CN203699908U - Anthraquinone process hydrogen peroxide production device - Google Patents
Anthraquinone process hydrogen peroxide production device Download PDFInfo
- Publication number
- CN203699908U CN203699908U CN201420008834.2U CN201420008834U CN203699908U CN 203699908 U CN203699908 U CN 203699908U CN 201420008834 U CN201420008834 U CN 201420008834U CN 203699908 U CN203699908 U CN 203699908U
- Authority
- CN
- China
- Prior art keywords
- outlet
- pipeline
- import
- injector
- interchanger
- 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.)
- Withdrawn - After Issue
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an anthraquinone process hydrogen peroxide production device. The anthraquinone process hydrogen peroxide production device is characterized in that an ejector I is arranged on the top of a hydrogenation reactor, the bottom of the hydrogenation reactor is connected to an inlet of a circulating pump I through a pipeline, an outlet of the circulating pump I is connected to an inlet of a heat exchanger I through a pipeline, an outlet of the heat exchanger I is connected to an inlet of a cross flow filter through a pipeline, an outlet of the cross flower filter is connected to an inlet of the ejector I through a pipeline in which a working liquid inlet is formed; an ejector II is arranged on the top of an oxidization reactor, the bottom of the oxidization reactor is connected to an inlet of a circulating pump II through a pipeline, an outlet of the circulating pump II is connected to an inlet of a heat exchanger II through a pipeline, an outlet of the heat exchanger II is connected to an inlet of the ejector II through a pipeline in which inlets are respectively formed; a hydrogenation liquid inlet is connected to a hydrogenation liquid outlet in the cross flow filter through a pipeline, an outlet of a static mixer is connected to an inlet of an oil-water separator through a pipeline, and the upper part and the lower part of the oil-water separator are respectively provided with outlets.
Description
Technical field
The utility model relates to oxydol production apparatus, is specifically related to anthraquinone oxydol production apparatus.
Background technology
Hydrogen peroxide is a kind of green chemical industry product, and it is produced and use procedure is not almost polluted, therefore be called as the Chemicals of " cleaning ", its application prospect is increasingly good.Initial hydrogen peroxide is only for medicine and military project, is progressively applied to that chemical is synthetic, weaving, papermaking, environmental protection, food, medicine, metallurgy and the wide spectrum such as agriculture, market requirement expanding day.
The production method of hydrogen peroxide has multiple, wherein hydrogen dioxide solution production by anthraquinone process is one of production method that the sector is the most ripe in the world at present, external large-scale manufacturer all adopts hydrogen dioxide solution production by anthraquinone process, and the preparation of domestic current hydrogen peroxide is nearly all also anthraquinone.The concrete production technique of the method is: 2-alkyl-anthraquinone and organic solvent (C
9～C
10) be mixed with working solution, be under the condition of 0.30～0.50MPa, 55 DEG C～65 DEG C of temperature, catalyzer (Ni or Pd) existence at pressure, pass into H
2carry out hydrogenation, then carry out counter flow oxidation at 40～44 DEG C with air, through extraction, regeneration, the refining and concentrated H that obtains
2o
2aqueous solution finished product.
The main chemical reactions of hydrogen dioxide solution production by anthraquinone process is identical with ultimate principle both at home and abroad, but concrete technical scheme difference to some extent, the key distinction is the hydrogenation mode of working fluid composition, hydrogenation catalyst and employing.The hydrogenation mode adopting at present mainly contains suspension bed nickel or palladium-carbon catalyst technique, fixed-bed palladium catalysts technique and fluidized-bed palladium-carbon catalyst reaction process.
Before domestic 20th century the mid-80s, the production of hydrogen peroxide is mainly taking nickel catalyzator stirring tank hydrofenating anthraquinone method technique as main, along with the continuous expansion of throughput, compared with stirring tank technique, fixed-bed process taking palladium as catalyzer demonstrates its superiority gradually: hydrogenation equipment is simple in structure, plant capacity is large, in production process, do not need often to add catalyzer, safety performance is good, easy to operate, by means of computer centralized distribution control techniques, can greatly improve the safety performance of device, this technique has become the direction of hydrogen peroxide production development.Though palladium catalytic fixed bed technique is simple to operate, catalyzer need not separate, but also there is open defect, inhomogeneous such as each several part reaction, easily form short circuit, cause hot localised points, easily produce working fluid degraded, break-up of catalyst, caking, utilization ratio are low, speed of response is subject to extending influence of hydrogen, and domestic widely used fixed bed hydrogenation efficiency is (with H
2o
2meter) be generally 6g/L～7g/L, with the fluidized-bed hydrogenation efficiency of external employing can reach 18g/L above compared with, there is huge spread.
Although fluidized-bed process can improve device production efficiency greatly, reduce production costs, make anthraquinone hydrogenation reaction evenly, avoid reaction process hot localised points to form and cause working fluid degraded, be conducive to improve hydrogen peroxide quality product, meet better the demand of the industries such as food, but also do not occur at home the bibliographical information of hydrogenation fluidized-bed at present, only have hydrogen peroxide company of Shanghai Atofina and Fujian the first chemical plant introduction of foreign technology to adopt the patent technique of palladium catalyzed hydrogenation fluidized-bed.
No matter be fixed-bed process or fluidized-bed process, except hydrogenation equipment difference, other parts are basic identical.
The oxidation of hydride is to carry out in the oxidizing tower of the three joint void tower compositions with decollator, existing mode of oxidizing and oxidation furnaces exist following shortcoming: air-flow skewness, gas-to-liquid contact is insufficient, and mass transfer effect is poor, and air utilising efficiency and oxidation efficiency are low; Hydride oxidation not exclusively, has increased the weight of the burden of subsequent handling, moves not steady; Inhomogeneous cooling is even, and hydrogen peroxide easily decomposes.
The extraction of hydrogen peroxide is carried out in sieve-tray tower, pure water carries out counter-current extraction, separates with oxidation solution, and this extraction mode exists following shortcoming: two-phase undercompounding, and the pure water amount needing is large, the hydrogen peroxide concentration of separating is low, affects equipment capacity etc.
In addition, existing anthraquinone oxydol production apparatus also exists the shortcomings such as equipment is many, complex structure, volume is large, floor space is large, facility investment is large.
Summary of the invention
The purpose of this utility model is: be respectively gas-liquid-solid three-phase and solution-air two phase reaction according to hydrogen dioxide solution production by anthraquinone process hydrogenation, oxidizing reaction, speed of reaction and total efficiency are subject to this feature of mass transfer effect control, provide a kind of novel anthraquinone oxydol production apparatus, the many defects that exist to solve existing anthraquinone oxydol production apparatus.
Technical solution of the present utility model is: this oxydol production apparatus is made up of hydrogenation unit, oxidizing reaction unit and extracting and separating unit; It comprises hydrogenation reactor, 1
#recycle pump, 1
#interchanger, cross-flow filter, 1
#injector, oxidation reactor, 2
#recycle pump, 2
#interchanger, 2
#injector, static mixer and water-and-oil separator; Hydrogenation reactor top installs 1
#injector, hydrogenation reactor top and 1
#hydrogen recycle pipe is set between injector, on hydrogen recycle pipe, hydrogen inlet is set, hydrogenation reactor bottom is by pipeline and 1
#the import of recycle pump connects, and 1
#circulation pump outlet is by pipeline and 1
#the import of interchanger connects, and 1
#the outlet of interchanger is connected with the import of cross-flow filter by pipeline, and hydride discharge port is set on cross-flow filter, and the outlet of cross-flow filter is by pipeline and 1
#on the import connection of injector and this segment pipe, working fluid import is set; Oxidation reactor top arranges oxidized tail gas discharge outlet, and oxidation reactor top installs 2
#injector, oxidation reactor top and 2
#gas circulating tube is set between injector, air or oxygen import is set on gas circulating tube, oxidation reactor bottom is by pipeline and 2
#the import of recycle pump connects, and 2
#circulation pump outlet is by pipeline and 2
#the import of interchanger connects, and 2
#the outlet of interchanger is by pipeline and 2
#on the import connection of injector and this segment pipe, oxidation solution outlet and hydride import are set respectively; Hydride import is connected with the hydride outlet on cross-flow filter by pipeline, oxidation solution outlet is connected with static mixer import by pipeline, purified water inlet is also set on this segment pipe, static mixer outlet is connected with water-and-oil separator import by pipeline, water-and-oil separator upper and lower arranges respectively raffinate outlet and hydrogen peroxide crude product (extraction liquid) outlet, and entirety forms anthraquinone oxydol production apparatus.
The utility model adopts an empty pressure-pot as hydrogenation reactor, and configuration cycles pump, interchanger, cross-flow filter and injector form a hydrogenation unit, when production, start recycle pump, in hydrogenation reactor, first the hydride of mixed catalyst enters interchanger by recycle pump, remove reaction heat, maintenance system temperature of reaction, isolate hydride by cross-flow filter again, the hydride outlet from cross-flow filter of sub-fraction hydride flows to oxidizing reaction unit, overwhelming majority hydride and catalyzer one start shipment circulation, enter injector with together with fresh working fluid, through injector high-velocity jet, in air chamber, form negative pressure, hydrogen and the working fluid that contains catalyzer acutely mix, gas-liquid-solid three-phase fully contacts, at mixing zone highly effective reaction, go out rear continuation reacts in reactor, through buffering, gas and liquid separation, gas is got back to reactor top, again suck and continue to participate in reaction by the injected device of circulation tube, in hydrogenation reactor, the hydride of mixed catalyst enters recycle pump and enters interchanger and cross-flow filter again, the continuous extraction of hydride, reaction continues to loop.
The utility model adopts an empty pressure-pot as oxidation reactor, and configuration cycles pump, interchanger and injector form an oxidizing reaction unit, when production, in reactor, inject reaction solution, start recycle pump, first oxidation solution in oxidation reactor enters interchanger by recycle pump, remove reaction heat, maintenance system temperature of reaction, sub-fraction oxidation solution flows to static mixer from oxidation solution outlet, overwhelming majority oxidation solution goes circulation, with together with hydride from hydrogenation unit, enter injector, through injector high-velocity jet, in air chamber, form negative pressure, reaction solution in reactor is sucked, gas and reaction solution acutely mix, at mixing zone highly effective reaction, go out rear continuation reacts in reactor, through buffering, gas and liquid separation, gas is got back to reactor top, again suck and continue to participate in reaction by the injected device of circulation tube, oxidation solution in oxidation reactor will again be recycled pump and siphon away, enter after interchanger heat exchange, extraction sub-fraction oxidation solution, most of oxidation solution enters injector again, reaction is proceeded.
The utility model at least adopts one-level extracting and separating unit, while adopting multi-stage solvent extraction separate mode, the extraction liquid of next stage is as the extraction agent of upper level, pure water is as the extraction agent of last step, hydrogen peroxide crude product spills out cleaning section from the water-and-oil separator of the first step, and raffinate spills out reprocessing cycle from last step water-and-oil separator and uses.
The utlity model has following advantage:
The use of 1, hydrogenation, oxidizing reaction unit injection device and recycle pump, not only make reaction system obtain high mass transfer effect, improved speed of reaction, also make whole reaction system realize circulation fast, ensure that the temperature in reaction system is impartial everywhere, reacting balance and carrying out fast; Splendid mass transfer effect, makes hydrogenation efficiency (with H
2o
2meter) can reach 25g/L more than, speed of response is fast, the reaction times is short, has greatly improved production efficiency high; Good heat-transfer effect, makes anthraquinone hydrogenation reaction evenly, has avoided reaction process local superheating and causes working fluid to decompose, and has improved hydrogen peroxide quality product high.
2, device structure and technical process are simple, and volume is little, and the hydrogen peroxide (27.5%) of a set of 100,000 t/a installs the reactor volume adopting and only has 2m
3left and right, is 1/tens of fluidized-bed or suspended-bed reactor volume, and facility investment is saved greatly, and fixed bed (or suspension bed) the process unit facility investment of same throughput is 8～10 times of the present utility model.
3, the usage quantity that has greatly reduced precious metal (Pd/C) catalyzer and working fluid, utilization ratio is high, and consumption is few, only has 1/tens of pre-existing reactors structure usage quantity, thereby has saved running cost and investment.
4, when oxidation unit adopts pure oxygen as oxygenant, only need form nitrogen envelope at the slow-witted end perfusion nitrogen on oxidation reactor top, both improve the security of device, can make it again to become the safety top space without discharge, both reach safety in production, do not produced again oxidized tail gas, realized cleaner production.
5, hydrogenation, oxidizing reaction unit adopt external heat exchanger, make heat interchanging area not be subject to the restriction of reactor capacity and reaction mass, can configure according to need of production the size of heat exchanger area.
6, adopt static mixer and water-and-oil separator to replace the extraction tower of existing technique, oxidation solution and pure water enter water-and-oil separator after fully mixing in static mixer, separate with proportion difference according to the immiscible property of hydrogen peroxide and working fluid.Because static mixer has extraordinary mixing functions, can obtain good effect of extracting; Extracting and separating unit at least adopts one-level simultaneously, if adopt multi-stage solvent extraction to separate, without the concentrated hydrogen peroxide product that can obtain high density, concentration can, up to 40～50%, both reduce equipment investment, had realized again energy-saving and emission-reduction.
7, equipment has been realized miniaturization, has reduced the floor space of device, saves land used more than 50 percent; Simplify technical process, reduced recruitment cost.
Brief description of the drawings
Fig. 1 is structural principle schematic flow sheet of the present utility model.
Fig. 2 is that multi-stage solvent extraction separation process of the present utility model and material move towards schematic diagram.
In figure: 1 hydrogenation reactor, 21
#recycle pump, 31
#interchanger, 4 cross-flow filters, 51
#injector, 6 oxidation reactors, 72
#recycle pump, 82
#interchanger, 92
#injector, 10 static mixers, 11 water-and-oil separators.
Embodiment
As shown in Figure 1, this oxydol production apparatus is made up of hydrogenation unit, oxidizing reaction unit and extracting and separating unit; It comprises hydrogenation reactor 1,1
#recycle pump 2,1
#interchanger 3, cross-flow filter 4,1
#injector 5, oxidation reactor 6,2
#recycle pump 7,2
#interchanger 8,2
#injector 9, static mixer 10 and water-and-oil separator 11; Hydrogenation reactor 1 top installs 1
#injector 5, hydrogenation reactor 1 top and 1
#hydrogen recycle pipe is set between injector 5, on hydrogen recycle pipe, hydrogen inlet is set, hydrogenation reactor 1 bottom is by pipeline and 1
#the import of recycle pump 2 connects, and 1
#the outlet of recycle pump 2 is by pipeline and 1
#the import of interchanger 3 connects, and 1
#the outlet of interchanger 3 is connected with the import of cross-flow filter 4 by pipeline, and hydride discharge port is set on cross-flow filter 4, and the outlet of cross-flow filter 4 is by pipeline and 1
#on the import connection of injector 5 and this segment pipe, working fluid import is set; During taking air as oxygenant, at oxidation reactor top, oxidized tail gas discharge outlet is set, oxidation reactor 6 tops install 2
#injector 9, oxidation reactor 6 tops and 2
#between injector 9, gas circulating tube is set, air or oxygen import is set on gas circulating tube, oxidation reactor 6 bottoms are by pipeline and 2
#the import of recycle pump 7 connects, and 2
#the outlet of recycle pump 7 is by pipeline and 2
#the import of interchanger 8 connects, and 2
#the outlet of interchanger 8 is by pipeline and 2
#on the import connection of injector 9 and this segment pipe, oxidation solution outlet and hydride import are set respectively; Hydride import is connected with the hydride outlet on cross-flow filter 4 by pipeline, oxidation solution outlet is connected with static mixer 10 imports by pipeline, purified water inlet is also set on this segment pipe, static mixer 10 exports by pipeline and is connected with water-and-oil separator 11 imports, the upper and lower of water-and-oil separator 11 arranges respectively raffinate outlet and hydrogen peroxide crude product (extraction liquid) outlet, and entirety forms anthraquinone oxydol production apparatus.
As shown in Figure 2, for multi-stage solvent extraction separates, the extraction liquid of next stage is as the extraction agent of upper level, and pure water is as the extraction agent of last step, hydrogen peroxide crude product spills out cleaning section from the water-and-oil separator of the first step, and raffinate spills out reprocessing cycle from last step water-and-oil separator and uses.
When production, in hydrogenation reactor, inject working fluid, the front every preparation work of driving is carried out rear unlatching 1
#recycle pump 2, and working fluid and hydrogen are sent into hydrogenation reactor 1 continuously, carry out hydrogenation reaction, pass through 1 containing the hydride of catalyzer
#recycle pump 2 sends into 1
#interchanger 3 is removed the heat that reaction produces, maintenance system temperature of reaction, then enter cross-flow filter 4, isolates a part of hydride and enters oxidation reactor 6 and carry out oxidizing reaction, another part goes circulation containing the hydride of catalyzer, enters 1 with together with fresh working fluid
#injector 5 is spurted into hydrogenation reactor 1, and hydrogenation is proceeded; The hydride and the oxygen that enter oxidation reactor 6 carry out oxidizing reaction, and the oxidation solution of generation is by 2
#recycle pump 7 sends into 2
#interchanger 8 is removed the heat that reaction produces, maintenance system temperature of reaction, and a part of oxidation solution goes circulation, enters 2 with together with hydride from cross-flow filter
#injector 9 is spurted into oxidation reactor 6, oxidizing reaction is proceeded, another part oxidation solution enters static mixer 10 and pure water hybrid extraction, after hybrid extraction, entering water-and-oil separator 11 separates, isolated raffinate returns hydrogenation reactor and recycles from regeneration is flowed out on the top of water-and-oil separator 11, and hydrogen peroxide crude product (being also extraction liquid) spills out cleaning section from water-and-oil separator 11 bottoms and purifies to obtain hydrogen peroxide finished product.
Claims (2)
1. anthraquinone oxydol production apparatus, is made up of hydrogenation unit, oxidizing reaction unit and three of extracting and separating unit part, it is characterized in that: it comprises hydrogenation reactor (1), 1
#recycle pump (2), 1
#interchanger (3), cross-flow filter (4), 1
#injector (5), oxidation reactor (6), 2
#recycle pump (7), 2
#interchanger (8), 2
#injector (9), static mixer (10) and water-and-oil separator (11); Hydrogenation reactor (1) top installs 1
#injector (5), hydrogenation reactor (1) top and 1
#injector arranges hydrogen recycle pipe between (5), on hydrogen recycle pipe, hydrogen inlet is set, and hydrogenation reactor (1) bottom is by pipeline and 1
#the import of recycle pump (2) connects, and 1
#the outlet of recycle pump (2) is by pipeline and 1
#the import of interchanger (3) connects, and 1
#the outlet of interchanger (3) is connected with the import of cross-flow filter (4) by pipeline, and cross-flow filter arranges hydride discharge port on (4), and the outlet of cross-flow filter (4) is by pipeline and 1
#on the import connection of injector (5) and this segment pipe, working fluid import is set; During taking air as oxygenant, oxidation reactor top arranges oxidized tail gas discharge outlet, and oxidation reactor (6) top installs 2
#injector (9), oxidation reactor (6) top and 2
#injector arranges gas circulating tube between (9), and air or oxygen import is set on gas circulating tube, and oxidation reactor (6) bottom is by pipeline and 2
#the import of recycle pump (7) connects, and 2
#the outlet of recycle pump (7) is by pipeline and 2
#the import of interchanger (8) connects, and 2
#the outlet of interchanger (8) is by pipeline and 2
#on the import connection of injector (9) and this segment pipe, oxidation solution outlet and hydride import are set respectively; Hydride import is connected with the hydride outlet on cross-flow filter (4) by pipeline, oxidation solution outlet is connected with static mixer (10) import by pipeline, on this segment pipe, purified water inlet is set, static mixer (10) outlet is connected with water-and-oil separator (11) import by pipeline, the upper and lower of water-and-oil separator (11) arranges respectively raffinate outlet and hydrogen peroxide crude product (extraction liquid) outlet, and entirety forms the production equipment of anthraquinone hydrogen peroxide.
2. anthraquinone oxydol production apparatus according to claim 1, it is characterized in that: at least adopt one-level extracting and separating unit, while adopting multi-stage solvent extraction separate mode, the extraction liquid of next stage is as the extraction agent of upper level, pure water is as the extraction agent of last step, hydrogen peroxide crude product spills out cleaning section from the water-and-oil separator of the first step, and raffinate spills out reprocessing cycle from last step water-and-oil separator and uses.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420008834.2U CN203699908U (en) | 2014-01-08 | 2014-01-08 | Anthraquinone process hydrogen peroxide production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420008834.2U CN203699908U (en) | 2014-01-08 | 2014-01-08 | Anthraquinone process hydrogen peroxide production device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203699908U true CN203699908U (en) | 2014-07-09 |
Family
ID=51050375
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420008834.2U Withdrawn - After Issue CN203699908U (en) | 2014-01-08 | 2014-01-08 | Anthraquinone process hydrogen peroxide production device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203699908U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708426A (en) * | 2014-01-08 | 2014-04-09 | 石祖嘉 | Device for producing hydrogen peroxide by adopting anthraquinone process |
| CN104098475A (en) * | 2014-07-28 | 2014-10-15 | 淮安嘉诚高新化工股份有限公司 | Device and method for producing diaminotoluene (TDA) by continuous liquid phase catalysis hydrogenation reduction of dinitrotoluene (DNT) |
| CN104098474A (en) * | 2014-07-28 | 2014-10-15 | 淮安嘉诚高新化工股份有限公司 | Device and method for producing methyl aniline through performing continuous liquid-phase catalytic hydrogenation reduction on nitrotoluene |
| CN106629618A (en) * | 2017-01-03 | 2017-05-10 | 河北美邦工程科技股份有限公司 | Fluidized bed hydrogenation reaction and separation process and device for producing hydrogen peroxide by virtue of anthraquinone method |
-
2014
- 2014-01-08 CN CN201420008834.2U patent/CN203699908U/en not_active Withdrawn - After Issue
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708426A (en) * | 2014-01-08 | 2014-04-09 | 石祖嘉 | Device for producing hydrogen peroxide by adopting anthraquinone process |
| CN103708426B (en) * | 2014-01-08 | 2015-07-29 | 石祖嘉 | Anthraquinone oxydol production apparatus |
| CN104098475A (en) * | 2014-07-28 | 2014-10-15 | 淮安嘉诚高新化工股份有限公司 | Device and method for producing diaminotoluene (TDA) by continuous liquid phase catalysis hydrogenation reduction of dinitrotoluene (DNT) |
| CN104098474A (en) * | 2014-07-28 | 2014-10-15 | 淮安嘉诚高新化工股份有限公司 | Device and method for producing methyl aniline through performing continuous liquid-phase catalytic hydrogenation reduction on nitrotoluene |
| CN104098474B (en) * | 2014-07-28 | 2016-01-20 | 淮安嘉诚高新化工股份有限公司 | Nitrotoluene Continuous Liquid Phase catalytic hydrogenating reduction produces the device and method of monomethylaniline |
| CN106629618A (en) * | 2017-01-03 | 2017-05-10 | 河北美邦工程科技股份有限公司 | Fluidized bed hydrogenation reaction and separation process and device for producing hydrogen peroxide by virtue of anthraquinone method |
| CN106629618B (en) * | 2017-01-03 | 2019-05-10 | 河北美邦工程科技股份有限公司 | Fluidized-bed hydrogenation reaction and separating technology and the device of a kind of hydrogen dioxide solution production by anthraquinone process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103708426B (en) | Anthraquinone oxydol production apparatus | |
| CN103936559B (en) | The method of continuous prodution Resorcinol | |
| CN203699908U (en) | Anthraquinone process hydrogen peroxide production device | |
| CN103613126B (en) | A kind of method and system removing vanadium impurity from titanic tetrachloride | |
| CN103663385B (en) | A kind of method and apparatus producing hydrogen peroxide | |
| CN104098474B (en) | Nitrotoluene Continuous Liquid Phase catalytic hydrogenating reduction produces the device and method of monomethylaniline | |
| CN106629622A (en) | Hydrogenation method and hydrogenation device for oxanthranol-containing working solution | |
| CN104130216A (en) | Process for continuously producing epoxy propane through propylene and propane mixed gas directly oxidized by hydrogen peroxide | |
| CN206616014U (en) | A kind of hydrogenation apparatus of hydrogeneous anthraquinone working solution | |
| CN206814394U (en) | A kind of anthraquinone legal system hydrogen peroxide two phase countercurrent flow contact type high-efficiency aoxidizes tower reactor | |
| CN204865839U (en) | Nitrobenzene liquid -phase hydrogenatin system aniline reaction unit | |
| CN106479562B (en) | A kind of dissolving method and application for strengthening hydrogen in reformed oil | |
| CN204342435U (en) | The hydrogenation fluidized-bed reactor of anthraquinone legal system hydrogen peroxide | |
| CN102285861B (en) | Reaction device for preparing cyclohexene by heterogeneous catalysis of selective hydrogenation of benzene with liquid phase method | |
| CN108640838A (en) | A kind of apparatus and method of continuous production dibutyl phthalate | |
| CN204211485U (en) | Hydrogen peroxide production system | |
| CN107056670A (en) | A kind of preparation method of two tertiary base peroxide | |
| CN202860529U (en) | Reaction device for producing cyclohexene by partial hydrogenation of benzene | |
| CN207413365U (en) | Formaldehyde produces the gas-solid phase reactor of polymethoxy dimethyl ether with dimethoxym ethane reaction | |
| CN111151201A (en) | Reaction device and system and method for synthesizing acetic acid by methanol carbonylation | |
| CN203625266U (en) | Ammoximation reactor | |
| CN214634626U (en) | System for be used for cyclohexyl hydrogen peroxide to decompose and separate | |
| CN205556513U (en) | Continuous hydrogenation ware of organic intermediate | |
| CN101759534A (en) | Formaldehyde prepration process and device | |
| CN202047018U (en) | Device for preparing cyclohexene from benzene through selective hydrogenation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140709 Effective date of abandoning: 20150729 |
|
| RGAV | Abandon patent right to avoid regrant |