CN1631488A - Method for pre-reclaiming and anew-reclaiming mechanism for removing CO#[2] from converting gas of pressure swing adsorption device - Google Patents
Method for pre-reclaiming and anew-reclaiming mechanism for removing CO#[2] from converting gas of pressure swing adsorption device Download PDFInfo
- Publication number
- CN1631488A CN1631488A CNA2004100410002A CN200410041000A CN1631488A CN 1631488 A CN1631488 A CN 1631488A CN A2004100410002 A CNA2004100410002 A CN A2004100410002A CN 200410041000 A CN200410041000 A CN 200410041000A CN 1631488 A CN1631488 A CN 1631488A
- Authority
- CN
- China
- Prior art keywords
- pressure
- adsorption tower
- gas
- tower
- adsorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention unfurls a kind of way of removing carbon dioxide by attach equipment. Every attach tower including the craft step as follows: attach A, advanced recycle YR, balance and reduce press, recycle ZR, absorb VC, balance and increase press ER and last increase presser, the invention can change the attach equipment to the no-recycle craft step by auto or hand under the condition of machine working; the invention realizes the maximum recycle of validity air like hydrogen, nitrogen spirit and carbon monoxide, so we can increase the total yield of ammonia and methyl alcohol by maximum.
Description
Technical field:
The present invention relates to adopt the transformation suction type from conversion gas, to remove CO
2Method, concrete, the present invention relates to a kind of employing transformation adsorbed gas isolation technics band pre-reclaim and reclaim again remove CO in the conversion gas
2Method, this method is mainly used in little nitrogenous fertilizer or the fertilizer industry.
Background technology:
From conversion gas, remove CO with the transformation suction type
2Method, though existing both at home and abroad a lot of disclosed patent documentation report, but in these patent documentations, all do not relate to the process units of whole nitrogenous fertilizer or chemical fertilizer production front and back workshop section and the relation between the pressure-swing absorption apparatus, and just to the single disclosure of pressure-swing absorption apparatus, caused the pressure-swing absorption apparatus investment excessive thus, and available gas H
2, N
2, CO loss, especially N
2, CO loss bigger, thereby cause H in whole nitrogenous fertilizer or the chemical fertilizer production device
2, N
2Or the serious imbalance of CO ratio, and then the total output and the operating cost of synthetic ammonia and methanol production have been influenced.
Summary of the invention:
The present invention is intended to overcome above-mentioned defective, and pre-the recovery with reclaiming again of the pressure-swing absorption apparatus band that provides a kind of and whole Ammonia Production technological process to combine removes CO in the conversion gas
2Method.This method can make available gas H
2, N
2, CO the rate of recovery reach maximization, and can be according to the concrete condition of different manufacturers, adjust H
2, N
2, CO ratio, thereby improve the total output of Ammonia Production to greatest extent.
For achieving the above object, the technical solution used in the present invention is as follows:
The pre-recovery with reclaiming again of a kind of pressure-swing absorption apparatus band removes CO in the conversion gas
2Method, it is characterized in that: each adsorption tower is once comprising following processing step in the circulation successively:
A, absorption A
Conversion gas from moisture trap, in the absorption operating pressure from bottom to top during the ground warp adsorption tower, saturation water, sulphur, carbon dioxide are adsorbed agent and optionally adsorb in the air-flow, and the Purge gas that removes behind the carbon dioxide is discharged from the adsorption tower top, as product gas input workshop section down.When impurity arrives the adsorbent certain altitude, promptly stop the input of raw material and the output of product gas.Adsorb this moment and still leave one section between the forward position and the port of export and " also do not adsorb saturated CO
2Adsorbent " i.e. the reservation section of contaminated adsorbent not.
Described adsorbent is a kind of in activated carbon, Kiselgel A or the activated alumina, perhaps according to the different situations of source of the gas press different proportion layering filling wherein two or three.
B, reclaim YR in advance
Adsorption process is opened program-controlled valve after finishing, and the gas in the adsorption tower is reclaimed in advance to the gas that the carbonization secondary tower carries out isostasy, and this moment, the absorption forward position of adsorption tower continued to push ahead, and after pressure was in a basic balance, pre-removal process promptly finished.
Because after adsorption process finishes, therefore still keep the high pressure that equates with adsorptive pressure in the adsorption tower, can implement the pre-recovery of conversion gas according to carbonization workshop section resistance drop in the chemical fertilizer production usually than the characteristics of the high 0～0.3MPa of resistance drop (gauge pressure) of pressure-swing absorption apparatus.
C, drop pressure ED
After pre-removal process finishes, still keep higher pressure in the adsorption tower, between adsorption tower and adsorption tower, or carry out isostasy between adsorption tower and the downflow releasing tank, make the pressure of adsorption tower drop to minimum as far as possible.
The number of times of all pressing continuously between described adsorption tower and the adsorption tower is 1～6 time.
The number of times of all pressing indirectly between described adsorption tower and the downflow releasing tank is 1～5 time.
D, reclaim ZR again
After the drop pressure process finishes, also have certain pressure in the adsorption tower, the residual gas in the adsorption tower put into a downflow releasing tank, with hydrogen gas compressor downflow releasing tank is forced into adsorptive pressure again after, enter recycling can and store.
Described hydrogen gas compressor is the ZW type.
The pressure of described downflow releasing tank is controlled at-0.02～0.03MPa scope in.
CO in the described downflow releasing tank
2Concentration of volume percent be 0～8%.
The adsorbent filler is housed in the described downflow releasing tank or is unkitted the adsorbent filler.
Be filled with adsorbent or filled with adsorbent not in the described recycling can.
E, VC finds time
After removal process finished again, the pressure in the adsorption tower was essentially negative pressure, vacuumizes further step-down by vavuum pump, made adsorbent obtain resolving regeneration.
Described vavuum pump vacuumizes, and is meant to adopt two pipelines respectively adsorption tower to be vacuumized; Perhaps adopt two pipelines simultaneously adsorption tower to be vacuumized by opening program-controlled valve.
F, boost pressure ER
After evacuation process finished, adsorption tower was accepted boosting of other adsorption tower or downflow releasing tank drop pressure gas from the port of export, and the pressure of adsorption tower is progressively raise.
The number of times of described boost pressure is 1～6 time that equates fully with the number of times of drop pressure.
G, fill the FR that boosts eventually
After the boost pressure process finishes, calm the anger by adding in the recovery tower and from the adsorption tower top adsorption tower finally to be boosted, until the pressure that reaches product gas from adsorption tower bottom and product gas.
Unstripped gas of the present invention is the conversion gas of synthetic ammonia or the flashed vapour of wet method decarburization, and its synthetic-ammonia transformation gas typical case is composed as follows:
Component H
2N
2CO CO
2CH
4Other total sulfur H
2O (vapour)
Concentration 45～57% 13～20% 0.2～10% 20～32% 1～3%～1＜250mg/m
3Saturated
Described adsorption tower is 4～16.
Described adsorptive pressure is 0.1～3.0MPa.
The invention has the advantages that:
1, in pre-removal process, a sequencing valve and a segment process pipeline have only been increased, pressure-swing absorption apparatus and carbonizing plant serial or parallel connection are used, just the rate of recovery that improves the effective gas of device has been played crucial effect, its small investment, effect is obvious, has also reduced the hardware investment of whole device simultaneously.
2, employed downflow releasing tank breaks down at some equipment of device in removal process again, but need do not stop it is switched to when not having the technological process of recovery, can be used as equalizer tank again and use.
3, in removal process again, the gas that not only will be in the adsorption tower of negative pressure has carried out a large amount of recovery, the available gas of device is almost all reclaimed, also reduced the load of vavuum pump, equipment investment and operating cost have been reduced, the gas of recycling can storage afterwards can be used as inflation eventually and returns pressure-swing absorption apparatus from the bottom of adsorption tower, to reclaim this part again by the gas of emptying.If tolerance is little or pressure-swing absorption apparatus and the series connection of carbonization workshop section, also this part gas directly can be sent into the carbonization secondary tower.If pack the adsorbent filler in addition in the recycling can into, also the gas-pressurized that reclaims in the gas tank directly can be gone into workshop section down as the product pneumatic transmission, also can be used as inflation eventually and enter pressure-swing absorption apparatus from the adsorption tower bottom.The recycling can of dress adsorbent filler is worked as CO
2Adsorb saturated after, can be by the handoff functionality of control system, under the situation that device does not stop, resolve the processing that brings back to life adsorbent to recycling can.
4, in evacuation process, adsorption tower is CO in resolving vacuum gas at every turn
2Initial concentration and CO
2Finish concentration all more than 90%, not only improved H greatly
2, N
2, CO the rate of recovery, but also be food-class CO
2Production technical guarantee is provided.
5, vavuum pump adopts two pipelines respectively two adsorption towers to be vacuumized or two pipelines connect the method that simultaneously an adsorption tower is vacuumized by program-controlled valve, under equal conditions, can improve the pumpdown time more than 60%.
6, when the control system of pressure-swing absorption apparatus when recovery system partly breaks down, also can under the situation of not stopping, pressure-swing absorption apparatus be switched to without going in the processing step that reclaims by the automatic or manual operation.
7, the present invention has realized available gas H
2, N
2, the CO rate of recovery maximization, thereby improved the total output of synthetic ammonia and methanol production to greatest extent.
Description of drawings:
Fig. 1 is the process chart of the embodiment of the invention 1
Fig. 2 is the process chart of the embodiment of the invention 2
Fig. 3 is the program list of the embodiment of the invention 1 technological process
Fig. 4 is the program list of the embodiment of the invention 2 technological processes
The specific embodiment:
The pre-recovery with reclaiming again of a kind of pressure-swing absorption apparatus band removes CO in the conversion gas
2Method, it is the conversion gas of raw material with the carbonated coal balls, by optimized proportion activated alumina, activated carbon, Kiselgel A is housed in the adsorption tower, its gas composition is as follows:
Component H
2N
2CO CO
2CH
4Other total sulfur H
2O (vapour)
Concentration (V)～50%～15%～3%～31%～1%～1＜40mg/m
3Saturated
Unstripped gas temperature≤40 ℃ wherein, pressure: 0.70MPa
As shown in Figure 1, it is characterized in that: each adsorption tower following processing step of experience successively in circulation once: absorption, pre-reclaim, one all fall, two all fall, three all fall, four all fall, reclaim again, find time, four all rise, three all rise, two all rise, one all rise and whole filling boosted.
Described adsorbent equipment is made up of eight adsorption towers, a steam-water separator, two downflow releasing tanks and a recycling can; Activated alumina, activated carbon, three kinds of adsorbents of Kiselgel A are equipped with in layering from bottom to up in the described adsorption tower.
Be that example describes (referring to Fig. 1, Fig. 3) with the A tower below:
A, absorption
Conversion gas from moisture trap, under the absorption operating pressure of 0.7MPa, after V-1A flows through adsorption tower from bottom to up from A tower lower end, saturation water in the air-flow, sulphur, carbon dioxide are adsorbed agent and optionally adsorb, the Purge gas that removes behind the carbon dioxide is discharged from the adsorption tower top through KV-2A, as product gas input workshop section down.When the absorption forward position of impurity component (promptly refer in the product allowed maximum impurity concentration) when arriving the adsorbent bed certain altitude, promptly stops the input of unstripped gas and the output of product gas.
B, the pre-recovery
After adsorption process stops, KV-1A, KV-2A valve closing, still keep the high pressure that equates with adsorptive pressure in the adsorption tower, make the gas in the adsorption tower carry out isostasy by opening valve KV-3A, KV6 to the carbonization secondary tower, this moment, the absorption forward position of A tower continued to push ahead, and after pressure is in a basic balance, closed KV5, at this moment, the absorption forward position of A tower does not reach the port of export yet.The effect of this process is the portioned product gas that reclaims A tower dead space, and the product gas of its gas composition purity and output is basic identical.
C, one all falls
After removal process stops, also keeping higher pressure in the adsorption tower, adsorption tower A, E are communicated carry out isostasy by opening valve KV-3A, KV3E, this moment, the absorption forward position of A tower continued to push ahead, and after A, E two pressure towers are in a basic balance, closed KV3E.
D, two all falls
One all end is fallen and after, A Ta Neishang has higher pressure, continues to stay open the KV-3A valve this moment and open KV2 to make the gas in the A tower put into equalizer tank V0301, makes the two pressure balance, closes KV3A, KV2 valve then simultaneously.
E, three all falls
Open sequencing valve KV3A, KV3F, allow the A tower be communicated with, after two pressure tower balances, close KV3A, KV3F with adsorption tower F.
F, four all falls
Continue to stay open KV4A, and open sequencing valve KV4G, allow the A tower be communicated with, after two pressure tower balances, close KV4G with adsorption tower G.
G, recovery again
Continue to stay open KV4A and open valve KV3, residual gas in the adsorption tower is entered V0201 along the absorption direction reclaim along the venting jar again, the operator can control pressure and the CO that reclaims again by the mode of regulating again recovery time
2Concentration.
H, find time
Utilize KV6 to be communicated with, adsorption tower is implemented to find time,, find time to finish, close KV6A with further desorb with vavuum pump.
I, four all rises
Open KV4A, the KV4C valve makes the A tower be communicated with the C tower, until A, C two pressure tower balances, closes KV4A, KV4C.
J, three all rises
Open sequencing valve KV3A, KV3D, make that gas charges in the A tower in the D tower, after the two pressure balance, close KV3A, KV3D.
K, two all rises
Continue to open sequencing valve KV3A, and open sequencing valve KV2 and make that gas charges into the A tower among the equalizer tank V0301, after the two pressure balance, close KV2.
L, one all rises
Continue to open sequencing valve KV3A, and open sequencing valve KV3E, accept to boost, after the two pressure balance, close KV3A, KV3E from the gas that the E tower comes.
M, fill and boost eventually
Open sequencing valve KV5A, use the gas of recovery again that the A tower is boosted, boost to the product atmospheric pressure, close KV5A until the A tower from compressor.The adsorbent bed of this moment has been the work of getting ready that next time circulates.
Through after the complete cycle of this adsorbent equipment, the CO in the product gas
2Concentration is used to produce liquefied ammonia and methyl alcohol less than 0.5%.
Draw after the detection through driving continuously: available gas H
2, N
2, almost free of losses of CO, total hydrazine yield raises.
Embodiment 2
The pre-recovery with reclaiming again of a kind of pressure-swing absorption apparatus band removes CO in the conversion gas
2Method, it is to be the conversion gas of raw material with common coal, by optimized proportion (please specifically writing exactly) activated alumina, activated carbon, Kiselgel A is housed in the adsorption tower, its gas composition is as follows:
Component H
2N
2CO CO
2CH
4Other total sulfur H
2O (vapour)
Concentration (V)～52%～17%～1%～28%～1%～1＜150mg/m
3Saturated
Unstripped gas temperature≤40 ℃ wherein, pressure: 0.60MPa
As shown in Figure 2, it is characterized in that: each adsorption tower following processing step of experience successively in circulation once: absorption, pre-reclaim, one all fall, two all fall, three all fall, four all fall, reclaim again, find time, four all rise, three all rise, two all rise, one all rise and whole filling boosted.
Described adsorbent equipment is made up of eight adsorption towers, a steam-water separator, two downflow releasing tanks and a recycling can; Activated alumina, activated carbon, three kinds of adsorbents of Kiselgel A are equipped with in layering from bottom to up in the described adsorption tower.
Be that example describes (referring to Fig. 2, Fig. 4) with the A tower below:
A, absorption
Conversion gas from moisture trap, absorption operating pressure under after KV-1A flows through adsorption tower from bottom to up from A tower lower end, saturation water, sulphur, carbon dioxide are adsorbed agent and optionally adsorb in the air-flow, the Purge gas that removes behind the carbon dioxide is discharged from the adsorption tower top through KV-2A, as product gas input workshop section down.When the absorption forward position of impurity component (promptly refer in the product allowed maximum impurity concentration) when arriving the adsorbent bed certain altitude, promptly stops the input of unstripped gas and the output of product gas.
B, the pre-recovery
After adsorption process stops, KV-1A and KV-2A valve closing, still keep the high pressure that equates with adsorptive pressure in the adsorption tower, make the gas in the adsorption tower carry out isostasy by opening valve KV-3A, KV6 to the carbonization secondary tower, this moment, the absorption forward position of A tower continued to push ahead, and after pressure is in a basic balance, closed KV5, at this moment, the absorption forward position of the A tower no show port of export still.The effect of this process is the portioned product gas that reclaims A tower dead space, and the product gas of its gas composition purity and output is basic identical.
C, one all falls
After removal process stops, also keeping higher pressure in the adsorption tower, adsorption tower A, E are communicated carry out isostasy by opening valve KV-3A, KV3E, this moment, the absorption forward position of A tower continued to push ahead, and after A, E two pressure towers are in a basic balance, closed KV3E.
D, two all falls
One all end is fallen and after, A Ta Neishang has higher pressure, continue to stay open the KV-3A valve and open KV2 this moment, makes the gas in the A tower put into equalizer tank V0301, makes the two pressure balance, closes KV3A, KV2 valve then simultaneously.
E, three all falls
Open sequencing valve KV3A, KV3F, allow the A tower be communicated with, after two pressure tower balances, close KV3A, KV3F with adsorption tower F.
F, four all falls
Continue to stay open KV4A, and open sequencing valve KV3, make the gas in the A tower put into downflow releasing tank V0201, after two pressure tower balances, close KV3.
G, recovery again
Continue to stay open KV4A and open valve KV4, residual gas in the adsorption tower is entered V0401 along the absorption direction reclaim along the venting jar again, the operator can control pressure and the CO that reclaims again by the mode of regulating again recovery time
2Concentration.
H, find time
Utilize KV6 to be communicated with, adsorption tower is implemented to find time,, find time to finish, close KV6A with further desorb with vavuum pump.
I, four all rises
Open KV4A, the KV3 valve makes that gas charges into A among the downflow releasing tank V0201, until both pressure balances, closes KV4A, KV3.
J, three all rises
Open sequencing valve KV3A, KV3D, make that gas charges in the A tower in the D tower, after the two pressure balance, close KV3A, KV3D.
K, two all rises
Continue to open sequencing valve KV3A, and open sequencing valve KV2, make that gas charges into the A tower among the equalizer tank V0301, after the two pressure balance, close KV2.
L, one all rises
Continue to open sequencing valve KV3A, and open sequencing valve KV3E, accept to boost, after the two pressure balance, close KV3A, KV3E from the gas that the E tower comes.
M, fill and boost eventually
Open sequencing valve KV5A, use the gas of recovery again that the A tower is boosted, boost to the product atmospheric pressure, close KV5A until the A tower from compressor.The adsorbent bed of this moment has been the work of getting ready that next time circulates.
Through after the complete cycle of this adsorbent equipment, the CO in the product gas
2Concentration is used to produce liquefied ammonia less than 0.2%.
Draw after the detection through driving continuously: available gas H
2, N
2Almost free of losses, total hydrazine yield does not fall.
Claims (10)
1, a kind of pressure-swing absorption apparatus band reclaims in advance and reclaims and removes CO in the conversion gas
2Method, it is characterized in that: each adsorption tower is once comprising following processing step in the circulation successively:
A, absorption A
Conversion gas from moisture trap, in the absorption operating pressure from bottom to top during the ground warp adsorption tower, saturation water, sulphur, carbon dioxide are adsorbed agent and optionally adsorb in the air-flow, and the Purge gas that removes behind the carbon dioxide is discharged from the adsorption tower top, as product gas input workshop section down.When impurity arrives the adsorbent certain altitude, promptly stop the input of raw material and the output of product gas.Adsorb this moment and still leave one section between the forward position and the port of export and " also do not adsorb saturated CO
2Adsorbent " i.e. the reservation section of contaminated adsorbent not;
B, reclaim YR in advance
Adsorption process is opened program-controlled valve after finishing, and the gas in the adsorption tower is reclaimed in advance to the gas that the carbonization secondary tower carries out isostasy, and this moment, the absorption forward position of adsorption tower continued to push ahead, and after pressure was in a basic balance, pre-removal process promptly finished;
C, drop pressure ED
After pre-removal process finishes, still keep higher pressure in the adsorption tower, between adsorption tower and adsorption tower, or carry out isostasy between adsorption tower and the downflow releasing tank, make the pressure of adsorption tower drop to minimum as far as possible;
D, reclaim ZR again
After the drop pressure process finishes, also have certain pressure in the adsorption tower, the residual gas in the adsorption tower put into a downflow releasing tank, with hydrogen gas compressor downflow releasing tank is forced into adsorptive pressure again after, enter recycling can and store;
E, VC finds time
After removal process finished again, the pressure in the adsorption tower was essentially negative pressure, vacuumizes further step-down by vavuum pump, made adsorbent obtain resolving regeneration;
F, boost pressure ER
After evacuation process finished, adsorption tower was accepted boosting of other adsorption tower or downflow releasing tank drop pressure gas from the port of export, and the pressure of adsorption tower is progressively raise;
G, fill the FR that boosts eventually
After the boost pressure process finishes, calm the anger by adding in the recovery tower and from the adsorption tower top adsorption tower finally to be boosted, until the pressure that reaches product gas from adsorption tower bottom and product gas.
2, method according to claim 1 is characterized in that: pressure-swing absorption apparatus has increased pre-removal process between absorption and drop pressure step.
3, method according to claim 1 is characterized in that: pressure-swing absorption apparatus vacuumizes in drop pressure and parsing has increased removal process again between the step.
4, method according to claim 1 is characterized in that: described adsorption tower is 4～16.
5, according to claim 1 or 4 described methods, it is characterized in that: described adsorptive pressure is 0.1～3.0MPa.
6, method according to claim 1 is characterized in that: the pressure of described downflow releasing tank is controlled at-0.02～0.03MPa scope in.
7, according to claim 1 or 4 described methods, it is characterized in that: the number of times of all pressing continuously between described adsorption tower and the adsorption tower is 1～6 time; The number of times of all pressing indirectly between described adsorption tower and the downflow releasing tank is 1～5 time.
8, method according to claim 1 is characterized in that: CO in the described downflow releasing tank
2Concentration of volume percent be 0～8%.
9, according to claim 1 or 4 described methods, it is characterized in that: the number of times of described boost pressure is 1～6 time that equates fully with the number of times of drop pressure.
10, according to claim 1 or 4 described methods, it is characterized in that: described vavuum pump vacuumizes, and is meant to adopt two pipelines respectively adsorption tower to be vacuumized; Perhaps adopt two pipelines simultaneously adsorption tower to be vacuumized by opening program-controlled valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2004100410002A CN1631488A (en) | 2004-11-09 | 2004-11-09 | Method for pre-reclaiming and anew-reclaiming mechanism for removing CO#[2] from converting gas of pressure swing adsorption device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2004100410002A CN1631488A (en) | 2004-11-09 | 2004-11-09 | Method for pre-reclaiming and anew-reclaiming mechanism for removing CO#[2] from converting gas of pressure swing adsorption device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1631488A true CN1631488A (en) | 2005-06-29 |
Family
ID=34845911
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2004100410002A Pending CN1631488A (en) | 2004-11-09 | 2004-11-09 | Method for pre-reclaiming and anew-reclaiming mechanism for removing CO#[2] from converting gas of pressure swing adsorption device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1631488A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100364644C (en) * | 2005-12-27 | 2008-01-30 | 温州瑞气空分设备有限公司 | Process for improving gas reclaiming rate of pressure swing absorption separation process |
| CN102160955A (en) * | 2011-03-04 | 2011-08-24 | 四川同盛科技有限责任公司 | One-stage pressure swing adsorption process in ammonia-urea synthesizing production |
| CN110252083A (en) * | 2019-06-27 | 2019-09-20 | 天津大沽化工股份有限公司 | Synthesis tail gas pressure swing absorption process in a kind of PVC production |
-
2004
- 2004-11-09 CN CNA2004100410002A patent/CN1631488A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100364644C (en) * | 2005-12-27 | 2008-01-30 | 温州瑞气空分设备有限公司 | Process for improving gas reclaiming rate of pressure swing absorption separation process |
| CN102160955A (en) * | 2011-03-04 | 2011-08-24 | 四川同盛科技有限责任公司 | One-stage pressure swing adsorption process in ammonia-urea synthesizing production |
| CN110252083A (en) * | 2019-06-27 | 2019-09-20 | 天津大沽化工股份有限公司 | Synthesis tail gas pressure swing absorption process in a kind of PVC production |
| CN110252083B (en) * | 2019-06-27 | 2022-05-20 | 天津大沽化工股份有限公司 | Pressure swing adsorption method for synthetic tail gas in PVC production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1165363C (en) | Improved vacuum pressure swing absorption process | |
| CN1100587C (en) | Single bed pressure swing adsorption process for recovery of oxygen from air | |
| CN1035993A (en) | Reclaim the method for oxygen rich gas | |
| CN1062781C (en) | Improved vacuum pressure swing adsorption process | |
| CN1229167C (en) | Vacuum rotary adsorptive process utilizing controlled waste gas extraction | |
| CN101108295B (en) | Pressure swing adsorption with displacement and recovery steps for removing CO from shift gas2Method (2) | |
| CN1195571C (en) | PSA process and system using simultaneous top and bottom evacuation of adsorbent bed | |
| CN100336577C (en) | Off-gas feed method and object gas purification system | |
| CN1861246A (en) | Method for producing oxygen by using air as raw material | |
| CN1599636A (en) | Psa process for co-producing nitrogen and oxygen | |
| CN1038017C (en) | Method for recovering ethylene from vent gas from ethylene oxide plant vent gas | |
| CN1861245A (en) | Pressure-variation absorption method for separating and recovering adsorbed phase products from mixed gas | |
| CN1631488A (en) | Method for pre-reclaiming and anew-reclaiming mechanism for removing CO#[2] from converting gas of pressure swing adsorption device | |
| CN1195572A (en) | Pressure swing adsorption gas separation method for simultaneously purifying easy-adsorption phase and difficult-adsorption phase from mixed gas | |
| CN1850319A (en) | Pressure-changing adsorption method for recovering low-partial-pressure gas | |
| CN1279006C (en) | Method for purification and recovery of methane from refuse landfill gas | |
| CN1405129A (en) | Method for subtracting hydrocarbor impurities of above C3+ from mixed acetylene gas and recovering acetylene | |
| CN1126585C (en) | Variable-pressure adsorption separating method for simultaneously purifying easy-to-adsorb phase and difficult-to-adsorb phase | |
| CN1117603C (en) | Pressure variable adsorptive method for separating hydrogen nitrogen and pure carbon dioxide from exchange air | |
| CN1073876C (en) | Pressure swing adsorption process for separating carbon monooxide from carbon monooxide contg. mixed gas | |
| CN1019475B (en) | Pressure swing adsorption process for extracting carbon dioxide from mixed gas | |
| CN1075394C (en) | Variable-pressure adsorption process for removing CO2 from transformation gas | |
| CN1302983C (en) | Pressure swing adsorption continuous oxygen generation method | |
| CN1671462A (en) | Method of separating target gas | |
| CN1680002A (en) | Pressure varying adsorption of recovering effective components from relaxed methanol gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |