CN1327874A - Synthesizing slurry-bed reactor - Google Patents
Synthesizing slurry-bed reactor Download PDFInfo
- Publication number
- CN1327874A CN1327874A CN 01118470 CN01118470A CN1327874A CN 1327874 A CN1327874 A CN 1327874A CN 01118470 CN01118470 CN 01118470 CN 01118470 A CN01118470 A CN 01118470A CN 1327874 A CN1327874 A CN 1327874A
- Authority
- CN
- China
- Prior art keywords
- reactor
- riser
- comer
- catalyst
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 230000002194 synthesizing effect Effects 0.000 title abstract description 3
- 238000006243 chemical reaction Methods 0.000 claims abstract description 50
- 239000002002 slurry Substances 0.000 claims description 22
- 238000012546 transfer Methods 0.000 abstract description 9
- 239000000126 substance Substances 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 120
- 239000003054 catalyst Substances 0.000 description 36
- 230000015572 biosynthetic process Effects 0.000 description 26
- 238000003786 synthesis reaction Methods 0.000 description 26
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 20
- 230000018044 dehydration Effects 0.000 description 18
- 238000006297 dehydration reaction Methods 0.000 description 18
- 238000000034 method Methods 0.000 description 15
- 239000002904 solvent Substances 0.000 description 15
- 230000000694 effects Effects 0.000 description 9
- 238000013461 design Methods 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 239000007788 liquid Substances 0.000 description 6
- 239000000376 reactant Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 230000016507 interphase Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000005587 bubbling Effects 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 239000008187 granular material Substances 0.000 description 3
- 238000010907 mechanical stirring Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000012808 vapor phase Substances 0.000 description 3
- 230000001143 conditioned effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A synthesizing slurry-bed reactor is composed of lifting pipe, down-flow pipe, gas distributor and stirrer. The top and bottom ends of said lifting pipe are communicated to the top and bottom ends of down-flow pipe. Its gas distributor is at lower part of lifting pipe. said stirrer is at upper part of down-flow pipe. Controlling circulation speed can regulate the stay time of reaction substance in reactor, improve the breaking and disperson of bubbles, increase air content, and improve mass transfer between phases.
Description
The present invention relates to a kind of slurry attitude bed synthetic reaction device, be applicable to the novel pulpous bed synthetic reaction device that reaction is subjected to mass transfer, conducts heat and influence, belong to the field of engineering technology in the chemical engineering process.Especially, the present invention is applicable to having in the presence of the solvent, is produced the course of reaction of methyl alcohol or dimethyl ether by the synthesis gas liquid phase method.
Produce methyl alcohol and dimethyl ether by synthesis gas, comprise following chemical reaction: the methyl alcohol synthetic reaction
-90.4kJ/mol (1) water gas shift reaction
-41.0kJ/mol (2) Dehydration of methanol
-23.0.0kJ/mol (3)
More than the general vapor phase method that adopts of reaction carries out in fixed bed reactors.Reaction temperature is 200-300 ℃, and pressure 5.0-15MPa reacts and is strong exothermal reaction.Move heat problem for solving reaction, synthesis gas will circulate and compress in a large number, and recycle ratio is up to 5-10, makes that the conversion per pass of CO is very low in the building-up process, and has also increased equipment investment and energy consumption greatly.Simultaneously, because H
2Thermal capacitance reach the easy coking and deactivation of catalyst more greatly, use higher H
2The synthesis gas of/CO ratio.
For solving the problem of above-mentioned existence, can use a kind of atent solvent as moving thermal medium, adopt paste state bed reactor to replace fixed bed reactors, carry out liquid phase method and synthesize.In slurry attitude system, because the thermal capacitance of liquid phase solvent is big, liquid phase method is easy to realize constant temperature method.Utilize liquid phase as moving thermal medium, avoided the circulation compression of a large amount of synthesis gas in the vapor phase method, reduced energy consumption, make synthesis gas can reach higher conversion per pass.Because of using much smaller heat exchange area, realize the heat exchange of liquid phase and reaction system, make that the reactor manufacturing is simple on the one hand, can utilize reaction heat to produce middle pressure steam easily on the other hand, the energy utilization efficiency height.
In the three phase slurry bed application process, at present more is three phase slurry bubbling bed and mechanical stirring kettle.To in the bubbling bed, realize good dispersion and mixed effect, improve mass-transfer efficiency, need the higher turbulence of air speed to promote that it is inner, but shortened the time of staying of reactant in reactor, the utilization rate of catalyst reduces, and reacts complete inadequately, and then has reduced conversion ratio.Mechanical stirring kettle can be realized turbulence effect preferably, but because the limitation of himself is mainly used in laboratory research at present, is difficult to carry out industry and amplifies.And directly produce the dimethyl ether building-up process for similar synthesis gas, use the synthetic and two kinds of catalyst of methanol dehydration of the different methyl alcohol of active temperature.The general serviceability temperature 220-280 of methanol synthesis catalyst ℃, and the methanol dehydration catalyst serviceability temperature is generally about 280 ℃.In use, two kinds with the catalyst of equigranular by a certain percentage, adopts physical mixed, and the reactor of packing into is with solvent mutual group pulping attitude system.Because the easy inactivation of methanol synthesis catalyst high temperature, reaction must be carried out under the suitable temperature of methanol dehydration catalyst, therefore Dehydration of methanol speed can be low slower because of reaction temperature, and rate of water loss can limit the conversion ratio of entire reaction in the course of reaction of reality like this.
The objective of the invention is to design a kind of slurry attitude bed synthetic reaction device, make reaction system under lower air speed, also can obtain higher dispersion and mixed effect.The present invention mainly combines the characteristics of type of reactor such as bubbling bed, mechanical stirring kettle, three-phase circulating fluidized bed and circulation flow reactor, adopts paddle or circulating pump to make to produce in the reactor to circulate.One can improve its conversion ratio by the control circulation rate conditioned reaction time of staying of thing in reactor; Two can also strengthen the broken and dispersion of bubble by circulation, and bubble diameter is reduced, and gas holdup increases, and improves the interphase mass transfer in the slurry reactor; Three can use two kinds of varigrained solid particles, and the bubble crushing effect that utilizes bulky grain to deposit to play further increases gas-liquid interphase mass transfer area, improves interphase mass transfer.
The slurry attitude bed synthetic reaction device of the present invention's design, comprise riser, down-comer, gas distributor and agitator, the upper and lower end of riser wherein is connected with the upper and lower end of down-comer respectively, and gas distributor is located at the bottom of riser, and agitator is located at the top of down-comer.
The another kind of structure of the slurry attitude bed synthetic reaction device of the present invention's design is: reaction unit comprises riser, down-comer, gas distributor and circulating pump, the upper and lower end of riser wherein is connected with the upper and lower end of down-comer respectively, the lower end of riser is connected with down-comer by circulating pump, and gas distributor is located at the bottom of riser.
The slurry attitude bed synthetic reaction device of the present invention's design, to be used for the synthetic process of one-step method dimethyl ether is example, has following advantage, as shown in Figure 1, use varigrained methanol synthesis catalyst and methanol dehydration catalyst, with the ciculation fluidized system of the two particles of the solvent composition of inertia.Wherein methanol synthesis catalyst is a bulky grain, is decentralized photo, the fluid bed traditional with solvent composition.Methanol dehydration catalyst is a granule, forms the plan homogeneous phase with solvent, forms ciculation fluidized system.And by regulating cycle rate, can make oarse-grained methanol synthesis catalyst only be present in the lifting area under control of reactor, and not flow into the decline area under control; Short grained methanol dehydration catalyst then with the plan homogeneous phase of solvent composition, in whole reactor, circulate.Can make methanol synthesis catalyst and methanol dehydration catalyst under the active temperature that itself is suited, carry out catalytic reaction respectively by the reaction temperature of control reactor both sides like this, thereby further improve the conversion ratio of reaction.Oarse-grained in addition existence can also be played the effect of bubble crushing, has increased gas-liquid interphase mass transfer area.It is low so just to have overcome traditional paste state bed reactor mass-transfer efficiency, and two kinds of problems that the catalyst serviceability temperature does not match and brought.
Description of drawings:
Fig. 1 is the structural representation of the reaction unit that designs of the present invention.
Fig. 2 is the another kind of structural representation of this reaction unit.
Fig. 3 is the upper end of riser in the reaction unit and the another kind of frame mode of down-comer.
Below in conjunction with accompanying drawing, introduce content of the present invention in detail.
As shown in Figure 1, the slurry attitude bed synthetic reaction device of the present invention's design, comprise riser 1, down-comer 2, gas distributor 4 and agitator 5, the upper and lower end of riser 1 wherein is connected with the upper and lower end of down-comer 2 respectively, gas distributor 4 is located at the bottom of riser 1, and agitator 5 is located at the top of down-comer 2.
The another kind of structure of the slurry attitude bed synthetic reaction device of the present invention's design is: reaction unit comprises riser 1, down-comer 2, gas distributor 4 and circulating pump 6, the upper and lower end of riser 1 wherein is connected with the upper and lower end of down-comer 2 respectively, the lower end of riser 1 is connected with down-comer 2 by circulating pump 6, and gas distributor 4 is located at the bottom of riser 1.
The course of work of this reaction unit is as described below: vapor-phase reactant is introduced by the bottom of reactor, enter the lifting area under control 1 of reactor through gas distributor 4, in this zone, there are two kinds of varigrained catalyst, be methanol synthesis catalyst and methanol dehydration catalyst for the one-step method dimethyl ether is synthetic, wherein methanol synthesis catalyst is a bulky grain, the about 0.2-1.0mm of granularity, be decentralized photo, the fluid bed traditional with solvent composition.Methanol dehydration catalyst is a granule, and the about 30-100 of granularity m forms the plan homogeneous phase with solvent.The temperature that promotes area under control 1 can be controlled at 220-280 ℃, is the active temperature of methanol synthesis catalyst, carries out the synthetic and Dehydration of methanol of methyl alcohol simultaneously.Simultaneously, oarse-grained existence can be played the effect of bubble crushing, makes the size of bubble become littler, improves gas holdup, has increased gas-liquid mass transfer area.
At gas-liquid separation zone 3, the unreacted reactant of gas-phase product and part is separated with the slurry attitude and takes out from reactor head as product, and another part unreacted reactant completely then is brought into down-comer 2.Design different internal structures and can obtain different gas-liquid separation effects, can guarantee simultaneously that granule can be brought down-comer into and bulky grain is retained in the riser 1.To bring the gas flow in the down-comer 2 into and prevent that bulky grain from entering down-comer 2 in order to control, can adopt Fig. 1 or structure shown in Figure 3, control in conjunction with the air speed in the conditioned reaction device.The top of gas-liquid separation zone 3 is provided with the gaseous products outlet, and in the running of reactor, atent solvent can lose gradually, therefore also is provided with the liquid phase inlet at the top of reactor, is used for supplementing solvent.
The intermediate product methyl alcohol that enters down-comer 2 dewaters under the effect of catalyst particle and generates the product dimethyl ether.The temperature of one's respective area is controlled at 250-320 ℃, is the active temperature zone of dehydration catalyst, mainly carries out Dehydration of methanol.This just can solve two kinds of unmatched problems of catalyst serviceability temperature to a certain extent, and every kind of catalyst can both be worked under its optimum active temperature.
Because gas feeds from riser 1 one sides, cause the difference of gas holdup in riser 1 and the down-comer 2, and then caused the difference of both sides density, thereby produced circulating in the reactor, this is the basic principle of Airlift circulating reactor.When the air inlet air speed of reactant was big, the effect of gas lift just can the interior good circulation of realization response device; When the air inlet air speed of reactant hour only relies on gas lift possibly can't guarantee circulating in the whole reactor, can adopt the way of forced circulation to realize this moment, and can control the gas flow of bringing down-comer into by the intensity that changes forced circulation, this moment, system just became the reactor that gas lift combines with forced circulation.The implementation method of forced circulation also has multiple, and Fig. 1 and Fig. 2 are two examples of the present invention.Fig. 1 adopts the way that adds a pusher paddle 5 at the down-comer top to come the logistics in the driving a reaction device to circulate.In order to improve near the flow condition the paddle, eliminate the phenomenon of turning round and round, inner members such as baffle plate need be installed near the tube wall the paddle, flow the motive force of enhancing axial flow to destroy its hoop.Fig. 2 adopts the method that installs circulating pump 6 in reactor additional to realize forced circulation.
Introduce embodiments of the invention below.
Embodiment 1: synthesis of dimethyl ether with synthesis gas one-step
Adding a kind of high boiling atent solvent in reactor, can be atoleine.A kind of short grained methanol synthesis catalyst of 1 filling in the reactor riser district then, the about 0.5-1.0mm of granularity adds a kind of oarse-grained methanol dehydration catalyst again, the about 30-50 of granularity m, and catalyst carried out preliminary treatment.
The weight ratio of catalyst and atent solvent is 5-60%, and synthesis gas is formed H
2/ (CO+CO
2)=1: 1-4: 1, enter reactor riser district 1 by tower pucking bubble after compressed, the heat exchange.Methanol dehydration catalyst is formed slurries with solvent, carries out forced circulation by agitator 5 or slurry attitude pump 6; Synthesis gas is on the slurries and the flow direction, cycle rate by the control slurries, keep the fluidized state of bulky grain methanol synthesis catalyst in the reactor riser district 1, and make oarse-grained methanol synthesis catalyst only be present in lifting area under control 1, and do not enter decline area under control 2.
Reaction temperature is controlled to be lifting area under control 1 and is 220-280 ℃, carries out the synthetic and Dehydration of methanol generation dimethyl ether of methyl alcohol simultaneously.Dehydration of methanol is mainly carried out for 250-320 ℃ in decline area under control 2.Whole reactor internal pressure 30-100MPa, the synthesis gas air speed is 1000-10000h
-1Slurries are carried the decline area under control 2 that a spot of gas enters reactor secretly after rising to reactor head by 1 bottom, reactor riser district, proceed reaction.By the control heat-obtaining, when slurries loop back reactor riser district 1, make slurry temperature reduce to 220-280 ℃.Dimethyl ether and small amount of methanol that reaction generates, the CO conversion per pass can reach 80-95%, and the dimethyl ether selectivity is greater than 90%.Embodiment 2: the synthesis gas synthesizing methanol
Only in reactor, dose methanol synthesis catalyst.Catalyst can be the individual particle system, also constitutes two granular systems by self or with varigrained inert particle, and temperature is controlled to be 220-280 ℃ in the whole reactor.All the other conditions are with embodiment 1.Get CO conversion per pass 40-80%, the methyl alcohol selectivity is greater than 95%.
Claims (2)
1, a kind of slurry attitude bed synthetic reaction device is characterized in that this device comprises riser, down-comer, gas distributor and agitator; The upper and lower end of described riser is connected with the upper and lower end of down-comer respectively, and gas distributor is located at the bottom of riser, and agitator is located at the top of down-comer.
2, a kind of slurry attitude bed synthetic reaction device is characterized in that this reaction unit comprises riser, down-comer, gas distributor and circulating pump; The upper and lower end of described riser is connected with the upper and lower end of down-comer respectively, and the lower end of riser is connected with down-comer by circulating pump, and gas distributor is located at the bottom of riser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011184701A CN1137769C (en) | 2001-06-01 | 2001-06-01 | Synthesizing slurry-bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011184701A CN1137769C (en) | 2001-06-01 | 2001-06-01 | Synthesizing slurry-bed reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1327874A true CN1327874A (en) | 2001-12-26 |
| CN1137769C CN1137769C (en) | 2004-02-11 |
Family
ID=4663211
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011184701A Expired - Fee Related CN1137769C (en) | 2001-06-01 | 2001-06-01 | Synthesizing slurry-bed reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1137769C (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007140710A1 (en) * | 2006-05-31 | 2007-12-13 | China Petroleum & Chemical Corporation | A slurry bed loop reactor and use thereof |
| CN100404118C (en) * | 2003-07-15 | 2008-07-23 | 萨索尔技术(控股)有限公司 | Process for separating a catalyst from a liquid |
| CN101314120B (en) * | 2007-05-31 | 2010-05-26 | 中国石油化工股份有限公司 | Slurry bed reactor and uses thereof |
| CN102784597A (en) * | 2012-07-20 | 2012-11-21 | 浙江环兴机械有限公司 | Efficient heating fluidizing integration device and its processing method |
| CN103769009A (en) * | 2012-10-19 | 2014-05-07 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| WO2014117725A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| WO2014117723A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| CN106890604A (en) * | 2017-03-29 | 2017-06-27 | 天津西敦津洋环保科技有限公司 | A kind of hybrid particles suspension system |
-
2001
- 2001-06-01 CN CNB011184701A patent/CN1137769C/en not_active Expired - Fee Related
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100404118C (en) * | 2003-07-15 | 2008-07-23 | 萨索尔技术(控股)有限公司 | Process for separating a catalyst from a liquid |
| WO2007140710A1 (en) * | 2006-05-31 | 2007-12-13 | China Petroleum & Chemical Corporation | A slurry bed loop reactor and use thereof |
| CN100443155C (en) * | 2006-05-31 | 2008-12-17 | 中国石油化工股份有限公司 | Slurry bed circulatory flow reactor and uses thereof |
| US7919536B2 (en) | 2006-05-31 | 2011-04-05 | China Petroleum & Chemical Corporation | Slurry bed loop reactor and use thereof |
| US8263007B2 (en) | 2006-05-31 | 2012-09-11 | China Petroleum Chemical Corporation | Slurry bed loop reactor and use thereof |
| CN101314120B (en) * | 2007-05-31 | 2010-05-26 | 中国石油化工股份有限公司 | Slurry bed reactor and uses thereof |
| CN102784597A (en) * | 2012-07-20 | 2012-11-21 | 浙江环兴机械有限公司 | Efficient heating fluidizing integration device and its processing method |
| CN102784597B (en) * | 2012-07-20 | 2014-05-07 | 浙江环兴机械有限公司 | Efficient heating fluidizing integration device and its processing method |
| CN103769009A (en) * | 2012-10-19 | 2014-05-07 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| CN103769009B (en) * | 2012-10-19 | 2016-01-20 | 中国石油化工股份有限公司 | A kind of fluidized bed reactor |
| WO2014117725A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| WO2014117723A1 (en) * | 2013-01-31 | 2014-08-07 | Shanghai Advanced Research Institute, Chinese Academy Of Sciences | Slurry-bed reactor and method of use thereof |
| CN106890604A (en) * | 2017-03-29 | 2017-06-27 | 天津西敦津洋环保科技有限公司 | A kind of hybrid particles suspension system |
| CN106890604B (en) * | 2017-03-29 | 2023-09-05 | 天津西敦津洋环保科技有限公司 | Mixed particle suspension system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1137769C (en) | 2004-02-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5961933A (en) | Process and apparatus for operation of a slurry bubble column with application to the fischer-tropsch synthesis | |
| CN1929908A (en) | Gas distributor for a reactor | |
| CN1137769C (en) | Synthesizing slurry-bed reactor | |
| CN1216853C (en) | Apparatus and method for preparing aminobenzene by nitrobenzene gas-phase hydrogenation | |
| CN1127519C (en) | Method and apparatus for preparing polymers | |
| CN101659588B (en) | Method and device of combined process for producing ethylene by ethanol dehydration and catalytic cracking | |
| CN1958146B (en) | Multiple stage fluidized-bed reactor and method for synthesizing chloroethylene | |
| CN115430368A (en) | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing | |
| CN206616014U (en) | A kind of hydrogenation apparatus of hydrogeneous anthraquinone working solution | |
| CN106278836A (en) | Intermediate concentration formaldehyde and the apparatus and method of methylal synthesis polymethoxy dimethyl ether | |
| CN1020411C (en) | Mixed phase catalysis reaction distillation technology and equipment | |
| CN101328107B (en) | Gas distributor in chloroethylene synthesis fluidized bed and chloroethylene synthetic method | |
| CN102276453A (en) | Method for preparing isobomyl acetate through camphene esterification | |
| CN101579638B (en) | Catalyst for preparing ethylene by ethanol dehydration and preparation method thereof | |
| CN108273452B (en) | Grease epoxidation reactor | |
| CN100569725C (en) | Formaldehyde absorbing method and system | |
| CN216404259U (en) | System for continuously preparing acetophenone | |
| CN112657223B (en) | Reaction bulkhead rectifying tower for eliminating gas phase segmentation in formic acid production process | |
| CN208824453U (en) | The isothermal fixed bed tandem reactor of propylene oxide is prepared for HPPO method | |
| CN206103913U (en) | Reaction unit of benzene part hydrogenation synthesis cyclohexene | |
| CN112023852A (en) | Production device for preparing cyclohexene through partial hydrogenation of benzene | |
| CN205886832U (en) | It is listed as reactor to gather methoxy dimethyl ether synthesis | |
| CN1438250A (en) | Condensation and cooling combined gas-phase fluidized-bed polymerization method and apparatus | |
| CN118437265A (en) | Olefin hydroformylation reactor | |
| CN115650833B (en) | Process method for strengthening olefin hydroformylation by microbubble flow |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20040211 Termination date: 20120601 |