CN109647289A - A kind of iris type vinyl ethers product reactor - Google Patents
A kind of iris type vinyl ethers product reactor Download PDFInfo
- Publication number
- CN109647289A CN109647289A CN201910039703.8A CN201910039703A CN109647289A CN 109647289 A CN109647289 A CN 109647289A CN 201910039703 A CN201910039703 A CN 201910039703A CN 109647289 A CN109647289 A CN 109647289A
- Authority
- CN
- China
- Prior art keywords
- region
- reactor
- venturi
- vinyl ethers
- acetylene
- 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
- QYKIQEUNHZKYBP-UHFFFAOYSA-N Vinyl ether Chemical class C=COC=C QYKIQEUNHZKYBP-UHFFFAOYSA-N 0.000 title claims abstract description 22
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 67
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 37
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 37
- 239000007791 liquid phase Substances 0.000 claims abstract description 23
- 230000007423 decrease Effects 0.000 claims abstract description 22
- 239000007921 spray Substances 0.000 claims abstract description 12
- 230000011218 segmentation Effects 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 15
- 238000005192 partition Methods 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 9
- 239000007788 liquid Substances 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 7
- 239000007792 gaseous phase Substances 0.000 claims description 4
- 239000006260 foam Substances 0.000 claims description 3
- 238000009434 installation Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 15
- 238000010924 continuous production Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 9
- 229960000834 vinyl ether Drugs 0.000 description 6
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- ZNQVEEAIQZEUHB-UHFFFAOYSA-N 2-ethoxyethanol Chemical compound CCOCCO ZNQVEEAIQZEUHB-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- -1 Vinyl ether compound Chemical class 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000012084 conversion product Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 239000012776 electronic material Substances 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 238000006266 etherification reaction Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/001—Controlling catalytic processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of iris type vinyl ethers product reactors, which is characterized in that reactor is divided into the acetylene distributor chamber of lower part and two, the liquid phase reactor region separate chamber on top by venturi distribution grid, is equipped with acetylene rough segmentation orchestration in acetylene distributor chamber；Liquid phase reactor region on venturi distribution grid is provided with muti-piece vertical baffle, and liquid phase reactor region is separated into multiple elevated areas and decline region, forms local circulation；Venturi spray head only is installed in the elevated areas that separator lined goes out, each decline region lower part is equipped with virgin ethylene glycol distributor.This Novel air Liquid-phase reactor greatly improves gas-liquid phase reaction one after another, improves the conversion ratio of reaction.Reactor continuous and steady operation, yield is big, product ability can be increased to 10,000 tons from annual hundred tonnes, has breakthrough meaning for the large-scale industry biochemistry continuous production of vinyl ethers product.
Description
Technical field
The present invention relates to vinyl ethers product reactor, which can be used for alcohols (such as ethylene glycol, 1,4-butanediol
Deng) and acetylene generation etherification reaction, generate vinyl ethers product, especially glycol divinyl ether.
Background technique
Vinyl ether compound has a extensive future in fields such as printing, ink, electronic materials, in recent years, living in coating
Effect in terms of property diluent is concerned, and is quickly grown.By taking glycol divinyl ether as an example, ethylene glycol and acetylene are urged in alkalinity
Under conditions of agent, reaction generates glycol divinyl ether, is gas-liquid phase reaction, strengthens gas-liquid and is in contact and shortens product in liquid
Residence time in phase is the core of reactor design.But such reaction has low selectivity, low-conversion and byproduct more
The characteristics of, it does not adapt to be actually needed.
Summary of the invention
The object of the present invention is to provide a kind of iris type vinyl ethers product reactor, should be recycled by acetylene quickly from
Product is taken out of in reaction system, improves conversion ratio.With efficient, continuous, stable, big processing capacity.Especially adapt to ethylene
Ethyl glycol ether product.
The technical scheme is that a kind of iris type vinyl ethers product reactor, including reactor shell, reaction
Gaseous phase outlet is equipped at the top of device, top is equipped with high-efficiency foam remover, and bottom is equipped with dead catalyst discharge outlet, continuously discharges dead catalyst
Liquid, which is characterized in that reactor is divided into the acetylene distributor chamber of lower part and the liquid phase reactor region on top by venturi distribution grid
Two separate chambers, acetylene distributor chamber is interior to be equipped with acetylene rough segmentation orchestration；Liquid phase reactor region on venturi distribution grid is provided with
Liquid phase reactor region is separated into multiple elevated areas and decline region, forms local circulation by muti-piece vertical baffle；Only in partition
The elevated areas installation venturi spray head marked off, each decline region lower part is equipped with virgin ethylene glycol distributor.
Preferably, reactor straight tube pars infrasegmentalis is equipped with uniformly distributed acetylene gas import, corresponds to one in each acetylene distribution cavity
Independent acetylene gas import.
Preferably, venturi spray head is higher than partition bottom level, therefore only can suck ethylene glycol from decline region, and formation follows
Ring.
Preferably, venturi height about 200~400mm, vertical baffle distance from bottom venturi 100~500mm of distribution grid,
Go deep into inside area of diaphragm at the top of venturi.
Preferably, elevated areas is ten, and decline region is nine, forms multiple liquid phase circulation regions.
Preferably, every layer of vertical baffle two sides hang with steam pipe coil or plate heat exchanger, steam pipe coil can be used light pipe or
Finned tube.
Preferably, virgin ethylene glycol distributor is installed apart from venturi distribution grid 500mm eminence in each decline region,
Virgin ethylene glycol is uniformly sprayed into decline region.
Preferably, virgin ethylene glycol distributor is equipped with multiple flutings directed downwardly.
Preferably, the corresponding housing exterior walls in liquid phase reactor region are equipped with steam jacket, collet height and liquid phase region height phase
Together.
The invention the liquid phase haptoreaction condition of efficient, continuous, stable, big processing capacity, gas phase are once led to
Reactor is left after crossing reaction zone, takes away reaction product, substantially increases conversion ratio.
Detailed description of the invention
Fig. 1 is structure of reactor schematic diagram of the invention.
Fig. 2 is venturi and partition distribution map of the invention.
Specific embodiment
Below in conjunction with attached drawing, the present invention will be further described.
As shown in Figure 1, reactor of the present invention includes shell of tank 1, acetylene gas import 2, acetylene rough segmentation orchestration 3, venturi
Distribution grid 4, venturi spray head 5, partition 6, steam pipe coil or plate heat exchanger 7, virgin ethylene glycol distributor 8, dead catalyst row
Put mouth 9, high-efficiency foam remover 10, gaseous phase outlet 11, discharge outlet 12, elevated areas 13, decline region 14, acetylene distributor chamber 15, steaming
Vapour collet 16.
As shown in Fig. 2, shell of reactor 1 is vertical pressure vessel, venturi distribution grid 4 will be divided into acetylene inside the container
Two separate chambers of distributor chamber 15 and reaction chamber.Venturi distribution grid 4 is tube-sheet type, screw thread mouth is above provided with, with venturi screw thread
Connection, facilitates installation.
Six 60 ° uniformly distributed acetylene gas imports 2 are equipped in reactor straight tube pars infrasegmentalis, on the one hand in order to reduce acetylene import
On the other hand acetylene can be uniformly distributed by size, acetylene gas import volume can be adjusted according to air inflow.
Acetylene, which enters after lower part acetylene distributor chamber 15, to be first allocated by acetylene rough segmentation orchestration 3, makes to enter each venturi
Acetylene amount it is uniform as far as possible.
Venturi height about 200~400mm, vertical baffle distance from bottom venturi 4100~500mm of distribution grid, venturi
Top is goed deep into inside area of diaphragm.
Venturi quantity is a from several to up to ten thousand, can arbitrarily be adjusted according to designed capacity, quantity is only big by venturi spray head
The limitation of small and reactor size.
Venturi distribution grid 4 is only provided with about 4000 threaded holes in the elevated areas 13 that partition 6 marks off, for installing
Venturi spray head is not installed in venturi spray head 5, decline region 14.Apart from venturi distribution grid 4500mm high in each decline region
Place is equipped with virgin ethylene glycol distributor 8, and virgin ethylene glycol is uniformly sprayed into descending area.
The elevated areas 13 is ten, and decline region 14 is nine, forms multiple race ways.Practical 6 quantity of partition
It can be adjusted according to shell dimension and venturi quantity, being formed by elevated areas 13 and decline the quantity in region 14 also therewith can be with
Adjustment.
Every layer of 6 two sides of vertical baffle hang with steam pipe coil or plate heat exchanger 7, and light pipe or fin can be used in steam pipe coil
Pipe, to react and evaporation provides heat.
Partition 6 and coil pipe are divided into two from centre, can enter from reactor head gaseous phase outlet 11 and install.
Technical process is as follows:
Gas phase acetylene enters the acetylene distributor chamber 13 of lower part of the housing by six acetylene gas imports 2 that bottom symmetrical is distributed,
It is sprayed at a high speed after being mixed by the venturi spray head 5 being mounted on venturi distribution grid 4 with liquid phase after acetylene rough segmentation orchestration 3
Out, the conversion zone reacted in 4 or more venturi distribution grid carries out.Acetylene gas is produced by venturi central region when normal operating
Raw suction will mix high speed ejection in the ethylene glycol sucking acetylene gas of surrounding.Since venturi spray head 5 is higher than 6 bottom of partition height
Degree, therefore only ethylene glycol can be sucked from decline region, form circulation.
Gas phase leaves reactor after once passing through liquid phase region, while taking away reactor product, after liquid phase crosses vertical baffle 6
Into decline region 14.Virgin ethylene glycol enters decline 14 bottom of region by distributor 8.
Reactor top is equipped with high efficient gas and liquid separator 10.
Reactor bottom is equipped with dead catalyst discharge outlet 12, continuously to discharge spent catalyst liquid.
In liquid phase reactor regional scope, the outside of reactor is equipped with steam jacket 16, it is further provided heat, and use
Liquidus temperature controls to adjust steam inlet.
It is chain that Liquid level, low liquid level are provided on reactor, it is ensured that acetylene gas will not seal in liquid phase downstream.
Produce glycol divinyl ether using reactor of the present invention, conversion ratio be one times of common bubbling style reactor with
On, can continuous and steady operation, glycol divinyl ether production capacity is increased to 10,000 tons from hundred tonnes, have very important application
Value.
Above embodiments are only that preferred embodiments of the present invention will be described, are not limited the scope of the present invention
Fixed, without departing from the spirit of the design of the present invention, those of ordinary skill in the art make technical solution of the present invention
Various changes and improvements should all be fallen into the protection scope that claims of the present invention determines.
Claims (9)
1. a kind of iris type vinyl ethers product reactor, including reactor shell (1), reactor head is equipped with gaseous phase outlet
(11), top is equipped with high-efficiency foam remover (10), and bottom is equipped with dead catalyst discharge outlet (12), continuously discharges spent catalyst liquid,
It is characterized in that, reactor is divided into acetylene distributor chamber (15) and the liquid phase reactor area on top of lower part by venturi distribution grid (4)
Two, domain separate chamber, acetylene distributor chamber (15) is interior to be equipped with acetylene rough segmentation orchestration (3)；Liquid phase on venturi distribution grid (4) is anti-
It answers region to be provided with muti-piece vertical baffle (6), liquid phase reactor region is separated into multiple elevated areas (13) and decline region
(14), local circulation is formed；Elevated areas (13) installation venturi spray head (5) only marked off in partition (6), each descending area
Domain (14) lower part is equipped with virgin ethylene glycol distributor (8).
2. iris type vinyl ethers product reactor according to claim 1, which is characterized in that under reactor direct tube section
Portion is equipped with uniformly distributed acetylene gas import (2), a corresponding independent acetylene gas import (2) on each acetylene distribution cavity (3).
3. iris type vinyl ethers product reactor according to claim 1, which is characterized in that venturi spray head (5)
Ethylene glycol can be sucked from decline region (14) higher than partition (6) bottom level, therefore only, form circulation.
4. iris type vinyl ethers product reactor according to claim 1, which is characterized in that venturi height is about
Baffle region is goed deep at 200~400mm, (4) 100~500mm of vertical baffle (6) distance from bottom venturi distribution grid, venturi top
Inside domain.
5. iris type vinyl ethers product reactor according to claim 1, which is characterized in that elevated areas (13) and
The specific number of decline region (14) can be adjusted according to plant capacity, and preferably elevated areas (13) is ten, decline region
It (14) is nine.
6. iris type vinyl ethers product reactor according to claim 1, which is characterized in that every layer of vertical baffle
(6) two sides hang with steam pipe coil or light pipe or finned tube can be used in plate heat exchanger (7), steam pipe coil.
7. iris type vinyl ethers product reactor according to claim 1, which is characterized in that each decline region
(14) it is equipped with virgin ethylene glycol distributor (8) in apart from venturi distribution grid (4) 500mm eminence, virgin ethylene glycol is uniform
It sprays into decline region (14).
8. iris type vinyl ethers product reactor according to claim 1, which is characterized in that virgin ethylene glycol distribution
Device (8) is equipped with multiple flutings directed downwardly.
9. iris type vinyl ethers product reactor according to claim 1, which is characterized in that liquid phase reactor region pair
The housing exterior walls answered are equipped with steam jacket (16), and collet height is identical as liquid phase region height.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910039703.8A CN109647289A (en) | 2019-01-16 | 2019-01-16 | A kind of iris type vinyl ethers product reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910039703.8A CN109647289A (en) | 2019-01-16 | 2019-01-16 | A kind of iris type vinyl ethers product reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109647289A true CN109647289A (en) | 2019-04-19 |
Family
ID=66120261
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910039703.8A Pending CN109647289A (en) | 2019-01-16 | 2019-01-16 | A kind of iris type vinyl ethers product reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109647289A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110052224A (en) * | 2019-06-10 | 2019-07-26 | 大连海事大学 | Gas distributor, fixed bubbling bed reactor |
| CN110433759A (en) * | 2019-09-03 | 2019-11-12 | 湖北襄化机械设备有限公司 | A kind of methoxy ethylene synthetic tower |
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Application publication date: 20190419 |