CN117304010B - Method for separating phenol acetophenone azeotrope - Google Patents
Method for separating phenol acetophenone azeotrope Download PDFInfo
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- CN117304010B CN117304010B CN202311617931.1A CN202311617931A CN117304010B CN 117304010 B CN117304010 B CN 117304010B CN 202311617931 A CN202311617931 A CN 202311617931A CN 117304010 B CN117304010 B CN 117304010B
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- 238000000034 method Methods 0.000 title claims abstract description 31
- YPYLQUJJMQMVFA-UHFFFAOYSA-N phenol;1-phenylethanone Chemical compound OC1=CC=CC=C1.CC(=O)C1=CC=CC=C1 YPYLQUJJMQMVFA-UHFFFAOYSA-N 0.000 title claims abstract description 18
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 112
- KWOLFJPFCHCOCG-UHFFFAOYSA-N Acetophenone Chemical compound CC(=O)C1=CC=CC=C1 KWOLFJPFCHCOCG-UHFFFAOYSA-N 0.000 claims abstract description 100
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 87
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 66
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 56
- 239000000498 cooling water Substances 0.000 claims abstract description 53
- 238000003860 storage Methods 0.000 claims abstract description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000012074 organic phase Substances 0.000 claims abstract description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000003546 flue gas Substances 0.000 claims abstract description 16
- 239000012071 phase Substances 0.000 claims abstract description 16
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 13
- 239000000243 solution Substances 0.000 claims description 55
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 34
- 238000006243 chemical reaction Methods 0.000 claims description 20
- NESLWCLHZZISNB-UHFFFAOYSA-M sodium phenolate Chemical compound [Na+].[O-]C1=CC=CC=C1 NESLWCLHZZISNB-UHFFFAOYSA-M 0.000 claims description 19
- 238000005406 washing Methods 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 18
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 17
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 16
- 239000002912 waste gas Substances 0.000 claims description 15
- 239000011259 mixed solution Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 239000001569 carbon dioxide Substances 0.000 claims description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 6
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 239000008346 aqueous phase Substances 0.000 claims 1
- 239000000047 product Substances 0.000 description 18
- 235000011121 sodium hydroxide Nutrition 0.000 description 17
- 239000003513 alkali Substances 0.000 description 10
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 4
- 238000009776 industrial production Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- YBYIRNPNPLQARY-UHFFFAOYSA-N 1H-indene Chemical compound C1=CC=C2CC=CC2=C1 YBYIRNPNPLQARY-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000008031 plastic plasticizer Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000012266 salt solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000012938 design process Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 159000000011 group IA salts Chemical class 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
Classifications
-
- 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
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/685—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/70—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment
- C07C37/72—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/68—Purification; separation; Use of additives, e.g. for stabilisation
- C07C37/86—Purification; separation; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification
-
- 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
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/80—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
-
- 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
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/85—Separation; Purification; Stabilisation; Use of additives by treatment giving rise to a chemical modification
Abstract
The invention relates to a method for separating a phenol acetophenone azeotrope, which mainly comprises an azeotrope storage tank, a salinization kettle, an azeotrope input pipeline, a water pipeline, a sodium carbonate solution storage tank, a sodium carbonate solution input pipeline, a cooling water output pipeline, an organic phase output pipeline, a water phase output pipeline, a cooling water tank, an acetophenone kettle, an anhydrous sodium sulfate input pipeline, an acetophenone output pipeline, a filter tank, an acetophenone storage tank, a phenol kettle, a sodium hydroxide solution input pipeline, a boiler flue gas output pipeline, a sodium carbonate solution output pipeline, a phenol storage tank and a transfer pump.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a method for separating a phenol acetophenone mixed azeotrope generated in recycling phenol tar produced in petrochemical industry.
Background
In the industrial production of petrochemical industry, the synthesis of phenol/acetone by the cumene method is a domestic common production process. During the synthesis process, hazardous waste phenol raffinate, also called phenol tar, is mixed raffinate (slag) containing one or more organic components such as phenol, acetophenone, alpha-methylstyrene, isopropylbenzene, indene and derivatives thereof. According to the basic principles of 'reduction, reclamation and harmlessness' followed by the environmental protection of solid waste pollution in China, the utilization of the residual liquid as a raw material through a green chemical technology is a recent development trend. The main component phenol in the phenol raffinate has a boiling point of 181.84 ℃ under normal pressure, the acetophenone has a boiling point of 202.11 ℃ under normal pressure, a phenol acetophenone azeotrope can be produced in industrial production, the azeotropic temperature under normal pressure is 202.32 ℃, and the azeotrope can not be completely separated by conventional distillation or fractionation means.
In the recycling process, acetophenone products in the residual liquid are industrial products with great economic value. The acetophenone product has wide application, can be used as raw materials of organic synthesis industries such as pesticides, medicines, spices, paints, fuels and the like, is also a good extractant and solvent, and has high purity of 99.5 percent, and can be used as a high-quality plasticizer material with high price. Therefore, under the condition of reducing the recovery treatment cost, the development process flow is short, the operation condition is simple, and the high added value of the high-purity acetophenone separation and purification and phenol raffinate recycling treatment product can be realized.
At present, the phenol acetophenone azeotrope is separated mainly by a pressure-changing process mode, the process can not completely separate or remove the azeotrope, and the problems of high energy consumption, resource waste and the like exist.
Carbon dioxide is generated in the combustion process of the fuel oil, the fuel gas and the coal-fired boiler, and the industrial standard emission is usually carried out after denitration, desulfurization and dust removal. How to effectively reduce carbon dioxide emissions in industrial production is also a new subject to be continuously searched in industrial production.
Disclosure of Invention
The invention aims to overcome the problems in the prior art, and provides a method for separating a phenol acetophenone azeotrope, which utilizes the characteristic of high carbon dioxide content in exhaust gas discharged from a natural gas boiler, adopts an alkali circulation regeneration process method to effectively separate a phenol and acetophenone mixture, so as to obtain high-purity phenol and acetophenone, improve the added value of products, shorten the process flow and reduce the production energy consumption.
The technical scheme of the invention is as follows: the method for separating the phenol acetophenone azeotrope mainly comprises an azeotrope storage tank, a salinization kettle, an azeotrope input pipeline, a water pipeline, a sodium carbonate solution storage tank, a sodium carbonate solution input pipeline, a first cooling water output pipeline, an organic phase output pipeline, a water phase output pipeline, a cooling water tank, an acetophenone kettle, an anhydrous sodium sulfate input pipeline, an acetophenone output pipeline, a first filter tank, an acetophenone storage tank, a phenol kettle, a sodium hydroxide solution input pipeline, a boiler flue gas output pipeline, a second cooling water input pipeline, a second cooling water output pipeline, a sodium carbonate solution output pipeline, a phenol output pipeline, a second filter tank, a phenol storage tank and a transfer pump; the method is characterized by comprising the following steps of:
a. the phenol acetophenone azeotrope is pumped into a salinization kettle through an azeotrope input pipeline by an azeotrope storage tank through a transfer pump, and sodium carbonate with the molar ratio is added into the azeotrope storage tank through a sodium carbonate solution input pipeline: phenol=1.1: 1, sodium carbonate can fully react with phenol in the azeotrope, and the phenol in the azeotrope is completely changed into sodium phenolate and sodium bicarbonate;
b. after the reaction is completed, opening cooling water in the salinization kettle, cooling the kettle, and outputting the cooling water through a first cooling water input pipeline and a first cooling water output pipeline;
c. separating liquid, wherein the organic phase in the salinization kettle is acetophenone product. The mixture is output to an acetophenone kettle through an organic phase output pipeline by a transfer pump, is subjected to water washing, is subjected to liquid separation again, is input into anhydrous sodium sulfate through an anhydrous sodium sulfate input pipeline for drying, is output by an acetophenone output pipeline, is filtered by a first filter box by the transfer pump, and is sent to an acetophenone storage tank for storage;
d. the water phase in the salinization kettle is combined into a mixed solution of sodium phenolate, sodium bicarbonate and a small amount of sodium carbonate. The waste gas is output to a phenol kettle through a water phase output pipeline by a transfer pump, the treated waste gas of the boiler is introduced into a boiler flue gas input pipeline, the water phase is mixed with the solution, carbon dioxide in the waste gas of the boiler can convert sodium phenolate in the solution into phenol and sodium bicarbonate, and the sodium phenolate is output through the boiler flue gas output pipeline after the reaction is finished;
e. after the reaction is finished, opening cooling water in the phenol kettle, cooling the interior of the kettle, wherein the cooling water enters through a second cooling water input pipeline and is output through a second cooling water output pipeline;
f. separating the liquid, wherein the organic phase in the phenol kettle is phenol product. Outputting by a phenol output pipeline, filtering by a transfer pump in a second filter tank, and delivering to a phenol storage tank for storage to obtain a qualified phenol product;
g. sodium bicarbonate is added into the phenol kettle solution in a molar ratio through a sodium hydroxide solution input pipeline: sodium hydroxide=1:1 sodium hydroxide, so that sodium bicarbonate in the solution is converted into sodium carbonate to obtain a sodium carbonate mixed solution;
h. after the reaction is finished, the sodium carbonate mixed solution in the phenol kettle is output to a sodium carbonate solution storage tank through a sodium carbonate solution output pipeline by a transfer pump for recycling.
The salinization kettle, the acetophenone kettle and the phenol kettle are stainless steel reaction kettles with jackets and inner coils 304.
A method for separating a phenol acetophenone azeotrope utilizes the chemical property of reaction of phenol and acetophenone with an alkaline salt solution, treats the phenol acetophenone azeotrope through a salinization reaction, converts the phenol azeotroped with a target product acetophenone through an autonomous design process to obtain an acetophenone product with the purity of more than or equal to 99.7%, and realizes the efficient high-purity production of the acetophenone product.
A method for separating acetophenone azeotrope of phenol, abandon the traditional caustic soda washing method of sodium hydroxide, add sodium carbonate solution to carry on caustic wash, but the sodium carbonate solution can be recycled in the liquid-liquid separation of phenol of technological process, this method has reduced the waste salt and produced, has raised the utilization ratio of the reaction product.
A method for separating phenol acetophenone azeotrope includes such steps as adding the treated waste gas of boiler, desulfurizing, denitrating, removing dust and cooling, and features that the carbon dioxide content is 6-8% and the carbon dioxide in the waste gas of boiler can transform sodium phenolate in solution into phenol and sodium hydrogen carbonate.
Comparative document 1, application number: 202111215213.2A method, system and application of acetophenone recovery "another technical scheme is that after water washing in the effluent stream of the heavy-duty tower top, alkali liquor is added for alkali washing, since phenol belongs to weak acid, sodium hydroxide solution is preferably added for strengthening alkali washing, sodium phenolate is produced by the reaction of phenol and sodium hydroxide, and the sodium phenolate solution is easily dissolved in water; the material to be treated enters a heavy-removal tower A, heavy components are extracted from the tower bottom of the heavy-removal tower A, water and/or water vapor are sprayed into the light components extracted from the tower top of the heavy-removal tower A at a high speed, alkali liquor is sprayed into a mixture of the light components and the water and/or the water vapor, the mixture enters an alkali washing unit D for alkali washing and liquid-liquid separation, an organic phase II after alkali washing enters a water washing unit B for water washing and liquid-liquid separation, the water phase after water washing is subjected to post-treatment such as cooling crystallization to recover phenol, the organic phase after water washing is used as the feed of a rectifying tower C, acetophenone products are extracted from the side line of the rectifying tower C, a material flow from the tower top of the rectifying tower enters a water washing unit B, and material flow from the tower bottom of the rectifying tower is extracted or returned to the heavy-removal tower A as the feed. The reference is to add sodium hydroxide for alkali washing after heavy components are removed, then to extract phenol and acetophenone by water washing, and the reference is to add sodium carbonate solution for alkali washing, wherein the sodium carbonate solution can be recycled in the liquid-liquid separation of phenol in the process flow.
The beneficial effects of the invention are as follows: the invention solves the problem that the phenol acetophenone azeotrope can be separated without changing the pressure, the process can completely separate the azeotrope, the purity of the acetophenone is more than or equal to 99.7 percent, and the acetophenone can be directly used as a novel plastic plasticizer; the process flow is simple, the operability is high, the energy consumption is low, the recycling of the salt solution is realized, the waste gas of the natural gas boiler is secondarily utilized, the carbon emission is effectively reduced, the disposal cost and the process difficulty of enterprises are reduced, the recycling of high added value resources of dangerous wastes is realized, and the pollution-removing effect on the environment is greatly promoted.
Drawings
FIG. 1 is a schematic illustration of the process flow of the present invention;
in fig. 1: 1. an azeotrope storage tank; 2. a salinization kettle; 3. an azeotrope input conduit; 4. a water pipe; 5. a sodium carbonate solution storage tank; 6. a sodium carbonate solution input pipe; 7. a first cooling water input pipe; 8. a first cooling water output pipe; 9. an organic phase output conduit; 10. a water phase output pipeline; 11. a cooling water tank; 12. an acetophenone kettle; 13. anhydrous sodium sulfate input pipeline; 14. an acetophenone output pipe; 15. a first filter box; 16. an acetophenone storage tank; 17. a phenol kettle; 18. a sodium hydroxide solution input pipeline; 19. a boiler flue gas input pipeline; 20. a boiler flue gas output duct; 21. a second cooling water input pipe; 22. a second cooling water output pipe; 23. a sodium carbonate solution output pipe; 24. a phenol output pipe; 25. a second filter box; 26. a phenol storage tank; 27. and a material transferring pump.
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 provides the following technical scheme: the method for separating the phenol acetophenone azeotrope mainly comprises an azeotrope storage tank 1, a salinization kettle 2, an azeotrope input pipeline 3, a water pipeline 4, a sodium carbonate solution storage tank 5, a sodium carbonate solution input pipeline 6, a first cooling water input pipeline 7, a first cooling water output pipeline 8, an organic phase output pipeline 9, a water phase output pipeline 10, a cooling water tank 11, an acetophenone kettle 12, an anhydrous sodium sulfate input pipeline 13, an acetophenone output pipeline 14, a first filter tank 15, an acetophenone storage tank 16, a phenol kettle 17, a sodium hydroxide solution input pipeline 18, a boiler flue gas input pipeline 19, a boiler flue gas output pipeline 20, a second cooling water input pipeline 21, a second cooling water output pipeline 22, a sodium carbonate solution output pipeline 23, a phenol output pipeline 24, a second filter tank 25, a phenol storage tank 26 and a transfer pump 27; the method is characterized by comprising the following steps of:
a. the phenol acetophenone azeotrope is pumped into a salinization kettle 2 from an azeotrope storage tank 1 through an azeotrope input pipeline 3 by a transfer pump 27, and sodium carbonate is added into the azeotrope storage tank 1 through a sodium carbonate solution input pipeline 6 according to the molar ratio: phenol=1.1: 1, sodium carbonate can fully react with phenol in the azeotrope, and the phenol in the azeotrope is completely changed into sodium phenolate and sodium bicarbonate;
b. after the reaction is completed, cooling water in the salinization kettle 2 is opened to cool the kettle, the cooling water enters through a first cooling water input pipeline 7 and is output through a first cooling water output pipeline 8;
c. separating liquid, wherein the organic phase in the salinization kettle 2 is acetophenone product. The mixture is output to an acetophenone kettle 12 through an organic phase output pipeline 9 by a transfer pump 27, is subjected to water washing, is subjected to liquid separation again, is input into anhydrous sodium sulfate through an anhydrous sodium sulfate input pipeline 13, is dried, is output by an acetophenone output pipeline 14, is filtered by a first filter tank 15 by the transfer pump 27, and is sent to an acetophenone storage tank 16 for storage;
d. the water phase in the salinization kettle 2 is combined into a mixed solution of sodium phenolate, sodium bicarbonate and a small amount of sodium carbonate. The waste gas is output to a phenol kettle 17 through a water phase output pipeline 10 by a transfer pump 27, the treated waste gas of the boiler is introduced into a boiler flue gas input pipeline 19, the water phase is mixed with the solution, carbon dioxide in the waste gas of the boiler can convert sodium phenolate in the solution into phenol and sodium bicarbonate, and the sodium phenolate is output through a boiler flue gas output pipeline 20 after the reaction is finished;
e. after the reaction is finished, opening cooling water in the phenol kettle 17, cooling the interior of the kettle, and outputting the cooling water through a second cooling water input pipeline 21 and a second cooling water output pipeline 22;
f. the organic phase in the phenol tank 17 is phenol product. The mixture is output by a phenol output pipeline 24, enters a second filter tank 25 through a transfer pump 27 for filtering, and is sent to a phenol storage tank 26 for storage, so that a qualified phenol product is obtained;
g. sodium bicarbonate is added to the solution in the phenol tank 17 in molar ratio through a sodium hydroxide solution input line 18: sodium hydroxide=1:1 sodium hydroxide, so that sodium bicarbonate in the solution is converted into sodium carbonate to obtain a sodium carbonate mixed solution;
h. after the reaction is completed, the sodium carbonate mixed solution in the phenol kettle 17 is output to the sodium carbonate solution storage tank 5 through the sodium carbonate solution output pipeline 23 by the transfer pump 27 for recycling.
Example 1:
the azeotrope composition in the raw materials is:
5t of phenol acetophenone azeotrope is pumped into a salinization kettle 2 from an azeotrope storage tank 1 through an azeotrope input pipeline 3 by a transfer pump 27, and sodium carbonate with the molar ratio is added into the azeotrope storage tank 1 through a sodium carbonate solution input pipeline 6: a solution of sodium carbonate with phenol=1.1:1, wherein the dropping speed is 2-3t/h, and the sodium carbonate can fully react with phenol in the azeotrope to completely change the phenol in the azeotrope into sodium phenolate and sodium bicarbonate;
after the reaction is completed, cooling water in the salinization kettle 2 is opened, the temperature in the kettle is reduced to 25-35 ℃, the cooling water enters through a first cooling water input pipeline 7 and is output through a first cooling water output pipeline 8;
separating liquid, wherein the organic phase in the salinization kettle 2 is acetophenone product. The mixture is output to an acetophenone kettle 12 through an organic phase output pipeline 9 by a transfer pump 27, is subjected to water washing and liquid separation again, is input into anhydrous sodium sulfate through an anhydrous sodium sulfate input pipeline 13 for drying, is output by an acetophenone output pipeline 14, enters a first filter tank 15 for filtering by the transfer pump 27, is sent to an acetophenone storage tank 16 for storage, and the acetophenone purity is more than or equal to 99.7 percent, and can be directly used as a novel plastic plasticizer and a medical intermediate.
The water phase in the salinization kettle 2 is combined into a mixed solution of sodium phenolate, sodium bicarbonate and a small amount of sodium carbonate. The waste gas is output to a phenol kettle 17 through a water phase output pipeline 10 by a transfer pump 27, the treated waste gas of the boiler is introduced into a boiler flue gas input pipeline 19, the water phase is mixed with the solution, carbon dioxide in the waste gas of the boiler can convert sodium phenolate in the solution into phenol and sodium bicarbonate, and the sodium phenolate is output through a boiler flue gas output pipeline 20 after the reaction is finished;
after the reaction is completed for 1.5 hours, opening cooling water in the phenol kettle 17, cooling the interior of the kettle to 20-30 ℃, wherein the cooling water enters through a second cooling water input pipeline 21 and is output through a second cooling water output pipeline 22;
the organic phase in the phenol tank 17 is phenol product. The mixture is output by a phenol output pipeline 24, enters a second filter tank 25 through a transfer pump 27 for filtering, and is sent to a phenol storage tank 26 to obtain a qualified phenol product;
to the solution in the phenol tank 17 was added 100kg sodium hydroxide molar ratio sodium bicarbonate via sodium hydroxide solution input line 18: sodium hydroxide=1:1, converting sodium bicarbonate in the solution into sodium carbonate to obtain a sodium carbonate mixed solution;
after the reaction is completed, the sodium carbonate mixed solution in the phenol kettle 17 is output to the sodium carbonate solution storage tank 5 through the sodium carbonate solution output pipeline 23 by the transfer pump 27 for recycling.
Claims (1)
1. The separation method of the phenol acetophenone azeotrope mainly comprises an azeotrope storage tank (1), a salinization kettle (2), an azeotrope input pipeline (3), a water pipeline (4), a sodium carbonate solution storage tank (5), a sodium carbonate solution input pipeline (6), a first cooling water input pipeline (7), a first cooling water output pipeline (8), an organic phase output pipeline (9), an aqueous phase output pipeline (10), a cooling water tank (11), an acetophenone kettle (12), an anhydrous sodium sulfate input pipeline (13), an acetophenone output pipeline (14), a first filter tank (15), an acetophenone storage tank (16), a phenol kettle (17), a sodium hydroxide solution input pipeline (18), a boiler flue gas input pipeline (19), a boiler flue gas output pipeline (20), a second cooling water input pipeline (21), a second cooling water output pipeline (22), a sodium carbonate solution output pipeline (23), a phenol output pipeline (24), a second filter tank (25), a phenol storage tank (26) and a transfer pump (27); the method is characterized by comprising the following steps of:
a. the phenol acetophenone azeotrope is pumped into a salinization kettle (2) through an azeotrope input pipeline (3) by an azeotrope storage tank (1) through a transfer pump (27), and sodium carbonate with a molar ratio is added into the azeotrope storage tank (1) through a sodium carbonate solution input pipeline (6): phenol=1.1: 1, sodium carbonate can fully react with phenol in the azeotrope, and the phenol in the azeotrope is completely changed into sodium phenolate and sodium bicarbonate;
b. after the reaction is finished, cooling water in the salinization kettle (2) is opened to cool the kettle, the cooling water enters through a first cooling water input pipeline (7) and is output through a first cooling water output pipeline (8);
c. separating liquid, wherein an organic phase in the salinization kettle (2) is an acetophenone product; the mixture is output to an acetophenone kettle (12) through an organic phase output pipeline (9) by a material transferring pump (27), is subjected to water washing, is subjected to liquid separation again, is input into anhydrous sodium sulfate by an anhydrous sodium sulfate input pipeline (13) for drying, is output by an acetophenone output pipeline (14), enters a first filter tank (15) by the material transferring pump (27) for filtering, and is sent to an acetophenone storage tank (16) for storage;
d. the water phase in the salinization kettle (2) is combined to form a mixed solution of sodium phenolate, sodium bicarbonate and a small amount of sodium carbonate; the waste gas is output to a phenol kettle (17) through a water phase output pipeline (10) by a transfer pump (27), the treated waste gas of the boiler is introduced into a boiler flue gas input pipeline (19), carbon dioxide in the waste gas of the boiler can convert sodium phenolate in the solution into phenol and sodium bicarbonate, and the sodium phenolate is output through a boiler flue gas output pipeline (20) after the reaction is finished;
e. after the reaction is finished, opening cooling water in the phenol kettle (17), cooling the interior of the kettle, wherein the cooling water enters through a second cooling water input pipeline (21) and is output through a second cooling water output pipeline (22);
f. separating liquid, wherein an organic phase in the phenol kettle (17) is a phenol product; outputting by a phenol output pipeline (24), filtering by a transfer pump (27) in a second filter tank (25), and delivering to a phenol storage tank (26) for storage to obtain a qualified phenol product;
g. sodium bicarbonate is added into the solution of the phenol kettle (17) through a sodium hydroxide solution input pipeline (18) in a molar ratio of: sodium hydroxide=1:1 sodium hydroxide, so that sodium bicarbonate in the solution is converted into sodium carbonate to obtain a sodium carbonate mixed solution;
h. after the reaction is finished, the sodium carbonate mixed solution in the phenol kettle (17) is output to a sodium carbonate solution storage tank (5) through a sodium carbonate solution output pipeline (23) by a transfer pump (27) for recycling.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB824024A (en) * | 1956-03-16 | 1959-11-25 | California Research Corp | Oxidation process |
| CN105669383A (en) * | 2016-03-10 | 2016-06-15 | 张殿豪 | Method for removing acid in phenol-acetone device decomposition liquid |
| CN214537448U (en) * | 2021-02-24 | 2021-10-29 | 乐陵力维化学品有限责任公司 | Phenol waste gas high-efficient utilization device |
| CN217410739U (en) * | 2022-06-19 | 2022-09-13 | 乐陵力维化学品有限责任公司 | Device for producing crude acetophenone in phenol residual liquid |
| CN115991640A (en) * | 2021-10-19 | 2023-04-21 | 中国石油化工股份有限公司 | Method, system and application for recovering acetophenone |
-
2023
- 2023-11-30 CN CN202311617931.1A patent/CN117304010B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB824024A (en) * | 1956-03-16 | 1959-11-25 | California Research Corp | Oxidation process |
| CN105669383A (en) * | 2016-03-10 | 2016-06-15 | 张殿豪 | Method for removing acid in phenol-acetone device decomposition liquid |
| CN214537448U (en) * | 2021-02-24 | 2021-10-29 | 乐陵力维化学品有限责任公司 | Phenol waste gas high-efficient utilization device |
| CN115991640A (en) * | 2021-10-19 | 2023-04-21 | 中国石油化工股份有限公司 | Method, system and application for recovering acetophenone |
| CN217410739U (en) * | 2022-06-19 | 2022-09-13 | 乐陵力维化学品有限责任公司 | Device for producing crude acetophenone in phenol residual liquid |
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