CN106082235A - A kind of apparatus and method mixed for STC vaporization and hydrogen - Google Patents
A kind of apparatus and method mixed for STC vaporization and hydrogen Download PDFInfo
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- CN106082235A CN106082235A CN201610442155.XA CN201610442155A CN106082235A CN 106082235 A CN106082235 A CN 106082235A CN 201610442155 A CN201610442155 A CN 201610442155A CN 106082235 A CN106082235 A CN 106082235A
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- Prior art keywords
- stc
- hydrogen
- carburator
- charging aperture
- outlet
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/08—Compounds containing halogen
- C01B33/107—Halogenated silanes
- C01B33/1071—Tetrachloride, trichlorosilane or silicochloroform, dichlorosilane, monochlorosilane or mixtures thereof
-
- 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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- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The invention discloses a kind of apparatus and method mixed for STC vaporization and hydrogen, this device includes carburator, carburator is sequentially provided with the outlet of liquid STC, hydrogen inlet, packing section, STC charging aperture, demister and mixed gas outlet from the bottom to top, the outlet of liquid STC connects heat exchanger by circulating pump, the outlet of heat exchanger is connected to STC charging aperture, this device also includes STC feed pipe, and it is connected to STC charging aperture.These apparatus and method can efficiently, stable, equably STC is vaporized while and H2Mixing；Having control difficulty low, operating flexibility is big, requires low to thermal source, and boil-off rate is stable, and heat utilization rate is high, the advantage such as mixs homogeneously and ratio adjusting range is big with hydrogen.
Description
Technical field
The present invention relates to STC vaporization and hydrogen mixed cell in cold hydrogenation apparatus, be specifically related to a kind of for STC vaporization and
The apparatus and method of hydrogen mixing, can be greatly reduced STC vapourizing temperature.
Background technology
Cold hydrogenation apparatus is will to react the mistake producing TCS (trichlorosilane) after hydrogen, STC (Silicon chloride .) mixing with silica flour
Journey.This reaction is to complete under ＞ 500 DEG C and ＞ 2MPa, and this just requires the vaporization feeding pressure ＞ 2MPa of STC and hydrogen.This dress
Put the carburetion system that must be equipped with STC and hydrogen.The vaporization mode of a kind of efficient stable can ensure that the operation of cold hydrogenation apparatus
Stable and higher reaction conversion ratio.And STC boiling point ＞ 194 DEG C, the vaporization of STC to be completed, heating source temperature under operating pressure
Degree have to be larger than the boiling point of STC.Steam source common in factory, generally within 200 DEG C, is difficult to use in this as thermal source.
For solving heat source, common employing heated by natural gas conduction oil in industry, the heat-conducting oil heating STC vaporization of high temperature
Mode.Which long flow path, equipment complexity (includes natural gas fired incinerators, heat conduction oil circulating pump, conduction oil expansion drum, heat conduction
Oil tank, the equipment such as conduction oil light component condenser), operation complicated difficult is safeguarded, conduction oil is big for environment pollution, if conduction oil leakage
Enter system, whole cold hydrogenation system will be produced the biggest pollution, it is difficult to remove.Construction cost and maintenance cost also compare simultaneously
High.
Summary of the invention
It is an object of the invention to provide a kind of apparatus and method mixed for STC vaporization and hydrogen；It can not use and lead
Thermal oil system, reduces the vapourizing temperature of STC in the case of not dropping low operating pressure.
For solving above-mentioned technical problem, the technical solution adopted in the present invention is: a kind of vaporization for STC mixes with hydrogen
Device, including carburator, carburator be sequentially provided with from the bottom to top the outlet of liquid STC, hydrogen inlet, packing section, STC charging
Mouth, demister and mixed gas outlet, the outlet of liquid STC connects heat exchanger by circulating pump, and the outlet of heat exchanger is connected to STC
Charging aperture, this device also includes STC feed pipe, and it is connected to STC charging aperture.
The bottom of described carburator or circulating-pump outlet are provided with impurity outlet.Can in carburator high-boiling components interval or
Person discharges continuously.Impurity therein includes high-boiling components.
Described packing section is built-in regular or irregular filler.
Described heat exchanger is vapor heat exchanger.
Described STC feed pipe converges between heat exchanger exit and STC charging aperture, is then connected to STC charging aperture.
Hydrogen and the STC of STC charging aperture at described hydrogen inlet are above its corresponding vapourizing temperature.
Described circulating pump is set to multiple, and is connected in parallel.
Described carburator top pressure normal value is 2.0～4.0MPa, and head temperature normal value is 120～170 DEG C.
Device described in employing, to STC vaporization and the method for hydrogen mixing, concretely comprises the following steps:
Hydrogen adds carburator from hydrogen inlet, and STC carries out spray charging from STC charging aperture, without the STC vaporized by filling out
Material section overflow is to bottom carburator, and a part of liquid phase STC vaporizes, bottom carburator with the abundant counter current contact of hydrogen at packing section
Liquid phase STC through circulating pump be delivered to heat exchanger heating after enter STC charging aperture be circulated, circulating-pump outlet flow 130～
150t/h；The STC of vaporization mixes through carburator top with hydrogen, and controlling carburator top pressure is 2.0～4.0MPa, and temperature is
120～170 DEG C, the blended gas outlet of gas discharges.
The flow of the hydrogen that described hydrogen inlet adds is 1.0～2.0t/h, from the flow of the STC that STC charging aperture adds
Scope 45～75t/h.
The present invention is for reducing STC vapourizing temperature, and in using hydrogen to reduce carburator, STC dividing potential drop is to ensure at a lower temperature
Complete the vaporization of STC.
It is fully contacted at carburator packing section, hydrogen and STC, largely reduces STC dividing potential drop, reduce STC boiling point, exchange
The temperature requirement of hot device reduces, and steam common in factory can be used as heating source and uses.And avoid gas-liquid mixed in heat exchange
Carry out at pipe, prevent heat exchanger tube from shaking, the safe long-term operation of equipment is effectively ensured.Meanwhile, STC and hydrogen are in packing section pair
Stream vaporization, it is ensured that both have bigger contact area, make hydrogen and STC reach saturated at the operational, is more beneficial for control
Make both charge proportions, to reach the purpose of steady production.
The present invention can efficiently, stable, equably STC is vaporized while and H2Mixing, has control difficulty low, operation
Elastic big, thermal source is required low, boil-off rate is stable, and heat utilization rate is high, mixs homogeneously with hydrogen and ratio adjusting range is big
Etc. advantage.Meanwhile, the situations such as carburator tube bank produced by tradition vaporization mode shakes, vaporization is unstable all obtain the most substantially
Improve.The heat-conducting oil system cancelled decreases the fault rate of vaporization unit, also reduces production cost and maintenance cost can be done
To the most non-maintaining, owing to system becomes simpler, operation is more stable, the most more convenient management.
Accompanying drawing explanation
Fig. 1 is the structural representation of apparatus of the present invention.
Detailed description of the invention
Further illustrate the present invention below in conjunction with embodiment and accompanying drawing, but the scope of protection of present invention is not limited to
Scope in embodiment statement.
As it is shown in figure 1, a kind of device mixed for STC vaporization and hydrogen, including carburator 1, carburator 1 is from the bottom to top
It is sequentially provided with liquid STC outlet 11, hydrogen inlet 12, packing section 13, STC charging aperture 14, demister 15 and mixed gas outlet
16, liquid STC outlet 11 connects heat exchanger 3 by circulating pump 2, and the outlet of heat exchanger is connected to STC charging aperture 14, and this device is also
Including STC feed pipe 4, it is connected to STC charging aperture 14.
Further, bottom or the circulating-pump outlet of described carburator is provided with impurity outlet.
Further, described packing section is built-in regular or irregular filler, and filler material used is 316L, foam removal equipment
Matter is 316L.
Further, described heat exchanger 3 is vapor heat exchanger.
Further, described STC feed pipe 4 converges between heat exchanger exit and STC charging aperture, is then connected to
STC charging aperture 14.
Further, the STC of hydrogen at described hydrogen inlet 12 and STC charging aperture 14 is above it and vaporizes temperature accordingly
Degree.
Further, described circulating pump 2 is set to multiple, and is connected in parallel.
Device described in employing is to STC vaporization and the method for hydrogen mixing, it is characterised in that concretely comprise the following steps:
Hydrogen adds carburator from hydrogen inlet, and STC carries out spray charging from STC charging aperture, without the STC vaporized by filling out
Material section overflow is to bottom carburator, and a part of liquid phase STC vaporizes, bottom carburator with the abundant counter current contact of hydrogen at packing section
Liquid phase STC enters STC charging aperture after circulating pump is delivered to heat exchanger heating and is circulated；The STC of vaporization is blended with hydrogen
Discharge by mixed gas outlet.
Use this device example operation design parameter as follows: (following example heating steam is that the 1.4MPa of 195 DEG C steams
Vapour)
According to above example data analysis, when STC charging and hydrogen are adjusted, the steam source of 1.4MPa
Working condition requirement can be met very well.Boil-off rate and outlet mixed gases matching are stable simultaneously, and the STC in mixed gas is after testing
Reach the saturation under outlet temperature and pressure.Absolutely prove this carburettor design and the reasonability of vaporization mode.
Claims (10)
1. one kind for STC vaporization and hydrogen mixing device, it is characterised in that: include carburator (1), carburator (1) by under
Supreme liquid STC that is sequentially provided with exports (11), hydrogen inlet (12), packing section (13), STC charging aperture (14), demister (15)
With mixed gas outlet (16), liquid STC outlet (11) connects heat exchanger (3) by circulating pump (2), and the outlet of heat exchanger connects
To STC charging aperture (14), this device also includes STC feed pipe (4), and it is connected to STC charging aperture (14).
Device the most according to claim 1, it is characterised in that: the bottom of described carburator or circulating-pump outlet are provided with miscellaneous
Matter outlet.
Device the most according to claim 1, it is characterised in that: described packing section is built-in regular or irregular filler.
Device the most according to claim 1, it is characterised in that: described heat exchanger (3) is vapor heat exchanger.
Device the most according to claim 1, it is characterised in that: described STC feed pipe (4) is entered at heat exchanger exit and STC
Converge between material mouth, be then connected to STC charging aperture (14).
Device the most according to claim 1, it is characterised in that: the hydrogen at described hydrogen inlet (12) place and STC charging aperture
(14) STC is above its corresponding vapourizing temperature.
Device the most according to claim 1, it is characterised in that: described carburator top pressure normal value is 2.0 ~
4.0MPa, head temperature normal value is 120 ~ 170 DEG C.
Device the most according to claim 1, it is characterised in that: described circulating pump (2) is set to multiple, and is connected in parallel.
9. use the device described in claim 1-8 any one to STC vaporization and the method for hydrogen mixing, it is characterised in that
Concretely comprise the following steps:
Hydrogen adds carburator from hydrogen inlet, and STC carries out spray charging from STC charging aperture, without the STC vaporized by packing section
Overflow is to bottom carburator, and a part of liquid phase STC vaporizes with the abundant counter current contact of hydrogen at packing section, carburator bottom liquid phases
STC enters STC charging aperture after circulating pump is delivered to heat exchanger heating and is circulated, circulating-pump outlet flow 130 ~ 150t/h；
The STC of vaporization mixes through carburator top with hydrogen, and controlling carburator top pressure is 2.0 ~ 4.0MPa, and temperature is 120 ~ 170
DEG C, the blended gas outlet of gas discharges.
Method the most according to claim 9, it is characterised in that: the flow of hydrogen that described hydrogen inlet adds is 1.0 ~
2.0t/h, from the range of flow 45 ~ 75t/h of the STC that STC charging aperture adds.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610442155.XA CN106082235B (en) | 2016-06-17 | 2016-06-17 | A kind of device and method for STC vaporizations and hydrogen mixing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610442155.XA CN106082235B (en) | 2016-06-17 | 2016-06-17 | A kind of device and method for STC vaporizations and hydrogen mixing |
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| Publication Number | Publication Date |
|---|---|
| CN106082235A true CN106082235A (en) | 2016-11-09 |
| CN106082235B CN106082235B (en) | 2018-06-15 |
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| CN201610442155.XA Active CN106082235B (en) | 2016-06-17 | 2016-06-17 | A kind of device and method for STC vaporizations and hydrogen mixing |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201701755U (en) * | 2010-03-12 | 2011-01-12 | 安徽昊源化工集团有限公司 | Improved gasifier for producing morpholine |
| CN102249242A (en) * | 2011-06-15 | 2011-11-23 | 四川新光硅业科技有限责任公司 | Trichlorosilane vaporizing process |
| CN102730691A (en) * | 2012-07-10 | 2012-10-17 | 内蒙古盾安光伏科技有限公司 | Energy utilization in polysilicon hydrogenation process |
| CN102766021A (en) * | 2012-07-24 | 2012-11-07 | 唐山市冀东溶剂有限公司 | Production system and production method for continuously producing ethanol by ethyl acetate through using hydrogenation |
| CN203451229U (en) * | 2013-09-23 | 2014-02-26 | 华陆工程科技有限责任公司 | Novel silicon tetrachloride vaporizing device |
| CN204529328U (en) * | 2015-04-01 | 2015-08-05 | 四川永祥多晶硅有限公司 | A kind of silicon tetrachloride vaporization device |
-
2016
- 2016-06-17 CN CN201610442155.XA patent/CN106082235B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201701755U (en) * | 2010-03-12 | 2011-01-12 | 安徽昊源化工集团有限公司 | Improved gasifier for producing morpholine |
| CN102249242A (en) * | 2011-06-15 | 2011-11-23 | 四川新光硅业科技有限责任公司 | Trichlorosilane vaporizing process |
| CN102730691A (en) * | 2012-07-10 | 2012-10-17 | 内蒙古盾安光伏科技有限公司 | Energy utilization in polysilicon hydrogenation process |
| CN102766021A (en) * | 2012-07-24 | 2012-11-07 | 唐山市冀东溶剂有限公司 | Production system and production method for continuously producing ethanol by ethyl acetate through using hydrogenation |
| CN203451229U (en) * | 2013-09-23 | 2014-02-26 | 华陆工程科技有限责任公司 | Novel silicon tetrachloride vaporizing device |
| CN204529328U (en) * | 2015-04-01 | 2015-08-05 | 四川永祥多晶硅有限公司 | A kind of silicon tetrachloride vaporization device |
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| CN106082235B (en) | 2018-06-15 |
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