CN101440027B - Alkene hydroformylation flow reactor - Google Patents
Alkene hydroformylation flow reactor Download PDFInfo
- Publication number
- CN101440027B CN101440027B CN2008102362393A CN200810236239A CN101440027B CN 101440027 B CN101440027 B CN 101440027B CN 2008102362393 A CN2008102362393 A CN 2008102362393A CN 200810236239 A CN200810236239 A CN 200810236239A CN 101440027 B CN101440027 B CN 101440027B
- Authority
- CN
- China
- Prior art keywords
- gas
- liquid
- mass transfer
- section
- liquid separation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000007037 hydroformylation reaction Methods 0.000 title claims abstract description 43
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 32
- 239000007788 liquid Substances 0.000 claims abstract description 104
- 239000003054 catalyst Substances 0.000 claims abstract description 38
- 238000006276 transfer reaction Methods 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 239000007789 gas Substances 0.000 claims abstract description 29
- 238000009826 distribution Methods 0.000 claims abstract description 21
- 239000000835 fiber Substances 0.000 claims abstract description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 14
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 14
- 239000001257 hydrogen Substances 0.000 claims abstract description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 12
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 4
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 claims abstract 5
- 238000000926 separation method Methods 0.000 claims description 44
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 17
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 17
- 229910000831 Steel Inorganic materials 0.000 claims description 15
- 239000010959 steel Substances 0.000 claims description 15
- 239000000203 mixture Substances 0.000 claims description 9
- 239000000498 cooling water Substances 0.000 claims description 7
- 239000000047 product Substances 0.000 claims description 7
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 5
- 230000001143 conditioned effect Effects 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 2
- 230000022244 formylation Effects 0.000 claims 1
- 238000006170 formylation reaction Methods 0.000 claims 1
- 238000002156 mixing Methods 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000012528 membrane Substances 0.000 abstract 2
- 229910052751 metal Inorganic materials 0.000 abstract 2
- 239000002184 metal Substances 0.000 abstract 2
- 239000000243 solution Substances 0.000 description 23
- 150000001299 aldehydes Chemical class 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- 239000012071 phase Substances 0.000 description 10
- NBBJYMSMWIIQGU-UHFFFAOYSA-N Propionic aldehyde Chemical compound CCC=O NBBJYMSMWIIQGU-UHFFFAOYSA-N 0.000 description 8
- 239000007864 aqueous solution Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 239000008346 aqueous phase Substances 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000012074 organic phase Substances 0.000 description 3
- 229910052703 rhodium Inorganic materials 0.000 description 3
- 239000010948 rhodium Substances 0.000 description 3
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 230000003014 reinforcing effect Effects 0.000 description 2
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical class CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 1
- 229910001069 Ti alloy Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 230000007480 spreading Effects 0.000 description 1
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 1
- ABDKAPXRBAPSQN-UHFFFAOYSA-N veratrole Chemical compound COC1=CC=CC=C1OC ABDKAPXRBAPSQN-UHFFFAOYSA-N 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to a continuous reactor for olefin hydroformylation, which consists of a gas-liquid distribution section A at the upper part, a mass transfer reaction section B at the middle part, and a gas-liquid distribution section C at the lower part. The gas-liquid distribution section A at the upper part is provided with an inlet pipe of mixed gases consisting of hydrogen and carbon monoxide and an inlet pipe of catalyst solution; the mass transfer reaction section B at the middle part is a key part of the reactor, is cylindrical, and is filled with hydrophilic fibrous membrane consisting of metal fiber the diameter of which is 0.01 to 0.2 millimeter; a cylinder of the mass transfer reaction section B extends into the gas-liquid distribution section C, while the fibrous membrane consisting of the metal fiber extends to the bottom of the gas-liquid distribution section C; and the side wall of the gas-liquid distribution section C is provided with a reaction residual gas outlet 3 and an outlet 4 of reaction product liquid aldehyde, and the bottom of the gas-liquid distribution section C is provided with a catalyst solution outlet 7 which is connected with a circulating pump through a pipeline to make catalyst solution flow circularly. The reactor has the advantages of high reaction efficiency, no back mixing, low production cost and durability.
Description
Technical field
The present invention relates to petrochemical industry alkene and carbon monoxide and gas hydrogen the industrial reactor that hydroformylation reaction generates corresponding aldehyde takes place under catalyst action.
Technical background
Hydroformylation reaction takes place in alkene and carbon monoxide and hydrogen under catalyst action
The aldehyde that generates can be made into corresponding alcohol through hydrogenation.Millions of ton of meter of throughput of synthol in this way in the world.Hydroformylation reaction takes place and generates propionic aldehyde or butyraldehyde in ethene or propylene and carbon monoxide and hydrogen under the effect of rhodium carbonyl catalyst, and further hydrogenation generates propyl alcohol or butanols is exactly one of them important chemical process.
No matter used hydroformylation reaction device on the industrial production is the reactor drum that still formula band stirs at present, or tower reactor; All belong to back-mix reactor; For the hydroformylation reaction of ethene (or propylene) with carbon monoxide and hydrogen, under reaction conditions, ethene (or propylene), carbon monoxide and hydrogen all are gas phases; Catalyst dissolution is a liquid phase in water.And ethene (or propylene), carbon monoxide and hydrogen solubleness in water are very little, in back-mix reactor, can only just can make mixing of materials by means of the bubbling of gas.In industrial reactor, this reaction is controlled by the rate of mass transfer of gas-liquid two-phase interface in fact.So for the hydroformylation reaction device of alkene, reinforcing mass transfer is to improve the key of reactor efficiency.
The main path of reactor drum reinforcing mass transfer is to increase the mass transfer interface, for the bubbling style reactor that does not add stirring, has only through suitable gas distributor and tightens and improves mass transfer.In this bubbling style back-mixing equipment (like the tower kind equipment), owing to there is not the input of mixing energy, it is enough thin that bubble can not reach; For enough mass transfer areas are arranged, just enough big space must be arranged, this just makes that equipment is huger; The utilising efficiency of equipment is just lower, and investment is also big.To the tank reactor of stirring is arranged,, thereby increase the mass transfer interface though the input of mixing energy can make bubble attenuate; But also cause the gas-liquid and the liquid liquid separation difficulty of reaction product simultaneously; And under than higher pressure (like reaction pressure at 2.2MPa), the solution of whipping device dynamic seal neither a nothing the matter, and it will spend very high cost; The height of its expense often makes the expense of other part of equipment to ignore, and this has just increased investment cost greatly.And the dynamic seal under the high pressure damages easily, and work-ing life is short, and this makes that the maintenance cost of production process is very high, and usually can influence normally carrying out of production.
Summary of the invention
The object of the invention will solve an above-mentioned difficult problem exactly, makes the hydroformylation reaction of alkene existing than higher plant efficiency, does not have the difficult problem of high pressure dynamic sealing again.
Technical scheme of the present invention is following:
A kind of alkene hydroformylation flow reactor; It forms (see figure 1) by the gas-liquid distribution segment A on top, the mass transfer reaction section B at middle part and three parts of gas-liquid separation section C of bottom; The gas mixture inlet pipe that the gas-liquid distribution segment A on top is made up of hydrogen and carbon monoxide and the liquid-inlet pipe and the liquid distributor 2 of gas distributor 1 and catalyst solution; The mass transfer reaction section B at middle part is the core of this reactor drum, and it be cylindric, and that inside is full of is hydrophilic, diameter is the tunica fibrosa of 0.01～0.2mm steel fiber composition; Mass transfer reaction section B and gas-liquid distribution segment A are tightly connected; The diameter of gas-liquid separation section C is greater than the diameter of mass transfer reaction section B, and the cylinder of mass transfer reaction section B extend in the gas-liquid separation section C, and the tunica fibrosa that steel fiber is formed then reaches the bottom of gas-liquid separation section C always; Mass transfer reaction section B also seals with gas-liquid separation section C and combines; The residual air that responds on the sidewall of gas-liquid separation section C outlet 3, reaction residual air outlet 3 is higher than the bottom end opening of the cylinder of the mass transfer reaction section B that stretches into gas-liquid separation section C, the outlet 4 of the product liquid aldehyde that responds on the sidewall of gas-liquid separation section C; The outlet 4 of the liquid aldehyde of reaction product is positioned on the liquid level of the catalyst solution bottom the gas-liquid separation section C; Catalyst solution outlet 7 is arranged at the bottom of gas-liquid separation section C, and it is connected with recycle pump through pipeline, through recycle pump catalyst solution is gone into this alkene hydroformylation flow reactor 2 times through the liquid-inlet pipe and the liquid distributor of the catalyst solution of gas-liquid distribution segment A.
Above-mentioned alkene hydroformylation flow reactor, the different heights on the sidewall of described mass transfer reaction section B has the import of several reaction masses, constitutes humidity control system 8.
Above-mentioned alkene hydroformylation flow reactor, cooling water jecket can be arranged at the bottom of described gas-liquid separation section C.
Above-mentioned alkene hydroformylation flow reactor, described mass transfer reaction section B can have several TPs, with the temperature of control mass transfer reaction section B.
Above-mentioned alkene hydroformylation flow reactor, TP can be arranged at described gas-liquid separation section C bottom, with the temperature of control catalyst solution.
Above-mentioned alkene hydroformylation flow reactor, pressure transmitter or tensimeter are arranged at described gas-liquid separation section C top.
Above-mentioned alkene hydroformylation flow reactor, organic aldehyde level sensor or liquidometer can be arranged at described gas-liquid separation section C bottom, in order to the flow of the outlet 4 of conditioned reaction product liquid aldehyde.
The method that alkene hydroformylation flow reactor of the present invention is set up the mass transfer interface is different from backmixed reactor.Backmixed reactor produces bubble (or drop) through dispersing and mixing and sets up the mass transfer interface.Tunica fibrosa mass transfer reaction device among the present invention forms liquid film through liquid on the tunica fibrosa surface and sets up the mass transfer interface.Water is surperficial because the surface tension effects between liquid and solid at hydrophilic tunica fibrosa; Water is just along the surface spreading of steel fiber, form no back-mixing, greatly and the surface of book, if second kind of fluid flows through near the of water coequally; Then the friction between two kinds of liquid will make liquid along fiber flow; And the surface tension effects between aqueous phase liquid and the steel fiber tends to make liquid attached on the fiber, and under the acting in conjunction of these two kinds of power, aqueous phase liquid can be along steel fiber along stretching; Calculate thereby produce by unit volume; Its contact surface is more much bigger than backmixed reactor, and is constrained on the mass transfer interface on steel fiber surface, and the mass transfer interface that its unit volume produces is compared with backmixed reactor and will be exceeded more than hundred times.
Another characteristics of alkene hydroformylation flow reactor of the present invention are when producing very high mass transfer interface, accomplish alternate not back-mixing, owing to there is not the input of mixing energy, make to be separated just than being easier to.Be dissolved with the catalyzer water and can flow into the bottom of gas-liquid separator along the surface of steel fiber, gas phase exports out reactor drum on the top of gas-liquid separator, and reaction product aldehyde goes out reactor drum as organic phase from the centre exit of gas-liquid separator.Because alternate not back-mixing, so the separating of gas phase and liquid phase, organic phase is separated just than being easier to water.Gas phase band liquid problem is just very little.It is also very little that gas phase and organic phase are carried the catalyst solution loss that causes secretly.
The 3rd characteristics of alkene hydroformylation flow reactor of the present invention are that the reaction product aldehydes is realized separating automatically with the water that is dissolved with catalyzer in the bottom of reactor drum; And be to be mixed with a large amount of waters in the product aldehyde to go out reactor drum simultaneously in the stirred-tank reactor, must there be special equipment to realize the separation of product.This reactor drum is isolated the later catalyzer water of product and only need be given very little power and just can be implemented in the circulation in the reactor drum.And the catalyzer liquid film that is strapped in the steel fiber surface is flowed by gas phase and the effect of gravity, and the liquid film surface is brought in constant renewal in, so very high catalyzer service efficiency is arranged.
The 4th characteristics of alkene hydroformylation flow reactor of the present invention are that the temperature in the reactor drum is adjustable, reach temperature of reaction automatic control condition, and the hydroformylation reaction of alkene is a thermopositive reaction; Carrying out along with reaction; Material temperature constantly rises in the reactor drum, after the temperature in the reactor drum is elevated to certain value, and the further rising of temperature; With making the by product of hydroformylation reaction of alkene increase; The selectivity that reaction generates aldehyde reduces, and therefore, reaction must be controlled in certain TR to be carried out.For the temperature of controlling reactor, hydroformylation of olefin device of the present invention has two humidity control systems, and one is the chilled water modulation system of reactor bottom, in order to regulate the temperature of round-robin catalyzer water.Another is the humidity control system in the tunica fibrosa mass transfer reaction device, and it is to be lowered reactor drum by too high temperature rise through injecting cold reaction mass in the different parts of reactor drum, thus the temperature adjusting in the realization response device.These characteristics make reactor drum of the present invention not only have very high reaction conversion ratio, and keep higher reaction preference.
The 5th characteristics of alkene hydroformylation flow reactor of the present invention are the reactor drum long service life, and maintenance cost is low.Except the routine cleaning reactor drum of necessity, need repairing hardly, this has just reduced process cost and production cost greatly.
The These characteristics of alkene hydroformylation flow reactor of the present invention makes it have very high reaction efficiency.Its reaction efficiency than stirring reactor high more than 10 times.
Description of drawings
Fig. 1 is the synoptic diagram of alkene hydroformylation flow reactor of the present invention, and wherein: A is the gas-liquid distribution segment; B is the mass transfer reaction section; C is the gas-liquid separation section; 1 is gas mixture inlet pipe and gas distributor; 2 is catalyst solution liquid-inlet pipe and liquid distributor; 3 are the outlet of reaction residual air; 4 is the liquid aldehyde outlet of reaction product; 5 is cooling water outlet; 6 is entrance of cooling water; 7 are the catalyst solution outlet; 8 is the temperature of reactor regulation system.
Embodiment
The operational process of this reactor drum is following:
Hydroformylation successive reaction with ethene and carbon monoxide and hydrogen is an example, earlier the aqueous solution of catalyzer is squeezed into alkene hydroformylation flow reactor from catalyst solution liquid-inlet pipe 2, treats that hydroformylation of olefin device bottom contains a certain amount of catalyst solution; Start recycle pump; Simultaneously the mixed gas of ethene, carbon monoxide and hydrogen is squeezed into from the gas mixture inlet pipe 1 of gas-liquid distribution segment A, the aqueous solution of catalyzer is squeezed into from catalyst solution liquid-inlet pipe 2, passes through gas and liquid distributor respectively; Water flows downward along the steel fiber among the mass transfer reaction device B; Gas phase is parallel flowing downward between steel fiber, is 60～105 ℃ in temperature, and pressure is under the condition of 1.8～2.5MPa; The hydroformylation reaction of ethene takes place on liquid-gas interface; The residual gas of reaction and pay the gas-phase product that reaction produces and go out reactor drum from reaction residual air outlet 3, aqueous phase catalyst flows to gas-liquid separation section C bottom and removes the catalyst recirculation pump by the catalyst solution outlet 7 of bottom along the steel fiber surface, and the reaction product propionic aldehyde goes out reactor drum by reaction product aldehyde outlet 4; In order to remove the heat that reaction produces; The temperature of Control Circulation aqueous catalyst solution, water coolant is advanced by entrance of cooling water 6, is gone out by cooling water outlet 5.According to the temperature conditions in the tunica fibrosa mass transfer reaction device, get into reactor drums by temperature of reactor regulation system 8 in order to the cold material of conditioned reaction actuator temperature.
Embodiment:
Following examples are used for explaining the present invention, but the present invention is not limited to following examples.
Comparative Examples 1
Being equipped with in the stirring-type reaction kettle of 2 liters of the aqueous solution that water-soluble rhodium catalyzer (provide from Sichuan University, down with) concentration is 10-80ppm, feed ethene, the mixed gas of hydrogen and carbon monoxide, the gas mixture ratio example is ethene: H
2: CO=1: 1.2: 1.5, keep reactor pressure 2.2MPa, the reaction conditions that temperature is 95 ℃, the productive rate of propionic aldehyde are 120g/ hour.
Embodiment 1
An alkene hydroformylation flow reactor; It forms (see figure 1) by the gas-liquid distribution segment A on top, the mass transfer reaction section B at middle part and three parts of gas-liquid separation section C of bottom, the gas mixture inlet pipe that the gas-liquid distribution segment A on top is made up of hydrogen and carbon monoxide and the liquid-inlet pipe and the liquid distributor 2 of gas distributor 1 and catalyst solution, and the mass transfer reaction section B at middle part is cylindric; Diameter is 59mm; High 2500mm (not comprising the part that stretches into gas-liquid separation section C), that inside is full of is hydrophilic, diameter is the tunica fibrosa (Cr Ni Ti alloy, Nanjing gold refining development in science and technology ltd provides) that 0.01～0.2mm steel fiber is formed; In the mass transfer reaction section B TP is arranged; Mass transfer reaction section B and gas-liquid distribution segment A are tightly connected, and the diameter of gas-liquid separation section C is 159mm, high 700mm; Tensimeter is arranged at gas-liquid separation section C top; The cylinder of mass transfer reaction section B extend into 350mm in the gas-liquid separation section C, and the tunica fibrosa that steel fiber is formed then reaches the bottom of gas-liquid separation section C always, and mass transfer reaction section B also seals with gas-liquid separation section C and combines; The residual air that responds on the sidewall of gas-liquid separation section C outlet 3; Reaction residual air outlet 3 is higher than the bottom end opening of the cylinder of the mass transfer reaction section B that stretches into gas-liquid separation section C, and the outlet 4 of the product liquid aldehyde that responds on the sidewall of gas-liquid separation section C, the outlet 4 of the liquid aldehyde of reaction product are positioned on the liquid level of the catalyst solution bottom the gas-liquid separation section C; TP in the catalyst solution; Catalyst solution outlet 7 is arranged at the bottom of gas-liquid separation section C, and it is connected with recycle pump through pipeline, through recycle pump catalyst solution is gone into this alkene hydroformylation flow reactor 2 times through the liquid-inlet pipe and the liquid distributor of the catalyst solution of gas-liquid distribution segment A.External diameter is arranged at the bottom of gas-liquid separator C is 219mm, the cooling water jecket of high 240mm.
Be that the aqueous solution of 10-80ppm is squeezed into alkene hydroformylation flow reactor from the liquid-inlet pipe and the liquid distributor 2 of catalyst solution earlier with the water-soluble rhodium catalyst concn; When treating that catalyst solution amount that alkene hydroformylation flow reactor bottom contains reaches required amount; Open recycle pump, realize the circulation of catalyzer in reactor drum, under steady state conditions; The dispersed phase holdup of the tunica fibrosa of reactor drum is under 2 liters the condition; Feed the mixed gas of ethene, hydrogen and carbon monoxide, the ratio of mixed gas, flow velocity, reaction pressure and temperature are with Comparative Examples 1, and the productive rate of propionic aldehyde is 1380g/ hour.
Claims (7)
1. ethene or hydroformylation of propene flow reactor; It is characterized in that: it partly is made up of the gas-liquid distribution segment (A) on top, the mass transfer reaction section (B) at middle part and three of the gas-liquid separation sections (C) of bottom; The gas mixture inlet pipe that the gas-liquid distribution segment (A) on top is made up of hydrogen and carbon monoxide and the liquid-inlet pipe and the liquid distributor (2) of gas distributor (1) and catalyst solution; The mass transfer reaction section (B) at middle part is the core of this reactor drum; It is cylindric; That inside is full of is hydrophilic, diameter is the tunica fibrosa that 0.01～0.2mm steel fiber is formed, and mass transfer reaction section (B) is tightly connected with gas-liquid distribution segment (A), and the diameter of gas-liquid separation section (C) is greater than the diameter of mass transfer reaction section (B); The cylinder of mass transfer reaction section (B) extend in the gas-liquid separation section (C); The tunica fibrosa that steel fiber is formed then reaches the bottom of gas-liquid separation section (C) always, and mass transfer reaction section (B) also seals with gas-liquid separation section (C) and combines, the residual air that responds on the sidewall of gas-liquid separation section (C) outlet (3); Reaction residual air outlet (3) is higher than the bottom end opening of the cylinder of the mass transfer reaction section (B) that stretches into gas-liquid separation section (C); Respond on the sidewall of gas-liquid separation section (C) outlet (4) of product liquid aldehyde, the outlet (4) of the liquid aldehyde of reaction product are positioned on the liquid level of catalyst solution of gas-liquid separation section (C) bottom, and catalyst solution outlet (7) is arranged at the bottom of gas-liquid separation section (C); It is connected with recycle pump through pipeline, through recycle pump catalyst solution is returned this hydroformylation of olefin device through the liquid-inlet pipe and the liquid distributor (2) of the catalyst solution of gas-liquid distribution segment (A).
2. ethene according to claim 1 or propylene formylation flow reactor is characterized in that: the different heights on the sidewall of described mass transfer reaction section (B) has the import of several reaction masses, constitutes humidity control system (8).
3. ethene according to claim 1 or hydroformylation of propene flow reactor is characterized in that: cooling water jecket can be arranged at the bottom of described gas-liquid separation section (C).
4. ethene according to claim 1 or hydroformylation of propene flow reactor is characterized in that: described mass transfer reaction section (B) has several TPs, with the temperature of control mass transfer reaction section (B).
5. ethene according to claim 1 or hydroformylation of propene flow reactor is characterized in that: TP is arranged at described gas-liquid separation section (C) bottom, with the temperature of control catalyst solution.
6. ethene according to claim 1 or hydroformylation of propene flow reactor is characterized in that: pressure transmitter or tensimeter are arranged at described gas-liquid separation section (C) top.
7. ethene according to claim 1 or hydroformylation of propene flow reactor is characterized in that: organic aldehyde level sensor or liquidometer are arranged at described gas-liquid separation section (C) bottom, in order to the flow of the outlet (4) of conditioned reaction product liquid aldehyde.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102362393A CN101440027B (en) | 2008-11-27 | 2008-11-27 | Alkene hydroformylation flow reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102362393A CN101440027B (en) | 2008-11-27 | 2008-11-27 | Alkene hydroformylation flow reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101440027A CN101440027A (en) | 2009-05-27 |
| CN101440027B true CN101440027B (en) | 2012-03-21 |
Family
ID=40724658
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008102362393A Expired - Fee Related CN101440027B (en) | 2008-11-27 | 2008-11-27 | Alkene hydroformylation flow reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101440027B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101575272B (en) * | 2009-06-16 | 2012-10-10 | 南京荣欣化工有限公司 | Process for continuously producing corresponding aldehyde by alkene hydroformylation reaction |
| CN104513143A (en) * | 2013-09-26 | 2015-04-15 | 陶氏技术投资有限责任公司 | Hydroformylation process |
| CN110038499B (en) * | 2019-04-23 | 2021-03-16 | 宁波巨化化工科技有限公司 | Hydroformylation reactor |
| CN112619564A (en) * | 2020-12-31 | 2021-04-09 | 中海油天津化工研究设计院有限公司 | Novel olefin epoxidation reactor |
| CN116212771B (en) * | 2023-03-09 | 2024-09-24 | 宁波巨化化工科技有限公司 | Liquid phase single reaction kettle capable of circularly reacting to improve overall yield |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5367106A (en) * | 1993-09-20 | 1994-11-22 | Hoechst Celanese Corporation | Coupled secondary oxo reaction system |
| CN1594255A (en) * | 2004-06-25 | 2005-03-16 | 新疆新峰股份有限公司 | Method and reaction still for continuous propionaldehyde production |
| JP4080555B2 (en) * | 1994-12-09 | 2008-04-23 | 三菱化学株式会社 | Method for producing aldehydes |
-
2008
- 2008-11-27 CN CN2008102362393A patent/CN101440027B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5367106A (en) * | 1993-09-20 | 1994-11-22 | Hoechst Celanese Corporation | Coupled secondary oxo reaction system |
| JP4080555B2 (en) * | 1994-12-09 | 2008-04-23 | 三菱化学株式会社 | Method for producing aldehydes |
| CN1594255A (en) * | 2004-06-25 | 2005-03-16 | 新疆新峰股份有限公司 | Method and reaction still for continuous propionaldehyde production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101440027A (en) | 2009-05-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2120820C1 (en) | Catalytic solid-liquid multiphase reactor | |
| CN101440027B (en) | Alkene hydroformylation flow reactor | |
| KR20010072453A (en) | Method for Producing Aldehydes and/or Alcohols or Amines | |
| CN101850225B (en) | Benzene selective hydrogenation device | |
| CN101784511B (en) | Method and apparatus for oxidizing organic compounds | |
| CN100584445C (en) | Stirred/Directed Heterogeneous Reactors | |
| CN101575272B (en) | Process for continuously producing corresponding aldehyde by alkene hydroformylation reaction | |
| CN102241558A (en) | Reaction device and process for preparing cyclohexene by selectively hydrogenating benzene | |
| CN105399604A (en) | Energy-efficient super-large scale methanol-synthesizing method with production of steam of different grades and apparatus thereof | |
| CN111153782A (en) | Method for preparing high-carbon aldehyde by hydroformylation of high-carbon olefin | |
| JP4731553B2 (en) | Production of liquid and optionally gaseous hydrocarbons from gaseous reactants into an expanding slurry bed | |
| CN106622045A (en) | Device and method for improving reaction efficiency of bubble tower by using micro-nano bubbles | |
| CN110709374B (en) | Hydroformylation process | |
| CN106278836A (en) | Intermediate concentration formaldehyde and the apparatus and method of methylal synthesis polymethoxy dimethyl ether | |
| CN101668869B (en) | Cobalt recovery from cobalt catalysed hydroformylation reactions | |
| CN110201611B (en) | Three-phase flow reaction device for olefin hydroformylation and operation method thereof | |
| CN209985425U (en) | A high-efficiency continuous washing separation tower | |
| CN100522897C (en) | Cyclohexane oxidation reactor | |
| CN101898930A (en) | Device for producing cyclohexane by adding hydrogen in benzene and synthesis process | |
| CN202410627U (en) | Cycloolefin hydration reactor | |
| CN202047018U (en) | Device for preparing cyclohexene from benzene through selective hydrogenation | |
| CN106540637B (en) | A kind of circulation flow reactor and application method | |
| CN215162250U (en) | Device of cyclohexene preparation methyl cyclopentane | |
| CN102649718A (en) | Olefin hydroformylation method | |
| CN113004143A (en) | Method and device for synthesizing ethyl chloroacetate |
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 | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120321 Termination date: 20141127 |
|
| EXPY | Termination of patent right or utility model |