CN102826970B - A kind of low-carbon alkene hydroformylation second-stage reaction process and device - Google Patents
A kind of low-carbon alkene hydroformylation second-stage reaction process and device Download PDFInfo
- Publication number
- CN102826970B CN102826970B CN201110163788.4A CN201110163788A CN102826970B CN 102826970 B CN102826970 B CN 102826970B CN 201110163788 A CN201110163788 A CN 201110163788A CN 102826970 B CN102826970 B CN 102826970B
- Authority
- CN
- China
- Prior art keywords
- reactor
- reaction
- synthetic gas
- low
- carbon alkene
- 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.)
- Active
Links
Abstract
The present invention relates to a kind of method and device thereof of hydroformylation second-stage reaction of low-carbon alkene, described method comprises: (1) low-carbon alkene and synthetic gas contact with the solution containing catalyzer and generate aldehyde in the first reactor being equivalent to a complete mixed reaction theory level under temperature 80-120 DEG C of pressure 0.5-5.0Mpa condition; (2) product flowed out from the first reactor enters the second reactor without separation, continues react and obtain aldehyde product in the condition and range identical with the first reactor; Described second reactor is equivalent to the reactor that at least two are mixed reaction theory level entirely, introduces described second reactor respectively as the supplementary synthetic gas of reaction raw materials by the reaction process of olefin feedstock simultaneously.The two-stage reaction method of the low-carbon alkene hydroformylation adopting the present invention to propose, can effectively improve second segment reactor efficiency, compared with double-stirred cell technique, eliminate the mechanical stirring device of the second reactor, technical process is simple.
Description
Technical field
The present invention relates to field of chemical technology, specifically, relate to a kind of two-stage reaction method and device of low-carbon alkene hydroformylation.
Background technology
Olefine in low carbon number is utilized to have developing history for many years through the industrial technology of hydroformylation reaction aldehyde.Current mainstream technology adopts rhodium-phosphine complex to be what is called " low pressure oxo process " technology of catalyzer.Its technical characteristics is: unstripped gas (alkene and synthetic gas (H2/CO)) contacts with the catalyst solution containing rhodium-phosphine complex and free organophosphine ligand and reacts, select certain condition to make reaction mainly occur in liquid phase main body, reaction process is controlled by intrinsic kinetics.The background document relating to this technology can with reference to " hydroformylation reaction of the rhodium catalysis " book jointly edited by C. Clavel gentle in P.W.N.M.Van.
For analyzing prior art, the dynamic characteristic understanding hydroformylation of olefin is very important.The generating rate of principal product and just, the selectivity (so-called just different ratio, is denoted as n/i) of isomerized products is very important, its influence factor is a lot of and relation is complicated.Wherein, the impact of two the most key factors can be described as: olefin partial pressures and the positive correlation of aldehyde generating rate, and reaction order is about one-level, and on n/i almost without impact; The impact of CO dividing potential drop on aldehyde generating rate is irregular normal distribution relation, namely then contrary during the high CO dividing potential drop of positive correlation during low CO dividing potential drop, there is maximum value between the two.CO dividing potential drop is negative correlation on the impact of n/i, namely declines along with CO dividing potential drop raises n/i.About dynamic (dynamical) description also can be published in " Chim.Ind. (Milan) 1980; 62, the paper etc. on 572 with reference to auspicious etc. in " application of organometallic compound in the homogeneous catalytic reaction " book jointly write by B. Kao Niersi and W.A. Herman and P. slips except above-mentioned document.
At present, the hydroformylation reaction of low-carbon alkene all adopts complete mixing flow formula reactor.This is because this type of reactor meets the serious practical situation of backmixing of liquid phase in reaction on the one hand, it can meet the aforementioned dynamic characteristic for the impact of CO dividing potential drop on the other hand, namely in total overall reaction region, effective control CO pressure component is certain value, to obtain the reaction result expected.When selecting this type of reactor, adopting continuous flow to stir autoclave (CSTR) gas-liquid reaction device is a kind of preferably way.This is because the effect of agitator can make the adjoint transmittance process of reaction be strengthened, thus intrinsic speed of response can be made to be selected in higher level.
But, as pointed by chemical reactor general theory, adopt the shortcoming of CSTR reactor to be that the efficiency of separate unit reactor is lower.This can find detailed demonstration in pertinent texts.Therefore how improving reaction efficiency is the focus that those skilled in the art pay close attention to, with regard to hydroformylation reaction, have two kinds of ways of raising the efficiency at present, a kind of way is employing one section of reactive mode, control lower alkene per pass conversion, unconverted alkene is carried out recycle; Another kind of way adopts two-stage reaction method, allows the unconverted alkene of first paragraph continue reaction at second segment, reduce internal circulating load.Belong to the former visible US Patent No. 4247486, US5426238 of typical technical solution etc.The technical scheme belonging to the latter can with reference to English Patent GB1387657 and Chinese patent CN86101063 etc.
In the technical scheme of employing one section reaction, for making a large amount of unconverted olefin Returning reactor, needing to be separated reaction product and needing isolated unconverted olefin supercharging, this will cause the further increase of the complicated of technical process and power consumption.
And adopt the technical scheme of two-stage reaction method, the problem needing the second segment reaction efficiency caused in the face of declining with concentration of olefin to decline further, for addressing this problem, in US Patent No. 5105018, propose a kind of two-stage reaction method of hydroformylation.First paragraph adopts CSTR reactor, and this conversion zone circulates and liquid phase circulation system with the gas phase of self.In one section of gas phase circulation loop, draw one streams containing art converted olefin send into second segment continuation reaction.Second segment adopts plug flow reactor, and also with self gas phase and liquid phase circulation system, wherein liquid phase circulation system is connected with first paragraph.This patent is pointed out because second segment have employed plug flow reactor and improves efficiency.
The problem of this scheme is that two-stage reaction needs the independent recycle system, and the separating unit needed between other two sections makes flow process complicated.In addition, for second segment reaction, owing to only disclosing the reaction result data of band circulation, therefore whether cannot improve reaction efficiency and accurately judge.
Another low-carbon alkene hydroformylation two-stage reaction method is proposed in Chinese patent CN94193456; in tool, first paragraph reaction adopts gas phase circulation technology; second segment reaction have employed what is called " slug flow " reactor; the obvious program notices that second segment reaction is according to complete mixing flow reactor; lower efficiency can be caused; but in order to realize the imagination of " slug flow "; the program have selected baroque row cast reactor; in addition; other ways of the program adopt gas phase circulation technology etc. as first paragraph, are also the ways that efficiency is not high.
For above-mentioned defect, the object of this invention is to provide a kind of low-carbon alkene hydroformylation two-part reaction method and device.
Summary of the invention
For in prior art; the low efficiency problem that the hydroformylation reaction of low-carbon alkene adopts complete mixing flow reactor to bring; especially for the problem that efficiency in the second segment reaction of two-stage reaction declines further; according to the dynamic characteristic of the hydroformylation reaction of low-carbon alkene, the object of this invention is to provide a kind of method and apparatus of two-stage reaction.
By aforementioned known; such judgement can be drawn according to the dynamic characteristic of hydroformylation reaction and related chemistry principle of peactor; namely the most effective hydroformylation reaction method is the complete mixing flow reactor adopting multiple serial operation; but this will make investment and process cost strengthen undoubtedly because increasing number of devices.
Accordingly, main points of the present invention are proposed as follows:
The method of the hydroformylation second-stage reaction of low-carbon alkene of the present invention, comprises
(1) low-carbon alkene and synthetic gas contact with the solution containing catalyzer and generate aldehyde in the first reactor under temperature 80-120 DEG C of pressure 0.5-5.0Mpa condition, wherein said first reactor is be equivalent to the reactor that is mixed reaction theory level entirely, and the transformation efficiency of low-carbon alkene in described first reactor is greater than 50%, is preferably greater than 60%;
(2) product flowed out from the first reactor enters the second reactor without separation, continues react and obtain aldehyde product in the condition and range identical with the first reactor; Wherein, described second reactor is be equivalent to the reactor that at least two are mixed reaction theory level entirely, introduces described second reactor respectively as the supplementary synthetic gas of reaction raw materials by the reaction process of olefin feedstock simultaneously.
Wherein, described complete mixed reaction theory level refers to the number of the complete mixing flow reactor of the serial operation described in the general chemical reactor textbook in this area, namely single complete mixing flow reactor provides a theoretical stage, the complete mixing flow reactor of two and two or more serial operation provides two and two or more theoretical stage, " perfectly mixed reactor " refers to a kind of desirable type of reactor, and " theoretical stage " described in the present invention refers to the ideal response result that can reach according to the ideal model of full mixing.(principal character is: liquid phase does not have temperature and concentration gradient).But the chemical reactor due to reality is general has difference with theoretic ideal reactor, therefore, first reactor of the present invention is equivalent to a reactor entirely mixing reaction theory level to refer to that described first reactor is the reactor that can reach a complete mixed reaction theory level that can be applied to industry or laboratory that those skilled in the art think, as autoclave (CSTR) gas-liquid reaction device etc. is stirred in common stirring tank, HV XLPE power cables, continuous flow; Second reactor of the present invention is that at least two reactors entirely mixing reaction theory level refer to that described second reactor is the reactors that can reach at least two complete mixed reaction theory levels that can be applied to industry or laboratory that those skilled in the art think, as multistage bubbling column reactor (Multi-Stage Bubble Columns); This type of reactor not belt stirrer, structure is simple, manufacture and process cost low.Especially the situation that when hydroformylation second segment reacts, speed of reaction is relatively low is suitable for.Multistage bubbling column reactor is existing successful Application industrially, representational example has the application in F-T synthesis reaction (to consult: Maretto C., " Catalysis today " 2001,66:241-248), and the application in desulphurization reaction (is consulted: Meikap B C., " ChemicalEngineeering J., " 2002,86:331-342).
Therefore; the present invention proposes to adopt following method to realize especially: adopt separate unit complete mixing flow formula reactor as the first paragraph reactor of hydroformylation; adopt multistage complete mixing flow formula reactor as the second segment reactor of hydroformylation, be improved to make the efficiency of reaction with the dynamic characteristic more effectively utilizing this reaction.
Especially, described multistage complete mixing flow formula reactor is multistage bubbling column reactor.
Described supplementary synthetic gas is introduced reactor respectively by the reaction process of olefin feedstock and is referred to and provide at least two synthetic gas opening for feeds, wherein first opening for feed provides supplementary raw material of synthetic gas for the direct unconverted olefin come from the first reactor, and other synthetic gas opening for feeds provide raw material of synthetic gas for the material through partial reaction.
In the present invention, described low-carbon alkene refers to C2-C4 alkene.
The invention has the beneficial effects as follows:
The two-stage reaction method of the low-carbon alkene hydroformylation adopting the present invention to propose; can effectively improve second segment reactor efficiency; compared with double-stirred cell technique, eliminate the mechanical stirring device of the second reactor, this can make equipment, energy consumption and process cost reduce.When final transformation efficiency is identical with two still technique, the cumulative volume efficiency of reactor can improve; When the cumulative volume of reactor is identical with two still technique, propylene per pass conversion can be improved.And compared with the two-stage reaction method be separated with centre with other, the scheme that the present invention proposes, technical process is comparatively simple.
Accompanying drawing explanation
Fig. 1 is the device schematic diagram of the embodiment of the present invention, and wherein R1 is the first reactor; E1 is external cooler; R2 is the second reactor; E2 is condenser; 1-alkene; 2,6-synthetic gas; 3-catalyst solution; 4-first reactor vapor phase product stream; 5-first reactor liquid product stream; 7-reaction end gas; 8-liquid product stream.In figure, the synthetic gas opening for feed number of the second reactor side is not limited to three.
Embodiment
Following examples for illustration of the present invention, but are not used for limiting the scope of the invention.As nothing specializes, the raw material adopted in embodiment is commercial.
Below in conjunction with accompanying drawing, the invention will be further described.
As shown in Figure 1, alkene (1), synthetic gas (2) and catalyst solution (3) are admitted to the first reactor R1.This reactor is a continuous flow stirring tank.Under the effect of catalyzer, in temperature 80-120 DEG C, there is hydroformylation reaction under pressure 0.5-5MPa condition and generate butyraldehyde in raw material.An external cooler E1 is used for removing exothermic heat of reaction.Obvious first reactor is equivalent to a mixed reaction theory level entirely.First reactor has a gaseous phase outlet and a liquid-phase outlet, in order to the logistics containing unreacting material, reaction product and catalyst solution is caused the second reactor R2 by the first reactor.Second reactor is a multistage bubbling column reactor (being three grades) in figure.With regard to every one-level, arrange one for introducing the opening for feed of synthetic gas (6) and one group for removing the spiral coil cooling tube of exothermic heat of reaction.In reactor R2, unconverted raw material continues under the effect of catalyzer, hydroformylation reaction occur and generate butyraldehyde with the synthetic gas supplemented.Multistage bubbling column reactor allows reaction reach the effect of entirely mixing reaction theory level more than two.Be provided with condenser E2 on the top of reactor R2, the reaction end gas (7) through condensation is discharged, and liquid product stream (8) is admitted to subsequent processing units.
Embodiment 1
Be 2L with a volume and with the autoclave of mechanical stirrer as the first reactor; be 56mm with a diameter; height is 510mm; tower reactor not with mechanical stirrer is as the second reactor; also comprise external cooler and water cooler, form the reaction that two sections of hydroformylation reaction systems carry out propylene producing butyladehyde thus.First reactor is provided with the opening for feed of propylene, synthetic gas and catalyst solution and gas phase discharge port and liquid phase discharge port, the reaction mass part that liquid phase discharge port is drawn enters the second reactor, all the other get back in the first reactor after removing reaction heat by external cooler, and gas phase discharge port is directly connected with the opening for feed of the second reactor lower end.
Be horizontally disposed with 6 pieces of perforated baffles in second reactor, baffle plate is uniformly distributed vertically in tower, correspondingly above tower reactor and every block baffle plate arranges a synthetic gas opening for feed for the introducing supplementing synthetic gas.Wherein first opening for feed provides supplementary raw material of synthetic gas for the direct unconverted olefin come from the first reactor, and other synthetic gas opening for feeds are at first paragraph, or comprise second segment further through the material of partial reaction raw material of synthetic gas is provided, a pneumatic outlet for emission and a liquid exit for extraction liquid-phase product is provided with in the second reactor upper end.Second inside reactor is provided with spiral coil cooling tube shifting out for reaction heat.
Entering/discharging pipeline is provided with the collection of thief hole for analytic sample.
Two reactors run continuously by following operational condition:
| Temperature of reaction (DEG C) | Reaction pressure (Mpa) | Rhodium concentration (ppm) | Triphenylphosphine concentration (wt%) | |
| First reactor | 90 | 1.9 | 250 | 12 |
| Second reactor | 90 | 1.8 | 250 | 12 |
Can be calculated by sampling analysis: when the first reactor feed propylene is 210g/h, in the first reactor, the cumulative volume of the transformation efficiency of propylene to be the total conversion rate of 78.0%, two reactors be 93.5%, two reactors is 3.26L.
Comparative example 1
The second reactor in embodiment 1 is changed into and the identical mechanical stirring autoclave of the first reactor, and carry out the serialization hydroformylation reaction of propylene producing butyladehyde according to reaction conditions same as Example 1.
Can calculate when the first reactor feed propylene is 210g/h by sampling analysis, in the first reactor, the cumulative volume of the transformation efficiency of propylene to be 78.0%, two reactor total conversion rates be 93.0%, two reactors is 4L.
This shows, adopt the two-stage reaction method that the present invention proposes, the second reactor eliminates mechanical stirring and the cumulative volume of reactor is decreased to 3.26L by 4L.Calculate reactor cumulative volume efficiency by this and improve 18.5%.
Comparative example 2
Second reactor of embodiment 1 is changed into the band churned mechanically 400ml pressure autoclave type reactor of three serial operations, the identical and cumulative volume of the volume of three stirring tanks is close to the volume of the second reactor in embodiment 1.This reactive system carries out the serialization hydroformylation reaction of propylene producing butyladehyde according to condition same as Example 1.
Can calculate when the first reactor feed propylene is 210g/h by sampling analysis, in the first reactor, the transformation efficiency of propylene is the propylene total conversion rate of 78.0%, 4 reactors is 93.2%, and cumulative volume and the embodiment 1 of reactor are close.
This shows, in the two-stage reaction method that the present invention proposes, the second reactor is equivalent to the stirring tank of three serial operations, is namely equivalent to three mixed reaction theory levels entirely.
Embodiment 2
The height of the second reactor in embodiment 1 is increased to 800mm, and diameter is constant, inside establishes perforated baffle plate number to be increased to 10 pieces, increases the synthetic gas import corresponding to every block baffle plate simultaneously.Rest part is constant and enter the serialization hydroformylation reaction of propylene producing butyladehyde according to reaction conditions same as Example 1.
Can calculate when the first reactor propylene feed amount is 210g/h by sampling analysis, in first reactor, propylene conversion is 78.0%, and the cumulative volume of two reactors is with when when adopting two stirring tanks in comparative example 1, cumulative volume is substantially identical, propylene total conversion rate is increased to 96.8% by 93.0%.
Claims (3)
1. a method for the hydroformylation two-stage reaction of low-carbon alkene, is characterized in that, comprising:
(1) low-carbon alkene and synthetic gas contact with the solution containing catalyzer and generate aldehyde in the first reactor under temperature 80-120 DEG C of pressure 0.5-5.0Mpa condition, wherein said first reactor is be equivalent to the stirring tank that is mixed reaction theory level entirely, and the transformation efficiency of low-carbon alkene in described first reactor is greater than 50%;
(2) product flowed out from the first reactor enters the second reactor without separation, continues react and obtain aldehyde product in the condition and range identical with the first reactor; Wherein, described second reactor is be equivalent to the multistage bubbling column reactor that at least two are mixed reaction theory level entirely, introduces described second reactor respectively as the supplementary synthetic gas of reaction raw materials by the reaction process of olefin feedstock simultaneously;
Described complete mixed reaction theory level refers to the number of the complete mixing flow reactor of the serial operation described in the general chemical reactor textbook in this area, namely single complete mixing flow reactor provides a theoretical stage, and the complete mixing flow reactor of two and two or more serial operation provides two and two or more theoretical stage.
2. method according to claim 1, it is characterized in that, described supplementary synthetic gas is introduced reactor respectively by the reaction process of olefin feedstock and is referred to and provide at least two synthetic gas opening for feeds, wherein first opening for feed provides supplementary raw material of synthetic gas for the direct unconverted olefin come from the first reactor, and other synthetic gas opening for feeds provide raw material of synthetic gas for the material through partial reaction.
3. method according to claim 1, is characterized in that, the transformation efficiency of described low-carbon alkene in described first reactor is greater than 60%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110163788.4A CN102826970B (en) | 2011-06-17 | 2011-06-17 | A kind of low-carbon alkene hydroformylation second-stage reaction process and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110163788.4A CN102826970B (en) | 2011-06-17 | 2011-06-17 | A kind of low-carbon alkene hydroformylation second-stage reaction process and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102826970A CN102826970A (en) | 2012-12-19 |
| CN102826970B true CN102826970B (en) | 2015-08-19 |
Family
ID=47330313
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110163788.4A Active CN102826970B (en) | 2011-06-17 | 2011-06-17 | A kind of low-carbon alkene hydroformylation second-stage reaction process and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102826970B (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI788364B (en) | 2017-06-23 | 2023-01-01 | 美商陶氏科技投資有限公司 | Hydroformylation reaction processes |
| CN108273453B (en) * | 2017-11-28 | 2021-09-14 | 聊城市鲁西化工工程设计有限责任公司 | Reaction heat taking method of hydroformylation synthesizer |
| CN108586219A (en) * | 2018-06-28 | 2018-09-28 | 南京荣欣化工有限公司 | A kind of method that hydroformylation of olefin prepares aldehyde |
| CN111153782A (en) * | 2019-12-31 | 2020-05-15 | 南京中设石化工程有限公司 | Method for preparing high-carbon aldehyde by hydroformylation of high-carbon olefin |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1131413A (en) * | 1993-09-20 | 1996-09-18 | 赫希斯特人造丝公司 | Two stage hydroformylation procedure |
| CN1276364A (en) * | 1999-06-02 | 2000-12-13 | 奥克森诺奥勒芬化学股份有限公司 | Method for carrying out heterogeneous catalytic reaction, especially hydroformylation |
| CN1312785A (en) * | 1998-08-14 | 2001-09-12 | 巴斯福股份公司 | Method for producing aldehydes and/or alcohols amines |
| JP3850439B2 (en) * | 1994-09-30 | 2006-11-29 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Process for preparing 1,3-alkanediol and 3-hydroxyaldehyde |
| US7615645B2 (en) * | 2003-10-21 | 2009-11-10 | Basf Aktiengesellschaft | Method for the continuous production of aldehydes |
-
2011
- 2011-06-17 CN CN201110163788.4A patent/CN102826970B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1131413A (en) * | 1993-09-20 | 1996-09-18 | 赫希斯特人造丝公司 | Two stage hydroformylation procedure |
| JP3850439B2 (en) * | 1994-09-30 | 2006-11-29 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Process for preparing 1,3-alkanediol and 3-hydroxyaldehyde |
| CN1312785A (en) * | 1998-08-14 | 2001-09-12 | 巴斯福股份公司 | Method for producing aldehydes and/or alcohols amines |
| CN1276364A (en) * | 1999-06-02 | 2000-12-13 | 奥克森诺奥勒芬化学股份有限公司 | Method for carrying out heterogeneous catalytic reaction, especially hydroformylation |
| US7615645B2 (en) * | 2003-10-21 | 2009-11-10 | Basf Aktiengesellschaft | Method for the continuous production of aldehydes |
Non-Patent Citations (1)
| Title |
|---|
| 左识之等.细化工反应器及车间工艺设计.《精细化工反应器及车间工艺设计》.华东理工大学出版社,1996,201. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102826970A (en) | 2012-12-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102826974B (en) | A kind of propene hydroformylation reaction prepares the method for butyraldehyde | |
| CN102826970B (en) | A kind of low-carbon alkene hydroformylation second-stage reaction process and device | |
| JPH1066859A (en) | Operation method of bubble three-phase column accompanied by adaptation to fischer-tropsch synthesis and apparatus therefor | |
| CN106795081A (en) | The method that ethylene glycol is continuously prepared by carbohydrate | |
| CN111153782A (en) | Method for preparing high-carbon aldehyde by hydroformylation of high-carbon olefin | |
| CN101291726A (en) | Method for oligomerization of ethylene and reactor system therefor with removal of heavy molecular weight oligomers | |
| WO2015149646A1 (en) | Fluidized bed apparatus and method for preparing polymethoxy dimethylether from methylal and paraformaldehyde | |
| CN106479562B (en) | A kind of dissolving method and application for strengthening hydrogen in reformed oil | |
| CN103055792B (en) | A kind of using method of the vibration tubular reactor for cyclohexane liquid-phase oxidation | |
| CN1458914A (en) | Fisher-Tropsch process | |
| CN103627427B (en) | Two-stage hydrogenation system, and hydrogenation method | |
| CN200955019Y (en) | Synthesized multi-sectional radial cold-exciting type reactor | |
| CN103788272B (en) | A kind of method of hydrotreating containing olefines unsaturated bond polymer | |
| CN100378043C (en) | Process for producing liquid and, optionally, gaseous products from gaseous reactants | |
| Herrmann et al. | Improving Aqueous Biphasic Hydroformylation of Unsaturated Oleochemicals Using a Jet‐Loop‐Reactor | |
| CN102746111A (en) | Cosynthesis device and method of cyclohexanol, cyclohexanone and adipic acid in microchannels | |
| CN107457001B (en) | A kind of polystyrene sulfonic acid resin catalyst and its preparation method and application | |
| CN103130623A (en) | Reaction system and reaction method of gas-liquid double-circulation hydroformylation of preparing butyraldehyde with propylene | |
| CN109485535A (en) | The full method of hydrotreating of unsaturated hydrocarbons in C-4-fraction | |
| CN102649718B (en) | Olefin hydroformylation method | |
| CN211078980U (en) | Device for synthesizing acetic anhydride and co-producing propionic acid through carbonylation | |
| CN202688232U (en) | Cyclohexanol, cyclohexanone and hexanedioic acid cosynthesis device in microchannel | |
| CN103073381A (en) | Method for preparing butadiene through multistage isothermal oxydehydrogenation of butylene | |
| CN1911876A (en) | Method of preparing methyl cyclo penlene by continuous hydrogenation of methyl cyclo pentadiene | |
| CN210994350U (en) | Reaction device for preparing methyl ethyl ketone by dehydrogenating sec-butyl alcohol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |