CN106076211A - A kind of bubble-liquid two-phase jet reactor and bubble-liquid two-phase jet response system - Google Patents
A kind of bubble-liquid two-phase jet reactor and bubble-liquid two-phase jet response system Download PDFInfo
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
- B01J10/002—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor carried out in foam, aerosol or bubbles
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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- C—CHEMISTRY; METALLURGY
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- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/54—Preparation of carboxylic acid anhydrides
- C07C51/56—Preparation of carboxylic acid anhydrides from organic acids, their salts, their esters or their halides, e.g. by carboxylation
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Abstract
本发明公开了一种气液两相射流反应器，包括反应器筒体，在反应器筒体顶部设有液体喷射装置，液体喷射装置包括进液口和伸入反应器筒体内的缩径式喷嘴；在反应器筒体上部设有排气口；在反应器筒体的内壁设有多个挡板；在反应器筒体下部设有进气口和循环液进口，进气口与位于缩径式喷嘴下方的气体分布器连通；在反应器筒体的底部设有排液口。本发明还公开了一种气液两相射流反应系统，包括前述气液两相射流反应器、蒸发器、闪蒸罐。本发明气液两相射流反应器系统，利用高速液体射流的剪切作用来破碎气泡，实现气液两相的高效分散混合，具有流程简洁、反应器结构简单、气液混合效果好等优点，适用于甲醇羰基化生成醋酸或醋酸甲酯羰基化生产醋酐工艺。
The invention discloses a gas-liquid two-phase jet reactor, which comprises a reactor cylinder, and a liquid injection device is arranged on the top of the reactor cylinder, and the liquid injection device includes a liquid inlet and a diameter-reducing nozzle extending into the reactor cylinder. Nozzle; an exhaust port is provided on the upper part of the reactor cylinder; multiple baffles are provided on the inner wall of the reactor cylinder; an air inlet and a circulating liquid inlet are arranged on the lower part of the reactor cylinder, and the air inlet The gas distributor below the radial nozzle is connected; a liquid outlet is provided at the bottom of the reactor cylinder. The invention also discloses a gas-liquid two-phase jet flow reaction system, which comprises the aforementioned gas-liquid two-phase jet flow reactor, an evaporator, and a flash tank. The gas-liquid two-phase jet reactor system of the present invention uses the shearing action of the high-speed liquid jet to break the bubbles, realizes the efficient dispersion and mixing of the gas-liquid two-phase, and has the advantages of simple process, simple reactor structure, and good gas-liquid mixing effect. It is suitable for the carbonylation of methanol to produce acetic acid or the carbonylation of methyl acetate to produce acetic anhydride.
Description
Technical field
The present invention relates to a kind of bubble-liquid two-phase jet reactor and include the gas-liquid two of this bubble-liquid two-phase jet reactor
Phase jet reaction system, this bubble-liquid two-phase jet reactor and system thereof are applicable to carbonylation and produce acetic acid, acetic anhydride technique.
Background technology
Acetic anhydride is a kind of important Organic Chemicals, mainly for the production of acetate fiber, photographic film, weaving acetic acid
Fiber, plastics, be also widely used in the industries such as medicine, food, pesticide, dyestuff.Wherein, produce acetic anhydride mainly have acetaldehyde oxidation,
Acetic acid cracking method, oxo synthesis etc..Though acetaldehyde oxidation flow process is simple, technical maturity, it is possible to achieve acetic acid and the connection of acetic anhydride
Producing, but seriously corroded and operating condition require higher, consume high, cost height, oneself is eliminated at present.Acetic acid cracking law technology becomes
Ripe, production security is high, but the technological process of production is complicated, and side reaction is many, and energy consumption is high, and investment is big, the dress built in early days abroad
Put this method of application.The dependence to petroleum of the methyl acetate preparing acetic anhydride by carbonylation process free, is C1 chemistry large industrialized
The important breakthrough of technological development, represents the advanced technology trend that current acetic anhydride produces, and has that flow process is short, product quality is good, disappears
The advantages such as consumption index is low, " three wastes " discharge is few.
Existing carbonylation synthesis acetic anhydride reactor generally uses churned mechanically mode to realize the most mixed of gas-liquid two-phase
Close.In industrial processes, the performance of reactor stirring mixing directly influences product quality, production cost and energy consumption etc.
Problem, but owing to there is gas phase dispersion, liquid-phase mixing and solid suspension in stirring mixed process, reaction system is rotten to dynamic equipment
The various problems such as erosion is serious.Therefore, developing a kind of novel non-stirred formula gas-liquid two-phase reactor is to compel during current acetic anhydride produces
The requirement cut.
Patent CN 201272754Y discloses a kind of reactor, wire mesh demister, heating coil and flash distillation baffle plate of including
Methyl acetate generates the reactor of acetic anhydride course of reaction with carbon monoxide liquid phase carbonyl.Reactor shell top is silk screen foam removal
Device, pattern is column type or ∧ font；Material feeding tube is connected with flash distillation baffle plate, buffers and improves gas-liquid two-phase and enter reaction
Mixing in device, the anti-swirl baffle structure of reactor lower part is cross or intersecting parallels structure.It is tight that this reactor has structure
Gather, gas-liquid mixed is uniform, heat exchange efficiency is high, the liquid-phase catalyst response rate relatively high.
Patent CN1562939A is by complete mixing flow conversion zone tank reactor and tower reactor anabolic reaction device.By regulation
Tower section of temperature of reactor, controls the temperature on tower section of reactant liquor inlet plate to adjust tower section of reactor outlet reactant liquor
Temperature, carbonylation reactor is connected with flash separator, simultaneously anti-with catalyst cooler, carbonylation respectively by catalyst pump
Device is answered to be connected.This invents the shortcoming overcoming simple piston flow reactor so that in emptying end gas, CO concentration reduces, and improves CO
Conversion ratio.
Patent CN 102008912A discloses a kind of air and liquid mixer, and this air and liquid mixer includes: an air inlet pipe, its end
End is provided with a perforated-pipe distributor；This perforated-pipe distributor is containing the pipe having multiple hole；Have the multiple of multiple hole and take turns radial canal,
It connects air inlet pipe and pipe.This air and liquid mixer can make gas-liquid be sufficiently mixed, thus reduce energy consumption, improve mixing effect
The purpose of rate.
Although above-mentioned patent enhances the mixed effect of gas-liquid two-phase to a certain extent, but it is multiple to still suffer from structure of reactor
Miscellaneous, use tradition rectification or stir the weak points such as unrealized optimal gas-liquid mixed effect.
Summary of the invention
For the problems referred to above in the presence of prior art, the invention provides one and send out with fluid injector and gas
The bubble-liquid two-phase jet reactor of raw bubbling parts and bubble-liquid two-phase jet response system.
It is an object of the invention to be achieved through the following technical solutions:
A kind of bubble-liquid two-phase jet reactor, including reactor shell 1, described reactor shell 1 is by upper and lower semicircle
End socket and middle part cylindrical tube composition；Liquid injection apparatus 3, described liquid spray it is provided with at described reactor shell 1 top
Injection device 3 includes inlet and the diameter reduced nozzle stretched in reactor shell 1；It is provided with air vent on reactor shell 1 top
2；Inwall at described reactor shell 1 is provided with multiple baffle plate 8, leaves a spacing between baffle plate 8 and reactor shell 1 inwall
From；Be provided with air inlet 5 and circulation fluid import 6 in the bottom of described reactor shell 1, described air inlet 5 be positioned at undergauge
Gas distributor 4 below formula nozzle connects；It is provided with leakage fluid dram 7 in the bottom of described reactor shell 1.
The ratio of height to diameter of described cylindrical tube is (2-5): 1.
The number of described air vent 2 is at least 1, preferably 1；The number of described circulation fluid import 6 is at least 1
Individual, preferably 1.
Described diameter reduced nozzle entrance flow area diameter and cylindrical tube diameter ratio are 0.05-0.2:1, are preferably
0.08-0.15:1；Described diameter reduced nozzle includes the different cylinder in two sections of cross sections and connects the truncated cone-shaped of two sections of cylinders even
The section of connecing；Before and after the undergauge of described diameter reduced nozzle, ratio is 1:(0.4-0.75), preferably 1:(0.55-0.65)；Before and after undergauge
Ratio is entrance flow area and the diameter ratio in outlet stream cross section of diameter reduced nozzle, and entrance, outlet stream cross section are circle
Shape.
The length of described diameter reduced nozzle is 1:(2-4.5 with the ratio of described cylindrical tube height), preferably 1:
(2.5-4)；After described diameter reduced nozzle undergauge, before length and undergauge, length ratio is 1:(6.1-11.2), preferably 1:
(7.5-9.5)。
Described gas distributor 4 is disc type gas distributor；In described gas distributor 4 with circle disk center is
Heart uniform pore openings, the perforate number of turns is 3-6 circle, and percent opening is 0.4%-2.8%.
Within the scope of the present invention, maintain ratio before and after undergauge constant, reduce entrance flow area diameter and can improve liquid and penetrate
Intensity of flow, the percent opening increasing gas distributor can increase gas dispersibility, and then can improve gas-liquid two-phase in reactor
Dispersion mixing.
The diameter of described gas distributor 4 and the diameter ratio of cylindrical tube are (0.2-0.7): 1, are preferably (0.25-
0.5): 1.
The number of described baffle plate 8 is 4-6.Baffle plate 8 is uniformly distributed along the inwall of reactor shell 1.
Described baffle plate 8 length is (0.7-1.0) with the ratio of cylindrical tube height: 1；Described baffle plate 8 width and cylinder
The ratio of barrel diameter is (0.1-0.2): 1；Described baffle plate 3 from span from (i.e. baffle plate 8 proximal response device cylinder 1 inwall side is with anti-
Answer the distance between device cylinder 1 inwall) with cylindrical tube diameter ratio for (0.05-0.1): 1, play back-mixing effect.
A kind of bubble-liquid two-phase jet response system, including aforementioned bubble-liquid two-phase jet reactor, vaporizer 11, flash tank
13；The liquid injection apparatus 3 of described bubble-liquid two-phase jet reactor is connected raw material input with liquid phase feed intake line 14
Bubble-liquid two-phase jet reactor, the air inlet 5 of described bubble-liquid two-phase jet reactor is connected with phase feed intake line 16
CO gas is sent into bubble-liquid two-phase jet reactor, and is flowed up by gas distributor 4；Described bubble-liquid two-phase jet is anti-
Answering device leakage fluid dram 7 to be connected with the entrance of vaporizer 11, vaporizer 11 top is provided with product output pipe 17, bottom vaporizer 11
Circulation fluid outlet is connected, at liquid circulating pipe with the circulation fluid import 6 of bubble-liquid two-phase jet reactor through liquid circulation line 15
Road 15 is provided with First Heat Exchanger 101；The air vent 2 on bubble-liquid two-phase jet reactor top is through the second heat exchanger 102 and flash distillation
The entrance of tank 13 connects, and gas outlet, flash tank 13 top is connected with gas exhaust piping 18, and bottom flash tank 13, liquid outlet is former with liquid phase
Material intake line 14 connects.
Preferably, phase feed intake line 16 is provided with compressor 12.
Preferably, the circulation fluid at described vaporizer 11 exports and is provided with the first outer circulation pump 91；At described flash tank
13 liquid outlets are provided with the second outer circulation pump 92.
Preferably, it is provided with gas circulation line 19 at described gas exhaust piping 18 and connects general with phase feed intake line 16
The gases such as part unreacted CO are transmitted back to bubble-liquid two-phase jet reactor.
Using bubble-liquid two-phase jet response system carbonylation of the present invention to produce acetic acid or acetic anhydride, reaction starts rank
Section, liquid phase feed is entered in bubble-liquid two-phase jet reactor by inlet, pass through after the liquid level required by reaction to be achieved into
QI KOU 5 starts to be passed through CO gas continuously, and is flowed up by gas distributor 4.After reaction starts, reactant liquor is from leakage fluid dram 7
Flow out, with after discharge through vaporizer 11 flash distillation, product flash-pot 11 top product output pipe 17, liquid flash-pot 11 end
The circulation fluid outlet in portion returns bubble-liquid two-phase jet reactor through liquid circulation line 15 and again participates in reaction；Reactor head gas
Body is discharged through air vent 2, and after flash tank 13 vacuum flashing, liquid merges, by gas-liquid two-phase with liquid phase feed stream stock through circulation
Liquid injection apparatus 3 high velocity spray at jet reactor top is injected in reactor, utilizes the shear action of liquid jet to crush
Bubble, it is achieved the high efficiency dispersion mixing of gas-liquid two-phase in reactor；Part unreacted CO gas is via gas circulation line 19
Being combined into reactor with phase feed stream stock, portion gas is delivered to torch via gas exhaust piping 18.
Beneficial effects of the present invention:
The bubble-liquid two-phase jet structure of reactor that the present invention proposes is simple, the bubble-liquid two-phase jet reactor assembly tool of composition
There is flow process succinct, the features such as gas-liquid mixed is effective, solve in existing bubbling type reactor and there is shaft and equipment
The problems such as the mechanical seal of housing junction is easily revealed, equipment corrosion serious, stirring slurry cost is high, gas-liquid mixed effect is undesirable,
Being particularly well-suited to methanol carbonyl metaplasia becomes acetic acid, methyl acetate carbonylation to produce acetic anhydride technique, on the one hand reduces the machinery of equipment
Maintenance cost, on the other hand when liquid circulation amount is bigger, efficiently avoid the vibration of stirring paddle in stirred autoclave, easily lets out
The problem of dew.
In production process: raw material liq, in nozzle at high speeds is injected into reactor, utilizes cutting of high-velocity liquid jet
The effect of cutting carrys out bubble crushing, it is achieved the high efficiency dispersion mixing of gas-liquid two-phase in reactor；Compared with bubbling type reactor,
Under equal conditions, using bubble-liquid two-phase jet reactor of the present invention, it is left that carbonylation conversion per pass at least can improve 9%
Right.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of bubble-liquid two-phase jet response system of the present invention.
Fig. 2 is the schematic diagram of diameter reduced nozzle.
Fig. 3 is the top view of the gas distributor of embodiment 1
In figure: 1-reactor shell, 2-air vent, 3-liquid injection apparatus, 4-gas distributor, 5-air inlet, 6-follow
Ring liquid import, 7-leakage fluid dram, 8-baffle plate, 91-the first outer circulation pump, 92-the second outer circulation pump, 101-First Heat Exchanger, 102-
Second heat exchanger, 11-vaporizer, 12-compressor, 13-flash tank, 14-liquid phase feed intake line, 15-liquid circulation line,
16-phase feed intake line, 17-product output pipe, 18-gas exhaust piping, 19-gas circulation line.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention is described in detail.It should be appreciated, however, that accompanying drawing is merely to preferably
Understand the present invention, be not to be construed as limitation of the present invention.
As shown in Figure 1-Figure 3, a kind of bubble-liquid two-phase jet response system, including bubble-liquid two-phase jet reactor, vaporizer
11, flash tank 13.
Described bubble-liquid two-phase jet reactor, including reactor shell 1, described reactor shell 1 is by upper and lower semicircle
Shape end socket and middle part cylindrical tube composition；It is provided with liquid injection apparatus 3, described liquid at described reactor shell 1 top
Injection apparatus 3 includes inlet and diameter reduced nozzle, and diameter reduced nozzle makes liquid jet angle in extending vertically into reactor shell 1
Vertical with horizontal direction；It is provided with air vent 2 on reactor shell 1 top；Inwall at described reactor shell 1 is provided with multiple
Baffle plate 8, leaves certain distance between baffle plate 8 and reactor shell 1 inwall；It is provided with air inlet in the bottom of described reactor shell 1
Mouth 5 and circulation fluid import 6, described air inlet 5 connects with the disc type gas distributor 4 being positioned at below diameter reduced nozzle,
Described gas distributor 4 uniform pore openings centered by circle disk center, the perforate number of turns is 3-6 circle；At described reactor shell 1
Bottom be provided with leakage fluid dram 7.
The liquid injection apparatus 3 of described bubble-liquid two-phase jet reactor is connected with liquid phase feed intake line 14, passes through
Diameter reduced nozzle by raw material high velocity jet reactor, the air inlet 5 of described bubble-liquid two-phase jet reactor and phase feed
Intake line 16 connects, and is compressed by compressor 12 and CO gas is sent into bubble-liquid two-phase jet reactor, and be distributed by gas
Device 4 flows up, and the shear action bubble in high-velocity liquid jet crushes；Described bubble-liquid two-phase jet reactor leakage fluid dram
7 are connected with the entrance of vaporizer 11, and vaporizer 11 top is provided with product output pipe 17, the circulation fluid outlet bottom vaporizer 11
It is connected with the circulation fluid import 6 of bubble-liquid two-phase jet reactor through liquid circulation line 15, on liquid circulation line 15 successively
It is provided with the first outer circulation pump 91, First Heat Exchanger 101；The air vent 2 on bubble-liquid two-phase jet reactor top is through the second heat exchanger
102 are connected with the entrance of flash tank 13, and gas outlet, flash tank 13 top is connected with gas exhaust piping 18, at described gas exhaust piping 18
It is provided with gas circulation line 19 to connect with phase feed intake line 16 and part unreacted CO gas is transmitted back to gas-liquid two-phase penetrates
Flow reactor；Bottom flash tank 13, liquid outlet connects with liquid phase feed intake line 14, sets at described flash tank 13 liquid outlet
There is the second outer circulation pump 92.
Embodiment 1
The ratio of height to diameter of described bubble-liquid two-phase jet reactor is 4:1；The length of diameter reduced nozzle and cylindrical tube height
Than being 1:2.5, after diameter reduced nozzle undergauge, before length and undergauge, length ratio is 1:8；Entrance, outlet stream cross section are circle
Shape, entrance flow area diameter and cylindrical tube diameter are than for 0.1:1, the diameter between entrance flow area and outlet stream cross section
Ratio be 1:0.6；The diameter of described gas distributor 4 and the diameter ratio of cylindrical tube are 0.29:1, and the perforate number of turns is 4 layers,
Often the ratio of circle number of aperture is 1:6:8:10, and aperture is 1:40 with the diameter ratio of gas distributor.Baffle plate number is 4, length
Being 1:1 with the ratio of cylindrical tube height, width and cylindrical tube diameter ratio are 0.15:1, from span from reactor shell 1
Diameter ratio is 0.075:1.
The present embodiment bubble-liquid two-phase jet response system carbonylation is used to produce acetic anhydride (C4H6O3) time, react the incipient stage,
Liquid phase feed is entered in bubble-liquid two-phase jet reactor by inlet, passes through air inlet after the liquid level required by reaction to be achieved
5 start to be passed through continuously CO gas, and are flowed up by gas distributor 4.After reaction starts, reactant liquor flows out from leakage fluid dram 7,
Through vaporizer 11 flash distillation after with, product flash-pot 11 top product output pipe 17 is discharged, bottom liquid flash-pot 11
Circulation fluid outlet returns bubble-liquid two-phase jet reactor through liquid circulation line 15 and again participates in reaction；Reactor head gas warp
Air vent 2 is discharged, and after flash tank 13 vacuum flashing, liquid merges, by bubble-liquid two-phase jet with liquid phase feed stream stock through circulation
Liquid injection apparatus 3 high velocity spray of reactor head is injected in reactor, utilizes the shear action of liquid jet to carry out bubble crushing,
Realize the high efficiency dispersion mixing of gas-liquid two-phase in reactor；Part unreacted CO gas is via gas circulation line 19 and gas phase
Raw material stream stock is combined into reactor, and portion gas is delivered to torch via gas exhaust piping 18.After stable reaction, be one continuously
Charging, the process of continuous discharge, the stream stock of each pipeline is shown in Table 1.
Above-mentioned reaction is carried out under the VIIIth transition metal is active center chelate catalyst system, carbonylation one way
Conversion ratio is 48%.
Conventional carbonylation reactor uses bubbling type reactor, and stirring paddle uses multilamellar axial flow, the combination of runoff to stir
Mix oar, when using bubbling type reactor carbonylation to produce acetic anhydride, liquid phase admixture by speed of agitator, superficial gas velocity and
, in practical application in industry, there is shaft easy with the mechanical seal of apparatus casing junction in the controlling factors such as liquid phase outer circulation flow
The problem revealed, and agitator cost is high, operation expense is high.Under reaction condition similarly to Example 1, bubbling type
Reactor carbonylation conversion per pass only up to reach about 44%.
Each pipeline stream stock when table 1 embodiment 1 bubble-liquid two-phase jet response system carbonylation produces acetic anhydride
Embodiment 2
The ratio of height to diameter of described bubble-liquid two-phase jet reactor is 4:1, the length of diameter reduced nozzle and cylindrical tube height
Than being 1:2.5, after diameter reduced nozzle undergauge, before length and undergauge, length ratio is 1:8；Entrance, outlet stream cross section are circle
Shape, entrance flow area diameter and cylindrical tube diameter than for 0.08:1, straight between entrance flow area and outlet stream cross section
The ratio in footpath is 1:0.6；Described gas distributor 4 diameter and described cylindrical tube diameter ratio are 0.29:1, and the perforate number of turns is 4
Layer, often the ratio of circle number of aperture is 1:8:8:10, and aperture and former dish diameter ratio are 1:35.Baffle plate number is 5, length and cylinder
The ratio of cylinder height is 1:1, and width and cylindrical tube diameter ratio are 0.15:1, from span from cylindrical tube diameter ratio are
0.075:1.
When using the present embodiment bubble-liquid two-phase jet response system carbonylation to produce acetic anhydride, reacting the incipient stage, liquid phase is former
Expect to enter in bubble-liquid two-phase jet reactor by inlet, started by air inlet 5 after the liquid level required by reaction to be achieved
It is passed through CO gas continuously, and is flowed up by gas distributor 4.After reaction starts, reactant liquor flows out from leakage fluid dram 7, subsequently
Through vaporizer 11 flash distillation, product flash-pot 11 top product output pipe 17 is discharged, the circulation bottom liquid flash-pot 11
Liquid outlet returns bubble-liquid two-phase jet reactor through liquid circulation line 15 and again participates in reaction；Reactor head gas is through aerofluxus
Mouth 2 is discharged, and after flash tank 13 vacuum flashing, liquid merges with liquid phase feed stream stock through circulation, bubble-liquid two-phase jet react
Liquid injection apparatus 3 high velocity spray at device top is injected in reactor, utilizes the shear action of liquid jet to carry out bubble crushing, it is achieved
The high efficiency dispersion mixing of gas-liquid two-phase in reactor；Part unreacted CO gas is via gas circulation line 19 and phase feed
Stream stock is combined into reactor, and portion gas is delivered to torch via gas exhaust piping 18.After stable reaction, it is one and enters continuously
Material, the process of continuous discharge, the stream stock of each pipeline is shown in Table 2.
Above-mentioned reaction is carried out under the VIIIth transition metal is active center chelate catalyst system, carbonylation one way
Conversion ratio is 50%, compared with Example 1, improves 4.2%.
Each pipeline stream stock when table 2 embodiment 2 bubble-liquid two-phase jet response system carbonylation produces acetic anhydride
Embodiment 3
The ratio of height to diameter of described bubble-liquid two-phase jet reactor is 4:1；The length of diameter reduced nozzle and cylindrical tube height
Than being 1:2.5, after diameter reduced nozzle undergauge, before length and undergauge, length ratio is 1:8；Entrance, outlet stream cross section are circle
Shape, entrance flow area diameter and cylindrical tube diameter than for 0.08:1, straight between entrance flow area and outlet stream cross section
The ratio in footpath is 1:0.55；Described gas distributor 4 diameter and described reactor shell diameter ratio are 0.29:1, the perforate number of turns
Being 4 layers, often the ratio of circle number of aperture is 1:8:10:10, and aperture and former dish diameter ratio are 1:35.Baffle plate number is 4, length with
The ratio of cylindrical tube height is 1:1, and width and reactor shell 1 diameter ratio are 0.15:1, from span from reactor shell 1
Diameter ratio is 0.075:1.
When using the present embodiment bubble-liquid two-phase jet response system carbonylation to produce acetic anhydride, reacting the incipient stage, liquid phase is former
Expect to enter in bubble-liquid two-phase jet reactor by inlet, started by air inlet 5 after the liquid level required by reaction to be achieved
It is passed through CO gas continuously, and is flowed up by gas distributor 4.After reaction starts, reactant liquor flows out from leakage fluid dram 7, subsequently
Through vaporizer 11 flash distillation, product flash-pot 11 top product output pipe 17 is discharged, the circulation bottom liquid flash-pot 11
Liquid outlet returns bubble-liquid two-phase jet reactor through liquid circulation line 15 and again participates in reaction；Reactor head gas is through aerofluxus
Mouth 2 is discharged, and after flash tank 13 vacuum flashing, liquid merges with liquid phase feed stream stock through circulation, bubble-liquid two-phase jet react
Liquid injection apparatus 3 high velocity spray at device top is injected in reactor, utilizes the shear action of liquid jet to carry out bubble crushing, it is achieved
The high efficiency dispersion mixing of gas-liquid two-phase in reactor；Part unreacted CO gas is via gas circulation line 19 and phase feed
Stream stock is combined into reactor, and portion gas is delivered to torch via gas exhaust piping 18.After stable reaction, it is one and enters continuously
Material, the process of continuous discharge, the stream stock of each pipeline is shown in Table 3.
Above-mentioned reactor is carried out under the VIIIth transition metal is active center chelate catalyst system, carbonylation list
Journey conversion ratio is 52%, compared with Example 1, improves 8.3%.
Each pipeline stream stock when table 3 embodiment 3 bubble-liquid two-phase jet response system carbonylation produces acetic anhydride
Embodiment described above is only to be described the preferred embodiment of the present invention, the not structure to the present invention
Thinking and scope is defined, without departing under design concept premise of the present invention, in this area, ordinary skill technical staff is to this
Various modification that bright technical scheme is made and improvement, all should fall into protection scope of the present invention, the skill that the present invention is claimed
Art content is the most all recorded in detail in the claims.
Claims (10)
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| CN110420609A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of micro/nano-scale multiphase flow process intensification reaction unit |
| CN110898698A (en) * | 2018-09-17 | 2020-03-24 | 浙江大学 | Microbubble generator and gas-liquid reactor comprising same |
| CN111646894A (en) * | 2019-09-10 | 2020-09-11 | 上海浦景化工技术股份有限公司 | Method for synthesizing acetic acid by low-pressure methanol carbonylation |
| CN114452903A (en) * | 2022-01-27 | 2022-05-10 | 中石化南京工程有限公司 | Oxo gas-liquid reactor |
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| CN110420609B (en) * | 2019-09-02 | 2024-02-20 | 杭州烃能科技研究有限公司 | Micro-nano scale multiphase flow process strengthening reaction device |
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| WO2022148162A1 (en) * | 2021-01-06 | 2022-07-14 | 上海华谊能源化工有限公司 | Reaction device, and system and method for synthesizing acetic acid from carbonyl |
| CN114452903A (en) * | 2022-01-27 | 2022-05-10 | 中石化南京工程有限公司 | Oxo gas-liquid reactor |
| CN115518604A (en) * | 2022-09-16 | 2022-12-27 | 成都中科普瑞净化设备有限公司 | A tubular reactor unit and system |
| CN115518604B (en) * | 2022-09-16 | 2025-08-15 | 成都中科普瑞净化设备有限公司 | Tubular reactor unit and system |
| CN117049953A (en) * | 2023-01-08 | 2023-11-14 | 南京诚志清洁能源有限公司 | Method for producing butyraldehyde by propylene carbonylation |
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