CN112588210A - Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year - Google Patents
Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year Download PDFInfo
- Publication number
- CN112588210A CN112588210A CN202110056348.2A CN202110056348A CN112588210A CN 112588210 A CN112588210 A CN 112588210A CN 202110056348 A CN202110056348 A CN 202110056348A CN 112588210 A CN112588210 A CN 112588210A
- Authority
- CN
- China
- Prior art keywords
- loop
- phthalic anhydride
- molten salt
- reaction
- reaction apparatus
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
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
- B01J8/02—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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/77—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom ortho- or peri-condensed with carbocyclic rings or ring systems
- C07D307/87—Benzo [c] furans; Hydrogenated benzo [c] furans
- C07D307/89—Benzo [c] furans; Hydrogenated benzo [c] furans with two oxygen atoms directly attached in positions 1 and 3
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a phthalic anhydride reaction device capable of producing 8 ten thousand tons per year, wherein a reactor main body of the reaction device comprises an upper end socket channel, a reaction tube bundle and a lower end socket channel; the reaction tube bundle is provided with reaction tubes, the outer wall of the reaction tube bundle is provided with an upper loop and a lower loop which are molten salt loops, and the wall of the reactor corresponding to the upper loop and the lower loop is provided with a groove and a cylindrical screen plate; the two ends of the reactor are provided with a gas inlet and a gas outlet, and the gas inlet is provided with a gas distributor and a static mixer; two groups of fused salt inlets and outlets are arranged on the upper loop and the lower loop, and two fused salt pipelines and two groups of fused salt pumps are arranged. According to the invention, the multi-stage flow equalizer is arranged in the molten salt loop, so that the molten salt flows more uniformly, and the heat transfer is more efficient; the static mixer is arranged at the gas inlet, so that the raw material gas and the air can make multidimensional rotation and play, coking blockage can be avoided, the raw material gas and the air can be mixed more fully, and the comprehensive cost of the production unit yield of the phthalic anhydride is reduced by about 5 percent.
Description
Technical Field
The invention relates to the technical field of chemical equipment, in particular to a phthalic anhydride reaction device capable of producing 8 ten thousand tons per year.
Background
The reaction device for producing phthalic anhydride by using industrial naphthalene or o-xylene as a raw material has the following technical problems at present: 1. the single set of production capacity of the system is limited, and the requirement of market development cannot be met; 2. because the diameter of the equipment is larger, the flowing uniformity of the molten salt in the shell pass is limited, and the optimal temperature environment cannot be provided for the catalyst; 3. the gas flow is large, the diameter of an inlet pipeline is thick, on one hand, the raw material gas and air are not sufficiently mixed, and the conversion rate of the raw material is not high; on the other hand, industrial naphthalene contains more impurities, so that coking and blockage of a system gas pipeline are easily caused.
Disclosure of Invention
The invention aims to provide a phthalic anhydride reaction device capable of producing 8 ten thousand tons every year, which overcomes the defects in the prior art and has the advantages of more reasonable structure, more efficient heat transfer and lower energy consumption.
The technical scheme adopted by the invention is as follows:
benzoic anhydride reaction unit of 8 ten thousand tons of annual productions, its characterized in that:
the reactor main body of the reaction device comprises an upper end socket pipe box, a reaction pipe bundle and a lower end socket pipe box; the reaction tube bundle is provided with reaction tubes, the outer wall of the reaction tube bundle is provided with an upper loop and a lower loop which are molten salt loops, and the wall of the reactor corresponding to the upper loop and the lower loop is provided with a groove and a cylindrical screen plate;
the two ends of the reactor are provided with a gas inlet and a gas outlet, and the gas inlet is provided with a gas distributor and a static mixer;
two groups of fused salt inlets and outlets are arranged on the upper loop and the lower loop, and two fused salt pipelines and two groups of fused salt pumps are arranged.
At least 25000 reaction tubes in the reaction tube bundle are arranged, the outer diameter is 30mm, the wall thickness is 2.5mm, and the length is 4000 mm.
The diameter of the upper ring track and the lower ring track is 8000-9000mm, and the width is 600-700 mm.
And another molten salt circulating pipeline is arranged between the upper ring channel and the lower ring channel and comprises a molten salt regulating valve, a molten salt cooler and a molten salt balance valve.
The reaction device also comprises a steam superheater which is hung outside the molten salt loop.
The reaction device also comprises an electric heater which is hung outside the molten salt loop.
And multistage flow equalizers are arranged in the upper loop and the lower loop.
The area in the loop close to the molten salt pump is a pump port area, and the flow equalizer in the pump port area is a Y-shaped clapboard or a double-C-shaped clapboard;
the area far away from the molten salt pump in the loop is a loop central area, and the flow equalizer in the loop central area is a Z-shaped partition plate or a linear partition plate.
The static mixer is a paddle plate type static mixer and comprises a plurality of coaxial cylinders, and paddles arranged in the circumferential direction are welded among the cylinders.
The static mixer is a corrugated plate type static mixer and comprises a plurality of bent thin plates which are connected in a welding mode.
The invention has the following advantages:
1. the reactor of the present invention has lowered comprehensive cost of producing phthalic anhydride in unit yield by about 5%.
2. According to the reactor, the multistage flow equalizer is arranged in the molten salt loop, so that the molten salt flows more uniformly in the shell pass of the reactor, the heat transfer is more efficient, and a more stable temperature environment is provided for the catalyst;
3. the reactor of the invention is provided with a static mixer and a gas distributor at the gas inlet side. According to the physical properties of different raw material gases, the mixer with the corresponding structure is selected, so that the raw material liquid is gasified and then rotates and moves with air in multiple angles and multiple dimensions, coking blockage can be avoided, and the raw material liquid can be mixed more fully.
Drawings
FIG. 1 is a block diagram of the present invention.
FIG. 2 is a view showing a structure of a cylindrical screen.
FIG. 3 is a structural view of a paddle type static mixer.
FIG. 4 is a structural view of a corrugated plate type static mixer.
FIG. 5 is a view showing the structure of a Y-shaped separator.
Fig. 6 is a structural view of a double C-type separator.
FIG. 7 is a view showing the structure of a Z-shaped separator.
Fig. 8 is a view showing a structure of a linear type partition plate.
The labels in the figure are: the system comprises a reactor main body 1, a molten salt cooler 2, a molten salt regulating valve 3, a first molten salt pump 4a, a second molten salt pump 4b, a multistage flow equalizer 5, a gas distributor 6, a static mixer 7, a molten salt balance valve 8, a steam superheater 9 and an electric heater 10.
Detailed Description
The present invention will be described in detail with reference to specific embodiments.
The invention relates to a phthalic anhydride reaction device capable of producing 8 ten thousand tons per year, wherein a reactor main body 1 of a reactor comprises an upper end socket pipe box, a reaction pipe bundle and a lower end socket pipe box; a certain number of reaction tubes are arranged in the reaction tube bundle, an upper loop and a lower loop are arranged on the outer wall of the reaction tube bundle and are molten salt loops, and holes are formed in the reactor wall corresponding to the upper loop and the lower loop and are provided with cylindrical screen plates; the two ends of the reactor are provided with a gas inlet and a gas outlet, and the gas inlet is provided with a gas distributor 6 and a static mixer 7. The number of reaction tubes in the reaction tube bundle is large, at least 25000 reaction tubes are arranged, the outer diameter is 30mm, the wall thickness is 2.5mm, and the length is 4000 mm. The upper ring track and the lower ring track have larger sizes, the diameter is 8000-9000mm, and the width is 600-700 mm.
Two groups of fused salt inlets and outlets are arranged on the upper loop and the lower loop, and two fused salt pipelines and two groups of fused salt pumps are arranged. And another molten salt circulating pipeline is also arranged between the upper ring channel and the lower ring channel and comprises a molten salt regulating valve 3, a molten salt cooler 2 and a molten salt balance valve 8.
The reactor also comprises a steam superheater 9 which is hung outside the molten salt loop. The reactor also comprises an electric heater 10 which is hung outside the molten salt loop.
And a multistage flow equalizer 5 is arranged in the upper loop and the lower loop. The area in the loop close to the molten salt pump is a pump port area, and the flow equalizer in the pump port area is a Y-shaped clapboard or a double-C-shaped clapboard; the area far away from the molten salt pump in the loop is a loop central area, and the flow equalizer in the loop central area is a Z-shaped partition plate or a linear partition plate.
The static mixer 7 is a paddle-plate type static mixer, and comprises a plurality of coaxial cylinders, and paddles arranged in the circumferential direction are welded among the cylinders. The static mixer 7 is either a corrugated plate static mixer comprising a plurality of welded-on bent sheets.
The invention is explained in further detail with reference to the drawings in which:
the invention comprises a reactor body 1, a molten salt cooler 2, a molten salt regulating valve 3, two molten salt pumps, a multistage flow equalizer 5 arranged in a molten salt loop, a gas distributor 6 and a static mixer 7 arranged at a gas inlet of the reactor, a molten salt balance valve 8, a steam superheater 9 and an electric heater 10.
The reactor of the invention adopts a molten salt pump circulation technology, and two groups of fused salt inlets and outlets are arranged on a loop. When the system is operated, according to the specific physical properties of raw materials (industrial naphthalene, o-xylene or a mixture of the industrial naphthalene and the o-xylene in a certain proportion) with different components, the raw materials are fully mixed with air through a static mixer 7 after being sprayed and gasified, and then enter an upper head channel from the top of a reactor.
The static mixer 7 is a paddle-plate type static mixer, and is suitable for the working condition that raw material gas contains viscous impurities and is easy to coke and block. Namely, the reaction raw material is industrial naphthalene, and a plurality of groups of mixers with different rotational flow angles are combined for use by adjusting the number of blades and the deflection angles thereof according to the physical properties of the raw material gas. The raw material gas and the air are repeatedly swirled at multiple angles, so that the raw material gas and the air are fully mixed, and coking is avoided.
Static mixer 7 can also be the corrugated plate static mixer, and this simple structure, the processing cost is low, is applicable to the comparatively pure operating mode of raw materials gas. According to the concrete physical properties of the raw material gas, a plurality of groups of corrugated plates with opposite bending directions are combined for use, and the flow directions of the raw material gas and the air are repeatedly changed, so that the raw material gas and the air are fully mixed.
The mixed gas equally flows into each reaction tube through the gas distributor 6, and reacts through the catalyst bed layer in the tube, and the product generated by the reaction is collected by the lower tube box of the reactor and flows into the next working section; the heat is released in the reaction process, and the reaction heat is transferred to the molten salt from the wall of the reaction tube. Molten salt removes reaction heat from the reactor by circulation, which can produce large amounts of saturated steam and superheated steam.
The invention provides power for molten salt flowing circulation through two molten salt pumps, wherein a part of molten salt is pumped into a lower molten salt loop of the reactor through a first molten salt pump 4a and a second molten salt pump 4b, and flows through a multistage flow equalizer 5 arranged in the loop to enable the molten salt to uniformly flow outside each reaction tube, take away reaction heat, and then flows into an upper loop to return to the molten salt pump, so as to form molten salt main circulation.
The multistage flow equalizer 5 is a series of special-shaped partition plates with different shapes and is arranged in a molten salt loop of the reactor. The cylindrical screen plates arranged in the reactors corresponding to the upper loop and the lower loop also play the role of the flow equalizer. The fused salt ring channel is positioned at the upper end part and the lower end part of the shell-pass cylinder of the reactor and used for radially distributing, entering, collecting and flowing out the fused salt. The diameter of the loop is about 8000-. In order to ensure that the flow of the molten salt in the loop is uniform, the loop is divided into two areas according to the physical property and the flow rule of the high-temperature molten salt: and the pump opening area is positioned near the molten salt pump, and the annular direction of the pump opening area is perpendicular to the central area of the molten salt pump. The Y-shaped partition plate and the double C-shaped partition plate are arranged in the pump port area, so that the flowing direction of the fused salt is changed, the vertical impact of the fused salt on the shell pass cylinder is avoided, the flowing stagnation point is eliminated, and the pressure of a fused salt flow field in the area is stable. The central area of the loop is farthest from the molten salt pump, the molten salt flows to the position where the pressure is increased, the flow speed is slow, and two strands of molten salt in double-pump circulation meet. By arranging the Z-shaped partition plate and the linear partition plate, the problem that two strands of molten salt flow oppositely to cause power loss is avoided; and two strands of fused salt are mixed in a cross way in the shell, so that the effect of uniform flow is achieved. The cylinder screen plates are respectively arranged in the cylinder bodies corresponding to the upper and lower circular channels, and before the fused salt enters and flows out of the tube bundle, the fused salt needs to flow through the small holes of the screen plates, so that the flow speed and the pressure of the fused salt are further stabilized, the flow dead zone in the flow field is eliminated, and the heat exchange efficiency is improved.
The balance valve 8 is used for adjusting the flow difference caused by different partitions of the loop and further homogenizing a molten salt flow field.
The other part of fused salt is adjusted through the governing valve 3 and is got into the flow of fused salt cooler 2, carries out the heat transfer cooling back through fused salt cooler 2, gets into the last pipeline of reactor, flows into the fused salt pump after mixing with the hot molten salt to reach the continuous heat transfer purpose of fused salt in the system, form another circulation of fused salt. The boiler water is heated by a molten salt cooler to generate saturated steam, and the saturated steam is heated by a steam superheater 9 to generate superheated steam.
The electric heater 10 is used for maintaining a certain temperature of the molten salt when the system is started and stopped, and can be closed when the system normally operates.
The invention is also suitable for the downward-in and upward-out mode in the gas flowing direction.
The invention is not limited to the examples, and any equivalent changes to the technical solution of the invention by a person skilled in the art after reading the description of the invention are covered by the claims of the invention.
Claims (10)
1. Benzoic anhydride reaction unit of 8 ten thousand tons of annual productions, its characterized in that:
the reactor main body (1) of the reaction device comprises an upper end socket channel, a reaction tube bundle and a lower end socket channel; the reaction tube bundle is provided with reaction tubes, the outer wall of the reaction tube bundle is provided with an upper loop and a lower loop which are molten salt loops, and the wall of the reactor corresponding to the upper loop and the lower loop is provided with holes and a cylindrical screen plate;
the two ends of the reactor are provided with a gas inlet and a gas outlet, and the gas inlet is provided with a gas distributor (6) and a static mixer (7);
two groups of fused salt inlets and outlets are arranged on the upper loop and the lower loop, and two fused salt pipelines and two groups of fused salt pumps are arranged.
2. The phthalic anhydride reaction apparatus of claim 1, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and is characterized in that:
at least 25000 reaction tubes in the reaction tube bundle are arranged, the outer diameter is 30mm, the wall thickness is 2.5mm, and the length is 4000 mm.
3. The phthalic anhydride reaction apparatus of claim 2, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and is characterized in that:
the diameter of the upper ring track and the lower ring track is 8000-9000mm, and the width is 600-700 mm.
4. The phthalic anhydride reaction apparatus of claim 3, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and is characterized in that:
and another molten salt circulating pipeline is arranged between the upper ring channel and the lower ring channel and comprises a molten salt regulating valve (3), a molten salt cooler (2) and a molten salt balance valve (8).
5. The phthalic anhydride reaction apparatus of claim 4, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and the reaction apparatus further comprises:
the reaction device also comprises a steam superheater (9) which is hung outside the molten salt loop.
6. The phthalic anhydride reaction apparatus of claim 5, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and the reaction apparatus further comprises:
the reaction device also comprises an electric heater (10) which is hung outside the molten salt loop.
7. The phthalic anhydride reaction apparatus of claim 6, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and the reaction apparatus further comprises:
and a multistage flow equalizer (5) is arranged in the upper loop and the lower loop.
8. The phthalic anhydride reaction apparatus of claim 7, wherein the reaction apparatus produces 8 million tons/year of phthalic anhydride, and further comprises:
the area in the loop close to the molten salt pump is a pump port area, and the flow equalizer in the pump port area is a Y-shaped clapboard or a double-C-shaped clapboard;
the area far away from the molten salt pump in the loop is a loop central area, and the flow equalizer in the loop central area is a Z-shaped partition plate or a linear partition plate.
9. The phthalic anhydride reaction apparatus of claim 8, wherein:
the static mixer (7) is a paddle plate type static mixer and comprises a plurality of coaxial cylinders, and paddles arranged in the circumferential direction are welded among the cylinders.
10. The phthalic anhydride reaction apparatus of claim 8, wherein:
the static mixer (7) is a corrugated plate type static mixer and comprises a plurality of bent thin plates which are connected in a welding way.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110056348.2A CN112588210A (en) | 2021-01-15 | 2021-01-15 | Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110056348.2A CN112588210A (en) | 2021-01-15 | 2021-01-15 | Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112588210A true CN112588210A (en) | 2021-04-02 |
Family
ID=75207290
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110056348.2A Pending CN112588210A (en) | 2021-01-15 | 2021-01-15 | Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112588210A (en) |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2511681Y (en) * | 2001-11-05 | 2002-09-18 | 田原宇 | Internal recycling static mixed dimethyl ehter fluidized-bed reactor |
| CN1817435A (en) * | 2005-01-14 | 2006-08-16 | 曼德韦有限公司 | Multi-tube reactor for carrying exothermic or endothermic gas phase reaction |
| CN201008784Y (en) * | 2006-12-27 | 2008-01-23 | 西安航天华威化工生物工程有限公司 | Shell pass multi-cavity type multi-layer bed fixed bed reactor |
| CN201055770Y (en) * | 2007-03-15 | 2008-05-07 | 山东宏信化工股份有限公司 | Benzoic anhydride reactor |
| CN201087180Y (en) * | 2007-05-15 | 2008-07-16 | 西安航天华威化工生物工程有限公司 | Fixed bed reactor group for producing benzoic anhydride by ortho-xylene with yearly capacity of 50 thousand ton |
| CN201815298U (en) * | 2010-08-23 | 2011-05-04 | 中国石油化工股份有限公司 | Reactor for preparing ethylene by dehydrating ethanol |
| DE102010014642A1 (en) * | 2010-04-12 | 2011-10-13 | Man Diesel & Turbo Se | Device for tempering tube bundle reactor for catalytic reactions by tempering gas, comprises a gas supply, a heating device and conveying device for the gas, an elastic intermediate piece for connecting a heat carrier-inlet and/or -outlet |
| CN204933425U (en) * | 2015-09-01 | 2016-01-06 | 云南大为恒远化工有限公司 | A kind of calandria type fixed bed reactor of benzene oxidatoin cis-butenedioic anhydride |
| CN205007953U (en) * | 2015-08-24 | 2016-02-03 | 安徽瑞邦生物科技有限公司 | A reaction unit for preparing vitamin B3 |
| CN105565273A (en) * | 2014-11-11 | 2016-05-11 | 上海氯碱化工股份有限公司 | Method for preparing chlorine by taking hydrogen chloride as raw material |
| CN106281727A (en) * | 2016-09-14 | 2017-01-04 | 浙江工业大学 | A kind of New Ester exchange reaction device |
| CN107243300A (en) * | 2017-05-17 | 2017-10-13 | 山东新和成氨基酸有限公司 | A kind of preparation facilities of cyanalcohol and preparation method thereof |
| CN211463090U (en) * | 2019-11-08 | 2020-09-11 | 西安航天华威化工生物工程有限公司 | Methyl mercaptan reaction system |
-
2021
- 2021-01-15 CN CN202110056348.2A patent/CN112588210A/en active Pending
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2511681Y (en) * | 2001-11-05 | 2002-09-18 | 田原宇 | Internal recycling static mixed dimethyl ehter fluidized-bed reactor |
| CN1817435A (en) * | 2005-01-14 | 2006-08-16 | 曼德韦有限公司 | Multi-tube reactor for carrying exothermic or endothermic gas phase reaction |
| CN201008784Y (en) * | 2006-12-27 | 2008-01-23 | 西安航天华威化工生物工程有限公司 | Shell pass multi-cavity type multi-layer bed fixed bed reactor |
| CN201055770Y (en) * | 2007-03-15 | 2008-05-07 | 山东宏信化工股份有限公司 | Benzoic anhydride reactor |
| CN201087180Y (en) * | 2007-05-15 | 2008-07-16 | 西安航天华威化工生物工程有限公司 | Fixed bed reactor group for producing benzoic anhydride by ortho-xylene with yearly capacity of 50 thousand ton |
| DE102010014642A1 (en) * | 2010-04-12 | 2011-10-13 | Man Diesel & Turbo Se | Device for tempering tube bundle reactor for catalytic reactions by tempering gas, comprises a gas supply, a heating device and conveying device for the gas, an elastic intermediate piece for connecting a heat carrier-inlet and/or -outlet |
| CN201815298U (en) * | 2010-08-23 | 2011-05-04 | 中国石油化工股份有限公司 | Reactor for preparing ethylene by dehydrating ethanol |
| CN105565273A (en) * | 2014-11-11 | 2016-05-11 | 上海氯碱化工股份有限公司 | Method for preparing chlorine by taking hydrogen chloride as raw material |
| CN205007953U (en) * | 2015-08-24 | 2016-02-03 | 安徽瑞邦生物科技有限公司 | A reaction unit for preparing vitamin B3 |
| CN204933425U (en) * | 2015-09-01 | 2016-01-06 | 云南大为恒远化工有限公司 | A kind of calandria type fixed bed reactor of benzene oxidatoin cis-butenedioic anhydride |
| CN106281727A (en) * | 2016-09-14 | 2017-01-04 | 浙江工业大学 | A kind of New Ester exchange reaction device |
| CN107243300A (en) * | 2017-05-17 | 2017-10-13 | 山东新和成氨基酸有限公司 | A kind of preparation facilities of cyanalcohol and preparation method thereof |
| CN211463090U (en) * | 2019-11-08 | 2020-09-11 | 西安航天华威化工生物工程有限公司 | Methyl mercaptan reaction system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN207102558U (en) | A kind of modularization temperature control reactor | |
| CN105032305B (en) | A kind of new radial direction plate-type reactor | |
| CN103240036B (en) | A kind of heat transfer reactor of Anti-temperature difference stress and combinations thereof device and application | |
| CN108892600B (en) | Method for continuously preparing 1-bromobutane | |
| CN105536654B (en) | A kind of large-scale axial multistage mixed heat transfer formula butylene oxidation-dehydrogenation reactor | |
| CN106643227B (en) | A kind of mixing deflector type reboiler | |
| CN108654534B (en) | Double-coil energy-saving efficient reaction kettle | |
| CN114405413B (en) | Reaction device for producing maleic anhydride by n-butane method | |
| CN108671865B (en) | Double-coil energy-saving efficient reaction kettle adopting jacket for exhausting | |
| CN112588210A (en) | Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year | |
| CN202876771U (en) | Industrialized plate type reactor for preparing glycol by oxalate hydrogenation or alcohol by ester hydrogenation | |
| CN218189677U (en) | Reaction device for synthesizing N-methyl pyrrolidone | |
| CN219984693U (en) | String pipe reactor with multi-head cyclone plates | |
| CN209530880U (en) | A kind of multi-thread sequentially reaction system | |
| CN205182690U (en) | Shell and tube heat exchanger and ft synthesis thick liquid attitude bed reactor | |
| CN205886831U (en) | Gather methoxy dimethyl ether synthesis fixed bed reactor | |
| CN205235936U (en) | Modular fixed bed reactor reaches device by its formation | |
| CN109966998B (en) | Tubular reactor | |
| CN202387465U (en) | Large adipic acid reactor | |
| CN205886832U (en) | It is listed as reactor to gather methoxy dimethyl ether synthesis | |
| CN201815298U (en) | Reactor for preparing ethylene by dehydrating ethanol | |
| CN215464455U (en) | Annular continuous nitration reaction device | |
| CN216440591U (en) | Special microchannel reaction device for toluene nitration | |
| CN209810134U (en) | Sectional temperature control reaction device | |
| CN210036376U (en) | Novel combined heat exchange device |
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 | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20210402 |