A fumed white carbon black preparation system

Abstract

The application discloses a fumed white carbon black preparation system, which comprises an air inlet pipeline, a hydrogen inlet pipeline, an air inlet of a static mixer, a gas phase pipeline of a chlorosilane vaporizer, a steam heater installed on the air inlet pipeline and the hydrogen inlet pipeline, a reactant inlet of a burner, and an air inlet cavity of the burner. The air inlet cavity is tangent to the air inlet pipeline. The air inlet pipeline and the hydrogen inlet pipeline are connected to the air inlet of the static mixer. The air inlet of the burner is connected to the outlet of the static mixer. The air at the top of the reaction furnace enters the burner along the tangent direction of the air inlet cavity. The advantages are as follows: the reactants, chlorosilane, hydrogen and air, are fully mixed in the static mixer and then enter the burner to perform a high-temperature hydrolysis reaction; the hydrogen and air mixed gas sent into the reaction furnace through a sleeve serves as a protective gas, which can ensure the long-lasting flame of the burner; and the normal-temperature hydrogen and air are heated by corresponding steam heaters and then sent into the burner, so that the temperature field is improved, the chlorosilane is prevented from being liquefied, the reactants are fully hydrolyzed and combusted, and the product quality is improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of gas phase white carbon black production equipment, in particular to a gas phase white carbon black preparation system. BACKGROUND

[0002] The gas phase white carbon black is one of the most important high-tech ultra-fine inorganic new materials. Because of its small particle size, it has large specific surface area, strong surface adsorption, large surface energy, high chemical purity, good dispersion performance, and special properties in thermal resistance, electrical resistance, etc. It has unique properties in many disciplines and fields due to its superior stability, reinforcement, thickening and thixotropy, and cannot be replaced.

[0003] The reaction material for producing the gas phase white carbon black in industry is chlorosilane, air and hydrogen. The gas phase white carbon black process is to generate the gas phase white carbon black from chlorosilane, air and hydrogen in the reaction furnace, and the reaction temperature reaches 800-1400℃. In order to ensure the continuous reaction in the reaction furnace, the combustion-supporting mixed gas of air and hydrogen is additionally introduced into the reaction furnace. The cooled gas phase white carbon black is sent into the deacidification furnace for deacidification treatment.

[0004] The existing problems are: a. The air and hydrogen introduced into the reaction furnace can reduce the temperature of the reactants, resulting in insufficient combustion of carbon elements in the reactants and affecting the product quality; b. There is a phenomenon of hydrogen chloride and water liquidization and mixing with silicon dioxide accumulation in the dead angle at the top of the combustion chamber, which can cause corrosion of the reaction furnace equipment; c. The steam produced by the power plant and introduced into the deacidification furnace contains impurities, which affects the product quality. SUMMARY

[0005] The purpose of the present application is to provide a gas phase white carbon black preparation system which is beneficial to improve the product quality.

[0006] The application is implemented by the following technical scheme: a fumed white carbon black preparation system, comprising an air inlet pipeline, a hydrogen inlet pipeline, a chlorosilane vaporizer, a static mixer, a burner, a reaction furnace, a collector, a first cyclone separator, a deacidification furnace, a drying furnace, a bag-type dust collector and a hydrogen burner; the top of the reaction furnace is provided with an air inlet cavity, the air inlet cavity is provided with the burner, the top of the burner is provided with the static mixer in communication; the air inlet of the static mixer is in communication with the air inlet pipeline, the hydrogen inlet pipeline and the gas phase pipeline of the chlorosilane vaporizer, the steam heater is installed on the air inlet pipeline and the hydrogen inlet pipeline; the air inlet of the sleeve of the burner is in communication with the air inlet pipeline and the hydrogen inlet pipeline, the air inlet cavity is in communication with the air inlet pipeline in the tangential direction; the bottom discharge port of the reaction furnace is connected with the starting end of the discharge pipeline, the end of the discharge pipeline is in communication with the pipe passage inlet of the collector, the pipe passage outlet of the collector is in communication with the inlet of the first cyclone separator, the exhaust port of the first cyclone separator is in communication with the inlet of the bag-type dust collector; the bottom discharge port of the first cyclone separator and the bottom discharge port of the bag-type dust collector are in communication with the feed inlet of the deacidification furnace through the discharge pipeline, the discharge port of the deacidification furnace is in communication with the drying furnace; the inlet of the hydrogen burner is in communication with the hydrogen inlet pipeline and the air inlet pipeline, the steam outlet of the hydrogen burner is in communication with the air inlet pipeline and then in communication with the bottom of the deacidification furnace.

[0007] Further, the initial section of the discharge pipeline is a vertical section with a length of 2-5 m.

[0008] Further, it further comprises a first water pump and a vapor-liquid separator; the outer wall of the reaction furnace is provided with a cooling interlayer, the discharge pipeline is provided with a heat exchange sleeve, and the two ends of the heat exchange sleeve are sealed;

[0009] The water outlet of the first water pump is in communication with the bottom water inlet of the cooling interlayer of the reaction furnace and one end of the heat exchange sleeve on the discharge pipeline of the reaction furnace through pipelines, the other end of the heat exchange sleeve and the top water outlet of the cooling interlayer are in communication with the inlet of the vapor-liquid separator through pipelines, the top exhaust port of the vapor-liquid separator is connected with a steam exhaust pipeline, and the bottom liquid outlet of the vapor-liquid separator is in communication with the water inlet of the first water pump; the circulating desalted water temperature of the first water pump is 120-160 DEG C.

[0010] Further, the water inlet of the first water pump is connected with a desalted water supplement pipeline.

[0011] Further, the steam exhaust pipeline and the desalted water supplement pipeline are both provided with an electric control valve, and the pressure in the vapor-liquid separator is 0.2-0.5 MPa.

[0012] Further, it further comprises a second water pump and a cooler; the water outlet of the second water pump is communicated with the shell side inlet of the end of the collector through a pipeline, the shell side outlet of the initial end of the collector is communicated with the water inlet of the second water pump through a backwater pipeline, and the cooler is installed on the backwater pipeline; the desalted water temperature of the second water pump is 65-95 DEG C.

[0013] Further, the discharge port of the deacidification furnace is communicated with the drying furnace, the gas discharge port of the deacidification furnace and the gas discharge port of the drying furnace are communicated with the inlet of the second cyclone separator, the exhaust port of the second cyclone separator is communicated with the inlet of the bag-type dust collector, and the bottom discharge port of the second cyclone separator is communicated with the discharging pipe.

[0014] Further, it further comprises an electric heater, the outlet of the hydrogen gas burner is communicated with the gas inlet of the electric heater, and the gas outlet of the electric heater is communicated with the bottom of the deacidification furnace.

[0015] The application has the advantages that: the heated air is introduced into the static mixer through the air inlet pipeline, the heated hydrogen is introduced into the static mixer through the hydrogen inlet pipeline, the gaseous reactant chlorosilane is fully mixed with the air and hydrogen in the static mixer, and then enters the burner to perform the high-temperature hydrolysis reaction; during the reaction, the hydrogen and air mixture sent into the reaction furnace through the sleeve serves as the protective gas, which can ensure the long-lasting flame of the burner and the reaction temperature; in addition, the normal-temperature hydrogen and air are heated by the corresponding steam heaters and then sent into the burner, which avoids affecting the reaction temperature of the reactants, ensures the full hydrolysis combustion reaction of the reactants, and improves the product quality; in addition, the heated air is sent into the reaction furnace along the tangent direction of the air inlet cavity, which is beneficial to blowing down the hydrogen chloride droplet product in the dead angle of the reaction furnace and avoiding the long-term formation and accumulation of the hydrogen chloride droplet product to corrode the equipment.

[0016] The air introduced through the air inlet pipeline and the hydrogen introduced through the hydrogen inlet pipeline enter the hydrogen burner to perform the reaction, generate clean water vapor, and provide clean steam for the deacidification furnace, which is beneficial to ensuring the product quality of the white carbon black; the generated steam is mixed with the air, heated by the electric heater, and then sent into the deacidification furnace, in which the white carbon black powder, hot steam and hot air form the fluidized state, and the white carbon black is fully mixed with the steam and hot air to remove the adsorbed hydrogen chloride on the white carbon black. BRIEF DESCRIPTION OF DRAWINGS

[0017] Figure 1 It is a structural schematic view of the application.

[0018] Figure 2 It is a structural schematic view of the reaction furnace.

[0019] The labels of the components in the drawings are as follows: air inlet pipeline 1, hydrogen inlet pipeline 2, steam heater 3, chlorosilane vaporizer 4, static mixer 5, reaction furnace 6, gas inlet cavity 6.1, sight glass 6.2, burner 7, sleeve 7.1, igniter 8, discharge pipeline 9, cooling jacket 10, heat exchange sleeve 11, first water pump 12, vapor-liquid separator 13, steam exhaust pipeline 14, desalted water supplement pipeline 15, electric control valve 16, collector 17, second water pump 18, water return pipeline 19, cooler 20, first cyclone separator 21, discharge pipe 22, deacidification furnace 23, drying furnace 24, second cyclone separator 25, bag-type dust collector 26, hydrogen burner 27, air inlet pipeline 28, hydrogen inlet pipeline 29, electric heater 30, steam generator 31. DETAILED DESCRIPTION

[0020] The technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are only part of the embodiments of the present application, rather than all the embodiments of the present application. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative work fall within the scope of protection of the present application.

[0021] As shown in Figure 1 and Figure 2 , the present embodiment provides a fumed silica preparation system, which comprises an air inlet pipeline 1, a hydrogen inlet pipeline 2, a chlorosilane vaporizer 4, a static mixer 5, a burner 7, a reaction furnace 6, a collector 17, a first cyclone separator 21, a deacidification furnace 23, a drying furnace 24, a bag-type dust collector 26, and a hydrogen burner 27.

[0022] The top of the reaction furnace 6 is provided with a gas inlet cavity 6.1, and the burner 7 is arranged on the gas inlet cavity 6.1. The top reactant inlet of the burner 7 is in communication with the outlet of the static mixer 5. The burner 7 comprises a reactant feeding pipe and a sleeve 7.1 coaxially sleeved and arranged on the reactant feeding pipe. The reactant feeding pipe is used to feed the reactant for reaction. The passage between the reactant feeding pipe and the sleeve 7.1 is used to feed the air and hydrogen mixed gas as combustion-supporting gas. The igniter 8 is arranged in the reaction furnace 6 below the burner 7 to provide temperature for the reaction of the reactant. The sight glass 6.2 is arranged on the side wall of the reaction furnace 6 opposite to the igniter 8, so as to facilitate the observation of the working condition in the reaction furnace 6.

[0023] The air inlet of the static mixer 5 is communicated with the air inlet pipeline 1, the hydrogen inlet pipeline 2 and the gas phase pipeline of the chlorosilane vaporizer 4. The chlorosilane vaporizer 4 is used for vaporizing liquid chlorosilane. The chlorosilane raw material is one or more than one mixture of methyltrichlorosilane, silicon tetrachloride, trichlorosilane hydrogen and methyldichlorosilane. The steam heaters 3 are installed on the air inlet pipeline 1 and the hydrogen inlet pipeline 2, and are used for heating air and hydrogen to ensure the inlet temperature required by the process.

[0024] The heated air is introduced into the static mixer 5 through the air inlet pipeline 1, and the heated hydrogen is introduced into the static mixer 5 through the hydrogen inlet pipeline 2. The gas phase reactant chlorosilane, the air and the hydrogen are fully mixed in the static mixer 5, and then enter the burner 7 to perform a high-temperature hydrolysis reaction. That is, the air and the hydrogen react to generate water at high temperature, and the chlorosilane performs a hydrolysis reaction. Then, the chlorosilane enters the reaction furnace 6 to continue the reaction.

[0025] The air inlet on the sleeve 7.1 of the burner 7 is communicated with the air inlet pipeline 1 and the hydrogen inlet pipeline 2. The air inlet cavity 6.1 is communicated with the air inlet pipeline 1 in a tangential direction. The top air of the reaction furnace 6 enters the burner 7 in a tangential direction of the air inlet cavity 6.1. In the reaction process, the hydrogen and air mixture sent into the reaction furnace 6 through the sleeve 7.1 serves as a protective gas, which can ensure the long-lasting flame of the burner 7 and ensure the reaction temperature. Moreover, the hydrogen and air at normal temperature are heated by the corresponding steam heaters 3 and then sent into the burner 7, which avoids affecting the reaction temperature of the reactants and ensures the full hydrolysis and combustion reaction of the reactants, so as to improve the product quality. In addition, the heated air sent into the reaction furnace 6 in a tangential direction of the air inlet cavity 6.1 is beneficial to liquefying hydrogen chloride and water in the dead angle of the reaction furnace 6 and blowing down the mixed accumulation of silicon dioxide, so as to avoid long-term accumulation and corrosion of the equipment.

[0026] The bottom discharge port of the reaction furnace 6 is connected with one end of the discharge pipeline 9. The other end of the discharge pipeline 9 is communicated with the pipe inlet of the collector 17. The pipe outlet of the collector 17 is communicated with the inlet of the first cyclone separator 21. The initial section of the discharge pipeline 9 connected with the reaction furnace 6 is a vertical section with a length of 2-5 meters, which is beneficial to prolong the reaction time to ensure the full combustion of carbon elements and further improve the product quality.

[0027] The outer wall of the reaction furnace 6 is provided with a cooling sandwich 10, and the discharge pipeline 9 is provided with a heat exchange sleeve 11, the two ends of which are sealed; the outlet of the first water pump 12 is connected to the bottom inlet of the cooling sandwich 10 and one end of the heat exchange sleeve 11 through pipelines, the other end of the heat exchange sleeve 11 and the top outlet of the cooling sandwich 10 are connected to the inlet of the vapor-liquid separator 13 through pipelines, the bottom outlet of the vapor-liquid separator 13 is connected to the inlet of the first water pump 12, the circulating desalinated water temperature of the first water pump 12 is 120-160℃, and the top exhaust port of the vapor-liquid separator 13 is connected to a steam exhaust pipeline 14; the desalinated water with a temperature of 120-160℃ is sent into the cooling sandwich 10 and the heat exchange sleeve 11 through the first water pump 12, which can cool the furnace wall of the reaction furnace 6 under the premise of ensuring the reaction temperature in the reaction furnace 6, avoid too high temperature to shorten the service life of the equipment, and at the same time, can cool the product in the discharge pipeline 9 to a certain extent, and can also ensure the continuous full reaction of the material in the vertical section of the discharge pipeline 9, avoiding too low temperature to affect the reaction efficiency; the desalinated water after heat exchange enters the vapor-liquid separator 13 in the form of a vapor-liquid mixture, is separated, the gas after separation enters the steam pipe network along the steam exhaust pipeline 14, and the desalinated water after separation continues to circulate through the first water pump 12.

[0028] The inlet of the first water pump 12 is connected to a desalinated water supplement pipeline 15 for timely supplement of desalinated water; the steam exhaust pipeline 14 and the desalinated water supplement pipeline 15 are both provided with an electric control valve 16, the pressure in the vapor-liquid separator 13 is 0.2-0.5 MPa; a pressure transmitter and a liquid level sensor are installed in the vapor-liquid separator 13 for real-time monitoring of the pressure and liquid level in the vapor-liquid separator 13 and feeding back signals to a control system, and an industrial controller is commonly used; when the liquid level drops to a set lower limit value, the electric control valve 16 on the desalinated water supplement pipeline 15 is opened through the controller to realize water supplement; when the pressure in the vapor-liquid separator 13 reaches a set upper limit value, the electric control valve 16 on the steam exhaust pipeline 14 is opened through the controller to realize exhaust and ensure safe production.

[0029] The outlet of the second water pump 18 is connected to the shell inlet of the end of the collector 17 through a pipeline, the shell outlet of the initial end of the collector 17 is connected to the inlet of the second water pump 18 through a backwater pipeline 19, and a cooler 20 is installed on the backwater pipeline 19 to cool the hot water after heat exchange; the desalinated water temperature of the second water pump 18 is 65-95℃; after the first-stage cooling of the material in the front section of the discharge pipeline 9 by the circulating hot water in the heat exchange sleeve 11, the product in the discharge pipeline 9 is cooled again by the desalinated water in the collector 17 under the action of the second water pump 18, so that the discharge temperature of the discharge pipeline 9 meets the process requirements.

[0030] The exhaust port of the first cyclone separator 21 is communicated with the inlet of the bag-type dust collector 26; the bottom discharge port of the first cyclone separator 21 and the bottom discharge port of the bag-type dust collector 26 are communicated with the feed inlet of the deacidification furnace 23 through the downcomer 22, and the downcomer 22 is provided with a rotary down valve; the outlet of the bag-type dust collector 26 is connected to the tail gas recovery system through an induced draft fan, and the tail gas recovery system is a prior art system for absorbing acid gas, and the specific structure is not described herein; the product after reaction in the reaction furnace 6 includes hydrogen chloride gas, chlorine gas and white carbon black powder, and under the action of negative pressure, the product in the discharge pipeline 9 is sequentially introduced into the first cyclone separator 21 and the bag-type dust collector 26 after heat exchange and cooling; the gas-solid separation is realized through the first cyclone separator 21 and the bag-type dust collector 26, that is, the hydrogen chloride gas and the chlorine gas after separation are introduced into the subsequent tail gas recovery system for recovery treatment, and the white carbon black trapped in the first cyclone separator 21 and the bag-type dust collector 26 is discharged to the downcomer 22 through the bottom discharge port and is introduced into the deacidification furnace 23 through the rotary down valve, and since a small amount of hydrogen chloride and chlorine is adsorbed in the white carbon black, it is necessary to introduce the deacidification furnace 23 for further separation to ensure the quality of the white carbon black product.

[0031] The discharge port of the deacidification furnace 23 is communicated with the drying furnace 24 through a drop tube, and the drop tube is provided with a rotary down valve; the gas discharge port of the deacidification furnace 23 and the gas discharge port of the drying furnace 24 are communicated with the inlet of the second cyclone separator 25, and the exhaust port of the second cyclone separator 25 is communicated with the inlet of the bag-type dust collector 26; the bottom discharge port of the second cyclone separator 25 is communicated with the downcomer 22; the hydrogen chloride adsorbed on the white carbon black is removed through the deacidification furnace 23, and under the action of negative pressure, the tail gas in the deacidification furnace 23 and the drying furnace 24 is introduced into the subsequent tail gas recovery system after the second cyclone separator 25 and the bag-type dust collector 26, and is subjected to recovery treatment, and the white carbon black product in the deacidification furnace 23 is introduced into the drying furnace 24 through the drop tube for drying treatment.

[0032] The inlet of the hydrogen gas burner 27 is communicated with the hydrogen gas pipeline 29 and the air pipeline 28, the outlet of the hydrogen gas burner 27 is communicated with the gas inlet of the electric heater 30, the steam outlet of the hydrogen gas burner 27 is communicated with the air pipeline 28, and the gas outlet of the electric heater 30 is communicated with the bottom of the deacidification furnace 23; the air introduced through the air pipeline 28 and the hydrogen gas introduced through the hydrogen gas pipeline 29 are introduced into the hydrogen gas burner 27 to react, generate clean water vapor, provide clean steam for the deacidification furnace 23, and are beneficial to ensuring the product quality of the white carbon black; the generated steam is mixed with air, heated by the electric heater 30, and then introduced into the deacidification furnace 23, and in the deacidification furnace 23, the white carbon black powder, hot steam and hot air form a fluidized state, the white carbon black is fully mixed with the steam and hot air to remove the hydrogen chloride adsorbed on the white carbon black.

[0033] The above merely provides the preferred embodiment of the present application, and is not used to limit the present application. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the protection scope of the present application.

Claims

1. A fumed silica preparation system, characterized in that: It includes air inlet pipeline, hydrogen inlet pipeline, chlorosilane vaporizer, static mixer, burner, reactor, aggregator, first cyclone separator, deacidification furnace, drying furnace, bag dust collector, hydrogen burner; An air inlet cavity is provided on the top of the reactor, a burner is provided on the air inlet cavity, and the static mixer is connected to the top of the burner; The air inlet of the static mixer is in communication with the air inlet pipeline, the hydrogen inlet pipeline and the gas phase pipeline of the chlorosilane vaporizer, and a steam heater is installed on both the air inlet pipeline and the hydrogen inlet pipeline; The air inlet on the sleeve of the burner is connected to the air inlet pipeline and the hydrogen inlet pipeline, and the air inlet cavity is connected to the air inlet pipeline along the tangential direction; The bottom discharge port of the reaction furnace is connected to the starting end of the discharge pipeline, the end of the discharge pipeline is connected to the tube-side inlet of the aggregator, the tube-side outlet of the aggregator is connected to the inlet of the first cyclone separator, and the exhaust port of the first cyclone separator is connected to the inlet of the bag-type dust collector; the bottom discharge port of the first cyclone separator and the bottom discharge port of the bag-type dust collector are connected to the feed port of the deacidification furnace through a feed pipe, and the discharge port of the deacidification furnace is connected to the drying furnace; The inlet of the hydrogen burner is connected to the hydrogen inlet pipeline and the air inlet pipeline. The steam outlet of the hydrogen burner is connected to the air inlet pipeline and then to the bottom of the deacidification furnace.

2. A fumed silica preparation system according to claim 1, characterized in that: The initial section of the discharge pipeline is a vertical section with a length of 2 meters to 5 meters.

3. The system for preparing fumed silica according to claim 1, wherein: It also includes a first water pump and a vapor-liquid separator; the outer wall of the reactor is provided with a cooling interlayer, the discharge pipeline is provided with a heat exchange sleeve, and both ends of the heat exchange sleeve are sealed; The water outlet of the first water pump is connected to the bottom water inlet of the cooling interlayer of the reactor and one end of the heat exchange sleeve on the discharge pipeline of the reactor through a pipeline. The other end of the heat exchange sleeve and the top water outlet of the cooling interlayer are connected to the inlet of the vapor-liquid separator through a pipeline. The top exhaust port of the vapor-liquid separator is connected to the steam exhaust pipeline, and the bottom liquid outlet of the vapor-liquid separator is connected to the water inlet of the first water pump. The temperature of the circulating desalted water of the first water pump is 120℃-160℃.

4. A fumed silica preparation system according to claim 3, characterized in that: The water inlet of the first water pump is connected to a desalted water replenishment pipeline.

5. The system for preparing fumed silica according to claim 4, characterized in that: The steam exhaust pipeline and the desalted water supply pipeline are both installed with electric control valves, and the pressure in the vapor-liquid separator is 0.2 to 0.5 MPa.

6. The system for preparing fumed silica according to claim 1, characterized in that: It also includes a second water pump and a cooler; the water outlet of the second water pump is connected to the shell-side inlet at the end of the aggregator through a pipeline, and the shell-side outlet at the initial end of the aggregator is connected to the water inlet of the second water pump through a return pipeline, and the cooler is installed on the return pipeline; the desalted water temperature of the second water pump is 65°C-95°C.

7. The system for preparing fumed silica according to claim 1, characterized in that: The gas exhaust port of the deacidification furnace and the gas exhaust port of the drying furnace are connected to the inlet of the second cyclone separator, the exhaust port of the second cyclone separator is connected to the inlet of the bag dust collector; the bottom discharge port of the second cyclone separator is connected to the discharge pipe.

8. The system for preparing fumed silica according to claim 1, characterized in that: It also includes an electric heater, the outlet of the hydrogen burner is communicated with the gas inlet of the electric heater, and the gas outlet of the electric heater is communicated with the bottom of the deacidification furnace.

Images