CN103212275A - Method for resolving decarburization absorbent rich liquid of synthetic ammonia shift gas - Google Patents
Method for resolving decarburization absorbent rich liquid of synthetic ammonia shift gas Download PDFInfo
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- CN103212275A CN103212275A CN201210016741XA CN201210016741A CN103212275A CN 103212275 A CN103212275 A CN 103212275A CN 201210016741X A CN201210016741X A CN 201210016741XA CN 201210016741 A CN201210016741 A CN 201210016741A CN 103212275 A CN103212275 A CN 103212275A
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- 230000002745 absorbent Effects 0.000 title claims abstract description 42
- 239000002250 absorbent Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 31
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 17
- 239000007788 liquid Substances 0.000 title abstract description 31
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title abstract description 14
- 238000005261 decarburization Methods 0.000 title description 5
- 238000005262 decarbonization Methods 0.000 claims abstract description 11
- 239000007791 liquid phase Substances 0.000 claims abstract description 8
- 230000009471 action Effects 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 22
- 230000008929 regeneration Effects 0.000 claims description 18
- 238000011069 regeneration method Methods 0.000 claims description 18
- 230000009466 transformation Effects 0.000 claims description 10
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 8
- 239000012190 activator Substances 0.000 claims description 5
- 230000002411 adverse Effects 0.000 claims description 4
- 239000007792 gaseous phase Substances 0.000 claims description 4
- 239000000243 solution Substances 0.000 claims 15
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims 2
- 235000011114 ammonium hydroxide Nutrition 0.000 claims 1
- 239000007864 aqueous solution Substances 0.000 claims 1
- 230000005540 biological transmission Effects 0.000 claims 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 claims 1
- 238000012546 transfer Methods 0.000 abstract description 8
- 239000012071 phase Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000004458 analytical method Methods 0.000 abstract description 4
- 230000003213 activating effect Effects 0.000 abstract 1
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- CXHHBNMLPJOKQD-UHFFFAOYSA-M methyl carbonate Chemical compound COC([O-])=O CXHHBNMLPJOKQD-UHFFFAOYSA-M 0.000 abstract 1
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 19
- 230000008569 process Effects 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 9
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 239000011736 potassium bicarbonate Substances 0.000 description 6
- 235000015497 potassium bicarbonate Nutrition 0.000 description 6
- 229910000028 potassium bicarbonate Inorganic materials 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 230000001133 acceleration Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 230000016507 interphase Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 101150103244 ACT1 gene Proteins 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 101100161918 Glycine max SAC1 gene Proteins 0.000 description 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 229940043237 diethanolamine Drugs 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 125000001434 methanylylidene group Chemical group [H]C#[*] 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 235000011181 potassium carbonates Nutrition 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0042—Degasification of liquids modifying the liquid flow
- B01D19/0052—Degasification of liquids modifying the liquid flow in rotating vessels, vessels containing movable parts or in which centrifugal movement is caused
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a method for resolving decarbonization absorbent rich liquid of synthetic ammonia shift gas, which comprises the steps of feeding the absorbent rich liquid and steam into a hypergravity rotating bed reactor, leading the absorbent rich liquid to flow from the inner edge of a rotor to the outer edge of the rotor under the action of centrifugal force, leading the absorbent rich liquid to be in countercurrent or cross-current contact with the steam in the hypergravity rotating bed reactor, and regenerating the rich liquid under the condition of hypergravity; the resolved CO2 and the low-pressure steam after heat transfer are discharged from a gas phase outlet, and the regenerated solution flows out from a liquid phase outlet at the lower part of the supergravity reactor; the pressure of the system during analysis is 0.1-0.5 MPa, and the temperature is 90-160 ℃; the rotating speed of the rotor of the super-gravity rotating bed reactor is 100-3000 r/min; the mass percentage concentration of the absorbent rich solution of the methyl carbonate in the solution is 20-60%; the mass percentage concentration of the activating agent in the solution is 1-5%; the invention has high pregnant solution resolution ratio, low energy consumption and small equipment occupied space.
Description
Technical field
The present invention relates to a kind of method of resolving synthetic-ammonia transformation gas decarbonization absorbent rich solution, also relate to the application of high-gravity technology in the absorbent rich solution is resolved.
Background technology
In the Ammonia Production technical process, two sections reformed gas of natural gas, CO after pyrolytic conversion
2Content is up to 18～19%, because CO
2Can make catalyst poisoning, so conversion gas must be removed thoroughly before entering synthesis loop; CO in addition
2Be again the raw material of urea plant, must be reclaimed CO
2Remove and reclaim the Carbon balance that is directly connected to the ammonia synthesis process system, therefore, CO
2Remove and reclaim most important.Decarburization energy consumption accounts for about 10% of whole ammonia energy consumption, therefore removes CO
2The energy consumption height of technology is very big to the influence of ammonia factory total energy consumption.
The method of present industrial parsing decarburization rich solution is a lot, but principle is all identical, mainly slightly different because of the difference of absorption process, all be to be mass transfer apparatus with the regenerator, low-pressure steam enters from the bottom of tower, and rich solution enters from cat head, gas-liquid is counter current contacting in packing layer, and then reach the purpose of regeneration. still, no matter adopt any method decarburization, the mass-transfer efficiency of tower equipment directly affects and absorbs CO
2After the internal circulating load and the CO of rich solution
2Reclaim, also just affect the regeneration cost of decarbonizing process.The efficient height of resolver, the internal circulating load of rich solution are with regard to corresponding minimizing, and the regeneration load reduces simultaneously, thereby has saved the energy, has reduced the cost of regenerative process.Therefore, the mass-transfer efficiency of raising analyzing device is the most direct valid approach that reduces cost, increases economic efficiency.
In the legacy equipment between the vapour-liquid power resources of reverse contact be gravitational field.Because of gravity acceleration value limited (9.8m/s2), cause the dirty speed of liquid slower, for preventing liquid flooding and serious entrainment, the vapour phase rate of climb is also little, so relative velocity is less between the two-phase, and mass transfer effect is not good.
High-gravity technology is a new technology of utilizing the hypergravity environment more much bigger than terrestrial gravitation acceleration that mass transfer, diabatic process and micro mixing are strengthened, produces the hypergravity environment of simulating by rotation on earth and obtains.It can increase substantially the conversion ratio and the selectivity of reaction, dwindles the volume of reactor significantly, simplifies technology, flow process, and implementation procedure energy-efficient reduces disposal of pollutants.Research and analysis show, under the hypergravity environment, molecular diffusion between different sized molecules and interphase mass transfer process are all than in after the match faster of terrestrial gravitation, produce the contact of flowing in gas one liquid, liquid-liquid, the liquid one solid porous media of two-phase under the hypergravity environment bigger hundreds of times to thousand times than earth gravitational field, great shear forces makes liquid crushing become nano level film, silk and drips, produce boundary huge and that upgrade fast, make and improve 1～3 order of magnitude in the traditional tower of interphase mass transfer speed ratio, mass transport process is greatly strengthened.
Aspect the energy-conservation regeneration techniques of exploitation new technological process, Uop Inc. early develops steam jet ejector flash regeneration lean solution technology, pressure swing regeneration power-saving technology in recent years and towers regeneration technology, and isolate steam in the regeneration gas and other condensable gas with membrane separating method, will return regenerator as thermal source after its compression.
Aspect the high-gravity technology decarburization, U.S. FlourDaniel company is to H
2S and CO
2Selectivity absorbs to be studied, and utilizes the difference of two component reaction rates, has reached better separating effect.Domestic the most representative is Beijing University of Chemical Technology aspect the high-gravity technology research and development, has carried out a series of innovative research work.At first hypergravity water deoxygenation technology was realized industrial applications in the world in 1998; Cooperated with U.S. DOW chemical company in 1999, and successfully high-gravity technology was applied to the gas liquid reaction separation process in the chlorine industry.And adopt high-gravity technology to resolve the research that synthetic ammonia process purifies the rich solution in the part solution recycle system, be not reported so far both at home and abroad.
Summary of the invention
The purpose of this invention is to provide the method for absorbent rich solution in a kind of deep analysis synthetic-ammonia transformation gas decarbonization technology, it is to resolve absorbent rich solution, KHCO with supergravity reactor as analyzing device
3To be 24.5% benzene Fei Er solution contact with low-pressure steam adverse current or cross-flow in rotating packed bed reactor content, thereby finish the resolving of absorbent rich solution.
Main technical schemes of the present invention:
(a) the absorbent rich solution is sent into the raw material flow container, open steam valve, adjust quantity of steam and respectively material liquid and reaction system are heated to corresponding temperature, adjust the revolution of supergravity reactor by variable-frequency governor, start supergravity reactor, after treating that supergravity reactor is stable, open the liquid reactor inlet valve, send into liquid to reactor by fluid flowmeter.
(b) absorbent rich solution and steam are sent in the rotating packed bed reactor, the absorbent rich solution flows to the rotor outer rim by the rotor inner edge under action of centrifugal force, contact with steam adverse current or cross-flow in rotating packed bed reactor, finish the resolving of absorbent.
In deep analysis synthetic-ammonia transformation gas decarbonization technology provided by the invention in the method for absorbent rich solution, used high-gravity rotating bed including, but not limited to hypergravity whirligigs such as RPB, deflector type, helical duct, fixed-rotor, rotating compact discs.The rotating speed of high-gravity rotating bed rotor is 100～3000 rev/mins, is preferably 300～2000 rev/mins, most preferably is 450～1500 rev/mins.
The absorbent that the present invention is used, employing be hot potassium carbonate solution, sodium hydroxide solution or the potassium hydroxide solution etc. of industrial interpolation activator commonly used.When adopting hot methine solution to be absorbent, used activator is including, but not limited to diethanol amine, ACT-1 etc.
The mass percent concentration of hot potassium carbonate in solution is 20～60% in the described absorbent rich solution, and be preferred 25～40%, especially preferred 30～35%, and the mass percent concentration of activator in solution is 1～5%, preferred 1.5～4%, especially preferred 2～3.5%.
The pressure of system is 0.1～0.5MPa during parsing, is preferably 0.1～0.3MPa, most preferably is 0.1～0.2MPa.The temperature of system is preferably 100～130 ℃ at 80～140 ℃, most preferably is 110～120 ℃.
The invention effect
The invention provides a kind of method that adopts high-gravity rotating bed parsing absorbent rich solution, purpose of the present invention provides a kind of new technology to replace the resolving that traditional technology based on tower equipment is finished the absorbent rich solution, the present invention is with respect to the prior art of resolving the absorbent rich solution with tower, having the absorbent rich solution resolves thoroughly, advantages such as equipment investment is few, and it is little that energy consumption is low, equipment takes up space.KHCO in the rich solution
3Content be 24.5% benzene Fei Er solution through behind the rotating packed bed reactor, KHCO
3Content can drop to below 10%.
Description of drawings
Fig. 1 is a process chart of the present invention.
Wherein: 3-is high-gravity rotating bed for the import of 1-liquid phase import 2-gas phase
The outlet of 4-rotor 5-gaseous phase outlet 6-liquid phase
The specific embodiment
The reacting flow chart of a kind of embodiment of the present invention as shown in Figure 1.Open high-gravity rotating bedly 3, regulate rotating speed to desired speed.The absorbent rich solution is sprayed the inner edge of high-gravity rotating bed rotor 4 by liquid distribution trough via liquid phase inlet tube 1, low-pressure steam enters into rotating packed bed reactor via gas phase inlet tube 2, contact with absorption liquid adverse current or cross-flow in high-gravity rotating bed rotor, under the hypergravity condition, finish KHCO
3Decomposition, the CO2 of discharge discharges from gaseous phase outlet 5, enters follow-up workshop section.The absorbent lean solution flows out from the liquid phase outlet 6 that is positioned at the rotating packed bed reactor bottom.Adopt Q/SY DH0126.02-2001 titrator to analyze HCO in the rotating packed bed reactor outlet liquid
3 -Content.
Embodiment 1
Table 1 absorbent rich solution is formed
The regulating system temperature is 120 ℃, pressure is adjusted to 0.2Mpa, start rotating packed bed reactor, adjusting rotor speed is 1200r/m, open the by-pass valve control of liquid reactor import then, absorbent is sprayed the inner edge of high-gravity rotating bed rotor 4 by liquid distribution trough via liquid phase inlet tube 1, the flow of regulating liquid is 50Kg/h, low-pressure steam enters into rotating packed bed reactor by gas phase inlet tube 2, with absorption liquid counter current contacting in high-gravity rotating bed rotor, under the hypergravity condition, finish KHCO
3Decomposition, the CO of discharge
2Discharge from gaseous phase outlet 5, enter follow-up workshop section.The flow of low-pressure steam is 2Kg/h.The absorbent lean solution flows out from the liquid phase outlet 6 that is positioned at the rotating packed bed reactor bottom.Adopt Q/SY DH0126.02-2001 potentiometric titrimeter, analyze HCO in the rotating packed bed reactor outlet liquid
3 -Content.
Embodiment 2-5
Remove the gas liquid ratio in the Change Example 1, all the other are by example 1 conditional operation, and experimental result sees Table 2.
The different gas liquid ratio regeneration test of table 2 result
As can be seen from Table 2, along with reducing gradually of gas liquid ratio, KHCO3 concentration raises gradually in the regeneration lean solution, that is to say, the regeneration of absorbent rich solution is more and more not thorough.At steam/rich solution mass ratio is 1: when (25～50), and KHCO in the lean solution
3Concentration can be reduced to below 10%.Compare with tower equipment, under the equal conditions, reach same parsing effect, tower equipment steam/rich solution mass ratio is generally 1: (18～30), hypergravity equipment steam consumption is compared with tower equipment, obviously reduces.
Embodiment 6-9
Adopt the method for example 1, change regeneration temperature, all the other are by example 1 conditional operation, and experimental result sees Table 3.
Table 3 different temperatures regeneration test result
As can be seen from Table 3, along with the rising of temperature, KHCO3 concentration descends gradually in the solution, that is to say that the resolution ratio of KHCO3 improves; When reaction temperature reaches after 120 ℃, curve tends to be steady, and absorbent KHCO3 content is reduced to below 10%, has been lower than the tower regeneration lean solution KHCO3 of factory content (the tower regeneration lean solution KHCO3 of factory content 11%～12%), consider that from energy-saving and cost-reducing angle suitable reaction temperature is 120 ℃.
Embodiment 10-13
Adopt the method for example 1, change rotor revolution number, all the other are by example 1 conditional operation, and experimental result sees Table 4.
Table 4 different rotor revolution regeneration test result
As can be seen from Table 4, than the slow-speed of revolution time, KHCO in the absorbent
3Concentration, reduce, but when rotor speed is higher than 1200r/min KHCO in the solution gradually with the increase of rotating speed
3Concentration begins to increase.Analyze its reason, because the revolution of rotor is high more, the size of liquid film, brin and the drop that can cut into liquid becomes littler, and the heat absorption effect can be more better, is beneficial to the carrying out of decomposition reaction; But, when rotating speed surpasses 1200r/min, can cause Partial K HCO because the height of rotating speed can influence the time of staying of material in reactor
3Do not have enough time to decompose and just thrown away packing layer, cause KHCO by rotor
3Decomposition efficiency reduces.Relatively Shi Yi rotor speed is 1200r/min.
Claims (6)
1. method of resolving synthetic-ammonia transformation gas decarbonization absorbent rich solution, it is characterized in that: absorbent rich solution and steam are sent in the rotating packed bed reactor, the absorbent rich solution flows to the rotor outer rim by the rotor inner edge under action of centrifugal force, contact with low-pressure steam adverse current or cross-flow in rotating packed bed reactor, under the hypergravity condition, carry out rich solution regeneration; CO2 after the parsing and the low-pressure steam that carries out after the heat transmission are discharged from gaseous phase outlet, and the solution after the regeneration flows out from the liquid phase outlet that is positioned at the supergravity reactor bottom; The pressure of system is 0.1～0.5MPa during parsing, and temperature is at 90～160 ℃; The rotating speed of rotating packed bed reactor rotor is 100～3000 rev/mins;
Described absorbent rich solution is that the mass percent concentration of carbonic acid first in solution is 20～60%; The mass percent concentration of activator in solution is 1～5%.
2. the method for parsing synthetic-ammonia transformation gas decarbonization absorbent rich solution according to claim 1, it is characterized in that: employed equipment is rotating packed bed reactor, comprises RPB, deflector type hypergravity whirligig, helical duct hypergravity whirligig, fixed-rotor hypergravity whirligig or rotating compact disc hypergravity whirligig.
3. the method for parsing synthetic-ammonia transformation gas decarbonization absorbent rich solution according to claim 1, it is characterized in that: the rotating speed of rotating packed bed reactor rotor is 300～2000 rev/mins minutes.
4. the method for parsing synthetic-ammonia transformation gas decarbonization absorbent rich solution according to claim 1 is characterized in that: the absorbent rich solution absorbs solution behind the CO2 for hot potassium carbonate solution, ammoniacal liquor or the alcamines aqueous solution that adopts industrial interpolation activator commonly used.
5. the method for parsing synthetic-ammonia transformation gas decarbonization absorbent rich solution according to claim 1, it is characterized in that: the pressure of system is 0.1～0.3MPa when resolving.
6. the method for parsing synthetic-ammonia transformation gas decarbonization absorbent rich solution according to claim 1, it is characterized in that: the temperature of system is 100～140 ℃ when resolving.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210016741XA CN103212275A (en) | 2012-01-18 | 2012-01-18 | Method for resolving decarburization absorbent rich liquid of synthetic ammonia shift gas |
| PCT/CN2012/001009 WO2013106974A1 (en) | 2012-01-18 | 2012-07-27 | Method for desorbing rich liquid of synthetic ammonia shift gas decarbonization absorbent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210016741XA CN103212275A (en) | 2012-01-18 | 2012-01-18 | Method for resolving decarburization absorbent rich liquid of synthetic ammonia shift gas |
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| CN201210016741XA Pending CN103212275A (en) | 2012-01-18 | 2012-01-18 | Method for resolving decarburization absorbent rich liquid of synthetic ammonia shift gas |
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| CN (1) | CN103212275A (en) |
| WO (1) | WO2013106974A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106422667A (en) * | 2015-08-04 | 2017-02-22 | 北京思践通科技发展有限公司 | Method for removing acidic components and water from gas in one step |
| CN107596903A (en) * | 2017-04-14 | 2018-01-19 | 蒋本基 | Method for capturing carbon dioxide in flue gas by using supergravity carbonating device |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2566716A (en) * | 2017-09-22 | 2019-03-27 | Fjell Biodry As | Gas capture system |
| CN110261216B (en) * | 2019-06-20 | 2024-02-27 | 浙江大学 | Material performance testing system under supergravity environment suspension type multi-field coupling effect |
| CN110982076A (en) * | 2019-12-26 | 2020-04-10 | 江苏美思德化学股份有限公司 | Method for preparing low-volatile polysiloxane by using supergravity device |
| CN113477188B (en) * | 2021-07-02 | 2023-08-29 | 北京化工大学 | Immersed rotary packed bed reactor and application thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101168115A (en) * | 2007-08-27 | 2008-04-30 | 中国石油天然气股份有限公司 | CO in desorption conversion gas2Method (2) |
| CN101549274A (en) * | 2008-04-01 | 2009-10-07 | 北京化工大学 | Supergravity revolving bed device and application in carbon dioxide collecting and passivating process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20110131937A1 (en) * | 2009-12-08 | 2011-06-09 | Yang Hsien Ming | absorptive device to carbon dioxide in the air |
| CN102125795A (en) * | 2011-01-28 | 2011-07-20 | 中北大学 | Method and device for removing CO2 from conversion gas of synthetic ammonia |
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- 2012-01-18 CN CN201210016741XA patent/CN103212275A/en active Pending
- 2012-07-27 WO PCT/CN2012/001009 patent/WO2013106974A1/en active Application Filing
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101168115A (en) * | 2007-08-27 | 2008-04-30 | 中国石油天然气股份有限公司 | CO in desorption conversion gas2Method (2) |
| CN101549274A (en) * | 2008-04-01 | 2009-10-07 | 北京化工大学 | Supergravity revolving bed device and application in carbon dioxide collecting and passivating process |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106422667A (en) * | 2015-08-04 | 2017-02-22 | 北京思践通科技发展有限公司 | Method for removing acidic components and water from gas in one step |
| CN106422667B (en) * | 2015-08-04 | 2019-07-30 | 北京思践通科技发展有限公司 | The method of one-step removal acidic components and water from gas |
| CN107596903A (en) * | 2017-04-14 | 2018-01-19 | 蒋本基 | Method for capturing carbon dioxide in flue gas by using supergravity carbonating device |
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| Publication number | Publication date |
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| WO2013106974A1 (en) | 2013-07-25 |
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Application publication date: 20130724 |