CN206094746U - Extract novel device of liquid methane in follow high methane gas - Google Patents
Extract novel device of liquid methane in follow high methane gas Download PDFInfo
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- CN206094746U CN206094746U CN201621096327.4U CN201621096327U CN206094746U CN 206094746 U CN206094746 U CN 206094746U CN 201621096327 U CN201621096327 U CN 201621096327U CN 206094746 U CN206094746 U CN 206094746U
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Abstract
The utility model relates to an extracting the structure design of equipment's of liquid methane technical field, specifically disclosing an extract novel device of liquid methane in follow high methane gas, it includes main heat exchanger, subcooler, LNG rectifying column condenser, LNG rectifying column reboiler, LNG rectifying column, return tank and cryogen knockout drum, main heat exchanger in be provided with A passageway, B passageway, C passageway, D passageway, E passageway, G passageway, F passageway, H passageway and L passageway, the subcooler in be provided with I passageway, J passageway and K passageway, LNG rectifying column condenser in be provided with N passageway and M passageway. The utility model discloses on more original patent's basis, redesign one kind can extract novel device of liquid methane in follow high methane gas, not only kept original technological some advantages, for example draw the structure of principle, refrigeration principle, indivedual spare parts etc. Have still that the operation degree of difficulty is low, a low in manufacturing cost, energy consumption is low, recovery efficiency is high characteristics.
Description
Technical field
The utility model is related to extract the technical field of the device structure design of liquid methane, and particularly one kind is from methane rich
The new device of liquid methane is extracted in gas.
Background technology
Liquefied natural gas（LNG）Main component be liquid methane, LNG solves natural gas transportation and storage problem.It is logical
Often about -162 DEG C of the storage temperature of LNG, pressure are normal pressure, and its liquid is more than 600 times of methane under standard state, is extremely had
Beneficial to transport and storage.There is the defeated day of pipe in terms of transport by sea, the utilization of outlying gas field gas, the peak regulation of city natural gas
The incomparable advantage of right gas.Methane is very wide in the distribution of nature, and methane is simplest organic matter, is natural gas, biogas
With the main component of hole gas etc., gas is commonly called as, is also that phosphorus content is minimum（Hydrogen content is maximum）Hydrocarbon, be also natural gas, biogas, oil
The main component of field gas and coal mine gallery gas.It can be used as fuel and manufacture hydrogen, carbon black, carbon monoxide, acetylene, hydrogen cyanogen
The raw material of the material such as acid and formaldehyde.In modern industrial production, the preparation method of methane generally includes the decomposition of debirs, day
Right source（Such as marsh）, from fossil fuel extract, animal（Such as ox）Digestion process, rice field among bacterium decompose and raw
Thing material anoxic is heated or burnt, and methane prepared by these methods is not pure, wherein containing plurality of impurities gas, therefore this is just
It is related to the extractive technique of methane.In recent years, the technology through chemical industry develops, and about the extractive technique of methane one has been obtained
Determine the solution of degree, but in productive life, the methane of gaseous state can not fully meet the needs of people, many times
Need to use liquid methane to make fuel or need to be transported with liquid methane and stored in industrial production activities, this is just
Involve how to prepare the technical problem of liquid methane.
Patent " the method for liquefaction gaseous state, the charging rich in methane to obtain liquiefied product（The patent No.：
CN200480003111.2）" liquifying method and liquefying plant of a kind of methane are disclosed, the patented technology is using cold-producing medium, system
Cold compressor, heat exchanger and separator etc. are combined design, can realize the liquefaction of methane gas, but its liquefaction process
More complicated, operating, it is loaded down with trivial details slightly show, and it can not be to extracting to impure more methane gas, and it can only liquid
Change the very high methane gas of purity, therefore for impure more methane gas, the patent equipment cannot be suitable for, it is necessary to attached
Plus methane equipment for purifying can just complete the liquefaction of methane gas；A kind of patent " producing liquefied natural gas by coke oven gas through low-temperature rectification
Device（The patent No.：CN201120246458.7）", using nitrogen supercharging expansion, ladder Refrigeration Technique, although the technique is adopted
Nitrogen expansion freezes, and liquid nitrogen has relatively low evaporating temperature, provides relatively low temperature can to rectifying column condenser, it is ensured that methane
The rate of recovery or liquefied fraction are 99%, but the technique adopts single refrigeration nitrogen, and energy consumption is higher, and using multi-stage booster and many
The mode of level expansion, power-equipment is more, on the one hand increased equipment investment, on the other hand also increases fault rate, and operation is difficult
Degree also increases.Patent " a kind of method that utilization oven gas prepares liquefied natural gas（The patent No.： CN200910310655.8）",
Using rear methane decompressor, increase refrigeration source, the cold energy gas recovery of nitrogen, hydrogen tail gas can be will be enriched in, but should
Technique is not provided with subcooler, is only exchanged heat by main heat exchanger, and the temperature of rectifying column condenser is higher, it is impossible to regulate and control, if raw material
When gas tolerance increases, it is impossible to ensure the rate of recovery of methane, and the energy consumption of the technique is also higher.
From the above mentioned, it is also less perfect about the patented technology of extraction and the liquefaction of methane gas, it need to be continued optimization
And Curve guide impeller, methane is extracted and the method and apparatus of liquefaction is still required further study, how to design a behaviour
Make that low difficulty, low cost of manufacture, organic efficiency be high, more energy-conservation extraction liquid methane device is currently practical to need to solve
Problem.
Utility model content
The purpose of this utility model is the shortcoming for overcoming prior art, there is provided a kind of operation difficulty is low, low cost of manufacture,
The new device that liquid methane is extracted from high methane gas that energy ezpenditure is low, organic efficiency is high.
The purpose of this utility model is achieved through the following technical solutions：It is a kind of that liquid methane is extracted from high methane gas
New device, it includes main heat exchanger, subcooler, LNG rectifying column condensers, LNG rectifying column reboilers, LNG rectifying columns, backflow
Tank and cryogen knockout drum, are provided with A channel, channel B, C-channel, D passages, E passages, G passages, F and lead in described main heat exchanger
Road, H passages and L * channel, are provided with I passages, J passages and K channel, described LNG rectifying column condensers in described subcooler
Inside it is provided with N channel and M passages；
The arrival end of the A channel of described main heat exchanger is connected with outside high methane gas pipeline, and the port of export of A channel passes through
Pipeline connects with the arrival end of LNG rectifying columns, and between the port of export of A channel and the arrival end of LNG rectifying columns regulating valve is provided with
The port of export of a, LNG rectifier bottoms is connected with the arrival end of the H passages of main heat exchanger, and H channel outlets are connected with LNG outputs
Pipeline, is provided with the M passages of regulating valve b, the port of export at the top of LNG rectifying columns and LNG rectifying column condensers on LNG export pipelines
Arrival end connection, the port of export of M passages connects with the arrival end of return tank, the port of export and LNG rectifying columns of the pot bottom that flows back
The backflow end connection of tower top, the port of export at the top of return tank is connected with the arrival end of the K channel of subcooler, going out at the top of return tank
It is provided with regulating valve c between mouthful end and the arrival end of K channel, the arrival end phase of the port of export of K channel and the channel B of main heat exchanger
Connection, the port of export of channel B is connected with the defeated pipeline of external exhaust gas；
The arrival end of the C-channel of described main heat exchanger is connected with external high pressure gas phase cryogen pipeline, is provided with C-channel
Two port of export I and port of export II, the port of export I and port of export II of C-channel with the cryogen arrival end of LNG rectifying column reboilers
It is connected, between the cryogen arrival end of the port of export I and LNG rectifying column reboiler of C-channel regulating valve f, LNG rectifying columns is provided with
The cryogen port of export of reboiler is connected with the arrival end of the L * channel of main heat exchanger, the cryogen entrance end pipe of LNG rectifying column reboilers
Bypass line a is provided between line and its cryogen port of export pipeline, regulating valve g, the L of main heat exchanger are provided with bypass line a
The port of export of passage is connected with the arrival end of cryogen knockout drum, the G passages of the port of export at the top of cryogen knockout drum and main heat exchanger
Arrival end connection, G channel outlets are connected with the arrival end of the J passages of subcooler, the port of export and LNG rectifying columns of J passages
The arrival end of the N channel of condenser is connected, and regulating valve e, N channel are provided between the port of export of J passages and the arrival end of N channel
The port of export be connected with the arrival end of the I passages of subcooler, be provided with side on the arrival end pipeline of N channel and its port of export pipeline
Stylet b, bypass line b is located between the port of export of the J passages of subcooler and regulating valve e, and regulation is provided with bypass line b
Valve i；The arrival end of the D passages of main heat exchanger is provided with access port III, access port IV and access port VI, the I passages of subcooler
The port of export is connected with the access port IV of the D passages of main heat exchanger, and the port of export of cryogen knockout drum bottom leads to the F of main heat exchanger
The arrival end connection in road, F channel outlets are divided into gas phase cryogen pipeline VII and gas phase refrigerant line VIII, gas phase cryogen pipeline
Regulating valve d is provided with VII, gas phase cryogen pipeline VII is connected with the access port IV of the D passages of main heat exchanger, gas phase cryogen pipe
Regulating valve h is provided with line VIII, gas phase cryogen pipeline VIII is connected with the access port III of the D passages of main heat exchanger, master changes
The arrival end of the E passages of hot device is connected with external high pressure liquid phase cryogen pipeline, the port of export of E passages and the D passages of main heat exchanger
Access port VI be connected, regulating valve j, the port of export of D passages are provided between the access port VI of E channel outlets and D passages
It is connected with external mix refrigerant compressor pipeline.
Described main heat exchanger, subcooler, LNG rectifying columns condenser and LNG rectifying column reboilers are respectively plate-fin and change
Any one in hot device, wound tube heat exchanger or shell-and-tube heat exchanger.
Described LNG rectifying columns are packed tower or plate column.
The operation temperature of described LNG rectifying column tower tops is operating pressure, the J passage of subcooler by LNG rectifying columns
Temperature and cold-producing medium determine；The operating pressure of LNG rectifying columns is adjusted by regulating valve c, and the temperature of the J passages of subcooler is by adjusting
Section valve i is adjusted；The temperature of LNG tower bottom of rectifying tower is adjusted by regulating valve g, and the liquid level of LNG tower bottom of rectifying tower is by adjusting
Valve b is adjusted.
The temperature of described LNG rectifying column reboilers is adjusted by regulating valve f.
The temperature of the L * channel of described main heat exchanger is adjusted by regulating valve h.
The methane content of described high methane gas is not less than 15%..
The utility model has advantages below：
1st, the utility model sets up regulating valve h and cryogen knockout drum, can adjust the cryogen of control LNG rectifying column condensers
In nitrogen content, the temperature of effective control LNG rectifying column condenser, so as to control and improve the rate of recovery of methane.
2nd, equipment investment cost necessary to the utility model is relatively low, and operation principle is easy-to-understand, and operation is difficult
Degree is low, thus low cost of manufacture, can popularization it is strong.
3rd, the utility model compared with existing some patented technologies, is reduced only with a refrigerant compressor
Other power-equipments, reduce fault rate.
4th, the utility model adopts the high pressure vapor cryogen extracted out from main heat exchanger middle part as LNG rectifying column reboilers
Thermal source, and by arranging regulating valve f and regulating valve g, the temperature of LNG rectifying column reboilers is accurately controlled, such that it is able to control
With raising liquefied natural gas（LNG）Purity.
5th, the utility model has higher economic benefit and reduces the advantage of environmental pollution.The utility model can be to coke oven
The gases rich in methane such as coal gas, the tail gas of synthesis ammonia pond releasing or gas carry out cryogenic rectification separating-purifying, directly by its liquid
Change obtains LNG, and it is purified after other gases can then return the raw material that previous workshop section is used as synthesis other products, realize
Turn waste into wealth, it is to avoid the wasting of resources.
Description of the drawings
Fig. 1 is structural representation of the present utility model；
In figure：1- main heat exchangers, 2- subcoolers, 3- LNG rectifying column condensers, 4- LNG rectifying column reboilers, 5- LNG
Rectifying column, 6- return tanks, 7- cryogen knockout drums, 8-A passages, 9- channel Bs, 10- C-channels, 11- D passages, 12- E passages,
14-L passages, 15- G passages, 16- F passages, 17- H passages, 19- LNG export pipelines, 20- gas phase cryogen pipeline VIII,
21- regulating valves h, 22-I passages, 23- J passages, 24-K passages, 25- regulating valves a, 26- regulating valves b, 27- regulating valves c, 28- is adjusted
Section valve d, 29- regulating valves e, 30- regulating valves f, 31- regulating valves g, 32-N passages, 33-M passages, 34- bypass line a, 35- bypass
Line b, 36- gas phase cryogen pipeline VII, 37- regulating valves j, 38- regulating valves i.
Specific embodiment
The utility model is further described below in conjunction with the accompanying drawings, but protection domain of the present utility model is not limited to
Described below.
As shown in figure 1, a kind of new device that liquid methane is extracted from high methane gas, it includes main heat exchanger 1, supercooling
Device 2, LNG rectifying columns condenser 3, LNG rectifying columns reboiler 4, LNG rectifying columns 5, return tank 6 and cryogen knockout drum 7, it is described
A channel 8, channel B 9, C-channel 10, D passages 11, E passages 12, G passages 15, F passages 16, H passages are provided with main heat exchanger 1
17 and L * channel 14, I passages 22, J passages 23 and K channel 24, described LNG rectifying columns condensation are provided with described subcooler 2
N channel 32 and M passages 33 are provided with device 3；
The arrival end of the A channel 8 of described main heat exchanger 1 is connected with outside high methane gas pipeline, the port of export of A channel 8
Connected with the arrival end of LNG rectifying columns 5 by pipeline, be provided between the port of export of A channel 8 and the arrival end of LNG rectifying columns 5
Regulating valve a25, the port of export of the bottom of LNG rectifying columns 5 is connected with the arrival end of the H passages 17 of main heat exchanger 1, and H passages 17 are exported
End is connected with LNG export pipelines 19, is provided with regulating valve b26 on LNG export pipelines 19, the port of export at the top of LNG rectifying columns 5 with
The arrival end connection of the M passages 33 of LNG rectifying columns condenser 3, the port of export of M passages 33 is connected with the arrival end of return tank 6, returned
The port of export of stream tank 6 bottom is connected with the backflow end of the tower top of LNG rectifying columns 5, the K of the port of export and subcooler 2 at the top of return tank 6
The arrival end connection of passage 24, between the port of export and the arrival end of K channel 24 at the top of return tank 6 regulating valve c27, K are provided with
The port of export of passage 24 is connected with the arrival end of the channel B 9 of main heat exchanger 1, and the port of export of channel B 9 is connected with external exhaust gas
Defeated pipeline；
The arrival end of the C-channel 10 of described main heat exchanger 1 is connected with external high pressure gas phase cryogen pipeline, on C-channel 10
Be provided with two port of export I and port of export II, the port of export I and port of export II of C-channel 10 with LNG rectifying columns reboiler 4
Cryogen arrival end is connected, and between the cryogen arrival end of the port of export I and LNG rectifying column reboiler 4 of C-channel 10 regulation is provided with
The cryogen port of export of valve f30, LNG rectifying column reboiler 4 is connected with the arrival end of the L * channel 14 of main heat exchanger 1, LNG rectifying columns
Bypass line a34 is provided between the cryogen arrival end pipeline of reboiler 4 and its cryogen port of export pipeline, on bypass line a34
Regulating valve g31 is provided with, the port of export of the L * channel 14 of main heat exchanger 1 is connected with the arrival end of cryogen knockout drum 7, cryogen is separated
The port of export at the top of tank 7 is connected with the arrival end of the G passages 15 of main heat exchanger 1, the J passages of the port of export of G passages 15 and subcooler 2
23 arrival end connection, the port of export of J passages 23 is connected with the arrival end of the N channel 32 of LNG rectifying columns condenser 3, J passages 23
The port of export and the arrival end of N channel 32 between be provided with regulating valve e29, the port of export of N channel 32 and the I passages of subcooler 2
22 arrival end connection, on the arrival end pipeline of N channel 32 and its port of export pipeline bypass line b35, bypass line are provided with
B35 is located between the port of export of the J passages 23 of subcooler 2 and regulating valve e29, and on bypass line b35 regulating valve i38 is provided with；
The arrival end of the D passages 11 of main heat exchanger 1 is provided with access port III, access port IV and access port VI, the I passages 22 of subcooler 2
The port of export be connected with the access port IV of the D passages 11 of main heat exchanger 1, the port of export and main heat exchange of the bottom of cryogen knockout drum 7
The arrival end connection of the F passages 16 of device 1, the port of export of F passages 16 is divided into gas phase cryogen pipeline VII36 and gas phase refrigerant line
VIII20, is provided with the D passages of regulating valve d28, gas phase cryogen pipeline VII36 and main heat exchanger 1 on gas phase cryogen pipeline VII36
11 access port IV connections, are provided with regulating valve h21 on gas phase cryogen pipeline VIII20, gas phase cryogen pipeline VIII20 is changed with master
The access port III of the D passages 11 of hot device 1 is connected, and the arrival end of the E passages 12 of main heat exchanger 1 is connected with external high pressure liquid phase
Refrigerant line, the port of export of E passages 12 is connected with the access port VI of the D passages 11 of main heat exchanger 1, the port of export of E passages 12 and D
Regulating valve j37 is provided between the access port VI of passage 11, the port of export of D passages 11 is connected with external mix refrigerant compressor pipe
Line.
Described main heat exchanger 1, subcooler 2, LNG rectifying columns condenser 3 and LNG rectifying columns reboiler 4 are respectively plate wing
Any one in formula heat exchanger, wound tube heat exchanger or shell-and-tube heat exchanger；Described LNG rectifying columns 5 are packed tower or plate
Formula tower；The operation temperature of the described tower top of LNG rectifying columns 5 is operating pressure, the J passage 23 of subcooler 2 by LNG rectifying columns 5
Temperature and cold-producing medium determine；The operating pressure of LNG rectifying columns 5 is adjusted by regulating valve c27, the J passages 23 of subcooler 2
Temperature is adjusted by regulating valve i38；The temperature of the tower reactor of LNG rectifying columns 5 is adjusted by regulating valve g31, the tower of LNG rectifying columns 5
The liquid level of kettle is adjusted by regulating valve b26；The temperature of described LNG rectifying columns reboiler 4 is adjusted by regulating valve f30；
The temperature of the L * channel 14 of described main heat exchanger 1 is adjusted by regulating valve h21；The methane content of described high methane gas is not
Less than 15%.
The course of work of the present utility model is as follows：（1）High methane gas cooling, condensation：It is purified it is qualified after high methane gas
The cryogenic coolant cooling backflowed during by the A channel 8 of main heat exchanger 1, partial condensation obtains a part of liquid, while other
Rectifying in LNG rectifying columns 5 is delivered in the adjusted valve a25 decompressions of gas；（2）LNG rectifying column rectifying：What the tower reactor of LNG rectifying columns 5 was arranged
LNG rectifying columns reboiler 4 can be used in the kettle liquid evaporation of LNG rectifying columns 5, so as to obtain qualified LNG, then LNG be sent into into master
The H passages 17 of heat exchanger 1 are subcooled, adjusted valve b26 decompressions, deliver in storage tank and store；The tower top of LNG rectifying columns 5 is provided with LNG rectifying
Tower condenser 3 and return tank 6, LNG rectifying columns condenser 3 be used for condensing tower top out rich in methane, carbon monoxide, hydrogen,
The mixed gas of nitrogen, argon gas etc., condensed vapour-liquid phase mixture Jing return tank 6 separation after, the adjusted valve of gas phase mixture
As low-temperature receiver after c27, outer defeated another use after the K channel 24 of cooler 2, the re-heat of channel B 9 of main heat exchanger 1, liquid phase mixing are sequentially passed through
Thing leans on gravity reflux to the top of tower of LNG rectifying columns 5 as the phegma of LNG rectifying columns 5, this ensure that the rate of recovery of methane；（3）
Azeotrope freezes：High pressure vapor cryogen from refrigerant compressor compression unit is cooled in the C-channel 10 of main heat exchanger 1
Uniform temperature, extracts out from the middle part of main heat exchanger 1, and into LNG rectifying columns reboiler 4 as thermal source, high pressure vapor cryogen is smart in LNG
After evaporating the inner cooling by the kettle liquid of LNG rectifying columns 5 of tower reboiler 4, the L * channel 14 for returning again to main heat exchanger 1 continues to be cooled to a constant temperature,
Formed high pressure vapor, high pressure vapor enter cryogen knockout drum 7 after separate, the liquid that bottom is isolated be mainly methane, ethene and
Heavier component, the F passages 16 that remaining gas phase enters main heat exchanger 1 are cooled, condensation, after adjusted valve d28 decompressions cooling, enter
Enter the D passages 11 of main heat exchanger 1, each hot-fluid stock for main heat exchanger 1 provides low-temperature receiver；The top of cryogen knockout drum 7 gas phase out
Mainly nitrogen and methane, sequentially enter the G passages 15 of main heat exchanger 1 and the J passages 23 of subcooler 2, are then cooled, condense
To uniform temperature, then into the N channel 32 of LNG rectifying columns condenser 3 after adjusted valve e29 decompression coolings, as LNG rectifying columns
The low-temperature receiver of condenser 3, from the cryogen out of rectifying column condenser 3 the I passages 22 of subcooler 2 are again introduced into, and are each heat of subcooler 2
Fluid provides low-temperature receiver, and the D passages 11 for then entering back into main heat exchanger 1 are that main heat exchanger 1 provides low-temperature receiver；High pressure vapor cryogen is entered
Uniform temperature is cooled to after the E passages 12 of main heat exchanger 1, also into the D passages 11 of main heat exchanger 1 after the cooling of adjusted valve 37,
Various gas phase cryogens finally merge in formation azeotrope at D passages 11, then return again to azeotrope compressor.It is more than this
The substantially course of work of utility model, wherein both having completed high methane gas cooling, condensation and rectifying, realizes high pressure vapor cold again
The repetitive cycling of agent is utilized, and efficiently and optimally solves the problems, such as the essential technique of extraction and the liquefaction of methane gas.
The above is only preferred embodiment of the present utility model, it should be understood that the utility model is not limited to herein
Disclosed form, is not to be taken as the exclusion to other embodiment, and can be used for various other combinations, modification and environment, and
Can be modified by the technology or knowledge of above-mentioned teaching or association area in contemplated scope described herein.And this area
Change and change without departing from spirit and scope of the present utility model that personnel are carried out, then all should be in right appended by the utility model
In the protection domain of requirement.
Claims (7)
1. it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：It includes main heat exchanger（1）, mistake
Cooler（2）, LNG rectifying column condensers（3）, LNG rectifying column reboilers（4）, LNG rectifying columns（5）, return tank（6）With cryogen point
From tank（7）, described main heat exchanger（1）Inside it is provided with A channel（8）, channel B（9）, C-channel（10）, D passages（11）, E passages
（12）, G passages（15）, F passages（16）, H passages（17）And L * channel（14）, described subcooler（2）Inside it is provided with I passages
（22）, J passages（23）And K channel（24）, described LNG rectifying column condensers（3）Inside it is provided with N channel（32）With M passages
（33）；
Described main heat exchanger（1）A channel（8）Arrival end be connected with outside high methane gas pipeline, A channel（8）Outlet
End is by pipeline and LNG rectifying columns（5）Arrival end connect, A channel（8）The port of export and LNG rectifying columns（5）Arrival end it
Between be provided with regulating valve a（25）, LNG rectifying columns（5）The port of export and main heat exchanger of bottom（1）H passages（17）Arrival end
Connection, H passages（17）The port of export is connected with LNG export pipelines（19）, LNG export pipelines（19）On be provided with regulating valve b（26）,
LNG rectifying columns（5）The port of export at top and LNG rectifying column condensers（3）M passages（33）Arrival end connection, M passages（33）
The port of export and return tank（6）Arrival end connect, return tank（6）The port of export of bottom and LNG rectifying columns（5）The backflow of tower top
End connection, return tank（6）The port of export and subcooler at top（2）K channel（24）Arrival end connection, return tank（6）Top
The port of export and K channel（24）Arrival end between be provided with regulating valve c（27）, K channel（24）The port of export and main heat exchanger
（1）Channel B（9）Arrival end be connected, channel B（9）The port of export be connected with the defeated pipeline of external exhaust gas；
Described main heat exchanger（1）C-channel（10）Arrival end be connected with external high pressure gas phase cryogen pipeline, C-channel（10）
On be provided with two port of export I and port of export II, C-channel（10）Port of export I and port of export II with LNG rectifying column reboilers
（4）Cryogen arrival end be connected, C-channel（10）Port of export I and LNG rectifying column reboilers（4）Cryogen arrival end between
It is provided with regulating valve f（30）, LNG rectifying column reboilers（4）The cryogen port of export and main heat exchanger（1）L * channel（14）Enter
The connection of mouth end, LNG rectifying column reboilers（4）Cryogen arrival end pipeline and its cryogen port of export pipeline between be provided with bypass pipe
Line a（34）, bypass line a（34）On be provided with regulating valve g（31）, main heat exchanger（1）L * channel（14）The port of export and cryogen
Knockout drum（7）Arrival end connection, cryogen knockout drum（7）The port of export and main heat exchanger at top（1）G passages（15）Entrance
End connection, G passages（15）The port of export and subcooler（2）J passages（23）Arrival end connection, J passages（23）The port of export with
LNG rectifying column condensers（3）N channel（32）Arrival end be connected, J passages（23）The port of export and N channel（32）Entrance
Regulating valve e is provided between end（29）, N channel（32）The port of export and subcooler（2）I passages（22）Arrival end connection, N
Passage（32）Arrival end pipeline and its port of export pipeline on be provided with bypass line b（35）, bypass line b（35）Positioned at supercooling
Device（2）J passages（23）The port of export and regulating valve e（29）Between, bypass line b（35）On be provided with regulating valve i（38）；It is main
Heat exchanger（1）D passages（11）Arrival end be provided with access port III, access port IV and access port VI, subcooler（2）I lead to
Road（22）The port of export and main heat exchanger（1）D passages（11）Access port IV be connected, cryogen knockout drum（7）Bottom goes out
Mouth end and main heat exchanger（1）F passages（16）Arrival end connection, F passages（16）The port of export is divided into gas phase cryogen pipeline VII
（36）With gas phase refrigerant line VIII（20）, gas phase cryogen pipeline VII（36）On be provided with regulating valve d（28）, gas phase cryogen pipe
Line VII（36）With main heat exchanger（1）D passages（11）Access port IV connection, gas phase cryogen pipeline VIII（20）On be provided with
Regulating valve h（21）, gas phase cryogen pipeline VIII（20）With main heat exchanger（1）D passages（11）Access port III be connected, it is main
Heat exchanger（1）E passages（12）Arrival end be connected with external high pressure liquid phase cryogen pipeline, E passages（12）The port of export and master
Heat exchanger（1）D passages（11）Access port VI be connected, E passages（12）The port of export and D passages（11）Access port VI between
It is provided with regulating valve j（37）, D passages（11）The port of export be connected with external mix refrigerant compressor pipeline.
2. it is according to claim 1 it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：Institute
The main heat exchanger stated（1）, subcooler（2）, LNG rectifying column condensers（3）With LNG rectifying column reboilers（4）Respectively plate-fin
Any one in heat exchanger, wound tube heat exchanger or shell-and-tube heat exchanger.
3. it is according to claim 1 it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：Institute
The LNG rectifying columns stated（5）For packed tower or plate column.
4. it is according to claim 1 it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：Institute
The LNG rectifying columns stated（5）The operation temperature of tower top is by LNG rectifying columns（5）Operating pressure, subcooler（2）J passages（23）
Temperature and cold-producing medium determine；LNG rectifying columns（5）Operating pressure by regulating valve c（27）It is adjusted, subcooler（2）J
Passage（23）Temperature by regulating valve i（38）It is adjusted；LNG rectifying columns（5）The temperature of tower reactor is by regulating valve g（31）Adjusted
Section, LNG rectifying columns（5）The liquid level of tower reactor is by regulating valve b（26）It is adjusted.
5. it is according to claim 1 it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：Institute
The LNG rectifying column reboilers stated（4）Temperature by regulating valve f（30）It is adjusted.
6. it is according to claim 1 it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：Institute
The main heat exchanger stated（1）L * channel（14）Temperature by regulating valve h（21）It is adjusted.
7. it is according to claim 1 it is a kind of from high methane gas extract liquid methane new device, it is characterised in that：Institute
The methane content of the high methane gas stated is not less than 15%.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108641750A (en) * | 2018-05-09 | 2018-10-12 | 天津市天地创智科技发展有限公司 | A kind of dry gas piece-rate system dry gas piece-rate system and separation method based on argon circularly cooling |
| CN109405413A (en) * | 2018-11-17 | 2019-03-01 | 杭州宏盛中弘新能源有限公司 | A kind of coalbed methane containing oxygen low temperature distillation system that avoiding explosion limit and method |
| CN116987536A (en) * | 2023-06-15 | 2023-11-03 | 英德市西洲气体有限公司 | Argon removal process for methane tower |
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2016
- 2016-09-30 CN CN201621096327.4U patent/CN206094746U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108641750A (en) * | 2018-05-09 | 2018-10-12 | 天津市天地创智科技发展有限公司 | A kind of dry gas piece-rate system dry gas piece-rate system and separation method based on argon circularly cooling |
| CN108641750B (en) * | 2018-05-09 | 2023-04-25 | 天津市天地创智科技发展有限公司 | Dry gas separation system and separation method based on argon circulation refrigeration |
| CN109405413A (en) * | 2018-11-17 | 2019-03-01 | 杭州宏盛中弘新能源有限公司 | A kind of coalbed methane containing oxygen low temperature distillation system that avoiding explosion limit and method |
| CN109405413B (en) * | 2018-11-17 | 2024-01-30 | 杭州宏盛中弘新能源有限公司 | Oxygen-containing coal bed gas cryogenic rectification system and method avoiding explosion limit |
| CN116987536A (en) * | 2023-06-15 | 2023-11-03 | 英德市西洲气体有限公司 | Argon removal process for methane tower |
| CN116987536B (en) * | 2023-06-15 | 2024-03-08 | 英德市西洲气体有限公司 | Argon removal process for methane tower |
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