CN104226078B - A kind of temperature swing absorption unit for the protection of membrane separation plant is utilized to carry out the method for Temp .-changing adsorption - Google Patents
A kind of temperature swing absorption unit for the protection of membrane separation plant is utilized to carry out the method for Temp .-changing adsorption Download PDFInfo
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- CN104226078B CN104226078B CN201410508680.8A CN201410508680A CN104226078B CN 104226078 B CN104226078 B CN 104226078B CN 201410508680 A CN201410508680 A CN 201410508680A CN 104226078 B CN104226078 B CN 104226078B
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Abstract
Utilize a kind of temperature swing absorption unit for the protection of membrane separation plant to carry out the method for Temp .-changing adsorption, it relates to a kind of temperature swing absorption unit for the protection of membrane separation plant and utilizes this device to carry out the method for Temp .-changing adsorption.The present invention will solve adsorption tanks and separation equipment in existing methanol synthesizer thoroughly can not adsorb and intercept the harmful constituent of carrying secretly in unstripped gas to the infringement of film, cause film device hydraulic performance decline, service life shortens and affects the problem that safe and stable arrangement is run.Device comprises coalescing filter, the first packed tower, the second packed tower, regeneration gas cooler, regeneration gas heater and regeneration gas separator; Method: one, adsorption process; Two, pressure reduction; Three, heating process; Four, blast-cold process; Five, boost process.The present invention is used for methyl alcohol blow-out gas and extracts in coal-based gas device.
Description
Technical field
The present invention relates to a kind of temperature swing absorption unit for the protection of membrane separation plant and utilize this device to carry out the method for Temp .-changing adsorption.
Background technology
A large amount of blow-out gas is had to discharge in existing pressurized gasification combined production of methanol process, the main enrich methane of this part gas and hydrogen, also containing a small amount of carbon monoxide and carbon dioxide, this part gas can enter gas ductwork can pass through UF membrane by the blow-out gas produced in Production of methanol again for town gas, carbon monodixe conversion, carbon dioxide such as to deviate from the means, reclaim hydrogen wherein, and returned methanol-fueled CLC and do methanol feedstock gas, namely hydrogen wherein can be reclaimed concentrate by UF membrane and return methanol synthesizer methanol, remaining gas is containing the methane of high concentration, again by after a small amount of carbon monoxide and carbon dioxide removing, methane can as the natural gas of civilian or industrial high heating value, further pressurization can as vehicle fuel.
But the decarburization unit in existing methanol synthesizer is to methane concentration unit band amine liquid, and the steady salt of catabolite heat of absorbent also enters methane concentration unit with unstripped gas, through heater, the steady salt of catabolite heat of MDEA accumulates in heat exchanger and follow-up pipeline, not only blocking pipeline, and the separating property of various organic principles to subsequent film in the steady salt of heat and amine liquid causes decay, have a strong impact on the safe and stable operation of device and the quality of product, and significantly increase operating cost because changing film.So be badly in need of a kind of device that can adsorb and intercept various organic principles in the steady salt of heat and amine liquid, prevent the steady salt of heat from gathering at pipeline and protect subsequent film, the service life of prolongation film.
Summary of the invention
The present invention will solve adsorption tanks and separation equipment in existing methanol synthesizer thoroughly can not adsorb and intercept the harmful constituent of carrying secretly in unstripped gas to the infringement of film; cause film device hydraulic performance decline; service life shortens and affects the problem that safe and stable arrangement is run, and provides a kind of temperature swing absorption unit for the protection of membrane separation plant and utilize this device to carry out the method for Temp .-changing adsorption.
A kind of temperature swing absorption unit for the protection of membrane separation plant of the present invention comprises coalescing filter, the first packed tower, the second packed tower, regeneration gas cooler, regeneration gas heater and regeneration gas separator; Decarburization gas inlet pipe is connected with the arrival end of described coalescing filter, and described coalescing filter outlet at bottom end is connected with out-of-bounds outlet, described coalescing filter upper outlet end respectively with plug valve X
1arrival end and plug valve X
2arrival end be connected, the top port of described first packed tower respectively with plug valve X
1the port of export, plug valve X
3arrival end and plug valve X
5arrival end be connected, the top port of described second packed tower respectively with plug valve X
2the port of export, plug valve X
4arrival end and plug valve X
6arrival end be connected; Described gases at high pressure discharge pipe respectively with plug valve X
3the port of export and plug valve X
4the port of export be connected, the centre entrance end of described regeneration gas cooler respectively with plug valve X
5the port of export and plug valve X
6the port of export be connected, the centre exit end of described regeneration gas cooler is connected with the centre entrance end of regeneration gas separator, the top exit end of described regeneration gas separator is connected with regeneration gas outlet, and the outlet at bottom end of regeneration gas separator is connected with condensed water outlet pipe; The end port of export of described regeneration gas cooler with loop back water pipe and be connected, the end inlet end of described regeneration gas cooler is connected with circulation upper hose; The bottom port of described first packed tower respectively with plug valve X
7the port of export, plug valve X
9the port of export and plug valve X
11arrival end be connected, the bottom port of described second packed tower respectively with plug valve X
8the port of export, plug valve X
10the port of export and plug valve X
12arrival end be connected; Described regeneration gas inlet tube respectively with plug valve X
7arrival end and plug valve X
8arrival end be connected, the end port of export of described regeneration gas heater respectively with plug valve X
9arrival end and plug valve X
10arrival end be connected, the end inlet end of described regeneration gas heater is connected with regeneration gas inlet tube, and the centre entrance end of described regeneration gas heater is connected with steam inlet tube, and the centre exit end of described regeneration gas heater is connected with condensate pipe; Described striping be separated outlet respectively with plug valve X
11the port of export and plug valve X
12the port of export be connected.
The operation principle of this device: this device adopts Temp .-changing adsorption technology to carry out gas separaion purification, Temp .-changing adsorption technology is to based on the physical absorption of gas molecule by adsorbent (porosu solid material) interior surface, utilize adsorbent to the adsorption capacity of gas with adsorption temp different with pressure and change characteristic, adsorbent is under the condition of the selective absorption of gas with various component, some component in gaseous mixture is adsorbed during cryogenic high pressure, do not gone out by adsorption tower laminar flow by adsorbent component, during high-temperature low-pressure desorption these by the component adsorbed, to carry out cryogenic high pressure absorption next time, multiple adsorption tower can be adopted and reach the object be continuously separated of gas.
The method utilizing said apparatus to carry out Temp .-changing adsorption is carried out according to the following steps:
One, adsorption process: the natural gas after decarburization is entered into coalescing filter by decarburization gas inlet pipe, the natural gas after then filtering passes through plug valve X from the port of export on coalescing filter top
1with plug valve X
2enter into the first packed tower and the second packed tower from the top port of the first packed tower and the second packed tower, the natural gas after adsorbing and removing is discharged from the bottom port of the first packed tower and the second packed tower and is separated outlet by striping and enters film separation unit; Adsorbent is contained in described first packed tower and the second packed tower;
Two, pressure reduction: after completing adsorbing and removing, cut-out tap valve X
1, plug valve X
2, plug valve X
11with plug valve X
12, open plug valve X
3with plug valve X
4, cut-out tap valve X after tower inner high voltage gas is discharged
3with plug valve X
4;
Three, heating process: nitrogen enters into regeneration gas heater by regeneration gas inlet tube, adopts middle pressure steam regeneration gas heater to be heated to 200 DEG C, then through plug valve X
9with plug valve X
10enter into the first packed tower after step-down and the second packed tower from the bottom port of the first packed tower and the bottom port of the second packed tower, the filler in the first packed tower and the second packed tower generates regeneration gas through heating, and regeneration gas is through plug valve X
5with plug valve X
6regeneration gas cooler is entered into from the centre entrance end of regeneration gas cooler, when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator from the centre exit end of regeneration gas cooler and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet by regeneration gas separator top exit end, and liquid is discharged from condensed water outlet pipe by the outlet at bottom end of regeneration gas separator;
Four, blast-cold process: nitrogen is directly through plug valve X
7with plug valve X
8enter into the first packed tower and the second packed tower from the bottom port of the first packed tower and the bottom port of the second packed tower, be cooled to 60 DEG C ~ 80 DEG C to the first packed tower after thermal regeneration and the second packed tower, cooled regeneration gas is through plug valve X
5with plug valve X
6regeneration gas cooler is entered into from the centre entrance end of regeneration gas cooler, when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator from the centre exit end of regeneration gas cooler and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet by regeneration gas separator top exit end, and liquid is discharged from condensed water outlet pipe by the outlet at bottom end of regeneration gas separator;
Five, boost process: be passed in the first packed tower after blast-cold and the second packed tower by the natural gas after purification, after the natural gas after being full of purification in the first packed tower and the second packed tower, can carry out the adsorption process of next circulation.
The invention has the beneficial effects as follows:
1, the present invention utilize adsorbent to the adsorption capacity of gas with adsorption temp different with pressure and change characteristic, adsorbent is under the condition of the selective absorption of gas with various component, some component in gaseous mixture is adsorbed during cryogenic high pressure, do not gone out by adsorption tower laminar flow by adsorbent component, during high-temperature low-pressure desorption these by the component adsorbed, with carry out next time cryogenic high pressure absorption.This device use adsorbent to have very strong adsorption effect to MDEA etc., can reach and remove in unstripped gas the contained harmful components damaging film device, realize the purification to unstripped gas.
2, the present invention is by setting up temperature swing adsorption unit at methane concentration unit, eliminates and causes e-quipment and pipe superpressure, the risk of explosion caused because the steady salt of heat gathers pipeline, eliminate great potential safety hazard.
3, the present invention is after setting up temperature swing adsorption unit, effectively can intercept various organic principles in the steady salt of heat and amine liquid to the infringement of film, extend the service life of film, improve the quality index of gas product.By increasing temperature swing absorption unit, extend the life cycle of film, for enterprise has saved fund.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation of the temperature swing absorption unit for the protection of membrane separation plant.
Detailed description of the invention
Technical solution of the present invention is not limited to following cited detailed description of the invention, also comprises any combination between each detailed description of the invention.
Detailed description of the invention one: composition graphs 1 illustrates present embodiment, present embodiment comprises coalescing filter 1, first packed tower 2, second packed tower 3, regeneration gas cooler 4, regeneration gas heater 5 and regeneration gas separator 6 for the protection of the temperature swing absorption unit of membrane separation plant; Decarburization gas inlet pipe 7 is connected with the arrival end of described coalescing filter 1, and described coalescing filter 1 outlet at bottom end is connected with out-of-bounds outlet 8, described coalescing filter 1 upper outlet end respectively with plug valve X
1the arrival end of 18 and plug valve X
2the arrival end of 19 is connected, the top port of described first packed tower 2 respectively with plug valve X
1the port of export, the plug valve X of 18
3the arrival end of 20 and plug valve X
5the arrival end of 22 is connected, the top port of described second packed tower 3 respectively with plug valve X
2the port of export, the plug valve X of 19
4the arrival end of 21 and plug valve X
6the arrival end of 23 is connected; Described gases at high pressure discharge pipe respectively with plug valve X
3the port of export of 20 and plug valve X
4the port of export of 21 is connected, the centre entrance end of described regeneration gas cooler 4 respectively with plug valve X
5the port of export of 22 and plug valve X
6the port of export of 23 is connected, the centre exit end of described regeneration gas cooler 4 is connected with the centre entrance end of regeneration gas separator 6, the top exit end of described regeneration gas separator 6 is connected with regeneration gas outlet 14, and the outlet at bottom end of regeneration gas separator 6 is connected with condensed water outlet pipe 15; The end port of export of described regeneration gas cooler 4 with loop back water pipe 12 and be connected, the end inlet end of described regeneration gas cooler 4 is connected with circulation upper hose 13; The bottom port of described first packed tower 2 respectively with plug valve X
7the port of export, the plug valve X of 24
9the port of export of 26 and plug valve X
11the arrival end of 28 is connected, the bottom port of described second packed tower 3 respectively with plug valve X
8the port of export, the plug valve X of 25
10the port of export of 27 and plug valve X
12the arrival end of 29 is connected; Described regeneration gas inlet tube 16 respectively with plug valve X
7the arrival end of 24 and plug valve X
8the arrival end of 25 is connected, the end port of export of described regeneration gas heater 5 respectively with plug valve X
9the arrival end of 26 and plug valve X
10the arrival end of 27 is connected, the end inlet end of described regeneration gas heater 5 is connected with regeneration gas inlet tube 16, the centre entrance end of described regeneration gas heater 5 is connected with steam inlet tube 9, and the centre exit end of described regeneration gas heater 5 is connected with condensate pipe 10; Described striping be separated outlet 17 respectively with plug valve X
11the port of export of 28 and plug valve X
12the port of export of 29 is connected.
The characteristic that present embodiment utilizes adsorbent different with pressure with adsorption temp to the adsorption capacity of gas and changes, adsorbent is under the condition of the selective absorption of gas with various component, some component in gaseous mixture is adsorbed during cryogenic high pressure, do not gone out by adsorption tower laminar flow by adsorbent component, during high-temperature low-pressure desorption these by the component adsorbed, with carry out next time cryogenic high pressure absorption.This device use adsorbent to have very strong adsorption effect to MDEA etc., can reach and remove in unstripped gas the contained harmful components damaging film device, realize the purification to unstripped gas.
Present embodiment, by setting up temperature swing adsorption unit at methane concentration unit, eliminates and causes e-quipment and pipe superpressure, the risk of explosion caused because the steady salt of heat gathers pipeline, eliminate great potential safety hazard.
Present embodiment, after setting up temperature swing adsorption unit, effectively can intercept various organic principles in the steady salt of heat and amine liquid to the infringement of film, extend the service life of film, improve the quality index of gas product.By increasing temperature swing absorption unit, extend the life cycle of film, for enterprise has saved fund.
Detailed description of the invention two: the method utilizing device described in detailed description of the invention one to carry out Temp .-changing adsorption is carried out according to the following steps:
One, adsorption process: the natural gas after decarburization is entered into coalescing filter 1 by decarburization gas inlet pipe 7, the natural gas after then filtering passes through plug valve X from the port of export on coalescing filter 1 top
118 and plug valve X
219 enter into the first packed tower 2 and the second packed tower 3 from the top port of the first packed tower 2 and the second packed tower 3, and the natural gas after adsorbing and removing is discharged from the bottom port of the first packed tower 2 and the second packed tower 3 and is separated outlet 17 by striping and enters film separation unit; Adsorbent is contained in described first packed tower 2 and the second packed tower 3;
Two, pressure reduction: after completing adsorbing and removing, cut-out tap valve X
118, plug valve X
219, plug valve X
1128 and plug valve X
1229, open plug valve X
320 and plug valve X
421, cut-out tap valve X after tower inner high voltage gas is discharged
320 and plug valve X
421;
Three, heating process: nitrogen enters into regeneration gas heater 5 by regeneration gas inlet tube 16, adopts middle pressure steam regeneration gas heater 5 to be heated to 200 DEG C, then through plug valve X
926 and plug valve X
1027 fillers entered in the first packed tower 2 after step-down and the second packed tower 3, first packed tower 2 and the second packed tower 3 from the bottom port of the first packed tower 2 and the bottom port of the second packed tower 3 generate regeneration gas through heating, and regeneration gas is through plug valve X
522 and plug valve X
623 enter into regeneration gas cooler 4 from the centre entrance end of regeneration gas cooler 4, when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator 6 from the centre exit end of regeneration gas cooler 4 and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet 14 by regeneration gas separator 6 top exit end, and liquid is discharged from condensed water outlet pipe 15 by the outlet at bottom end of regeneration gas separator 6;
Four, blast-cold process: nitrogen is directly through plug valve X
724 and plug valve X
825 enter into the first packed tower 2 and the second packed tower 3 from the bottom port of the first packed tower 2 and the bottom port of the second packed tower 3, be cooled to 60 DEG C ~ 80 DEG C to the first packed tower 2 after thermal regeneration and the second packed tower 3, cooled regeneration gas is through plug valve X
522 and plug valve X
623 enter into regeneration gas cooler 4 from the centre entrance end of regeneration gas cooler 4, when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator 6 from the centre exit end of regeneration gas cooler 4 and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet 14 by regeneration gas separator 6 top exit end, and liquid is discharged from condensed water outlet pipe 15 by the outlet at bottom end of regeneration gas separator 6;
Five, boost process: be passed in the first packed tower 2 after blast-cold and the second packed tower 3 by the natural gas after purification, after the natural gas after being full of purification in the first packed tower 2 and the second packed tower 3, can carry out the adsorption process of next circulation.
Following examples are adopted to verify beneficial effect of the present invention:
Embodiment: composition graphs 1 illustrates the present embodiment, the method that the present embodiment utilizes device described in the device described in detailed description of the invention one to carry out Temp .-changing adsorption is carried out according to the following steps:
One, adsorption process: the natural gas after decarburization is entered into coalescing filter 1 by decarburization gas inlet pipe 7, the natural gas after then filtering passes through plug valve X from the port of export on coalescing filter 1 top
118 and plug valve X
219 enter into the first packed tower 2 and the second packed tower 3 from the top port of the first packed tower 2 and the second packed tower 3, and the natural gas after adsorbing and removing is discharged from the bottom port of the first packed tower 2 and the second packed tower 3 and is separated outlet 17 by striping and enters film separation unit; Adsorbent is contained in described first packed tower 2 and the second packed tower 3;
Two, pressure reduction: after completing adsorbing and removing, cut-out tap valve X
118, plug valve X
219, plug valve X
1128 and plug valve X
1229, open plug valve X
320 and plug valve X
421, cut-out tap valve X after tower inner high voltage gas is discharged
320 and plug valve X
421;
Three, heating process: nitrogen enters into regeneration gas heater 5 by regeneration gas inlet tube 16, adopts middle pressure steam regeneration gas heater 5 to be heated to 200 DEG C, then through plug valve X
926 and plug valve X
1027 fillers entered in the first packed tower 2 after step-down and the second packed tower 3, first packed tower 2 and the second packed tower 3 from the bottom port of the first packed tower 2 and the bottom port of the second packed tower 3 generate regeneration gas through heating, and regeneration gas is through plug valve X
522 and plug valve X
623 enter into regeneration gas cooler 4 from the centre entrance end of regeneration gas cooler 4, when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator 6 from the centre exit end of regeneration gas cooler 4 and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet 14 by regeneration gas separator 6 top exit end, and liquid is discharged from condensed water outlet pipe 15 by the outlet at bottom end of regeneration gas separator 6;
Four, blast-cold process: nitrogen is directly through plug valve X
724 and plug valve X
825 enter into the first packed tower 2 and the second packed tower 3 from the bottom port of the first packed tower 2 and the bottom port of the second packed tower 3, be cooled to 60 DEG C ~ 80 DEG C to the first packed tower 2 after thermal regeneration and the second packed tower 3, cooled regeneration gas is through plug valve X
522 and plug valve X
623 enter into regeneration gas cooler 4 from the centre entrance end of regeneration gas cooler 4, when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator 6 from the centre exit end of regeneration gas cooler 4 and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet 14 by regeneration gas separator 6 top exit end, and liquid is discharged from condensed water outlet pipe 15 by the outlet at bottom end of regeneration gas separator 6;
Five, boost process: be passed in the first packed tower 2 after blast-cold and the second packed tower 3 by the natural gas after purification, after the natural gas after being full of purification in the first packed tower 2 and the second packed tower 3, can carry out the adsorption process of next circulation.
The present invention is by Temp .-changing adsorption (TSA) technology of industrial maturation; be applied to the filtration to film device unstripped gas and absorption; adsorb by using this device and intercept the various organic principles in the steady salt of heat and amine liquid; prevent the steady salt of heat from gathering at pipeline and protecting subsequent film; extend the service life of film, ensure safe operation and the gas product quality requirement of coal preparing natural gas device.
Claims (1)
1. utilize a kind of temperature swing absorption unit for the protection of membrane separation plant to carry out the method for Temp .-changing adsorption, adsorbent equipment comprises coalescing filter (1), the first packed tower (2), the second packed tower (3), regeneration gas cooler (4), regeneration gas heater (5) and regeneration gas separator (6); Decarburization gas inlet pipe (7) is connected with the arrival end of described coalescing filter (1), described coalescing filter (1) outlet at bottom end is connected with out-of-bounds outlet (8), described coalescing filter (1) upper outlet end respectively with plug valve X
1(18) arrival end and plug valve X
2(19) arrival end is connected, the top port of described first packed tower (2) respectively with plug valve X
1(18) the port of export, plug valve X
3(20) arrival end and plug valve X
5(22) arrival end is connected, the top port of described second packed tower (3) respectively with plug valve X
2(19) the port of export, plug valve X
4(21) arrival end and plug valve X
6(23) arrival end is connected; Gases at high pressure discharge pipe (11) respectively with plug valve X
3(20) the port of export and plug valve X
4(21) the port of export is connected, the centre entrance end of described regeneration gas cooler (4) respectively with plug valve X
5(22) the port of export and plug valve X
6(23) the port of export is connected, the centre exit end of described regeneration gas cooler (4) is connected with the centre entrance end of regeneration gas separator (6), the top exit end of described regeneration gas separator (6) is connected with regeneration gas outlet (14), and the outlet at bottom end of regeneration gas separator (6) is connected with condensed water outlet pipe (15); The end port of export of described regeneration gas cooler (4) with loop back water pipe (12) and be connected, the end inlet end of described regeneration gas cooler (4) is connected with circulation upper hose (13); The bottom port of described first packed tower (2) respectively with plug valve X
7(24) the port of export, plug valve X
9(26) the port of export and plug valve X
11(28) arrival end is connected, the bottom port of described second packed tower (3) respectively with plug valve X
8(25) the port of export, plug valve X
10(27) the port of export and plug valve X
12(29) arrival end is connected; Regeneration gas inlet tube (16) respectively with plug valve X
7(24) arrival end and plug valve X
8(25) arrival end is connected, the end port of export of described regeneration gas heater (5) respectively with plug valve X
9(26) arrival end and plug valve X
10(27) arrival end is connected, the end inlet end of described regeneration gas heater (5) is connected with regeneration gas inlet tube (16), the centre entrance end of described regeneration gas heater (5) is connected with steam inlet tube (9), and the centre exit end of described regeneration gas heater (5) is connected with condensate pipe (10); Striping be separated outlet (17) respectively with plug valve X
11(28) the port of export and plug valve X
12(29) the port of export is connected; The method that it is characterized in that carrying out Temp .-changing adsorption is carried out according to the following steps:
One, adsorption process: the natural gas after decarburization is entered into coalescing filter (1) by decarburization gas inlet pipe (7), the natural gas after then filtering passes through plug valve X from the port of export on coalescing filter (1) top
1and plug valve X (18)
2(19) enter into the first packed tower (2) and the second packed tower (3) from the top port of the first packed tower (2) and the second packed tower (3), the natural gas after adsorbing and removing is discharged from the bottom port of the first packed tower (2) and the second packed tower (3) and is separated outlet (17) by striping and enters film separation unit; Adsorbent is contained in described first packed tower (2) and the second packed tower (3);
Two, pressure reduction: after completing adsorbing and removing, cut-out tap valve X
1(18), plug valve X
2(19), plug valve X
11and plug valve X (28)
12(29) plug valve X, is opened
3and plug valve X (20)
4(21), cut-out tap valve X after tower inner high voltage gas is discharged
3and plug valve X (20)
4(21);
Three, heating process: nitrogen enters into regeneration gas heater (5) by regeneration gas inlet tube (16), adopts middle pressure steam that regeneration gas heater (5) is heated to 200 DEG C, then through plug valve X
9and plug valve X (26)
10(27) the first packed tower (2) after step-down and the second packed tower (3) is entered into from the bottom port of the first packed tower (2) and the bottom port of the second packed tower (3), filler in first packed tower (2) and the second packed tower (3) generates regeneration gas through heating, and regeneration gas is through plug valve X
5and plug valve X (22)
6(23) regeneration gas cooler (4) is entered into from the centre entrance end of regeneration gas cooler (4), when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator (6) from the centre exit end of regeneration gas cooler (4) and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet (14) by regeneration gas separator (6) top exit end, and liquid is discharged from condensed water outlet pipe (15) by the outlet at bottom end of regeneration gas separator (6);
Four, blast-cold process: nitrogen is directly through plug valve X
7and plug valve X (24)
8(25) the first packed tower (2) and the second packed tower (3) is entered into from the bottom port of the first packed tower (2) and the bottom port of the second packed tower (3), be cooled to 60 DEG C ~ 80 DEG C to the first packed tower (2) after thermal regeneration and the second packed tower (3), cooled regeneration gas is through plug valve X
5and plug valve X (22)
6(23) regeneration gas cooler (4) is entered into from the centre entrance end of regeneration gas cooler (4), when the temperature of regeneration gas is down to 40 DEG C, regeneration gas after cooling is entered regeneration gas separator (6) from the centre exit end of regeneration gas cooler (4) and carries out gas-liquid separation, gas after separation is discharged from regeneration gas outlet (14) by regeneration gas separator (6) top exit end, and liquid is discharged from condensed water outlet pipe (15) by the outlet at bottom end of regeneration gas separator (6);
Five, boost process: the natural gas after adsorbing and removing is passed in the first packed tower (2) after blast-cold and the second packed tower (3), after natural gas after being full of adsorbing and removing in the first packed tower (2) and the second packed tower (3), the adsorption process of next circulation can be carried out.
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|---|---|---|---|
| CN201410508680.8A CN104226078B (en) | 2014-09-28 | 2014-09-28 | A kind of temperature swing absorption unit for the protection of membrane separation plant is utilized to carry out the method for Temp .-changing adsorption |
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| CN201410508680.8A CN104226078B (en) | 2014-09-28 | 2014-09-28 | A kind of temperature swing absorption unit for the protection of membrane separation plant is utilized to carry out the method for Temp .-changing adsorption |
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| CN108479322B (en) * | 2018-06-19 | 2020-06-30 | 四川天一科技股份有限公司 | Low-pressure air continuous drying process and equipment |
| CN116764398A (en) * | 2023-08-18 | 2023-09-19 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide dehydration drying system and process |
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| JPS57107222A (en) * | 1980-12-25 | 1982-07-03 | Mitsubishi Heavy Ind Ltd | Method for adsorption and separation of mixed gases |
| AU3329200A (en) * | 1999-03-30 | 2000-10-23 | Kuraray Chemical Co., Ltd. | Mixed gas separating method and separating apparatus |
| KR20120010640A (en) * | 2010-07-22 | 2012-02-06 | 주식회사 씨플러스 | Nitrogen supply device and its control method |
| CN203284374U (en) * | 2013-04-09 | 2013-11-13 | 北京石油化工工程有限公司 | Pure integration dehydration device of liquefied hydrocarbon |
| CN103265986A (en) * | 2013-05-30 | 2013-08-28 | 中煤能源黑龙江煤化工有限公司 | Method for extracting coal-based natural gas from methanol blowdown gas and method for producing CNG (compressed natural gas) |
| CN204093268U (en) * | 2014-09-28 | 2015-01-14 | 中煤能源黑龙江煤化工有限公司 | A kind of temperature swing absorption unit for the protection of membrane separation plant |
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