CN109966998B - Tubular reactor - Google Patents
Tubular reactor Download PDFInfo
- Publication number
- CN109966998B CN109966998B CN201910314214.9A CN201910314214A CN109966998B CN 109966998 B CN109966998 B CN 109966998B CN 201910314214 A CN201910314214 A CN 201910314214A CN 109966998 B CN109966998 B CN 109966998B
- Authority
- CN
- China
- Prior art keywords
- tube
- end cover
- inner tube
- pipe
- tubular reactor
- 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.)
- Active
Links
- 239000002994 raw material Substances 0.000 claims abstract description 39
- 238000012546 transfer Methods 0.000 claims abstract description 13
- 239000003054 catalyst Substances 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 229920006395 saturated elastomer Polymers 0.000 claims description 8
- 239000000498 cooling water Substances 0.000 claims description 2
- 150000003839 salts Chemical class 0.000 claims description 2
- 238000010276 construction Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 38
- 238000003756 stirring Methods 0.000 abstract description 3
- 230000002159 abnormal effect Effects 0.000 abstract 1
- 239000010408 film Substances 0.000 description 14
- 239000007788 liquid Substances 0.000 description 9
- 238000006277 sulfonation reaction Methods 0.000 description 8
- 239000011148 porous material Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 239000012528 membrane Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 230000001681 protective effect Effects 0.000 description 2
- 230000005856 abnormality Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000013341 scale-up Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000010409 thin film Substances 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
- B01J8/008—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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
- B01J8/065—Feeding reactive fluids
-
- 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a novel tubular reactor, which comprises an inner tube, an inlet end cover, an outlet end cover, an outer tube and a hollow tube, wherein the inner tube is coaxially arranged in the outer tube, the hollow tube is respectively arranged above and below the outer tube, the hollow tube is communicated with the inside of the outer tube, two ends of the inner tube pass through the hollow tube, the bottom of the inner tube is communicated with the inlet end cover, the top of the inner tube is communicated with the outlet end cover, a raw material inlet tube is coaxially arranged below the inner tube, and the raw material inlet tube passes through the inlet end cover and stretches into the inner tube. The novel tubular reactor disclosed by the invention is utilized for reaction, so that raw materials can be uniformly mixed and fully reacted in a reaction tube under the condition that a stirring device is not arranged; the device has high heat transfer rate, can absorb the difference of thermal expansion of the inner tube and the outer tube, and is suitable for abnormal temperature of the reaction tube; the applicable reaction pressure and temperature range are wider.
Description
Technical Field
The invention relates to the field of chemical reaction equipment, in particular to a tubular reactor.
Background
Chemical reactions are classified into endothermic reactions and exothermic reactions. For exothermic reactions, the heat generated by the reaction needs to be quickly removed, so that the occurrence of side reactions is reduced, and the possibility of catalyst failure is reduced. For endothermic reactions, a stable amount of heat is required to maintain the conversion and selectivity of the reaction.
The equipment for realizing the chemical reaction is called a reactor and can be divided into the following components according to the structural characteristics of the equipment: kettle type reactors, tubular reactors, tower type reactors, and jet type reactors. The tubular reactor mainly comprises a tubular reactor, a sleeve-type reactor, a micro-tube reactor and a tubular film sulfonation reactor.
The tube type reactor is improved by a fixed tube plate type heat exchanger, wherein the fixed tube plate type heat exchanger is vertically arranged, and is filled or not filled with catalysis. The raw materials of single or mixed components react through the tube array, and the heat released by the reaction is transferred from the medium outside the tube array. The tubular reactor is more commonly used in existing industrial settings. However, the fixed tube sheet tube array reactor has several disadvantages:
a) If the reaction raw materials are all liquid or gas, the mixing is completed outside the tubular reactor;
b) Under the condition that the reaction raw materials have gas phase and liquid phase, a film forming head is required to be arranged at the upper end part of the tube array;
c) The reaction is carried out in a tube array, and the metal wall temperature of the tube array along the length direction is higher than the wall temperature of the shell, so that the thermal expansion amount of the tube array and the shell along the length direction is inconsistent, and an expansion joint is possibly required to be arranged on the shell to solve the problems of strength and safety of equipment;
4. for structural reasons, the method is suitable for industrial devices with low requirements on reaction pressure and reaction temperature.
The double pipe reactor is improved by a double pipe heat exchanger. The raw materials of the single or mixed components are reacted through the inner tube. The outer tube and the inner tube are welded and sealed by adopting end plates to form an annular section, heat released rapidly by the reaction is transferred through a medium in the annular section, and the reactor has the following defects in the operation process:
a) The reaction is carried out in the inner tube, the heat generated by the reaction makes the metal wall temperature of the inner tube higher than that of the outer tube in the length direction, and the possibility that a pipeline compensator needs to be arranged on the outer tube exists;
b) The inner tube is a hollow tube, so that the requirement of uniform mixing of raw materials is difficult to meet;
c) For reasons of b), the inner tube diameter is generally not more than 20mm;
d) For reasons of b) and c), the sleeve reactors are difficult to scale up industrially, rarely found in industrial plants, and are generally used for experimental investigation.
The microchannel reactor is one of the tubular reactors, the diameter of the reaction tube is small, and the reaction tube is placed in a water bath or an oil bath. The single or mixed component materials are passed through a reaction tube to obtain the desired product, and the heat released by the reaction is transferred from a water bath or an oil bath. Microreactors are commonly found in scientific laboratories, rarely found in industrial devices, and the diameter of the reaction tube is small, which cannot meet the industrial production requirements.
The tubular film sulfonation reactor is found in the sulfonation process and comprises three types of single-film type sulfonation reactor, double-film type sulfonation reactor and tubular type sulfonation reactor, wherein the double-film type sulfonation reactor is the most used one. The main defects of the tubular film sulfonation reactor in the use process are as follows:
a) The tube type thin film reactor needs to be additionally provided with a film former at the tube end of the reaction tube, so that liquid raw materials are formed into films, and gas-phase raw materials enter the reaction tube at the same time;
b) The single film type and the double film type adopt excessive protective gas to push the liquid film to form, the film thickness is not easy to control, a fan is needed to be used when excessive air is added, and the electric energy is consumed greatly;
c) The single-membrane type and double-membrane type liquid membrane is formed by pushing the liquid membrane by excessive protective gas, the length of a reaction tube is longer, the operation condition is small, the process condition is strict, the device is not suitable for frequent start and stop, the structure is complex, the requirements on equipment processing and installation precision are high, and the investment cost is high.
Disclosure of Invention
Aiming at the problems, the invention aims to provide a tubular reactor which has simple structure, stable operation, high reliability and convenient maintenance.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows: the utility model provides a tubular reactor, includes inner tube, entry end cover, exit end cover, outer tube and cavity pipe fitting, the inner tube coaxial arrangement is inside the outer tube, is equipped with a cavity pipe fitting respectively in the top and the below of outer tube, and cavity pipe fitting is preferably flat pipe, and cavity pipe fitting communicates with the outer tube is inside, and the inner tube both ends are passed in the cavity pipe fitting and its bottom with the entry end cover link up, the top with the exit end cover link up, is equipped with a raw materials below the inner tube coaxial, and raw materials advances the pipe and pass the entry end cover and stretch into in the inner tube.
Further, the heat transfer medium enters the space formed by the outer tube and the inner tube from the opening on one of the hollow tube members, and flows out from the opening on the other hollow tube member.
Further, the heat transfer medium comprises cooling water, saturated water, molten salt, heat conducting oil and the like, and preferably, the heat transfer medium is saturated water.
Further, a nozzle is arranged at one end of the raw material inlet pipe, which is positioned in the inner pipe.
Further, a pipe mixer is arranged inside the inner pipe and above the raw material inlet pipe to promote heat and mass transfer.
Further, the catalyst is filled in the inner tube, the outlet end cover is of a flange connection structure, a wire mesh or a pore plate is arranged in the inner tube, and the catalyst is filled in the wire mesh or the pore plate from the outlet end cover.
The beneficial effects of the invention are as follows:
1. the tubular reactor disclosed by the invention is utilized for reaction, so that raw materials can be uniformly mixed and fully reacted in a reaction tube under the condition that a stirring device is not arranged;
2. the heat released rapidly for exothermic reactions is transferred rapidly from the medium outside the tube, and the heat required for endothermic reactions is transferred rapidly from the medium outside the tube into the tube;
3. on the premise of not arranging expansion joints, the thermal expansion difference between the inner tube and the outer tube is absorbed, and the temperature abnormality of the reaction tube is adapted;
4. the applicable reaction pressure and temperature range are wider.
Drawings
FIG. 1 is a schematic view showing the structure of a tubular reactor according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of a tubular reactor according to a second embodiment of the present invention.
Wherein, 1-inner tube, 2-inlet end cover, 3-outlet end cover, 4-outer tube, 5-hollow pipe fitting, 6-raw material inlet tube, 7-pipe mixer, 8-catalyst.
Detailed Description
In order to enable those skilled in the art to better understand the technical solution of the present invention, the technical solution of the present invention is further described below with reference to fig. 1-2 and examples.
It should be noted that the embodiments provided in the present invention are only for effectively describing technical features of the present invention, and the positioning words such as left side, right side, upper end, lower end and the like are only for better describing the embodiments of the present invention, and are not to be construed as limiting the technical scheme of the present invention.
Example 1
The invention provides a tubular reactor, which comprises an inner tube 1, an inlet end cover 2, an outlet end cover 3, an outer tube 4 and two hollow tubes 5, wherein the inner tube 1 is coaxially arranged in the outer tube 4, the hollow tubes 5 are respectively arranged above and below the outer tube 4, the hollow tubes 5 are communicated with the inside of the outer tube, the two ends of the inner tube 1 pass through the hollow tubes 5, the bottoms of the inner tube are communicated with the inside of the inlet end cover 2, the tops of the inner tube 1 are communicated with the inside of the outlet end cover 3, saturated water is directly vaporized into steam after absorbing heat, so that the saturated water needs to enter a space formed by enclosing the outer tube 4 and the inner tube 1 from an opening on the hollow tube 5 at the bottom, and flows out from an opening on the hollow tube 5 at the top, and the direction indicated by an arrow in fig. 1 is the flowing direction of the saturated water. A raw material inlet pipe 6 is coaxially arranged below the inner pipe 1, the raw material inlet pipe 6 penetrates through the inlet end cover 2 and stretches into the inner pipe, and a nozzle is arranged at one end of the raw material inlet pipe 6 positioned in the inner pipe 1.
A pipeline mixer 7 for promoting mass transfer and heat transfer is arranged inside the inner pipe 1 and above the raw material inlet pipe 6, a catalyst 8 is filled in the inner pipe 1, the outlet end cover 3 is in a flange connection structure, a silk screen or a pore plate is arranged in the inner pipe 1, and the catalyst 8 is filled in the silk screen or the pore plate from the outlet end cover 3.
When in use, the raw material A enters the inner tube from the inlet end cover 2, the raw material B enters the inner tube from the raw material inlet tube 6, and the raw material A and the raw material B can be single substances or mixtures, and the phase state of the raw material A and the raw material B can be gas or liquid. The raw material inlet pipe 6 has a function of dispersing liquid or gas, and the passing liquid and/or gas can be uniformly distributed on the cross section of the inner pipe 1 through the pipe orifice nozzle, so that the mixing efficiency with the raw material A is enhanced under the condition of not adding a stirring device, if necessary, the pipe diameter of the raw material inlet pipe 6 can be increased, the pipe length can be prolonged, the liquid raw material passing through the space formed by the surrounding of the raw material inlet pipe 6 and the inner pipe 1 is formed into a film shape, and the reaction product flows out of the reactor from the outlet end cover 3 after the reaction is completed.
Example two
The difference between the tubular reactor disclosed in this embodiment and the first embodiment is that the tubular reactor is formed by connecting a plurality of reactors in parallel, and specifically comprises a plurality of outer tubes 4 which are arranged in parallel, an inner tube 1 corresponding to the number of the outer tubes 4, an inlet end cover 2, an outlet end cover 3 and two hollow tubes 5, wherein the inner tube 1 is coaxially arranged inside each outer tube 4, one hollow tube 5 is respectively arranged above and below each outer tube 4, the hollow tubes 5 are communicated with the inside of the outer tube 4, two ends of the inner tube 1 pass through the hollow tubes 5, the bottoms of the inner tubes pass through the inside of the inlet end cover 2, the tops of the inner tubes pass through the inside of the outlet end cover 3, and saturated water enters a space formed by encircling the outer tube 4 and the inner tube 1 from the hollow tubes 5 at the bottoms and flows out from the hollow tubes 5 at the tops. A raw material inlet pipe 6 is coaxially arranged below each inner pipe 1, the raw material inlet pipe 6 penetrates through the inlet end cover 2 and stretches into the inner pipe, and a nozzle is arranged at one end of the raw material inlet pipe 6 positioned in the inner pipe 1.
A pipeline mixer 7 for promoting mass transfer and heat transfer is arranged inside the inner pipe 1 and above the raw material inlet pipe 6, the inner pipe 1 is filled with catalyst, the outlet end cover is of a flange connection structure, a silk screen or a pore plate is arranged in the inner pipe 1, and the catalyst is filled in the silk screen or the pore plate from the outlet end cover.
The foregoing has outlined and described the basic principles, features, and advantages of the present invention. However, the foregoing is merely specific examples of the present invention, and the technical features of the present invention are not limited thereto, and any other embodiments that are derived by those skilled in the art without departing from the technical solution of the present invention are included in the scope of the present invention.
Claims (5)
1. The tubular reactor is characterized by comprising a plurality of outer tubes (4) which are arranged in parallel, inner tubes (1), an inlet end cover (2), an outlet end cover (3) and two hollow tubes (5) which are corresponding to the outer tubes (4), wherein one inner tube (1) is coaxially arranged in each outer tube (4), one hollow tube (5) is respectively arranged above and below each outer tube (4), the hollow tubes (5) are communicated with the inside of the outer tube (4), two ends of each inner tube (1) penetrate through the hollow tube (5), the bottoms of the inner tubes penetrate through the inside of the inlet end cover (2), and the tops of the inner tubes penetrate through the inside of the outlet end cover (3);
the heat transfer medium enters a space formed by enclosing the outer tube (4) and the inner tube (1) from the hollow tube (5) at the bottom and flows out from the hollow tube (5) at the top;
a raw material inlet pipe (6) is coaxially arranged below each inner pipe (1), and the raw material inlet pipe (6) penetrates through the inlet end cover (2) and stretches into the inner pipe (1);
a nozzle is arranged at one end of the raw material inlet pipe (6) positioned in the inner pipe (1).
2. A tubular reactor as claimed in claim 1 wherein the heat transfer medium comprises cooling water, saturated water, molten salt and heat transfer oil.
3. A tubular reactor as claimed in claim 2 wherein the heat transfer medium is saturated water.
4. A tubular reactor according to claim 1, characterized in that a pipe mixer (7) is provided inside the inner pipe (1) above the feed inlet pipe (6).
5. A tubular reactor according to claim 1, characterized in that the inner tube is filled with catalyst (8), the outlet end cap (3) is of flanged construction, a wire mesh or orifice plate is provided in the inner tube (1), and the catalyst (8) is fed from the outlet end cap (3) onto the wire mesh or orifice plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910314214.9A CN109966998B (en) | 2019-04-18 | 2019-04-18 | Tubular reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910314214.9A CN109966998B (en) | 2019-04-18 | 2019-04-18 | Tubular reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109966998A CN109966998A (en) | 2019-07-05 |
| CN109966998B true CN109966998B (en) | 2024-03-26 |
Family
ID=67085259
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910314214.9A Active CN109966998B (en) | 2019-04-18 | 2019-04-18 | Tubular reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109966998B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111960971B (en) * | 2020-09-19 | 2023-04-11 | 寿光市荣晟新材料有限公司 | Production process and production equipment of 2-acrylamide-2-methylpropanesulfonic acid |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE734892A (en) * | 1968-06-20 | 1969-12-22 | ||
| US4865817A (en) * | 1987-03-02 | 1989-09-12 | University Of Waterloo | Gas reacting apparatus |
| US5445801A (en) * | 1992-05-19 | 1995-08-29 | Meccaniche Moderne S.R.L. Chemical Plants Division | Multitube falling-film reactor |
| CA2214751A1 (en) * | 1995-03-07 | 1996-09-12 | Shell Canada Limited | Feed nozzle assembly |
| CN1183059A (en) * | 1995-03-28 | 1998-05-27 | 比格·达尔 | Multitube falling film reactor for the continuous mfg. of sulfonated and/or sulfated compounds |
| CN202921278U (en) * | 2012-11-20 | 2013-05-08 | 迈瑞尔实验设备（上海）有限公司 | Efficient heat exchange reactor |
| CN103228349A (en) * | 2010-10-13 | 2013-07-31 | 布斯化工技术股份公司 | Process and apparatus for continuous high temperature short-ime alkoxylation (ethoxylation, propoxylation) of chemical substances with active hydrogen atoms |
| CN108079932A (en) * | 2018-02-01 | 2018-05-29 | 贵州道元生物技术有限公司 | The continuous flow deferent Dow Chemical reactor of fast assembling-disassembling |
| CN210252196U (en) * | 2019-04-18 | 2020-04-07 | 常州瑞凯化工装备有限公司 | Novel tubular reactor |
-
2019
- 2019-04-18 CN CN201910314214.9A patent/CN109966998B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE734892A (en) * | 1968-06-20 | 1969-12-22 | ||
| US4865817A (en) * | 1987-03-02 | 1989-09-12 | University Of Waterloo | Gas reacting apparatus |
| US5445801A (en) * | 1992-05-19 | 1995-08-29 | Meccaniche Moderne S.R.L. Chemical Plants Division | Multitube falling-film reactor |
| CA2214751A1 (en) * | 1995-03-07 | 1996-09-12 | Shell Canada Limited | Feed nozzle assembly |
| CN1183059A (en) * | 1995-03-28 | 1998-05-27 | 比格·达尔 | Multitube falling film reactor for the continuous mfg. of sulfonated and/or sulfated compounds |
| CN103228349A (en) * | 2010-10-13 | 2013-07-31 | 布斯化工技术股份公司 | Process and apparatus for continuous high temperature short-ime alkoxylation (ethoxylation, propoxylation) of chemical substances with active hydrogen atoms |
| CN202921278U (en) * | 2012-11-20 | 2013-05-08 | 迈瑞尔实验设备（上海）有限公司 | Efficient heat exchange reactor |
| CN108079932A (en) * | 2018-02-01 | 2018-05-29 | 贵州道元生物技术有限公司 | The continuous flow deferent Dow Chemical reactor of fast assembling-disassembling |
| CN210252196U (en) * | 2019-04-18 | 2020-04-07 | 常州瑞凯化工装备有限公司 | Novel tubular reactor |
Non-Patent Citations (1)
| Title |
|---|
| 王建华主编.《化学反应工程 下 化学反应器设计》.成都科技大学出版社,1989,第377页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109966998A (en) | 2019-07-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US9504979B2 (en) | Radial-parallel catalytic reactor | |
| CN109966998B (en) | Tubular reactor | |
| CN102059081A (en) | Tubular reactor for performing liquid phase oxidation on cyclohexane by utilizing pure oxygen (enriched oxygen) | |
| CN210252196U (en) | Novel tubular reactor | |
| CN112387218A (en) | Self-heating type tubular reforming hydrogen production reactor | |
| AU2018330243A1 (en) | Conversion reactor and management of method | |
| CN105833804B (en) | Steam ascending manner radial flow reactors | |
| CN102085467A (en) | Fixed bed catalytic reactor | |
| CN219186845U (en) | Gas-liquid-solid three-phase flow tube type spiral micro-channel reactor | |
| CN111013497B (en) | Tube array reactor | |
| CN105413592A (en) | Combined type fixed bed reactor and device formed thereby | |
| WO2018205943A1 (en) | Modularized temperature control reactor | |
| CN205235936U (en) | Modular fixed bed reactor reaches device by its formation | |
| CN201551994U (en) | Fixed bed catalytic reactor | |
| CN204656515U (en) | A kind of isothermal reactor being applicable to strong exothermal reaction | |
| US3271116A (en) | Apparatus for continuous pyrolysis of liquid materials | |
| CN219186849U (en) | Vertical pipe type micro-channel reactor suitable for gas-liquid continuous in-out reaction | |
| CN216826213U (en) | Double-cooling static reactor | |
| CN216879280U (en) | Barrel type reactor | |
| CN213493744U (en) | Take heat preservation function's baffling pipe case and reactor | |
| CN108774113A (en) | The process units and its production method of bisphenol-A | |
| CN219580511U (en) | Tubular fixed bed reactor | |
| CN221132285U (en) | Efficient falling film absorption tubular reactor | |
| CN219186844U (en) | Gas-liquid-solid three-phase flow spin flow tube type microchannel reactor | |
| CN221656594U (en) | High-efficient clean reaction unit of dimethyl disulfide coproduction dimethyl disulfide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |