CN101165443A - Chloro-silicane gaseous mixture condensation process - Google Patents
Chloro-silicane gaseous mixture condensation process Download PDFInfo
- Publication number
- CN101165443A CN101165443A CNA200710062546XA CN200710062546A CN101165443A CN 101165443 A CN101165443 A CN 101165443A CN A200710062546X A CNA200710062546X A CN A200710062546XA CN 200710062546 A CN200710062546 A CN 200710062546A CN 101165443 A CN101165443 A CN 101165443A
- Authority
- CN
- China
- Prior art keywords
- condensation
- chloro
- gaseous mixture
- compressor
- condensation process
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Silicon Compounds (AREA)
Abstract
This invention is a chlorosilane mixed gas condensation technique. It belongs to the field of chemical industrial gas condensation element. The steps include: chlorosilane combined gas is firstly undertaken liquefied condensation by normal pressure condensation technique. The normal pressure condensing pressure is within 0.005MPa-0.1MPa. The waste gas is then undertaken high pressure liquefied condensation by compressor. The compression condensing pressure is within 0.4MPa-1.5MPa. After combined condensing, the product is washed and then discharged. This invention has low material loss.
Description
Technical field:
The present invention relates to chemical gases condensing unit field, be specially adapted to the chlorosilane synthesis gas condensation process of trichlorosilane synthesis system.
Background technology:
At present, the chloro-silicane gaseous mixture that synthesizes in the domestic trichlorosilane production system, all adopt the normal pressure condensation process, promptly, behind purifying and dedusting, enter condenser system again from the chloro-silicane gaseous mixture of trichlorosilane synthetic furnace, under near normal pressure (about 0.05MPa) situation, by recirculated water, the condensation of calcium chloride chilled brine two-stage indirect condenser, form the liquefaction condensation working cell of chloro-silicane gaseous mixture, the emptying behind water wash of condensation tail gas.
Normal pressure condensation process major defect is:
1, the condensation yield is low, and material loss is big.Normal pressure condensation yield is less than 94%, and primary raw material silica flour unit consumption is greater than the 285kg/ ton.
2, tail is large-minded after the condensation, and waste water, waste sludge discharge amount are many, are unsuitable for heavy industrialization.
Summary of the invention:
Goal of the invention of the present invention is low at prior art condensation yield, material loss is big, tail is large-minded after the condensation, and waste water, the deficiency that the waste sludge discharge amount is many provide the chlorosilane synthesis gas condensation process of a kind of condensation of synthesis gas through normal pressure condensation and twice condensation of pressurization condensation.This process condensate yield height, material loss is little, and energy consumption is low, and operating cost is minimum.
Realize the foregoing invention purpose by the following technical solutions: a kind of chloro-silicane gaseous mixture condensation process, comprise condenser, compressor, cooling medium, described processing step is: the chlorosilane synthesis gas is at first adopted the condensation of liquefying of normal pressure condensation process, and the normal pressure condensing pressure is between 0.005MPa～0.1MPa; The condensed tail gas of normal pressure carries out the high-pressure liquefaction condensation with compressor pressurizes again, and the pressurization condensing pressure is between 0.4MPa～1.5MPa; Emptying after the drip washing after the combination condensation.
Adopt technique scheme, compared with prior art, remarkable advantage of the present invention is:
1) condensation yield height, material loss is little.Combination condensation total recovery is greater than 98.5%, and primary raw material silica flour unit consumption is less than the 255kg/ ton.
2) condensed tail is narrow-minded, and waste water, waste sludge discharge amount have only 15～25% of normal pressure condensation process.
3) adopt normal pressure, pressurization combination technique, promptly solved the low problem of normal pressure condensation yield, avoided big, the high shortcoming of power consumption of independent pressurization condensation investment again.
4) after group goes into to pressurize condensation, can to the operating mode of condensing pressure and refrigerant, bigger selection space be arranged according to resource situation.
5) investment in fixed assets is between normal pressure condensation and pressurization condensation process, but operating cost is minimum.Combination condensation process operating cost is lower by 4～5% than normal pressure condensation process, than independent pressurization condensation process low 1～1.5%.
Description of drawings:
Accompanying drawing 1 is the synthetic condensation process general flow chart of trichlorosilane of the present invention.
Among the figure: measuring tank 8, compression back measuring tank 9, sintetics basin 10 before automatic pressure regulator 4, compression back water cooler 5, compression back low-temperature condenser 6, compression back automatic pressure regulator 7, the compression before low-temperature condenser 2, compressor 3, the compression before water cooler 1, the compression before the compression.
The specific embodiment
The present invention will be further described below in conjunction with accompanying drawing.
Referring to accompanying drawing 1, water cooler 1 is connected with low-temperature condenser 2 usefulness pipelines before the compression before the compression, be connected with measuring tank 8 before the compression, and measuring tank 8 and compression back measuring tank 9 before the compression, sintetics basin 10 connects, and compression back measuring tank 9 is connected with sintetics basin 10.Compression back water cooler 5 is connected the back and is connected with compression back measuring tank 9 with compression back low-temperature condenser 6.Compressor 3 is connected between preceding low-temperature condenser 2 of compression and the compression back water cooler 5, automatic pressure regulator 4 before the link circuit of compressor 3 is provided with and compresses.Water cooler 1 is the one-level water cooler with compression back water cooler 5 before the compression, and low-temperature condenser 2 is a secondary coolers with compression back low-temperature condenser 6 before the compression.
The course of work of the present invention: chlorosilane synthesis gas, order enters the preceding water cooler 1 of compression, cooling condensation, low-temperature condenser 2 carried out condensation again before fixed gas entered compression, this moment, about chlorosilane of about 80% was condensed, the fixed gas of the chlorine-containing silane that the condensation of low-temperature condenser 2 is not got off before overcompression, after process diaphragm type compressor 3 is forced into 0.45-1.5MPa, water cooler 5 cooling condensations after compression again, fixed gas air inlet compression back low-temperature condenser condensation 6, carry out having the chlorosilane condensation about 20% to get off again in the gaseous mixture of condensation after compression, the gas disposal that truncates of the fixed gas of last chlorine-containing silane about 1.5%, the mixed liquor that condensation is got off enters preceding measuring tank 8 of compression and compression back measuring tank 9 respectively, carries out rectifying through all compressing into into synthetic output basin 10 then.Steady for guaranteeing condenser system pressure simultaneously, with delaying unloading before the 4 adjusting compressions of automatic pressure regulator before the compression, with low-temperature condenser 2 before automatic pressure regulator 7 pressure regulation are contracted after the compression, condensed tail is narrow-minded, and waste water at first adopts the condensation of liquefying of normal pressure condensation process, tail gas after the condensation, again with after the dedicated compressor pressurization, carry out the high-pressure liquefaction condensation, the two constitutes the new technology device, makes up the emptying behind water wash of condensed tail gas.
Important technological parameters of the present invention:
1, normal pressure condensation portion:
Pressure: 0.005～0.10MPa; One-level water cooler cooling medium: industrial circulating water; Secondary coolers cooling medium :-20～-80 ℃ of refrigerants.
2, pressurization condensation portion:
Pressure: 0.4～1.5MPa; One-level water cooler cooling medium: industrial circulating water; Secondary coolers cooling medium :-20～-80 ℃ of refrigerants.
Condenser of the present invention all is a tubular heat exchanger, and the operating pressure scope is 0.010-1.5MPa, and operating temperature is-20 ℃-80 ℃, and cooling medium is industrial circulating water, calcium chloride chilled brine.
Compressor adopts the chlorosilane gas dedicated compressor, and the compressor air-discharging amount is 80-240Nm
2/ h (folding air).
Claims (4)
1. chloro-silicane gaseous mixture condensation process, comprise condenser, compressor, cooling medium, it is characterized in that described processing step is: the chlorosilane synthesis gas is at first adopted the condensation of liquefying of normal pressure condensation process, and the normal pressure condensing pressure is between 0.005MPa～0.1MPa; The condensed tail gas of normal pressure carries out the high-pressure liquefaction condensation with compressor pressurizes again, and the pressurization condensing pressure is between 0.4MPa～1.5MPa; Emptying after the drip washing after the combination condensation.
2. chloro-silicane gaseous mixture condensation process according to claim 1 is characterized in that, described compressor is the diaphragm type compressor of compression chloro-silicane gaseous mixture special use, and the compressor air-discharging amount is 80-240Nm
2/ h.
3. according to the described chloro-silicane gaseous mixture condensation process of claim 1, it is characterized in that: the one-level water condenser of described condenser is made cooling medium with industrial circulating water, and the secondary low-temperature condenser is made cooling medium with-20 ℃～-80 ℃ low temperature refrigerants.
4. according to the described chloro-silicane gaseous mixture condensation process of claim 1, it is characterized in that: described condenser all is a tubular heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA200710062546XA CN101165443A (en) | 2007-08-08 | 2007-08-08 | Chloro-silicane gaseous mixture condensation process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA200710062546XA CN101165443A (en) | 2007-08-08 | 2007-08-08 | Chloro-silicane gaseous mixture condensation process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101165443A true CN101165443A (en) | 2008-04-23 |
Family
ID=39334227
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA200710062546XA Pending CN101165443A (en) | 2007-08-08 | 2007-08-08 | Chloro-silicane gaseous mixture condensation process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101165443A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102229432A (en) * | 2011-05-19 | 2011-11-02 | 蒋超 | Chlorosilane condensate reservoir |
| CN105084369A (en) * | 2014-04-23 | 2015-11-25 | 新特能源股份有限公司 | Chlorosilane-containing waste gas recovery treatment apparatus |
| CN112964747A (en) * | 2021-03-10 | 2021-06-15 | 北京科技大学 | Gas condensation visualization and heat exchange characteristic detection device and method |
-
2007
- 2007-08-08 CN CNA200710062546XA patent/CN101165443A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102229432A (en) * | 2011-05-19 | 2011-11-02 | 蒋超 | Chlorosilane condensate reservoir |
| CN102229432B (en) * | 2011-05-19 | 2012-10-31 | 蒋超 | Chlorosilane condensate reservoir |
| CN105084369A (en) * | 2014-04-23 | 2015-11-25 | 新特能源股份有限公司 | Chlorosilane-containing waste gas recovery treatment apparatus |
| CN112964747A (en) * | 2021-03-10 | 2021-06-15 | 北京科技大学 | Gas condensation visualization and heat exchange characteristic detection device and method |
| CN112964747B (en) * | 2021-03-10 | 2022-04-22 | 北京科技大学 | Gas condensation visualization and heat exchange characteristic detection device and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109140903B (en) | Air separation system and air separation method utilizing cold energy of liquefied natural gas | |
| CN202139209U (en) | Direct expansion type natural gas liquefaction device | |
| CN100404988C (en) | Air-contained coal gas gasification and separation process and equipment | |
| CN108211671B (en) | Energy-saving carbon dioxide regeneration and compression system and method | |
| CN109163506A (en) | With the device for assisting lower tower low energy consumption to produce low purity oxygen and high pure oxygen product simultaneously | |
| CN101285639B (en) | Pre-cooled type coal bed gas nitrogen dilated and liquefied process taking advantage of variable pressure for adsorbing residual pressure | |
| CN101165443A (en) | Chloro-silicane gaseous mixture condensation process | |
| CN109437234A (en) | A kind of compound semiconductor epitaxial tail gas recycling device and method | |
| CN112651140A (en) | Method for analyzing double-stage compression refrigeration system | |
| CN102229427B (en) | Carbon dioxide purifying device | |
| CN202382518U (en) | Device for washing and purifying synthesis gas with liquid nitrogen and cryogenically separating and recovering LNG (liquefied natural gas) | |
| CN217929406U (en) | System for liquefying synthetic ammonia | |
| CN103900346A (en) | Method and device for liquefying carbon dioxide generated through efficient gas source heat pump in cold and hot combination mode | |
| CN114485051B (en) | Liquid ammonia double-working-condition refrigerating system and liquid carbon dioxide production equipment | |
| CN102923731B (en) | Utilizing device and method for cold energy in high-purity ammonia preparation process | |
| CN102538394B (en) | Method for separating ammonia and carbon dioxide by low-temperature rectification | |
| CN105314611A (en) | Dilute nitric acid device adopting double pressure method | |
| CN101928617B (en) | Gas-liquid separation device for oxygenous coal bed | |
| CN114440553A (en) | Low-energy-consumption double-tower pure nitrogen preparation device adopting nitrogen expansion refrigeration and application method | |
| CN210624985U (en) | Carbon dioxide refrigeration heat pump system | |
| CN211821716U (en) | Recovery device for emptying gas of liquid carbon dioxide storage tank | |
| CN202304056U (en) | Double-working medium cascade directly-heated type heat pump hot water unit | |
| CN212109209U (en) | Nitrogen making device for sodium methoxide | |
| CN212504013U (en) | Energy-saving quality-improving production system for liquid carbon dioxide | |
| CN215113526U (en) | Dirty nitrogen cooling capacity utilization device in air separation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Open date: 20080423 |