CN212188425U - Gaseous phase white carbon black tail gas processing system - Google Patents
Gaseous phase white carbon black tail gas processing system Download PDFInfo
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- CN212188425U CN212188425U CN202020685113.0U CN202020685113U CN212188425U CN 212188425 U CN212188425 U CN 212188425U CN 202020685113 U CN202020685113 U CN 202020685113U CN 212188425 U CN212188425 U CN 212188425U
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Abstract
The utility model provides a gaseous phase white carbon black tail gas processing system, including the booster fan, sack cleaner and the synthetic furnace that link to each other in proper order, along the air current flow direction, the exit end of synthetic furnace connects gradually cooling device, drying tower, gas compressor, high-pressure buffer tank and pressure swing adsorption tower group, still is provided with chlorine concentration detector at the exit end of cooling device simultaneously, the utility model discloses in the synthetic furnace through excessive hydrogen with the chlorine in the tail gas transform into hydrogen chloride gas, through subsequent dehydration, cooling separation and pressure swing adsorption separation obtain high-purity compressed hydrogen chloride gas, compare with the conventional art, the utility model discloses a mode of burning turns into chlorine into hydrogen chloride gas, the quality of product can not receive the influence of tail gas composition concentration change, also need not be equipped with a large amount of hydrogen chloride and chlorine absorption equipment simultaneously, the environmental protection discharge pressure of enterprise obtains reducing, and the economic benefit of enterprises is improved.
Description
Technical Field
The utility model relates to a fumed silica production facility technical field, concretely relates to fumed silica tail gas processing system.
Background
At present, a large amount of tail gas containing hydrogen chloride gas is generated in the production process of fumed silica and needs to be treated, and the tail gas is generally treated by the following steps in the prior art: 1. spraying hydrochloric acid on the tail gas of the fumed silica to remove dust in the tail gas; 2. the absorption of hydrogen chloride in tail gas is generally divided into a multistage filler absorption tower which uses dilute hydrochloric acid to absorb hydrogen chloride; 3. washing the tail gas with water, wherein water is used as an absorbent in a washing tower to absorb hydrogen chloride; 4. the alkaline tower absorbs chlorine in the tail gas by using sodium hydroxide as an absorbent and produces sodium hypochlorite as a byproduct; 5. and (5) exhausting tail gas.
However, in the field of fumed silica production, because fumed silica formulations of different manufacturers are different, even if the formulations of the same manufacturer are adjusted, if the above method is adopted for tail gas treatment, the concentration of hydrogen chloride in tail gas is often changed, the quality and concentration of hydrochloric acid and sodium hypochlorite are unstable, the hydrochloric acid and the sodium hypochlorite are not suitable for recycling, and the recycled product cannot be treated; meanwhile, the hydrochloric acid serving as a byproduct in the market is in excess supply at present, and post-treatment can be carried out only by subsidy, so that the economic burden of enterprises is increased invisibly.
SUMMERY OF THE UTILITY MODEL
Aiming at the defect of unstable quality of byproducts in the prior art, the utility model discloses a gas phase white carbon black tail gas treatment system, which can convert chlorine in tail gas into hydrogen chloride gas for utilization, thereby not only realizing the purification of tail gas, but also reducing the environmental protection discharge pressure of enterprises; meanwhile, compared with hydrochloric acid, the application range of the hydrogen chloride gas is wider, and the economic value of the by-product of the product is improved.
The utility model discloses a following technical scheme realizes above-mentioned purpose:
a fumed silica tail gas treatment system comprises a bag-type dust remover, wherein the inlet end of the bag-type dust remover is connected with a tail gas booster fan, and the outlet end of the bag-type dust remover is connected with a synthesis furnace for burning and synthesizing hydrogen chloride gas; the outlet end of the synthesis furnace is sequentially provided with a cooling device, a drying tower, a gas compressor and a high-pressure buffer tank, and the outlet end of the high-pressure buffer tank is provided with a pressure swing adsorption tower set for separating out hydrogen chloride gas; and a chlorine concentration detector is arranged at the outlet end of the cooling device.
Preferably, the bottom of the bag-type dust collector is provided with a discharge opening, and the discharge opening is connected with a rotary unloader.
Preferably, the cooling device comprises a waste heat boiler and a gas cooler which are connected in sequence, and the chlorine concentration detector is positioned between the waste heat boiler and the gas cooler.
Preferably, the upper end and the lower end of the drying tower are respectively provided with a spray pipe and a return pipe, and a circulating pump and a cooler are sequentially connected between the return pipe and the spray pipe according to the flowing direction; the bottom of the drying tower is also provided with a discharge outlet, the discharge outlet is connected with a pressure filtration pump and a membrane filter at one time according to the flowing direction, and the outlet end of the membrane filter is connected with a cooler.
Preferably, a cyclone separator and a low-pressure buffer tank are sequentially arranged between the drying tower and the gas compressor, a solid discharge port of the cyclone separator is communicated with the drying tower, and a gas discharge port of the cyclone separator is connected with the low-pressure buffer tank.
Preferably, the outer surface of the synthesis furnace is provided with a cooling cavity, and the upper end and the lower end of the cooling cavity are respectively provided with a cooling medium outlet and a cooling medium inlet.
Preferably, the upper part of the synthesis furnace is provided with a hydrogen inlet, a chlorine inlet and a reaction gas inlet, the synthesis furnace is internally provided with a first annular guide plate and a second annular guide plate which respectively correspond to the chlorine inlet and the reaction gas inlet, and a chlorine layer and a reaction tail gas layer are sequentially formed in the circumferential direction of the hydrogen flow from inside to outside.
Preferably, a third annular guide plate and a second hydrogen inlet which are matched with each other are also arranged in the synthesis furnace, so that a circle of hydrogen layer is wrapped outside the reaction tail gas layer.
Preferably, a first-stage condenser and a second-stage condenser are sequentially connected between the gas compressor and the high-pressure buffer tank, and discharge ports of the first-stage condenser and the second-stage condenser are connected to the silane condensing tank.
Preferably, the nitrogen and oxygen discharge ports of the pressure swing adsorption tower set are also connected with a washing tower, and the washing tower adopts clear water or alkali solution as a cleaning agent.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. the utility model comprises a booster fan, a bag-type dust collector and a synthesis furnace which are connected in turn, wherein the outlet end of the synthesis furnace is connected with a cooling device, a drying tower, a gas compressor, a high-pressure buffer tank and a pressure swing adsorption tower set in turn along the flow direction of air flow, meanwhile, a chlorine concentration detector is arranged at the outlet end of the cooling device, the utility model uses excessive hydrogen to find chlorine in the tail gas in the synthesis furnace and convert the chlorine into hydrogen chloride gas, and then high-purity compressed hydrogen chloride gas is obtained through subsequent dehydration, cooling separation and pressure swing adsorption separation, compared with the prior art, the product of the utility model is compressed hydrogen chloride gas, the unstable content of the hydrogen chloride gas in the tail gas only has certain influence on the yield of the hydrogen chloride gas, without any influence on the quality of the product, while the quality of the final product is not stable if the by-product is hydrochloric acid.
Secondly, the final product of the utility model is high-purity hydrogen chloride gas which is a more elementary chemical raw material, and compared with hydrochloric acid, the high-concentration hydrogen chloride gas has larger freedom in use; the hydrochloric acid in the existing market has serious surplus capacity and can be treated only by patching, so that the relevant equipment of the utility model can avoid the malignant competition of the market, find breakthrough ports for treating tail gas of enterprises in other fields and reduce the economic burden of the enterprises;
simultaneously compared with the prior art, the utility model discloses need not be equipped with equipment such as corresponding tail gas cleaning and caustic wash tower, can not produce a large amount of industrial waste water, environmental protection performance has obtained showing and has improved.
2. The utility model discloses a sack cleaner bottom is provided with the bin outlet, the bin outlet is connected with rotatory unloader, through piling up quick, timely continuous discharge of material in the rotatory unloader realizes the dust remover, avoids the material to pile up in the dust remover inside and influences its normal work, guarantees the continuity of whole system operation, improves the efficiency of tail gas treatment.
3. The utility model discloses a cooling device is including consecutive exhaust-heat boiler and gas cooler, chlorine concentration detector is located between exhaust-heat boiler and the gas cooler, cools down the gas of accomplishing the burning through exhaust-heat boiler and gas cooler on the one hand, guarantees going on smoothly of follow-up dehydration reaction, and on the other hand retrieves the heat of gas and recycles, reduces the equipment energy consumption, improves the economic benefits of mill.
4. The utility model is characterized in that the upper and lower ends of the re-drying tower are respectively provided with a spray pipe and a return pipe, and a circulating pump and a cooler are sequentially connected between the return pipe and the spray pipe according to the flowing direction; chlorosilane is adopted in the drying tower as a dehydrating agent, the reaction of chlorosilane and water is an exothermic reaction, the temperature of spraying silane is effectively controlled by a circulating pump and a cooler, the abnormal rise of the temperature of the drying tower is avoided, and the safe operation of equipment is ensured; simultaneously the bottom of drying tower still is provided with the bin outlet, according to the flow direction, and the bin outlet once is connected with pressure filtration pump and membrane filter, the exit end of membrane filter links to each other with the cooler, installs micron order ceramic membrane filter core in the membrane filter, and it can be with the silica separation that the hydrolysis produced, guarantees the purity of chlorosilane to guarantee the dehydration quality of drying tower to the tail gas.
5. The utility model discloses still set gradually cyclone and low pressure buffer tank between drying tower and gas compressor, cyclone's solid bin outlet and drying tower intercommunication, its gas bin outlet then links to each other with the low pressure buffer tank, separate the chlorosilane liquid drop in the tail gas through cyclone, and flow it back to in the drying tower, improve the utilization ratio of chlorosilane on the one hand, avoid extravagant, on the other hand can avoid a large amount of chlorosilanes to go on in the follow-up equipment and take place hydrolysis reaction with water, not only can bring in unnecessary impurity, also can cause the unusual rising of follow-up equipment temperature simultaneously; meanwhile, the pressure of the tail gas can be effectively reduced through the decompression buffering operation of the low-pressure buffer tank, on one hand, the degradation and separation effects on liquid drops in the tail gas are improved, on the other hand, continuous tail gas flow can be provided for the subsequent process, and continuous and stable production of equipment is guaranteed while the safety of the equipment is improved.
6. The utility model discloses set up the cooling chamber on the external surface of synthetic furnace, the upper and lower both ends of cooling chamber are provided with coolant outlet and coolant entry respectively, can carry out effective management and control to the temperature of synthetic furnace through the cooling chamber, guarantee that the temperature of synthetic furnace is in about 400 ℃ of best reaction temperature, have guaranteed the stable, continuous output of hydrogen chloride gas on the one hand; on the other hand, potential safety hazards caused by abnormal rise of the temperature of the synthesis furnace are avoided, and safe operation of the equipment is guaranteed.
7. The top of the synthesis furnace is provided with a hydrogen inlet, a chlorine inlet and a reaction gas inlet, the inside of the synthesis furnace is provided with a first annular guide plate and a second annular guide plate which respectively correspond to the hydrogen inlet and the reaction gas inlet, and a chlorine layer and a reaction tail gas layer are sequentially formed in the circumferential direction of hydrogen flow from inside to outside; meanwhile, a third annular guide plate and a second hydrogen inlet which are matched with each other are also arranged in the synthesis furnace, so that a circle of hydrogen layer is wrapped outside the reaction tail gas layer; in the special structural design, the center of the airflow is a circular hydrogen injection channel, the periphery of the hydrogen channel is an annular chlorine injection channel, hydrogen and chlorine meet through the two channels and then are ignited to form reaction flame, the periphery of the hydrogen channel is provided with an annular tail gas channel, tail gas in the channel is heated at the periphery of the flame, the position of the tail gas has the highest reaction temperature, stable output of hydrogen chloride gas is guaranteed, and meanwhile, the outermost periphery of the tail gas is coated with a layer of hydrogen, so that on one hand, the hydrogen in the synthesis furnace is always in an excessive state relative to the chlorine, the chlorine in the tail gas is guaranteed to be completely converted into the hydrogen chloride gas, on the other hand, the high temperature of hydrogen combustion is directly conducted to the reaction tail gas, and the.
8. The utility model discloses a one-level condenser and second grade condenser still have connected gradually between gas compressor and the high-pressure buffer tank, the bin outlet of one-level condenser and second grade condenser all is connected to the silane condensate tank, further retrieves the silane in the tail gas through the effect of condenser, can improve the purity of tail gas, also can avoid its normal operating that takes place hydrolysis reaction influence equipment in the back channel equipment simultaneously.
9. The utility model discloses nitrogen gas and oxygen discharge port at pressure swing adsorption tower group still are connected with the scrubbing tower, the scrubbing tower adopts clear water or alkali solution as the cleaner, absorbs or neutralizes remaining hydrogen chloride gas in with nitrogen gas and oxygen through the cleaner, can enough avoid the environmental pollution that hydrogen chloride gas arouses, also can retrieve certain accessory substance simultaneously.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic view of the structure of the synthesis furnace of the present invention;
fig. 3 is a schematic structural view of embodiment 2 of the present invention;
FIG. 4 is a schematic structural view of a synthesis furnace according to embodiment 2 of the present invention;
reference numerals: 1. a bag-type dust collector, 2, a booster fan, 3, a synthesis furnace, 4, a cooling device, 5, a drying tower, 6, a gas compressor, 7, a high-pressure buffer tank, 8, a pressure swing adsorption tower set, 9, a chlorine concentration detector, 10, a discharge outlet, 11, a rotary unloader, 12, a cyclone separator, 13, a low-pressure buffer tank, 14, a primary condenser, 15, a secondary condenser, 16, a condensing tank, 17, a washing tower, 31, a cooling cavity, 32, a cooling medium outlet, 33, a cooling medium inlet, 34, a hydrogen inlet, 35, a chlorine inlet, 36, a reaction gas inlet, 37, a first annular guide plate, 38, a second annular guide plate, 39, a third annular guide plate, 310, a second hydrogen inlet, 41, a preheating boiler, 42, a gas cooler, 51, a spray pipe, 52, a return pipe, 53, a circulating pump, 54, a cooler, 55 and a filter press pump, 56. a membrane filter.
Detailed Description
The present invention will be further described with reference to the following description and examples, which include but are not limited to the following embodiments.
Embodiment mode 1
This embodiment is regarded as the utility model discloses a fumed silica tail gas processing system, and the concrete structure is as shown in fig. 1 and fig. 2, along the flow direction of air current, has connected gradually booster fan 2, sack cleaner 1, synthetic furnace 3, cooling device 4, drying tower 5, gas compressor 6, high-pressure buffer tank 7 and pressure swing adsorption tower group 8, wherein the upper and lower both sides on the sack cleaner 1 are provided with gas vent and solid material discharge port respectively, and its lateral wall is provided with the air inlet, and the air inlet links to each other with booster fan 2, and the solid material discharge port then connects corresponding dust recovery plant through rotatory unloader 11;
the synthesis furnace 3 comprises a furnace body, wherein a hydrogen inlet 34, a chlorine inlet 35 and a reaction gas inlet 36 are arranged at the upper part of the furnace body, the hydrogen inlet 34 is arranged at the top of the furnace body, the axis of the hydrogen inlet is coincident with the axis of the furnace body, the chlorine inlet 35 and the reaction gas inlet 36 are both arranged on the side wall of the furnace body, a first annular guide plate 37 and a second annular guide plate 38 which respectively correspond to the chlorine inlet 35 and the reaction gas inlet 36 are arranged in the synthesis furnace 3, and therefore a chlorine layer and a reaction tail gas layer are sequentially formed in the circumferential direction of hydrogen flow from inside to outside; the hydrogen inlet 34 and the chlorine inlet 35 are respectively connected with corresponding gas sources, and the reaction gas inlet 36 is communicated with an exhaust port at the top of the bag-type dust collector 1;
the bottom of the synthesis furnace 3 is provided with a discharge hole, the discharge hole is connected with a cooling device 4, the cooling device 4 comprises a waste heat boiler 41 and a gas cooler 42, the waste heat boiler 41 is positioned at the front end of the gas cooler 42 along the airflow direction, meanwhile, a chlorine concentration detector 9 is also arranged between the waste heat boiler 41 and the gas cooler 42, and the chlorine concentration detector 9 can adopt an electronic type or an artificial reading type;
the upper end and the lower end of the drying tower 5 are respectively provided with an exhaust port and a discharge port, and the side wall of the drying tower is also provided with a feed inlet which is connected with the outlet end of the gas cooler 42; a plurality of clapboards are arranged inside the drying tower 5 in a staggered mode, a snake-shaped movement loop is formed inside the drying tower through the clapboards, and the retention time of airflow is prolonged; the upper end and the lower end of the drying tower 5 are respectively provided with a spray pipe 51 and a return pipe 52, and a plurality of spray heads are uniformly arranged on the spray pipe 51;
a circulating pump 53 and a cooler 54 are connected between the spray pipe 51 and the return pipe 52 along the flowing direction of the materials, a pressure filtration pump 55 and a membrane filter 56 are sequentially connected at the discharge port at the bottom of the drying tower 5, and the outlet end of the membrane filter 56 is connected with the inlet end of the cooler 54;
according to the requirement, the gas compressor 6 adopts a conventional process gas compressor such as an oil-free screw compressor, a diaphragm compressor and the like, the inlet end of the gas compressor is communicated with the exhaust port at the top of the drying tower 5, the outlet end of the gas compressor is communicated with a high-pressure buffer tank 7, and the outlet end of the high-pressure buffer tank 7 is connected with a pressure swing adsorption tower group 8;
according to the requirement, the pressure swing adsorption tower group 8 comprises 4-6 pressure swing adsorption towers which are connected in parallel, the top of each pressure swing adsorption tower is provided with a hydrogen chloride gas outlet, the hydrogen chloride gas outlet is connected with a corresponding storage tank through a pipeline, meanwhile, the nitrogen and oxygen outlets are connected with a washing tower 17, and clear water or alkali solution is adopted in the washing tower 17 as a cleaning agent.
Embodiment mode 2
As a preferred embodiment of the present invention, the present invention discloses a fumed silica tail gas treatment system, which has a specific structure as shown in fig. 3 and 4, and is sequentially connected with a booster fan 2, a bag-type dust collector 1, a synthesis furnace 3, a cooling device 4, a drying tower 5, a cyclone separator 6, a low-pressure buffer tank 13, a gas compressor 6, a primary condenser 14, a secondary condenser 15, a high-pressure buffer tank 7, a pressure swing adsorption tower group 8 and a washing tower 17 along the flow direction of air flow;
the upper part of the synthesis furnace 3 is provided with a hydrogen inlet 34, a chlorine inlet 35 and a reaction gas inlet 36, wherein the hydrogen inlet 34 is arranged at the top of the synthesis furnace 3, the axis of the hydrogen inlet is coincident with the axis of the furnace body, the chlorine inlet 35 and the reaction gas inlet 36 are both arranged on the side wall of the synthesis furnace, a first annular guide plate 37 and a second annular guide plate 38 which are respectively corresponding to the chlorine inlet 35 and the reaction gas inlet 36 are arranged in the synthesis furnace 3, meanwhile, a third annular guide plate 39 is also arranged in the synthesis furnace 3, and the third annular guide plate 39 is positioned on the periphery of the second annular guide plate 38 and is arranged concentrically with the second annular guide plate; the synthesis furnace 3 is also provided with a second hydrogen inlet 310 opposite to the third annular guide plate 39, and the second hydrogen inlet 310 and the hydrogen inlet 34 are connected to the same hydrogen source, so that a circle of hydrogen layer is wrapped outside the reaction tail gas layer;
meanwhile, the wall of the synthesis furnace 3 is also provided with a cooling cavity 31, the upper end and the lower end of the cooling cavity 31 are respectively provided with a cooling medium outlet 32 and a cooling medium inlet 33, and the cooling medium outlet 32 and the cooling medium inlet 33 are respectively connected with corresponding cooling medium sources;
an exhaust port is arranged at the top of the drying tower 5 and is connected with a gas inlet of a cyclone separator 12, a gas outlet end at the top of the cyclone separator 12 is communicated with an inlet end of a low-pressure buffer tank 13, and a discharge port at the bottom of the cyclone separator 12 reflows to the top of the drying tower 5 through a pipeline; the outlet end of the low-pressure buffer tank 15 is connected with the inlet end of the gas compressor 6;
along the flow direction of material, the exit end of gas compressor 6 then has connected gradually one-level condenser 14 and second grade condenser 15, the bin outlet of one-level condenser 14 and second grade condenser 15 bottom is connected simultaneously in silane condensate tank 16, and the air inlet of second grade condenser 15 links to each other with the gas vent of one-level condenser 14, and the gas vent of second grade condenser 15 is then lug connection to high pressure buffer tank 7.
The utility model discloses directly let in the synthetic furnace behind the tail gas through the sack cleaner during use, let in chlorine and excessive hydrogen (for chlorine) in the synthetic furnace, and light the reaction gas of mixing to poisonous chlorine in with the tail gas through excessive hydrogen is whole to be turned into hydrogen chloride gas, and finally obtains highly compressed pure hydrogen chloride gas through steps such as dehydration, adsorption separation, compares with prior art, the utility model discloses obtain hydrogen chloride gas, product quality does not change because of the change of gaseous phase white carbon black prescription, and the stability of product is higher; meanwhile, as a primary chemical raw material, the hydrogen chloride gas has higher flexibility in use, which is beneficial for enterprises to avoid the vicious competition caused by the excessive hydrochloric acid in the current market and improve the economic value of byproducts;
simultaneously the utility model discloses an end product is hydrogen chloride gas, consequently does not need a large amount of hydrochloric acid to absorb and alkali wash equipment, therefore can not produce a large amount of industrial waste water that can't handle, and the gas that finally discharges is nitrogen gas and oxygen, and the environmental protection of enterprise discharges nearly zero, has effectively reduced the environmental protection expenditure of enterprise, improves the economic benefits of enterprise.
Claims (10)
1. The utility model provides a white carbon black tail gas processing system of gaseous phase, includes sack cleaner (1), its characterized in that: the inlet end of the bag-type dust collector (1) is connected with a tail gas booster fan (2), and the outlet end of the bag-type dust collector is connected with a synthesis furnace (3) for burning and synthesizing hydrogen chloride gas; the outlet end of the synthesis furnace (3) is sequentially provided with a cooling device (4), a drying tower (5), a gas compressor (6) and a high-pressure buffer tank (7), and the outlet end of the high-pressure buffer tank (7) is provided with a pressure swing adsorption tower group (8) for separating out hydrogen chloride gas; and a chlorine concentration detector (9) is arranged at the outlet end of the cooling device (4).
2. The fumed silica tail gas treatment system according to claim 1, characterized in that: the bag-type dust collector is characterized in that a discharge opening (10) is formed in the bottom of the bag-type dust collector (1), and the discharge opening (10) is connected with a rotary unloading machine (11).
3. The fumed silica tail gas treatment system according to claim 1, characterized in that: the cooling device (4) comprises a waste heat boiler (41) and a gas cooler (42) which are connected in sequence, and the chlorine concentration detector (9) is positioned between the waste heat boiler (41) and the gas cooler (42).
4. The fumed silica tail gas treatment system according to claim 1, characterized in that: the upper end and the lower end of the drying tower (5) are respectively provided with a spray pipe (51) and a return pipe (52), and a circulating pump (53) and a cooler (54) are sequentially connected between the return pipe (52) and the spray pipe (51) according to the flowing direction; the bottom of the drying tower (5) is also provided with a discharge outlet (10), the discharge outlet (10) is sequentially connected with a pressure filtration pump (55) and a membrane filter (56) according to the flowing direction, and the outlet end of the membrane filter (56) is connected with a cooler (54).
5. The fumed silica tail gas treatment system according to claim 1, characterized in that: still set gradually cyclone (12) and low pressure buffer tank (13) between drying tower (5) and gas compressor (6), the solid bin outlet of cyclone (12) communicates with drying tower (5), and its gas bin outlet then links to each other with low pressure buffer tank (13).
6. The fumed silica tail gas treatment system according to claim 1, characterized in that: the outer surface of the synthesis furnace (3) is provided with a cooling cavity (31), and the upper end and the lower end of the cooling cavity (31) are respectively provided with a cooling medium outlet (32) and a cooling medium inlet (33).
7. The fumed silica tail gas treatment system according to claim 1, characterized in that: the upper part of the synthesis furnace (3) is provided with a hydrogen inlet (34), a chlorine inlet (35) and a reaction gas inlet (36), and a first annular guide plate (37) and a second annular guide plate (38) which respectively correspond to the chlorine inlet (35) and the reaction gas inlet (36) are arranged inside the synthesis furnace (3), so that a chlorine layer and a reaction tail gas layer are sequentially formed in the circumferential direction of the hydrogen flow from inside to outside.
8. The fumed silica tail gas treatment system according to any one of claims 1 or 7, characterized in that: and a third annular guide plate (39) and a second hydrogen inlet (310) which are matched with each other are also arranged in the synthesis furnace (3), so that a circle of hydrogen layer is wrapped outside the reaction tail gas layer.
9. The fumed silica tail gas treatment system according to claim 1, characterized in that: still be connected with one-level condenser (14) and second grade condenser (15) in proper order between gas compressor (6) and high-pressure buffer tank (7), bin outlet (10) of one-level condenser (14) and second grade condenser (15) all are connected to silane condensate tank (16).
10. The fumed silica tail gas treatment system according to claim 1, characterized in that: the nitrogen and oxygen discharge ports of the pressure swing adsorption tower set (8) are also connected with a washing tower (17), and the washing tower (17) adopts clear water or alkali solution as a cleaning agent.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111498808A (en) * | 2020-04-29 | 2020-08-07 | 宁夏福泰硅业有限公司新材料分公司 | Gas-phase white carbon black tail gas treatment system and treatment method thereof |
| CN113797661A (en) * | 2021-10-22 | 2021-12-17 | 南通友拓新能源科技有限公司 | Tail gas treatment system and method in electronic grade polycrystalline silicon production |
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2020
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111498808A (en) * | 2020-04-29 | 2020-08-07 | 宁夏福泰硅业有限公司新材料分公司 | Gas-phase white carbon black tail gas treatment system and treatment method thereof |
| CN111498808B (en) * | 2020-04-29 | 2023-04-07 | 宁夏福泰硅业有限公司新材料分公司 | Gas-phase white carbon black tail gas treatment system and treatment method thereof |
| CN113797661A (en) * | 2021-10-22 | 2021-12-17 | 南通友拓新能源科技有限公司 | Tail gas treatment system and method in electronic grade polycrystalline silicon production |
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