CN202047018U - Device for preparing cyclohexene from benzene through selective hydrogenation - Google Patents
Device for preparing cyclohexene from benzene through selective hydrogenation Download PDFInfo
- Publication number
- CN202047018U CN202047018U CN2011201577709U CN201120157770U CN202047018U CN 202047018 U CN202047018 U CN 202047018U CN 2011201577709 U CN2011201577709 U CN 2011201577709U CN 201120157770 U CN201120157770 U CN 201120157770U CN 202047018 U CN202047018 U CN 202047018U
- Authority
- CN
- China
- Prior art keywords
- benzene
- reactor
- reaction
- inlet
- static mixing
- 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.)
- Expired - Lifetime
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本实用新型涉及到一种苯选择性加氢制备环己烯反应装置，其包括用于对原料苯进行精制的苯精制器、用于混合氢气和催化剂浆料的气液混合器、作为选择性加氢的主要场所的静态混合反应器和用于分离静态混合反应器送来的反应产物和催化剂的分离罐。与现有技术相比较，本实用新型所提供的反应器反应平稳易控制，且苯转化率和环己烯的选择性更好。
The utility model relates to a reaction device for preparing cyclohexene by selective hydrogenation of benzene, which comprises a benzene refiner for refining raw benzene, a gas-liquid mixer for mixing hydrogen and catalyst slurry, and a selective The main place of hydrogenation is the static mixing reactor and the separation tank used to separate the reaction product and catalyst sent from the static mixing reactor. Compared with the prior art, the reaction of the reactor provided by the utility model is stable and easy to control, and the conversion rate of benzene and the selectivity of cyclohexene are better.
Description
Technical field
The utility model relates to the chemical industry equipment field, specifically refers to a kind of benzene selective hydrogenation preparing tetrahydrobenzene reaction unit.
Background technology
Along with synthon and nylon 66 polymeric amide industrial expansions, the benzene selective hydrogenation to prepare cyclohexene more and more is subject to people's attention because of the complete hydrogenation technique of its traditional relatively benzene has the advantage of economy, safety, environmental protection.The benzene selective hydrogenation to prepare cyclohexene is important research direction in the chemical field in recent years.The benzene selective hydrogenation to prepare cyclohexene be one by water, oil, gas, the solid heterogeneous catalytic reaction of forming.Catalyzed reaction occurs on the surface of solid catalyst.Want to make catalyzed reaction to carry out smoothly, reactant benzene, hydrogen must contact, adsorb with solid catalyst, just can react.Reaction product must in time be left catalyst surface simultaneously, and new reactant in time diffusion is come in, and reaction just can continually be carried out.Therefore, to having relatively high expectations of stirring.The method that European patent EP 93101010.2, the disclosed aromatic hydrocarbons partial hydrogenation of Japanese Patent JP32936/92, Chinese patent CN1696087A are produced tetrahydrobenzene, use a kind of special catalyst, be suspended in the successive aqueous phase, hydrogen enters reaction system with the form of bubbling, utilize to stir benzene, hydrogen, catalyzer are fully contacted, can reach higher selectivity and higher yield.But present benzene selective hydrogenation device exists oil phase in the reactor, water and gas phase mixing difficulty, and stirring requires very high, and reaction efficiency is low; Reaction back oily water separation difficulty, the problem that catalyst attrition is big.
The existing technical process of benzene selective hydrogenation preparing tetrahydrobenzene is: benzene, hydrogen, catalyzer are placed in-line and have in the reactor of stirring and carry out at two, reaction liquid is with catalyzer inflow catalyst separating tank, at separating tank inner catalyst gravity settling, product after the separation is discharged from separating tank, and catalyzer is extracted out by recycle pump and recycled.In order to guarantee reaction uniformity, need gas, liquid, solid three thorough mixing of being on good terms, therefore, prior art needs bigger stirring kinetic energy to having relatively high expectations of stirring in the reactor, could guarantee the triphasic mixing of gas, liquid, solid, and energy consumption is big and reaction efficiency is low; And be to adopt gravity settling separation between catalyzer and the liquid in the separating tank, oil-water separation is bad, and the part catalyzer can flow out along with product liquid, and catalyst attrition is big, and the zinc sulfate in the catalyzer also can bring corrosion to follow-up system simultaneously.
For this reason, Chinese invention patent application CN201010210982.9 has proposed " a kind of benzene selective hydrogenation device ", and it comprises: (1) liquid-phase mixing device, and this liquid-phase mixing device links to each other with a plurality of feeding lines that under meter and flow control valve are housed on it; (2) gas phase mixing tanks, the opening for feed of this gas phase mixing tank links to each other by the reaction feed pump with the discharge port of described liquid-phase mixing device, described gas phase mixing tank with its on hydrogen flowmeter and hydrogen flowing quantity variable valve be housed the hydrogen inlet pipe be connected; (3) tubular reactors, the tube side opening for feed of this tubular reactor is connected by first connection line with the discharge port of described gas phase mixing tank, be outside equipped with chuck at described tubular reactor, be connected with heat transferring medium in the chuck, on described chuck, temperature sensor is housed; (4) separating tanks, the top of this separating tank is connected with described tubular reactor tube side discharge port by second connection line, the top of described separating tank with its on pressure regulator valve is housed and manometric hydrogen discharge pipe is connected, and its bottom is connected with the circulation fluid import of liquid-phase mixing device by the circulation line that under meter is housed on it, and described separating tank is provided with liquidometer and level meters; (5) film filters, the bottom feed mouth of this film filter is connected with oil phase discharge port on the separating tank by the reaction discharging pump, and its top is connected with the top fluid inlet of described separating tank by liquid line, has products export on described film filter top.This application before reaction earlier with benzene and catalyzer by pre-mixing, and then mixes with hydrogen, the tubular reactor that reactive system adopts strap clamp to overlap helps controlling the temperature of reaction, raising speed of reaction.But because the existence of stirring, its energy consumption is still higher; Simultaneously, product tetrahydrobenzene and reactant, catalyzer exist simultaneously during reaction, and the tetrahydrobenzene deep hydrogenation is that the by-product rate of hexanaphthene is higher, and the tetrahydrobenzene transformation efficiency is low.
Summary of the invention
Technical problem to be solved in the utility model is the benzene selective hydrogenation preparing tetrahydrobenzene reaction unit that the situation at prior art provides a kind of less energy-consumption and tetrahydrobenzene transformation efficiency height, hexanaphthene pair to yield poorly.
Another technical problem to be solved in the utility model provides that a kind of energy consumption is low, tetrahydrobenzene transformation efficiency height, the hexanaphthene pair yields poorly and catalyst attrition is little benzene selective hydrogenation preparing tetrahydrobenzene reaction unit.
The utility model solves the problems of the technologies described above the technical scheme that is adopted: this benzene selective hydrogenation preparing tetrahydrobenzene reaction unit comprises:
The benzene treater is made with extra care crude benzol, is used for removing the sulfur-containing impurities of benzene feedstock, avoids that impurities makes poisoning of catalyst in the benzene feedstock;
Gas liquid mixer has hydrogen inlet and catalyst pulp inlet, is used to mix hydrogen and catalyst pulp;
Static mixing reactor, its inlet connects the outlet of above-mentioned benzene treater and the outlet of gas liquid mixer, is the main place of selective hydrogenation; Static mixing reactor is provided with outward static mixing reactor internal reaction material is carried out the refrigerative refrigerating unit;
Separating tank, be used to separate reaction product and the catalyzer that static mixing reactor is sent here, the inlet of separating tank connects the outlet of static mixing reactor, the top of separating tank is provided with the oil phase outlet, the bottom of separating tank is provided with catalyst outlet, and this catalyst outlet connects the catalyst pulp inlet of described gas liquid mixer.
The oil phase outlet of described separating tank connects the inlet of wet cyclone, and the top of wet cyclone is provided with products export, and the outlet of wet cyclone bottom connects the catalyst inlet that is arranged on described separator middle part.
Further, can also between the inlet of outlet of the oil phase of described separator and described wet cyclone, also be provided with oil-water mixer.
In order effectively to improve speed of response, can be provided with the high efficiency nozzle of dispersion liquid in the ingress, inside of described benzene treater, and 1～6 layer of effective radially current gradient liquid re-distributor of liquid that reduces is set in the desulfuration adsorbent packing layer at interval, to improve the processing power of benzene treater.
Described liquid re-distributor is the disc grizzly pore structure, and the aperture of sieve aperture is 5～10mm, and the long-pending sum of each mesh surface is 5～30% of a benzene treater cross-sectional area.
In order further to reduce the generation of hexanaphthene, when needs control slurry than less than 2 or the residence time can select for use during less than 20 minutes and many a static mixing reactor series connection use, described static mixing reactor can have 2～4, and each static mixing reactor is connected successively.The inner parts structure of static mixing reactor has taken into full account the physical properties of material, makes each material thorough mixing in the reaction system, and unconventional salt solution in the jacket pipe is realized the effective control to temperature.
Improve, can also be provided with auxiliary reactor between described static mixing reactor and the described separating tank, the opening for feed of auxiliary reactor connects the discharge port of described static mixing reactor, and the discharge port of this auxiliary reactor connects the opening for feed of described separating tank; The top of auxiliary reactor is communicated with the hydrogen discharge pipeline, and described hydrogen discharge pipeline is provided with pressure regulator valve and pressure warning unit, and auxiliary reactor is outside equipped with the heat exchange jacket that has temperature sensor, is provided with whipping appts in the auxiliary reactor.
The aspect ratio of described auxiliary reactor is 2～3, is interval with the baffle plate that multilayer prevents the reaction solution back-mixing in the auxiliary reactor; Described whipping appts comprises stir shaft and 2～5 stirring-heads that are disposed on the stir shaft.
Principle of work of the present utility model is:
Hydrogen and catalyst premixing close, benzin system, the liquid phase benzene of reaction needed, vapor phase hydrogen, solid catalyst three-phase be fully contact in one or more static mixing reactor, satisfy repeatedly mixing, separation, the diffusion of oil-water-gas, and remove reaction heat in the static mixing reactor by water coolant, keep stable temperature of reaction; The stirring of auxiliary reactor inside and the baffle plate that prevents back-mixing impel reaction to reach intended conversion rate and selectivity, and in time shift out reaction heat by cooling off, and keep temperature of reaction; And the guide shell of separating tank inside at first outgases profit, profit coarse separation under the internal part effect, and the heavy phase catalyst pulp recycles; The light phase oil phase of separating tank goes wet cyclone to isolate product, wet cyclone is provided with heavy alloyed inner barrel and outer cylinder body, after the process oil-water mixer added the water mixing, noble metal catalyst, water were separated with product under cyclonic action, and precious metal is recycled.Can finish the serialization production of this device thus;
Described device can be realized the continuity and the stability production of benzene selective hydrogenation, the adding of under meter, variable valve control benzene and the continuous certainty ratio of hydrogen, and the recycle pump control catalyst circulates continuously, and product is able to the successive extraction.
Controls such as each under meter, variable valve, pump can take PLC module and DCS Controlling System to carry out automatization control production in the described device.
Described device recycles by jacket water (J.W.), and reaction heat is shifted out, and makes the carrying out that reaction can continous-stable;
Compared with prior art, reaction unit provided by the utility model and process using the main reactor of static mixing reactor as benzene hydrogenation, can make the material uniform mixing that enters in the static mixing reactor, improved the chance that hydrogen, benzene and catalyzer fully contact, avoided the use of stirring, energy consumption reduces greatly, and reaction mass air-teturning mixed phenomenon can not occur, the concentration of hexanaphthene can be not too high in the static mixing reactor like this, effectively reduced the probability of cyclohexene hydrogenation generation hexanaphthene, the yield height of tetrahydrobenzene; And the series connection of a plurality of static mixing reactors is used, and has further guaranteed the control of tetrahydrobenzene concentration in the reactor, makes that the transformation efficiency of tetrahydrobenzene is better.And in the preferred version static mixing reactor and auxiliary reactor unite use, more help the control section hydrogenation and send out the process of answering, improve speed of reaction, make catalyzer reach rational selectivity and transformation efficiency, to improve the yield of tetrahydrobenzene, can control the optimum response ratio of benzene, hydrogen, catalyzer, and realize serialization production by the catalyst recirculation pump.In the separation system gravity settling separation jar and wet cyclone unite use, fully guaranteed the separating effect of profit, and can reclaim and be entrained in the catalyzer that runs off in the oil phase, reduced the loss of noble metal catalyst.
Description of drawings
The schema of Fig. 1 the utility model embodiment;
Fig. 2 is the structural representation of benzene treater among the utility model embodiment;
Fig. 3 is the structural representation of static mixing reactor among the utility model embodiment;
Fig. 4 is the structural representation of oil-water mixer among the utility model embodiment;
Fig. 5 is the structural representation of auxiliary reactor among the utility model embodiment;
Fig. 6 is temperature among the utility model embodiment, pressure and time relation line;
Fig. 7 is benzene flow among the utility model embodiment, slurry internal circulating load and time relation line;
Fig. 8 is benzene transformation efficiency among the utility model embodiment, tetrahydrobenzene selectivity and time relation line.
Embodiment
Embodiment describes in further detail the utility model below in conjunction with accompanying drawing.
To shown in Figure 5, this benzene selective hydrogenation preparing tetrahydrobenzene reaction unit comprises as Fig. 1:
Benzene treater 1, the sorbent material packing layer 12 that interior dress is filled by desulfuration adsorbent is fixed bed; The inner ingress of benzene treater is provided with high efficiency nozzle 11 and liquid re-distributor 13.Liquid re-distributor has four layers, is disposed between the sorbent material packing layer.Liquid re-distributor is the disc grizzly pore structure, and the aperture of sieve aperture is 2～8mm, and the long-pending sum of each mesh surface is 5～20% of a benzene treater cross-sectional area.The outlet of benzene treater connects the benzene inlet of first static mixing reactor 31 after 9 heat exchange of chuck interchanger.
Gas liquid mixer 2 has hydrogen inlet and catalyst pulp inlet, is used to mix hydrogen and catalyst pulp; The outlet of this gas liquid mixer connects following static mixing reactor 3.
Static mixing reactor is the main place of selective hydrogenation; Present embodiment adopts two static mixing reactor series connection to use.Static mixing reactor in the present embodiment is the SV type, is filled with the V-type filler in it; The outside of static mixing reactor is provided with and is used for the coil pipe of heat exchange.Can also replace coil pipe with chuck.Wherein, the inlet of first static mixing reactor 31 is arranged on the gas-liquid mixed material inlet of bottom, and its material outlet is arranged on the top of first static mixing reactor, is connected with the material inlet of second static mixing reactor bottom.The material outlet of second static mixing reactor 32 connects the opening for feed of following auxiliary reactor bottom.Water coolant feeds cooling by coil pipe or chuck.
In the present embodiment, in order to make full use of the temperature difference of each component cooling water, reduce energy expenditure, 90～115 ℃ water coolant enters from the inlet of the second static mixing reactor spiral coil cooling tube, and behind the cycle heat exchange, the water coolant that its outlet is 100～125 ℃ enters the inlet of the first static mixing reactor spiral coil cooling tube, behind the cycle heat exchange, this moment, the temperature of water coolant was 115～145 ℃, entered the inlet of chuck interchanger from the outlet of the first static mixing reactor spiral coil cooling tube, and commercial benzene is heated to 120 ℃.
Separating tank 5, be used to separate reaction product and the catalyzer that static mixing reactor is sent here, the inlet of separating tank connects the discharge port of auxiliary reactor 4, the top of separating tank is provided with the oil phase outlet, the bottom of separating tank is provided with catalyst outlet, and this catalyst outlet connects the catalyst pulp inlet of gas liquid mixer by recycle pump 51; The sidewall middle part of separating tank also is provided with catalyst inlet.The inside of separating tank is provided with the liquid guide flow tube, and the separating tank bottom is its aspect ratio 2～3: 1 of cone shape, can realize the internal circulating load of the effusive catalyst slurry in separating tank bottom is controlled with the catalyst recirculation pump in this device.
Oil-water mixer 6, its inlet have two, and one is the water inlet 62 that connects water pipe, and another is the oil phase inlet 63 that connects the oil phase outlet of separating tank by reaction discharging pump 61, and its outlet 64 connects the inlet of following wet cyclone 7; The effect one of this oil-water mixer 6 is to the reactive system moisturizing, and is used for separate and subside and is entrained in catalyzer in the oil phase, reclaims the zinc sulfate of carrying secretly in the oil phase besides.
Wet cyclone 7 is used for catalyzer and oil mixture are separated.The aspect ratio of this wet cyclone is 5: 1, and the aspect ratio of wet cyclone can be 2～10: between 1.The catalyst outlet of wet cyclone bottom is communicated with the catalyst inlet that is arranged on the separating tank middle part, and the oil phase outlet at wet cyclone top connects the product separation system.
Above-mentioned all equipment that contact with catalyzer, for example auxiliary reactor, separating tank, wet cyclone etc., its material adopts Hastelloy or high-alloy stainless steel, avoid metal ion to enter reacting slurry, prevent the catalyst deactivation that causes thus, avoid poisoning of catalyst, guarantee the work-ing life of catalyzer.
It is as follows that benzene selective hydrogenation prepares the technical process of hexanaphthene:
(1) benzene feedstock is sent into the benzene treater and is removed sulfur-containing impurities in the benzene feedstock, the benzene that from the benzene treater, comes out after chuck interchanger heat exchange to 120 ℃ with following gas-liquid mixture and stream;
(2) catalyst pulp and hydrogen are sent into the described gas liquid mixer from described catalyst pulp inlet and described hydrogen inlet respectively; The pressure that control hydrogen enters in the gas liquid mixer is 5.0Mpa, and the mass ratio of catalyst pulp and benzene is 2.8: 1, and the mol ratio of hydrogen and benzene is 2.5: 1; Wherein catalyst quality content is 0.8% in the catalyst pulp;
(3) above-mentioned benzene and mixed hydrogen and catalyst pulp are sent in first static mixing reactor, behind first static mixing reactor internal reaction the reaction mixture that obtains are sent into successively and continue reaction in follow-up placed in-line second static mixing reactor; The reaction mixture that will come out in second static mixing reactor is sent into described auxiliary reactor, further reaction in auxiliary reactor; Wherein, the flow velocity of controlling temperature of reaction in each described static mixing reactor and be 143 ℃, reaction pressure and be 5.0Mpa, reaction mixture is 5m/s, controlling temperature of reaction in the described auxiliary reactor and be 140 ℃, reaction pressure is that 5.0Mpa, stirring velocity are 80rpm, obtains containing the mixture of tetrahydrobenzene at the discharge port of auxiliary reactor;
(4) the tetrahydrobenzene mixture is sent into separating tank, behind separate and subside, isolated catalyzer is sent from the catalyst outlet of separating tank bottom, enters above-mentioned gas liquid mixer internal recycle and uses, and obtains containing the oil mixture of tetrahydrobenzene on separating tank top;
(5) described oil mixture is sent into described oil-water mixer, mix in oil-water mixer with the water of adding, form the globule of 0.5～2mm, send into wet cyclone then, after wet cyclone separates, the catalyzer and the zinc sulfate that obtain carrying secretly in the oil mixture in the bottom of wet cyclone, this part catalyzer returns separating tank from the catalyst inlet at described separating tank middle part, and the top exit of wet cyclone obtains benzene, tetrahydrobenzene and hexanaphthene oil mixture.
Implementation result is as follows:
(1) can realize the strictness of temperature and pressure is controlled, be illustrated in figure 6 as 720h with interior temperature and pressure changing conditions.As shown in Figure 6,143 ℃ of average reaction temperature, reaction pressure 4.9MpaG, temperature and pressure control is steadily.
(2) can realize benzene flow and the strict control of internal circulating load, as seen from Figure 7, the cabling of benzene flow and internal circulating load is very steady, and interior benzene flow of 720h and catalyst recirculation amount be change curve in time, the average benzene flow of benzene 30KG/h, the average internal circulating load 85.5KG/h of catalyst pulp.Benzene flow and internal circulating load mass ratio are 1: 2.86, are strict controlled within the scope of processing parameter requirement.
(3) selectivity of benzene transformation efficiency and tetrahydrobenzene is better, as shown in Figure 8,720h benzene transformation efficiency 55.5%, the tetrahydrobenzene selectivity reaches 79-85%.
Claims (8)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201577709U CN202047018U (en) | 2011-05-13 | 2011-05-13 | Device for preparing cyclohexene from benzene through selective hydrogenation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201577709U CN202047018U (en) | 2011-05-13 | 2011-05-13 | Device for preparing cyclohexene from benzene through selective hydrogenation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202047018U true CN202047018U (en) | 2011-11-23 |
Family
ID=44987336
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011201577709U Expired - Lifetime CN202047018U (en) | 2011-05-13 | 2011-05-13 | Device for preparing cyclohexene from benzene through selective hydrogenation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202047018U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102241558A (en) * | 2011-05-13 | 2011-11-16 | 化学工业第二设计院宁波工程有限公司 | Reaction device and process for preparing cyclohexene by selectively hydrogenating benzene |
| CN102895932A (en) * | 2012-10-17 | 2013-01-30 | 联化科技股份有限公司 | Device for photo-catalytic bromination reaction |
| CN109158113A (en) * | 2018-07-18 | 2019-01-08 | 北京华和拓科技开发有限责任公司 | A kind of partial hydrogenation of benzene catalyst recovery system and its implementation |
-
2011
- 2011-05-13 CN CN2011201577709U patent/CN202047018U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102241558A (en) * | 2011-05-13 | 2011-11-16 | 化学工业第二设计院宁波工程有限公司 | Reaction device and process for preparing cyclohexene by selectively hydrogenating benzene |
| CN102241558B (en) * | 2011-05-13 | 2014-02-19 | 中国化学赛鼎宁波工程有限公司 | Reaction device and process for preparing cyclohexene by selectively hydrogenating benzene |
| CN102895932A (en) * | 2012-10-17 | 2013-01-30 | 联化科技股份有限公司 | Device for photo-catalytic bromination reaction |
| CN109158113A (en) * | 2018-07-18 | 2019-01-08 | 北京华和拓科技开发有限责任公司 | A kind of partial hydrogenation of benzene catalyst recovery system and its implementation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102241558B (en) | Reaction device and process for preparing cyclohexene by selectively hydrogenating benzene | |
| RU2562770C2 (en) | Method and device for carrying out fischer-tropsch synthesis | |
| CN105944652B (en) | Tubular microchannel alkylation reactor and method of using the same | |
| CN101850225B (en) | Benzene selective hydrogenation device | |
| WO2011120374A1 (en) | Heterogeneous catalytic tower type collision flow reactor | |
| EP0552809A1 (en) | Method for partially hydrogenating a monocyclic aromatic hydrocarbon | |
| RU2742576C1 (en) | Apparatus and method for synthesis of paraxylol and combined synthesis of light olefins from methanol and/or dimethyl ether and benzene | |
| CN110961067B (en) | Continuous reaction device and method for benzoic acid hydrogenation | |
| CN101351526A (en) | Bubble column Fischer-Tropsch synthesis slurry bed reaction system | |
| CN102580629B (en) | Gas-liquid-liquid-solid reaction device | |
| CN202047018U (en) | Device for preparing cyclohexene from benzene through selective hydrogenation | |
| EP1636151B1 (en) | Process for producing liquid and, optionally, gaseous products from gaseous reactants | |
| CN202527171U (en) | Reaction device applied to gas-liquid-liquid-solid multiphase reaction | |
| WO2006097906A1 (en) | Production of liquid and, optionally, gaseous products from gaseous reactants | |
| CN117000150B (en) | Continuous hydrogenation reaction device and reaction method for nitronaphthalene sulfonic acid | |
| CN202860529U (en) | Reaction device for producing cyclohexene by partial hydrogenation of benzene | |
| CN101440027A (en) | Alkene hydroformylation flow reactor | |
| CN104478642B (en) | Device and method for producing olefin from methanol | |
| US20020143075A1 (en) | Low-profile moving bed reactor | |
| CN106540637B (en) | A kind of circulation flow reactor and application method | |
| CN101397255B (en) | Catalyst continuous separation recycling method in toluenediamine synthetic process and equipment thereof | |
| CN115197171A (en) | A kind of method and system for producing propylene oxide | |
| RU2384603C1 (en) | Reaction system with bubble column type suspended layer for fischer-tropsch synthesis | |
| TW201307253A (en) | Improved process for the production of hexamethylenediamine | |
| US8894939B2 (en) | Three phase reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: CNCEC SEDIN NINGBO ENGINEERING CO., LTD. Free format text: FORMER NAME: NINGBO ENGINEERING CO., LTD, SECOND DESIGN INSTITUTE OF CHEMICAL INDUSTRY |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 315040 No. 999, Lane 1, sailing Road, hi tech Zone, Zhejiang, Ningbo Patentee after: Sedin Ningbo Engineering Co., Ltd. Patentee after: Huafeng Group Corp., Ltd. Address before: 315040 No. 999, Lane 1, sailing Road, hi tech Zone, Zhejiang, Ningbo Patentee before: Ningbo Engineering Co., Ltd, Second Design Institute of Chemical Industry Patentee before: Huafeng Group Corp., Ltd. |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20180530 Address after: 315040 1 Lane 999 lane, Yang Fan Road, Ningbo, Zhejiang, 5-1, 5-2, 5-5, 5-6 Co-patentee after: Chongqing Huafeng Chemical Co., Ltd. Patentee after: Sedin Ningbo Engineering Co., Ltd. Address before: 315040 No. 999 lane, Yang Fan Road, Ningbo high tech Zone, Zhejiang, China 1 Co-patentee before: Huafeng Group Corp., Ltd. Patentee before: Sedin Ningbo Engineering Co., Ltd. |
|
| TR01 | Transfer of patent right | ||
| CX01 | Expiry of patent term |
Granted publication date: 20111123 |
|
| CX01 | Expiry of patent term |