CN105837407A - Preparation method of isobutyl vinyl ether - Google Patents
Preparation method of isobutyl vinyl ether Download PDFInfo
- Publication number
- CN105837407A CN105837407A CN201610268671.5A CN201610268671A CN105837407A CN 105837407 A CN105837407 A CN 105837407A CN 201610268671 A CN201610268671 A CN 201610268671A CN 105837407 A CN105837407 A CN 105837407A
- Authority
- CN
- China
- Prior art keywords
- gas
- ive
- preparation
- riser
- liquid separator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
- C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
- C07C41/08—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only to carbon-to-carbon triple bonds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a preparation method of isobutyl vinyl ether and relates to isobutyl vinyl ether. An isobutyl alcohol solution containing a catalyst is pumped into a circulation flow reactor from the bottom of a lifting pipe through a metering pump, and mixed gas of acetylene and nitrogen gas enters a gas ejector from the bottom of the lifting pipe after passing through a gas buffer tank, a compressor and absorption and drying columns; materials are driven to flow into a downcomer from the upper portion of the lifting pipe and recycled and flow back to the lifting pipe after heat exchange conducted by a heat exchanger and conduction oil, sprayed-out micro bubbles are mixed with and contact with an isobutanol solution, a reaction is conducted, and a reaction mixture is obtained, the reaction mixture flows out of an outlet in the top of the lifting pipe and enters a gas-liquid separator for gas-liquid separation after being cooled by a cooler, the gas phase flows out of the top of the gas-liquid separator and is recycled to the gas buffer tank after being subjected to decompression with a decompressor, and liquid flowing out of the gas-liquid separator is the isobutyl vinyl ether. Mass transfer is good in heat transfer effect, a device is simple in structure, safe, efficient, easy to operate, low in cost and prone to industrialization.
Description
Technical field
The present invention relates to IVE, especially relate to the preparation method of a kind of IVE.
Background technology
IVE is a kind of unsaturated ethers compound, has preferable reactivity, and its derivant is widely used in being coated with
The fields such as material, ink, binding agent, plasticizer.IVE is important organic synthesis intermediate, for medicine,
The preparation of the materials such as pesticide；Also it is important polymerization monomer, can with many unsaturated compounds (such as: vinyl chloride, maleic anhydride
Deng) copolymerization, prepare specific function material.
The conventional preparation method of IVE is in the presence of alkali metal hydroxide or alkali metal alcoholates, by acetylene and different
Butanol reacts generation IVE under uniform temperature and pressure.The reaction unit used has pressure autoclave type stirring reaction
Device (sees Chinese patent CN 200810062915.X；" Zhejiang chemical industry ", 2006,12:1-4.), tubular reactor is (in seeing
State's patent CN 201210570442.0), spray column (see Chinese patent CN 02138285.9；CN 200510040652.9).
Pressure autoclave type stirred reactor can only carry out intermittently operated, and the reaction participated in for pressurization acetylene is difficult to amplify, and is unfavorable for work
Industry metaplasia is produced.Tubular reactor heat-transfer effect is good, it is easy to industry is amplified, and safety is high, but this technique is at ambient pressure by acetylene
It is previously dissolved in the mixed liquor of raw alcohol and catalyst, then carries out full liquid phase circulation reaction under high pressure, due to acetylene content in liquid phase
Relatively low, therefore the single transformation rate of raw alcohol is relatively low, need to take the highest recycle ratio.Spray column gas-liquid mass transfer efficiency is low, catalyst
Consumption is big, and the heat-transfer effect of reactor is poor, and has the exhaust emissions containing acetylene.
Summary of the invention
Mass-and heat-transfer is effective, apparatus structure is simple, safe and efficient, simple to operate, cost to it is an object of the invention to provide one
Low and be prone to the preparation method of industrialized IVE.
The present invention specifically comprises the following steps that
1) isobutanol solution containing catalyst is squeezed into the mixed of circulation flow reactor, acetylene and nitrogen through dosing pump from the bottom of riser
Close gas after gas buffer tank, compressor and adsorption dry post, enter gas ejector from the bottom of riser.Gas injection is made
Become the pressure differential of riser top and bottom, drive material to flow into downspout from the top of riser, enter with conduction oil through heat exchanger
Row heat exchange Posterior circle flows back to riser, and the micro-bubble of ejection mixes with isobutanol solution and contacts to carry out reacting obtaining to react and mixes
Thing；
2) reactant mixture outlet from riser top is flowed out, and enters gas-liquid separator and carry out gas-liquid separation after the cooling of cooled device,
Wherein gas phase flows out from gas-liquid separator top, through decompressor decompression Posterior circle return-air body surge tank, flows out bottom gas-liquid separator
Liquid be IVE.
In step 1) in, the riser of described circulation flow reactor and the internal diameter ratio of downspout can be (1.5～3): 1；Described second
In alkynes and nitrogen mixed gas, the volume fraction of acetylene can be 40%～80%；Described gas ejector can use single head jet rose gas
Body ejector or bull jet rose gas ejector, the aperture of described nozzle can be 1～50 μm；Described catalyst can use different
Butanol potassium etc., the consumption of catalyst can be the 1%～8% of isobutanol quality by mass percentage；The temperature of described reaction can be 130～
170 DEG C, the pressure of reaction can be 0.3～1.0MPa.
The thick product of IVE and isobutanol, through extracting rectifying, makes the IVE of purity more than 99.5%
Product, unreacted isobutanol then recycles.The conversion per pass of acetylene can reach more than 85%, and the selectivity of reaction is 95%
Above.
The present invention uses external loop airlift reactor to prepare IVE to carry out the reaction of acetylene and isobutanol.Institute
State external loop airlift reactor and include gas ejector, riser, downspout and heat exchanger.External loop airlift reactor and
Dosing pump, cooler, gas-liquid separator, decompressor, gas buffer tank, compressor, adsorption dehumifier composition iso-butyl vinyl
The preparation facilities of base ether.
Compared with the preparation method of existing IVE, present invention have the advantage that
1) structure of reactor is simple, without running gear, it is to avoid the hidden danger of flammable explosive gas leakage.
2) gas jet drive liquid circulation, improves the gas holdup in liquid phase and gas-liquid mass transfer rate, makes reaction with speed faster
Rate is carried out, thus catalyst amount can be made to greatly reduce.
3) liquid circulation removes rapidly exothermic heat of reaction by the heat exchanger on downspout, and this heat exchanger can provide enough as required
Heat exchange area and do not limited by reactor volume.
4) emission-free discharge in course of reaction.
5) technological process is simple, with low cost, it is easy to accomplish industrialization.
Accompanying drawing explanation
Fig. 1 is the preparation facilities structural representation of the embodiment of the present invention.
Figure is respectively labeled as: 1-riser；2-gas ejector；3-downspout；4-heat exchanger；5-dosing pump；6-absorption is dry
Dry post；7-cooler；8-gas-liquid separator；9-decompressor；10-compressor；11-gas buffer tank.
Detailed description of the invention
Specific examples below combines accompanying drawing, and the present invention will be further described.
Embodiment 1:
The reaction of acetylene and isobutanol uses the reaction unit shown in Fig. 1.The riser internal diameter 0.15m of circulation flow reactor, high 2.5m.
Gas ejector is single head jet rose, and aperture is 3 μm.Process condition is as follows:
Catalyst amount: for the 2% of isobutanol quality；
Isobutanol (containing catalyst) feed rate 16L/h；
Mixed gas feed rate 15Nm3/h；
In mixture of feed body, the volume fraction of acetylene is 60%；
Heat exchange temperature: 150 DEG C；
Reaction pressure: 0.5MPa；
The conversion per pass of result isobutanol is 88%, and reacting the selectivity to IVE is 95.5%.
Embodiment 2:
The reaction of acetylene and isobutanol uses the reaction unit shown in accompanying drawing 1.The riser internal diameter 0.15m of circulation flow reactor, height
2.5m.Gas ejector is single head jet rose, and aperture is 10 μm.Process condition is as follows:
Catalyst amount: for the 3% of isobutanol quality；
Isobutanol (containing catalyst) feed rate 16L/h；
Mixed gas feed rate 15Nm3/h；
In mixture of feed body, the volume fraction of acetylene is 70%；
Heat exchange temperature: 140 DEG C；
Reaction pressure: 0.6MPa；
The conversion per pass of result isobutanol is 85.7%, and reacting the selectivity to IVE is 97%.
Embodiment 3:
The reaction of acetylene and isobutanol uses the reaction unit shown in accompanying drawing 1.The riser internal diameter 0.15m of circulation flow reactor, height
2.5m.Gas ejector is double-end porous nozzle, and aperture is 5 μm.Process condition is as follows:
Catalyst amount: for the 5% of isobutanol quality；
Isobutanol (containing catalyst) feed rate 16L/h；
Mixed gas feed rate 15Nm3/h；
In mixture of feed body, the volume fraction of acetylene is 65%；
Heat exchange temperature: 160 DEG C；
Reaction pressure: 0.8MPa；
The conversion per pass of result isobutanol is 92%, and reacting the selectivity to IVE is 95%.
The present invention provides that a kind of mass-and heat-transfer is effective, apparatus structure is simple, safe and efficient, simple to operate, low cost and being prone to
The preparation method of industrialized IVE.Described method uses external loop airlift reactor to carry out acetylene and isobutyl
The reaction of alcohol and prepare IVE.External loop airlift reactor include gas ejector, riser, downspout and
Heat exchanger.External loop airlift reactor and dosing pump, cooler, gas-liquid separator, decompressor, gas buffer tank, compression
The preparation facilities of machine, adsorption dehumifier composition IVE.Isobutanol solution containing catalyst through dosing pump from riser
Bottom squeeze into reactor, acetylene and nitrogen mixed gas (volume fraction of acetylene is 40～80%) compression, after drying from
The bottom of riser enters gas ejector.React pressure 0.3～1.0MPa and temperature 130～170 DEG C.Reaction is mixed
The compound outlet from riser top is flowed out, and enters gas-liquid separator and carry out gas-liquid separation after the cooling of cooled device, wherein gas phase from
Gas-liquid separator top out, through decompressor reduce pressure Posterior circle return-air body surge tank.Bottom gas-liquid separator, liquid out is
Thick product containing IVE.
Claims (8)
1. the preparation method of IVE, it is characterised in that specifically comprise the following steps that
1) isobutanol solution containing catalyst is squeezed into the mixed of circulation flow reactor, acetylene and nitrogen through dosing pump from the bottom of riser
Close gas after gas buffer tank, compressor and adsorption dry post, enter gas ejector from the bottom of riser；Gas injection is made
Become the pressure differential of riser top and bottom, drive material to flow into downspout from the top of riser, enter with conduction oil through heat exchanger
Row heat exchange Posterior circle flows back to riser, and the micro-bubble of ejection mixes with isobutanol solution and contacts to carry out reacting obtaining to react and mixes
Thing；
2) reactant mixture outlet from riser top is flowed out, and enters gas-liquid separator and carry out gas-liquid separation after the cooling of cooled device,
Wherein gas phase flows out from gas-liquid separator top, through decompressor decompression Posterior circle return-air body surge tank, flows out bottom gas-liquid separator
Liquid be IVE.
2. the preparation method of IVE as claimed in claim 1, it is characterised in that in step 1) in, described circulation
The riser of reactor and the internal diameter of downspout are than being (1.5～3): 1.
3. the preparation method of IVE as claimed in claim 1, it is characterised in that in step 1) in, described acetylene
It is 40%～80% with the volume fraction of acetylene in nitrogen mixed gas.
4. the preparation method of IVE as claimed in claim 1, it is characterised in that in step 1) in, described gas
Ejector uses single head jet rose gas ejector or bull jet rose gas ejector.
5. the preparation method of IVE as claimed in claim 4, it is characterised in that in step 1) in, described nozzle
Aperture be 1～50 μm.
6. the preparation method of IVE as claimed in claim 1, it is characterised in that in step 1) in, described catalysis
Agent uses isobutyl potassium alcoholate.
7. the preparation method of IVE as claimed in claim 1, it is characterised in that in step 1) in, described catalysis
The consumption of agent is the 1%～8% of isobutanol quality by mass percentage.
8. the preparation method of IVE as claimed in claim 1, it is characterised in that in step 1) in, described reaction
Temperature be 130～170 DEG C, the pressure of reaction is 0.3～1.0MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610268671.5A CN105837407A (en) | 2016-04-27 | 2016-04-27 | Preparation method of isobutyl vinyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610268671.5A CN105837407A (en) | 2016-04-27 | 2016-04-27 | Preparation method of isobutyl vinyl ether |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105837407A true CN105837407A (en) | 2016-08-10 |
Family
ID=56589144
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610268671.5A Pending CN105837407A (en) | 2016-04-27 | 2016-04-27 | Preparation method of isobutyl vinyl ether |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105837407A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113173837A (en) * | 2021-04-24 | 2021-07-27 | 浙江锦华新材料股份有限公司 | Preparation method of vinyl isobutyl ether |
| CN113200828A (en) * | 2021-05-04 | 2021-08-03 | 浙江锦华新材料股份有限公司 | Refining method of vinyl isobutyl ether |
| WO2022168949A1 (en) * | 2021-02-04 | 2022-08-11 | 丸善石油化学株式会社 | Method for producing isobutyl vinyl ether and method for purifying isobutyl vinyl ether |
| CN115490575A (en) * | 2022-10-13 | 2022-12-20 | 辽宁惠风生物医药科技有限公司 | Preparation method of 2-ethoxypropylene |
| CN115650825A (en) * | 2022-11-11 | 2023-01-31 | 厦门大学 | Method for synthesizing dihydric alcohol monovinyl ether |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3281213A (en) * | 1963-02-18 | 1966-10-25 | Phillips Petroleum Co | Alkylation apparatus |
| CN2813623Y (en) * | 2005-04-08 | 2006-09-06 | 洪厚胜 | Multi-tube external circulating reactor |
| CN1994547A (en) * | 2006-12-30 | 2007-07-11 | 中国石油大学(北京) | Air lift type external loop reactor with two spray nozzles |
| CN102976904A (en) * | 2012-12-24 | 2013-03-20 | 厦门大学 | Preparation device of isobutyl vinyl ether and preparation method thereof |
-
2016
- 2016-04-27 CN CN201610268671.5A patent/CN105837407A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3281213A (en) * | 1963-02-18 | 1966-10-25 | Phillips Petroleum Co | Alkylation apparatus |
| CN2813623Y (en) * | 2005-04-08 | 2006-09-06 | 洪厚胜 | Multi-tube external circulating reactor |
| CN1994547A (en) * | 2006-12-30 | 2007-07-11 | 中国石油大学(北京) | Air lift type external loop reactor with two spray nozzles |
| CN102976904A (en) * | 2012-12-24 | 2013-03-20 | 厦门大学 | Preparation device of isobutyl vinyl ether and preparation method thereof |
Non-Patent Citations (4)
| Title |
|---|
| 姜信真等: "《气体反应理论与应用基础》", 30 March 1990 * |
| 张庆文等: "一种改进型外环流气升式反应器及其应用的初步研究", 《化工时刊》 * |
| 张洵立等: "气升式外环流生化反应器", 《医药工程设计》 * |
| 石东升等: "气升式外环流反应器研究进展", 《食品与机械》 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022168949A1 (en) * | 2021-02-04 | 2022-08-11 | 丸善石油化学株式会社 | Method for producing isobutyl vinyl ether and method for purifying isobutyl vinyl ether |
| CN113173837A (en) * | 2021-04-24 | 2021-07-27 | 浙江锦华新材料股份有限公司 | Preparation method of vinyl isobutyl ether |
| CN113173837B (en) * | 2021-04-24 | 2022-05-06 | 浙江锦华新材料股份有限公司 | Preparation method of vinyl isobutyl ether |
| CN113200828A (en) * | 2021-05-04 | 2021-08-03 | 浙江锦华新材料股份有限公司 | Refining method of vinyl isobutyl ether |
| CN115490575A (en) * | 2022-10-13 | 2022-12-20 | 辽宁惠风生物医药科技有限公司 | Preparation method of 2-ethoxypropylene |
| CN115650825A (en) * | 2022-11-11 | 2023-01-31 | 厦门大学 | Method for synthesizing dihydric alcohol monovinyl ether |
| CN115650825B (en) * | 2022-11-11 | 2024-06-04 | 厦门大学 | Synthesis method of dihydric alcohol monovinyl ether |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105837407A (en) | Preparation method of isobutyl vinyl ether | |
| TWI417136B (en) | Parallelized jet loop reactors | |
| CN203291868U (en) | Jet reaction device | |
| CN103030622B (en) | Method for preparing glyceride carbonate by using loop reaction device | |
| CN101391974B (en) | Process for production of N-vinyl pyrrolidone | |
| CN102976904B (en) | Preparation device of isobutyl vinyl ether and preparation method thereof | |
| CN105237409A (en) | Method used for reductive amination using jet reactor | |
| CN107151194B (en) | Process and device for rapid sulfonation neutralization reaction | |
| CN115650825B (en) | Synthesis method of dihydric alcohol monovinyl ether | |
| CN113372192B (en) | Synthetic method of low-carbon sodium alkoxide | |
| CN109608340A (en) | The preparation method of N, N- dimethyl cyclohexyl amine | |
| CN111151205A (en) | Propionaldehyde continuous production method and reaction system | |
| CN213222199U (en) | Reaction device of vinyl ether compound | |
| CN110201611A (en) | A kind of three-phase flow reaction unit and its operating method for olefin hydroformylation | |
| CN106883198A (en) | A kind of method that utilization micro-reaction device prepares expoxy propane | |
| CN111825553A (en) | Preparation method of methyl acetoacetate | |
| CN105439823B (en) | A kind of method for synthesizing the alcohol of 3 methyl, 3 butylene 1 | |
| CN113563213B (en) | Preparation method of 3, 5-diaminobenzoic acid | |
| CN112430188B (en) | Novel method for preparing isopropyl aniline by hydrogenation technology | |
| CN211677677U (en) | Continuous reaction system for propionaldehyde production | |
| CN112457163B (en) | Micro-channel mixed catalytic hydrogenation device and method for preparing isophorol | |
| CN209759344U (en) | Acrylic ester product production device | |
| CN111892479B (en) | Method and device for improving primary conversion rate of methanol in chloromethane synthesis | |
| CN113549209A (en) | Method for continuously producing AEO (aerated Acoustic Acrylonitrile) and AES (atomic emission Spectrometry) by using microchannel reactor and microchannel system | |
| CN112569871A (en) | For CO2Gas-liquid uniform distribution tube type reactor for carbonylation reaction |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160810 |