CN113292425A - Production method of bis (2-propyl) heptyl terephthalate - Google Patents
Production method of bis (2-propyl) heptyl terephthalate Download PDFInfo
- Publication number
- CN113292425A CN113292425A CN202110674612.9A CN202110674612A CN113292425A CN 113292425 A CN113292425 A CN 113292425A CN 202110674612 A CN202110674612 A CN 202110674612A CN 113292425 A CN113292425 A CN 113292425A
- Authority
- CN
- China
- Prior art keywords
- propyl
- product
- heptanol
- crude product
- alcohol
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- -1 bis (2-propyl) heptyl terephthalate Chemical compound 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 20
- 239000000047 product Substances 0.000 claims abstract description 74
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 claims abstract description 63
- 238000005886 esterification reaction Methods 0.000 claims abstract description 47
- YLQLIQIAXYRMDL-UHFFFAOYSA-N propylheptyl alcohol Chemical compound CCCCCC(CO)CCC YLQLIQIAXYRMDL-UHFFFAOYSA-N 0.000 claims abstract description 39
- VXUYXOFXAQZZMF-UHFFFAOYSA-N titanium(IV) isopropoxide Chemical compound CC(C)O[Ti](OC(C)C)(OC(C)C)OC(C)C VXUYXOFXAQZZMF-UHFFFAOYSA-N 0.000 claims abstract description 38
- 239000012043 crude product Substances 0.000 claims abstract description 37
- 239000002994 raw material Substances 0.000 claims abstract description 37
- 238000011282 treatment Methods 0.000 claims abstract description 35
- 238000003756 stirring Methods 0.000 claims abstract description 24
- 239000003054 catalyst Substances 0.000 claims abstract description 22
- 238000002156 mixing Methods 0.000 claims abstract description 22
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 8
- 239000012467 final product Substances 0.000 claims abstract description 5
- 238000002360 preparation method Methods 0.000 claims abstract description 4
- 238000005303 weighing Methods 0.000 claims abstract description 4
- 238000000926 separation method Methods 0.000 claims description 29
- 239000011259 mixed solution Substances 0.000 claims description 22
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 21
- 230000032050 esterification Effects 0.000 claims description 21
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 16
- 239000012808 vapor phase Substances 0.000 claims description 15
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 12
- 238000006386 neutralization reaction Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 7
- 239000003463 adsorbent Substances 0.000 claims description 7
- 239000000243 solution Substances 0.000 claims description 7
- 238000001179 sorption measurement Methods 0.000 claims description 5
- 239000012535 impurity Substances 0.000 claims description 3
- 239000005909 Kieselgur Substances 0.000 claims description 2
- 230000003472 neutralizing effect Effects 0.000 claims description 2
- 239000004014 plasticizer Substances 0.000 abstract description 8
- 239000002253 acid Substances 0.000 abstract description 5
- ORTYRKBSNXTIFO-UHFFFAOYSA-N bis(2-propylheptyl) benzene-1,4-dicarboxylate Chemical compound CCCCCC(CCC)COC(=O)C1=CC=C(C(=O)OCC(CCC)CCCCC)C=C1 ORTYRKBSNXTIFO-UHFFFAOYSA-N 0.000 abstract description 4
- 238000012805 post-processing Methods 0.000 abstract description 2
- 238000004042 decolorization Methods 0.000 abstract 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 16
- BBMCTIGTTCKYKF-UHFFFAOYSA-N 1-heptanol Chemical compound CCCCCCCO BBMCTIGTTCKYKF-UHFFFAOYSA-N 0.000 description 10
- 238000001514 detection method Methods 0.000 description 7
- 239000008029 phthalate plasticizer Substances 0.000 description 7
- RZKSECIXORKHQS-UHFFFAOYSA-N Heptan-3-ol Chemical compound CCCCC(O)CC RZKSECIXORKHQS-UHFFFAOYSA-N 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000012295 chemical reaction liquid Substances 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 231100000053 low toxicity Toxicity 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- KJFMBFZCATUALV-UHFFFAOYSA-N phenolphthalein Chemical compound C1=CC(O)=CC=C1C1(C=2C=CC(O)=CC=2)C2=CC=CC=C2C(=O)O1 KJFMBFZCATUALV-UHFFFAOYSA-N 0.000 description 2
- XNGIFLGASWRNHJ-UHFFFAOYSA-L phthalate(2-) Chemical compound [O-]C(=O)C1=CC=CC=C1C([O-])=O XNGIFLGASWRNHJ-UHFFFAOYSA-L 0.000 description 2
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 206010021928 Infertility female Diseases 0.000 description 1
- 206010021929 Infertility male Diseases 0.000 description 1
- 208000007466 Male Infertility Diseases 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000002280 anti-androgenic effect Effects 0.000 description 1
- 239000000051 antiandrogen Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000004567 concrete Substances 0.000 description 1
- 230000002124 endocrine Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000005556 hormone Substances 0.000 description 1
- 229940088597 hormone Drugs 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 208000006155 precocious puberty Diseases 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- OVYTZAASVAZITK-UHFFFAOYSA-M sodium;ethanol;hydroxide Chemical compound [OH-].[Na+].CCO OVYTZAASVAZITK-UHFFFAOYSA-M 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 238000004448 titration Methods 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本申请涉及增塑剂的领域，具体公开了一种对苯二甲酸二(2‑丙基)庚酯的生产方法。一种对苯二甲酸二(2‑丙基)庚酯的生产方法包包括以下步骤：步骤1，原料的准备，称取2‑丙基‑1‑庚醇、对苯二甲酸和钛酸四异丙酯，其中2‑丙基‑1‑庚醇和对苯二甲酸的摩尔比为2.0‑4.0：1，所述钛酸四异丙酯的用量为2‑丙基‑1‑庚醇和对苯二甲酸总质量的0.01‑0.20%；步骤2，酯化反应，将步骤1准备的原料于170℃‑245℃温度下混合搅拌2‑5小时，得到粗产品；步骤3，后处理，将粗产品中和后，水洗1‑3次；步骤4，脱色处理，将步骤3经后处理的产品冷却后，脱色过滤得到最终产品。本申请的生产方法具有降低催化剂的使用量、提高对苯二甲酸二(2‑丙基庚)酯生产安全性的优点。The application relates to the field of plasticizers, and specifically discloses a production method of di(2-propyl)heptyl terephthalate. A production method package of bis(2-propyl)heptyl terephthalate comprises the following steps: step 1, preparation of raw materials, weighing 2-propyl-1-heptanol, terephthalic acid and tetrakis titanate Isopropyl ester, wherein the mol ratio of 2-propyl-1-heptanol and terephthalic acid is 2.0-4.0: 1, and the consumption of described tetraisopropyl titanate is 2-propyl-1-heptanol and p-benzene 0.01-0.20% of the total mass of diformic acid; step 2, esterification reaction, mixing and stirring the raw materials prepared in step 1 at a temperature of 170 ℃-245 ℃ for 2-5 hours to obtain a crude product; step 3, post-processing, the crude product After the product is neutralized, washed with water 1-3 times; step 4, decolorization treatment, after cooling the post-treated product in step 3, decolorization and filtration to obtain the final product. The production method of the present application has the advantages of reducing the amount of catalyst used and improving the production safety of bis(2-propylheptyl) terephthalate.
Description
Technical Field
The present application relates to the field of plasticizers, and more particularly, to a process for the production of bis (2-propyl) heptyl terephthalate.
Background
The plasticizer is an additive for increasing the plasticity of polymers, is widely applied to the preparation of materials such as plastic products, concrete, gypsum and the like, and is low in cost, colorless and tasteless and good in plasticizing effect, so that the phthalate plasticizer is the largest plasticizer used at home and abroad at present.
However, the phthalate plasticizer has environmental hormone toxicity and migratability, and because the phthalate plasticizer is only physically mixed with plastics and other materials, the phthalate plasticizer is easily dissolved out by grease and the like and migrates to the environment to pollute the environment, and the anti-androgen performance of the phthalate plasticizer interferes with the endocrine of human bodies, is closely related to the problems of male and female sterility, female sexual precocity and the like and harms human health, so the dosage of the phthalate plasticizer is limited in European Union instructions and national standards in China.
Due to the disadvantages of phthalate plasticizers, non-phthalate plasticizers have come into play, and di (2-propyl) heptyl terephthalate is a non-phthalate plasticizer with low toxicity and environmental friendliness.
Chinese patent publication No. CN103664621A discloses a synthesis process of bis (2-propylheptyl) terephthalate, which comprises the following process steps: (1) according to the weight ratio of terephthalic acid: taking raw materials according to the mole ratio of 1: 2.7-2.9 of heptanol, and taking isopropyl titanate catalyst according to 3.3 percent of the total mass of phthalic acid and heptanol; (2) putting all terephthalic acid and 1/3 heptanol into a reaction kettle, heating to 150 ℃ and 180 ℃, adding 50% of the total amount of the catalyst, and finishing the addition of the catalyst within 4-6 minutes; (3) heating the reaction liquid in the step (2) to 190-210 ℃, adding 1/3 heptanol, and adding 25% of catalyst after 5-10 minutes; (4) preserving the temperature of the reaction liquid in the step (3) at 210-220 ℃, and adding the residual heptanol and the catalyst into the reaction liquid for reaction to obtain a crude product; (5) and washing the crude product with water, dealcoholizing, decoloring and filtering to obtain a finished product.
However, isopropyl titanate is a toxic and dangerous chemical because isopropyl titanate is used as a catalyst for esterification reaction, and reacts with water or water vapor to give out toxic or flammable gas, and the possibility of explosion under high temperature or high pressure is high.
In view of the above-mentioned related technologies, the inventors believe that the use amount of isopropyl titanate catalyst in the related process is large, which increases the risk of producing bis (2-propylheptyl) terephthalate.
Disclosure of Invention
In order to reduce the using amount of a catalyst and improve the safety of the production of the bis (2-propyl heptyl) terephthalate, the application provides a production method of the bis (2-propyl) heptyl terephthalate.
The application provides a production method of bis (2-propyl) heptyl terephthalate, which adopts the following technical scheme:
a method for producing bis (2-propyl) heptyl terephthalate, comprising the steps of:
step 1, preparing raw materials, namely weighing 2-propyl-1-heptanol, terephthalic acid and tetraisopropyl titanate, wherein the molar ratio of the 2-propyl-1-heptanol to the terephthalic acid is 2.0-4.0: 1, the dosage of the tetraisopropyl titanate is 0.01 to 0.20 percent of the total mass of the 2-propyl-1-heptanol and the terephthalic acid;
step 2, esterification reaction, namely mixing and stirring the raw materials prepared in the step 1 at the temperature of 170-245 ℃ for 2-5 hours to obtain a crude product;
step 3, post-treatment, namely neutralizing the crude product and washing the neutralized crude product for 1 to 3 times;
and 4, decoloring, namely cooling the product subjected to the post-treatment in the step 3, decoloring and filtering to obtain a final product.
By adopting the technical scheme, the application limits the molar ratio of the 2-propyl-1-heptanol to the terephthalic acid, and reduces the using amount of the tetraisopropyl titanate, thereby improving the safety of the application.
Preferably, in the preparation of the starting material in step 1, the molar ratio of 2-propyl-1-heptanol to terephthalic acid is 3.0 to 4.0: 1.
by adopting the technical scheme, the molar ratio of the 2-propyl-1-heptanol to the terephthalic acid is further limited, so that the product yield and the product purity can be comprehensively improved.
Preferably, the esterification reaction of step 2 specifically comprises the following steps:
step 21, premixing raw materials, and uniformly stirring 75-85% of the weight of 2-propyl-1-heptanol and the mixing rate of all terephthalic acid at the room temperature at the speed of 80-110r/min to obtain a premix A;
and step 22, reacting the raw materials, sequentially adding 15-25% of the mass of the tetraisopropyl titanate catalyst and the 2-propyl-1-heptanol into the premix A at the temperature of 170-245 ℃, and mixing and stirring for 2-5 hours to obtain a crude product.
By adopting the technical scheme, the 2-propyl-1-heptanol is put into the reactor in batches at different temperatures, so that the mixing efficiency of the raw materials is improved, the 2-propyl-1-heptanol and terephthalic acid are fully reacted, and the purity and the yield of the product are improved.
Preferably, the step 22 of raw material reaction specifically comprises the following steps:
step 221, pre-esterification, adding all catalysts into the premix A at the temperature of 170-;
step 222, post-esterification, heating to 215 ℃ and 245 ℃ at the speed of 2-5 ℃/min, mixing and stirring the residual 2-propyl-1-heptanol and the mixed solution B for 2-5 hours, and stirring to obtain a crude product.
By adopting the technical scheme, the raw material reaction step is divided into two sections of esterification reaction by adopting a sectional esterification method at different temperatures, so that the product selectivity is improved, the side reaction is inhibited, the product purity is improved, and the product chromaticity is improved.
Preferably, the post-esterification in step 222 specifically comprises the following steps:
step 2221, heating to 215-220 ℃ at a rate of 2-5 ℃/min, and mixing the rest 2-propyl-1-heptanol with the mixed solution B and stirring uniformly to obtain a mixed solution C;
step 2222, the temperature is raised in the second step, the temperature is continuously raised to 225-245 ℃ at the speed of 2-5 ℃/min, the mixed solution C is mixed and stirred for 2-5 hours to obtain a crude product, and the vapor phase component generated by the reaction is separated from the crude product for the post-treatment in the step 3.
By adopting the technical scheme, the post-esterification step is subjected to two-stage esterification reaction by means of sectional esterification, so that the product selectivity is further improved, the side reaction is inhibited, and the reaction is promoted to be carried out in the forward direction by separating water in time, thereby being beneficial to improving the yield of the product.
Preferably, the post-treatment of step 3 specifically comprises the following steps:
step 31, dealcoholization, namely condensing vapor phase components generated by the reaction and then performing first alcohol-water separation, wherein alcohol obtained by the first alcohol-water separation is used as a raw material in the esterification reaction step in the step 1;
step 32, neutralization treatment;
and step 33, water washing treatment, namely washing the neutralized crude product for 1-3 times by using the water obtained after the first alcohol-water separation in the step 31.
By adopting the technical scheme, because the first alcohol-water separation is adopted, the water of the first alcohol-water separation is used for water washing treatment, and the alcohol of the first alcohol-water separation is recycled as the raw material, so that the production cost is reduced, and the recycling of the alcohol and the water is realized.
Preferably, the neutralization treatment in step 32 is specifically: cooling the dealcoholized crude product to 100 ℃, and then adding sodium hydroxide solution to neutralize the crude product until the pH value is 7-7.5.
By adopting the technical scheme, the acid value of the product is adjusted by adding the sodium hydroxide solution.
Preferably, in the step 4, the product after being washed by water in the step 33 is subjected to the following treatment: heating the product neutralized in the step 32 to 180 ℃ and 190 ℃, stripping for 1-3h, and keeping the temperature of the stripped product for 0.5-1 h.
By adopting the technical scheme, the stripping operation is favorable for removing the soluble stripping and volatile substances in the product, thereby being favorable for the subsequent alcohol-water separation.
Preferably, in the step 4, after the steam-stripped vapor phase component is separated from the heat-preserved product, the steam-stripped vapor phase component is subjected to second alcohol-water separation; wherein the water of the second alcohol-water separation is used in the water washing treatment step of step 33; wherein the alcohol of the second alcohol-water separation is used as a raw material in the esterification reaction step of step 1.
By adopting the technical scheme, because the second alcohol-water separation is adopted, the water of the second alcohol-water separation is used for water washing treatment, and the alcohol of the second alcohol-water separation is recycled as the raw material, so that the production cost is further reduced, and the recycling of the alcohol and the water is realized.
Preferably, in the step 4, after the product separated from the stripped vapor phase component is cooled to 120 ℃ of 100-; the adsorbent comprises one or more of activated carbon and diatomaceous earth.
By adopting the technical scheme, as the adsorbent adopts one or more of the active carbon and the diatomite, the active carbon and the diatomite have excellent adsorption effect, the chromaticity and the acid value of the product can be comprehensively improved after the active carbon and the diatomite are compounded, and the diatomite has the function of assisting filtration, so that the aggregation state of particles is reduced, thereby being beneficial to filtering and removing more impurities and further being beneficial to improving the purity of the product.
In summary, the present application has the following beneficial effects:
1. the application provides a method for preparing a low-toxicity terephthalic acid di (2-propyl) heptyl ester product, the molar ratio of 2-propyl-1-heptanol to terephthalic acid is limited, the using amount of tetraisopropyl titanate is reduced, and therefore the safety of the method provided by the application is improved.
2. The method improves the mixing efficiency of the raw materials, reduces byproducts and improves the conversion rate and the product yield of the purified terephthalic acid by means of premixing and multistage esterification.
3. Acid-base neutralization, water washing and decoloration are adopted, so that the acid value and the chroma of the product are comprehensively reduced.
Detailed Description
The present application will be described in further detail with reference to examples and comparative examples.
Raw materials
Table 1 source table of raw materials used in the present application
Examples
Example 1
A production method of bis (2-propyl) heptyl terephthalate specifically comprises the following steps:
step 1, preparing raw materials, namely weighing 24.771kg of 2-propyl-1-heptanol, 13.000kg of terephthalic acid and 0.022kg of tetraisopropyl titanate, wherein the molar ratio of the 2-propyl-1-heptanol to the terephthalic acid is 2: 1; the dosage of the titanium tetraisopropyl ester catalyst is 0.058 percent of the total mass of the 2-propyl-1-heptanol and the terephthalic acid;
step 2, the esterification reaction specifically comprises the following steps:
step 21, premixing raw materials, namely mixing 80 percent of 2-propyl-1-heptanol and all terephthalic acid in an esterification kettle at room temperature at a rotating speed of 100r/min for 0.8h to obtain a premixed solution A;
step 22, the reaction of the raw materials specifically comprises the following steps:
step 221, pre-esterification, namely adding all catalysts into an esterification kettle containing the premix A at the temperature of 180 ℃, and mixing and stirring at the rotating speed of 100r/min for 1.5 hours to obtain a mixed solution B;
step 222, the post-esterification specifically comprises the following steps:
step 2221, heating to 220 ℃ at a rate of 3 ℃/min, adding the rest 2-propyl-1-heptanol into an esterification kettle containing the mixed solution B, and mixing and stirring for 1h to obtain a mixed solution C;
step 2222, heating up to 230 ℃ at a rate of 3 ℃/min, stirring the mixed solution C for 3 hours at a rotation speed of 100r/min to obtain a crude product, and separating vapor phase components (alcohol steam and water vapor) generated by the reaction from the crude product for post-treatment in step 3;
and 3, post-processing specifically comprises the following steps:
step 31, dealcoholization, namely introducing alcohol steam and water vapor generated in the esterification kettle into an esterification condenser for liquefaction, and then performing first alcohol-water separation by using an oil-water separator (a cyclone oil-water separator, the model of which is JHGL, Jiahang filtration equipment, Inc., of Xingxiang city), wherein alcohol obtained by the first alcohol-water separation is refluxed and then used as a raw material in the esterification reaction step of step 1;
step 32, neutralization treatment; transferring the dealcoholized crude product to a refining kettle, cooling to 100 ℃, adding sodium hydroxide solution to neutralize the dealcoholized crude product to pH 7;
step 33, water washing treatment, namely washing the neutralized crude product with water obtained after the first alcohol-water separation in the step 31 for 1-3 times;
and 4, decoloring, which specifically comprises the following steps:
step 41, steam stripping, namely heating the product neutralized in the step 32 to 185 ℃ for 2 hours, then carrying out flash point test on the product after steam stripping, wherein the flash point of the product is 230 ℃, namely the product after steam stripping is qualified, preserving the heat of the qualified product after steam stripping at 185 ℃ for 0.6 hour, separating the steam phase components (alcohol steam and water steam) after steam stripping from the product after heat preservation, and carrying out second alcohol-water separation on the separated steam phase components (alcohol steam and water steam) through an oil-water separator, wherein the water obtained by the second alcohol-water separation is used in the water washing treatment step of the step 33, and the alcohol obtained by the second alcohol-water separation is used as a raw material in the esterification reaction step of the step 1;
step 42, decoloring, namely cooling a product separated from the extracted vapor phase components to 110 ℃, transferring the cooled product into a filter (ZPG-A/B automatic deslagging filter, Zhejiang Xuan valve Co., Ltd.) for adsorption and decoloring, and filtering an adsorbent and impurities after adsorption is finished to obtain a final product; wherein the filter is internally provided with an adsorbent which consists of 10kg of active carbon and 5kg of diatomite.
Examples 2 to 9
Examples 2-9 differ from example 1 in that: the amounts of 2-propyl-1-heptanol, terephthalic acid and tetraisopropyl titanate used were varied, and are specified in table 2, wherein the tetraisopropyl titanate catalyst percentage is the mass of catalyst/(mass of terephthalic acid + mass of 2-propyl-1-heptanol) × 100%.
Table 2 examples 1-9 raw material compositions and amounts
Example 10
The difference between this embodiment and embodiment 1 is that step 2222 is different in the second temperature rise, which in this embodiment specifically is as follows: and (3) continuously raising the temperature to 220 ℃ at the speed of 3 ℃/min, stirring the mixed solution C for 3 hours at the rotating speed of 100r/min to obtain a crude product, and separating vapor phase components (alcohol steam and water vapor) generated by the reaction from the crude product for post-treatment in the step (3).
Example 11
The difference between this embodiment and embodiment 1 is that step 2221 is different in the first temperature rise, which in this embodiment specifically is as follows: heating to 230 ℃ at the speed of 3 ℃/min, adding the rest 2-propyl-1-heptanol into the esterification kettle containing the mixed solution B, and mixing and stirring for 1h to obtain a mixed solution C.
Example 12
The difference between this example and example 1 is that the reaction of the raw materials in step 22 is different, and the reaction of the raw materials in this example specifically includes the following steps:
step 221, pre-esterification, namely adding all catalysts into an esterification kettle containing the premix A at the temperature of 220 ℃, and mixing and stirring at the rotating speed of 100r/min for 1.5 hours to obtain a mixed solution B;
step 222, the post-esterification specifically comprises the following steps:
step 2221, heating in the first step, adding the rest 2-propyl-1-heptanol into the esterification kettle containing the mixed solution B at 220 ℃, and mixing and stirring for 1h to obtain a mixed solution C;
step 2222, heating, stirring the mixed solution C at 220 deg.C for 3 hours at 100r/min to obtain crude product, and separating the vapor phase components (alcohol vapor and water vapor) from the crude product for post-treatment in step 3;
example 13
The difference between this example and example 1 is that step 2 is different from the esterification reaction, and the esterification reaction in this example specifically includes the following steps:
step 21, premixing raw materials, namely mixing all 2-propyl-1-heptanol and all terephthalic acid in an esterification kettle at the room temperature for 0.8h at the rotating speed of 100r/min to obtain a premix A;
step 22, the reaction of the raw materials specifically comprises the following steps:
step 221, pre-esterification, namely adding all catalysts into an esterification kettle containing the premix A at the temperature of 180 ℃, and mixing and stirring at the rotating speed of 100r/min for 1.5 hours to obtain a mixed solution B;
step 222, the post-esterification specifically comprises the following steps:
step 2221, heating to 220 ℃ at the rate of 3 ℃/min in the first step, and mixing and stirring for 1h to obtain a mixed solution C;
step 2222, heating up to 230 ℃ at a rate of 3 ℃/min, stirring the mixed solution C for 3 hours at a rotation speed of 100r/min to obtain a crude product, and separating vapor phase components (alcohol steam and water vapor) generated by the reaction from the crude product for post-treatment in step 3.
Comparative example
Comparative examples 1 to 3
Comparative examples 1-3 differ from example 1 in that: the amounts of 2-propyl-1-heptanol, terephthalic acid and tetraisopropyl titanate used were varied and are shown in Table 3.
TABLE 3 comparative examples 1-3 raw material compositions and amounts
Comparative example 4
The comparative example differs from example 1 in that the step 3 post-treatment is different, and the post-treatment in the comparative example specifically comprises the following steps:
step 31, dealcoholization, namely introducing alcohol steam and water vapor generated in the esterification kettle into an esterification condenser for liquefaction, and then performing first alcohol-water separation by using an oil-water separator (a cyclone oil-water separator, the model of which is JHGL, Jiahang filtration equipment, Inc., of Xingxiang city), wherein alcohol obtained by the first alcohol-water separation is refluxed and then used as a raw material in the esterification reaction step of step 1;
step 32, neutralization treatment; transferring the dealcoholized crude product to a refining kettle, and cooling to 100 ℃;
step 33, water washing treatment, namely washing the neutralized crude product with water obtained after the first alcohol-water separation in the step 31 for 1-3 times;
detection method
1. And (3) detecting the purity of the product: the purity of the products in examples 1 to 13 and comparative examples 1 to 4 was checked by a gas chromatograph;
2. and (3) testing acidity: the acid value and acidity of GB/T1668-2008 plasticizer are measured, colorless ethanol is used as a solvent for dissolving a sample, phenolphthalein is used as an indicator solution, sodium hydroxide-ethanol standard titration solution is used for carrying out parallel detection twice on the products in examples 1-13 and comparative examples 1-4, if the difference value of the parallel detection twice is not more than 0.01mg/g, the arithmetic mean value of the parallel detection results of the two times is taken as the measurement result, if the difference value of the parallel detection on the two sides is more than 0.01mg/g, repeated sampling is carried out for parallel detection, and the qualified standard of the acidity of the product is not more than 0.1%;
3. the product yield is as follows: the products in examples 1 to 13 and comparative examples 1 to 4 were calculated and examined, wherein the product yield is (mass of product actually produced/mass of product calculated theoretically) × 100%;
4. product chromaticity detection: the products of examples 1-13 and comparative examples 1-4 were tested using the appearance chromaticity test of GB/T1664-1995 plasticizer.
Table 4 shows the parameters of the measured data of examples 1 to 13 and comparative examples 1 to 4
It can be seen from the combination of examples 1 to 5 and table 4 that the molar ratio of 2-propyl-1-heptanol to terephthalic acid affects the product purity and the product yield, the greater the molar ratio of 2-propyl-1-heptanol to terephthalic acid, the greater the product purity and the product yield both tend to increase and decrease, and at a molar ratio of 2-propyl-1-heptanol to terephthalic acid of 3.2:1, the product yield can reach 99.72%, and the product purity can reach 99.60%.
It can be seen from the combination of examples 5 to 9 and comparative example 1 and from table 4 that the amount of tetraisopropyl titanate used affects the product purity, product acidity, product color and product yield, that the greater the percentage of tetraisopropyl titanate catalyst, the greater the product purity and product yield both tend to increase and decrease, and that when the percentage of tetraisopropyl titanate catalyst is less than 0.010% or greater than 0.200%, both the product color and the product acidity increase.
As can be seen by combining example 7, comparative examples 2-3 and Table 4, the product yield and product purity were optimized for a 3.2:1 molar ratio of 2-propyl-1-heptanol to terephthalic acid at a given percentage of tetraisopropyl titanate catalyst.
As can be seen by combining example 7, examples 10-13 and Table 4, the premixing and multistage esterification improve the purity and yield of the product.
As can be seen by combining example 7 and comparative example 4 with table 4, the product which was not subjected to neutralization treatment had a low product purity and a high product color although the product yield was high, and thus the product purity and the product color could be improved though the product yield was slightly lowered by the neutralization treatment.
The present embodiment is only for explaining the present application, and it is not limited to the present application, and those skilled in the art can make modifications of the present embodiment without inventive contribution as needed after reading the present specification, but all of them are protected by patent law within the scope of the claims of the present application.
Claims (10)
1. A production method of bis (2-propyl) heptyl terephthalate is characterized by comprising the following steps:
step 1, preparing raw materials, namely weighing 2-propyl-1-heptanol, terephthalic acid and tetraisopropyl titanate, wherein the molar ratio of the 2-propyl-1-heptanol to the terephthalic acid is 2.0-4.0: 1, the dosage of the tetraisopropyl titanate is 0.01 to 0.20 percent of the total mass of the 2-propyl-1-heptanol and the terephthalic acid;
step 2, esterification reaction, namely mixing and stirring the raw materials prepared in the step 1 at the temperature of 170-245 ℃ for 2-5 hours to obtain a crude product;
step 3, post-treatment, namely neutralizing the crude product and washing the neutralized crude product for 1 to 3 times;
and 4, decoloring, namely cooling the product subjected to the post-treatment in the step 3, decoloring and filtering to obtain a final product.
2. The process for producing di (2-propyl) heptyl terephthalate according to claim 1, wherein the molar ratio of 2-propyl-1-heptanol to terephthalic acid in the preparation of the raw material of said step 1 is 3.0 to 4.0: 1.
3. the method for producing bis (2-propyl) heptyl terephthalate according to claim 2, wherein the esterification reaction of step 2 comprises the following steps:
step 21, premixing raw materials, and uniformly stirring 75-85% of the weight of 2-propyl-1-heptanol and the mixing rate of all terephthalic acid at the room temperature at the speed of 80-110r/min to obtain a premix A;
and step 22, reacting the raw materials, sequentially adding 15-25% of the mass of the tetraisopropyl titanate catalyst and the 2-propyl-1-heptanol into the premix A at the temperature of 170-245 ℃, and mixing and stirring for 2-5 hours to obtain a crude product.
4. The method for producing bis (2-propyl) heptyl terephthalate according to claim 3, wherein said step 22 of raw material reaction comprises the following steps:
step 221, pre-esterification, adding all catalysts into the premix A at the temperature of 170-;
step 222, post-esterification, heating to 215 ℃ and 245 ℃ at the speed of 2-5 ℃/min, mixing and stirring the residual 2-propyl-1-heptanol and the mixed solution B for 2-5 hours, and stirring to obtain a crude product.
5. The method for producing bis (2-propyl) heptyl terephthalate according to claim 4, wherein said post-esterification step 222 comprises the following steps:
step 2221, heating to 215-220 ℃ at a rate of 2-5 ℃/min, and mixing the rest 2-propyl-1-heptanol with the mixed solution B and stirring uniformly to obtain a mixed solution C;
step 2222, the temperature is raised in the second step, the temperature is continuously raised to 225-245 ℃ at the speed of 2-5 ℃/min, the mixed solution C is mixed and stirred for 2-5 hours to obtain a crude product, and the vapor phase component generated by the reaction is separated from the crude product for the post-treatment in the step 3.
6. The method for producing bis (2-propyl) heptyl terephthalate according to claim 5, wherein the post-treatment of step 3 comprises the following steps:
step 31, dealcoholization, namely condensing vapor phase components generated by the reaction and then performing first alcohol-water separation, wherein alcohol obtained by the first alcohol-water separation is used as a raw material in the esterification reaction step in the step 1;
step 32, neutralization treatment;
and step 33, water washing treatment, namely washing the neutralized crude product for 1-3 times by using the water obtained after the first alcohol-water separation in the step 31.
7. The method for producing di (2-propyl) heptyl terephthalate according to claim 6, wherein the neutralization treatment of the step 32 is specifically: cooling the dealcoholized crude product to 100 ℃, and then adding sodium hydroxide solution to neutralize the crude product until the pH value is 7-7.5.
8. The process for producing di (2-propyl) heptyl terephthalate according to claim 6, wherein in the step 4, the product after the water washing treatment in the step 33 is previously subjected to the following treatments: heating the product neutralized in the step 32 to 180 ℃ and 190 ℃, stripping for 1-3h, and keeping the temperature of the stripped product for 0.5-1 h.
9. The method of claim 8, wherein in the step 4, after the separation of the stripped vapor phase component from the incubated product, the stripped vapor phase component is subjected to a second alcohol-water separation; wherein the water of the second alcohol-water separation is used in the water washing treatment step of step 33; wherein the alcohol of the second alcohol-water separation is used as a raw material in the esterification reaction step of step 1.
10. The process according to claim 9, wherein in the step 4, the product separated from the vapor phase component after the stripping is cooled to 120 ℃ and then is decolorized by adsorption with an adsorbent, and after the adsorption is completed, the adsorbent and impurities are filtered to obtain the final product; the adsorbent comprises one or more of activated carbon and diatomaceous earth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110674612.9A CN113292425A (en) | 2021-06-17 | 2021-06-17 | Production method of bis (2-propyl) heptyl terephthalate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110674612.9A CN113292425A (en) | 2021-06-17 | 2021-06-17 | Production method of bis (2-propyl) heptyl terephthalate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113292425A true CN113292425A (en) | 2021-08-24 |
Family
ID=77328675
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110674612.9A Pending CN113292425A (en) | 2021-06-17 | 2021-06-17 | Production method of bis (2-propyl) heptyl terephthalate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113292425A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114456062A (en) * | 2022-02-23 | 2022-05-10 | 中国科学院大连化学物理研究所 | Method for converting terephthalic acid into terephthalic acid diester through catalytic esterification |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103664618A (en) * | 2013-11-28 | 2014-03-26 | 浙江海利业科技有限公司 | Novel synthesis process of octyl 2-propylheptyl phthalate |
| CN103664597A (en) * | 2013-11-27 | 2014-03-26 | 浙江海利业科技有限公司 | Novel synthesis technology of adipic acid (2-propyl heptyl) ester |
| CN107922671A (en) * | 2016-05-18 | 2018-04-17 | 株式会社Lg化学 | Plasticizer composition, resin composition and their preparation method |
| CN109563309A (en) * | 2017-02-10 | 2019-04-02 | 株式会社Lg化学 | Plasticizer composition and resin composition comprising the same |
-
2021
- 2021-06-17 CN CN202110674612.9A patent/CN113292425A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103664597A (en) * | 2013-11-27 | 2014-03-26 | 浙江海利业科技有限公司 | Novel synthesis technology of adipic acid (2-propyl heptyl) ester |
| CN103664618A (en) * | 2013-11-28 | 2014-03-26 | 浙江海利业科技有限公司 | Novel synthesis process of octyl 2-propylheptyl phthalate |
| CN107922671A (en) * | 2016-05-18 | 2018-04-17 | 株式会社Lg化学 | Plasticizer composition, resin composition and their preparation method |
| CN109563309A (en) * | 2017-02-10 | 2019-04-02 | 株式会社Lg化学 | Plasticizer composition and resin composition comprising the same |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114456062A (en) * | 2022-02-23 | 2022-05-10 | 中国科学院大连化学物理研究所 | Method for converting terephthalic acid into terephthalic acid diester through catalytic esterification |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP6173463B2 (en) | Method for producing polyol ester | |
| CN113004142B (en) | Novel preparation method of 2,4, 5-trifluoro-phenylacetic acid | |
| JP6392877B2 (en) | Post-treatment method of polyol ester | |
| CN113292425A (en) | Production method of bis (2-propyl) heptyl terephthalate | |
| CN104370791B (en) | A kind of purification process of Levetiracetam | |
| CN101376631B (en) | Environment-protective preparation method of diglycol ethylene dibenzoate plasticiser | |
| CN105254501A (en) | Preparation method of cyclohexane-1,2-diisononyl phthalate | |
| CN103922901B (en) | The process for purification of polidocanol | |
| CN103012152B (en) | Production technique of diethylene glycol dibenzoate | |
| CN102351696B (en) | Process for synthesizing acetyl citrate | |
| CN111269113A (en) | Method for treating mixture containing long-chain dibasic acid, dibutyl long-chain dibasic acid mixture and application thereof | |
| CN110372504B (en) | Method for producing polybasic acid ester by recovering light components from side product of meta-anhydride | |
| CN103664618A (en) | Novel synthesis process of octyl 2-propylheptyl phthalate | |
| CN102643198B (en) | Preparation method of tripalmitin citrate | |
| CN103429307A (en) | Method for recovery of organic acid from dilute aqueous solution | |
| KR20160029026A (en) | Process for the preparation of 3-heptanol from a mixture containing 2-ehthylhexanal and 3-heptyl formate | |
| CN101906035A (en) | Refining method of high-purity butyl stearate | |
| CN102503824B (en) | Process for synthesizing long-chain acylated citrate | |
| CN101880232B (en) | Method for synthesizing environment-friendly plasticizer by using benzoic acid, diethylene glycol and isooctyl alcohol | |
| CN103102267B (en) | A kind of preparation method of pharmaceutic adjuvant grade Glyceryl Behenate | |
| CN114920642A (en) | Separation process for obtaining high-purity fatty acid monoglyceride and fatty acid diglyceride | |
| CN119552075B (en) | Method for preparing 1, 1-ethylene glycol diacetate | |
| CN105622679A (en) | Preparation method of edible tannic acid | |
| CN113214079A (en) | Production method of DPHP | |
| TWI588127B (en) | DINT plasticizer and its manufacturing method and use |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20210824 |
|
| RJ01 | Rejection of invention patent application after publication |