CN206858509U - Mixed carbon four integrated process dry gas comprehensive utilization device - Google Patents
Mixed carbon four integrated process dry gas comprehensive utilization device Download PDFInfo
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- CN206858509U CN206858509U CN201720690181.4U CN201720690181U CN206858509U CN 206858509 U CN206858509 U CN 206858509U CN 201720690181 U CN201720690181 U CN 201720690181U CN 206858509 U CN206858509 U CN 206858509U
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- outlet
- gas
- carbon
- hydrogen
- membrane separator
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- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 56
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000007789 gas Substances 0.000 claims abstract description 77
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000012528 membrane Substances 0.000 claims abstract description 35
- 239000001257 hydrogen Substances 0.000 claims abstract description 28
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 22
- 239000007791 liquid phase Substances 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000011084 recovery Methods 0.000 claims abstract description 13
- 239000002737 fuel gas Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims description 18
- 239000007792 gaseous phase Substances 0.000 claims description 4
- 238000009434 installation Methods 0.000 claims description 2
- 239000012510 hollow fiber Substances 0.000 claims 1
- 229930195733 hydrocarbon Natural products 0.000 abstract description 9
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 9
- 239000012071 phase Substances 0.000 abstract description 7
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- 238000006317 isomerization reaction Methods 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 5
- 238000007781 pre-processing Methods 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 4
- 239000001294 propane Substances 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000001273 butane Substances 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- 230000008595 infiltration Effects 0.000 description 2
- 238000001764 infiltration Methods 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- 235000013847 iso-butane Nutrition 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model relates to a mixed carbon four-in-one process dry gas comprehensive utilization device, which consists of a preheater, a membrane separator, a membrane post-condenser, a gas-liquid separation tank, a hydrogen compressor, a deethanizer and connecting pipelines therebetween, wherein the cold side of the preheater is connected with a dry gas inlet, the cold side material outlet of the preheater is connected with the air inlet of the membrane separator, the permeation gas outlet of the membrane separator is connected with the inlet of the hydrogen compressor, and the outlet of the hydrogen compressor is the outlet of recovered hydrogen material; the tail gas outlet of the membrane separator is connected with the hot side inlet of the membrane post-condenser, the hot side outlet of the membrane post-condenser is connected with the inlet of the gas-liquid separation tank, the liquid phase outlet of the gas-liquid separation tank is a carbon four-material recovery outlet, the gas phase outlet of the gas-liquid separation tank is connected with the deethanizer, the top of the deethanizer is a fuel gas outlet, and the bottom of the deethanizer is a carbon three liquefied gas outlet. The whole set of device has less equipment, low investment, high yield and strong applicability, and can be applied to the comprehensive utilization of various dry gases containing hydrogen and C1-C3 hydrocarbons.
Description
Technical field
The utility model belongs to petrochemical industry dry gas comprehensive utilization field, and four integral chemical industry of carbon is mixed more particularly to one kind
Skill dry gas comprehensive utilization device.
Background technology
The resource of mixing carbon four in China is very abundant, and by-product largely mixes carbon four in petroleum refining and Chemical Manufacture, by
In the backwardness of process aspect, its utilization rate is not high always, and only 40% or so, wherein most is used as fuel, only a small amount of
For chemicals market.Since the nineties in last century, have benefited from the progress of isolation technics, in terms of fine chemistry industry, mix carbon four
It is fully utilized.After 2012, with the decline of aromatisation deep processing, isomerization, alkylation are a dark horse, and carbon four is deep
Processing starts to step into development in pluralism.Therefore, on the basis of existing process technology, the utilization of C_4 hydrocarbon is developed to greatest extent
Value, the downstream product that development energy consumption is low, pollution is small, utilization rate is high, added value is high, it will turn into and improve petroleum chemical enterprise's synthesis competition
One important means of power.
Due to the continuous improvement of the continuous growth and environmental requirement of high-knock rating gasoline demand, in considerable time,
It is still the main utilization ways of C_4 hydrocarbon to produce environment protection type gasoline Blend Stocks.Contain C1~C3 hydro carbons in the mixing raw material of carbon four,
Carbon four purifies and hydrogen is added in isomerization process, and follow-up workshop section takes off C1~C3 hydro carbons and excess hydrogen from mixing carbon four
Remove, the dry gas containing C1~C3 hydro carbons and hydrogen produced during this, while a certain amount of carbon four can be carried in dry gas secretly, at present this
A little dry gas provide thermal source as fuel gas for boiler, or are directly vented burning as tail gas, and this processing mode causes three groups of carbon
The waste and the loss of C_4 hydrocarbon raw material divided, influences final products yield.The dry gas value of existing process is relatively low, causes to provide
The waste in source.Carbon three in dry gas, the component of carbon four and hydrogen are recycled, not only make full use of resource, reduces cost of material,
And embody the advantage of the mixing integrated apparatus of carbon four.
The content of the invention
The purpose of this utility model is to provide a kind of mixing integral process dry gas comprehensive utilization device of carbon four, and the device is fitted
It is strong with property, it can be applied to the comprehensive utilization of a variety of hydrogens and C1~C3 hydro carbons dry gas.
The utility model is realized by the following technical scheme：
One kind mixing the integral process dry gas comprehensive utilization device of carbon four, by preheater, membrane separator, film post-condenser,
Knockout drum, hydrogen gas compressor, dethanizer and connecting line therebetween are formed, preheater cold side connection dry gas entrance,
Preheater cold side material outlet is connected with membrane separator air inlet, and membrane separator oozes vent outlet and connected with hydrogen gas compressor entrance
Connect, hydrogen gas compressor outlet is recovery hydrogen material outlet；Membrane separator offgas outlet is connected with film post-condenser hot side entrance,
Film post-condenser hot side outlet is connected with knockout drum entrance, and knockout drum liquid-phase outlet is the outlet of recovery C 4 materials,
Knockout drum gaseous phase outlet is connected with dethanizer, and deethanizer overhead exports for fuel gas, and dethanizer tower reactor is carbon three
Liquefied gas exports.
The membrane separator includes gas separation membrane module.
Installation Ho llow fiber membrane for gas separation inside the gas separation membrane module.
The dethanizer is rectifying column.
Knockout drum liquid-phase outlet is connected with liquid phase pump.
The utility model discloses a kind of new equipment for mixing the integral process dry gas comprehensive utilization of carbon four.It will wait to locate first
Manage dry gas to merge, be preheated to higher than dew point, the hydrogen in dry gas, and carbon three, four groups of carbon are then separated by film separation system
Point.By economic value than reclaiming hydrogen, carbon three, the component of carbon four in relatively low dry gas, improve the utilization rate of mixing carbon four and do
The economic value of gas.The hydrogen purity of film separation system separation can be used as the mixing other dresses of the integral process of carbon four more than 80%
The hydrogen source put；Further isolated fuel gas, the liquefied gas of carbon three and the component of carbon four, wherein fuel gas can be made hydrocarbon mixture after film
For thermal source, the liquefied gas of carbon three can be used as civil liquefied gas to sell, and the component of carbon four of recovery can return to the mixing integral process of carbon four
The comprehensive utilization device of carbon four.The device use gaseous jet simulation technique take up an area it is small, energy consumption is low, simple to operate.Package unit
Equipment is few, investment is low, income is high, can be widely applied to mix the dry gas comprehensive utilization of the integrated production equipment of carbon four.
Brief description of the drawings
Fig. 1 is the integral process dry gas comprehensive utilization device sketch of the utility model mixing carbon four.
Description of reference numerals：
The pending dry gas of 1-, 2- recovery hydrogen, 3- fuel gas, the liquefied gas of 4- carbon three, 5- recovery carbon four
E1- preheaters, F1- membrane separators, E2- film post-condensers, V1- knockout drums, P1- liquid phase pumps, C1- hydrogen
Compressor, T1- dethanizers.
Embodiment
The utility model is described in further detail below in conjunction with the accompanying drawings：
As shown in Figure 1：One kind mixing integral process dry gas comprehensive utilization device of carbon four, by preheater (E1), UF membrane
Device (F1), film post-condenser (E2), knockout drum (V1), liquid phase pump (P1), hydrogen gas compressor (C1), dethanizer (T1) with
And connecting line therebetween is formed, pending dry gas (1) enters preheater (E1) cold side, preheater (E1) cold side material outlet and
Membrane separator (F1) air inlet connects, and membrane separator (F1) oozes vent outlet and is connected with hydrogen gas compressor (C1) entrance, hydrogen pressure
Contracting machine (C1) outlet material is recovery hydrogen (2), membrane separator (F1) offgas outlet and film post-condenser (E2) hot side entrance phase
Even, film post-condenser (E2) hot side outlet is connected with knockout drum (V1) entrance, and knockout drum (V1) gaseous phase outlet is with taking off
Ethane tower (T1) connects, and dethanizer (T1) tower top outlet material is fuel gas (3), and dethanizer (T1) tower reactor outlet material is
The liquefied gas of carbon three (4), knockout drum (V1) liquid-phase outlet are connected with liquid phase pump (P1), and liquid phase pump (P1) outlet material is mixed
Close carbon four (5).
Caused dry gas during the integral process of carbon four is mixed, pressure mainly contains hydrogen, first in 1.8~2.5MpaG
The components such as alkane, ethane, ethene, propane, propylene, iso-butane and normal butane, the difference formed according to mixing carbon 4 liquid gas raw material,
The composition of each component is slightly different above.Because dry gas contains hydrogen, dew point is relatively low, causes the entrainment of carbon three, the component of carbon four.
The utility model is first separated the hydrogen in dry gas with gaseous jet simulation, improves the dew point of dry gas, then condense recovery carbon three,
The component of carbon four.The preheated device of pending dry gas (1) (E1) enters membrane separator (F1), film after being heated to remote dew point certain temperature
The effect of separator (F1) is to separate the hydrogen in dry gas with other macromolecular components, and membrane separator (F1) has two gases
Outlet, one is infiltration gas, and another is tail gas after film, and infiltration gas key component is recovery hydrogen (2), through hydrogen gas compressor
(C1) sent outside after pressure-raising；Tail gas is the dry gas of removing hydrogen after film, is entered after film post-condenser (E2) is condensed into gas-liquid two-phase
Knockout drum (V1), the wherein constituent content of liquid-phase C four is higher, and the mixing integral process of carbon four is delivered to through liquid phase pump (P1)
Other devices；The gas phase of knockout drum (V1) mainly contains methane, ethane, ethene, propane, propylene etc., and this burst of gas phase is entered
Enter dethanizer (T1), after separation, the component such as overhead extraction methane, ethane, ethene, fuel gas (3), tower reactor extraction can be used as
The components such as propane, propylene, civil liquefied gas (4) can be used as to sell.
Embodiment：
Certain fine chemistry industry integral process of carbon four includes raw material preprocessing device, butane isomerization device, dehydrogenation of isobutane
Device, MTBE devices and related intermediate reaction thing recovery EGR, wherein raw material preprocessing device and butane isomerization dress
Putting has dry gas discharge.This two strands of dry gas are merged, recycled using device provided by the utility model.Two strands are waited to locate
Reason dry gas, which mainly forms, is shown in Table 1.
The dry gas of table 1 mainly forms (mol%)
Raw material preprocessing device dry gas and alkane isomerization unit dry gas enter preheater E1 cold sides after merging, and preheater E1 is
One shell-and-tube heat exchanger, heating medium are low-pressure steam.Preheater E1 cold sides material outlet is connected with membrane separator F1 air inlets,
Filling Ho llow fiber membrane for gas separation component inside membrane separator F1.Membrane separator F1 oozes vent outlet and hydrogen gas compressor C1
Entrance connects, and hydrogen gas compressor C1 is a centrifugal compressor.Hydrogen gas compressor C1 outlet materials are recovery hydrogen.Membrane separator
F1 offgas outlets are connected with film post-condenser E2 hot side entrances, and film post-condenser E2 is a shell-and-tube heat exchanger, and cooling medium is
Regular circulation water, upper 30 DEG C of coolant-temperature gage, 37 DEG C of return water temperature.Film post-condenser E2 hot side outlets connect with knockout drum V1 entrances
Connect, knockout drum V1 is horizontal pressure-resistant storage tank.Knockout drum V1 gaseous phase outlets are connected with dethanizer T1, dethanizer T1
For the rectifying column of an inside filling random packing.Dethanizer T1 tower top outlets material is fuel gas, and dethanizer T1 tower reactors go out
Mouth material is the liquefied gas of carbon three.Knockout drum V1 liquid-phase outlets are connected with liquid phase pump P1, and liquid phase pump P1 uses centrifugal pump, liquid phase
Pump P1 outlet materials are mixing carbon four.
Detailed process flow is as follows：Mixing dry gas pressure 1.8MpaG, preheated device enter UF membrane after being heated to 75 DEG C
Device, after separation, atmospheric pressure 0.2MpaG is permeated after film, wherein hydrogen content is more than 80%, into after hydrogen gas compressor pressure-raising
The hydrogenation reactor of raw material preprocessing device is returned as hydrogen source.Film rear molding atmospheric pressure 1.6MpaG, compared with dry gas before film, hydrogen
Gas removal efficiency reaches 70%.Tail gas is condensed to 35 DEG C into recirculated water cooling condenser after film, into knockout drum, the liquid after separation
The content of phase carbon four is higher, and as the backflow of raw material preprocessing device depropanization, the component of carbon four therein is entered by depropanizing tower tower reactor
Enter follow-up butane isomerization device.The gas phase of knockout drum enters dethanizer, and overhead extraction is done after dethanizer separates
Gas, the light components such as methane, ethane, ethene are mainly contained, fuel gas can be used as；Tower reactor extraction propane, propylene and a small amount of carbon four, can
Sold as civil liquefied gas.Each outlet material composition is shown in Table 2.
Each outlet material composition (mol%) of the dry gas comprehensive utilization device of table 2
Example described above is only the preferred embodiment for absolutely proving the utility model and being lifted, guarantor of the present utility model
Protect scope not limited to this.The equivalent substitute or conversion that those skilled in the art are made on the basis of the utility model,
Within the scope of protection of the utility model.The scope of protection of the utility model is defined by claims.
Claims (5)
1. one kind mixing integral process dry gas comprehensive utilization device of carbon four, by preheater, membrane separator, film post-condenser, gas
Liquid knockout drum, hydrogen gas compressor, dethanizer and connecting line therebetween are formed, it is characterized in that preheater cold side connects dry gas
Entrance, preheater cold side material outlet are connected with membrane separator air inlet, and membrane separator oozes vent outlet and entered with hydrogen gas compressor
Mouth connection, hydrogen gas compressor outlet are recovery hydrogen material outlet；Membrane separator offgas outlet and film post-condenser hot side entrance
It is connected, film post-condenser hot side outlet is connected with knockout drum entrance, and knockout drum liquid-phase outlet is recovery C 4 materials
Outlet, knockout drum gaseous phase outlet are connected with dethanizer, and deethanizer overhead exports for fuel gas, and dethanizer tower reactor is
The liquefied gas of carbon three exports.
2. device as claimed in claim 1, it is characterized in that the membrane separator includes gas separation membrane module.
3. device as claimed in claim 2, it is characterized in that installation hollow fiber gas point inside the gas separation membrane module
From film.
4. device as claimed in claim 1, it is characterized in that the dethanizer is rectifying column.
5. device as claimed in claim 1, it is characterized in that knockout drum liquid-phase outlet is connected with liquid phase pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720690181.4U CN206858509U (en) | 2017-06-14 | 2017-06-14 | Mixed carbon four integrated process dry gas comprehensive utilization device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720690181.4U CN206858509U (en) | 2017-06-14 | 2017-06-14 | Mixed carbon four integrated process dry gas comprehensive utilization device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206858509U true CN206858509U (en) | 2018-01-09 |
Family
ID=60831858
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720690181.4U Active CN206858509U (en) | 2017-06-14 | 2017-06-14 | Mixed carbon four integrated process dry gas comprehensive utilization device |
Country Status (1)
| Country | Link |
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| CN (1) | CN206858509U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108507277A (en) * | 2018-04-28 | 2018-09-07 | 中国石油工程建设有限公司 | A kind of the cold comprehensive utilization device and method of natural gas ethane recovery |
-
2017
- 2017-06-14 CN CN201720690181.4U patent/CN206858509U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108507277A (en) * | 2018-04-28 | 2018-09-07 | 中国石油工程建设有限公司 | A kind of the cold comprehensive utilization device and method of natural gas ethane recovery |
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