CN205784230U - High purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane - Google Patents
High purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane Download PDFInfo
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- CN205784230U CN205784230U CN201620494223.2U CN201620494223U CN205784230U CN 205784230 U CN205784230 U CN 205784230U CN 201620494223 U CN201620494223 U CN 201620494223U CN 205784230 U CN205784230 U CN 205784230U
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- pipeline
- heat exchanger
- main heat
- tower
- methane
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 174
- 239000007789 gas Substances 0.000 title claims abstract description 74
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 38
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 35
- 239000001257 hydrogen Substances 0.000 title claims abstract description 35
- 239000007788 liquid Substances 0.000 title claims abstract description 34
- 229910002091 carbon monoxide Inorganic materials 0.000 title claims abstract description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 40
- 239000006200 vaporizer Substances 0.000 claims abstract description 40
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 20
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 239000007791 liquid phase Substances 0.000 claims description 26
- 239000012071 phase Substances 0.000 claims description 23
- 239000007792 gaseous phase Substances 0.000 claims description 19
- 238000005406 washing Methods 0.000 claims description 9
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 8
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 8
- 239000002912 waste gas Substances 0.000 claims description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 4
- 239000005977 Ethylene Substances 0.000 claims description 4
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 4
- 239000001294 propane Substances 0.000 claims description 4
- 238000005219 brazing Methods 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 3
- 239000000284 extract Substances 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims 1
- 238000009833 condensation Methods 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 18
- 238000000926 separation method Methods 0.000 abstract description 10
- 239000012535 impurity Substances 0.000 abstract description 8
- 238000000605 extraction Methods 0.000 abstract description 3
- 238000001816 cooling Methods 0.000 description 15
- 238000005057 refrigeration Methods 0.000 description 9
- 239000000203 mixture Substances 0.000 description 8
- 239000000463 material Substances 0.000 description 5
- 238000002309 gasification Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000519996 Teucrium chamaedrys Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
This utility model relates to gas low temperature separation field, particularly to a kind of high purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane, this system mainly includes raw material gas purifying unit, low-temperature liquefaction separative element, CO product compressor and azeotrope compressor；Described low-temperature liquefaction separative element includes main heat exchanger, washes methane tower, dehydrogenation tower, domethanizing column and denitrification column, it is provided with the first vaporizer at the bottom of described dehydrogenation tower tower, be provided with the second vaporizer at the bottom of described demethanizer, tower top is provided with the first condenser, be provided with the 3rd vaporizer at the bottom of described denitrification column tower, tower top is provided with the second condenser, and this utility model obtains highly purified rich H by this four-column process flow2While CO product, high-purity liquid methane can be obtained, adaptable to unstripped gas of device, reduce the device requirement to unstripped gas impurity, according to the pressure of CO product gas, circulate the low-temperature receiver as rectifying column and thermal source from final stage or the intergrade a part of CO of extraction of CO compressor, eliminate nitrogen compressor and decompressor, equipment is less, invests little.
Description
Technical field
This utility model relates to gas low temperature separation field, particularly to a kind of high purity carbon monoxide and hydrogen rich gas connection
Produce the system of liquid methane.
Background technology
CO and H2It is the important synthesis material of chemical process, is widely used in a series of Organic chemical products and intermediate
Synthesis, and CO and H2Produce general with coal, natural gas or oil as raw material, obtain through certain method conversion, producing
Except producing active component CO and H in journey2Outward, a certain amount of CH is also produced4, N2、CO2Exist as a mixture Deng impurity,
Chemical industry building-up process typically requires highly purified CO, and this is accomplished by suitable method and is mixed thing separating-purifying.
CO and H2Separation method mainly have pressure swing adsorption method, membrane separation process and cryogenic rectification partition method.Membrane separating method
Owing to the price of efficient selective film is high, apply less.Pressure swing adsorption method is generally used for midget plant, and flexible operation is reliable, but
Be as chemical field maximize development, pressure-variable adsorption process extensive gas load time, equipment is many, floor space is big and
Operating cost is high.Low temperature processing is to utilize the difference of physical property between component, carries out separating-purifying by the method for cryogenic rectification,
It is usually used in CO and H in large-size chemical field2Mixed gas separating-purifying.
Liquid methane is that a kind of cleaning, the efficient energy, and calorific value height are readily transported, CO and H disclosed in China2Low
In temperature process for separation and purification, simply consider CO and H2Carry out separating-purifying, in the case of nitrogen, methane content are higher, methane
Discharging as fuel with other impurity, the value of methane does not obtain Appropriate application, and Application No.
201510014562.6, the China of the method and apparatus of entitled a kind of synthesis gas separation hydrogen making and high-purity CO is specially
Profit, in the case of impurity content is more complicated, uses multitower to separate, and however it is necessary that increase nitrogen circulation compression and decompressor, flow process
Complexity, machine is more, and energy consumption is high, and does not has to propose the Appropriate application to methane.The market of LNG is preferable in recent years, at CO and
H2Higher liquid methane can be worth with production economy while separation, increase value-added content of product, thus improve the whole of device
Body economic benefit.
Summary of the invention
The purpose of this utility model is to overcome above-mentioned deficiency of the prior art, when the impurity nitrogen in unstripped gas, first
When alkane content is higher, it is provided that a kind of energy-efficient high purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane, this
Utility model, while producing high-purity CO and hydrogen rich gas, can obtain the liquid methane that economic worth is high.
The technical solution of the utility model is achieved in that a kind of high purity carbon monoxide and hydrogen rich gas coproduction liquid
The system of methane, this system mainly includes raw material gas purifying unit, low-temperature liquefaction separative element, CO product compressor and mixes cold
Agent compressor；Described low-temperature liquefaction separative element includes main heat exchanger, washes methane tower, dehydrogenation tower, domethanizing column and denitrification column,
It is provided with the first vaporizer at the bottom of described dehydrogenation tower tower, is provided with the second vaporizer at the bottom of the tower of described domethanizing column, tower top is provided with first
Condenser, is provided with the 3rd vaporizer at the bottom of described denitrification column tower, tower top is provided with the second condenser；The entrance of described clean unit is even
Logical the first pipeline supplied gas, the outlet of described clean unit is connected with main heat exchanger by second pipe；The described methane tower washed
Lower entrances is connected with described main heat exchanger by the 3rd pipeline, described in wash methane tower top gas phase export by the 4th pipe
Road is connected with main heat exchanger, and the 5th pipeline of hydrogen rich gas is sent in the connection of described primary heat exchanger warm end, described in wash the end of methane tower
Portion's liquid-phase outlet passes through the 6th pipeline communication first throttle valve；Described first throttle valve passes through the 7th pipeline communication main heat exchanger,
Described main heat exchanger is connected by the centre entrance of the 8th pipeline with described dehydrogenation tower, and described first throttle valve is by the 9th pipe
Road is connected with the upper entrance of described dehydrogenation tower；Described dehydrogenation top of tower gaseous phase outlet is by the tenth pipeline and described main heat exchange
Device connects, and the 11st pipeline of flash steam is sent in the connection of described primary heat exchanger warm end；The bottom liquid phases outlet of described dehydrogenation tower is logical
Crossing the 12nd pipeline to be connected with second throttle, described second throttle is connected with described main heat exchanger by the 13rd pipeline
Logical, described main heat exchanger is connected with described domethanizing column lower entrances by the 14th pipeline, and described second throttle is passed through
15th pipeline is connected with described main heat exchanger, and described main heat exchanger is entered in the middle part of described domethanizing column by the 16th pipeline
Mouth is connected；Described demethanizer bottom liquid-phase outlet is connected with described main heat exchanger by the 17th pipeline, and described master changes
The 18th pipeline of liquid methane is sent in the connection of hot device hot junction；The top gas phase of described domethanizing column exports by the 19th pipeline
Being connected with the 26th pipeline, the upper gaseous phase outlet of described domethanizing column is by the 20th pipeline and denitrification column centre entrance
Being connected, top first condensator outlet of described domethanizing column is de-with described through the 3rd choke valve by the 21st pipeline
The entrance of nitrogen top of tower the second condenser is connected；Bottom liquid phases outlet the 22nd pipeline of described denitrification column, second
Arranging the 4th choke valve on 12 pipelines, described 4th choke valve is by the top second of the 23rd pipeline with described denitrification column
Condenser inlet connects, and the upper gaseous phase outlet of described denitrification column is connected with described main heat exchanger by the 24th pipeline, institute
State primary heat exchanger warm end connection and send the 25th pipeline of waste gas；The top gas phase of described denitrification column exports by the 26th
Pipeline connects with described main heat exchanger, and described main heat exchanger produces mouth suction port of compressor phase by the 27th pipeline with described CO
Connection.
Described CO product compressor is connected with described main heat exchanger by the 28th pipeline, and described main heat exchanger passes through
29th pipeline is connected with the first evaporator inlet at the bottom of described dehydrogenation tower tower, the 29th pipeline and the 30th pipeline phase
Logical, entrance connection the 30th pipeline of the second vaporizer at the bottom of described demethanizer, outlet the 31st pipeline, the 30th
One pipeline and the 32nd pipeline are connected, and described first evaporator outlet passes through the 32nd pipeline and described main heat exchanger phase
Connection, described main heat exchanger is connected with described methane tower upper entrance of washing by the 33rd pipeline；Described first condenser
Entrance connection the 34th pipeline, the 34th pipeline is respectively communicated with the 33rd pipeline and the 35th pipeline, and the 35th
Pipeline connects with described main heat exchanger, and described main heat exchanger is by the 36th pipeline and described CO product compressor centre entrance
Being connected, described CO product compressor centre exit is connected with described main heat exchanger by the 37th pipeline, and described master changes
Hot device is connected with the 3rd evaporator inlet bottom described denitrification column by the 38th pipeline, and described 3rd evaporator outlet leads to
Crossing the 39th pipeline and the 5th choke valve is connected, described 5th choke valve and the 23rd pipeline are connected, and described CO produces
Product compressor outlet connection the 45th pipeline.
The gaseous phase outlet of described azeotrope compressor is connected with described main heat exchanger by the 40th pipeline, described
Main heat exchanger is connected with described main heat exchanger through the 6th choke valve by the 41st pipeline, and described main heat exchanger passes through the 4th
12 pipelines are connected with azeotrope suction port of compressor；Described azeotrope compressor liquid-phase outlet passes through the 43rd pipeline
Being connected with described main heat exchanger, described main heat exchanger passes through the 44th pipeline through the 7th choke valve and described main heat exchanger phase
Connection.
Described main heat exchanger, described first vaporizer, described second vaporizer, described 3rd vaporizer, described first cold
Condenser and described second condenser are vacuum brazing plate-fin heat exchanger, described in wash methane tower, dehydrogenation tower, domethanizing column, de-
Nitrogen tower is regular packed tower or filler and float valve combination type rectifying column.
Described CO product compressor delivery pressure is: 0.5 MPa ~ 3.5MPa；Described CO product compressor is used for circulation portions
Point extract out pressure be: 0.5MPa ~ 3.5MPa.
Described clean unit inlet pressure is: 3.0MPa ~ 6.0MPa, and methane content volume fraction is 0.5% ~ 10%, nitrogen
Content volume mark is 4% ~ 8%；Described dehydrogenation pressure tower is 0.9MPa ~ 2.5MPa；Described domethanizing column and denitrification column pressure
Power is 0.2MPa ~ 0.6MPa.
Azeotrope uses nitrogen, methane, ethylene, propane and isopentane to mix according to a certain percentage.
A kind of high purity carbon monoxide and the method for hydrogen rich gas coproduction liquid methane, the method is as follows:
High nitrogen, the raw material of methane content enter clean unit through the first pipeline, by the adsorbent in clean unit
By the trace amounts of CO in unstripped gas after absorption2Removing with water, the unstripped gas after imurity-removal enters main heat exchanger by second pipe
Be cooled to uniform temperature, after cooling by the 3rd pipeline enter described in wash methane tower by the methane wash in raw material out,
Washing methane top of tower gaseous phase outlet and obtain hydrogen rich gas, hydrogen rich gas enters main heat exchanger by the 4th pipeline and reclaims cold re-heat,
Sent by the 5th pipeline after hydrogen rich gas re-heat, washing the raw material after methane tower bottom liquid-phase outlet obtains methane concentration by the
Six pipelines throttle through first throttle valve, are divided into two parts after throttling, and a part enters main heat exchanger re-heat by the 7th pipeline, multiple
Entering in the middle part of dehydrogenation tower through the 8th pipeline after heat, another part is directly accessed dehydrogenation tower upper entrance by the 9th pipeline, de-
Carrying out rectification separation in hydrogen tower, obtain flash steam at dehydrogenation top of tower gaseous phase outlet, flashed vapour enters main changing by the tenth pipeline
Hot device reclaims cold re-heat, is sent by the 11st pipeline, entered at dehydrogenation tower bottom liquid-phase outlet after flashed vapour re-heat
Raw material after one step concentrates is throttled through second throttle by the 12nd pipeline, is divided into two parts after throttling, and a part is by the
13 pipelines enter main heat exchanger re-heat, enter domethanizing column lower entrances through the 14th pipeline after re-heat, and another part passes through
15th pipeline enters main heat exchanger and is cooled to uniform temperature, enters to enter in the middle part of domethanizing column by the 16th pipeline after cooling
Mouthful, obtaining high-purity liquid methane at demethanizer bottom liquid-phase outlet, liquid methane enters main heat exchange by the 17th pipeline
Device is supercool, supercool after send by the 18th pipeline, obtain certain density CO in the outlet of domethanizing column upper gaseous phase and pass through the
20 pipelines enter denitrification column centre entrance, further imurity-removal in denitrification column, obtain in the outlet of denitrification column bottom liquid phases
High-purity CO is throttled through the 4th choke valve by the 22nd pipeline, enters denitrification column top by the 23rd pipeline after throttling
Second condenser inlet, as low-temperature receiver, obtains rich nitrogen waste gas in the outlet of denitrification column upper gaseous phase, and waste gas is by the 24th pipe
Road enters main heat exchanger re-heat and reclaims cold, after re-heat, is sent by the 25th pipeline.
The cold of device provides mainly by CO circulation throttling and refrigerant cycle throttling refrigeration, goes out from CO product compressor
A part of CO of mouth enters main heat exchanger by the 28th pipeline and is cooled to uniform temperature, respectively by the 29th after cooling
Pipeline and the 30th pipeline enter the second vaporizer at the bottom of dehydrogenation tower bottom the first vaporizer, demethanizer, make in vaporizer
It is cooled for thermal source, mixes after cooling and enter main heat exchanger continuation cooling by the 32nd pipeline, after cooling, be divided into three parts,
A part is entered by the 33rd pipeline and washes methane tower, as cleaning mixture by the methane wash in raw material out, and another part
Demethanizer overhead the first condenser is entered as low-temperature receiver by re-heat partial gasification, at the first condenser by the 34th pipeline
Top is obtained gas phase CO and is mixed by the 19th pipeline and the 26th pipeline gas phase, obtains liquid phase CO at the first condenser lower curtate
After the 3rd choke valve throttles, enter denitrification column the second condenser by the 21st pipeline to pass through as low-temperature receiver, last part
35th pipeline returns main heat exchanger re-heat and reclaims cold, enters CO product by the 36th pipeline and compress after reclaiming cold
Machine centre entrance, extracts a part out and enters main heat exchanger cooling by the 37th pipeline, after cooling in the middle part of CO product compressor
Enter denitrification column the 3rd vaporizer by the 38th pipeline to be cooled as thermal source, by the 39th pipeline through the after cooling
Five choke valves and the 23rd pipeline material mix mutually, enter denitrification column the second condenser, make in the second condenser after mixing
Being obtained CO product for low-temperature receiver by re-heat gasification, CO product enters main heat exchanger re-heat by the 26th pipeline and reclaims cold, returns
Enter CO product suction port of compressor after receiving cold to be compressed to certain pressure being sent as product by the 45th pipeline；Come
Enter main heat exchanger from the gas phase cryogen of azeotrope compressor by the 40th pipeline to cool down, be cooled to uniform temperature
Afterwards by the 41st pipeline through the 6th choke valve throttling refrigeration, backflow entrance main heat exchanger, from azeotrope compressor
Liquid phase cryogen enters main heat exchanger by the 43rd pipeline and is cooled to uniform temperature extraction, by the 44th pipeline through the 7th
Choke valve throttling refrigeration, backflow after throttling refrigeration entrance main heat exchanger, sends main heat exchanger with another burst of cryogen mixing re-heat, logical
Cross the 42nd pipeline and enter azeotrope compressor, complete kind of refrigeration cycle.
The good effect that the technical solution of the utility model produces is as follows: for height containing nitrogen, methane feed gas, by this
Four-column process flow obtains highly purified rich H2While CO product, can obtain high-purity liquid methane, CO purity reaches volume
Mark more than 99%, liquid methane purity volume content reaches more than 98%, and impurity removal is clean, and H2, CO and the recovery of methane
Rate is high, H2With the response rate more than 99% of methane, the CO response rate more than 88%, adaptable to unstripped gas of device, reduce
The device requirement to unstripped gas impurity.
This utility model produces the system of hydrogen rich gas and carbon monoxide on the premise of not increase equipment from unstripped gas, according to
The pressure of CO product gas, circulates the low-temperature receiver as rectifying column and heat from final stage or the intergrade a part of CO of extraction of CO compressor
Source, eliminates nitrogen compressor and decompressor, and equipment is less, invests little.
This utility model liquid methane that production economy added value is high while high purity carbon monoxide and hydrogen rich gas,
Be provided with single azeotrope refrigeration system, increase equipment azeotrope compressor, but mix refrigerant mainly by nitrogen,
The materials such as methane, ethylene, propane, isopentane configure a certain proportion of cryogen according to the different compositions of unstripped gas and mix, system
Cold energy consumption is low.
Accompanying drawing explanation
Fig. 1 is the structural representation of the system of this utility model high purity carbon monoxide and hydrogen rich gas coproduction liquid methane
Figure.
Figure is labeled as: 1, azeotrope compressor；2, raw material gas purifying unit；3, CO product compressor；4, Low Temperature Liquid
Change separative element；5, main heat exchanger；6, methane tower is washed；7, dehydrogenation tower；8, domethanizing column；9, denitrification column；10, the first vaporizer；
11, the second vaporizer；12, the 3rd vaporizer；13, the first condenser；14, the second condenser；15, the 7th choke valve；16, the 6th
Choke valve, 17, first throttle valve；18, second throttle；19, the 3rd choke valve；20, the 5th choke valve；21, the 4th choke valve；
100, the first pipeline；101, second pipe；102, the 3rd pipeline；103, the 4th pipeline；104, the 5th pipeline；105, the 6th pipe
Road；106, the 7th pipeline；107, the 8th pipeline；108, the 9th pipeline；109, the tenth pipeline；110, the 11st pipeline；111,
12 pipelines；112, the 13rd pipeline；113, the 14th pipeline；114, the 15th pipeline；115, the 16th pipeline；116, the tenth
Seven pipelines；117, the 18th pipeline；118, the 19th pipeline；119, the 20th pipeline；120, the 21st pipeline；121, second
12 pipelines；122, the 23rd pipeline；123, the 24th pipeline；124, the 25th pipeline；125, the 26th pipeline；
126, the 27th pipeline；127, the 28th pipeline；128, the 29th pipeline；129, the 30th pipeline；130, the 30th
One pipeline；131, the 32nd pipeline；132, the 33rd pipeline；133, the 34th pipeline；134, the 35th pipeline；
135, the 36th pipeline；136, the 37th pipeline；137, the 38th pipeline；138, the 39th pipeline；139, the 4th
Ten pipelines；140, the 41st pipeline；141, the 42nd pipeline；142, the 43rd pipeline；143, the 44th pipeline；
144, the 45th pipeline.
Detailed description of the invention
Below in conjunction with specific embodiment, the present invention is further elaborated.
Embodiment one
As it is shown in figure 1, a kind of high purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane, this system is mainly wrapped
Include raw material gas purifying unit 2, low-temperature liquefaction separative element 4, CO product compressor 3, azeotrope compressor 1；Described low temperature
Liquefaction separative element includes main heat exchanger 5, washes methane tower 6, dehydrogenation tower 7, domethanizing column 8, denitrification column 9, described dehydrogenation tower tower
The end, is provided with the first vaporizer 10, is provided with the second vaporizer 11, tower top is provided with the first condenser 13, institute at the bottom of described demethanizer
Be provided with the 3rd vaporizer 12 at the bottom of the denitrification column tower stated, tower top is provided with the second condenser 14；Described clean unit 2 entrance connection the
One pipeline 100, the outlet of described clean unit is connected with main heat exchanger 5 by second pipe 101；Described wash methane tower 6 times
Portion's entrance is connected with described main heat exchanger 5 by the 3rd pipeline 102, washes methane top of tower gaseous phase outlet by the 4th pipeline
103 are connected with main heat exchanger 5, and main heat exchanger 5 connects with the 5th pipeline 104, wash methane tower bottom liquid-phase outlet by the 6th
Pipeline 105 is connected with first throttle valve 17；First throttle valve 17 is connected with main heat exchanger 5 by the 7th pipeline 106, and master changes
Hot device 5 is connected with described dehydrogenation tower 7 centre entrance by the 8th pipeline 107, and first throttle valve 17 is by the 9th pipeline 108
It is connected with described dehydrogenation tower 7 upper entrance；The outlet of described dehydrogenation tower 7 top gas phase is by the tenth pipeline 109 and main heat exchanger 5
Being connected, main heat exchanger 5 is connected with the 11st pipeline 110, and dehydrogenation tower bottom liquid-phase outlet is by the 12nd pipeline 111 and the
Two choke valves 18 are connected；Second throttle 18 is connected with main heat exchanger 5 by the 13rd pipeline 112, and main heat exchanger 5 passes through
14th pipeline 113 is connected with domethanizing column 8 lower entrances, and second throttle 18 is by the 15th pipeline 114 and main heat exchange
Device 5 is connected, and main heat exchanger 5 is connected with domethanizing column 8 centre entrance by the 16th pipeline 115；Described domethanizing column 8 end
Portion's liquid-phase outlet is connected with main heat exchanger 5 by the 17th pipeline 116, and main heat exchanger 5 is connected with the 18th pipeline 117,
The outlet of domethanizing column 8 top gas phase is connected with the 26th pipeline 125 by the 19th pipeline 118, domethanizing column 8 top gas
Exporting mutually and be connected with denitrification column 9 centre entrance by the 20th pipeline 119, domethanizing column 8 top the first condenser 13 exports
It is connected with denitrification column 9 top the second condenser 14 entrance through the 3rd choke valve 19 by the 21st pipeline 120；Described de-
The outlet of nitrogen tower 9 bottom liquid phases is connected with the 4th choke valve 21 by the 22nd pipeline 121, and the 4th choke valve 21 is by second
13 pipelines 122 connect with denitrification column 9 top the second condenser 14 entrance, and the outlet of denitrification column upper gaseous phase is by the 24th pipe
Road 123 connects with main heat exchanger 5, and main heat exchanger 5 connects with the 25th pipeline 124, and the outlet of denitrification column top gas phase is by the
26 pipelines 125 connect with main heat exchanger 5, and main heat exchanger 5 produces mouth compressor by the 27th pipeline 126 with described CO
3 entrances are connected.
Described CO product compressor 3 is connected with main heat exchanger 5 by the 28th pipeline 127, and main heat exchanger 5 passes through the
29 pipelines 128 are connected with the first vaporizer 10 entrance at the bottom of described dehydrogenation tower 7 tower, and the 29th pipeline 128 is by the 3rd
Ten pipelines 129 are connected with the second vaporizer 11 entrance at the bottom of demethanizer, and the second vaporizer 11 exports by the 31st pipe
Road 130 is connected with the 32nd pipeline 131, and the first vaporizer 10 exports by the 32nd pipeline 132 and main heat exchanger 5 phase
Connection, main heat exchanger 5 is connected with washing methane tower 6 upper entrance by the 33rd pipeline 132, and the first condenser 13 entrance leads to
Crossing the 34th pipeline 133 to be connected with the 33rd pipeline 132, main heat exchanger passes through the 35th pipeline 134 and the 30th
Four pipelines 133 are connected, and main heat exchanger 5 is connected with CO product compressor 3 centre entrance by the 36th pipeline 135, CO
Product compressor 3 centre exit is connected with main heat exchanger 5 by the 37th pipeline 136, and main heat exchanger 5 is by the 38th
Pipeline 137 is connected with the 3rd vaporizer 12 entrance bottom denitrification column 9, and the 3rd vaporizer 12 exports by the 39th pipeline
138 are connected with the 23rd pipeline 122 through the 5th choke valve 20, the outlet of described CO product compressor 3 and the 45th pipe
Road 144 is connected.
Described azeotrope compressor 1 gaseous phase outlet is connected with main heat exchanger 5 by the 40th pipeline 139, and master changes
Hot device 5 is connected with main heat exchanger 5 through the 6th choke valve 16 by the 41st pipeline 140, and main heat exchanger 5 is by the 42nd
Pipeline 141 is connected with azeotrope compressor 1 entrance, completes circulation, and azeotrope compressor 1 liquid-phase outlet passes through the 40th
Three pipelines 142 are connected with main heat exchanger 5, and main heat exchanger 5 passes through the 44th pipeline 143 through the 7th choke valve 15 and main heat exchange
Device 5 is connected.
Described main heat exchanger 5, described first vaporizer 10, described second vaporizer 11, described 3rd vaporizer 12, described
First condenser 13 and described second condenser 14 are vacuum brazing plate-fin heat exchanger, described in wash methane tower 6, dehydrogenation tower 7,
Domethanizing column 8, denitrification column 9 are regular packed tower or filler and float valve combination type rectifying column.
Embodiment two
A kind of high purity carbon monoxide and the method for hydrogen rich gas coproduction liquid methane, methane volumetric content is 0.5% ~
10%, nitrogen volume content is that to be 3.0MPa ~ 6.0MPa enter clean unit through the first pipeline to the raw gas pressure of 4% ~ 8%, logical
Cross the trace amounts of CO in unstripped gas after the adsorbent in clean unit2Removing with water, the unstripped gas after imurity-removal passes through
Second pipe enter main heat exchanger be cooled to ~ 100K, after cooling by the 3rd pipeline enter described in wash methane tower by raw material
Methane wash out, obtain the hydrogen rich gas that hydrogen volume content is more than 77%, hydrogen rich gas washing methane top of tower gaseous phase outlet
Enter main heat exchanger by the 4th pipeline and reclaim cold re-heat, sent by the 5th pipeline after hydrogen rich gas re-heat and obtain hydrogen rich gas
Product, in washing methane tower, methane is washed down, and the hydrogen rich gas methane losses of tower top is few, is washing methane tower bottom liquid-phase outlet
Obtain methane and be concentrated into raw material that volume content is about 16% by the 6th pipeline through first throttle valve throttling refrigeration, throttling
Rear pressure is 0.9MPa ~ 2.5MPa, is divided into two parts after throttling, a part by the 7th pipeline enter main heat exchanger re-heat to ~
118K, enters in the middle part of dehydrogenation tower through the 8th pipeline after re-heat, and another part is directly accessed dehydrogenation tower top by the 9th pipeline and enters
Mouthful, in dehydrogenation tower, carry out rectification separation, obtain, at dehydrogenation top of tower gaseous phase outlet, the flash distillation that hydrogen volume content is more than 63%
Vapour, flashed vapour is entered main heat exchanger by the tenth pipeline and reclaims cold re-heat, made by the 11st pipeline after flashed vapour re-heat
Send for flashed vapour product, the raw material after dehydrogenation tower bottom liquid-phase outlet is concentrated further by the 12nd pipeline through the
Two choke valves throttle to 0.2MPa ~ 0.6MPa, are divided into two parts after throttling, and a part enters main heat exchange by the 13rd pipeline
Device re-heat, to ~ 132K, enters domethanizing column lower entrances through the 14th pipeline after re-heat, and another part is entered by the 15th pipeline
Enter main heat exchanger and be cooled to ~ 99K, enter domethanizing column centre entrance by the 16th pipeline after cooling, enter in domethanizing column
Methane in row rectification separation removal raw material, obtains methane volumetric content more than 98% at demethanizer bottom liquid-phase outlet
High-purity liquid methane, liquid methane enters supercool 2 K of main heat exchanger ~ 3K by the 17th pipeline, supercool rear by the 18th
Pipeline is sent as liquid methane product, obtains, in the outlet of domethanizing column upper gaseous phase, the raw material that CO volume content is more than 92%
Enter denitrification column centre entrance by the 20th pipeline, in denitrification column, remove Nitrogen gas impurity further, in denitrification column bottom liquid
Outlet obtains the high-purity CO that CO volume content is more than 99% and passes through the 22nd pipeline through the 4th choke valve throttling extremely mutually
0.15MPa ~ ~ 0.19MPa, enters denitrification column top the second condenser inlet as low-temperature receiver quilt by the 23rd pipeline after throttling
Re-heat is gasified, and obtains, in the outlet of denitrification column upper gaseous phase, the rich nitrogen waste gas that nitrogen volume content is more than 82%, and waste gas passes through second
14 pipelines enter main heat exchanger re-heat and reclaim cold, after re-heat, are sent by the 25th pipeline.
The cold of device provides mainly by CO circulation throttling and refrigerant cycle throttling refrigeration, goes out from CO product compressor
A part of CO pressure of mouth is that 0.5MPa ~ 3.5MPa is cooled to 145K ~ 160K by the 28th pipeline entrance main heat exchanger, cold
The most respectively by the bottom of the 29th pipeline and the 30th pipeline entrance dehydrogenation tower bottom the first vaporizer, demethanizer second
Vaporizer, is cooled as thermal source in vaporizer, mixes and continue cold by the 32nd pipeline entrance main heat exchanger after cooling
But to ~ 100K, being divided into three parts after cooling, a part is entered by the 33rd pipeline and washes methane tower, as cleaning mixture by former
Out, another part enters demethanizer overhead the first condenser as low-temperature receiver by the 34th pipeline to methane wash in material
By re-heat partial gasification, obtain gas phase CO in the first condenser overhead and mixed by the 19th pipeline and the 26th pipeline gas phase
Close, obtain liquid phase CO at the first condenser lower curtate and after the 3rd choke valve throttles, enter denitrification column second by the 21st pipeline
Condenser is as low-temperature receiver, and last part returns main heat exchanger re-heat by the 35th pipeline and reclaims cold, after reclaiming cold
Entering CO product compressor centre entrance by the 36th pipeline, extracting a part of CO pressure in the middle part of CO product compressor out is
0.5MPa ~ 3.5MPa enters main heat exchanger by the 37th pipeline and is cooled to 118K ~ 125K, by the 38th pipe after cooling
Road enters denitrification column the 3rd vaporizer and is cooled as thermal source, is throttled extremely through the 5th choke valve by the 39th pipeline after cooling
0.15MPa ~ ~ 0.19MPa and the 23rd pipeline material mix mutually, enter denitrification column the second condenser after mixing, cold second
Being obtained, by re-heat gasification, the CO product that CO volume content is more than 99% as low-temperature receiver in condenser, CO product is by the 26th pipe
Road enters main heat exchanger re-heat and reclaims cold, reclaim enter after cold CO product suction port of compressor be compressed to 0.5MPa ~ ~
3.5MPa is sent as product by the 45th pipeline；Mixed in a ratio by methane, ethylene, propane, isopentane and nitrogen
Form azeotrope that pressure is 0.25MPa ~ 0.35MPa by cooled after azeotrope compressor compresses to 3.0 ~ 4.0Mpa
Separate, from azeotrope compressor gas phase cryogen by the 40th pipeline entrance main heat exchanger carry out being cooled to 118K ~
125K, is freezed to 0.3 ~ 0.4MPa through the 6th choke valve throttling by the 41st pipeline after being cooled, and backflow entrance main heat exchange
Device re-heat, the liquid phase cryogen from azeotrope compressor enters main heat exchanger by the 43rd pipeline and is cooled to ~ 150K, logical
Crossing the 44th pipeline to freeze to 0.3 ~ 0.4MPa through the 7th choke valve throttling, the entrance main heat exchanger that backflows after throttling refrigeration is multiple
Heat, sends main heat exchanger with another burst of cryogen mixing re-heat, enters azeotrope compressor by the 42nd pipeline, completes system
SAPMAC method.
The system of the high purity carbon monoxide described in the present embodiment and hydrogen rich gas coproduction liquid methane is embodiment one
Described in, this is no longer going to repeat them.
Claims (7)
1. a high purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane, it is characterised in that: this system is mainly wrapped
Include raw material gas purifying unit, low-temperature liquefaction separative element, CO product compressor and azeotrope compressor；Described low-temperature liquefaction
Separative element includes main heat exchanger, washes methane tower, dehydrogenation tower, domethanizing column and denitrification column, is provided with at the bottom of described dehydrogenation tower tower
One vaporizer, is provided with the second vaporizer, tower top is provided with the first condenser, at the bottom of described denitrification column tower at the bottom of the tower of described domethanizing column
Be provided with the 3rd vaporizer, tower top is provided with the second condenser；The entrance of described clean unit connects the first pipeline supplied gas, described only
Change unit outlet to be connected with main heat exchanger by second pipe；The described lower entrances of methane tower of washing is by the 3rd pipeline and institute
State main heat exchanger to be connected, described in wash methane tower top gas phase outlet be connected with main heat exchanger by the 4th pipeline, described
The 5th pipeline of hydrogen rich gas is sent in primary heat exchanger warm end connection, described in wash the bottom liquid phases outlet of methane tower by the 6th pipeline even
Logical first throttle valve；Described first throttle valve passes through the 7th pipeline communication main heat exchanger, and described main heat exchanger passes through the 8th pipeline
Being connected with the centre entrance of described dehydrogenation tower, described first throttle valve is by the upper entrance of the 9th pipeline with described dehydrogenation tower
It is connected；Described dehydrogenation top of tower gaseous phase outlet is connected with described main heat exchanger by the tenth pipeline, described primary heat exchanger warm end
The 11st pipeline of flash steam is sent in connection；The bottom liquid phases of described dehydrogenation tower exports by the 12nd pipeline and second throttle
Being connected, described second throttle is connected with described main heat exchanger by the 13rd pipeline, and described main heat exchanger passes through the tenth
Four pipelines are connected with described domethanizing column lower entrances, and described second throttle is by the 15th pipeline and described main heat exchanger
Being connected, described main heat exchanger is connected with described domethanizing column centre entrance by the 16th pipeline；Described demethanizer bottoms
Portion's liquid-phase outlet is connected with described main heat exchanger by the 17th pipeline, and liquid methane is sent in the connection of described primary heat exchanger warm end
The 18th pipeline；The top gas phase outlet of described domethanizing column is connected by the 19th pipeline and the 26th pipeline, institute
The upper gaseous phase outlet stating domethanizing column is connected with denitrification column centre entrance by the 20th pipeline, the top of described domethanizing column
Portion's the first condensator outlet is by the 21st pipeline entering through the 3rd choke valve and described denitrification column top the second condenser
Mouth is connected；Bottom liquid phases outlet the 22nd pipeline of described denitrification column, the 22nd pipeline arranges the 4th throttling
Valve, described 4th choke valve is connected with top second condenser inlet of described denitrification column by the 23rd pipeline, described de-
The upper gaseous phase outlet of nitrogen tower is connected with described main heat exchanger by the 24th pipeline, and the connection of described primary heat exchanger warm end is sent
25th pipeline of waste gas；The top gas phase outlet of described denitrification column is by the 26th pipeline with described main heat exchanger even
Logical, described main heat exchanger produces mouth suction port of compressor by the 27th pipeline with described CO and is connected.
A kind of high purity carbon monoxide the most according to claim 1 and the system of hydrogen rich gas coproduction liquid methane, it is special
Levy and be: described CO product compressor is connected with described main heat exchanger by the 28th pipeline, and described main heat exchanger passes through
29th pipeline is connected with the first evaporator inlet at the bottom of described dehydrogenation tower tower, the 29th pipeline and the 30th pipeline phase
Logical, entrance connection the 30th pipeline of the second vaporizer at the bottom of described demethanizer, outlet the 31st pipeline, the 30th
One pipeline and the 32nd pipeline are connected, and described first evaporator outlet passes through the 32nd pipeline and described main heat exchanger phase
Connection, described main heat exchanger is connected with described methane tower upper entrance of washing by the 33rd pipeline；Described first condenser
Entrance connection the 34th pipeline, the 34th pipeline is respectively communicated with the 33rd pipeline and the 35th pipeline, and the 35th
Pipeline connects with described main heat exchanger, and described main heat exchanger is by the 36th pipeline and described CO product compressor centre entrance
Being connected, described CO product compressor centre exit is connected with described main heat exchanger by the 37th pipeline, and described master changes
Hot device is connected with the 3rd evaporator inlet bottom described denitrification column by the 38th pipeline, and described 3rd evaporator outlet leads to
Crossing the 39th pipeline and the 5th choke valve is connected, described 5th choke valve and the 23rd pipeline are connected, and described CO produces
Product compressor outlet connection the 45th pipeline.
A kind of high purity carbon monoxide the most according to claim 1 and the system of hydrogen rich gas coproduction liquid methane, it is special
Levy and be: the gaseous phase outlet of described azeotrope compressor is connected with described main heat exchanger by the 40th pipeline, described
Main heat exchanger is connected with described main heat exchanger through the 6th choke valve by the 41st pipeline, and described main heat exchanger passes through the 4th
12 pipelines are connected with azeotrope suction port of compressor；Described azeotrope compressor liquid-phase outlet passes through the 43rd pipeline
Being connected with described main heat exchanger, described main heat exchanger passes through the 44th pipeline through the 7th choke valve and described main heat exchanger phase
Connection.
A kind of high purity carbon monoxide the most according to claim 1 and the system of hydrogen rich gas coproduction liquid methane, it is special
Levy and be: described main heat exchanger, described first vaporizer, described second vaporizer, described 3rd vaporizer, described first condensation
Device and described second condenser are vacuum brazing plate-fin heat exchanger, described in wash methane tower, dehydrogenation tower, domethanizing column, denitrogenation
Tower is regular packed tower or filler and float valve combination type rectifying column.
A kind of high purity carbon monoxide the most according to claim 1 and the system of hydrogen rich gas coproduction liquid methane, it is special
Levy and be: described CO product compressor delivery pressure is: 0.5 MPa ~ 3.5MPa；Described CO product compressor is used for circulation portions
Point extract out pressure be: 0.5MPa ~ 3.5MPa.
A kind of high purity carbon monoxide the most according to claim 1 and the system of hydrogen rich gas coproduction liquid methane, it is special
Levy and be: described clean unit inlet pressure is: 3.0MPa ~ 6.0MPa, and methane content volume fraction is 0.5% ~ 10%, and nitrogen contains
Amount volume fraction is 4% ~ 8%；Described dehydrogenation pressure tower is 0.9MPa ~ 2.5MPa；Described domethanizing column and denitrification column pressure
For 0.2MPa ~ 0.6MPa.
A kind of high purity carbon monoxide the most according to claim 1 and the system of hydrogen rich gas coproduction liquid methane, it is special
Levy and be: azeotrope uses nitrogen, methane, ethylene, propane and isopentane to mix according to a certain percentage.
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| CN201620494223.2U CN205784230U (en) | 2016-05-27 | 2016-05-27 | High purity carbon monoxide and the system of hydrogen rich gas coproduction liquid methane |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105865147A (en) * | 2016-05-27 | 2016-08-17 | 开封空分集团有限公司 | System and method for preparing high purity carbon monoxide and hydrogen-enriched co-production liquid methane |
| CN109269223A (en) * | 2018-09-19 | 2019-01-25 | 成都深冷液化设备股份有限公司 | A kind of purification CO, CH4Cryogenic separation system and method |
-
2016
- 2016-05-27 CN CN201620494223.2U patent/CN205784230U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105865147A (en) * | 2016-05-27 | 2016-08-17 | 开封空分集团有限公司 | System and method for preparing high purity carbon monoxide and hydrogen-enriched co-production liquid methane |
| CN105865147B (en) * | 2016-05-27 | 2018-05-11 | 开封空分集团有限公司 | The system and method for high purity carbon monoxide and hydrogen rich gas coproduction liquid methane |
| CN109269223A (en) * | 2018-09-19 | 2019-01-25 | 成都深冷液化设备股份有限公司 | A kind of purification CO, CH4Cryogenic separation system and method |
| CN109269223B (en) * | 2018-09-19 | 2023-07-28 | 四川蜀道装备科技股份有限公司 | Purification of CO and CH 4 Cryogenic separation system and method |
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