CN108421503A - A kind of soaking type spiral plate fixed bed reactors of gas solid catalytic reaction - Google Patents
A kind of soaking type spiral plate fixed bed reactors of gas solid catalytic reaction Download PDFInfo
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- CN108421503A CN108421503A CN201810286020.8A CN201810286020A CN108421503A CN 108421503 A CN108421503 A CN 108421503A CN 201810286020 A CN201810286020 A CN 201810286020A CN 108421503 A CN108421503 A CN 108421503A
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- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 17
- 238000002791 soaking Methods 0.000 title claims abstract description 16
- 239000007787 solid Substances 0.000 title claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 71
- 230000000694 effects Effects 0.000 claims abstract description 9
- 239000003054 catalyst Substances 0.000 claims description 26
- 238000009826 distribution Methods 0.000 claims description 11
- 230000008676 import Effects 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 4
- 238000011068 loading method Methods 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 230000002687 intercalation Effects 0.000 claims description 2
- 238000009830 intercalation Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000004140 cleaning Methods 0.000 abstract description 2
- 238000003466 welding Methods 0.000 description 5
- LOMVENUNSWAXEN-UHFFFAOYSA-N Methyl oxalate Chemical compound COC(=O)C(=O)OC LOMVENUNSWAXEN-UHFFFAOYSA-N 0.000 description 4
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000003416 augmentation Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000005304 joining Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
Classifications
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- 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
- B01J8/0242—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 the fluid flow within the bed being predominantly vertical
- B01J8/0271—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 the fluid flow within the bed being predominantly vertical in a spiral shaped bed
-
- 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
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
-
- 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
- B01J8/0285—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction, include the inlet and outlet of gas phase and heat transferring medium, one or more spiral plate type fixed bed reaction sections are arranged in reactor.Advantages of the present invention：1) the shell side coefficient of heat transfer is significantly increased, overall heat-transfer coefficient is made to increase, enhances heat-transfer effect, reduces heat transfer temperature difference；2) can flexibly Heat Transfer Control distance and heat transfer area, be conducive to the uniform of reaction bed temperature with control；3) capacity utilization is big (maximum up to 70% or more, shell and tube reactor is up to 40% or so), and single set equipment production capacity is high, and floor space is significantly reduced with investment；4) heat exchanging medium passage has self-cleaning effect, is not likely to produce dirt and blocks.
Description
Technical field
The present invention relates to fixed bed reactors, and in particular to a kind of soaking type spiral plate fixed bed of gas solid catalytic reaction is anti-
Answer device.
Background technology
Fixed bed catalytic reactor has a wide range of applications in chemical industry and petroleum industry.
The advantages of fixed bed reactors is：1. back-mixing is small, fluid can be contacted effectively with catalyst, when reaction is with string
It can be obtained when joining side reaction more highly selective；2. catalytic mechanical loss is small；3. simple in structure.The disadvantage is that：1. shell-side heat transfer is imitated
Fruit is poor, and especially for strong exothermal reaction, being susceptible to temperature runaway, (reaction temperature is out of hand, steeply rises, and is more than to allow model
It encloses)；2. catalyst cannot be replaced in operating process, catalyst needs the reaction of frequent regeneration that should not generally use, often instead
Fluidized-bed reactor or moving-burden bed reactor.
It can be divided into three kinds of heat-insulating, heat exchange type and self-heating by heat exchange mode fixed bed reactors.Insulation fix bed reaction
Device and self-heating fixed bed reactors in actual industrial production using less, using it is relatively broad and ripe be that heat exchange type is consolidated
Calandria type fixed bed reactor in fixed bed reactor.It is chiefly used in strong exothermal reaction, and yield is temperature sensitive and requires high
Conversion ratio and highly selective reaction process.Its structure is similar to shell-and-tube heat exchanger, by groups such as tube bank, shell, both ends end sockets
At.When applied to gas solid catalytic reaction, tube side loading catalyst particle, and be fixed by bottom support, shell side has heat exchange
Media flow maintains the stabilization of tube side reaction temperature to carry out heat exchange with tube side.
The tube side flexible structure of calandria type fixed bed reactor, can be single tube, multitube parallel, can also be U-tube etc.,
Compared with the fixed bed reactors of other forms, have：1. the distance radially conducted heat is small, reaction heat can be made to pass to pipe in time
Wall, to accurately control reaction bed temperature；2. using for reference ripe tubular heat exchanger manufacturing technology, it is easily achieved in engineering
Advantage.But exist：1. shell-side heat transfer coefficient is small, required heat transfer area is big；2. the low space utilization of catalyst bed, causes
The shortcomings of reactor volume is huge, and equipment making is of high cost, and device is not easy enlargement.
Spiral-plate heat exchanger is to be made two closed spirality channels by two parallel metal plate coils, cold fluid and hot fluid it
Between the heat exchanger that is exchanged heat by spiral wooden partition.With small, facility compact, that heat transfer efficiency is high, metal consumption is few is excellent
Point has a wide range of applications in industries such as chemical industry, oil, medicine, electric power.
Invention content
In order to solve, existing calandria type fixed bed reactor shell-side heat transfer effect is poor, space availability ratio of catalyst bed
Low, device is not easy the technical problem of enlargement, uses for reference the structure and performance characteristics of spiral-plate heat exchanger, and the present invention provides a kind of gas
The soaking type spiral plate fixed bed reactors of solid phase contact catalysis reaction.
Technical scheme is as follows：
A kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction, including gas phase and heat transferring medium
Inlet and outlet, the one or more spiral plate type fixed bed reaction sections of the interior setting of reactor.The structure of spiral plate type fixed bed reaction section
It is similar to spiral-plate heat exchanger structure, two spiral channels, one of channel is made by two parallel metal plate coils
Upper and lower ends are closed, and as heat exchanging medium passage, heat transferring medium is flowed through helical duct and exchanged heat by wooden partition, are reached anti-
After the central tube for answering device center, then the outlet of the heat transferring medium by being connected with central tube outflow；Another channel upper and lower ends is not
It seals, forms fixed bed after loading catalyst, bed is topmost connected with gas feed, and bottom is connected with gas vent
Logical, gas enters reactor by import, after being reacted axially through catalyst fixed bed layer, is discharged by gas vent.
One or more spiral plate type conversion zones can be flexibly arranged in spiral plate fixed bed reactors, and particular number can be by anti-
Required heat exchange area is answered to determine.The gas passage of wherein multistage spiral plate type conversion zone is connected in the axial direction, and gas leads to successively
The catalyst fixed bed layer for crossing each conversion zone, is discharged after reaction by gas vent；For changing for multistage spiral plate type conversion zone
Hot media channel can be by being arranged heat transferring medium distribution apparatus or multiple heat transferring medium imports, to realize that heat transferring medium multistage is in parallel
Into each spiral plate type conversion zone, it is threaded into after the central tube of reactor center to go out from heat transferring medium by heat exchanging medium passage
Mouthful outflow, the out temperature of each spiral plate type conversion zone heat transferring medium is identical, be conducive to the uniform of reaction bed temperature and
Control.
The spacing of two wing passage of spiral plate type conversion zone can flexible design.The interchannel of heat transferring medium side is away from can be according to changing
The flow set of thermal medium improves heat transfer coefficient, augmentation of heat transfer effect by promoting the flowing velocity of heat transferring medium；Catalyst
The interchannel of fixed bed side increases as possible away under the premise of ensuring heat transfer effect, to promote the utilization rate of reactor volume.
The gas feed of spiral plate fixed bed reactors is generally located on reactor head, and outlet is generally located on reactor
Bottom is conducive to the fixation of catalyst granules, but in certain special cases, gas feed may also be arranged on reactor bottom,
Outlet is arranged in reactor head.
When spiral plate fixed bed reactors only need a heat transferring medium entrance, reactor head flange can be disposed at
Side, inlet tube is inserted into inside equipment to be connected with heat transferring medium distribution apparatus；It, can be each if need multiple heat transferring medium entrances
A heat transferring medium entrance is arranged in section spiral plate type conversion zone, and multiple entrances are arranged in parallel on the outside of reactor, realizes sectional temperature-controlled；
Outlet setting is connected in reactor top side, outlet intercalation reaction device with central tube.Heat transferring medium distribution apparatus is
The circle shaped tube type distributor being arranged below outlet, it is anti-that circle shaped tube type distributor by distributor pipe is connected to each section of spiral plate type
Section is answered, realizes that each conversion zone import heat exchange medium temperature is consistent with flow；The outlet of conversion zone heat transferring medium is connected to central tube,
After heat transferring medium heat exchange, collect in central tube, then is exported and flowed out by heat transferring medium.
Spiral plate fixed bed reactors bottom and top are by the support of inertia magnetic ball and sealing catalyst bed.
Spiral plate fixed bed reactors side wall annular space also fills inertia magnetic ball, to avoid local run aways.
The making of spiral plate fixed bed reactors is using assembling outside single hop making, conversion zone and distributor and distributor pipe device
Pattern carries out；When two sections of more parallels, groove is reserved in the central tube upper and lower side of conversion zone, it is internal after outer set fills
There are two types of the welding manners of central tube：When center pipe diameter is smaller, automatic welding bar can be used deeply into being welded in pipe；
If center pipe diameter meets into people's condition, welding personnel can enter each conversion zone by central tube, carry out the welding of inside center pipe,
Multistage conversion zone is formed a whole.After being connect again with heat exchange of top part dielectric distribution device, integral hoisting is put into group in reactor
Dress, completes the processing and fabricating of reactor.
Welding, spiral shell can be used between changing section medium inlet in heat exchange of top part dielectric distribution device of the present invention and each spiral plate reactor
Line connects or the mode of pipe collar connection is attached.
Advantages of the present invention：
1) the shell side coefficient of heat transfer is significantly increased, overall heat-transfer coefficient is made to increase, enhances heat-transfer effect, reduces heat transfer temperature
Difference；
2) can flexibly Heat Transfer Control distance and heat transfer area, be conducive to the uniform of reaction bed temperature with control；
3) capacity utilization is big (maximum up to 70% or more, shell and tube reactor is up to 40% or so), single set equipment
Production capacity is high, and floor space is significantly reduced with investment；
4) heat exchanging medium passage has self-cleaning effect, is not likely to produce dirt and blocks.
Description of the drawings
Fig. 1 is the structural schematic diagram of the present invention, and Fig. 2 is the vertical view of Fig. 1.
Wherein：1 heat transferring medium import, the outlet of 2 heat transferring mediums, 3 gas feeds, 4 gas vents, 5 circle shaped tube type distributors,
6 liquid distribution pipes, 7 central tubes, 8-N are spiral plate conversion zone.
Fig. 3 is the structural schematic diagram of the embodiment of the present invention 1, and Fig. 4 is the vertical view of Fig. 3.
Wherein：1 heat transferring medium import, the outlet of 2 heat transferring mediums, 3 gas feeds, 4 gas vents, 5 circle shaped tube type distributors,
6 liquid distribution pipes, 7 central tubes, 8-15 are spiral plate conversion zone.
Fig. 5 is the structural schematic diagram of the embodiment of the present invention 2, and Fig. 6 is the vertical view of Fig. 5.
Wherein：1 heat transferring medium exports, 2 heat transferring medium imports, 3 gas feeds, 4 gas vents, 5-1 heat transferring medium imports,
6-1 central tubes, 7-17 are spiral plate conversion zone.
Specific implementation mode
Embodiment 1
150000 tons/year of dimethyl oxalate (DMO) hydrogenation reactors
When the reactor of the present invention is used as 150,000 tons/year of DMO hydrogenation reactors, 8 sections of spiral plate type conversion zones are needed through calculating,
Its structure is shown in Fig. 3 and Fig. 4.The setting of heat transferring medium entrance 1 is arranged in reactor head side, outlet 2 in reactor top side.
Gas by top air inlet 3 enter reactor, across catalyst fixed bed layer (8~15) react after together with product the bottom of by
Portion's gas vent 4 leaves reactor；The reacted device top annular pipe distributor 5 of heat transferring medium, in proportion by several distributor pipes 6
Distribution is exchanged heat, into conversion zone to each section of spiral plate type conversion zone (08~15) outer inlets by heat exchanging medium passage spiral
After the central tube 7 of the heart summarizes, from 2 outflow of heat transferring medium outlet.
150000 tons/year of DMO hydrogenation reactors use the performance indicator of reactor of the present invention and calandria type fixed bed reactor
Comparison is shown in Table 1.
1 150kt/aDMO reactors of table compare
| Project | Fixed bed reactors of the present invention | Calandria type fixed bed reactor |
| Device diameters (mm) | 3600 | 4000 |
| Catalyst bed layer height (mm) | 8000 | 8000 |
| Loaded catalyst (m3) | 44 | 36 |
As can be seen from the above table, the capacity utilization of two kinds of reactor catalyst beds is respectively：54.06% He
35.83%, loaded catalyst of the present invention promotes 50% or more, the production capacity of device can be substantially improved, and device diameters are small, takes up an area
Area and small investment；Simultaneously by controlling heat exchanging medium passage width, improves heat transferring medium and flow speed, increase total heat transfer system
Number, reduces heat transfer temperature difference, is convenient for the control of reaction bed temperature.
Embodiment 2
3.5 ten thousand tons/year of vinyl acetate synthesis reactors
When the reactor of the present invention is used as 3.5 ten thousand tons/year of vinyl acetate synthesis reactors, 10 sections of spiral plate types are needed through calculating
Conversion zone, structure are shown in Fig. 5 and Fig. 6.To further enhance heat transfer effect, one heat exchange is arranged in each section of spiral plate type conversion zone
Medium, realization is sectional temperature-controlled, specially：Heat transferring medium entrance 2,5-1 (medium temperature may be the same or different) settings exist
Spiral plate type reacts pars infrasegmentalis, is connected with the outside of conversion zone internal heat medium channel, is exchanged heat by heat exchanging medium passage spiral,
Into conversion zone center central tube 6-1 summarize after, from heat transferring medium outlet 1 outflow.Gas is entered by top air inlet 3 to react
Device, across catalyst fixed bed layer (7~17) react after together with product reactor 4 is left by bottom gas outlet
3.5 ten thousand tons/year of vinyl acetate synthesis reactors use the property of reactor of the present invention and calandria type fixed bed reactor
Energy index comparison is shown in Table 2.
2 3.5 ten thousand tons/year of vinyl acetate synthesis reactor comparisons of table
| Project | Fixed bed reactors of the present invention | Calandria type fixed bed reactor |
| Device diameters (mm) | 3800 | 4200 |
| Catalyst bed layer height (mm) | 10000 | 10000 |
| Loaded catalyst (m3) | 61.5 | 49.6 |
As can be seen from the above table, the capacity utilization of two kinds of reactor catalyst beds is respectively：54.25% He
35.81%, loaded catalyst of the present invention promotes 50% or more, the production capacity of device can be substantially improved, and device diameters are small, takes up an area
Area and small investment；Simultaneously by controlling heat exchanging medium passage width, improves heat transferring medium and flow speed, increase total heat transfer system
Number, reduces heat transfer temperature difference, is convenient for the control of reaction bed temperature.
Claims (10)
1. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction, it is characterised in that：Including gas phase and
The inlet and outlet of heat transferring medium, the one or more spiral plate type fixed bed reaction sections of the interior setting of reactor；Spiral plate type fixed bed is anti-
Section is answered to be made two spiral channels by two parallel metal plate coils, one of channel upper and lower ends closing, as changing
Hot media channel, heat transferring medium is flowed through helical duct and is exchanged heat by wooden partition, after the central tube for reaching reactor center,
Outflow is exported by the heat transferring medium being connected with central tube again；Another channel upper and lower ends blow-by, shape after loading catalyst
At fixed bed, bed is topmost connected with gas feed, and bottom is connected with gas vent, and gas is entered anti-by import
Device is answered, after being reacted axially through catalyst fixed bed layer, is discharged by gas vent.
2. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：The quantity of spiral plate type fixed bed reaction section is determined by the heat exchange area needed for reacting.
3. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：The gas passage of multiple spiral plate type fixed bed reaction sections is connected in the axial direction, and gas passes sequentially through each conversion zone
Catalyst fixed bed layer, be discharged by gas vent after reaction.
4. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：The heat exchanging medium passage of multiple spiral plate type fixed bed reaction sections can be by being arranged heat transferring medium distribution apparatus or multiple
Heat transferring medium entrance is led to realizing that heat transferring medium multistage parallel connection enters each spiral plate type fixed bed reaction section by heat transferring medium
Road is threaded into after the central tube of reactor center and exports outflow from heat transferring medium, each spiral plate type conversion zone heat transferring medium
Out temperature is identical, is conducive to the uniform of reaction bed temperature and control.
5. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：The interchannel of heat transferring medium side is away from the flow set according to heat transferring medium.
6. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：The interchannel of catalyst fixed bed layer side increases as possible away under the premise of ensuring heat transfer effect.
7. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：In reactor head, outlet is arranged in reactor bottom for the gas feed setting of spiral plate fixed bed reactors；Or
Gas feed setting is arranged in reactor bottom, outlet in reactor head.
8. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：When spiral plate fixed bed reactors only need a heat transferring medium entrance, reactor head flange can be disposed at
Side, inlet tube is inserted into inside equipment to be connected with heat transferring medium distribution apparatus；It, can be each if need multiple heat transferring medium entrances
A heat transferring medium entrance is arranged in section spiral plate type conversion zone, and multiple entrances are arranged in parallel on the outside of reactor, realizes sectional temperature-controlled；
Outlet setting is connected in reactor top side, outlet intercalation reaction device with central tube.
9. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：Heat transferring medium distribution apparatus is the circle shaped tube type distributor being arranged below outlet, and circle shaped tube type distributor passes through
Distributor pipe is connected to each section of spiral plate type conversion zone, realizes that each conversion zone import heat exchange medium temperature is consistent with flow.
10. a kind of soaking type spiral plate fixed bed reactors of gas-solid contact catalysis reaction as described in claim 1, special
Sign is：The outlet of conversion zone heat transferring medium is connected to central tube, after heat transferring medium heat exchange, is collected in central tube, then be situated between by heat exchange
Matter outlet outflow.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810286020.8A CN108421503A (en) | 2018-04-03 | 2018-04-03 | A kind of soaking type spiral plate fixed bed reactors of gas solid catalytic reaction |
| CN201811042302.XA CN109382045A (en) | 2018-04-03 | 2018-09-07 | A kind of spiral plate fixed bed reactors of gas-solid contact catalysis reaction |
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| CN201810286020.8A CN108421503A (en) | 2018-04-03 | 2018-04-03 | A kind of soaking type spiral plate fixed bed reactors of gas solid catalytic reaction |
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| CN201811042302.XA Pending CN109382045A (en) | 2018-04-03 | 2018-09-07 | A kind of spiral plate fixed bed reactors of gas-solid contact catalysis reaction |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111701548A (en) * | 2020-06-19 | 2020-09-25 | 宁波巨化化工科技有限公司 | Fixed bed propionaldehyde synthesis reactor |
| CN113694835A (en) * | 2021-09-30 | 2021-11-26 | 江苏航运职业技术学院 | Spiral propelling fixed bed reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110327847B (en) * | 2019-08-07 | 2024-01-26 | 华东理工大学 | Radial flow heat exchange type fixed bed catalytic reactor |
| EP4347102A1 (en) * | 2021-05-27 | 2024-04-10 | Basf Se | Method for producing phosgene |
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| JPS61118132A (en) * | 1984-11-14 | 1986-06-05 | Mitsubishi Petrochem Co Ltd | Catalytic reactor |
| CN201653205U (en) * | 2010-04-21 | 2010-11-24 | 苏州市锦翔压力容器制造有限公司 | Channel series-connection helical plate heat exchanger |
| CN104801240B (en) * | 2015-03-24 | 2017-04-05 | 德艾柯工程技术（上海）有限公司 | A kind of plate-type heat-exchange reactor |
| CN105107434A (en) * | 2015-09-02 | 2015-12-02 | 李东儒 | Novel reactor for preparing epoxy propane by oxidizing propylene with hydrogen peroxide |
| CN105879790A (en) * | 2016-06-06 | 2016-08-24 | 江苏怡达化学股份有限公司 | Novel HPPO reactor |
| CN106732204A (en) * | 2017-02-04 | 2017-05-31 | 济南承乾工程技术有限公司 | One kind segmentation spiral plate type ultralow pressure isothermal ammonia convertor |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111701548A (en) * | 2020-06-19 | 2020-09-25 | 宁波巨化化工科技有限公司 | Fixed bed propionaldehyde synthesis reactor |
| CN111701548B (en) * | 2020-06-19 | 2021-06-08 | 宁波巨化化工科技有限公司 | Fixed bed propionaldehyde synthesis reactor |
| WO2021254194A1 (en) * | 2020-06-19 | 2021-12-23 | 宁波巨化化工科技有限公司 | Fixed bed propanal synthesis reactor |
| CN113694835A (en) * | 2021-09-30 | 2021-11-26 | 江苏航运职业技术学院 | Spiral propelling fixed bed reactor |
| CN113694835B (en) * | 2021-09-30 | 2023-06-27 | 江苏航运职业技术学院 | Spiral propulsion fixed bed reactor |
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| CN109382045A (en) | 2019-02-26 |
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Application publication date: 20180821 |
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