CN110420614A - A kind of multiphase flow process intensification reactor - Google Patents
A kind of multiphase flow process intensification reactor Download PDFInfo
- Publication number
- CN110420614A CN110420614A CN201910824430.8A CN201910824430A CN110420614A CN 110420614 A CN110420614 A CN 110420614A CN 201910824430 A CN201910824430 A CN 201910824430A CN 110420614 A CN110420614 A CN 110420614A
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- Prior art keywords
- tubulation
- sealing plate
- flow process
- charging aperture
- multiphase flow
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Links
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000007789 sealing Methods 0.000 claims abstract description 50
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- 239000000463 material Substances 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 239000007791 liquid phase Substances 0.000 claims abstract description 9
- 239000012071 phase Substances 0.000 claims description 13
- 239000007787 solid Substances 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 7
- 239000011949 solid catalyst Substances 0.000 claims description 5
- 238000012546 transfer Methods 0.000 abstract description 15
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 239000012530 fluid Substances 0.000 description 7
- 239000003345 natural gas Substances 0.000 description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- -1 alkane alkene Chemical class 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000002283 diesel fuel Substances 0.000 description 3
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 2
- 230000029936 alkylation Effects 0.000 description 2
- 238000005804 alkylation reaction Methods 0.000 description 2
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000001282 iso-butane Substances 0.000 description 2
- 235000013847 iso-butane Nutrition 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000005501 phase interface Effects 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 230000001052 transient effect Effects 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-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
- NHTMVDHEPJAVLT-UHFFFAOYSA-N Isooctane Chemical compound CC(C)CC(C)(C)C NHTMVDHEPJAVLT-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 description 1
- 150000004056 anthraquinones Chemical class 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000010538 cationic polymerization reaction Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- QTTRZHGPGKRAFB-OOKHYKNYSA-N rimexolone Chemical compound C1CC2=CC(=O)C=C[C@]2(C)[C@@H]2[C@@H]1[C@@H]1C[C@@H](C)[C@@](C(=O)CC)(C)[C@@]1(C)C[C@@H]2O QTTRZHGPGKRAFB-OOKHYKNYSA-N 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000002834 transmittance Methods 0.000 description 1
- FLTJDUOFAQWHDF-UHFFFAOYSA-N trimethyl pentane Natural products CCCCC(C)(C)C FLTJDUOFAQWHDF-UHFFFAOYSA-N 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
Abstract
A kind of multiphase flow process intensification reactor, first charging aperture is offered including lower end, side wall offers second charging aperture, upper end offers the shell of discharge port, it is sequentially installed with upper sealing plate and lower sealing plate from top to bottom in shell, on, shell is separated into the first material chamber being connected with first charging aperture by lower sealing plate, the intermediate cavity being connected with second charging aperture and the reaction chamber being connected with discharge port, and the tubulation that several tube walls offer micro-or nano size duct is installed in intermediate cavity, gap between each tubulation forms reactor cavity, lower sealing plate hole corresponding with tubulation is offered on the lower sealing plate, the upper sealing plate is to offer the aperture sealing plate in upper sealing plate corresponding with tubulation hole or to be provided with the tubulation head plate of tubulation end socket corresponding with tubulation.Since the present invention offers micro-or nano size duct on tubulation, strengthens the mass-transfer efficiency of gas-liquid reaction from microcosmic point, improve reactor liquid phase mass-transfer efficiency.
Description
Technical field
The invention belongs to field of chemical equipment, and in particular to a kind of multiphase flow process intensification reactor.
Background technique
Chemical, chemical field heterophase reactor structure directly determines the depth and rate of chemical reaction, for quick
Or for transient chemical reaction, the mass transfer rate between multi-phase reactants determines the overall rate of chemical reaction.Especially
For temperature controlled reaction, reaction heat is timely supplemented or takes away, for control reaction conversion ratio and target product
Selectivity has great importance.
For traditional quickly or for transient response, mass transfer rate is largely determined by the heterogeneous reaction that gas participates in
Double membrane mass transfers control of liquid-vapor interface, liquid-solid boundary.In traditional reactor, the mixture of vapor-liquid two phases or airwater mist cooling
In system, bubble diameter is generally millimeter or Centimeter Level, and the area so as to cause whole phase interface is smaller, mixes not between multiphase
Uniformly, mass-transfer efficiency is low, finally makes overall chemical reaction insufficient, the residence time of reactant is long in device, material consumption, energy
Consumption is high, and the treating capacity of unit volume reactor is low, and the processing cost of unit product is higher.To promote mass-and heat-transfer efficiency, tubulation
Formula reactor is more satisfactory consersion unit, it has been disclosed that patent CN201310359167, CN201810520389 passes through design
The technical solutions such as reactor component structure, tubulation arrangement mode and angle optimize traditional shell and tube reactor, but pass
Matter, heat transfer efficiency do not improve substantially.Publication CN201310359167 has delivered a kind of anti-by tubulation aperture raising
The reactor of mass-and heat-transfer is answered, but it is still insufficient with the technical solution efficiency that macroscopical open-celled structure is realized, there is very big mention
Between lift-off.
Summary of the invention
The object of the present invention is to provide one kind can strengthen gas-liquid-solid, gas-liquid reaction mass-transfer efficiency from microcosmic point,
And then solve the multiphase flow process intensification reactor of above-mentioned realistic problem.
In order to achieve the above objectives, the technical solution adopted by the present invention is that: offer first charging aperture including lower end, side wall is opened
The shell that discharge port is offered equipped with second charging aperture, upper end is sequentially installed with upper sealing plate and lower envelope from top to bottom in shell
Shell is separated into the first material chamber being connected with first charging aperture, the centre being connected with second charging aperture by plate, upper and lower sealing plate
Chamber and the reaction chamber being connected with discharge port, and the column that several tube walls offer micro-or nano size duct are installed in intermediate cavity
It manages, the gap between each tubulation forms reactor cavity, and lower sealing plate corresponding with tubulation is offered on the lower sealing plate
Hole, the upper sealing plate are to offer the aperture sealing plate in upper sealing plate corresponding with tubulation hole or corresponding with tubulation to be provided with
The tubulation head plate of tubulation end socket.
The material flow that the first charging aperture enters is gas phase, liquid phase or gas-liquid mixed phase without solid particle.
The material flow that the second charging aperture enters is gas phase, liquid phase or gas-liquid mixed phase without solid particle.
The aperture in the micro-or nano size duct of the tubulation tube wall is 10nm~300 μm
The aperture in the micro-or nano size duct of the tubulation tube wall is 10nm~100 μm.
The aperture in the micro-or nano size duct of the tubulation tube wall is 10nm~200nm.
The diameter in the upper sealing plate hole and lower sealing plate hole is less than or equal to the diameter of corresponding tubulation.
The tubulation end socket diameter is more than or equal to the diameter of corresponding tubulation.
Contain solid catalyst support plate in the tubulation, and also loads solid catalyst particle in tubulation.
Based on the present invention apply disclosed in a kind of multiphase flow process intensification reactor, with conventional solution-air, it is gas-liquid-solid instead
It answers device to compare, can produce following effective effect:
1) micro-or nano size duct is offered on tubulation due to the present invention, strengthens gas-liquid-solid, solution-air from microcosmic point
The mass-transfer efficiency of reaction improves reactor liquid phase mass-transfer efficiency；
2) nanoscale, micron order, the microlayer model of submicron order, microbubble can be formed in multiphase flow process intensification reactor,
The microcosmic mass transfer time can be foreshortened within the scope of the time scale of 0.01-0.001s, significantly improve the change controlled by diffusion mass transfer
It learns and reacts macroscopical rate；
3) phase interface existing for script is made by waterpower, mechanical force collaboration between reactant in multiphase flow process intensification reactor
If uniformly being mixed between each component in reaction system with dry reaction infinitesimal is cut into, hot localised points can be effectively suppressed, it is easier to realize anti-
Answer the reasonable layout of area's temperature gradient；
4) since microcosmic transmittance process is greatly optimized, the technical indicators such as raw material availability, product distribution, space-time yield
It is greatly improved and optimizes compared to conventional reactor.
Detailed description of the invention
Fig. 1 is overall structure diagram of the invention；
Fig. 2 is the structural schematic diagram of sealing plate 6 under the present invention；
Fig. 3 is the structural schematic diagram of upper sealing plate 5 of the present invention；
Fig. 4 is another structural schematic diagram of upper sealing plate 5 of the present invention.
In figure, 1, first charging aperture, 2, second charging aperture, 3, discharge port 3, shell 4,411, reactor cavity, 412, anti-
Answer chamber, 413, intermediate cavity, the 414, first material chamber, upper sealing plate 5,51, tubulation head plate, 511, the hole of tubulation head plate, 512,
Tubulation end socket, 52, aperture sealing plate, 521, upper sealing plate hole, 6, lower sealing plate, 611, lower sealing plate hole, 7, tubulation.
Specific embodiment
The present invention is described in further detail below in conjunction with the accompanying drawings.
Embodiment 1:
Referring to Fig. 1,2,3, the present invention include lower end offers first charging aperture 1, side wall offers second charging aperture 2, on
End offers the shell 4 of discharge port 3, is sequentially installed with upper sealing plate 5 and lower sealing plate 6, upper and lower sealing plate from top to bottom in shell 4
5,6 shell 4 is separated into the first material chamber 414 being connected with first charging aperture, the intermediate cavity 413 being connected with second charging aperture
The reaction chamber 412 being connected with discharge port, and being equipped with several tube walls to offer aperture in intermediate cavity 413 is 50~100nm
Micro-or nano size duct tubulation 7, solid catalyst support plate is contained in the tubulation 7, and also load solid in tubulation 7
Catalyst granules, the gap between each tubulation 7 form reactor cavity 411, offer on the lower sealing plate 6 and tubulation 7
Corresponding diameter is less than or equal to the lower sealing plate hole 611 of corresponding 7 diameter of tubulation, offers on the upper sealing plate 5 opposite with tubulation 7
The diameter answered is less than or equal to the aperture sealing plate 52 with upper sealing plate hole 521 of corresponding 7 diameter of tubulation.
The fluid material of second charging aperture 2 enters after reactor cavity 411 across the micro-or nano size hole of 7 tube wall of tubulation
Road is sprayed to fluid material tubulation 7 inside and entered in tubulation 7 through the lower sealing plate hole 611 of first charging aperture 1 and lower sealing plate 6
The raw reaction of hybrid concurrency, is then expelled in reaction chamber 412 from 7 other end of tubulation through the upper sealing plate hole 521 of aperture sealing plate 52, most
Reactor is discharged from discharge port 3 afterwards, wherein the material flow that the first and second feed inlet 1,2 enters be gas phase without solid particle,
Liquid phase or gas-liquid mixed phase.
According to the reactor design of embodiment 1, carry out distillate hydrogenation experiment.Wherein sulfur-containing diesel (S content 867ppm)
Fluid enters after reactor, enters and is filled in commercialization diesel oil hydrofining Clover-shaped catalyzer bed, and reacts
Device cavity enters through the hydrogen that tubulation tube wall nano pore enters in tubulation and diesel oil hydrofining reaction occurs, and then produces
Object and unreacted hydrogen are discharged by outlet together.The experimental results showed that reactor of the present invention is real in distillate hydrogenation technology
Showed efficient application, S content 9.5ppm in product natural gas has reached state VI finished diesel fuel sulfur content standard, while with biography
The fixed bed reactors of system are compared, and hydrogen-oil ratio (volume ratio) reduces 60~90%, realize quantitative hydrogen supply substantially, and can remove
The circulating hydrogen compressor in traditional fixed bed hydrogenation technical matters is sold, energy consumption is successively reduced.In addition, same reactor volume is anti-
It answers object air speed to significantly improve more than half, to be obviously improved the processing capacity of identical scale reaction device, integrally realizes energy conservation
Consumption reduction.
Embodiment 2:
Referring to Fig. 1,2,4, the upper sealing plate 5 of the present embodiment is provided with diameter corresponding with tubulation 7 more than or equal to respective column
The tubulation head plate 51 with tubulation end socket 512 of 7 diameter of pipe, wherein the aperture in the micro-or nano size duct on tubulation 7 is 100
~450nm.Other structures are the same as embodiment 1.
The present embodiment tubulation head plate 51 completely encloses one end of all tubulations 7, and keeps reactor cavity 411 and anti-
It answers and is connected to completely between chamber 412, form the hole 511 of tubulation head plate.1 fluid material of first charging aperture passes through lower sealing plate 6
Lower sealing plate hole 611 enters in tubulation 7, sprays then across the micro-or nano size duct of 7 tube wall of tubulation to reactor cavity 411
It is interior, it is reacted with the fluid material hybrid concurrency life that second charging aperture 2 enters in reactor cavity 411, then from the tubulation of tubulation 7
The hole 511 of head plate is expelled in reaction chamber 412, and reactor finally is discharged from discharge port 3.
According to the reactor design of embodiment 2, carry out hydramine method selexol process decarburization experiment.Wherein contain high hydrogen sulfide
With the natural gas (H of carbon dioxide2S content 6.4wt%, CO2Content 4.5wt%) tubulation is entered later from tubulation wall nano-pore
Road is sprayed into the alkanolamine solution (MDEA, 40wt%) between tubulation, and gas-liquid volume ratio (status of criterion) reaches 580v/v, and
Selexol process decarburizing reaction occurs in tubulation, hydramine rich solution and purified natural gas are discharged by outlet together, and are separated.It is real
Test the result shows that, reactor of the present invention realizes efficient application in natural gas wet desulphurization decarburization technique, in product natural gas
H2S content 5.1ppm, CO2Content 2.8wt% has reached H in a national class natural gas2S and CO2Content standard (GB 17820-
2018), while compared with traditional packed tower, board-like tower reactor, under same treatment amount, due to reactor liquid phase of the present invention
Mass-transfer efficiency is high, and 1/2 to 1/3 (difference due to content of sour gas in natural gas is different) is obviously reduced in reactor size.In addition,
It is able to achieve highly selective efficient depth and takes off H2S, the de- CO of appropriateness2Effect, to effectively reduce unit sour gas (H2S、CO2)
The consumption of hydramine liquid, to significantly reduce the energy consumption of hydramine rich solution regenerative system.
The aperture in the micro-or nano size duct on the tubulation 7 of embodiment 2 is used into 450nm~1 μm.It is anti-to carry out C4 alkylation
It should test.Wherein the catalyst concentrated sulfuric acid is sprayed from the micro-nano duct of tubulation wall to the iso-butane between tubulation after entering tubulation
In 2- butylene mixed raw material (alkane alkene ratio is 8) fluid, catalyzing iso-butane alkane and 2- butylene react, and generate a large amount of trimethyl
Pentane, subsequent product and unreacted fluid are mutually discharged by outlet together.The experimental results showed that reactor of the present invention is in C4 alkyl
Efficient application is realized in change technology, the octane number of product is up to 96~102, C8 selectively more than 50wt%, can be used as height
Quality gasoline blend component.In addition, the residence time of the catalyst concentrated sulfuric acid and alkane alkene mixture Two Liquid Phases in reactor is by passing
System C4 alkylation reactor is reduced within 1 minute for 30 minutes, so that the processing capacity of device is greatly improved, to effectively drop
The low energy consumption and material consumption of production unit alkylate oil.
It is anti-that multiphase flow reactor of the invention can be applied to gas-liquid-solid reaction, vapor-liquid two phases reaction and liquid-liquid
It answers.
The multiphase flow reactor can be applied to wet process selexol process decarburizing reaction, C4 alkylated reaction, anthraquinone life
Produce hydrogen peroxide reaction, n butane oxidation prepares cis-butenedioic anhydride reaction, the reaction of methylbenzene oxidation reaction, distillate hydrogenation, propenecarbonyl
Synthesize octyl alconyl reaction, cationic polymerization and ethylene polymerization.
Claims (9)
1. a kind of multiphase flow process intensification reactor, it is characterised in that:
First charging aperture (1) is offered including lower end, side wall offers second charging aperture (2), upper end offers discharge port (3)
Shell (4), is sequentially installed with upper sealing plate (5) and lower sealing plate (6) in the shell (4) from top to bottom, and upper and lower sealing plate (5,6) is by shell
Body (4) is separated into the first material chamber (414) being connected with first charging aperture, the intermediate cavity (413) being connected with second charging aperture
The reaction chamber (412) being connected with discharge port, and several tube walls are installed in intermediate cavity (413) and offer micro-or nano size hole
The tubulation (7) in road, the gap between each tubulation (7) form reactor cavity (411), offer on the lower sealing plate (6)
Lower sealing plate hole (611) corresponding with tubulation (7), the upper sealing plate (5) are to offer upper sealing plate corresponding with tubulation (7) hole
(521) aperture sealing plate (52) or to be provided with the tubulation head plate (51) of tubulation end socket (512) corresponding with tubulation (7).
2. multiphase flow process intensification reactor according to claim 1, it is characterised in that: the first charging aperture (1)
The material flow of entrance is gas phase, liquid phase or gas-liquid mixed phase without solid particle.
3. multiphase flow process intensification reactor according to claim 1, it is characterised in that: the second charging aperture (2)
The material flow of entrance is gas phase, liquid phase or gas-liquid mixed phase containing solid particle.
4. multiphase flow process intensification reactor according to claim 1, it is characterised in that: described tubulation (7) tube wall
The aperture in micro-or nano size duct is 10nm~300 μm.
5. multiphase flow process intensification reactor according to claim 1, it is characterised in that: described tubulation (7) tube wall
The aperture in micro-or nano size duct is 10nm~100 μm.
6. multiphase flow process intensification reactor according to claim 1, it is characterised in that: described tubulation (7) tube wall
The aperture in micro-or nano size duct is 10nm~200nm.
7. multiphase flow process intensification reactor according to claim 1, it is characterised in that: the upper sealing plate hole (521)
It is less than or equal to the diameter of corresponding tubulation (7) with the diameter in lower sealing plate hole (611).
8. multiphase flow process intensification reactor according to claim 1, it is characterised in that: the tubulation end socket (512)
Diameter is more than or equal to the diameter of corresponding tubulation (7).
9. multiphase flow process intensification reactor according to claim 1, it is characterised in that: contain in the tubulation (7)
Solid catalyst support plate, and solid catalyst particle is also loaded in tubulation (7).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201910824430.8A CN110420614A (en) | 2019-09-02 | 2019-09-02 | A kind of multiphase flow process intensification reactor |
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| CN201910824430.8A CN110420614A (en) | 2019-09-02 | 2019-09-02 | A kind of multiphase flow process intensification reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111468065A (en) * | 2020-04-24 | 2020-07-31 | 烟台大学 | Production device and production process of high-activity polyisobutylene |
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