CN117019033A - Production device and method of 4-methyl-delta-decalactone perfume - Google Patents
Production device and method of 4-methyl-delta-decalactone perfume Download PDFInfo
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- CN117019033A CN117019033A CN202310984016.XA CN202310984016A CN117019033A CN 117019033 A CN117019033 A CN 117019033A CN 202310984016 A CN202310984016 A CN 202310984016A CN 117019033 A CN117019033 A CN 117019033A
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 239000002304 perfume Substances 0.000 title claims abstract description 11
- 238000000034 method Methods 0.000 title abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 82
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 42
- SJWFXCIHNDVPSH-UHFFFAOYSA-N octan-2-ol Chemical compound CCCCCCC(C)O SJWFXCIHNDVPSH-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 claims abstract description 28
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000000203 mixture Substances 0.000 claims abstract description 25
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 22
- 238000003756 stirring Methods 0.000 claims abstract description 19
- LSXWFXONGKSEMY-UHFFFAOYSA-N di-tert-butyl peroxide Chemical compound CC(C)(C)OOC(C)(C)C LSXWFXONGKSEMY-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000005086 pumping Methods 0.000 claims abstract description 13
- 238000007710 freezing Methods 0.000 claims abstract description 4
- 230000008014 freezing Effects 0.000 claims abstract description 4
- 150000003839 salts Chemical class 0.000 claims abstract description 4
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 70
- KFSLWBXXFJQRDL-UHFFFAOYSA-N Peracetic acid Chemical compound CC(=O)OO KFSLWBXXFJQRDL-UHFFFAOYSA-N 0.000 claims description 68
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 48
- 238000004821 distillation Methods 0.000 claims description 37
- 238000006462 rearrangement reaction Methods 0.000 claims description 36
- 239000003208 petroleum Substances 0.000 claims description 35
- 238000005406 washing Methods 0.000 claims description 35
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical group CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 claims description 32
- 238000007259 addition reaction Methods 0.000 claims description 31
- 239000000463 material Substances 0.000 claims description 31
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 20
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 20
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 20
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 claims description 19
- 239000000047 product Substances 0.000 claims description 19
- 239000012295 chemical reaction liquid Substances 0.000 claims description 17
- 239000003205 fragrance Substances 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 15
- 238000002360 preparation method Methods 0.000 claims description 14
- 238000009835 boiling Methods 0.000 claims description 13
- 239000006227 byproduct Substances 0.000 claims description 13
- 238000011010 flushing procedure Methods 0.000 claims description 13
- 238000010992 reflux Methods 0.000 claims description 13
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 10
- 239000003054 catalyst Substances 0.000 claims description 9
- 229910001220 stainless steel Inorganic materials 0.000 claims description 9
- 239000010935 stainless steel Substances 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 7
- ALWUKGXLBSQSMA-UHFFFAOYSA-N 5-Hexyldihydro-5-methyl-2(3H)-furanone Chemical compound CCCCCCC1(C)CCC(=O)O1 ALWUKGXLBSQSMA-UHFFFAOYSA-N 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- KTUQUZJOVNIKNZ-UHFFFAOYSA-N butan-1-ol;hydrate Chemical compound O.CCCCO KTUQUZJOVNIKNZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 6
- 238000005194 fractionation Methods 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- 239000001257 hydrogen Substances 0.000 claims description 6
- 239000000945 filler Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- 235000013599 spices Nutrition 0.000 claims description 4
- VGECIEOJXLMWGO-UHFFFAOYSA-N 2-hexylcyclopent-2-en-1-one Chemical compound CCCCCCC1=CCCC1=O VGECIEOJXLMWGO-UHFFFAOYSA-N 0.000 claims description 3
- ZISGOYMWXFOWAM-UHFFFAOYSA-N 3-methyl-2-pentylcyclopentan-1-one Chemical compound CCCCCC1C(C)CCC1=O ZISGOYMWXFOWAM-UHFFFAOYSA-N 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 239000007868 Raney catalyst Substances 0.000 claims description 3
- 229910000564 Raney nickel Inorganic materials 0.000 claims description 3
- NPXOKRUENSOPAO-UHFFFAOYSA-N Raney nickel Chemical compound [Al].[Ni] NPXOKRUENSOPAO-UHFFFAOYSA-N 0.000 claims description 3
- PQLVXDKIJBQVDF-UHFFFAOYSA-N acetic acid;hydrate Chemical compound O.CC(O)=O PQLVXDKIJBQVDF-UHFFFAOYSA-N 0.000 claims description 3
- 239000003377 acid catalyst Substances 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 210000003298 dental enamel Anatomy 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- 229910002804 graphite Inorganic materials 0.000 claims description 3
- 239000010439 graphite Substances 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 3
- 239000010865 sewage Substances 0.000 claims description 3
- 239000007790 solid phase Substances 0.000 claims description 3
- 230000000087 stabilizing effect Effects 0.000 claims description 3
- 238000013329 compounding Methods 0.000 claims 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims 1
- 238000012856 packing Methods 0.000 claims 1
- 239000002994 raw material Substances 0.000 abstract description 9
- 230000003647 oxidation Effects 0.000 abstract description 6
- 238000005886 esterification reaction Methods 0.000 abstract description 4
- 230000008707 rearrangement Effects 0.000 abstract description 4
- 238000006049 ring expansion reaction Methods 0.000 abstract description 4
- 101100298222 Caenorhabditis elegans pot-1 gene Proteins 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 241000207840 Jasminum Species 0.000 description 4
- 235000010254 Jasminum officinale Nutrition 0.000 description 4
- 244000014047 Polianthes tuberosa Species 0.000 description 3
- 235000016067 Polianthes tuberosa Nutrition 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- GHBSPIPJMLAMEP-UHFFFAOYSA-N 6-pentyloxan-2-one Chemical compound CCCCCC1CCCC(=O)O1 GHBSPIPJMLAMEP-UHFFFAOYSA-N 0.000 description 2
- 241000233855 Orchidaceae Species 0.000 description 2
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 2
- 150000002596 lactones Chemical class 0.000 description 2
- UKVIEHSSVKSQBA-UHFFFAOYSA-N methane;palladium Chemical compound C.[Pd] UKVIEHSSVKSQBA-UHFFFAOYSA-N 0.000 description 2
- ZHMCDZHVHDFSHO-UHFFFAOYSA-N undecane-2,5-dione Chemical compound CCCCCCC(=O)CCC(C)=O ZHMCDZHVHDFSHO-UHFFFAOYSA-N 0.000 description 2
- YCIXWYOBMVNGTB-UHFFFAOYSA-N 3-methyl-2-pentylcyclopent-2-en-1-one Chemical compound CCCCCC1=C(C)CCC1=O YCIXWYOBMVNGTB-UHFFFAOYSA-N 0.000 description 1
- WIFKBFWYBNWBQS-UHFFFAOYSA-N 5-methyl-6-pentyloxan-2-one Chemical compound CCCCCC1OC(=O)CCC1C WIFKBFWYBNWBQS-UHFFFAOYSA-N 0.000 description 1
- 235000003261 Artemisia vulgaris Nutrition 0.000 description 1
- 240000006891 Artemisia vulgaris Species 0.000 description 1
- 240000007436 Cananga odorata Species 0.000 description 1
- 244000060011 Cocos nucifera Species 0.000 description 1
- 235000013162 Cocos nucifera Nutrition 0.000 description 1
- 240000001972 Gardenia jasminoides Species 0.000 description 1
- XMLSXPIVAXONDL-PLNGDYQASA-N Jasmone Chemical compound CC\C=C/CC1=C(C)CCC1=O XMLSXPIVAXONDL-PLNGDYQASA-N 0.000 description 1
- 241000218378 Magnolia Species 0.000 description 1
- 240000002292 Psychopsis papilio Species 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- -1 propionyl compound Chemical class 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000010189 synthetic method Methods 0.000 description 1
- XMLSXPIVAXONDL-UHFFFAOYSA-N trans-jasmone Natural products CCC=CCC1=C(C)CCC1=O XMLSXPIVAXONDL-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D309/00—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only ring hetero atom, not condensed with other rings
- C07D309/16—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only ring hetero atom, not condensed with other rings having one double bond between ring members or between a ring member and a non-ring member
- C07D309/28—Heterocyclic compounds containing six-membered rings having one oxygen atom as the only ring hetero atom, not condensed with other rings having one double bond between ring members or between a ring member and a non-ring member with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D309/30—Oxygen atoms, e.g. delta-lactones
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00004—Scale aspects
- B01J2219/00006—Large-scale industrial plants
Abstract
The invention discloses a production device and a production method of 4-methyl-delta-decalactone perfume, which relate to the technical field of perfume production and comprise the following steps: s1, metering and adding the sec-octanol into a batching pot from a sec-octanol elevated tank, starting a freezing salt water valve and a stirrer of the stirring pot, controlling the temperature of the stirring pot to be 20+/-5 ℃, then metering and adding the acrylic acid and the di-tert-butyl peroxide into the acrylic acid elevated tank and the di-tert-butyl peroxide elevated tank respectively, stirring uniformly to obtain a batching mixture, and pumping the batching mixture into the batching mixture elevated tank for standby. The invention takes acrylic acid and sec-octanol as initial raw materials, and prepares 4-methyl-delta-decalactone through addition, molecular rearrangement, hydrogenation and oxidation ring-expansion esterification reaction, the raw materials are easy to obtain, the process flow is shortened, and the reaction yield is improved.
Description
Technical Field
The invention relates to the technical field of spice production, in particular to a device and a method for producing 4-methyl-delta-decalactone spice.
Background
4-methyl-delta-decalactone is chemically named tetrahydro-5-methyl-6-pentyl-pyran-2-one, CAS number 145441-24-3, has strong and fresh fragrance of tuberose and gardenia, and reminds delta-decalactone and typical lactone odor of coconut, a key component of the main fragrance of African orchid, naturally occurring in butterfly orchid, white orchid.
The 4-methyl-delta-decalactone is colorless to yellowish liquid in appearance, can be dissolved in most organic solvents such as ethanol and the like, is dissolved in oily perfume, and is insoluble in water. The 4-methyl-delta-decalactone has wide application, has strong and durable tuberose and jasmine fragrance and strong and mild lactone fragrance, is commonly used as a fragrance raw material of cosmetic essence, is mainly used for preparing jasmine flower fragrance type essence, and has the highest use amount of 5 percent in jasmine blue type essence. The fruit-flower type can be used for improving the vigor of flower-type essence such as jasmine, ylang-ylang, mugwort, magnolia, tuberose and the like.
The main synthetic route of 4-methyl-delta-decalactone includes: firstly, condensing propionyl compound with aldehyde, and then carrying out hydroxyl protection reduction, oxidation and Witting reaction, and hydrogenating and removing hydroxyl protecting groups to prepare the 4-methyl-delta-decalactone. The jasmone catalytic reduction method has problems of raw material sources and cost. Secondly, heating and refluxing 2, 5-undecanedione, ethanol and 2% sodium hydroxide solution for 6 hours under the protection of nitrogen, concentrating the reaction solution, extracting with petroleum ether, distilling the extracting solution to remove the solvent, decompressing and distilling, collecting 113-115 ℃ (1.33 kPa) fractions, obtaining the dihydro-jasmone, and then carrying out hydrogenation oxidation to prepare the 4-methyl-delta-decalactone. Therefore, the existing synthetic method has the defects of long routes, high cost, harsh reaction conditions, complex operation, low total yield and the like, so that the synthesis and application of the 4-methyl-delta-decalactone have larger limitations.
Disclosure of Invention
The invention aims to provide a device and a method for producing 4-methyl-delta-decalactone perfume, and provides a method for synthesizing 4-methyl-delta-decalactone perfume with high content, high yield and relatively simple process flow. Acrylic acid and sec-octanol are used as initial materials, and 4-methyl-delta-decalactone is prepared through addition, molecular rearrangement, hydrogenation and oxidation ring-expansion esterification, the raw materials are easy to obtain, the process flow is shortened, and the reaction yield is improved.
The aim of the invention can be achieved by the following technical scheme:
a method for producing 4-methyl-delta-decalactone fragrance, comprising the steps of:
s1, metering and adding sec-octyl alcohol into a batching pot from a sec-octyl alcohol overhead tank, starting a freezing salt water valve and a stirrer of the stirring pot, controlling the temperature of the stirring pot to be 20+/-5 ℃, then metering and adding acrylic acid and di-tert-butyl peroxide from an acrylic acid overhead tank and a di-tert-butyl peroxide overhead tank respectively, stirring uniformly to obtain a batching mixture, and pumping the batching mixture into the batching mixture overhead tank for standby;
s2, adding sec-octanol into an addition reaction kettle with a fractionating tower from a sec-octanol high-level tank in a metering mode, starting a steam valve of the addition reaction kettle, starting a stirrer, and heating the addition reaction kettle and maintaining the temperature at 120-160 ℃;
s3, dropwise adding the mixture obtained in the step S1 into an addition reaction kettle through a dropwise adding pump A, controlling the dropwise adding temperature to be 150+/-5 ℃ and the dropwise adding time to be 8-12 hours, condensing byproduct water and tertiary butanol from the top of the addition reaction kettle through a spiral plate heat exchanger A, collecting the condensed product water and tertiary butanol into a tertiary butanol/water receiving tank, and separating a water layer through centralized water diversion treatment to obtain the byproduct tertiary butanol;
s4, after the dripping is finished, continuing to keep the temperature and stir for 1-2 hours, finishing the reaction, and transferring the reaction liquid into a kettle type distillation tower A by using a pump;
s5, opening a steam valve of the kettle type fractionating tower A, starting a vacuum pump, heating, and recovering the sec-octanol by reduced pressure distillation under the conditions that the temperature of the top of the tower is 90-120 ℃ and the vacuum pressure is 6667Pa, condensing the sec-octanol by a spiral plate heat exchanger B, collecting the sec-octanol by a sec-octanol vacuum receiving tank, and transferring the sec-octanol into a sec-octanol overhead tank by using the pump for application; when the temperature of the tower top is reduced or the tower top is not discharged, the secondary octanol recovery is finished, and the reaction liquid at the bottom of the kettle is transferred into a rearrangement reaction kettle by a pump;
s6, starting a stirrer and a steam valve of the rearrangement reaction kettle, heating to the kettle temperature of 80-120 ℃, metering white oil into the rearrangement reaction kettle with a distillation tower from a white oil overhead tank, slowly metering phosphoric acid into the rearrangement reaction kettle from a phosphoric acid overhead tank, reacting for 4-8 hours, keeping reflux in the reaction process, condensing byproduct water from the top of the rearrangement reaction kettle through a spiral plate heat exchanger C, and collecting the condensed byproduct water into a water distribution receiving tank;
s7, after the rearrangement reaction is finished, continuously maintaining the temperature, stirring and refluxing for 30min, stopping the reaction, transferring the reaction liquid into a water washing kettle A, adding clear water for washing, standing and layering for 2h, separating a water layer, and transferring an oil layer into a hydrogenation reaction kettle by a pump;
s8, filling a hydrogenation catalyst into the hydrogenation reaction kettle at one time, adding petroleum ether into the hydrogenation reaction kettle by metering from a solvent petroleum ether overhead tank, introducing nitrogen for replacement for 3-5 times, introducing hydrogen for stabilizing the pressure of the reaction kettle at 0.5-2.0Mpa, starting a steam valve to heat the hydrogenation reaction kettle to the kettle temperature of 30-80 ℃, continuously introducing hydrogen for hydrogenation for 4-12 hours, and cooling, decompressing and terminating the reaction after the hydrogenation is finished;
s9, back flushing the solid-phase hydrogenation catalyst into a hydrogenation reaction kettle through an automatic back flushing precision filter for repeated application, and transferring the liquid-phase reaction liquid into a kettle type distillation tower B;
s10, starting a steam valve, heating the kettle type distillation column B to the kettle temperature of 60-100 ℃, recovering petroleum ether under the conditions of the tower top temperature of 60-90 ℃ and normal pressure, transferring the petroleum ether into a petroleum ether overhead tank for reuse, ending the recovery of petroleum ether when the tower top temperature is reduced or the tower top is not discharged, and transferring the reaction liquid at the bottom of the kettle into an oxidation reaction kettle by a pump;
s11, starting a stirrer and a cooling water valve of a peracetic acid preparation kettle, controlling the kettle temperature below 30 ℃, respectively metering acetic acid and hydrogen peroxide into the peracetic acid preparation kettle from an acetic acid high-level tank and a hydrogen peroxide high-level tank, slowly metering sulfuric acid into the peracetic acid preparation kettle from a sulfuric acid high-level tank, uniformly stirring, and pumping to the peracetic acid high-level tank for standby;
s12, starting a stirrer and a cooling water valve of the oxidation reaction kettle, controlling the kettle temperature below 30 ℃, then dropwise adding peracetic acid into the oxidation reaction kettle from a peracetic acid overhead tank through a dropwise adding pump D, controlling the dropwise adding temperature at 25-30 ℃ for 4-12 hours, continuing to keep the temperature for reaction for 1-2 hours after the dropwise adding is finished, adding clear water to terminate the reaction, and pumping the reaction liquid into a water washing kettle B;
s13, adding clear water into the water washing kettle B in a metering way, starting a stirrer to wash for three times, standing for 2 hours, intensively carrying out acetic acid purification treatment on acetic acid water separated from the primary water washing, enabling water layers separated from the secondary water washing and the tertiary water washing to enter a sewage treatment station for treatment, and pumping the separated oil layer into a kettle type rectifying tower;
s14, opening a steam valve of the kettle type rectifying tower, starting a vacuum pump, heating to 80-120 ℃ at the tower top temperature, distilling under reduced pressure under the vacuum pressure of 6667Pa, collecting residual low-boiling substances such as acetic acid and the like, condensing by a spiral plate heat exchanger E, collecting the low-boiling substances in a low-boiling vacuum receiving tank by a gas-liquid separator, then opening high vacuum, distilling under reduced pressure under the vacuum pressure of 1333Pa at the tower top temperature of 90-130 ℃, condensing by a spiral plate heat exchanger E35, collecting the products in a vacuum receiving tank by a gas-liquid separator, and transferring the products into a product temporary storage tank.
As a further scheme of the invention: the batch pan, acrylic acid elevated tank and batch mixture elevated tank are all insulated by 20+ -5 ℃.
As a further scheme of the invention: the molar ratio of acrylic acid to secondary octanol of the batching mixture in the step S1 is 1:2-1:5; the molar ratio of acrylic acid to di-tert-butyl peroxide is 1:0.1-1:0.5.
As a further scheme of the invention: the molar ratio of the secondary octanol in the step S2 to the acrylic acid in the step S1 is 1:1-5:1.
As a further scheme of the invention: in the step S6, the volume ratio of the white oil to the gamma-methyl decalactone is 0.1:1-0.5:1, and the mass ratio of the acid catalyst to the gamma-methyl decalactone is 0.05:1-0.5:1.
As a further scheme of the invention: in the step S6, the rearrangement reaction kettle is made of one of enamel or 904 stainless steel, and the distillation tower with the rearrangement reaction kettle is made of graphite.
As a further scheme of the invention: the hydrogenation catalyst in the step S8 is one of 5% palladium carbon or Raney nickel, the volume ratio of petroleum ether to 2-hexyl cyclopentenone is 1:1-5:1, and the preferable volume ratio is 1:1-2:1.
As a further scheme of the invention: the molar ratio of the peracetic acid to the 3-methyl-2-amyl cyclopentanone in the step S12 is 1:1-3:1.
As a further scheme of the invention: the kettle type fractionating tower is filled with cy500 stainless steel corrugated filler; and the kettle type rectifying tower is filled with cy700 stainless steel corrugated filler.
The production device of the 4-methyl-delta-decalactone spice comprises a batching pot, wherein an acrylic acid overhead tank and a di-tert-butyl peroxide overhead tank are respectively connected with the batching pot through pipelines; the secondary octanol overhead tank is connected with the batching kettle and the addition reaction kettle through pipelines respectively; the batching mixture overhead tank is connected with a batching pot and an addition reaction kettle through a pump and a dripping pump A respectively; the addition reaction kettle is provided with a fractionation reflux device; the tertiary butanol/water receiving tank and the kettle type distillation tower A are respectively connected with an addition reaction kettle through a spiral plate heat exchanger A and a material pump; the secondary octanol vacuum receiving tank is connected with the top of the kettle type distillation tower A and the secondary octanol overhead tank through a spiral plate heat exchanger B and a material pump respectively; the phosphoric acid high-level tank and the white oil high-level tank are respectively connected through a pipeline rearrangement reaction kettle, the rearrangement reaction kettle is connected with a kettle type distillation tower A through a material pump, and the rearrangement reaction kettle is provided with a fractionation reflux device; the water diversion receiving tank and the water washing kettle A are respectively connected with the rearrangement reaction kettle through a spiral plate heat exchanger C and a material pump; the hydrogenation reaction kettle is connected with the washing kettle A and the petroleum ether overhead tank through a material pump and a pipeline respectively; the automatic back flushing precision filter is connected with the hydrogenation reaction kettle and the petroleum ether overhead tank through a U-shaped bent pipe and a material pump respectively; the kettle type distillation tower B is connected with the automatic back flushing precision filter and the oxidation reaction kettle through a material pump respectively; the petroleum ether receiving tank is connected with the top of the kettle type distillation tower B and the petroleum ether overhead tank through a spiral plate heat exchanger D and a pipeline respectively; the peroxyacetic acid preparation kettle is connected with a hydrogen peroxide head tank and a peroxyacetic acid head tank through a dripping pump C and a material pump respectively; the acetic acid elevated tank and the sulfuric acid elevated tank are respectively connected with a peroxyacetic acid preparation kettle through pipelines; the oxidation reaction kettle is connected with a peracetic acid overhead tank and a washing kettle B through a dripping pump D and a material pump respectively; the kettle type rectifying tower is connected with the water washing kettle B and the gas-liquid separator through a material pump and a spiral plate heat exchanger E respectively; the low-boiling vacuum receiving tank and the product temporary storage tank are respectively connected with the gas-liquid separator through a pipeline and the product vacuum receiving tank.
The invention has the beneficial effects that:
the invention takes acrylic acid and sec-octanol as initial raw materials, and prepares 4-methyl-delta-decalactone through addition, molecular rearrangement, hydrogenation and oxidation ring-expansion esterification reaction, the raw materials are easy to obtain, the process flow is shortened, and the reaction yield is improved.
Drawings
The invention is further described below with reference to the accompanying drawings.
FIG. 1 is a schematic diagram of a production apparatus for 4-methyl-delta-decalactone fragrance provided by the present invention.
In the figure: 1. a batching pot; 2. acrylic acid high level tank; 3. a di-t-butyl peroxide overhead tank; 4. a secondary octanol elevated tank; 5. a batch mixture overhead tank; 6. an addition reaction kettle; 7. dropwise adding a pump A; 8. a spiral plate heat exchanger A; 9. a t-butanol/water receiving tank; 10. a kettle type distillation column A; 11. a spiral plate heat exchanger B; 12. a sec-octyl alcohol vacuum receiving tank; 13. a rearrangement reaction kettle; 14. a phosphoric acid elevated tank; 15. a white oil overhead tank; 16. a spiral plate heat exchanger C; 17. a water division receiving tank; 18. washing the kettle A; 19. a hydrogenation reaction kettle; 20. petroleum ether overhead tank; 21. automatically backwashing the precision filter; 22. a kettle type distillation column B; 23. a spiral plate heat exchanger D; 24. a petroleum ether receiving tank; 25. preparing a kettle by peracetic acid; 26. a hydrogen peroxide elevated tank; 27. acetic acid overhead tank; 28. a sulfuric acid overhead tank; 29. dropwise adding a pump C; 30. a peroxyacetic acid overhead tank; 31. an oxidation reaction kettle; 32. dropwise adding a pump D; 33. washing the kettle B; 34. a kettle type rectifying tower; 35. a spiral plate heat exchanger E; 36. a gas-liquid separator; 37. a low boiling vacuum receiving tank; 38. a product vacuum receiving tank; 39. the product temporary storage tank.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1
Referring to FIG. 1, the invention is a method for producing 4-methyl-delta-decalactone perfume, comprising the following steps:
s1, metering and adding sec-octanol into a batching pot 1 from a sec-octanol overhead tank 4, starting a freezing salt water valve and a stirrer of the batching pot 1, controlling the temperature of the stirring pot to be 20+/-5 ℃, then metering and adding acrylic acid and di-tert-butyl peroxide from an acrylic acid overhead tank 2 and a di-tert-butyl peroxide overhead tank 3 respectively, uniformly stirring to obtain a batching mixture, and pumping the batching mixture into a batching mixture overhead tank 5 for standby;
s2, adding sec-octanol into an addition reaction kettle 6 with a fractionating tower from a sec-octanol overhead tank 4 in a metering manner, starting a steam valve of the addition reaction kettle 6, starting a stirrer, and heating the addition reaction kettle 6 and maintaining the temperature at 120-160 ℃;
s3, dropwise adding the mixture obtained in the step S1 into an addition reaction kettle 6 through a dropwise adding pump A7, controlling the dropwise adding temperature to be 150+/-5 ℃ and the dropwise adding time to be 8-12h, condensing byproduct water and tertiary butanol from the top of the addition reaction kettle 6 through a spiral plate heat exchanger A8, collecting the condensed product water and tertiary butanol into a tertiary butanol/water receiving tank 9, and obtaining the byproduct tertiary butanol after separating a water layer through concentrated water diversion treatment;
s4, after the dripping is finished, continuing to keep the temperature and stir for 1-2 hours, finishing the reaction, and transferring the reaction liquid into a kettle type distillation tower A10 by using a pump;
s5, opening a steam valve of a kettle type fractionating tower A10, starting a vacuum pump, heating, recovering the sec-octanol by reduced pressure distillation under the condition that the tower top temperature is 90-120 ℃ and the vacuum pressure is 6667Pa, condensing the sec-octanol by a spiral plate heat exchanger B11, collecting the sec-octanol by a sec-octanol vacuum receiving tank 12, and transferring the sec-octanol into a sec-octanol overhead tank 4 by using the pump for application; when the temperature of the tower top is reduced or the tower top is not discharged, the secondary octanol recovery is finished, and the reaction liquid at the bottom of the kettle is transferred into a rearrangement reaction kettle 13 by a pump;
s6, starting a stirrer and a steam valve of the rearrangement reaction kettle 13, heating to the kettle temperature of 80-120 ℃, metering white oil into the rearrangement reaction kettle 13 with a distillation tower from a white oil overhead tank 15, slowly metering phosphoric acid into the rearrangement reaction kettle 13 from a phosphoric acid overhead tank 14, reacting for 4-8 hours, keeping reflux in the reaction process, condensing byproduct water from the top of the rearrangement reaction kettle 13 through a spiral plate heat exchanger C16, and collecting the condensed byproduct water into a water distribution receiving tank 17;
s7, after the rearrangement reaction is finished, continuously maintaining the temperature, stirring and refluxing for 30min, terminating the reaction, transferring the reaction liquid into a water washing kettle A18, adding clear water for washing, standing and layering for 2h, separating a water layer, and transferring an oil layer into a hydrogenation reaction kettle 19 by a pump;
s8, filling a hydrogenation catalyst into the hydrogenation reaction kettle 19 at one time, metering petroleum ether into the hydrogenation reaction kettle 19 from a solvent petroleum ether overhead tank 20, introducing nitrogen for replacement for 3-5 times, introducing hydrogen for stabilizing at the pressure of the reaction kettle of 0.5-2.0Mpa, starting a steam valve to heat the hydrogenation reaction kettle 19 to the kettle temperature of 30-80 ℃, continuously introducing hydrogen for hydrogenation, reacting for 4-12h, and cooling, decompressing and terminating the reaction after the hydrogenation is finished;
s9, back flushing the solid-phase hydrogenation catalyst into the hydrogenation reaction kettle 19 through an automatic back flushing precision filter 21 for repeated application, and transferring the liquid-phase reaction liquid into a kettle type distillation tower B22;
s10, starting a steam valve, heating the kettle type distillation column B22 to the kettle temperature of 60-100 ℃, recovering petroleum ether under the conditions of the tower top temperature of 60-90 ℃ and normal pressure, transferring the petroleum ether into a petroleum ether overhead tank 20 for application, ending the recovery of petroleum ether when the tower top temperature is reduced or the tower top is not discharged, and transferring the reaction liquid at the bottom of the kettle into an oxidation reaction kettle 31 by a pump;
s11, starting a stirrer and a cooling water valve of a peracetic acid preparation kettle 25, controlling the kettle temperature below 30 ℃, respectively metering acetic acid and hydrogen peroxide into the peracetic acid preparation kettle 25 from an acetic acid overhead tank 27 and a hydrogen peroxide overhead tank 26, slowly metering sulfuric acid into the peracetic acid preparation kettle 25 from a sulfuric acid overhead tank 28, uniformly stirring, and pumping to the peracetic acid overhead tank 30 for standby;
s12, starting a stirrer and a cooling water valve of an oxidation reaction kettle 31, controlling the kettle temperature below 30 ℃, then dripping peracetic acid into the oxidation reaction kettle 31 from a peracetic acid overhead tank 30 through a dripping pump D32, controlling the dripping temperature at 25-30 ℃ for 4-12 hours, continuing to perform heat preservation reaction for 1-2 hours after dripping is finished, adding clear water to terminate the reaction, and pumping the reaction liquid into a water washing kettle B33;
s13, adding clear water into the water washing kettle B33 in a metering way, starting a stirrer to wash for three times, standing for 2 hours, intensively carrying out acetic acid purification treatment on acetic acid water separated from the primary water washing, enabling water layers separated from the secondary water washing and the tertiary water washing to enter a sewage treatment station for treatment, and pumping a separated oil layer into a kettle type rectifying tower 34;
s14, opening a steam valve of the kettle type rectifying tower 34, starting a vacuum pump, heating to a temperature of between 80 and 120 ℃ at the top of the tower, distilling under reduced pressure under the condition that the vacuum pressure is 6667Pa, collecting low-boiling substances such as residual acetic acid and the like, condensing by a spiral plate heat exchanger E35, collecting the low-boiling substances into a low-boiling vacuum receiving tank 37 by a gas-liquid separator 36, then opening high vacuum, distilling under reduced pressure under the condition that the temperature of the top of the tower is between 90 and 130 ℃ and the vacuum pressure is 1333Pa, condensing by the spiral plate heat exchanger E35, collecting the substances into a product vacuum receiving tank 38 by the gas-liquid separator 36, and transferring the substances into a product temporary storage tank 39.
The temperature of the batching pot 1, the acrylic acid elevated tank 2 and the batching mixture elevated tank 5 is kept at 20+/-5 ℃.
The molar ratio of acrylic acid to secondary octanol of the batching mixture in the step S1 is 1:2-1:5; the preferred molar ratio is 1: 2.5-1:3.5; the molar ratio of the acrylic acid to the di-tert-butyl peroxide is 1:0.1-1:0.5; the preferred molar ratio is 1:0.10 to 1:0.15.
The molar ratio of the sec-octanol in the step S2 to the acrylic acid in the step S1 is 1:1-5:1; the preferred molar ratio is 3.5: 1-4.0:1.
In the step S3, the tertiary butanol/water receiving tank should timely separate the byproduct tertiary butanol/water generated in the addition reaction kettle in the addition reaction process from the reaction system through the self-contained tower top condenser and spiral plate heat exchanger A to ensure the reaction rate and yield
In the step S6, the volume ratio of the white oil to the gamma-methyl decalactone is 0.1:1-0.5:1; the preferable volume ratio is 0.1:1-0.15:1, and the mass ratio of the acid catalyst to the gamma-methyl decalactone is 0.05:1-0.5:1; the preferable mass ratio is 0.05:1-0.1:1.
In the step S6, the rearrangement reaction kettle 13 is made of one of enamel and 904 stainless steel, and the distillation tower of the rearrangement reaction kettle is made of graphite.
The hydrogenation catalyst in the step S8 is one of 5% palladium carbon or Raney nickel, the volume ratio of petroleum ether to 2-hexyl cyclopentenone is 1:1-5:1, and the preferable volume ratio is 1:1-2:1; the preferred volume ratio is 1:1 to 2:1.
In the step S12, the molar ratio of the peracetic acid to the 3-methyl-2-amyl cyclopentanone is 1:1-3:1; the preferred molar ratio is 1:1 to 1.5:1.
The kettle type fractionating tower is internally 10 filled with cy500 stainless steel corrugated filler; and the kettle type rectifying tower 34 is filled with cy700 stainless steel corrugated filler.
Example 2
On the basis of the embodiment 1, referring to fig. 1, a production device of 4-methyl-delta-decalactone perfume comprises a batching pot 1, an acrylic acid high-level tank 2 and a di-tert-butyl peroxide high-level tank 3 which are respectively connected with the batching pot 1 through pipelines; the sec-octyl alcohol overhead tank 4 is respectively connected with the batching kettle 1 and the addition reaction kettle 6 through pipelines; the batching mixture overhead tank 5 is connected with the batching pot 1 and the addition reaction kettle 6 through a pump and a dripping pump A7 respectively; the addition reaction kettle 6 is provided with a fractionation reflux device; the tertiary butanol/water receiving tank 9 and the kettle type distillation tower A10 are respectively connected with the addition reaction kettle 6 through a spiral plate heat exchanger A8 and a material pump; the secondary octanol vacuum receiving tank 12 is connected with the top of the kettle type distillation tower A10 and the secondary octanol overhead tank 4 through a spiral plate heat exchanger B11 and a material pump respectively; the phosphoric acid high-level tank 14 and the white oil high-level tank 15 are respectively connected through a pipeline rearrangement reaction kettle 13, the rearrangement reaction kettle 13 is connected with a kettle type distillation tower A10 through a material pump, and a fractionation reflux device is arranged on the rearrangement reaction kettle; the water diversion receiving tank 17 and the water washing kettle A18 are respectively connected with the rearrangement reaction kettle 13 through a spiral plate heat exchanger C16 and a material pump; the hydrogenation reaction kettle 19 is connected with the water washing kettle A18 and the petroleum ether overhead tank 20 through a material pump and a pipeline respectively; the automatic back flushing precision filter 21 is connected with the hydrogenation reaction kettle 19 and the petroleum ether overhead tank 20 through a U-shaped bent pipe and a material pump respectively; the kettle type distillation tower B22 is respectively connected with the automatic back flushing precision filter 21 and the oxidation reaction kettle 31 through a material pump; the petroleum ether receiving tank 24 is connected with the top of the kettle type distillation column B22 and the petroleum ether overhead tank 20 through a spiral plate heat exchanger D23 and a pipeline respectively; the peracetic acid preparation kettle 25 is connected with a hydrogen peroxide elevated tank 26 and a peracetic acid elevated tank 30 through a dripping pump C29 and a material pump respectively; the acetic acid elevated tank 27 and the sulfuric acid elevated tank 28 are respectively connected with the peroxyacetic acid preparation kettle 25 through pipelines; the oxidation reaction kettle 31 is connected with the peracetic acid overhead tank 30 and the water washing kettle B33 through a dripping pump D32 and a material pump respectively; the kettle type rectifying tower 34 is connected with the water washing kettle B33 and the gas-liquid separator 36 through a material pump and a spiral plate heat exchanger E35 respectively; the low-boiling vacuum receiving tank 37 and the product temporary storage tank 39 are connected to the gas-liquid separator 36 through a pipe and a product vacuum receiving tank 38, respectively.
The working principle of the invention is as follows: the method is suitable for producing the 4-methyl-delta-decalactone synthesized perfume by taking the sec-octanol and the acrylic acid as the initial raw materials through addition reaction, molecular rearrangement, hydrogenation and oxidation ring-expansion esterification reaction, and adopts an automatic back flushing filtration technology to realize solid-liquid separation, so that the process flow is relatively short, the raw materials are easy to obtain, and the total yield is improved.
The foregoing describes one embodiment of the present invention in detail, but the description is only a preferred embodiment of the present invention and should not be construed as limiting the scope of the invention. All equivalent changes and modifications within the scope of the present invention are intended to be covered by the present invention.
Claims (10)
1. A method for producing a 4-methyl-delta-decalactone fragrance, comprising the steps of:
s1, metering sec-octyl alcohol into a batching pot (1) from a sec-octyl alcohol overhead tank (4), starting a freezing salt water valve and a stirrer of the batching pot (1), controlling the temperature of the stirring pot to be 20+/-5 ℃, then metering acrylic acid and di-tert-butyl peroxide into an acrylic acid overhead tank (2) and a di-tert-butyl peroxide overhead tank (3) respectively, uniformly stirring to obtain a batching mixture, and pumping the batching mixture into a batching mixture overhead tank (5) for standby;
s2, metering sec-octanol into an addition reaction kettle (6) with a fractionating tower from a sec-octanol overhead tank (4), starting a steam valve of the addition reaction kettle (6), starting a stirrer, and heating the addition reaction kettle (6) and maintaining the temperature at 120-160 ℃;
s3, dropwise adding the mixture obtained in the step S1 into an addition reaction kettle (6) through a dropwise adding pump A (7), controlling the dropwise adding temperature to be 150+/-5 ℃ and the dropwise adding time to be 8-12 hours, condensing byproduct water and tertiary butanol from the top of the addition reaction kettle (6) through a spiral plate heat exchanger A (8), collecting the condensed product water and tertiary butanol into a tertiary butanol/water receiving tank (9), and separating a water layer through centralized water diversion treatment to obtain the byproduct tertiary butanol;
s4, after the dripping is finished, continuing to keep the temperature and stir for 1-2 hours, finishing the reaction, and transferring the reaction liquid into a kettle type distillation tower A (10) by using a pump;
s5, opening a steam valve of a kettle type fractionating tower A (10), starting a vacuum pump, heating, recovering the sec-octanol by reduced pressure distillation under the conditions that the temperature of the top of the tower is 90-120 ℃ and the vacuum pressure is 6667Pa, condensing the sec-octanol by a spiral plate heat exchanger B (11), collecting the sec-octanol by a sec-octanol vacuum receiving tank (12), and transferring the sec-octanol into a sec-octanol overhead tank (4) by a pump for application; when the temperature of the tower top is reduced or the tower top is not discharged, the secondary octanol recovery is finished, and the reaction liquid at the bottom of the kettle is transferred into a rearrangement reaction kettle (13) by a pump;
s6, starting a stirrer and a steam valve of a rearrangement reaction kettle (13), heating to the kettle temperature of 80-120 ℃, metering white oil into the rearrangement reaction kettle (13) with a distillation tower from a white oil overhead tank (15), slowly metering phosphoric acid into the rearrangement reaction kettle (13) from a phosphoric acid overhead tank (14), reacting for 4-8 hours, keeping reflux in the reaction process, condensing byproduct water from the top of the rearrangement reaction kettle (13) through a spiral plate heat exchanger C (16), and collecting the condensed byproduct water into a water distribution receiving tank (17);
s7, after the rearrangement reaction is finished, continuously maintaining the temperature, stirring and refluxing for 30min, terminating the reaction, transferring the reaction liquid into a water washing kettle A (18), adding clear water for washing, standing and layering for 2h, separating a water layer, and transferring an oil layer into a hydrogenation reaction kettle (19) by using a pump;
s8, filling a hydrogenation catalyst into the hydrogenation reaction kettle (19) at one time, metering petroleum ether into the hydrogenation reaction kettle (19) from a solvent petroleum ether overhead tank (20), introducing nitrogen for replacement for 3-5 times, introducing hydrogen for stabilizing at the pressure of the reaction kettle of 0.5-2.0Mpa, starting a steam valve to heat the hydrogenation reaction kettle (19) to the kettle temperature of 30-80 ℃, continuously introducing hydrogen for hydrogenation, and cooling, decompressing and terminating the reaction after the hydrogenation is finished for 4-12 hours;
s9, back flushing the solid-phase hydrogenation catalyst into a hydrogenation reaction kettle (19) through an automatic back flushing precision filter (21) for repeated use, and transferring the liquid-phase reaction liquid into a kettle type distillation tower B (22);
s10, starting a steam valve, heating a kettle type distillation column B (22) to the kettle temperature of 60-100 ℃, recovering petroleum ether under the conditions of the tower top temperature of 60-90 ℃ and normal pressure, transferring the petroleum ether into a petroleum ether overhead tank (20) for reuse, and transferring the reaction solution at the bottom of the kettle into an oxidation reaction kettle (31) by a pump after the temperature of the tower top is reduced or the tower top is not discharged;
s11, starting a stirrer and a cooling water valve of a peracetic acid preparation kettle (25), controlling the kettle temperature below 30 ℃, respectively metering acetic acid and hydrogen peroxide into the peracetic acid preparation kettle (25) from an acetic acid high-level tank (27) and a hydrogen peroxide high-level tank (26), slowly metering sulfuric acid into the peracetic acid preparation kettle (25) from a sulfuric acid high-level tank (28), uniformly stirring, and pumping to the peracetic acid high-level tank (30) for standby;
s12, starting a stirrer and a cooling water valve of an oxidation reaction kettle (31), controlling the kettle temperature below 30 ℃, then dropwise adding peracetic acid into the oxidation reaction kettle (31) through a dropwise adding pump D (32), controlling the dropwise adding temperature at 25-30 ℃ for 4-12h, continuing to keep the temperature for reaction for 1-2h after dropwise adding, adding clear water to terminate the reaction, and pumping the reaction liquid into a water washing kettle B (33);
s13, adding clear water into the water washing kettle B (33) in a metering way, starting a stirrer to wash for three times, standing for 2 hours, concentrating acetic acid water separated from the primary water washing to perform acetic acid purification treatment, enabling water layers separated from the secondary water washing and the tertiary water washing to enter a sewage treatment station for treatment, and pumping the separated oil layer into a kettle type rectifying tower (34);
s14, opening a steam valve of a kettle type rectifying tower (34), starting a vacuum pump, heating to a temperature of between 90 and 130 ℃ at the top of the tower, collecting low-boiling substances such as residual acetic acid by reduced pressure distillation under the condition that the vacuum pressure is 6667Pa, condensing by a spiral plate heat exchanger E (35), collecting the low-boiling substances into a low-boiling vacuum receiving tank (37) by a gas-liquid separator (36), then opening high vacuum, decompressing and distilling 4-methyl-delta-decalactone under the condition that the vacuum pressure is 1333Pa at the top of the tower, condensing by the spiral plate heat exchanger E35, collecting the products by the gas-liquid separator (36), and transferring the products into a product temporary storage tank (39).
2. The method for producing 4-methyl-delta-decalactone fragrance according to claim 1, characterized in that the compounding pot (1), the acrylic acid head tank (2) and the compounding mixture head tank (5) are all insulated by 20±5 ℃.
3. The method for producing a 4-methyl-delta-decalactone fragrance according to claim 1, wherein the molar ratio of acrylic acid to secondary octanol of the dosing mixture in step S1 is between 1:2 and 1:5; the molar ratio of acrylic acid to di-tert-butyl peroxide is 1:0.1-1:0.5.
4. The method for producing a 4-methyl-delta-decalactone fragrance according to claim 1, wherein the molar ratio of the secondary octanol in step S2 to the acrylic acid in step S1 is 1:1 to 5:1.
5. The method for producing a 4-methyl-delta-decalactone fragrance according to claim 1, wherein the volume ratio of white oil to gamma-methyl decalactone in step S6 is 0.1:1-0.5:1, and the mass ratio of the acid catalyst to gamma-methyl decalactone is 0.05:1-0.5:1.
6. The method for producing 4-methyl-delta-decalactone perfume according to claim 1, wherein in the step S6, the rearrangement reaction kettle (13) is made of one of enamel and 904 stainless steel, and the distillation tower of the rearrangement reaction kettle is made of graphite.
7. The method for producing a 4-methyl-delta-decalactone fragrance according to claim 1, wherein the hydrogenation catalyst in step S8 is one of 5% palladium on charcoal or raney nickel, the volume ratio of petroleum ether to 2-hexylcyclopentenone is 1:1-5:1, preferably 1:1-2:1.
8. The method for producing a 4-methyl-delta-decalactone fragrance according to claim 1, wherein the molar ratio of peracetic acid to 3-methyl-2-amyl cyclopentanone in step S12 is 1:1-3:1.
9. The method for producing 4-methyl-delta-decalactone fragrance according to claim 1, wherein the kettle-type fractionating tower (10) is filled with cy500 stainless steel corrugated packing; and the kettle type rectifying tower (34) is filled with cy700 stainless steel corrugated filler.
10. The production device of the 4-methyl-delta-decalactone spice is characterized by comprising a batching pot (1), wherein an acrylic acid overhead tank (2) and a di-tert-butyl peroxide overhead tank (3) are respectively connected with the batching pot (1) through pipelines; the sec-octyl alcohol overhead tank (4) is respectively connected with the batching kettle (1) and the addition reaction kettle (6) through pipelines; the batching mixture overhead tank (5) is connected with the batching pot (1) and the addition reaction kettle (6) through a pump and a dripping pump A (7) respectively; the addition reaction kettle (6) is provided with a fractionation reflux device; the tertiary butanol/water receiving tank (9) and the kettle type distillation tower A (10) are respectively connected with the addition reaction kettle (6) through a spiral plate heat exchanger A (8) and a material pump; the secondary octanol vacuum receiving tank (12) is connected with the top of the kettle type distillation tower A (10) and the secondary octanol overhead tank (4) through a spiral plate heat exchanger B (11) and a material pump respectively; the phosphoric acid overhead tank (14) and the white oil overhead tank (15) are respectively connected through a pipeline rearrangement reaction kettle (13), the rearrangement reaction kettle (13) is connected with the kettle type distillation tower A (10) through a material pump, and the kettle type distillation tower A is provided with a fractionation reflux device; the water diversion receiving tank (17) and the water washing kettle A (18) are respectively connected with the rearrangement reaction kettle (13) through a spiral plate heat exchanger C (16) and a material pump; the hydrogenation reaction kettle (19) is connected with the water washing kettle A (18) and the petroleum ether overhead tank (20) through a material pump and a pipeline respectively; the automatic back flushing precision filter (21) is connected with the hydrogenation reaction kettle (19) and the petroleum ether overhead tank (20) through a U-shaped bent pipe and a material pump respectively; the kettle type distillation tower B (22) is respectively connected with the automatic back flushing precision filter (21) and the oxidation reaction kettle (31) through a material pump; the petroleum ether receiving tank (24) is connected with the top of the kettle type distillation tower B (22) and the petroleum ether overhead tank (20) through a spiral plate heat exchanger D (23) and a pipeline respectively; the peracetic acid preparation kettle (25) is connected with a hydrogen peroxide elevated tank (26) and a peracetic acid elevated tank (30) through a dripping pump C (29) and a material pump respectively; the acetic acid elevated tank (27) and the sulfuric acid elevated tank (28) are respectively connected with a peroxyacetic acid configuration kettle (25) through pipelines; the oxidation reaction kettle (31) is connected with a peracetic acid overhead tank (30) and a water washing kettle B (33) through a dripping pump D (32) and a material pump respectively; the kettle type rectifying tower (34) is connected with the water washing kettle B (33) and the gas-liquid separator (36) through a material pump and a spiral plate heat exchanger E (35) respectively; the low-boiling vacuum receiving tank (37) and the product temporary storage tank (39) are respectively connected with the gas-liquid separator (36) through a pipeline and the product vacuum receiving tank (38).
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| CN202310984016.XA CN117019033A (en) | 2023-08-07 | 2023-08-07 | Production device and method of 4-methyl-delta-decalactone perfume |
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| CN202310984016.XA CN117019033A (en) | 2023-08-07 | 2023-08-07 | Production device and method of 4-methyl-delta-decalactone perfume |
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