CN105837612B - A kind of production method and production system of γ-chloropropyl trichloro-silane - Google Patents
A kind of production method and production system of γ-chloropropyl trichloro-silane Download PDFInfo
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- CN105837612B CN105837612B CN201610054939.5A CN201610054939A CN105837612B CN 105837612 B CN105837612 B CN 105837612B CN 201610054939 A CN201610054939 A CN 201610054939A CN 105837612 B CN105837612 B CN 105837612B
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 31
- OOXSLJBUMMHDKW-UHFFFAOYSA-N trichloro(3-chloropropyl)silane Chemical compound ClCCC[Si](Cl)(Cl)Cl OOXSLJBUMMHDKW-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 47
- 239000003054 catalyst Substances 0.000 claims abstract description 36
- 239000012043 crude product Substances 0.000 claims abstract description 26
- 230000035484 reaction time Effects 0.000 claims abstract description 9
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 claims description 28
- ZDHXKXAHOVTTAH-UHFFFAOYSA-N trichlorosilane Chemical compound Cl[SiH](Cl)Cl ZDHXKXAHOVTTAH-UHFFFAOYSA-N 0.000 claims description 27
- 239000005052 trichlorosilane Substances 0.000 claims description 26
- 230000003068 static effect Effects 0.000 claims description 15
- 229910052710 silicon Inorganic materials 0.000 claims description 5
- 239000010703 silicon Substances 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims 1
- 239000000460 chlorine Substances 0.000 claims 1
- 229910052801 chlorine Inorganic materials 0.000 claims 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000004913 activation Effects 0.000 abstract description 3
- 238000003860 storage Methods 0.000 description 12
- 238000000034 method Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- -1 γ-chloropropyl Chemical group 0.000 description 3
- 239000006087 Silane Coupling Agent Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000004587 chromatography analysis Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000002815 homogeneous catalyst Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- WYTZZXDRDKSJID-UHFFFAOYSA-N (3-aminopropyl)triethoxysilane Chemical compound CCO[Si](OCC)(OCC)CCCN WYTZZXDRDKSJID-UHFFFAOYSA-N 0.000 description 1
- HHXYJYBYNZMZKX-PYQRSULMSA-N 22(29)-Hopene Chemical compound C([C@]1(C)[C@H]2CC[C@H]34)CCC(C)(C)[C@@H]1CC[C@@]2(C)[C@]4(C)CC[C@@H]1[C@]3(C)CC[C@@H]1C(=C)C HHXYJYBYNZMZKX-PYQRSULMSA-N 0.000 description 1
- VXEGSRKPIUDPQT-UHFFFAOYSA-N 4-[4-(4-methoxyphenyl)piperazin-1-yl]aniline Chemical compound C1=CC(OC)=CC=C1N1CCN(C=2C=CC(N)=CC=2)CC1 VXEGSRKPIUDPQT-UHFFFAOYSA-N 0.000 description 1
- ACJJZEUIOAXCJJ-UHFFFAOYSA-N C(CC)[Si](Cl)(Cl)Cl.[Cl] Chemical compound C(CC)[Si](Cl)(Cl)Cl.[Cl] ACJJZEUIOAXCJJ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- BGPCFXZWLWDDDU-UHFFFAOYSA-N chloro(propyl)silane Chemical compound CCC[SiH2]Cl BGPCFXZWLWDDDU-UHFFFAOYSA-N 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- YJVFFLUZDVXJQI-UHFFFAOYSA-L palladium(ii) acetate Chemical compound [Pd+2].CC([O-])=O.CC([O-])=O YJVFFLUZDVXJQI-UHFFFAOYSA-L 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 125000001436 propyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 229910000077 silane Inorganic materials 0.000 description 1
- 239000005049 silicon tetrachloride Substances 0.000 description 1
Classifications
-
- 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 Table
- C07F7/02—Silicon compounds
- C07F7/08—Compounds having one or more C—Si linkages
- C07F7/12—Organo silicon halides
- C07F7/121—Preparation or treatment not provided for in C07F7/14, C07F7/16 or C07F7/20
- C07F7/122—Preparation or treatment not provided for in C07F7/14, C07F7/16 or C07F7/20 by reactions involving the formation of Si-C linkages
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
Abstract
The present invention provides the production method and production system of a kind of γ-chloropropyl trichloro-silane, which includes tubular reactor；Tank reactor, the entrance of the tank reactor are connected with the outlet of the tubular reactor；The first outlet of the tank reactor is connected with the first entrance of the tubular reactor；Rectifier unit, the entrance of the rectifier unit are connected with the second outlet of the tank reactor.Compared with prior art, the part crude product of tank reactor is returned to tubular reactor by the present invention, is reacted with the catalyst of activation to start, is reduced catalyst start-up course, can shorten the reaction time, reduce the dosage of catalyst；Crude product part in tank reactor is returned into tubular reactor simultaneously, the temperature in tubular reactor is maintained by its heat, reduces energy consumption；And the selectivity of reaction can also be improved by the reaction temperature in control tubular reactor, the reaction temperature improved in tank reactor promotes fully reacting.
Description
Technical field
The invention belongs to chemical reagent preparation technical field more particularly to a kind of producers of γ-chloropropyl trichloro-silane
Method and production system.
Background technique
γ-chloropropyl trichloro-silane is monomer most basic in silane coupling agent, can be deep using it as main production raw material
The products such as tens kinds of high-grade silane coupling agents are processed, such as aminopropyl triethoxysilane (KH-550), bis- (triethoxysilicanes
Propyl) tetrasulfide (Si-69) etc..γ-chloropropyl trichloro-silane is to be added using chloropropene and trichlorosilane as raw material by silicon hydrogen
At reacting, Main By product has propylene, silicon tetrachloride and propyl chlorosilane.
Since γ-chloropropyl trichloro-silane realizes industrialized production, both at home and abroad around catalyst, optimization reaction condition,
It reduces the hot research problems such as cost, raising yield never to interrupt the study on the synthesis of the product, although proposing more
Kind has the technique and scheme of theoretical research value, but just using trichlorosilane and chloropropene as Material synthesis γ-chloropropyl trichlorine silicon
For alkane, there is the process program of industrial application value and few, wherein can be divided by taking homogeneous catalyst synthesis technology as an example
Still reaction, pipe reaction etc., advantage and disadvantage are shown in Table 1.
The existing industrialization continuous production γ-chloropropyl trichloro-silane technique comparison of table 1
Summary of the invention
In view of this, the technical problem to be solved in the present invention is that providing that a kind of reaction efficiency is preferable and energy consumption is less
γ-chloropropyl trichloro-silane production method and production system.
The present invention provides a kind of production systems of γ-chloropropyl trichloro-silane, comprising:
Tubular reactor；
Tank reactor, the entrance of the tank reactor are connected with the outlet of the tubular reactor；The autoclave
The first outlet of reactor is connected with the first entrance of the tubular reactor；
Rectifier unit, the entrance of the rectifier unit are connected with the second outlet of the tank reactor.
It preferably, further include static mixer；The outlet of the static mixer enters with the second of the tubular reactor
Mouth is connected.
It preferably, further include metering pump；The first outlet of the tank reactor passes through metering pump and the pipe reaction
The first entrance of device is connected.
It preferably, further include condenser；The entrance of the condenser is connected with the outlet of the third of the tank reactor.
Preferably, the tubular reactor outer surface is provided with heat transfer medium.
The present invention also provides a kind of production methods of γ-chloropropyl trichloro-silane, comprising:
A chloropropene, trichlorosilane are passed through with catalyst) and reacted into tubular reactor, it is anti-subsequently into autoclave
It answers device to be reacted, obtains crude product；
B) a part of the crude product be back in tubular reactor mixed with chloropropene, trichlorosilane and catalyst after
Continuous reaction, another part, which enters, carries out rectifying in rectifier unit, obtain γ-chloropropyl trichloro-silane.
Preferably, the temperature reacted in the tubular reactor is 65 DEG C~82 DEG C, and the reaction time is 0.1~1h.
Preferably, the temperature reacted in the tank reactor is 80 DEG C~90 DEG C, and the reaction time is 1~3h.
Preferably, the step B) in chloropropene, trichlorosilane and catalyst gross mass and be back to tubular reactor
The mass ratio of middle crude product is (2~1): 1.
Preferably, the step A) in specifically:
Chloropropene, trichlorosilane are mixed with catalyst, mixed liquor is obtained, is then passed through and is carried out into tubular reactor again
Reaction, is reacted subsequently into tank reactor, obtains crude product；In the mixed liquor concentration of catalyst be 10~
200ppm。
The present invention provides the production method and production system of a kind of γ-chloropropyl trichloro-silane, which includes:
Tubular reactor；Tank reactor, the entrance of the tank reactor are connected with the outlet of the tubular reactor；The kettle
The first outlet of formula reactor is connected with the first entrance of the tubular reactor；Rectifier unit, the rectifier unit enter
Mouth is connected with the second outlet of the tank reactor.Compared with prior art, the present invention is thick by the part of tank reactor
Product returns to tubular reactor reuse, and catalyst therein has been activated, then is directly mixed with the raw material in tubular reactor,
It is reacted with the catalyst of activation to start, reduces catalyst start-up course, the reaction time can be shortened, reduce the use of catalyst
Amount, stabilizes reaction system；Meanwhile the reaction is exothermic reaction, reaction system of the present invention is by crude product part in tank reactor
Tubular reactor is returned to, the temperature in tubular reactor is maintained by its heat, reduces energy consumption；Also, it can also pass through
The reaction temperature in tubular reactor is controlled to improve the selectivity of reaction, the reaction temperature improved in tank reactor promotes instead
Conversion ratio should be improved completely.
Detailed description of the invention
Fig. 1 is γ of the present invention-chloropropyl trichloro-silane production system schematic diagram.
Specific embodiment
Below in conjunction with the attached drawing of the embodiment of the present invention, technical solution in the embodiment of the present invention carries out clear, complete
Ground description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.Based on this
Embodiment in invention, every other reality obtained by those of ordinary skill in the art without making creative efforts
Example is applied, shall fall within the protection scope of the present invention.
The present invention provides a kind of production systems of γ-chloropropyl trichloro-silane characterized by comprising pipe reaction
Device；Tank reactor, the entrance of the tank reactor are connected with the outlet of the tubular reactor；The tank reactor
First outlet be connected with the first entrance of the tubular reactor；Rectifier unit, the entrance of the rectifier unit with it is described
The second outlet of tank reactor is connected.
It is also preferable to include static mixer, the outlets of the static mixer and the second of the tubular reactor by the present invention
Entrance is connected.
It is also preferable to include catalyst storage tank, chloropropene storage tank and trichlorosilane storage tanks；The outlet of the catalyst storage tank with
The first entrance of the static mixer is connected；The outlet and the second entrance of the static mixer of the chloropropene storage tank
It is connected；The outlet of the trichlorosilane storage tank is connected with the third entrance of the static mixer.
It is also preferable to include the first metering pump, the second metering pump and third metering pumps by the present invention；The catalyst storage tank goes out
Mouth is connected by first metering pump with the first entrance of the static mixer；The outlet of the chloropropene storage tank passes through
Second metering pump is connected with the second entrance of the static mixer；The outlet of the trichlorosilane storage tank passes through described
Third metering pump is connected with the third entrance of the static mixer.First metering pump, the second metering pump and third metering pump
For controlling catalyst, chloropropene and the additional amount of trichlorosilane respectively, mix three in proportion in static mixer, so
After enter back into tubular reactor, and then entered in tank reactor by the outlet of tubular reactor.
The tubular reactor outer surface is preferably additionally provided with heat transfer medium, and heat is carried out using it as external circulating device and is turned
Move, thus make in tank reactor flow back crude product bring heat transfer to entire tubular reactor, to maintain pipe reaction
The reaction temperature of device makes entirely reaction not need to heat, reduces energy consumption.
It is also preferable to include metering pump in the present invention, the first outlet of the tank reactor passes through metering pump and the tubular type
The first entrance of reactor is connected.Reaction product in tank reactor can be back in tubular reactor by metering pump.
It is also preferable to include condensers for production system of the present invention；The third of the entrance of the condenser and the tank reactor
Outlet is connected.The by-product propylene reacted in tank reactor can leave production system by condenser, while unreacted
Trichlorosilane can also be condensed back by condenser into tank reactor that the reaction was continued, so as to reduce by-product propylene trichlorine
The amount of silane.
The second outlet of the tank reactor is connected with the rectifier unit.Reaction product one in tank reactor
Part is back in tubular reactor by first outlet, remaining enters rectifier unit and carries out rectifying.
The part crude product of tank reactor is returned to tubular reactor reuse by the present invention, and catalyst therein is lived
Change, then directly mixed with the raw material in tubular reactor, is reacted with the catalyst of activation to start, reduce catalyst and started
Journey can shorten the reaction time, reduce the dosage of catalyst, stabilize reaction system；Meanwhile the reaction is exothermic reaction, this hair
Crude product part in tank reactor is returned to tubular reactor by bright reaction system, is maintained in tubular reactor by its heat
Temperature reduces energy consumption；Also, the selectivity of reaction can also be improved by the reaction temperature in control tubular reactor,
The reaction temperature improved in tank reactor promotes fully reacting, improves conversion ratio.
γ-chloropropyl trichloro-silane method is produced using above-mentioned production system the present invention also provides a kind of, comprising: A)
Chloropropene, trichlorosilane are passed through with catalyst and reacted into tubular reactor, is carried out subsequently into tank reactor anti-
It answers, obtains crude product；B) a part of the crude product is back in tubular reactor and chloropropene, trichlorosilane and catalyst
The reaction was continued for mixing, and another part, which enters, carries out rectifying in rectifier unit, obtain γ-chloropropyl trichloro-silane.
The present invention is not particularly limited the source of reaction raw materials, is commercially available；The catalyst is this field
Homogeneous catalyst known to technical staff has no special limitation, is preferably chloroplatinic acid and/or palladium acetate in the present invention.
The present invention preferably mixes chloropropene, trichlorosilane with catalyst, obtains mixed liquor, is then passed through again anti-to tubular type
It answers in device.Wherein, the molar ratio of the chloropropene and trichlorosilane is preferably (0.95~1.1): 1；It is catalyzed in the mixed liquor
The concentration of agent is 10~200ppm, more preferably 50~200ppm, is further preferably 50~150ppm, most preferably 80~
120ppm。
Mixed liquor is reacted in tubular reactor, and the temperature of the reaction is preferably 65 DEG C~82 DEG C, more preferably
70 DEG C~80 DEG C；The time of the reaction is preferably 0.1~1h, more preferably 0.1~0.5h1.5~2h.
Subsequently into being reacted in tank reactor, crude product is obtained.The temperature of the reaction is preferably 80 DEG C~90
DEG C, more preferably 85 DEG C~90 DEG C；The time of the reaction is preferably 1~3h, more preferably 2~3h.The present invention will be in tubular type
The complete feed liquid of unreacted is input in tank reactor that the reaction was continued to complete in reactor, while by-product propylene is through condenser
Quickly leave reaction system.
A part of the crude product, which is back in tubular reactor, mixes continuation with chloropropene, trichlorosilane and catalyst
Reaction.The gross mass of the chloropropene, trichlorosilane and catalyst is with the mass ratio for being back to crude product in tubular reactor
(2~1): 1, more preferably (2~1.5): 1.
Another part enters rectifier unit and carries out rectifying, obtains γ-chloropropyl trichloro-silane.
The present invention is reacted by the catalyst activated in part reuse tank reactor in tubular reactor to start,
Induction period existing for catalyst is shortened, reaction efficiency is improved；Pass through the crude product in part reuse tank reactor simultaneously
Heat transfer is carried out, maintaining reaction temperature can be carried out by the heat in crude product in tubular reactor, to make entirely to react
It does not need to heat, reduces energy consumption.
In order to further illustrate the present invention, with reference to embodiments to a kind of γ-chloropropyl trichlorine silicon provided by the invention
The production method and production system of alkane are described in detail.
Reagent used in following embodiment is commercially available.
Examples 1 to 7
Using production system shown in FIG. 1, wherein Cat is catalyst storage tank, AC is chloropropene storage tank, TCS is trichlorine hydrogen
Silicon storage tank, (1) are the first metering pump, (2) are the second metering pump, (3) are third metering pump, (4) are static mixer, (R1) is
Tubular reactor, (R2) are tank reactor, (5) are condenser, (6) are metering pump, (7) are metering pump.
The trichlorosilane flow is 127Kg/h, chloropropene flow is 65Kg/h (total flow 192Kg/h), catalyst
The dosage of chloroplatinic acid is 100ppm, inputs static mixer by a certain percentage after mixing by metering pump, and input tubular type is anti-
Device is answered to be reacted, the reaction time in tubular reactor is 0.3h；Meanwhile controlling tank reactor reaction temperature is 90 DEG C,
Reaction time in tank reactor is 2h, and the reuse of tubular reactor is inputted by stepping up crude product in tank reactor
Amount measures reaction temperature at tubular type reactor feed mouth, the results are shown in Table 2.
Reaction temperature test result at 2 tubular reactor feed inlet of table
With above-mentioned tubular reactor entrance, trichlorosilane flow is 127Kg/h, and chloropropene flow is 65Kg/h, autoclave
For crude product reuse amount is 200Kg/h in reactor, tubular reactor material inlet temperature is 81.8 DEG C at this time, still reaction
The gas-chromatography map analysis of crude product sample the results are shown in Table 3, γ-chloropropyl trichloro-silane and selectively be shown in Table 4 in device.
3 embodiment of table, 7 tank reactor crude assay result
Embodiment 8~11
Using production system shown in FIG. 1
Tubular reactor entrance, trichlorosilane flow, chloropropene flow total flow are 192Kg/h, thick in tank reactor
Product reuse amount is 200Kg/h, and under different trichlorosilanes/chloropropene molar ratio, crude product gas chromatographic analysis the results are shown in Table 5, chlorine
Propyltrichlorosilan is selectively shown in Table 6.
The tank reactor crude product gas chromatographic analysis result of the different trichlorosilane/chloropropene molar ratios of table 5
Different trichlorosilane/chloropropene the molar ratios of table 6 are for the influence of γ-chloropropyl trichloro-silane selectivity
Claims (7)
1. a kind of production system of γ-chloropropyl trichloro-silane characterized by comprising
Tubular reactor；The tubular reactor outer surface is provided with heat transfer medium；
Tank reactor, the entrance of the tank reactor are connected with the outlet of the tubular reactor；The still reaction
The first outlet of device is connected with the first entrance of the tubular reactor；
Rectifier unit, the entrance of the rectifier unit are connected with the second outlet of the tank reactor；
It further include condenser；The entrance of the condenser is connected with the outlet of the third of the tank reactor.
2. production system according to claim 1, which is characterized in that further include static mixer；The static mixer
Outlet be connected with the second entrance of the tubular reactor.
3. production system according to claim 1, which is characterized in that further include metering pump；The of the tank reactor
One outlet is connected by metering pump with the first entrance of the tubular reactor.
4. a kind of production method of γ-chloropropyl trichloro-silane characterized by comprising
A chloropropene, trichlorosilane are passed through with catalyst) and reacted into tubular reactor, subsequently into tank reactor
It is reacted, obtains crude product；The molar ratio of the chloropropene and trichlorosilane is preferably (0.95~1.1): 1；
B) a part of the crude product, which is back in tubular reactor, mixes continuation with chloropropene, trichlorosilane and catalyst instead
It answers, another part, which enters, carries out rectifying in rectifier unit, obtain γ-chloropropyl trichloro-silane；The step B) in chloropropene, three
The gross mass of chlorine hydrogen silicon and catalyst is (2~1) with the mass ratio for being back to crude product in tubular reactor: 1.
5. production method according to claim 4, which is characterized in that the temperature reacted in the tubular reactor is 65 DEG C
~82 DEG C, the reaction time is 0.1~1h.
6. production method according to claim 4, which is characterized in that the temperature reacted in the tank reactor is 80 DEG C
~90 DEG C, the reaction time is 1~3h.
7. production method according to claim 5, which is characterized in that the step A) in specifically:
Chloropropene, trichlorosilane are mixed with catalyst, obtain mixed liquor, is then passed through into tubular reactor and is carried out instead again
It answers, is reacted subsequently into tank reactor, obtain crude product；In the mixed liquor concentration of catalyst be 10~
200ppm。
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1369497A (en) * | 2001-02-03 | 2002-09-18 | 德古萨股份公司 | Method for preparing 3-position functional propyl silane |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1369497A (en) * | 2001-02-03 | 2002-09-18 | 德古萨股份公司 | Method for preparing 3-position functional propyl silane |
Non-Patent Citations (2)
| Title |
|---|
| γ-氯丙基三氯硅烷的合成;田瑞亭等;《山东教育学院学报》;20041231;第102-103页 |
| 常压组合反应器中连续合成巯基乙酸工艺;王松等;《化学反应工程与工艺》;20110228;第26-31页 |
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