Acetylene generator and acetylene production device adopting acetylene generator

Abstract

The invention relates to a device for producing acetylene by a dry method, and discloses an acetylene generator and an acetylene production device adopting the acetylene generator. The acetylene generator comprises a venturi mixer, a first raw material inlet of the venturi mixer is connected with a premixing device, the premixing device is provided with a first powder inlet, a first gas inlet and a first mixing area, a second raw material inlet of the venturi mixer is connected with a steam generator, and the outlet end of the venturi mixer is connected with a pipe wall opening of a tail gas flattening pipe. One end of the tail gas leveling pipe is provided with a heat-carrying gas interface, and the other end of the tail gas leveling pipe is a product outlet. According to the invention, the nanoscale calcium carbide powder is used as a raw material and is mixed with steam to react to generate the crude acetylene gas, so that the reaction completeness rate is increased, the reaction device and the control system thereof are simplified, the steam content of the reaction product is reduced, and gas-solid separation of subsequent products, purification of the crude acetylene gas and recycling of impurities in the product are facilitated.

Description

Technical Field

[0001] The present invention relates to a device for producing acetylene by dry process, in particular to an acetylene generator used in the device. Background Art

[0002] Acetylene is a common industrial gas with a wide range of industrial applications. Carbide-process polyvinyl chloride production relies on large-scale equipment to generate stable acetylene gas. Common equipment includes wet-process and dry-process acetylene generators. Dry-process acetylene is generally less stable and safe than wet-process acetylene. However, dry-process acetylene offers advantages in terms of sufficient raw material reaction, low water consumption, and easy handling of carbide slag. A comparison of the carbide slag handling costs of wet-process acetylene with those of dry-process acetylene for the same purpose reveals significant advantages in operating costs and total investment.

[0003] Currently, dry acetylene generators are typically disc-type reactors, similar in appearance to reactors. Internally, they feature multiple layers of distribution discs, agitation, and a raking mechanism. Acetylene gas is released through a chemical reaction between misted water and fine calcium carbide particles. However, common issues with existing dry acetylene reactors include insufficient reaction efficiency, requiring further improvement in acetylene yield. The use of steam to control reactor temperature results in high levels of steam and phosphine entrained in the crude acetylene gas, hindering subsequent purification. Furthermore, the reaction is unstable, necessitating the use of dedicated acetylene gas cabinets for storage and transfer. Acetylene is a flammable and explosive gas with an explosion limit in air of 2.5-82% (V / V), requiring ample spacing around the equipment, resulting in a large footprint and reduced land utilization within the production area. Summary of the Invention

[0004] To overcome at least one of the problems of existing dry-process acetylene reactors, the present invention provides an acetylene generator and an acetylene production device utilizing the same. The device utilizes nanometer-sized calcium carbide powder as a raw material, which reacts with steam to produce crude acetylene gas. This improves the reaction completion rate, simplifies the reaction apparatus and its control system, reduces the steam content of the reaction product, and facilitates subsequent gas-solid separation of the product, purification of the crude acetylene gas, and recovery of impurities in the product.

[0005] The technical solution adopted by the present invention to solve its technical problems is: an acetylene generator includes a Venturi mixer, the Venturi mixer is provided with a first raw material inlet arranged in the radial direction and a second raw material inlet arranged in the axial direction, the first raw material inlet is connected to a premixing device, the premixing device is provided with a first powder inlet, a first gas inlet and a first mixing zone, the mixing pipe section of the Venturi mixer is the second mixing zone, the outlet end of the mixing pipe section is connected to a pipe wall opening of an exhaust gas smoothing pipe, one end of the exhaust gas smoothing pipe is provided with a heat carrier gas interface, and the other end of the exhaust gas smoothing pipe is a product outlet.

[0006] The premixing device also adopts a Venturi mixer, with the axial inlet of the Venturi mixer serving as the first powder inlet and the radial inlet of the Venturi mixer serving as the first gas inlet.

[0007] A feed control valve is provided between the premixing device and the first raw material inlet.

[0008] A second hot gas interface is further provided on the tail gas smoothing pipe, and the hot gas interface, the second hot gas interface and the first gas inlet are all connected to the hot gas main pipe.

[0009] The product outlet of the tail gas leveling pipe is connected to the inlet of the tail gas separation device. The tail gas separation device includes a gas outlet and a solid outlet. The gas outlet is connected to the air inlet end of the heat carrier gas main pipe.

[0010] The present invention also provides an acetylene production device, comprising an acetylene generator. The acetylene generator utilizes the aforementioned acetylene generator, wherein the first powder inlet is connected to a calcium carbide powder silo, and the second raw material inlet is connected to a steam outlet of a steam generator. The steam generator's high-temperature medium is crude acetylene gas from the gas outlet of a tail gas leveling pipe, and the low-temperature medium is pure water. The device utilizes the heat released by the reaction between calcium carbide powder and water to heat the pure water into steam, which is then fed into the generator. The steam reacts with the gas-dispersed calcium carbide powder, achieving a self-sustaining reaction, improving reaction completion, and enabling precise feed control. The reaction product is a mixture of gas and powder, simplifying reaction control.

[0011] A heating jacket is positioned around the connection area between the mixing pipe section and the tail gas smoothing pipe of the acetylene generator. The steam outlet of the steam generator is connected to the medium inlet of the heating jacket, which in turn is connected to the second raw material inlet. The heating jacket further superheats the steam before feeding it into the acetylene generator, thereby utilizing and regulating the heat released by the acetylene generator reaction.

[0012] Since the reaction product after using the device of the present invention is a mixture of gas and powder, the separation and collection of acetylene gas can adopt a cyclone separator that cannot be used in conventional dry acetylene production. Therefore, a cyclone separator, a bag dust collector, a crude acetylene gas cabinet and a crude acetylene blower are connected in sequence between the product outlet of the tail gas smoothing pipe and the high-temperature medium inlet of the steam generator, and the solid outlet of the cyclone separator is connected to the pelletizer.

[0013] The cyclone separator comprises a primary cyclone separator and a secondary cyclone separator. A selenium-iron remover is provided in the pipeline between the two stages of the cyclone separators to achieve purification of calcium hydroxide powder and recovery of ferroselenium.

[0014] The steam generator's high-temperature medium is equipped with two outlets at different temperatures. The higher-temperature outlet is connected to the heat carrier port of the tail gas leveling pipe, while the lower-temperature outlet is connected to the pressure swing adsorption equipment and acetylene purification device in sequence. Based on the requirements for smooth and continuous reaction, the temperature reduction control range of the high-temperature medium at different outlets can be determined through calculation.

[0015] The beneficial effects of the present invention are as follows: using nanometer-sized calcium carbide powder and steam as raw materials, compared with the existing dry acetylene particles participating in the reaction, the reaction surface area is multiplied, and the reaction environment temperature is increased, so that the main reaction can be completed quickly; the two raw materials of the main reaction are one in gas phase and the other is powder dispersed by gas, which has good uniformity and dispersion, so the reaction system can be simplified, and a fixed reactor is used to monitor and adjust the reaction process through the two key factors of pressure and temperature. The use of the above-mentioned reaction device simplifies the reaction process control, facilitates the realization of DCS automatic control, and at the same time, facilitates production capacity regulation, and can eliminate the acetylene gas cabinet commonly used in the original conventional acetylene generation device, reducing the number of major hazardous sources in the system and improving safety; the above conditions can achieve a higher reaction completeness rate, thereby reducing the steam content entrained in the product, facilitating subsequent dust removal and purification treatment, and the solid product produced by the reaction is also nano-scale, among which calcium hydroxide powder can be used as a high-quality raw material for calcium carbide production, and the impurity ferroselenium therein is easier to separate from the calcium hydroxide powder; the heat release of the reaction can be removed in a self-sustaining cycle to maintain the stability of the reaction system, steam can be generated by evaporating pure water through heat transfer from the reaction heat release, and steam can be produced as a by-product, thereby reducing the energy consumption of the system operation; the internal structure of the reaction device is simple, and steam can be used for flushing and regeneration in a very short time, effectively extending the normal operating cycle of the generator; the material balance and heat balance of the acetylene generator can be adjusted by the solid discharge amount of the buffer feed bin and the diversion flow rate and partial pressure of the by-product steam, thereby improving the safety and stability of the system. The present invention can be used when a new acetylene production system is built. A single acetylene generator can also be used to convert acetylene from crushed calcium carbide powder in conjunction with an existing dry acetylene generator. The generated crude acetylene gas can be directly combined with the gas generated by the main acetylene generator for processing. The reaction of the acetylene generator produces dry and single crude acetylene gas, which is convenient for subsequent processing and recycling of impurity elements. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1 It is a structural schematic diagram of the acetylene generator of the present invention.

[0017] Figure 2 It is a structural schematic diagram of the acetylene production device of the present invention.

[0018] Figure 3 It is a schematic diagram of arranging a selenium iron remover between two-stage cyclone separators in the present invention.

[0019] The markings in the figure are: 1- calcium carbide powder silo, 2- buffer silo, 3- acetylene generator, 4- cyclone separation equipment, 5- bag dust collector, 6- crude acetylene gas cabinet, 7- steam generator, 8- pressure swing adsorption equipment, 9- acetylene purification device, 10- acetylene storage cabinet, 11- pellet machine, 12- calcium hydroxide warehouse, 13- hot gas main, 14- crude acetylene fan, 15- selenium iron remover, 16- heating jacket, 17- insulation layer, 18- ash carrying fan, 19- purification air duct, 20- calcium carbide raw material silo, 21- grinding equipment, 3 1-premixing device, 32-feed control valve, 33-Venturi mixer, 34-exhaust smoothing pipe, 41-primary cyclone separator, 42-secondary cyclone separator, 301-first mixing zone, 302-second mixing zone, 331-first raw material inlet, 332-second raw material inlet, 311-first powder inlet, 312-first gas inlet, 341-heat carrier gas inlet, 342-product outlet, 343-second heat carrier gas inlet, 344-sedimentation section, 401-first ash cleaning valve, 402-second ash cleaning valve. DETAILED DESCRIPTION

[0020] The present invention will be further described below with reference to the accompanying drawings and examples.

[0021] like Figure 1 As shown, the acetylene generator of the present invention includes a Venturi mixer 33, which is provided with a first raw material inlet 331 arranged in the radial direction and a second raw material inlet 332 arranged in the axial direction. It is characterized in that: the first raw material inlet 331 is connected to the premixing device 31, the premixing device 31 is provided with a first powder inlet 311, a first gas inlet 312 and a first mixing zone 301, the mixing pipe section of the Venturi mixer 33 is the second mixing zone 302, the outlet end of the mixing pipe section is connected to the pipe wall opening of a tail gas smoothing pipe 34, one end of the tail gas smoothing pipe 34 is provided with a heat carrier gas interface 341, and the other end of the tail gas smoothing pipe is a product outlet 342.

[0022] When the generator is in use, nanometer-scale calcium carbide powder with a particle size diameter of 50nm to 10000nm is used as the first powder, and the gas generated in the reaction is recycled as a carrier gas for the calcium carbide powder after gas-solid separation. It enters the premixing device 31 from the first gas inlet, and steam is added to the Venturi mixer 33 as the second raw material. The calcium carbide powder dispersed by the gas is also added to the Venturi mixer 33, mixed with the steam to react and release heat, generating crude acetylene gas and calcium hydroxide powder, and the reaction is further completed in the tail gas smoothing pipe 34.

[0023] Through calculation, the overall heat released by the reaction exceeds the heat generated by the same mass of reaction water being converted from room temperature to water vapor. Therefore, using the heat generated by the chemical reaction itself to generate steam as raw material can ensure the continuous progress of the reaction. Since the heat emitted will cause the temperature of the mixing zone to rise to above 200°C, hot gas is introduced into the tail gas smoothing pipe to take away the heat released by the reaction to reduce the occurrence of side reactions, and the reaction temperature is regulated to keep the temperature relatively constant during the reaction to ensure the smoothness and safety of the reaction.

[0024] Since the reaction is completed in the present invention, compared with the conventional dry acetylene reactor, the mass ratio of added water to calcium carbide can be reduced, the reaction surface area is multiplied, and the reaction environment temperature is increased, so that the main reaction can be completed quickly; the two raw materials of the main reaction are one in gas phase and the other is powder after gas dispersion, which has good uniformity and dispersibility, so the reaction system can be simplified. A fixed reactor is used, and the reaction process is monitored and adjusted by the two key factors of pressure and temperature. The use of the above-mentioned reaction device simplifies the reaction process control, facilitates the realization of DCS automatic control, and at the same time, facilitates production capacity regulation.

[0025] Because the reaction is more complete, the calcium carbide consumption and water consumption in the acetylene generation process can be reduced, the reaction degassing rate can be increased, and the yield of acetylene from the calcium carbide method can be increased, which is conducive to the miniaturization and simplification of the reactor; due to the simplification of the acetylene generation device, the production capacity impact and potential safety problems caused by equipment maintenance are reduced.

[0026] The premixing device 31 also adopts a Venturi mixer, with the axial inlet of the Venturi mixer being the first powder inlet 311, and the radial inlet of the Venturi mixer being the first gas inlet 312. The above structure can evenly mix the calcium carbide powder and the carrier gas. The mixture of the carrier gas and the calcium carbide powder enters the Venturi mixer 33 through the first raw material inlet 331, and can be more evenly mixed with the steam to react, thereby promoting the improvement of the reaction completeness. The exhaust smoothing pipe 34 is arranged perpendicular to the axis of the Venturi mixer 33.

[0027] A feed control valve 32 is provided between the premixing device 31 and the first raw material inlet 331 to facilitate the control of the reaction process and abnormal situation control.

[0028] like Figure 1 and Figure 2As shown, a second heat carrier gas interface 343 is provided on the tail gas smoothing pipe 34. Both the heat carrier gas interface 341 and the second heat carrier gas interface 343 are connected to the heat carrier gas main pipe 13. The product outlet 342 of the tail gas smoothing pipe 34 is connected to the inlet of the tail gas separation device. The tail gas separation device includes a gas outlet and a solid outlet. The gas outlet is connected to the air inlet of the heat carrier gas main pipe 13. In other words, the heat carrier gas and the carrier gas of the acetylene generator in the present invention are both derived from the gas after gas-solid separation of the reaction products, and no other impurities are introduced. It is recommended that the heat carrier gas comes from the crude acetylene gas that has been heat exchanged and cooled in the steam generator 7, and the carrier gas comes from the crude acetylene gas that has not been heat exchanged and cooled. The carrier gas can be used to preheat the calcium carbide powder. A plurality of second heat carrier gas interfaces 343 can be arranged at intervals along the tail gas smoothing pipe 34, which can be put into use when necessary to further achieve temperature control. It can also be used to introduce steam to complete the flushing and regeneration of the reactor, and together with the backflushing process, troubleshoot the reactor.

[0029] The acetylene production device of the present invention includes an acetylene generating device, which adopts the aforementioned acetylene generator. The first powder inlet 311 is connected to the calcium carbide powder silo 1, and the second raw material inlet 332 is connected to the steam outlet of the steam generator 7.

[0030] Example: like Figure 1 、 Figure 2 、 Figure 3 As shown, a certain acetylene production system includes a calcium carbide powder silo 1, a buffer silo 2, an acetylene generator 3 of the present invention, a cyclone separation device 4, a bag dust collector 5, a crude acetylene gas tank 6, a crude acetylene blower 14, a steam generator 7, a pressure swing adsorption device 8, an acetylene purification device 9, and an acetylene storage cabinet 10, wherein the steam generator 7 adopts an array-type tube-and-tube evaporator arranged at the periphery of the connection area between the mixing pipe section of the acetylene generator 3 and the tail gas smoothing pipe 34, which can utilize the reaction radiation heat, and the high-temperature medium of the array-type tube-and-tube evaporator adopts the crude acetylene gas from the gas outlet of the tail gas smoothing pipe 34 to reuse the reaction heat to achieve a self-sustaining reaction, and the low-temperature medium adopts pure water. After the pure water is heated, steam is generated as the raw material of the acetylene generator 3 and is introduced from the second raw material port to avoid premature contact with the first raw material and no other impurities are introduced.

[0031] Since the steam addition amount can be controlled relatively accurately during the reaction, the steam content in the reaction product can be controlled to a relatively low level. The cyclone separation equipment 4 can be used to perform gas-solid separation on the reaction product at the outlet of the tail gas smoothing pipe 34. After separation, the solid outlet of the cyclone separation equipment 4 is connected to the pelletizer 11, and the pelletizer 11 is used to extrude the dry calcium carbide slag particles. The acetylene gas contained in the solid product can be fully recovered, thereby reducing the waste of acetylene gas and reducing the safety risk at the finished product slag bin.

[0032] The cyclone separation device 4 includes a primary cyclone separator 41 and a secondary cyclone separator 42. A ferroselenium remover 15 is provided in the pipeline between the two cyclone separators to recover ferroselenium impurities contained in the solid reaction product, thereby enhancing separation efficiency and improving the purity of the calcium hydroxide powder product. Acetylene gas remaining adsorbed by the solid after cyclone separation and sedimentation is further squeezed out by a bag filter 5, ensuring that a safe nano-calcium hydroxide product is obtained from the device. The finished product is then sent to a calcium hydroxide warehouse 12 for storage.

[0033] The high-temperature medium outlet of the steam generator 7 is crude acetylene gas after heat exchange. The activated carbon in the pressure swing adsorption device 8 adsorbs the phosphine contained in the gas. Because the crude acetylene gas in the present invention has a low moisture content and a high phosphine content, adsorption can achieve significant phosphorus and sulfur recovery, reducing environmental pollution. A portion of the crude acetylene gas after heat exchange can also be diverted to enter the heat carrier gas main pipe 13. After control by a control valve, it can be sent to the acetylene generator 3 as carrier gas to the premixing device 31 for powder dispersion and mixing, or as heat carrier gas to enter the tail gas leveling pipe 34 through the heat carrier gas inlet 341 for reaction temperature control. A second heat carrier gas inlet 343 is located at the settling section 344 at the tail of the tail gas leveling pipe 4 to backflush the tail gas leveling pipe 4.

[0034] After the majority of phosphine has been removed by adsorption, the gas enters the acetylene purification device 9. The acetylene purification device 9 can adopt existing technology, for example, including at least one group of sodium hydroxide solution absorption towers, one group of sodium hypochlorite solution absorption towers, or one group of concentrated sulfuric acid absorption towers to purify the gas and obtain acetylene gas with qualified moisture content and impurity gas content, which is then sent to the acetylene storage cabinet 10 for standby use.

[0035] Specifically, the nano-scale calcium carbide powder of the present invention is obtained by crushing external calcium carbide into particles with a diameter of 5 mm in a step-by-step manner and storing it in a calcium carbide raw material bin 20. The powder is then processed into nano-scale calcium carbide powder with a particle size of 50 nm to 10,000 nm using a grinding device 21, such as a dedicated Raymond mill or a dedicated circulating airflow pulverizer. The powder is then stored in a sufficiently safe calcium carbide powder bin 1 for future use. During use, the powder is metered into a buffer bin 2 through the hopper below the calcium carbide powder bin 1, and the amount of raw material steam is adjusted according to the amount added.

[0036] The acetylene production apparatus of this embodiment operates as follows: pure water is heated to steam by a steam generator 7 and then enters the second raw material inlet 332 of the acetylene generator 3. A portion of the crude acetylene gas introduced from the crude acetylene gas tank 6 via the crude acetylene blower 14 is separated and used for mixing in the first mixing zone 301, following the changes in the steam dosage. This portion, referred to as carrier gas, is then propelled from the first gas inlet 312 to the venturi mixer 33 via the first raw material inlet 331 from the premixing device 31. In the second mixing zone 302, a highly exothermic reaction occurs, with the coexistence of two primary gases, acetylene gas and water vapor, and two primary solids, calcium carbide powder particles and nano-calcium hydroxide powder particles. Temperature and pressure are monitored at the second raw material inlet 332 and the outlet of the crude acetylene blower 14, and a regulating valve is used to control the steam dosage and carrier gas dosage. A housing temperature measuring point is provided outside the main heat release area where the heating jacket 16 is located to indirectly determine the mixing operation state of the reaction generator and implement interlock protection.

[0037] After a brief transition, the two gases and the two granular powders are subjected to pressure from the pipe end and rush into the tail airflow and powder leveling area, namely the tail gas leveling pipe 4, where they are mixed with a large amount of dust-free acetylene gas introduced by the crude acetylene blower 14. This part of the acetylene gas entering the tail gas leveling pipe 4 is collectively referred to as heat carrier gas. The heat carrier gas is mainly concentrated near the heat carrier inlet 341 to disperse the reaction heat concentration area. After being lengthened and lifted to a certain height through the tail gas leveling pipe 4, it turns downward and enters the primary cyclone separator 41. A manual air valve is provided immediately at the inlet of the primary cyclone separator 41. This section of the tail gas leveling pipe 34 is called the sedimentation section 344 of the tail gas leveling pipe. A second heat carrier inlet 343 is provided within the sedimentation section 344 to adjust the temperature and backblow the entire tail gas leveling pipe 34. Before entering the primary cyclone separator 41, a thermometer is used to monitor the operation of the reaction, a pressure gauge is used to monitor the vacuum extraction of the crude acetylene gas tank 6 and the crude acetylene blower 14, and a highly sensitive moisture monitor is used to interlock the adjustment of the steam addition amount.

[0038] like Figure 3 As shown, after the primary cyclone separator 41 separates most of the dust, the gas is transported to the secondary cyclone separator 42 for further gas-solid separation. The dust separated by the primary cyclone separator 41 is transported along the powder descending pipe provided with the first cleaning valve 401 and the second cleaning valve 402. In the powder descending pipe between the two, a hollow self-cooling iron-selenium remover 15 and its curved pipe structure are used to adsorb and enrich particles with larger particle size, larger mass and magnetic properties. Part of the attracted iron-selenium and large dust particles are temporarily stored in the iron-selenium remover 15, and are replaced regularly and then processed separately. The nano calcium hydroxide after removing impurities enters the secondary cyclone separator 42.

[0039] like Figure 3As shown, the secondary cyclone separator 42 is transferred by the powder hopper feeder of a common pneumatic conveying device and is fed by the circulating air provided by the ash-carrying fan 18 as the separation power. A spray water nozzle is installed on the top of the secondary cyclone separator 42, into which mist water at room temperature is added to entrain the reactant nanoparticles into granules and agglomerates, causing them to quickly settle to the bottom of the cyclone separator. After falling into the star-shaped discharger at the lower end, the powder agglomerates and the powder from the bag filter 5 enter the pelletizer 11 together. At this time, the added mist water partially vaporizes and absorbs the heat brought by the solid material. The ash-carrying air and the small amount of steam generated, plus the product acetylene, are extracted by the ash-carrying fan 18, and after pre-cooling treatment, they are circulated back to the powder hopper feeder of the secondary cyclone separator 42 for use as circulating air.

[0040] After a small amount of ash-carrying air has gone through the above-mentioned pre-cooling process, a very small portion is separated and introduced into the settling section of the generator tail gas leveling pipe for recycling. The pressure and gas output of this small amount of ash-carrying air are adjusted to make the circulation balanced.

[0041] After primary settling and purification, the gas in the primary cyclone separator 41 is connected to the dust removal air duct 12 through the air outlet. Temperature measurement and control are used to maintain a high temperature above 125°C to prevent water vapor condensation. The manual air valve arranged here opens, allowing the dust-laden crude acetylene gas to enter the bag filter 5 for physical dust removal. The dust-removed crude acetylene gas enters the approximately 500m³ crude acetylene gas tank 6. The bag filter 5 can use pressure differential sensing, automatic vibration and backflushing control to prevent excessive accumulation of nano-calcium hydroxide dust from affecting the pressure difference between the two ends of the exhaust and the filtering and dust removal effect.

[0042] Crude acetylene blower 14 extracts and transports the gas from one end of the crude acetylene tank 6. The hot crude acetylene gas first enters the subsequent array-type tube evaporator, or steam generator 7. Most of the gas, after cooling to approximately 115°C, returns to the reactor for use as heat carrier gas in the tail gas leveling pipe 34. A small portion of the gas is further cooled in the steam generator 7 before entering the purge air duct 19. The crude acetylene tank 14 contains high levels of phosphine and hydrogen sulfide impurities, necessitating the installation of sufficient external toxic and combustible gas detectors, connected to a flare via an emergency evacuation line. In the event of an abnormality, the flare can be used to rapidly evacuate and combust the gas for disposal.

[0043] The steam outlet of the array-type shell-and-tube evaporator uses a contraction hole to ensure constant pressure within each tube. The individual tube outlet acts as a pressure cooker lid. The lower section of all the tubular evaporators is connected together to ensure that the water temperature rises uniformly to around 100°C. Its overall appearance is similar to a vertically arranged shell-and-tube heat exchanger. When used in series, the crude acetylene gas used for purification can be cooled to a temperature close to the inlet water temperature before entering the purification air duct 19. Alternatively, a dedicated tube-sheet heat exchanger can be used to complete the final cooling process of the crude acetylene gas.

[0044] The low-temperature crude acetylene gas obtained in the purified air duct 19 enters the pressure swing adsorption unit 8, where the modified activated carbon utilizes pressure swing adsorption to remove large amounts of phosphine gas. After removal, the phosphine content is reduced to a level comparable to that of existing dry acetylene processes. Acetylene purification equipment 9 then purifies the gas using alkaline solution, recycled sodium hypochlorite solution, and concentrated sulfuric acid, producing acetylene gas with very low moisture and impurity content, which serves as feed gas for the VCM reactor. The consumption of this operation is comparable to that of other dry acetylene processes.

[0045] The apparatus of this embodiment is further described as follows: The buffer bin 2 in the aforementioned process equipment is a specially designed structure that allows direct heating of the buffer bin 2 and the materials therein using crude acetylene gas or a heat carrier gas, ensuring a temperature of approximately 100°C to ensure smooth reaction progress. Insulation layers 17 are installed at appropriate locations on the primary cyclone separator 41, crude acetylene gas holder 14, array-type tube-and-tube evaporator, and tail gas leveling pipe 34 or connecting pipelines to ensure that the system temperature drops within an appropriate range, ensuring that the reaction can proceed thermally self-sustainingly and produce some steam as a by-product.

Claims

1. An acetylene generator, comprising a venturi mixer (33), the venturi mixer (33) being provided with a first raw material inlet (331) arranged in a radial direction and a second raw material inlet (332) arranged in an axial direction, wherein: The first raw material inlet (331) is connected to the premixing device (31), and the premixing device (31) is provided with a first powder inlet (311), a first gas inlet (312) and a first mixing zone (301). The mixing pipe section of the venturi mixer (33) is the second mixing zone (302), and the outlet end of the mixing pipe section is connected to the pipe wall opening of a tail gas smoothing pipe (34). One end of the tail gas smoothing pipe (34) is provided with a heat carrier gas interface (341), and the other end of the tail gas smoothing pipe is a product outlet (342).

2. The acetylene generator according to claim 1, wherein: The premixing device (31) also uses a Venturi mixer, with the axial inlet of the Venturi mixer serving as the first powder inlet (311) and the radial inlet of the Venturi mixer serving as the first gas inlet (312).

3. The acetylene generator according to claim 1 or 2, characterized in that: A feed control valve (32) is provided between the premixing device (31) and the first raw material inlet (331).

4. The acetylene generator according to claim 1 or 2, characterized in that: A second heat carrier gas interface (343) is further provided on the tail gas smoothing pipe (34), and the heat carrier gas interface (341) and the second heat carrier gas interface (343) are both connected to the heat carrier gas main pipe (13).

5. The acetylene generator according to claim 4, characterized in that: The product outlet (342) of the tail gas leveling pipe (34) is connected to the inlet of the tail gas separation device. The tail gas separation device includes a gas outlet and a solid outlet. The gas outlet is connected to the gas inlet end of the heat carrier gas main pipe (13).

6. Acetylene production equipment, including an acetylene generator, characterized by: The acetylene generating device adopts the acetylene generator described in any one of claims 1 to 5 above, the first powder inlet (311) is connected to the calcium carbide powder silo (1), the second raw material inlet (332) is connected to the steam outlet of the steam generator (7), the high-temperature medium of the steam generator (7) adopts the crude acetylene gas from the gas outlet of the tail gas smoothing pipe (34), and the low-temperature medium adopts pure water.

7. The acetylene production device according to claim 6, characterized in that: A heating jacket (16) is arranged outside the connection area between the mixing pipe section of the acetylene generator and the tail gas smoothing pipe (34), the steam outlet of the steam generator (7) is connected to the medium inlet of the heating jacket (16), and the medium outlet of the heating jacket (16) is connected to the second raw material inlet (332).

8. The acetylene production device according to claim 7, characterized in that: A cyclone separation device (4), a bag filter (5), a crude acetylene gas holder (6) and a crude acetylene blower (14) are sequentially connected between the product outlet (342) of the tail gas leveling pipe (34) and the high-temperature medium inlet of the steam generator (7), and the solid outlet of the cyclone separation device (4) is connected to the pelletizer (11).

9. The acetylene production device according to claim 8, characterized in that: The cyclone separation device (4) comprises a primary cyclone separator (41) and a secondary cyclone separator (42), and a selenium iron remover (15) is provided in the pipeline between the two cyclone separators.

10. The acetylene production device according to claim 6, characterized in that: The high-temperature medium of the steam generator (7) is provided with two outlets with different temperatures, wherein the outlet with the higher temperature is connected to the heat-carrying gas interface (341) of the tail gas leveling pipe (34), and the outlet with the lower temperature is connected to the pressure swing adsorption device (8) and the acetylene purification device (9) in sequence.

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