CN109351125A - A novel catalytic desorption tower for reducing energy consumption for regeneration of CO2-rich amine solution - Google Patents
A novel catalytic desorption tower for reducing energy consumption for regeneration of CO2-rich amine solution Download PDFInfo
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- 238000003795 desorption Methods 0.000 title claims abstract description 42
- 150000001412 amines Chemical class 0.000 title claims abstract description 40
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 34
- 238000005265 energy consumption Methods 0.000 title claims abstract description 24
- 230000008929 regeneration Effects 0.000 title claims abstract description 22
- 238000011069 regeneration method Methods 0.000 title claims abstract description 22
- 239000003054 catalyst Substances 0.000 claims abstract description 47
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 36
- 238000000034 method Methods 0.000 claims abstract description 29
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 18
- 230000008569 process Effects 0.000 claims abstract description 14
- 238000010438 heat treatment Methods 0.000 claims abstract description 3
- 239000011949 solid catalyst Substances 0.000 claims abstract description 3
- 239000007864 aqueous solution Substances 0.000 claims description 19
- 239000000243 solution Substances 0.000 claims description 19
- 238000006555 catalytic reaction Methods 0.000 claims description 18
- 239000000945 filler Substances 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- 238000012856 packing Methods 0.000 claims description 5
- 229910001220 stainless steel Inorganic materials 0.000 claims description 5
- 239000010935 stainless steel Substances 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000006004 Quartz sand Substances 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000011324 bead Substances 0.000 claims description 2
- 239000000919 ceramic Substances 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 239000011521 glass Substances 0.000 claims description 2
- 238000011068 loading method Methods 0.000 claims description 2
- 239000011236 particulate material Substances 0.000 claims description 2
- 230000002195 synergetic effect Effects 0.000 claims description 2
- 239000002904 solvent Substances 0.000 abstract description 19
- 229910052799 carbon Inorganic materials 0.000 abstract description 10
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- 239000003377 acid catalyst Substances 0.000 abstract description 2
- 230000001172 regenerating effect Effects 0.000 abstract description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 14
- 239000007788 liquid Substances 0.000 description 9
- 239000011973 solid acid Substances 0.000 description 8
- 229910003158 γ-Al2O3 Inorganic materials 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 7
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 3
- -1 carbon amine Chemical class 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- WIHIUTUAHOZVLE-UHFFFAOYSA-N 1,3-diethoxypropan-2-ol Chemical compound CCOCC(O)COCC WIHIUTUAHOZVLE-UHFFFAOYSA-N 0.000 description 2
- 229940058020 2-amino-2-methyl-1-propanol Drugs 0.000 description 2
- BTANRVKWQNVYAZ-UHFFFAOYSA-N 2-butanol Substances CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 2
- VZEZONWRBFJJMZ-UHFFFAOYSA-N 3-allyl-2-[2-(diethylamino)ethoxy]benzaldehyde Chemical compound CCN(CC)CCOC1=C(CC=C)C=CC=C1C=O VZEZONWRBFJJMZ-UHFFFAOYSA-N 0.000 description 2
- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical compound NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 description 2
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 2
- 229940043237 diethanolamine Drugs 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- RRSCTVNXMNXSHR-UHFFFAOYSA-N C(O)CN.[C] Chemical compound C(O)CN.[C] RRSCTVNXMNXSHR-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- MCMNRKCIXSYSNV-UHFFFAOYSA-N ZrO2 Inorganic materials O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- HPNMFZURTQLUMO-UHFFFAOYSA-N diethylamine Chemical compound CCNCC HPNMFZURTQLUMO-UHFFFAOYSA-N 0.000 description 1
- 235000019441 ethanol Nutrition 0.000 description 1
- 229940031098 ethanolamine Drugs 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
- 239000008399 tap water Substances 0.000 description 1
- 235000020679 tap water Nutrition 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—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
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
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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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本发明公开了一种用于降低富二氧化碳的胺溶液再生能耗的新型催化解吸塔，相较于传统的解吸塔，本发明将催化反应器引入传统的CO2解吸流程中，而不改变传统解吸塔的工艺流程、管道布局及加热方式等。其中催化反应器中装填固体催化剂，富CO2胺溶液从反应器底部通过泵的作用进入，通过催化剂和胺溶液的充分接触，使得催化剂的性能得到最大化的利用。新型催化解吸装置主要由催化反应器和填料塔组成。酸性催化剂的引入，加快了富碳胺溶剂的再生速率，降低其再生温度，从而实现高效低能耗再生富碳胺溶剂的目的。该新型催化解吸塔催化性能高于现在的催化解吸塔及传统解吸塔。
The invention discloses a novel catalytic desorption tower for reducing the energy consumption of carbon dioxide-rich amine solution regeneration. Compared with the traditional desorption tower, the invention introduces a catalytic reactor into the traditional CO2 desorption process without changing the traditional desorption The process flow, pipeline layout and heating method of the tower. The catalytic reactor is filled with a solid catalyst, and the CO2-rich amine solution enters from the bottom of the reactor through the action of a pump, and the performance of the catalyst is maximized through the full contact between the catalyst and the amine solution. The new catalytic desorption device is mainly composed of a catalytic reactor and a packed tower. The introduction of the acid catalyst accelerates the regeneration rate of the carbon-rich amine solvent and reduces its regeneration temperature, thereby realizing the purpose of regenerating the carbon-rich amine solvent with high efficiency and low energy consumption. The catalytic performance of the new catalytic desorption tower is higher than that of the current catalytic desorption tower and the traditional desorption tower.
Description
Technical field
The present invention relates to a kind of for the carbon dioxide enriched regenerated new catalytic desorber of amine aqueous solution.
Background technique
In recent years, because of a large amount of uses of the fossil energies such as coal, petroleum and natural gas, greenhouse effects is caused to get worse,
The survival and development of the Global Climate Changes threat mankind of initiation, and carbon dioxide (CO2) it is most important greenhouse gases
One of.
Existing carbon capture technique mainly includes capture before burning, oxygen-enriched combusting capture and captures these three skills after burning
Art, wherein capture technique is current most mature, most widely used carbon capture technique after burning, post combustion carbon capture technology is main
There are chemical absorption method, physisorphtion and membrane separation process etc..In chemical solvent absorption method, organic amine solvent is because of its fast absorption speed
The characteristics such as rate, big absorptive capacity and renewable performance and be widely used in industrial-scale production.
Chemical absorption method, principle are by chemically reacting in the selective absorption and separation flue gas of alkalinity using organic amine
CO2.For repeated recycling utilize organic amine solvent, the general CO removed using stripping process in rich solution amine solvent2, make rich carbon
Absorbent is regenerated.Fig. 1 show traditional rich CO2Amine solvent regeneration technology flow chart.It mainly includes desorber, condensation
Device, tower bottom reboiler, poor rich liquid heat exchanger and pump.Primary operational process is to absorb CO2Rich solution through rich solution pump pressurization send to
Poor rich liquid heat exchanger carries out heat exchange with the regeneration lean solution of desorber bottom discharge, reaches and enter desorption from top after certain temperature
Tower is sprayed after liquid phase distributor at the top of desorber into tower, and tower bottom reboiler, which provides enough water vapours for rich solution desorption, makes richness
Liquid load drops to required range.Lean solution after desorption is flowed out by desorber bottom, after the heat exchange of rich or poor liquid, is pumped to lean solution
Cooler is cooled to required temperature.Lean solution after cooling returns to absorption tower and is recycled.
As described above, traditional rich carbon amine solvent regenerative process needs to consume a large amount of energy consumption, it is mainly due to from rich solution
Solvent strips CO2Required heat.According to related document report, the energy consumption for solvent reclamation accounts for CO2Total stream of acquisition equipment
60% or more (the Idem et al.Ind.Eng.Chem.Res.2006,45 (8), 2414-2420.) that journey expends.Early period is reported
Reduction regeneration energy consumption patent and document in, be all the optimization concentrated on to existing regeneration technology process and portion of energy returned
It receives and utilizes, have biggish gap (Liang et al.Int.J.Greenhouse Gas from theoretical regeneration energy consumption value
Control,2015,34:75-84；Rochelle G T.Science,2009,325(5948):1652-1654.).
Therefore, develop a kind of novel, efficient rich carbon amine solvent regenerating unit and method, promote rich carbon solution regeneration speed
Rate, the regeneration energy consumption for reducing rich carbon amine solvent, and then reduce desorber scale, reduce CO2It is very necessary for capturing cost.?
In previous work, by the basic research of batch-type system, we demonstrate typical solid acid catalyst such as molecular sieve catalytic
Agent HZSM-5, SAPO-34, exceed the time limit solid acid and its mixed catalyst to all have the rich carbon monoethanolamine (MEA) of good catalysis molten
The regenerated performance of liquid can significantly reduce regeneration energy consumption (Liang et al.AlChE J., 2016,62 (3): 753- of MEA
765；Zhang et al.Appl.Energy 2017(202):673–684；Liu et al.Ind.Eng.Chem.Res.,
2017 56(27):7656-7664；Zhang et al.Appl.Energy 2018(218)417–429).But how will consolidate
Body acid catalyst is coupled with traditional desorber, can efficiently carry out industrial amplification, and be applied to industrial production
In, it is the main problem faced at present.Canadian Univ Regina professor Idem etc. proposes a kind of by solid acid catalyst
After inert particle mixing, scattered heap is loaded on the method in traditional CO2 desorber, but there are gas-liquid mass transfers for the type of feed
Can be poor, gas-liquid-solid three-phase contact area is small, the lower problem of the utilization efficiency and catalysis desorption system efficiency of catalyst
(Srisang et al.Chem.Eng.Sci.,2017(170):48-57.).Thus, by catalyst simultaneous interpretation with suitable process
The CO2 desorber of system is coupled, and the catalysis desorption performance of the utilization efficiency and catalysis desorption system that improve catalyst has pole
Big industrial value.
Summary of the invention
Present invention solves the technical problem that be, by using the coupling technique of novel catalyst and traditional desorber, into
One step lowers richness CO2Amine aqueous solution regeneration energy consumption, and then reduce CO2Capture cost.
It a kind of is urged the technical scheme is that providing for reducing carbon dioxide enriched the novel of amine aqueous solution regeneration energy consumption
Change desorber, the catalysis desorber is catalytic reactor to be introduced into traditional CO2 desorption process, without changing tradition desorption
Process flow, layout of beam line and heating method of tower etc..Wherein filling solid catalyst in catalytic reactor, rich co2 amine aqueous solution
Enter from reactor bottom by the effect of pump, by coming into full contact with for catalyst and amine aqueous solution, so that the performance of catalyst obtains
It is utilized to maximized.New catalytic desorption apparatus is mainly made of catalytic reactor and packed tower, and catalytic reactor is by two sections
Independent catalytic tower composition.
Further, catalysis desorber main flow is as follows: after rich amine solution passes through packed tower first layer packing layer, entering
Catalytic reactor 1 desorbs and then is entered by catalysis packed tower second layer filler, catalytic reactor is entered back into after reaction
2, it is catalyzed desorption process again, subsequently into packed tower the last layer filler.
Further, it is catalyzed in desorber, packed tower is made of stainless steel material, is divided into 3 packing layers, is passed through
Flange is attached, and independent can carry out handling filler operation.
Further, it is catalyzed tower body height and filler in packed column layer height proportional region is: 0.2-1.
Further, the material of catalyst reactor can be glass and stainless steel.
Further, in catalyst reactor, single catalyst granules, or filling different catalysts can be loaded
Mixing or loading catalyst particle and inert particle mixing, wherein inert particle can be bead, quartz sand and
The inert particulate materials such as inert ceramic balls.
Further, in catalyst reactor 1 and 2, same catalyst can be used and loaded, also can be used not
Same catalyst is loaded, to reach the synergistic effect of different catalysts catalytic performance.
Further, the mass ratio range of catalyst amount and amine aqueous solution is 0-1 in catalyst reactor.
Further, heat medium can be the conduction oil in traditional desorption technique in reboiler, be also possible to water, desorption
85-120 DEG C of regeneration temperature range.
Common solid acid catalyst includes: molecular sieve catalyst, such as HZSM-5, γ-Al2O3Deng；Superpower solid acid is such as
SO4 2-/TiO2, SO4 2-/ZrO2Deng；Transition metal oxide such as TiO2, V2O5It is absorbed etc. being easy to be separated by solid-liquid separation and do not influence amine solvent
The solid acid catalyst of performance and its their mixture.
The common organic amine solvent for adsorbing carbon dioxide includes: monoethanolamine (MEA), diethanol amine (DEA), and three
Ethanol amine (TEOA), N methyldiethanol amine (MDEA), the tradition such as 2-amino-2-methyl-1-propanol (AMP) and piperazine (PZ) is often
Amine solvent and novel amine solvent, such as 4- (diethylin) -2- butanol (DEAB), diethylenetriamine (DETA), diethylamine
Base ethyl alcohol (DEAE) etc. and its binary or ternary and the multiple mixed solvent such as MEA-DEAB and MEA-AMP-PZ of various amine etc..；
The concentration range of amine solvent is 1-7mol/L.
The beneficial effects of the present invention are:
(1) catalytic reactor simple process, low cost.
(2) it carries out on the basis of traditional CO2 desorber compared with minor modification, cost is small.
(3) catalysis desorption performance is superior, and catalytic performance is higher than traditional desorber.
(4) carbon dioxide absorption of amine aqueous solution can be influenced small.
Detailed description of the invention
Fig. 1 shows traditional carbon dioxide enriched amine aqueous solution desorption technique flow charts.
The process flow chart of Fig. 2 expression carbon dioxide enriched amine aqueous solution desorption apparatus of new catalytic.
Specific embodiment
Embodiment 1
The 5M monoethanolamine (MEA) for the use of catalysis desorption apparatus of the invention being 0.5mol/mol amine to rich solution load
Carry out catalysis desorption.Catalysis desorber composition is as follows, and tower body is made of stainless steel, and tower internal diameter is 35mm, and packed height 0.6m is filled out
Material is structured packing；Two catalyst reactors height is 0.3m, and the mass ratio of catalyst and amine aqueous solution is 1/80.It uses
Solid acid catalyst is HZSM-5, γ-Al2O3With SAPO-34 molecular sieve catalyst.Heat medium is conduction oil, and desorption temperature is
95 DEG C, liquid inventory 6m3/m2。
Solvent desorption energy consumption (Qreg, kJ/kg CO2) calculated by two parts numerical value, i.e. reboiler heat duty (Hreb,kJ/h)
And CO2Mass flowrate (the m of gasCO2, kg/h) ratio.
Wherein, Hloss: system energy loss, kJ/h
Heat consumed by solution stripping is all provided by conduction oil, calculation formula:
Hreb=moilCoil.f(Tin-TOUT) (2)
Wherein, moil: the mass flowrate of conduction oil, kg/h
Coil,f: the specific heat capacity of conduction oil under experimental conditions, kJ/ (kg DEG C)
Tin, Tout: it is respectively temperature of the conduction oil in reboiler inlet and outlet, DEG C
CO2The mass flowrate calculation formula of gas:
Wherein, namine: the molar flow rate of amine aqueous solution, kmol/h
MCO2: CO2Formula weight, g/mol
αrich, αlean: it is respectively the rich solution load and lean solution load of amine aqueous solution, mol CO2/mol amine.
Experimental result, which shows each catalyst, can substantially reduce the desorption energy consumption of MEA, and minimum desorption is shown with HZSM-5
Secondly energy consumption is respectively γ-Al2O3And SAPO-34.Energy consumption is desorbed relative to blank MEA, HZSM-5 mixed catalyst can drop
Low regeneration energy consumption 40% or so, γ-Al2O3Its regeneration energy consumption 30% and 33% can be reduced respectively with SAPO-34.
Embodiment 2
Use the monoethanolamine for the 6M that catalysis desorption apparatus of the invention is 0.5mol/mol amine to rich solution load
(MEA) and 4- (diethylin) -2- butanol (DEAB) mixing amine aqueous solution (molar ratio 5:1) carries out catalysis desorption, in order to compare
Research is that (i.e. rich amine solution does not flow through catalysis reaction for 0.5mol/mol amine5M MEA progress blank desorption to rich solution load
Device).It desorbs tower structure and embodiment 1 is identical.The solid acid catalyst used is HZSM-5, γ-Al2O3With HZSM-5/ γ-
Al2O3Mixed catalyst.Heat medium is tap water, and desorption temperature is set as 95 DEG C, liquid inventory 6m3/m2.Solvent desorption
Energy consumption (Qreg, kJ/kg CO2) calculated by two parts numerical value, i.e. reboiler heat duty (Hreb, kJ/h) and CO2The quality stream of gas
Rate (mCO2, kg/h) ratio, calculation method is the same as example 1.
Experimental result shows that each catalyst can substantially reduce rich CO2The desorption energy consumption of amine aqueous solution, wherein with HZSM-5/
γ-Al2O3It shows minimum desorption energy consumption, is secondly respectively HZSM-5, γ-Al2O3.Energy consumption is desorbed relative to blank MEA,
MEA-DEAB mixed solution and HZSM-5/ γ-Al2O3The combination of mixed catalyst can reduce regeneration energy consumption 60% or so, display
Optimal catalytic regeneration performance.
Claims (9)
1. a kind of new catalytic desorber for reducing carbon dioxide enriched amine aqueous solution regeneration energy consumption, it is characterised in that will be catalyzed
Reactor is introduced into traditional CO2 desorption process, process flow, layout of beam line and heating method without changing traditional desorber
Deng.Wherein filling solid catalyst in catalytic reactor, rich co2 amine aqueous solution are entered by the effect of pump from reactor bottom, are led to
Coming into full contact with for catalyst and amine aqueous solution is crossed, so that the performance of catalyst maximizes the use.New catalytic desorption apparatus
It is mainly made of catalytic reactor and packed tower, catalytic reactor is made of two sections of independent catalytic towers.
2. content according to claim 1, which is characterized in that its main flow is as follows: rich amine solution passes through packed tower first
After layer packing layer, into catalytic reactor 1, packed tower second layer filler is desorbed and then entered by catalysis, after reaction again
Into catalytic reactor 2, it is catalyzed desorption process again, subsequently into packed tower the last layer filler.
3. content according to claim 1, which is characterized in that in the catalysis desorber, packed tower is by stainless steel material group
At, be divided into 3 packing layers, be attached by flange, independent can carry out handling filler operation.
4. content according to claim 1, which is characterized in that catalysis tower body height and filler in packed column layer height proportional region
It is: 0.2-1.
5. content according to claim 1, which is characterized in that the material of catalyst reactor can be glass and stainless steel.
6. content according to claim 1, which is characterized in that in catalyst reactor, single catalyst particles can be loaded
Grain loads the mixing of different catalysts or the mixing of loading catalyst particle and inert particle, wherein inertia grain
Son can be the inert particulate materials such as bead, quartz sand and inert ceramic balls.
7. content according to claim 1, which is characterized in that in catalyst reactor 1 and 2, same catalysis can be used
Agent is loaded, and different catalyst also can be used and loaded, to reach the synergistic effect of different catalysts catalytic performance.
8. content according to claim 1, which is characterized in that the quality of catalyst amount and amine aqueous solution in catalyst reactor
Proportional region is 0-1.
9. content according to claim 1, which is characterized in that heat medium can be in traditional desorption technique in reboiler
Conduction oil is also possible to water, 85-120 DEG C of desorption and regeneration temperature range.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201811099663.8A CN109351125A (en) | 2018-09-20 | 2018-09-20 | A novel catalytic desorption tower for reducing energy consumption for regeneration of CO2-rich amine solution |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811099663.8A CN109351125A (en) | 2018-09-20 | 2018-09-20 | A novel catalytic desorption tower for reducing energy consumption for regeneration of CO2-rich amine solution |
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| CN109351125A true CN109351125A (en) | 2019-02-19 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113491946A (en) * | 2020-04-08 | 2021-10-12 | 中石化南京化工研究院有限公司 | Absorbent regeneration equipment and regeneration method |
| CN113731489A (en) * | 2021-09-10 | 2021-12-03 | 湖南大学 | Ionic liquid catalyst for regeneration of carbon dioxide-rich amine solution |
| CN113856412A (en) * | 2021-08-25 | 2021-12-31 | 南京工业大学 | A kind of method and device for desorbing carbon dioxide from alcohol amine rich liquid |
| CN114160113A (en) * | 2021-12-07 | 2022-03-11 | 南京大学 | Titanium-zirconium bimetallic oxide catalyst for reinforcing carbon dioxide desorption and application thereof |
| CN114699883A (en) * | 2022-04-22 | 2022-07-05 | 浙江大学 | Catalyst cooperates with external field to strengthen carbon dioxide low energy consumption desorption system and method |
| WO2024187272A1 (en) * | 2023-03-10 | 2024-09-19 | Entropy Inc. | Methods and systems for spouted bed and jet flow solvent regeneration |
| CN118925447A (en) * | 2024-08-05 | 2024-11-12 | 深圳市深汕特别合作区华润电力有限公司 | A carbon dioxide capture system and method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100319532A1 (en) * | 2009-06-17 | 2010-12-23 | Mitsubishi Heavy Industries, Ltd. | Co2 recovery apparatus and co2 recovery method |
| CN102198368A (en) * | 2010-03-26 | 2011-09-28 | 巴布科克和威尔科克斯能量产生集团公司 | Chemical compounds for the removal of carbon dioxide from gases |
| JP2016129877A (en) * | 2015-01-14 | 2016-07-21 | 株式会社東芝 | Acid gas absorbent, acid gas removal method and acid gas removal device |
| CN107519824A (en) * | 2017-10-10 | 2017-12-29 | 天津市新天进科技开发有限公司 | A kind of combined type high flux catalytic distillation tower member |
-
2018
- 2018-09-20 CN CN201811099663.8A patent/CN109351125A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100319532A1 (en) * | 2009-06-17 | 2010-12-23 | Mitsubishi Heavy Industries, Ltd. | Co2 recovery apparatus and co2 recovery method |
| CN102198368A (en) * | 2010-03-26 | 2011-09-28 | 巴布科克和威尔科克斯能量产生集团公司 | Chemical compounds for the removal of carbon dioxide from gases |
| JP2016129877A (en) * | 2015-01-14 | 2016-07-21 | 株式会社東芝 | Acid gas absorbent, acid gas removal method and acid gas removal device |
| CN107519824A (en) * | 2017-10-10 | 2017-12-29 | 天津市新天进科技开发有限公司 | A kind of combined type high flux catalytic distillation tower member |
Non-Patent Citations (1)
| Title |
|---|
| WAYUTA SRISANG等: "Evaluation of the heat duty of catalyst-aided amine-based post combustion CO2 capture", 《CHEMICAL ENGINEERING SCIENCE》 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113491946A (en) * | 2020-04-08 | 2021-10-12 | 中石化南京化工研究院有限公司 | Absorbent regeneration equipment and regeneration method |
| CN113491946B (en) * | 2020-04-08 | 2023-04-11 | 中国石油化工股份有限公司 | Absorbent regeneration equipment and regeneration method |
| CN113856412A (en) * | 2021-08-25 | 2021-12-31 | 南京工业大学 | A kind of method and device for desorbing carbon dioxide from alcohol amine rich liquid |
| CN113731489A (en) * | 2021-09-10 | 2021-12-03 | 湖南大学 | Ionic liquid catalyst for regeneration of carbon dioxide-rich amine solution |
| CN114160113A (en) * | 2021-12-07 | 2022-03-11 | 南京大学 | Titanium-zirconium bimetallic oxide catalyst for reinforcing carbon dioxide desorption and application thereof |
| CN114699883A (en) * | 2022-04-22 | 2022-07-05 | 浙江大学 | Catalyst cooperates with external field to strengthen carbon dioxide low energy consumption desorption system and method |
| WO2024187272A1 (en) * | 2023-03-10 | 2024-09-19 | Entropy Inc. | Methods and systems for spouted bed and jet flow solvent regeneration |
| CN118925447A (en) * | 2024-08-05 | 2024-11-12 | 深圳市深汕特别合作区华润电力有限公司 | A carbon dioxide capture system and method |
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Application publication date: 20190219 |