bushing type microreactor is arranged in absorption tower in the cavity of side, activator piperazine entrance connects with bushing type microreactor outboard chambers and is arranged on cavity bottom, the lower end import of bushing type microreactor is connected with raw material gas tank by unstripped gas booster pump；
Cavity upper end above bushing type microreactor upper end outlet is provided with vertical exit, vertical exit is connected with the gas-liquid separator entrance of upper end in absorption tower, gas-liquid separator upper end gas outlet is connected with water washing groove, the gas outlet of water washing groove collecting box of regulating the flow of vital energy with place is connected, and the liquid outlet of water washing groove is connected with the centre inlet of vertical regenerator by sink reflux pump；Gas-liquid separator is provided with downward liquid outlet away from cavity side lower end, in liquid outlet absorption tower outer with cavity, space connects, lower end, absorption tower is provided with the horizontal rich solution outlet connected with space in absorption tower outside cavity, rich solution outlet is connected with the import of hydraulic turbine, the outlet of hydraulic turbine by flash vessel respectively the first heat exchanger channels entrance with poor rich liquid heat exchanger, semi lean solution heat exchanger be connected, poor rich liquid heat exchanger, the first heat exchanger channels of semi lean solution heat exchanger export and are connected with the rich solution import of reboiler；
The drive output of hydraulic turbine is connected with the driving input of circulating pump, circulation delivery side of pump is connected with the semi lean solution import being arranged on cavity bottom with the connection of bushing type microreactor outboard chambers, the import of circulating pump is connected with the second heat exchanger channels outlet of semi lean solution heat exchanger by semi lean solution aftercooler, and the second heat exchanger channels entrance of semi lean solution heat exchanger is connected with semi lean solution outlet in the middle part of regenerator；
Second heat exchanger channels entrance of poor rich liquid heat exchanger is connected with the outlet of regenerator lower end lean solution, and the second heat exchanger channels outlet of poor rich liquid heat exchanger passes sequentially through lean solution aftercooler, MDEA circulating pump is connected with the lean solution import being arranged on cavity top with the connection of bushing type microreactor outboard chambers；
The gas outlet of reboiler is connected with the gas access of regenerator bottom, and the semi lean solution outlet of reboiler is connected with the liquid inlet of regenerator bottom；The semi lean solution outlet of regenerator lower end is connected with semi lean solution entrance, the heat pump semi lean solution heating gate of reboiler respectively；
The condensation-water drain of reboiler is connected with the condensing water inlet of cooling water tank, and the condensation-water drain of cooling water tank is connected with the heat exchanging liquid import of heat pump, and the heat exchanging liquid outlet of heat pump is connected with condensing water inlet after the heat exchange of cooling water tank；The recuperated gas entrance of heat pump is connected with the sour moisture outlet of the heat of regenerator upper end, export the entrance with separator after the heat exchange of heat pump to be connected, the acid gas outlet of separator is connected with acid gas collection box, and the sour water outlet of separator is connected with the sour water refluxing opening of regenerator upper end by sour water reflux pump.
The most according to claim 1, a kind of double-tower type MEDA processes landfill gas system, it is characterised in that be provided with valve between described semi lean solution aftercooler and the second heat exchanger channels outlet of semi lean solution heat exchanger.
The most according to claim 1, a kind of double-tower type MEDA processes landfill gas system, it is characterised in that be provided with valve between the second heat exchanger channels entrance of described poor rich liquid heat exchanger and the outlet of regenerator lower end lean solution.
The most according to claim 1, a kind of double-tower type MEDA processes landfill gas system, it is characterised in that be provided with valve between described MDEA circulating pump and lean solution import.
The most according to claim 1, a kind of double-tower type MEDA processes landfill gas system, it is characterised in that flashed vapour outlet in described flash vessel top is connected with regenerator or acid gas collection box.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113041799A (en) * | 2021-03-12 | 2021-06-29 | 中国华能集团清洁能源技术研究院有限公司 | IGCC-based pre-combustion CO2Pressure energy recovery device of trapping system |
| CN113847430A (en) * | 2021-09-16 | 2021-12-28 | 宣达实业集团有限公司 | Sour gas self-sealing system |
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| US4775519A (en) * | 1985-10-31 | 1988-10-04 | Texaco Inc. | Removal of acid gases from gas streams |
| EP2125164A1 (en) * | 2007-01-25 | 2009-12-02 | Shell Internationale Research Maatschappij B.V. | Process for producing a pressurised co2 stream in a power plant integrated with a co2 capture unit |
| CN102657998A (en) * | 2012-04-25 | 2012-09-12 | 中国石油化工股份有限公司 | Mixed solvent for removing acid gas |
| CN205850531U (en) * | 2016-07-20 | 2017-01-04 | 辽宁工业大学 | A kind of double-tower type MEDA processes landfill gas system |
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| CN113041799A (en) * | 2021-03-12 | 2021-06-29 | 中国华能集团清洁能源技术研究院有限公司 | IGCC-based pre-combustion CO2Pressure energy recovery device of trapping system |
| CN113847430A (en) * | 2021-09-16 | 2021-12-28 | 宣达实业集团有限公司 | Sour gas self-sealing system |
| CN113847430B (en) * | 2021-09-16 | 2023-09-12 | 宣达实业集团有限公司 | Sour gas self-sealing system |
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