CN112062656A - Micro-interface preparation system and method for p-methylphenol - Google Patents
Micro-interface preparation system and method for p-methylphenol Download PDFInfo
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- IWDCLRJOBJJRNH-UHFFFAOYSA-N p-cresol Chemical compound CC1=CC=C(O)C=C1 IWDCLRJOBJJRNH-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000002360 preparation method Methods 0.000 title claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 66
- HFPZCAJZSCWRBC-UHFFFAOYSA-N p-cymene Chemical compound CC(C)C1=CC=C(C)C=C1 HFPZCAJZSCWRBC-UHFFFAOYSA-N 0.000 claims abstract description 50
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000001301 oxygen Substances 0.000 claims abstract description 42
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 42
- 230000003647 oxidation Effects 0.000 claims abstract description 39
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 238000005507 spraying Methods 0.000 claims abstract description 4
- 239000007788 liquid Substances 0.000 claims description 74
- 238000000926 separation method Methods 0.000 claims description 48
- 239000007789 gas Substances 0.000 claims description 28
- 239000007791 liquid phase Substances 0.000 claims description 28
- 239000012071 phase Substances 0.000 claims description 25
- YTZKOQUCBOVLHL-UHFFFAOYSA-N p-methylisopropylbenzene Natural products CC(C)(C)C1=CC=CC=C1 YTZKOQUCBOVLHL-UHFFFAOYSA-N 0.000 claims description 18
- 239000000047 product Substances 0.000 claims description 18
- 238000003860 storage Methods 0.000 claims description 11
- 238000002156 mixing Methods 0.000 claims description 9
- 239000007795 chemical reaction product Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 3
- 239000000126 substance Substances 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 2
- 238000005191 phase separation Methods 0.000 claims description 2
- WWRCMNKATXZARA-UHFFFAOYSA-N 1-Isopropyl-2-methylbenzene Chemical compound CC(C)C1=CC=CC=C1C WWRCMNKATXZARA-UHFFFAOYSA-N 0.000 abstract description 14
- 238000012546 transfer Methods 0.000 abstract description 12
- 238000006243 chemical reaction Methods 0.000 description 20
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 15
- 230000000694 effects Effects 0.000 description 7
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 239000003513 alkali Substances 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 239000006185 dispersion Substances 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 238000001308 synthesis method Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- CFMZSMGAMPBRBE-UHFFFAOYSA-N 2-hydroxyisoindole-1,3-dione Chemical compound C1=CC=C2C(=O)N(O)C(=O)C2=C1 CFMZSMGAMPBRBE-UHFFFAOYSA-N 0.000 description 2
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 238000005660 chlorination reaction Methods 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000006193 diazotization reaction Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 238000007500 overflow downdraw method Methods 0.000 description 2
- 150000002978 peroxides Chemical class 0.000 description 2
- 238000006277 sulfonation reaction Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- QTWJRLJHJPIABL-UHFFFAOYSA-N 2-methylphenol;3-methylphenol;4-methylphenol Chemical compound CC1=CC=C(O)C=C1.CC1=CC=CC(O)=C1.CC1=CC=CC=C1O QTWJRLJHJPIABL-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- AFBPFSWMIHJQDM-UHFFFAOYSA-N N-methylaniline Chemical compound CNC1=CC=CC=C1 AFBPFSWMIHJQDM-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- KCXMKQUNVWSEMD-UHFFFAOYSA-N benzyl chloride Chemical compound ClCC1=CC=CC=C1 KCXMKQUNVWSEMD-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Classifications
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- 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
- C07C37/08—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by decomposition of hydroperoxides, e.g. cumene hydroperoxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0036—Flash degasification
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0093—Microreactors, e.g. miniaturised or microfabricated reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
- B01J4/002—Nozzle-type elements
-
- 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
- C07C37/74—Purification; separation; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C407/00—Preparation of peroxy compounds
-
- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/00891—Feeding or evacuation
- B01J2219/00894—More than two inlets
-
- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/0095—Control aspects
- B01J2219/00952—Sensing operations
- B01J2219/00954—Measured properties
- B01J2219/00961—Temperature
-
- 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
- B01J2219/00781—Aspects relating to microreactors
- B01J2219/0095—Control aspects
- B01J2219/00952—Sensing operations
- B01J2219/00954—Measured properties
- B01J2219/00963—Pressure
Abstract
The invention provides a micro-interface preparation system and a method for p-methylphenol, wherein the micro-interface preparation system comprises: an oxidation reactor and a pipeline reactor, wherein the inner diameter of the pipeline reactor is 2-25 mm; the side wall of the oxidation reactor is sequentially provided with an oxygen inlet and a mixed inlet of the isopropyltoluene and the catalyst, a micro-interface generator is arranged in the oxidation reactor, a plurality of gushing ports are arranged right below the micro-interface generator, the spraying direction of the gushing ports is upward, and the oxygen inlet is directly communicated with the inside of the micro-interface generator through a pipeline so as to realize that oxygen is broken into micro-bubbles at the micron level in the micro-interface generator before the oxidation reaction. According to the micro-interface preparation system, the micro-interface generator is arranged in the oxidation reactor, so that oxygen is broken into micro bubbles before the methyl cumene is subjected to oxidation reaction, the mass transfer area of a phase boundary between the oxygen and the methyl cumene is increased, and the mass transfer area of the phase boundary in the oxidation reaction process is increased.
Description
Technical Field
The invention relates to the field of preparation of p-methylphenol, in particular to a system and a method for preparing a micro-interface of p-methylphenol.
Background
P-methylphenol, also known as p-cresol or p-phenol (p-cresol), can be dissolved in common organic solvents and sodium hydroxide solutions, is slightly soluble in water, can volatilize with water vapor, is toxic and has a phenolic odor; the compound is used as an important fine chemical intermediate, is mainly prepared by a natural separation method (such as separation from petroleum and coal tar) and chemical synthesis, and is widely applied to the fields of plastics, foods, dyes, pesticides, medicines and macromolecules.
P-methylphenol was extracted from natural coal tar and the waste liquid from petroleum refinery washing of petroleum fractions before 1965. The artificial synthesis method is available only after 1965. With the continuous expansion of the application range of p-methylphenol, the yield of p-methylphenol increases year by year, and the synthesis method gradually takes a leading position.
The existing synthesis methods of p-methylphenol include a toluene sulfonation alkali fusion method, a toluene chlorination hydrolysis method, a diazotization method, a methyl isopropylbenzene oxidation method and the like. The toluene sulfonation alkali fusion method is the earliest method for producing p-cresol, but uses a large amount of strong acid and strong base, and causes serious equipment corrosion and environmental pollution. The chlorination and hydrolysis method of toluene is to chlorinate toluene to obtain three chloro-toluene mixtures, and then to continuously hydrolyze at high temperature and high pressure to obtain p-cresol. The diazotization method is that methylaniline is diazotized and hydrolyzed to obtain a target product, but the method has complex process, uses a large amount of sulfuric acid, has serious pollution and is not suitable for large-scale long-term production. The methyl isopropyl benzene oxidation method utilizes oxygen or hydrogen peroxide for oxidation, and utilizes sulfuric acid for treatment after peroxide is generated, so that the peroxide is decomposed to generate p-cresol.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The first purpose of the invention is to provide a micro-interface preparation system for p-methylphenol, which is characterized in that a micro-interface generator is arranged in an oxidation reactor, so that oxygen is broken into micro-bubbles before the oxidation reaction of methyl isopropylbenzene, the phase boundary mass transfer area between the oxygen and the p-isopropylbenzene is increased, and the phase boundary mass transfer area in the oxidation reaction process is increased, thereby solving the problems of high reaction pressure, high temperature and low liquid hourly space velocity caused by the fact that the oxygen and the p-isopropylbenzene cannot be fully mixed in the reactor in the prior art, and improving the yield by increasing the phase boundary mass transfer area.
The second purpose of the invention is to provide a method for preparing p-methylphenol by adopting the micro-interface preparation system, the p-methylphenol obtained by the reaction has high purity and wide application, the application range of the p-methylphenol is improved, and the method is worthy of wide popularization and application.
In order to achieve the above purpose of the present invention, the following technical solutions are adopted:
the invention provides a micro-interface preparation system of p-methylphenol, which comprises an oxidation reactor and a pipeline reactor, wherein the inner diameter of the pipeline reactor is 2-25 mm;
the side wall of the oxidation reactor is sequentially provided with an oxygen inlet and a mixed inlet of the isopropyltoluene and the catalyst, a micro-interface generator is arranged in the oxidation reactor, a plurality of surge ports are arranged right below the micro-interface generator, the spraying directions of the surge ports are upward, and the oxygen inlet is directly communicated with the inside of the micro-interface generator through a pipeline so as to realize that the oxygen is crushed into micro-bubbles at the micron level in the micro-interface generator before the oxidation reaction;
and the oxidation reaction product from the oxidation reactor enters the pipeline reactor to continue to react, and the pipeline reactor is sequentially connected with a gas-liquid separation device and a rectification device to purify the oxidation reaction product.
Preferably, the p-methyl isopropylbenzene and catalyst mixing inlet is arranged at the lower part of the oxygen inlet, and the p-methyl isopropylbenzene and catalyst mixing inlet is communicated with the gushing port through a pipeline.
Preferably, the p-methyl isopropylbenzene and catalyst mixing inlet is connected with a liquid phase storage tank, and the liquid phase storage tank is used for storing the pretreated p-methyl isopropylbenzene and the catalyst.
Preferably, the oxygen inlet is connected with a gas phase feeding pipeline of an elongated round pipe type, and the gas phase feeding pipeline is externally connected with a gas source.
Preferably, the micro-interface generator inside the oxidation reactor is single and is arranged at a lower position inside the oxidation reactor.
The micro-interface generator is arranged in the oxidation reactor, the micro-interface generator is preferably arranged at a lower position in the oxidation reactor, so that oxygen can enter from the bottom to fill the whole oxidation reactor, a plurality of surge ports are also arranged in the oxidation reactor and are matched with the micro-interface generator for use, the spraying direction of the surge ports is upward, after the surge ports are communicated with the methyl isopropylbenzene and catalyst mixing inlet, the entering mixed liquid just sprays against the micro-interface generator, the effect of taking a liquid phase as a medium is further enhanced, and the oxygen dispersion and crushing effect can be further improved, so in view of the excellent combination mode, the methyl isopropylbenzene and catalyst mixing inlet is arranged at the lower part of the oxygen inlet, so that the liquid phase is lower than the gas phase entering the oxidation reactor, the liquid phase can be sprayed to the position of the micro-interface generator through the gushing port. The fusion effect between two phases can be enhanced, and the mass transfer effect is improved.
Preferably, the micro-interface generator is a single one that can meet practical process requirements, and its specific type is preferably a pneumatic micro-interface generator because the pneumatic type is relatively low cost and easy to install.
The micro-interface generator in the oxidation reactor breaks the hydrogen into micro-bubbles with micron scale, and releases the micro-bubbles into the reactor, so as to increase the mass transfer area of the phase boundary between the oxygen and the catalyst and between the oxygen and the p-methyl isopropyl benzene in the oxidation reaction process, so that the oxygen is fully contacted with the liquid phase in the micro-bubble state, and the oxidation reaction is carried out. The catalyst selected by the oxidation reaction is N-hydroxyphthalimide, which replaces the discharge of strong acid and strong base waste liquid and the corrosion to equipment in the traditional process.
It will be appreciated by those skilled in the art that the micro-interface generator used in the present invention is described in the prior patents of the present inventor, such as the patents of application numbers CN201610641119.6, CN201610641251.7, CN201710766435.0, CN106187660, CN105903425A, CN109437390A, CN205833127U and CN 207581700U. The detailed structure and operation principle of the micro bubble generator (i.e. micro interface generator) is described in detail in the prior patent CN201610641119.6, which describes that "the micro bubble generator comprises a body and a secondary crushing member, wherein the body is provided with a cavity, the body is provided with an inlet communicated with the cavity, the opposite first end and second end of the cavity are both open, and the cross-sectional area of the cavity decreases from the middle of the cavity to the first end and second end of the cavity; the secondary crushing member is disposed at least one of the first end and the second end of the cavity, a portion of the secondary crushing member is disposed within the cavity, and an annular passage is formed between the secondary crushing member and the through holes open at both ends of the cavity. The micron bubble generator also comprises an air inlet pipe and a liquid inlet pipe. "the specific working principle of the structure disclosed in the application document is as follows: liquid enters the micro-bubble generator tangentially through the liquid inlet pipe, and gas is rotated at a super high speed and cut to break gas bubbles into micro-bubbles at a micron level, so that the mass transfer area between a liquid phase and a gas phase is increased, and the micro-bubble generator in the patent belongs to a pneumatic micro-interface generator.
In addition, the first patent 201610641251.7 describes that the primary bubble breaker has a circulation liquid inlet, a circulation gas inlet and a gas-liquid mixture outlet, and the secondary bubble breaker communicates the feed inlet with the gas-liquid mixture outlet, which indicates that the bubble breakers all need to be mixed with gas and liquid, and in addition, as can be seen from the following drawings, the primary bubble breaker mainly uses the circulation liquid as power, so that the primary bubble breaker belongs to a hydraulic micro-interface generator, and the secondary bubble breaker simultaneously introduces the gas-liquid mixture into an elliptical rotating ball for rotation, thereby realizing bubble breaking in the rotating process, so that the secondary bubble breaker actually belongs to a gas-liquid linkage micro-interface generator. In fact, the micro-interface generator is a specific form of the micro-interface generator, whether it is a hydraulic micro-interface generator or a gas-liquid linkage micro-interface generator, however, the micro-interface generator adopted in the present invention is not limited to the above forms, and the specific structure of the bubble breaker described in the prior patent is only one of the forms that the micro-interface generator of the present invention can adopt.
Furthermore, the prior patent 201710766435.0 states that the principle of the bubble breaker is that high-speed jet flows are used to achieve mutual collision of gases, and also states that the bubble breaker can be used in a micro-interface strengthening reactor to verify the correlation between the bubble breaker and the micro-interface generator; moreover, in the prior patent CN106187660, there is a related description on the specific structure of the bubble breaker, see paragraphs [0031] to [0041] in the specification, and the accompanying drawings, which illustrate the specific working principle of the bubble breaker S-2 in detail, the top of the bubble breaker is a liquid phase inlet, and the side of the bubble breaker is a gas phase inlet, and the liquid phase coming from the top provides the entrainment power, so as to achieve the effect of breaking into ultra-fine bubbles, and in the accompanying drawings, the bubble breaker is also seen to be of a tapered structure, and the diameter of the upper part is larger than that of the lower part, and also for better providing the entrainment power for the liquid phase. Since the micro-interface generator was just developed in the early stage of the prior patent application, the micro-interface generator was named as a micro-bubble generator (CN201610641119.6), a bubble breaker (201710766435.0) and the like in the early stage, and is named as a micro-interface generator in the later stage along with the continuous technical improvement, and the micro-interface generator in the present invention is equivalent to the micro-bubble generator, the bubble breaker and the like in the prior art, and has different names.
In summary, the micro-interface generator of the present invention belongs to the prior art, although some micro-interface generators belong to the pneumatic type micro-interface generator, some micro-interface generators belong to the hydraulic type micro-interface generator, and some micro-interface generators belong to the gas-liquid linkage type micro-interface generator, the difference between the types is mainly selected according to the different specific working conditions, and the connection between the micro-interface generator and the reactor and other devices, including the connection structure and the connection position, is determined according to the structure of the micro-interface generator, which is not limited.
Preferably, the pipe reactor has an internal diameter of 4 to 16 mm. In addition to this, the internal diameter of the pipe reactor may be 3mm, 10mm, 11mm, 12mm, 13mm, 15mm, or the like. Since the control of the inner diameter of the pipeline reactor within the range required by the present invention can effectively control the residence time of the reaction materials in the reactor, thereby achieving good reaction effect.
Preferably, the gas-liquid separation device comprises a first-stage gas-liquid separation tank and a second-stage gas-liquid separation tank, the first-stage gas-liquid separation tank is used for carrying out preliminary liquid phase separation on a reaction product of the pipeline reactor, and the second-stage gas-liquid separation tank is used for carrying out further gas-liquid separation on a substance ejected from the top of the first-stage gas-liquid separation tank.
Preferably, the tank top of the secondary gas-liquid separation tank is communicated with the oxygen inlet through a pipeline so as to realize the recycling of the gas phase after gas-liquid separation.
Preferably, the rectifying device includes the one-level rectifying column and the second grade rectifying column of establishing ties in proper order, the lateral wall of one-level rectifying column with the bottom of one-level gas-liquid separation jar is connected in order to be used for carrying out the rectification with the liquid phase product of separating and is handled, the bottom of one-level rectifying column with the lateral wall of second grade rectifying column communicates with each other through the pipeline and is used for right the cauldron bottom product of one-level rectifying column carries out further rectification.
Preferably, the top of the primary rectification column is in communication with the liquid phase storage tank for recycling the separated para-cymene back to utilization.
The gas-liquid separation device is used for carrying out gas-liquid separation on a reaction product discharged from the oxidation reactor, the gas-liquid separation device comprises a first-stage gas-liquid separation tank and a second-stage gas-liquid separation tank, after primary separation through the first-stage gas-liquid separation tank, a gas phase is sent to the second-stage gas-liquid separation tank for further treatment, a liquid phase enters the rectification device for rectification and purification, after gas-liquid separation of the gas phase in the second-stage gas-liquid separation tank, the gas phase returns to be communicated with an oxygen inlet through a pipeline so as to ensure the reutilization of raw materials, and the liquid phase is directly. The rectification device comprises a primary rectification tower and a secondary rectification tower, firstly, rectification treatment is carried out in the primary rectification tower, the isopropyltoluene is separated according to the difference of boiling points and recycled to a liquid phase storage tank, a kettle bottom product is introduced into the secondary rectification tower for next rectification treatment to obtain a target product, namely the methylphenol, and the kettle bottom product is subjected to byproduct treatment; the product is further refined to obtain a finished product of p-methyl phenol, and other components generated in the reaction process are discharged out of the system.
In a word, the novel method for preparing the methyl isopropyl benzene ring in a protecting mode provided by the invention has the advantages that N-hydroxyphthalimide catalyst is selected to replace strong acid and strong alkali waste liquid discharge and equipment corrosion in the traditional process, the micro-interface generator connected with the oxygen inlet is arranged in the reaction kettle through the design scheme of the process system, and the oxygen is contacted with the methyl isopropyl benzene in a bubble state through the reaction of the micro-interface generator, so that the phase boundary mass transfer area between the oxygen and the methyl isopropyl benzene in the oxidation reaction is increased, the reaction conversion rate is improved, and the problems of pollution and low reaction efficiency in the prior art are solved.
In addition, be provided with the circulating pump between liquid phase storage jar and the oxidation reactor, when this system operation, the circulating pump can provide power for the transportation to methyl cumene, makes methyl cumene can carry to reation kettle with appointed speed, has improved the operating efficiency of this system.
The invention also provides a preparation method of the p-methylphenol, which comprises the following steps:
the p-methyl isopropylbenzene, the catalyst and the oxygen are dispersed and crushed in a mixed micro interface to carry out oxidation reaction, and the p-methyl phenol is obtained after gas-liquid separation, rectification and purification.
Preferably, the temperature of the oxidation reaction is 60-100 ℃, and the pressure of the oxidation reaction is 2-3 MPa.
The p-methylphenol product prepared by the preparation method has good quality and high yield. And the preparation method has low reaction temperature, greatly reduced pressure and high liquid hourly space velocity, which is equivalent to improving the productivity.
Compared with the prior art, the invention has the beneficial effects that:
(1) according to the micro-interface preparation system for p-methyl phenol, the micro-interface generator is arranged in the oxidation reactor, so that oxygen is crushed into micro bubbles before the oxidation reaction of the p-methyl isopropylbenzene, the mass transfer area of a phase boundary between the oxygen and the p-methyl isopropylbenzene is increased, and the mass transfer area of the phase boundary in the oxidation reaction process is increased;
(2) the p-methylphenol prepared by the p-methylphenol preparation method has high purity and wide application, improves the application range of the p-methylphenol and is worthy of wide popularization and application.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of a micro-interface preparation system for p-methylphenol provided in embodiment 1 of the present invention.
Description of the drawings:
10-an oxidation reactor; 101-an oxygen inlet;
102-p-methyl isopropylbenzene and a catalyst mixing inlet; 103-a micro-interface generator;
104-a gushing port; 20-a liquid phase storage tank;
30-a gas phase feed conduit; 40-first stage gas-liquid separation tank;
50-first-stage rectifying tower; 60-a secondary rectifying tower;
70-product tank; 80-a secondary gas-liquid separation tank;
90-pipeline reactor.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to more clearly illustrate the technical solution of the present invention, the following description is made in the form of specific embodiments.
Example 1
Referring to fig. 1, a system for preparing p-methylphenol by a micro interface according to an embodiment of the present invention mainly includes an oxidation reactor 10, a pipeline reactor 90, a gas-liquid separation device (a first-stage gas-liquid separation tank 40 and a second-stage gas-liquid separation tank 80), and a rectification device (a first-stage rectification tower 50 and a second-stage rectification tower 60), wherein an inner diameter of the pipeline reactor 90 is 25 mm.
An oxygen inlet 101 and a methyl isopropyl benzene and catalyst mixing inlet 102 are sequentially arranged on the side wall of the oxidation reactor 10 from top to bottom, a single micro-interface generator 103 is arranged in the oxidation reactor 10, the oxygen inlet 101 is directly communicated with the inside of the micro-interface generator 103 through a pipeline so as to break oxygen into micro-bubbles at a micron level in the micro-interface generator 103 before oxidation reaction, a plurality of spouting ports 104 are arranged right below the micro-interface generator 103, the spouting direction of the spouting ports 104 is upward, and the spouting ports 104 are connected with the methyl isopropyl benzene and catalyst mixing inlet 102 through a pipeline so as to make a liquid phase spouted from the spouting ports 104 enter the micro-interface generator 103 as a medium and realize better dispersion and breaking of a gas phase.
A mixed inlet of the p-isopropylbenzene and the catalyst is connected with a liquid phase storage tank 20, sufficient p-isopropylbenzene and the catalyst in a corresponding proportion are filled into the liquid phase storage tank 20 in advance, an oxygen inlet 101 is connected with a long and thin circular tube type gas phase feeding pipeline 30, a 200L oxygen gas source is connected outside the gas phase feeding pipeline 30, a system is started, the temperature of the system is set to be 60 ℃, the pressure is set to be 2.0MPa, the p-isopropylbenzene and the catalyst are conveyed into an oxidation reactor 10, and meanwhile, the oxygen is conveyed into a micro interface generator 103 through the gas phase feeding pipeline 30.
The micro-interface generator 103 releases oxygen in the form of bubbles into the oxidation reactor 10, so that the oxygen is in sufficient contact with p-cymene in the form of bubbles to perform an oxidation reaction. The reacted product in oxidation reactor 10 is then transferred to pipeline reactor 90 for further reaction.
One side of the pipeline reactor 90 is connected with the oxidation reactor 10, and the other side is communicated with the primary gas-liquid separation tank 40, and is used for further purifying and recovering primary raw materials of oxidation reaction products. The liquid phase separated by the primary gas-liquid separation tank 40 goes to a rectification device for rectification treatment, the gas phase goes to the secondary gas-liquid separation tank 80 for further gas-liquid separation, the gas phase after gas-liquid separation returns from the top of the secondary gas-liquid separation tank 80 to be communicated with the oxygen inlet 101 through a pipeline, and the liquid phase is directly discharged and collected. The first-stage rectifying tower 50 and the second-stage rectifying tower 60 in the rectifying device are sequentially connected in series, the side wall of the first-stage rectifying tower 50 is connected with the bottom of the first-stage gas-liquid separation tank 40 to rectify the separated liquid phase product, and the bottom of the first-stage rectifying tower 50 is communicated with the side wall of the second-stage rectifying tower 60 through a pipeline to further rectify the bottom product of the first-stage rectifying tower 50.
The top of the first-stage rectifying tower 50 is communicated with the liquid-phase storage tank 20 so as to recycle the p-cymene separated from the top of the rectified tower as a raw material for reuse, the substance discharged from the top of the second-stage rectifying tower 60 is a finished product p-cymene, the p-cymene is collected and stored in the product tank 70, and other components generated in the reaction process are removed from the system. The yield of p-methylphenol was measured and calculated to be 90% conversion of p-cymene and 85% selectivity to p-methylphenol.
In the above embodiment, the micro-interface generator 103 converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubbles and transmits the surface energy to the bubbles, so that the bubbles are broken into micro-bubbles with a diameter of 1 μm or more and a diameter of less than 1mm, and the micro-bubbles are divided into the pneumatic micro-interface generator 103, the hydraulic micro-interface generator 103 and the gas-liquid linkage micro-interface generator 103 according to the energy input mode or the gas-liquid ratio, wherein the pneumatic micro-interface generator 103 is driven by gas, and the input gas amount is much larger than the liquid amount; the hydraulic micro-interface generator 103 is driven by liquid, and the input air quantity is generally smaller than the liquid quantity; the gas-liquid linkage type micro-interface generator 103 is driven by gas and liquid at the same time, and the input gas quantity is close to the liquid quantity. The micro-interface generator 103 is selected from one or more of a pneumatic micro-interface generator 103, a hydraulic micro-interface generator 103 and a gas-liquid linkage micro-interface generator 103.
In order to increase the dispersion and mass transfer effects, an additional micro-interface generator 103 can be additionally arranged, the installation position is not limited, the micro-interface generator can be externally arranged or internally arranged, and the micro-interface generator can be arranged on the side wall in the kettle in a relative mode when the micro-interface generator is internally arranged, so that micro-bubbles discharged from the outlet of the micro-interface generator 103 are opposite.
In the above embodiment, the number of the pump bodies is not specifically required, and the pump bodies may be arranged at corresponding positions as required.
Example 2
Compared to example 1, with the other operating conditions unchanged, when the oxidation reaction temperature was set at 80 ℃ and the pressure was set at 2.5MPa, the final calculated conversion of p-cymene was 92% and the selectivity to p-methylphenol was 88%.
Example 3
Other operating conditions were unchanged from example 1, with the oxidation temperature set at 100 ℃ and the pressure set at 3.0MPa, and finally a p-cymene conversion of 89% and a p-methylphenol selectivity of 84% were calculated.
Example 4
Other operating conditions were unchanged from example 1 except that the internal diameter of the pipeline reactor 90 was 16mm, and finally the conversion of p-cymene was calculated to be 91% and the selectivity to p-methylphenol was calculated to be 86%.
Example 5
Other operating conditions were unchanged from example 1 except that the internal diameter of the pipe reactor 90 was 4mm, and finally the conversion of p-cymene was calculated to be 89% and the selectivity to p-methylphenol was calculated to be 86%.
Comparative example 1
Other operating conditions were unchanged from example 1, and the p-cymene conversion was calculated to be 80% and the p-methylphenol selectivity to be 85% without the micro-interface generator being placed in the oxidation reactor.
Comparative example 2
Other operating conditions were unchanged from example 1, and the conversion of p-cymene was calculated to be 88% and the selectivity to p-methylphenol was calculated to be 76% without the provision of a surge port in the oxidation reactor.
In a word, compared with the micro-interface preparation system for the p-methylphenol in the prior art, the micro-interface preparation system disclosed by the invention is few in equipment components, small in occupied area, low in energy consumption, low in cost, high in safety, controllable in reaction and high in raw material conversion rate, is equivalent to providing a micro-interface preparation system with higher operability for the field of p-methylphenol preparation, and is worthy of wide popularization and application.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A micro-interface preparation system for p-methylphenol, which is characterized by comprising the following components: the device comprises an oxidation reactor and a pipeline reactor, wherein the inner diameter of the pipeline reactor is 2-25 mm;
the side wall of the oxidation reactor is sequentially provided with an oxygen inlet and a mixed inlet of the isopropyltoluene and the catalyst, a micro-interface generator is arranged in the oxidation reactor, a plurality of surge ports are arranged right below the micro-interface generator, the spraying directions of the surge ports are upward, and the oxygen inlet is directly communicated with the inside of the micro-interface generator through a pipeline so as to realize that the oxygen is crushed into micro-bubbles at the micron level in the micro-interface generator before the oxidation reaction;
and the oxidation reaction product from the oxidation reactor enters the pipeline reactor to continue to react, and the pipeline reactor is sequentially connected with a gas-liquid separation device and a rectification device to purify the oxidation reaction product.
2. The system of claim 1, wherein the gas-liquid separation device comprises a primary gas-liquid separation tank and a secondary gas-liquid separation tank, the primary gas-liquid separation tank is used for performing primary liquid phase separation on the reaction product of the pipeline reactor, and the secondary gas-liquid separation tank is used for performing further gas-liquid separation on the substance discharged from the top of the primary gas-liquid separation tank.
3. The micro-interface preparation system according to claim 2, wherein the top of the secondary gas-liquid separation tank is communicated with the oxygen inlet through a pipeline to realize the recycling of the gas phase after gas-liquid separation.
4. The system of claim 1, wherein the pipe reactor has an inner diameter of 4-16 mm.
5. The system of claim 2, wherein the inlet for mixing p-cymene with catalyst is connected to a liquid storage tank for storing pretreated p-cymene and catalyst.
6. The system of any of claims 1-4, wherein the micro-interface generator is a single micro-interface generator disposed at a lower position within the oxidation reactor.
7. The micro-interface preparation system according to claim 5, wherein the rectifying device comprises a first-stage rectifying tower and a second-stage rectifying tower which are connected in series in sequence, the side wall of the first-stage rectifying tower is connected with the bottom of the first-stage gas-liquid separation tank for rectifying the separated liquid-phase product, and the bottom of the first-stage rectifying tower is communicated with the side wall of the second-stage rectifying tower through a pipeline for further rectifying the bottom product of the first-stage rectifying tower.
8. The system of claim 7, wherein the top of the primary rectification column is in communication with the liquid phase storage tank for recycling the separated para-cymene back to utilization.
9. The method for producing a p-methylphenol micro-interfacial production system according to any one of claims 1 to 8, comprising the steps of:
the p-methyl isopropylbenzene, the catalyst and the oxygen are dispersed and crushed in a mixed micro interface to carry out oxidation reaction, and the p-methyl phenol is obtained after gas-liquid separation, rectification and purification.
10. The method according to claim 9, wherein the temperature of the oxidation reaction is 60 to 100 ℃ and the pressure of the oxidation reaction is 2 to 3 MPa.
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| CN202010978781.7A CN112062656A (en) | 2020-09-17 | 2020-09-17 | Micro-interface preparation system and method for p-methylphenol |
| JP2022600019U JP3239352U (en) | 2020-09-17 | 2020-10-22 | Micro-interface production system for p-methylphenol |
| DE212020000694.6U DE212020000694U1 (en) | 2020-09-17 | 2020-10-22 | Microinterfacial manufacturing system for p-methylphenol |
| PCT/CN2020/122815 WO2022057004A1 (en) | 2020-09-17 | 2020-10-22 | Microinterface preparation system for p-methylphenol and method |
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| WO2022057004A1 (en) | 2022-03-24 |
| DE212020000694U1 (en) | 2022-03-11 |
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Application publication date: 20201211 |