CN207113409U - One kind uses bicirculating CO cryogenic separations system - Google Patents
One kind uses bicirculating CO cryogenic separations system Download PDFInfo
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- CN207113409U CN207113409U CN201720922370.XU CN201720922370U CN207113409U CN 207113409 U CN207113409 U CN 207113409U CN 201720922370 U CN201720922370 U CN 201720922370U CN 207113409 U CN207113409 U CN 207113409U
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Abstract
The utility model discloses one kind to use bicirculating CO cryogenic separations system, and it includes main heat exchanger, cold catch pot, hydrogen stripper, denitrification column, domethanizing column, CO compressors and circulating nitrogen gas compressor.The beneficial effects of the utility model are：CO is played to compress the low energy consumption of rectification circulated and the compression energy consumption of nitrogen circulation and invest low double dominant；The low-temperature receiver of thermal source and condenser to rectifying column evaporator optimizes configuration, and the control of rectifying load is reliably, stably；Can be with the startup of shortening device and purification time, the emptying amount for reducing startup stage；Energy consumption is low, startup is fast, reduced investment, discharge are few, meets energy-saving main trend, has good economic benefit and environmental benefit.
Description
Technical field
Cryogenic gas separation field is the utility model is related to, it is particularly a kind of to use bicirculating CO cryogenic separations system.
Background technology
CO is important carbonylation feed gas, and almost all of organic chemicals can be produced by CO.System at present
CO synthesis gas is taken to mostly come from coal pressure gasification or natural gas/naphtha steam conversion, in the synthesis gas that coal gasification is produced
In, in addition to containing CO, hydrogen, also containing a small amount of methane, nitrogen and argon gas, in view of production ethylene glycol, acetic acid and dimethyl two
Purity requirement during the chemical products such as acid amides to raw material CO is very high（≥98.5%）, it is therefore desirable to by the hydrogen in synthesis gas
Gas, methane, nitrogen and argon gas etc. remove.Cold separation technology technical maturity, stable operation, treating capacity are big, product purity is high, receive
Rate is high, is the one preferred technique of current CO separation.
The C of Chinese utility model patent CN 100427862 " method and apparatus that carbon monoxide is produced by low temperature distillation "
With the B of CN 101823709 " carbon monoxide is separated from the admixture of gas containing carbon monoxide " using pure CO compressions, refrigeration
Circulation, in view of CO compressors and the less efficient of expanding machine, technical requirements are high, it is larger using the energy consumption and investment of this kind of technique,
Device starts simultaneously, the time of purification is grown, and the emptying amount of startup stage is big.
The B of Chinese utility model patent CN 104326472 " a kind of nitrogen cycle technique produces CO system and method " are adopted
Compressed with pure nitrogen gas, kind of refrigeration cycle, although the efficiency of nitrogen compressor and expanding machine is higher, technology maturation, the technique is used for
When needing the occasion of smart demethanation and nitrogen, the shortcomings that energy consumption of rectification is too high be present.
The utility model proposes one kind to use bicirculating CO cryogenic separations system, practical, perfect and easily
Solves above mentioned problem.
Utility model content
The shortcomings that the purpose of this utility model is to overcome prior art, there is provided one kind start fast, power consumption is low, discharge less,
The bicirculating CO cryogenic separations system of the low use of cost.
The purpose of this utility model is achieved through the following technical solutions：One kind uses bicirculating CO cryogenic separations system
System, including main heat exchanger A, main heat exchanger B, cold catch pot, hydrogen stripper, denitrification column, domethanizing column, denitrification column overhead condensation
Device, CO compressors, circulating nitrogen gas compressor；
Runner IA, runner IIA, the A of runner III, the A of runner IV, the A of runner V, stream are set side by side with described main heat exchanger A
Runner IB, runner IIB, the B of runner III, the B of runner IV, stream are set side by side with the A of road VI, the A of runner VII, runner VIII A, main heat exchanger B
The B of road V, the B of runner VI, the B of runner VII, the B of runner VIII, IC, runner IIC, the C of runner III are set side by side with denitrification column overhead condenser；
Main heat exchanger A runner IIA porch is connected with the air inlet pipe of mixing purified gas, main heat exchanger A runner IIA
Outlet and main heat exchanger B runner IIB entrances, main heat exchanger B runner IIB outlets are connected with the entrance of cold catch pot, low
The outlet of warm separator includes two liquid-phase outlets and a gaseous phase outlet, the gaseous phase outlet of cold catch pot successively with main heat exchange
The device B B of runner III, the main heat exchanger A A of runner III is connected with gas phase escape pipe, one of liquid-phase outlet in cold catch pot
Finally it is connected on the centre entrance of hydrogen stripper after being connected successively with pressure loading valve V1, heat exchanger B runner IB, cryogenic separation
Reconnected after another liquid-phase outlet is connected with pressure loading valve V2 in device on the upper entrance of hydrogen stripper, in hydrogen stripper
Top is provided with hydrogen stripper gaseous phase outlet, and hydrogen stripper gaseous phase outlet is finally connected to after being connected with main heat exchanger A runner IA
On flashed vapour holder, the bottom of hydrogen stripper is provided with hydrogen stripper liquid-phase outlet, hydrogen stripper liquid-phase outlet and pressure loading valve
V3 is reconnected on the centre entrance of denitrification column after being connected；
The bottom of denitrification column is provided with denitrification column liquid-phase outlet, and denitrogenation liquid-phase outlet passes through the stream in pipeline and main heat exchanger B
Road IX entrance is connected, and main heat exchanger B runners IX outlet is connected with the bottom inlet of denitrification column, in denitrogenation liquid phase exit again
Entrance after being connected by another root pipeline with pressure loading valve V4 again with denitrification column overhead condenser runner IIC is connected, denitrogenation
Column overhead condenser runner IIC outlet is connected with the centre entrance of domethanizing column, and the top of denitrification column is also provided with denitrification column gas
Mutually export, the runner VIB and main heat exchanger A with main heat exchanger B successively again after denitrification column gaseous phase outlet is connected with pressure loading valve V7
Runner VIA entrance is connected, and main heat exchanger A runners VIA outlet is connected on fuel reservoir, denitrification column gaseous phase outlet and subtracts
Branched pipe is provided with pipeline connected pressure valve V7, the branched pipe is connected with denitrification column overhead condenser runner IC entrance,
Denitrification column overhead condenser runner IC outlet is connected with the upper entrance of denitrification column；
The bottom of described domethanizing column is provided with domethanizing column liquid-phase outlet, domethanizing column liquid-phase outlet and pressure loading valve V6
Reconnect on the pipeline that pressure loading valve V7 is connected with main heat exchanger B runners VIB after being connected, be also provided with the top of domethanizing column
Domethanizing column gaseous phase outlet, domethanizing column gaseous phase outlet are connected to main heat exchanger A's after being connected with main heat exchanger B runners VIIIB
On runner VIIIA entrance, main heat exchanger A runner VIIIA outlet is connected with the entrance of CO compressors, and CO compressors go out
Mouth is connected with CO product holders, also passes through another pipe on the pipeline that the outlet of CO compressors is connected with CO product holders
Road is connected in main heat exchanger A runner VIIA import, main heat exchanger A runners VIIA outlet and main heat exchanger B runner
VIIB is connected, and main heat exchanger B runner VIIB, which is connected with the upper entrance of domethanizing column and is provided with the pipeline of connection, to be subtracted
Pressure valve V5；
Lower position in described domethanizing column is provided with domethanizing column bottom of towe evaporator, and circulating nitrogen gas compressor goes out
Mouth is connected with main heat exchanger A runners IVA import, main heat exchanger A runners IVA outlet and entering for main heat exchanger B runner IVB
Mouth is connected, and main heat exchanger B runner IVB outlet is connected with the import of domethanizing column bottom of towe evaporator, in main heat exchanger B stream
Branched pipe is additionally provided with the pipeline that road IVB outlet is connected with the import of domethanizing column bottom of towe evaporator, the branched pipe is with subtracting
Pressure valve V9 is connected in the C of denitrification column overhead condenser runner III import through pressure loading valve V10 again after being connected, demethanizer
The outlet of bottom evaporator is connected to by pipeline on the branched pipe that pressure loading valve V9 is connected with pressure loading valve V10, in denitrification column tower
The C of top condenser runner III exit is provided with liquid nitrogen storage, and the exit of liquid nitrogen storage is provided with pressure loading valve V11,
Outlet of the C of denitrification column overhead condenser runner III outlet with being connected to the pressure loading valve V11 after liquid nitrogen storage merges, the conjunction
And locate to be connected by the pipeline successively B of runner V with main heat exchanger B, main heat exchanger the A A of runner V, main heat exchanger A runner V
A outlet is connected in the import of circulating nitrogen gas compressor, the pipeline that main heat exchanger A is connected with the import of circulating nitrogen gas compressor
On be also connected by branched pipe with emptying device, be provided with switch valve on the branched pipe；
Lower position in described hydrogen stripper is provided with hydrogen stripper bottom of towe evaporator, in main heat exchanger A runner
Hydrogen stripper bottom of towe evaporator node and hydrogen stripper tower are provided with the pipeline that IVA is connected with main heat exchanger B runners IVB
Bottom evaporator outlet node, hydrogen stripper bottom of towe evaporator node is close to main heat exchanger A runner IVA sides, hydrogen stripper
Bottom of towe evaporator outlet node passes through pipeline close to main heat exchanger B runner IVB sides, hydrogen stripper bottom of towe evaporator node
It is connected in the import of hydrogen stripper bottom of towe evaporator, hydrogen stripper bottom of towe evaporator outlet node is connected to hydrogen vapour by pipeline
On stripper bottom of towe evaporator outlet, in hydrogen stripper bottom of towe evaporator node and hydrogen stripper bottom of towe evaporator outlet node
Between be provided with pressure loading valve V8.
Described hydrogen stripper is first separation type or evaporation stripping type.
Described CO compressors and circulating nitrogen gas compressor is that centrifugal, piston compressor or both combinations are formed
All-in-one.
Described CO compressors and circulating nitrogen gas compressor are that motor drives or steam turbine one drag two drives.
The utility model has advantages below：
（1）Using the Two-way Cycle of CO compressions and nitrogen compression, play CO compression circulations energy consumption of rectification is low and nitrogen circulation
Compression energy consumption and invest low double dominant；
（2）The low-temperature receiver of thermal source and condenser to rectifying column evaporator optimizes configuration, the control of rectifying load is reliable,
It is stable；
（3）Nitrogen is set to compress, kind of refrigeration cycle can shorten the time for starting and purifying, and reduce the emptying of startup stage
Amount；
（4）Because energy consumption is low, startup is fast, cost of investment is few, discharge is few, there is good economic benefit and environmental benefit.
Brief description of the drawings
Fig. 1 is the structural representation of embodiment one of the present utility model；
Fig. 2 is the structural representation of embodiment two of the present utility model；
Fig. 3 is the structural representation of embodiment three of the present utility model；
Fig. 4 is the structural representation of example IV of the present utility model；
Fig. 5 is the structural representation of embodiment five of the present utility model；
In figure, 1- main heat exchangers A, 2- main heat exchanger B, 3- cold catch pot, 4- hydrogen strippers, 4A- low-flash tanks, 5-
Hydrogen stripper bottom of towe evaporator, 6- denitrification columns, 7- domethanizing columns, 8- domethanizing column bottom of towe evaporators, 9- denitrification column overhead condensations
Device, 10- CO compressors, 11- circulating nitrogen gas compressors, 12- turbo-expanders, 13- demethanizer column overhead condensers.
Embodiment
The utility model is further described below in conjunction with the accompanying drawings, the scope of protection of the utility model be not limited to
It is lower described：
Embodiment one：As shown in figure 1, a kind of use bicirculating CO cryogenic separations system, it includes main heat exchanger A1, master
Heat exchanger B2, cold catch pot 3, hydrogen stripper 4, hydrogen stripper bottom of towe evaporator 5, denitrification column 6, domethanizing column 7, domethanizing column
Bottom of towe evaporator 8, denitrification column overhead condenser 9, CO compressors 10 and circulating nitrogen gas compressor 11；Containing CO, hydrogen and a small amount of
The entrance of methane, nitrogen, the purified gas of argon gas successively with main heat exchanger A1 runners II and main heat exchanger B2 runners II is connected, and master changes
Hot device B2 runners II outlet is connected with the entrance of cold catch pot 3, the gaseous phase outlet of cold catch pot 3 successively with main heat exchanger
B2 runners III is connected with main heat exchanger A1 runners III entrance, and the liquid-phase outlet of cold catch pot 3 is divided into two strands：One stock-traders' know-how valve
It is connected after door V1 decompressions with main heat exchanger B2 runners I entrance, main heat exchanger B2 runners I outlet and the middle part of hydrogen stripper 4
Entrance is connected, and is connected after another stock-traders' know-how valve V2 decompressions with the top entry of hydrogen stripper 4；
In the present embodiment, the gaseous phase outlet of the hydrogen stripper 4 is connected with main heat exchanger A1 runners I entrance, hydrogen vapour
The liquid-phase outlet of stripper 4 is connected after valve V3 decompressions with the centre entrance of denitrification column 6；
In the present embodiment, the liquid-phase outlet of the denitrification column 6 is divided into two strands：One enters with main heat exchanger B2 runners IX's
Mouth is connected, and main heat exchanger B2 runners IX outlet is connected with the bottom inlet of denitrification column 6, with taking off after another stock-traders' know-how valve V4 decompressions
The runner II of nitrogen column overhead condenser 9 entrance is connected, in the runner II of denitrification column overhead condenser 9 outlet and domethanizing column 7
Portion's entrance is connected, and the gaseous phase outlet of denitrification column 6 is divided into two strands：One is connected with the runner I of denitrification column overhead condenser 9 entrance, takes off
The runner I of nitrogen column overhead condenser 9 outlet is connected with the top entry of denitrification column 6, after another stock-traders' know-how valve V7 decompression successively with
Main heat exchanger B2 runners VI is connected with main heat exchanger A1 runners VI entrance；
In the present embodiment, the liquid-phase outlet of the domethanizing column 7 through valve V6 decompression after with being mixed after valve V7 valve,
Entrance of the gaseous phase outlet of domethanizing column 7 successively with main heat exchanger B2 runners VIII and main heat exchanger A1 runners VIII is connected, main
Heat exchanger A1 runners VIII outlet is connected with the entrance of CO compressors 10, and the outlet of CO compressors 10 is divided into two strands：One is made
Go out battery limit (BL) for CO products, another strand as CO circulating air successively with main heat exchanger A1 runners VII's and main heat exchanger B2 runners VII
Entrance is connected, and main heat exchanger B2 runners VII outlet is connected after valve V5 decompressions with the top entry of domethanizing column 7；
In the present embodiment, the outlet of the circulating nitrogen gas compressor 11 is connected with main heat exchanger A1 runners IV entrance,
Main heat exchanger A1 runners IV outlet is divided into two strands：One is connected with the entrance of hydrogen stripper bottom of towe evaporator 5, another stock-traders' know-how valve
Mixed after door V8 decompressions with the outlet of hydrogen stripper bottom of towe evaporator 5, the entrance with main heat exchanger B2 runners IV is connected together, main
Heat exchanger B2 runners IV outlet is divided into two strands：One is connected with the entrance of domethanizing column bottom of towe evaporator 8, another stock-traders' know-how valve
Mixed after V9 decompressions with the outlet of domethanizing column bottom of towe evaporator 8, together the denitrification column overhead condenser 9 after valve V10 decompressions
Runner III entrance is connected, and the runner III of denitrification column overhead condenser 9 outlet mixes with the liquid nitrogen depressurized through valve V11, and one
Play the entrance successively with main heat exchanger B2 runners V and main heat exchanger A1 runners V to be connected, main heat exchanger A1 runners V outlet is with following
The entrance of ring nitrogen compressor 11 is connected, and completes nitrogen compression, kind of refrigeration cycle.
In the present embodiment, described hydrogen stripper 4 is evaporation stripping type.
In the present embodiment, described CO compressors 10 and circulating nitrogen gas compressor 11 are centrifugal compressor.
In the present embodiment, described CO compressors 10 and circulating nitrogen gas compressor 11 drive for motor.
During work：
S1, containing CO, hydrogen and a small amount of methane, nitrogen, argon gas purified gas through main heat exchanger A1 and main heat exchanger B2 quilts
Cold fluid cooling and partial condensation, progress first time separation in cold catch pot 3 is subsequently entered, the gas phase after separation is hydrogen-rich
Gas, go out battery limit (BL) after main heat exchanger B2 and main heat exchanger A1 re-heats to normal temperature, the liquid phase after separation is divided into two strands：One stock-traders' know-how valve
After V1 decompressions enter back into main heat exchanger B2 re-heats to certain temperature, the middle part for being sent into hydrogen stripper 4 participates in rectifying, another stock-traders' know-how valve
Do phegma in the top that hydrogen stripper 4 is sent directly into after door V2 decompressions；
S2, the further rectifying dehydrogenation by hydrogen stripper 4, the flashed vapour rich in hydrogen, flashed vapour are obtained at the top of it
Go out battery limit (BL) after main heat exchanger A1 re-heats to normal temperature, the rich CO liquid obtained in its bottom is sent into de- after pressure loading valve V3 decompressions
Continue rectifying in nitrogen tower 6, the bottom of hydrogen stripper 4 is provided with hydrogen stripper bottom of towe evaporator 5, provides what is risen for hydrogen stripper 4
Boil-off gas, thermal source is done using circulating nitrogen gas or purified gas；
S3, the further rectifying denitrogenation by denitrification column 6, the rich nitrogen obtained at the top of it is after pressure loading valve V7 decompressions
Mixed with methane-rich liquid, going out battery limit (BL) after main heat exchanger B2 and main heat exchanger A1 re-heats to normal temperature does fuel gas, in its bottom
Obtained rich CO liquid is sent into de- after pressure loading valve V4 decompressions enter back into the re-heat of denitrification column overhead condenser 9 to certain temperature
Continue rectifying in methane tower 7, the evaporator of the bottom of denitrification column 6 uses main heat exchanger B2 runner IX, and rising is provided for denitrification column 6
Boil-off gas, the top of denitrification column 6 is provided with denitrification column overhead condenser 9, phegma is provided for denitrification column 6, using rich CO liquid
Low-temperature receiver is done with liquid nitrogen；
S4, the further rectifying demethanation by domethanizing column 7, in the methane-rich liquid that its bottom obtains through pressure loading valve
Mixed with rich nitrogen after V6 decompressions and do fuel gas, the CO gas obtained at the top of it through main heat exchanger B2 and main heat exchanger A1 re-heats extremely
It is sent into after normal temperature in CO compressors 10, the middle pressure CO gas being pressurized through CO compressors 10 goes out battery limit (BL), small portion mostly as CO products
It is allocated as CO circulating air, first after main heat exchanger A1 and main heat exchanger B2 are cooled down, condense and are subcooled by cold fluid, then through pressure-reducing valve
Phegma is done at the top that domethanizing column 7 is sent into after door V5 decompressions, and the bottom of domethanizing column 7 is provided with domethanizing column bottom of towe evaporator 8,
The boil-off gas risen is provided for domethanizing column 7, thermal source is done using circulating nitrogen gas；
S5, the medium pressure nitrogen gas discharged from circulating nitrogen gas compressor 11 evaporate through main heat exchanger A1, hydrogen stripper bottom of towe successively
Device 5, main heat exchanger B2 and domethanizing column bottom of towe evaporator 8 are cooled down by cold fluid, condense and are subcooled, and the liquid nitrogen being too cold is through decompression
Supplement low-temperature receiver as denitrification column overhead condenser 9 after valve V10 decompressions, low pressure liquid nitrogen is wherein by partial gasification, then through master
It is sent into circulating nitrogen gas compressor 11 after heat exchanger B2 and main heat exchanger A1 re-heats to normal temperature to continue to be pressurized, so as to complete nitrogen pressure
Contracting, kind of refrigeration cycle.
In the present embodiment, CO compressors 10 control its inlet guide vane by inlet pressure（IGV）Aperture.
In the present embodiment, the inlet pressure of CO compressors 10 is 0.08MPa.G, pressure at expulsion 0.6MPa.G.
In the present embodiment, the inlet pressure of circulating nitrogen gas compressor 11 is 0.2MPa.G, pressure at expulsion 1.2MPa.G.
In the present embodiment, hydrogen stripper bottom of towe evaporator 5, domethanizing column bottom of towe evaporator 8 do heat using circulating nitrogen gas
Source.
In the present embodiment, domethanizing column 7 does overhead reflux liquid using circulation CO liquid.
In the present embodiment, denitrification column overhead condenser 9 does low-temperature receiver using rich CO liquid and liquid nitrogen.
In the present embodiment, the evaporator of the bottom of denitrification column 6 uses under main heat exchanger 2 heat exchange runner, main heat exchange
2 bottom that should be placed in denitrification column 6 under device.
In the present embodiment, the operating pressure of hydrogen stripper 4 is 1.7MPa.G.
In the present embodiment, the operating pressure of denitrification column 6 is 0.4MPa.G.
In the present embodiment, the operating pressure of domethanizing column 7 is 0.15MPa.G.
Embodiment 2：As shown in Fig. 2 the present embodiment and the difference of embodiment 1 are：In pressure loading valve V8 and main heat exchanger
Branched pipe is additionally provided with the connected passage in the outlet of A1 runners IV, the branched pipe is connected to turbine after being connected with pressure loading valve V12
On the entrance of expanding machine 12, the outlet of turbo-expander 12 is connected to main heat exchanger B2 runners V and the phase of main heat exchanger A1 runners V
On pipeline even.Going out main heat exchanger A1 runners IV outlet in medium pressure nitrogen gas increases one logistics, is sent after pressure loading valve V12
Enter the entrance of turbo-expander 12, the outlet of turbo-expander 12 is connected with low-pressure nitrogen house steward, device start or cold not
When sufficient, cold is produced using turbo-expander 12.
Embodiment 3：As shown in figure 3, the present embodiment and the difference of embodiment 1 are：The import of hydrogen stripper bottom of towe evaporator 5
Node and the Egress node of hydrogen stripper bottom of towe evaporator 5 are arranged on main heat exchanger A1 runner IIA and main heat exchanger B2 runners IIB
Connected pipeline, and set between the import node of hydrogen stripper bottom of towe evaporator 5 and the Egress node of hydrogen stripper bottom of towe evaporator 5
There is pressure loading valve V8A, the import node of hydrogen stripper bottom of towe evaporator 5 is connected to hydrogen stripper bottom of towe evaporator 5 by pipeline
In import, the Egress node of hydrogen stripper bottom of towe evaporator 5 is connected in the outlet of hydrogen stripper bottom of towe evaporator 5 by pipeline.I.e.
The thermal source of hydrogen stripper bottom of towe evaporator 5 uses purified gas, for some occasions can reduce circulation nitrogen compressor 11 flow and
Energy consumption.
Embodiment 4：As shown in figure 4, the present embodiment and the difference of embodiment 1 are：There was only one in the outlet of cold catch pot 3
Individual liquid-phase outlet and a gaseous phase outlet, the gaseous phase outlet of cold catch pot 3 are connected directly between entering for the B of main heat exchanger B2 runners III
On mouth, the liquid-phase outlet of cold catch pot 3 is connected to low-flash tank 4A middle part and decompression is provided with the pipeline of connection
Outlet at the top of valve V1A, low-flash tank 4A is connected on the entrance of main heat exchanger A1 runners I, low-flash tank 4A bottom
Outlet is connected to the middle part of denitrification column 6 and pressure loading valve V3 is provided with the pipeline of connection.Use low-flash tank 4A generations
For hydrogen stripper 4, for the less demanding occasion of the rate of recovery to CO and hydrogen, energy consumption and the investment of device can be reduced.
Embodiment 5：As shown in figure 5, the present embodiment and the difference of embodiment 1 are：
The liquid-phase outlet of the bottom of hydrogen gas tower 4 is connected to after being connected with pressure loading valve V3 on the entrance at the middle part of domethanizing column 7,
Demethanizer column overhead condenser 13 is also additionally provided with the upper position of domethanizing column 7, is set in demethanizer column overhead condenser 13
There are the D of runner I and the D of runner II, the bottom of domethanizing column 7 is provided with liquid-phase outlet, and the liquid-phase outlet of domethanizing column 7 flows with main heat exchanger B2
The entrance of road Ⅸ is connected, and the outlet of main heat exchanger B2 runners Ⅸ is connected on the lower entrances of domethanizing column 7, the top of domethanizing column 7
Gaseous phase outlet is provided with, domethanizing column gaseous phase outlet is connected to after pressure loading valve V7 on the centre entrance of denitrification column 6, domethanizing column 7
Branched pipe is also associated with the pipeline that gaseous phase outlet is connected with pressure loading valve V7, the branched pipe is connected to demethanizer column overhead condensation
On the D entrances of 13 runner of device I, the D of 13 runner of demethanizer column overhead condenser I outlets reconnect the upper entrance in domethanizing column 7.
The top of denitrification column 6 is provided with gaseous phase outlet, and the gaseous phase outlet of denitrification column 6 is connected in turn after pressure loading valve V13
On the B of main heat exchanger B2 runners VI, the A of main heat exchanger A1 runners VI, finally it is connected on fuel reservoir, goes out in the gas phase of denitrification column 6
Branched pipe is additionally provided between mouth and pressure loading valve B13, the branched pipe is connected to the C entrances of 9 runner of denitrification column overhead condenser I
On, the C of 9 runner of denitrification column overhead condenser I outlets are connected on denitrification column upper entrance, and the bottom of denitrification column 6 is provided with liquid-phase outlet,
The liquid-phase outlet of denitrification column 6 is connected to after pressure loading valve V14 on the C entrances of 9 runner of denitrification column overhead condenser II, denitrogenation column overhead
After the C of 9 runner of condenser II outlets are connected with the B of main heat exchanger B2 runners VIII, A, CO compressor 10 of main heat exchanger A1 runners VIII successively
It is connected on CO product holders, is provided with branched pipe on the pipeline that CO compressors 10 are connected with CO product holders, this point
Branch pipe is connected to the bottom of denitrification column 6 after the A of main heat exchanger A1 runners VII, the B of main heat exchanger B2 runners VII, pressure loading valve V5 successively
Porch.
Liquid nitrogen storage through pressure loading valve V11 successively with the B of main heat exchanger B2 runners V, the A of main heat exchanger A1 runners V, circulation
The entrance of nitrogen compressor 11 is connected, and is set on the pipeline that the entrance of circulating nitrogen gas compressor 11 is connected with the A of main heat exchanger A1 runners V
There is branched pipe, the branched pipe is connected on emptying device after controlled valve, and circulating nitrogen gas compressor 11 exports to be changed through master successively
The hot A of device A1 runners IV, the B of main heat exchanger B2 runners IV are connected, and the runner in the B exits of main heat exchanger B2 runners IV has two branch pipes,
One of branch pipe is connected to after pressure loading valve V12 on the D entrances of 13 runner of demethanation overhead condenser II, demethanizer column overhead
The D of 13 runner of condenser II outlets are connected on the pipeline that liquid nitrogen storage is connected with the B of main heat exchanger B2 runners V, another branch pipe
It is connected to after pressure loading valve V10 on the C entrances of 9 runner of denitrification column overhead condenser III, the C of 9 runner of denitrification column overhead condenser III
Outlet is again connected on the pipeline that liquid nitrogen storage is connected with the B of main heat exchanger B2 runners V.
Embodiment 5 using first demethanation nitrogen rejection again process route, suitable for requiring the demethanation of CO product coarses, smart denitrogenation
The occasion of gas.
Finally it should be noted that：Various embodiments above is only to illustrate the technical solution of the utility model, rather than it is limited
System；Although the utility model is described in detail with reference to foregoing embodiments, one of ordinary skill in the art should
Understand：It can still modify to the technical scheme described in foregoing embodiments, either to which part or whole
Technical characteristic carries out equivalent substitution；And these modifications or replacement, the essence of appropriate technical solution is departed from this practicality newly
The scope of each embodiment technical scheme of type.
Claims (4)
1. one kind uses bicirculating CO cryogenic separations system, it is characterised in that：Including main heat exchanger A（1）, main heat exchanger B
（2）, cold catch pot（3）, hydrogen stripper（4）, denitrification column（6）, domethanizing column（7）, denitrification column overhead condenser（9）, CO pressure
Contracting machine（10）, circulating nitrogen gas compressor（11）；
Described main heat exchanger A（1）In be set side by side with runner IA, runner IIA, the A of runner III, the A of runner IV, the A of runner V, runner
VI A, the A of runner VII, runner VIII A, main heat exchanger B（2）In be set side by side with runner IB, runner IIB, the B of runner III, the B of runner IV, stream
The B of road V, the B of runner VI, the B of runner VII, the B of runner VIII and runner Ⅸ, denitrification column overhead condenser（9）In be set side by side with IC, runner
IIC, the C of runner III；
Main heat exchanger A（1）Runner IIA porch be connected with mixing purified gas air inlet pipe, main heat exchanger A（1）Runner
IIA is exported and main heat exchanger B（2）Runner IIB entrances, main heat exchanger B（2）Runner IIB outlet and cold catch pot（3）'s
Entrance is connected, cold catch pot（3）Outlet include two liquid-phase outlets and a gaseous phase outlet, cold catch pot（3）Gas
Mutually outlet successively with main heat exchanger B（2）The B of runner III, main heat exchanger A（1）The A of runner III be connected with gas phase escape pipe, low temperature
Separator（3）In one of liquid-phase outlet successively with pressure loading valve V1, heat exchanger B（2）Runner IB be connected after final connection
In hydrogen stripper（4）Centre entrance on, cold catch pot（3）In another liquid-phase outlet be connected with pressure loading valve V2 after connect again
It is connected on hydrogen stripper（4）Upper entrance on, in hydrogen stripper（4）Top be provided with hydrogen stripper gaseous phase outlet, hydrogen stripper
Gaseous phase outlet and main heat exchanger A（1）Runner IA be connected after be finally connected on flashed vapour holder, hydrogen stripper（4）Bottom
Portion is provided with hydrogen stripper liquid-phase outlet, and hydrogen stripper liquid-phase outlet is reconnected in denitrification column after being connected with pressure loading valve V3（6）'s
On centre entrance；
Denitrification column（6）Bottom be provided with denitrification column liquid-phase outlet, denitrogenation liquid-phase outlet passes through pipeline and main heat exchanger B（2）In
Runner IX entrance is connected, main heat exchanger B（2）Runner IX outlet and denitrification column（6）Bottom inlet be connected, in denitrogenation liquid phase
Exit be connected again by another root pipeline with pressure loading valve V4 after again with denitrification column overhead condenser（9）Runner IIC's enters
Mouth is connected, denitrification column overhead condenser（9）Runner IIC outlet and domethanizing column（7）Centre entrance be connected, denitrification column（6）
Top be also provided with denitrification column gaseous phase outlet, denitrification column gaseous phase outlet be connected with pressure loading valve V7 after again successively with main heat exchanger B
（2）Runner VIB and main heat exchanger A（1）Runner VIA entrance is connected, main heat exchanger A（1）Runner VIA outlet is connected to combustion
Expect on holder, be provided with branched pipe on the pipeline that denitrification column gaseous phase outlet is connected with pressure loading valve V7, the branched pipe and denitrogenation
Column overhead condenser（9）Runner IC entrance is connected, denitrification column overhead condenser（9）Runner IC outlet and denitrification column（6）'s
Upper entrance is connected；
Described domethanizing column（7）Bottom be provided with domethanizing column liquid-phase outlet, domethanizing column liquid-phase outlet and pressure loading valve V6
Reconnected after being connected in pressure loading valve V7 and main heat exchanger B（2）On pipeline connected runner VIB, in domethanizing column（7）Top
Also it is provided with domethanizing column gaseous phase outlet, domethanizing column gaseous phase outlet and main heat exchanger B（2）Runner VIIIB is connected to master after being connected
Heat exchanger A（1）Runner VIIIA entrance on, main heat exchanger A（1）Runner VIIIA outlet and CO compressors（10）Enter
Mouth is connected, CO compressors（10）Outlet be connected with CO product holders, in CO compressors（10）Outlet and CO products store
Main heat exchanger A is also connected to by another pipeline on the connected pipeline of device（1）Runner VIIA import on, main heat exchanger A
（1）Runner VIIA outlet and main heat exchanger B（2）Runner VIIB be connected, main heat exchanger B（2）Runner VIIB and demethanation
Tower（7）Upper entrance be connected and be provided with pressure loading valve V5 on the pipeline of connection；
Described domethanizing column（7）Interior lower position is provided with domethanizing column bottom of towe evaporator（8）, circulating nitrogen gas compressor
（11）Outlet and main heat exchanger A（1）Runner IVA import is connected, main heat exchanger A（1）Runner IVA outlet and main heat exchanger
B（2）Runner IVB import be connected, main heat exchanger B（2）Runner IVB outlet and domethanizing column bottom of towe evaporator（8）'s
Import is connected, in main heat exchanger B（2）Runner IVB outlet and domethanizing column bottom of towe evaporator（8）The connected pipeline of import
On be additionally provided with branched pipe, it is cold that the branched pipe is connected to denitrogenation column overhead through pressure loading valve V10 again after being connected with pressure loading valve V9
Condenser（9）In the C of runner III import, domethanizing column bottom of towe evaporator（8）Outlet by pipeline be connected to pressure loading valve V9 with
On branched pipe connected pressure loading valve V10, in denitrification column overhead condenser（9）The C of runner III exit is provided with liquid nitrogen storage
Device, the exit of liquid nitrogen storage are provided with pressure loading valve V11, denitrification column overhead condenser（9）The C of runner III outlet and connection
The outlet of pressure loading valve V11 after liquid nitrogen storage merges, at the merging by pipeline successively with main heat exchanger B（2）Stream
The B of road V, main heat exchanger A（1）The A of runner V be connected, main heat exchanger A（1）The A of runner V outlet be connected to circulating nitrogen gas compression
Machine（11）Import on, main heat exchanger A（1）With circulating nitrogen gas compressor（11）The connected pipeline of import on also pass through branched pipe
It is connected with emptying device, switch valve is provided with the branched pipe；
Described hydrogen stripper（4）Interior lower position is provided with hydrogen stripper bottom of towe evaporator（5）, in main heat exchanger A（1）'s
Runner IVA and main heat exchanger B（2）Hydrogen stripper bottom of towe evaporator node and hydrogen are provided with pipeline connected runner IVB
Stripper bottom of towe evaporator outlet node, hydrogen stripper bottom of towe evaporator node is close to main heat exchanger A（1）Runner IVA mono-
Side, hydrogen stripper bottom of towe evaporator outlet node is close to main heat exchanger B（2）Runner IVB sides, hydrogen stripper bottom of towe evaporator enter
Mouth node is connected to hydrogen stripper bottom of towe evaporator by pipeline（5）Import on, hydrogen stripper bottom of towe evaporator outlet node
Hydrogen stripper bottom of towe evaporator is connected to by pipeline（5）In outlet, in hydrogen stripper bottom of towe evaporator node and hydrogen vapour
Pressure loading valve V8 is provided between stripper bottom of towe evaporator outlet node.
It is 2. according to claim 1 a kind of using bicirculating CO cryogenic separations system, it is characterised in that：Described hydrogen vapour
Stripper（4）For first separation type or evaporation stripping type.
It is 3. according to claim 1 a kind of using bicirculating CO cryogenic separations system, it is characterised in that：Described CO pressures
Contracting machine（10）With circulating nitrogen gas compressor（11）For centrifugal, the piston compressor all-in-one that either both combinations are formed.
It is 4. according to claim 1 a kind of using bicirculating CO cryogenic separations system, it is characterised in that：Described CO pressures
Contracting machine（10）With circulating nitrogen gas compressor（11）For motor driving or the driving of steam turbine one drag two.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107328166A (en) * | 2017-07-27 | 2017-11-07 | 成都深冷液化设备股份有限公司 | One kind uses bicirculating CO cryogenic separations system and its separation method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107328166A (en) * | 2017-07-27 | 2017-11-07 | 成都深冷液化设备股份有限公司 | One kind uses bicirculating CO cryogenic separations system and its separation method |
| CN107328166B (en) * | 2017-07-27 | 2023-02-10 | 成都深冷液化设备股份有限公司 | Double-circulation CO cryogenic separation system and separation method thereof |
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Address after: 611700 No. 335, Gangbei 4th Road, north area of Chengdu modern industrial port, Pidu District, Chengdu, Sichuan Patentee after: Sichuan Shudao Equipment Technology Co.,Ltd. Address before: 611700 No. 335, Gangbei 4th Road, north area of Chengdu modern industrial port, Pidu District, Chengdu, Sichuan Patentee before: CHENGDU SHENLENG LIQUEFACTION PLANT Co.,Ltd. |