CN118290472A - Bisphenol A tetrachlorodiphosphate production method - Google Patents
Bisphenol A tetrachlorodiphosphate production method Download PDFInfo
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- CN118290472A CN118290472A CN202410345534.1A CN202410345534A CN118290472A CN 118290472 A CN118290472 A CN 118290472A CN 202410345534 A CN202410345534 A CN 202410345534A CN 118290472 A CN118290472 A CN 118290472A
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- Prior art keywords
- bisphenol
- tetrachlorodiphosphate
- tubular reactor
- phosphorus oxychloride
- mixed solution
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- IISBACLAFKSPIT-UHFFFAOYSA-N bisphenol A Chemical compound C=1C=C(O)C=CC=1C(C)(C)C1=CC=C(O)C=C1 IISBACLAFKSPIT-UHFFFAOYSA-N 0.000 title claims abstract description 138
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- XHXFXVLFKHQFAL-UHFFFAOYSA-N phosphoryl trichloride Chemical compound ClP(Cl)(Cl)=O XHXFXVLFKHQFAL-UHFFFAOYSA-N 0.000 claims abstract description 60
- 238000006243 chemical reaction Methods 0.000 claims abstract description 21
- 239000011259 mixed solution Substances 0.000 claims abstract description 17
- 239000003054 catalyst Substances 0.000 claims abstract description 11
- 239000000243 solution Substances 0.000 claims abstract description 11
- 238000003756 stirring Methods 0.000 claims abstract description 11
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 238000000967 suction filtration Methods 0.000 claims abstract description 7
- 238000004821 distillation Methods 0.000 claims abstract description 5
- 239000012295 chemical reaction liquid Substances 0.000 claims description 17
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical group [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 15
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 7
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 7
- 239000002841 Lewis acid Substances 0.000 claims description 3
- 150000007517 lewis acids Chemical class 0.000 claims description 3
- 229910001510 metal chloride Inorganic materials 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 239000002245 particle Substances 0.000 claims 1
- 239000000539 dimer Substances 0.000 abstract description 13
- 239000013638 trimer Substances 0.000 abstract description 13
- 230000002194 synthesizing effect Effects 0.000 abstract description 5
- BQPNUOYXSVUVMY-UHFFFAOYSA-N [4-[2-(4-diphenoxyphosphoryloxyphenyl)propan-2-yl]phenyl] diphenyl phosphate Chemical compound C=1C=C(OP(=O)(OC=2C=CC=CC=2)OC=2C=CC=CC=2)C=CC=1C(C)(C)C(C=C1)=CC=C1OP(=O)(OC=1C=CC=CC=1)OC1=CC=CC=C1 BQPNUOYXSVUVMY-UHFFFAOYSA-N 0.000 abstract description 4
- 238000010924 continuous production Methods 0.000 abstract description 4
- -1 tetrachloro diphosphate Chemical compound 0.000 abstract description 2
- 238000010025 steaming Methods 0.000 description 9
- 229930185605 Bisphenol Natural products 0.000 description 8
- 238000004090 dissolution Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 229910001629 magnesium chloride Inorganic materials 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 238000005086 pumping Methods 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- FAIAAWCVCHQXDN-UHFFFAOYSA-N phosphorus trichloride Chemical compound ClP(Cl)Cl FAIAAWCVCHQXDN-UHFFFAOYSA-N 0.000 description 4
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 239000003063 flame retardant Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 210000003298 dental enamel Anatomy 0.000 description 2
- 238000000227 grinding Methods 0.000 description 2
- 231100000053 low toxicity Toxicity 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000004677 Nylon Substances 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000004676 acrylonitrile butadiene styrene Substances 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 125000005340 bisphosphate group Chemical group 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000006471 dimerization reaction Methods 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 150000004712 monophosphates Chemical class 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 239000012994 photoredox catalyst Substances 0.000 description 1
- 239000004417 polycarbonate Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000005829 trimerization reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a production method of bisphenol A tetrachlorodiphosphate, which comprises the steps of heating bisphenol A, a catalyst and phosphorus oxychloride to 40-50 ℃, stirring and dissolving to obtain a mixed solution, heating the mixed solution to 80-90 ℃, reacting for 2-2.5 h to obtain a reaction solution, and sequentially carrying out suction filtration and reduced pressure distillation to obtain bisphenol A tetrachlorodiphosphate; the mass ratio of bisphenol A to phosphorus oxychloride is 1: 10-15. The method for producing bisphenol A tetrachloro diphosphate provided by the invention can be used for synthesizing high-quality bisphenol A-bis (diphenyl phosphate) by controlling the system concentration and the temperature while realizing continuous production, so that the reaction selectivity is greatly improved, and the production of dimers and trimers is effectively avoided.
Description
Technical Field
The invention belongs to the technical field of fine chemicals, and particularly relates to a production method of bisphenol A tetrachlorodiphosphate.
Background
Bisphenol A tetrachlorodiphosphate is an important intermediate for the synthesis of bisphenol A-bis (diphenyl phosphate) (BDP for short). BDP is an important organophosphorus flame retardant, is used as bisphosphate, has the advantages of migration resistance, volatilization resistance, radiation resistance, low toxicity, high durability and the like compared with a monophosphate flame retardant, and is widely applied to the preparation of various high polymer engineering plastics, such as PC, ABS, nylon, foam polyurethane and the like. BDP also meets the requirements of the market on the development of the flame retardant to halogen-free, efficient, low-smoke, low-toxicity and environment-friendly, and has strong market competitiveness.
Currently, the main methods for synthesizing BDP are: under the catalysis of Lewis acid, phosphorus oxychloride and bisphenol A react to obtain an intermediate bisphenol A tetrachlorodiphosphate, then phenol is used for blocking bisphenol A tetrachlorodiphosphate, and after post-treatment such as purification, the product BDP is prepared, and the synthetic route is as follows:
From the above formula, the first step of reaction produces intermediate bisphenol a tetrachlorodiphosphate and its oligomer and hydrochloric acid, and since bisphenol a tetrachlorodiphosphate is easy to polymerize, the oligomer with polymerization degree n=2 or 3 can continue to react to produce BDP, so that the product quality is reduced, and the polymerization degree n=1 of bisphenol a tetrachlorodiphosphate, which is an ideal intermediate; the reactants and the products have high melting boiling points, are solid at normal temperature, and are not beneficial to the reaction operation, especially in the condition that the whole reaction environment cannot contain water.
The patent CN101348500A and the patent CN116693572A both improve the feeding mode, use liquid feeding to replace solid feeding, and consider the absorption of the generated hydrogen chloride, so that the reaction process is more stable and safer; the patent CN106496264A and the patent CN112409404A respectively provide a continuous production method of bisphenol A-bis (diphenyl phosphate) on the basis, and the continuous production mode is used for replacing the intermittent kettle production mode, so that the production efficiency is effectively improved.
The above technical improvements all solve many of the technical barriers and problems of the existing production of BDP, but do not relate to how to avoid the problem of oligomer production, the resulting product is still a mixture of oligomers. From the course of the reaction, it can be seen that the control of BDP oligomer formation is critical in how to avoid further dimerization and trimerization of the intermediate bisphenol A tetrachlorodiphosphate. But so far there is no solution to the problem.
Disclosure of Invention
Aiming at the problem that a dimer or a trimer is easy to generate in the process of synthesizing an intermediate bisphenol A tetrachlorodiphosphate in the prior art, the invention provides a production method of bisphenol A tetrachlorodiphosphate, which improves the selectivity of generating bisphenol A tetrachlorodiphosphate monomers by reaction and can effectively avoid the generation of the dimer and the trimer.
The invention is realized by the following technical scheme:
a method for producing bisphenol a tetrachlorodiphosphate, comprising the steps of:
(1) Heating bisphenol A, a catalyst and phosphorus oxychloride to 40-50 ℃, stirring and dissolving to obtain a mixed solution;
(2) Heating the mixed solution in the step (1) to 80-90 ℃ and reacting for 2-2.5 h to obtain a reaction solution;
(3) And (3) sequentially carrying out suction filtration and reduced pressure distillation on the reaction liquid in the step (2) to obtain bisphenol A tetrachlorodiphosphate.
Further, in the step (2), the mixed solution is uniformly pumped into a tubular reactor, the temperature of the tubular reactor is kept at 80-90 ℃, and after 2-2.5 hours, the reaction solution flows out from an outlet of the tubular reactor.
Further, the flow rate of the mixed liquid uniformly injected into the tubular reactor is determined by the volume of the tubular reactor and the reaction time.
Further, the length of the tubular reactor is 200-500 m, and the inner diameter of the section is 5-15 cm.
Further, the length of the tubular reactor is 300-400 m, and the inner diameter of the section is 5-15 cm.
Further, the catalyst is metal chloride Lewis acid, and the granularity D50 is less than or equal to 0.4 mu m.
Further, the catalyst is anhydrous magnesium chloride or anhydrous ferric chloride.
Further, the mass ratio of bisphenol A to phosphorus oxychloride is 1: 10-15% of catalyst, wherein the dosage of the catalyst is 1-3% of the total feeding mass.
Further, the vacuum degree of the reduced pressure distillation in the step (3) is minus 90 to minus 80KPa.
The beneficial effects of the invention are as follows:
The method for producing bisphenol A tetrachloro diphosphate provided by the invention can be used for synthesizing high-quality bisphenol A-bis (diphenyl phosphate) by controlling the system concentration and the temperature while realizing continuous production, so that the reaction selectivity is greatly improved, and the production of dimers and trimers is effectively avoided.
Detailed Description
The above-described matters of the present invention will be described in further detail by way of examples, but it should not be construed that the scope of the above-described subject matter of the present invention is limited to the following examples, and all techniques realized based on the above-described matters of the present invention are within the scope of the present invention.
In the specific embodiment of the invention, the specification of partial equipment and materials is as follows:
The dissolution kettles are 10 cubic enamel kettles; the outer steaming kettles are all 5 cubic enamel kettles; the inner diameter of the tubular reactor is 10cm, and the length is 300m; bisphenol A content 99.9%; phosphorus oxychloride content 99.5%; the anhydrous magnesium chloride content is 99.9 percent, and the granularity D50 after grinding treatment is 0.35 mu m; the anhydrous ferric chloride content is 99.9%, and the granularity D50 after grinding treatment is 0.38 mu m.
Example 1
(1) Sequentially adding 10 tons of phosphorus trichloride, 1000kg of bisphenol A and 110kg of anhydrous magnesium chloride into a dissolution kettle, stirring, heating to 40 ℃, and continuing stirring for 20min to obtain a mixed solution; dissolution vessels ② and ③ were operated identically, in parallel with dissolution vessel ①;
(2) Pumping the mixed solution obtained in the step (1) into a tubular reactor according to the flow rate of 75L/min, keeping the internal temperature of the tubular reactor at 82+/-2 ℃, and after 2.09 hours, starting overflowing the reaction solution from the outlet of the tubular reactor;
(3) Filtering the overflowed reaction liquid in the step (2) by a suction filtration pump, sequentially pumping the filtrate into an external steaming kettle connected in parallel, and steaming out phosphorus oxychloride for reuse under the vacuum degree-90 KPa pressure, wherein the rest of the kettle is BDP to synthesize an intermediate bisphenol A tetrachlorodiphosphate.
Collecting the overflowed reaction liquid for 2 hours, and separating to obtain 155kg of wet magnesium chloride, 12.41 tons of phosphorus oxychloride and 2864kg of bisphenol tetrachlorodiphosphate; detecting the phosphorus oxychloride content 81.28%, the bisphenol A tetrachlorodiphosphate content 18.72%, the bisphenol A content 0, the dimer content 0 and the trimer content 0 in the reaction liquid overflowed from the outlet of the tubular reactor; the purity of the bisphenol A tetrachlorodiphosphate is 99.56%.
Example 2
(1) Sequentially adding 12 tons of phosphorus trichloride, 800kg of bisphenol A and 384kg of anhydrous magnesium chloride into a dissolution kettle, stirring, heating to 50 ℃, and continuing stirring for 20min to obtain a mixed solution;
(2) Pumping the mixed solution obtained in the step (1) into a tubular reactor according to the flow rate of 65L/min, keeping the internal temperature of the tubular reactor at 88+/-2 ℃, and starting overflowing of the reaction solution from an outlet of the tubular reactor after 2.41 hours;
(3) And (3) filtering the overflowed reaction liquid in the step (2) by a suction filtration pump, and steaming out phosphorus oxychloride in an external filtrate steaming kettle under the vacuum degree of-80 KPa pressure to recycle the phosphorus oxychloride, wherein BDP is remained in the kettle to synthesize an intermediate bisphenol A tetrachlorodiphosphate.
Collecting the overflowed reaction liquid for 2 hours, and separating to obtain 400kg of wet magnesium chloride, 11.50 tons of phosphorus oxychloride and 1732kg of bisphenol tetrachlorodiphosphate; detecting the phosphorus oxychloride content 86.94%, the bisphenol A tetrachlorodiphosphate content 13.06%, the bisphenol A content 0, the dimer content 0 and the trimer content 0 in the reaction liquid overflowed from the outlet of the tubular reactor; the purity of the bisphenol A tetrachlorodiphosphate is 99.53%.
Example 3
(1) Sequentially adding 10 tons of phosphorus trichloride, 1000kg of bisphenol A and 110kg of anhydrous ferric chloride into a dissolution kettle, stirring, heating to 40 ℃, and continuing stirring for 20min to obtain a mixed solution;
(2) Pumping the mixed solution obtained in the step (1) into a tubular reactor according to the flow rate of 75L/min, keeping the internal temperature of the tubular reactor at 82+/-2 ℃, and after 2.09 hours, starting overflowing the reaction solution from the outlet of the tubular reactor;
(3) And (3) filtering the overflowed reaction liquid in the step (2) by a suction filtration pump, and steaming out phosphorus oxychloride in an external filtrate steaming kettle under the vacuum degree of-90 KPa pressure to recycle the phosphorus oxychloride, wherein BDP is remained in the kettle to synthesize an intermediate bisphenol A tetrachlorodiphosphate.
Collecting the overflowed reaction liquid for 2 hours, and separating to obtain 155kg of wet ferric chloride, 12.34 tons of phosphorus oxychloride and 2945kg of bisphenol tetrachlorodiphosphate; detecting the content of phosphorus oxychloride in the reaction liquid overflowed from the outlet of the tubular reactor to be 80.75%, 19.25% of bisphenol A tetrachlorodiphosphate, 0% of bisphenol A, 0% of dimer and 0% of trimer; the purity of the bisphenol A tetrachlorodiphosphate is 99.60 percent.
Example 4
(1) Sequentially adding 12 tons of phosphorus trichloride, 800kg of bisphenol A and 384kg of anhydrous ferric chloride into a dissolution kettle, stirring, heating to 50 ℃, and continuing stirring for 20min to obtain a mixed solution;
(2) Pumping the mixed solution obtained in the step (1) into a tubular reactor according to the flow rate of 65L/min, keeping the internal temperature of the tubular reactor at 88+/-2 ℃, and starting overflowing of the reaction solution from an outlet of the tubular reactor after 2.41 hours;
(3) And (3) filtering the overflowed reaction liquid in the step (2) by a suction filtration pump, and steaming out phosphorus oxychloride in an external filtrate steaming kettle under the vacuum degree of-80 KPa pressure to recycle the phosphorus oxychloride, wherein BDP is remained in the kettle to synthesize an intermediate bisphenol A tetrachlorodiphosphate.
Collecting the overflowed reaction liquid for 2 hours, and separating to obtain 399kg of wet ferric chloride, 11.51 tons of phosphorus oxychloride and 1741kg of bisphenol tetrachlorodiphosphate; detecting the phosphorus oxychloride content 86.87%, the bisphenol A tetrachlorodiphosphate content 13.13%, the bisphenol A content 0, the dimer content 0 and the trimer content 0 in the reaction liquid overflowed from the outlet of the tubular reactor; the purity of the bisphenol A tetrachlorodiphosphate is 99.55%.
Comparative example 1
Unlike example 1, the mass ratio of bisphenol A and phosphorus oxychloride in step (1) of comparative example 1 is 1:5, and the other steps and conditions are the same as in example 1, and the 2h overflow liquid is collected and separated to obtain 154kg of wet magnesium chloride, 10.08 tons of phosphorus oxychloride and 5175kg of bisphenol tetrachlorodiphosphate;
through detection, the phosphorus oxychloride content in the overflowed reaction liquid is 66.29%, the bisphenol A tetrachlorodiphosphate content is 31.80%, the bisphenol A content is 0, the dimer content is 1.48, and the trimer content is 0.43; the purity of the bisphenol A tetrachlorodiphosphate is 94.33%.
Comparative example 2
Unlike example 1, the internal temperature of the tubular reactor in step 2 of comparative example 2 was 98.+ -. 2 ℃ and the remaining steps and conditions were the same as in example 1;
The overflow liquid is collected for 2 hours, 155kg of wet magnesium chloride, 12.60 tons of phosphorus oxychloride and 2691kg of bisphenol tetrachlorodiphosphate are separated.
Through detection, the phosphorus oxychloride content 82.41% in the overflowed reaction liquid, the bisphenol A tetrachlorodiphosphate content 14.38%, the bisphenol A content 0, the dimer content 2.67 and the trimer content 0.54; the purity of the bisphenol A tetrachlorodiphosphate is 81.75%.
Comparative example 3
Unlike example 1, the internal temperature of the tubular reactor in step 2 of comparative example 2 was 67.+ -. 2 ℃ and the remaining steps and conditions were the same as those of example 1.
Collecting 2h overflowed liquid, separating 155kg of wet magnesium chloride, 12.46 tons of phosphorus oxychloride, 2826kg of bisphenol tetrachlorodiphosphate;
Through detection, the phosphorus oxychloride content 81.53% in the overflowed reaction liquid, the bisphenol A tetrachlorodiphosphate content 15.65%, the bisphenol A content 2.82, the dimer content 0 and the trimer content 0; the purity of the bisphenol A tetrachlorodiphosphate is 84.73 percent.
The invention effectively avoids the generation of dimers and trimers by controlling the concentration and the reaction temperature of bisphenol A in the system, can obtain high-purity bisphenol tetrachlorodiphosphate, and can be used for synthesizing high-quality BDP. The bisphenol A concentration of the system is too high and the reaction temperature is too high, so that the formation of dimers and trimers can be promoted, and the bisphenol A reaction is incomplete due to the too low reaction temperature, so that the product yield and quality are affected.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (9)
1. A method for producing bisphenol a tetrachlorodiphosphate, comprising the steps of:
(1) Heating bisphenol A, a catalyst and phosphorus oxychloride to 40-50 ℃, stirring and dissolving to obtain a mixed solution;
(2) Heating the mixed solution in the step (1) to 80-90 ℃ and reacting for 2-2.5 h to obtain a reaction solution;
(3) And (3) sequentially carrying out suction filtration and reduced pressure distillation on the reaction liquid in the step (2) to obtain bisphenol A tetrachlorodiphosphate.
2. The method for producing bisphenol A tetrachlorodiphosphate according to claim 1, wherein in the step (2), the mixed solution is fed into a tubular reactor at a constant speed, the temperature of the tubular reactor is maintained at 80-90 ℃, and after 2-2.5 hours, the reaction solution flows out from the outlet of the tubular reactor.
3. The method for producing bisphenol A tetrachlorodiphosphate according to claim 2, wherein the flow rate of the mixed solution to be fed into the tubular reactor at a constant speed is determined by the volume of the tubular reactor and the reaction time.
4. The method for producing bisphenol A tetrachlorodiphosphate according to claim 2, wherein the tubular reactor has a length of 200 to 500m and a cross-sectional inner diameter of 5 to 15cm.
5. The method for producing bisphenol A tetrachlorodiphosphate according to claim 4, wherein the tubular reactor has a length of 300 to 400m and a cross-sectional inner diameter of 5 to 15cm.
6. The method for producing bisphenol A tetrachlorodiphosphate according to claim 1, wherein the catalyst is a metal chloride Lewis acid, and the particle size D50 is less than or equal to 0.4 μm.
7. The method for producing bisphenol A tetrachlorodiphosphate according to claim 6, wherein the catalyst is anhydrous magnesium chloride or anhydrous ferric chloride.
8. The method for producing bisphenol A tetrachlorodiphosphate according to claim 1, wherein the mass ratio of bisphenol A to phosphorus oxychloride is 1: 10-15% of catalyst, wherein the dosage of the catalyst is 1-3% of the total feeding mass.
9. The method for producing bisphenol A tetrachlorodiphosphate according to claim 1, wherein the vacuum degree of the reduced pressure distillation in the step (3) is-90 to-80 KPa.
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