CN115025731A - Continuous production device and process of o-phenylphenol - Google Patents

Continuous production device and process of o-phenylphenol Download PDF

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CN115025731A
CN115025731A CN202210821809.5A CN202210821809A CN115025731A CN 115025731 A CN115025731 A CN 115025731A CN 202210821809 A CN202210821809 A CN 202210821809A CN 115025731 A CN115025731 A CN 115025731A
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reactor
heat exchanger
dibenzofuran
continuous
phenylphenol
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杨连成
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Liaoning Petrocchemical College
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Liaoning Petrocchemical College
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    • 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
    • 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
    • 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
    • B01J19/0006—Controlling or regulating processes
    • B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • 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
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/02—Feed or outlet devices; Feed or outlet control devices for feeding measured, i.e. prescribed quantities of reagents
    • 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
    • C07C37/01—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by replacing functional groups bound to a six-membered aromatic ring by hydroxy groups, e.g. by hydrolysis
    • C07C37/055—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by replacing functional groups bound to a six-membered aromatic ring by hydroxy groups, e.g. by hydrolysis the substituted group being bound to oxygen, e.g. ether group
    • 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
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00027—Process aspects
    • B01J2219/00033—Continuous processes
    • 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
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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  • Organic Chemistry (AREA)
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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a continuous production device and a continuous production process of o-phenylphenol, wherein the device comprises: metal sodium melting tank, first constant current pump, dibenzofuran dissolving tank, second constant current pump, continuous reactor, metal sodium melting tank is through first constant current pump output material to continuous reactor, and dibenzofuran dissolving tank is through second constant current pump output material to continuous reactor, still includes: the system comprises a delay pipeline, a first heat exchanger, a quenching reactor, a second heat exchanger and a product tank; the inlet of the delay pipeline is communicated with the continuous reactor, and the outlet of the delay pipeline is communicated with the inlet of the first heat exchanger; the outlet of the first heat exchanger is communicated with the quenching reactor, the quenching reactor is communicated with the inlet of the second heat exchanger, and the outlet of the second heat exchanger is communicated with the product tank, so that the problems that continuous production cannot be realized and the process is complex in the prior art are solved, the reaction temperature and flow can be accurately controlled during application, the intrinsic safety of the reaction is obviously improved, and the reaction yield and selectivity are high.

Description

Continuous production device and process of o-phenylphenol
Technical Field
The invention relates to the field of organic chemical industry, in particular to a continuous production device and a continuous production process of o-phenylphenol.
Background
O-phenylphenol, also known as 2-hydroxybiphenyl, known by the english name othiophenylenol, abbreviated as OPP, is a white or off-white crystal in appearance; has special odor and is slightly soluble in water. It is an important fine organic chemical product with wide application. The product can be used for producing sterilization preservative, flame retardant, antistaling agent for vegetables and fruits, printing and dyeing auxiliary, medicine and dye intermediate, etc.
The synthesis method of o-phenylphenol mainly comprises a biphenyl sulfonation or halogenated alkali fusion method, an amino biphenyl diazotization hydrolysis method, a diazonium salt and phenol condensation method, a diphenyl ether rearrangement method, a phenol alkylation dehydrogenation method, a dibenzofuran ring opening method, a cyclohexanone dimerization dehydrogenation method and a transition metal catalytic coupling method, wherein the dibenzofuran catalytic hydrogenation method is a synthesis method with relatively high industrial application value, and has the advantages of cheap and easily obtained raw materials and certain development prospect. The catalytic hydrogenation method of the dibenzofuran uses dibenzofuran as a raw material, ethylene glycol dimethyl ether or diethylene glycol dimethyl ether as a solvent, metal sodium is added, and the reaction is carried out under the protection of nitrogen; in the existing preparation process, links such as feeding of solid sodium exist, great potential safety hazard exists, serialization cannot be realized, and the existing production equipment is too complex and not beneficial to industrial production.
Disclosure of Invention
The invention provides a continuous production device and a continuous production process for o-phenylphenol, which solve the problems that the continuous production cannot be realized and the process is complex in the prior art, can accurately control the reaction temperature and flow during application, obviously improve the intrinsic safety of the reaction and have high reaction yield and selectivity.
In order to solve the technical problem, the invention provides the following technical scheme:
an apparatus for continuously producing o-phenylphenol, comprising: metal sodium melting tank, first constant current pump, dibenzofuran dissolving tank, second constant current pump, continuous reactor, metal sodium melting tank is through first constant current pump output material to continuous reactor, and dibenzofuran dissolving tank is through second constant current pump output material to continuous reactor, still includes: the system comprises a delay pipeline, a first heat exchanger, a quenching reactor, a second heat exchanger and a product tank;
the inlet of the delay pipeline is communicated with the continuous reactor, and the outlet of the delay pipeline is communicated with the inlet of the first heat exchanger; the outlet of the first heat exchanger is communicated with the quenching reactor, the quenching reactor is communicated with the inlet of the second heat exchanger, and the outlet of the second heat exchanger is communicated with the product tank.
Further, the apparatus further comprises: the first check valve is arranged between the first constant flow pump and the continuous reactor, and the second check valve is arranged between the second constant flow pump and the continuous reactor.
Further, the quenching reactor is connected with a third constant flow pump for pumping the quenching agent, and a third one-way valve is arranged between the third constant flow pump and the quenching reactor.
The continuous reactor is selected from any one of a micromixer, a static mixer or a tubular reactor.
The scheme also provides a continuous production process of o-phenylphenol, and the device comprises the following steps:
s1, putting the metal sodium into a metal sodium melting tank, and heating to completely melt the metal sodium to obtain molten metal sodium;
s2, mixing dibenzofuran and diethylene glycol dimethyl ether, adding into a dibenzofuran dissolving tank, heating to completely dissolve dibenzofuran to obtain a dibenzofuran solution;
s3, opening a constant flow pump and a constant flow pump, and conveying the molten metal sodium and the dibenzofuran solution into a continuous reactor for mixing reaction; the materials enter a delay pipeline to continue reacting, then enter a first heat exchanger for cooling, then enter a quenching reactor, and are added with a quenching agent, so that the reaction materials are quenched in the quenching reactor, and the quenched materials enter a second heat exchanger for cooling and then enter a product tank;
s4, solvent recovery: distilling the material in the product tank to recover solvent, acidifying the residue with dilute sulfuric acid, extracting with toluene, evaporating to remove toluene solvent, and rectifying the product to obtain o-phenylphenol.
The method comprises the following steps of continuously producing o-phenylphenol by using metal sodium and dibenzofuran as initial raw materials and ethers as solvents and adopting a continuous reactor, wherein the reaction formula is shown as a formula (1):
Figure BDA0003742551510000021
the method can accurately control the reaction temperature and flow, remarkably improve the intrinsic safety of the reaction, and have high reaction yield and selectivity.
Preferably, the mass ratio of the dibenzofuran to the diethylene glycol dimethyl ether in step S2 is 1:1 to 1: 10.
Preferably, the feeding molar ratio of the sodium metal and the dibenzofuran in the step S3 is 1: 1-2.2: 1.
Preferably, the mixing reaction temperature of the sodium metal and the oxygen in the step S3 is 100-120 ℃.
Preferably, the residence time of the material in the delay line in step S3 is 1-10 minutes.
Preferably, the quenching agent in step S3 is selected from any one of methanol, ethanol, water or alcohol-water mixture.
Preferably, the cooling temperature of the first heat exchanger is below 30 ℃; the temperature of the second heat exchanger is reduced to below 30 DEG C
Compared with the prior art, the invention has the following advantages:
the method takes metal sodium and dibenzofuran as initial raw materials and ethers as solvents, adopts a continuous reactor to continuously produce o-phenylphenol, can accurately control reaction temperature and flow, obviously improves reaction yield, and has high selectivity.
The mode of conveying materials by using a constant-flow pump avoids potential safety hazards caused by opening a reactor and adding sodium and dibenzofuran in the reaction process, so that the use safety can be improved; the arrangement of the delay pipeline increases the reaction time, and the arrangement of the quenching reactor can finish the reaction, thereby realizing the continuity of the reaction and saving the time and the cost.
Drawings
The accompanying drawings, which are included to provide a further understanding of the embodiments of the invention and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the invention and together with the description serve to explain the principles of the invention. In the drawings:
FIG. 1 is a schematic view of the structure of the present invention.
Reference numbers and corresponding part names in the drawings:
1. a metallic sodium melting tank; 2. a first constant flow pump; 3. a first check valve; 4. a dibenzofuran dissolving tank; 5. a second constant flow pump; 6. a second one-way valve; 7. a continuous reactor; 8. a delay line; 9. a first heat exchanger; 10. a third constant flow pump; 11. a third check valve; 12. a quench reactor; 13. a second heat exchanger; 14. and (5) a product tank.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to examples, and the exemplary embodiments and descriptions thereof are only used for explaining the present invention and are not used as limitations of the present invention.
Example 1
As shown in fig. 1, a continuous production apparatus for o-phenylphenol, comprising: metal sodium melting tank 1, first constant current pump 2, dibenzofuran dissolve jar 4, second constant current pump 5, continuous reactor 7, metal sodium melting tank 1 is through 2 output material of first constant current pump to continuous reactor 7, and dibenzofuran dissolve jar 4 is through 5 output material of second constant current pump to continuous reactor 7, still includes: a delay line 8, a first heat exchanger 9, a quench reactor 12, a second heat exchanger 13, and a product tank 14; the inlet of the delay pipeline 8 is communicated with the continuous reactor 7, and the outlet of the delay pipeline 8 is communicated with the inlet of the first heat exchanger 9; an outlet of the first heat exchanger 9 is communicated with a quenching reactor 12, an inlet of the quenching reactor 12 is communicated with an inlet of a second heat exchanger 13, and an outlet of the second heat exchanger 13 is communicated with a product tank 14; a first check valve 3 is arranged between the first constant flow pump 2 and the continuous reactor 7, and a second check valve 6 is arranged between the second constant flow pump 5 and the continuous reactor 7; the quenching reactor 12 is connected with a third constant flow pump 10 for pumping a quenching agent, and a third one-way valve 11 is arranged between the third constant flow pump 10 and the quenching reactor 12.
Example 2
The continuous production process of o-phenylphenol using the apparatus in example 1 was as follows:
s1, putting metal sodium into a metal sodium melting tank 1, and heating to 120 ℃ to completely melt the metal sodium;
s2, carrying out mass ratio of dibenzofuran to diethylene glycol dimethyl ether of 1: 4, adding the mixture into a dibenzofuran dissolving tank 4, heating to 120 ℃, and completely dissolving dibenzofuran;
s3, starting a first constant flow pump 2 and a second constant flow pump 5, conveying the molten metal sodium and the dibenzofuran solution into a continuous reactor 7, mixing and reacting at 200 ℃, and adjusting the flow ratio to ensure that the feeding molar ratio of the metal sodium and the dibenzofuran is 1.6: 1; the materials enter a delay pipeline 8 to continue reacting, the residence time of the materials is 10 minutes, then the materials enter a first heat exchanger 9 to be cooled to a temperature below 30 ℃, then the materials enter a quenching reactor 12, a quenching agent methanol enters the quenching reactor 12 through a third constant flow pump 10 and a one-way valve 11, the reaction materials are quenched in the quenching reactor, the quenching reaction releases heat, and the quenched materials enter a second heat exchanger 13 to be cooled to a temperature below 30 ℃ and then enter a product tank 14;
s4, solvent recovery: adding the materials in the product tank into a distillation kettle, and distilling to recover the solvent; and acidifying the residue by adding dilute sulfuric acid until the pH value is less than 3, extracting by using toluene, evaporating to remove the toluene solvent, and obtaining the product of rectified o-phenylphenol with the yield of 98%.
Example 3
The continuous production process of o-phenylphenol using the apparatus in example 1 was as follows:
s1, putting metal sodium into a metal sodium melting tank 1, and heating to 120 ℃ to completely melt the metal sodium;
s2, carrying out mass ratio of dibenzofuran to diethylene glycol dimethyl ether of 1:10 adding the mixture into a dibenzofuran dissolving tank 4, heating to 120 ℃ to completely dissolve dibenzofuran;
s3, starting a first constant flow pump 2 and a second constant flow pump 5, conveying the molten metal sodium and the dibenzofuran solution into a continuous reactor 7, mixing and reacting at 120 ℃, and adjusting the flow ratio to ensure that the feeding molar ratio of the metal sodium and the dibenzofuran is 2.2: 1; the materials enter a delay pipeline 8 to continue reacting, the residence time of the materials is 1 minute, then the materials enter a first heat exchanger 9 to be cooled to a temperature below 30 ℃, then the materials enter a quenching reactor 12, a quenching agent methanol enters the quenching reactor 12 through a third constant flow pump 10 and a one-way valve 11, the reaction materials are quenched in the quenching reactor, the quenching reaction releases heat, and the quenched materials enter a second heat exchanger 13 to be cooled to a temperature below 30 ℃ and then enter a product tank 14;
s4, solvent recovery: adding the materials in the product tank into a distillation kettle, and distilling to recover the solvent; and acidifying the residue by adding dilute sulfuric acid until the pH value is less than 3, extracting by using toluene, evaporating to remove the toluene solvent, and obtaining the product of rectified o-phenylphenol with the yield of 96%.
Example 4
The continuous production process of o-phenylphenol using the apparatus in example 1 was as follows:
s1, putting metal sodium into a metal sodium melting tank 1, and heating to 120 ℃ to completely melt the metal sodium;
s2, carrying out mass ratio of dibenzofuran to diethylene glycol dimethyl ether of 1:1, adding the dibenzofuran into a dibenzofuran dissolving tank 4, heating to 120 ℃ to completely dissolve dibenzofuran;
s3, starting a first constant flow pump 2 and a second constant flow pump 5, conveying the molten metal sodium and the dibenzofuran solution into a continuous reactor 7, mixing and reacting at 100 ℃, and adjusting the flow ratio to ensure that the feeding molar ratio of the metal sodium and the dibenzofuran is 1: 1; the materials enter a delay pipeline 8 to continue reacting, the residence time of the materials is 5 minutes, then the materials enter a first heat exchanger 9 to be cooled to a temperature below 30 ℃, then the materials enter a quenching reactor 12, a quenching agent methanol enters the quenching reactor 12 through a third constant flow pump 10 and a one-way valve 11, so that the reaction materials are quenched in the quenching reactor, the quenching reaction releases heat, and the quenched materials enter a second heat exchanger 13 to be cooled to a temperature below 30 ℃ and then enter a product tank 14;
s4, solvent recovery: adding the materials in the product tank into a distillation kettle, and distilling to recover the solvent; and acidifying the residue by adding dilute sulfuric acid until the pH is less than 3, extracting by using toluene, evaporating to remove the toluene solvent, and obtaining the product of rectified o-phenylphenol with the yield of 97%.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are merely exemplary embodiments of the present invention, and are not intended to limit the scope of the present invention, and any modifications, equivalent substitutions, improvements and the like made within the spirit and principle of the present invention should be included in the scope of the present invention.

Claims (10)

1. A continuous production device of o-phenylphenol comprises: metallic sodium melting tank (1), first constant current pump (2), dibenzofuran dissolve tank (4), second constant current pump (5), continuous reactor (7), metallic sodium melting tank (1) through first constant current pump (2) output material to continuous reactor (7), dibenzofuran dissolve tank (4) through second constant current pump (5) output material to continuous reactor (7), its characterized in that still includes: a delay line (8), a first heat exchanger (9), a quenching reactor (12), a second heat exchanger (13) and a product tank (14);
the inlet of the delay pipeline (8) is communicated with the continuous reactor (7), and the outlet of the delay pipeline (8) is communicated with the inlet of the first heat exchanger (9); the outlet of the first heat exchanger (9) is communicated with a quenching reactor (12), the quenching reactor (12) is communicated with the inlet of a second heat exchanger (13), and the outlet of the second heat exchanger (13) is communicated with a product tank (14).
2. The continuous production apparatus of o-phenylphenol according to claim 1, further comprising: a first one-way valve (3) arranged between the first constant flow pump (2) and the continuous reactor (7) and a second one-way valve (6) arranged between the second constant flow pump (5) and the continuous reactor (7).
3. The continuous production device of o-phenylphenol according to claim 1, wherein the quenching reactor (12) is connected with a third constant flow pump (10) for pumping a quenching agent, and a third check valve (11) is provided between the third constant flow pump (10) and the quenching reactor (12).
4. The continuous production apparatus of o-phenylphenol according to claim 1, wherein the continuous reactor (7) is selected from any one of a micromixer, a static mixer, or a tubular reactor.
5. A continuous production process of o-phenylphenol, characterized by using the apparatus according to any one of claims 1 to 4, comprising the steps of:
s1, putting the metal sodium into a metal sodium melting tank (1), and heating to completely melt the metal sodium to obtain molten metal sodium;
s2, mixing dibenzofuran and diethylene glycol dimethyl ether, adding the mixture into a dibenzofuran dissolving tank (4), and heating to completely dissolve dibenzofuran to obtain a dibenzofuran solution;
s3, opening the constant flow pump (2) and the constant flow pump (5), and conveying the molten metal sodium and the dibenzofuran solution into a continuous reactor (7) for mixing reaction; the materials enter a delay pipeline (8) for continuous reaction, then enter a first heat exchanger (9) for cooling, enter a quenching reactor (12), add a quenching agent to quench the reaction materials in the quenching reactor, enter a second heat exchanger (13) for cooling and then enter a product tank (14);
s4, solvent recovery: distilling the material in the product tank (14) to recover the solvent, adding dilute sulfuric acid into the residue to acidify, extracting with toluene, distilling to remove the toluene solvent, and rectifying the product to obtain the o-phenylphenol.
6. The continuous production process of o-phenylphenol according to claim 5, wherein the mass ratio of dibenzofuran to diethylene glycol dimethyl ether in step S2 is 1: 1-1: 10, and the feed molar ratio of sodium metal and dibenzofuran in step S3 is 1: 1-2.2: 1.
7. The continuous production process of o-phenylphenol according to claim 5, wherein the mixing reaction temperature of sodium metal and oxygen in step S3 is 100-200 ℃.
8. The continuous production process of o-phenylphenol according to claim 5, wherein the residence time of the material in the delay line (8) in step S3 is 1-10 min.
9. The continuous production process of o-phenylphenol according to claim 5, wherein the quenching agent in step S3 is selected from any one of methanol, ethanol, water or alcohol-water mixture.
10. The continuous production process of o-phenylphenol according to claim 5, wherein the cooling temperature of the first heat exchanger (9) is below 30 ℃; the temperature of the second heat exchanger (13) is reduced to below 30 ℃.
CN202210821809.5A 2022-07-12 2022-07-12 Continuous production device and process of o-phenylphenol Pending CN115025731A (en)

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Citations (9)

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Publication number Priority date Publication date Assignee Title
CN103319313A (en) * 2013-07-18 2013-09-25 辽宁石化职业技术学院 Method for preparing o-phenyl phenol by ring opening of dibenzofuran
CN109796312A (en) * 2019-02-12 2019-05-24 上海阿拉丁生化科技股份有限公司 A kind of synthetic method of 3- xenol
CN109928884A (en) * 2019-04-23 2019-06-25 沈阳化工研究院有限公司 A kind of serialization hydrogenating reduction aromatic amine prepares the device and method of cycloaliphatic amines
CN110218139A (en) * 2019-08-05 2019-09-10 山东冠森高分子材料科技股份有限公司 A method of biphenyl derivatives are prepared using microchannel continuous flow reactor
CN111100040A (en) * 2019-12-23 2020-05-05 沈阳化工研究院有限公司 Micro-channel continuous heterogeneous sulfonation reaction device and method
CN111285749A (en) * 2020-03-26 2020-06-16 阮楚君 Improved method for preparing biphenyl derivative by micro-channel continuous flow
CN113105332A (en) * 2021-04-27 2021-07-13 深圳市华先医药科技有限公司 Method for preparing eltrombopag nitration intermediate in micro-channel continuous flow reactor
CN113121585A (en) * 2021-04-21 2021-07-16 黄山利臻新材料科技有限公司 Micro-reaction system and method for continuously preparing gamma-chloropropyltrichlorosilane
CN113429267A (en) * 2021-04-30 2021-09-24 沧州临港丰亚化工有限公司 Novel continuous process and device for preparing o-phenylphenol

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103319313A (en) * 2013-07-18 2013-09-25 辽宁石化职业技术学院 Method for preparing o-phenyl phenol by ring opening of dibenzofuran
CN109796312A (en) * 2019-02-12 2019-05-24 上海阿拉丁生化科技股份有限公司 A kind of synthetic method of 3- xenol
CN109928884A (en) * 2019-04-23 2019-06-25 沈阳化工研究院有限公司 A kind of serialization hydrogenating reduction aromatic amine prepares the device and method of cycloaliphatic amines
CN110218139A (en) * 2019-08-05 2019-09-10 山东冠森高分子材料科技股份有限公司 A method of biphenyl derivatives are prepared using microchannel continuous flow reactor
CN111100040A (en) * 2019-12-23 2020-05-05 沈阳化工研究院有限公司 Micro-channel continuous heterogeneous sulfonation reaction device and method
CN111285749A (en) * 2020-03-26 2020-06-16 阮楚君 Improved method for preparing biphenyl derivative by micro-channel continuous flow
CN113121585A (en) * 2021-04-21 2021-07-16 黄山利臻新材料科技有限公司 Micro-reaction system and method for continuously preparing gamma-chloropropyltrichlorosilane
CN113105332A (en) * 2021-04-27 2021-07-13 深圳市华先医药科技有限公司 Method for preparing eltrombopag nitration intermediate in micro-channel continuous flow reactor
CN113429267A (en) * 2021-04-30 2021-09-24 沧州临港丰亚化工有限公司 Novel continuous process and device for preparing o-phenylphenol

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