CN117942895A - Butanol device reactor gas-liquid mixing reaction system - Google Patents
Butanol device reactor gas-liquid mixing reaction system Download PDFInfo
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- CN117942895A CN117942895A CN202410095977.XA CN202410095977A CN117942895A CN 117942895 A CN117942895 A CN 117942895A CN 202410095977 A CN202410095977 A CN 202410095977A CN 117942895 A CN117942895 A CN 117942895A
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- reactor
- oxo
- pipe
- micromixer
- butanol
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- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 239000007788 liquid Substances 0.000 title claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 27
- 238000001816 cooling Methods 0.000 claims abstract description 46
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 36
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 15
- 239000012452 mother liquor Substances 0.000 claims description 18
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 9
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 9
- 238000004891 communication Methods 0.000 claims description 5
- 238000000034 method Methods 0.000 abstract description 10
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 abstract description 6
- 230000008569 process Effects 0.000 abstract description 5
- 238000004581 coalescence Methods 0.000 abstract description 2
- 230000005501 phase interface Effects 0.000 abstract description 2
- 238000012545 processing Methods 0.000 abstract description 2
- 238000012546 transfer Methods 0.000 abstract description 2
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical class CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- AMIMRNSIRUDHCM-UHFFFAOYSA-N Isopropylaldehyde Chemical compound CC(C)C=O AMIMRNSIRUDHCM-UHFFFAOYSA-N 0.000 description 4
- 230000006315 carbonylation Effects 0.000 description 4
- 238000005810 carbonylation reaction Methods 0.000 description 4
- 239000000839 emulsion Substances 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 239000010413 mother solution Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 2
- 238000012824 chemical production Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
- C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
- C07C45/505—Asymmetric hydroformylation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
A butanol device reactor gas-liquid mixing reaction system relates to the technical field of butanol synthesis process by a carbonyl method, and comprises a first micromixer, a first carbonyl synthesis reactor, a second micromixer, a second carbonyl synthesis reactor, a first cooling circulation device and a second cooling circulation device, wherein the first micromixer is arranged in the first carbonyl synthesis reactor; the second micromixer is disposed within the second oxo reactor; the first oxo reactor is connected with the second oxo reactor, a first cooling circulation device is arranged between the first oxo reactor and the second oxo reactor, and the second oxo reactor is connected with the second cooling circulation device. The invention increases the contact area of gas and liquid, increases the phase interface area and mass transfer rate of the reaction, and improves the material conversion rate and the processing capacity of the reaction kettle; the coalescence of bubbles in the mixed liquid is reduced, the equipment is integrated, and the investment cost is reduced.
Description
Technical Field
The invention relates to the technical field of butanol synthesis processes by using a carbonyl method, in particular to a butanol device reactor gas-liquid mixing reaction system.
Background
The butanol device 11 months in the Runan chemical butanol device 2020 implements the cogeneration reformation of the alcohol and aldehyde by adding a butyraldehyde isomer tower, realizes the separation of the n-butyraldehyde and the isobutyraldehyde, and improves the productivity to 16.5 ten thousand tons/year, including 15 ten thousand tons/year n-butanol/n-butyraldehyde and 1.5 ten thousand tons/year isobutanol/isobutyraldehyde.
In recent years, the carbonylation slurry gas-liquid mixing technology is successfully applied to the fields of medicine, agriculture, environmental protection and the like, remarkable effects are achieved, breakthrough is sought in the field of large chemical industry, and the industries of domestic butanol and octanol, acetic acid and the like start to operate a pilot plant of the gas-liquid micro-interface mixing technology, so that the main indexes of the butanol carbonylation slurry gas-liquid mixing technology are better than the indexes of the traditional process. Therefore, the method is an important way for occupying the market, obtaining the technical advantages of autonomous patents and realizing the yield improvement and consumption reduction of butanol devices, and is in face of the vigorous technical competition of industry and accelerating the implementation of the improvement of carbonylation slurry gas-liquid mixing technology.
The gas-liquid micro-mixing technology is a key equipment technology in the process industry, can optimize the reaction condition in the chemical reaction process, can improve the reaction speed, reduce the occurrence of side reaction, reduce the emission, the material consumption, the energy consumption and the cost, improve the intrinsic safety of chemical production, and provide high and new power for the high-quality development of chemical production in China under the conditions of adjusting the reaction pressure downwards and properly reducing the reaction temperature. In recent years, the method has been successfully applied to the fields of fine chemical industry such as medicine, agriculture, environmental protection and the like, and has remarkable effect, so that the method faces to the vigorous technical competition of industry, accelerates the application of the micro-mixing technology of the large chemical industry, and is an urgent matter for realizing the yield improvement and consumption reduction of the butanol device.
Therefore, how to optimize the material liquid state of the outlet pipeline into a gas-liquid mixing state in the application of the carbonylation slurry gas-liquid mixing process, and strengthen the mixing effect; after the micro-mixing technology is developed and applied to the butanol device, development and innovation are carried out on the connection mode of the outlet pipeline so as to improve the reaction rate of the carbonyl system; is a technical problem which needs to be solved.
Disclosure of Invention
The invention aims to solve the problems in the background art, and further provides a butanol device reactor mixed reaction system.
The technical scheme adopted for solving the technical problems is as follows:
A butanol device reactor gas-liquid mixing reaction system comprises a first micromixer, a first oxo reactor, a second micromixer, a second oxo reactor, a first cooling circulation device and a second cooling circulation device, wherein the first micromixer is arranged in the first oxo reactor; the second micromixer is disposed within the second oxo reactor; the first oxo reactor is connected with the second oxo reactor, a first cooling circulation device is arranged between the first oxo reactor and the second oxo reactor, and the second oxo reactor is connected with the second cooling circulation device.
Further, a first synthesis gas pipe and a first mother liquor feeding pipe are arranged on the first micromixer, and a first discharging pipe is arranged at the bottom of the first oxo synthesis reactor.
Further, a second synthesis gas pipe and a second mother liquor feed pipe are arranged on the second micromixer, a second discharge pipe is arranged at the bottom of the second oxo synthesis reactor, and a first mother liquor communicating pipe is connected to the side wall of the second oxo synthesis reactor.
Further, the first cooling circulation device comprises a first circulation pump, a first heat exchanger and a first cooling circulation pipe; the outlet material of the first oxo reactor is discharged from a first discharge pipe, a first circulating pump is connected with a first cooling circulating pipe, and the first cooling circulating pipe is connected with a first heat exchanger.
Further, the second cooling circulation device comprises a second circulation pump, a second heat exchanger and a second cooling circulation pipe; the outlet material of the second oxo reactor is discharged from a second discharge pipe, a second circulating pump is connected with a second cooling circulating pipe, and the second cooling circulating pipe is connected with a second heat exchanger.
Further, the side wall of the first oxo reactor is provided with a first propylene feed pipe, and the side wall of the second oxo reactor is provided with a second propylene feed pipe.
Further, the second oxo reactor comprises an outer shell, a second micromixer is arranged in the outer shell, a second synthesis gas pipe and a second mother solution feeding pipe are connected to the side wall of the second micromixer, a first mother solution communicating pipe is arranged on the side wall of the second oxo reactor, a second discharging pipe is arranged at the bottom of the second oxo reactor, a mixing chamber is arranged in the second oxo reactor, the mixing chamber is communicated with the second micromixer through a vertical pipe, and the end part of the first mother solution communicating pipe extends into the mixing chamber.
Compared with the prior art, the invention has the beneficial effects that: the invention increases the contact area of gas and liquid, increases the phase interface area and mass transfer rate of the reaction, and improves the material conversion rate and the processing capacity of the reaction kettle; compared with an external mixer, the internal mixer design shortens the time for the mixed solution to enter the reaction kettle, reduces the coalescence of bubbles in the mixed solution, integrates equipment and reduces investment cost.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
FIG. 2 is a cross-sectional view of a second micromixer;
Wherein: 1 first micromixer, 2 first oxo reactor, 3 first circulation pump, 4 first heat exchanger, 5 second oxo reactor, 51 shell, 53 vertical tube, 54 mixing chamber, 6 second micromixer, 7 second circulation pump, 8 second heat exchanger, 101 first synthesis gas pipe, 102 first mother liquor feed pipe, 103 first mother liquor communication pipe, 104 second synthesis gas pipe, 105 second mother liquor feed pipe, 106 first discharge pipe, 107 second discharge pipe.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. The invention will be further described with reference to the accompanying drawings and examples:
As shown in fig. 1 and 2, a butanol device reactor gas-liquid mixing reaction system comprises a first micromixer 1, a first oxo reactor 2, a second micromixer 6, a second oxo reactor 5, a first cooling circulation device and a second cooling circulation device, wherein the first micromixer is arranged in the first oxo reactor; the second micromixer is disposed within the second oxo reactor; the first oxo reactor is connected with the second oxo reactor, a first cooling circulation device is arranged between the first oxo reactor and the second oxo reactor, and the second oxo reactor is connected with the second cooling circulation device.
Further, a first synthesis gas pipe 101 and a first mother liquor feed pipe 102 are arranged on the first micromixer, and a first discharge pipe 106 is arranged at the bottom of the first oxo reactor.
Further, a second synthesis gas pipe 104 and a second mother liquor feed pipe 105 are arranged on the second micromixer, and a second discharge pipe 107 is arranged at the bottom of the second oxo reactor. The side wall of the second oxo reactor is connected with a first mother liquor communication pipe 103.
The first micro mixer is used for fully crushing and mixing propylene and synthesis gas to form a gas-liquid emulsion; the first oxo reactor is used for oxo-synthesizing the catalyst and the gas-liquid emulsion to generate butyraldehyde; the second micromixer is used for fully crushing and mixing propylene and the synthesis gas to form a gas-liquid emulsion; the second oxo reactor is used for oxo-synthesizing the catalyst and the gas-liquid emulsion to generate butyraldehyde.
In at least one embodiment, the first cooling circulation device comprises a first circulation pump 3, a first heat exchanger 4 and a first cooling circulation pipe; the outlet material of the first oxo reactor is discharged from a first discharge pipe, a first circulating pump is connected with a first cooling circulating pipe, and the first cooling circulating pipe is connected with a first heat exchanger.
The material flowing out of the first oxo reactor is subjected to heat exchange and temperature reduction sequentially through a first circulating pump and a first heat exchanger to be used as oxo reactor cooling circulating liquid, the oxo reactor cooling circulating liquid flows into the first micro mixer through a first circulating pipe, and the material can also flow into the second micro mixer after passing through the first circulating pump.
In at least one embodiment, the second cooling circulation device comprises a second circulation pump 7, a second heat exchanger 8 and a second cooling circulation pipe; the outlet material of the second oxo reactor is discharged from a second discharge pipe, a second circulating pump is connected with a second cooling circulating pipe, and the second cooling circulating pipe is connected with a second heat exchanger.
The material flowing out of the second oxo reactor is subjected to heat exchange and temperature reduction sequentially through a second circulating pump and a second heat exchanger to be used as oxo reactor cooling circulating liquid, the oxo reactor cooling circulating liquid flows into the second micromixer through a second circulating pipe, and the material can flow to the outside of the system after passing through the second circulating pump.
In at least one embodiment, the side wall of the first oxo reactor is provided with a first propylene feed pipe and the side wall of the second oxo reactor is provided with a second propylene feed pipe.
In at least one embodiment, as shown in FIG. 2, the second oxo reactor comprises an outer shell 51 having a second micromixer 6 disposed therein, wherein the second micromixer is known in the art and has been disclosed by applicant in 2022, 11/07/202210808425. X. The side wall of the second mixer is connected with a second synthesis gas pipe 104 and a second mother liquor feed pipe 105, the side wall of the second oxo synthesis reactor is provided with a first mother liquor communication pipe 103, the bottom of the second oxo synthesis reactor is provided with a second discharge pipe 107, a mixing chamber 54 is arranged in the second oxo synthesis reactor, the mixing chamber is communicated with the second mixer through a vertical pipe 53, and the end part of the first mother liquor communication pipe extends into the mixing chamber.
In the working mode, propylene and synthesis gas enter a first mother liquor feed pipe into a first oxo-synthesis reactor under the action of a catalyst, oxo-synthesis reactor cooling circulating liquid is used as liquid-phase feed of a first micro-mixer, synthesis gas fed by a synthesis gas pipe is used as gas-phase feed of the first micro-mixer, after gas-liquid mixing, the reaction is carried out in the first oxo-synthesis reactor, gas-liquid mixed liquid passing through the first micro-mixer enters a first circulating pump from a first discharge pipe at the bottom of a kettle and enters a second oxo-synthesis reactor, cooled mother liquor and synthesis gas enter a second micro-mixer in the second oxo-synthesis reactor, the second micro-mixer is required to be added with a second circulating pump and a second heat exchanger for circulating cooling, and reacted materials enter a subsequent section.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the foregoing examples, and that the foregoing description and description are merely illustrative of the principles of this invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (7)
1. The butanol device reactor gas-liquid mixing reaction system is characterized by comprising a first micro-mixer, a first oxo-synthesis reactor, a second micro-mixer, a second oxo-synthesis reactor, a first cooling circulation device and a second cooling circulation device, wherein the first micro-mixer is arranged in the first oxo-synthesis reactor; the second micromixer is disposed within the second oxo reactor; the first oxo reactor is connected with the second oxo reactor, a first cooling circulation device is arranged between the first oxo reactor and the second oxo reactor, and the second oxo reactor is connected with the second cooling circulation device.
2. The butanol device reactor gas-liquid mixing reaction system of claim 1, wherein the first micromixer is provided with a first synthesis gas pipe and a first mother liquor feed pipe, and a first discharge pipe is provided at the bottom of the first oxo reactor.
3. The butanol device reactor gas-liquid mixing reaction system according to claim 1, wherein a second synthesis gas pipe and a second mother liquid feed pipe are disposed on the second micromixer, a second discharge pipe is disposed at the bottom of the second oxo reactor, and a first mother liquid communication pipe is connected to a side wall of the second oxo reactor.
4. A butanol plant reactor gas-liquid mixing reaction system according to claim 2 or 3 wherein said first cooling circulation means comprises a first circulation pump, a first heat exchanger and a first cooling circulation tube; the outlet material of the first oxo reactor is discharged from a first discharge pipe, a first circulating pump is connected with a first cooling circulating pipe, and the first cooling circulating pipe is connected with a first heat exchanger.
5. The butanol plant reactor gas-liquid mixing reaction system of claim 4, wherein said second cooling circulation device comprises a second circulation pump, a second heat exchanger, and a second cooling circulation tube; the outlet material of the second oxo reactor is discharged from a second discharge pipe, a second circulating pump is connected with a second cooling circulating pipe, and the second cooling circulating pipe is connected with a second heat exchanger.
6. The butanol plant reactor vapor-liquid mixing reaction system of claim 5 wherein a first propylene feed line is provided to a side wall of a first oxo reactor and a second propylene feed line is provided to a side wall of a second oxo reactor.
7. The butanol plant reactor gas-liquid mixing reaction system according to claim 6, wherein the second oxo reactor comprises an outer shell, a second micromixer is disposed in the outer shell, a second synthesis gas pipe and a second mother liquor feed pipe are connected to a side wall of the second micromixer, a first mother liquor feed pipe is disposed on a side wall of the second oxo reactor, a second discharge pipe is disposed at a bottom of the second oxo reactor, a mixing chamber is disposed in the second oxo reactor, the mixing chamber is communicated with the second micromixer through a vertical pipe, and an end portion of the first mother liquor feed pipe extends into the mixing chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410095977.XA CN117942895A (en) | 2024-01-23 | 2024-01-23 | Butanol device reactor gas-liquid mixing reaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202410095977.XA CN117942895A (en) | 2024-01-23 | 2024-01-23 | Butanol device reactor gas-liquid mixing reaction system |
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| Publication Number | Publication Date |
|---|---|
| CN117942895A true CN117942895A (en) | 2024-04-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202410095977.XA Pending CN117942895A (en) | 2024-01-23 | 2024-01-23 | Butanol device reactor gas-liquid mixing reaction system |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5105018A (en) * | 1989-10-19 | 1992-04-14 | Mitsubishi Kasei Corporation | Process for hydroformylation of an olefin |
| CN112479815A (en) * | 2019-09-12 | 2021-03-12 | 南京延长反应技术研究院有限公司 | Reaction system and process for preparing butanol and octanol through propylene carbonylation based on micro-interface reinforcement |
| CN214400308U (en) * | 2020-09-15 | 2021-10-15 | 山东华鲁恒升化工股份有限公司 | Single-double reactor system for synthesizing butyraldehyde by carbonyl |
| CN115178168A (en) * | 2022-07-11 | 2022-10-14 | 兖矿鲁南化工有限公司 | Carbonylation slurry gas-liquid mixer and use method thereof |
| CN115430368A (en) * | 2022-08-31 | 2022-12-06 | 兖矿鲁南化工有限公司 | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing |
-
2024
- 2024-01-23 CN CN202410095977.XA patent/CN117942895A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5105018A (en) * | 1989-10-19 | 1992-04-14 | Mitsubishi Kasei Corporation | Process for hydroformylation of an olefin |
| CN112479815A (en) * | 2019-09-12 | 2021-03-12 | 南京延长反应技术研究院有限公司 | Reaction system and process for preparing butanol and octanol through propylene carbonylation based on micro-interface reinforcement |
| CN214400308U (en) * | 2020-09-15 | 2021-10-15 | 山东华鲁恒升化工股份有限公司 | Single-double reactor system for synthesizing butyraldehyde by carbonyl |
| CN115178168A (en) * | 2022-07-11 | 2022-10-14 | 兖矿鲁南化工有限公司 | Carbonylation slurry gas-liquid mixer and use method thereof |
| CN115430368A (en) * | 2022-08-31 | 2022-12-06 | 兖矿鲁南化工有限公司 | System and process for preparing butanol and octanol by carbonylation slurry gas-liquid mixing |
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