CN104437287A - Reaction apparatus - Google Patents
Reaction apparatus Download PDFInfo
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- CN104437287A CN104437287A CN201310430805.5A CN201310430805A CN104437287A CN 104437287 A CN104437287 A CN 104437287A CN 201310430805 A CN201310430805 A CN 201310430805A CN 104437287 A CN104437287 A CN 104437287A
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- reaction unit
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 64
- 239000000463 material Substances 0.000 claims abstract description 67
- 239000000047 product Substances 0.000 claims description 19
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000003756 stirring Methods 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 5
- 239000007795 chemical reaction product Substances 0.000 claims description 3
- 239000012774 insulation material Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 abstract description 4
- 238000010586 diagram Methods 0.000 description 8
- 239000007789 gas Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 239000000126 substance Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 230000005855 radiation Effects 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 229920000426 Microplastic Polymers 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012075 bio-oil Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003086 colorant Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/18—Stationary reactors having moving elements inside
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00277—Apparatus
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00761—Details of the reactor
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
The invention discloses a reaction apparatus. The reaction apparatus comprises at least one sub-reactor used for a reaction of a material, a main reactor connected with the at least one sub-reactor and used for mixing a product, and a first forced circulation device used for circulating the product and the material between the main reactor and the sub-reactor, wherein the volume of the sub-reactor is smaller than the volume of the main reactor. The reaction apparatus is formed by combining a plurality of small reactors with the main reactor, effectively accelerates the mass and heat conduction, and increases the reaction efficiency.
Description
Technical field
The present invention relates to the reaction unit used in chemical industry.
Background technology
The scale and benefit of chemical industry cause chemical enterprise scale day huger, and single machine yield day more increases.For reactor the most frequently used in chemical enterprise, from the 1m in past
3~ 5m
3develop into 10m
3~ 100m
3, there is a problem that must solve in the continuous increase of reactor, that is exactly that quality in reactor and heat transmit unbalanced caused reaction mass and decline.Such as Large Copacity reactor, especially need to heat to sticky material, the outer heating mode of traditional reactor wall, such as electricity heating or steam are heated, and are easy to cause formation temperature skewness in large-scale reactor, thus cause reaction efficiency to decline.Even if install stirring additional in large-size reactor, be still difficult to reach being uniformly distributed of temperature and quality, easily occur dead angle.
Summary of the invention
The object of the invention is to provide a kind of reaction unit, to meet the requirement of quality and homogeneous temperature distribution in large-scale reactor.
For this reason, the invention provides a kind of reaction unit, the main reactor mixed for product that at least one the sub-reactor comprised for material reaction is connected with at least one sub-reactor and the first forced circulation device circulated between main reactor and sub-reactor for product and material, wherein, the volume of sub-reactor is less than the volume of main reactor.
Further, the quantity of above-mentioned at least one sub-reactor is two or more, and is satellite-type arrangement around main reactor.
Further, above-mentioned in main reactor and at least one sub-reactor, at least one sub-reactor is provided with device material being carried out to selective heating, heat radiation and/or stirring, and main reactor is the reactor of insulation material is housed or has the reactor of heat sinking function.
Further, above-mentioned reaction unit also comprises the gas-phase product treating apparatus be connected with main reactor top.Gas-phase product can be separated by the difference of boiling point.
Further, the above-mentioned first forced circulation device paddle that is product pump and/or arranges in sub-reactor.
Further, above-mentioned main reactor comprises vessel, is positioned at the discharge nozzle of vessel bottom and is positioned at the feed pipe on vessel top, and wherein, the material inlet of sub-reactor is connected with discharge nozzle, and the material outlet of sub-reactor is connected with feed pipe.
Further, the top of above-mentioned main reactor and/or the bottom of sub-reactor have the feed(raw material)inlet added for raw material, and the bottom of main reactor has end product outlet.
Further, above-mentioned sub-reactor and the main shaft both main reactor are arranged in parallel or the main shaft of the two has the angle that is less than or equal to 45 °.
Further, above-mentioned at least one sub-reactor is the sub-reactor of one-level, the second forced circulation device that the sub-reactor of one-level also comprises the sub-reactor of at least one secondary and circulates between the sub-reactor of one-level and the sub-reactor of secondary for material.
Further, the material inlet of above-mentioned sub-reactor is positioned at the core of main reactor and the material outlet of sub-reactor is connected with main reactor with tangential way; Or the material inlet of sub-reactor to be connected with main reactor with tangential way and the material outlet of sub-reactor is positioned at the core of main reactor.
Reaction unit of the present invention is combined with a main reactor by multiple small-sized reactor and effectively accelerates the conduction of quality and heat, thus improve reaction efficiency.This reactor of the present invention can be used for the specific course of reaction of some large-scale plastics industries, petrochemical industry, biochemical industry.
Except object described above, feature and advantage, other object, feature and advantage that the present invention has, will be described in further detail by reference to the accompanying drawings.
Accompanying drawing explanation
Forming the part of this description, showing the preferred embodiments of the present invention for understanding accompanying drawing of the present invention further, and be used for principle of the present invention is described together with description.In figure:
Fig. 1 is the structural representation of the first embodiment according to reaction unit of the present invention;
Fig. 2 is the structural representation of the main reactor according to reaction unit of the present invention;
Fig. 3 a is the schematic diagram of the first layout type of sub-reactor according to reaction unit of the present invention;
Fig. 3 b is the schematic diagram of the second layout type of sub-reactor according to reaction unit of the present invention;
Fig. 4 a is the schematic diagram of normal pressure reactor according to the sub-reactor of reaction unit of the present invention;
Fig. 4 b is the structural representation of voltage-resistant reactor according to the sub-reactor of reaction unit of the present invention;
Fig. 5 is the schematic diagram of the third layout type of sub-reactor according to reaction unit of the present invention;
Fig. 6 is the structural representation of the second embodiment according to reaction unit of the present invention;
Fig. 7 a is the schematic diagram of the first arrangement of the material import and export of sub-reactor according to reaction unit of the present invention;
Fig. 7 b is the schematic diagram of the second arrangement of the material import and export of sub-reactor according to reaction unit of the present invention,
Fig. 8 a is the schematic diagram be connected with destilling tower according to the main reactor of reaction unit of the present invention; And
Fig. 8 b is the schematic diagram be connected with condensing tower according to the main reactor of reaction unit of the present invention.
Description of reference numerals
10, main reactor; 20, sub-reactor;
11, feed pipe; 12, discharge nozzle;
26, material outlet; 24, pump;
21, motor; 23, paddle;
26, material inlet; 25, material outlet;
24, product pump; 26, material inlet;
30, rectifying column 40, the sub-reactor of secondary;
The main shaft of 10a, main reactor; The main shaft of 20a, sub-reactor.
Detailed description of the invention
Below in conjunction with accompanying drawing, embodiments of the invention are described in detail, but the multitude of different ways that the present invention can be defined by the claims and cover is implemented.
The industrial process conditions that the present invention is suitable for: A, be applicable to volume and be greater than 5m
3large-scale or ultra-large type reaction system, with 10m
3~ 100m
3for good; B, reaction mass are thick liquid or the thick liquid containing solia particle, and its viscosity is minimum should at normal temperatures higher than 20000 centistokes (Centistokes-Cst), and what material viscosity was most concentrates on 50000 ~ 300000Cst; The temperature range of C, reaction: normal temperature ~ 400.C; The pressure limit of reaction is: normal pressure ~ 10MPa; D, reaction can be liquid-liquid, liquid-solid two reactions or gas-liquid-solid, liquid-three, liquid-gas reaction.
As shown in Figure 1, in figure, the surrounding of main reactor 10 is multiple sub-reactors 20 to the schematic structure of reaction unit of the present invention, and the top of main reactor 10 is rectifying column 30.Raw material and catalyst feed postition have three selections, and first, add by bottom sub-reactor 20; The second, added by the top of main reactor 10; Three, simultaneously bottom sub-reactor 20 and the top of main reactor 10 add.Material enters sub-reactor from the bottom of main reactor, in sub-reactor, push main reactor after reaction by the top of sub-reactor, and forms circulation.The time of staying of material in sub-reactor can require according to different reactions and determine.In a preferred embodiment, reaction unit of the present invention is also referred to as satellite-type polyfunctional reactant device.
Sub-reactor is the same with general reactor, can complete all functions that single reactor has, such as, react, stir, pressurize, heat or heat sinking function etc.Gaseous product is separated and enters rectifying column in main reactor.The function of main reactor is that the Homogeneous phase mixing of product is separated and release with the rapid of gas phase in product.Product and material repeatedly run between main reactor and sub-reactor.Gaseous product is separated by boiling spread in the rectifying column connected with main reactor.Bottom by main reactor is taken out by end-product.
The schematic structure of main reactor as shown in Figure 2, is cylindrical in the middle part of main reactor 10, and bottom is circular arc and has discharging opening 13, and top is the funnel-shaped structure of back-off, to connect rectifying column 30.There is the pipeline 11,12 of two connexon reactors the side of the cylindrical part of main reactor 10.The pipeline 12 that the pipeline 11 being positioned at cylindrical upper section is feed pipe and cylindrical lower portion is discharge nozzle.The function of main reactor is solid-liquid or the mixed uniformly space of liquid liquid material and rapid separation and the release making gas phase in material.Main reaction due to volume huge, therefore the functions such as agitating heating are not set, but for the reaction having heating or heat radiation to have requirement, main reactor should have good insulation or cooling settings.
Preferably, the blade diameter length ratio of main reactor is: blade diameter length ratio=D/H=0.6 ~ 1.0, and wherein, D is reactor diameter, and H is reactor effective depth.
Sub-reactor is satellite-type arrangement round main reactor.The quantity of sub-reactor be 2 ~ 10 even more, as shown in Figure 3 a, the quantity of sub-reactor is three, and as shown in Figure 3 b, the quantity of sub-reactor is 5.The quantity of sub-reactor and volume depend on the volume of main reactor, material and reaction property, and such as react fierce, need fast heating, heat radiation or stirring, then the quantity of sub-reactor is more, and the volume ratio of main reactor antithetical phrase reactor should be larger.The time that material can be made like this to stop in sub-reactor is few.Generally speaking, sub-reactor volume/main reactor volume=5% ~ 20%.
In one embodiment, sub-reactor volume/main reactor volume=8%, the quantity of sub-reactor is 5, in another embodiment, sub-reactor volume/main reactor volume=15%, the quantity of sub-reactor is 3, in another embodiment, sub-reactor volume/main reactor volume=15%, the quantity of sub-reactor is 6.
In conjunction with reference Fig. 1, Fig. 2, Fig. 3 a and Fig. 3 b, material continuous print flows into sub-reactor from the pipeline 12 of the bottom of main reactor, stirs and push the pipeline 11 on top and discharge material through stirrer paddle, forms circulation.The circulation of this material is stirred oar or independent pump has been forced, and this forced circulation impels all even homogeneous heating of mixing of materials in main reactor.Sub-reactor bottom is provided with fresh feed and adds entrance (as shown in Figure 1), especially when need to add the material of heterogeneity and needs constantly adjustment various material ratio time, add the mode of material from sub-reactor, just seem more convenient.Such as mixing and when needing constantly to mix colours at multiple color, different plastic pellets can be inputted from every sub-reactor, adjust each sub-reactor add material number, i.e. adjustable overall color.
Sub-reactor has two kinds of design alternatives.The first is selected, and sub-reactor is that (gauge pressure <1bar as shown in fig. 4 a), has heating, (or insulation or cooling), the function that stirs and carry to normal pressure.The material outlet 25 of sub-reactor should be located at a little more than or the upper surface of the reactant in main reactor that maintains an equal level.The second select, sub-reactor be pressure-resistant equipment (gauge pressure <10bar, as shown in Figure 4 b).Pressure can be produced by reaction or produce pressure by product pump 24 when pressurized delivered material.Material is for the sub-reactor with pressure, and sub-reactor content outlet 25 should enter main reactor with tangential direction and exceed the liquid level at least 20cm of main reactor, thus plays the effect of flash distillation.For the sub-reactor (as shown in Figure 4 b) having pressure, when material enters main reactor from sub-reactor, earth pressure release, completes circulation and flash distillation double process.Flash distillation can make gas be separated rapidly, avoids producing unwanted side reaction.
The annexation of sub-reactor and main reactor is shown in Figure 4, and as shown in Figure 4, sub-reactor 20 is connected with the side of main reactor 10 cylindrical part.Every sub-reactor has a vertical agitating device to comprise motor 21 and paddle 23.22 is insulation material or heater or cooling device, determines according to the reaction of reality and requirement.The material inlet 26 of sub-reactor is generally arranged on the bottom of main reactor and the material outlet 25 of sub-reactor is located at the top of sub-reactor.The circulation of material between two reactors mainly relies on the combination of the paddle 23 or paddle 23 and product pump 24 with thrust to realize, and this forced circulation impels material and uniform heat distribution in main reactor.
If material needs the longer time of staying in sub-reactor, regulate the rotating speed of the capacity of sub-reactor, length and paddle or pump, the requirement of reaction to the time of staying can be met.Such as, sub-reactor in fig. 4b, advances and stirs independent control, thus can meet the requirement of different material to reaction condition.
Sub-reactor and main reactor also have two kinds of mounting means.The first selection is that sub-reactor is parallel with main reactor, as shown in figures 4 a and 4b.If during the height limitation of the main reactor length of sub-reactor, the second can be adopted to select, namely sub-reactor is installed with certain angular slope, and as shown in Figure 5, its main shaft 20a and main reactor 10a main shaft are an angle being not more than 450.
When main reactor has 100m
3during above ultra-large type capacity, sub-reactor can be excessive, even affects reaction efficiency, therefore, can be arranged to secondary satellite-type reaction unit, and its horizontal layout preferably as shown in Figure 6.
For the material of comparatively thickness, in order to make not occur material dead band in main reactor, the material inlet 26 of sub-reactor can have the layout of various ways.Fig. 7 a and Fig. 7 b shows the citing of two kinds of arrangements.In figure 7 a, sub-reactor content entrance 26 is positioned at the core of main reactor, and material outlet 25 is then connected with main reactor with tangential way.During operation, in main reactor, material liquid surface is the high swirling of middle low surrounding, and the increase of liquid level area and the depression of core, be conducive to the effusion of gas in material.In fig .7b, it is contrary that its material import and export is arranged with shown in Fig. 7 a, and material outlet 25 is positioned at the core of reactor and material inlet 26 is connected with main reactor with tangential way.This kind is furnished with and is beneficial to solid particle in material or heavy constituent and sinks the bottom centre staying main reactor.
The top of main reactor directly connects the condenser or the rectifying column that produce gas in a processing reaction.When the gas phase in reacting also is object product, the mode of this direct connection is by the highest efficiency of acquisition and yield.The height of condenser and rectifier is between 2m ~ 20m, if in the gas-phase product of reaction, what can be obtained by condensation is only 1 ~ 2 kind of component, only needs can reach target with 1 ~ 2 grade of condenser series connection.If reaction gas phases is multicomponent product, then need to carry out distilling or rectifying.Such as vapor-phase reactant is oil gas, then main reactor top directly can connect column plate type or the material filling type rectifying column that is only had rectifying section.Rectifying, destilling tower or condenser have ripe design and running experience, be directly installed on main reactor, to reach the special requirement of reaction, wherein, Fig. 8 a schematically shows above main reactor and is connected with destilling tower, and Fig. 8 b schematically shows the connection with condensing tower above main reactor.
Embodiment
Design the reactor that is produced per year 1000 tons of bio oil.For meeting the demands, the volume requirement of main reactor is 15m
3, the diameter of the cylindrical part of main reactor is 2500mm is highly 3000mm; 5 sub-reactors are connected with main reactor, and the diameter of every sub-reactor is 1200mm, is highly 2000mm.The volume of sub-reactor is 2.26m
3.The time of staying of material in the sub-reactor of separate unit is 0.15 hour, and when 5 estrade reactions work simultaneously, in main reactor, the cycle-index of material is 6.25 times/hour.Calculating simulation result shows, reactor when being heated to 320 DEG C, temperature being evenly distributed in main reactor and sub-reactor.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. a reaction unit, it is characterized in that, the main reactor mixed for product that at least one the sub-reactor comprised for material reaction is connected with described at least one sub-reactor and the first forced circulation device circulated between described main reactor and described sub-reactor for product and material, wherein, the volume of described sub-reactor is less than the volume of described main reactor.
2. reaction unit according to claim 1, is characterized in that, the quantity of described at least one sub-reactor is two or more, and is satellite-type arrangement around described main reactor.
3. reaction unit according to claim 1, it is characterized in that, in described main reactor and described at least one sub-reactor, only described at least one sub-reactor is provided with device material being carried out to selective heating and/or stirring, and described main reactor is the reactor of insulation material is housed or has the reactor of heat sinking function.
4. reaction unit according to claim 1, is characterized in that, also comprises the gas-phase product treating apparatus be connected with described main reactor top.
5. reaction unit according to claim 1, is characterized in that, the paddle that described first forced circulation device is product pump and/or arranges in described sub-reactor.
6. reaction unit according to claim 1, it is characterized in that, described main reactor comprises vessel, is positioned at the discharge nozzle of described vessel bottom and is positioned at the feed pipe on described vessel top, wherein, the material inlet of described sub-reactor is connected with described discharge nozzle, and the material outlet of described sub-reactor is connected with described feed pipe.
7. reaction unit according to claim 1, is characterized in that, the top of described main reactor and/or the bottom of sub-reactor have the feed(raw material)inlet added for raw material, and the bottom of described main reactor has end product outlet.
8. reaction unit according to claim 1, is characterized in that, the main shaft of described sub-reactor and described both main reactors is arranged in parallel or the main shaft of the two has the angle that is less than or equal to 45 °.
9. reaction unit according to claim 1, it is characterized in that, described at least one sub-reactor is the sub-reactor of one-level, the second forced circulation device that the sub-reactor of described one-level also comprises the sub-reactor of at least one secondary and circulates between the sub-reactor of described one-level and the sub-reactor of described secondary for material.
10. reaction unit according to claim 1, is characterized in that, the material inlet of described sub-reactor is positioned at the core of described main reactor and the material outlet of described sub-reactor is connected with main reactor with tangential way; Or the material inlet of described sub-reactor to be connected with main reactor with tangential way and the material outlet of described sub-reactor is positioned at the core of described main reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310430805.5A CN104437287A (en) | 2013-09-18 | 2013-09-18 | Reaction apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310430805.5A CN104437287A (en) | 2013-09-18 | 2013-09-18 | Reaction apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104437287A true CN104437287A (en) | 2015-03-25 |
Family
ID=52884499
Family Applications (1)
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|---|---|---|---|
| CN201310430805.5A Pending CN104437287A (en) | 2013-09-18 | 2013-09-18 | Reaction apparatus |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109306272A (en) * | 2017-07-27 | 2019-02-05 | 郑莹 | Heavy-oil hydrogenation processing system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000002933A1 (en) * | 1998-07-10 | 2000-01-20 | S.C. Johnson Commercial Markets, Inc. | Process for producing polymers by free radical polymerization and condensation reaction, and apparatus and products related thereto |
| CN2367383Y (en) * | 1998-10-30 | 2000-03-08 | 山东省化工规划设计院 | Gas-liquid reactor |
| CN102030348A (en) * | 2010-10-15 | 2011-04-27 | 北京化工大学 | Device and method for continuously preparing magnesium hydroxide flame retardant |
| CN202898291U (en) * | 2012-09-25 | 2013-04-24 | 中国石油化工股份有限公司 | PBT (polybutylece terephthalate) esterification device |
| CN203484148U (en) * | 2013-09-18 | 2014-03-19 | 郑莹 | Reaction device |
-
2013
- 2013-09-18 CN CN201310430805.5A patent/CN104437287A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000002933A1 (en) * | 1998-07-10 | 2000-01-20 | S.C. Johnson Commercial Markets, Inc. | Process for producing polymers by free radical polymerization and condensation reaction, and apparatus and products related thereto |
| CN2367383Y (en) * | 1998-10-30 | 2000-03-08 | 山东省化工规划设计院 | Gas-liquid reactor |
| CN102030348A (en) * | 2010-10-15 | 2011-04-27 | 北京化工大学 | Device and method for continuously preparing magnesium hydroxide flame retardant |
| CN202898291U (en) * | 2012-09-25 | 2013-04-24 | 中国石油化工股份有限公司 | PBT (polybutylece terephthalate) esterification device |
| CN203484148U (en) * | 2013-09-18 | 2014-03-19 | 郑莹 | Reaction device |
Non-Patent Citations (1)
| Title |
|---|
| 潘传九: "《化工设备机械基础》", 31 January 2007, article "反应设备", pages: 29-32 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109306272A (en) * | 2017-07-27 | 2019-02-05 | 郑莹 | Heavy-oil hydrogenation processing system |
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