CN116041291A - Production process for preparing succinic anhydride by maleic anhydride hydrogenation - Google Patents
Production process for preparing succinic anhydride by maleic anhydride hydrogenation Download PDFInfo
- Publication number
- CN116041291A CN116041291A CN202111261156.1A CN202111261156A CN116041291A CN 116041291 A CN116041291 A CN 116041291A CN 202111261156 A CN202111261156 A CN 202111261156A CN 116041291 A CN116041291 A CN 116041291A
- Authority
- CN
- China
- Prior art keywords
- maleic anhydride
- reaction
- hydrogenation
- inner cylinder
- production process
- 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.)
- Granted
Links
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 110
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 title claims abstract description 109
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 46
- FALRKNHUBBKYCC-UHFFFAOYSA-N 2-(chloromethyl)pyridine-3-carbonitrile Chemical compound ClCC1=NC=CC=C1C#N FALRKNHUBBKYCC-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 229940014800 succinic anhydride Drugs 0.000 title claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 125
- 239000000463 material Substances 0.000 claims abstract description 76
- 239000001257 hydrogen Substances 0.000 claims abstract description 52
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 52
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 238000002156 mixing Methods 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 30
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000007791 liquid phase Substances 0.000 claims abstract description 16
- 238000005194 fractionation Methods 0.000 claims abstract description 3
- 239000002994 raw material Substances 0.000 claims description 44
- YEJRWHAVMIAJKC-UHFFFAOYSA-N 4-Butyrolactone Chemical compound O=C1CCCO1 YEJRWHAVMIAJKC-UHFFFAOYSA-N 0.000 claims description 36
- 150000002431 hydrogen Chemical class 0.000 claims description 30
- 239000003054 catalyst Substances 0.000 claims description 27
- 239000002904 solvent Substances 0.000 claims description 20
- 239000000047 product Substances 0.000 claims description 14
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims description 12
- 238000007789 sealing Methods 0.000 claims description 8
- 239000012263 liquid product Substances 0.000 claims description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 6
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 238000000605 extraction Methods 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000006185 dispersion Substances 0.000 claims description 5
- 239000007858 starting material Substances 0.000 claims description 5
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 4
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims description 4
- 239000000919 ceramic Substances 0.000 claims description 4
- 239000000084 colloidal system Substances 0.000 claims description 4
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 claims description 4
- 238000010907 mechanical stirring Methods 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 4
- 230000003068 static effect Effects 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- XNWFRZJHXBZDAG-UHFFFAOYSA-N 2-METHOXYETHANOL Chemical compound COCCO XNWFRZJHXBZDAG-UHFFFAOYSA-N 0.000 claims description 2
- DKMROQRQHGEIOW-UHFFFAOYSA-N Diethyl succinate Chemical compound CCOC(=O)CCC(=O)OCC DKMROQRQHGEIOW-UHFFFAOYSA-N 0.000 claims description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 2
- 229910010413 TiO 2 Inorganic materials 0.000 claims description 2
- 241000219793 Trifolium Species 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 claims description 2
- 239000008096 xylene Substances 0.000 claims description 2
- 238000000265 homogenisation Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 19
- 239000007795 chemical reaction product Substances 0.000 description 11
- 238000007086 side reaction Methods 0.000 description 8
- KDYFGRWQOYBRFD-UHFFFAOYSA-N succinic acid Chemical compound OC(=O)CCC(O)=O KDYFGRWQOYBRFD-UHFFFAOYSA-N 0.000 description 8
- 239000007789 gas Substances 0.000 description 5
- 239000012295 chemical reaction liquid Substances 0.000 description 4
- 239000001384 succinic acid Substances 0.000 description 4
- 239000004631 polybutylene succinate Substances 0.000 description 3
- 229920002961 polybutylene succinate Polymers 0.000 description 3
- 229920000704 biodegradable plastic Polymers 0.000 description 2
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 208000012839 conversion disease Diseases 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009827 uniform distribution Methods 0.000 description 2
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000009472 formulation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- -1 polybutylene succinate Polymers 0.000 description 1
- 230000000379 polymerizing effect Effects 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- 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
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D307/56—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D307/60—Two oxygen atoms, e.g. succinic anhydride
-
- 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
- B01J8/04—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 passing successively through two or more beds
- B01J8/0446—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 passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—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 passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0465—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 passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being concentric
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a production process for preparing succinic anhydride by maleic anhydride hydrogenation, which comprises the following steps: (1) Firstly, mixing maleic anhydride solution and hydrogen to form a mixed material; (2) The liquid phase material enters the inner cylinders of two sleeve reactors with the same structure in two ways to carry out up-flow hydrogenation reaction, and two reaction effluents flow out from the top of the inner cylinder and respectively enter the annular channels of the sleeve reactors of the other side after heat is taken out to carry out down-flow hydrogenation reaction; (3) And (3) after the hydrogenation reaction effluent enters a gas-liquid separation, part of the hydrogenation reaction effluent is recycled to the maleic anhydride hydrogenation reaction zone, and the other part of the hydrogenation reaction effluent is subjected to fractionation operation to obtain a succinic anhydride product. The invention realizes the homogenization of heat in the whole reaction process by the flowing mode of the reaction materials and the matching of sleeve reactors, effectively solves the problems of concentrated heat release and easy generation of local hot spots in the maleic anhydride hydrogenation process, maximally utilizes and recovers the reaction heat, has more uniform and controllable temperature and ensures higher conversion rate and selectivity in the maleic anhydride hydrogenation process.
Description
Technical Field
The invention belongs to the technical field of degradable material production, and particularly relates to a production process for preparing succinic anhydride by hydrogenating maleic anhydride.
Background
Succinic acid is an important chemical raw material, and is listed as one of 12 most valuable platform compounds in the future by the U.S. department of energy, and is widely applied to the fields of chemical industry, materials, medicines and foods. Succinic acid is an important monomer raw material of PBS series degradable materials, PBS (polybutylene succinate) can be obtained by polymerizing succinic acid and 1, 4-butanediol, and the biodegradable plastic is excellent in performance, is one of the biodegradable plastics which realize industrialization and are widely applied at present, and is an important support for implementing plastic forbidden command in China.
At present, the production method of succinic anhydride is mainly divided into a succinic anhydride dehydration method, a biological fermentation method and a maleic anhydride catalytic hydrogenation method, wherein the maleic anhydride catalytic hydrogenation method is the method with the highest conversion rate of succinic anhydride and the highest product, and is most suitable for large-scale industrialization, but the succinic anhydride produced by maleic anhydride hydrogenation is the strong exothermic reaction (delta H=128 kJ/mol), and the reaction heat cannot be timely removed by adopting conventional trickle bed hydrogenation and conventional liquid phase hydrogenation, so that the temperature of the reaction process cannot be controlled, the problems of local hot spot of a catalyst bed layer, serious side reaction and the like are caused, and the safety, the conversion rate and the selectivity of the reaction process cannot be controlled.
CN103570650a proposes a technological process for continuously producing succinic anhydride and co-producing succinic acid by maleic anhydride hydrogenation, the method adopts a two-stage hydrogenation reactor, wherein the first-stage hydrogenation reactor is a fixed bed reactor for feeding hydrogen and reaction liquid downwards and discharging upwards, and the second-stage hydrogenation reactor is a trickle bed reactor for feeding hydrogen and reaction liquid upwards and discharging downwards, and an external circulation heat removal mode is adopted to remove reaction heat, so as to control the average operation temperature of the whole reactor and equalize the temperature in the reactor. In the method, a primary reactor adopts a parallel flow upward flow mode of hydrogen and reaction liquid, and based on the specificity of large heat release of maleic anhydride hydrogenation reaction, the conventional technology cannot ensure uniform material mixing and uniform distribution, and cannot ensure uniform reaction and solve the problem of local hot spots; the secondary reactor adopts a parallel-flow downward trickle bed reactor flow mode, so that the timely taking away of the reaction heat can not be ensured, and the problem of local hot spots can be solved.
CN 105801536B proposes a method for preparing succinic anhydride by liquid phase selective hydrogenation of maleic anhydride, the liquid phase hydrogenation reaction adopts a two-stage low-temperature low-pressure reaction process method to prepare succinic anhydride, two reactors, namely a first-stage reactor and a second-stage reactor, are adopted, and the first-stage reactor and the second-stage reactor are used in series; the maleic anhydride, the solvent and the hydrogen enter a first-stage reactor to carry out partial catalytic selective hydrogenation, after the reaction, the residual maleic anhydride, the generated succinic anhydride and the solvent mixed liquid material enter a second-stage reactor to carry out complete catalytic selective hydrogenation, and the succinic anhydride product is obtained after gas-liquid separation and rectification of the product of the second-stage reactor. In the method, the two-stage reactor adopts a liquid-phase hydrogenation method of hydrogen and reaction liquid, and based on the specificity of large heat release of maleic anhydride hydrogenation reaction, the conventional liquid-phase hydrogenation mixing and reaction technology cannot ensure uniform material mixing and uniform distribution, and cannot ensure uniform reaction and solve the problem of local hot spots.
Disclosure of Invention
Aiming at the defects of the prior art, the invention discloses a production process for preparing succinic anhydride by hydrogenating maleic anhydride. The invention realizes the homogenization of heat in the whole reaction process by the flowing mode of the reaction materials and the matching of sleeve reactors, effectively solves the problems of concentrated heat release and easy generation of local hot spots in the maleic anhydride hydrogenation process, maximally utilizes and recovers the reaction heat, simultaneously ensures more uniform and controllable temperature and ensures higher conversion rate and selectivity in the maleic anhydride hydrogenation process.
The invention relates to a production process for preparing succinic anhydride by maleic anhydride hydrogenation, which comprises the following steps: the production process for preparing succinic anhydride by hydrogenating maleic anhydride is characterized by comprising the following steps: (1) In the reaction raw material mixing zone, maleic anhydride solution and hydrogen are mixed to form a mixed material; (2) In the maleic anhydride hydrogenation reaction zone, the liquid phase material obtained in the step (1) respectively enters an inner cylinder of a sleeve-type reactor in two paths for up-flow hydrogenation reaction, two reaction effluents flow out from the top of the inner cylinder, and after heat extraction, the two reaction effluents respectively enter an annular channel between an outer cylinder and an inner cylinder of the sleeve-type reactor of the other side for down-flow hydrogenation reaction; (3) The hydrogenation effluent of the annular channel enters a gas-liquid separation zone, part of the hydrogenation effluent is recycled to the maleic anhydride hydrogenation reaction zone after gas-liquid separation, and the other part of the hydrogenation effluent is subjected to fractionation operation to obtain a succinic anhydride product.
In the production process, the reaction raw material mixing area is used for uniformly mixing maleic anhydride solution and hydrogen to obtain a mixture material with hydrogen as a disperse phase and maleic anhydride solution as a continuous phase, the dispersion size of the hydrogen is generally 100 nm-1000 microns, preferably 50-600 microns, and the reaction raw material mixing area is internally provided with gas-liquid mixing equipment which is one or a plurality of combinations of a static mixer, a gas dissolving pump, mechanical stirring equipment, a colloid mill, a micro-pore plate nano/micro hydrogen dispersion component, a micro-bubble generator, a ceramic membrane nano/micro hydrogen dispersion component, a jet mixer, a micro-channel mixer and the like.
In the production process, the maleic anhydride solution is selected from any one or more of benzene, toluene, xylene, acetone, tetrahydrofuran, gamma-butyrolactone, first-class acetone, cyclohexanone, ethyl acetate, diethyl succinate or ethylene glycol monomethyl ether; the concentration of maleic anhydride solution is generally 0.03 to 0.3g/mL, preferably 0.05 to 0.15g/mL. The maleic anhydride solution may be prepared in advance, or maleic anhydride, solvent and hydrogen may be mixed in the reaction raw material mixing zone.
In the production process of the invention, the proportion of the two paths of liquid phase materials in the step (2) is 1: 90-90: 1, preferably 1:1.
in the production process, the two sleeve reactors have the same structure, preferably the same size, and comprise an inner cylinder and an outer cylinder, wherein the inner cylinder is axially arranged in the outer cylinder, an annular channel is arranged between the inner cylinder and the outer cylinder, and the inner cylinder is not communicated with the annular channel; the bottom of the inner cylinder is provided with a raw material inlet, and the top of the inner cylinder is provided with a material outlet; the top of the annular channel is provided with a material inlet, and the bottom of the annular channel is provided with a material outlet; the material outlets at the tops of the inner cylinders of the two sleeve-type reactors are communicated with the material inlets at the tops of the annular channels through pipelines; the material inlet pipeline of the inner cylinder is communicated with the feeding pipeline, and the material outlet pipeline of the annular channel is communicated with the discharging pipeline; the top of the outer cylinder is an upper sealing head, and the bottom of the outer cylinder is a lower sealing head; the top and the bottom of the inner cylinder wall are respectively fixedly welded and sealed with the upper seal head and the lower seal head. The height-diameter ratio of the inner cylinder is 1-15, preferably 4-10; the height-diameter ratio of the outer cylinder is 1-5, preferably 1.0-3.0.
In the production process of the invention, maleic anhydride hydrogenation catalysts are filled in the inner cylinder and the annular channel, which can be the same or different, and are adjusted according to the reaction requirement, preferably a supported nickel-based catalyst, wherein the catalyst carrier can be SiO 2 、Al 2 O 3 、SiO 2 - Al 2 O 3 、TiO 2 One or more of activated carbon or molecular sieves, and the like; the catalyst may be in the form of one of sphere, bar, clover, toothed sphere, etc., preferably a sphere or toothed sphere catalyst. Typically 1 to 3 catalyst beds are provided.
In the production process of the invention, the hydrogen (Nm) in the inner cylinder 3 And/h) with fresh maleic anhydride solution starting material (m) 3 The ratio of the volume flows of/h) is 5:1 to 80:1, preferably 10: 1-30: 1.
in the production process of the invention, the upflow hydrogenation reaction conditions are as follows: the reaction temperature is 40-140 ℃, preferably 50-120 ℃; the reaction pressure is 0.5-10.0 MPa, preferably 1-5.0 MPa; the liquid hourly space velocity is 0.5 to 15.0h -1 Preferably 3.0 to 8.0h -1 The method comprises the steps of carrying out a first treatment on the surface of the The height-diameter ratio of the inner cylinder is 1-15, preferably 4-10.
In the production process of the present invention, the hydrogen (Nm) in the annular channel 3 And/h) with fresh maleic anhydride solution starting material (m) 3 The ratio of the volume flows per h) is generally 1: 1-20: 1, preferably 2:1 to 15:1. the hydrogen of the annular channel can be replenished through a replenishing hydrogen line.
In the production process of the invention, the downflow hydrogenation reaction conditions are as follows: the reaction temperature is 40-150 ℃, preferably 50-100 ℃; the reaction pressure is 0.5-10.0 MPa, preferably 1-5.0 MPa; the liquid hourly space velocity is 0.1 to 8.0h -1 Preferably 0.5 to 3.0h -1 。
In the production process of the invention, the hydrogen gas generally adopts hydrogen gas with purity of more than 90% by volume, preferably adopts pure hydrogen with purity of 99.9% by volume.
In the production process of the invention, the heat extraction process is generally realized by arranging heat extraction equipment, such as a heat exchanger, an air cooler or a water cooler, and the like, so that the materials entering the annular space reach the required reaction temperature.
In the production process, the gas-liquid separation zone is used for gas-liquid separation of hydrogenation reaction effluent of the annular channel, and part of separated liquid product is recycled to the inner cylinder and/or the annular channel, and part of materials are fractionated; further, the liquid product recycled to the inner drum is 5wt% to 90wt% of the fresh feed, preferably 10wt% to 50wt%; the liquid product recycled to the annular channel represents 0 to 80wt%, preferably 0 to 40wt% of the fresh feed.
In the production process of the invention, the maleic anhydride conversion rate of the inner cylinder is generally 50-95%, preferably 55-85%.
The invention also provides a production system for preparing succinic anhydride by hydrogenating maleic anhydride, which comprises a reaction raw material mixing area, a maleic anhydride hydrogenation reaction area and a gas-liquid separation area;
the reaction raw material mixing zone is used for mixing maleic anhydride solution and hydrogen, and a gas-liquid mixing device is arranged in the reaction raw material mixing zone and is selected from one or a plurality of combinations of a static mixer, a dissolved air pump, a mechanical stirring device, a colloid mill, a micro-pore plate nano/micro-hydrogen dispersing component, a micro-bubble generator, a ceramic membrane nano/micro-hydrogen dispersing component, a jet mixer, a micro-channel mixer and the like;
the maleic anhydride hydrogenation zone is used for maleic anhydride liquid phase hydrogenation reaction, a plurality of groups of hydrogenation reaction units are arranged in the maleic anhydride hydrogenation zone, and each unit comprises two sleeve-type reactors with the same structure; the sleeve-type reactor comprises an inner cylinder and an outer cylinder, wherein the inner cylinder is axially arranged in the outer cylinder, an annular channel is arranged in the area between the inner cylinder and the outer cylinder, and the inner cylinder is not communicated with the annular channel; the bottom of the inner cylinder is provided with a raw material inlet, and the top of the inner cylinder is provided with a material outlet; the top of the annular channel is provided with a material inlet, and the bottom of the annular channel is provided with a material outlet; the material outlets at the tops of the inner cylinders of the two sleeve-type reactors are communicated with the material inlets at the tops of the annular channels through pipelines; the material inlet pipeline of the inner cylinder is communicated with the feeding pipeline, and the material outlet pipeline of the annular channel is communicated with the discharging pipeline; the top of the outer cylinder is an upper sealing head, and the bottom of the outer cylinder is a lower sealing head; the top and the bottom of the inner cylinder wall are respectively fixedly welded and sealed with the upper seal head and the lower seal head. The height-diameter ratio of the inner cylinder is 1-15, preferably 4-10; the height-diameter ratio of the outer cylinder is 1-5, preferably 1.0-3.0.
The gas-liquid separation zone is used for gas-liquid separation of hydrogenation products, and is generally completed through a gas-liquid separation tank, gas is separated from the top of the separation tank, and liquid-phase products are obtained from the bottom of the separation tank.
The invention adopts two sleeve reactors with the same structure, wherein the inner cylinder adopts an up-flow type, and the annular channel is a down-flow type; materials enter the inner cylinders of the two reactors respectively to complete partial hydrogenation reaction, and then enter the annular channel to continue hydrogenation reaction; the initial stage of the maleic anhydride hydrogenation reaction is carried out in the inner cylinder based on a micro-expansion state of the catalyst in the upflow reaction process, so that mass transfer and heat transfer of materials are facilitated during the initial stage of the maleic anhydride hydrogenation reaction, local hot spots and coking and hardening of the catalyst are prevented, the maleic anhydride hydrogenation reaction is carried out in the inner cylinder under the conditions of high concentration, high airspeed and high aspect ratio (relative to an annular channel), the residence time of the maleic anhydride is reduced, the generation of side reaction and local hot spots can be reduced to the greatest extent, the flow velocity of the materials in the reactor is high during the high aspect ratio, the turbulence of the materials is increased, the diffusion and heat transfer of the materials are facilitated, in addition, the upflow reaction flow state easily enables the materials to be axially backmixed, the materials are in a state close to plug flow, the axial backmixing is reduced, the conversion rate is improved, the side reaction is reduced as much as possible, and the inner cylinder is subjected to 50% -95% reaction conversion rate under the rapid reaction condition, and the reaction conversion rate is preferably 55% -85%; the reaction materials entering the annular channel are downflow reaction processes, because side reactions are easier to occur in the later period of maleic anhydride hydrogenation reaction and are difficult to control by conventional means, a small amount of unconverted materials are left in the reaction materials, a small height-diameter ratio, low airspeed and downflow reaction form is adopted, so that on one hand, the high conversion rate can be kept, the reaction materials flow to be the same as the gravity direction, the material backmixing is reduced, the problem that local residence time is overlong, the local hot spot and side reactions in the later period of reaction are effectively controlled and are difficult to control is solved, on the other hand, the reaction materials can be subjected to efficient heat exchange with the inner barrel materials of the same hydrogenation reactor, the materials of the inner barrel and the annular space flow in a countercurrent manner, the materials of the inner barrel are fresh reaction materials, the temperature of the annular space is gradually increased from bottom to top, the temperature of the annular space is gradually increased from top to bottom, the heat conduction is realized through the barrel wall of the inner barrel, and meanwhile, the annular space with the small height-diameter ratio is wrapped in the inner barrel with the large height-diameter ratio, the reaction heat of the whole reactor is more favorably balanced, the temperature of the inner barrel and the annular channel is more uniform, so that the reaction is more uniform and controllable. After the reaction materials pass through the annular channel, the maleic anhydride conversion rate is generally close to 100%, and the selectivity is more than or equal to 98%.
Drawings
FIG. 1 is a schematic diagram of a process for producing succinic anhydride by hydrogenating maleic anhydride.
The production system for preparing succinic anhydride by hydrogenating maleic anhydride comprises a reaction raw material mixing area, a maleic anhydride hydrogenation reaction area and a gas-liquid separation area; 1 is maleic anhydride solution, 2 is hydrogen, 3 is mixer I,4 is liquid phase reaction feed, 5 is inner tube I reaction feed, 6 is inner tube II reaction feed, 7 is sleeve reactor I, 8 is inner tube I, 9 is inner tube I catalyst, 10 is annular channel I catalyst, 11 is sleeve reactor II,12 is inner tube II,13 is inner tube II catalyst, 14 is annular channel II catalyst, 15 is inner tube I effluent, 16 is inner tube II effluent, 17 is make-up hydrogen I,18 is make-up hydrogen II,19 is mixer II,20 is mixer III,21 is annular channel I feed, 22 is annular channel II discharge, 23 is annular channel II feed, 24 is annular channel I discharge, 25 is maleic anhydride hydrogenation reaction product, 26 is gas-liquid separator, 27 is separated gas, 28 is separated liquid phase hydrogenation product, 29 is heat collector I,30 is heat collector II,31 is heat collector III.
Detailed Description
The invention will now be described in more detail with reference to the accompanying drawings and examples, which are not intended to limit the invention thereto.
Taking the attached figure 1 as an example, the invention relates to an application process of a production process for preparing succinic anhydride by hydrogenating maleic anhydride, which comprises the following steps: firstly, in a reaction raw material mixing zone, uniformly mixing maleic anhydride solution 1 and hydrogen 2 through a mixer I3, and then entering a maleic anhydride hydrogenation reaction zone; the reaction feed from the reaction raw material mixing zone is divided into two paths, one path enters an inner cylinder I of a sleeve-type reactor I7 from bottom to top to generate an up-flow hydrogenation reaction, an inner cylinder I effluent 15 of the sleeve-type reactor I7 is heated, then enters a mixer II 19 together with supplementary hydrogen to be uniformly mixed, then enters an annular channel II to generate hydrogenation reaction from top to bottom, and an annular channel II discharge 22 leaves and enters a gas-liquid separation zone; the other path enters an inner cylinder II from the bottom, an up-flow hydrogenation reaction occurs in the catalyst bed 13 from bottom to top, an inner cylinder II effluent 16 is heated and then enters a mixer III 20 together with supplementary hydrogen to be uniformly mixed, then enters an annular channel I, the hydrogenation reaction occurs from top to bottom, and the annular channel I of the sleeve-type reactor is discharged and enters a gas-liquid separation zone; the materials from the maleic anhydride hydrogenation reaction zone are heated and then enter a gas-liquid separator 26, the gas 27 after gas-liquid separation is led out of the reaction system, and the separated liquid product 28 can partially enter a subsequent separation unit and partially circulate back to the maleic anhydride hydrogenation reaction zone.
The method is applied to the production process of preparing succinic anhydride by hydrogenating maleic anhydride. Maleic anhydride starting material and gamma-butyrolactone solvent were commercially available, the specific properties are shown in tables 1 and 2, respectively, and the catalyst properties are shown in table 3.
TABLE 1 maleic anhydride raw material Properties
TABLE 2 solvent Properties of gamma butyrolactone
TABLE 3 physical and chemical indicators of catalyst
Comparative example 1
The conventional fixed bed hydrogenation process is adopted, and maleic anhydride is subjected to maleic anhydride hydrogenation reaction in the first reactor and the second reactor in sequence in a mode of connecting two up-flow hydrogenation reactors in series. Firstly, maleic anhydride raw materials are dissolved in gamma-butyrolactone solvent and uniformly mixed to prepare maleic anhydride solution, the maleic anhydride solution is regulated to the temperature of an inlet of a reactor and then mixed with hydrogen, the maleic anhydride solution enters from the bottom of an up-flow hydrogenation reactor, hydrogenation reaction is carried out through a catalyst bed layer from bottom to top, the obtained hydrogenation product enters from the bottom of a down-flow hydrogenation reactor after being regulated to be mixed with supplementary hydrogen, hydrogenation reaction is carried out through the catalyst bed layer from top to bottom, the maleic anhydride solution leaves the reactor after the hydrogenation reaction is completed, gas-liquid separation is carried out through a separator, and separated materials are partially circulated, and the other part of the material enters a separation unit.
The operating conditions of the first hydrogenation reactor were as follows:
the reaction temperature is 50-150 ℃;
the reaction pressure is 6.0-6.5 MPaG;
the height-diameter ratio of the reactor is as follows: 2.5
Volume space velocity: 2.0h -1
Maleic anhydride formulation concentration: 12g/mL
Hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 And/h) (the volume ratio of maleic anhydride dissolved in gamma-butyrolactone solvent) is 50:1, a step of;
the mass ratio of the recycle amount of the reaction product entering the primary reaction to the fresh raw materials: 35%;
the second hydrogenation reactor was operated as follows:
the reaction temperature is 50-150 ℃;
the reaction pressure is 6.0-6.5 MPaG;
volume space velocity: 1.0h -1 ；
The height-diameter ratio of the reactor is as follows: 2.5;
hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 And/h) (the volume ratio of maleic anhydride dissolved in the gamma-butyrolactone solvent) is 30:1, a step of;
the mass ratio of the recycle amount of the reaction product entering the secondary reaction to the fresh raw materials: 30%;
under the reaction conditions, maleic anhydride and gamma-butyrolactone solvents in table 1 and table 2 are taken as raw materials, and enter a first reactor and a second reactor to continuously carry out hydrogenation reaction to obtain a hydrogenation product, wherein the average total conversion rate is 98.0%, and the average total selectivity is 96.1%; when the average total conversion rate is more than or equal to 99.5%, the average total selectivity is 94.5%.
Example 1
By adopting the method of the invention, two identical sleeve reactors are arranged in the maleic anhydride hydrogenation reaction zone. Firstly, uniformly mixing a pre-prepared 15% maleic anhydride (gamma-butyrolactone solvent) solution and hydrogen to form a liquid phase material, then, dividing reaction feed into two equal paths, wherein one path enters an inner cylinder of a sleeve-type reactor from bottom to top, an up-flow hydrogenation reaction occurs in a catalyst bed layer, an inner cylinder effluent of the sleeve-type reactor and supplementary hydrogen are mixed and enter an annular channel of another sleeve-type reactor, hydrogenation reaction occurs through an annular channel catalyst from top to bottom, and a reaction product leaves and enters a gas-liquid separation region; the other path enters an inner cylinder of another sleeve-type reactor from bottom to top through the bottom, an up-flow hydrogenation reaction occurs in a catalyst bed layer, the effluent of the inner cylinder is mixed with supplementary hydrogen and then enters an annular channel of the other sleeve-type reactor, the hydrogenation reaction occurs in the catalyst bed layer from top to bottom, and a reaction product leaves and then enters a gas-liquid separation zone; the materials in the maleic anhydride hydrogenation reaction zone enter a gas-liquid separator for gas-liquid separation, the separated gas is led out of the reaction system, and the separated liquid part enters a subsequent separation unit to be recycled to the maleic anhydride hydrogenation reaction zone.
The inner barrel operating conditions of the two sleeve reactors were as follows:
the reaction temperature is 50-75 ℃;
the reaction pressure is 3.0-4.0 MPaG;
volume space velocity: 6.0h -1 ；
Height-to-diameter ratio of inner cylinder of reactor: 6.0;
hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 Volume ratio of (solution of maleic anhydride dissolved in gamma-butyrolactone solvent)Is 16:1, a step of;
the mass ratio of the circulation amount of the reaction product entering the inner cylinder to the fresh raw materials: 25%;
the operating conditions of the annular channels of the two sleeve reactors are as follows:
the reaction temperature is 50-65 ℃;
the reaction pressure is 3.0-4.0 MPaG;
volume space velocity: 2.5h -1
The height-diameter ratio of the reactor is as follows: 2.0;
hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 And/h) (solution of maleic anhydride in gamma-butyrolactone solvent) in a volume ratio of 12.5:1, a step of;
circulation amount of reaction product entering annular channel of sleeve-type reactor and mass ratio of fresh raw material: 15%:
under the reaction condition, taking maleic anhydride and gamma-butyrolactone solvents shown in table 1 and table 2 as raw materials, and entering a reaction system for hydrogenation reaction to obtain a hydrogenation product, wherein the average conversion rate of an inner cylinder of a sleeve-type reactor is 70.6%; when the total conversion rate of the sleeve type reactor is 98.0%, the total selectivity is 99.0-99.2%; when the average total conversion rate is 99.9%, the average total selectivity is 98.5-98.7%.
Example 2
The reaction system and method for hydrogenating maleic anhydride are the same as in example 1. The reaction conditions differ from the examples as follows:
the two sleeve reactor inner cylinders operate as follows:
the reaction temperature is 55-70 ℃;
the reaction pressure is 3.0-4.0 MPaG;
volume space velocity: 7.0h -1 ；
The height-diameter ratio of the reactor is as follows: 8.0;
hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 /h) (solution of maleic anhydride in gamma-butyrolactone solvent) in a volume ratio of 17.5:1, a step of;
the mass ratio of the circulation quantity of the reaction product entering the sleeve-type reactor inner cylinder to the fresh raw material: 30%;
the two sleeve reactor annular channels operate as follows:
the reaction temperature is 55-68;
the reaction pressure is 3.0-4.0 MPaG;
volume space velocity: 2.0h -1
Hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 And/h) (the volume ratio of maleic anhydride dissolved in the gamma-butyrolactone solvent) is 10:1, a step of;
circulation amount of reaction product entering annular channel of sleeve-type reactor and mass ratio of fresh raw material: 25%:
under the reaction condition, taking maleic anhydride and gamma-butyrolactone solvents shown in table 1 and table 2 as raw materials, and entering a reaction system for hydrogenation reaction to obtain a hydrogenation product, wherein the average conversion rate of an inner cylinder of a sleeve-type reactor is 77.2%; when the total conversion rate of the sleeve type reactor is 98.0%, the total selectivity is 99.2-99.5%; when the average total conversion rate of the sleeve type reactor is more than or equal to 99.9%, the average total selectivity is 98.7-98.9%.
Example 3
Maleic anhydride hydrogenation reaction system and method were the same as in example 1. The reaction conditions differ from the examples as follows:
the inner cylinders of the two sleeve reactors operate as follows:
the reaction temperature is 58-70 ℃;
the reaction pressure is 3.0-4.0 MPaG;
volume space velocity: 8.0h -1 ；
The height-diameter ratio of the reactor is as follows: 10.0;
hydrogen (Nm) 3 And/h) with fresh raw materials (m 3 And/h) (the volume ratio of maleic anhydride dissolved in the gamma-butyrolactone solvent) is 15:1, a step of;
the mass ratio of the circulation quantity of the reaction product entering the inner cylinders of the two sleeve-type reactors to the fresh raw materials: 35%;
the annular channels of the two sleeve reactors operate as follows:
the reaction temperature is 58-68;
the reaction pressure is 3.0-4.0 MPaG;
volume space velocity: 1.5h -1
Hydrogen (Nm) 3 /h) and NewFresh raw material (m) 3 And/h) (the volume ratio of maleic anhydride dissolved in the gamma-butyrolactone solvent) is 12:1, a step of;
circulation amount of reaction product entering annular channel of sleeve type reactor and mass ratio of fresh raw material: 30%:
under the reaction condition, taking maleic anhydride and gamma-butyrolactone solvents shown in table 1 and table 2 as raw materials, and entering a reaction system for hydrogenation reaction to obtain a hydrogenation product, wherein the average conversion rate of an inner cylinder of a sleeve-type reactor is 83.2%; when the total conversion rate of the sleeve type reactor is 98.0%, the total selectivity is 99.2-99.5%; when the average total conversion rate of the sleeve type reactor is more than or equal to 99.9%, the average total selectivity is 98.9-99.1%.
As can be seen from the effects of the embodiment and the comparative example, by adopting the production process, the reaction feed is in an upflow, high space velocity and large height-diameter ratio when the inner cylinders of the two reactors react, on one hand, the catalyst is in a micro-expansion state, which is beneficial to controlling the generation of local hot spots, and on the other hand, the materials in the reactors are in a state close to a plug flow by the reaction materials, so that the axial back mixing is reduced to the maximum extent, and the side reaction is reduced while the conversion rate is improved; the reaction feeding is in a downflow reaction mode when reacting in the annular channels of the two sleeve reactors, so that the problems of back mixing of materials, long local residence time and multiple side reactions are reduced. In addition, as can be seen from the reaction results of the embodiment, the temperature rise of the reactor, whether the reactor is an inner cylinder or an annular channel, is effectively controlled, and particularly, the later reaction period is arranged in the annular channel, so that the heat transfer and temperature equalization of materials are facilitated, the higher total conversion rate of maleic anhydride hydrogenation is ensured, and the side reaction of maleic anhydride hydrogenation can be effectively controlled.
Claims (19)
1. The production process for preparing succinic anhydride by hydrogenating maleic anhydride is characterized by comprising the following steps: (1) In the reaction raw material mixing zone, maleic anhydride solution and hydrogen are mixed to form a mixed material with hydrogen as a disperse phase and maleic anhydride solution as a continuous phase; (2) In the maleic anhydride hydrogenation reaction zone, the liquid phase material obtained in the step (1) enters the inner cylinders of the two sleeve reactors respectively in two paths for upflow hydrogenation reaction, and two reaction effluents flow out from the top of the inner cylinders and respectively enter annular channels between the outer cylinders and the inner cylinders of the sleeve reactors of the other side after heat extraction for downflow hydrogenation reaction; (3) The hydrogenation effluent of the annular channel enters a gas-liquid separation zone, part of the hydrogenation effluent is recycled to the maleic anhydride hydrogenation reaction zone after gas-liquid separation, and the other part of the hydrogenation effluent is subjected to fractionation operation to obtain a succinic anhydride product.
2. The production process according to claim 1, characterized in that: the reaction raw material mixing zone is used for uniformly mixing maleic anhydride solution and hydrogen to obtain a mixture material with hydrogen as a disperse phase and maleic anhydride solution as a continuous phase, wherein the disperse size of the hydrogen is 100 nm-1000 mu m, preferably 50-600 mu m.
3. The production process according to claim 1, characterized in that: the reaction raw material mixing zone is internally provided with gas-liquid mixing equipment, wherein the gas-liquid mixing equipment is one or more of a static mixer, a dissolved air pump, mechanical stirring equipment, a colloid mill, a micro-pore plate nano/micro-hydrogen dispersing component, a micro-bubble generator, a ceramic membrane nano/micro-hydrogen dispersing component, a jet mixer and a micro-channel mixer.
4. The production process according to claim 1, characterized in that: the maleic anhydride solution is prepared from one or more of benzene, toluene, xylene, acetone, tetrahydrofuran, gamma-butyrolactone, methyl-grade acetone, cyclohexanone, ethyl acetate, diethyl succinate or ethylene glycol monomethyl ether; the concentration of maleic anhydride solution is 0.03-0.3 g/mL.
5. The production process according to claim 1, characterized in that: maleic anhydride solution is prepared in advance or maleic anhydride, solvent and hydrogen are mixed in a reaction raw material mixing zone.
6. The production process according to claim 1, characterized in that: the ratio of the two paths of liquid phase materials in the step (2) is 1: 90-90: 1, preferably 10:1 to 1:10.
7. The production process according to claim 1, characterized in that: the two sleeve-type reactors have the same structure and comprise an inner cylinder and an outer cylinder, wherein the inner cylinder is axially arranged in the outer cylinder, an annular channel is arranged in the area between the inner cylinder and the outer cylinder, and the inner cylinder is not communicated with the annular channel; the bottom of the inner cylinder is provided with a raw material inlet, and the top of the inner cylinder is provided with a material outlet; the top of the annular channel is provided with a material inlet, and the bottom of the annular channel is provided with a material outlet; the material outlets at the tops of the inner cylinders of the two sleeve reactors are communicated with the material inlet at the top of the annular space II through pipelines; the material inlet pipeline of the inner cylinder is communicated with the feeding pipeline, and the material outlet pipeline of the annular channel is communicated with the discharging pipeline; the top of the outer cylinder is an upper sealing head, and the bottom of the outer cylinder is a lower sealing head; the top and the bottom of the inner cylinder wall are respectively fixedly welded and sealed with the upper seal head and the lower seal head.
8. The production process according to claim 1, characterized in that: the height-diameter ratio of the inner cylinder is 1-15, preferably 4-10; the height-diameter ratio of the outer cylinder is 1-5, preferably 1.0-3.0.
9. The production process according to claim 1, characterized in that: maleic anhydride hydrogenation catalyst, preferably supported nickel-based catalyst, is filled in the inner cylinder and the annular channel, wherein the catalyst carrier is SiO 2 、Al 2 O 3 、SiO 2 - Al 2 O 3 、TiO 2 One or more of activated carbon or molecular sieves; the catalyst is one of sphere, bar, clover and tooth sphere.
10. The production process according to claim 1, characterized in that: hydrogen (Nm) in the inner cylinder 3 And/h) with fresh maleic anhydride solution starting material (m) 3 The ratio of the volume flows of/h) is 5:1 to 50:1.
11. the production process according to claim 1, characterized in that: the upflow hydrogenation reaction conditions are as follows:the reaction temperature is 40-140 ℃, the reaction pressure is 0.5-10.0 MPa, and the liquid hourly space velocity is 0.5-15.0 h -1 。
12. The production process according to claim 1, characterized in that: hydrogen (Nm) in the annular channel 3 And/h) with fresh maleic anhydride solution starting material (m) 3 The ratio of the volume flows of/h) is 1: 1-20: 1.
13. the production process according to claim 1, characterized in that: the down-flow hydrogenation reaction conditions are as follows: the reaction temperature is 40-150 ℃, the reaction pressure is 0.5-10.0 MPa, and the liquid hourly space velocity is 0.1-8.0 h -1 。
14. The production process according to claim 1, characterized in that: the heat extraction process is realized by arranging heat extraction equipment, so that the materials entering the annular space reach the required reaction temperature.
15. The production process according to claim 1, characterized in that: the gas-liquid separation zone is used for gas-liquid separation of hydrogenation reaction effluent of the annular channel, and part of separated liquid product is recycled to the inner barrel and/or the annular channel, and part of material is fractionated; further, the liquid product recycled to the inner barrel is 5-90 wt% of the fresh feed; the liquid product recycled back to the annular channel represents 0 to 80wt% of the fresh feed.
16. The production process according to claim 1, characterized in that: the maleic anhydride conversion rate of the inner cylinder is 50-95%, preferably 55-85%.
17. A production system for preparing succinic anhydride by maleic anhydride hydrogenation is characterized in that: comprises a reaction raw material mixing zone, a maleic anhydride hydrogenation reaction zone and a gas-liquid separation zone; the reaction raw material mixing zone is used for mixing maleic anhydride solution and hydrogen, and gas-liquid mixing equipment is arranged in the reaction raw material mixing zone; the maleic anhydride hydrogenation zone is used for maleic anhydride liquid phase hydrogenation reaction, a plurality of groups of hydrogenation reaction units connected in parallel are arranged in the maleic anhydride hydrogenation zone, and each unit comprises two sleeve-type reactors with the same structure; the gas-liquid separation zone is used for gas-liquid separation of hydrogenation products.
18. The production system of claim 17, wherein: the gas-liquid mixing equipment is one or a plurality of combinations selected from a static mixer, a dissolved air pump, a mechanical stirring device, a colloid mill, a micro-pore plate nano/micro hydrogen dispersion component, a micro-bubble generator, a ceramic membrane nano/micro hydrogen dispersion component, a jet mixer and a micro-channel mixer.
19. The production system of claim 17, wherein: the sleeve-type reactor comprises an inner cylinder and an outer cylinder, wherein the inner cylinder is axially arranged in the outer cylinder, an annular channel is arranged in the area between the inner cylinder and the outer cylinder, and the inner cylinder is not communicated with the annular channel; the bottom of the inner cylinder is provided with a raw material inlet, and the top of the inner cylinder is provided with a material outlet; the top of the annular channel is provided with a material inlet, and the bottom of the annular channel is provided with a material outlet; the material outlets at the tops of the inner cylinders of the two sleeve-type reactors are communicated with the material inlets at the tops of the annular channels through pipelines; the material inlet pipeline of the inner cylinder is communicated with the feeding pipeline, and the material outlet pipeline of the annular channel is communicated with the discharging pipeline; the top of the outer cylinder is an upper sealing head, and the bottom of the outer cylinder is a lower sealing head; the top and the bottom of the wall of the inner cylinder are respectively fixedly welded and sealed with the upper seal head and the lower seal head; the height-diameter ratio of the inner cylinder is 1-15, preferably 4-10; the height-diameter ratio of the outer cylinder is 1-5, preferably 1.0-3.0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111261156.1A CN116041291B (en) | 2021-10-28 | 2021-10-28 | Production process for preparing succinic anhydride by maleic anhydride hydrogenation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111261156.1A CN116041291B (en) | 2021-10-28 | 2021-10-28 | Production process for preparing succinic anhydride by maleic anhydride hydrogenation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN116041291A true CN116041291A (en) | 2023-05-02 |
| CN116041291B CN116041291B (en) | 2024-09-03 |
Family
ID=86129981
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111261156.1A Active CN116041291B (en) | 2021-10-28 | 2021-10-28 | Production process for preparing succinic anhydride by maleic anhydride hydrogenation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116041291B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116041290A (en) * | 2021-10-28 | 2023-05-02 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation method and maleic anhydride hydrogenation system |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4792391A (en) * | 1987-06-11 | 1988-12-20 | Amoco Corporation | Floating recycle pan and process for ebullated bed reactors |
| CN102389751A (en) * | 2011-08-17 | 2012-03-28 | 徐志刚 | Fixed bed reactor and method for preparing butanedioic anhydride through maleic anhydride solution hydrogenation |
| CN103566837A (en) * | 2013-11-13 | 2014-02-12 | 山西大学 | External circular reaction device suitable for hydrogenation exothermic reaction |
| CN110013801A (en) * | 2018-01-10 | 2019-07-16 | 何巨堂 | The hydrocarbon material hydrogenator system of socket type containing upper reaction zone and product gas-liquid separation zone |
| CN116041289A (en) * | 2021-10-28 | 2023-05-02 | 中国石油化工股份有限公司 | Production process for preparing succinic anhydride by maleic anhydride hydrogenation |
| CN116041290A (en) * | 2021-10-28 | 2023-05-02 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation method and maleic anhydride hydrogenation system |
-
2021
- 2021-10-28 CN CN202111261156.1A patent/CN116041291B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4792391A (en) * | 1987-06-11 | 1988-12-20 | Amoco Corporation | Floating recycle pan and process for ebullated bed reactors |
| CN102389751A (en) * | 2011-08-17 | 2012-03-28 | 徐志刚 | Fixed bed reactor and method for preparing butanedioic anhydride through maleic anhydride solution hydrogenation |
| CN103566837A (en) * | 2013-11-13 | 2014-02-12 | 山西大学 | External circular reaction device suitable for hydrogenation exothermic reaction |
| CN110013801A (en) * | 2018-01-10 | 2019-07-16 | 何巨堂 | The hydrocarbon material hydrogenator system of socket type containing upper reaction zone and product gas-liquid separation zone |
| CN116041289A (en) * | 2021-10-28 | 2023-05-02 | 中国石油化工股份有限公司 | Production process for preparing succinic anhydride by maleic anhydride hydrogenation |
| CN116041290A (en) * | 2021-10-28 | 2023-05-02 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation method and maleic anhydride hydrogenation system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116041290A (en) * | 2021-10-28 | 2023-05-02 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation method and maleic anhydride hydrogenation system |
| CN116041290B (en) * | 2021-10-28 | 2024-05-07 | 中国石油化工股份有限公司 | Maleic anhydride hydrogenation method and maleic anhydride hydrogenation system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN116041291B (en) | 2024-09-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106518608B (en) | The continuous preparation method and device of cyclohexanedimethanol | |
| CN101735182B (en) | Process for continuously producing succinic anhydride through hydrogenation of maleic anhydride | |
| CN116037021A (en) | Maleic anhydride hydrogenation system and maleic anhydride hydrogenation method | |
| CN116041291B (en) | Production process for preparing succinic anhydride by maleic anhydride hydrogenation | |
| CN109678661A (en) | The equipment of hydrogenated bisphenol A and the continuous preparation method of hydrogenated bisphenol A are prepared for serialization | |
| CN113563201A (en) | Method for continuously and efficiently synthesizing 3, 4-dichloroaniline based on fixed bed microreactor | |
| CN112661625A (en) | Preparation process of succinic acid | |
| CN111689849B (en) | Method for producing succinic acid by liquid-phase two-stage hydrogenation | |
| CN112058185A (en) | Reaction system and method for petroleum resin hydrogenation | |
| CN103360265A (en) | Method for continuous hydrogenation of dinitrobenzene and recycling of reaction heat thereof | |
| CN116041290B (en) | Maleic anhydride hydrogenation method and maleic anhydride hydrogenation system | |
| CN101891718A (en) | Continuous production process for preparing succinyl oxide by maleic anhydride hydrogenation | |
| JP2024537486A (en) | Production method and production system for producing succinic anhydride by hydrogenating maleic anhydride | |
| CN110639623B (en) | Activation method and reaction device for preparing methyl ethyl ketone catalyst by dehydrogenating sec-butyl alcohol | |
| CN219963967U (en) | Maleic anhydride hydrogenation reaction device | |
| CN110862302B (en) | Method for preparing 1, 4-butanediol by combining slurry bed hydrogenation and fixed bed hydrogenation | |
| CN116036999B (en) | Maleic anhydride hydrogenation system and method for preparing succinic anhydride by maleic anhydride hydrogenation | |
| CN117920057A (en) | Hydrogenation reaction system and maleic anhydride hydrogenation method | |
| CN210994350U (en) | Reaction device for preparing methyl ethyl ketone by dehydrogenating sec-butyl alcohol | |
| CN117960046A (en) | Reaction process for preparing succinic anhydride | |
| CN112759505B (en) | Method and system for preparing ethylene glycol | |
| CN116042272A (en) | Liquid phase hydrogenation reaction system and liquid phase hydrogenation method | |
| CN115093330B (en) | Preparation method of p-phenylenediamine | |
| CN112011366A (en) | Micro-interface reaction system and method for petroleum resin hydrogenation | |
| CN206103913U (en) | Reaction unit of benzene part hydrogenation synthesis cyclohexene |
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 | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20240117 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant after: CHINA PETROLEUM & CHEMICAL Corp. Applicant after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant before: CHINA PETROLEUM & CHEMICAL Corp. Applicant before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |