CN209317377U - Purification organosilicon fractionation tail gas and the adsorption separation device for recycling organic silicon monomer - Google Patents
Purification organosilicon fractionation tail gas and the adsorption separation device for recycling organic silicon monomer Download PDFInfo
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- CN209317377U CN209317377U CN201822212137.XU CN201822212137U CN209317377U CN 209317377 U CN209317377 U CN 209317377U CN 201822212137 U CN201822212137 U CN 201822212137U CN 209317377 U CN209317377 U CN 209317377U
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Abstract
The utility model relates to Waste Disposal Technology fields, more particularly to a kind of purification organosilicon is fractionated tail gas and recycles the device of organic silicon monomer, including being equipped with adsorption tower, vacuum pump and pipeline, vacuum pump is located at below adsorption tower, it is connected between adsorption tower tower bottom and vacuum pump by pipeline, it is characterized by: adsorption tower >=2, and be connected in parallel；Described device is additionally provided with heater and cooler, and cooler one end is connect with adsorption tower tower bottom, and the other end is controlled to a vacuum pump；Heater is connect by raw material air valve with adsorption tower tower bottom.The organic silicon monomer that organosilicon is fractionated in tail gas is purified by utility model device, reduction generates the problems such as cleaning of waste heat boiler caused by a large amount of silica is difficult during the burning process, and organic silicon monomer is concentrated and is recycled, and avoids the wasting of resources；Organosilicon can be fractionated to recovery yield of monomer in addition to M4 in tail gas and reach 98% or more, monomer overall recovery is up to 95% or more；Easy to operate, adult is low.
Description
Technical field
The utility model relates to Waste Disposal Technology field more particularly to a kind of purification organosilicon fractionation tail gas and recycle
The adsorption separation device of organic silicon monomer.
Background technique
Fractionation (rectifying) process of organosilicon production can generate partial tail gas in organic silicon production process, and the tail gas is main
Ingredient is nitrogen and a small amount of chloromethanes, hydrogen chloride and methyl trichlorosilane (M1), dimethyldichlorosilane (M2), front three
The organic silicon monomers such as base chlorosilane (M3), tetramethylsilane (M4), chlorodimethyl silane (M2H), dimethyl dichlorosilane (DMCS) (MH).
Processing for organosilicon fractionation tail gas, most domestic organosilicon manufacturing enterprise are handled using burning mode,
By its burning and exhausting；External Some Enterprises produce the processing mode of gas-phase silica using burning low-boiling-point substance.
Organosilicon fractionation tail gas incineration treatment technology predominantly be fractionated tail gas enter incinerator, under the high temperature conditions with sky
Combustion reaction occurs for gas, and the organic matter in tail gas is decomposed into water vapour, carbon dioxide and hydrogen chloride；High-temperature flue gas passes through waste heat boiler
After furnace, thermal energy is recovered, and successively passes through second level cyclone dust removal, flue gas chilling, wet dedusting, hydrogen chloride absorption and alkali cleaning, will
Silica and chlorination hydrogen retrieval in flue gas, and guarantee that flue gas meets national standard discharge.
Organosilicon fractionation process generate exhaust gas during the burning process, due to the presence of silicon in organic silicon monomer, after burning
It generates a large amount of silica and is directly entered waste heat boiler, there is waste heat boiler collection ashes easily to block up, clears up the problems such as difficult, and makes
At the serious wasting of resources, such as the organic silicon monomer of these high economy is rationally recycled, then can achieve energy-saving
With the purpose for saving production cost.
With absorption method, (absorption method is that the difference of the adsorption capacity using substance on the sorbent reaches for the utility model trial
Isolated purpose is adsorbed under high pressure, is reduced pressure desorption and is known as pressure-variable adsorption；Increase temperature desorption and be known as temp.-changing adsorption) to having
Machine silicon fractionation tail gas is handled.Conventional pressure-variable adsorption separation system is run at normal temperature, this is conducive to adsorbent and sufficiently inhales
It is attached, but adsorbent reactivation is highly difficult.The organic silicon monomer of macromolecule abundant desorption, monomer can not be returned from adsorbent
Yield is low, of poor benefits, and sorbent life is short.Inventor also once attempted in such a way that the transformation that relents combines, i.e., in low temperature
It is adsorbed under high pressure, then is depressured heating desorption, theoretically recycling of the which most beneficial for organic silicon monomer.But it invents
People has found that adsorption separation system is a continuous unbroken mistake to the processing of organosilicon fractionation tail gas during actual process
Journey, when an adsorption tower heat up desorption, cool down again restore low temperature when, it is necessary to other adsorption towers are adsorbed, and
The former is time-consuming very long, completes primary heating desorption, is cooling down in the time for restoring low temperature again, is there is several adsorption tower lands
It is continuous to reach adsorption saturation state, therefore a pressure-variable adsorption separation system needs to include many adsorption towers, equipment cost is very high,
And energy consumption is also larger.
Inventor has found that the organic silicon monomer with larger molecular weight is in certain temperature higher than room temperature in the course of the research
Spend range in, adsorbent has no its adsorbance and is substantially reduced, and keep within this temperature range when, the solution of organic silicon monomer
Absorption will become to be relatively easy to, and because alternating temperature is not present, adsorption tower is substantially reduced without undergoing the temperature-fall period after desorption
Quantitative requirement of the adsorption system to adsorption tower.
Summary of the invention
In order to solve the above technical problems, the utility model provides a kind of purification organosilicon fractionation tail gas and recycles organosilicon
The adsorption separation device of monomer, heat up transformation, purifies the organic silicon monomer in organic silicon waste gas, and reduction generates during the burning process
The problems such as waste heat boiler cleaning caused by a large amount of silica is difficult, and organic silicon monomer concentration is recycled, it avoids
The wasting of resources.The recovery yield of monomer that organosilicon is fractionated in tail gas in addition to M4 can be reached 98% or more by the utility model, and monomer is total
The rate of recovery is up to 95% or more；Easy to operate, adult is low.
It solves a kind of purification organosilicon fractionation tail gas of the above technical problem and recycles the adsorbing separation dress of organic silicon monomer
It sets, including is equipped with adsorption tower, vacuum pump and pipeline, vacuum pump is located at below adsorption tower, is led between adsorption tower tower bottom and vacuum pump
Piping connection, it is characterised in that: adsorption tower >=2, and be connected in parallel；Described device is additionally provided with heater and cooler,
Cooler one end is connect with adsorption tower tower bottom, and the other end is controlled to a vacuum pump；Heater passes through raw material air valve and adsorption tower tower bottom
Connection.
Equalizing valve, flushing valve and adsorption outlet valve, equalizing valve are successively arranged above each absorption tower top in the adsorption tower
Positioned at rinsing between gas pipeline and equalizing valve pipeline, flushing valve and adsorption outlet valve be located at rinse gas pipeline and purification gas pipeline it
Between, flushing valve is located above adsorption outlet valve；It is additionally provided between purification gas pipeline and flushing gas pipeline and rinses gas regulating valve, purification
It is equipped with inflation regulating valve eventually between gas pipeline and equalizing valve, rinses gas regulating valve and inflation regulating valve is located at equalizing valve, rinses eventually
The side of valve and adsorption outlet valve；Absorption intake valve and evacuation valve, vacuum pump and evacuation are just successively arranged under each adsorption tower
Valve is connected；Cooler one end is connect with evacuation valve, and the other end is controlled to a vacuum pump；By managing accordingly between above each device
Road connection；Raw material air valve is connect with absorption intake valve, is located between absorption intake valve and evacuation valve.
Unstripped gas enters from absorption tower bottom and carries out adsorption process in adsorption tower in the utility model, and purified gas is from adsorption tower
Top discharge carries out evacuation regeneration to adsorbent bed in adsorption tower using vacuum pump, and opens at the top of adsorption tower simultaneously
Flushing valve is rinsed, and adsorption column pressure is finally finally pressurized to adsorptive pressure.
Unstripped gas successively passes through heater, raw material air valve, adsorption tower, cooler and vacuum pump, raw material in the utility model
Gas successively by absorption transformation, cooling and concentration and recovery, is cleaned and is recycled with organic silicon monomer.Being rich in after concentration is organic
The gas of silicon monomer is recovered into recycling can from evacuation gas pipeline, and the organic silicon monomer in recycling fractionation tail gas has purified original
The gas come allows the content of monomer come out inside purification gas pipeline to substantially reduce.
Optional inverse put valve is equipped between the raw material air valve and evacuation valve, raw material air valve is connect with absorption intake valve, position
Between absorption intake valve and inverse put valve.
The equalizing valve and whole fill are equipped with optional pans between regulating valve, pressure is used
Solid absorbent is filled in the adsorption tower.
Active carbon, spy can be selected according to the feed gas composition and concentration for entering absorption transformation system in the solid absorbent
Different adsorbent volume proportions can be used in kind one or more of silica gel or activated alumina combination of adsorbents, combine adsorption agent
Adsorption tower is loaded.
The monomer that organosilicon is fractionated in tail gas is adsorbed on adsorbent by utility model device in adsorption process, then
It is rinsed by vacuum pump depletion, organic silicon monomer is recycled from adsorbent, the product gas for obtaining concentrating organic silicon monomer (is taken out
Air).
The partial size of the adsorbent are as follows: 2 ~ 4mm of active carbon, 2 ~ 4mm of special silica-gel, 3 ~ 5mm of activated alumina.
The adsorption tower top and the bottom are respectively equipped with temperature measuring point.Temperature can be constant temperature in the adsorption tower.
Temperature is 30 ~ 180 DEG C in unstripped gas temperature or absorption transformer kiosk, and temperature described in prioritization scheme is 50 ~ 80 DEG C.It is former
Expect that gas is that organosilicon is fractionated tail gas.Adsorbing temperature in transformation is constant temperature.
Heated device increases unstripped gas and adsorption tower temperature in the utility model, reaches the absorption of adsorbent and regenerative process
To under the conditions of optimum balance, the absorption and regenerability of adsorbent are maximally utilized, low energy consumption and high-efficient.
Adsorptive pressure is 0.05MPa ~ 0.15MPa in adsorption tower；Adsorptive pressure 0.08MPa described in prioritization scheme ~
0.12MPa。
Unstripped gas is rinsed by absorption, equal pressure drop, inverse put (optional), evacuation in adsorption tower, is pressed in absorption transformer kiosk
Liter and final pressurising step, adsorption tower recycles in the above sequence and the timing mode of interlocking is operated.In heating pressure-variable adsorption system
In system, each adsorption tower passes through identical step, but mutually staggers in timing, to guarantee that separation process is carried out continuously.Press
There are also inverse put steps between drop step and evacuation rinsing step.Evacuate rinsing step in evacuated pressure be -0.095 ~ -
0.08MPa。
The utility model is from organosilicon fractionation tail gas, and by adsorbing separation, concentration and recovery organic silicon monomer passes through other
Mode is used, and reduces the organic silicon monomer content in emptying end gas.Using heating pressure-variable adsorption, the regeneration of adsorbent
Effect is more preferable, improves the adsorption efficiency of adsorbent.Purification and recycling organic silicon monomer for organosilicon fractionation tail gas, have
Vast market prospect and considerable economic results in society.
The organic silicon monomer that organosilicon is fractionated in tail gas is adsorbed on adsorbent by device in the utility model, remaining nitrogen
The components such as gas, chloromethanes, hydrogen chloride are discharged into incineration system from adsorption tower top.Tetramethylsilane can will be removed in purified gas
(M4) organic silicon monomer total volume content outside takes off to≤0.05%, and overall recovery >=95% of organic silicon monomer removes tetramethylsilane
The organic silicon monomer rate of recovery >=98% of alkane (M4) outside.
Detailed description of the invention
More detailed description is done to the utility model with reference to the accompanying drawing
Fig. 1 is three towers heating pressure-swing absorption apparatus flow chart in the utility model
Fig. 2 is four towers heating pressure-swing absorption apparatus flow chart in the utility model
Fig. 3 is five towers heating pressure-swing absorption apparatus flow chart in the utility model
Wherein, it is identified in figure specific as follows:
1. adsorption tower, 2. heaters, 3. coolers, 4. vacuum pumps, 5. pans, 6. adsorption outlet valves, 7. flushing valves, 8.
Equalizing valve (or filling valve eventually), 9. temperature measuring points, 10. absorption intake valves, 11. inverse put valves, 12. evacuation valves, 13. rinse gas regulating valve,
14. filling regulating valve eventually, 15. equalizing valves, 16. raw material air valves, 17. evacuate air valve.
Specific embodiment
The utility model is further described With reference to embodiment:
Embodiment 1
Device is equipped with adsorption tower, vacuum pump and pipeline, and vacuum pump is located at below adsorption tower, adsorption tower tower bottom and vacuum pump it
Between pass through pipeline and connect, it is characterised in that: the adsorption tower is 4, and is connected in parallel；Described device is additionally provided with heater and cold
But device, cooler one end are connect with adsorption tower tower bottom, and the other end is controlled to a vacuum pump；Heater passes through raw material air valve and adsorption tower
Tower bottom connection；Vacuum pump is connect with recycling can, and product gas (taking out air) is packed into recycling can.In adsorption tower on each absorption tower top
Side is successively arranged equalizing valve, flushing valve and adsorption outlet valve, and equalizing valve, which is located at, to be rinsed between gas pipeline and equalizing valve pipeline, rinses
Valve and adsorption outlet valve, which are located at, rinses between gas pipeline and purification gas pipeline, and flushing valve is located above adsorption outlet valve；Purified gas
It is additionally provided between pipeline and flushing gas pipeline and rinses gas regulating valve, purified and adjusted between gas pipeline and equalizing valve equipped with whole inflate
Valve, rinses gas regulating valve and inflation regulating valve is located at the side of equalizing valve, flushing valve and adsorption outlet valve eventually；Each adsorption tower bottom
Lower section is successively arranged absorption intake valve and evacuation valve, vacuum pump are connected with evacuation valve；Cooler one end is connect with evacuation valve, another
End is controlled to a vacuum pump；It is connected between above each device by corresponding pipeline；Raw material air valve is connect with absorption intake valve, position
Between absorption intake valve and evacuation valve.Unstripped gas enters from absorption tower bottom and carries out adsorption process in adsorption tower, purified gas from
Discharge at the top of adsorption tower carries out evacuation regeneration to adsorbent bed in adsorption tower using vacuum pump, and opens adsorption tower simultaneously
The flushing valve at top is rinsed, and adsorption column pressure is finally finally pressurized to adsorptive pressure.Adsorption tower top and the bottom are respectively equipped with
Temperature measuring point；Solid absorbent is filled in adsorption tower.The partial size of adsorbent are as follows: active carbon 2 or 4mm, special silica-gel 2 or 4mm, work
Property aluminium oxide 3 or 5mm.
Unstripped gas successively passes through heater, raw material air valve, adsorption tower, cooler and vacuum pump, raw material in the utility model
Gas successively by absorption transformation, cooling and concentration and recovery, is cleaned and is recycled with organic silicon monomer.Being rich in after concentration is organic
The gas of silicon monomer is recovered into recycling can from evacuation gas pipeline, and the organic silicon monomer in recycling fractionation tail gas has purified original
The gas come allows the content of monomer come out inside purification gas pipeline to substantially reduce.
Embodiment 2
Device is equipped with adsorption tower, vacuum pump and pipeline, and vacuum pump is located at below adsorption tower, adsorption tower tower bottom and vacuum pump it
Between pass through pipeline and connect, it is characterised in that: the adsorption tower is 4, and is connected in parallel；Described device is additionally provided with heater and cold
But device, cooler one end are connect with adsorption tower tower bottom, and the other end is controlled to a vacuum pump；Heater passes through raw material air valve and adsorption tower
Tower bottom connection.It is successively arranged equalizing valve, flushing valve and adsorption outlet valve above each absorption tower top in adsorption tower, equalizing valve is located at
It rinses between gas pipeline and equalizing valve pipeline, flushing valve and adsorption outlet valve are located between flushing gas pipeline and purification gas pipeline,
Flushing valve is located above adsorption outlet valve；It is additionally provided between purification gas pipeline and flushing gas pipeline and rinses gas regulating valve, purified gas
It is equipped with inflation regulating valve eventually between pipeline and equalizing valve, rinses gas regulating valve and inflation regulating valve is located at equalizing valve, flushing valve eventually
With the side of adsorption outlet valve；Absorption intake valve and evacuation valve, vacuum pump and evacuation valve are just successively arranged under each adsorption tower
It is connected；Cooler one end is connect with evacuation valve, and the other end is controlled to a vacuum pump；Pass through corresponding pipeline between above each device
Connection；Raw material air valve is connect with absorption intake valve, is located between absorption intake valve and evacuation valve.Unstripped gas from absorption tower bottom into
Enter and carry out adsorption process in adsorption tower, purified gas is discharged at the top of adsorption tower, using vacuum pump to the adsorbent bed in adsorption tower
Layer carries out evacuation regeneration, and the flushing valve opened at the top of adsorption tower simultaneously is rinsed, finally by the final pressurising of adsorption column pressure
To adsorptive pressure.Adsorption tower top and the bottom are respectively equipped with temperature measuring point；Solid absorbent is filled in adsorption tower.Equalizing valve fills tune with whole
It saves and is equipped with a pans between valve.
Optional inverse put valve is additionally provided between raw material air valve and evacuation valve, raw material air valve connect with absorption intake valve, is located at
It adsorbs between intake valve and inverse put valve.
Solid absorbent is filled in adsorption tower.
Active carbon, extraordinary silicon can be selected according to the feed gas composition and concentration for entering absorption transformation system in solid absorbent
Different adsorbent volume proportions can be used to suction in one or more of glue or activated alumina combination of adsorbents, combine adsorption agent
Attached tower is loaded.The partial size of adsorbent are as follows: active carbon 3mm, special silica-gel 3mm, activated alumina 4mm.Adsorption tower top and the bottom
It is respectively equipped with temperature measuring point.Temperature can be constant temperature in the adsorption tower.
Unstripped gas successively passes through heater, raw material air valve, adsorption tower, cooler in the utility model, and unstripped gas successively passes through
Absorption transformation, cooling and recycling are crossed, is cleaned and is recycled with organic silicon monomer.Temperature in unstripped gas temperature or absorption transformer kiosk
It is 30 ~ 180 DEG C.Unstripped gas is that organosilicon is fractionated tail gas.Temperature described in prioritization scheme is 50 ~ 80 DEG C.It is adsorbed in prioritization scheme
Temperature is constant temperature in transformation.
Heated device increases unstripped gas and adsorption tower temperature in the utility model, reaches the absorption of adsorbent and regenerative process
To under the conditions of optimum balance, the absorption and regenerability of adsorbent are maximally utilized, low energy consumption and high-efficient.
Adsorptive pressure is 0.05MPa ~ 0.15MPa in adsorption tower；Adsorptive pressure 0.08MPa described in prioritization scheme ~
0.12MPa.Absorption transformation step described in the utility model is specific as follows:
(1) (A) is adsorbed:
Enter using organosilicon fractionation tail gas as unstripped gas from absorption tower bottom, is carried out in the adsorption tower equipped with adsorbent
Adsorption process, adsorption tower group can be by more than two adsorption tower groups at when adsorbent adsorption saturation or purified gas (dropping a hint)
After setting index, stop absorption.
(2) pressure drop (ED):
For the rate of recovery for improving organic silicon monomer, pressure is carried out in the adsorption tower and adsorption tower group after the completion of adsorption step and is risen
The adsorption tower or pans of step carry out equal voltage drop step, and can reduce fluid phase nitrogen, hydrogen chloride and chloromethanes in tower
Content, improve product gas in organic silicon monomer concentration.
(3) inverse put (D):
After the completion of equal voltage drop step, in order to reduce the evacuation load of vacuum pump, it is inverse from absorption tower bottom to open inverse put valve
It puts to normal pressure.This step can be according to specific operating condition and pressure reduced pressure chooses whether to carry out, and such as without inverse put step, presses
Evacuation rinsing step is directly entered after drop step.
(4) it evacuates and rinses (VP):
After the completion of equal pressure drop or inverse put, the evacuation valve of adsorption tower bottom part down is opened, using vacuum pump in adsorption tower
It is adsorbent bed to carry out evacuation regeneration；And the flushing valve of adsorption tower over top is opened, using being adsorbed in adsorption tower group
The purified gas of step is rinsed adsorbent in tower simultaneously, to reach optimal adsorbent regeneration effect.
(5) pressure rises (ER):
Equalizing valve is opened, the absorption of equal voltage drop step is carried out in the adsorption tower and adsorption tower group after evacuation rinsing step
Tower or pans carry out pressure and rise a step, to improve organic silicon monomer yield, and reduce absorption to rise to adsorptive pressure institute necessary
Energy consumption.
(6) final pressurising (FR):
After the completion of pressure rises step, final equalizer valve is opened, purified gas is introduced at the top of adsorption tower, by adsorption column pressure
It finally is pressurized to adsorptive pressure, a complete cycle period is completed with this, carries out sorption cycle next time as needed.
Test example one
Referring to Fig. 1, the present apparatus is heated up pressure-variable adsorption process using three towers, filling centainly matches in adsorption tower active carbon and
Special silica-gel and activated alumina adsorbents combination.Unstripped gas treating capacity 80Nm3/ h, unstripped gas admission pressure 0.08MPa, vacuum
Spend -0.095 ~ -0.08MPa.
Process flow steps: unstripped gas is warming up to 60 DEG C by heater or adsorption tower is warming up to 60 DEG C, and absorption is pressed
Drop, inverse put are evacuated and are rinsed, and pressure rises, final pressurising.
It can obtain purification 67 Nm of tolerance3/ h evacuates 13 Nm of product tolerance3/h。
1 three tower of table heating pressure-variable adsorption time-scale
Table 2 tests 1 unstripped gas composition
Table 3 tests 1 purified gas composition
Table 4 tests 1 product gas (taking out air) composition
Test example two
Referring to fig. 2, the present apparatus is heated up pressure-variable adsorption process using four towers, filling centainly matches in adsorption tower active carbon and
Special silica-gel combination of adsorbents.Unstripped gas treating capacity 150Nm3/h, unstripped gas admission pressure 0.1MPa, vacuum degree -0.095 ~ -
0.08MPa。
Process flow steps: unstripped gas is warming up to 45 DEG C by heater or adsorption tower is warming up to 45 DEG C, and absorption is pressed
Drop is evacuated and is rinsed, and pressure rises, final pressurising.
Purification 113 Nm3/h of tolerance can be obtained, 37 Nm3/h of product tolerance is evacuated.
5 four tower of table heating pressure-variable adsorption time-scale
Table 6 tests 2 unstripped gas composition
Table 7 tests 2 purified gas composition
Table 8 tests 2 product gas (taking out air) composition
Test example three
Referring to Fig. 3, the present apparatus using double tower while feeding absorption, in adsorption tower using five towers heating pressure-variable adsorption process
Load the active carbon and special silica-gel combination of adsorbents centainly matched.Unstripped gas treating capacity 350Nm3/h, unstripped gas admission pressure
0.1 ~ 0.12MPa, vacuum degree -0.095 ~ -0.08MPa.
Process flow steps: unstripped gas is warming up to 70 DEG C by heater or adsorption tower is warming up to 70 DEG C, and absorption is pressed
Drop is evacuated and is rinsed, and pressure rises, final pressurising.
Purification 255 Nm3/h of tolerance can be obtained, product tolerance 95Nm3/h is evacuated.
9 five tower of table heating pressure-variable adsorption time-scale
Table 10 tests 3 unstripped gas composition
Table 11 tests 3 purified gas composition
Table 12 tests 3 product gas (taking out air) composition
The utility model uses heating pressure swing adsorption technique and returns to the organic silicon monomer in organosilicon fractionation tail gas
It receives, pressure-variable adsorption and temp.-changing adsorption, which are combined, desorbs organic silicon monomer component from adsorbent.And by repetition test, determine
The technological parameter of heating pressure-variable adsorption, and selected reasonable adsorbent, so that technique is reached optimum efficiency and industrial requirement.
The monomer that organosilicon is fractionated in tail gas is adsorbed on adsorbent by utility model device in adsorption process, then
By evacuating the method rinsed, organic silicon monomer is recycled from adsorbent, the product gas for obtaining concentrating organic silicon monomer (is taken out
Air).The organic silicon monomer that organosilicon is fractionated in tail gas is purified by utility model device, reduction produces during the burning process
The problems such as waste heat boiler cleaning caused by raw a large amount of silica is difficult, and organic silicon monomer is concentrated and is recycled, it avoids
The wasting of resources.The recovery yield of monomer that organosilicon is fractionated in tail gas in addition to M4 can be reached 98% or more by the utility model, and monomer is total
The rate of recovery is up to 95% or more；Easy to operate, adult is low.
The method that the utility model application heating pressure swing adsorption method is fractionated tail gas recycle organic silicon monomer from organosilicon, by two
Platform or two or more are filled with the adsorption tower and a series of sequence valves composition adsorption separation system of adsorbent, to organosilicon point
Tail gas is evaporated to be adsorbed and recycle organic silicon monomer.In the range of absorption bed temperature is maintained at 30 ~ 180 DEG C in adsorption tower
(50 ~ 80 DEG C of optimum operating temperature), under process control valve action organosilicon be fractionated tail gas in each adsorption tower respectively by with
Under several steps: absorption, pressure, and/or inverse put, evacuate rinse, final boosting, adsorption tower recycle in the above sequence and timing friendship
Wrong mode is operated；The monomer that organosilicon is fractionated in tail gas is adsorbed on adsorbent, then by evacuating the method rinsed,
Organic silicon monomer is recycled from adsorbent, the rate of recovery of organic silicon monomer is up to 95% or more.This method can be organic by recycling
Silicon is fractionated the monomer in tail gas, avoids organosilicon fractionation tail gas during the burning process, generates a large amount of silica and be directly entered
Waste heat boiler makes waste heat boiler there is the problems such as collection ash is easily stifled, cleaning is difficult, and recycling gas can be used, and is a kind of
Method novel process organosilicon fractionation tail gas and recycle organic silicon monomer.
The advantages of basic principles and main features and the utility model of the utility model have been shown and described above, on
It states and only illustrates the principles of the present invention described in embodiment and specification, do not departing from the spirit and scope of the utility model
Under the premise of, the utility model also has various changes and improvements, these changes and improvements fall within claimed reality
With in novel range.The range of the requires of the utility model protection is defined by the appending claims and its equivalent thereof.
Claims (8)
1. a kind of purification organosilicon fractionation tail gas simultaneously recycles the adsorption separation device of organic silicon monomer, including it is equipped with adsorption tower, true
Sky pump and pipeline, vacuum pump are located at below adsorption tower, are connected between adsorption tower tower bottom and vacuum pump by pipeline, and feature exists
In: adsorption tower >=2, and be connected in parallel；Described device is additionally provided with heater and cooler, cooler one end and adsorption tower tower
Bottom connection, the other end are controlled to a vacuum pump；Heater is connect by raw material air valve with adsorption tower tower bottom.
2. a kind of purification organosilicon fractionation tail gas according to claim 1 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: it is successively arranged equalizing valve, flushing valve and adsorption outlet valve above each absorption tower top in the adsorption tower,
Equalizing valve, which is located at, to be rinsed between gas pipeline and equalizing valve pipeline, and flushing valve and adsorption outlet valve are located at flushing gas pipeline and purified gas
Between pipeline, flushing valve is located above adsorption outlet valve；It is additionally provided between purification gas pipeline and flushing gas pipeline and rinses controlled atmosphere section
Valve purifies and is equipped with inflation regulating valve eventually between gas pipeline and equalizing valve, and flushing gas regulating valve and eventually inflation regulating valve, which are located at, presses
Valve, flushing valve and adsorption outlet valve side；Absorption intake valve and evacuation valve, vacuum pump are just successively arranged under each adsorption tower
It is connected with evacuation valve；Cooler one end is connect with evacuation valve, and the other end is controlled to a vacuum pump；Pass through phase between above each device
The pipeline connection answered；Raw material air valve is connect with absorption intake valve, is located between absorption intake valve and evacuation valve.
3. a kind of purification organosilicon fractionation tail gas according to claim 2 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: optional inverse put valve is equipped between the raw material air valve and evacuation valve, raw material air valve and absorption intake valve connect
It connects, is located between absorption intake valve and inverse put valve.
4. a kind of purification organosilicon fractionation tail gas according to claim 2 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: the equalizing valve and whole fill are equipped with optional pans between regulating valve.
5. a kind of purification organosilicon fractionation tail gas according to claim 1 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: be filled with solid absorbent in the adsorption tower.
6. a kind of purification organosilicon fractionation tail gas according to claim 5 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: the solid absorbent can be selected and live according to the feed gas composition and concentration for entering absorption transformation system
Different adsorbents can be used in one or more of property charcoal, special silica-gel or activated alumina combination of adsorbents, combine adsorption agent
Volume proportion loads adsorption tower.
7. a kind of purification organosilicon fractionation tail gas according to claim 5 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: the partial size of the adsorbent are as follows: 2 ~ 4mm of active carbon, 2 ~ 4mm of special silica-gel, 3 ~ 5mm of activated alumina.
8. a kind of purification organosilicon fractionation tail gas according to claim 1 and the adsorbing separation dress for recycling organic silicon monomer
It sets, it is characterised in that: the adsorption tower top and the bottom are respectively equipped with temperature measuring point.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111204712A (en) * | 2020-03-09 | 2020-05-29 | 西南化工研究设计院有限公司 | Pressure swing adsorption gas hydrogen separation and purification system and separation and purification method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111204712A (en) * | 2020-03-09 | 2020-05-29 | 西南化工研究设计院有限公司 | Pressure swing adsorption gas hydrogen separation and purification system and separation and purification method thereof |
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