A production device and process for high-temperature gas-phase condensation method

Abstract

The present invention belongs to the technical field of silicone production, and particularly relates to a production device and process for high-temperature gas-phase condensation method, including: a raw material pretreatment module, which is used for vaporizing, first-stage overheating treatment and second-stage overheating treatment of the raw materials; a reaction module, which at least includes a reaction furnace, and the reaction furnace includes a plurality of reaction pipes arranged vertically; when carrying out the production by high-temperature gas-phase condensation method, the raw materials are first vaporized by the raw material pretreatment module and heated to a set temperature, and then introduced into the reaction pipes to generate products by high-temperature gas-phase condensation method. The production device and process provided by this application have the advantages of fast temperature control response, can reduce the reaction temperature in the reaction zone, reduce corrosion, and reduce the shutdown and maintenance time by 90%.

Description

Technical Field

[0001] The present invention belongs to the technical field of organosilicon production, and particularly relates to a production device and process for high-temperature gas-phase condensation method. Background Art

[0002] The production of phenylchlorosilane by high-temperature gas-phase condensation reaction process has the advantages of low reaction pressure, simple process equipment, and the ability to flexibly switch raw materials to produce different types of phenylchlorosilane products. In addition, since no metal-containing catalyst is used in the production process and the amount of polychlorinated biphenyls generated by the reaction is much less than that of the direct method for synthesizing phenylchlorosilane, it is more environmentally friendly and is an important method for large-scale production of phenylchlorosilane at present.

[0003] The existing high-temperature gas-phase condensation method for producing phenylchlorosilane usually uses a reaction temperature above 600 °C to obtain good reaction activity, so that the reaction residence time can be made as short as possible to reduce the complexity of the reaction device. However, too high a reaction temperature easily causes serious cracking of the raw materials, resulting in coking and blockage of the reaction pipeline. Therefore, it is often necessary to stop the production and clean the reaction pipeline.

[0004] In addition, in the prior art, the high-temperature gas-phase condensation method for producing phenylchlorosilane usually uses a horizontal pipeline as the main space of the reaction zone, which makes it easier for dust to settle and accumulate to form coke, and the reaction pipeline is more likely to be blocked. At the same time, the high-temperature reaction will cause serious high-temperature chlorine corrosion. When the high-temperature chlorine corrosion exceeds the tolerance limit of the metal pipe material, the reaction pipeline is likely to corrode and perforate, further shortening the pipeline replacement cycle. In addition, when the existing device is overhauled, the corroded horizontal straight-section reaction pipelines need to be replaced one by one, and it takes a long time to remove and weld the thick-walled reaction pipelines by fire, which seriously affects the effective utilization time of the production device. Moreover, the main space of the reaction zone arranged horizontally relies on natural convection for heat exchange, and the heat exchange is slow, resulting in a large temperature control lag in the reaction zone, easy over-temperature, and over-temperature will further exacerbate coking. Generally, the larger the reaction device, the greater the temperature control lag, making it difficult to stabilize the production and difficult to obtain the best reaction effect. Summary of the Invention

[0005] The purpose of the present invention is to provide a production device and process for high-temperature gas-phase condensation method to overcome the problems of large temperature control lag, easy coking, blockage, corrosion and perforation leakage of the reaction pipeline, and frequent shutdown for maintenance existing in the existing high-temperature gas-phase condensation method during the production process.

[0006] In view of this, the present invention provides a production device for high-temperature gas-phase condensation method, comprising:

[0007] A raw material pretreatment module for vaporizing, first-stage overheating treatment and second-stage overheating treatment of the raw materials;

[0008] A reaction module, which at least includes a reaction furnace, and the reaction furnace includes a plurality of reaction pipes arranged vertically;

[0009] When producing by high-temperature gas-phase condensation method, the raw materials are first vaporized and heated to a set temperature by the raw material pretreatment module, and then introduced into the reaction pipes to produce products by high-temperature gas-phase condensation method.

[0010] Furthermore, the raw material pretreatment module includes:

[0011] A raw material vaporization unit, which vaporizes the raw materials through a vaporizer;

[0012] A primary overheating treatment unit for raw materials, which performs primary overheating treatment on the raw materials through a primary coil superheater;

[0013] A secondary overheating treatment unit for raw materials, which performs secondary overheating treatment on the raw materials through a secondary coil superheater.

[0014] Furthermore, the raw material vaporization unit includes:

[0015] A raw material storage tank, which is used to store raw materials;

[0016] A filter, which is connected to the raw material storage tank and is used to filter the raw materials output from the raw material storage tank;

[0017] A flowmeter, which is connected to the filter and is used to output a set amount of raw materials;

[0018] A vaporizer, which is connected to the flowmeter and is used to vaporize the raw materials output from the flowmeter.

[0019] Furthermore, the primary overheating treatment unit for raw materials includes:

[0020] A gas-liquid separator, the lower end of the vaporizer is connected to the flowmeter, and the upper end is connected to the gas-liquid separator;

[0021] A primary coil superheater, the upper end of the gas-liquid separator is connected to the upper end of the primary coil superheater;

[0022] A jet mixer I, which is respectively connected to the lower end of the gas-liquid separator and the lower end of the primary coil superheater.

[0023] Furthermore, the secondary overheating treatment unit for raw materials includes:

[0024] A jet mixer II, which is connected to the jet mixer I, substances from different jet mixers I enter the jet mixer II, are quickly mixed in the jet mixer II, and are atomized and ejected;

[0025] A secondary coil superheater has one end connected to the jet mixer II and the other end connected to the raw material inlet of the reactor.

[0026] Furthermore, the reactor comprises:

[0027] A plurality of reaction pipes arranged in a vertical direction;

[0028] A plurality of elbows for connecting the reaction pipes;

[0029] The plurality of reaction pipes are connected end to end in sequence through the elbows to form a bent pipeline.

[0030] Furthermore, a ceramic ring is arranged inside the elbow, or a high temperature and wear-resistant lining layer is arranged on the inner wall of the elbow.

[0031] Furthermore, the diameter of the flow channel inside the elbow is smaller than that of the reaction pipe.

[0032] The reactor also includes:

[0033] A ratchet ring, with inner and outer ratchet teeth arranged in a ring shape on the inner and outer sides thereof;

[0034] The multiple reaction pipes are distributed in a ring shape on the inner side and the outer side of the ratchet ring, so that the multiple reaction pipes form a pipe bundle arranged in a double ring shape as a whole.

[0035] Furthermore, the reaction module includes one or more reaction furnaces. When the reaction module includes a reaction furnace, each reaction furnace is connected in series, in parallel, or in a combination of series and parallel through an auxiliary pipeline.

[0036] Further, the reaction module comprises:

[0037] At least two reactors connected in series;

[0038] and, high temperature circulation fans and hot air molten salt heat exchangers;

[0039] The reaction furnace, high temperature circulation fan and hot air molten salt heat exchanger are connected by pipelines to form a ring-shaped flue gas circulation system;

[0040] The high-temperature flue gas generated in the raw material pretreatment module is introduced into the flue gas circulation system to heat the reaction pipeline.

[0041] A production process for a high-temperature gas phase condensation method, wherein the production process adopts the above-mentioned production device for a high-temperature gas phase condensation method for production.

[0042] The beneficial effects of the present invention are:

[0043] 1. The present application realizes the vaporization of raw materials and the two-stage superheating pretreatment process through modular design to obtain a continuously enhanced raw material flow dispersion function, solving the problems of easy accumulation and coking of solid waste in the vaporizer.

[0044] 2. The present application uses a coil-type flame heating furnace to complete the high-temperature vaporization and superheating of raw materials, which is easy to adapt to high-temperature and high-pressure working conditions, is beneficial to increasing the reaction pressure, and the coil-type flame heating furnace is easy to avoid the flame touching the heat exchange tubes. It has a large heat exchange area and the lowest wall temperature, which is beneficial to reducing the high-temperature cracking of raw materials. Its equipment is compact, and manufacturing, transportation, and installation are convenient. Although the process of modular design is relatively complex, it can occupy less land and be easy to operate through compact installation. At the same time, it also has the advantages that the material capacity in each device during operation is small, which is very beneficial to safety.

[0045] 3. The present application uses vertical tubes as the main body of the reaction space. In this way, large-diameter pipes with low gas velocities can be used to extend the reaction time, which is beneficial to reducing equipment costs. At the same time, it can use high-gas-velocity elbows lined with wear-resistant ceramics to continuously break the agglomeration and deposition of solid particles to ensure the normal operation of the reaction pipeline.

[0046] 4. Through a specific assembly method, the present application obtains the most compact large-diameter pipes, and through the tube bundle structure composed of elbows in series, it is easy to transport by road and can be manufactured in a professional factory, meeting the requirements of greatly reducing the equipment construction, installation, and shutdown maintenance time when building a large-capacity phenylchlorosilane production device.

[0047] 5. By the method of forming a flue gas circulation system by connecting multiple reaction furnaces in series, the temperature in the reaction zone is made more uniform, which is beneficial to reducing the reaction temperature, reducing corrosion, and its temperature control response is fast, ensuring the operation stability of the large-scale device.

[0048] 6. Adopting the device and process of the present application is beneficial to reducing production costs through the large-scale single-unit production capacity of phenylchlorosilane monomers with more economical and reliable operation. It can reduce the reaction temperature, reduce the corrosion rate of the reaction pipeline by 50%, extend the cycle of replacing the pipeline, and make the transformation plan not increase equipment costs when extending the reaction residence time. At the same time, reducing the reaction temperature is also beneficial to reducing the high-boiling slag slurry hazardous waste produced as a by-product, reducing environmental protection costs. The production device and process described in the present application can reduce the shutdown maintenance time by 90% and can greatly reduce equipment maintenance costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0049] Figure 1 is a schematic diagram of the production device for the high-temperature gas-phase condensation method described in the present invention;

[0050] Figure 2 is a schematic diagram of the connection mode of the reaction pipeline and the elbow described in the present invention;

[0051] Figure 3 It is a schematic structural diagram of the spiny ring described in the present invention;

[0052] Figure 4 It is a schematic structural diagram of the reaction module of the present invention.

[0053] The markings in the figure are shown as:

[0054] 1 - reaction pipeline, 2 - elbow, 3 - spiny ring, 4 - inner spiny teeth, 5 - outer spiny teeth, 6 - reaction furnace, 7 - high-temperature circulating fan, 8 - hot air molten salt heat exchanger, 9 - scrubber. Specific embodiments

[0055] Next, the technical solutions in the embodiments of the present application will be clearly described in conjunction with the accompanying drawings in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, rather than all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those of ordinary skill in the art belong to the scope of protection of the present application.

[0056] In the description of the present application, it should be noted that the terms used here are only for describing specific embodiments, rather than intending to limit the exemplary embodiments according to the present application. For the sake of description, the dimensions of the various parts shown in the drawings are not drawn in actual proportional relationship. Technologies, methods, and devices known to those of ordinary skill in the relevant fields may not be discussed in detail, but in appropriate cases, the said technologies, methods, and devices should be regarded as part of the authorization specification. In all the examples shown and discussed here, any specific value should be interpreted as merely exemplary, rather than as a limitation. Therefore, other examples of the exemplary embodiments may have different values. It should be noted that similar reference numerals and letters denote similar items in the following drawings. Therefore, once an item is defined in one drawing, it does not need to be further discussed in subsequent drawings.

[0057] It should be noted that the terms "first", "second", etc. in the description and claims of the present application are used to distinguish similar objects, rather than to describe a specific order or sequence. It should be understood that such data can be interchanged under appropriate circumstances so that the embodiments of the present application can be implemented in an order other than those illustrated or described here, and the objects distinguished by "first", "second", etc. are usually of the same type, and the number of objects is not limited. For example, the first object can be one or multiple. In addition, "and / or" in the description and claims means at least one of the connected objects, and the character " / " generally means an "or" relationship between the associated objects before and after.

[0058] It should be noted that in the description of the present application, the orientation or positional relationships indicated by the orientation terms such as "front, rear, upper, lower, left, right", "lateral, vertical, perpendicular, horizontal" and "top, bottom", etc. are usually based on the orientation or positional relationships shown in the drawings. This is only for the convenience of describing the present application and simplifying the description. Without contrary explanations, these orientation terms do not indicate and imply that the devices or elements referred to must have a specific orientation or be constructed and operated in a specific orientation. Therefore, they should not be construed as limiting the protection scope of the present application; the orientation terms "inner, outer" refer to the inside and outside relative to the contour of each component itself.

[0059] It should be noted that in the present application, the term "comprising", "including" or any other variants thereof is intended to cover non-exclusive inclusion, so that a process, method, article or device including a series of elements not only includes those elements, but also includes other elements not expressly listed, or also includes elements inherent to such process, method, article or device. Without further limitations, the element defined by the statement "including one..." does not exclude the existence of additional identical elements in the process, method, article or device including that element. In addition, it should be pointed out that the scope of the methods and devices in the embodiments of the present application is not limited to performing functions in the order shown or discussed, and may also include performing functions in a substantially simultaneous manner or in a reverse order according to the functions involved. For example, the described methods may be performed in an order different from that described, and various steps may also be added, omitted, or combined. Additionally, the features described with reference to certain examples may be combined in other examples.

[0060] As Figures 1 to 4 shown, a production device for the high-temperature gas-phase condensation method includes:

[0061] A raw material pretreatment module for vaporizing, performing primary overheating treatment and secondary overheating treatment on the raw material;

[0062] A reaction module including at least a reaction furnace 6, and the reaction furnace 6 includes a plurality of reaction pipes 1 arranged in the vertical direction;

[0063] When producing phenylchlorosilane by the high-temperature gas-phase condensation method, the raw material is first vaporized by the raw material pretreatment module and heated to a set temperature, and then introduced into the reaction pipe 1 to produce phenylchlorosilane by the high-temperature gas-phase condensation method.

[0064] Furthermore, the raw material pretreatment module includes:

[0065] A raw material vaporization unit for vaporizing the raw material through a vaporizer;

[0066] A raw material primary overheating treatment unit for performing primary overheating treatment on the raw material through a primary coil superheater;

[0067] The secondary overheating treatment unit for raw materials, which performs secondary overheating treatment on the raw materials through a secondary coil superheater.

[0068] Specifically, in this application, the primary overheating treatment refers to heating the vaporized raw materials to a set temperature T1, and the secondary overheating treatment refers to further heating the raw materials after the primary overheating treatment to a set temperature T2. Therefore, it can be obtained that: T1 < T2, and T2 is the temperature at which the raw materials can undergo high-temperature gas-phase condensation reaction. In addition, the values of T1 and T2 can be set according to the reaction temperature requirements or the heating capacity of the coil superheater.

[0069] As some embodiments of this application, during use, multiple raw material pretreatment modules can be set according to the types and quantities of reaction raw materials, and some devices can be shared among different raw material pretreatment modules according to the reaction characteristics between the raw materials.

[0070] Furthermore, the raw material vaporization unit includes:

[0071] A raw material storage tank, which is used to store raw materials;

[0072] A filter, which is connected to the raw material storage tank and is used to filter the raw materials output from the raw material storage tank;

[0073] A flowmeter, which is connected to the filter and is used to output a set amount of raw materials;

[0074] A vaporizer, which is connected to the flowmeter and is used to vaporize the raw materials output from the flowmeter.

[0075] Even further, the raw material vaporization unit further includes:

[0076] A pump, which is arranged between the raw material storage tank and the filter and is used to transport the materials in the raw material storage tank to the filter.

[0077] Preferably, the filter is a precision filter.

[0078] Preferably, the vaporizer is a coil vaporizer.

[0079] Furthermore, the primary overheating treatment unit for raw materials includes:

[0080] A gas-liquid separator, the lower end of the vaporizer is connected to the flowmeter, and the upper end is connected to the gas-liquid separator;

[0081] A primary coil superheater, the upper end of the gas-liquid separator is connected to the upper end of the primary coil superheater.

[0082] Even further, the primary overheating treatment unit for raw materials further includes:

[0083] The injection mixer I is respectively connected to the lower end of the gas-liquid separator and the lower end of the primary coil superheater.

[0084] The raw materials output by the flowmeter enter the vaporizer through the lower end of the vaporizer, are vaporized by the vaporizer, discharged from the upper end of the vaporizer, and then enter the gas-liquid separator. Most of the gas after gas-liquid separation enters the primary coil superheater through the upper end of the gas-liquid separator, is heated to the primary superheat temperature T1 by the primary coil superheater, and then discharged from the lower end of the primary coil superheater and enters the injection mixer I; the liquid and a small amount of remaining gas in the gas-liquid separator are discharged from the lower end of the gas-liquid separator and enter the injection mixer I, and the gas and liquid in the injection mixer I are quickly mixed and atomized and ejected therein.

[0085] Further, the raw material secondary superheat treatment unit includes:

[0086] The injection mixer II is connected to the injection mixer I, and substances from different injection mixers I enter the injection mixer II, are quickly mixed and atomized and ejected in the injection mixer II;

[0087] The secondary coil superheater has one end connected to the injection mixer II and the other end connected to the raw material inlet of the reaction furnace 6. The raw materials heated to the secondary superheat temperature T2 by the secondary coil superheater directly enter the reaction furnace 6 for high-temperature gas-phase condensation reaction.

[0088] Preferably, the coil vaporizer, the primary coil superheater and the secondary coil superheater adopt a coil-type flame heating furnace to complete the high-temperature gasification and superheating of the raw materials.

[0089] By adopting a modular design, the present application changes the existing way of mixing, vaporizing and superheating raw materials, and adopts the way of vaporizing and superheating separately, which can effectively prevent the formation of coarse dust that is difficult to be carried by gas during the mixing, vaporizing and superheating process of raw materials and accumulate in the reaction pipeline, resulting in coking and blockage of the reaction pipeline.

[0090] Further, the reaction furnace 6 includes:

[0091] Multiple reaction pipes 1 arranged vertically;

[0092] Multiple elbows 2 for connecting the reaction pipes 1;

[0093] The multiple reaction pipes 1 are connected end to end in sequence through the elbows 2 to form a bent pipeline.

[0094] Preferably, the elbow 2 is a 180° connecting elbow. In this way, the reaction pipes 1 connected end to end through the elbow 2 are all arranged vertically.

[0095] Preferably, a wear-resistant and high-temperature-resistant ceramic ring obtained by isostatic pressing sintering is arranged inside the elbow 2, or other methods are used to form a high-temperature-resistant and wear-resistant lining layer on the inner wall of the elbow 2.

[0096] More preferably, the diameter of the flow channel inside the elbow 2 is smaller than that of the reaction pipe 1, so that when the reaction gas carries dust through the elbow 2, the flow rate will increase, which can prompt the solid particles to strengthen the impact and break the agglomeration, thereby maintaining the continuous suspension and flow ability of the dust in the reaction pipe 1.

[0097] Furthermore, the reaction furnace 6 further includes:

[0098] A sprag ring 3, with inner sprags 4 and outer sprags 5 arranged in a ring shape on its inner and outer sides;

[0099] A plurality of reaction pipes 1 are arranged in a ring shape on the inner and outer sides of the sprag ring 3, so that the plurality of reaction pipes 1 form a tube bundle with an overall double-ring arrangement.

[0100] Preferably, as Figure 3 shown, the vertices of the inner sprags 4 and outer sprags 5 in the sprag ring 3 are respectively the projection positions of the reaction pipes 1 for downward gas flow and the reaction pipes 1 for upward gas flow, that is, among them, the reaction pipes 1 for downward gas flow are located at the vertices of the inner sprags 4, and the reaction pipes 1 for upward gas flow are located at the vertices of the outer sprags 5.

[0101] More preferably, the number of the inner sprags 4 and the outer sprags 5 is equal, and they are evenly arranged in the circumferential direction. Each inner sprag 4 corresponds to an outer sprag 5 located in the same radial direction. Correspondingly, two reaction pipes 1 distributed in the same radial direction are called a group. One end of any group of reaction pipes 1 is connected through the elbow 2, and the ports of the two reaction pipes 1 at the other end are respectively connected to the reaction pipes 1 of the previous group or the next group.

[0102] As some embodiments of the present application, the reaction pipes 1 can be welded and assembled with the sprag ring 3 respectively, and then assembled into a whole through other common brackets.

[0103] Further, loading the tube bundle with a double-ring arrangement into the furnace wall can form the reaction furnace 6.

[0104] In this way, the high-temperature gas-phase condensation reaction will be completed through a high-temperature flow reaction in a very long single pipeline. And in the reaction furnace 6, this pipeline is composed of straight pipes connected in series through elbows with different turning directions. By adopting a double-ring arrangement structure composed of inner ratchet teeth 4 and outer ratchet teeth 5 for the reaction pipeline 1, among which, the vertices of adjacent inner ratchet teeth 4 and outer ratchet teeth 5 are respectively the projection positions of adjacent gas ascending vertical pipes and gas descending vertical pipes, and the connection line of the vertices of adjacent inner ratchet teeth 4 and outer ratchet teeth 5 is the projection position of the elbow 2. Each group of adjacent gas ascending vertical pipes and gas descending vertical pipes are connected in series through upper and lower elbows to form a very long bent pipeline respectively, and then are connected in series integrally to form an even longer pipeline. After that, the reaction pipeline 1 can be welded and assembled with the ratchet ring 3 respectively, and then assembled into one body through other common brackets to become the most compact tube bundle assembly structure of a large-diameter pipeline. This compact structure can be hoisted as a whole and is easy to transport by road. Therefore, most of the operations for installing the reaction pipeline 1 can be prefabricated in a professional machinery factory and then transported to the chemical plant for hoisting and installation as a whole. The efficiency is high, and the installation quality is easy to guarantee. When replacing the corroded reaction pipeline 1, it can be lifted and removed as a whole, and the shutdown maintenance time can be reduced by 90%.

[0105] Preferably, the reaction furnace 6 is a vertical cylindrical reaction furnace.

[0106] As some embodiments of the present application, the reaction furnace 6 can also be a vertical square reaction furnace, a rectangular reaction furnace, a regular polygon furnace, and other vertical reaction furnaces with other cross-sections. Correspondingly, different most compact vertical reaction tube bundles can be designed for reaction furnaces 6 with different cross-sectional shapes to meet the requirements of saving investment, facilitating manufacturing, and road transportation, etc.

[0107] Furthermore, the reaction module can include one or more of the reaction furnaces 6. When the reaction module includes several reaction furnaces 6, the reaction furnaces 6 can be connected in series, in parallel, or in a series-parallel hybrid manner through auxiliary pipelines. At this time, the scale of the device can be increased through series connection, or backup equipment can be set up in parallel for rotation use to achieve non-stop production maintenance of the reactor system.

[0108] Preferably, as Figure 4 shown, the reaction module includes two reaction furnaces 6 connected in series.

[0109] During use, two sets of tube bundles with the above-mentioned compact installation structure are respectively installed in two adjacent cylindrical reaction furnaces 6 with the same size, and then connected in series to form an even longer reaction pipeline, which can avoid using a tube bundle with too long a length and reduce the difficulty of manufacturing, transportation, and hoisting.

[0110] Even further, the reaction module further includes:

[0111] A high-temperature circulating fan 7 and a hot-air molten salt heat exchanger 8. The reaction furnace 6, the high-temperature circulating fan 7, and the hot-air molten salt heat exchanger 8 are connected by pipelines to form an annular flue gas circulation system. Through the high-temperature flue gas circulating fan 7, the high-temperature flue gas outside the reaction pipeline 1 can be circulated to uniformly heat the reaction pipeline 1. Through the hot-air molten salt heat exchanger 8, the high-temperature flue gas in the flue gas circulation system can be energy-stored, so that the temperature of the gas outside the reaction pipeline 1 is relatively constant, and further the temperature of the reaction pipeline 1 can be made more uniform.

[0112] In this application, connecting the high-temperature flue gas circulating fan 7 through a large-diameter short elbow can achieve low-circulation pressure drop for large-airflow circulation to control the reaction temperature, making the temperature of the reaction pipeline 1 in the furnace more uniform. The highest reaction temperature can be reduced by more than 40 °C, and the corrosion rate of the reaction pipeline 1 can be reduced by more than 50%.

[0113] Preferably, the high-temperature flue gas generated by the heating flame in the vaporizer, and / or the primary coil superheater, and / or the secondary coil superheater can be introduced into the flue gas circulation system and used as the high-temperature flue gas to heat the reaction pipeline 1 to realize waste heat utilization. The hot flue gas of the heating flame for vaporizing and superheating the raw materials is discharged into the flue gas circulation system, and then the temperature of the high-temperature circulating flue gas is adjusted and controlled by the hot-air molten salt heat exchanger 8 with low flow-through pressure drop to stably control the reaction temperature. The high-temperature reaction waste heat can be introduced into the molten salt system for storage and buffering and then supplied to high-temperature equipment for use.

[0114] In this application, due to the use of the method of forced and rapid circulation of high-temperature flue gas for heating, the heat transfer speed in the reaction zone is fast, the temperature control lag of large-scale devices is small, it is not easy to operate over-temperature, and the coking risk is reduced.

[0115] In addition, the reaction module further includes: a scrubbing tower 9, and the scrubbing tower 9 is used for washing and purifying the carbon black particle-containing high-temperature gas discharged after the reaction module finishes the reaction.

[0116] As some embodiments of this application, a burner can be installed at the bottom of the reaction furnace 6 to complete the temperature-raising and preheating operation of the reaction pipeline 1 during start-up.

[0117] In addition, this application also provides a production process for high-temperature gas-phase condensation. The production process uses the above-mentioned production device for high-temperature gas-phase condensation to produce products such as phenylchlorosilane.

[0118] Of course, in addition to the production of phenylchlorosilane, the production device and process described in this application can also use the high-temperature gas-phase condensation method to prepare other materials.

[0119] The following specifically illustrates the production device and process for high-temperature gas-phase condensation described in this application through specific examples:

[0120] Example 1

[0121] As Figure 1 shown, the raw material liquid from the raw material storage tank is pressurized by a pump and then enters a precision filter to remove the over-sized solid particles carried. Then, it enters the spiral coil vaporizer from the lower end of the coil through a flowmeter to control the flow rate. Most of the liquid is vaporized by flame heating and flows out from the upper end of the coil into the gas-liquid separator. Most of the gas flows out from the upper part of the gas-liquid separator, enters the first-stage spiral coil superheater from the upper end and is heated by flame to 350 - 400 °C. After that, the superheated gas flows out from the lower end of the coil, and is mixed with the gas-liquid mixture discharged from the orifice plate at the bottom of the gas-liquid separator through ejector mixer I to atomize and vaporize the liquid. The solids carried in the liquid are dispersed into fine dust and easily carried away by the gas, preventing the solids in the liquid from accumulating and coking in the pipeline due to over-concentration during the vaporization process.

[0122] Among them, fresh chlorobenzene containing trace moisture and the catalyst can share a set of spiral coil vaporizer, gas-liquid separator, first-stage coil superheater and ejector mixer I; hydrogen-containing chlorosilane and recycled chlorobenzene without moisture share another set of spiral coil vaporizer, gas-liquid separator, first-stage coil superheater and ejector mixer I.

[0123] The two streams of materials that have completed vaporization and first-stage superheating are quickly mixed in ejector mixer II so that moisture and chlorosilane react rapidly to completely eliminate active hydroxyl groups, inhibit the formation of hydrolyzates with high molecular weight and high boiling point, make the hydrolyzates easily carried away by the gas, and prevent them from accumulating in the pipeline and cross-linking and coking at high temperature.

[0124] After that, the mixed gas is heated by flame in the second-stage coil superheater to a temperature capable of initiating the condensation reaction and then sent into the reaction pipeline of the reaction furnace for reaction.

[0125] In the production device and process for high-temperature gas-phase condensation method described in the present application, it is allowed to use a large-diameter reaction pipeline by increasing the reaction pressure to reduce the gas flow rate and extend the reaction time, and thereby reduce the reaction temperature for production use. In this way, high-temperature chlorine corrosion can be significantly reduced and the overhaul and replacement cycle of the reaction pipeline can be extended.

[0126] In addition, the internal space of the vertical pipe is used as the reaction zone in the present application, so that the gas in the reaction pipeline can easily form a suspended flow to carry the solid dust generated by the reaction, preventing deposition and coking.

[0127] The embodiments of the present application have been described above in conjunction with the accompanying drawings. Without conflict, the embodiments and features in the embodiments of the present application can be combined with each other. The present application is not limited to the above specific embodiments. The above specific embodiments are merely illustrative and not restrictive. Under the inspiration of the present application, those of ordinary skill in the art can also make many forms without departing from the purpose of the present application and the scope protected by the claims, and all of them fall within the protection scope of the present application.

Claims

1. A production device for the high-temperature gas-phase condensation method, characterized in that, it includes: A raw material pretreatment module, which is used for vaporizing, first-stage overheating treatment, and second-stage overheating treatment of the raw materials; A reaction module, which at least includes a reaction furnace (6), and the reaction furnace (6) includes a plurality of reaction pipes (1) arranged vertically; When carrying out the production by the high-temperature gas-phase condensation method, the raw materials are first vaporized by the raw material pretreatment module and heated to a set temperature, and then introduced into the reaction pipe (1) to generate products by the high-temperature gas-phase condensation method; The raw material pretreatment module includes: A raw material vaporization unit, which vaporizes the raw materials through a vaporizer; A raw material first-stage overheating treatment unit, which conducts first-stage overheating treatment on the raw materials through a first-stage coil superheater; A raw material second-stage overheating treatment unit, which conducts second-stage overheating treatment on the raw materials through a second-stage coil superheater; The raw material vaporization unit includes: A vaporizer, which is used to vaporize the raw materials, and the vaporizer is a coil vaporizer; The raw material first-stage overheating treatment unit includes: A gas-liquid separator, the lower end of the vaporizer is connected to a flowmeter, and the upper end is connected to the gas-liquid separator; A first-stage coil superheater, the upper end of the gas-liquid separator is connected to the upper end of the first-stage coil superheater; A jet mixer I, which is respectively connected to the lower end of the gas-liquid separator and the lower end of the first-stage coil superheater; The raw material second-stage overheating treatment unit includes: A jet mixer II, which is connected to the jet mixer I, and substances from different jet mixers I enter the jet mixer II, where they are quickly mixed and atomized and ejected; A second-stage coil superheater, one end of which is connected to the jet mixer II, and the other end is connected to the raw material inlet of the reaction furnace (6); The fresh chlorobenzene containing trace moisture and the catalyst share a set of coil vaporizer, gas-liquid separator, first-stage coil superheater, and jet mixer I; the hydrogen-containing chlorosilane and recycled chlorobenzene without moisture share another set of coil vaporizer, gas-liquid separator, first-stage coil superheater, and jet mixer I; The reaction furnace (6) further includes: A plurality of elbows (2) for connecting the reaction pipes (1); A plurality of the reaction pipes (1) are connected end to end in sequence through the elbows (2) to form a bent pipeline; The diameter of the flow channel inside the elbow (2) is smaller than that of the reaction pipe (1).

2. The production device for the high-temperature gas-phase condensation method according to claim 1, characterized in that, The raw material vaporization unit further includes: A raw material storage tank, which is used for storing raw materials; A filter, which is connected to the raw material storage tank and is used for filtering the raw materials output from the raw material storage tank; A flowmeter, which is connected to the filter and is used for outputting a set amount of raw materials; The vaporizer is connected to the flowmeter and is used for vaporizing the raw materials output by the flowmeter.

3. The production device for the high-temperature gas-phase condensation method according to claim 1, characterized in that, Ceramic rings are arranged inside the elbow (2), or a high-temperature resistant and wear-resistant lining layer is arranged on the inner wall of the elbow (2).

4. The production device for the high-temperature gas-phase condensation method according to claim 1, characterized in that, The reactor (6) further includes: A ratchet ring (3) with inner ratchet teeth (4) and outer ratchet teeth (5) arranged in a ring shape on its inner and outer sides; A plurality of reaction pipes (1) are arranged in a ring shape on the inner and outer sides of the ratchet ring (3), so that the plurality of reaction pipes (1) form a tube bundle with an overall double-ring layout.

5. The production device for high-temperature gas-phase condensation method according to claim 1, characterized in that the reaction module includes one or more of the reactors (6). When the reaction module includes a plurality of the reactors (6), the reactors (6) are connected in series, in parallel or in a mixed series-parallel manner through auxiliary pipes.

6. The production device for high-temperature gas-phase condensation method according to claim 1, characterized in that the reaction module includes: at least two reactors (6) connected in series; and a high-temperature circulating fan (7) and a hot air molten salt heat exchanger (8); the reactor (6), the high-temperature circulating fan (7) and the hot air molten salt heat exchanger (8) are connected through pipes to form a circular flue gas circulation system; The high-temperature flue gas generated in the raw material pretreatment module is introduced into the flue gas circulation system to heat the reaction pipes (1).

7. A production process for high-temperature gas-phase condensation method, characterized in that the production process is carried out using the production device for high-temperature gas-phase condensation method according to any one of claims 1 to 6 above.

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