CN109134527A - A kind of scrubber system and its application in separation methyl chlorosilane monomer - Google Patents
A kind of scrubber system and its application in separation methyl chlorosilane monomer Download PDFInfo
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- CN109134527A CN109134527A CN201811041360.0A CN201811041360A CN109134527A CN 109134527 A CN109134527 A CN 109134527A CN 201811041360 A CN201811041360 A CN 201811041360A CN 109134527 A CN109134527 A CN 109134527A
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- chilling tank
- chilling
- tank
- scrubbing tower
- synthesis gas
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- 239000000178 monomer Substances 0.000 title claims abstract description 60
- YGZSVWMBUCGDCV-UHFFFAOYSA-N chloro(methyl)silane Chemical compound C[SiH2]Cl YGZSVWMBUCGDCV-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 238000000926 separation method Methods 0.000 title claims abstract description 22
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 77
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 77
- 238000005201 scrubbing Methods 0.000 claims abstract description 67
- 239000000470 constituent Substances 0.000 claims abstract description 42
- 238000005406 washing Methods 0.000 claims abstract description 37
- BLRPTPMANUNPDV-UHFFFAOYSA-N Silane Chemical compound [SiH4] BLRPTPMANUNPDV-UHFFFAOYSA-N 0.000 claims abstract description 32
- 229910000077 silane Inorganic materials 0.000 claims abstract description 32
- 238000000034 method Methods 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims description 105
- 230000008676 import Effects 0.000 claims description 41
- 239000007792 gaseous phase Substances 0.000 claims description 38
- 239000007791 liquid phase Substances 0.000 claims description 36
- 239000012071 phase Substances 0.000 claims description 30
- 239000007788 liquid Substances 0.000 claims description 25
- 238000002309 gasification Methods 0.000 claims description 17
- 239000000843 powder Substances 0.000 claims description 11
- 210000001015 abdomen Anatomy 0.000 claims description 10
- 239000012530 fluid Substances 0.000 claims description 7
- 230000001788 irregular Effects 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 11
- 230000000694 effects Effects 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000005046 Chlorosilane Substances 0.000 abstract description 2
- KOPOQZFJUQMUML-UHFFFAOYSA-N chlorosilane Chemical compound Cl[SiH3] KOPOQZFJUQMUML-UHFFFAOYSA-N 0.000 abstract description 2
- 238000012423 maintenance Methods 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract description 2
- 238000009835 boiling Methods 0.000 description 7
- 238000012545 processing Methods 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 238000012216 screening Methods 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000011863 silicon-based powder Substances 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 239000006200 vaporizer 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
-
- 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
- C07F7/20—Purification, separation
-
- 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
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention provides a kind of scrubber system and its application in separation methyl chlorosilane monomer, it not only improves washing system separating effect, and reduce reboiler system and column plate of washing column number, reduce energy consumption, technique is simplified simultaneously, so that reaching heat energy recycle, the purpose of equipment work efficiency is improved.The present invention also achieves efficiently separating for direct synthesis chlorosilane heavy constituent and silane simultaneously, and increased chilling tank arrangement is compared with traditional handicraft and found, effectively reduces column plate of washing column number, reduce scrubbing tower regurgitant volume；It obviously slows down impact of the mixed raw material to wash tower bottoms column plate, increases its service life and reduces year parking maintenance number；Scrubber system of the present invention, easy to operate, benefit is evident, can large scale investment use.
Description
Technical field
The present invention is a kind of scrubber system and its application in separation methyl chlorosilane monomer.
Background technique
Conventional washing system process: high-temperature synthesis gas enters scrubbing tower by bottom, removes the gas phase silane monomer of heavy constituent
With chloromethanes by being discharged at the top of scrubbing tower, cold silane monomer is back to scrubbing tower, and liquid phase heavy constituent is by scrubbing tower abdomen liquid phase
Pipe is discharged into reboiler system, and reboiler system is heated using hot oil, and light silane monomer is discharged into scrubbing tower by reboiler gas phase pipe, then
Heavy constituent in boiling device is discharged into flash system again, and monomer synthesis unit is discharged in the heavy constituent after flash distillation.The washing system technique needs
More column plate (no less than 18 pieces) are used, by the way of reboiler system and flash system heating, not only consume more heat
Amount, and still contain more light silane monomer in the screenings being discharged.
Synthesizing methyl-chloro-silane process flow in the present invention: liquid phase chloromethanes after metering, gasifies through vaporizer, superheater
Enter fluidized bed through distribution grid after heating, after silicon powder is mixed with catalyst, fluidized bed is entered by fluidized bed material-feeding port, passes through thermal conductivity
The reaction of hot oil heating starting takes away exothermic heat of reaction by cold conduction oil after reaction is normal.In order to maintain fluidized bed material position and anti-
It answers, needs that silicon powder and catalyst is continuously replenished.Synthesis gas is (for reaction product silane, unreacted chloromethanes, fine silica powder and catalysis
Agent) by entering cyclone system at the top of fluidized bed, synthesis gas enters scrubber system after cyclone system traps part fine powder, washes
It washs Tower System and isolates heavy constituent in methylchlorosilane, heavy constituent includes the fine powder and higher boiling silicon not trapped by cyclone system
Alkane (boiling point > 140 DEG C).
Summary of the invention
The invention solves task be to provide a kind of application of scrubber system in separation methyl chlorosilane monomer,
Washing system separating effect is not only improved, but also reduces reboiler system and column plate of washing column number, energy consumption is reduced, simplifies simultaneously
Technique improves the purpose of equipment work efficiency so that reaching heat energy recycle.
Also being solved for task is a kind of scrubber system and side of separation for separating methyl chlorosilane monomer to the present invention simultaneously
Method.
To solve the above-mentioned problems, the present invention is achieved by the following technical solutions:
A kind of scrubber system separating methyl chlorosilane monomer, comprising: chilling tank 1 and scrubbing tower 2；Wherein, methylchlorosilane
Monomer and heavy constituent pass through synthesis gas import 3 and enter chilling tank 1, and chilling tank gaseous phase outlet 4 and scrubbing tower gas phase import 5 pass through gas
The connection of phase conduit, chilling tank fluid inlet 7 are connected with scrubbing tower liquid-phase outlet 8；The bottom of chilling tank 1 passes through liquid phase conduit and washes
The bottom for washing tower 2 is connected.
Further, 1 liquid phase level of chilling tank or less is immersed in 2 end of synthesis gas import；Chilling tank gaseous phase outlet 4 is arranged
On the top of connection chilling tank 1, the abdomen of scrubbing tower 2 is arranged in scrubbing tower gas phase import 5；Chilling tank heavy component discharge gate 6
In 1 bottom of chilling tank, a chilling tank baiting valve 13 is installed on heavy component discharge gate 6；1 top side of chilling tank is equipped with one
A chilling tank gas phase temperature meter 11,1 bottom side of chilling tank are equipped with a chilling tank liquid thermometer 9；Scrubbing tower 2 is by washing
Tower gaseous phase outlet 10 is washed to be connected with downstream unit；Methyl chlorosilane monomer after washing passes through scrubbing tower gaseous phase outlet 10 and downstream
Device is connected；Heavy constituent after washing is connected by chilling tank heavy component discharge gate 6 with downstream unit.
Further, the liquid phase level in the chilling tank 1 is located at end and the chilling tank gaseous phase outlet 4 of synthesis gas import 3
Between, and synthesis gas import end is apart from liquid level 2-30cm；
Further, it is full edge shape, wave that the end that the methyl chlorosilane monomer and heavy constituent pass through synthesis gas import 3, which is in shape,
One of shape, zigzag, irregular shape.
Further, the temperature difference control of the gas phase temperature meter 11 on the chilling tank 1 and liquid thermometer 12 is for 3-20
℃。
Further, 2 number of plates of scrubbing tower is 7-15 block.
Further, application of a kind of scrubber system in separation methyl chlorosilane monomer.
A method of separation methyl chlorosilane monomer, concrete operations process flow are as follows:
(1) synthesis gas is entered cyclone system, the synthesis gas for removing most of fine powder can be obtained by whirlwind at the top of fluidized bed,
Temperature is 230-300 DEG C；
(2) chilling, the high-temperature synthesis gas in step (1) are passed through chilling tank 1；Synthesis gas temperature is sharply down to 90-180 DEG C at this time,
Liquid phase is boiled in chilling tank 1, and light silane monomer gasification, heavy constituent is utilized towards 1 bottom deposit of chilling tank, and in chilling tank 1
Synthesis gas heat continues heavy constituent gasification separation；
(3) it washing, the light silane monomer of gasification is discharged into scrubbing tower 2 by chilling tank gaseous phase outlet 4 in step (2) further washs,
Light silane monomer is discharged by gaseous phase outlet 10 at the top of scrubbing tower.
The present invention has the advantages that
1, the present invention realizes efficiently separating for direct synthesis chlorosilane heavy constituent and silane, and it is poor to overcome conventional washing effect
When fine powder can with washing column overhead synthesis gas enter rear system the problems such as；
2, through the invention in increased chilling tank arrangement, with traditional handicraft compare find, effectively reduce column plate of washing column number,
Reduce scrubbing tower regurgitant volume；
3, through the invention in increased chilling tank arrangement, with traditional handicraft compare find, hence it is evident that slow down mixed raw material to washing
The impact of tower bottom column plate increases its service life and reduces year parking maintenance number；
4, through the invention in increased chilling tank arrangement, with traditional handicraft compare find, discharge chilling tank heavy constituent use
The recycling of light silane monomer can be realized in a small amount of heat, greatly reduces energy consumption, the only 1/4-1/2 of traditional handicraft energy consumption；
5, by the processing to 3 end of synthesis gas import, make the full contact of synthesis gas and liquid phase, can greatly ensure synthesis gas
Achieve the effect that abundant chilling in the liquid phase；It is effectively formed gas-liquid interface boiling bed, bubble is uniformly distributed, no dead zone；
6, through control 3 end of synthesis gas import at a distance from liquid level and the thermal gradient energy of gas phase thermometer 11 and liquid thermometer 12
It effectively maintains liquid level steady, prevents liquid phase boiling from acutely liquid phase being caused to enter blocking caused by chilling tank gaseous phase outlet 4；
7, through the invention in increased chilling tank arrangement, with traditional handicraft compare find, reduce reboiler system after, heavy constituent
It is discharged into flash system, using less heat, light silane monomer content control in the screenings of discharge synthesizer may be implemented and exist
5%wt or less；
8, scrubber system in the present invention, easy to operate, benefit is evident, can large scale investment use.
Detailed description of the invention
Fig. 1 is the structural diagram of the present invention；
Appended drawing reference: chilling tank 1, scrubbing tower 2, synthesis gas import 3, chilling tank gaseous phase outlet 4, scrubbing tower gas phase import 5, chilling
Tank heavy component discharge gate 6, chilling tank fluid inlet 7, scrubbing tower liquid-phase outlet 8, refluxing opening 9, scrubbing tower gaseous phase outlet 10, chilling
Tank gas phase temperature meter 11, chilling tank liquid thermometer 12, chilling tank baiting valve 13.
Specific embodiment
Working principle:
A kind of scrubber system and its application in separation methyl chlorosilane monomer, comprising: chilling tank 1, scrubbing tower 2, synthesis gas
Import 3, scrubbing tower gas phase import 5, chilling tank heavy component discharge gate 6, chilling tank fluid inlet 7, is washed chilling tank gaseous phase outlet 4
Wash tower liquid-phase outlet 8, refluxing opening 9, scrubbing tower gaseous phase outlet 10, chilling tank gas phase temperature meter 11, chilling tank liquid thermometer 12,
Chilling tank baiting valve 13；Wherein: synthesis gas is made of reaction product silane, unreacted chloromethanes, fine silica powder and catalyst,
And entered in chilling tank by synthesis gas import 3；1 liquid phase level of chilling tank is immersed hereinafter, chilling tank gas phase in 3 end of synthesis gas import
Outlet 4 is connected with scrubbing tower gas phase import 5 by gas phase conduit, and chilling tank fluid inlet 7 is connected with scrubbing tower liquid-phase outlet 8；
The top of connection chilling tank 1 is arranged in chilling tank gaseous phase outlet 4, and the abdomen of scrubbing tower 2 is arranged in scrubbing tower gas phase import 5；It is anxious
Cold tank heavy component discharge gate 6 is located at 1 bottom of chilling tank, and a chilling tank baiting valve 13 is equipped on heavy component discharge gate 6；Chilling
1 top side of tank is equipped with a chilling tank gas phase temperature meter 11, and 1 bottom side of chilling tank is equipped with a chilling tank liquid phase temperature
Degree meter 9；Scrubbing tower 2 is connected by scrubbing tower gaseous phase outlet 10 with downstream unit；Methyl chlorosilane monomer after washing is by washing
Tower gaseous phase outlet 10 is washed to be connected with downstream unit；Heavy constituent after washing passes through chilling tank heavy component discharge gate 6 and downstream unit
It is connected.
The high-temperature synthesis gas come out from cyclone system is entered in chilling tank 1 by synthesis gas import 3；3 end of synthesis gas import
Below liquid phase level in end insertion chilling tank 1；Synthesis gas is sharply cooled to 120 DEG C or so by 260 DEG C or more；In chilling tank 1
Liquid phase boiling, light silane monomer gasification, is discharged into scrubbing tower 2 by the chilling tank gaseous phase outlet 4 on chilling tank 1, heavy constituent towards
The congregate of chilling tank 1 goes down；3 nozzle of synthesis gas import uses indefinite shape, and liquid level submerges catheter tip, prevents synthesis gas
Non- chilling is directly run out of from catheter tip, can be effectively formed gas-liquid interface boiling bed using the synthesis gas import 3 of indefinite shape,
Bubble is uniformly distributed, no dead zone；By the chilling tank gaseous phase outlet 4 of chilling tank 1 be discharged into the synthesis gas of scrubbing tower 2 scrubbing tower 2 into
The washing of one step；Light silane monomer is discharged downstream device by the scrubbing tower gaseous phase outlet 10 at 2 top of scrubbing tower；Heavy constituent is by scrubbing tower
2 bottom is discharged into chilling tank tapering by scrubbing tower liquid-phase outlet 8 and chilling tank fluid inlet 7, using closing in chilling tank 1
At gas heat gasification separation；According to 1 liquidus temperature of chilling tank, chilling tank baiting valve 13,6 row of chilling tank heavy component discharge gate are opened
Heavy constituent is deposited out；Chilling tank 1 and scrubbing tower 2 are gas-liquid mouth connectivity device, the liquid level of chilling tank 1 by scrubbing tower 2 liquid level control
System.
Embodiment 1
A kind of scrubber system separating methyl chlorosilane monomer, comprising: chilling tank 1 and scrubbing tower 2；Wherein, methylchlorosilane
Monomer and heavy constituent pass through synthesis gas import 3 and enter chilling tank 1, and chilling tank gaseous phase outlet 4 and scrubbing tower gas phase import 5 pass through gas
The connection of phase conduit, chilling tank fluid inlet 7 are connected with scrubbing tower liquid-phase outlet 8；The bottom of chilling tank 1 passes through liquid phase conduit and washes
The bottom for washing tower 2 is connected；
Further, 1 liquid phase level of chilling tank or less is immersed in 2 end of synthesis gas import；The setting of chilling tank gaseous phase outlet 4 is even
The top of chilling tank 1 is connect, the abdomen of scrubbing tower 2 is arranged in scrubbing tower gas phase import 5；Chilling tank heavy component discharge gate 6 is located at anxious
Cold 1 bottom of tank is equipped with a chilling tank baiting valve 13 on heavy component discharge gate 6；1 top side of chilling tank is equipped with a urgency
Cold tank gas phase temperature meter 11,1 bottom side of chilling tank are equipped with a chilling tank liquid thermometer 9；Scrubbing tower 2 passes through scrubbing tower
Gaseous phase outlet 10 is connected with downstream unit；Methyl chlorosilane monomer after washing passes through scrubbing tower gaseous phase outlet 10 and downstream unit
It is connected；Heavy constituent after washing is connected by chilling tank heavy component discharge gate 6 with downstream unit；
Further, the liquid phase level in the chilling tank 1 be located at synthesis gas import 3 end and chilling tank gaseous phase outlet 4 it
Between, and synthesis gas import end is apart from 16 cm of liquid level；
Further, the methyl chlorosilane monomer is wavy in shape by the end of synthesis gas import 3 with heavy constituent；
Further, the temperature difference of the gas phase temperature meter 11 on the chilling tank 1 and liquid thermometer 12 control is being 18 DEG C；
It is 7 pieces by column plate of washing column number in the technique；
Further, the method concrete operations process flow of the separation methyl chlorosilane monomer are as follows:
(1) synthesis gas is entered cyclone system, the synthesis gas for removing most of fine powder can be obtained by whirlwind at the top of fluidized bed,
Temperature is 260 DEG C；
(2) chilling, the high-temperature synthesis gas in step (1) are passed through chilling tank 1；Synthesis gas temperature is sharply down to 130 DEG C at this time, chilling
Liquid phase is boiled in tank 1, and light silane monomer gasification, heavy constituent utilizes synthesis gas towards 1 bottom deposit of chilling tank in chilling tank
Heat continues heavy constituent gasification separation；
(3) it washing, the light silane monomer of gasification is discharged into scrubbing tower 2 by chilling tank gaseous phase outlet 4 in step (2) further washs,
Light silane monomer is discharged by gaseous phase outlet 10 at the top of scrubbing tower.
When the heavy constituent processing being discharged by the process system, required energy consumption is the 1/4 of traditional handicraft energy consumption.
Embodiment 2
Remaining is the same as embodiment 1
Liquid phase level in chilling tank 1 is located between the end of synthesis gas import 3 and chilling tank gaseous phase outlet 4, synthesis gas import
End is apart from liquid level 2cm；
Methyl chlorosilane monomer is wavy in shape by the end of synthesis gas import 3 with heavy constituent；
The temperature difference control of gas phase temperature meter 11 and liquid thermometer 12 on chilling tank 1 is being 10 DEG C；
It is 14 pieces by column plate of washing column number in the technique；
The method concrete operations process flow of the separation methyl chlorosilane monomer are as follows:
(1) synthesis gas is entered cyclone system, the synthesis gas for removing most of fine powder can be obtained by whirlwind at the top of fluidized bed,
Temperature is 260 DEG C；
(2) chilling, the high-temperature synthesis gas in step (1) are passed through chilling tank 1；Synthesis gas temperature is sharply down to 145 DEG C at this time, chilling
Liquid phase is boiled in tank 1, and light silane monomer gasification, heavy constituent utilizes synthesis towards 1 bottom deposit of chilling tank in chilling tank 1
Gas heat continues heavy constituent gasification separation；
(3) it washing, the light silane monomer of gasification is discharged into scrubbing tower 2 by chilling tank gaseous phase outlet 4 in step (2) further washs,
Light silane monomer is discharged by gaseous phase outlet 10 at the top of scrubbing tower.
When the heavy constituent processing being discharged by the process system, required energy consumption is the 1/3 of traditional handicraft energy consumption.
Embodiment 3
Remaining is the same as embodiment 1
Liquid phase level in chilling tank 1 is located between the end of synthesis gas import 3 and chilling tank gaseous phase outlet 4, synthesis gas import
End is apart from liquid level 30cm；
It is full edge shape that the end that methyl chlorosilane monomer and heavy constituent pass through synthesis gas import 3, which is in shape,；
The temperature difference control of gas phase temperature meter 11 and liquid thermometer 12 on chilling tank 1 is being 5 DEG C；
It is 10 pieces by column plate of washing column number in the technique；
The method concrete operations process flow of the separation methyl chlorosilane monomer are as follows:
(1) synthesis gas is entered cyclone system, the synthesis gas for removing most of fine powder can be obtained by whirlwind at the top of fluidized bed,
Temperature is 260 DEG C；
(1) chilling, the high-temperature synthesis gas in step (1) are passed through chilling tank 1；Synthesis gas temperature is sharply down to 120 DEG C at this time, chilling
Liquid phase is boiled in tank 1, and light silane monomer gasification, heavy constituent utilizes synthesis towards 1 bottom deposit of chilling tank in chilling tank 1
Gas heat continues heavy constituent gasification separation；
(3) it washing, the light silane monomer of gasification is discharged into scrubbing tower 2 by chilling tank gaseous phase outlet 4 in step (2) further washs,
Light silane monomer is discharged by gaseous phase outlet 10 at the top of scrubbing tower.
When the heavy constituent processing being discharged by the process system, required energy consumption is the 1/2 of traditional handicraft energy consumption.
Comparative example 1
The scrubber system of tradition separation methyl chlorosilane monomer and heavy constituent, the fabrication processing are as follows:
(1) synthesis gas is entered cyclone system, the synthesis gas for removing most of fine powder can be obtained by whirlwind at the top of fluidized bed；
(2) it washs, whirlwind treated synthesis gas is discharged into scrubbing tower tower abdomen, about 2 meters of liquid of tower abdomen by wash tower bottoms in step (1)
Position, synthesis gas enter column plate layer after the washing of tower abdomen liquid phase material, and synthesis gas continues to carry out on column plate with cold phegma
Caloic exchange washing, the synthesis gas after washing are discharged by scrubbing tower tower top outlet.The silane of scrubbing tower tower abdomen condensation and recombination
Divide through the overflow of tower abdomen liquid-phase tube to reboiler, goes out light silane by reboiler system heating evaporation, light silane passes through reboiler
Gas phase pipe enters scrubbing tower, and heavy constituent drains into flash system by reboiler feed opening, synthesizer is discharged after heavy constituent flash distillation.
The conventional washing tower number of plates is generally no less than 18 pieces, simultaneously because synthesis gas is directly toward column plate charging from tower bottom,
Operation is slightly fluctuated, and causes first block of column plate of tower bottom to be easily turned over damage, not only equipment damage, but also influences washing effect, is blocked up
Plug phenomenon may occur；Reboiler system and flash system are heated by thermal oil system, evaporate light silane, compare traditional work
Skill, new scrubber system and separation method cancel reboiler system, and heavy constituent is directly discharged into flash system.
After scrubber system of the invention and separation method flash distillation, light silane monomer content is discharged in the screenings of synthesizer
Control is only the 1/4-1/2 of traditional handicraft energy consumption in the heat that 5%wt or less needs.
The embodiment of the present invention is as follows: with data specific in comparative example
Claims (8)
1. a kind of scrubber system for separating methyl chlorosilane monomer, comprising: chilling tank (1) and scrubbing tower (2)；Its feature exists
Enter chilling tank (1) by synthesis gas import (3) in: methyl chlorosilane monomer and heavy constituent, chilling tank gaseous phase outlet (4) and washes
It washs tower gas phase import (5) to connect by gas phase conduit, chilling tank fluid inlet (7) is connected with scrubbing tower liquid-phase outlet (8)；Chilling
The bottom of tank (1) is connected by liquid phase conduit with the bottom of scrubbing tower (2).
2. a kind of scrubber system for separating methyl chlorosilane monomer as described in claim 1, it is characterised in that: the synthesis
1 liquid phase level of chilling tank or less is immersed in gas import (2) end；Chilling tank gaseous phase outlet (4) setting is in the upper of connection chilling tank (1)
The abdomen in scrubbing tower (2) is arranged in portion, scrubbing tower gas phase import (5)；Chilling tank heavy component discharge gate (6) is located at chilling tank (1)
Bottom is equipped with a chilling tank baiting valve (13) on heavy component discharge gate (6)；Chilling tank (1) top side is equipped with one
Chilling tank gas phase temperature meter (11), chilling tank (1) bottom side are equipped with a chilling tank liquid thermometer (9)；Scrubbing tower (2)
It is connected by scrubbing tower gaseous phase outlet (10) with downstream unit；Methyl chlorosilane monomer after washing passes through scrubbing tower gaseous phase outlet
(10) it is connected with downstream unit；Heavy constituent after washing is connected by chilling tank heavy component discharge gate (6) with downstream unit.
3. a kind of scrubber system for separating methyl chlorosilane monomer as claimed in claim 2, it is characterised in that: the chilling
Liquid phase level in tank (1) is located between the end of synthesis gas import (3) and chilling tank gaseous phase outlet (4), and synthesis gas import
End is apart from liquid level 2-30cm.
4. a kind of scrubber system for separating methyl chlorosilane monomer as claimed in claim 2, it is characterised in that: the methyl
Chlorosilane monomer and heavy constituent by the end of synthesis gas import (3) be full edge shape in shape, wavy, zigzag, irregular
One of shape.
5. a kind of scrubber system for separating methyl chlorosilane monomer as claimed in claim 3, it is characterised in that: the chilling tank
(1) temperature difference control of gas phase temperature meter (11) and liquid thermometer (12) on is being 3-20 DEG C.
6. a kind of scrubber system for separating methyl chlorosilane monomer as claimed in claim 1 or 2, it is characterised in that: described to wash
Washing tower (2) number of plates is 7-15 block.
7. a kind of scrubber system answering in separation methyl chlorosilane monomer as described in any one of claim 1-6
With.
8. a kind of method for separating methyl chlorosilane monomer, it is characterised in that: concrete operations process flow are as follows:
(1) synthesis gas is entered cyclone system, the synthesis gas for removing most of fine powder can be obtained by whirlwind at the top of fluidized bed,
Temperature is 230-300 DEG C；
(2) chilling, the high-temperature synthesis gas in step (1) are passed through chilling tank (1)；Synthesis gas temperature is sharply down to 90-180 at this time
DEG C, liquid phase is boiled in chilling tank (1), the gasification of light silane monomer, and heavy constituent is towards chilling tank (1) bottom deposit, and in chilling tank
(1) continued using synthesis gas heat by heavy constituent gasification separation in；
(3) it washs, the light silane monomer of gasification is discharged into scrubbing tower (2) by chilling tank gaseous phase outlet (4) in step (2) further washes
It washs, light silane monomer is discharged by gaseous phase outlet (10) at the top of scrubbing tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811041360.0A CN109134527B (en) | 2018-09-07 | 2018-09-07 | Washing tower system and application thereof in separation of methyl chlorosilane monomers |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811041360.0A CN109134527B (en) | 2018-09-07 | 2018-09-07 | Washing tower system and application thereof in separation of methyl chlorosilane monomers |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109134527A true CN109134527A (en) | 2019-01-04 |
| CN109134527B CN109134527B (en) | 2020-11-24 |
Family
ID=64827599
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| Application Number | Title | Priority Date | Filing Date |
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| CN201811041360.0A Active CN109134527B (en) | 2018-09-07 | 2018-09-07 | Washing tower system and application thereof in separation of methyl chlorosilane monomers |
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Cited By (2)
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| CN110128463A (en) * | 2019-04-10 | 2019-08-16 | 湖北兴瑞硅材料有限公司 | A kind of process for separating and purifying and system of methylchlorosilane mix monomer |
| CN112707930A (en) * | 2021-01-04 | 2021-04-27 | 江西蓝星星火有机硅有限公司 | Method for recovering high-boiling-point substances in organic silicon slurry slag |
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| CN1438226A (en) * | 2003-01-07 | 2003-08-27 | 蓝星化工新材料股份有限公司江西星火有机硅厂 | Wet-dusting and high-boiling-point separation technology for organic silane chloride synthesized gas |
| CN201626931U (en) * | 2009-12-17 | 2010-11-10 | 浙江恒业成有机硅有限公司 | Methylchlorosilane mixture monomer high boiling removal device |
| CN201855644U (en) * | 2011-03-02 | 2011-06-08 | 特变电工新疆硅业有限公司 | Washing tower |
| CN203816419U (en) * | 2014-04-11 | 2014-09-10 | 天津市华瑞奕博化工科技有限公司 | Tower equipment for removing solid particles from methyl chlorosilane synthesis gas |
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| CN1438226A (en) * | 2003-01-07 | 2003-08-27 | 蓝星化工新材料股份有限公司江西星火有机硅厂 | Wet-dusting and high-boiling-point separation technology for organic silane chloride synthesized gas |
| CN201626931U (en) * | 2009-12-17 | 2010-11-10 | 浙江恒业成有机硅有限公司 | Methylchlorosilane mixture monomer high boiling removal device |
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| CN110128463A (en) * | 2019-04-10 | 2019-08-16 | 湖北兴瑞硅材料有限公司 | A kind of process for separating and purifying and system of methylchlorosilane mix monomer |
| CN112707930A (en) * | 2021-01-04 | 2021-04-27 | 江西蓝星星火有机硅有限公司 | Method for recovering high-boiling-point substances in organic silicon slurry slag |
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| CN109134527B (en) | 2020-11-24 |
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