CN208454846U - A kind of process unit separating ethane and carbon dioxide - Google Patents
A kind of process unit separating ethane and carbon dioxide Download PDFInfo
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- CN208454846U CN208454846U CN201821011186.0U CN201821011186U CN208454846U CN 208454846 U CN208454846 U CN 208454846U CN 201821011186 U CN201821011186 U CN 201821011186U CN 208454846 U CN208454846 U CN 208454846U
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Abstract
The utility model discloses a kind of process units for separating ethane and carbon dioxide, including sequentially connected dethanizer, dethanizer condenser, deethanizer reflux tank, deethanizer reflux pump, the deethanizer reflux pump discharge is divided into two-way, it is connect all the way with dethanizer top entry, another way is connect with carbon dioxide separation tower centre entrance；The carbon dioxide separation top of tower outlet, carbon dioxide separation tower condenser, carbon dioxide separation tower return tank, carbon dioxide separation tower reflux pump, carbon dioxide separation top of tower entrance are sequentially connected；The carbon dioxide separation tower return tank gaseous phase outlet, heat exchanger, level-one seperation film are sequentially connected, and the impermeable gas outlet of the level-one seperation film, heat exchanger, compressor, dethanizer centre entrance are sequentially connected.The utility model carries out the ethane for efficiently separating, producing high-purity of ethane and carbon dioxide using rectification process and membrane separation process, easy to operate.
Description
Technical field
The utility model relates to ethane purification techniques field, in particular to the technique dress of a kind of separation ethane and carbon dioxide
It sets.
Background technique
Domestic annual gas production is huge, and domestic natural gas yield reaches 1480.3 billion cubic meters, natural gas within 2017
In contain a large amount of ethane, be used to produce ethylene after being recycled, have good economic benefits.As domestic natural gas lighter hydrocarbons return
The development of receipts technology, can be more and more to recycle the lighter hydrocarbons recovery factory of ethane and the above component purpose of ethane.Since ethane returns
Minimum temperature is about -100 DEG C during receipts, carries out that dioxy can be controlled containing a small amount of carbon dioxide in the natural gas of recycling ethane
Changing carbon content not will cause the frozen block of ethane recovery process device and pipeline.The ethane and carbon dioxide of recycling are from deethanization tower top
Portion obtains, and cannot be kept completely separate ethane and carbon dioxide using rectification method.
Natural gas carbon dioxide removal generallys use hydramine method in industry, using the ethane after hydramine method carbon dioxide removal
In have vaporous water, to produce liquid ethane product, it is necessary to molecular sieve dehydration device is set after carbon dioxide removal, this
Sample not only increases investment, also increases operating cost.
Membrane separation technique have separative efficiency is high, low energy consumption, without phase-change, easy to operate, without secondary pollution, separation product is easy
In the recycling, high degree of automation the advantages that, thus using membrane separation technique be used to separate ethane and carbon dioxide have it is certain
Technical advantage.
Summary of the invention
The shortcomings that in order to overcome the prior art, the utility model provide the technique dress of a kind of separation ethane and carbon dioxide
It sets, can be realized ethane and carbon dioxide efficiently separates, produce the ethane of high-purity.The utility model combine rectification process and
The characteristics of membrane separation process, has many characteristics, such as easy to operate, without secondary pollution, reduction investment and increases economic efficiency, is suitable for
The mixture of ethane and carbon dioxide.
The technical scheme adopted by the utility model is a kind of process unit for separating ethane and carbon dioxide, including according to
Dethanizer, dethanizer condenser, deethanizer reflux tank, the deethanizer reflux pump of secondary connection, the dethanizer return
Stream pump discharge is divided into two-way, connect all the way with dethanizer top entry, and another way and carbon dioxide separation tower centre entrance connect
It connects；The carbon dioxide separation top of tower outlet, carbon dioxide separation tower condenser, carbon dioxide separation tower return tank, dioxy
Change carbon knockout tower reflux pump, carbon dioxide separation top of tower entrance is sequentially connected；The carbon dioxide separation tower return tank gas phase
Outlet, heat exchanger, level-one seperation film are sequentially connected, and the impermeable gas outlet of the level-one seperation film, compressor, takes off heat exchanger
Ethane tower centre entrance is sequentially connected.
Compared with prior art, the good effect of the utility model is: the utility model uses rectification process and UF membrane
Technique carries out the ethane for efficiently separating, producing high-purity of ethane and carbon dioxide, has easy to operate, without secondary pollution, drop
Low investment and the features such as increase economic efficiency.
Detailed description of the invention
The utility model will illustrate by example and with reference to the appended drawing, in which:
Fig. 1 is the system principle schematic diagram of the separation ethane of embodiment one and the process unit of carbon dioxide；
Fig. 2 is the system principle schematic diagram of the separation ethane of embodiment two and the process unit of carbon dioxide；
In figure: 1, pipeline；2, dethanizer；3, pipeline；4, dethanizer condenser；5, pipeline；6, deethanizer reflux
Tank；7, pipeline；8, deethanizer reflux pumps；9, pipeline；10, pipeline；11, pipeline；12, deethanizer reboiler；13, pipeline；
14, pipeline；15, carbon dioxide separation tower；16, pipeline；17, carbon dioxide separation tower condenser；18, pipeline；19, carbon dioxide
Knockout tower return tank；20, pipeline；21, carbon dioxide separation tower reflux pump；22, pipeline；23, pipeline；24, carbon dioxide separation
Tower reboiler；25, pipeline；26, pipeline；27, pipeline；28, heat exchanger；29, pipeline；30, level-one seperation film；31, pipeline；32,
Permeate air compressor；33, pipeline；34, cooler；35, pipeline；36, the second-order separation film；37, pipeline；38, pipeline；39, pipeline；
40, pipeline；41, compressor；42, pipeline.
Specific embodiment
Embodiment one
As shown in Figure 1, including dethanizer 2, dethanizer condenser 4, deethanizer reflux tank 6, deethanizer reflux
Pump 8, deethanizer reboiler 12, carbon dioxide separation tower 15, carbon dioxide separation tower condenser 17, carbon dioxide separation tower return
It flows tank 19, carbon dioxide separation tower reflux pump 21, carbon dioxide separation tower reboiler 24, heat exchanger 28, level-one seperation film 30, seep
Ventilative compressor 32, cooler 34, the second-order separation film 36, compressor 41 etc.；
2 top exit of dethanizer, dethanizer condenser 4, deethanizer reflux tank 6, deethanizer reflux pump
8,2 top entry of dethanizer passes sequentially through the connection of pipeline 3,5,7,9；2 lower part outlet of dethanizer, dethanizer boil again
Device 12,2 lower entrances of dethanizer pass sequentially through the connection of pipeline 11,13；2 bottom liquid phases of the dethanizer outlet and pipeline 14
Connection；
The deethanizer reflux pump 8,15 centre entrance of carbon dioxide separation tower are connected by pipeline 10；The titanium dioxide
15 top exit of carbon knockout tower, carbon dioxide separation tower condenser 17, carbon dioxide separation tower return tank 19, carbon dioxide separation
Tower reflux pump 21,15 top entry of carbon dioxide separation tower pass sequentially through the connection of pipeline 16,18,20,22；The carbon dioxide point
From 15 lower part outlet of tower, carbon dioxide separation tower reboiler 24,15 lower entrances of carbon dioxide separation tower pass sequentially through pipeline 23,
25 connections；The outlet of 15 bottom liquid phases of carbon dioxide separation tower is connect with pipeline 26；
19 gaseous phase outlet of carbon dioxide separation tower return tank, heat exchanger 28, level-one seperation film 30, infiltration air compressor
32, cooler 34, the second-order separation film 36 pass sequentially through the connection of pipeline 27,29,31,33,35,38；
30 impermeable gas of the level-one seperation film outlet, heat exchanger 28, compressor 41,2 centre entrance of dethanizer are successively
Pass through 39,40,42,1 connection.The second-order separation film 36 seeps vent outlet and connect with pipeline 37；
The dethanizer and carbon dioxide separation tower are plate column or packed tower.
The technique for separating ethane and carbon dioxide includes following content:
One, dethanizer:
Will from pipeline 1 after remove methane contain 5%~25% (molar content) carbon dioxide ethane and ethane with
Upper component (2000kPa.a~4000kPa.a) enters in the middle part of dethanizer 2 (1800kPa.a~3800kPa.a) as charging；
Carbonated ethane gas enters dethanizer condenser 4 by pipeline 3 from 2 top exit of dethanizer and condenses to -30 DEG C
~-5 DEG C, is entered after deethanizer reflux tank 6 by pipeline 5 and be pressurized to by pipeline 7 through deethanizer reflux pump 8
Be divided into two strands after 2200kPa.a~4400kPa.a: one (40%-80%) logistics enters at the top of dethanizer 2 through pipeline 9 to be made
The purity of ethane is improved for deethanizer reflux to reduce propane content in 2 tower overhead gas of dethanizer；Another stock (20%-
60%) logistics removes carbon dioxide through feeding in the middle part of pipeline 10 to carbon dioxide separation tower 15 from ethane.Dethanizer 2
Lower liquid phase enters after deethanizer reboiler 12 heats through pipeline 11 returns to 2 lower entrances of dethanizer through pipeline 13, according to
Subsequent processing product requirement, which controls the content of ethane in the liquid phase of dethanizer bottom, (to be normally controlled in 0.1%~3% to rub
That content)；Propane and the above component of propane are handled from 2 outlet at bottom of dethanizer through pipeline 14 to subsequent processing；
Two, the rectifying separation of carbon dioxide and ethane:
Carbonated ethane lime set from pipeline 10 enter carbon dioxide separation tower 15 (2500kPa.a~
4000kPa.a) middle part is as charging；Carbon dioxide gas rich in ethane passes through pipe from 15 top exit of carbon dioxide separation tower
Road 16 enters the condensation of carbon dioxide separation tower condenser 17 to -30 DEG C~0 DEG C, enters carbon dioxide separation tower by pipeline 18 and returns
Stream tank 19 carries out gas-liquid separation: wherein: the liquid phase after separation is pressurized to through pipeline 20 into carbon dioxide separation tower reflux pump 21
2900kPa.a~4400kPa.a enters at the top of carbon dioxide separation tower 15 through pipeline 22 to flow back as carbon dioxide separation tower, with
Ethane content in 15 tower overhead gas of carbon dioxide separation tower is reduced, the yield of ethane is improved；Gas phase after separation by pipeline 27 into
Enter 28 re-heat of heat exchanger and carries out UF membrane to entering level-one seperation film 30 through pipeline 29 after 10 DEG C~40 DEG C.Carbon dioxide separation tower
15 lower liquid phases enter after carbon dioxide separation tower reboiler 24 heats through pipeline 23 returns to carbon dioxide separation tower through pipeline 25
15 lower entrances require to carry out the content of carbon dioxide in carbon dioxide separation tower bottom liquid phase according to subsequent processing ethane product
It controls (molar content for being normally controlled in 0.5%-2%)；Ethane product is from 15 outlet at bottom of carbon dioxide separation tower through pipeline
26 to subsequent processing processing；
Three, the UF membrane of carbon dioxide and ethane:
Ethane and carbon dioxide gas mixture enter level-one seperation film 30 from pipeline 29 and carry out UF membrane: rich in the non-of ethane
Infiltration gas is cooled to -25 DEG C~0 DEG C into heat exchanger 28 by pipeline 39, is pressurized to through piping 40 into compressor 41
Entered in the middle part of dethanizer 2 by pipeline 42 as charging after 2500kPa.a~4000kPa.a, further recycle ethane, improved
The rate of recovery of ethane；Rich carbonated infiltration gas enters infiltration air compressor 32 by pipeline 31 and is pressurized to 2000kPa.a
After~4000kPa.a, enter the second-order separation through piping 25 after piping 33 is cooled to 30 DEG C~40 DEG C into cooler 34
Film 36 carries out UF membrane: the impermeable gas rich in ethane returns to 30 entrance of level-one seperation film by pipeline 38, further recycles second
Alkane improves the rate of recovery of ethane；Rich carbonated infiltration gas enters subsequent processing by pipeline 37 and handles.According to ethane
The requirement of product recovery rate, control pass through carbon dioxide molar content≤10% in the impermeable gas of level-one seperation film；Same time control
Ethane molar content≤5% in the infiltration gas that system passes through the second-order separation film.
Embodiment two
There is following difference in second of recyclable device process structure of the present embodiment and the first recyclable device process structure,
Other structures are all the same: it is handled as shown in Fig. 2, the infiltration gas rich in carbon dioxide gas enters subsequent processing by pipeline 31, it is real
The recyclable device for applying example two cancels setting infiltration air compressor 32, cooler 34, second level relative to the recyclable device of embodiment one
Except seperation film 36 and the pipeline 33 being sequentially connected, pipeline 35, pipeline 36, pipeline 37, pipeline 38, other structures are all the same.
There is following difference in second of recovery method of the present embodiment and the first recovery method, other processes are homogeneous
Same: rich carbonated infiltration gas enters subsequent processing by pipeline 31 and handles in step third step.According to ethane product
The requirement of the rate of recovery, control pass through carbon dioxide molar content≤10% in the impermeable gas of level-one seperation film, permeate second in gas
Alkane molar content≤5%.
Claims (7)
1. a kind of process unit for separating ethane and carbon dioxide, it is characterised in that: including sequentially connected dethanizer, de- second
Alkane tower condenser, deethanizer reflux tank, deethanizer reflux pump, the deethanizer reflux pump discharge are divided into two-way, all the way
It is connect with dethanizer top entry, another way is connect with carbon dioxide separation tower centre entrance；The carbon dioxide separation tower
Top exit, carbon dioxide separation tower condenser, carbon dioxide separation tower return tank, carbon dioxide separation tower reflux pump, dioxy
Change carbon separation column entrance to be sequentially connected；The carbon dioxide separation tower return tank gaseous phase outlet, heat exchanger, level-one seperation film
It is sequentially connected, the impermeable gas outlet of the level-one seperation film, heat exchanger, compressor, dethanizer centre entrance are sequentially connected.
2. a kind of process unit for separating ethane and carbon dioxide according to claim 1, it is characterised in that: the level-one
Infiltration vent outlet, infiltration air compressor, cooler and the second-order separation film of seperation film are sequentially connected.
3. a kind of process unit for separating ethane and carbon dioxide according to claim 2, it is characterised in that: the second level
The infiltration vent outlet of seperation film accesses subsequent processing by pipeline.
4. a kind of process unit for separating ethane and carbon dioxide according to claim 2, it is characterised in that: the second level
The impermeable gas outlet of seperation film returns to the entrance of level-one seperation film by pipeline.
5. a kind of process unit for separating ethane and carbon dioxide according to claim 1, it is characterised in that: described de-
Deethanizer reboiler is arranged in ethane tower lower part.
6. a kind of process unit for separating ethane and carbon dioxide according to claim 1, it is characterised in that: described two
Carbon dioxide separation tower reboiler is arranged in carbonoxide knockout tower lower part.
7. a kind of process unit for separating ethane and carbon dioxide according to claim 1, it is characterised in that: the de- second
Alkane tower and carbon dioxide separation tower are plate column or packed tower.
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| CN201821011186.0U CN208454846U (en) | 2018-06-28 | 2018-06-28 | A kind of process unit separating ethane and carbon dioxide |
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| CN201821011186.0U CN208454846U (en) | 2018-06-28 | 2018-06-28 | A kind of process unit separating ethane and carbon dioxide |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108546227A (en) * | 2018-06-28 | 2018-09-18 | 中国石油工程建设有限公司 | A kind of process unit and method of separation ethane and carbon dioxide |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108546227A (en) * | 2018-06-28 | 2018-09-18 | 中国石油工程建设有限公司 | A kind of process unit and method of separation ethane and carbon dioxide |
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20210225 Address after: No. 6, Sichuan hi tech Zone, sublime Road, Chengdu, Sichuan Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee after: CHINA NATIONAL PETROLEUM Corp. Address before: No. 6, Sichuan hi tech Zone, sublime Road, Chengdu, Sichuan Patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. |
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| TR01 | Transfer of patent right |