CN1306880A - Single-stage process of mixing partial material gas and permeate gas - Google Patents
Single-stage process of mixing partial material gas and permeate gas Download PDFInfo
- Publication number
- CN1306880A CN1306880A CN 00110082 CN00110082A CN1306880A CN 1306880 A CN1306880 A CN 1306880A CN 00110082 CN00110082 CN 00110082 CN 00110082 A CN00110082 A CN 00110082A CN 1306880 A CN1306880 A CN 1306880A
- Authority
- CN
- China
- Prior art keywords
- gas
- flow
- infiltration
- membrane module
- stage process
- 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.)
- Granted
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The single stage process features that the feed gas is divided into two parts, one into the high pressure end of membrane assembly and the other mixed with the osmotic gas of low pressure end; and product gas is the mixture of osmotic gas and partial material gas. The present invention needs less membrane assemblies than traditional process for the same design requirement and is more flexible in operation.
Description
The present invention relates to membrane separation technique, a kind of partial raw gas and infiltration gas mixing single-stage process flow are provided especially.
Desirable stage theory has been experienced in the research of flow scheme design, optimization method and principle, continuous film post theory, a series of processes such as circulated in countercurrent stage theory.Along with the raising of membrane module separating property, some simple multistage flow processs just are being subjected to more and more researchers' attention at present.Because membrane module separating property in the past is lower, therefore in order to reach higher separation requirement, when flow scheme design, separating property how to give full play to membrane module becomes an important design philosophy.But, in flow scheme design the membrane module separating property to demonstrate fully often to sacrifice permeance property be cost.As a simple two-stage process (this flow process often is used to the higher separation process of product gas concentration requirement), because total pressure differential equals the pressure differential sum of membrane modules at different levels, therefore the pressure differential of each grade membrane module has reduced, the infiltration capacity of this grade has also reduced, thereby causes the infiltration life of membrane module to be not in full use in this flow process.Prassad is at US Pat5 in 1992, proposed three grades of flow processs that prepare extreme high purity nitrogen with air in 102,432.In this flow process, distribute by the membrane area of adjusting three grades of membrane modules, nitrogen gas concn can reach 99%～99.999%.This flow process reduces required membrane module quantity by increasing compressor or compressor power consumption.Prassad is also at US Pat5 in 1993, proposed a two-stage process for preparing oxygen rich air with air in 185,014, in this flow process, partly or entirely raw air is entered by second level per-meate side, and second level infiltration gas is introduced into first order high-pressure side, and product gas is first order infiltration gas.Because the oxygen concentration of second level infiltration gas is greater than airborne oxygen concentration, therefore can improve product gas concentration as the unstripped gas of the first order with second level infiltration gas.Xu is at US Pat5 in 1993, proposed a secondary gas film separation process in 282,969, and this flow process is used for the fast gas concentration of unstripped gas when low, and fast gas is put forward dense process, and the oxygen enrichment process is one of them application example.This flow process is to utilize second level per-meate side light concentration gas to purge first order per-meate side, to reduce first order per-meate side concentration, improves the mass transfer force of the fast gas in film both sides, thereby reaches the purpose that increases the fast impervious amount of the first order.Xu is also at USPat5 in 1994, proposed three grades of gas film separation process in 306,427, and this flow process is used for the fast gas concentration of unstripped gas when low, and fast gas is put forward dense process, and the oxygen enrichment process is one of them application example.This flow process has increased a gas enrichment section slowly on stream, and promptly stripping section is further purified the concentration of gas slowly in the non-infiltration gas.Can making slowly by this flow process, gas, fast gas obtain enrichment simultaneously in separation process.At present, along with the development of membrane separation technique, the separating property of membrane module is greatly improved, and in flow scheme design, permeance property how to give full play to membrane module has become important research project, and the research report of relevant this respect also seldom.Give full play to the permeance property of membrane module, under most economical condition, realize designing requirement, engineering design is had important and practical meanings.
The object of the present invention is to provide a kind of partial raw gas and infiltration gas mixing single-stage process flow, it is when finishing identical designing requirement, and required membrane module quantity is less than traditional process, also has more flexibility in the operation simultaneously.
The invention provides a kind of partial raw gas and infiltration gas mixing single-stage process flow, it is characterized in that: unstripped gas is divided into two-way, wherein one tunnel high-pressure side from membrane module enters, and mix with membrane module low-pressure end infiltration gas on another road, and product gas is the gaseous mixture of infiltration gas and partial raw gas.
Flow process mesohigh side of the present invention and low-pressure side gas flow can be and stream, adverse current, cross-flow.
Because unstripped gas is not to be passed through by membrane module inside, a part of unstripped gas does not directly mix with infiltration gas through film, so the total flow of product gas has increased, when one timing of product throughput, the quantity of required membrane module has reduced,
It is higher that the present invention is specially adapted to the membrane module separation, and product gas is the separation process of infiltration gas, as: synthetic ammonia relief gas hydrogen recovery process; Film oxygen enriching process etc.
Below by embodiment in detail the present invention is described in detail.
Accompanying drawing 1 is partial raw gas and infiltration gas mixing single-stage process flow.
Accompanying drawing 2 is that the synthetic ammonia relief gas hydrogen of tradition reclaims single-stage process flow.
Embodiment
Synthesize ammonia relief gas hydrogen recovery process flow scheme design as shown in Figure 1: unstripped gas is divided into two-way, wherein one tunnel high-pressure side from membrane module enters, mix with membrane module low-pressure end infiltration gas on another road, and product gas is the gaseous mixture of infiltration gas and partial raw gas, and required membrane area is 113m
2Used membrane module hydrogen infiltration coefficient 5.0 * 10
-5Cm
3(STP)/cm
2S cmHg, separation 50; Adopt unstripped gas hydrogen concentration 0.6, raw gas flow 1000m
3(STP)/and hr, feed side pressure 11MPa, osmotic lateral pressure 2MPa, gained final products gas hydrogen yield 0.85, product gas hydrogen concentration 0.85.
Comparative example
Flow process tradition is as shown in Figure 1 synthesized ammonia relief gas hydrogen recovery process, the same embodiment of used membrane module, i.e. membrane module hydrogen infiltration coefficient 5.0 * 10
-5Cm
3(STP)/cm
2S cmHg, separation 50; Adopt same unstripped gas and operating parameter, promptly the unstripped gas hydrogen concentration 0.6, raw gas flow 1000m
3(STP)/and hr, feed side pressure 11MPa, osmotic lateral pressure 2MPa, when final products were same identical with embodiment, promptly product gas hydrogen yield 0.85, product gas hydrogen concentration 0.85; Required membrane area is 155m
2, high more a lot of than the required membrane area of embodiment.
Claims (2)
1. partial raw gas and infiltration gas mixing single-stage process flow, it is characterized in that: unstripped gas is divided into two-way, wherein one tunnel high-pressure side from membrane module enters, and mix with membrane module low-pressure end infiltration gas on another road, and product gas is the gaseous mixture of infiltration gas and partial raw gas.
2. according to described partial raw gas of claim 1 and infiltration gas mixing single-stage process flow, it is characterized in that: high-pressure side and low-pressure side gas flow are and stream, adverse current, cross-flow.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00110082 CN1206018C (en) | 2000-01-28 | 2000-01-28 | Single-stage process of mixing partial material gas and permeate gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00110082 CN1206018C (en) | 2000-01-28 | 2000-01-28 | Single-stage process of mixing partial material gas and permeate gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1306880A true CN1306880A (en) | 2001-08-08 |
| CN1206018C CN1206018C (en) | 2005-06-15 |
Family
ID=4580102
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 00110082 Expired - Fee Related CN1206018C (en) | 2000-01-28 | 2000-01-28 | Single-stage process of mixing partial material gas and permeate gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1206018C (en) |
-
2000
- 2000-01-28 CN CN 00110082 patent/CN1206018C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1206018C (en) | 2005-06-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8808427B2 (en) | Process and apparatus for the treatment of a carbon dioxide-containing gas stream form a large-scale combustion plant | |
| CN1032518C (en) | Membrane oxygen process and system | |
| KR101985551B1 (en) | Process for separation of gases | |
| US7875101B2 (en) | Hybrid membrane—PSA system for separating oxygen from air | |
| US5282969A (en) | High pressure feed membrane separation process | |
| CN1063053A (en) | Three-stage membrane gas spearation process and system | |
| JPH07748A (en) | High purity membrane nitrogen | |
| CN1083731C (en) | Simulataneous step pressure swing adsorption process | |
| EP2616163A1 (en) | Gas separation process using membranes with permeate sweep to remove co2 from gaseous fuel combustion exhaust | |
| US5306427A (en) | Low pressure feed membrane separation process | |
| CN103140571A (en) | Two-stage membrane process | |
| CA2277669A1 (en) | Method and apparatus for recovering a gas from a gas mixture | |
| CN1474783A (en) | Multiple pressure process for production of ammonia | |
| CN104001408A (en) | Helium recovery from natural gas | |
| EP1078677A2 (en) | Method and apparatus for regulating mixed gas concentration | |
| US5252219A (en) | Compressed permeate sweep membrane separation process | |
| CN1206018C (en) | Single-stage process of mixing partial material gas and permeate gas | |
| CN1114583C (en) | Manufacture method for methanol by use of raw coal | |
| CN1202898C (en) | Two-stage process with intermediate gas sweeping | |
| CN1202901C (en) | Single-stage process flow for side scavengeing with partial raw gas at low-pressure end | |
| CN1202900C (en) | Single-stage process flow for side scavenging with partial tail gas at low-pressure end | |
| CN1202899C (en) | Multistage sweeping process | |
| KR102409244B1 (en) | Purification and recycling system and method for improving the efficiency of methane recovery in biogas | |
| CN1082509A (en) | The method of hydrogen recovery by variable-pressure absorption low temperature separation | |
| CA3113200C (en) | Membrane process and system for high recovery of a nonpermeating 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 | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |