CN106748746B - Isooctanoic acid production system - Google Patents
Isooctanoic acid production system Download PDFInfo
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- CN106748746B CN106748746B CN201710100417.9A CN201710100417A CN106748746B CN 106748746 B CN106748746 B CN 106748746B CN 201710100417 A CN201710100417 A CN 201710100417A CN 106748746 B CN106748746 B CN 106748746B
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- kettle
- acidification
- oxidation
- tank
- pipeline
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- OEOIWYCWCDBOPA-UHFFFAOYSA-N 6-methyl-heptanoic acid Chemical compound CC(C)CCCCC(O)=O OEOIWYCWCDBOPA-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 41
- 230000003647 oxidation Effects 0.000 claims abstract description 43
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 43
- 230000020477 pH reduction Effects 0.000 claims abstract description 41
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 30
- BWDBEAQIHAEVLV-UHFFFAOYSA-N 6-methylheptan-1-ol Chemical compound CC(C)CCCCCO BWDBEAQIHAEVLV-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000000034 method Methods 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000011084 recovery Methods 0.000 claims abstract description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000013505 freshwater Substances 0.000 claims abstract description 12
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 9
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 9
- 239000011734 sodium Substances 0.000 claims abstract description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000001257 hydrogen Substances 0.000 claims abstract description 8
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 8
- 239000003054 catalyst Substances 0.000 claims abstract description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 230000001105 regulatory effect Effects 0.000 claims description 11
- 238000002347 injection Methods 0.000 claims description 5
- 239000007924 injection Substances 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 3
- 235000011149 sulphuric acid Nutrition 0.000 abstract description 2
- 239000001117 sulphuric acid Substances 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 13
- 239000002253 acid Substances 0.000 description 10
- 239000000047 product Substances 0.000 description 7
- YIWUKEYIRIRTPP-UHFFFAOYSA-N 2-ethylhexan-1-ol Chemical compound CCCCC(CC)CO YIWUKEYIRIRTPP-UHFFFAOYSA-N 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 2
- 239000007806 chemical reaction intermediate Substances 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 239000000543 intermediate Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- VYPDUQYOLCLEGS-UHFFFAOYSA-M sodium;2-ethylhexanoate Chemical compound [Na+].CCCCC(CC)C([O-])=O VYPDUQYOLCLEGS-UHFFFAOYSA-M 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/02—Preparation of carboxylic acids or their salts, halides or anhydrides from salts of carboxylic acids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The invention relates to the technical field of isooctanoic acid production, in particular to an isooctanoic acid production system. The structure of the device comprises an oxidation device, an acidification device and a rectification device which are sequentially connected according to working procedures, wherein the oxidation device comprises an oxidation kettle, an external heating device of the oxidation kettle is connected with a heat conduction oil mechanism, and the oxidation kettle is respectively connected with a fresh water input pipeline, a nitrogen supply pipeline, an isooctanol tank, a hydrogen recovery pipeline and a catalyst input pipeline; the oxidation kettle pass through sodium isooctanoate discharge line connection acidification device, acidification device include acidification kettle, acidification kettle pass through the pipeline and connect fresh water pitcher and sulphuric acid tank respectively, acidification kettle still be connected with cooling circulation water system and crude isooctanoate discharge line, acidification kettle in be provided with rabbling mechanism, crude isooctanoate discharge line connect rectification device. The isooctanoic acid production system can improve production efficiency and product quality.
Description
Technical Field
The invention relates to the technical field of isooctanoic acid production, in particular to an isooctanoic acid production system.
Background
In the prior art, for the isooctanoic acid production process, a 2-ethylhexanol medium pressure catalytic oxidation method is generally adopted: under the alkaline and medium pressure conditions, 2-ethylhexanol is dehydrogenated at 240-260 ℃ with alkaline earth metal oxide as catalyst to produce sodium 2-ethylhexanoate (sodium isooctanoate), the sodium isooctanoate is acidified by sulfuric acid to produce crude isooctanoic acid, and then the crude isooctanoic acid is rectified to obtain the finished product of isooctanoic acid.
In the existing isooctanoic acid production process, because equipment is relatively crude, control over process temperature, reaction pressure and raw material proportion is relatively coarse in oxidation and acidification processes, so that production efficiency is low, and the quality of produced products is poor.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides an isooctanoic acid production system which can improve the production efficiency and the product quality.
The technical scheme adopted by the invention is as follows:
the isooctanoic acid production system comprises an oxidation device, an acidification device and a rectification device which are sequentially connected according to working procedures, wherein the oxidation device comprises an oxidation kettle, an external heating device of the oxidation kettle is connected with a heat conduction oil mechanism, and the oxidation kettle is respectively connected with a fresh water input pipeline, a nitrogen supply pipeline, an isooctanol tank, a hydrogen recovery pipeline and a catalyst input pipeline; the oxidation kettle pass through sodium isooctanoate discharge line connection acidification device, acidification device include acidification kettle, acidification kettle pass through the pipeline and connect fresh water pitcher and sulphuric acid tank respectively, acidification kettle still be connected with cooling circulation water system and crude isooctanoate discharge line, acidification kettle in be provided with rabbling mechanism, crude isooctanoate discharge line connect rectification device.
A water injection pump, an automatic cut-off valve and a flowmeter are arranged on a pipeline between the acidification kettle and the fresh water tank.
A sulfuric acid pump, a regulating valve and a flowmeter are arranged on a pipeline between the acidification kettle and the sulfuric acid tank.
The crude isooctanoic acid discharge pipe is provided with crude isooctanoic acid Xin Suanbeng.
The isooctanol jar is connected with isooctanol recovery jar, isooctanol recovery jar be connected with the blowdown jar.
An isooctanol pump, an automatic shut-off valve and a flowmeter are arranged between the oxidation kettle and the isooctanol tank.
The hydrogen recovery pipeline is provided with a pressure transmitter and a regulating valve.
The rectification device comprises a rectification kettle connected with a crude isooctanoic acid discharge pipeline, the rectification kettle is connected with a front fractionation tank through a rectification condenser, and the front fractionation tank is connected with a finished product tank through an isooctanoic acid intermediate tank.
The oxidation device of the invention is in useFirstly, the temperature of an oxidation kettle is controlled within a certain range by heating heat conduction oil, and then, a certain amount of caustic soda flakes, catalyst and isooctanol are added. After the material feeding is completed, the residual oxygen in the clean kettle is replaced by nitrogen, and the oxidation kettle is closed. Stirring is started, the reaction starts to be carried out, and H is continuously generated in the process 2 The pressure and the temperature of the oxidation kettle are gradually increased, and when the temperature reaches 240 ℃ and the pressure reaches 1.8MPa, H discharge is started 2 This stage must ensure H 2 The discharge amount and the production amount are approximately equal, and the reaction can be ensured to be carried out efficiently and sufficiently only by stabilizing the pressure at 1.8MPa. When the reaction is near the end, H 2 Little production amount, pressure maintaining for 30min to ensure complete reaction and pressure relief. After the pressure relief is finished, adding a certain amount of water, and discharging residual H in the oxidation kettle 2 After the completion, the oxidation kettle is closed, the temperature in the oxidation kettle is very high, a large amount of steam is generated later, when the pressure reaches 0.6MPa, finally, the mixed solution of the reaction intermediate sodium isooctanoate is hydraulically pressed to the acidification kettle, and the first-step reaction is finished.
In the use of the acidification device, firstly, the mixed solution of sodium iso-octoate after the reaction of the oxidation device is pressurized to an acidification kettle, and quantitative pure water is added. Then, sulfuric acid is slowly added at a constant speed, the process releases heat, cooling circulating water is opened, the temperature of the acidification kettle is controlled below 100 ℃, the PH value of materials gradually decreases along with the reaction, and the acid addition is finished after the PH value reaches a set value PH of 3.0. Standing for a period of time, layering the crude isooctanoic acid and the sodium sulfate solution, finally discharging the sodium sulfate solution to a wastewater treatment tank, and discharging the crude isooctanoic acid to a middle storage tank.
The technical scheme provided by the invention has the beneficial effects that:
1. the temperature control is carried out through the heat conduction oil, so that the whole oxidation process is at the optimal reaction temperature, the pressure in the oxidation kettle is controlled through nitrogen input and hydrogen discharge, the safest reaction environment is obtained, and the raw materials and the catalyst addition speed are controlled according to the pressure and the flow rate in the reaction kettle, so that the raw materials in the oxidation kettle can be oxidized most rapidly, the generated reaction intermediate sodium iso-octoate is discharged, and the production efficiency and the product quality are greatly improved.
2. The sodium salt in the acidification kettle can be acidified most rapidly by controlling the temperature, the water supply and the sulfuric acid supply, so that the isooctanoic acid crude product is discharged, and the production efficiency and the product quality are greatly improved.
In conclusion, the isooctanoic acid production system can improve the stability and the yield of the isooctanoic acid production process, is safe and stable in equipment, has high environmental friendliness, and can reduce the production cost and prolong the service life of the equipment.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for the description of the embodiments will be briefly described below, and it is apparent that the drawings in the following description are only some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic system diagram of an isooctanoic acid production system of the present invention.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present invention more apparent, the embodiments of the present invention will be described in further detail with reference to the accompanying drawings.
Example 1
The isooctanoic acid production system comprises an oxidation device, an acidification device and a rectification device which are sequentially connected according to working procedures, wherein the oxidation device comprises an oxidation kettle 1, an external heating device of the oxidation kettle 1 is connected with a heat conduction oil mechanism 33, and the oxidation kettle 1 is respectively connected with a fresh water input pipeline 2, a nitrogen supply pipeline 3, an isooctanol tank 4, a hydrogen recovery pipeline 5 and a catalyst input pipeline 6; the oxidation kettle 1 is connected with the acidification device through a sodium iso-octoate discharge pipeline 7, the acidification device comprises an acidification kettle 8, the acidification kettle 8 is respectively connected with a fresh water tank 9 and a sulfuric acid tank 10 through pipelines, the acidification kettle 8 is also connected with a cooling circulating water system 11 and a crude iso-octoate discharge pipeline 12, a stirring mechanism 13 is arranged in the acidification kettle 8, and the crude iso-octoate discharge pipeline 12 is connected with the rectification device.
The rectifying device in the embodiment comprises a rectifying still 14 connected with a crude isooctanoic acid discharge pipeline 12, wherein the rectifying still 14 is connected with a front fractionating tank 16 through a rectifying condenser 15, and the front fractionating tank 16 is connected with a finished product tank 18 through an isooctanoic acid intermediate tank 17.
A water injection pump 19, an automatic shut-off valve 20 and a flowmeter 21 are arranged on the pipeline between the acidification kettle 8 and the fresh water tank 9.
A sulfuric acid pump 22, a regulating valve 23 and a flowmeter 24 are arranged on a pipeline between the acidification kettle 8 and the sulfuric acid tank 10.
Crude iso Xin Suanbeng 25 is provided on the crude iso-octanoic acid discharging pipe 12.
Isooctanol jar 4 is connected with isooctanol recovery jar 26, isooctanol recovery jar 26 be connected with blow tank 27.
An isooctanol pump 28, an automatic shut-off valve 29 and a flowmeter 30 are arranged between the oxidation kettle 1 and the isooctanol tank 4.
The hydrogen recovery line 5 is provided with a pressure transmitter 31 and a regulating valve 32.
Under the premise of ensuring that the isooctanol storage tank has enough raw materials, the oil temperature of the oxidation kettle 1 and the state of related equipment meet the production, when production personnel send out production instructions, a main operation is performed on a computer to set the feeding amount, a determining button is pressed, a PLC system sequentially starts an isooctanol pump 28, and an automatic cut-off valve 29. The flowmeter 30 starts to have a flow value and transmits a signal to the PLC system, the system performs accumulation operation on the flow, when the accumulated flow reaches a set value, the automatic shut-off valve 29 is immediately closed, the isooctanol pump 28 is stopped, and quantitative feeding is completed. After the process is completed, the computer automatically records the feeding amount into a production report of the corresponding production batch, and the process master can monitor the flow value on line and control the running state of related equipment of the system.
With the progress of the reaction, hydrogen gas is continuously generated, and the pressure is continuously increased, and in order to ensure the efficiency and the quality of the reaction, the pressure must be controlled at 1.8MPa. The main operation only needs to set the pressure maintaining value of the system to 1.8MPa, the pressure transmitter 13 transmits the measured analog value to the automatic control system, the system converts the operation result into analog value signals through proportional, integral and differential operation (PID) and transmits the analog value signals to the regulating valve 23, in order to ensure the regulating effect, the system operates PID regulation once every 0.1S, and even if various disturbance factors exist, the pressure value of the oxidation kettle can still be accurately stabilized at the set value.
In order to obtain various technological parameters in the production process, an oxidation kettle oil temperature measuring instrument, a kettle temperature measuring instrument and the like are also installed, and the system automatically records the measured values to a historical database and has upper and lower limit temperature alarm prompts.
The automatic water feeding process is as follows: under the premise of ensuring that the fresh water storage tank has enough reserves, the kettle temperature of the acidification kettle 8 and the related equipment conditions meet the production, when production personnel send out production instructions, a main operator presses a determination button after setting the feeding amount on a computer, and a PLC system sequentially starts a water injection pump 19 and an automatic shut-off valve 20. The flowmeter 21 starts to have a flow value and transmits a signal to the PLC system, the system performs accumulation operation on the flow, when the accumulated flow reaches a set value, the pneumatic cut-off valve automatic cut-off valve 20 is immediately closed, the water injection pump 19 is stopped, and quantitative feeding is completed. After the process is completed, the computer automatically records the feeding amount into a production report of the corresponding production batch, and the process master can monitor the flow value on line and control the running state of related equipment of the system.
When acid is added, the acid adding speed and the end point PH value of the acid adding completion are set, after clicking and starting, the system firstly starts the sulfuric acid pump 22, compares the instantaneous flow rate of the acid adding detected by the flowmeter 24 with the set speed of the system, transmits a signal to the regulating valve 23 through Proportional Integral Derivative (PID), the regulating valve 23 is opened to a corresponding opening degree, the flow value is correspondingly changed at the moment, and is transmitted to the system again to be fed back to the regulating valve 23, and the acid adding speed is accurately stabilized at the set value after a plurality of regulating periods. The system can accurately calculate the cumulative amount of added sulfuric acid while adjusting, and the PH value gradually becomes smaller along with the continuous addition of acid, and after the PH value reaches the set PH value, the system judges that the acid addition is finished, and the adjusting valve 23 and the sulfuric acid pump 22 are rapidly closed, so that the acid addition is finished. The system records the pH value into a trend curve in real time, and the acid adding amount is recorded into a production report.
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (6)
1. The isooctanoic acid production system comprises an oxidation device, an acidification device and a rectification device which are sequentially connected according to working procedures, and is characterized in that the oxidation device comprises an oxidation kettle, an external heating device of the oxidation kettle is connected with a heat conduction oil mechanism, and the oxidation kettle is respectively connected with a fresh water input pipeline, a nitrogen supply pipeline, an isooctanol tank, a hydrogen recovery pipeline and a catalyst input pipeline; the oxidation kettle is connected with the acidification device through a sodium iso-octoate discharge pipeline, the acidification device comprises an acidification kettle, the acidification kettle is respectively connected with a fresh water tank and a sulfuric acid tank through pipelines, the acidification kettle is also connected with a cooling circulating water system and a crude iso-octoate discharge pipeline, a stirring mechanism is arranged in the acidification kettle, and the crude iso-octoate discharge pipeline is connected with the rectification device;
the hydrogen recovery pipeline on be provided with pressure transmitter and governing valve, oxidation cauldron and isooctanol jar between be provided with isooctanol pump, automatic trip valve and flowmeter.
2. The isooctanoic acid production system of claim 1 wherein a water injection pump, an automatic shut-off valve and a flow meter are disposed on the line between the acidification tank and the fresh water tank.
3. The isooctanoic acid production system of claim 1, wherein a sulfuric acid pump, a regulating valve and a flowmeter are arranged on a pipeline between the acidification tank and the sulfuric acid tank.
4. The isooctanoic acid production system of claim 1 wherein the crude isooctanoic acid discharge line is provided with crude isooctanoic acid Xin Suanbeng.
5. The isooctanoic acid production system of claim 1 wherein the isooctanol canister is connected to an isooctanol recovery canister, the isooctanol recovery canister being connected to a blow-down canister.
6. The isooctanoic acid production system of claim 1, wherein the rectifying device comprises a rectifying still connected with a crude isooctanoic acid discharge pipeline, wherein the rectifying still is connected with a front fractionating tank through a rectifying condenser, and the front fractionating tank is connected with a finished product tank through an isooctanoic acid intermediate tank.
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| CN201710100417.9A CN106748746B (en) | 2017-02-23 | 2017-02-23 | Isooctanoic acid production system |
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| CN201710100417.9A CN106748746B (en) | 2017-02-23 | 2017-02-23 | Isooctanoic acid production system |
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| CN106748746B true CN106748746B (en) | 2024-04-02 |
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| CN108285426A (en) * | 2017-10-30 | 2018-07-17 | 赵君 | A kind of continuously acidizing device and its technique |
| CN115093318A (en) * | 2022-05-06 | 2022-09-23 | 青岛三瑞节能环保技术有限公司 | Process and device for producing isovaleric acid from isoamyl alcohol |
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