CN111763192B - Preparation method and device of epsilon-caprolactone - Google Patents
Preparation method and device of epsilon-caprolactone Download PDFInfo
- Publication number
- CN111763192B CN111763192B CN202010674122.4A CN202010674122A CN111763192B CN 111763192 B CN111763192 B CN 111763192B CN 202010674122 A CN202010674122 A CN 202010674122A CN 111763192 B CN111763192 B CN 111763192B
- Authority
- CN
- China
- Prior art keywords
- bed reactor
- fixed bed
- acid
- epsilon
- caprolactone
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D313/00—Heterocyclic compounds containing rings of more than six members having one oxygen atom as the only ring hetero atom
- C07D313/02—Seven-membered rings
- C07D313/04—Seven-membered rings not condensed with other rings
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Other In-Based Heterocyclic Compounds (AREA)
Abstract
The invention relates to the field of epsilon-caprolactone preparation, and discloses a epsilon-caprolactone preparation method and a epsilon-caprolactone preparation device. Wherein the method comprises the following steps: (I) Mixing an oxidant, a water carrying agent and a stabilizer in a raw material premixing tank, and then dehydrating through a first dehydrating tower to obtain a first product; (II) mixing the first product and acid in a first mixer, then carrying out a first reaction in a first fixed bed reactor, and dehydrating the obtained reaction product through a second dehydration tower to obtain a second product; (III) mixing the second product with cyclohexanone in a second mixer and then carrying out a second reaction in a third fixed bed reactor to obtain a crude ester; and (IV) rectifying to obtain epsilon-caprolactone. The epsilon-caprolactone prepared by the method has high yield.
Description
Technical Field
The invention relates to the field of preparation of epsilon-caprolactone, in particular to a preparation method and a device of epsilon-caprolactone.
Background
With the strengthening of global environmental awareness, domestic environmental protection policies are gradually tightened, and more strict requirements are also put forward on environmental pollution control. The epsilon-caprolactone is an important polymer synthesized by the monomer, is a material which can be completely biodegraded, and is a high-solubility substance when being used as a solvent, so that the epsilon-caprolactone has quite wide application and is widely valued at home and abroad.
However, the synthesis process is relatively complex, the requirements on production equipment and production safety are high, and the possibility of large-scale industrialization is restricted. The influence of the environmental protection policy also causes the increase of the demand and the price, which in turn restricts the application of the epsilon-caprolactone, but brings great space for the development of epsilon-caprolactone. At present, epsilon-caprolactone in China basically depends on import, and forms restriction on related industries in China.
In the prior art, peroxide acid is prepared by oxidizing organic acid with hydrogen peroxide in a stirred tank, and epsilon-caprolactone is prepared by reacting cyclohexanone with percarboxylic acid by utilizing the Bayer-Willig oxidation reaction principle after a certain amount of peroxide is stored.
CN1071923a discloses a process for producing epsilon-caprolactone, wherein the process comprises using a percarboxylic acid solution prepared by oxidizing an organic carboxylic acid in an organic solvent in the presence of hydrogen peroxide and a boric acid catalyst, feeding 0.012 mole or less of hydrogen peroxide per mole of percarboxylic acid of 1 to 1.5 mole or less of boric acid catalyst into a reaction system, and then reacting the aforementioned hexanone with the aforementioned percarboxylic acid to produce epsilon-caprolactone. That is, it has been proposed to oxidize carboxylic acids containing 2 to 4 carbon atoms with hydrogen peroxide under boric acid catalysis to produce percarboxylic acids (reaction while continuously removing water under azeotropic conditions), and then to oxidize cyclohexanone to produce epsilon-caprolactone. The percarboxylic acid and hydrogen peroxide have self-decomposition properties, and the use of a single stabilizer is poor in effect, so that the percarboxylic acid is liable to decompose, resulting in a decrease in yield, and consequently, both economy and safety are lowered. Boric acid is not separated from the system after the epsilon-caprolactone is prepared, and a large amount of epsilon-caprolactone is self-polymerized in the high-temperature rectification process, so that the product yield is reduced.
In CN202786068U, there are mentioned an epsilon-caprolactone preparation reactor with heat exchange equipment and an epsilon-caprolactone purification device with a plurality of rectification towers connected in series, which are continuous epsilon-caprolactone preparation devices, and the device is essentially a batch device, but the batch time is reduced, and the real continuity cannot be realized.
CN103570667a discloses a process for continuously preparing epsilon-caprolactone, in the presence of boric acid, continuously oxidizing a carboxylic acid solution with hydrogen peroxide in a plurality of stirred tanks with rectifying towers, continuously introducing the obtained peroxycarboxylic acid and cyclohexanone into a plurality of stirred tanks connected in series for reaction to obtain epsilon-caprolactone.
CN104003972a discloses a method for preparing caprolactone, mixing organic acid, hydrogen peroxide, organic solvent, stabilizer and catalyst at normal temperature, continuously stirring, dewatering, distilling to obtain product, reacting the product with cyclohexanone, and rectifying to separate epsilon-caprolactone. The method is simple, but does not involve the problems of specific rectification product separation and product stability maintenance, and meanwhile, the method is poor in safety and difficult to realize industrialization.
CN105646433a discloses a process for continuously preparing Gao Chunchun epsilon-caprolactone, which adopts a catalytic rectification technology, and the process comprises the steps of reacting in a tower, using a stirred reaction kettle as a supplementary means, and rectifying the product. The method is that the catalytic rectifying tower is filled with strong acid cation exchange resin or perfluorinated sulfonic acid resin in the preparation process. However, from the reaction mechanism, the obtaining of peroxides and the subsequent oxidation reaction are not possible at all with the same catalyst, and therefore there is a problem in the process. Meanwhile, the catalyst filled in the catalyst rectifying tower has the problem of loading and unloading, so that the catalyst can be industrialized to a lower degree.
In conclusion, research and development of a method for continuously preparing epsilon-caprolactone have important significance.
Disclosure of Invention
The invention aims to solve the problems that epsilon-caprolactone is easy to self-polymerize in rectification and the epsilon-caprolactone yield is low in the method disclosed by the prior art, and provides a preparation method and a device of epsilon-caprolactone. The product prepared by the method has high purity. The method has high conversion rate of the oxidant and cyclohexanone, high yield of the prepared epsilon-caprolactone, and can continuously, safely and efficiently prepare the epsilon-caprolactone with high purity.
In order to achieve the above object, the first aspect of the present invention provides a method for producing epsilon-caprolactone, wherein the method comprises:
(I) Mixing an oxidant, a water-carrying agent and a stabilizer in a raw material premixing tank 1, and dehydrating the obtained mixture through a first dehydrating tower 2 to obtain a first product;
(II) mixing the first product and an acid in a first mixer 3, and subjecting the obtained first mixture to a first reaction in a first fixed bed reactor 4, and dehydrating the obtained reaction product through a second dehydrating tower 5 to obtain a second product;
(III) mixing the second product with cyclohexanone in a second mixer 6 and subjecting the resulting second mixture to a second reaction in a third fixed-bed reactor 8 to obtain a crude ester;
(IV) rectifying the crude ester to obtain epsilon-caprolactone.
In a second aspect, the present invention provides an apparatus for producing epsilon-caprolactone, wherein the apparatus comprises a pretreatment system, a reaction system and a rectification system, which are sequentially connected;
wherein the pretreatment system comprises a raw material premixing tank 1, a first dehydration tower 2 and a first mixer 3; the first dehydration tower 2 is respectively connected with the raw material premixing tank 1 and the first mixer 3 through a circulating pump;
wherein the reaction system comprises a first fixed bed reactor 4, a second dehydration tower 5, a second mixer 6 and a third fixed bed reactor 8; the first mixer 3 is respectively connected with an acid tank 12 and the first fixed bed reactor 4; the second dehydration tower 5 is respectively connected with the first fixed bed reactor 4 and the third fixed bed reactor 8;
the rectification system comprises a rectification device, and the third fixed bed reactor 8 is connected with the rectification device.
Through the technical scheme, the technical scheme provided by the invention has the following advantages:
(1) The method of the invention avoids the problems of pollution and difficult separation of impurities caused by the use of the liquid acid catalyst in the prior art;
(2) The stabilizer used in the method can effectively inhibit the decomposition of intermediate products and target products;
(3) The method adopts the fixed bed reactor filled with the solid acid catalyst, abandons the use of a stirring kettle, ensures continuous production under the conditions of a certain residence time and partial circulation of reaction materials, and reduces the production cost due to the use of the solid acid catalyst and the reduction of waste liquid discharge.
(4) The method for preparing epsilon-caprolactone by adopting the device has the advantages of high conversion rate, stable operation, high product yield in the whole production process and continuous production.
Drawings
FIG. 1 is a schematic diagram of an apparatus for producing epsilon-caprolactone of the present invention.
Description of the reference numerals
1-raw material premixing tank 2-first dehydration tower 3-first mixer
4-first fixed bed reactor 5-second dehydration tower 6-second mixer
7-second fixed bed reactor 8-third fixed bed reactor 9-first separation column
10-second separation tower 11-refining tower 12-acid tank
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
The first aspect of the invention provides a method for preparing epsilon-caprolactone, which comprises the following steps:
(I) Mixing an oxidant, a water-carrying agent and a stabilizer in a raw material premixing tank 1, and dehydrating the obtained mixture through a first dehydrating tower 2 to obtain a first product;
(II) mixing the first product and an acid in a first mixer 3, and subjecting the obtained first mixture to a first reaction in a first fixed bed reactor 4, and dehydrating the obtained reaction product through a second dehydrating tower (5) to obtain a second product;
(III) mixing the second product with cyclohexanone in a second mixer 6 and subjecting the resulting second mixture to a second reaction in a third fixed-bed reactor 8 to obtain a crude ester;
(IV) rectifying the crude ester to obtain epsilon-caprolactone.
Aiming at the problems that in the method disclosed by the prior art, peroxide is easy to decompose, epsilon-caprolactone is easy to self-polymerize in rectification, and an added stabilizer is difficult to remove, and the problems of low percarboxylic acid yield, poor safety and low epsilon-caprolactone yield; the inventor of the present invention found through experiments that: the fixed bed reactor filled with the solid acid catalyst can avoid the problems of pollution and difficult separation of impurities caused by the use of the liquid acid catalyst in the prior art; moreover, the method for preparing epsilon-caprolactone by adopting the device provided by the invention has the advantages of stable operation in the whole production process, high product purity and continuous production.
According to the invention, epsilon-caprolactone (epsilon-caprolactone) has the molecule C 6 H 10 O 2 The structural formula is shown as formula (1):
according to the invention, in the step (I), the stabilizer is a compound stabilizer, and the stabilizer is at least two selected from picolinic acid, picoline, lutidine, 8-hydroxyquinoline, tributyl phosphate and dipicolinic acid, and the decomposition of peroxide can be reduced by adopting the compound stabilizer, so that the safety and the economy are improved; in addition, in the present invention, preferably, the stabilizer is selected from two kinds of optional stabilizers selected from picolinic acid, dipicolinic acid, picoline, lutidine, 8-hydroxyquinoline and tributyl phosphate, and the weight ratio of the amounts of the two optional stabilizers in picolinic acid, dipicolinic acid, picoline, lutidine, 8-hydroxyquinoline and tributyl phosphate is 1: (1-20); the weight ratio of the optional three stabilizers in picolinic acid, dipicolinic acid, picoline, lutidine, 8-hydroxyquinoline and tributyl phosphate is 1: (1-20): (1-20), more preferably 1: (1-5): (1-6); more preferably, the stabilizer is dipicolinic acid and picoline; wherein the dipicolinic acid may be a pyridine 2,5 dicarboxylic acid.
According to the present invention, in actual production, the stabilizer must be added to the raw material premix tank 1, so that not only can the stability of the peroxide as a raw material in the reaction system be ensured, but also the stability of the intermediate product in the reactor can be ensured; and its components are recovered to the system after being withdrawn from the top of the first separation column 9 and the bottom of the refining column 11, respectively, so that it is necessary to periodically analyze the content of the components in the stabilizer in the raw material mixing tank 1.
In the invention, the composite stabilizer is adopted, and is added into the raw material premixing tank 1, and in the specific proportion range, the decomposition of intermediate products and target products can be effectively inhibited, and the whole process is safe.
According to the invention, the oxidizing agent is hydrogen peroxide. In the present invention, the concentration of the oxidizing agent is 10 to 70%, preferably 10 to 50%. Hydrogen peroxide (hydrogen peroxide), formula H 2 O 2 . Pure hydrogen peroxide is light blue viscous liquid, can be mixed with water in any proportion, is a strong oxidant, and the aqueous solution is commonly called hydrogen peroxide and is colorless transparent liquid.
In the invention, the water-carrying agent is added while the oxidant is dehydrated, so that the safety can be ensured and the reaction rate can be not reduced.
According to the present invention, the first dehydration tower 2 performs dehydration by using the azeotropic effect of the oxidizing agent and the water-carrying agent, and in the present invention, the water-carrying agent is mixed while the oxidizing agent is concentrated, so that the safety can be ensured to the maximum extent while the concentration of the oxidizing agent is provided.
According to the invention, the water carrying agent is selected from one or more of ethyl acetate, ethyl propionate, methyl propionate, isopropyl acetate and propyl formate, preferably ethyl acetate.
According to the invention, the weight ratio of the amounts of the oxidizing agent, the water-carrying agent and the stabilizing agent is 1: (4-15): (0.001-0.02); more preferably, the oxidant, the water-carrying agent and the stabilizer are used in an amount of 1 by weight: (6-12): (0.005-0.01).
According to the invention, in the step (II), an azeotrope of water and the first product is obtained at the top of the first dehydration tower 2, and is layered after condensation, the water carrying agent at the upper layer of the phase separator returns to the first dehydration tower 2, and the water phase at the lower layer is extracted; the first dehydration tower 2 is a mixture of an oxidant and a water-carrying agent, and the mixture is pumped into the first mixer 3 through a pump.
According to the invention, the acid is selected from one or more of formic acid, acetic acid and propionic acid, preferably acetic acid.
According to the invention, the molar ratio of the oxidant to the acid used is 1 (1-5), preferably 1: (1.5-2.5).
According to a preferred embodiment of the present invention, the present invention confirms that the content of the oxidizing agent (hydrogen peroxide) in the second fixed bed reactor (7) is not more than 1wt%, preferably 0.06 to 1wt% by continuous chinese experiment; too high of the two can accelerate the self-polymerization of epsilon-caprolactone in the subsequent process. The content of the peroxy acid is not preferably less than 18wt%, preferably 18 to 22wt%, and too high a content may cause an increase in risk.
According to the invention, in actual production, the first mixer 3 is a three-strand mixer.
According to the invention, the conditions of the first reaction include: the temperature is 30-90 ℃, the pressure is-0.1 MPa to 0MPa, and the time is 0.2-3h; more preferably, the temperature is 40-90 ℃, the pressure is-0.095 MPa to-0.05 MPa, and the time is 0.5-1h.
According to the invention, in step (III), the acid is stored in the acid tank 12. The acid is preheated and then enters a first mixer 3, is mixed with the first product, and then enters a first fixed bed reactor 4 filled with a solid acid catalyst, and part of the reacted material is recycled to the first mixer 3 and the other part enters a second dehydration tower 5.
According to the invention, the molar ratio of the second product to the amount of cyclohexanone is 1: (1-5), preferably 1: (1.5-3).
According to the invention, the conditions of the second reaction include: the temperature is 30-100 ℃, the pressure is 0MPa to 0.1MPa, and the time is 0.2-2h; more preferably, the temperature is 40-90 ℃, the pressure is 0.08MPa to 0.2MPa, and the time is 0.5-1h.
According to the invention, the method further comprises: in step (III), the second product is treated by a second fixed bed reactor 7; preferably, the second fixed bed reactor 7 is charged with the oxidizing agent.
According to the invention, the first fixed bed reactor 4, the second fixed bed reactor 7 and the third fixed bed reactor 8 are all jacketed solid bed reactors; preferably, the first fixed bed reactor 4 and the second fixed bed reactor 7 are filled with a solid acid catalyst; wherein the solid acid catalysts are respectively filled in the tube arrays arranged in the first fixed bed reactor 4; in the present invention, the peripheries of the tube arrays in the first fixed bed reactor 4 and the second fixed bed reactor 7 are filled with a heat medium (circulated hot water), so that the reaction temperature can be rapidly raised, and the reaction can be ensured to be carried out toward the production product by controlling the temperature of the hot water; the periphery of the tube array in the third fixed bed reactor 8 is filled with cold medium (circulating cold water), and the arrangement can effectively draw heat generated by the reaction, control the reaction degree and reduce the decomposition of epsilon-caprolactone.
According to the present invention, the active component-supported molecular sieve catalyst packed in the first fixed bed reactor 4 and the second fixed bed reactor 7, wherein the active component-supported molecular sieve catalyst is a carrier and an active component supported on the carrier, wherein the carrier is selected from the group consisting of B 2 O 3 /γ-Al 2 O 3 One or more of ZSM-5 (H-ZSM-5), modified beta molecular sieve and modified Y molecular sieve, wherein the active component is phosphotungstic heteropolyacid and/or boric acid.
In the present invention, the active component-supporting molecular sieve catalyst is packed in the first fixed bed reactor 4 and the second fixed bed reactor 7, wherein the first fixed bed reactor 4 is provided with a pump capable of self-circulation, and the second fixed bed reactor 7 is provided with a dehydration column capable of removing product water. The arrangement of the device can effectively reduce the water content in the second product and ensure that the reaction is carried out towards the direction of the production product, so that the production can be continuous.
According to the present invention, the third fixed bed reactor 8 is filled with an organic acid synthetic resin catalyst.
Wherein the organic acid synthetic resin catalyst is one of Amberlyst-15, 001×7 strong acid styrene cation exchange resin and D001 macroporous strong acid styrene cation exchange resin, wherein the D001 macroporous strong acid styrene cation exchange resin is preferable.
Wherein Amberlyst-15, which is a solid acid catalyst, belongs to ion exchange resin, and is a strongly acidic catalyst formed by sulfonation on the basis of macroporous styrene divinylbenzene copolymer. The detailed parameters are as follows: the mass total exchange capacity is more than or equal to 4.60, and the specific surface area is 30-50m 2 Per g, pore volume is 0.2-0.4ml/g, and granularity (0.315-1.25 mm) is more than or equal to 96%.
Wherein the 001×7 strongly acidic styrene cation exchange resin has sulfonic acid group (-SO) on the polymer matrix with styrene-divinylbenzene copolymer cross-linked structure 3 H) Styrene-divinylbenzene with resin structure, functional group-SO 3 H, brown to tan spherical particles. The detailed parameters are as follows: the mass total exchange capacity is more than or equal to 4.80, the uniformity coefficient is 1.6, the ball rate after grinding is more than or equal to 90 percent, and the granularity (0.315-1.25 mm) is more than or equal to 95 percent.
Wherein, the D001 macroporous strong acid styrene cation exchange resin has a resin structure of styrene-divinylbenzene and a functional group-SO 3 H, light hump opaque spherical particles, other parameters are: the mass total exchange capacity is more than or equal to 4.70, and the specific surface area is 35-58m 2 Per g, pore volume is 0.2-0.4ml/g, and granularity (0.315-1.25 mm) is more than or equal to 95%.
According to the present invention, the third fixed bed reactor 8 is filled with the organic acid synthetic resin catalyst and provided with a self-circulation device, and this arrangement can maintain the components in the separation column 1 stable, which is advantageous for continuous production.
According to the invention, in step (III), in a second mixer 6, the second product is fed into a third fixed bed reactor 8 with cyclohexanone and unreacted material in a certain ratio, and after reaction, part of the material is taken out and fed into a rectifying device.
In actual production, the residence time of the material (the second product) in the fixed bed reactor at the catalyst surface is measured in terms of weight hourly space velocity, defined as 1m in 1h 3 Volume of material (m) through which the catalyst flows 3 /(m 3 H), i.e., h -1 。
In the present invention, in the step (II), the weight hourly space velocity is from 0.5 to 2h -1 Preferably 0.6-1.5h -1 More preferably0.6-0.8h -1 An initial weight hourly space velocity of 0.5h -1 The circulation ratio is 10, and according to the content of the target product, the circulation amount can be gradually reduced while the airspeed is increased.
In the present invention, in the step (III), the weight hourly space velocity is 1 to 3 hours -1 Preferably 2 to 2.5h -1 An initial weight hourly space velocity of 1h -1 The circulation ratio is 5, and according to the content of the target product, the circulation amount can be gradually reduced while the airspeed is increased.
In addition, the "recycle ratio" is the ratio of the flow rate of the material returned to the inlet in the outlet of the third fixed bed reactor to the flow rate of the portion of the separation column 1.
According to the present invention, more preferably, the oxidizing agent is hydrogen peroxide, the water-carrying agent is ethyl acetate, and in the present invention, the reaction for obtaining peracetic acid by performing the first reaction in the first fixed bed reactor 4 is:
in the present invention, the reaction in the first fixed bed reactor 4 is an endothermic reaction, and the shell side is hot water.
In the present invention, the second reaction in the third fixed bed reactor 8 gives epsilon-caprolactone as follows:
in the present invention, the reaction in the third fixed bed reactor 8 is exothermic and the shell side is cold water.
In actual production, the circulating water passes through the third fixed bed reactor 8 and then goes to the first fixed bed reactor 4.
In the present invention, the second fixed bed reactor 7 is used as a supplement to the first fixed bed reactor 4 in order to reduce the hydrogen peroxide content and ensure efficient subsequent reactions.
In the present invention, the reaction in the second fixed bed reactor 7 is an endothermic reaction, and the shell side is hot water.
In actual production, the circulating water passes through the third fixed bed reactor 8 and then goes to the first fixed bed reactor 4 and the second fixed bed reactor 7.
According to the invention, in the step (IV), the material to be rectified sequentially enters a first separation tower 9 and a second separation tower 10, and water preparation agent and cyclohexanone are removed respectively; meanwhile, the first separation tower 9 and the second separation tower 10 form a multi-effect rectifying system, so that energy consumption can be effectively reduced.
According to the invention, the material in the tower bottom of the second separation tower 10 enters a refining tower, light components are separated from the tower top under certain vacuum and temperature, and epsilon-caprolactone with the content of not less than 99.4% is obtained from the tower top, and heavy components are separated from the tower bottom.
According to the invention, the first separation column 9 is operated at a temperature of 80 to 130 ℃, preferably 90 to 120 ℃; the operating pressure is 1 to 30kPa, preferably 4 to 25kPa.
According to the invention, the second separation column 10 is operated at a temperature of 80-130 ℃, preferably 100-120 ℃; the operating pressure is from 0.1 to 10kPa, preferably from 0.3 to 5kPa.
Through strict analog calculation and Chinese experiments, in actual production, the first separation tower 9 and the second separation tower 10 form a double-effect rectifying tower system adopting a concurrent flow process, namely, the top steam of the first separation tower 9 is used as a heating medium of a reboiler of the second separation tower 10; the preliminary estimation saves about 38% of energy compared with the traditional system.
According to the invention, the operating temperature of the refining column 11 is between 90 and 140 ℃, preferably between 110 and 130 ℃; the operating pressure is from 0.5 to 10kPa, preferably from 1 to 8kPa.
The second aspect of the invention provides a device for preparing epsilon-caprolactone, wherein the device comprises a pretreatment system, a reaction system and a rectification system which are sequentially connected;
wherein the pretreatment system comprises a raw material premixing tank 1, a first dehydration tower 2 and a first mixer 3; the first dehydration tower 2 is respectively connected with the raw material premixing tank 1 and the first mixer 3 through a circulating pump;
wherein the reaction system comprises a first fixed bed reactor 4, a second dehydration tower 5, a second mixer 6 and a third fixed bed reactor 8; the first mixer 3 is respectively connected with an acid tank 12 and the first fixed bed reactor 4; the second dehydration tower 5 is respectively connected with the first fixed bed reactor 4 and the third fixed bed reactor 8;
the rectification system comprises a rectification device, and the third fixed bed reactor 8 is connected with the rectification device.
According to the invention, the rectifying device comprises a first separation tower 9, a second separation tower 10 and a refining tower 11 which are connected in sequence.
According to the present invention, the first separation column 9, the second separation column 10 and the refining column 11 each include a condenser, a reboiler, a condensing tank and a bottom discharge pump.
According to the invention, the plant also comprises a second fixed-bed reactor 7, and the second fixed-bed reactor 7 is connected to the first fixed-bed reactor 4 and the third fixed-bed reactor 8, respectively.
The method and the device provided by the invention have the advantages of wide raw material selection range, high safety coefficient, low system energy consumption and low waste discharge, and can realize industrialized continuous production. Meanwhile, the expansion production can be performed according to actual production conditions.
The present invention will be described in detail by examples.
Example 1
This example is intended to illustrate the preparation of epsilon-caprolactone using the apparatus and method of the present invention.
In the apparatus for producing epsilon-caprolactone shown in fig. 1, epsilon-caprolactone was produced by the following steps:
the tubes arranged in the first fixed bed reactor 4 and the second fixed bed reactor 7 are filled with H-ZSM-5 catalyst loaded with heteropolyacid.
The column tube arranged in the third fixed bed reactor 8 is filled with organic acid resin catalyst D001 macroporous strong acid styrene cation exchange resin.
Wherein the first fixed bed reactor 4, the second fixed bed reactor 7 and the third fixed bed reactor 8 are all jacketed solid bed reactors; the peripheries of the tubes in the first fixed bed reactor 4 and the second fixed bed reactor 7 are filled with a heat medium (circulated hot water); the periphery of the tube array in the third fixed bed reactor 8 is filled with a cold medium (circulated cold water).
The first step: preparation of the first product
Mixing oxidant hydrogen peroxide, water-carrying agent ethyl acetate and a composite stabilizer in a raw material premixing tank 1, and dehydrating the obtained mixture through a first dehydrating tower 2 to obtain a first product;
wherein the weight ratio of the usage amount of the oxidant, the water-carrying agent and the stabilizer is 1:6:0.008; the selected composite stabilizer is lutidine, 8-hydroxyquinoline and pyridine 2,5 dicarboxylic acid according to the proportion of 1:4:5, mixing, wherein the mass fraction of the raw material hydrogen peroxide is 50%.
And a second step of: preparation of the second product
Mixing acetic acid and a first product in a first mixer 3, carrying out a first reaction on the obtained first mixture in a first fixed bed reactor 4, and dehydrating the obtained reaction product through a second dehydrating tower 5 to obtain a second product;
wherein the weight ratio of acetic acid to the first product is 1:1, and the molar ratio of the oxidant to the acid is 1:3, acid excess, space velocity of the catalyst of 1m 3 /(m 3 H) initial airspeed of 0.5m 3 /(m 3 H) the circulation ratio is 10; wherein the conditions of the first reaction include: the temperature is 60 ℃, the pressure is-0.08 MPa, and the time is 1h.
The materials are fully circulated in the first dehydration tower 2 and the second fixed bed reactor 7, and the components of the tower bottom materials of the analysis dehydration tower after 60min are as follows:
the peroxyacetic acid mixed solution mainly comprises the following components (weight percent, excluding catalysts and stabilizers):
peracetic acid 20.05%
Acetic acid 51.6%
Ethyl acetate 28.2%
Hydrogen peroxide 0.06%
The conversion of hydrogen peroxide was 99.3% and the selective yield of peroxyacetic acid was 96.5%.
And a third step of: preparation of epsilon-caprolactone
Mixing the second product and cyclohexanone according to a molar ratio of 1:2.5, then entering a third fixed bed reactor 8, simultaneously starting to inject cold water into a jacket for heat extraction, and carrying out a second reaction in the third fixed bed reactor 8 to obtain crude ester; the outlet material was fully circulated and after 120min the outlet composition was analyzed.
Wherein the conditions of the second reaction include: the temperature is 70 ℃, the pressure is 0.04MPa, and the time is 1h; weight hourly space velocity of 2h -1 ；
The epsilon-caprolactone mixed solution mainly comprises the following components (weight percent, excluding catalysts and stabilizers):
epsilon-caprolactone 21.2%
Cyclohexanone 0.16%
Peracetic acid 2.22%
Acetic acid 53.3%
Ethyl acetate 23.1%
Hydrogen peroxide 0.01%
The conversion of cyclohexanone was 99.2% and the selectivity yield of epsilon-caprolactone was 99.8%. The conversion of peroxy acid was 86.4% and the selectivity yield to epsilon-caprolactone was 99.9%.
Fourth step: epsilon-caprolactone
The materials sequentially pass through a first separation tower 9, a second separation tower 10 and a refining tower 11.
Obtaining epsilon-caprolactone with the content of 99.9 weight percent at the outlet of a reflux tank at the top of the refining tower 11; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 96.4 percent.
Example 2
Epsilon-caprolactone was prepared in the same manner as in example 1 except that the catalyst was filled in the same manner as in example 1: the raw materials and the proportions are changed, in particular:
the first step: preparation of the first product
Mixing oxidant hydrogen peroxide, water-carrying agent ethyl propionate and a composite stabilizer in a raw material premixing tank 1, and dehydrating the obtained mixture through a first dehydrating tower 2 to obtain a first product;
wherein the weight ratio of the usage amounts of the oxidant, the water-carrying agent and the stabilizer is 1:8:0.006; the selected composite stabilizer is 8-hydroxyquinoline and pyridine 2,5 dicarboxylic acid according to the proportion of 1:1, mixing, wherein the mass fraction of the raw material hydrogen peroxide is 30%.
And a second step of: preparation of the second product
The molar ratio of the propionic acid to the hydrogen peroxide used was 1:1.5, and the space velocity of the catalyst was 1m 3 /(m 3 H) initial airspeed of 0.6m 3 /(m 3 H) the circulation ratio is 15; wherein the conditions of the first reaction include: the temperature was 75℃and the pressure-0.09 MPa for 1.5h.
The materials are fully circulated in the first dehydration tower 2 and the second fixed bed reactor 7, and the components of the tower bottom materials of the analysis dehydration tower after 90 minutes are as follows:
peroxypropionic acid 19.6%
Propionic acid 52.04%
Ethyl propionate 28.3%
Hydrogen peroxide 0.06%
The conversion of hydrogen peroxide was 99.3% and the selective yield of peroxypropionic acid was 94.3%.
And a third step of: preparation of epsilon-caprolactone
Mixing a second product and cyclohexanone according to a molar ratio of 1:2 in a second fixed bed reactor 8, simultaneously starting to inject cold water into a jacket for heating, and performing a second reaction in a third fixed bed reactor 8 to obtain crude ester; the outlet material was fully circulated and after 120min the outlet composition was analyzed.
Wherein the conditions of the second reaction include: the temperature is 80 ℃, the pressure is 0.06MPa, and the time is 1.5h; weight hourly space velocity of 2h -1 ；
The calculated conversion of cyclohexanone was 98.5% and the selective yield to epsilon-caprolactone was 92.5%;
reference example 1 gave an epsilon-caprolactone content of 99.7% by weight at the outlet of the reflux drum at the top of the rectifying column 11; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 95.2 percent.
Example 3
Epsilon-caprolactone was prepared in the same manner as in example 1 except that the catalyst was filled in the same manner as in example 1:
the first step: preparation of the first product
Mixing oxidant hydrogen peroxide, water-carrying agent propyl formate and a composite stabilizer in a raw material premixing tank 1, and dehydrating the obtained mixture through a first dehydration tower 2 to obtain a first product;
wherein the weight ratio of the usage amount of the oxidant, the water-carrying agent and the stabilizer is 1:8:0.01; the selected composite stabilizer is picoline and lutidine according to the proportion of 2:3, mixing, wherein the mass fraction of the raw material hydrogen peroxide is 50%.
And a second step of: preparation of the second product
As shown in example 1, is different in that
The molar ratio of the amounts of formic acid and hydrogen peroxide used was 1:2, the space velocity of the catalyst was 1m 3 /(m 3 H) initial airspeed of 0.5m 3 /(m 3 H) the circulation ratio is 10; wherein the conditions of the first reaction include: the temperature is 55 ℃, the pressure is-0.06 MPa, and the time is 1.5h.
The materials are fully circulated in the first dehydration tower 2 and the second fixed bed reactor 7, and the components of the tower bottom materials of the analysis dehydration tower after 60min are as follows:
the peroxyformic acid mixed solution mainly comprises the following components (weight percent, excluding catalysts and stabilizers):
peroxyformic acid 18.2%
Formic acid 51.9%
Propyl formate 29.3%
Hydrogen peroxide 0.6%
The calculated conversion of hydrogen peroxide was 99%.
And a third step of: preparation of epsilon-caprolactone
Mixing a second product and cyclohexanone according to a molar ratio of 1:1.8, then in a second fixed bed reactor 8, simultaneously starting a jacket to be filled with cold water for heat extraction, and carrying out a second reaction in a third fixed bed reactor 8 to obtain crude ester; the outlet material was fully circulated and after 120min the outlet composition was analyzed.
Wherein the conditions of the second reaction include: the temperature is 65 ℃, the pressure is 0.09MPa, and the time is 1h; weight hourly space velocity of 2h -1 ；
The calculated conversion of cyclohexanone was 99% and the selective yield to epsilon-caprolactone was 82.2%; the conversion of peroxy acid was 86.4% and the selectivity yield to epsilon-caprolactone was 84.2%.
Fourth step: epsilon-caprolactone
The materials sequentially pass through a first separation tower 9, a second separation tower 10 and a refining tower 11.
Obtaining epsilon-caprolactone with the content of 99.5 weight percent at the outlet of a reflux tank at the top of the refining tower 11; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 90.2 percent.
Example 4
Epsilon-caprolactone was prepared by the same equipment and method as in example 1 except that: in the first step, the weight ratio of the usage amount of the oxidant, the water-carrying agent and the stabilizer is 1:4, a step of; 0.01 is selected from the compound stabilizer of lutidine and dipicolinate according to the proportion of 1:3, mixing, wherein the mass fraction of the raw material hydrogen peroxide is 50%.
As a result, epsilon-caprolactone was obtained in an amount of 99.4% by weight; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 90.5 percent.
Example 5
Epsilon-caprolactone was prepared by the same equipment and method as in example 1 except that:
in the first step, the weight ratio of the usage amount of the oxidant, the water-carrying agent and the stabilizer is 1:3:0.05; the selected composite stabilizer is picolinic acid, picolinic acid and tributyl phosphate according to a proportion of 1:1:3, mixing, wherein the mass fraction of the raw material hydrogen peroxide is 50%.
In the second step, the use of acetic acid and hydrogen peroxideThe molar ratio of the amounts is 1:2, space velocity of the catalyst is 1m 3 /(m 3 H) initial airspeed of 0.6m 3 /(m 3 H) the circulation ratio is 10; wherein the conditions of the first reaction include: the temperature is 50 ℃, the pressure is-0.08 MPa, and the time is 0.8h.
As a result, epsilon-caprolactone was obtained in an amount of 99.4% by weight; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 91.2 percent.
Comparative example 1
Epsilon-caprolactone was prepared by the same equipment and method as in example 1 except that:
the stabilizer is selected from lutidine;
in the second step, the third step was identical to example 1.
As a result, epsilon-caprolactone was obtained in an amount of 98.1% by weight; the yield of epsilon-caprolactone during purification was calculated to be 80.3%.
Comparative example 2
Epsilon-caprolactone was prepared by the same equipment and method as in example 1 except that:
the stabilizer is pyridine 2,5 dicarboxylic acid;
in the second step, the third step was identical to example 1.
As a result, epsilon-caprolactone was obtained in an amount of 99.1% by weight; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is 84.3 percent.
Comparative example 3
Epsilon-caprolactone was prepared by the same equipment and method as in example 1 except that:
the first fixed bed reactor 4 and the third fixed bed reactor 7 are catalyst exchanged for Amberlyst-15.
As a result, epsilon-caprolactone was obtained in an amount of 99.2% by weight; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 83.3 percent.
Comparative example 4
Epsilon-caprolactone was prepared by the same equipment and method as in example 1 except that:
the first fixed bed reactor 4 and the third fixed bed reactor 7 were replaced with 001×7 strongly acidic styrene-based cation exchange resins.
As a result, epsilon-caprolactone was obtained in an amount of 99.3% by weight; according to the molar ratio, the yield of epsilon-caprolactone in the purification process is calculated to be 85.1 percent.
The results show that the device and the method can continuously prepare high-quality epsilon-caprolactone, have little by-product yield, and have the advantages of high yield, low consumption of oxidant and cyclohexanone, good safety and the like.
Whereas comparative examples 1 and 2, because they do not use a complex stabilizer, do not have high yields due to decomposition of epsilon-caprolactone in a fixed bed reactor and column system during the reaction.
In comparative example 3, amberlyst-15 was packed in the column tubes provided in the first fixed bed reactor 4 and the third fixed bed reactor 7, and it was preliminarily judged that Amberlyst-15 was relatively small in mass total exchange capacity, resulting in a lower yield of epsilon-caprolactone.
The tubes arranged in the first fixed bed reactor 4 and the third fixed bed reactor 7 in comparative example 4 were filled with 001X 7 strongly acidic styrene-based cation exchange resin, and the reaction proceeded to a relatively low extent due to the relatively high water content thereof, so that the epsilon-caprolactone yield was low.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (23)
1. A process for the preparation of epsilon-caprolactone, comprising:
(I) Mixing an oxidant, a water-carrying agent and a stabilizer in a raw material premixing tank (1), and dehydrating the obtained mixture through a first dehydrating tower (2) to obtain a first product; the stabilizer is at least two selected from picolinic acid, dipicolinic acid, picoline, lutidine, 8-hydroxyquinoline, tributyl phosphate and dipicolinic acid;
(II) mixing the first product and an acid in a first mixer (3), and subjecting the obtained first mixture to a first reaction in a first fixed bed reactor (4), and dehydrating the obtained reaction product through a second dehydrating tower (5) to obtain a second product; the first fixed bed reactor (4) is filled with a molecular sieve catalyst loaded with active components, the molecular sieve catalyst comprises a carrier and the active components loaded on the carrier, and the carrier comprises B 2 O 3 /γ-Al 2 O 3 One or more of H-ZSM-5, modified beta molecular sieve and modified Y molecular sieve, wherein the active components are phosphotungstic heteropolyacid and/or boric acid;
(III) mixing the second product with cyclohexanone in a second mixer (6) and subjecting the resulting second mixture to a second reaction in a third fixed-bed reactor (8) to obtain a crude ester; the third fixed bed reactor (8) is filled with an organic acid synthetic resin catalyst, wherein the organic acid synthetic resin catalyst is D001 macroporous strong acid styrene cation exchange resin;
(IV) rectifying the crude ester to obtain epsilon-caprolactone;
the method is carried out in an epsilon-caprolactone device, and the device comprises a pretreatment system, a reaction system and a rectification system which are sequentially connected;
wherein the pretreatment system comprises a raw material premixing tank (1), a first dehydration tower (2) and a first mixer (3); the first dehydration tower (2) is respectively connected with the raw material premixing tank (1) and the first mixer (3) through a circulating pump;
wherein the reaction system comprises a first fixed bed reactor (4), a second dehydration tower (5), a second mixer (6) and a third fixed bed reactor (8); the first mixer (3) is respectively connected with an acid tank (12) and the first fixed bed reactor (4); the second dehydration tower (5) is respectively connected with the first fixed bed reactor (4) and the third fixed bed reactor (8);
the rectification system comprises a rectification device, and the third fixed bed reactor (8) is connected with the rectification device.
2. The method of claim 1, wherein the oxidizing agent is hydrogen peroxide; the concentration of the oxidant is 10-70%.
3. The method of claim 1, wherein the water-carrying agent is selected from one or more of ethyl acetate, ethyl propionate, methyl propionate, isopropyl acetate, and propyl formate.
4. A method according to any one of claims 1 to 3, wherein the oxidizing agent, the water-carrying agent and the stabilizing agent are used in an amount of 1 by weight: (4-15): (0.001-0.02).
5. The method of claim 4, wherein the oxidant, the water-carrying agent and the stabilizer are used in an amount of 1 by weight: (6-12): (0.005-0.01).
6. The method of claim 1, wherein in step (II), the acid is selected from one or more of formic acid, acetic acid, and propionic acid.
7. The method of claim 1 or 6, wherein the oxidant and the acid are used in a molar ratio of 1: (1-5).
8. The method of claim 7, wherein the oxidant and the acid are used in a molar ratio of 1: (1.5-2.5).
9. The method of claim 1, wherein the conditions of the first reaction comprise: the temperature is 30-90 ℃, the pressure is-0.1 MPa to 0MPa, and the time is 0.2-3h.
10. The method of claim 9, wherein the conditions of the first reaction comprise: the temperature is 40-90 ℃, the pressure is-0.095 MPa to-0.05 MPa, and the time is 0.5-1h.
11. A process according to claim 1, wherein in step (III), the molar ratio of the second product to the amount of cyclohexanone is 1: (1-5).
12. The process according to claim 11, wherein in step (III), the molar ratio of the second product to the amount of cyclohexanone is 1: (1.5-3).
13. The method of claim 1, wherein the conditions of the second reaction comprise: the temperature is 30-100deg.C, the pressure is 0MPa to 0.1MPa, and the time is 0.2-2h.
14. The method of claim 13, wherein the conditions of the second reaction comprise: the temperature is 40-90 ℃, the pressure is 0.08-0.2 MPa, and the time is 0.5-1h.
15. The method of claim 1, wherein in step (II), the conditions of the first reaction further comprise: weight hourly space velocity of 0.5-2h -1 ；
In step (III), the conditions of the second reaction further comprise: weight hourly space velocity of 1-3h -1 。
16. The method of claim 1, wherein in step (II), the conditions of the first reaction further comprise: weight hourly space velocity of 0.6-1.5h -1 ；
In step (III), the conditions of the second reaction further comprise: weight hourly space velocity of 2-2.5h -1 。
17. The method of claim 1, wherein the method further comprises: in step (III), the second product is treated by a second fixed bed reactor (7).
18. The method according to claim 17, wherein the second fixed bed reactor (7) is filled with solid acid catalyst.
19. The method according to claim 1 or 18, wherein the first fixed bed reactor (4) and the periphery of the column of the second fixed bed reactor (7) are filled with a thermal medium.
20. The method according to claim 1, wherein the periphery of the column tubes within the third fixed bed reactor (8) is filled with a cold medium.
21. The method according to claim 1, wherein the rectifying device comprises a first separation column (9), a second separation column (10) and a refining column (11) connected in sequence.
22. The method according to claim 21, wherein the first separation column (9), the second separation column (10) and the refining column (11) each comprise a condenser, a reboiler, a condensing tank and a bottom discharge pump.
23. The method according to claim 21, wherein the apparatus further comprises a second fixed bed reactor (7), and the second fixed bed reactor (7) is connected to the first fixed bed reactor (4) and the third fixed bed reactor (8), respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010674122.4A CN111763192B (en) | 2020-07-14 | 2020-07-14 | Preparation method and device of epsilon-caprolactone |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010674122.4A CN111763192B (en) | 2020-07-14 | 2020-07-14 | Preparation method and device of epsilon-caprolactone |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111763192A CN111763192A (en) | 2020-10-13 |
| CN111763192B true CN111763192B (en) | 2023-09-12 |
Family
ID=72726462
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010674122.4A Active CN111763192B (en) | 2020-07-14 | 2020-07-14 | Preparation method and device of epsilon-caprolactone |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111763192B (en) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1071923A (en) * | 1990-04-25 | 1993-05-12 | 宇部兴产株式会社 | The method for preparing 6-caprolactone |
| CN102304117A (en) * | 2011-09-19 | 2012-01-04 | 武汉理工大学 | Method for synthesizing epsilon-caprolactone |
| CN102584776A (en) * | 2011-01-12 | 2012-07-18 | 中国石油化工集团公司 | Method for preparing epsilon-caprolactone |
| CN102584775A (en) * | 2011-01-12 | 2012-07-18 | 中国石油化工集团公司 | Method for preparing epsilon-caprolactone |
| CN104003972A (en) * | 2014-04-28 | 2014-08-27 | 安徽红太阳新材料有限公司 | Method for preparing caprolactone |
| CN108863883A (en) * | 2018-08-17 | 2018-11-23 | 湖南聚仁化工新材料科技有限公司 | A method of preparing anhydrous Perpropionic Acid |
| CN110183417A (en) * | 2019-04-30 | 2019-08-30 | 武汉理工大学 | A kind of method and device of catalytic reaction rectification continuous production 6-caprolactone |
-
2020
- 2020-07-14 CN CN202010674122.4A patent/CN111763192B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1071923A (en) * | 1990-04-25 | 1993-05-12 | 宇部兴产株式会社 | The method for preparing 6-caprolactone |
| CN102584776A (en) * | 2011-01-12 | 2012-07-18 | 中国石油化工集团公司 | Method for preparing epsilon-caprolactone |
| CN102584775A (en) * | 2011-01-12 | 2012-07-18 | 中国石油化工集团公司 | Method for preparing epsilon-caprolactone |
| CN102304117A (en) * | 2011-09-19 | 2012-01-04 | 武汉理工大学 | Method for synthesizing epsilon-caprolactone |
| CN104003972A (en) * | 2014-04-28 | 2014-08-27 | 安徽红太阳新材料有限公司 | Method for preparing caprolactone |
| CN108863883A (en) * | 2018-08-17 | 2018-11-23 | 湖南聚仁化工新材料科技有限公司 | A method of preparing anhydrous Perpropionic Acid |
| CN110183417A (en) * | 2019-04-30 | 2019-08-30 | 武汉理工大学 | A kind of method and device of catalytic reaction rectification continuous production 6-caprolactone |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111763192A (en) | 2020-10-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108484545B (en) | Method and system for continuously synthesizing furan dicarboxylic acid | |
| US11299450B2 (en) | System and process for co-producing dimethyl carbonate and ethylene glycol | |
| CN101255109B (en) | Process for producing acrylic acid by dehydrating biomass lactic acid | |
| KR20150056645A (en) | Method and device for coproducing cyclohexanol and alkanol | |
| CN109456190A (en) | A kind of method of the continuous synthesizing propylene glycol monomethyl ether acetate of the highly selective catalytic distillation of low temperature | |
| JP7305848B2 (en) | Method and apparatus for producing high-purity 1,6-hexanediol | |
| JPH0235728B2 (en) | ||
| CN110759801A (en) | Method for producing diisobutylene by mixing C4 | |
| CN105732354A (en) | Method for synthesizing 2,2,4, 4-tetramethyl-1, 3-cyclobutanedione | |
| WO2023071938A1 (en) | Maleic anhydride hydrogenation method and succinic acid production method comprising same | |
| CN102452934B (en) | Preparation method of sec-butyl acetate | |
| CN103965040B (en) | A kind of method of preparing dibasic acid dimethyl ester | |
| CN109748791B (en) | Energy-saving method for producing dimethyl adipate | |
| US10047035B2 (en) | Process for continuously preparing di-C1-3-alkyl succinates | |
| CN101108790B (en) | Method for manufacturing dimethyl ether with solid acid catalysis methanol dehydration reaction | |
| CN108002995A (en) | A kind of method and its equipment of acetone two-step method synthesizing methyl isobutyl ketone | |
| CN112457176B (en) | Method for continuously producing hexafluoroacetone | |
| CN102452935A (en) | Preparation method of p-acetoxyacetophenone, and hydrogenation and dehydration products thereof | |
| CN111763192B (en) | Preparation method and device of epsilon-caprolactone | |
| CN112047838B (en) | Relay type ethyl acetate industrial preparation process | |
| CN101423454B (en) | Method for preparing tert-butyl alcohol by reaction extraction of carbon-tetrahydrocarbon containing isobutene | |
| CN102603486A (en) | Method for preparing cyclopentanol from cyclopentene | |
| US20130053600A1 (en) | Method for preparing a carboxylic acid ester | |
| CN1024464C (en) | Method for preparing isoborneol by catalyzing camphene hydration with resin | |
| CN109225349B (en) | Preparation method of catalyst for preparing isobutene by cracking methyl tert-butyl ether |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Liu Cheng Inventor before: Peng Ye Inventor before: Liu Cheng Inventor before: Ye Yuxiang Inventor before: Ling Pengwu |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20230809 Address after: 414009 Across from Yuehua Machinery Factory, Minzhu Road, Yuehua Avenue, Yunxi District, Yueyang City, Hunan Province Applicant after: HUNAN RUIYUAN PETROCHEMICAL Co.,Ltd. Address before: 414009 Shangwushiji, Daorenji Town, Yunxi District, Yueyang City, Hunan Province, China Merchants Gas Co., Ltd. Comprehensive Building Applicant before: Hunan Hongyuan petrochemical storage Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |