CN110152453A - Use the method and apparatus of sour gas in solvent absorption captured gas mixture - Google Patents

Use the method and apparatus of sour gas in solvent absorption captured gas mixture Download PDF

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CN110152453A
CN110152453A CN201910405578.8A CN201910405578A CN110152453A CN 110152453 A CN110152453 A CN 110152453A CN 201910405578 A CN201910405578 A CN 201910405578A CN 110152453 A CN110152453 A CN 110152453A
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absorption
desorber
heat exchange
temperature
barren liquor
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CN110152453B (en
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陈健
于燕梅
费维扬
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Tsinghua University
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Tsinghua University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • 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
    • B01D53/1493—Selection of liquid materials for use as 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • 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 present invention provides a kind of method and apparatus using sour gas in solvent absorption captured gas mixture, this method comprises the following steps: the high-temperature barren liquor that the bottom of desorber is flowed out being shunted before heat exchange or in heat exchange, is exchanged heat respectively with the internal liquid during the solvent absorption and the cold fluid outside the solvent absorption process.The technique that this high-temperature barren liquor by solvent absorption of the present invention is shunted before heat exchange or in heat exchange, referred to as lean solution shunt, and the absorption process of the sour gas such as carbon dioxide may make to trap isolated comprehensive energy consumption and reduce 5-10% or so.

Description

Use the method and apparatus of sour gas in solvent absorption captured gas mixture
Technical field
The present invention relates to gas separation technique fields, more particularly, to a kind of mixed using solvent absorption captured gas The method and apparatus for closing sour gas in object.
Background technique
Carbon dioxide (CO2) discharge of isothermal chamber gas is to cause a principal element of climate change, how from being rich in CO2Admixture of gas or liquefied gas in, low energy consumption and at low cost trap or separate CO2Just seem particularly important.These mixing Object includes flue gas, refinery gas, natural gas, liquefied gas, synthesis gas, conversion gas and hydrogen etc..Contain in admixture of gas 5%~50% CO2, other sour gas include SO2、H2S and organic sulfur CH3S, COS etc., other gas compositions have N2、O2、 Ar、CO、H2、CH4、C2H6.The pressure range of gas is big (0.5~90bar), is suitble to use chemical absorption method, Physical Absorption The trapping of the method for method or Chemical Physics composite absorption and separation CO2Etc. acid gas components.
Industrial more mature trapping separates CO both at home and abroad at present2The main organic amine of solvent of equal sour gas and inorganic The Physical Absorptions solvent such as the chemical absorption solvents such as salt and alcohols, esters, ethers.Monoethanolamine method (MEA), diethanolamine method (DEA), 2-amino-2-methyl-1-propanol (AMP), diisopropanolamine process (DIPA) and methyl diethanolamine method (MDEA) etc. have Machine amine solvent is primarily adapted for use in the trapping separation of the sour gas in mesolow gas.And methanol, propene carbonate, Aethoxy Sklerol Equal physical solvents are primarily adapted for use in the separation of the high-concentration acidic wastewater gas of high pressure system.In order to improve absorbent solution to sour gas CO2Infiltration rate, in the slower solvent of infiltration rate, be added the faster solvent of infiltration rate such as MEA and piperazine (PZ) etc., Form the mixed solvent for absorbing that solubility is high, infiltration rate is fast, can be greatly lowered the isolated energy consumption of trapping of sour gas with Cost.
In addition to lyosoption, the process flow of absorption process is also to reduce CO2The trapping of equal sour gas and separating energy consumption With the key of cost.Conventional absorption technique process includes feed gas preprocessing, absorption, purifies the gentle liquid separation of air cooling, is poor Liquid and rich solution heat exchange, heating desorption, regeneration air cooling and separation and lean solution cooling etc..On the basis of conventional process flow, The improvement of following process flow, so that trapping isolated energy consumption obtains different degrees of reduction.
In absorption tower it is cold be the modified flow being widely studied in numerous documents (Woertz, B.B., 1966.Process for removing acidic constituents from gaseous mixtures.Patent No.US 3266220A1,Union Oil Co.).It is cold in absorption tower to refer to from the centre on absorption tower, take out part or all Liquid phase material, the liquid phase of taking-up is cooled down by heat exchange equipment, then logistics after cooling is sent back in absorption tower.It can also Using the direct heating/cooling device in the middle part of absorption tower.Due to CO2The absorption process of equal sour gas is exothermic, so inhaling During receipts, the rising of the temperature in absorption tower is unfavorable for absorbing, and reduces solvent to CO2Assimilation effect, increase solvent Internal circulating load, then increase the energy consumption of desorption tower reboiler.And pass through flow scheme improvements cold in absorption tower, in the middle part of absorption tower Solvent temperature decline, improves solvent absorption CO2Ability, finally reduce the internal circulating load of solvent, reduce the energy of reboiler Consumption.For different solvents, reboiler energy consumption can decline 3-7%.
The research of rich solution branching process can be traced to the research (Eisenberg of Eisenberg and Johnson earliest and Johnson,1979.Amine regeneration process.Patent No.US 4152217A1,Exxon Research and Engineering Company.).This simple modified flow is the rich solution for taking out absorbing tower bottom It is divided into two strands, wherein one is heated without heat exchanger, it is directly injected into the top of desorber, and another stock then first passes through heat exchanger The top of desorber position on the lower side is entered back into after being heated.By shunting this modified flow using rich solution, desorber is again Boiling device energy consumption can have apparent decline.Since the cold rich solution not being heated enters from desorption column overhead, encounter at tower top (main component is gaseous state H to high temperature gas phase2O and CO2) after, the heat of high temperature gas phase is absorbed, and release CO2, and in high temperature gas phase The cooled liquefaction of part vapor, CO2Then continue to be discharged from tower top.The gas phase temperature of overhead extraction is lower, reduces gas phase The heat taken away reduces reboiler energy consumption.Meanwhile another cold rich solution of stock is due to the reduction of amount, it can be by when passing through heat exchanger It is heated to a higher temperature, it is easier to release CO2 in desorber, reduce the energy consumption of reboiler needs.For not Same solvent, the process flow shunted using rich solution, reboiler energy consumption can decline 8-15%.
Another similar method using stripping gas heat is the method using the heat exchange of rich solution and stripping gas (Herrin,1989.Process sequencing for amine regeneration.Patent No.US 4798910A1.), principle is actually as rich solution shunts, but does not have mass exchange between rich solution and stripping gas, only There is heat exchange.
Semi lean solution dividing technology can also be referred to as solution shunt, first by Shoeld propose (Shoeld, 1934.Purification and separation of gaseous mixtures.Patent No.US 1971798,The Koppers Co.).Absorption tower and desorber are all divided into two parts up and down, and the liquid that more gas is absorbed in absorbing lower part exists The top of desorber desorbs, and the solution that less gas is absorbed in the top of absorption tower is desorbed in the lower part of desorber.Separately A kind of improved method is produced a part of molten using single absorption tower and single desorber in the middle part of desorber Liquid is sent into middle part (Reddy, et al., 2004.Improved the split flow on absorption tower after heat exchange and cooling process and apparatus.Patent No.WO 2004005818A2,Fluor Corporation.).Technology benefit With the lower advantage of CO2 heat of desorption in the solution of high load capacity, 7-10% or so can save energy.
Lean solution flash distillation compression be one of studied widest modified flow (Benson and McRea, 1979.Removal of acid gases from hot gas mixtures.Patent No.US4160810A1, Benfield Corporation.)(Reddy et al.,2007.Integrated compressor/stripper configurations and methods.Patent No.WO2007075466A2,Fluor Technologies Corporation).The hot lean solution produced from desorber tower bottom, which is passed into first in a low pressure flash chamber, to be flashed, and is flashed Obtained gas phase is passed through the position of desorber tower bottom or more after compressor compresses again, and the liquid phase after flashing still by heat exchange and Enter absorption tower after cooling.The gas phase obtained in the flash tank can achieve higher temperature, be passed through desorption through compressor work After tower, a part of heat can be provided for desorption process, reduce the thermic load of desorption tower reboiler.For different solvents, use The process flow of lean solution flash distillation compression, reboiler energy consumption can decline 10-13%.Due to introducing compressor in process, it is considered After power consumption, overall energy consumption has dropped 3-5%.
It by the improvement of above-mentioned process flow, is combined, the energy consumption of trapping separation process can be further decreased.Such as it inhales Cold in tower+rich solution shunts, cold in absorption tower+lean solution flash distillation is compressed etc. is received, energy consumption 10-20% can be totally reduced.
And the integrated aspect of energy, main technique stream are carried out in other industrial process such as separation and collection process and coal fired power generation Journey has the utilization of gas energy and utilizing for stripping gas energy.
Using high-temperature flue gas energy there are two ways to, one is using high-temperature flue gas heat rich solution (Benson Homer and Mccrea Donald,1979.Removal of acid gases from hot gas mixtures.Patent No.US4160810.Benfield Corp.).Another kind is using in high-temperature flue gas heating desorption tower Portion's liquid (TAKASHI et al., 2006.Apparatus and method for CO2recovery.JP200500478 57.Mitsubishi Heavy Ind Ltd,Kansai Electric Power Co.).But contain titanium dioxide in flue gas Sulphur will form sulfuric acid after flue gas is cooled, need the anti-corrosion material of high standard.
Using the method for the energy of the stripping gas of carbon dioxide capture device regenerator, gas temperature is improved by compression, Water spray generates steam, is then utilized (Woodhouse, 2008.Improved absorbent to heat by heat exchange regeneration.Patent No.WO2008063082,CN101610828A.Aker clean carbon As.).Recycling Energy, can be used for the regeneration steam at regenerator bottom, it can also be used to the heating of other logistics.
In above-mentioned process flow, there is the technology of reduction trapping energy consumption during absorption process trapping, also have flue gas heat The comprehensive utilization of amount and stripping gas heat.During above-mentioned absorption process trapping, from desorber bottom or desorption tower reboiler bottom The high-temperature barren liquor that portion comes out is used to heat rich solution in heat exchanger, or first flashes off some steam and exchange heat in heat exchanger again Cooling, the temperature of lean solution can be reduced to 333K or so, then carry out by cooling water the temperature for being cooled to 313K or so, subsequently into suction Tower is received to be recycled.Before cooled water is cooling, the temperature of lean solution only has 333K or so, this temperature is in coal-burning power plant Etc., without very big use, can only being cooled down with cooling water in other industrial process.
Summary of the invention
The purpose of the present invention is to provide a kind of method using sour gas in solvent absorption captured gas mixture, This method comprises the following steps:
The high-temperature barren liquor that the bottom of desorber is flowed out is shunted, respectively with the inside during the solvent absorption Cold fluid outside liquid and the solvent absorption process exchanges heat.
Sour gas refers to carbon dioxide, sulfur dioxide etc. in the present invention.
The method that high-temperature barren liquor is shunted can be described as lean solution shunting.The present invention will desorb the high temperature of tower bottom outflow Lean solution shunts, and is respectively used to carry out heat exchange and the cryogen for heating other processes with internal liquid, may make titanium dioxide The absorption process of the sour gas such as carbon, which traps isolated comprehensive energy consumption, reduces 5-10% or so.
Wherein, desorber includes reboiler, and high-temperature barren liquor may be the high-temperature barren liquor of reboiler bottom outflow.
The high-temperature barren liquor can be divided into two streams by the present invention, i.e., high-temperature barren liquor is divided at least two strands of liquid, In at least one be used to be changed with internal liquid during solvent absorption (can be the rich solution during solvent absorption) Heat, for exchanging heat with the cold fluid outside solvent absorption process, i.e. first part's lean solution is used for and rich solution at least another stock Exchange heat, second part lean solution be used to heat it is other during cold fluid, such as the recirculated water of coal fired power generation etc..
Absorption corresponding with the desorber is added after can also further cooling down the high-temperature barren liquor after heat exchange in the present invention In tower, it to be used for cyclic absorption sour gas.It is specifically as follows, as shown in Figure 1, flue gas G1 enters absorption tower, with absorption tower jacking The lean solution L4 (subcooler E5 is cooling at this time) entered is contacted, and CO is absorbed2Rich solution R1 afterwards is exported from tower bottom, removing portion Divide CO2Overhead gas stream afterwards separates after E3 cools down in gas-liquid separator F1, the purified gas G2 output absorption tower isolated, liquid Body flows back into absorption tower.And rich solution R1 is desorbed after heat exchanger E1 heating into desorber top.In desorption tower bottom Equipped with reboiler E2, is heated with steam Z1 and boiled again.The high temperature flowed out from the reboiler bottom of desorption tower bottom or desorber Lean solution L1, is divided into two strands (L2 and L3) or two strands or more, and at least one L2 is used for and the liquid (such as rich solution R1) in absorption process It is exchanged heat and (is carried out in heat exchanger E1), in addition at least one L3 with the cold fluid W1 other than absorption process for exchanging heat (being carried out in heat exchanger E6).Lean solution after heat exchange merges L4 or enters absorption tower after being further cooled respectively, for recycling The sour gas such as absorbing carbon dioxide.The stripping gas G3 being ejected from desorber, after subcooler E4 is cooling, into gas-liquid point From device F2, the gas G4 that isolates discharge, liquid reflux is at the top of desorber.
The concatenated heat exchanger that can also be divided into poor rich liquid heat exchanger more than two or three in the present invention, was exchanging heat The intermediate of journey produces a part of lean solution, for heat it is other during cryogen.It is specifically as follows, as shown in Fig. 2, flue gas G1 enters absorption tower, and the lean solution L4 (subcooler E5 is cooling at this time) entered with absorption tower jacking is contacted, and absorbs CO2Afterwards Rich solution R1 from tower bottom export, remove part CO2Overhead gas stream afterwards separates after E3 cools down in gas-liquid separator F1, separation Purified gas G2 out exports absorption tower, and liquid reflux is into absorption tower.And rich solution R1 by heat exchanger E1 and E7 heating after, into solution Top of tower is inhaled to be desorbed.It is equipped with reboiler E2 in desorption tower bottom, is heated with steam Z1 and is boiled again.From desorption tower bottom or The high-temperature barren liquor L1 of the reboiler bottom outflow of desorber (is exchanging heat with liquid (such as rich solution R2) heat exchange in absorption process Carried out in device E7) after, it is divided into two strands (L2 and L3) or two strands or more, at least one L2 continues on for and the liquid in absorption process (such as rich solution R1) is exchanged heat and (is carried out in heat exchanger E1), and in addition at least one L3 is used for and the cold fluid other than absorption process W1 is exchanged heat and (is carried out in heat exchanger E6).Lean solution after heat exchange, which merges L4 or enters after being further cooled respectively, to be absorbed Tower, for sour gas such as cyclic absorption carbon dioxide.The stripping gas G3 being ejected from desorber, it is cooling through subcooler E4 Afterwards, into gas-liquid separator F2, the gas G4 that isolates discharge, liquid reflux is at the top of desorber.
The present invention can also using complicated heat exchanger, will be other during cryogen and the multiplies such as lean solution, rich solution Logistics exchanges heat together.Can by high-temperature barren liquor with during at least one described solvent absorption internal liquid and Cold fluid at least outside one described solvent absorption process exchanges heat, and enters absorption tower after the lean solution after heat exchange is cooling, uses In cyclic absorption sour gas.It is specifically as follows, as shown in figure 3, flue gas G1 enters absorption tower, the lean solution entered with absorption tower jacking L4 (subcooler E5 is cooling at this time) is contacted, and CO is absorbed2Rich solution R1 afterwards is exported from tower bottom, removes part CO2Afterwards Overhead gas stream separates after E3 cools down in gas-liquid separator F1, the purified gas G2 that isolates output absorption tower, liquid reflux into Absorption tower.And rich solution R1 is desorbed after heat exchanger E1 heating into desorber top.It is equipped in desorption tower bottom and boils again Device E2 is heated with steam Z1 and is boiled again.Desorb high-temperature barren liquor L1 that the reboiler bottom of tower bottom or desorber comes out, at least Liquid (such as rich solution R1) in one absorption process and the cold fluid W1 at least other than one absorption process are complicated at one It exchanges heat in heat exchanger E1.Lean solution L4 after heat exchange enters absorption tower after being further cooled, and is used for cyclic absorption titanium dioxide The sour gas such as carbon.The stripping gas G3 being ejected from desorber, into gas-liquid separator F2, divides after subcooler E4 is cooling The gas G4 discharge separated out, liquid reflux is at the top of desorber.
In the present invention, can also by method and other power-saving technologies of the invention (in such as absorption tower cold, rich solution shunt, Semi lean solution shunt, lean solution flash distillation compression etc.) in one or more techniques combine, form increasingly complex energy saving technique, Further decrease the overall energy consumption of the sour gas such as absorption process trapping separation carbon dioxide.
The present invention also provides a kind of equipment using sour gas in solvent absorption captured gas mixture, comprising: The bottom of absorption tower and desorber, the desorber is equipped with high-temperature barren liquor output channel, and the high-temperature barren liquor output channel is used for Make the high-temperature barren liquor shunt for outside internal liquid during the solvent absorption and the solvent absorption process Cold fluid heat exchange.
In a preferred embodiment of the invention, the equipment further include:
The internal liquid conveyance conduit being connected with the absorption tower, for conveying the inside during the solvent absorption Liquid；
Cold fluid conveyance conduit, for conveying the cold fluid outside the solvent absorption process；
After the high-temperature barren liquor output channel high temperature lean solution shunts, conveyed respectively with the internal liquid by heat exchanger Cold fluid exchanges heat in internal liquid and the cold fluid conveyance conduit in pipeline；
The lean solution conveyance conduit being connected with the absorption tower, for the lean solution after heat exchange to be delivered to absorption tower；
The internal liquid conveyance conduit being connected with the desorber, for the internal liquid after heat exchange to be delivered to desorption Tower.
In a preferred embodiment of the invention, the equipment further include:
It is positioned close to the heat exchanger of the high-temperature barren liquor output channel and desorber junction, for the high temperature is poor Liquid and internal liquid carry out part heat exchange, and then the high-temperature barren liquor is shunted again.
This new method that the present invention uses, the first part's lean solution being diverted is used for and rich solution exchanges heat, and second Part lean solution be used for heat it is other during cold fluid.The temperature of second part lean solution can achieve 353-403K or so, most It is equal to the lean solution temperature of reboiler in the case where height.After the temperature will be apparently higher than the heat exchange of the rich or poor liquid in original technology The lean solution temperature of 333K or so.Certainly, specific temperature is according to the flow of lean solution and rich solution, temperature, shunt ratio, heat exchange area It is related with runner design.The present invention shunts the high-temperature barren liquor for desorbing tower bottom outflow, is respectively used to and the internal liquids such as rich solution Heat exchange and the cryogen for heating other processes are carried out, the absorption process of the sour gas such as carbon dioxide may make to trap separation Comprehensive energy consumption reduce 5-10% or so.
Detailed description of the invention
Fig. 1 is in a preferred embodiment of the invention using sour gas in solvent absorption captured gas mixture The flow chart of (lean solution shunts before exchanging heat)；
Fig. 2 is in presently preferred embodiment using sour gas in solvent absorption captured gas mixture The flow chart of (lean solution shunts in heat exchange)；
Fig. 3 is in presently preferred embodiment using sour gas in solvent absorption captured gas mixture The flow chart of (lean solution in Complex Heat device shunts).
Specific embodiment
With reference to embodiment, the embodiment of the present invention is furthur described in detail.Following embodiment is used for Illustrate the present invention, but is used to limit the scope of the invention incessantly.
Embodiment 1
One concentration is 13.1%CO2, 73.5%N2, 8.0%O2And 5.4%H2O, flow are 4310 standard cubic meters/small When, 25% ethanol amine (MEA) for being 20.5 cubes ms/h with flow in absorption tower, CO2It is 0.28 with MEA molar ratio Aqueous solution contacted, CO2Absorptivity is 90%.The logarithmic mean temperature difference (LMTD) of poor rich liquid heat exchanger is 7.5K, poor after heat exchange Liquid temperature is 328.85K, and desorption tower bottom pressure is 1.6bar, and desorber bottom lean solution temperature is 385.75K.There is an absorption Tower, a desorber, a poor rich liquid heat exchanger and a reboiler old process in, energy consumption for heating in reboiler For 3.86GJ/ tons of CO2。
And on the basis of old process, increase lean solution dividing technology using the process of Fig. 1 and increase a heat exchanger E6, For the high-temperature barren liquor of shunting and the heat exchange of external cold fluid, the shunt ratio L3/L1 of the lean solution at desorber bottom is 20% (general For 15%-35%, can be optimized according to process condition), temperature 385.75K, reboiler energy consumption is 4.05GJ/ tons of CO2, can Heat (385.75K-328.85K) for heating other cold fluids is 0.87GJ/ tons of CO2.Temperature range is 385.75K- The ratio of the steam-electric power efficiency of the steam-electric power efficiency and 393.15K of the mean temperature 357.3K of 328.85K is 0.635, whole Physical efficiency consumption is 4.05-0.87*0.635=3.5GJ/ tons of CO2And the 3.86GJ/ ton CO of original old process2Compared to energy conservation 9.4%.
Embodiment 2
The process shunted using cold in absorption tower and rich solution is increased on the basis of same 1 old process of embodiment, one is dense Degree is 13.1%CO2, 73.5%N2, 8.0%O2And 5.4%H2O, flow is 4310 standard cubes m/h, in absorption tower 25% ethanol amine (MEA) for being 18.7 cubes ms/h with flow, CO2The aqueous solution for being 0.28 with MEA molar ratio is connect Touching.Using absorption tower inner cold technology, absorption tower is sent after cooling down to the liquid in the middle part of absorption tower back to, cooling capacity is 0.485GJ/ tons CO2。CO2Absorptivity is 90%.It being shunted simultaneously using rich solution, the first part's rich solution distributed is directly at the top of desorber, and second Part enters the top of desorber after poor rich liquid heat exchanger.The ratio that first part's rich solution accounts for whole rich solutions is 25%, poor The logarithmic mean temperature difference (LMTD) of rich solution heat exchanger is 7.5K, and the lean solution temperature after heat exchange is 333.45K, and desorption tower bottom pressure is 1.6bar, desorber bottom lean solution temperature are 385.75K, and energy consumption for heating is 3.49GJ/ tons of CO in reboiler2。
And on the basis of above-mentioned process, increase the lean solution dividing technology in heat exchange, increases by two heat exchangers (in such as Fig. 2 E7 and E6), increased E7 be used for high-temperature barren liquor and rich solution heat exchange, increased heat exchanger E6 for shunting lean solution and outside The heat exchange of cold fluid, the shunt ratio L3/L1 of the lean solution at desorber bottom are 25%, temperature 373.45K, and reboiler energy consumption is 3.55GJ/ ton CO2, increasing the heat (temperature range 373.45K-333.45K) for heating other cold fluids newly is 0.69GJ/ Ton CO2.Temperature range is the steam-electric power efficiency of the mean temperature 353.45K of 373.45K-333.45K and the steam of 393.15K The ratio 0.0.592 of generating efficiency, whole energy consumption are 3.55-0.69*0.592=3.14GJ/ tons of CO2, and it is original using absorption 3.49GJ/ tons of CO of process energy consumption that cold and rich solution shunts in tower2Compared to energy conservation 10.0%.
Embodiment 3
It is shunted using rich solution and the process of semi lean solution shunting, one concentration is 15.0%CO2, 72.0%N2, 8.0%O2With 5.0%H2O, flow be 4784 standard cubes m/h, the flow that absorption tower neutralizing tower jacking enters be 14.54 cubic metres/it is small When 20% 2-amino-2-methyl-1-propanol (AMP)+10% ethanol amine (MEA), CO2With rubbing for organic amine AMP+MEA You are contacted than the semi lean solution that the flow of entrance in the middle part of the aqueous solution and tower for 0.20 is 2.67 cubes ms/h, CO2 Absorptivity is 85%.It is shunted simultaneously using rich solution and semi lean solution shunts.First part's rich solution that rich solution shunts is directly into desorber Top, second part enter the top of desorber after poor rich liquid heat exchanger.First part's rich solution accounts for the shunting of whole rich solutions Ratio is 25%.It is 15% that semi lean solution, which produces ratio,.The part semi lean solution produced in the middle part of from desorber, and the rich solution shunted carry out The logarithmic mean temperature difference (LMTD) of the heat exchanger of heat exchange, rich solution and semi lean solution is 9.3K.The logarithmic mean temperature difference (LMTD) of poor rich liquid heat exchanger is 8.0K, the lean solution temperature after heat exchange is 332.85K, and the logarithmic mean temperature difference (LMTD) of second poor rich liquid heat exchanger is 5.0K.Desorber Bottom pressure is 1.6bar, and desorber bottom lean solution temperature is 386.15K, and energy consumption for heating is 2.81GJ/ tons in reboiler CO2。
And on the basis of above-mentioned process, using the lean solution dividing technology in heat exchange, increase by two heat exchangers (in Fig. 2 E7 and E6), increased E7 is used for the heat exchange of high-temperature barren liquor and rich solution, and increased heat exchanger E6 is cold for the lean solution of shunting and outside The heat exchange of fluid, the shunt ratio L3/L1 of the lean solution at desorber bottom are 25%, temperature 377.65K, and reboiler energy consumption is 2.97GJ/ ton CO2, increasing the heat (temperature range 377.65K-332.85K) for heating other cold fluids newly is 0.61GJ/ Ton CO2.Temperature range is the steam-electric power efficiency of the mean temperature 355.25K of 377.65K-332.85K and the steam of 393.15K The ratio 0.612 of generating efficiency, whole energy consumption are 2.97-0.61*0.612=2.60GJ/ tons of CO2, and using rich solution shunt and 2.81GJ/ tons of CO of process energy consumption that semi lean solution shunts2Compared to energy conservation 7.5%.
Embodiment 4
It is shunted using cold in absorption tower, rich solution and lean solution flashes the process compressed, the side that cold and rich solution shunts in absorption tower Method is the same as embodiment 2 and embodiment 3.One concentration is 13.1%CO2, 73.5%N2, 8.0%O2And 5.4%H2O, flow 4310 Standard cube m/h, 25% ethanol amine, CO in absorption tower with flow for 18.7 cubes ms/h2It rubs with ethanol amine You for 0.28 aqueous solution than being contacted, and cold cooling capacity is 0.485GJ/ tons of CO in absorption tower2, CO2Absorptivity is 90%.Together Shi Caiyong rich solution shunts, shunt ratio 15%, and the logarithmic mean temperature difference (LMTD) of poor rich liquid heat exchanger is 7.5K, the lean solution temperature after heat exchange Degree is 328.15K.Desorption tower bottom pressure is 1.6bar, and desorber bottom lean solution temperature is 385.55K, is flowed out from desorber bottom poor Liquid is directly entered lean solution flash tank, flashing pressure 1.0bar, and the compression pressure of flashed vapour is 1.6bar, the liquid after flash distillation into Enter poor rich liquid heat exchanger and rich solution exchanges heat.Energy consumption for heating is 2.39GJ/ tons of CO in reboiler2。
And on the basis of above-mentioned process, the lean solution after lean solution flash distillation uses dividing technology.First part goes successively to poor Rich solution heat exchanger and rich solution exchange heat, and second part and external cold fluid are exchanged heat and (increase a heat exchanger, as shown in figure 1 E6).The ratio (shunt ratio) that second part lean solution accounts for all lean solutions is 20%, temperature 373.35K, and reboiler energy consumption is 2.52GJ/ ton CO2, increasing the heat (temperature range 373.35K-328.15K) for heating other cold fluids newly is 0.48GJ/ Ton CO2.Temperature range is the steam-electric power efficiency of the mean temperature 350.75K of 373.35K-328.15K and the steam of 393.15K The ratio 0.561 of generating efficiency, whole energy consumption are 2.52-0.48*0.561=2.25GJ/ tons of CO2, and only in absorption tower Cold, rich solution shunts and 2.39GJ/ tons of CO of process energy consumption of lean solution flash distillation compression2Compared to energy conservation 5.8%.
Finally, method of the invention is only preferable embodiment, it is not intended to limit the scope of the present invention.It is all Within the spirit and principles in the present invention, any modification, equivalent replacement, improvement and so on should be included in protection of the invention Within the scope of.

Claims (10)

1. a kind of method using sour gas in solvent absorption captured gas mixture, which is characterized in that including walking as follows It is rapid:
The high-temperature barren liquor that the bottom of desorber is flowed out is shunted before heat exchange or in heat exchange, respectively with the solvent absorption Cold fluid outside internal liquid in the process and the solvent absorption process exchanges heat.
2. the method according to claim 1, wherein specifically comprising the following steps:
The high-temperature barren liquor is directly divided at least two strands of liquid, wherein at least one is used for and the solvent absorption process In internal liquid exchange heat, at least another stock with the cold fluid outside the solvent absorption process for exchanging heat.
3. the method according to claim 1, wherein specifically comprising the following steps:
After internal liquid during the high-temperature barren liquor and the solvent absorption is carried out part heat exchange, then shunted, For carrying out secondary heat exchange with the internal liquid during the solvent absorption, another part is used for and the solvent a part Cold fluid outside absorption process process exchanges heat.
4. the method according to claim 1, wherein specifically comprising the following steps:
By the high-temperature barren liquor, with the internal liquid during at least one described solvent absorption and at least, one is described molten Cold fluid outside agent absorption process process exchanges heat in a Heat Exchangers.
5. method according to claim 1 to 4, which is characterized in that further include, by the lean solution after heat exchange into one Enter in absorption tower corresponding with the desorber after step is cooling, is used for cyclic absorption sour gas.
6. method according to claim 1 to 4, which is characterized in that the internal liquid is solvent suction Rich solution during receipts method.
7. method according to claim 1 to 4, which is characterized in that it further include reboiler in the desorber, The high-temperature barren liquor is the high-temperature barren liquor of reboiler bottom outflow.
8. a kind of equipment using sour gas in solvent absorption captured gas mixture characterized by comprising absorption tower And desorber, the bottom of the desorber are equipped with high-temperature barren liquor output channel, the high-temperature barren liquor output channel is described for making High-temperature barren liquor shunt and be used for during the solvent absorption internal liquid and the solvent absorption process outside Cold fluid heat exchange.
9. equipment according to claim 8, which is characterized in that further include:
The internal liquid conveyance conduit being connected with the absorption tower, for conveying the inside liquid during the solvent absorption Body；
Cold fluid conveyance conduit, for conveying the cold fluid outside the solvent absorption process；
After the high-temperature barren liquor output channel high temperature lean solution shunts, by heat exchanger respectively with the internal liquid conveyance conduit Cold fluid exchanges heat in middle internal liquid and the cold fluid conveyance conduit；
The lean solution conveyance conduit being connected with the absorption tower, for the lean solution after heat exchange to be delivered to absorption tower；
The internal liquid conveyance conduit being connected with the desorber, for the internal liquid after heat exchange to be delivered to desorber.
10. equipment according to claim 8 or claim 9, which is characterized in that further include:
Be positioned close to the heat exchanger of the high-temperature barren liquor output channel and desorber junction, for by the high-temperature barren liquor with Internal liquid carries out part heat exchange, and then the high-temperature barren liquor is shunted again.
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