CN118164839A - Preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst - Google Patents
Preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst Download PDFInfo
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- SJEBAWHUJDUKQK-UHFFFAOYSA-N 2-ethylanthraquinone Chemical compound C1=CC=C2C(=O)C3=CC(CC)=CC=C3C(=O)C2=C1 SJEBAWHUJDUKQK-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 239000003054 catalyst Substances 0.000 title claims abstract description 25
- 238000002360 preparation method Methods 0.000 title claims abstract description 20
- 239000011973 solid acid Substances 0.000 title claims abstract description 17
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 claims abstract description 72
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 61
- 239000000463 material Substances 0.000 claims abstract description 39
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 230000007062 hydrolysis Effects 0.000 claims abstract description 28
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 28
- 238000009833 condensation Methods 0.000 claims abstract description 27
- 230000005494 condensation Effects 0.000 claims abstract description 27
- 239000012071 phase Substances 0.000 claims abstract description 22
- 238000007599 discharging Methods 0.000 claims abstract description 16
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims abstract description 13
- 239000002253 acid Substances 0.000 claims abstract description 12
- 238000007363 ring formation reaction Methods 0.000 claims abstract description 12
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims abstract description 7
- 239000012074 organic phase Substances 0.000 claims abstract description 7
- 150000003839 salts Chemical class 0.000 claims abstract description 7
- 239000007787 solid Substances 0.000 claims abstract description 7
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 claims abstract description 4
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 53
- 238000010521 absorption reaction Methods 0.000 claims description 49
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 29
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 24
- 239000000047 product Substances 0.000 claims description 19
- 230000001276 controlling effect Effects 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 15
- 239000003513 alkali Substances 0.000 claims description 13
- 238000005086 pumping Methods 0.000 claims description 12
- 238000003756 stirring Methods 0.000 claims description 12
- 238000004821 distillation Methods 0.000 claims description 11
- 239000012043 crude product Substances 0.000 claims description 10
- 238000007670 refining Methods 0.000 claims description 10
- 239000000243 solution Substances 0.000 claims description 10
- 229920000049 Carbon (fiber) Polymers 0.000 claims description 9
- 239000008346 aqueous phase Substances 0.000 claims description 9
- 239000004917 carbon fiber Substances 0.000 claims description 9
- 238000004090 dissolution Methods 0.000 claims description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 9
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 7
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 7
- HSKPJQYAHCKJQC-UHFFFAOYSA-N 1-ethylanthracene-9,10-dione Chemical compound O=C1C2=CC=CC=C2C(=O)C2=C1C=CC=C2CC HSKPJQYAHCKJQC-UHFFFAOYSA-N 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 239000012452 mother liquor Substances 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 239000013078 crystal Substances 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000000706 filtrate Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- 238000004806 packaging method and process Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000005070 sampling Methods 0.000 claims description 3
- 238000004062 sedimentation Methods 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- 239000002904 solvent Substances 0.000 claims description 3
- 230000007306 turnover Effects 0.000 claims description 3
- 238000005292 vacuum distillation Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims 5
- 238000011010 flushing procedure Methods 0.000 claims 1
- 239000000203 mixture Substances 0.000 claims 1
- 238000010025 steaming Methods 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 abstract description 11
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000002351 wastewater Substances 0.000 abstract description 4
- 239000000543 intermediate Substances 0.000 description 7
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- FECNOIODIVNEKI-UHFFFAOYSA-N 2-[(2-aminobenzoyl)amino]benzoic acid Chemical class NC1=CC=CC=C1C(=O)NC1=CC=CC=C1C(O)=O FECNOIODIVNEKI-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 description 1
- 150000004056 anthraquinones Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000000016 photochemical curing Methods 0.000 description 1
- 238000001782 photodegradation Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a preparation process of 2-ethyl anthraquinone by adopting a BE solid acid catalyst, which comprises the following steps: step one condensation: adding the metered methylene dichloride into a condensation kettle, adding phthalic anhydride, slowly adding solid aluminum trichloride into the condensation kettle, reducing the reaction temperature in the kettle to 25 ℃, slowly dripping ethylbenzene, controlling the reaction temperature at 30-40 ℃, and obtaining a condensation material after dripping is finished; step two, hydrolysis: and (3) adding the metered water into a hydrolysis kettle, slowly discharging the condensation material obtained in the step (I), adding the condensation material into the hydrolysis kettle, controlling the hydrolysis temperature to be below 40 ℃, standing for layering after the hydrolysis is finished, and placing the lower organic phase into an oil phase desolventizing kettle. The method adopts BE solid acid as the catalyst to replace concentrated sulfuric acid catalyst for ring closure reaction, thereby avoiding the generation of waste water, waste acid and waste salt, being safe and environment-friendly, and the catalyst can BE regenerated and reused for many times and has greater advantages in the aspect of economy.
Description
Technical Field
The invention relates to the technical field of 2-ethyl anthraquinone preparation, in particular to a preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst,
Background
The 2-ethyl anthraquinone is light yellow flaky crystal, is dissolved in organic solvent, has a melting point of 107-111 ℃, is mainly used for preparing hydrogen peroxide, dye intermediates, photocuring resin catalysts, photodegradation films, coatings and photopolymerization initiators, the existing 2-ethyl anthraquinone preparation process mainly adopts fuming concentrated sulfuric acid as a catalyst, and generates 6-10 tons of waste concentrated sulfuric acid when producing one ton of anthraquinone products, 15 tons of waste sulfuric acid when producing one ton of 2-ethyl anthraquinone, and the waste sulfuric acid contains more tar and other organic impurities, and a large amount of waste water and waste salt are generated after neutralization by alkali, so that the environmental pollution is particularly large, and the waste sulfuric acid containing tar can only be treated as dangerous waste, so that the treatment cost is large, and the safety, the environmental protection and the economic benefit are not facilitated.
For this reason we propose a process for the preparation of 2-ethyl anthraquinone using BE solid acid catalyst to solve the above-mentioned problems,
Disclosure of Invention
The invention aims to provide a preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst, which solves the problems in the prior art,
In order to achieve the above purpose, the present invention provides the following technical solutions: a preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst comprises the following steps:
Step one condensation: adding the metered methylene dichloride into a condensation kettle, adding phthalic anhydride, slowly adding solid aluminum trichloride into the condensation kettle, reducing the reaction temperature in the kettle to 25 ℃, slowly dripping ethylbenzene, controlling the reaction temperature at 30-40 ℃, and obtaining a condensation material after dripping is finished;
step two, hydrolysis: adding water into a hydrolysis kettle, slowly discharging the condensation material obtained in the step one, adding the condensation material into the hydrolysis kettle, controlling the hydrolysis temperature to be below 40 ℃, standing for layering after the hydrolysis is finished, placing a lower organic phase into an oil phase desolventizing kettle, and adding an upper aluminum trichloride aqueous solution into an aqueous phase transfer tank and adding the aqueous phase transfer tank into an aluminum chloride solution pool through an aqueous phase transfer pump;
Step three, recycling dichloromethane: pumping the organic phase obtained in the second step into an oil phase desolventizing kettle, and then starting steam to recover dichloromethane; the ring closure reaction of BE acid obtained after the completion of the distillation of methylene dichloride.
Step four, closed loop preheating: pumping the metered C9 into a raw material preparation tank, adding the desolventized BE acid obtained in the step three into the raw material preparation tank, starting stirring, preheating the raw material preparation tank to 160 ℃ through heat conducting oil, stopping heating and stopping stirring to obtain a preheated material;
Step five ring closure reaction: discharging the preheated material obtained in the step four to a reaction circulation tank, heating by heat conducting oil, controlling the temperature of the material to be 220-250 ℃, adding the material into a fixed bed reactor for ring closure reaction, controlling the reaction pressure to be 0.6-0.8MPa, sampling and analyzing after the reaction is carried out for 5 hours, stopping a feed pump after the content of ethyl anthraquinone reaches 99%, ending the reaction, and then placing the material in the fixed bed reactor back to the reaction circulation tank for continuous reaction to obtain the reacted material;
Step six, rectifying: pumping the reacted material obtained in the step five into a desolventizing tower, controlling the tower kettle to carry out vacuum distillation at 270 ℃, and recovering C9;
And step seven, refining a product: pumping the metered ethanol into a dissolution refining kettle, putting the 2-ethyl anthraquinone crude product in the buffer tank of the crude product obtained in the step six into the dissolution refining kettle, adding 1 ton, heating by steam under stirring to raise the temperature to 75 ℃ for dissolution, discharging tail gas, feeding clear liquid into a cold separation kettle, cooling by low-temperature water under stirring, completely separating out crystals when the temperature reaches 25 ℃, and filtering to obtain the crystalline ethyl anthraquinone.
And step eight, crude product distillation: discharging the molten product of the seventh step in the intermediate tank to a distillation tower for distillation, heating to 240-270 ℃ under vacuum to obtain a finished product, collecting the finished product to a finished product tank, and slicing and packaging to obtain a 2-ethyl anthraquinone finished product;
Step nine ethanol recovery: recovering ethanol from the mother liquor in the intermediate tank of the eighth filtrate by a mother liquor scraper evaporator, controlling the temperature of a gas phase to 78 ℃, condensing the gas phase by a first-stage condenser and a second-stage condenser, drying the discharged material by a molecular sieve, feeding the dried material into an ethanol turnover tank, cooling and recovering tail gas by a third-stage condenser, removing the tail gas incineration system,
Preferably, the tail gas generated by the condensation kettle in the first step is condensed by an exhaust oil-water purification tower, condensate is separated into water and then enters a dichloromethane receiving tank for application, noncondensable gas is hydrogen chloride gas, the hydrogen chloride gas is prepared by three-stage water absorption, when the concentration of the primary absorption hydrochloric acid is controlled to be 30%, the primary absorption hydrochloric acid is pumped into a hydrochloric acid intermediate tank for hydrolysis, then the secondary absorption water is pumped into a primary absorption tank, the tertiary absorption water is pumped into a secondary absorption tank, the tertiary absorption supplementing water is added, the discharged tail gas is discharged to reach the high altitude after being absorbed by water absorption, alkali absorption and carbon fiber absorption, and the pH value of the alkali absorption is kept to be more than 8.5 in the operation process.
Preferably, the mixed gas of C5, water and a small amount of hydrogen chloride distilled in the third step is condensed by a first-stage second-stage condenser, the condensate enters an oil desolventizing receiving tank, water is separated by a water separator, dichloromethane is recovered, the recovered dichloromethane is dehydrated by a salt bed and then returned to the dichloromethane receiving tank, then the dichloromethane is sent to a C5 overhead tank for reuse, the water phase enters the recovered water receiving tank for reuse by a hydrolysis kettle, and the noncondensable gas is discharged up to the standard after being absorbed by the first-stage water, the first-stage alkali absorption and the carbon fiber absorption.
Preferably, a small amount of BE acid light component mixed gas distilled in the fourth step is condensed by a secondary condenser, the condensate enters a solvent intermediate tank for treatment, and the non-condensable gas is discharged up to the standard after water absorption, alkali absorption and carbon fiber absorption.
Preferably, the conduction oil inlet valve in the fifth step and the sixth step adopts an automatic control regulating valve, and the heating temperature is automatically regulated and controlled through a DCS system.
Preferably, the water generated in the solid bed reaction process in the step six is in a gas phase, the gas phase is decompressed, enters a tail gas buffer tank, is condensed and recovered through a primary condenser and a secondary condenser, C9 and water are separated by sedimentation, C9 is purified by a purification tower, water is recovered by a recovery water receiving tank, and is returned to a decomposing tank for reuse, and tail gas is incinerated and treated.
Compared with the prior art, the invention has the beneficial effects that:
The method adopts BE solid acid as the catalyst to replace concentrated sulfuric acid catalyst for ring closure reaction, thereby avoiding the generation of waste water, waste acid and waste salt, being safe and environment-friendly, and the catalyst can BE regenerated and reused for many times and has greater advantages in the aspect of economy.
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments, based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without making creative efforts fall within the protection scope of the present invention,
Example 1:
the invention provides a technical scheme that: a preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst comprises the following steps:
Step one condensation: adding the metered methylene dichloride into a condensation kettle, adding phthalic anhydride, slowly adding solid aluminum trichloride into the condensation kettle, reducing the reaction temperature in the kettle to 25 ℃, slowly dripping ethylbenzene, controlling the reaction temperature at 30-40 ℃, and obtaining a condensation material after dripping is finished;
step two, hydrolysis: adding water into a hydrolysis kettle, slowly discharging the condensation material obtained in the step one, adding the condensation material into the hydrolysis kettle, controlling the hydrolysis temperature to be below 40 ℃, standing for layering after the hydrolysis is finished, placing a lower organic phase into an oil phase desolventizing kettle, and adding an upper aluminum trichloride aqueous solution into an aqueous phase transfer tank and adding the aqueous phase transfer tank into an aluminum chloride solution pool through an aqueous phase transfer pump;
Step three, recycling dichloromethane: pumping the organic phase obtained in the second step into an oil phase desolventizing kettle, and then starting steam to recover dichloromethane; the ring closure reaction of BE acid obtained after the completion of the distillation of methylene dichloride.
Step four, closed loop preheating: pumping the metered C9 into a raw material preparation tank, adding the desolventized BE acid obtained in the step three into the raw material preparation tank, starting stirring, preheating the raw material preparation tank to 160 ℃ through heat conducting oil, stopping heating and stopping stirring to obtain a preheated material;
Step five ring closure reaction: discharging the preheated material obtained in the step four to a reaction circulation tank, heating by heat conducting oil, controlling the temperature of the material to be 220-250 ℃, adding the material into a fixed bed reactor for ring closure reaction, controlling the reaction pressure to be 0.6-0.8MPa, sampling and analyzing after the reaction is carried out for 5 hours, stopping a feed pump after the content of ethyl anthraquinone reaches 99%, ending the reaction, and then placing the material in the fixed bed reactor back to the reaction circulation tank for continuous reaction to obtain the reacted material;
Step six, rectifying: pumping the reacted material obtained in the step five into a desolventizing tower, controlling the tower kettle to carry out vacuum distillation at 270 ℃, and recovering C9;
And step seven, refining a product: pumping the metered ethanol into a dissolution refining kettle, putting the 2-ethyl anthraquinone crude product in the buffer tank of the crude product obtained in the step six into the dissolution refining kettle, adding 1 ton, heating by steam under stirring to raise the temperature to 75 ℃ for dissolution, discharging tail gas, feeding clear liquid into a cold separation kettle, cooling by low-temperature water under stirring, completely separating out crystals when the temperature reaches 25 ℃, and filtering to obtain the crystalline ethyl anthraquinone.
And step eight, crude product distillation: discharging the molten product of the seventh step in the intermediate tank to a distillation tower for distillation, heating to 240-270 ℃ under vacuum to obtain a finished product, collecting the finished product to a finished product tank, and slicing and packaging to obtain a 2-ethyl anthraquinone finished product;
Step nine ethanol recovery: recovering ethanol from the mother liquor in the intermediate tank of the eighth filtrate by a mother liquor scraper evaporator, controlling the temperature of a gas phase to 78 ℃, condensing the gas phase by a first-stage condenser and a second-stage condenser, drying the discharged material by a molecular sieve, feeding the dried material into an ethanol turnover tank, cooling and recovering tail gas by a third-stage condenser, removing the tail gas incineration system,
Example 2:
Condensing tail gas generated by the condensation kettle in the first step through an exhaust oil-water purification tower, separating water from the condensate, then feeding the condensate into a dichloromethane receiving tank for application, absorbing non-condensable gas into hydrogen chloride gas by three-stage water to prepare hydrochloric acid, when the concentration of the primary absorption hydrochloric acid is controlled to be 30%, feeding the primary absorption hydrochloric acid into a hydrochloric acid intermediate tank for hydrolysis, feeding the secondary absorption water into a primary absorption tank, feeding the tertiary absorption water into a secondary absorption tank, adding water into the tertiary absorption supplementary charging, and discharging the discharged tail gas to reach the high altitude after water absorption, alkali absorption and carbon fiber absorption, wherein the PH value of alkali absorption is kept to be more than 8.5 in the operation process.
And C5, water and a small amount of hydrogen chloride mixed gas distilled in the third step are condensed by a first-stage second-stage condenser, condensate enters an oil desolventizing receiving tank, water is separated by a water separator, dichloromethane is recovered, the recovered dichloromethane is dehydrated by a salt bed and then returned to the dichloromethane receiving tank, and then is sent to a C5 overhead tank for reuse, water phase enters the recovered water receiving tank for reuse by a hydrolysis kettle, and noncondensable gas is discharged up to the standard by going to the high altitude after being absorbed by first-stage water, first-stage alkali and carbon fiber.
And fourthly, condensing a small amount of BE acid light component mixed gas distilled in the step four through a secondary condenser, enabling condensate to enter a solvent middle tank for treatment, and discharging non-condensable gas up to the standard after water absorption, alkali absorption and carbon fiber absorption.
And fifthly, in the step six, the heat conduction oil inlet valve adopts an automatic control regulating valve, and the heating temperature is automatically regulated and controlled through a DCS system.
And step six, water generated in the solid bed reaction process is in a gas phase, the gas phase is subjected to pressure relief, enters a tail gas buffer tank, is condensed and recovered by a primary condenser and a secondary condenser, C9 and water are subjected to sedimentation separation, C9 is purified by a purification tower, water is recovered, is subjected to water recovery, is subjected to tank receiving, is returned to a hydrolysis tank for reuse, and is subjected to tail gas incineration treatment.
Example 3:
The method adopts BE solid acid as the catalyst to replace concentrated sulfuric acid catalyst for ring closure reaction, thereby avoiding the generation of waste water, waste acid and waste salt, being safe and environment-friendly, and the catalyst can BE regenerated and reused for many times and has greater advantages in the aspect of economy.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. A preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst is characterized by comprising the following steps:
Step one condensation: adding the metered methylene dichloride into a condensation kettle, adding phthalic anhydride, slowly adding solid aluminum trichloride into the condensation kettle, reducing the reaction temperature in the kettle to 25 ℃, slowly dripping ethylbenzene, controlling the reaction temperature at 30-40 ℃, and obtaining a condensation material after dripping is finished;
step two, hydrolysis: adding water into a hydrolysis kettle, slowly discharging the condensation material obtained in the step one, adding the condensation material into the hydrolysis kettle, controlling the hydrolysis temperature to be below 40 ℃, standing for layering after the hydrolysis is finished, placing a lower organic phase into an oil phase desolventizing kettle, and adding an upper aluminum trichloride aqueous solution into an aqueous phase transfer tank and adding the aqueous phase transfer tank into an aluminum chloride solution pool through an aqueous phase transfer pump;
Step three, recycling dichloromethane: pumping the organic phase obtained in the second step into an oil phase desolventizing kettle, and then starting steam to recover dichloromethane; performing ring closure reaction on BE acid obtained after steaming dichloromethane;
Step four, closed loop preheating: pumping the metered C9 into a raw material preparation tank, adding the desolventized BE acid obtained in the step three into the raw material preparation tank, starting stirring, preheating the raw material preparation tank to 160 ℃ through heat conducting oil, stopping heating and stopping stirring to obtain a preheated material;
Step five ring closure reaction: discharging the preheated material obtained in the step four to a reaction circulation tank, heating by heat conducting oil, controlling the temperature of the material to be 220-250 ℃, adding the material into a fixed bed reactor for ring closure reaction, controlling the reaction pressure to be 0.6-0.8MPa, sampling and analyzing after the reaction is carried out for 5 hours, stopping a feed pump after the content of ethyl anthraquinone reaches 99%, ending the reaction, and then placing the material in the fixed bed reactor back to the reaction circulation tank for continuous reaction to obtain the reacted material;
Step six, rectifying: pumping the reacted material obtained in the step five into a desolventizing tower, controlling the tower kettle to carry out vacuum distillation at 270 ℃, and recovering C9;
And step seven, refining a product: pumping the metered ethanol into a dissolution refining kettle, putting the 2-ethyl anthraquinone crude product in the buffer tank of the crude product obtained in the step six into the dissolution refining kettle, adding 1 ton of the 2-ethyl anthraquinone crude product into the dissolution refining kettle, heating the solution to 75 ℃ with steam under stirring, dissolving the solution, discharging tail gas, feeding clear solution into a cold separation kettle, cooling the solution with low temperature water under stirring, completely separating out crystals when the temperature reaches 25 ℃, and filtering the solution to obtain crystalline ethyl anthraquinone;
And step eight, crude product distillation: discharging the molten product of the seventh step in the intermediate tank to a distillation tower for distillation, heating to 240-270 ℃ under vacuum to obtain a finished product, collecting the finished product to a finished product tank, and slicing and packaging to obtain a 2-ethyl anthraquinone finished product;
Step nine ethanol recovery: and step eight, recovering ethanol from the mother liquor in the filtrate intermediate tank by a mother liquor scraper evaporator, controlling the temperature of a gas phase to be 78 ℃, condensing the gas phase by a first-stage condenser and a second-stage condenser, drying a discharged material by a molecular sieve, feeding the dried material into an ethanol turnover tank, cooling and recovering tail gas by a third-stage condenser, and removing a tail gas incineration system.
2. The process for preparing 2-ethylanthraquinone using BE solid acid catalyst according to claim 1, wherein the step of: the tail gas generated by the condensation kettle in the first step is condensed by an exhaust gas oil-water purification tower, the condensate is separated into water and then enters a dichloromethane receiving tank for application, noncondensable gas is hydrogen chloride gas, the hydrochloric acid is prepared by three-stage water absorption, when the concentration of the primary absorption hydrochloric acid is controlled to be 30%, the primary absorption hydrochloric acid is pumped into a hydrochloric acid intermediate tank for hydrolysis, then the secondary absorption water is pumped into a primary absorption tank, the tertiary absorption water is pumped into a secondary absorption tank, water is added by the tertiary absorption supplementary flushing, the discharged tail gas is discharged to reach the high altitude after being absorbed by water absorption, alkali absorption and carbon fiber absorption, and the PH value of the alkali absorption is kept to be more than 8.5 in the operation process.
3. The process for preparing 2-ethylanthraquinone using BE solid acid catalyst according to claim 1, wherein the step of: and C5, water and a small amount of hydrogen chloride gas mixture evaporated in the step three are condensed by a first-stage second-stage condenser, condensate enters an oil desolventizing receiving tank, water is separated by a water separator, dichloromethane is recovered, the recovered dichloromethane is dehydrated by a salt bed and then returned to the dichloromethane receiving tank, and then is sent to a C5 overhead tank for reuse, water phase enters the recovered water receiving tank for reuse by a hydrolysis kettle, and noncondensable gas is discharged up to the standard after being absorbed by first-stage water absorption, first-stage alkali absorption and carbon fiber absorption.
4. The process for preparing 2-ethylanthraquinone using BE solid acid catalyst according to claim 1, wherein the step of: and (3) condensing a small amount of BE acid light component mixed gas distilled in the step four through a secondary condenser, enabling condensate to enter a solvent middle tank for treatment, and discharging non-condensable gas up to the standard after water absorption, alkali absorption and carbon fiber absorption.
5. The process for preparing 2-ethylanthraquinone using BE solid acid catalyst according to claim 1, wherein the step of: and in the fifth step and the sixth step, the heat conduction oil inlet valve adopts an automatic control regulating valve, and the heating temperature is automatically regulated and controlled through a DCS system.
6. The process for preparing 2-ethylanthraquinone using BE solid acid catalyst according to claim 1, wherein the step of: and step six, water generated in the solid bed reaction process is in a gas phase, the gas phase is subjected to pressure relief, enters a tail gas buffer tank, is condensed and recovered through a primary condenser and a secondary condenser, C9 and water are subjected to sedimentation separation, then C9 is purified by a purification tower, water is recycled, is subjected to water receiving tank, and is returned to a hydrolysis tank for reuse, and tail gas is incinerated for disposal.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211573615.4A CN118164839A (en) | 2022-12-08 | 2022-12-08 | Preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211573615.4A CN118164839A (en) | 2022-12-08 | 2022-12-08 | Preparation process of 2-ethyl anthraquinone by adopting BE solid acid catalyst |
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