Acetone synthesis device

Abstract

The utility model relates to the technical field of fine chemical synthesis equipment, in particular to an acetone continuous synthesis device. The device comprises a raw material preparation unit, a reaction unit and a post-treatment separation unit, the raw material preparation unit is connected with the reaction unit through a pipeline, and the reaction unit is connected with the post-treatment separation unit through a pipeline; the raw material preparation unit comprises a pure water raw material tank, an acetylene raw material tank and an acetylene buffer tank group; a bottom discharge hole of the pure water raw material tank is simultaneously connected with a top material inlet and a bottom material inlet of the reaction unit through pipelines respectively; and the post-treatment separation unit comprises a condensing tower, a liquid product receiving tank and a rectification separation tower. According to the utility model, multi-layer area structures such as material gasification premixing, multi-stage catalytic reaction, gas-liquid heat exchange and the like are arranged in the tower type reaction unit, so that timely transfer and effective utilization of reaction heat can be realized.

Description

Technical Field

[0001] This utility model relates to the field of fine chemical synthesis equipment technology, and in particular to a continuous acetone synthesis apparatus. Background Art

[0002] Acetone, as an important organic solvent and chemical reaction intermediate, has wide applications in chemical, pharmaceutical, and coating industries. There are more than ten industrial methods for producing acetone, with the acetylene hydration method being one of the earliest researched and industrially implemented. This process involves a catalytic reaction of acetylene and water vapor at approximately 400°C under conditions of a large excess of water vapor to produce acetone. This process is strongly exothermic, and from both thermodynamic and kinetic perspectives, selecting suitable reaction equipment has always been a key issue restricting the production of acetone using the acetylene hydration method.

[0003] The design of reaction equipment must not only meet the requirements of sufficient contact area and time for material conversion, but also address the timely transfer and effective utilization of the heat released from the reaction system. Utility Model Content

[0004] To address the aforementioned problem, this invention provides a continuous acetone synthesis apparatus.

[0005] In order to achieve the above purpose, the utility model adopts the following technical solutions:

[0006] An acetone synthesis apparatus includes a raw material preparation unit, a reaction unit, and a post-processing separation unit; the raw material preparation unit is connected to the reaction unit via a pipeline, and the reaction unit is connected to the post-processing separation unit via a pipeline.

[0007] The raw material preparation unit includes a pure water raw material tank, an acetylene raw material tank, and an acetylene buffer tank group; the bottom outlet of the pure water raw material tank is simultaneously connected to the top material inlet and the bottom material inlet of the reaction unit through pipelines, wherein the pipeline connected to the top material inlet is connected in series with a control valve and a mass flow meter, and the pipeline connected to the bottom inlet is simultaneously connected in series with a gasification preheater, an electromagnetic control valve iii, and a volumetric flow meter b.

[0008] The post-processing separation unit includes a condenser, a liquid product receiving tank, and a distillation separation tower. The material inlet of the condenser is connected to the material outlet at the top of the reaction unit via a pipeline, and a control valve is connected in series on the pipeline. The material outlet at the bottom of the condenser is connected to the material inlet at the top of the liquid product receiving tank via a pipeline, and the material outlet at the bottom of the liquid product receiving tank is connected to the side feed inlet at the bottom of the distillation separation tower via a pipeline, and a control valve and a transfer pump are connected in series on the pipeline.

[0009] According to the provided acetone synthesis apparatus, the reaction unit is a tower reactor or a multi-stage batch reactor connected in series.

[0010] According to the provided acetone synthesis apparatus, the reaction unit is provided from bottom to top as a material gasification premixing zone, a multi-stage catalytic reaction zone, and a material heat exchange zone with a multi-stage bubbling unit.

[0011] According to the provided acetone synthesis apparatus, the multi-stage bubbling unit is a plate with a concave-convex structure, and has multiple layers with staggered distribution between the upper and lower layers.

[0012] According to the provided acetone synthesis apparatus, the reaction zone of the reaction unit is composed of n-stage catalyst-filled fixed beds, and there is an interlayer between each stage of catalyst-filled fixed beds, wherein n≥3.

[0013] According to the provided acetone synthesis apparatus, a liquid atomizing dispersion disk is provided at the material inlet at the top of the reaction unit, and a temperature sensor is provided in the upper part of the multi-stage catalytic reaction zone.

[0014] According to the provided acetone synthesis apparatus, a PLC automatic interlocking device is provided between the temperature sensor and the material vaporization disc in the reaction unit: the temperature sensor is set to the minimum temperature T0 for the material vaporization disc to operate, while the maximum temperature T is set simultaneously. t The material gasification disc is closed at that time.

[0015] According to the provided acetone synthesis apparatus, the bottom outlet of the distillation separation tower is connected to the material inlet on the side wall of the material heat exchange zone of the reaction unit via a pipeline;

[0016] According to the provided acetone synthesis apparatus, the top outlet of the distillation separation column is connected to the lower material inlet on the side wall of the reaction unit via a pipeline.

[0017] Compared with the prior art, the present invention has the following advantages:

[0018] By adopting a multi-layered structure in the tower reaction unit, including material gasification premixing, multi-stage catalytic reaction, and gas-liquid heat exchange, it is beneficial to realize the timely transfer and effective utilization of reaction heat.

[0019] By using a PLC automatic interlocking device installed between the temperature sensor in the multi-stage catalytic reaction zone of the reaction unit and the gasification disc in the material gasification premixing zone, the operation of the material gasification disc can be automatically turned on or off as the temperature T in the reaction zone changes.

[0020] By connecting the post-processing separation unit and the reaction unit through pipelines, the recycling of the separated substances can be achieved.

[0021] This utility model device has a simple structure, a high degree of automation, and is conducive to continuous operation, greatly improving equipment utilization and reaction efficiency, making it suitable for industrial applications. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is a schematic diagram of the overall structure of the utility model;

[0023] Figure 2 This is a schematic cross-sectional view of the reaction tower of this utility model.

[0024] Attached reference numerals: 1. Reaction unit; 101. Material gasification premixing zone; 102. Multi-stage catalytic reaction zone; 103. Material heat exchange zone; 104. Atomizing dispersion plate; 105. Bubbling unit; 106. Top material inlet of reaction unit; 107. Bottom material inlet of reaction unit; 108. Upper material inlet on side wall; 109. Top material outlet of reaction unit; 110. Lower material inlet on side wall; 111. Temperature sensor; 112. Gasification heating plate; 2. Acetylene feed tank; 3. Distillation separation tower; 301. Bottom inlet of separation tower. 302. Feed inlet at the bottom side of the separation tower; 303. Feed outlet at the middle and upper part of the separation tower; 304. Feed outlet at the top of the separation tower; 4. Pure water raw material tank; 401. Feed outlet at the bottom of the raw material tank; 5. Acetylene vaporization buffer tank; 6. Condensation tower; 7. Liquid product receiving tank; 701. Material inlet at the top of the receiving tank; 702. Material outlet at the bottom of the receiving tank; 8. Vaporization preheater; 9. Liquid product transfer pump; 10. Distillation liquid transfer pump; a. Acetylene gas volume flow meter V2; b. Hot water flow meter V1; i-vii. Solenoid valve. Implementation Method

[0025] To better illustrate the beneficial effects of this utility model, a tower-type reaction unit will be used as an example below, and the following detailed description will be provided in conjunction with the accompanying drawings and specific embodiments.

[0026] This utility model relates to an acetone synthesis apparatus, comprising a raw material preparation unit, a reaction unit, and a post-treatment separation unit, as well as related flow meters, transfer pumps, and several valves. The reaction unit is connected to the raw material preparation unit and the post-treatment separation unit via pipelines.

[0027] Specifically, such as Figure 1 As shown, the raw material preparation unit consists of a pure water raw material tank 4, an acetylene storage tank 2, and an acetylene gas buffer tank 5.

[0028] There are multiple sets of acetylene storage tanks 2 arranged side by side. Valves are installed on the pipes connected to the lower outlets of the tanks 2. The pipes connected to the outlets of the multiple sets of acetylene storage tanks 2 converge and connect to the acetylene gas buffer tank 5. A solenoid valve i is installed on the convergence pipe. The gas outlet of the acetylene gas buffer tank 5 is connected to the reaction unit via a pipe. A control valve and a volumetric flow meter V2 are connected in series on this pipe.

[0029] The bottom outlet 401 of the pure water raw material tank 4 is connected to the top material inlet 106 and the bottom material inlet 107 of the reaction unit via pipelines. The pipeline connected to the top material inlet 106 is connected in series with a control valve and a mass flow meter, while the pipeline connected to the bottom inlet 107 is connected in series with a gasification preheater 8, an electromagnetic control valve iii, and a volumetric flow meter V1b. This pipeline intersects with the outlet pipe of the acetylene gas buffer tank 5 and ultimately connects to the bottom inlet 107 of the reaction unit.

[0030] Reaction unit such as Figure 2 As shown, this is a tower-type reaction unit, which, from bottom to top, includes a material gasification premixing zone 101, a multi-stage catalytic reaction zone 102, and a material heat exchange zone 103 equipped with a multi-stage bubbling unit 105. The reaction unit also includes a material heating and gasification plate 112 in the material gasification premixing zone 101, a liquid material atomizing and dispersing plate 104 between the top of the material heat exchange zone 103 and the material inlet 106 at the top of the reaction unit, and a temperature sensor 111 in the upper part of the multi-stage catalytic reaction zone.

[0031] The reaction unit is also equipped with a top material inlet 106, a bottom material inlet 107, a bottom material inlet 108 for the exchange zone, a top material outlet 109, and an upper material inlet and a lower material inlet on the side wall of the multi-stage reaction zone.

[0032] In this device, the multi-stage catalytic reaction zone of the reaction unit is composed of n-stage catalyst-filled fixed beds, and there are interlayer buffer zones between each stage of catalyst-filled fixed beds, and n≥3.

[0033] Specifically, a PLC automatic interlock device is installed between the temperature sensor 111 and the material heating and vaporization plate 112 in the reaction unit: when the reaction zone temperature T ≤ the minimum temperature T0 of the preset reaction temperature range, the material vaporization plate is activated by controlling the opening button to enter the heating and vaporization working state; simultaneously, when the reaction zone temperature T > the maximum temperature T0 of the preset reaction temperature range, the device is activated by controlling the material vaporization plate opening button to enter the heating and vaporization working state. t When the time is right, the material gasification disc button will automatically turn off to end the gasification process.

[0034] Specifically, the catalyst filling the multi-stage catalytic reaction zone in this device is a zinc oxide dispersion with a particle size D < 50 nm.

[0035] The post-processing separation unit consists of a condenser tower 6, a liquid product receiving tank 7, and a distillation separation tower 3. Specifically: the material inlet of the condenser tower 6 is connected to the top material outlet 109 of the reaction unit via a pipeline, with a control valve connected in series on the pipeline; the bottom material outlet of the condenser tower 6 is connected to the top material inlet 701 of the liquid product receiving tank 7 via a pipeline; and the bottom material outlet 702 of the liquid product receiving tank 7 is connected to the bottom side feed inlet 302 of the distillation separation tower 3 via a pipeline, with relevant valves and a transfer pump 9 connected in series on the pipeline.

[0036] Furthermore, the bottom outlet 301 and top outlet 304 of the distillation separation tower 3 are respectively connected to the side wall material inlet 108 of the material heat exchange zone 103 of the reaction unit and the side wall material inlet 110 of the multi-stage reaction zone 102 through pipelines.

[0037] The working principle of this invention is as follows: All valves at the bottom outlet of the pure water raw material tank and the top material inlet of the reaction tower are kept closed, while all valves along the material inlet route at the bottom of the reaction tower are kept open. The pure water discharged from the pure water tank is preheated to a temperature >90℃ by a gasification preheater, and the flow rate of the hot pure water is controlled at V1. Simultaneously, the raw material acetylene flows through a buffer tank, and its flow rate is controlled at V2. The preheated pure water and acetylene gas enter the material mixing and preheating zone through the bottom material inlet of the reaction tower. After being heated, gasified, and mixed, they rise into the 4-6 stage catalytic reaction zone filled with zinc chloride dispersion for reaction. The volume ratio of water vapor to acetylene gas in the mixed gas is V. C2H2 V H2O Maintain the reaction ratio within the range of 1:10~15, keeping the reaction system temperature t>380. Once the reaction begins, the heat generated by the reaction causes the system temperature to gradually rise. When the system temperature rises to 420~450℃, close the valves at the bottom outlet of the pure water raw material tank and the bottom material inlet of the reaction tower, and open the valves at the bottom outlet of the pure water raw material tank and the top material inlet of the reaction tower. This allows the pure water entering the reaction unit through the top material inlet of the reaction tower to be atomized by the atomizing dispersion plate and then exchanged with the high-temperature mixture from the multi-stage catalytic reaction unit in a countercurrent heat exchange at the multi-stage bubbling unit. The high-temperature water-gas mixture generated by the heat exchange enters the reaction zone, while the low-temperature mixture containing the products acetone, carbon dioxide, and hydrogen, the intermediate acetaldehyde, and some water vapor enters the cooling tower from the top material outlet of the reaction unit for cooling.

[0038] The inlet and outlet temperatures of the cooling medium in the cooling tower are <20℃. After cooling, carbon dioxide and hydrogen gases are separated and enter the gas collection tank from the top of the cooling tower. Acetone, intermediates, and some water vapor are cooled and enter the liquid product receiving tank from the bottom of the cooling tower. The mixture entering the liquid product receiving tank enters the distillation separation tower for further distillation separation. The product acetone is collected from the upper outlet of the separation tower and enters the product storage tank. Low-boiling-point materials are circulated into the multi-stage catalytic reaction zone through the top outlet of the tower, while the main components of high-boiling-point materials are circulated into the bottom inlet of the heat exchange zone through the bottom outlet of the separation tower to participate in the reaction.

[0039] When the temperature of the multi-stage catalytic reaction system is lower than the set minimum reaction temperature limit, the system will activate the interlock device to keep the vaporization plate in a heated state; when the temperature of the multi-stage catalytic reaction system is higher than the set maximum reaction temperature limit, the system will automatically shut off the heating of the vaporization plate through the interlock device, thereby realizing the automatic exchange and recycling of the system's reaction heat.

[0040] This invention employs a multi-layered structure within a tower-type reaction unit, incorporating material gasification premixing, multi-stage catalytic reaction, and gas-liquid heat exchange zones, facilitating timely transfer and effective utilization of reaction heat. Temperature sensors are installed in the multi-stage catalytic reaction zone of the reaction unit, and a PLC automatic interlock device is established between the sensor and the gasification disc in the material gasification premixing zone. This allows for the automatic opening or closing of the material gasification disc based on changes in the reaction zone temperature (T). Furthermore, the invention enables the recycling of separated substances through pipeline connections between the post-treatment separation unit and the reaction unit.

[0041] The above is a preferred embodiment of the present invention. For ordinary technicians in this field, based on the teachings of the present invention, without departing from the principles and spirit of the present invention, changes, modifications, replacements and variations made to the implementation methods are still within the scope of protection of the present invention.

[0042] The above is a preferred embodiment of the present invention. For ordinary technicians in this field, based on the teachings of the present invention, without departing from the principles and spirit of the present invention, changes, modifications, replacements and variations made to the implementation methods are still within the scope of protection of the present invention.

Claims

1. An acetone synthesis device, characterized in that: It includes a raw material configuration unit, a reaction unit and a post-processing separation unit; the raw material configuration unit is connected to the reaction unit through a pipeline, and the reaction unit is connected to the post-processing separation unit through a pipeline; The raw material configuration unit comprises a pure water raw material tank (4), an acetylene raw material tank (2) and an acetylene buffer tank (5); the bottom discharge port (401) of the pure water raw material tank is respectively connected to the top material inlet (106) and the bottom material inlet (107) of the reaction unit through pipelines, wherein the pipeline connected to the top material inlet (106) is connected in series with a control valve and a mass flow meter, and the pipeline connected to the bottom material inlet (107) is connected in series with a gasification preheater (8), a solenoid valve and a volume flow meter; The post-processing separation unit comprises a condensation tower (6), a liquid product receiving tank (7) and a distillation separation tower (3), wherein the material inlet of the condensation tower is connected to the material outlet (109) at the top of the reaction unit via a pipeline, and a control valve is connected in series on the pipeline; The material outlet at the bottom of the condensation tower is connected to the material inlet (701) at the top of the liquid product receiving tank via a pipeline, and the material outlet (702) at the bottom of the liquid product receiving tank is connected to the side feed inlet (302) at the bottom of the distillation separation tower (3) via a pipeline, and a control valve and a material transfer pump are simultaneously connected in series on the pipeline.

2. An acetone synthesis device according to claim 1, characterized in that: The reaction unit is a tower reactor or a multi-stage kettle reactor connected in series head to tail.

3. An acetone synthesis device according to claim 1 or 2, characterized in that: The reaction unit is provided with a material gasification premixing zone (101), a multi-stage catalytic reaction zone (102), and a material heat exchange zone (103) provided with a multi-stage bubbling unit (105) in sequence from bottom to top.

4. An acetone synthesis device according to claim 3, characterized in that: The multi-stage bubbling unit (105) is in the shape of a plate with a concave-convex structure and is provided with multiple layers, with the upper and lower layers being staggered.

5. An acetone synthesis device according to claim 1 or 2, characterized in that: The reaction zone of the reaction unit is composed of n-level catalyst-filled fixed beds, and interlayers are arranged between the catalyst-filled fixed beds of each level, wherein n≥3.

6. An acetone synthesis device according to claim 3, characterized in that: A liquid atomizing dispersion plate (104) is provided at the material inlet (106) at the top of the reaction unit, and a temperature sensor (111) is provided at the upper middle portion of the multi-stage catalytic reaction zone (102).

7. An acetone synthesis device according to claim 6, characterized in that: A PLC automatic interlocking device is provided between the temperature sensor (111) and the material vaporization disk (112) in the reaction unit: when the temperature sensor (111) sets a minimum temperature limit T0, the material vaporization disk operates; and when the temperature limit Tt is reached, the material vaporization disk is closed.

8. An acetone synthesis device according to claim 7, characterized in that: The separation tower bottom discharge port (301) provided in the distillation separation tower (3) is connected to the side wall material upper inlet (108) provided in the material heat exchange zone of the reaction unit through a pipeline, and a distillation material transfer pump (10) is provided on the pipeline.

9. An acetone synthesis device according to claim 7, characterized in that: The separation tower top material outlet (304) provided in the rectification separation tower (3) is connected to the side wall material lower inlet (110) of the reaction unit via a pipeline.

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