CN201658935U - Membrane separation device for methanol purge gas recovery - Google Patents
Membrane separation device for methanol purge gas recovery Download PDFInfo
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- CN201658935U CN201658935U CN2010201118544U CN201020111854U CN201658935U CN 201658935 U CN201658935 U CN 201658935U CN 2010201118544 U CN2010201118544 U CN 2010201118544U CN 201020111854 U CN201020111854 U CN 201020111854U CN 201658935 U CN201658935 U CN 201658935U
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- gas
- cooler
- methanol
- separator
- membrane
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Abstract
The utility model discloses a membrane separation device for methanol purge gas recovery, which comprises a methanol separator, a membrane inlet heater, a membrane separator, a cooler 1, a cooler 2 and a turbomachine, wherein the turbomachine comprises a compression end and an expansion end, and all the components are connected via pipelines. By aid of the membrane separation device, recovery of methanol in purge gas can be realized without water scrubbers, and pressure lifting of permeating gas can be realized without electric compressors, thereby reducing equipment investment and energy consumption, simplifying processes, increasing operation stability and reducing production cost.
Description
Technical field
The utility model relates to the hydrogen gas recovering device technical field of hydrogen rich gas systems such as methyl alcohol and gas and synthetic ammonia purge, the membrane separation device that particularly a kind of methanol purge gas reclaims.
Background technology
Contain H in the system for methanol synthesis off-gas
2, CO, CO
2Deng composition, portioned product CH
3OH and N
2, inert component such as Ar.It forms according to the synthesis gas source different and slightly different, but hydrogen content is generally higher, at least about 60%.Available gas in the off-gas is carried out enriching and recovering can effectively reduce synthesis gas consumption, and then reduce front end gas making, the energy resource consumption of workshop sections such as conversion, purification and compression reduces the methanol production cost.
Off-gas recovery technology at present commonly used comprises that the transformation adsorbing separation separates two kinds of methods with film, and accordingly, the off-gas retracting device comprises two kinds of pressure-swing absorption apparatus and membrane separation devices.
Transformation adsorption separation device and technology are to utilize the difference of the adsorption capacity of different components on adsorbent in the gas medium, and adsorbent carries out selective absorption when pressure raises, obtain a kind of gas separation of desorption and regeneration when pressure reduces.Every cover pressure-swing absorption apparatus is made up of two towers at least, and each tower is finished an adsorption-regeneration cycle through steps such as absorption, all pressure drops, flushing/vacuumize, all voltage rises, final rises successively, and all has one or more tower to be in adsorbed state at any one time.During gas process adsorption bed, be adsorbed gas and be attracted in the bed, other gases that are not adsorbed then pass bed and obtain enriching and purifying from cat head; In the regeneration stage, be adsorbed gas and at the bottom of tower, be so incensed that as desorption.
In the transformation adsorbing separation removal process of methanol purge gas, the H in the off-gas
2Be not adsorbed, become purified hydrogen by adsorbent bed at cat head, other component then obtains at the bottom of tower as desorption gas by regenerative process.
The characteristics of transformation adsorbing separation methanol purge gas are:
1) hydrogen purity height can reach more than 99.9%;
2) pressure drop is little, the highest general pressure drop of having only 100～200KPa;
3) rate of recovery height can reach more than 85%;
4) need water scrubber that off-gas is washed before entering pressure swing adsorption system, reclaim CH
3OH.
Though this method has obtained high-purity hydrogen, lost most of CO, the CO in the off-gas
2Deng available gas, say it is irrational from the angle of resource recycling.Transformation adsorbing separation methanol purge gas is comparatively suitable in the occasion that needs high-purity hydrogen, but if the separation of methanol off-gas returns synthesis system, because this method loss available gas is not most economical.
Membrane separation device and technology are another effective means of gas separation field.Its operation principle is to utilize a kind of high molecular polymer (normally polyimides or polysulfones) film to select " filtration " feeding gas and reach the separation purpose.When two or more admixture of gas passed through thin polymer film, the difference of the dissolving diffusion coefficient of each gas component in polymer caused the speed difference of its infiltration by membranous wall.Thus, (the comparatively faster gas of infiltration rate is as H gas can be divided into " fast gas "
2O, H
2, He etc.) and " gas slowly " (gas that infiltration rate is relatively slow is as N
2, CH
4And other hydro carbons etc.).When mist in driving force--under the effect of film both sides respective components partial pressure difference, infiltration rate comparatively faster gas penetrated preferably membranous wall and in the low-pressure permeability side by enrichment, the relatively slow gas of infiltration rate then is detained side by enrichment at high pressure.
Traditional methanol purge gas membrane separation device as shown in Figure 1, its primary structure comprises: water scrubber, methanol separator, film inlet heater, membrane separator, motor compressor etc.; Off-gas removes wherein methyl alcohol through water scrubber T101 and methanol separator V101, and the off-gas that removes methyl alcohol is heated to 40～60 ℃ through film inlet heater E103 and enters membrane separator X101, X102 and separate.
Most H in the off-gas
2, CO, CO
2Obtain at the bottom of tower Deng as low-pressure permeability gas, through returning synthesis system after the hydrogen gas compressor compression; And most of CH
4, N
2, Ar and small part H
2, CO, CO
2Obtain non-infiltration gas (CH from cat head Deng as the non-infiltration gas of high pressure
4, N
2, Ar, H
2, CO, CO
2) go fuel gas system or do its usefulness.
The characteristics of film separation of methanol off-gas are:
1) the infiltration atmosphere pressure losses is big, and pressure drop is minimum at 2MPa;
2) the single stage membrane rate of recovery is lower, and the highest can only reaching about 80% adopts multistage film can improve the rate of recovery;
3) contained H simultaneously in the infiltration gas
2, CO, CO
2Deng the available gas composition;
4) need water scrubber that off-gas is washed before entering film separation system, reclaim CH
3OH.
Because the infiltration atmosphere pressure losses is big, infiltration gas be returned synthesis system need be with motor compressor with boost in pressure, and this method has been wasted the pressure head energy of non-infiltration gas 5～15MPa and additionally increased power consumption.Therefore, traditional membrane separation process separation of methanol off-gas utilizes angle to see from energy not to be the most rational.
In addition, the transformation adsorbing separation is separated with film all needs water scrubber that off-gas is washed, and also high to the stability requirement of operation, has increased equipment investment, and complex technical process.
The utility model content
Goal of the invention of the present utility model is: at the deficiency that two kinds of methanol purge gas retracting devices of above-mentioned prior art exist, the membrane separation device that provides a kind of new methanol purge gas to reclaim need not the separation that water scrubber can be realized methyl alcohol in the off-gas; Also need not motor compressor and can realize lifting, thereby reduce equipment investment and energy resource consumption, improve operational stability and reduce production costs the infiltration atmospheric pressure.
The technical solution adopted in the utility model is such:
The membrane separation device that methanol purge gas reclaims, critical piece comprises: methanol separator, film inlet heater, membrane separator also comprise cooler 1, cooler 2, turbine; Wherein: turbine comprises compression end and expanding end; And as follows between each parts by the pipeline annexation:
Cooler 1 is connected with system for methanol synthesis, so that enter the film separation and recovery system from the high pressure methanol purge gas of system for methanol synthesis as unstripped gas;
Cooler 1 also is connected with film inlet heater with the gas vent of methanol separator respectively, be chilled to 12～22 ℃ in advance so that carry out heat exchange in cooler 1 neutralization from the gas of methanol separator gas vent as unstripped gas, and make from the gas of methanol separator gas vent and through subcooler 1 precooling unstripped gas after, entering the film heater that enters the mouth from the high pressure methanol purge gas of system for methanol synthesis;
Cooler 1 also is connected with cooler 2, so that the off-gas that is chilled in advance after 12～22 ℃ through above-mentioned heat exchange enters cooler 2, further cools off 1～10 ℃ in cooler 2, makes the methyl alcohol in the off-gas be cooled to liquid;
Cooler 2 also is connected with methanol separator, so that enter methanol separator through the gas of above-mentioned further cooling, liquid methanol is separated;
Methanol separator has gas vent and thick methyl alcohol outlet, gas vent also is connected with cooler 1, so that in methanol separator, carry out gas-liquid separation through the gas of above-mentioned further cooling, liquid methanol is separated and obtain thick methyl alcohol (also can further go rectifying to obtain the higher methyl alcohol of purity) from the outlet of thick methyl alcohol, gas behind the separation of methanol then enters cooler 1 cooling unstripped gas to 12～22 ℃ from gas vent, enter film inlet heater after while self, temperature was increased to 30～50 ℃, in film inlet heater, be steam heated to 40-60 ℃;
Film inlet heater also is connected with membrane separator, membrane separator has outlet of infiltration gas and the outlet of non-infiltration gas, make the gas that in film inlet heater, is heated to 40-60 ℃ enter membrane separator, in membrane separator, separate, obtain permeating gas (main component H in outlet of infiltration gas and the outlet of non-infiltration gas respectively
2, and portion C O, CO
2And small amount of N
2Deng) and non-infiltration gas (contain N
2, Ar, CH
4, H
2, CO, CO
2Deng); Membrane separator can be provided with one or more snippets, takes all factors into consideration with hydrogen recovery rate and equipment cost etc., to be provided with two sections for excellent;
The outlet of the infiltration gas of membrane separator is connected with the compression end of turbine, and the compression end of turbine also is connected with system for methanol synthesis, is compressed into to meet and returns system for methanol synthesis behind the system for methanol synthesis required pressure and utilized once more so that permeate gas;
The non-infiltration gas outlet of membrane separator is connected with the expanding end of turbine, so that non-infiltration gas turbine expansion, be cooled to-40～-80 ℃;
The expanding end of turbine also is connected with cooler 2, returns in the cooler 2 off-gas is further cooled off so that be cooled to-40～-80 ℃ non-infiltration gas, makes methanol condensed wherein become liquid; Export mechanical power simultaneously and give the compression end (being compressor) of turbine.
Cooler 2 also can be connected with fuel gas system, so that the further gas output that acts as a fuel of the non-infiltration gas behind the cooling off-gas in cooler 2 enters fuel system and is fully used.
The infiltration gas outlet of membrane separator also can be connected with pressure-swing absorption apparatus, goes transformation to adsorb rough hydrogen will partly permeate pneumatic transmission.
In sum, owing to adopted technique scheme, the beneficial effects of the utility model are:
This device need not the separation that water scrubber equipment can be realized methyl alcohol in the off-gas; Also need not motor compressor equipment and can realize lifting, thereby reduce equipment investment and energy resource consumption, and simplify technical process, improve operational stability and reduce production costs the infiltration atmospheric pressure.
Description of drawings
Fig. 1 is traditional methanol purge gas membrane separation device schematic diagram.
Fig. 2 is the methanol purge gas membrane separation device schematic diagram that the utility model has only one group of membrane separator, also is the membrane separation device schematic diagram of embodiment 1 simultaneously.
Fig. 3 is the methanol purge gas membrane separation device schematic diagram that two groups of membrane separators are arranged among the present invention, also is the membrane separation device schematic diagram of embodiment 2 simultaneously.
Fig. 4 is the methanol purge gas membrane separation device schematic diagram that two groups of membrane separators, while FF hydrogen are arranged in the utility model, also is the membrane separation device schematic diagram of embodiment 3 simultaneously.
Mark among Fig. 1-4: T101 is a water scrubber, V101 is a methanol separator, E101 is a cooler 1, E102 is a cooler 2, and E103 is a film inlet heater, and X101 is one section of a membrane separator, X102 is two sections of membrane separators, C101-1 is the compression end of turbine, and C101-2 is the expanding end of turbine, and C102 is a motor compressor.
The specific embodiment
Below in conjunction with accompanying drawing, the utility model is done detailed explanation.
In order to make the purpose of this utility model, technical scheme and advantage clearer,, the utility model is further elaborated below in conjunction with drawings and Examples.Should be appreciated that specific embodiment described herein only in order to explanation the utility model, and be not used in qualification the utility model.
Embodiment 1
As shown in Figure 2, the membrane separation device of present embodiment methanol purge gas comprises:
Methanol separator V101, film inlet heater E103, membrane separator also comprise cooler 1E101, cooler 2E102, turbine, and turbine comprises compression end C101-1 and expanding end C101-2;
As follows between each parts by the pipeline annexation:
Cooler 1E101 is connected with system for methanol synthesis;
Cooler 1E101 also is connected with film inlet heater E103 with the gas vent of methanol separator V101 respectively;
Cooler 1E101 also is connected with cooler 2E102;
Cooler 2E102 also is connected with methanol separator V101;
Methanol separator V101 has gas vent and thick methyl alcohol outlet; Thick methyl alcohol outlet is connected with distillation system;
Film inlet heater E103 also is connected with membrane separator X101, and membrane separator X101 has outlet of infiltration gas and the outlet of non-infiltration gas; It is one section X101 of membrane separator that membrane separator is provided with one section;
The infiltration gas outlet of one section X101 of membrane separator is connected with the compression end C101-1 of turbine, and the compression end C101-1 of turbine also is connected with system for methanol synthesis;
The non-infiltration gas outlet of one section X101 of membrane separator is connected with the expanding end C101-2 of turbine;
The expanding end C101-2 of turbine also is connected with cooler 2E102;
Cooler 2E102 also is connected with fuel gas system.
Embodiment 2
As shown in Figure 3, the membrane separation device of present embodiment methanol purge gas comprises:
Methanol separator V101, film inlet heater E103, membrane separator also comprise cooler 1E101, cooler 2E102, turbine, and turbine comprises compression end C101-1 and expanding end C101-2;
As follows between each parts by the pipeline annexation:
Cooler 1E101 is connected with system for methanol synthesis;
Cooler 1E101 also is connected with film inlet heater E103 with the gas vent of methanol separator V101 respectively;
Cooler 1E101 also is connected with cooler 2E102;
Cooler 2E102 also is connected with methanol separator V101;
Methanol separator V101 has gas vent and thick methyl alcohol outlet; Thick methyl alcohol outlet is connected with distillation system;
Film inlet heater E103 also is connected with membrane separator, and membrane separator has outlet of infiltration gas and the outlet of non-infiltration gas; It is one section X101 of membrane separator and two sections X102 of membrane separator that membrane separator is provided with two sections;
The non-infiltration gas outlet of one section X101 of membrane separator is connected with two sections X102 of membrane separator, makes one section non-infiltration gas that comes out carry out the secondary film and separates;
The infiltration gas outlet of two sections X102 of membrane separator is connected with the compression end C101-1 inlet of turbine, the infiltration gas outlet of one section X101 of membrane separator is connected with the outlet of turbine compression end C101-1, and the compression end C101-1 of turbine also is connected with system for methanol synthesis;
The non-infiltration gas outlet of two sections X102 of membrane separator is connected with the expanding end C101-2 of turbine;
The expanding end C101-2 of turbine also is connected with cooler 2E102;
Cooler 2E102 also is connected with fuel gas system.
Embodiment 3
As shown in Figure 4, the membrane separation device of present embodiment methanol purge gas comprises:
Methanol separator V101, film inlet heater E103, membrane separator also comprise cooler 1E101, cooler 2E102, turbine, and turbine comprises compression end C101-1 and expanding end C101-2;
As follows between each parts by the pipeline annexation:
Cooler 1E101 is connected with system for methanol synthesis;
Cooler 1E101 also is connected with film inlet heater E103 with the gas vent of methanol separator V101 respectively;
Cooler 1E101 also is connected with cooler 2E102;
Cooler 2E102 also is connected with methanol separator V101;
Methanol separator V101 has gas vent and thick methyl alcohol outlet; Thick methyl alcohol outlet is connected with distillation system;
Film inlet heater E103 also is connected with membrane separator, and membrane separator has outlet of infiltration gas and the outlet of non-infiltration gas; It is one section X101 of membrane separator and two sections X102 of membrane separator that membrane separator is provided with two sections;
The non-infiltration gas outlet of one section X101 of membrane separator is connected with two sections X102 of membrane separator, makes one section non-infiltration gas that comes out carry out the secondary film and separates;
The infiltration gas outlet of two sections X102 of membrane separator is connected with the compression end C101-1 inlet of turbine, and the outlet of one section infiltration of membrane separator gas is connected with the outlet of turbine compression end C101-1, and the compression end C101-1 of turbine also is connected with system for methanol synthesis; The infiltration gas outlet of two sections X102 of membrane separator also is connected with pressure-swing absorption apparatus (PSA system);
The non-infiltration gas outlet of two sections X102 of membrane separator is connected with the expanding end C101-2 of turbine;
The expanding end C101-2 of turbine also is connected with cooler 2E102;
Cooler 2E102 also is connected with fuel gas system.
The above only is preferred embodiment of the present utility model, not in order to restriction the utility model, all any modifications of being done within spirit of the present utility model and principle, is equal to and replaces and improvement etc., all should be included within the protection domain of the present utility model.
Claims (4)
1. the membrane separation device of methanol purge gas recovery comprises methanol separator, film inlet heater, membrane separator, it is characterized in that:
Also comprise cooler (1), cooler (2), turbine;
Described turbine comprises compression end and expanding end;
As follows between each parts by the pipeline annexation:
Cooler (1) is connected with system for methanol synthesis;
Cooler (1) also is connected with film inlet heater with the gas vent of methanol separator respectively;
Cooler (1) also is connected with cooler (2);
Cooler (2) also is connected with methanol separator;
Methanol separator has gas vent and thick methyl alcohol outlet;
Film inlet heater also is connected with membrane separator, and membrane separator has outlet of infiltration gas and the outlet of non-infiltration gas; Membrane separator is provided with one or more snippets;
The infiltration gas outlet of membrane separator is connected with the compression end of turbine, and the compression end of turbine also is connected with system for methanol synthesis;
The non-infiltration gas outlet of membrane separator is connected with the expanding end of turbine;
The expanding end of turbine also is connected with cooler (2).
2. device according to claim 1 is characterized in that:
Described membrane separator is provided with two sections.
3. device according to claim 1 is characterized in that:
Described cooler (2) also is connected with fuel gas system.
4. device according to claim 1 is characterized in that:
The infiltration gas outlet of described membrane separator also is connected with pressure-swing absorption apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010201118544U CN201658935U (en) | 2010-02-10 | 2010-02-10 | Membrane separation device for methanol purge gas recovery |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010201118544U CN201658935U (en) | 2010-02-10 | 2010-02-10 | Membrane separation device for methanol purge gas recovery |
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| CN201658935U true CN201658935U (en) | 2010-12-01 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105460891A (en) * | 2014-09-03 | 2016-04-06 | 中国石油天然气股份有限公司 | Recycling method and system for methanol purge gas |
| CN105585425A (en) * | 2015-12-30 | 2016-05-18 | 七台河宝泰隆煤化工股份有限公司 | Hydrogen recycling device |
| CN107200679A (en) * | 2016-03-16 | 2017-09-26 | 乔治·克劳德方法的研究开发空气股份有限公司 | Methanol-fueled CLC is carried out by the synthesis gas for lacking hydrogen |
-
2010
- 2010-02-10 CN CN2010201118544U patent/CN201658935U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105460891A (en) * | 2014-09-03 | 2016-04-06 | 中国石油天然气股份有限公司 | Recycling method and system for methanol purge gas |
| CN105460891B (en) * | 2014-09-03 | 2017-11-07 | 中国石油天然气股份有限公司 | The recoverying and utilizing method and system of a kind of methanol purge gas |
| CN105585425A (en) * | 2015-12-30 | 2016-05-18 | 七台河宝泰隆煤化工股份有限公司 | Hydrogen recycling device |
| CN107200679A (en) * | 2016-03-16 | 2017-09-26 | 乔治·克劳德方法的研究开发空气股份有限公司 | Methanol-fueled CLC is carried out by the synthesis gas for lacking hydrogen |
| CN107200679B (en) * | 2016-03-16 | 2022-02-18 | 乔治·克劳德方法的研究开发空气股份有限公司 | Methanol synthesis from hydrogen deficient synthesis gas |
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| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20101201 Termination date: 20170210 |