CN104740972A - Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas - Google Patents
Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas Download PDFInfo
- Publication number
- CN104740972A CN104740972A CN201510101180.7A CN201510101180A CN104740972A CN 104740972 A CN104740972 A CN 104740972A CN 201510101180 A CN201510101180 A CN 201510101180A CN 104740972 A CN104740972 A CN 104740972A
- Authority
- CN
- China
- Prior art keywords
- gas
- adsorption
- adsorption tower
- pressure
- pressure swing
- 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
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas. According to the method, all or one part of the displacement waste gas flowing out from an adsorption tower is displaced by a pressure swing adsorption gas separation device, and is compressed and pressurized; and the waste gas returns back to be mixed with fresh raw gas and the mixed gas is used as raw gas of the pressure swing adsorption gas separation device. The method is applicable to a product mainly composed of adsorption phase components and the pressure swing adsorption gas separation device with a displacement operation step. According to the method which takes the displacement waste gas and the directly-discharged gas, which are pressurized and returned back to be mixed with the fresh raw gas, as the raw gas of the pressure swing adsorption gas separation device, other separation devices for separating and recycling the displacement waste gas and the directly-discharged gas do not need to be used, so that the recycling of the displacement waste gas and the directly-discharged gas is realized on one set of the pressure swing adsorption gas separation device. Compared with the prior art, the pressure swing adsorption gas separation method has a simple flow, low investment, low energy consumption and convenience for operation; and the waste gas can be recycled and the directly-discharged gas also can be recycled, and the high recycling rate of the adsorption phase product components in the fresh raw gas can be effectively guaranteed.
Description
Technical field
The present invention relates to a kind of pressure-changeable gas-adsorption separation method reclaiming displacement waste gas and suitable venting, particularly relate to the pressure-changeable gas-adsorption separation method mainly consisting of adsorbent phase component of product, belong to gas separaion field of purification.
Background technology
Pressure-variable adsorption is that a kind of discrepant characteristic of the adsorption capacity of solid absorbent to gas with various component that utilizes is to realize the method for gas separaion.The material be adsorbed on solid adsorbent surfaces is Adsorption Phase.Pressure swing adsorption gas separation device adsorbs under a certain pressure, by step-down, vacuumize, method that flushing etc. reduces adsorbent phase component partial pressure, reach the object of Adsorption Phase desorb, adsorbent reactivation.In adsorption operations step, unstripped gas enters the adsorption tower being filled with solid absorbent under a certain pressure, be adsorbed on adsorbent surface based on the portion gas of easy absorbed component, the gas that do not adsorb of major part flows out adsorption tower, realizes being separated of easy absorbed component and not easily absorbed component.
The product of pressure swing adsorption gas separation device, can using mainly consist of not easily absorbed component, adsorption operations step from adsorption tower effluent air as product, also can using mainly consist of discharge from adsorption tower in the adsorbent phase component of easily absorption, desorption process vacuumize gas and inverse put gas as product, or both as product.
The pressure swing adsorption gas separation device mainly consisting of adsorbent phase component of product is widely used.Representative application has: separating and concentrating carbon monoxide from the coal gasification gas after carbon dioxide removal; Separating and concentrating carbon monoxide CO gas is rich in from calcium carbide tail gas, steel mill's converter gas, yellow phosphoric tail gas etc.; Separating and concentrating carbon dioxide from conversion gas; Separating and concentrating carbon dioxide from lime-kiln gas; Separating and concentrating methane methane gas is rich in from coke-stove gas, coal bed gas etc.; Separating and concentrating C from oil plant catalytic cracked dry gas
2and C
2above hydrocarbon component is main gaseous mixture; Separating and concentrating hydrocarbon component from oil plant various mist.
The pressure swing adsorption gas separation device mainly consisting of adsorbent phase component of product, is provided with replacement operator step usually.Replacement operator is exactly that portioned product gas is sent into adsorption tower from the unstripped gas arrival end of absorption tower adsorbs operating procedure, gas in displacement sorption agent bed, improve the partial pressure of adsorbent bed middle Adsorption Phase product component, reduce adsorbent bed in the partial pressure of not easily absorbed component.By replacement operator, make the further desorb of not easily absorbed component and discharge adsorption tower, reaching the object improving adsorbent bed middle Adsorption Phase product component concentration.Replacement operator step is called displacement waste gas from adsorption tower effluent air.Because in displacement waste gas, Adsorption Phase product component concentration is higher, therefore the valuable gases in displacement waste gas how is reclaimed, improve the rate of recovery of Adsorption Phase product component in fresh feed gas, reduce the consumption of fresh feed gas, directly affect the economic benefit mainly consisting of the pressure swing adsorption gas separation device of adsorbent phase component of product.
The pressure swing adsorption gas separation device mainly consisting of adsorbent phase component of product is also provided with usually along putting operating procedure.Be exactly gas flow along absorption tower adsorbs operating procedure along putting operation, discharge the gas adsorption tower from the suitable bleeder holes of the port of export of absorption tower adsorbs operating procedure, adsorption column pressure is dropped to the operating pressure of next operating procedure as replacement operator step, inverse put operating procedure.By along putting operation, reduce adsorbent bed stressor layer, not easily absorbed component desorb, adsorbent bed middle Adsorption Phase product component concentration improves.Be called along venting from the gas that adsorption tower is discharged along putting operating procedure.Also higher along Adsorption Phase product component concentration in venting, reclaim the rate of recovery that effectively can improve Adsorption Phase product component in fresh feed gas along venting.
Patent ZL200510118241.7, patent ZL200510129369.3, patent ZL201210394237.3 and patent ZL201410271598.8 disclose the recoverying and utilizing method relating to displacement waste gas, but the recovery method do not related to along venting, and the recoverying and utilizing method of these displacement waste gas is all realized by 2 covers or the above combination comprising the adsorbent equipment of pressure swing adsorption gas separation device of 2 covers, not only invest high, flow process is complicated, practical range is also by multiple restriction.
Summary of the invention
Have problems for above-mentioned prior art, the object of the invention is to, do not use other in order to separation displacement waste gas with along the pressure-swing absorption apparatus of venting or the separator of other types, on a set of pressure swing adsorption gas separation device, realize the recovery of displacement waste gas, and when being provided with along realizing when putting operating procedure replacing waste gas and the recovery along venting simultaneously.
The object of the invention is to be achieved through the following technical solutions: a kind ofly reclaim displacement waste gas and the pressure-changeable gas-adsorption separation method along venting, comprise all or part of of displacement waste gas pressure swing adsorption gas separation device replacement operator step flowed out from adsorption tower, after compressed boosting, return the step mixing the unstripped gas as pressure swing adsorption gas separation device with fresh feed gas; And optionally by along put operating procedure from adsorption tower discharges all or part of along what exit, return the step mixing the unstripped gas as pressure swing adsorption gas separation device with fresh feed gas after compressed boosting.
In the present invention, the operating procedure of every platform adsorption tower within a cycling cycle, must comprise absorption, replaces, vacuumize, and can also include but not limited to equal pressure drop, along putting, inverse put, all voltage rises, finally boost.Such as, the equal pressure drop operating procedure of one or many is set after adsorption operations step; Arrange along putting operating procedure after adsorption operations step, before vacuum pumping step; Inverse put operating procedure is set before vacuum pumping step; The equal voltage rise operating procedure of one or many is set after vacuum pumping step, before adsorption operations step; Final boost operations step is set before adsorption operations step.Therefore, the operating procedure of every platform adsorption tower within a cycling cycle can comprise absorption, all pressure drop, along putting, replace, inverse put, vacuumize, all voltage rises, finally to boost.The sequencing of each operating procedure can set as required.
In the present invention, when not arranging along when putting operation, only reclaim displacement waste gas, the displacement waste gas that replacement operator step flows out from adsorption tower all or part of, after compressed boosting, return the unstripped gas mixed with fresh feed gas as this cover pressure swing adsorption gas separation device.When being provided with along when putting operation, can reclaim along venting simultaneously, along put operating procedure from adsorption tower discharges all or part of along what exit, also can return the unstripped gas mixed with fresh feed gas as this cover pressure swing adsorption gas separation device after compressed boosting.
Pressure swing adsorption gas separation device arranges the adsorption tower that more than 4 or 4 are filled with solid absorbent, and multiple stage adsorption tower, according to the operating procedure of setting and time sequencing, replaces switching, cycling.
Each operating procedure that above-mentioned pressure swing adsorption gas separation device adopts is described as follows:
Absorption: the unstripped gas containing product component enters adsorption tower from adsorption tower unstripped gas entrance, be adsorbed on adsorbent surface based on the portion gas of easy absorbed component, the gas that major part is not adsorbed flows out from adsorption tower, realizes being separated of easy absorbed component and not easily absorbed component.For the pressure swing adsorption gas separation device mainly consisting of adsorbent phase component of product, adsorption operations step is called absorption waste gas from adsorption tower effluent air.Adsorption operations step is labeled as A.
Equal pressure drop: all pressure is exactly isostasy.Equal pressure drop is by equal pressure drop low-pressure, and equal voltage rise is by equal voltage rise high pressure.Equal pressure drop operating procedure is the adsorption tower after adsorption operations step completes, to needing the adsorption tower pressurising implementing equal voltage rise operating procedure, the adsorption column pressure implementing equal pressure drop operating procedure reduces, the adsorption column pressure implementing equal voltage rise operating procedure raises, until the pressure of two adsorption towers is close or equal.All pressure directly can have been connected by two adsorption towers, also can complete by all pressing surge tank.The object of all pressing reclaims the useful constituent implemented equal pressure drop operating procedure and discharge from adsorption tower, and the adsorption tower of the equal voltage rise operating procedure of enforcement is boosted.Equal pressure drop operating procedure can arrange one or many.Equal pressure drop operating procedure is labeled as EnD, and all pressure drop was labeled as E1D, the equal pressure drop of second time is labeled as E2D first time, and the rest may be inferred.
Along putting: be exactly gas flow along absorption tower adsorbs operating procedure along putting operation, discharge the gas adsorption tower from the suitable bleeder holes of the port of export of absorption tower adsorbs operating procedure, adsorption column pressure is dropped to the operating pressure of next operating procedure as replacement operator step, inverse put operating procedure.By along putting operation, reduce adsorbent bed stressor layer, not easily absorbed component desorb, adsorbent bed middle Adsorption Phase product component concentration improves.Be called along venting from the gas that adsorption tower is discharged along putting operating procedure.All or part of along venting of the present invention, can return the unstripped gas mixed with fresh feed gas as this cover pressure swing adsorption gas separation device.PP is labeled as along putting operating procedure.
Displacement: vacuumize the gas product mainly consisting of adsorbent phase component obtained with inverse put operating procedure, enter adsorption tower from the displacement gas entrance of adsorption tower unstripped gas arrival end, flow out from the displacement waste gas outlet of the port of export of absorption tower adsorbs operating procedure.The object of replacement operator is: the gas in the gas product displacement sorption agent bed utilizing Adsorption Phase product component content higher, improve the partial pressure of adsorbent bed middle Adsorption Phase product component, reduce adsorbent bed in the dividing potential drop of not easily absorbed component, make not easily absorbed component desorb, Adsorption Phase product component adsorbs, and improves the concentration of adsorbent bed middle Adsorption Phase product component.Replacement operator step is called displacement waste gas from adsorption tower effluent air.Displacement waste gas of the present invention all or part of, returns the unstripped gas mixed with fresh feed gas as this cover pressure swing adsorption gas separation device after compressed boosting.Replacement operator step is labeled as RP.
Inverse put: complete equal pressure drop, along putting, the adsorption tower of replacement operator step, along the direction that absorption tower adsorbs operating procedure airflow direction is contrary, gas from the inverse bleeder holes discharge of adsorption tower unstripped gas arrival end is adsorbent bed, reduce the pressure of adsorption tower, make the component desorb be adsorbed on adsorbent surface.Inverse put gas of the present invention can make product.Inverse put operating procedure is labeled as D.
Vacuumize: with vavuum pump, adsorption tower is vacuumized, reduce adsorbent bed pressure further, make the further desorb of component be adsorbed on adsorbent surface.Of the present invention using vacuumizing the gas of acquisition as product.Vacuum pumping step is generally carried out after inverse put operating procedure.Vacuum pumping step is labeled as V.
Equal voltage rise: the adsorption tower after vacuum pumping step completes, by being directly connected with the adsorption tower being in equal pressure drop operating procedure, or be connected with all pressing surge tank, realize boosting, until the pressure of two adsorption towers is close or equal, and reclaim the useful constituent the gas of discharging from the adsorption tower implementing equal pressure drop operating procedure.Equal voltage rise operating procedure is corresponding with equal pressure drop operating procedure, can arrange one or many.Equal voltage rise operating procedure is labeled as EnR, and the equal voltage rise operating procedure corresponding with first time equal pressure drop is labeled as E1R, is labeled as E2R with the second time equal voltage rise operating procedure that all pressure drop is corresponding, and the rest may be inferred.
Final boosting: the absorption waste gas utilizing absorption tower adsorbs operating procedure to flow out from adsorption tower or unstripped gas boost to adsorption tower, make it to reach adsorption operations pressure.Final boost operations step is labeled as FR.
Gas product of the present invention is by inverse put and vacuumize two operating procedures acquisitions, and as do not arranged inverse put operating procedure, then gas product is obtained by vacuum pumping step.
The main composition of product of the present invention is one or more Adsorption Phase components, and described Adsorption Phase component includes but not limited to carbon monoxide, carbon dioxide and the hydro carbons containing 1 to 5 carbon atom.
During the invention process adsorption operations step, the operating pressure of adsorption tower is absolute pressure 0.30MPa-6.1MPa; The operating pressure implementing adsorption tower during replacement operator step is less than or equal to the operating pressure of adsorption tower when implementing adsorption operations step, and is more than or equal to local atmospheric pressure.The minimum operating pressure implementing adsorption tower during vacuum pumping step is absolute pressure 0.0005MPa-0.06MPa.
The solid absorbent of filling in the adsorption tower of pressure swing adsorption gas separation device of the present invention, includes but not limited to active carbon, aluminium oxide, silica gel, molecular sieve, polymeric adsorbent, copper-carrying adsorbent.A kind of solid absorbent can be only loaded in adsorption tower, also more than one solid absorbents can be loaded.
The pressure swing adsorption gas separation device mainly consisting of adsorbent phase component of product, product design is higher, and the displacement tolerance of needs is larger, and displacement exhausted air quantity also can be larger, and in displacement waste gas, the concentration of Adsorption Phase product component is also higher.Displacement waste gas of the present invention returns and mixes as unstripped gas with fresh feed gas, and the concentration ratio fresh feed gas of the Adsorption Phase product component in unstripped gas is high, and displacement exhausted air quantity is larger, and in mixed unstripped gas, the concentration of Adsorption Phase product component also can be higher.Therefore, unit volume adsorbent can increase to the disposal ability of unstripped gas, and the quantity of required adsorbent can not the proportional increase with the increase of raw gas flow.
The present invention is for the unstripped gas composition determined and product design requirement, and the rate of recovery of the Adsorption Phase product component in the fresh feed gas of device is negative correlativing relation with the concentration of Adsorption Phase product component in absorption waste gas.As replaced waste gas, returning as unstripped gas along whole recovery of venting, inverse put gas and vacuumize gas as gas product, the Adsorption Phase product component then not entering product only has the outlet of absorption waste gas one, for the unstripped gas composition determined and product design requirement, the rate of recovery of the Adsorption Phase product component in the fresh feed gas of device, has with the concentration of Adsorption Phase product component in absorption waste gas the negative correlativing relation determined.If displacement gas flow is enough large, the concentration of the attached phase product component in absorption waste gas can be made enough low, just can obtain the rate of recovery of the Adsorption Phase product component in sufficiently high fresh feed gas.When reality is implemented, as required, by setting suitable displacement gas flow, reducing the concentration of the Adsorption Phase product component in absorption waste gas, the rate of recovery of Adsorption Phase product component in higher fresh feed gas can be obtained.
For PSA-CO and pressure-changed adsorption concentrating carbon monoxide device, replace waste gas and mix as pressure swing adsorption gas separation device unstripped gas with fresh feed gas along returning after all compressed boosting of venting and be recycled, inverse put gas and vacuumize gas as gas product, do not enter in device product CO only have absorption waste gas one outlet, the rate of recovery of CO just depends on the CO content adsorbed in waste gas.As the CO content in fresh feed gas is 35%, requires that in product, CO content is 98.5%, then, when the CO content in absorption waste gas is 7.5%, the CO rate of recovery is 85.05%; When the CO content in absorption waste gas is 5.0%, the CO rate of recovery is 90.30%; If the CO content controlled in absorption waste gas is 2.5%, and displacement gas flow is still at economic limit, then the obtainable CO rate of recovery is 95.28%.
Utilizing the recovery displacement waste gas technological process of uniqueness of the present invention to arrange, due to can not outside displacement waste gas and along exitting, when device initial start-up, significantly reduction can obtain supplies consumption in cycle of operation of qualified products and running and energy ezpenditure.
Beneficial effect of the present invention is: do not need to use other in order to separation and recovery displacement waste gas and the separator along venting, on a set of pressure swing adsorption gas separation device, realize displacement waste gas and the recovery along venting.Compared with prior art, flow process is simple and direct, small investment, energy consumption are low, easy to operate, not only reclaims displacement waste gas, also recyclable along venting, and effectively can ensure the rate of recovery of Adsorption Phase product component in higher fresh feed gas.
Accompanying drawing explanation
Fig. 1 is technical scheme FB(flow block) of the present invention.
Fig. 2 is the process flow diagram of the embodiment of the present invention 1, wherein A/B/C/D is 4 adsorption towers, 1 is inverse put tank, and 2 is vacuum tank, and 3 is Product mix tank, 4 is displacement off-gas buffer tank, 5 is displacement gas surge tank, and 6 is vavuum pump, and 7 is displacement gas compressor, 8 is gas product compressor, and 9 for returning air compressor.
Detailed description of the invention
Embodiment 1
The present embodiment is the pressure-variable adsorption separator of separation and recovery carbon monoxide from water-gas, fresh feed throughput 500Nm
3/ h, adsorptive pressure is gauge pressure 0.25MPa, unstripped gas temperature 40 DEG C, and fresh feed gas composition is as shown in table 1:
Table 1 fresh feed gas forms
The present embodiment pressure-swing absorption apparatus adsorption tower volume is 5m
3, the adsorbent wherein loaded is respectively molecular sieve, active carbon, activated alumina from top to bottom, and its loading height ratio is 4:1:1.Device by 4 adsorption towers, 1 inverse put tank, 1 vacuum tank, 3 vavuum pumps, 1 displacement off-gas buffer tank, 1 Product mix tank, 1 displacement gas surge tank, 1 displacement gas compressor, 1 gas product compressor, 1 return air compressor and corresponding pipeline and sequencing valve and be formed by connecting.Every platform adsorption tower experiences 7 operating procedures such as absorption A, all pressure drop ED, displacement RP, inverse put D, the V that finds time, all voltage rise ER, finally boosting FR successively within a cycling cycle, and its program runs sequential, each operating procedure gauge pressure value in table 2:
Table 2 pressure-variable adsorption work schedule table
When pressure swing adsorption system runs, controlled the switch of each sequencing valve by certain procedures by computer.For adsorption tower A, describe each technological operation step:
Absorption A: open sequencing valve KV1A and KV2A, unstripped gas enters adsorption tower A, and the easy absorbed component based on CO is adsorbed on adsorbent surface, the gas that major part is not adsorbed is flowed out from adsorption tower A top by sequencing valve KV2A as absorption waste gas.At the end of the adsorption operations step time, shutoff valve KV1A and KV2A, stops absorption, and now unstripped gas enters another adsorption tower of completing final boost operations step and adsorption tower B adsorbs.
Equal pressure drop ED: open sequencing valve KV5A and KV5C, the adsorption tower A completing adsorption operations step and the adsorption tower C completing vacuum pumping step carry out isostasy, after two adsorption column pressures are in a basic balance, close KV5A and KV5C, complete the equal pressure drop operating procedure of adsorption tower A.
Displacement RP: open sequencing valve KV3A and KV4A, adsorption tower A is entered through product blending tank, displacement gas compressor bank, displacement gas surge tank by inverse put and the gas product vacuumizing acquisition, the adsorption tower A completing equal pressure drop operating procedure is replaced, to improve the concentration of adsorbent bed adsorbent phase component and CO.Displacement waste gas is flowed out from adsorption tower A top by valve KV4A, enters displacement off-gas buffer tank, then is forced into 0.3MPa and mixes with unstripped gas the system of reentering by returning air compressor.At the end of the replacement operator step time, shutoff valve KV3A and KV4A, stops displacement.
Inverse put D: open sequencing valve KV6A, KV7 and KV8, complete the adsorption tower A of replacement operator step by bottom Exhaust Gas, pressure reduces.Inverse put gas enters inverse put tank through valve KV6A and KV7, then enters gas product blending tank through manual modulation valve HV1, vacuum tank 2, KV8, vavuum pump group.When after adsorption tower A Pressure Drop to normal pressure, close KV7 and KV8, inverse put operating procedure completes.
Vacuumize V: after completing inverse put operating procedure, continue to open KV6A, open sequencing valve KV9 simultaneously, vacuumized by vavuum pump group to adsorption tower A, the gas that vavuum pump group is discharged mixes at gas product blending tank with inverse put gas.Vacuumize the pressure reducing adsorption tower A further, make the abundant desorb of Adsorption Phase product component CO be adsorbed on adsorbent surface, obtain product, complete adsorbent reactivation.A gas part in gas product blending tank exports after the pressurization of product air compressor as gas product, and a part is as displacement gas retrieval system after displacement gas compressor pressurizes.After vacuum pumping step completes, close KV6A and KV9.
Equal voltage rise ER: after completing vacuum pumping step, opens sequencing valve KV5A and KV5C, and adsorption tower A carries out isostasy with the adsorption tower C completing adsorption operations step, and when two pressure towers are substantially equal, shutoff valve KV5C, completes the equal voltage rise of adsorption tower A.
Final boosting FR: after completing equal voltage rise operating procedure, continue open valve KV5A, manually control valve HV2, utilize absorption waste gas to boost to the adsorption tower A completing equal voltage rise operating procedure, make it to reach adsorptive pressure, prepare the adsorption operations step entering next cycle.
So far, all operations step of adsorption tower A within a cycling cycle is all finished, and and then enters next cycling cycle.Other operating procedures performed by 3 adsorption towers are identical with adsorption tower A, just mutually stagger by the time sequential routine set in time.
The pressure of every platform adsorption tower is cyclically-varying with the replacement of operating procedure.As adjusted adsorptive pressure according to practical operation situation, then other operating procedure pressure also can correspondingly change.
The product composition of the present embodiment is as shown in table 3:
Table 3 gas product forms
CO content in the present embodiment absorption waste gas is 7.55%, and in fresh feed gas, the rate of recovery of CO reaches 85%.And under same apparatus level, identical operating condition, if do not reclaimed displacement waste gas, in fresh feed gas, the rate of recovery of CO is only 66%.
Embodiment 2
The present embodiment is the coke-stove gas concentrate methane device after conversion, carbon dioxide removal, coke gas flow 42000Nm
3/ h, adsorptive pressure is gauge pressure 0.95MPa, unstripped gas temperature 30 DEG C, and fresh feed gas composition is as shown in table 4:
Table 4 fresh feed gas forms
In the present embodiment, the volume of adsorption tower is 90m
3rice, the adsorbent wherein loaded is mainly activated alumina and active carbon, device by 8 adsorption towers, 2 inverse put tanks, 2 Product mix tanks, 1 displacement off-gas buffer tank, 1 pans, 1 displacement gas surge tank, vavuum pump group, gas product compressor, displacement gas compressor, return air compressor and corresponding pipeline and sequencing valve and be formed by connecting.Every platform adsorption tower within a cycling cycle successively experience absorption A, all fall E1D, two and all fall that E3D all falls in E2D, three, along putting PP, displacement RP, inverse put D, the V that finds time, three all rise E3R, two and all rise E2R, and all rise 12 operating procedures such as E1R, final boosting FR, its program runs sequential in table 5:
Table 5 pressure-variable adsorption work schedule table
In the present embodiment, in adsorption tower A and embodiment 1, the difference of the operating procedure of adsorption tower A is, equal pressure drop in the present embodiment, all voltage rise are respectively 3 times, wherein one all fall E1D by the adsorption tower A completing adsorption operations step with complete the two adsorption tower D all rising E2R and all press, two all fall E2D by completing an adsorption tower A all fallen and pans are all pressed, and three all fall by completing the two adsorption tower A all fallen and completing the adsorption tower E that finds time and all press.In addition, being provided with along putting operation, entering downflow releasing tank along venting and after compressor pressurizes, mixing the system of reentering as unstripped gas with fresh feed gas together with displacement waste gas.The present embodiment is substantially identical with all the other technological operation step process of embodiment 1, therefore no longer describes in detail.
After all operations step of adsorption tower A within a cycling cycle is all finished, and then enter next cycling cycle.Other technological operation steps performed by 7 adsorption towers are identical with adsorption tower A, but mutually stagger by the time sequential routine set in time.
The product composition of the present embodiment is as shown in table 6:
Table 6 gas product forms
Methane content in the present embodiment absorption waste gas is 4.34%, and in fresh feed gas, the rate of recovery of methane reaches 88%.And under same apparatus level, identical operating condition, if do not reclaimed displacement waste gas and suitable venting, in unstripped gas, the rate of recovery of methane is only 70%.
Claims (7)
1. one kind is reclaimed displacement waste gas and the pressure-changeable gas-adsorption separation method along venting, comprise all or part of of displacement waste gas pressure swing adsorption gas separation device replacement operator step flowed out from adsorption tower, after compressed boosting, return the step mixing the unstripped gas as pressure swing adsorption gas separation device with fresh feed gas; And optionally by along put operating procedure from adsorption tower discharges all or part of along what exit, return the step mixing the unstripped gas as pressure swing adsorption gas separation device with fresh feed gas after compressed boosting.
2. the method for claim 1, wherein pressure swing adsorption gas separation device arranges the adsorption tower being filled with solid absorbent of more than 4, and multiple stage adsorption tower alternately switches, cycling.
3. method as claimed in claim 1 or 2, wherein the every operating procedure of platform adsorption tower within a cycling cycle must comprise absorption, replaces, vacuumize.
4. the method as described in any one of claim 1-3, wherein the every operating procedure of platform adsorption tower within a cycling cycle also comprises equal pressure drop, along putting, inverse put, all voltage rises, finally to boost.
5. the method as described in any one of claim 1-4, wherein the main composition of product is more than one adsorbent phase component, and described adsorbent phase component is selected from carbon monoxide, carbon dioxide or the hydro carbons containing 1 to 5 carbon atom.
6. the method for claim 1, the operating pressure wherein implementing adsorption tower during adsorption operations step is absolute pressure 0.30MPa-6.10MPa; The operating pressure implementing adsorption tower during replacement operator step is less than or equal to the operating pressure of adsorption tower when implementing adsorption operations step, and is more than or equal to local atmospheric pressure; The minimum operating pressure implementing adsorption tower during vacuum pumping step is absolute pressure 0.0005MPa-0.04MPa.
7. the method for claim 1, in wherein said adsorption tower, the solid absorbent of filling is selected from least one or several in active carbon, aluminium oxide, silica gel, molecular sieve, polymeric adsorbent, copper-carrying adsorbent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510101180.7A CN104740972A (en) | 2015-03-09 | 2015-03-09 | Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510101180.7A CN104740972A (en) | 2015-03-09 | 2015-03-09 | Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104740972A true CN104740972A (en) | 2015-07-01 |
Family
ID=53581567
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510101180.7A Pending CN104740972A (en) | 2015-03-09 | 2015-03-09 | Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104740972A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105203440A (en) * | 2015-09-14 | 2015-12-30 | 大连理工大学 | Method of measuring variable-pressure absorption gas separation performance of carbon molecular sieve on basis of liquid absorption gas flooding principle |
| CN113041777A (en) * | 2021-03-12 | 2021-06-29 | 清华大学 | Gas purification method and gas purification system |
| CN114317052A (en) * | 2021-12-28 | 2022-04-12 | 西南化工研究设计院有限公司 | High-efficiency separation and purification method for low-concentration coal bed gas |
| CN114950071A (en) * | 2022-06-15 | 2022-08-30 | 北京化工大学 | Pressure swing adsorption device and process for efficiently recovering adsorbed components |
-
2015
- 2015-03-09 CN CN201510101180.7A patent/CN104740972A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105203440A (en) * | 2015-09-14 | 2015-12-30 | 大连理工大学 | Method of measuring variable-pressure absorption gas separation performance of carbon molecular sieve on basis of liquid absorption gas flooding principle |
| CN105203440B (en) * | 2015-09-14 | 2017-10-17 | 大连理工大学 | A kind of method that carbon molecular sieve PSA Gas separating property is determined based on imbibition purging principle |
| CN113041777A (en) * | 2021-03-12 | 2021-06-29 | 清华大学 | Gas purification method and gas purification system |
| CN113041777B (en) * | 2021-03-12 | 2022-06-21 | 清华大学 | Gas purification method and gas purification system |
| CN114317052A (en) * | 2021-12-28 | 2022-04-12 | 西南化工研究设计院有限公司 | High-efficiency separation and purification method for low-concentration coal bed gas |
| CN114950071A (en) * | 2022-06-15 | 2022-08-30 | 北京化工大学 | Pressure swing adsorption device and process for efficiently recovering adsorbed components |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106693608B (en) | A kind of process for separating and recovering of oil refinery dry gas | |
| CN101108295B (en) | Method of removing CO2 from switch gas by pressure swing adsorption with replacing and recycling step | |
| CN101978235B (en) | Method and apparatus for separating blast furnace gas | |
| CN100423811C (en) | Pressure-variation absorption method for separating and recovering adsorbed phase products from mixed gas | |
| CN104147896B (en) | Two-stage nitration pressure-variable adsorption reclaims the method for absorption phase product | |
| JP2008501514A (en) | Gas separation method by two-stage full recovery transformer adsorption | |
| CN104058371A (en) | Pressure swing adsorption gas production system and pressure swing adsorption gas production method | |
| CN101555186B (en) | Method for preparing methane by deeply purifying landfill gas | |
| CN104740972A (en) | Pressure swing adsorption gas separation method for recycling displacement waste gas and directly-discharged gas | |
| CN103585856A (en) | Multi-backflow pressure swing adsorption method | |
| CN104986735B (en) | A kind of method for improving hydrogen recovery rate | |
| CN101549856A (en) | Separation method of comprehensively recycled hydrogen and carbon monooxide from synthesis purge gas | |
| CN103752129A (en) | Device and process for separating and recycling non-methane total hydrocarbons and hydrogen gas from refinery dry gas | |
| CN107433107A (en) | C2+ two sections of points of concentration PSA methods are reclaimed from oil refinery dry gas | |
| CN102389682B (en) | Process flow for carrying out high-pressure and low-pressure adsorption treatments on polyolefin tail gas | |
| CN101249370A (en) | Voltage transformation adsorption method for circulation valuable gas | |
| CN102935324B (en) | Variable pressure absorption method for increasing absorption phase product yield | |
| CN100490939C (en) | Process for removing CO2 from conversion gas by pressure swing adsorption method | |
| CN104587795A (en) | Oil and gas recovery process for treating large quantity of oil and gas by using adsorption method | |
| CN104128073A (en) | Novel saturation adsorption process of pressure swing adsorption decarburization and device thereof | |
| CN101096907B (en) | Method for producing natural gas from coal bed gas under low pressure | |
| CN102009963A (en) | High-purity nitrogen preparing method and device | |
| CN105169888B (en) | The modified technique and device of a kind of complete recycling of tail gas of polyethylene device | |
| CN109126380A (en) | A kind of coal mine gas enriching apparatus and its method with the boosting of exhaust end air | |
| CN102091501A (en) | Upper and lower pressure-equalizing pressure swing adsorption method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20150701 |