CN209237905U - Co-production method is obtained the system and device that high-content butene-1 prepares raw material by carbon four - Google Patents
Co-production method is obtained the system and device that high-content butene-1 prepares raw material by carbon four Download PDFInfo
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- CN209237905U CN209237905U CN201821515661.8U CN201821515661U CN209237905U CN 209237905 U CN209237905 U CN 209237905U CN 201821515661 U CN201821515661 U CN 201821515661U CN 209237905 U CN209237905 U CN 209237905U
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- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 title claims abstract description 64
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 55
- 239000002994 raw material Substances 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 claims abstract description 87
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims abstract description 86
- 238000006703 hydration reaction Methods 0.000 claims abstract description 42
- 230000036571 hydration Effects 0.000 claims abstract description 27
- 238000011084 recovery Methods 0.000 claims abstract description 17
- 239000003112 inhibitor Substances 0.000 claims abstract description 15
- 238000000605 extraction Methods 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000000047 product Substances 0.000 claims abstract description 9
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 5
- 239000000203 mixture Substances 0.000 claims abstract description 5
- 238000006243 chemical reaction Methods 0.000 claims description 27
- 238000000034 method Methods 0.000 claims description 22
- 238000012856 packing Methods 0.000 claims description 22
- 239000003054 catalyst Substances 0.000 claims description 21
- 230000008569 process Effects 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 9
- 238000007747 plating Methods 0.000 claims description 8
- 150000001336 alkenes Chemical class 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 5
- 239000003456 ion exchange resin Substances 0.000 claims description 5
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 4
- 239000004744 fabric Substances 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 2
- 239000011521 glass Substances 0.000 claims description 2
- 238000006555 catalytic reaction Methods 0.000 claims 2
- 239000003795 chemical substances by application Substances 0.000 claims 2
- 238000002156 mixing Methods 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 5
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 10
- 230000003197 catalytic effect Effects 0.000 description 6
- 238000004821 distillation Methods 0.000 description 6
- -1 C12 alkene Chemical class 0.000 description 5
- 239000000945 filler Substances 0.000 description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 2
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 235000019441 ethanol Nutrition 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- 238000012946 outsourcing Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- IAQRGUVFOMOMEM-ONEGZZNKSA-N trans-but-2-ene Chemical compound C\C=C\C IAQRGUVFOMOMEM-ONEGZZNKSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000013538 functional additive Substances 0.000 description 1
- 235000013847 iso-butane Nutrition 0.000 description 1
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical class CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 1
- 125000000959 isobutyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])* 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000010977 jade Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 238000000622 liquid--liquid extraction Methods 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N sec-butylidene Natural products CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000005829 trimerization reaction Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
This application provides a kind of co-production methods to obtain the system and device that high-content butene-1 prepares raw material by carbon four, the composition of this system device includes superposition reactor, four knockout tower of hydration reactor, tert-butyl alcohol recovery tower and carbon, product is overlapped to hydration reactor, hydration reaction product is to tert-butyl alcohol recovery tower, the overhead line of tert-butyl alcohol recovery tower is back to inhibitor head tank, tower bottom pipeline and the water inlet pipe mouth for passing to hydration reactor, and hydration reactor overhead line is connected to four knockout tower of carbon.The technical program realizes depth removal isobutene in mixing carbon four, while from inhibitor consumption is more filled, last residual carbon four also being made to become the extraction raw material for extracting butene-1 most economic benefit.
Description
Technical field
Present patent application is related to the fraction fourth after petrochemical industry, more particularly to mixing four raw material of carbon removal isobutene
The method and its system and device that alkene -1 extracts.
Background technique
Energetically with " embodiment about expanding the production of bio-fuel ethyl alcohol and promoting the use of vehicle-use alcohol gasoline "
Promotion and implementation, MTBE face the reality disabled comprehensively under, it is necessary to consider that original MTBE process units utilizes and carbon four is applied
The technical problems such as prospect.
In the case where facing the reality that MTBE is disabled comprehensively, one of the best applications approach of isobutene in C-4-fraction is mixed
It is isobutene overlapping production C8/C12 alkene, residual carbon four can be used as raw material for alkylation.Currently, to realize that isobutene depth turns
Change, isobutene overlapping production is mainly catalytic distillation process, under normal circumstances, isobutene content in the residual carbon four after catalytic distillation
It can achieve≤0.3%, theoretically the residual carbon prepares raw material fourth is that can be used as butene-1 extraction, but, since isobutene overlaps
Part butene-1 participates in isobutylene copolymers reaction in reaction, and isomerization reaction occurs there are also part butene-1 and generates Trans-2-butene, leads
Under causing the butene-1 yield value in residual carbon four relatively low.If the residual carbon four is prepared raw material as butene-1 extraction, because folded
Butene-1 consumption is more in conjunction reaction, and loss amount reaches 50-70%, so do not have the economic value of butene-1 high-volume production,
If using the mating coproduction butene-1 device of original MTBE just with less the economy of large-scale production.
Isobutene overlapping is using ion exchange resin as catalyst, and needing to add the tert-butyl alcohol in technological design is inhibitor
Inhibit alkene trimerization and four poly- reactions.In building-up reactions, the inhibitor tert-butyl alcohol can be etherified anti-with isobutene under the action of catalyst
It answers, therefore there are the consumption of tert-butyl alcohol inhibitor.For this purpose, being this consumption of supplement reaction process in technological design, need
Outsourcing tert-butyl alcohol product.
Summary of the invention
Present invention purpose is that abandoning existing is the catalytic distillation coincidence process for realizing isobutene high conversion,
A kind of co-production method is provided, the system and device that high-content butene-1 prepares raw material is obtained by carbon four, realizes isobutyl in depth removal carbon four
While alkene, have inhibitor tert-butyl alcohol recycling ability on the one hand to supplement the consumption of isobutene building-up reactions, it is often more important that
Residual carbon four is set to have the raw material as butene-1 high-volume production economic value.
A kind of co-production method provided by the present application is obtained the system and device that high-content butene-1 prepares raw material by carbon four, by technique
Route process, the composition of this system device include superposition reactor, four knockout tower of hydration reactor, tert-butyl alcohol recovery tower and carbon,
The superposition reactor is interior fixed bed reactors, shell and tube reactor or the expanded bed for loading ion-exchange resin catalyst
One of any in reactor, the tert-butyl alcohol recovery tower and four knockout tower of carbon are azeotrope tower, and hydration reactor is
Extraction tower, overlapping product line are connected to hydration reactor, and hydration reaction product is connected to tert-butyl alcohol recovery tower by tower bottom pipeline,
The overhead line of tert-butyl alcohol recovery tower is back to inhibitor head tank, tower bottom pipeline and the water inlet pipe mouth for passing to hydration reactor,
Hydration reactor overhead line is connected to four knockout tower of carbon for implementing carbon four and C8/C12 separation of olefins.
In above-mentioned overall technical architecture, as the extraction tower of isobutene hydration reaction device, filling-material structure is set in tower
Tower tray, the upper section of packing section are the regular packing without catalyst, and lower section is the regular packing of loading catalyst, the hole of regular packing
Gap rate 10% ~ 80%, catalyst exchange capacity 3.0 ~ 5.4mmolH+/g butt.
As the optimization technique means of the technical program, the porosity 40% ~ 60% of regular packing, catalyst exchange capacity
5.0 ~ 5.4mmolH+/g butt.
Butene-1 is the raw material for synthesizing sec-butyl alcohol, dehydrogenation butadiene, is important one of basic chemical industry raw material.Carbon four evaporates
Mainly there is butene-1 in point, along components such as 2- butylene, Trans-2-butene, isobutene, normal butane, iso-butanes, wherein due to butylene-
1 and isobutene boiling point it is very close, only 0.6 DEG C of difference, the separation that conventional rectification method both can not be implemented.Not banned
Period, MTBE preparation be react by isobutene with methanol produce MTBE, thus remove mix carbon four in isobutene, and
The smallest separation method of butene-1 loss amount.As MTBE is disabled comprehensively, technical scheme is to solve above-mentioned skill at present
The effective scheme of art problem, application scheme organically combine and combine isobutene hydration reaction with isobutene building-up reactions,
The organic joint setting of twice reaction process realizes that isobutene is removed by depth efficient in mixing carbon four, has abandoned existing isobutene
Catalytic distillation method is overlapped, avoids the technical problem that butene-1 loss amount in catalytic distillation is big in material component, effectively
The butene-1 component in raw material is remained, loss amount is greatly reduced, and the 20-40% of only former butene-1 component amount makes last
Residual carbon four becomes the extraction raw material for extracting butene-1 most economic benefit, compensates for and efficiently separates disabled because of MTBE comprehensively after
Isobutene and butene-1 technological gap；The self-loopa supplement that technical scheme also achieves functional additive uses: wherein
Hydration reaction while further removal isobutene, the inhibitor tert-butyl alcohol required for output building-up reactions eliminates suppression
The outsourcing cost of preparation, remaining water to hydration reaction is recycled after tert-butyl alcohol recycling.The technical program also has technique stream
Journey is short, isobutene conversion is high, butene-1 loss is small, it is outstanding excellent that production tert-butyl alcohol economic benefit is hydrated using remaining isobutene
Point more can effectively utilize existing MTBE Preparation equipment, realize the transformation of high benefit production technology.
Detailed description of the invention
Fig. 1 is the system and device structural map of the application.
Fig. 2 is the tower principle assumption diagram of hydration reactor.
Fig. 3 is I filler element structure figure of the top Fig. 2 packing section.
Fig. 4 is the filling-material structure figure of the lower part Fig. 2 packing section II.
Specific embodiment
As shown, the application realizes that co-production method is filled by the system that carbon four obtains the method that high-content butene-1 prepares raw material
It sets, is moved towards by process line process, including superposition reactor 1, four knockout tower 4 of hydration reactor 2, tert-butyl alcohol recovery tower 3 and carbon.
The superposition reactor 1 is interior fixed bed reactors, shell and tube reactor or the expansion for loading ion-exchange resin catalyst
One of any in bed reactor, the feed line 101 in figure be the feed line of mixing carbon four, and another feed line 102 is
Inhibitor pipeline；The hydration reactor 2 is extraction tower；The tert-butyl alcohol recovery tower 3 and four knockout tower 4 of carbon is azeotropic
Destilling tower.Overlapping product line 103 is connected to hydration reactor 2, and hydration reaction product is connected to the tert-butyl alcohol by tower bottom pipeline 201
Recovery tower 3, the overhead line 301 of tert-butyl alcohol recovery tower are back to inhibitor head tank, tower bottom pipeline 302 and pass to hydration reaction
The water inlet pipe mouth of device 2；2 overhead line 202 of hydration reactor is connected to implementation carbon four and separates with the carbon four of C8/C12 separation of olefins
Tower 4, the tower bottom pipeline 401 and overhead line 402 of four knockout tower 4 of carbon are respectively four pipeline of residual carbon and C8/C12 olefin product pipe
Line.
The co-production method realized by above-mentioned system and device obtains the method that high-content butene-1 prepares raw material by carbon four:
Step 1: isobutene building-up reactions
In fixed bed reactors, shell and tube reactor or expanded bed reactor it is one of any in it is folded by well known isobutene
It closes process, under ion-exchange resin catalyst and the effect of the inhibitor tert-butyl alcohol, is with the mixing carbon four containing isobutene
Raw material implements the operation of isobutene building-up reactions.Fixed bed reactors, shell and tube reactor or the expanded bed reactor can be with
It is more serial or parallel connection operations.The mixing carbon four is not limited to following four raw material of several carbon: cracking c_4, isobutene contain
Amount is about 35 ~ 46wt%, and catalytically cracked C four, isobutene content is about 9 ~ 25wt%, residual carbon four, and isobutene content is about
2 ~ 5wt%, or the mixture of above several carbon four.Well known building-up reactions process can be used in this isobutene building-up reactions,
What this only casted a brick to attract jade enumerates a method and process condition: temperature is 40 ~ 100 DEG C, pressure is 0.5 ~ 2.0MPa, air speed be 0.2 ~
5h-1, inhibitor additive amount are the 0.1% ~ 5% of four raw material of carbon by mass percentage.
Step 2: isobutene hydration reaction
The overlapping product of step 1 enters extraction tower, and hydration overlapping product is inversely gone in tower, implements isobutene hydration
While reaction, the separation of the tert-butyl alcohol is completed in liquid-liquid extraction.For extraction tower as isobutene hydration reaction device 2, tower is interior to be arranged filler
The extraction tower of structure tower tray is to be preferably selected, the extraction tower: the rule without catalyst being intervally arranged are arranged in the top packing section I of tower
Then filler component A, the regular packing component A are silk screen, corrugated plating or uniformly distributed porose corrugated plating, are hydrated for control anti-
Answer the t butanol content of 2 overhead line 202 of device；The lower part packing section II of tower is to load the regular packing structure of hydration catalyst,
Promote isobutene and water that hydration reaction occurs and obtains the tert-butyl alcohol.Wherein hydration catalyst is wrapped up by glass fabric or wire mesh
At plate catalyst filling B, with the regular packings component A ' such as silk screen, the corrugated plating or uniformly distributed porose corrugated plating staggeredly row of interval
Cloth, as shown in figure 4, one or more pieces regular packings component A ' is arranged between two hydration catalyst filler B, preferably two panels is regular
Filler component A ', the porosity 10% ~ 80% of uniformly distributed porose regular packing component, catalyst exchange capacity are 3.0 ~ 5.4mmolH
+/g butt, wherein the porosity of uniformly distributed porose regular packing component is preferably 40% ~ 60%, catalyst exchange capacity is preferably
5.0 ~ 5.4mmolH+/g butt.Be in the reaction condition of this extraction tower: reaction temperature be 40 ~ 100 DEG C, 0.4 ~ 2.1MPa of pressure,
Than 0.2 ~ 10, optimum reaction condition is water/oil quality: 50 ~ 70 DEG C, 0.4 ~ 1.5MPa of pressure, water/oil quality than 1 ~ 4, isobutyl
Alkene conversion ratio is stablized compared to higher.The hydration reactor of filling-material structure through this embodiment, the carbon four that process separates after
It is≤0.2wt% containing isobutene, butene-1 loss late is lower, and compared to the amount of mixing carbon four, butene-1 loss late is lower than 40%.
The isobutene building-up reactions method of step 1, although the conversion ratio of isobutene is not high compared with catalytic distillation process,
The conversion of remaining isobutene in carbon four is completed by the hydration reaction method of step 2, two processing steps are combined, and manage realizing
While the isobutene deep conversion rate thought, the inhibitor tert-butyl alcohol needed for acquisition step 1 reaction, and two processing steps
Another big gratifying place that coproduction combines is to reduce the loss of butene-1, using original MTBE production technology, butene-1
Loss 50 ~ 70%, the loss of the application only has 20 ~ 40%, then by after separation process below, butene-1 in residual carbon four
The economic scale benefit production requirement extracted of satisfaction.
Step 3: the tert-butyl alcohol recycles
The hydration reaction product of step 2 in the azeotrope tower as tert-butyl alcohol recovery tower 3 carry out tert-butyl alcohol separation,
The overhead line 301 of this azeotrope tower is back to the inhibitor head tank of step 1, and the reflux of water recovery line 302 of tower bottom is simultaneously
Pass to the water inlet pipe mouth of hydration reactor 2；
Step 4: carbon four separates: implementing carbon in the azeotrope tower as four knockout tower 4 of carbon to the tower top material of step 2
Four with the separation of C8/C12 alkene, the tower bottom pipeline 401 and overhead line 402 of four knockout tower 4 of carbon be respectively four pipeline of residual carbon
With C8/C12 olefin product pipeline.
Claims (5)
1. a kind of co-production method is obtained the system and device that high-content butene-1 prepares raw material by carbon four, it is characterised in that press process line
Process, the composition of this system device include superposition reactor, four knockout tower of hydration reactor, tert-butyl alcohol recovery tower and carbon, described
Superposition reactor be interior to load the fixed bed reactors of ion-exchange resin catalyst, shell and tube reactor or expanded bed reaction
One of any in device, the tert-butyl alcohol recovery tower and four knockout tower of carbon are azeotrope tower, and hydration reactor is extraction
Tower, overlapping product line are connected to hydration reactor, and hydration reaction product is connected to tert-butyl alcohol recovery tower, tertiary fourth by tower bottom pipeline
The overhead line of alcohol recovery tower is back to inhibitor head tank, tower bottom pipeline and the water inlet pipe mouth for passing to hydration reactor, hydration
Reactor overhead line is connected to four knockout tower of carbon for implementing carbon four and C8/C12 separation of olefins.
2. system according to claim 1 device, it is characterised in that the fixed bed reactors, shell and tube reactor or
Expanded bed reactor is more and is in series or in parallel to form.
3. system and device according to claim 1 or 2, it is characterised in that the extraction as isobutene hydration reaction device (2)
Tower, tower is interior to be arranged filling-material structure tower tray, and the regular packing component without catalyst being intervally arranged, lower section is arranged in the upper section of packing section
For the regular packing structure of loading catalyst, the regular packing component is silk screen, corrugated plating or uniformly distributed porose corrugated plating；
Hydration catalyst is rolled into plate catalyst filling by glass fabric or wire mesh, and silk screen, corrugated plating or is evenly equipped with hole
Corrugated plating regular packing component staggeredly be intervally arranged.
4. system and device according to claim 3, it is characterised in that the porosity 10% ~ 80% of regular packing component, catalysis
Agent exchange capacity 3.0 ~ 5.4mmolH+/g butt.
5. system and device according to claim 4, it is characterised in that the porosity 40% ~ 60% of regular packing component, catalysis
Agent exchange capacity 5.0 ~ 5.4mmolH+/g butt.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821515661.8U CN209237905U (en) | 2018-09-17 | 2018-09-17 | Co-production method is obtained the system and device that high-content butene-1 prepares raw material by carbon four |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201821515661.8U CN209237905U (en) | 2018-09-17 | 2018-09-17 | Co-production method is obtained the system and device that high-content butene-1 prepares raw material by carbon four |
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| Publication Number | Publication Date |
|---|---|
| CN209237905U true CN209237905U (en) | 2019-08-13 |
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|---|---|---|---|
| CN201821515661.8U Withdrawn - After Issue CN209237905U (en) | 2018-09-17 | 2018-09-17 | Co-production method is obtained the system and device that high-content butene-1 prepares raw material by carbon four |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109012504A (en) * | 2018-09-17 | 2018-12-18 | 丹东明珠特种树脂有限公司 | Co-production method is obtained the method and its system and device that high-content butene-1 prepares raw material by carbon four |
-
2018
- 2018-09-17 CN CN201821515661.8U patent/CN209237905U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109012504A (en) * | 2018-09-17 | 2018-12-18 | 丹东明珠特种树脂有限公司 | Co-production method is obtained the method and its system and device that high-content butene-1 prepares raw material by carbon four |
| CN109012504B (en) * | 2018-09-17 | 2024-02-02 | 丹东明珠特种树脂有限公司 | Method for preparing raw material by preparing high-content butene-1 from carbon four by co-production method and system device thereof |
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