CN114288952A - Airlift type external circulation reactor and method - Google Patents
Airlift type external circulation reactor and method Download PDFInfo
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- CN114288952A CN114288952A CN202111674191.6A CN202111674191A CN114288952A CN 114288952 A CN114288952 A CN 114288952A CN 202111674191 A CN202111674191 A CN 202111674191A CN 114288952 A CN114288952 A CN 114288952A
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- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 79
- 230000001174 ascending effect Effects 0.000 claims abstract description 37
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000000926 separation method Methods 0.000 claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 69
- 239000003054 catalyst Substances 0.000 claims description 36
- XXROGKLTLUQVRX-UHFFFAOYSA-N allyl alcohol Chemical compound OCC=C XXROGKLTLUQVRX-UHFFFAOYSA-N 0.000 claims description 24
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 21
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- 239000010948 rhodium Substances 0.000 claims description 8
- 229910052703 rhodium Inorganic materials 0.000 claims description 7
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 5
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 4
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 4
- 239000003729 cation exchange resin Substances 0.000 claims description 4
- 239000007795 chemical reaction product Substances 0.000 claims description 4
- 239000002815 homogeneous catalyst Substances 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 239000000047 product Substances 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims 1
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- RIOQSEWOXXDEQQ-UHFFFAOYSA-N triphenylphosphine Chemical compound C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 RIOQSEWOXXDEQQ-UHFFFAOYSA-N 0.000 description 3
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- PIAOXUVIBAKVSP-UHFFFAOYSA-N γ-hydroxybutyraldehyde Chemical compound OCCCC=O PIAOXUVIBAKVSP-UHFFFAOYSA-N 0.000 description 2
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention discloses an airlift external loop reactor and a method, wherein the airlift external loop reactor comprises an ascending pipe, a descending pipe, a connecting pipe and a gas-liquid separation zone, wherein a valve is arranged in the connecting pipe to regulate and control the circulating liquid velocity flowing into the ascending pipe from the descending pipe; the invention can recycle the solid catalyst in the reactor without an additional solid-liquid separation device outside the reactor, improves the safety, has less power consumption, has simple structure, high safety and high flexibility, and is particularly suitable for the production of 1, 4-butanediol.
Description
Technical Field
The invention belongs to the field of airlift type loop reactors, relates to an airlift type external loop reactor with reaction and separation functions, and can be widely applied to a series of heterogeneous catalytic reaction processes, in particular to the synthesis of 1, 4-butanediol.
Background
The gas lift reactor is one reactor for gas-liquid mixing or gas-liquid-solid mixing and liquid phase circulation with gas stirring. The reactor has simple structure, good mass transfer and heat transfer effects and weak shearing action of fluid in the reactor, thereby being widely applied to the fields of biology and chemical industry. The airlift external loop reactor is a more common airlift reactor type, and has the characteristics of strong heat exchange capacity in addition to the advantages.
The most remarkable characteristic of the airlift type external circulation reactor is the liquid circulation between the ascending pipe and the descending pipe, because the gas content, namely the density, in the ascending pipe and the descending pipe is different, and the gas-liquid separation zone is an important part of the external circulation reactor, the better the degassing effect is, the less the bubbles enter the descending pipe, the larger the circulating liquid velocity is, and the gas content in the ascending pipe is further improved.
In the gas-liquid-solid three-phase heterogeneous catalytic reaction, in order to avoid continuous replenishment of the catalyst, liquid-solid separation is carried out on slurry before liquid phase extraction, so that the catalyst returns to the reactor again to participate in the reaction. Settling tanks and hydrocyclones are two typical settling devices, and the principles are gravity settling and centrifugal settling, respectively, and the efficiency of centrifugal settling is far higher than that of gravity settling, but the equipment cost and the system complexity are increased.
Disclosure of Invention
The invention aims to provide a gas lift type external circulation flow reactor and a method, which can recycle a solid catalyst in the reactor without an additional solid-liquid separation device outside the reactor, improve the safety, reduce the power consumption, have simple structure, high safety and high flexibility, and are particularly suitable for the production of 1, 4-butanediol.
In order to achieve one aspect of the above object, the invention adopts the following technical scheme:
an airlift type external loop reactor comprises an ascending pipe, a descending pipe, a connecting pipe and a gas-liquid separation zone, wherein the top of the gas-liquid separation zone is provided with an exhaust port for exhausting gas separated from liquid flow of the ascending pipe;
the tops of the ascending pipe and the descending pipe are respectively communicated to the bottom of the gas-liquid separation zone, so that liquid flow from the ascending pipe enters the descending pipe through the gas-liquid separation zone; the bottom of the downcomer is communicated with the lower part of the riser through the connecting pipe;
a riser gas distributor is arranged below the connection position of the riser and the connecting pipe, and a liquid inlet is arranged below the connection position of the riser and above the riser gas distributor; a riser gas inlet is formed in the bottom of the riser;
a solid charging opening is formed in the side wall of the downcomer, and a liquid outlet is formed in the lower portion of the downcomer below the solid charging opening; the upper part of the downcomer is provided with a downcomer gas inlet and a downcomer gas distributor positioned below the downcomer gas inlet, and the downcomer gas distributor is used for enabling gas fed from the downcomer gas inlet to enter the downcomer after being uniformly distributed in liquid;
a valve, such as a ball valve, is provided in the connecting pipe to regulate the rate of circulating liquid flowing from the downcomer into the riser.
In one embodiment of the invention, the bottom end of the downcomer is higher than the connection of the riser to the connecting pipe; preferably, the connecting tube is inclined at 30-60 °, such as 45 °. The connecting pipe of the invention is designed to be beneficial to being matched with a valve in the connecting pipe, so that the catalyst particles fluidized in the descending pipe are not easy to enter the ascending pipe or keep fluidized in the descending pipe through the connecting pipe.
In one embodiment of the invention the cross-sectional area of the riser is 3-5 times, such as 4 times that of the downcomer. It is understood by those skilled in the art that the diameter of the gas-liquid separation zone is not less than the sum of the diameters of the riser and the downcomer, so that the riser is subjected to gas-liquid separation due to the space expansion and pressure reduction when the riser enters, for example, the gas-liquid separation zone is horizontally arranged in a cylindrical shape, and the central axis of the riser and the central axis of the downcomer are symmetrical on both sides of the central axis of the gas-liquid separation zone.
In one embodiment of the present invention, a heat exchange coil is further disposed in the ascending pipe and/or the descending pipe to adjust the reaction temperature. The specific arrangement of the heat exchange coil is well known in the art and will not be described herein.
In order to achieve another aspect of the above object, the invention adopts the following technical scheme:
the method for preparing 1, 4-butanediol by utilizing the airlift external circulation reactor comprises the steps of performing hydroformylation reaction of diluted propanol and hydrogen/carbon monoxide mixed gas in the ascending pipe, and performing hydrogenation reaction on a hydroformylation reaction product of the diluted propanol in the descending pipe to obtain the 1, 4-butanediol.
The preparation of 1, 4-butanediol by hydroformylation and subsequent hydrogenation of allyl alcohol as a raw material is well known in the art, and thus the specific reaction mechanism and process thereof are not described herein, wherein the catalyst commonly used in hydroformylation is a rhodium catalyst, and the catalyst commonly used in the subsequent hydrogenation is an acidic resin catalyst.
In an embodiment of the present invention, during the reaction, a toluene solution of allyl alcohol is introduced from the liquid inlet, the toluene solution further contains a rhodium-based catalyst as a homogeneous catalyst for catalyzing the hydroformylation reaction of allyl alcohol, a mixed gas is introduced from the riser gas inlet, a hydrogen gas is introduced from the downcomer gas inlet, an acidic resin catalyst for catalyzing the hydrogenation reaction in the downcomer, preferably a weakly acidic acrylic cation exchange resin catalyst, is added from the solid feed inlet, and 1, 4-butanediol as a reaction product is discharged from the liquid outlet. Wherein the molar ratio of hydrogen to carbon dioxide in the mixed gas can be 3:2-2:3, such as 1: 1; the gas inlet molar ratio of the gas inlet of the ascending pipe to the gas inlet of the descending pipe is 3:1-5:1, such as 4:1, 4.2:1 or 4.5:1, and the gas inlet amount of the descending pipe is obviously lower than that of the ascending pipe because the reaction rate of the hydroformylation reaction is much lower than that of the hydrogenation reaction, so that the liquid circulation in the reactor still exists.
In the embodiment of the present invention, the opening degree of a valve (e.g., a ball valve) in the connecting pipe is gradually increased to fluidize the acidic resin catalyst in the downcomer. In the present invention, the valve opening degree refers to the area of the valve that can be communicated with two sides of the valve when the valve is opened, and the valve with the valve opening degree that can be gradually increased or decreased is well known in the art and will not be described herein.
The invention sets a valve on the connecting pipe of the ascending pipe and the descending pipe, controls the resistance of the liquid circulation flow in the reactor by controlling the valve opening to change the circulation liquid velocity and the gas content rate in the ascending pipe, and the corresponding resistance coefficient zeta under different valve opening can be obtained by the following formula:
ζ: a local drag coefficient;
ΔPv: differential pressure of the fluid across the valve;
ρl: the density of the liquid;
Uld: the flow rate of the liquid in the downcomer;
under the same apparent gas velocity, the resistance coefficient is reduced by increasing the opening of the valve, the circulating liquid velocity is increased, and the gas content in the ascending pipe is correspondingly reduced, so as to meet the requirements of different mass transfer rates.
In an embodiment of the present invention, the particle size of the acidic resin catalyst is larger than the pore size of the downcomer gas distributor, so that the acidic resin catalyst particles do not enter the gas-liquid separation zone. When the liquid velocity is zero, the resin catalyst is completely suspended in the liquid in the downcomer (below the downcomer gas distributor), when the valve is opened, the resin catalyst is fluidized, the opening degree of the valve is gradually increased, the circulating liquid velocity in the connecting pipe is gradually increased to a certain critical value, and the catalyst can be completely fluidized in the downcomer.
In an embodiment of the present invention, the opening degree of the valve in the connecting pipe is adjusted to prevent the valve from being excessively opened so that the acid resin catalyst fluidized in the downcomer enters the connecting pipe.
Those skilled in the art will appreciate that visual windows may be provided in the drop tube and connecting tube to facilitate additional monitoring.
In one embodiment, when the gas-lift external loop reactor is started to prepare 1, 4-butanediol, the acid resin catalyst is filled in the downcomer, the toluene solution is fed, when the liquid level rises to a gas-liquid separation region, the liquid outlet is partially opened to extract (extract at a small flow rate), and then the gas inlet of the riser is opened to feed H2And introducing hydrogen into a mixed gas of the CO and a gas inlet of a downcomer, further opening a liquid outlet to realize material balance in the reactor when the liquid level in the gas-liquid separation zone rises to a certain degree (at the moment, the downcomer is filled with liquid, and the resin catalyst is completely suspended in the liquid in the downcomer), and further gradually opening a valve in a connecting pipe to realize complete fluidization of the acid resin catalyst in the downcomer so as to continuously and normally carry out the reaction in the riser and the downcomer.
It will be appreciated by those skilled in the art that although heat exchange coils may be provided, it is difficult to maintain uniform temperatures along the respective lengths of the riser and the downcomer in the reactor. In one embodiment, the reaction is carried out by controlling the average temperature in the riser to 70-90 deg.C, such as 80 deg.C (e.g., by quartering the riser, providing temperature measurement points at 1/4, 2/4 and 3/4, respectively, and averaging the three points to obtain an average temperature), and controlling the average temperature in the downcomer to 130-170 deg.C, such as 150 deg.C or 160 deg.C; the pressure in the reactor is 8-15Barg, such as 10 or 12 Barg.
Compared with the prior art, the invention has the following beneficial effects:
the reactor disclosed by the invention has the advantages that through the design matching of the connecting pipe and the internal valve thereof, the air inlets are arranged on the ascending pipe and the descending pipe, the traditional limited mode that only the ascending pipe is used for introducing air is broken through, so that different reactions can be respectively carried out in the ascending pipe and the descending pipe, the high integration of the reactions is favorably realized, and the investment is greatly saved; meanwhile, the invention can couple reaction and separation, complete the process reinforcement, ensure the directional flow, mixing, mass transfer and heat transfer effects of reaction materials under the condition of lower energy consumption, and can recycle the solid catalyst in the reactor without an additional solid-liquid separation device outside the reactor, thereby improving the safety and reducing the power consumption. Particularly, when the method is suitable for preparing 1, 4-butanediol, homogeneous catalytic hydroformylation reaction can be carried out in an ascending pipe, and meanwhile, hydrogenation reaction is carried out in a descending pipe by using an acidic resin catalyst, so that high integration of the reaction is realized without being carried out in two reactors respectively, and the method has the advantages of simple structure, high safety and high flexibility.
Drawings
FIG. 1 is an illustration of one embodiment mode of the reactor of the present invention;
wherein the reference numerals are as follows:
1. a riser pipe; 2. a riser gas inlet; 3. a riser gas distributor; 4. a riser liquid inlet; 5. a gas-liquid separation zone exhaust port; 6. a gas-liquid separation zone; 7. a downcomer gas inlet; 8. a downcomer gas distributor; 9. a down pipe; 10. a solids addition port; 12. a liquid outlet; 14. connecting a valve in the pipe; 15. and (4) connecting the pipes.
Detailed Description
The present invention will be further described with reference to the following examples and the accompanying drawings, but the present invention is not limited to the examples shown, and includes equivalent modifications and variations of the technical solutions of the present invention.
As shown in fig. 1, the gas lift type external circulation flow reactor of the present invention comprises a riser 1, a downcomer 9, a connecting pipe 15 and a gas-liquid separation zone 6, wherein the top of the gas-liquid separation zone is provided with a gas outlet 5 for discharging gas separated from the liquid flow of the riser 1; the tops of the ascending pipe 1 and the descending pipe 9 are respectively communicated to the bottom of the gas-liquid separation zone 6, so that liquid flow from the ascending pipe 1 enters the descending pipe 9 through the gas-liquid separation zone 6; the bottom of the downcomer 9 is communicated with the lower part of the riser 1 through the connecting pipe 15; the ascending pipe 1 is provided with an ascending pipe gas distributor 3 below the connecting position of the ascending pipe 1 and the connecting pipe 15, and a liquid inlet 2 is arranged below the connecting position of the ascending pipe 1 and above the ascending pipe gas distributor 3; and a riser gas inlet 4 is formed at the bottom of the riser 1.
A solid feeding port 10 is arranged on the side wall of the downcomer 9, and a liquid outlet 12 is arranged at the lower part or the bottom of the downcomer below the solid feeding port 10; the upper part of the downcomer 9 is provided with a downcomer gas inlet 7 and a downcomer gas distributor 8 positioned below the downcomer gas inlet, and the downcomer gas distributor is used for enabling gas fed from the downcomer gas inlet to enter the downcomer 9 after being uniformly distributed in liquid. A valve 14, such as a ball valve, is provided in the connecting pipe 15 to regulate the circulation flow rate from the downcomer 9 into the riser 1. The bottom end of the downcomer is higher than the connecting position of the riser and the connecting pipe; the connecting tube is arranged inclined at 30-60 deg., such as 45 deg.. The cross-sectional area of the riser is 3-5 times, such as 4 times, the cross-sectional area of the downcomer. Heat exchange coils (not shown) are also arranged in the ascending pipe and/or the descending pipe to adjust the reaction temperature.
Taking allyl alcohol as a raw material to prepare 1, 4-butanediol through hydroformylation reaction and subsequent hydrogenation reaction as an example, when the method is in operation, a toluene solution of allyl alcohol is introduced from the liquid inlet, the toluene solution also contains a rhodium catalyst used as a homogeneous catalyst for catalyzing the hydroformylation reaction of allyl alcohol, a mixed gas is introduced from the gas inlet of the ascending tube, a hydrogen gas is introduced from the gas inlet of the descending tube, an acidic resin catalyst used for catalyzing the hydrogenation reaction in the descending tube, preferably a weakly acidic acrylic acid cation exchange resin catalyst, is added from the solid feeding port, and a reaction product 1, 4-butanediol is discharged from the liquid outlet.
After completing hydroformylation reaction of allyl alcohol and mixed gas in a riser, enabling liquid flow in the riser to enter a gas-liquid separator, discharging separated unreacted gas through a top exhaust port, enabling the liquid to enter a downcomer, enabling an acid resin catalyst in the downcomer to be fluidized through a valve in an adjusting connecting pipe, uniformly mixing the liquid and hydrogen at a gas distributor of the downcomer, and then carrying out hydrogenation reaction in the downcomer after catalysis to prepare 1, 4-butanediol. At the bottom of the descending pipe, part of liquid flows are discharged through a liquid outlet so as to obtain a product 1, 4-butanediol, and the rest liquid circularly enters the ascending pipe through a connecting pipe and is mixed with a fresh raw material to continue to react.
The invention is further illustrated below in connection with example 1 of the inventive reactor for the production of 1, 4-butanediol:
example 1
The reactor of figure 1 is adopted, the pressure in the reactor is about 10Barg, hydroformylation reaction is carried out in an ascending tube, the average temperature is 80 ℃, and the catalyst is a rhodium catalyst (a rhodium homogeneous catalyst prepared in a laboratory, wherein rhodium Rh is diphosphine ligand 2P triphenylphosphine PPh3In a ratio of 1:4:100), the liquid inlet was fed with a toluene solution of allyl alcohol (allyl alcohol mass fraction of 20 wt%), a mass flow of 2.5kg/hr, and a mixed gas flow of 3Nm3The conversion of allyl alcohol in the riser is 99.9% and the selectivity to the desired product, 4-hydroxybutyraldehyde, is 95% (1: 1 molar ratio of hydrogen to carbon monoxide).
Hydrogenation reaction is carried out in the downcomer, the average temperature is 150 ℃, the catalyst is weak acid acrylic cation exchange resin catalyst (Tianjinbo hong resin technology limited, model: D113), the inlet flow of hydrogen gas of the downcomer is 0.72Nm3Hr, the conversion of 4-hydroxybutyraldehyde in the downcomer was 99.9% and the selectivity to 1, 4-butanediol was 99.9%.
It should be understood that the above-described embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. Not all embodiments are exhaustive. All obvious changes or modifications of the technical solution of the present invention are within the spirit of the present invention.
Claims (10)
1. An airlift external loop reactor comprises an ascending pipe, a descending pipe, a connecting pipe and a gas-liquid separation zone, wherein the top of the gas-liquid separation zone is provided with an exhaust port for exhausting gas separated from liquid flow of the ascending pipe;
the tops of the ascending pipe and the descending pipe are respectively communicated to the bottom of the gas-liquid separation zone, so that liquid flow from the ascending pipe enters the descending pipe through the gas-liquid separation zone; the bottom of the downcomer is communicated with the lower part of the riser through the connecting pipe;
a riser gas distributor is arranged below the connection position of the riser and the connecting pipe, and a liquid inlet is arranged below the connection position of the riser and above the riser gas distributor; a riser gas inlet is formed in the bottom of the riser;
a solid charging opening is formed in the side wall of the downcomer, and a liquid outlet is formed in the lower portion of the downcomer below the solid charging opening; the upper part of the downcomer is provided with a downcomer gas inlet and a downcomer gas distributor positioned below the downcomer gas inlet, and the downcomer gas distributor is used for enabling gas fed from the downcomer gas inlet to enter the downcomer after being uniformly distributed in liquid;
and a valve is arranged in the connecting pipe to regulate and control the circulating liquid velocity flowing into the ascending pipe from the descending pipe.
2. The airlift external loop reactor of claim 1 wherein the bottom end of said downcomer is above the point of connection of said riser to said connecting tube.
3. The airlift external loop reactor of claim 1 or 2 wherein said connecting tube is disposed at an inclination of from 30 ° to 60 °.
4. The airlift external loop reactor of claim 3 wherein the cross-sectional area of said riser is from 3 to 5 times that of said downcomer.
5. The airlift external loop reactor of claim 1 or 4 wherein heat exchange coils are further disposed within said riser and/or downcomer to regulate reaction temperature.
6. A process for preparing 1, 4-butanediol using the airlift external loop reactor as claimed in any of claims 1 to 5, wherein the hydroformylation of dilute propanol with a hydrogen/carbon monoxide mixture is carried out in the riser and the hydroformylation product of the dilute propanol is hydrogenated in the downcomer to give 1, 4-butanediol.
7. The method according to claim 6, wherein during the reaction, a toluene solution of allyl alcohol containing a rhodium-based catalyst as a homogeneous catalyst for catalyzing hydroformylation of allyl alcohol is introduced from the liquid inlet, a mixed gas is introduced from the riser gas inlet, a hydrogen gas is introduced from the downcomer gas inlet, an acidic resin catalyst for catalyzing hydrogenation in the downcomer, preferably a weakly acidic acrylic cation exchange resin catalyst, is added from the solid feed port, and 1, 4-butanediol as a reaction product is discharged from the liquid outlet.
8. The method of claim 7, wherein the degree of opening of a valve in the connecting pipe is gradually increased to fluidize the acidic resin catalyst in the downcomer.
9. The method of claim 8, wherein the degree of opening of a valve in the connecting pipe is adjusted so that the acid resin catalyst fluidized in the downcomer does not enter the connecting pipe.
10. The process of claim 9 wherein said acidic resin catalyst has a particle size greater than the pore size of said downcomer gas distributor so that said acidic resin catalyst particles do not enter said vapor-liquid separation zone.
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| CN1612923A (en) * | 2001-11-06 | 2005-05-04 | 埃克森美孚研究工程公司 | Slurry hydrocarbon synthesis with external hydroisomerization in downcomer reactor loop |
| WO2009144144A1 (en) * | 2008-05-27 | 2009-12-03 | Basell Poliolefine Italia S.R.L. | Process for the gas-phase polymerization of olefins |
| CN103764607A (en) * | 2011-03-04 | 2014-04-30 | 堪萨斯大学 | Single solvent gas expanded hydroformylation process |
| CN103566837A (en) * | 2013-11-13 | 2014-02-12 | 山西大学 | External circular reaction device suitable for hydrogenation exothermic reaction |
| CN106582460A (en) * | 2017-01-20 | 2017-04-26 | 南京工业大学 | Novel air-lift external-circulation reactor device and process |
| CN106916727A (en) * | 2017-03-31 | 2017-07-04 | 江南大学 | Assemble the airlift reactor of baffling sieve plate |
| CN111801312A (en) * | 2018-02-26 | 2020-10-20 | 利安德化学技术有限公司 | Hydroformylation of allyl alcohol from glycerol to BDO |
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