CN216909824U - Absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production - Google Patents
Absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production Download PDFInfo
- Publication number
- CN216909824U CN216909824U CN202220479979.5U CN202220479979U CN216909824U CN 216909824 U CN216909824 U CN 216909824U CN 202220479979 U CN202220479979 U CN 202220479979U CN 216909824 U CN216909824 U CN 216909824U
- Authority
- CN
- China
- Prior art keywords
- hydrolysis
- tank
- tail gas
- leaching tower
- liquid
- 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.)
- Active
Links
Images
Classifications
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The application provides an absorption system for hydrolysis tail gas of high-boiling-point substances in trichlorosilane production, which comprises a high-boiling-point substance storage tank, a hydrolysis tank, a negative pressure fan, a first-stage leaching tower and a second-stage leaching tower; the hydrolysis tank is provided with a hydrolysis tank high-boiling residue inlet and a hydrolysis tank tail gas outlet, the first-stage leaching tower is provided with a first hydrolysis tail gas inlet and a first hydrolysis tail gas outlet, and the second-stage leaching tower is provided with a second hydrolysis tail gas inlet and a second hydrolysis tail gas outlet; the high boiling thing storage tank and the pond of hydrolysising high boiling thing import fixed connection of hydrolysising, the pond of hydrolysising tail gas export and the first tail gas import of hydrolysising pass through negative-pressure air fan fixed connection, and the first tail gas export of hydrolysising is hydrolysised with the second and is imported fixed connection. The method realizes the absorption of the high-boiling-point substance hydrolysis tail gas in the trichlorosilane production, improves the absorption rate of the hydrolysis tail gas, prolongs the service life of the system, and avoids the environmental pollution caused by the hydrolysis tail gas.
Description
Technical Field
The application relates to the technical field of tail gas absorption, in particular to an absorption system for hydrolysis tail gas of high-boiling-point substances in trichlorosilane production.
Background
In the synthesis process of trichlorosilane, a small amount of silicon dioxide filter residues are generated, and a small amount of high-boiling-point substances are also remained in the rectification separation process of trichlorosilane, and the silicon dioxide filter residues and the high-boiling-point substances still contain a small amount of silicon tetrachloride and trichlorosilane.
In the prior art, filter residue or high-boiling-point substances are usually added into water, so that silicon tetrachloride and trichlorosilane contained in the filter residue or the high-boiling-point substances react with the water to generate silicon dioxide and hydrogen chloride. The generated hydrogen chloride is a strong acid, has extremely strong volatility and corrosivity, and can be combined with water vapor in the air to generate small hydrochloric acid droplets after volatilization to form acid mist. Meanwhile, hydrogen chloride is toxic and can pollute the environment when being discharged into the air. In the prior art, water is often adopted to directly absorb hydrogen chloride gas based on the principle that HCl gas is easily soluble in water, but only water is used to absorb hydrogen chloride tail gas, so that the absorption efficiency of hydrogen chloride is low.
SUMMERY OF THE UTILITY MODEL
The application provides an absorption system for high-boiling-point substance hydrolysis tail gas in trichlorosilane production, which is used for solving the problem of low hydrogen chloride absorption efficiency in the absorption process of the high-boiling-point substance hydrolysis tail gas in trichlorosilane production.
The application provides an absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production, which comprises a high-boiling-point substance storage tank, a hydrolysis tank, a negative pressure fan, a first-stage leaching tower and a second-stage leaching tower.
The hydrolysis tank is provided with a hydrolysis tank high-boiling residue inlet and a hydrolysis tank tail gas outlet, the first-stage leaching tower is provided with a first hydrolysis tail gas inlet and a first hydrolysis tail gas outlet, and the second-stage leaching tower is provided with a second hydrolysis tail gas inlet and a second hydrolysis tail gas outlet.
The high boiling thing storage tank and the pond of hydrolysising high boiling thing import fixed connection of hydrolysising, the pond of hydrolysising tail gas export and the first tail gas import of hydrolysising pass through negative-pressure air fan fixed connection, and the first tail gas export of hydrolysising is hydrolysised with the second and is imported fixed connection.
The hydrolysis tank is used for hydrolyzing high-boiling residues from the high-boiling residue storage tank and spraying hydrolysis tail gas generated by hydrolysis.
The negative pressure fan is used for conveying the hydrolysis tail gas sprayed in the hydrolysis tank into the first-stage leaching tower.
The first-stage leaching tower and the second-stage leaching tower are used for absorbing hydrogen chloride gas in the hydrolysis tail gas.
Optionally, the system is further provided with a hydrolysis tank circulating spray assembly, the hydrolysis tank circulating spray assembly comprises a liquid collecting tank, a circulating spray pump and a first spray head, the liquid collecting tank is fixedly connected with the hydrolysis tank, the circulating spray pump is connected between the liquid collecting tank and the spray head, and the first spray head is fixedly arranged on the upper portion of the hydrolysis tank.
Optionally, a filter is arranged at the liquid inlet of the liquid collecting pool.
Optionally, the first leaching tower is provided with a first leaching device, the first leaching device includes a second spray header arranged at the top of the first leaching tower and a first leaching pump arranged at the bottom of the first leaching tower, and the second spray header and the first leaching pump are fixedly connected through a water pipe.
Optionally, the second leaching tower is provided with a second leaching device, the second leaching device includes a third spray header arranged at the top of the second leaching tower and a second leaching pump arranged at the bottom of the second leaching tower, and the third spray header and the second leaching pump are fixedly connected through a water pipe.
Optionally, a demister is arranged at the top of the second-stage leaching tower and arranged at the upper part of the third spray header.
Optionally, the absorption system further comprises an alkali liquor tank, and the alkali liquor tank is used for supplementing alkali liquor into the absorption system;
a first liquid conveying pipeline is arranged between the alkali liquor tank and the second leaching tower, a second liquid conveying pipeline is arranged between the second leaching tower and the first leaching tower, and a third liquid conveying pipeline is arranged between the first leaching tower and the hydrolysis tank;
the first liquid conveying pipeline is used for conveying alkali liquor from the alkali liquor tank into the second-stage leaching tower, the second liquid conveying pipeline is used for conveying leacheate in the second-stage leaching tower into the first-stage leaching tower from the second-stage leaching tower, and the third liquid conveying pipeline is used for conveying the leacheate in the first-stage leaching tower into the hydrolysis tank from the first-stage leaching tower.
Optionally, the absorption system further comprises a fourth liquid transfer line, the fourth liquid transfer line communicating the first liquid transfer line and the third liquid transfer line;
and the third liquid conveying pipeline, the fourth liquid conveying pipeline and the first liquid conveying pipeline are communicated and then used for conveying the alkali liquor in the alkali liquor tank into the hydrolysis tank, the first-stage leaching tower and the second-stage leaching tower respectively.
Optionally, the absorption system is further provided with a filter press, a feed inlet of the filter press is fixedly connected with a liquid phase outlet of the hydrolysis tank, and a liquid phase outlet of the filter press is fixedly connected with the hydrolysis tank.
Optionally, the absorption system is further provided with a neutralization stirring tank and a clear liquid tank, a feed inlet of the neutralization stirring tank is fixedly connected with a liquid phase outlet of the filter press, a feed inlet of the clear liquid tank is fixedly connected with a discharge outlet of the neutralization stirring tank, and a discharge outlet of the clear liquid tank is fixedly connected with the hydrolysis tank, the first-stage leaching tower and the second-stage leaching tower respectively.
The application provides an absorption system of high-boiling-point substance tail gas of hydrolysising in trichlorosilane production, has realized the absorption to high-boiling-point substance tail gas of hydrolysising in trichlorosilane production, compares with prior art, has following beneficial effect:
(1) through setting up negative pressure fan, will hydrolyze the hydrogen chloride gas that produces and defeated to one-level drip washing tower through the negative pressure for hydrogen chloride gas can fully contact with the leacheate, improves hydrogen chloride gas's absorptivity.
(2) The method comprises the steps of circularly spraying the hydrogen chloride gas generated by hydrolysis through a hydrolysis tank, and carrying out multi-stage leaching through a first-stage leaching tower and a second-stage leaching tower, further improving the absorption rate and absorption efficiency of the hydrogen chloride gas, circularly utilizing the leachates in the first-stage leaching tower and the second-stage leaching tower, increasing the utilization rate of the leachates, absorbing the hydrogen chloride gas by adopting alkali liquor, generating a product which is a chlorine salt solution, carrying out crystallization treatment on the chlorine salt solution, obtaining chlorine salt crystals, conveniently recycling and reusing the chlorine salt crystals, and having good environmental protection value and economic value.
(3) The filter that sets up through the collecting tank inlet prevents that solids such as silica in the pond of hydrolysising from causing the jam to the circulation spray pump, has reduced the periodic maintenance frequency of circulation spray pump, has also reduced equipment maintenance cost.
(4) The solution in the hydrolysis tank is subjected to filter pressing through a filter press, the obtained liquid phase is used for absorbing the hydrogen chloride gas again, resources are recycled, and the production cost of enterprises is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic structural diagram of an absorption system for hydrolysis tail gas of high-boiling residues in trichlorosilane production according to an embodiment of the present application;
fig. 2 is a schematic structural diagram of an absorption system for hydrolysis tail gas of high-boiling-point substances in trichlorosilane production according to another embodiment of the present application;
FIG. 3 is a schematic structural view of a filter in a sump according to an embodiment of the present disclosure;
fig. 4 is a schematic view of a liquid delivery pipeline structure of an absorption system for hydrolysis tail gas of high-boiling residues in trichlorosilane production according to an embodiment of the present application;
FIG. 5 is a schematic view of a liquid delivery pipeline structure of an absorption system for hydrolysis tail gas of high-boiling components in trichlorosilane production according to another embodiment of the present application;
FIG. 6 is a schematic structural diagram of an absorption system containing a filter press for hydrolysis tail gas of high-boiling components in trichlorosilane production according to an embodiment of the present application;
fig. 7 is a schematic structural diagram of a filter press-containing system of an absorption system for hydrolysis tail gas of high-boiling components in trichlorosilane production according to another embodiment of the present application.
Description of reference numerals:
1: a high-boiling-point substance storage tank;
2: a hydrolysis tank;
21: a high-boiling-point substance inlet of the hydrolysis tank;
22: a tail gas outlet of the hydrolysis tank;
23: a liquid collecting tank;
231: a filter;
24: a circulating spray pump;
25: a first shower head;
3: a negative pressure fan;
4: a first leaching tower;
41: a first hydrolysis tail gas inlet;
42: a first hydrolysis tail gas outlet;
431: a second shower head;
432: a first leaching pump;
5: a second stage leaching tower;
51: a second hydrolysis tail gas inlet;
52: a second hydrolysis tail gas outlet;
531: a third shower head;
532: a second leaching pump;
54: a demister;
61: a first liquid transfer line;
62: a second liquid transfer line;
63: a third liquid transfer line;
64: a fourth liquid transfer line;
7: a filter press;
8: a neutralization stirring tank;
9: and a clear liquid pool.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the technical solutions in the embodiments of the present application are clearly and completely described below, and it is obvious that the described embodiments are a part of the embodiments of the present application, but not all of the embodiments. All other embodiments obtained by a person of ordinary skill in the art based on the embodiments in the present application without making any creative effort also belong to the protection scope of the present application.
Fig. 1 is a schematic structural diagram of an absorption system for hydrolysis tail gas of high-boiling-point substances in trichlorosilane production according to an embodiment of the present application, and as shown in fig. 1, the present application provides an absorption system for hydrolysis tail gas of high-boiling-point substances in trichlorosilane production, which includes a high-boiling-point substance storage tank 1, a hydrolysis tank 2, a negative pressure fan 3, a first-stage elution tower 4, and a second-stage elution tower 5;
the hydrolysis tank 2 is provided with a hydrolysis tank high-boiling residue inlet 21 and a hydrolysis tank tail gas outlet 22, the first-stage leaching tower 4 is provided with a first hydrolysis tail gas inlet 41 and a first hydrolysis tail gas outlet 42, and the second-stage leaching tower 5 is provided with a second hydrolysis tail gas inlet 51 and a second hydrolysis tail gas outlet 52;
the high-boiling-point substance storage tank 1 is fixedly connected with a high-boiling-point substance inlet 21 of the hydrolysis tank, a tail gas outlet 22 of the hydrolysis tank is fixedly connected with a first hydrolysis tail gas inlet 41 through a negative pressure fan 3, and a first hydrolysis tail gas outlet 42 is fixedly connected with a second hydrolysis tail gas inlet 51;
the hydrolysis tank 2 is used for hydrolyzing the high-boiling residues from the high-boiling residue storage tank 1 and spraying hydrolysis tail gas generated by hydrolysis; the negative pressure fan 3 is used for conveying the hydrolysis tail gas sprayed in the hydrolysis tank 2 into the first-stage leaching tower 4;
the first leaching tower 4 and the second leaching tower 5 are used for absorbing hydrogen chloride gas in the hydrolysis tail gas.
Specifically, high-boiling-point substances generated in the trichlorosilane synthesis process are conveyed into the hydrolysis tank 2 from the high-boiling-point substance storage tank 1 through a hydrolysis tank high-boiling-point substance inlet 21 at the bottom of the hydrolysis tank 2, the high-boiling-point substances comprise silicon tetrachloride and trichlorosilane, wherein the silicon tetrachloride proportion is high, the silicon tetrachloride and the trichlorosilane are subjected to hydrolysis reaction with water in the hydrolysis tank 2 to generate silicon dioxide solid matters and hydrolysis tail gas, the hydrolysis tail gas is hydrogen chloride gas, and the silicon dioxide solid matters fall into liquid in the hydrolysis tank 2. The negative pressure fan 3 provides power for the hydrolysis tail gas in the hydrolysis tank 2, and the hydrolysis tail gas is conveyed into the first-stage leaching tower 4 from the first hydrolysis tail gas inlet 41 at the lower part of the first-stage leaching tower 4 for spray absorption, so that the hydrogen chloride gas can be fully contacted with the leacheate in the first-stage leaching tower 4, and the absorption rate of the hydrogen chloride gas is improved. After the hydrogen chloride in the hydrolysis tail gas is in countercurrent contact reaction with the leacheate sprayed in the first-stage leaching tower 4, the hydrogen chloride rises to the top of the first-stage leaching tower 4, enters the lower part of the second-stage leaching tower 5 from a second hydrolysis tail gas inlet 51 at the lower part of the second-stage leaching tower 5 through a first hydrolysis tail gas outlet 42, and is in countercurrent contact with the leacheate sprayed downwards in the second-stage leaching tower 5, further reacts and absorbs the leacheate and is discharged.
The negative pressure fan 3 adopts a glass fiber reinforced plastic draught fan, the corrosion resistance is good, the corrosion of hydrogen chloride gas can be avoided, the operation period of the system is prolonged, meanwhile, the negative pressure fan 3 can provide power and speed for the hydrolyzed tail gas, so that the hydrogen chloride gas in the hydrolyzed tail gas can be fully contacted with the leacheate in the first-level leaching tower 4, and the absorption rate of the hydrogen chloride gas is improved. The leacheate used by the first-stage leaching tower 4 and the second-stage leaching tower 5 is calcium hydroxide alkali liquor or sodium hydroxide alkali liquor, a product generated after spraying and absorption is chlorine salt solution, the chlorine salt solution is crystallized to obtain chlorine salt crystals, the chlorine salt crystals are recycled, and the method has good environmental protection value and economic value. The hydrogen chloride gas generated by hydrolysis is subjected to multi-stage leaching absorption through the first-stage leaching tower and the second-stage leaching tower, so that the absorption rate of the hydrogen chloride gas is further improved, the emission of the hydrogen chloride gas in the atmosphere is greatly reduced, the hydrolysis tail gas is recycled, the chlorine salt is produced, new economic benefits are created, and the pollution of the hydrolysis tail gas to the environment can be reduced.
By adopting the scheme, the absorption of the tail gas of hydrolysis of high-boiling-point substances in the production of trichlorosilane is realized, the high-boiling-point substances are hydrolyzed to generate hydrogen chloride gas, and the hydrogen chloride gas is conveyed to the first-stage leaching tower through the negative pressure fan, so that the hydrogen chloride gas can be fully contacted with the leaching solution in the first-stage leaching tower, and the absorption rate of the hydrogen chloride gas is improved; the hydrolyzed tail gas which is sprayed and absorbed by the first-stage leaching tower is conveyed to the second-stage leaching tower for secondary spraying and absorption, and the absorption rate of the hydrogen chloride gas is further improved through the spraying and absorption of the multi-stage leaching tower, so that the method has good environmental protection value.
Fig. 2 is a schematic structural diagram of an absorption system of high-boiling-point substance tail gas of hydrolysising provided in another embodiment of the present application, as shown in fig. 2, optionally, the absorption system is further provided with a hydrolysis tank circulating spray assembly, the hydrolysis tank circulating spray assembly includes a liquid collecting tank 23, a circulating spray pump 24 and a first spray header 25, the liquid collecting tank 23 is fixedly connected with the hydrolysis tank 2, the circulating spray pump 24 is connected between the liquid collecting tank 23 and the spray header 25, and the first spray header 25 is fixedly arranged on the upper portion of the hydrolysis tank 2.
Specifically, the high-level aqueous solution in the hydrolysis tank 2 is conveyed to a liquid collecting tank 23, the aqueous solution is pumped to a first spray head 25 through a circulating spray pump 24, the hydrolysis tail gas is in the hydrolysis tank 2 and is in countercurrent contact with the aqueous solution sprayed downwards by the first spray head 25 to be absorbed and reacted to generate a hydrochloric acid solution, and the hydrochloric acid solution falls into the aqueous solution at the lower part of the hydrolysis tank 2, so that the circulating spray absorption is performed, the hydrogen chloride gas generated by hydrolysis is dissolved in water, the primary spray absorption of the hydrolysis tail gas is completed, the emission of hydrogen chloride is reduced, and the load of a subsequent spray device is reduced.
Fig. 3 is a schematic structural diagram of a filter in the liquid collecting tank according to an embodiment of the present application, and as shown in fig. 3, optionally, a filter 231 is disposed at a liquid inlet of the liquid collecting tank 23.
Specifically, silicon tetrachloride and trichlorosilane contained in the high-boiling-point substances are subjected to hydrolysis reaction with water in the hydrolysis tank 2 to generate solid silicon dioxide and hydrolysis tail gas, the solid silicon dioxide is sunk into the aqueous solution in the hydrolysis tank 2, a filter 231 is arranged at a liquid inlet of the liquid collecting tank 23, the blockage of the solid silicon dioxide and other solids in the hydrolysis tank 2 on the circulating spray pump 24 can be prevented, the periodic maintenance frequency of the circulating spray pump is reduced, the maintenance cost of the system is reduced, the system operation period is prolonged, and the production efficiency is improved.
Optionally, the first leaching tower 4 is provided with a first leaching device, as shown in fig. 2, the first leaching device includes a second spray header 431 disposed at the top of the first leaching tower 4 and a first leaching pump 432 disposed at the bottom of the first leaching tower 4, and the second spray header 431 and the first leaching pump 432 are fixedly connected through a water pipe.
Specifically, the first leaching pump 432 pumps the leaching solution at the bottom of the first-stage leaching tower 4 to the second spray headers 431 through the conveying pipeline, the second spray headers 431 are distributed in the first-stage leaching tower 4 along the height direction of the first-stage leaching tower 4, and a plurality of the second spray headers 431 are arranged, so that the hydrolysis tail gas entering from the lower part of the first-stage leaching tower 4 and moving upwards is fully contacted with the leaching solution sprayed downwards, the contact time and the reaction time of hydrogen chloride in the hydrolysis tail gas and the leaching solution are increased, and the absorption efficiency of hydrogen chloride gas is improved.
Optionally, the second leaching tower 5 is provided with a second leaching device, as shown in fig. 2, the second leaching device includes a third spray header 531 arranged at the top of the second leaching tower 5 and a second leaching pump 532 arranged at the bottom of the second leaching tower 5, and the third spray header 531 and the second leaching pump 532 are fixedly connected through a water pipe.
Specifically, the second leaching device comprises a third spray header 531 arranged at the top of the second-stage leaching tower 5 and a second leaching pump 532 arranged at the bottom of the second-stage leaching tower 5, the second leaching pump 532 pumps the leaching solution at the bottom of the second-stage leaching tower 5 to the third spray header 531 through a conveying pipeline, the third spray headers 531 are distributed in the second-stage leaching tower 5 along the height direction of the second-stage leaching tower 5, and a plurality of the third spray headers 531 are arranged, the hydrolysis tail gas sprayed and absorbed by the first-stage leaching tower 4 enters the lower part of the second-stage leaching tower 5 from a second hydrolysis tail gas inlet 51 at the lower part of the second-stage leaching tower 5 and reacts with the leaching solution sprayed downwards by the third spray header 531 to be sprayed and absorbed again, and the absorption efficiency and the absorption rate of the hydrogen chloride gas are further improved.
Optionally, as shown in fig. 2, a demister 54 is disposed at the top of the second-stage leaching tower 5, and the demister 54 is disposed above the third spray header 531.
Specifically, the hydrolysis tail gas is sprayed and absorbed for multiple times and then discharged to the atmosphere from the top of the secondary leaching tower 5, the hydrolysis tail gas after being sprayed and absorbed for multiple times contains a small amount of water and hydrochloric acid fog drops, the demister 54 is arranged to collect and reflux the small amount of water and hydrochloric acid fog drops to the bottom of the secondary leaching tower 5, the pollution of hydrochloric acid to the environment is reduced, meanwhile, the corrosion of the hydrochloric acid fog drops to a discharge chimney is reduced, and the method has good economic benefits and environmental protection benefits.
Fig. 4 is a schematic view of a liquid delivery line structure of an absorption system for high-boiling-point substance hydrolysis tail gas in trichlorosilane production according to an embodiment of the present application, as shown in fig. 4, optionally, the absorption system further includes an alkali liquor tank, and the alkali liquor tank is used for supplementing alkali liquor into the absorption system;
a first liquid conveying pipeline 61 is arranged between the alkali liquor tank and the second-stage leaching tower 5, a second liquid conveying pipeline 62 is arranged between the second-stage leaching tower 5 and the first-stage leaching tower 4, and a third liquid conveying pipeline 63 is arranged between the first-stage leaching tower 4 and the hydrolysis tank 2.
The first liquid conveying pipeline 61 is used for conveying alkali liquor from the alkali liquor tank to the second-stage leaching tower 5, the second liquid conveying pipeline 62 is used for conveying leacheate in the second-stage leaching tower 5 from the second-stage leaching tower 5 to the first-stage leaching tower 4, and the third liquid conveying pipeline 63 is used for conveying the leacheate in the first-stage leaching tower 4 from the first-stage leaching tower 4 to the hydrolysis tank 2.
Specifically, the alkali liquor tank is used for supplementing alkali liquor into the absorption system, along with the operation of the system, the hydrogen chloride in the hydrolysis tail gas is continuously absorbed by the aqueous solution in the hydrolysis tank 2 and the leacheate in the first-stage leaching tower 4 and the second-stage leaching tower 5, the pH of the leacheate in the first-stage leaching tower 4 is detected by using pH test paper, when the pH value of the leacheate in the first-stage leaching tower 4 reaches 3-5, the leacheate in the first-stage leaching tower 4 is conveyed into the hydrolysis tank 2 through a third liquid conveying pipeline 63, the leacheate in the second-stage leaching tower 5 is conveyed into the first-stage leaching tower 4 through a second liquid conveying pipeline 62, and then new alkali liquor in the alkali liquor tank is conveyed into the second-stage leaching tower 5 through a first liquid conveying pipeline 61. By the arrangement, the utilization rate of the leacheate is increased, alkali liquor resources are saved, and the production cost of enterprises is reduced.
Fig. 5 is a schematic view of a liquid conveying line structure of an absorption system for hydrolysis tail gas of high boiling point substances in trichlorosilane production according to another embodiment of the present application, as shown in fig. 5, optionally, the absorption system further includes a fourth liquid conveying line 64, and the fourth liquid conveying line 64 connects the first liquid conveying line 61 and the third liquid conveying line 63;
and after the third liquid conveying pipeline 63, the fourth liquid conveying pipeline 64 and the first liquid conveying pipeline 61 are communicated, the alkali liquor in the alkali liquor tank is respectively conveyed to the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5.
Specifically, the absorption system further comprises a fourth liquid conveying pipeline 64, when the leaching solution needs to be supplemented into the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5 at the same time, the fourth liquid conveying pipeline 64 communicates the first liquid conveying pipeline 61 with the third liquid conveying pipeline 63, and the alkali liquor is respectively conveyed into the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5 to spray and absorb the hydrogen chloride in the hydrolysis tail gas.
Fig. 6 is a schematic structural diagram of an absorption system containing a filter press for high-boiling-point substance hydrolysis tail gas in trichlorosilane production according to an embodiment of the present application, and as shown in fig. 6, optionally, the absorption system is further provided with a filter press 7, a feed inlet of the filter press 7 is fixedly connected with a liquid phase outlet of the hydrolysis tank 2, and a liquid phase outlet of the filter press 7 is fixedly connected with the hydrolysis tank 2.
Specifically, the solution at the bottom of the hydrolysis tank 2 contains solids such as silica, and after the system stops operating, the liquid in the hydrolysis tank 2 is conveyed to a filter press for solid-liquid separation. The separated solid-phase silicon dioxide and calcium hydroxide are neutralized for producing building materials, and the material utilization rate is improved. The liquid phase filtered by pressure is hydrochloric acid solution, and the hydrochloric acid solution directly returns to the hydrolysis tank 2 through the liquid phase outlet of the pressure filter 7 for recycling, so that the production resources are saved.
Fig. 7 is a schematic structural diagram of an absorption system containing a filter press for high-boiling residue hydrolysis tail gas in trichlorosilane production according to another embodiment of the present application, and as shown in fig. 7, optionally, the absorption system is further provided with a neutralization stirring tank 8 and a clear liquid tank 9, a feed inlet of the neutralization stirring tank 8 is fixedly connected with a liquid phase outlet of the filter press 7, a feed inlet of the clear liquid tank 9 is fixedly connected with a discharge outlet of the neutralization stirring tank 8, and a discharge outlet of the clear liquid tank 9 is fixedly connected with the hydrolysis tank 2, the primary elution tower 4 and the secondary elution tower 5, respectively.
Specifically, after the system stops running, the liquid in the hydrolysis tank 2 is conveyed to a filter press 7 for solid-liquid separation, and the separated solid-phase silicon dioxide and calcium hydroxide are neutralized for producing building materials, so that the material utilization rate is improved. The liquid phase filtered by pressure is hydrochloric acid solution, and if the concentration of the hydrochloric acid is less than 10%, the hydrochloric acid solution directly returns to the hydrolysis tank 2 through a liquid phase outlet of a filter press 7 for recycling; if the concentration of the hydrochloric acid is more than 10 percent, the hydrochloric acid solution is conveyed to a neutralization stirring tank 8, and CaO or Ca (OH) is added2Neutralizing until the pH value is 6-6.5, temporarily storing the neutralized and filtered clear liquid in a clear liquid tank 9, and fixedly connecting a discharge port of the clear liquid tank 9 with the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5 respectively to be used as supplementary liquid of the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5.
The technical solution of the present application is illustrated in detail by the following specific examples.
In the embodiment, the operation flow of the absorption system for the hydrolysis tail gas of high-boiling residues in the production of trichlorosilane is as follows:
(1) hydrolysis in a hydrolysis tank and primary spraying: high-boiling-point substances generated in the trichlorosilane synthesis process are conveyed into the hydrolysis tank 2 from the high-boiling-point substance storage tank 1 through the hydrolysis tank high-boiling-point substance inlet 21 at the bottom of the hydrolysis tank 2, silicon tetrachloride and trichlorosilane contained in the high-boiling-point substances are subjected to hydrolysis reaction with water in the hydrolysis tank 2 to generate solid silicon dioxide and hydrolysis tail gas, the hydrolysis tail gas is hydrogen chloride gas, and the solid silicon dioxide is sunk into liquid in the hydrolysis tank 2. After being filtered by a filter 231 arranged at a liquid inlet of the liquid collecting tank 23, the aqueous solution in the hydrolysis tank 2 is conveyed into the liquid collecting tank 23, the aqueous solution in the liquid collecting tank 23 is pumped to the first spray head 25 through the circulating spray pump 24, the hydrogen chloride gas generated by hydrolysis is in countercurrent contact with the aqueous solution circularly sprayed by the first spray head 25 in the hydrolysis tank, the hydrochloric acid solution is generated by absorption reaction, and the aqueous solution sprayed by the first spray head 25 falls into the aqueous solution at the lower part of the hydrolysis tank 2 to finish primary spraying of the hydrolysis tail gas.
(2) Spraying by a first-stage leaching tower: the hydrolysis tail gas after primary spraying is conveyed from the hydrolysis tank tail gas outlet 22 to the first-stage leaching tower 4 through the first hydrolysis tail gas inlet 41 at the lower part of the first-stage leaching tower 4 through the negative pressure fan 3 for spraying absorption, and the negative pressure fan 3 adopts a glass fiber reinforced plastic induced draft fan. And after the hydrogen chloride in the hydrolysis tail gas is in countercurrent contact with the leacheate sprayed in the first-stage leaching tower 4 for absorption, the hydrogen chloride rises to the top of the first-stage leaching tower 4, and the generated hydrochloric acid solution falls to the bottom of the first-stage leaching tower 4.
(3) Spraying by a second-stage leaching tower: hydrolysis tail gas which is sprayed and absorbed by the first-stage leaching tower 4 enters the lower part of the second-stage leaching tower 5 from a second hydrolysis tail gas inlet 51 positioned at the lower part of the second-stage leaching tower 5 through a first hydrolysis tail gas outlet 42, is in countercurrent contact with leacheate which is sprayed downwards in the second-stage leaching tower 5, is further reacted and absorbed, is demisted by a demister and is discharged, and the leacheate used by the first-stage leaching tower 4 and the second-stage leaching tower 5 is calcium hydroxide lye.
(4) Conveying leacheate: with the operation of the system, the pH test paper is used for detecting the pH of the leacheate in the first-stage leaching tower 4, when the pH value of the leacheate in the first-stage leaching tower 4 reaches 3-5, the leacheate in the first-stage leaching tower 4 is conveyed into the hydrolysis tank 2 through the third liquid conveying pipeline 63, the leacheate in the second-stage leaching tower 5 is conveyed into the first-stage leaching tower 4 through the second liquid conveying pipeline 62, and then the new alkali liquor in the alkali liquor tank is conveyed into the second-stage leaching tower 5 through the first liquid conveying pipeline 61. When the leaching solution needs to be supplemented into the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5 at the same time, the first liquid conveying pipeline 61 and the third liquid conveying pipeline 63 are communicated through the fourth liquid conveying pipeline 64, and the alkali liquor is respectively conveyed into the hydrolysis tank 2, the first-stage leaching tower 4 and the second-stage leaching tower 5.
(5) Liquid filter pressing in the hydrolysis tank: after the system stops operating, the liquid in the hydrolysis tank 2 is conveyed to a filter press 7 for solid-liquid separation. The separated solid phase silicon dioxide is neutralized with calcium hydroxide for producing building materials. The liquid phase filtered by pressure is hydrochloric acid solution, and if the concentration of the hydrochloric acid is less than 10%, the hydrochloric acid solution is directly returned to the hydrolysis tank 2 for use through a liquid phase outlet of a filter press 7; if the concentration of the hydrochloric acid is more than 10 percent, the hydrochloric acid solution is conveyed to a neutralization stirring tank 8, and CaO or Ca (OH) is added2Neutralizing until pH is 6-6.5, and temporarily storing the neutralized and filtered clear liquid in a clear liquid pool 9 as a hydrolysis pool 2,Make-up liquid of the first-stage leaching tower 4 and the second-stage leaching tower 5 is used.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it will be understood by those skilled in the art; the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present application.
Claims (10)
1. The absorption system for the hydrolysis tail gas of the high-boiling-point substances in the production of the trichlorosilane is characterized by comprising a high-boiling-point substance storage tank (1), a hydrolysis tank (2), a negative pressure fan (3), a first-stage leaching tower (4) and a second-stage leaching tower (5);
the hydrolysis tank (2) is provided with a hydrolysis tank high-boiling residue inlet (21) and a hydrolysis tank tail gas outlet (22), the primary leaching tower (4) is provided with a first hydrolysis tail gas inlet (41) and a first hydrolysis tail gas outlet (42), and the secondary leaching tower (5) is provided with a second hydrolysis tail gas inlet (51) and a second hydrolysis tail gas outlet (52);
the high-boiling-point substance storage tank (1) is fixedly connected with the high-boiling-point substance inlet (21) of the hydrolysis tank, the tail gas outlet (22) of the hydrolysis tank is fixedly connected with the first hydrolysis tail gas inlet (41) through the negative pressure fan (3), and the first hydrolysis tail gas outlet (42) is fixedly connected with the second hydrolysis tail gas inlet (51);
the hydrolysis tank (2) is used for hydrolyzing the high-boiling-point substances from the high-boiling-point substance storage tank (1) and spraying hydrolysis tail gas generated by hydrolysis;
the negative pressure fan (3) is used for conveying the hydrolysis tail gas sprayed in the hydrolysis tank (2) into the primary leaching tower (4);
the first-stage leaching tower (4) and the second-stage leaching tower (5) are used for absorbing hydrogen chloride gas in the hydrolysis tail gas.
2. The absorption system according to claim 1, further comprising a hydrolysis tank circulating spray assembly, wherein the hydrolysis tank circulating spray assembly comprises a liquid collecting tank (23), a circulating spray pump (24) and a first spray head (25), the liquid collecting tank (23) is fixedly connected with the hydrolysis tank (2), the circulating spray pump (24) is connected between the liquid collecting tank (23) and the spray head (25), and the first spray head (25) is fixedly arranged at the upper part of the hydrolysis tank (2).
3. An absorption system according to claim 2, wherein the liquid inlet of the liquid collection basin (23) is provided with a filter (231).
4. The absorption system according to claim 1, wherein the first leaching tower (4) is provided with a first leaching device, the first leaching device comprises a second spray header (431) arranged at the top of the first leaching tower (4) and a first leaching pump (432) arranged at the bottom of the first leaching tower (4), and the second spray header (431) and the first leaching pump (432) are fixedly connected through a water pipe.
5. The absorption system according to claim 1, wherein the second leaching tower (5) is provided with a second leaching device, the second leaching device comprises a third spray header (531) arranged at the top of the second leaching tower (5) and a second leaching pump (532) arranged at the bottom of the second leaching tower (5), and the third spray header (531) and the second leaching pump (532) are fixedly connected through a water pipe.
6. The absorption system according to claim 5, wherein a demister (54) is provided at the top of the secondary leaching tower (5), and the demister (54) is provided at the upper part of the third spray header (531).
7. The absorption system according to claim 1, further comprising a lye tank for replenishing lye in the absorption system;
a first liquid conveying pipeline (61) is arranged between the alkali liquor tank and the second leaching tower (5), a second liquid conveying pipeline (62) is arranged between the second leaching tower (5) and the first leaching tower (4), and a third liquid conveying pipeline (63) is arranged between the first leaching tower (4) and the hydrolysis tank (2);
the first liquid conveying pipeline (61) is used for conveying alkali liquor from an alkali liquor tank to the second-stage leaching tower (5), the second liquid conveying pipeline (62) is used for conveying leaching liquor in the second-stage leaching tower (5) from the second-stage leaching tower (5) to the first-stage leaching tower (4), and the third liquid conveying pipeline (63) is used for conveying leaching liquor in the first-stage leaching tower (4) from the first-stage leaching tower (4) to the hydrolysis tank (2).
8. An absorption system according to claim 7, further comprising a fourth liquid transfer line (64), said fourth liquid transfer line (64) communicating said first liquid transfer line (61) and a third liquid transfer line (63);
and the third liquid conveying pipeline (63), the fourth liquid conveying pipeline (64) and the first liquid conveying pipeline (61) are communicated and then used for conveying alkali liquor in an alkali liquor tank into the hydrolysis tank (2), the first-stage leaching tower (4) and the second-stage leaching tower (5) respectively.
9. The absorption system according to any one of claims 1 to 8, wherein a filter press (7) is further provided, a feed inlet of the filter press (7) is fixedly connected with a liquid phase outlet of the hydrolysis tank (2), and the liquid phase outlet of the filter press (7) is fixedly connected with the hydrolysis tank (2).
10. The absorption system according to claim 9, further comprising a neutralization stirring tank (8) and a clear liquid tank (9), wherein a feed inlet of the neutralization stirring tank (8) is fixedly connected with a liquid phase outlet of the filter press (7), a feed inlet of the clear liquid tank (9) is fixedly connected with a discharge outlet of the neutralization stirring tank (8), and a discharge outlet of the clear liquid tank (9) is fixedly connected with the hydrolysis tank (2), the first-stage leaching tower (4) and the second-stage leaching tower (5), respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220479979.5U CN216909824U (en) | 2022-03-07 | 2022-03-07 | Absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220479979.5U CN216909824U (en) | 2022-03-07 | 2022-03-07 | Absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216909824U true CN216909824U (en) | 2022-07-08 |
Family
ID=82225997
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202220479979.5U Active CN216909824U (en) | 2022-03-07 | 2022-03-07 | Absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216909824U (en) |
-
2022
- 2022-03-07 CN CN202220479979.5U patent/CN216909824U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201862357U (en) | Device for absorbing tail gas | |
| CN201147664Y (en) | Whole set processing equipment for hydrogenchloride and sulfuric dioxide tail gas | |
| CN210366982U (en) | Absorption device for potassium sulfate byproduct hydrochloric acid by Mannheim method | |
| CN216909824U (en) | Absorption system of high-boiling-point substance hydrolysis tail gas in trichlorosilane production | |
| CN102160962B (en) | Tail gas recovering and purifying treatment device for polycrystalline production line | |
| CN210699529U (en) | Friedel-crafts reaction hydrogen chloride tail gas absorbing device | |
| CN204865499U (en) | Methyl nitrite's waste gas treatment system | |
| CN109224798B (en) | Desulfurization acid making device and vehicular desulfurization equipment | |
| CN1471997A (en) | Washing method and apparatus for phosphoric acid reacting trough extracting tail gas | |
| CN101642660B (en) | Method for treating exhaust gas in process of producing crude phenol from coal tar | |
| CN206188747U (en) | Dissolved acetylene's recycle device among wet acetylene waste water | |
| CN211025790U (en) | Plant liquid purifying box | |
| CN210176768U (en) | Treatment system for tail gas of chlorohydrination method propylene oxide device | |
| CN206783568U (en) | Alcoholysis method handles the reaction and rectification device of tail gas containing chlorsilane | |
| CN217391986U (en) | Leaching reaction tail gas removing device adopting double-tower absorption | |
| CN110585888A (en) | Flue gas desulfurization system of sintering machine | |
| CN220460299U (en) | Hydrochloric acid tail gas absorbing device | |
| CN213610699U (en) | Tail gas and exhaust gas washing unit for sodium chlorate plant | |
| CN218166545U (en) | Zinc volatilization kiln flue gas recovery unit | |
| CN217613972U (en) | Sulfur acid production tail gas treatment device | |
| CN220926685U (en) | Waste sodium hypochlorite recycling acetylene gas treatment system capable of recycling heat energy | |
| CN217794674U (en) | Chlorine-containing waste sulfuric acid dechlorination purification device | |
| CN213467388U (en) | Phosgene tail gas absorption system | |
| CN218393584U (en) | Device for discharging and purifying byproduct hydrogen sulfide in production of rubber auxiliary | |
| CN103570202B (en) | Method and device for recovering electrolytic residues produced in process of producing perfluorocaprylic acid by electrolytic process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |