CN1202901C - Single-stage process flow for side scavengeing with partial raw gas at low-pressure end - Google Patents
Single-stage process flow for side scavengeing with partial raw gas at low-pressure end Download PDFInfo
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- CN1202901C CN1202901C CN 00110113 CN00110113A CN1202901C CN 1202901 C CN1202901 C CN 1202901C CN 00110113 CN00110113 CN 00110113 CN 00110113 A CN00110113 A CN 00110113A CN 1202901 C CN1202901 C CN 1202901C
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Abstract
The present invention relates to a blown sweeping single-stage flow path for partial raw gases on the low-pressure side, which is characterized in that the raw gases are divided into two paths, wherein one path of the gases enter the blown sweeping permeation side from the high-pressure end of a membrane assembly, and the other path of the gases enter the blown sweeping permeation side from the low-pressure end of the membrane assembly; a product gas is a permeation gas on the low-pressure side. When the present invention completes the same design requirement, the number of the required membrane assemblies is less than that in the traditional flow path, and the operation is more flexible simultaneously.
Description
The present invention relates to membrane separation technique, provide a kind of partial raw gas to purge single-stage process flow especially in low-pressure side.
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 permeance property 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 to purge single-stage process flow in low-pressure side, 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 purge single-stage process flow in low-pressure side, it is characterized in that: unstripped gas is divided into two-way, wherein one tunnel high-pressure side from membrane module enters, and another road enters the purging per-meate side from the membrane module low-pressure end, and product gas is low-pressure side infiltration gas.
Flow process mesohigh side of the present invention and low-pressure side gas flow can be and stream or adverse current or cross-flow.
Because unstripped gas is not all 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; Unstripped gas enters low-pressure side simultaneously, has reduced the concentration of this side gas, has improved the mass transfer force of film both sides gases, has increased the flow of gas by film, thereby has further increased product gas total flow.When one timing of product throughput, required membrane module quantity has reduced film.
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 purges single-stage process flow for partial raw gas in low-pressure side.
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, and wherein one tunnel high-pressure side from membrane module enters, and another road enters the purging per-meate side from the membrane module low-pressure end, and product gas is low-pressure side infiltration gas, and required membrane area is 95m
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, a kind of partial raw gas purges single-stage process flow in low-pressure side, it is characterized in that: unstripped gas is divided into two-way, and wherein one tunnel high-pressure side from membrane module enters, and another road enters the purging per-meate side from the membrane module low-pressure end, and product gas is low-pressure side infiltration gas.
2, purge single-stage process flow according to the described partial raw gas of claim 1 in low-pressure side, it is characterized in that: high-pressure side and low-pressure side gas flow are and stream or adverse current or cross-flow.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00110113 CN1202901C (en) | 2000-02-16 | 2000-02-16 | Single-stage process flow for side scavengeing with partial raw gas at low-pressure end |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00110113 CN1202901C (en) | 2000-02-16 | 2000-02-16 | Single-stage process flow for side scavengeing with partial raw gas at low-pressure end |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1308984A CN1308984A (en) | 2001-08-22 |
| CN1202901C true CN1202901C (en) | 2005-05-25 |
Family
ID=4580132
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 00110113 Expired - Fee Related CN1202901C (en) | 2000-02-16 | 2000-02-16 | Single-stage process flow for side scavengeing with partial raw gas at low-pressure end |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1202901C (en) |
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2000
- 2000-02-16 CN CN 00110113 patent/CN1202901C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1308984A (en) | 2001-08-22 |
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Granted publication date: 20050525 Termination date: 20140216 |