CN116351338A - System and method for preparing isocyanate alkoxy silane by phosgene method - Google Patents
System and method for preparing isocyanate alkoxy silane by phosgene method Download PDFInfo
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- CN116351338A CN116351338A CN202111608693.9A CN202111608693A CN116351338A CN 116351338 A CN116351338 A CN 116351338A CN 202111608693 A CN202111608693 A CN 202111608693A CN 116351338 A CN116351338 A CN 116351338A
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- YGYAWVDWMABLBF-UHFFFAOYSA-N Phosgene Chemical compound ClC(Cl)=O YGYAWVDWMABLBF-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 56
- 239000012948 isocyanate Substances 0.000 title claims abstract description 43
- 229910000077 silane Inorganic materials 0.000 title claims abstract description 37
- 150000002513 isocyanates Chemical class 0.000 title claims abstract description 33
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 125000003545 alkoxy group Chemical group 0.000 title claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 70
- 238000000926 separation method Methods 0.000 claims abstract description 43
- 239000012295 chemical reaction liquid Substances 0.000 claims abstract description 32
- 239000012043 crude product Substances 0.000 claims abstract description 24
- 230000003068 static effect Effects 0.000 claims abstract description 24
- -1 amino alkoxy silane Chemical compound 0.000 claims abstract description 20
- IQPQWNKOIGAROB-UHFFFAOYSA-N isocyanate group Chemical group [N-]=C=O IQPQWNKOIGAROB-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000006552 photochemical reaction Methods 0.000 claims abstract description 9
- 238000006243 chemical reaction Methods 0.000 claims description 43
- WYTZZXDRDKSJID-UHFFFAOYSA-N (3-aminopropyl)triethoxysilane Chemical compound CCO[Si](OCC)(OCC)CCCN WYTZZXDRDKSJID-UHFFFAOYSA-N 0.000 claims description 6
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 5
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 4
- 239000003960 organic solvent Substances 0.000 claims description 4
- HXLAEGYMDGUSBD-UHFFFAOYSA-N 3-[diethoxy(methyl)silyl]propan-1-amine Chemical compound CCO[Si](C)(OCC)CCCN HXLAEGYMDGUSBD-UHFFFAOYSA-N 0.000 claims description 3
- ZYAASQNKCWTPKI-UHFFFAOYSA-N 3-[dimethoxy(methyl)silyl]propan-1-amine Chemical compound CO[Si](C)(OC)CCCN ZYAASQNKCWTPKI-UHFFFAOYSA-N 0.000 claims description 3
- SJECZPVISLOESU-UHFFFAOYSA-N 3-trimethoxysilylpropan-1-amine Chemical compound CO[Si](OC)(OC)CCCN SJECZPVISLOESU-UHFFFAOYSA-N 0.000 claims description 3
- 230000035484 reaction time Effects 0.000 claims description 3
- MCAKKROLTDGMBJ-UHFFFAOYSA-N 3-(dibutoxymethylsilyl)propan-1-amine Chemical compound CCCCOC(OCCCC)[SiH2]CCCN MCAKKROLTDGMBJ-UHFFFAOYSA-N 0.000 claims description 2
- WYZYIDCEVFJCRO-UHFFFAOYSA-N 3-(dipropoxymethylsilyl)propan-1-amine Chemical compound CCCOC(OCCC)[SiH2]CCCN WYZYIDCEVFJCRO-UHFFFAOYSA-N 0.000 claims description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 2
- 239000003759 ester based solvent Substances 0.000 claims description 2
- ARKBFSWVHXKMSD-UHFFFAOYSA-N trimethoxysilylmethanamine Chemical compound CO[Si](CN)(OC)OC ARKBFSWVHXKMSD-UHFFFAOYSA-N 0.000 claims description 2
- 238000009775 high-speed stirring Methods 0.000 claims 2
- 150000008280 chlorinated hydrocarbons Chemical class 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 35
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 abstract description 21
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 abstract description 20
- 229910000041 hydrogen chloride Inorganic materials 0.000 abstract description 20
- 238000002360 preparation method Methods 0.000 abstract description 7
- 238000003756 stirring Methods 0.000 abstract description 2
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 description 16
- 239000012071 phase Substances 0.000 description 16
- 239000000243 solution Substances 0.000 description 14
- 239000000047 product Substances 0.000 description 13
- 238000004821 distillation Methods 0.000 description 11
- 230000000052 comparative effect Effects 0.000 description 8
- 150000001412 amines Chemical class 0.000 description 7
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 description 6
- 238000004458 analytical method Methods 0.000 description 6
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 5
- 238000005336 cracking Methods 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- FRGPKMWIYVTFIQ-UHFFFAOYSA-N triethoxy(3-isocyanatopropyl)silane Chemical compound CCO[Si](OCC)(OCC)CCCN=C=O FRGPKMWIYVTFIQ-UHFFFAOYSA-N 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 239000011230 binding agent Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 239000000706 filtrate Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000007086 side reaction Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 150000003512 tertiary amines Chemical class 0.000 description 3
- NBXZNTLFQLUFES-UHFFFAOYSA-N triethoxy(propyl)silane Chemical compound CCC[Si](OCC)(OCC)OCC NBXZNTLFQLUFES-UHFFFAOYSA-N 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- RFFLAFLAYFXFSW-UHFFFAOYSA-N 1,2-dichlorobenzene Chemical compound ClC1=CC=CC=C1Cl RFFLAFLAYFXFSW-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- OIFBSDVPJOWBCH-UHFFFAOYSA-N Diethyl carbonate Chemical compound CCOC(=O)OCC OIFBSDVPJOWBCH-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 230000001174 ascending effect Effects 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- MVPPADPHJFYWMZ-IDEBNGHGSA-N chlorobenzene Chemical group Cl[13C]1=[13CH][13CH]=[13CH][13CH]=[13CH]1 MVPPADPHJFYWMZ-IDEBNGHGSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 150000008282 halocarbons Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 238000004227 thermal cracking Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- LZDKZFUFMNSQCJ-UHFFFAOYSA-N 1,2-diethoxyethane Chemical compound CCOCCOCC LZDKZFUFMNSQCJ-UHFFFAOYSA-N 0.000 description 1
- RYHBNJHYFVUHQT-UHFFFAOYSA-N 1,4-Dioxane Chemical compound C1COCCO1 RYHBNJHYFVUHQT-UHFFFAOYSA-N 0.000 description 1
- QCQCHGYLTSGIGX-GHXANHINSA-N 4-[[(3ar,5ar,5br,7ar,9s,11ar,11br,13as)-5a,5b,8,8,11a-pentamethyl-3a-[(5-methylpyridine-3-carbonyl)amino]-2-oxo-1-propan-2-yl-4,5,6,7,7a,9,10,11,11b,12,13,13a-dodecahydro-3h-cyclopenta[a]chrysen-9-yl]oxy]-2,2-dimethyl-4-oxobutanoic acid Chemical compound N([C@@]12CC[C@@]3(C)[C@]4(C)CC[C@H]5C(C)(C)[C@@H](OC(=O)CC(C)(C)C(O)=O)CC[C@]5(C)[C@H]4CC[C@@H]3C1=C(C(C2)=O)C(C)C)C(=O)C1=CN=CC(C)=C1 QCQCHGYLTSGIGX-GHXANHINSA-N 0.000 description 1
- KXDHJXZQYSOELW-UHFFFAOYSA-M Carbamate Chemical compound NC([O-])=O KXDHJXZQYSOELW-UHFFFAOYSA-M 0.000 description 1
- CKDWPUIZGOQOOM-UHFFFAOYSA-N Carbamyl chloride Chemical compound NC(Cl)=O CKDWPUIZGOQOOM-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000005046 Chlorosilane Substances 0.000 description 1
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 description 1
- XSTXAVWGXDQKEL-UHFFFAOYSA-N Trichloroethylene Chemical group ClC=C(Cl)Cl XSTXAVWGXDQKEL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 125000005370 alkoxysilyl group Chemical group 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 150000001735 carboxylic acids Chemical class 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical class Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 125000003963 dichloro group Chemical group Cl* 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- JBTWLSYIZRCDFO-UHFFFAOYSA-N ethyl methyl carbonate Chemical compound CCOC(=O)OC JBTWLSYIZRCDFO-UHFFFAOYSA-N 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- VKYKSIONXSXAKP-UHFFFAOYSA-N hexamethylenetetramine Chemical compound C1N(C2)CN3CN1CN2C3 VKYKSIONXSXAKP-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000010606 normalization Methods 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000004451 qualitative analysis Methods 0.000 description 1
- 238000004445 quantitative analysis Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 125000005373 siloxane group Chemical group [SiH2](O*)* 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- UBOXGVDOUJQMTN-UHFFFAOYSA-N trichloroethylene Natural products ClCC(Cl)Cl UBOXGVDOUJQMTN-UHFFFAOYSA-N 0.000 description 1
- ILWRPSCZWQJDMK-UHFFFAOYSA-N triethylazanium;chloride Chemical compound Cl.CCN(CC)CC ILWRPSCZWQJDMK-UHFFFAOYSA-N 0.000 description 1
- YFTHZRPMJXBUME-UHFFFAOYSA-N tripropylamine Chemical compound CCCN(CCC)CCC YFTHZRPMJXBUME-UHFFFAOYSA-N 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
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Classifications
-
- 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
- B01J19/0006—Controlling or regulating processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic System
- C07F7/02—Silicon compounds
- C07F7/08—Compounds having one or more C—Si linkages
- C07F7/18—Compounds having one or more C—Si linkages as well as one or more C—O—Si linkages
- C07F7/1804—Compounds having Si-O-C linkages
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07F—ACYCLIC, CARBOCYCLIC OR HETEROCYCLIC COMPOUNDS CONTAINING ELEMENTS OTHER THAN CARBON, HYDROGEN, HALOGEN, OXYGEN, NITROGEN, SULFUR, SELENIUM OR TELLURIUM
- C07F7/00—Compounds containing elements of Groups 4 or 14 of the Periodic System
- C07F7/02—Silicon compounds
- C07F7/08—Compounds having one or more C—Si linkages
- C07F7/18—Compounds having one or more C—Si linkages as well as one or more C—O—Si linkages
- C07F7/1804—Compounds having Si-O-C linkages
- C07F7/1872—Preparation; Treatments not provided for in C07F7/20
- C07F7/1892—Preparation; Treatments not provided for in C07F7/20 by reactions not provided for in C07F7/1876 - C07F7/1888
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention provides a system and a method for preparing isocyanate alkoxy silane by a phosgene method, wherein the system comprises the following steps: photochemical reactor: carrying out photochemical reaction on amino alkoxy silane and phosgene; static gas-liquid separator: separating the reaction liquid flowing out of the photochemical reactor to obtain reaction liquid I and gas phase I; dynamic gas-liquid separator: the first reaction liquid is subjected to gas-liquid separation under stirring to obtain a crude product containing isocyanate group alkoxy silane and a second gas phase; crude buffer tank: collecting crude products of isocyanate group-containing alkoxysilane; and (3) rectifying tower: rectifying and separating the crude product to obtain isocyanate alkoxy silane; the tail gas recoverer: the first and second gas phases are collected, condensed and the resulting phosgene is returned to the photochemical reactor. The preparation method provided by the invention can rapidly reduce the content of phosgene and hydrogen chloride in the system, and can prepare the silane isocyanate with excellent performance with lower cost and higher efficiency.
Description
Technical Field
The invention relates to the technical field of preparation of silane isocyanate, in particular to a system and a method for preparing silane isocyanate by a phosgene method.
Background
Currently, most of the industrial processes for the manufacture of isocyanates are made by reacting amines with phosgene. In the reaction process, the amine and the carbonyl chloride firstly form carbamoyl chloride, and then generate one mole of isocyanate groups and simultaneously generate two mole equivalents of hydrogen chloride; at the same time, once hydrogen chloride is produced in the system, it reacts with the amine precursor, the intermediate, and the functional groups in the isocyanate product of the system to produce various byproducts.
Similar problems exist in the preparation of isocyanates containing siloxane groups, where after hydrogen chloride is generated, the hydrogen chloride reacts with the alkoxysilane groups in the isocyanate product to produce chlorosilanes and corresponding alcohols, resulting in the formation of other by-products, reducing the overall yield of the target isocyanate.
To solve the above problems, US patent 4654428 discloses the use of tertiary amines, such as triethylamine or tripropylamine, in the reaction mixture. In the method, hydrogen chloride is neutralized by tertiary amine to form amine hydrochloride, and the amine hydrochloride precipitate is filtered out by a filtering operation to obtain filtrate containing isocyanate products, and the filtrate is distilled continuously to obtain the isocyanate products. However, this method has a number of disadvantages; for example, because amine salts formed from tertiary amines and hydrogen chloride are typically high volume, low density and fluffy solids, they are difficult and expensive to dispose of. At the same time, the patent uses alkali metal salts or alkaline earth metal salts of carboxylic acids to treat the filtrate or distillate, and the additional treatment steps described above add cost to the process. In specific practice, to ensure an effective quenching of hydrogen chloride, this also requires the further increase in the cost of the process by the use of an excess of amine, which also requires an additional step of stripping the excess amine from the final product.
The prior art CN104334565a separates an alkoxysilyl group-containing isocyanate compound from the hydrochloride salt of the base obtained in the step by adding a base and then performing centrifugation or filtration operation. For example, taking raw material amine KH550 (aminopropyl triethoxysilane) as an example, the existing isocyanate product prepared by the phosgene method is easy to have dichloro and monochloro impurities, the yield and quality are affected, and the specific reaction process is as follows:
in the phosgene method preparation process, the silicon-oxygen bond in the 3-isocyanate propyl triethoxy silane is easy to continuously react with HCI produced by the reaction, the chlorinated byproducts are more active, the storage stability is poorer, and the polymerization phenomenon is more easy to react with water.
After the photochemical reaction of the conventional isocyanate (such as MDI, TDI, HDI) is finished, the post-treatment process of the reaction solution is carried out; firstly, phosgene is removed to achieve that the content of phosgene and hydrogen chloride in photochemical reaction liquid is lower than 100ppm, and the phosgene and hydrogen chloride are removed by distillation or rectification and other modes generally using a vacuum system, and if necessary, the phosgene and hydrogen chloride are replaced by a small amount of nitrogen purge. However, distillation or rectification and other modes need to be heated, and certain residence time is provided in a high-temperature section. Because of the different stability of the isocyanate, for the isocyanate group siloxane, the longer separation time can lead to the silicon-oxygen bond in the isocyanate group alkoxy silane to be replaced by chlorine, and methanol or ethanol in the system and the like can also continuously carry out side reaction with the isocyanate group, so that the yield of the product is greatly reduced.
It can be seen that in the actual industrial production of isocyanatoalkoxysilane by phosgenation, the residual phosgene and hydrogen chloride in the system can seriously affect the yield. Therefore, how to grasp the optimal technical conditions to increase the yield of isocyanate-based alkoxysilane has become a major problem in expanding the productivity.
Disclosure of Invention
In order to overcome the defects in the prior art, the invention adopts a phosgene method to replace the traditional cracking reaction to prepare the isocyanate-based alkoxysilane, and the method for rapidly separating phosgene and hydrogen chloride avoids the use of an acid binding agent, so that the prepared isocyanate-based alkoxysilane has less impurity content. The method of the invention can reduce the production cost and reduce the environmental hazard.
In order to achieve the purpose of the invention, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a system for preparing isocyanate-based alkoxysilane by phosgene method, the system comprising:
photochemical reactor: the method is used for carrying out photochemical reaction on amino alkoxy silane and phosgene;
static gas-liquid separator: the method comprises the steps of carrying out gas-liquid separation on a reaction liquid flowing out of the photochemical reactor to obtain a separated reaction liquid I and a separated gas phase I;
dynamic gas-liquid separator: the first reaction liquid is subjected to gas-liquid separation under stirring to obtain a separated crude product containing isocyanate alkoxy silane and a gas phase II;
crude buffer tank: for collecting the crude isocyanate group-containing alkoxysilane;
and (3) rectifying tower: the method is used for rectifying and separating the crude product to obtain isocyanate alkoxy silane;
the tail gas recoverer: and the phosgene gas inlet is used for collecting the gas phase I and the gas phase II, condensing the gas phase I and the gas phase II and returning the condensed phosgene to the photochemical reactor.
In the system for preparing isocyanate-based alkoxy silane by the phosgene method, the photochemical reactor is a tubular reactor, and the tubular reactor is selected from a microchannel tubular reactor or a tubular reactor internally filled with a spiral plate and/or a silk screen, and is used for increasing turbulent flow of fluid in the reactor so as to ensure that materials are mixed more uniformly.
In the system provided by the invention, the static gas-liquid separator in the system is selected from a separation tower, and the separation tower is filled with a baffle plate and/or a silk screen. The reaction liquid flows rapidly in the static separator with the combination of the baffle plate and the silk screen, and the flow direction is influenced by the complicated and tortuous channels to be tortuous and changeable, so that liquid drops are impacted on the surface of the equipment to be captured under the action of inertia force, gradually gathered downwards under the action of gravity and discharged through the bottom discharge pipe, and enter the dynamic gas-liquid separator. In some preferred embodiments, after passing through the static gas-liquid separator, the phosgene and hydrogen chloride content is reduced to less than 1%.
In the system provided by the invention, the dynamic gas-liquid separator mainly utilizes the principle of cyclone separation, and when the gas and the liquid are mixed and flow together, the centrifugal force suffered by the liquid is larger than that of the gas, and the liquid is adhered to the separation wall surface and is gathered downwards due to the action of gravity and then is discharged from the discharge pipe. In some embodiments, the dynamic gas-liquid separator in the system provided by the invention can be selected from cyclone separators; in some embodiments, the separation chamber in the dynamic gas-liquid separator is of an "inverted cone" configuration, with a cone angle of between 10 and 45 °, preferably between 25 and 30 °.
In some specific embodiments, the reaction solution I enters a high-speed rotating chamber (separation chamber) through a feed inlet at the bottom of the dynamic gas-liquid separator, the reaction solution I rotates at a high speed in the separation chamber to form a spiral ascending movement form, and the gas-liquid is gradually separated to obtain a crude product containing isocyanate alkoxy silane and a gas phase II in the spiral ascending process due to different supergravity influences. More specifically, the bottom of the dynamic gas-liquid separator is provided with a high-speed rotating disk driven by a motor, a liquid poking convex plate with a blade structure is arranged on the rotating disk, and the rotating speed of the cyclone disk is adjusted through the liquid poking convex plate.
In some specific embodiments, the degassed crude product is discharged to a crude product buffer tank for standby through an overflow port on a dynamic gas-liquid separator, and the content of phosgene and hydrogen chloride in the obtained crude product is reduced to below 100 ppm. The residual phosgene and hydrogen chloride gas move upwards along with the internal rotation flow, are discharged from an air outlet pipe at the upper part of the dynamic gas-liquid separator, enter a tail gas recoverer, are separated from the hydrogen chloride after being condensed, and return to a phosgene air inlet of the photochemical reactor.
In the system provided by the invention, the rectifying tower is a packed tower, the packing material is preferably stainless steel, and the theoretical plate number is 2-30, preferably 5-20.
In a second aspect, the present invention provides a method for preparing an isocyanatoalkoxysilane using the system described above, the method comprising the steps of:
a. reacting amino alkoxy silane with phosgene in an photochemical reactor to obtain a reaction solution containing isocyanate alkoxy silane;
b. the reaction liquid is separated in a static gas-liquid separator to obtain a reaction liquid I and a gas phase I;
condensing the obtained gas phase by a tail gas recoverer, and returning the obtained phosgene to the photochemical reactor;
the obtained reaction liquid flows into a dynamic gas-liquid separator for separation to obtain crude products containing isocyanate alkoxy silane and gas phase II; condensing the obtained gas phase II by a tail gas recoverer, and returning the obtained phosgene to the photochemical reactor;
c. and rectifying and separating the crude product containing the isocyanate group alkoxy silane by a rectifying tower to obtain the isocyanate group alkoxy silane.
In step a of the process of the invention, the temperature of the reaction is from 0 to 50 ℃, preferably from 0 to 30 ℃; the reaction time is 0.1 to 20min, preferably 1 to 5min; in some preferred embodiments, the molar amount of phosgene supplied in the reaction is 2 to 20 times, preferably 5 to 10 times, such as 2 times, 3 times, 8 times, 15 times the molar amount of aminoalkoxysilane.
In a specific embodiment of the process of the present invention, the aminoalkoxysilane is dissolved in an organic solvent to form an aminoalkoxysilane solution, and the reaction (i.e., photochemical reaction) is performed with phosgene; preferably, the mass content of the aminoalkoxysilane in the aminoalkoxysilane solution is 1-50%, preferably 3-30%; more preferably, the organic solvent may be selected from one or more of benzene, toluene, n-hexane, cyclohexane, halogenated hydrocarbon or ester solvents; wherein the halogenated hydrocarbon may be selected from dichloromethane, chlorobenzene, o-dichlorobenzene, chloroform or trichloroethylene; the ester solvent may be selected from methyl acetate or ethyl acetate; the ether solvent may be selected from diethyl ether, 1, 2-diethoxyethane or dioxane.
In some specific embodiments, the aminoalkoxysilane in the aminoalkoxysilane is selected from one or more of 3-aminopropyl trimethoxysilane, 3-aminopropyl triethoxysilane, 3-aminopropyl dibutoxymethylsilane, 3-aminopropyl dipropoxymethyl silane, 3-aminopropyl dimethoxymethylsilane, 3-aminopropyl diethoxymethylsilane, 1-aminomethyltrimethoxysilane, 1-aminomethyldimethoxymethylsilane, and 1-aminomethyldiethoxymethylsilane.
In the separation process of the step b of the method, the residence time of the reaction liquid in the static gas-liquid separator is 0.1-10 min, preferably 1-3 min; the residence time of the first reaction liquid in the dynamic gas-liquid separator is 0.1 to 10min, preferably 1 to 3min. In the preparation process, the residence time of the reaction liquid in the static gas-liquid separation process and the dynamic gas-liquid separation process is short, so that side reactions such as substitution of siloxane bonds in isocyanate alkoxy silane and the like are avoided, and the yield of products is improved.
In the separation process of the step b of the method, the absolute pressure of static gas-liquid separation and dynamic gas-liquid separation is 80-99 kPa; in some preferred embodiments, the absolute pressure of the static gas-liquid separation and the dynamic gas-liquid separation is 90-98 kPa, so that effective separation of HCl and residual phosgene in the reaction system can be ensured, and the separation and recovery of the subsequent phosgene are not facilitated if the pressure is too low.
In step b of the method of the present invention, the phosgene in the gas phase one and the gas phase two is recycled to the photochemical reactor after being recycled, specifically, the recycling method comprises condensation absorption and other steps to realize separation of the phosgene and the hydrogen chloride, the separation steps are well known to those skilled in the art, and specific operation processes are not repeated herein.
In step c of the method of the invention, the temperature of the rectification separation process is 100-200 ℃; the absolute pressure of the rectification separation is 0.1 to 10kPa, preferably 0.5 to 5kPa.
By adopting the technical scheme, the method has the following technical effects:
the system for preparing the silane isocyanate by the phosgene method has the advantages of small equipment volume and small liquid holdup, thereby achieving large separation treatment capacity and obvious treatment effect.
The method for preparing the silane isocyanate by the phosgene method provided by the invention can rapidly reduce the content of phosgene and hydrogen chloride in a system, and can prepare the silane isocyanate with excellent performance with lower cost and higher efficiency. Compared with the prior art, the preparation method of the invention does not use acid binding agent, does not generate solid waste such as waste salt and the like, has low production cost and high reaction yield, and has larger implementation value and environmental protection benefit.
Drawings
Fig. 1: the phosgene method of the invention is a flow chart for preparing isocyanate alkoxy silane.
Wherein, 1, photochemical reactor, 2, static gas-liquid separator, 3, dynamic gas-liquid separator, 4, crude buffer tank, 5, tail gas recoverer, 6, rectifying tower.
Detailed Description
For a better understanding of the technical solution of the present invention, the following examples are further described below, but the present invention is not limited to the following examples.
The following test methods were used in the examples and comparative examples of the present invention:
(1) Purity and chlorinated impurity content in isocyanatoalkoxysilane: performing qualitative and quantitative analysis by gas chromatography;
analysis and detection were performed on an Agilent7890B gas chromatograph under the following analytical test conditions:
chromatographic column: agilent19091J-413DP-5;
0℃-325℃(350℃):30m×320μm×0.25μm；
carrier gas: purified and dried high purity N 2 (purity is above 99.999%);
combustion gas: h 2 (purity is above 99.999%) with a flow rate of 40mL/min;
combustion-supporting gas: purified and dried air with the flow rate of 400mL/min;
tail blowing: n (N) 2 The flow rate is 30mL/min;
column flow rate: 1.2mL/min, split ratio 30:1, a step of;
column box temperature, sample inlet temperature, detector temperature: 280 ℃;
sample injection amount: 0.001mL.
(2) Conversion rate: according to the calculation of the gas chromatographic area normalization analysis result,
conversion = (area percent of 100-aminoalkoxysilane)/100 x 100%.
The isocyanate-based alkoxysilane was prepared as shown in fig. 1:
a. a microchannel tube reactor is used as a photochemical reactor 1, chlorobenzene solutions of KH550 (3-aminopropyl triethoxysilane) with different concentrations are prepared, the chlorobenzene solutions are slowly introduced through the top of the photochemical reactor 1, phosgene is introduced into the photochemical reactor through an air inlet of the photochemical reactor 1 for photochemical reaction, the temperature range of the reaction is controlled, and the molar quantity of phosgene supply is adjusted;
b. the separation tower filled with baffles is used as a static gas-liquid separator 2, the reaction liquid at the outlet of the photochemical reactor 1 is sent into a feed inlet of the static gas-liquid separator 2, the flow rate of the reaction liquid is regulated, the absolute pressure of the static gas-liquid separator 2 is controlled, and corrugated plate type stainless steel filler is filled in the static gas-liquid separator 2. The reaction liquid is atomized and sprayed into small liquid drops for gas-liquid separation, so that a reaction liquid I and a gas phase I are obtained; the gas phase I obtained after separation is conveyed to a tail gas recoverer 5;
the cyclone separator is adopted as a dynamic gas-liquid separator 3, and the reaction liquid flowing out of the outlet of the static gas-liquid separator 2 is conveyed to the feed inlet of the dynamic gas-liquid separator 3 through a pump, and the dynamic gas-liquid separator 3 with different cone angle angles is used; after the motor of the separator is started, the rotational speed of a rotational flow disc is adjusted, the crude product containing isocyanate group alkoxy silane is sent into a crude product buffer tank 4 through an upper overflow port, and the separated gas phase II is sent into a tail gas recoverer 5. The tail gas recoverer 5 obtains phosgene by condensation at-10 ℃ and recycles it to the air inlet of the photochemical reactor 1.
c. Distilling and separating the crude product containing the isocyanate group alkoxy silane in a rectifying tower 6 of 10 theoretical plates, wherein the distillation solvent is chlorobenzene, the distillation pressure is 10kPa, and the distillation temperature is 80 ℃; after chlorobenzene is removed by vacuum distillation, colorless liquid is obtained by vacuum distillation in a rectifying tower with 20 theoretical plates under the distillation pressure of 0.1kPa and the kettle temperature of 140 ℃, and the colorless liquid is 3-isocyanate propyl triethoxy silane.
Examples 1 to 6 and comparative examples 1 to 6 of the present invention were each prepared by the above-described method, examples 7 to 9 were prepared by the same method as example 3, except that 3-aminopropyl methyldiethoxysilane, 3-aminopropyl trimethoxysilane, 3-aminopropyl methyldimethoxysilane were used as reaction raw materials for the photochemical reaction, and the parameter settings and analysis data in the specific examples are shown in the following tables 1 to 3:
specifically, the parameters of phosgene flux, reaction section residence time, reaction temperature and the like in the photochemical reactor 1 and analytical data of the reaction liquid are shown in table 1:
TABLE 1
Note that: the "reaction concentration" in the table refers to the mass percent of KH550 in the chlorobenzene solution of KH 550; "phosgene/amine" refers to the ratio of the molar amount of phosgene supplied to the reaction to the molar amount of aminoalkoxysilane; "purity of reaction solution" means purity of reaction solution containing isocyanate group alkoxysilane.
Parameters such as pressure, flow rate and the like of the static gas-liquid separator 2, and analysis of the obtained reaction liquid I, and data are shown in Table 2;
TABLE 2
Note that: the "separator pressure" in the table refers to the pressure of the static gas-liquid separator.
The cone angle of the dynamic gas-liquid separator 3, the motor rotation speed, the pressure parameters in the separator and the analysis of the obtained crude product containing isocyanate alkoxy silane are carried out, and the data are shown in table 3;
TABLE 3 Table 3
Note that: the pressure, the rotating speed and the cone angle in the table all refer to parameter indexes of the dynamic gas-liquid separator; the "purity of crude product" in the table means the content of isocyanatoalkoxysilane in the crude product.
Comparative examples 7 to 9
Comparative examples 7-9A kettle type cold and hot liquid phase phosgene method was used, and 1L of a reaction apparatus with a stirrer and a thermometer was placed in a water bath. Then 30g KH550 (3-aminopropyl triethoxysilane) is dissolved in 270g chlorobenzene, and then added into a reaction device and stirred, and the temperature is controlled to be 5-30 ℃;
then, carbonyl chloride is led into a reaction device at the speed of 150L/h for carrying out cold-hot photochemical reaction, the cold reaction temperature is controlled to be 5-50 ℃, the reaction residence time is controlled to be 40min, then, the thermal reaction is carried out, the thermal reaction temperature is controlled to be 50-100 ℃, and the reaction residence time is controlled to be 150min; after the reaction is finished, an acid binding agent is used for binding acid, triethylamine is used for neutralizing the reaction liquid, centrifugal filtration is carried out, triethylamine hydrochloride is separated out, and the obtained crude product is subjected to the following separation operation. Distilling and separating the mixture in a rectifying tower with 10 theoretical plates, wherein the distillation solvent is chlorobenzene, the distillation pressure is 10kPa, the distillation temperature is 80 ℃, and after the chlorobenzene is removed by vacuum distillation, the colorless liquid obtained by vacuum rectification in a rectifying tower with 20 theoretical plates is obtained by the distillation pressure of 0.1kPa and the kettle temperature of 140 ℃, so as to obtain the 3-isocyanate propyl triethoxysilane product.
Specific reaction conditions and analytical data for comparative examples 7 to 9 above are shown in Table 4:
TABLE 4 Table 4
As can be seen from the analytical data of comparative examples 7 to 9, the side reaction continues during the existing preparation process, which results in enrichment of byproducts, resulting in poor product purity and low product yield.
Comparative example 10
Taking KH550 (3-aminopropyl triethoxysilane) as an example, synthesizing the isocyanate group alkoxysilane by a thermal cracking process, and dividing the process into two steps:
the first step: firstly, synthesizing [3- (triethoxysilyl) propyl ] ethyl carbamate (UPTS); KH550, diethyl carbonate and sodium carbonate catalyst are sequentially added into a reaction kettle, the molar ratio of the materials is 1:1.3:0.05, and the materials react for 6 hours at 60 ℃. After the reaction, adding phosphoric acid into the mixture in a molar ratio of 1:1 to quench the catalyst, wherein the purity of the UPTS is 88.3%.
After the synthesis is finished, the UPTS reaction solution is subjected to post-treatment, and firstly, light components such as ethanol, acetic acid and diethyl carbonate in the reaction solution are removed under the condition of 70 ℃/10 KPaA. And (3) after removing the light components, distilling and removing the weight of the UPTS crude product under the condition of 120 ℃/20PaA to obtain the UPTS crude product.
And a second step of: and (3) thermally cracking the crude carbamate (UPTS) obtained in the synthesis step. UPTS product and pyrolytic catalyst (zinc oxide) are added into a reaction kettle, cracking reaction is carried out under the condition of 180 ℃/3KPaA respectively, distillation and extraction are carried out continuously, the extracted fraction is UPTS/IPTS mixed solution, and the purity of the 3-isocyanatopropyl triethoxysilane (IPTS) product is 83.6%.
And (3) rectifying and separating the UPTS/IPTS mixed fraction obtained by cracking under the separation condition of 150 ℃/20PaA to obtain a final isocyanato-alkoxy silane product, wherein the total yield is 58.6%.
In the cracking method of comparative example 10, the reaction steps are more, the auxiliaries such as a catalyst, a quencher and the like are used, the reaction time is longer, the energy consumption is higher, the thermal cracking process is difficult to control, the yield is low, the three wastes are difficult to treat, and the phosgene method has more advantages.
Claims (10)
1. A system for preparing isocyanate-based alkoxysilane by a phosgene method, the system comprising:
photochemical reactor (1): the method is used for carrying out photochemical reaction on amino alkoxy silane and phosgene;
static gas-liquid separator (2): the method comprises the steps of carrying out gas-liquid separation on a reaction liquid flowing out of an photochemical reactor (1) to obtain a separated reaction liquid I and a separated gas phase I;
dynamic gas-liquid separator (3): the first reaction liquid is subjected to gas-liquid separation under high-speed stirring to obtain a separated crude product containing isocyanate alkoxy silane and a gas phase II;
crude buffer tank (4): for collecting the crude isocyanate group-containing alkoxysilane;
rectifying column (6): the method is used for rectifying and separating the crude product to obtain isocyanate alkoxy silane;
tail gas recoverer (5): and the phosgene is used for collecting the gas phase I and the gas phase II, condensing the gas phase I and the gas phase II, and returning the condensed phosgene to the phosgene inlet of the photochemical reactor (1).
2. The system according to claim 1, characterized in that the photochemical reactor (1) is a tubular reactor;
the tubular reactor is selected from a microchannel tubular reactor or a tubular reactor internally filled with spiral plates and/or wire mesh.
3. System according to claim 1 or 2, characterized in that the static gas-liquid separator (2) in the system is selected from a separation column, which is filled with baffles and/or wire mesh.
4. A system according to claim 3, characterized in that the dynamic gas-liquid separator (3) in the system is selected from cyclone separators;
the separation chamber in the dynamic gas-liquid separator (3) is of a conical structure, and the cone angle of the separation chamber is 10-45 degrees, preferably 25-30 degrees.
5. A process for preparing isocyanatoalkoxysilanes using the system of any of claims 1 to 4, comprising the steps of:
a. reacting amino alkoxy silane with phosgene in an photochemical reactor (1) to obtain a reaction solution containing isocyanate alkoxy silane;
b. the reaction liquid is separated in a static gas-liquid separator (2) to obtain a reaction liquid I and a gas phase I;
after condensing the obtained gas phase by a tail gas recoverer (5), returning the obtained phosgene to the photochemical reactor (1);
the obtained reaction liquid flows into a dynamic gas-liquid separator (3) for separation to obtain crude products containing isocyanate alkoxy silane and gas phase II; condensing the obtained gas phase II by a tail gas recoverer (5), and returning the obtained phosgene to the photochemical reactor (1);
c. and (3) rectifying and separating the crude product containing the isocyanate group alkoxy silane by a rectifying tower (6) to obtain the isocyanate group alkoxy silane.
6. The process according to claim 5, characterized in that in step a the temperature of the reaction is between 0 and 50 ℃, preferably between 0 and 30 ℃; the reaction time is 0.1 to 20min, preferably 1 to 5min;
more preferably, the phosgene is supplied in a molar amount of 2 to 20 times, preferably 5 to 10 times the molar amount of the aminoalkoxysilane in the reaction.
7. The method of claim 6, wherein in step a, said reacting with phosgene is performed after said aminoalkoxysilane is dissolved in an organic solvent to form an aminoalkoxysilane solution;
preferably, in the aminoalkoxysilane solution, the mass content of the aminoalkoxysilane is 1-50%, preferably 3-30%;
more preferably, the aminoalkoxysilane is selected from one or more of 3-aminopropyl trimethoxysilane, 3-aminopropyl triethoxysilane, 3-aminopropyl dibutoxymethylsilane, 3-aminopropyl dipropoxymethylsilane, 3-aminopropyl dimethoxymethylsilane, 3-aminopropyl diethoxymethylsilane, 1-aminomethyltrimethoxysilane, 1-aminomethyldimethoxymethylsilane and 1-aminomethyldiethoxymethylsilane;
the organic solvent is selected from one or more of benzene, toluene, n-hexane, cyclohexane, chlorinated hydrocarbon or ester solvents.
8. The method according to any one of claims 5 to 7, characterized in that the residence time of the reaction liquid in the static gas-liquid separator (2) during the separation of step b is 0.1 to 10min, preferably 1 to 3min;
the residence time of the reaction liquid I in the dynamic gas-liquid separator (3) is 0.1-10 min, preferably 1-3 min;
more preferably, during the separation in step b, the absolute pressure of the static gas-liquid separator (2) and the dynamic gas-liquid separator (3) is 80 to 99kPa, preferably 90 to 98kPa.
9. The method according to claim 8, characterized in that during the separation of step b, the flow rate of the reaction liquid into the static gas-liquid separator (2) is 0.5-3 mL/s;
the flow rate of the reaction liquid flowing into the dynamic gas-liquid separator (3) is 0.5-3 mL/s; preferably, the rotating speed of high-speed stirring in the dynamic gas-liquid separator (3) is 300-3000 r/min.
10. The method according to claim 9, wherein in step c, the temperature of the rectification separation is 100-200 ℃;
the absolute pressure of the rectification separation is 0.1 to 10kPa, preferably 0.5 to 5kPa.
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