CN111892501A - Preparation method of methyl 6-hydroxycaproate - Google Patents
Preparation method of methyl 6-hydroxycaproate Download PDFInfo
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- CN111892501A CN111892501A CN202010678977.4A CN202010678977A CN111892501A CN 111892501 A CN111892501 A CN 111892501A CN 202010678977 A CN202010678977 A CN 202010678977A CN 111892501 A CN111892501 A CN 111892501A
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- YDJZXHZRXDLCEH-UHFFFAOYSA-N methyl 6-hydroxyhexanoate Chemical compound COC(=O)CCCCCO YDJZXHZRXDLCEH-UHFFFAOYSA-N 0.000 title claims abstract description 47
- 238000002360 preparation method Methods 0.000 title claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 64
- ZBYYWKJVSFHYJL-UHFFFAOYSA-L cobalt(2+);diacetate;tetrahydrate Chemical compound O.O.O.O.[Co+2].CC([O-])=O.CC([O-])=O ZBYYWKJVSFHYJL-UHFFFAOYSA-L 0.000 claims abstract description 25
- 229940071125 manganese acetate Drugs 0.000 claims abstract description 25
- UOGMEBQRZBEZQT-UHFFFAOYSA-L manganese(2+);diacetate Chemical compound [Mn+2].CC([O-])=O.CC([O-])=O UOGMEBQRZBEZQT-UHFFFAOYSA-L 0.000 claims abstract description 25
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims description 52
- 239000007788 liquid Substances 0.000 claims description 41
- 239000000463 material Substances 0.000 claims description 39
- 238000004821 distillation Methods 0.000 claims description 38
- 238000000227 grinding Methods 0.000 claims description 26
- 239000000843 powder Substances 0.000 claims description 26
- 239000007810 chemical reaction solvent Substances 0.000 claims description 23
- 239000013078 crystal Substances 0.000 claims description 14
- 239000007787 solid Substances 0.000 claims description 11
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Natural products CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 10
- 238000002156 mixing Methods 0.000 claims description 9
- 238000012216 screening Methods 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 6
- 125000000218 acetic acid group Chemical group C(C)(=O)* 0.000 claims description 5
- 238000005119 centrifugation Methods 0.000 claims description 5
- 150000001875 compounds Chemical class 0.000 claims description 5
- 238000002425 crystallisation Methods 0.000 claims description 5
- 230000008025 crystallization Effects 0.000 claims description 5
- 230000003247 decreasing effect Effects 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 238000005303 weighing Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 14
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 24
- 239000000243 solution Substances 0.000 description 12
- OZJPLYNZGCXSJM-UHFFFAOYSA-N 5-valerolactone Chemical compound O=C1CCCCO1 OZJPLYNZGCXSJM-UHFFFAOYSA-N 0.000 description 6
- PFURGBBHAOXLIO-UHFFFAOYSA-N cyclohexane-1,2-diol Chemical compound OC1CCCCC1O PFURGBBHAOXLIO-UHFFFAOYSA-N 0.000 description 6
- JYXTZNBQHSHEKP-UHFFFAOYSA-N methyl 5-hydroxypentanoate Chemical compound COC(=O)CCCCO JYXTZNBQHSHEKP-UHFFFAOYSA-N 0.000 description 6
- 239000002245 particle Substances 0.000 description 4
- LOMVENUNSWAXEN-UHFFFAOYSA-N Methyl oxalate Chemical compound COC(=O)C(=O)OC LOMVENUNSWAXEN-UHFFFAOYSA-N 0.000 description 3
- XTDYIOOONNVFMA-UHFFFAOYSA-N dimethyl pentanedioate Chemical compound COC(=O)CCCC(=O)OC XTDYIOOONNVFMA-UHFFFAOYSA-N 0.000 description 3
- 239000011259 mixed solution Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000000543 intermediate Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/04—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing carboxylic acids or their salts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/19—Catalysts containing parts with different compositions
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
- B01J2231/40—Substitution reactions at carbon centres, e.g. C-C or C-X, i.e. carbon-hetero atom, cross-coupling, C-H activation or ring-opening reactions
- B01J2231/49—Esterification or transesterification
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- Crystallography & Structural Chemistry (AREA)
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Abstract
The invention discloses a preparation method of methyl 6-hydroxycaproate, which is prepared from the following raw materials in mole percentage: CH (CH)4O 60％‑75％；C6H10O45％‑15％；C6H12O38‑10％；C6H12O210‑12％；C6H8O210 to 12 percent. The preparation method of the methyl 6-hydroxycaproate adopts manganese acetate and cobalt acetate tetrahydrate as catalysts to prepareAnd the temperature is controlled at 140 ℃, so that the reaction rate and the conversion rate are both improved, the conversion rate reaches the peak value of 200 percent when the overall molecular weight of the manganese acetate and the cobalt acetate tetrahydrate is controlled at 2.0 and the temperature is controlled at 140 ℃, and the molecular weight of the manganese acetate and the cobalt acetate tetrahydrate is continuously increased and the conversion rate at the increased temperature is not obviously changed, so that the method not only improves the conversion rate, but also saves energy and resources and reduces the production cost.
Description
Technical Field
The invention relates to a preparation method, in particular to a preparation method of methyl 6-hydroxycaproate.
Background
Methyl 6-hydroxycaproate, which is white powder in appearance, is a chemical substance, is slightly harmful to water, does not need to contact with underground water, a water channel or a sewage system without dilution or a large amount of products, and is applied to organic chemical intermediates.
Methyl 6-hydroxycaproate is a common organic chemical intermediate, but the preparation method of methyl 6-hydroxycaproate still has the following problems: 1. the material utilization rate is low and the cost is high; 2. the conversion of methyl 6-hydroxycaproate is low. We therefore improved this by providing a process for the preparation of methyl 6-hydroxycaproate.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention provides a preparation method of methyl 6-hydroxycaproate.
In order to solve the technical problems, the invention provides the following technical scheme:
the invention relates to a preparation method of methyl 6-hydroxycaproate, which is prepared from the following raw materials in mole percentage:
as a preferable technical scheme of the invention, the method comprises the following steps:
s1, batching: weighing compound raw materials and a reaction solvent according to the mol percentage of the components of the materials, wherein the reaction solvent is preferably acetic acid;
s2, crushing: putting the weighed materials into a grinder one by one for grinding, and separately placing the ground powder into each container;
s3, mixing reaction: firstly, injecting a reaction solvent into the reaction kettle through a feeding port of the reaction kettle, raising the temperature in the reaction kettle to 50 ℃, then injecting the powder of the materials into the reaction kettle one by one, controlling a stirring paddle in the reaction kettle to rotate, gradually raising the temperature in the reaction kettle to 140 ℃, and finally putting a catalyst into the reaction kettle;
s4, cooling and crystallizing: taking out the reacted solution, placing the solution into a container, and placing the container into a cooling chamber for cooling crystallization;
s5, centrifugation: placing the cooled mixture into a centrifuge, performing centrifugal treatment to separate solid from liquid, discharging the liquid through a filter hole in a centrifugal chamber under the action of centrifugal force, and collecting the liquid;
s6, distillation: putting the collected solution into a distillation kettle, carrying out distillation treatment, introducing an exhaust pipe on the distillation kettle into a condensing device, condensing the methyl 6-hydroxycaproate gas generated by distillation to form liquid, and collecting the condensed methyl 6-hydroxycaproate liquid;
s7, cooling: and putting the collected methyl 6-hydroxycaproate liquid into the cooling chamber again to enable the methyl 6-hydroxycaproate liquid to form methyl 6-hydroxycaproate crystals.
In the S2, the rotation speed of the grinding disc of the grinder is controlled to be 100r/min, and the grinding time is controlled to be 5 minutes, the ground powder is placed into a 500-plus-1000-mesh sieve for screening, the screened powder is collected and separately placed into each container, the powder which does not pass through the 500-plus-1000-mesh sieve is placed into the grinder for grinding again, and the steps are sequentially circulated until the materials all pass through the 500-plus-1000-mesh sieve.
In a preferred embodiment of the present invention, in S3, the catalyst is preferably manganese acetate and cobalt acetate tetrahydrate, the mole percentage of manganese acetate is 0.8%, the mole percentage of cobalt acetate tetrahydrate is 1.2%, the rotation speed of the stirring paddle is controlled to be 250r/min, the rotation direction is changed once per minute, and the overall reaction time is controlled to be 2 hours.
In a preferred embodiment of the present invention, in S4, the pressure in the cooling chamber is controlled to be normal pressure, the temperature in the cooling chamber is decreased at a rate of 5 ℃/min until the temperature reaches 15 ℃, the temperature is controlled to be constant, and the cooling time is controlled to be 10min when the temperature is constant.
In S5, the rotation speed of the centrifuge bowl is controlled to be 500r/min, and the aperture of the centrifuge bowl is 1 mm.
In a preferred embodiment of the present invention, in S6, the distillation temperature is controlled to 100 ℃, and the distillation time is controlled to 25 min.
In a preferred embodiment of the present invention, in S7, the temperature in the cooling chamber is controlled to be 5 ℃, and the cooling time is controlled to be 15 min.
The invention has the beneficial effects that:
1. according to the preparation method of the methyl 6-hydroxycaproate, the material is crushed, the mixing rate of the material and the reaction solvent is increased, the situation that large-particle materials are not completely dissolved in the reaction solvent is prevented, the time in the whole preparation process is shortened, the production efficiency is improved, the utilization rate of the material is increased through repeated sieving and grinding, and the production cost is reduced.
2. According to the preparation method of the methyl 6-hydroxycaproate, manganese acetate and cobalt acetate tetrahydrate are adopted as catalysts, the temperature is controlled to be 140 ℃, the reaction rate and the conversion rate are improved, the overall molecular weight of the manganese acetate and the cobalt acetate tetrahydrate is controlled to be 2.0, the conversion rate reaches the peak value of 200% when the temperature is controlled to be 140 ℃, and the molecular weight of the manganese acetate and the cobalt acetate tetrahydrate is continuously increased, and the conversion rate of the increased temperature is not obviously changed, so that the conversion rate is improved, energy and resources are saved, and the production cost is reduced.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic diagram of the structure of a process for preparing methyl 6-hydroxycaproate according to the invention;
FIG. 2 is a schematic diagram of the material composition of a process for the preparation of methyl 6-hydroxycaproate according to the invention;
FIG. 3 is a schematic representation of the conversion of a process for the preparation of methyl 6-hydroxycaproate according to the invention.
Detailed Description
The preferred embodiments of the present invention will be described in conjunction with the accompanying drawings, and it will be understood that they are described herein for the purpose of illustration and explanation and not limitation.
Example 1:
as shown in figure 1, figure 2 and figure 3, the invention relates to a preparation method of methyl 6-hydroxycaproate, which is prepared from the following raw materials in percentage by mole:
the method comprises the following steps:
s1, batching: weighing compound raw materials and a reaction solvent according to the mol percentage of the components of the materials, wherein the reaction solvent is preferably acetic acid;
s2, crushing: putting the weighed materials into a grinder one by one for grinding, and separately placing the ground powder into each container;
s3, mixing reaction: firstly, injecting a reaction solvent into the reaction kettle through a feeding port of the reaction kettle, raising the temperature in the reaction kettle to 50 ℃, then injecting the powder of the materials into the reaction kettle one by one, controlling a stirring paddle in the reaction kettle to rotate, gradually raising the temperature in the reaction kettle to 140 ℃, and finally putting a catalyst into the reaction kettle;
s4, cooling and crystallizing: taking out the reacted solution, placing the solution into a container, and placing the container into a cooling chamber for cooling crystallization;
s5, centrifugation: placing the cooled mixture into a centrifuge, performing centrifugal treatment to separate solid from liquid, discharging the liquid through a filter hole in a centrifugal chamber under the action of centrifugal force, and collecting the liquid;
s6, distillation: putting the collected solution into a distillation kettle, carrying out distillation treatment, introducing an exhaust pipe on the distillation kettle into a condensing device, condensing the methyl 6-hydroxycaproate gas generated by distillation to form liquid, and collecting the condensed methyl 6-hydroxycaproate liquid;
s7, cooling: and putting the collected methyl 6-hydroxycaproate liquid into the cooling chamber again to enable the methyl 6-hydroxycaproate liquid to form methyl 6-hydroxycaproate crystals.
In S2, the rotation speed of a grinding disc of a grinder is controlled to be 100r/min, the grinding time is controlled to be 5 minutes, the ground powder is placed into a 500-plus-1000-mesh sieve for screening, the screened powder is collected and separately placed into each container, the powder which does not pass through the 500-plus-1000-mesh sieve is placed into the grinder again for grinding, and the steps are sequentially circulated until the materials all pass through the 500-plus-1000-mesh sieve, the materials are crushed, the mixing rate of the materials and the reaction solvent is increased, the situation that large-particle materials are not completely dissolved in the reaction solvent is prevented, the time in the whole preparation process is shortened, the production efficiency is improved, the utilization rate of the materials is increased through repeated screening and grinding, and the production cost is reduced.
In S3, the catalyst is preferably manganese acetate and cobalt acetate tetrahydrate, the mole percentage of manganese acetate is 0.8%, the mole percentage of cobalt acetate tetrahydrate is 1.2%, the rotation speed of the stirring paddle is controlled to be 250r/min, the rotation direction is changed once per minute, the integral reaction time is controlled to be 2 hours, the catalyst is manganese acetate and cobalt acetate tetrahydrate, the temperature is controlled to be 140 ℃, the reaction rate and the conversion rate are improved, the molecular weight of the manganese acetate and cobalt acetate tetrahydrate is controlled to be 2.0, the conversion rate reaches a peak value of 200% when the temperature is controlled to be 140 ℃, the molecular weight of the manganese acetate and cobalt acetate tetrahydrate is continuously increased, the conversion rate is not obviously changed, energy and resources are saved, and the production cost is reduced.
In the step S4, the pressure in the cooling chamber is controlled to be normal pressure, the temperature in the chamber is decreased at a rate of 5 ℃/min until the temperature is 15 ℃, the temperature is controlled to be constant, and when the temperature is constant, the cooling time is controlled to be 10min, and the valerolactone, dimethyl oxalate, dimethyl glutarate and 1, 2-cyclohexanediol in the mixed solution are gradually formed into solid crystals by cooling, so that the solid crystals can be conveniently separated from the methyl 6-glycolate, the methyl 5-hydroxypentanoate and the methyl 6-glycolate.
In S5, the rotation speed of a centrifuge bowl of the centrifuge is controlled to be 500r/min, and the aperture of the selected centrifuge bowl is 1 mm.
Wherein in S6, the distillation temperature is controlled at 100 ℃, the distillation time is controlled at 25min, and the methyl 6-glycolate in the mixed liquid of the methyl 6-glycolate, the methyl 5-hydroxypentanoate and the methyl 6-glycolate is converted into a gas at 100 ℃ by distillation treatment, thereby purifying the methyl 6-glycolate.
In the step S7, the temperature in the cooling chamber is controlled to be 5 ℃, the cooling time is controlled to be 15min, and the liquid of the methyl 6-glycolate is converted into the crystals of the methyl 6-glycolate through cooling.
Example 2:
as shown in figure 1, figure 2 and figure 3, the invention relates to a preparation method of methyl 6-hydroxycaproate, which is prepared from the following raw materials in percentage by mole:
the method comprises the following steps:
s1, batching: weighing compound raw materials and a reaction solvent according to the mol percentage of the components of the materials, wherein the reaction solvent is preferably acetic acid;
s2, crushing: putting the weighed materials into a grinder one by one for grinding, and separately placing the ground powder into each container;
s3, mixing reaction: firstly, injecting a reaction solvent into the reaction kettle through a feeding port of the reaction kettle, raising the temperature in the reaction kettle to 50 ℃, then injecting the powder of the materials into the reaction kettle one by one, controlling a stirring paddle in the reaction kettle to rotate, gradually raising the temperature in the reaction kettle to 140 ℃, and finally putting a catalyst into the reaction kettle;
s4, cooling and crystallizing: taking out the reacted solution, placing the solution into a container, and placing the container into a cooling chamber for cooling crystallization;
s5, centrifugation: placing the cooled mixture into a centrifuge, performing centrifugal treatment to separate solid from liquid, discharging the liquid through a filter hole in a centrifugal chamber under the action of centrifugal force, and collecting the liquid;
s6, distillation: putting the collected solution into a distillation kettle, carrying out distillation treatment, introducing an exhaust pipe on the distillation kettle into a condensing device, condensing the methyl 6-hydroxycaproate gas generated by distillation to form liquid, and collecting the condensed methyl 6-hydroxycaproate liquid;
s7, cooling: and putting the collected methyl 6-hydroxycaproate liquid into the cooling chamber again to enable the methyl 6-hydroxycaproate liquid to form methyl 6-hydroxycaproate crystals.
In S2, the rotation speed of a grinding disc of a grinder is controlled to be 100r/min, the grinding time is controlled to be 5 minutes, the ground powder is placed into a 500-plus-1000-mesh sieve for screening, the screened powder is collected and separately placed into each container, the powder which does not pass through the 500-plus-1000-mesh sieve is placed into the grinder again for grinding, and the steps are sequentially circulated until the materials all pass through the 500-plus-1000-mesh sieve, the materials are crushed, the mixing rate of the materials and the reaction solvent is increased, the situation that large-particle materials are not completely dissolved in the reaction solvent is prevented, the time in the whole preparation process is shortened, the production efficiency is improved, the utilization rate of the materials is increased through repeated screening and grinding, and the production cost is reduced.
In S3, the catalyst is preferably manganese acetate and cobalt acetate tetrahydrate, the mole percentage of manganese acetate is 0.8%, the mole percentage of cobalt acetate tetrahydrate is 1.2%, the rotation speed of the stirring paddle is controlled to be 250r/min, the rotation direction is changed once per minute, the integral reaction time is controlled to be 2 hours, the catalyst is manganese acetate and cobalt acetate tetrahydrate, the temperature is controlled to be 140 ℃, the reaction rate and the conversion rate are improved, the molecular weight of the manganese acetate and cobalt acetate tetrahydrate is controlled to be 2.0, the conversion rate reaches a peak value of 200% when the temperature is controlled to be 140 ℃, the molecular weight of the manganese acetate and cobalt acetate tetrahydrate is continuously increased, the conversion rate is not obviously changed, energy and resources are saved, and the production cost is reduced.
In the step S4, the pressure in the cooling chamber is controlled to be normal pressure, the temperature in the chamber is decreased at a rate of 5 ℃/min until the temperature is 15 ℃, the temperature is controlled to be constant, and when the temperature is constant, the cooling time is controlled to be 10min, and the valerolactone, dimethyl oxalate, dimethyl glutarate and 1, 2-cyclohexanediol in the mixed solution are gradually formed into solid crystals by cooling, so that the solid crystals can be conveniently separated from the methyl 6-glycolate, the methyl 5-hydroxypentanoate and the methyl 6-glycolate.
In S5, the rotation speed of a centrifuge bowl of the centrifuge is controlled to be 500r/min, and the aperture of the selected centrifuge bowl is 1 mm.
Wherein in S6, the distillation temperature is controlled at 100 ℃, the distillation time is controlled at 25min, and the methyl 6-glycolate in the mixed liquid of the methyl 6-glycolate, the methyl 5-hydroxypentanoate and the methyl 6-glycolate is converted into a gas at 100 ℃ by distillation treatment, thereby purifying the methyl 6-glycolate.
In the step S7, the temperature in the cooling chamber is controlled to be 5 ℃, the cooling time is controlled to be 15min, and the liquid of the methyl 6-glycolate is converted into the crystals of the methyl 6-glycolate through cooling.
Example 3:
as shown in figure 1, figure 2 and figure 3, the invention relates to a preparation method of methyl 6-hydroxycaproate, which is prepared from the following raw materials in percentage by mole:
the method comprises the following steps:
s1, batching: weighing compound raw materials and a reaction solvent according to the mol percentage of the components of the materials, wherein the reaction solvent is preferably acetic acid;
s2, crushing: putting the weighed materials into a grinder one by one for grinding, and separately placing the ground powder into each container;
s3, mixing reaction: firstly, injecting a reaction solvent into the reaction kettle through a feeding port of the reaction kettle, raising the temperature in the reaction kettle to 50 ℃, then injecting the powder of the materials into the reaction kettle one by one, controlling a stirring paddle in the reaction kettle to rotate, gradually raising the temperature in the reaction kettle to 140 ℃, and finally putting a catalyst into the reaction kettle;
s4, cooling and crystallizing: taking out the reacted solution, placing the solution into a container, and placing the container into a cooling chamber for cooling crystallization;
s5, centrifugation: placing the cooled mixture into a centrifuge, performing centrifugal treatment to separate solid from liquid, discharging the liquid through a filter hole in a centrifugal chamber under the action of centrifugal force, and collecting the liquid;
s6, distillation: putting the collected solution into a distillation kettle, carrying out distillation treatment, introducing an exhaust pipe on the distillation kettle into a condensing device, condensing the methyl 6-hydroxycaproate gas generated by distillation to form liquid, and collecting the condensed methyl 6-hydroxycaproate liquid;
s7, cooling: and putting the collected methyl 6-hydroxycaproate liquid into the cooling chamber again to enable the methyl 6-hydroxycaproate liquid to form methyl 6-hydroxycaproate crystals.
In S2, the rotation speed of a grinding disc of a grinder is controlled to be 100r/min, the grinding time is controlled to be 5 minutes, the ground powder is placed into a 500-plus-1000-mesh sieve for screening, the screened powder is collected and separately placed into each container, the powder which does not pass through the 500-plus-1000-mesh sieve is placed into the grinder again for grinding, and the steps are sequentially circulated until the materials all pass through the 500-plus-1000-mesh sieve, the materials are crushed, the mixing rate of the materials and the reaction solvent is increased, the situation that large-particle materials are not completely dissolved in the reaction solvent is prevented, the time in the whole preparation process is shortened, the production efficiency is improved, the utilization rate of the materials is increased through repeated screening and grinding, and the production cost is reduced.
In S3, the catalyst is preferably manganese acetate and cobalt acetate tetrahydrate, the mole percentage of manganese acetate is 0.8%, the mole percentage of cobalt acetate tetrahydrate is 1.2%, the rotation speed of the stirring paddle is controlled to be 250r/min, the rotation direction is changed once per minute, the integral reaction time is controlled to be 2 hours, the catalyst is manganese acetate and cobalt acetate tetrahydrate, the temperature is controlled to be 140 ℃, the reaction rate and the conversion rate are improved, the molecular weight of the manganese acetate and cobalt acetate tetrahydrate is controlled to be 2.0, the conversion rate reaches a peak value of 200% when the temperature is controlled to be 140 ℃, the molecular weight of the manganese acetate and cobalt acetate tetrahydrate is continuously increased, the conversion rate is not obviously changed, energy and resources are saved, and the production cost is reduced.
In the step S4, the pressure in the cooling chamber is controlled to be normal pressure, the temperature in the chamber is decreased at a rate of 5 ℃/min until the temperature is 15 ℃, the temperature is controlled to be constant, and when the temperature is constant, the cooling time is controlled to be 10min, and the valerolactone, dimethyl oxalate, dimethyl glutarate and 1, 2-cyclohexanediol in the mixed solution are gradually formed into solid crystals by cooling, so that the solid crystals can be conveniently separated from the methyl 6-glycolate, the methyl 5-hydroxypentanoate and the methyl 6-glycolate.
In S5, the rotation speed of a centrifuge bowl of the centrifuge is controlled to be 500r/min, and the aperture of the selected centrifuge bowl is 1 mm.
Wherein in S6, the distillation temperature is controlled at 100 ℃, the distillation time is controlled at 25min, and the methyl 6-glycolate in the mixed liquid of the methyl 6-glycolate, the methyl 5-hydroxypentanoate and the methyl 6-glycolate is converted into a gas at 100 ℃ by distillation treatment, thereby purifying the methyl 6-glycolate.
In the step S7, the temperature in the cooling chamber is controlled to be 5 ℃, the cooling time is controlled to be 15min, and the liquid of the methyl 6-glycolate is converted into the crystals of the methyl 6-glycolate through cooling.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. The preparation method of methyl 6-hydroxycaproate is characterized in that the material is prepared from the following raw materials in mole percentage:
2. the method for preparing methyl 6-hydroxycaproate according to claim 1, characterized by comprising the following steps:
s1, batching: weighing compound raw materials and a reaction solvent according to the mol percentage of the components of the materials, wherein the reaction solvent is preferably acetic acid;
s2, crushing: putting the weighed materials into a grinder one by one for grinding, and separately placing the ground powder into each container;
s3, mixing reaction: firstly, injecting a reaction solvent into the reaction kettle through a feeding port of the reaction kettle, raising the temperature in the reaction kettle to 50 ℃, then injecting the powder of the materials into the reaction kettle one by one, controlling a stirring paddle in the reaction kettle to rotate, gradually raising the temperature in the reaction kettle to 140 ℃, and finally putting a catalyst into the reaction kettle;
s4, cooling and crystallizing: taking out the reacted solution, placing the solution into a container, and placing the container into a cooling chamber for cooling crystallization;
s5, centrifugation: placing the cooled mixture into a centrifuge, performing centrifugal treatment to separate solid from liquid, discharging the liquid through a filter hole in a centrifugal chamber under the action of centrifugal force, and collecting the liquid;
s6, distillation: putting the collected solution into a distillation kettle, carrying out distillation treatment, introducing an exhaust pipe on the distillation kettle into a condensing device, condensing the methyl 6-hydroxycaproate gas generated by distillation to form liquid, and collecting the condensed methyl 6-hydroxycaproate liquid;
s7, cooling: and putting the collected methyl 6-hydroxycaproate liquid into the cooling chamber again to enable the methyl 6-hydroxycaproate liquid to form methyl 6-hydroxycaproate crystals.
3. The method as claimed in claim 2, wherein in the step S2, the rotation speed of the grinding disc of the grinding machine is controlled to be 100r/min, the grinding time is controlled to be 5 minutes, the ground powder is placed into a 500-mesh and 1000-mesh sieve for screening, the screened powder is collected and separately placed into each container, the powder which does not pass through the 500-mesh and 1000-mesh sieve is placed into the grinding machine again for grinding, and the steps are sequentially circulated until the materials pass through the 500-mesh and 1000-mesh sieve.
4. The method of claim 2, wherein in the step S3, the catalyst is preferably manganese acetate and cobalt acetate tetrahydrate, the mole percentage of manganese acetate is 0.8%, the mole percentage of cobalt acetate tetrahydrate is 1.2%, the rotation speed of the stirring paddle is controlled to be 250r/min, the rotation direction is changed once per minute, and the overall reaction time is controlled to be 2 hours.
5. The method of claim 2, wherein in step S4, the pressure in the cooling chamber is controlled to be normal pressure, the temperature in the chamber is decreased at a rate of 5 ℃/min until the temperature reaches 15 ℃, the temperature is controlled to be constant, and when the temperature is constant, the cooling time is controlled to be 10 min.
6. The method according to claim 2, wherein in S5, the rotation speed of a centrifuge bowl is controlled to be 500r/min, and the aperture of the centrifuge bowl is 1 mm.
7. The method according to claim 2, wherein the distillation temperature of S6 is controlled at 100 ℃ and the distillation time is controlled at 25 min.
8. The method according to claim 2, wherein in S7, the temperature in the cooling chamber is controlled to be 5 ℃ and the cooling time is controlled to be 15 min.
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| CN1257470A (en) * | 1997-11-14 | 2000-06-21 | 巴斯福股份公司 | Method for producing 1,6-hexanediol and 6-hydroxycaproic acid or their esters |
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| CN102015615A (en) * | 2008-04-01 | 2011-04-13 | Sk化学株式会社 | Method for preparing fatty acid alkyl ester using fatty acid |
| US20110218355A1 (en) * | 2008-11-07 | 2011-09-08 | Soo-Hyun Kim | Method and apparatus for preparing alkyl ester fatty acid using fatty acid |
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| CN1257470A (en) * | 1997-11-14 | 2000-06-21 | 巴斯福股份公司 | Method for producing 1,6-hexanediol and 6-hydroxycaproic acid or their esters |
| CN1424302A (en) * | 2001-12-12 | 2003-06-18 | 中国科学院理化技术研究所 | Method for preparing aliphatic dibasic acid dihydric alcohol ester |
| CN101945847A (en) * | 2008-02-15 | 2011-01-12 | 巴斯夫欧洲公司 | Method for producing 6-hydroxy hexanoic acid esters |
| CN102015615A (en) * | 2008-04-01 | 2011-04-13 | Sk化学株式会社 | Method for preparing fatty acid alkyl ester using fatty acid |
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