CN208042615U - A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system - Google Patents
A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system Download PDFInfo
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- CN208042615U CN208042615U CN201820323887.1U CN201820323887U CN208042615U CN 208042615 U CN208042615 U CN 208042615U CN 201820323887 U CN201820323887 U CN 201820323887U CN 208042615 U CN208042615 U CN 208042615U
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Abstract
The utility model discloses a kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas systems.System includes nitrogen compressor, heat exchanger, domethanizing column, flash column, hydrogen flash tank, molecular sieve absorbing unit, pressure swing adsorption hydrogen production unit, raw material air pipe, circulating nitrogen gas pipeline, gas phase isolate pipeline and liquid phase separation property management road, the molecular sieve absorbing unit includes absorbing unit switch valve group, produce molecular sieve adsorber, regenerated molecular sieve absorber, regeneration gas heaters, regeneration gas cooler, the pressure swing adsorption hydrogen production unit includes that the first hydrogen manufacturing produces absorber, Hydrogen Unit switch valve group, hydrogen manufacturing regenerative adsorption device, second hydrogen manufacturing produces absorber；The utility model solves the problems such as traditional coal material gas separating technology low separation efficiency, equipment are complicated, operating cost is high and high energy consumption, the Highgrade integration process equipment ensure product gas high-purity while, production cost is reduced, efficiency is improved, reduces energy consumption.
Description
Technical field
The utility model is related to chemical separating system more particularly to a kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas
System.
Background technology
The utility model is related to Coal Chemical Engineering Project, be the synthesis gas that is exported using coal chemical industry clean unit as raw material, pass through
The separator of design obtains three kinds of hydrogen, carbon monoxide and methane products, go to respectively downstream production ethylene glycol, methanol and
SNG products.Currently, in industry there are mainly two types of common separating technologies：One is in cryogenic separation device by hydrogen, an oxygen
Change carbon separation, obtains hydrogen and carbon monoxide product, purpose is principally obtaining product hydrogen and carbon monoxide, goes to downstream respectively
Ethylene glycol is processed, then entering another set of system to the component containing methane such as tail gas again carries out liquefaction separation, and two systems are independent
It runs, is not related mutually；Another technique is to detach raw material gas liquefaction in cryogenic separation device, obtain methane or
The methane liquefaction cooling box that will be isolated, other components such as hydrogen, carbon monoxide and N2 etc. directly go out device as fuel gas, should
The main purpose of technique is to obtain methane or methane liquefaction as LNG.
The technologies such as molecular sieve adsorbing separation or cryogenic separation involved in technique generally use in industry, still
Due to lacking the system design of integrated planning and science, there is low separation efficiency, high energy consumption, number of devices in both the above technique
The shortcomings of mostly complicated, factory floor is big, increase the operating cost of enterprise, while generally existing system tail gas in prior art
The problems such as cost recovery is high, the rate of recovery is low, has derived the potential risks such as environmental pollution.
Invention content
The purpose of the utility model is to overcome the deficiencies in the prior art, provide a kind of coal chemical industry synthesis gas cryogenic separation coproduction
Methane gas system.
A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system, including nitrogen compressor, heat exchanger, demethanation
Tower, flash column, hydrogen flash tank, molecular sieve absorbing unit, pressure swing adsorption hydrogen production unit, raw material air pipe, circulating nitrogen gas pipeline,
Gas phase isolate pipeline and liquid phase separation property management road,
Circulating nitrogen gas pipeline accesses heat exchanger, and nitrogen compressor is accessed after being picked out from heat exchanger；Circulating nitrogen gas pipeline goes out nitrogen
Heat exchanger is accessed after air compressor again, two tributaries are divided into after being picked out from heat exchanger, one tributary g accesses heat exchanger again, from changing
Hot device takes back nitrogen compressor after picking out, another tributary h passes through domethanizing column, and accesses heat exchanger, picks out and is followed by from heat exchanger
Return nitrogen compressor；
Raw material air pipe enters molecular sieve absorbing unit, and after going out molecular sieve absorbing unit, raw material air pipe accesses heat exchanger,
Domethanizing column is passed through after being picked out from heat exchanger and is accessed heat exchanger again, then picked out from heat exchanger and is accessed hydrogen flash tank；
The lower part of hydrogen flash tank passes through gas phase point by liquid phase separation object piping connection flash column, hydrogen flash tank top
Heat exchanger is accessed from property management road, pressure swing adsorption hydrogen production unit is accessed after being picked out from heat exchanger；
The liquid phase separation property management road of flash column lower part is divided into two tributaries, and one tributary e accesses heat exchanger, picked out from heat exchanger
It is followed by back flash column, another tributary f accesses domethanizing column；Heat exchanger is accessed in flash column top by gas phase isolate pipeline, from
Heat exchanger, which goes out to produce battery limit (BL) after picking out, obtains flashed vapour；
Heat exchanger is accessed in the lower part of domethanizing column by liquid phase separation property management road, goes out to produce battery limit (BL) after picking out from heat exchanger and obtains
Methane gas product；Heat exchanger is accessed in domethanizing column top by gas phase isolate pipeline, goes out to produce battery limit (BL) after picking out from heat exchanger
Obtain carbon monoxide product gas.
Preferably, the molecular sieve absorbing unit includes at least absorbing unit switch valve group, production molecular sieve absorption
Device, regenerated molecular sieve absorber, regeneration gas heaters, regeneration gas cooler, absorbing unit switch valve group includes multiple
Switch valve；Raw material air pipe is divided into two tributaries in parallel after entering molecular sieve absorbing unit, and one tributary a passes through switch valve
It is filtered for unstripped gas with production molecular sieve adsorber, another tributary b passes through switch valve and regenerated molecular sieve absorber, is used for
Unstripped gas filtering is carried out when producing molecular sieve adsorber regeneration；
Regeneration air pipe enters regeneration gas heaters after entering molecular sieve absorbing unit production battery limit (BL), is then separately connected
Molecular sieve adsorber and regenerated molecular sieve absorber are produced, the regeneration gas of molecular sieve adsorber and regenerated molecular sieve absorber is produced
Outlet enters regeneration gas cooler by regenerating air pipe, then goes out to produce battery limit (BL).
Preferably, the production molecular sieve adsorber, regenerated molecular sieve absorber, regeneration gas heaters, regeneration gas
It is mounted on switch valve in pipeline between body cooler, production and regenerating molecular sieve are realized by the closing of switch valve
Automatically switch.
Preferably, the pressure swing adsorption hydrogen production unit includes at least the first hydrogen manufacturing production absorber, Hydrogen Unit switching
Valve group, hydrogen manufacturing regenerative adsorption device, the second hydrogen manufacturing produce absorber；Hydrogen Unit switch valve group includes multiple switch valves；
Hydrogen flash tank upper gaseous phase isolate pipeline is divided into parallel after heat exchanger enters pressure swing adsorption hydrogen production unit
Branched stream, for one tributary c in switch valve and hydrogen manufacturing production absorber, remaining tributary, an at least tributary d1 passes through switching
Valve and the second hydrogen manufacturing produce absorber, and an at least tributary d2 passes through switch valve and the first hydrogen manufacturing to produce absorber, each tributary
Converge and then goes out to produce battery limit (BL)；First hydrogen manufacturing produces under absorber, hydrogen manufacturing regenerative adsorption device and the second hydrogen manufacturing production absorber
Portion bottom is all connected with tail gas gas phase isolate pipeline, and each branch hydrogen production exhaust gas goes out to produce battery limit (BL) after converging；
Preferably, the first hydrogen manufacturing production absorber in the pressure swing adsorption hydrogen production unit, hydrogen manufacturing regenerative adsorption device, the
Be mounted on switch valve in the turnover pipeline of two hydrogen manufacturing production absorber, by the closing of switch valve realize hydrogen manufacturing production with
The automatic switchover of adsorbent reactivation
Using the utility model, the devices such as molecular sieve filtration, cryogenic separation, circularly cooling and pressure swing adsorption hydrogen production are carried out
Integration Design is produced using the process unit of a whole set of Highgrade integration, reduces investment in fixed assets, saved enterprise
Operating cost greatly improves the separative efficiency of unstripped gas, and carbon monoxide product purity is higher than 98.5%, in co-production of methane gas product
CH4+C2H6 contents are up to 99.7%, and hydrogen product gas purity is also up to 99.9%；In addition, the cryogenic separation system is by cryogen system
SAPMAC method and unstripped gas throttling effects of reduced temperature efficiently combine according to product requirement, improve the gross efficiency of device, reduce
Refrigerant cycle energy consumption；Simultaneity factor has recycled the available gas in unstripped gas, and three kinds of key components are all recycled and are used as product,
Reduce the periodic off-gases of downstream unit in this way, and byproduct has been obtained for device scene, increases income.
Description of the drawings
Fig. 1 is coal chemical industry synthesis gas cryogenic separation co-production of methane gas system schematic；
Fig. 2 is heat exchanger inlet port and outlet port distribution schematic diagram；
Fig. 3 is molecular sieve absorbing unit schematic diagram.
Fig. 4 is pressure swing adsorption hydrogen production cell schematics.
In figure, nitrogen compressor 1, heat exchanger 2, domethanizing column 3, flash column 4, hydrogen flash tank 5, absorbing unit switching valve
Door group 6, production molecular sieve adsorber 7, regenerated molecular sieve absorber 8, regeneration gas heaters 9, regeneration gas cooler 10, the
One hydrogen manufacturing produces absorber 11, Hydrogen Unit switch valve group 12, hydrogen manufacturing regenerative adsorption device 13, the second hydrogen manufacturing production absorber
14。
Specific implementation mode
As shown in figures 1-4, a kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system, it is characterised in that including nitrogen
Air compressor 1, heat exchanger 2, domethanizing column 3, flash column 4, hydrogen flash tank 5, molecular sieve absorbing unit, pressure swing adsorption hydrogen production
Unit, raw material air pipe, circulating nitrogen gas pipeline, gas phase isolate pipeline and liquid phase separation property management road, molecular sieve absorption
Unit includes absorbing unit switch valve group 6, production molecular sieve adsorber 7, regenerated molecular sieve absorber 8, regeneration gas heating
Device 9, regeneration gas cooler 10, the pressure swing adsorption hydrogen production unit include the first hydrogen manufacturing production absorber 11, Hydrogen Unit
Switch valve group 12, hydrogen manufacturing regenerative adsorption device 13, the second hydrogen manufacturing produce absorber 14；
Circulating nitrogen gas pipeline accesses heat exchanger 2 from the 11st feed inlet, and is picked out from the 7th discharge port, then accesses nitrogen
Compressor 1；Go out after nitrogen compressor 1 and access heat exchanger 2 from second charging aperture, and picked out from the 11st discharge port, is then divided into
Two tributaries, one direct current g accesses heat exchanger 2 from the 7th feed inlet, and is picked out from third discharge port, then takes back nitrogen compressor
1, another tributary h pass through domethanizing column 3, access heat exchanger 2 from the 9th feed inlet, and pick out from the 5th discharge port, then take back
Nitrogen compressor 1；
Raw material air pipe is divided into two tributaries in parallel after entering molecular sieve absorbing unit, and one tributary a passes through switch valve
With production molecular sieve adsorber 7, another tributary b passes through switch valve and regenerated molecular sieve absorber 8；Regeneration gas enters production circle
After area, regeneration gas heaters 9, regenerated molecular sieve absorber 8, regeneration gas cooler 10 and related switch valve are passed through,
Then go out to produce battery limit (BL)；Raw material air pipe goes out after molecular sieve absorbing unit accesses heat exchanger 2 from first charging aperture, from the 8th discharging
Mouth picks out, and accesses heat exchanger 2 from third feed inlet after domethanizing column 3, is then picked out from the tenth discharge port and access hydrogen
Flash tank 5；
By liquid phase separation object piping connection flash column 4, upper part detaches property management by gas phase for the lower part of hydrogen flash tank 5
Tetra- feed inlets of Lu Cong access heat exchanger 2, and are picked out from the first discharge port, then access pressure swing adsorption hydrogen production unit；
Gas phase isolate pipeline is divided into branched stream in parallel after entering pressure swing adsorption hydrogen production unit, and one tributary c is passed through and cut
Valve and hydrogen manufacturing production absorber 13 are changed, in remaining tributary, d1 passes through switch valve and the second hydrogen manufacturing to produce absorber 14, and d2 is worn
Switch valve and the first hydrogen manufacturing production absorber 11 are crossed, each tributary is converged and then goes out to produce battery limit (BL)；First hydrogen manufacturing produces absorber
11, the lower part of hydrogen manufacturing regenerative adsorption device 13 and the second hydrogen manufacturing production absorber 14 is all connected with tail gas gas phase isolate pipeline, each
Road goes out to produce battery limit (BL) after converging；
The liquid phase separation property management road of 4 lower part of flash column is divided into two tributaries, and one direct current e accesses heat exchanger from the 6th feed inlet
2, and picked out from the 9th discharge port, flash column 4 is then taken back, another tributary f accesses domethanizing column 3；4 top of flash column passes through gas
Five feed inlets of property management Lu Cong that are separated access heat exchanger 2, and are picked out from the second discharge port, then go out to produce battery limit (BL)；
Heat exchanger 2 is accessed in the lower part of domethanizing column 3 by ten feed inlets of liquid phase separation property management Lu Cong, and discharges from the 6th
Mouth picks out, and then goes out to produce battery limit (BL)；Upper part accesses heat exchanger 2 by gas phase isolate pipeline from the 8th feed inlet, and from the
Four discharge ports pick out, and then go out to produce battery limit (BL).
A kind of absorbing unit in the molecular sieve absorbing unit of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system is cut
Change valve group 6, production molecular sieve adsorber 7, regenerated molecular sieve absorber 8, regeneration gas heaters 9 and regeneration gas cooling
Device 10, is controlled by program, realizes the automatic switchover of production and regenerating molecular sieve.
A kind of first hydrogen manufacturing in the pressure swing adsorption hydrogen production unit of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system
Absorber 11, Hydrogen Unit switch valve group 12, hydrogen manufacturing regenerative adsorption device 13, the second hydrogen manufacturing production absorber 14 are produced, by journey
Sequence controls, and realizes the automatic switchover of hydrogen manufacturing production and adsorbent reactivation, and absorber total quantity is not less than three.
As shown in figures 1-4, a kind of process of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system, including with
Lower step：
1) liquid nitrogen enters heat exchanger 2 as circulating nitrogen gas from the 11st feed inlet, cold is provided for system, in heat exchanger
Go out heat exchanger 2 in 2 after re-heat, compressed into nitrogen compressor 1, is reentered from second charging aperture by compressed nitrogen
Heat exchanger 2 continues to provide cold；Circulating nitrogen gas goes out after heat exchanger 2 to be divided into two tributaries from the 11st discharge port, one direct current g from
7th feed inlet enters heat exchanger 2, and nitrogen compressor 1 is returned after re-heat and is compressed, another tributary h enters domethanizing column 3 and is
It provides cold, and then returning to nitrogen compressor 1 through 2 re-heat of heat exchanger is compressed；
2) after unstripped gas enters molecular sieve absorbing unit, enter production molecular sieve adsorber 7 by switch valve, it will wherein
Trace Methanol and carbon dioxide eliminating；Filtered unstripped gas enters heat exchanger 2 from first charging aperture and is used as hot-fluid, heat exchanger
As cold flow, hot-fluid is exchanging heat hydrogen-rich Process Gas, carbon monoxide, flashed vapour, methane gas product and circulating nitrogen gas in 2 with cold flow
Heat exchange is carried out in device 2, the unstripped gas after being condensed passes through domethanizing column 3 to carry out gas phase and liquid phase separation, and it is cold to remove part
Lime set body is then back to heat exchanger 2 and cools down again, enters back into hydrogen flash tank 5 and carries out carrying out gas phase and liquid phase separation；Regeneration gas
Into after production battery limit (BL), is heated by regeneration gas heaters 9, divided subsequently into regenerated molecular sieve absorber 8
Son sieve regeneration is passed through regeneration gas cooler 10 and is cooled down, then goes out to produce battery limit (BL) later；
3) the liquid phase separation object isolated from hydrogen flash tank 5 enters flash column 4 through liquid phase separation property management road；Upper part
Hydrogen-rich Process Gas 2 re-heat of heat exchanger is entered by gas phase isolate pipeline, subsequently into pressure swing adsorption hydrogen production unit, pass through
One hydrogen manufacturing produces absorber 11 and the second hydrogen manufacturing production absorber 14 is purified, and obtains hydrogen product；The hydrogen production exhaust gas of generation
Go out to produce battery limit (BL) and goes to next process；
4) the liquid phase separation object isolated from flash column 4 is divided into two tributaries, and one direct current e is changed from the return of the 6th feed inlet
Hot device 2 carries out re-heat, is then picked out from the 9th discharge port, is recycled into flash column 4；Another tributary f is through liquid phase separation property management road
Into domethanizing column 3；The flashed vapour of upper part enters 2 re-heat of heat exchanger by gas phase isolate pipeline, obtains flashed vapour product；
5) liquid methane isolated from domethanizing column 3 enters heat exchange by ten feed inlets of liquid phase separation property management Lu Cong
2 re-heat of device, obtains methane gas product；The CO gas of upper part is entered by gas phase isolate pipeline from the 8th feed inlet
2 re-heat of heat exchanger, obtains carbon monoxide product.
In a specific embodiment of the utility model, coal chemical industry synthesis gas cryogenic separation co-production of methane gas technique side
Method, the unstripped gas temperature are 25~35 DEG C, 2.8~3.5MPaG of pressure position, the molar percentage of Main Components, methane
It is 28~22, hydrogen is 55~62, and carbon monoxide is 19~24.
Before initial cycle nitrogen enters heat exchanger 2, temperature is -182 DEG C, pressure 0.4MPaG, after going out heat exchanger 2, temperature
It is 33 DEG C, pressure 0.2MPaG；The temperature of tributary h is -180 DEG C, pressure 3.06MPaG.It is described be condensed after raw material
Temperature is -110 DEG C when gas enters domethanizing column 3, pressure 3.08MPaG；When unstripped gas enters hydrogen flash tank 5 temperature be-
180 DEG C, pressure 3.05MPaG；5 operating temperature of hydrogen flash tank be -180 DEG C, in 5 top discharge of hydrogen flash tank, with mole
Percentages, hydrogen 91%, carbon monoxide 8.1%, methane 0.6%, nitrogen 0.3%；In bottom discharge, with Mole percent
Than meter, methane 51.7%, carbon monoxide 45%, hydrogen 3.8%, nitrogen 0.5%.
4 top discharge temperature of flash column is -162 DEG C, pressure 0.7MPaG, and component molar percentage is that methane is 8.7%,
Hydrogen is 11.8%, carbon monoxide 78.3%, nitrogen 1.2%；Bottom discharge temperature is -154 DEG C, pressure 0.72MPaG, main
It is 64.7% that want component molar percentage, which be methane, carbon monoxide 35%, nitrogen 0.3%.5 top of hydrogen flash tank
Discharge carbon monoxide 99%, nitrogen 1%, and bottom discharge temperature is -131 DEG C, pressure 0.65MPaG, methane 99.8%, an oxidation
Carbon 0.2%.
This is produced using the process unit of a whole set of Highgrade integration, is reduced investment in fixed assets, has been saved enterprise
Industry operating cost greatly improves the separative efficiency of unstripped gas, in addition, the cryogenic separation system by cryogen refrigeration recycle and unstripped gas
Throttling effects of reduced temperature efficiently combines according to product requirement, improves the gross efficiency of device, reduces refrigerant cycle energy consumption；
Simultaneity factor has recycled the available gas in unstripped gas, and three kinds of key components are all recycled and are used as product, under reducing in this way
The periodic off-gases of device are swum, and byproduct has been obtained for device scene, increase income.
Claims (5)
1. a kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system, it is characterised in that including nitrogen compressor（1）, heat exchange
Device（2）, domethanizing column（3）, flash column（4）, hydrogen flash tank（5）, molecular sieve absorbing unit, pressure swing adsorption hydrogen production unit, original
Expect air pipe, circulating nitrogen gas pipeline, gas phase isolate pipeline and liquid phase separation property management road,
Circulating nitrogen gas pipeline accesses heat exchanger（2）, from heat exchanger（2）Nitrogen compressor is accessed after picking out（1）；Circulating nitrogen gas pipeline
Go out nitrogen compressor（1）Access heat exchanger again afterwards（2）, from heat exchanger（2）It is divided into two tributaries after picking out, one tributary g connects again
Enter heat exchanger（2）, from heat exchanger（2）Nitrogen compressor is taken back after picking out（1）, another tributary h is across domethanizing column（3）, and connect
Enter heat exchanger（2）, from heat exchanger（2）Nitrogen compressor is taken back after picking out（1）；
Raw material air pipe enters molecular sieve absorbing unit, and after going out molecular sieve absorbing unit, raw material air pipe accesses heat exchanger（2）,
From heat exchanger（2）Domethanizing column is passed through after picking out（3）And heat exchanger is accessed again（2）, then from heat exchanger（2）It picks out and accesses
Hydrogen flash tank（5）；
Hydrogen flash tank（5）Lower part pass through liquid phase separation object piping connection flash column（4）, hydrogen flash tank（5）Top passes through
Gas phase isolate pipeline accesses heat exchanger（2）, from heat exchanger（2）Pressure swing adsorption hydrogen production unit is accessed after picking out；
Flash column（4）The liquid phase separation property management road of lower part is divided into two tributaries, and one tributary e accesses heat exchanger（2）, from heat exchanger
（2）It picks out and is followed by back flash column（4）, another tributary f accesses domethanizing column（3）；Flash column（4）Top detaches property management by gas phase
Heat exchanger is accessed on road（2）, from heat exchanger（2）Go out to produce battery limit (BL) after picking out and obtains flashed vapour；
Domethanizing column（3）Lower part pass through liquid phase separation property management road access heat exchanger（2）, from heat exchanger（2）Go out production after picking out
Battery limit (BL) obtains methane gas product；Domethanizing column（3）Heat exchanger is accessed in top by gas phase isolate pipeline（2）, from heat exchanger（2）It connects
Go out to produce battery limit (BL) after going out and obtains carbon monoxide product gas.
2. coal chemical industry synthesis gas cryogenic separation co-production of methane gas system according to claim 1, it is characterised in that described
Molecular sieve absorbing unit includes at least absorbing unit switch valve group（6）, production molecular sieve adsorber（7）, regenerated molecular sieve inhale
Adnexa（8）, regeneration gas heaters（9）, regeneration gas cooler（10）, absorbing unit switch valve group（6）It is cut including multiple
Change valve；Raw material air pipe, which enters after molecular sieve absorbing unit, is divided into two tributaries in parallel, one tributary a pass through switch valve and
Produce molecular sieve adsorber（7）It is filtered for unstripped gas, another tributary b passes through switch valve and regenerated molecular sieve absorber（8）,
For in production molecular sieve adsorber（7）Unstripped gas filtering is carried out when regeneration；
Regeneration air pipe enters regeneration gas heaters after entering molecular sieve absorbing unit production battery limit (BL)（9）, then it is separately connected
Produce molecular sieve adsorber（7）With regenerated molecular sieve absorber（8）, produce molecular sieve adsorber（7）It is adsorbed with regenerated molecular sieve
Device（8）Regeneration gas outlet by regeneration air pipe enter regeneration gas cooler（10）, then go out to produce battery limit (BL).
3. coal chemical industry synthesis gas cryogenic separation co-production of methane gas system according to claim 2, it is characterised in that described
Produce molecular sieve adsorber（7）, regenerated molecular sieve absorber（8）, regeneration gas heaters（9）, regeneration gas cooler（10）
Between pipeline in be mounted on switch valve, pass through switch valve closing realize production with regenerating molecular sieve automatically cut
It changes.
4. coal chemical industry synthesis gas cryogenic separation co-production of methane gas system according to claim 1, it is characterised in that described
Pressure swing adsorption hydrogen production unit includes at least the first hydrogen manufacturing and produces absorber（11）, Hydrogen Unit switch valve group（12）, hydrogen manufacturing again
Raw absorber（13）, the second hydrogen manufacturing produce absorber（14）；Hydrogen Unit switch valve group（12）Including multiple switch valves；
Hydrogen flash tank（5）Upper gaseous phase isolate pipeline is through heat exchanger（2）It is divided into parallel connection after into pressure swing adsorption hydrogen production unit
Branched stream, one tributary c pass through switch valve and hydrogen manufacturing regenerative adsorption device（13）, in remaining tributary, at least a tributary d1 is worn
Cross switch valve and the second hydrogen manufacturing production absorber（14）, an at least tributary d2 is across switch valve and the first hydrogen manufacturing production absorption
Device（11）, each tributary is converged and then goes out to produce battery limit (BL)；First hydrogen manufacturing produces absorber（11）, hydrogen manufacturing regenerative adsorption device（13）With
Two hydrogen manufacturing produce absorber（14）Bottom be all connected with tail gas gas phase isolate pipeline, each branch hydrogen production exhaust gas goes out production after converging
Battery limit (BL).
5. coal chemical industry synthesis gas cryogenic separation co-production of methane gas system according to claim 1, the pressure-variable adsorption system
The first hydrogen manufacturing in hydrogen unit produces absorber（11）, hydrogen manufacturing regenerative adsorption device（13）, the second hydrogen manufacturing produce absorber（14）'s
It is mounted on switch valve in turnover pipeline, realizes that hydrogen manufacturing production and the automatic of adsorbent reactivation are cut by the closing of switch valve
It changes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820323887.1U CN208042615U (en) | 2018-03-09 | 2018-03-09 | A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820323887.1U CN208042615U (en) | 2018-03-09 | 2018-03-09 | A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108253729A (en) * | 2018-03-09 | 2018-07-06 | 杭州中泰深冷技术股份有限公司 | A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system and its process |
| CN109812703A (en) * | 2019-03-12 | 2019-05-28 | 中冶焦耐(大连)工程技术有限公司 | It is a kind of to utilize self-produced hydrogen more than needed for Recovery of Seal Oil oil depot tail gas process |
-
2018
- 2018-03-09 CN CN201820323887.1U patent/CN208042615U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108253729A (en) * | 2018-03-09 | 2018-07-06 | 杭州中泰深冷技术股份有限公司 | A kind of coal chemical industry synthesis gas cryogenic separation co-production of methane gas system and its process |
| CN108253729B (en) * | 2018-03-09 | 2023-09-19 | 杭州中泰深冷技术股份有限公司 | System for cryogenic separation co-production of methane gas from coal chemical synthesis gas and process method thereof |
| CN109812703A (en) * | 2019-03-12 | 2019-05-28 | 中冶焦耐(大连)工程技术有限公司 | It is a kind of to utilize self-produced hydrogen more than needed for Recovery of Seal Oil oil depot tail gas process |
| CN109812703B (en) * | 2019-03-12 | 2023-11-28 | 中冶焦耐(大连)工程技术有限公司 | Process for recycling tail gas of oil depot by using self-produced surplus hydrogen as seal |
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