WO2022213890A1 - 有机硅线性体生产工艺 - Google Patents
有机硅线性体生产工艺 Download PDFInfo
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- WO2022213890A1 WO2022213890A1 PCT/CN2022/084729 CN2022084729W WO2022213890A1 WO 2022213890 A1 WO2022213890 A1 WO 2022213890A1 CN 2022084729 W CN2022084729 W CN 2022084729W WO 2022213890 A1 WO2022213890 A1 WO 2022213890A1
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- Prior art keywords
- hydrolyzate
- heat exchange
- vacuum stripping
- decompression
- pretreatment
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- 238000000034 method Methods 0.000 title abstract description 22
- 230000008569 process Effects 0.000 title abstract description 13
- 238000004519 manufacturing process Methods 0.000 claims abstract description 23
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 22
- LIKFHECYJZWXFJ-UHFFFAOYSA-N dimethyldichlorosilane Chemical compound C[Si](C)(Cl)Cl LIKFHECYJZWXFJ-UHFFFAOYSA-N 0.000 claims abstract description 21
- 230000006837 decompression Effects 0.000 claims description 37
- 239000007788 liquid Substances 0.000 claims description 28
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 20
- 239000012535 impurity Substances 0.000 claims description 19
- 238000001816 cooling Methods 0.000 claims description 17
- 238000003860 storage Methods 0.000 claims description 15
- 239000011347 resin Substances 0.000 claims description 14
- 229920005989 resin Polymers 0.000 claims description 14
- 239000002808 molecular sieve Substances 0.000 claims description 10
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 10
- 238000011045 prefiltration Methods 0.000 claims description 9
- 239000000084 colloidal system Substances 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- -1 chlorine ions Chemical class 0.000 abstract description 5
- 239000000460 chlorine Substances 0.000 abstract description 4
- 229910052801 chlorine Inorganic materials 0.000 abstract description 4
- 239000003292 glue Substances 0.000 abstract description 4
- 229920000435 poly(dimethylsiloxane) Polymers 0.000 abstract description 3
- 229920013822 aminosilicone Polymers 0.000 abstract description 2
- 229920000642 polymer Polymers 0.000 abstract description 2
- 229920002545 silicone oil Polymers 0.000 abstract description 2
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 abstract description 2
- 229920002554 vinyl polymer Polymers 0.000 abstract description 2
- 108010009736 Protein Hydrolysates Proteins 0.000 abstract 1
- 239000000047 product Substances 0.000 abstract 1
- 238000001704 evaporation Methods 0.000 description 30
- 230000008020 evaporation Effects 0.000 description 30
- 239000011552 falling film Substances 0.000 description 23
- 238000000926 separation method Methods 0.000 description 16
- 230000000052 comparative effect Effects 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000009833 condensation Methods 0.000 description 5
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- 238000001179 sorption measurement Methods 0.000 description 5
- 238000006482 condensation reaction Methods 0.000 description 4
- 238000001514 detection method Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- KPUWHANPEXNPJT-UHFFFAOYSA-N disiloxane Chemical class [SiH3]O[SiH3] KPUWHANPEXNPJT-UHFFFAOYSA-N 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- HMMGMWAXVFQUOA-UHFFFAOYSA-N octamethylcyclotetrasiloxane Chemical compound C[Si]1(C)O[Si](C)(C)O[Si](C)(C)O[Si](C)(C)O1 HMMGMWAXVFQUOA-UHFFFAOYSA-N 0.000 description 3
- 238000005191 phase separation Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- XMSXQFUHVRWGNA-UHFFFAOYSA-N Decamethylcyclopentasiloxane Chemical compound C[Si]1(C)O[Si](C)(C)O[Si](C)(C)O[Si](C)(C)O[Si](C)(C)O1 XMSXQFUHVRWGNA-UHFFFAOYSA-N 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000009827 uniform distribution Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- IUMSDRXLFWAGNT-UHFFFAOYSA-N Dodecamethylcyclohexasiloxane Chemical compound C[Si]1(C)O[Si](C)(C)O[Si](C)(C)O[Si](C)(C)O[Si](C)(C)O[Si](C)(C)O1 IUMSDRXLFWAGNT-UHFFFAOYSA-N 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
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- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000004205 dimethyl polysiloxane Substances 0.000 description 1
- 235000013870 dimethyl polysiloxane Nutrition 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004255 ion exchange chromatography Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 150000003961 organosilicon compounds Chemical class 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000005498 polishing Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920001296 polysiloxane Polymers 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
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Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G77/00—Macromolecular compounds obtained by reactions forming a linkage containing silicon with or without sulfur, nitrogen, oxygen or carbon in the main chain of the macromolecule
- C08G77/04—Polysiloxanes
- C08G77/14—Polysiloxanes containing silicon bound to oxygen-containing groups
- C08G77/16—Polysiloxanes containing silicon bound to oxygen-containing groups to hydroxyl groups
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G77/00—Macromolecular compounds obtained by reactions forming a linkage containing silicon with or without sulfur, nitrogen, oxygen or carbon in the main chain of the macromolecule
- C08G77/04—Polysiloxanes
- C08G77/06—Preparatory processes
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G77/00—Macromolecular compounds obtained by reactions forming a linkage containing silicon with or without sulfur, nitrogen, oxygen or carbon in the main chain of the macromolecule
- C08G77/04—Polysiloxanes
- C08G77/32—Post-polymerisation treatment
- C08G77/34—Purification
Definitions
- the invention belongs to the field of organosilicon compound synthesis, and in particular relates to a production process for organosilicon linear bodies.
- the organosilicon rings and chloride ion content are lower than 1 ppm and low volatile content is obtained by subjecting dimethyldichlorosilane hydrolyzate to pretreatment and debasing. At 0.5% silicone linearizer.
- Dimethyldichlorosilane hydrolyzate is composed of 20%-80% linear siloxane (linear body) and 80%-20% cyclic siloxane (ring body).
- the traditional process of hydrolyzate treatment is cracking technology, such as Chinese patent applications CN101148455A, CN104119372A, CN104497035A, etc., wherein CN101148455A discloses hydrolyzate under basic catalyst conditions, the linear body and the ring body are opened chain and re-cyclized to produce the ring body , the cracking reaction needs to carry out a slag discharge every 7 days, and the process has the disadvantages of high unit consumption of hydrolyzate and high energy consumption.
- CN104031084B, CN105175730B, CN106083910B all propose to separate the hydrolyzate from the ring body and the linear body, and the obtained ring body and linear body are respectively used for the production of 110 glue and 107 glue.
- CN106083910B adopts the method of first-level vacuum (-80 ⁇ -95KPa) flash evaporation, and strictly controls the low temperature of 120-150 °C, although claim 4 limits the linear body content in the separated linear body to be 85-99% , but the data of its examples show that the separation temperature is controlled at 130-135 ° C, and the linear body content is between 90-93%, which cannot reach more than 98%.
- the treatment scheme of the dimethyldichlorosilane hydrolyzate in the prior art cannot make the volatile content in the linear product less than 1%, that is, the problem of low volatile content and high content has not been solved.
- the SVHC in the EU REACH regulations and standards has added octamethylcyclotetrasiloxane (D4), decamethylcyclopentasiloxane (D5), and dodecamethylcyclohexasiloxane (D6).
- D4 octamethylcyclotetrasiloxane
- D5 decamethylcyclopentasiloxane
- D6 dodecamethylcyclohexasiloxane
- the content must be less than 0.01%.
- the inventors of the present invention have found through research that controlling the content of impurities in the dimethyldichlorosilane hydrolyzate, especially the content of chlorine, will help to improve the operating conditions for the subsequent separation of the ring body and the linear body, and on the one hand, avoid the separation operation process.
- the decomposition or reaction of the neutral body enables the hydrolyzate to adapt to higher separation conditions, and provides a path for reducing the content of low volatile matter in the linear body after separation, thereby completing the present invention.
- the invention provides a production method of an organosilicon linear product, comprising:
- step S2 depressurize the hydrolyzate after the pretreatment in step S1, and separate the organosilicon ring body and the organosilicon linear body.
- the dimethyldichlorosilane hydrolyzate comes from the upstream process and has the meaning well known in the art, and it mainly contains 80-20% linear siloxane, 20-80% ring body (including octamethylcyclotetrasiloxane) alkane (D4), decamethylcyclopentasiloxane (D5), etc.) and other trace impurities, among which the main impurities include water, chloride ions, and hydrocarbons.
- the pretreatment in step S1 can adopt various separation means for removing impurities known in the art, including but not limited to filtration, adsorption, etc., such as filter filtration, activated carbon adsorption, molecular sieve adsorption, resin adsorption, etc., so
- the activated carbon, molecular sieve and resin can be the activated carbon, molecular sieve and resin commonly used in the art for adsorbing or filtering impurities such as chloride ions, such as D201 resin, D301 resin and the like.
- various separation means can be used in combination, such as activated carbon, molecular sieve and resin adsorption; another example is the combination of means for removing large particles of impurities and means for removing small molecular substances.
- the dimethyldichlorosilane hydrolyzate flows through the pretreatment device of the S1 step at a flow rate of 3-15 m 3 /h, preferably through the S1 step at a flow rate of 7-15 m 3 /h preprocessing device.
- a primary pre-filter is used to remove mechanical impurities and colloids in the hydrolyzate first; then a secondary treatment is performed, and activated carbon filters, molecular sieves and/or resins are used to adsorb ions including chloride ions. Impurities of small molecular substances.
- the secondary treatment one of the activated carbon filter, molecular sieve and resin can be optionally used, or a combination of the two or a combination of the three can be used.
- the secondary treatment uses resin.
- a backwashing system is simultaneously set in the pretreatment device to improve the impurity removal effect of the pretreatment.
- the chloride ion content in the hydrolyzate is controlled to be less than 1 ppm, preferably less than 0.5 ppm, through the S1 step pretreatment.
- the linear body content obtained after de-lowering at 200°C was reduced to 82%, which was far lower than the reason why the linear body content obtained in Example 2 at 150°C was 98%.
- the inventors have found that, if the chlorine content in the hydrolyzate is reduced to 1 ppm or less, especially 0.5 ppm or less, before the separation of the ring body and the linear body of the dimethyldichlorosilane hydrolyzate is carried out, the obtained The linear body has low impurity content, and is self-stabilized without condensation reaction, and such hydrolyzate can withstand higher de-low temperature, so that the separation of the ring body and the linear body can be carried out at a higher temperature, which greatly improves the The efficiency of linear separation is improved, especially the low volatile content is significantly reduced.
- a step S11 of preheating the pretreated hydrolyzate can be added in the S1 step and the S2 step, that is, the pretreated hydrolyzate obtained in the S1 step is heated
- the exchange device is preheated first, and the heat of the heat exchange device can be derived from the ring body and/or the linear body separated in step S2.
- the heat exchange device is an economizer.
- the pretreated hydrolyzate in the step S2, can be heated to the temperature required for dehydration under reduced pressure by using a preheating device, and then enters the dehydration device for dehydration under reduced pressure.
- the hydrolyzate is heated to 180-280°C, preferably between 190-280°C, more preferably between 200-280°C.
- the temperature for decompression in step S2 is preferably 190-280°C, more preferably 220-280°C.
- the vacuum stripping in the S2 step can adopt the devices commonly used in the art that can carry out vacuum stripping, including but not limited to flash evaporation devices, packed towers, falling film evaporation devices, etc., as long as the devices are set through the structure Or filler distribution, etc. to achieve uniform distribution of the hydrolyzate.
- the decompression stripping device can be a decompression stripping device, or a cascade connection of multiple decompression stripping devices, that is, one-stage decompression stripping can be performed, or two-stage or two-stage decompression stripping can be performed. The multi-stage decompression above the level is lowered.
- the S2 step adopts two-stage vacuum stripping
- the temperature range of the first-stage vacuum stripping is 180-280 °C, preferably 200-280 °C, more preferably 220-280 °C
- the pressure is ⁇ -0.0955MPa
- the temperature range of the second-stage decompression is 190-280°C, preferably 220-280°C, more preferably 240-280°C
- the pressure is ⁇ -0.0955MPa
- the second-stage decompression is The low temperature is higher than the temperature of the first stage vacuum stripping.
- the liquid is discharged from the bottom of the first-stage vacuum stripping device and enters the second-stage vacuum stripping device for vacuum stripping.
- the ring body and short linear body obtained by the second-stage decompression depressurization are discharged from the top of the second-stage decompression decompression device, and enter the condenser at the top of the device, and collected after condensation; the liquid obtained by the second-stage decompression decompression device Linear body discharge.
- the ring body obtained by the first-stage decompression and decompression, and the ring body and short linear body obtained by the second-stage decompression decompression can be collected in the storage device using the same set of condensers, or can be collected by separate condensers. into the corresponding independent storage device.
- step S2 adopts a series connection of a flash evaporation device and a vertical falling film evaporation device to carry out reduced pressure decontamination, wherein the temperature of the flash evaporation is in the range of 180-280 °C, preferably 200-280 °C, and more It is preferably 220-280°C, the temperature range of falling film evaporation is 190-280°C, preferably 220-280°C, more preferably 240-280°C, and the temperature of falling film evaporation is higher than that of flash evaporation.
- the dimethyldichlorosilane hydrolyzate preheated to 180-280°C is sent to the flash distillation unit, and the flash separation operation is realized under the condition of ⁇ -0.0955MPa.
- the ring bodies D4 and D5 are partially gasified and discharged from the top of the flash device, enter the condenser at the top of the flash device, and collected after condensation; while most of the linear bodies are in the liquid phase and are discharged from the bottom of the flash device.
- the bottom liquid of the flash evaporation device enters the vertical falling film evaporation device.
- the light components including the ring body and the short linear body in the bottom liquid are vaporized, and the linear components of the heavy components are evaporated.
- the gas remains liquid, and they enter the gas-liquid phase separation space at the bottom of the falling film evaporation device at the same time.
- the light component gas enters the condenser at the top of the flash evaporation device under vacuum, and is collected after condensation; the heavy component linear liquid is discharged.
- the heavy-component linear body liquid is pumped to the economizer through the linear body discharge pump, conducts heat exchange with the pretreated hydrolyzate, and is then cooled by the linear body cooling device before being sent to the linear body storage device.
- the rings obtained by flash evaporation, the rings and the short linear bodies obtained by falling film evaporation can be collected in a storage device in combination, or can be collected in corresponding independent storage devices respectively.
- the vertical falling film evaporator is conducive to the uniform distribution of materials, and is a more preferred decompression device.
- the ring bodies and short linear bodies collected in the S2 step can be used in other technological processes, including but not limited to: the process of manufacturing products with the ring bodies as raw materials; and the ring bodies are further separated to obtain more Single-component ring bodies.
- the ring body and short linear body obtained in step S2 are condensed by the condenser at the top of the lowering device and then enter the processing device, then pumped out by a pump, and sent to the ring body and short linear body after dewatering
- the storage device will be used in the next process.
- the aforementioned processing methods for the ring body and the short linear body are applicable to the combined ring body and the short linear body, and also applicable to the unmerged ring body, the unmerged ring body and the short linear body.
- the stripping device operates under vacuum conditions.
- a vacuum pipeline is installed on the upper part of the condenser to be connected with a vacuum pump, so as to provide the vacuum degree of the whole system of the stripping device.
- the step S2 can be repeated again through the return line until Among them, the low volatile content is less than 0.5% before discharging.
- the linear body separated in step S2 is cooled to 20-50°C and collected.
- the present invention further provides a production apparatus for the aforementioned production method of organosilicon linear bodies.
- the device includes: a dimethyldichlorosilane hydrolyzate pretreatment device and a decompression reduction device.
- the pretreatment device includes a primary prefilter and a secondary treatment device, the primary prefilter filters and removes mechanical impurities and colloids, and the secondary treatment device is an activated carbon filter , molecular sieves and/or resins.
- the vacuum stripping device comprises two-stage vacuum stripping equipment connected in series.
- the first-stage vacuum stripping device is a flash evaporation device
- the second-stage vacuum stripping device is a falling film evaporation device.
- a preheating device is installed between the pretreatment device and the vacuum stripping device.
- a heat exchange device is installed between the pretreatment device and the preheating device, and the heat exchange device is connected with the gas outlet and/or the liquid outlet of the vacuum stripping device.
- the heat exchange device When the heat exchange device is connected with the gas outlet or the liquid outlet of the vacuum stripping device, the heat exchange device has a set of pipes for passing the gas or liquid.
- the heat exchange device When the heat exchange device is connected with the gas outlet and the liquid outlet of the vacuum stripping device, the heat exchange device has two separate sets of pipes for passing the gas and the liquid respectively.
- the gas outlet of the vacuum stripping device when the gas outlet of the vacuum stripping device is not connected to the heat exchange device, it is directly connected to the condenser thereafter.
- the condenser When the gas outlet of the vacuum stripping device is connected to the heat exchange device, the condenser is connected behind the gas outlet of the heat exchange device.
- the gas outlet of the vacuum stripping device may be the gas outlet of all the vacuum stripping devices in the vacuum stripping device, or any one or more of them. A gas outlet of the vacuum decompression equipment.
- the condenser is connected to the loop treatment device.
- the ring handling device is connected to the ring storage device.
- the liquid outlet of the vacuum stripping device when the liquid outlet of the vacuum stripping device is not connected to the heat exchange device, it is directly connected to the cooling device thereafter.
- the cooling device When the liquid outlet of the vacuum stripping device is connected to the heat exchange device, the cooling device is connected behind the liquid outlet of the heat exchange device.
- the liquid outlet of the vacuum stripping device is the outlet of the vacuum stripping device of the last stage in the vacuum stripping device. Liquid outlet.
- the cooling device is connected to the wire storage device.
- the production device used in the aforementioned method for producing organosilicon linear bodies includes: a dimethyldichlorosilane hydrolyzate pretreatment device and a vacuum de-lowering device.
- the pretreatment device includes a primary prefilter and a secondary treatment device, the primary prefilter filters and removes mechanical impurities and colloids, and the secondary treatment device is an activated carbon filter, molecular sieve and/or resin.
- the vacuum stripping device is a flash evaporation device and a falling film evaporation device connected in series.
- a preheating device is installed between the pretreatment device and the vacuum stripping device.
- a heat exchange device is installed between the pretreatment device and the preheating device, and the heat exchange device is connected with the gas outlet and/or the liquid outlet of the vacuum stripping device.
- the gas discharge port of the vacuum stripping device is connected to the heat exchange device, the gas discharge port in the heat exchange device is connected to the condenser; when the gas discharge port of the vacuum stripping device is not connected to the heat exchanger
- the gas outlet is directly connected to the condenser.
- the liquid discharge port in the heat exchange device is connected to the cooling device; when the vacuum stripping device ( When the liquid outlet of the falling film evaporation device is not connected to the heat exchange device, the liquid outlet is directly connected to the cooling device.
- the condenser is connected to the loop treatment device.
- the ring handling device is connected to the ring storage device.
- the cooling device is connected to the wire storage device.
- the linear viscosity of the organosilicon obtained by the method of the present invention is 50-120 mm 2 /s, the volatile content is lower than 0.5%, and the chloride ion content is lower than 1 ppm.
- the linear body can be widely used in the production of organic silicon follow-up products such as low-ring content 107 glue, low-ring content amino silicone oil, low-ring content methyl silicone oil, and low-ring content vinyl silicone oil.
- organic silicon follow-up products such as low-ring content 107 glue, low-ring content amino silicone oil, low-ring content methyl silicone oil, and low-ring content vinyl silicone oil.
- the linear body of the present invention is a hydroxyl-terminated chain dimethylpolysiloxane mixture with a normal molecular weight distribution, which can be used as a raw material for downstream products of organic silicon, and has the advantages of short polymerization time and low volatile content.
- FIG. 1 Device and process flow diagram in the embodiment of the present invention
- the hydrolyzate tank is connected to the pretreatment device; the pretreatment device is connected to the economizer; the heat exchange pipeline inlet of the economizer is connected to the bottom outlet of the falling film evaporator, and the heat exchange pipeline outlet of the economizer is connected to the cooling device
- the cooler is connected to the wire tank, and the outlet of the economizer is connected to the preheater; the preheater is connected to the feed port of the flash tank; the top of the flash tank is connected to the condenser; the condenser is connected to the processing tank and the vacuum pump respectively;
- the processing tank is connected to the ring tank; the bottom discharge port of the flash tank is connected to the falling film evaporator; the top of the gas-liquid phase separation space at the bottom of the falling film evaporator is connected to the aforementioned condenser.
- the dimethyldichlorosilane hydrolyzate from the upstream process is stored in the hydrolyzate tank, and sent to the pretreatment device through the pipeline for pretreatment to reduce the chloride ion content.
- the pretreated hydrolyzate is sent to the economizer through the pipeline, and is preheated by heat exchange with the linear body from the bottom discharge source of the falling film evaporator.
- the preheated hydrolyzate is then sent to the preheater through the pipeline, heated to the flash temperature and sent to the flash tank.
- the ring body in the hydrolyzate is vaporized in the flash tank, discharged from the top of the flash tank, condensed by the condenser and collected into the treatment tank.
- the linear body of the hydrolyzate remains liquid in the flash tank, and is discharged from the bottom of the flash tank and sent to the falling film evaporator.
- the top of the vapor-liquid phase separation space at the bottom of the evaporator is discharged, and is condensed and collected into the treatment tank by the condenser.
- the liquid linear body is discharged from the bottom of the falling film evaporator, sent to the economizer for heat exchange with the pretreated hydrolyzate, and then sent to the cooler for cooling and collected in the linear body tank.
- the rings and short linear bodies in the treatment tank are sent to the ring body tank for storage.
- Dimethyldichlorosilane hydrolyzate with flow rate of 8 m 3 /h from upstream mainly contains 60% linear siloxane, 27% octamethylcyclotetrasiloxane (D4), 8% decamethylcyclopentasiloxane Alkane (D5), 3% D6, 1% D7 and other trace impurities, among which the main impurities include water, chloride ions and hydrocarbons.
- a primary pre-filter is used to remove mechanical impurities and colloids in the hydrolyzate, and D201 resin is used in the secondary treatment.
- the chloride ion content in the hydrolyzate after the filtration treatment was 1 ppm.
- the pretreated hydrolyzate is sent to the wire loop separation raw material storage tank, and is pumped to the economizer through the flash feed pump.
- the economizer exchanges heat with the high temperature linear product, and then the hydrolyzate is heated to 220°C in the preheater.
- the hydrolyzate is sent to the flash tank, and the flash separation is realized under the condition of negative pressure -0.098MPa.
- the ring bodies D4 and D5 are partially gasified and discharged from the top of the flash tank. The bottom of the flash tank is discharged.
- the ring body enters the gas phase tube of the flash tank and is condensed by the tower top condenser and then enters the treatment tank.
- the ring body is pumped out by a pump and sent to the ring body tank for use in the next process.
- a small amount of ring body is entrained in the linear body from the bottom of the flash tank, which is further processed by falling film evaporation at a temperature of 240 ° C and -0.098MPa to obtain a linear body, and then sent to the economizer through the discharge pump and pretreated.
- the hydrolyzate is subjected to heat exchange, and then cooled to normal temperature through a cooler, and sent to the product storage tank.
- the linear product structural formula that embodiment 1 obtains is The molecular weight is 4000-7000, showing a normal distribution, and the detection data are shown in Table 1.
- Example 2 The operation steps and related parameters of Example 2 are the same as those of Example 1, except that the flash evaporation temperature of Example 2 is 180°C, and the temperature of falling film evaporation is 200°C.
- Comparative Example 1 The experimental steps of Comparative Example 1 were the same as those of Example 1, except that the hydrolyzate was not pretreated, but was directly preheated, followed by flash evaporation and falling film evaporation, and the chloride ion content in the hydrolyzate was 3 ppm.
- Comparative Example 2 The experimental steps of Comparative Example 2 are the same as those of Example 2, except that the hydrolyzate is not pretreated, but directly preheated, followed by flash evaporation and falling film evaporation, and the chloride ion content in the hydrolyzate is 3 ppm.
- the kinematic viscosity is measured by the method of Q/LXAXJ 02. Volatile content was determined by the method of Q/LXAXJM 21. The chromaticity was measured by the method of Q/LXAXJM 01. D4, D5 and total ring content were determined by chromatography. Chloride ion content was determined by ion chromatography.
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Abstract
Description
Claims (10)
- 一种有机硅线性体产品的生产方法,其特征在于包括以下步骤:S1:对二甲基二氯硅烷水解物进行预处理以使预处理后的水解物中氯离子含量小于等于1ppm;S2:将步骤S1预处理后水解物进行减压脱低,分离其中的有机硅环体和有机硅线性体,所述减压脱低的温度为180-280℃,压力为≤-0.0955MPa。
- 如权利要求1所述的生产方法,其特征在于:S1步骤中二甲基二氯硅烷水解物以3-15m 3/h的流量流经S1步骤的预处理装置。
- 如权利要求1或2所述的生产方法,其特征在于:S1步骤中,首先利用一级预过滤器除去水解物中的机械杂质及胶体;随后进行二级处理,利用活性炭过滤器、分子筛和/或树脂,吸附包括氯离子在内的小分子物质杂质;优选,预处理装置里设置反冲洗系统。
- 如权利要求1-3任一项所述的生产方法,其特征在于:S2步骤采用两级减压脱低,第一级减压脱低的温度范围为180-280℃,优选为200-280℃,更优选为220-280℃,压力≤-0.0955MPa,第二级减压脱低的温度范围为190-280℃,优选为220-280℃,更优选为240-280℃,压力≤-0.0955MPa,并且第二级减压脱低的温度高于第一级减压脱低的温度。
- 如权利要求1-4任一项所述的生产方法,其特征在于:S2步骤中在水解物减压脱低前,将S1步骤预处理后的水解物加热到减压脱低所需温度后,再进入脱低装置进行减压脱低;优选,将S1步骤预处理后的水解物加热到180-280℃。
- 如权利要求1-5任一项所述的生产方法,其特征在于:在S1步骤和S2步骤中增加一个对预处理后水解物进行预加热的步骤S11,将S1步骤得到的预处理后水解物经过热交换装置先被预加热,所述热交换装置的热量来源于S2步骤分离出的环体和/或线性体。
- 如权利要求1-6任一项所述的生产方法,其特征在于:经过S2步骤脱低获得的线性体在低挥发份含量大于0.5%时,通过返料管线再次重复S2步骤,直至其中低挥发份低于0.5%后再出料。
- 用于权利要求1-7任一项所述生产方法的生产装置,其特征在于:所述装置包括二甲基二氯硅烷水解物预处理装置和减压脱低装置;优选,所述预处理装置和减压脱低装置之间安装有预热装置;优选,所述预处理装置和预热装置之间安装有热交换装置,所述热交换装置与减压脱低装置的气体出料口和/或液体出料口连接;优选,当所述减压脱低装置的气体出料口不连接热交换装置时,其后直接连接冷凝器;当所述减压脱低装置的气体出料口连接热交换装置时,所述冷凝器连接在热交换装置的气体排出口后;优选,所述冷凝器连接环体处理装置;优选,所述环体处理装置连接环体储存装置;优选,当所述减压脱低装置的液体出料口不连接热交换装置时,其后直接连接冷却装置;当所述减压脱低装置的液体出料口连接热交换装置时,所述冷却装置连接在热交换装置的液体排出口后;优选,所述冷却装置连接线体储存装置。
- 如权利要求8所述的生产装置,其特征在于,所述预处理装置包括一级预过滤器和二级处理装置,所述一级预过滤器过滤去除机械杂质和胶体,二级处理装置是活性炭过滤器、分子筛和/或树脂。
- 如权利要求8或9所述的生产装置,其特征在于,所述减压脱低装置是串联连接的两级减压脱低设备。
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