CN213803579U - Novel adipic acid reaction device - Google Patents
Novel adipic acid reaction device Download PDFInfo
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- CN213803579U CN213803579U CN202022923276.0U CN202022923276U CN213803579U CN 213803579 U CN213803579 U CN 213803579U CN 202022923276 U CN202022923276 U CN 202022923276U CN 213803579 U CN213803579 U CN 213803579U
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Abstract
The utility model belongs to the technical field of chemical production equipment, concretely relates to new-type adipic acid reaction unit. The device comprises a tower reactor and a condensate circulating system. The tower reactor is internally divided into a reaction zone, a curing zone and a liquid storage zone from top to bottom in sequence; a plurality of tower trays are fixedly arranged in the reaction zone, and the tower trays divide the reaction zone into a plurality of reaction chambers; the curing area is positioned below the reaction area, a plurality of tower trays are also arranged in the curing area, and the tower trays divide the curing area into a plurality of curing chambers; the liquid storage area is positioned at the bottom of the tower reactor; the condensate circulating system comprises a vacuum pump, a condenser, a condensation liquid storage tank and a connecting pipeline; the tower reactor and the condensate circulating system are provided with a plurality of on-line detection devices. Compared with the existing equipment with multiple reactors connected in series, the device has the advantages of small occupied area, simple operation process, more uniform material liquid mixing and higher reaction efficiency.
Description
Technical Field
The utility model belongs to the technical field of chemical production equipment, concretely relates to new-type adipic acid reaction unit.
Background
At present, in the process of producing adipic acid by using nitric acid and cyclohexanol or KA oil (a mixture of cyclohexanol and ketone), a mode of connecting 4-6 reactors in series is commonly used: excessive nitric acid enters from the first reactor, cyclohexanol is sequentially added into each reactor, all the reactors are connected through overflow pipelines, and the overflow of the former reactor enters the latter reactor. The cyclohexanol and nitric acid oxidation reaction is an exothermic reaction, so that the reaction yield is improved at low temperature; however, if the reaction temperature is lower than 60 ℃, nitrous acid serving as a reaction initiator is difficult to fully play, and is easy to accumulate, so that potential production hazards exist. In addition, because the concentration of the adipic acid in each reactor is gradually increased along with the reaction, in order to control the crystallization rate of the adipic acid, the temperature of each reactor needs to be guaranteed to be controlled within the range of the crystallization point of the adipic acid in the reactor to be higher than 2 ℃, and the temperature needs to be separately regulated and controlled, so that the control steps of the actual production are complicated and error is easy to make.
CN102417662A discloses a liquid acid type trioxymethylene production process method and an extraction reaction tower, wherein an extracting agent inlet is arranged at the lower end of a tower body, a formaldehyde solution inlet and a liquid acid inlet are arranged at the upper part of the tower body, and a multi-stage extraction reaction chamber is arranged in the tower body from bottom to top, so that a device which needs to be subjected to multi-stage reaction kettle backflow in the prior art is improved into a counter-flow multi-stage layered reaction, the formaldehyde conversion rate is improved, and the polymerization and extraction separation steps of trioxymethylene are combined into one. The device provides a concept of integrating multiple stages of reactions into one reactor, but the device is not suitable for adipic acid production, such as recycling of byproduct nitrous gas in the adipic acid production, control of crystallization temperature and the like, and cannot be used for solving the problems.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem that adipic acid production technology operation is complicated among the prior art, the control degree of difficulty is high to and nitrous gas accumulation, the utility model aims at providing a novel adipic acid apparatus for producing, utilize the device to produce adipic acid easy operation, reaction evenly, the accessory substance is few, and the equipment investment is little. Based on a general inventive concept, the utility model also comprises a process for synthesizing adipic acid by using the device.
In order to realize the technical purpose, the utility model discloses a following technical scheme:
a novel adipic acid reaction device comprises a tower reactor and a condensate circulating system;
a gas phase pipeline is arranged at the top of the tower reactor and is communicated with the condensate circulating system; a discharge hole is formed in the bottom of the tower reactor, and a main discharge pipe is connected to the discharge hole; a feed liquid backflow pipeline is arranged on the main discharge pipe, and the end part of the feed liquid backflow pipeline, which is far away from the main discharge pipe, extends into the tower reactor; a discharge water pump is arranged on a main discharge pipe between the feed liquid reflux pipeline and the tower reactor to provide power for feed liquid output;
the tower reactor is internally divided into a reaction zone, a curing zone and a liquid storage zone from top to bottom in sequence;
a plurality of tower trays are fixedly arranged in the reaction zone; one end of the tower tray is provided with a liquid receiving disc, and the other end of the tower tray is provided with a down-extending down-flow plate; the tower tray divides the reaction area into a plurality of reaction chambers, and the down-flow plates in the adjacent reaction chambers are arranged oppositely; a first feeding pipe and a first condensing pipe are arranged in each reaction chamber; the first feeding pipe is communicated with a main feeding pipe arranged outside the tower reactor; the first condenser pipe is communicated with a water circulation system arranged outside the tower reactor; a second feeding pipe is also arranged in the reaction chamber at the top of the reaction zone;
the curing zone is positioned below the reaction zone; a plurality of tower trays are also arranged in the curing area, and the tower tray structure of the curing area is the same as that of the reaction area; the tower tray divides the curing area into a plurality of curing chambers, each curing chamber is internally provided with a first heating pipe, and the first heating pipes are communicated with a heat supply pipeline arranged outside the tower reactor;
the liquid storage area is positioned at the bottom of the tower reactor; a second heating pipe is arranged in the liquid storage area; the second heating pipe is communicated with a heating device arranged outside the tower reactor; an air inlet pipe is also arranged in the liquid storage area; the air inlet pipe is positioned below the second heating pipe;
the condensate circulating system comprises a vacuum pump, a condenser, a condensation liquid storage tank and a connecting pipeline; a gas phase pipeline at the top of the tower reactor is communicated with a vacuum pump through a condenser, and gas in the tower reactor enters the vacuum pump after being cooled by the condenser; the condenser is communicated with the condensation liquid storage tank through a liquid discharge pipe, and condensate in the condenser enters the condensation liquid storage tank through the liquid discharge pipe; a main liquid outlet pipe is arranged at the bottom of the condensation liquid storage tank, and a liquid outlet pump is arranged on the main liquid outlet pipe; a liquid return pipe is arranged on the main liquid outlet pipe, and the end part of the liquid return pipe far away from the main liquid outlet pipe extends into the tower reactor;
a plurality of on-line detection devices are arranged on the tower reactor and the condensate circulating system; the online monitoring device comprises a pressure gauge, a thermometer, a flowmeter and a liquid level meter.
Preferably, a first feed liquid reflux pipeline and a second feed liquid reflux pipeline are arranged on the main discharge pipe; the end part of the first feed liquid backflow pipeline, which is far away from the main discharge pipe, extends into a liquid storage area of the tower reactor; the end part of the second feed liquid reflux pipeline far away from the main discharge pipe extends into the top of the reaction zone of the tower reactor.
Preferably, a crystallization point measuring branch is arranged on the tower reactor; one end of the crystallization point measuring branch is communicated with the first feed liquid return pipeline or the second feed liquid return pipeline; the other end of the crystallization point measuring branch extends into a liquid storage area of the tower reactor; and a detection device for determining the crystallization point is arranged on the crystallization point measurement branch.
Preferably, a plurality of feed ports are formed in the side walls of the first feed pipe and the second feed pipe.
Preferably, the horizontal position of the liquid receiving plate is lower than that of the tower tray, so that a liquid receiving groove for containing reaction liquid is formed above the liquid receiving plate; the bottom end of the down-flow plate on the upper tower tray extends into the liquid receiving tank, so that the bottom of the down-flow plate is positioned below the reaction liquid level in the reaction process; and an overflow plate extending upwards is arranged at the joint of the downcomer plate and the tray.
Further preferably, the tray is provided with sieve holes.
Preferably, the condensation liquid storage tank is filled with liquid with a certain volume; the end part of the liquid discharge pipe extends into the condensation liquid storage tank and below the liquid level surface, and the negative pressure environment of the condenser during working is ensured through liquid seal.
Preferably, a vertical partition plate is arranged at the bottom of the condensation liquid storage tank, the condensation liquid storage tank is divided into a left cavity and a right cavity by the vertical partition plate, and the tops of the left cavity and the right cavity are communicated; the end part of the liquid discharge pipe extends into the position below the liquid level of the left chamber; the total liquid outlet pipe is positioned at the bottom of the right cavity.
The utility model discloses compare with current adipic acid reaction unit, its beneficial effect is:
1) the occupied area is small, the operation process is simple, and compared with equipment with a plurality of reactors connected in series, the tower reactor has the advantages that the feed liquid is mixed more uniformly, and the reaction efficiency is higher;
2) the air inlet pipe is arranged at the bottom of the tower reactor, so that on one hand, the solution at the bottom of the reactor can be stirred to be fully and uniformly mixed; on the other hand, the nitrous gas in the reaction liquid is carried away in the gas rising process, when the nitrous gas rises to the top of the tower reactor, the nitrous gas is cooled and oxidized into nitric acid which falls into the reaction liquid below again to participate in the reaction, so that the content of the nitrous gas in the reaction liquid is reduced;
3) by arranging a condensate circulating system, the gas pumped out from the tower reactor is condensed and liquefied and then is sent back to the tower reactor again, so that the material loss caused by volatilization of moisture and nitric acid is avoided, and a closed cycle is formed in a reaction device; meanwhile, the condensate flows back to lower the temperature at the top of the tower reactor, so that the nitrous gases are ensured to be condensed and fall into the reaction liquid below.
Drawings
FIG. 1 is a schematic structural view of an adipic acid reaction apparatus according to the present invention;
FIG. 2 is a schematic diagram of the distribution of a first feed tube and a first condensing coil in the reaction chamber of FIG. 1;
FIG. 3 is a schematic view of the distribution of a first heating coil within the maturation chamber of FIG. 1;
FIG. 4 is a schematic view of the arrangement of the feeding holes on the first feeding tube.
Detailed Description
The present invention will be described in further detail with reference to specific embodiments. The specific technical solution in the embodiment is only the best implementation manner of the present invention, and is not a limitation on the implementable range of the present invention; changes or adjustments of the relative relationships in the embodiments are also considered to be within the scope of the present invention without substantial technical changes.
Example 1
A novel adipic acid reaction device is shown in figures 1-4 and comprises a tower reactor and a condensate circulation system.
The tower reactor is a cylindrical reaction tower; the tower reactor is internally divided into a reaction zone 1, a curing zone 2 and a liquid storage zone 3 from top to bottom in sequence;
the reaction zone 1 is located in the upper part of the column reactor. A plurality of tower trays 4 are arranged in the reaction zone 1, and the tower trays 4 divide the interior of the reaction zone 1 into a plurality of reaction chambers. A plurality of 8-20mm ventilation sieve holes are formed in the tower tray 4, the peripheral shape of the tower tray 4 is matched with the shape of the inner wall of the tower reactor, and the tower tray 4 is fixedly connected with the inner wall of the tower reactor through a fixing frame or a bolt. The left and right sides of the tray 4 are respectively provided with a liquid receiving tray 41 and a down-flow plate 42. The liquid receiving disc 41 is semi-arc-shaped, the arc-shaped edge of the liquid receiving disc 41 is fixedly connected with the inner wall of the tower reactor, and the straight edge of the liquid receiving disc 41 is fixedly connected with the tower tray; the liquid receiving tray 41 is horizontally positioned lower than the tray 4, so that a liquid receiving groove for containing the reaction liquid is formed on the liquid receiving tray 41. The down-flow plate 42 is arranged in the vertical direction; the top of the down-flow plate 42 is fixedly connected with the tray 4; two side walls of the down-flow plate 42 are fixedly connected with the inner wall of the tower reactor; the bottom of the downcomer 42 is not connected to the inner wall of the tower reactor, so that a channel for the reaction liquid to fall down is formed between the downcomer 42 and the inner wall of the tower reactor. The connection of the downcomer 42 to the tray 4 is provided with a vertically upward weir (not shown). The down-flow plates 42 of the adjacent reaction chambers are oppositely arranged, and the bottom of the down-flow plate 42 of the previous stage extends into the liquid receiving groove of the tray of the next stage, so that the bottom of the down-flow plate 42 is ensured to be positioned below the reaction liquid level in the reaction process;
in order to ensure uniform feeding, four first feeding pipes 11 are horizontally arranged in each reaction chamber; the left and right sides of the first feeding pipe 11 are provided with a plurality of feeding holes 111 with the aperture of 2mm along the axial direction. The end part of the first feeding pipe 11, which is positioned outside the tower reactor, is connected through a connecting pipe and is communicated with a main feeding pipe 12 arranged outside; the total feeding pipe 12 is connected with a cyclohexanol storing device 5. A second feeding pipe 13 is arranged in the reaction chamber at the top of the tower reactor; the second feeding pipe 13 is arranged in parallel with the first feeding pipe 11, and the second feeding pipe 13 is positioned above the first feeding pipe 11. A plurality of liquid inlet holes are also formed in the left side and the right side of the second feeding pipe 13. The end of the second feeding pipe 13 far away from the tower reactor is connected with a nitric acid storage device 6 arranged outside. The connecting pipe of the first feeding pipe 11 and the second feeding pipe are both provided with a regulating valve and a flowmeter, and the feeding flow of the cyclohexanol and the nitric acid is controlled by a manual operation or a feedback signal of a controller;
a set of first condensing coils 14 is provided in each reaction chamber. The water inlet end of the first condensing coil 14 is connected with a condensed water inlet main pipe 15, and the water outlet end of the first condensing coil 14 is connected with a condensed water outlet main pipe 16; a water return pipeline can be arranged between the condensed water inlet main pipe 15 and the condensed water outlet main pipe 16, so that the circulating cooling of the condensed water is ensured. Two thermometers are arranged in each reaction chamber, and the reaction of the layer is automatically or manually stopped through signal feedback when 2 temperatures show inconsistency. And the double-temperature-point control is arranged, so that production accidents caused by failure of temperature control in the reaction chamber can be prevented. In this embodiment, the top of the overflow plate on the tray 4 is higher than the horizontal positions of the first condensing coil 14 and the first feeding pipe 11, so that the cyclohexanol directly enters the reaction solution to react with the nitric acid after entering the tower reactor through the first feeding pipe 11. The temperature control range in the reaction zone 1 is 70-88 ℃, and the temperature of each reaction chamber in the reaction zone 1 is gradually increased from top to bottom.
The maturation zone 2 is located below the reaction zone 1. A plurality of trays are arranged in the curing area 2, and the tray structure of the curing area 2 is the same as that of the reaction area 1. The tray divides the curing area 2 into a plurality of curing chambers, and a group of first heating coils 21 are arranged in each curing chamber; the first heating coil 21 is in communication with a heat supply conduit disposed outside the tower reactor. The inlet end of the first heating coil 21 is communicated with a main heating pipe 22 of the heating pipeline; the outlet end of the first heating coil 21 is communicated with a steam condensate return header pipe 23, and the temperature in the curing zone 2 is controlled within the range of 90-110 ℃ through low-pressure steam in the heat supply pipeline.
The liquid storage zone 3 is positioned at the bottom of the tower reactor. A second heating pipe 31 is arranged in the liquid storage area 3; the second heating pipe 31 is communicated with a low-pressure steam generator arranged outside the tower reactor, so that the temperature in the liquid storage area 3 is controlled within the range of 90-130 ℃. An air inlet pipe 32 is arranged below the second heating pipe 31; the end part of the air inlet pipe 32 far away from the tower reactor is connected with an air compressor, a plurality of air inlet holes are formed in the circumferential direction of the side wall of the air inlet pipe 32, and air enters the tower reactor through the air inlet holes; in the gas inlet process, gas uniformly mixes the feed liquid and simultaneously takes away nitrous gas in the feed liquid, oxygen carried in the air reacts with the gaseous nitrous gas at the top of the tower reactor, the nitric acid generated by cold condensation falls into the reaction liquid below to participate in the reaction, and the content of the nitrous gas in the reaction liquid is reduced. The flow meter arranged on the air inlet pipe 32 is adjusted in the production process of adipic acid, so that the air inlet flow is ensured to be 500-1500 NM3In the meantime.
A discharge hole is arranged on the tower reactor at the bottom of the liquid storage zone 3, and a total discharge pipe 7 is connected at the discharge hole. A discharge water pump 71 is arranged on the main discharge pipe 7, and the adipic acid feed liquid is conveyed to a downstream adipic acid crystallization system 101 for crystallization through the discharge water pump 71; the main discharge pipe 7 can also be connected with an adipic acid storage tank for storing feed liquid. A first feed liquid return pipeline 72 and a second feed liquid return pipeline 73 are arranged on the main discharge pipe 7; the end of the first feed liquid return pipeline 72 far away from the main discharge pipe 7 extends into the liquid storage area 3 of the tower reactor; the end of the second feed liquid return line 73 remote from the main outlet pipe 7 projects into the top of the column reactor. The first feed liquid reflux pipeline 72 and the second feed liquid reflux pipeline 73 are arranged, so that the material concentration can be quickly improved when the material concentration at the bottom of the tower at the initial stage of production does not meet the requirement, and the high-temperature feed liquid at the bottom can be conveyed to the top of the reactor in the production process, so that the temperature of the upper tray 4 is quickly improved. In order to dynamically monitor the crystallization point in the tower reactor, a crystallization point measuring branch 33 is arranged on the side wall of the liquid storage area 3, a crystallization point detection device 34 is arranged on the crystallization point measuring branch 33, the crystallization point of the reaction liquid in the liquid storage area is determined through the crystallization point detection device 34, the temperature in the liquid storage area is controlled to be about 2 ℃ higher than the crystallization point, and the crystallization of the feed liquid is avoided. A discharge pipe 75 is arranged on the main discharge pipe 7 and the second feed liquid reflux pipeline 73; the discharge pipe 75 is arranged to discharge after production is finished, so that pipeline blockage is avoided.
The top of the tower reactor is provided with a pressure gauge, the bottom of the tower reactor is provided with a liquid level meter and a thermometer, and the pressure, the height of the feed liquid and the temperature in the reactor are monitored in real time.
The tower reactor is communicated with the condensate circulating system through a gas phase pipeline arranged at the top;
the condensate circulating system comprises a vacuum pump 10, a condenser 8, a condensation liquid storage tank and a connecting pipeline; the tower reactor is communicated with the condenser 8 and the condenser 8 are communicated with the vacuum pump 10 through gas phase pipelines, and gas in the tower reactor is cooled by the condenser 8 and then is pumped out by the vacuum pump 10; a gas phase pipeline between the condenser 8 and the vacuum pump 10 is provided with an adjusting valve and a pressure gauge, so that the pressure control range in the tower reactor in adipic acid production is ensured to be 50-150 KPa; the outlet of the vacuum pump is communicated with a subsequent tail gas treatment system, so that the pumped nitrous gas is thoroughly absorbed and treated;
the condenser 8 is communicated with the condensation liquid storage tank through a liquid discharge pipe 81, and condensate in the condenser 8 enters the condensation liquid storage tank through the liquid discharge pipe 81. The bottom of condensation receiver tank is equipped with vertical baffle 91, and vertical baffle 91 is divided into left cavity 92 and right cavity 93 in with the condensation receiver tank, and the top of left cavity 92 and right cavity 93 is linked together. The left chamber 92 is filled with a liquid at a certain height; the end of the drain 81 extends below the level of the left chamber 92 and provides a liquid seal to ensure a closed environment within the condenser 8. In order to ensure the liquid sealing effect, the height difference from the top end to the bottom end of the liquid discharge pipe 81 is not less than 10 m. When the height of the condensate in the left chamber 92 exceeds the top of the vertical partition 91, the condensate flows into the right chamber 93 and is finally discharged through the main liquid outlet pipe 17 at the bottom of the right chamber 93; and a liquid outlet pump 18 is arranged on the main liquid outlet pipe 17 and provides power for conveying the condensate. In order to ensure that the liquid level in the left chamber 92 meets the liquid seal requirement, a liquid level meter is arranged in the right chamber 93, and the liquid level in the left chamber 92 is ensured to be always at the height of the vertical partition 91 by detecting the liquid level in the right chamber 93. The left and right chambers separated at the bottom are arranged in the condensation liquid storage tank, and the liquid sealing effect can be met by using less liquid. A liquid return pipe 19 is arranged on the main liquid outlet pipe 17, and the end part of the liquid return pipe 19 far away from the main liquid outlet pipe 17 extends into the tower reactor. A bypass branch pipe 191 is arranged between the liquid return pipe 19 and the condensation liquid storage tank, so that the redundant condensate liquid flows back to the condensation liquid storage tank for recycling.
The gas pumped out from the tower reactor is condensed and liquefied by arranging a condensate circulating system and is returned to the tower reactor again, so that the material loss caused by volatilization of moisture and nitric acid is avoided, and closed circulation is formed in a reaction device; meanwhile, the condensate flows back to lower the temperature of the top of the tower reactor, so that the nitrous gas at the top of the tower reactor is oxidized into nitric acid and then condensed and falls into the reaction liquid below.
When the device is used for producing adipic acid, firstly, a flow regulating valve arranged on the second feeding pipe 13 is opened, so that excessive nitric acid enters the tower reactor from the top, and the feeding amount of the nitric acid is controlled to be 60 t/h. When the nitric acid liquid level at the bottom of the tower reactor reaches about 30%, the discharging water pump 71 is started, a valve arranged on the second feed liquid backflow pipeline 73 is opened, the material circulation of the tower reactor is established, and the temperature rise of the upper tower tray 4 is accelerated. High-purity water is supplemented in the condensation liquid storage tank until reaching the detection point of the liquid level meter, the water source 94 is closed, and the condenser 8 is started. And starting the vacuum pump 10, opening a valve on the air pipe 32, and controlling the pressure in the tower reactor to be 50-150 KPa (absolute pressure). Starting a valve on a heat supply pipeline of the curing area 2 and a low-pressure steam generator of the liquid storage area 3, and starting heating; after the temperature of the tower tray in the reaction zone reaches above 60 ℃, opening a valve arranged on the main feeding pipe 12, and sequentially opening a valve on a connecting pipe of the first feeding pipe 13 from bottom to top to flow cyclohexanol from bottom to top; the total cyclohexanol feeding amount was controlled at 7.3 t/h. When cyclohexanol is fed, valves on a condensate water inlet manifold 15 and a condensate water outlet manifold 16 are opened, the temperature of the tower tray in each reaction chamber is controlled within the range of 70-88 ℃ by adjusting an adjusting valve at the water inlet end of a first condensing coil 14, and the temperature of the tower tray in each reaction chamber is ensured to be gradually increased from top to bottom. The temperature in the curing zone 2 is controlled to be 90-110 ℃, and the temperature in the liquid storage zone 3 is controlled to be 90-130 ℃. After the materials circulate for a period of time, the second material liquid backflow pipeline 73 is closed, the liquid discharge pipe is opened at the same time, and the second material liquid backflow pipeline 73 is subjected to back flushing replacement by utilizing the replacement mother liquor, so that pipeline blockage caused by crystallization of residual material liquid is avoided. The first feed liquid reflux pipeline 72 and the second feed liquid reflux pipeline 73 are opened simultaneously, so that the circulation of the feed liquid at the bottom of the tower reactor is established, and the uniform concentration of the feed liquid is ensured; in the circulation process of the feed liquid, the nitrous gas in the reaction feed liquid is brought out through air inlet, the nitrous gas reacts with oxygen carried in the air at the top of the tower reactor to generate nitric acid which falls into the tower plate again, and therefore the content of the nitrous gas in the adipic acid feed liquid is reduced. When the concentration of adipic acid in the feed liquid in the liquid storage zone 3 meets the requirement of a subsequent crystallization separation process, opening a control valve on a main discharge pipe, and feeding the feed liquid with the concentration meeting the requirement to an adipic acid crystallization system 101; the first feeding pipe and the second feeding pipe are continuously fed in the feeding process, so that the continuous production is ensured.
Claims (8)
1. A novel adipic acid reaction device is characterized in that: the device comprises a tower reactor and a condensate circulating system;
a gas phase pipeline is arranged at the top of the tower reactor and is communicated with the condensate circulating system; a discharge hole is formed in the bottom of the tower reactor, and a main discharge pipe is connected to the discharge hole; a feed liquid backflow pipeline is arranged on the main discharge pipe, and the end part of the feed liquid backflow pipeline, which is far away from the main discharge pipe, extends into the tower reactor; a discharge water pump is arranged on a main discharge pipe between the feed liquid reflux pipeline and the tower reactor to provide power for feed liquid output;
the tower reactor is internally divided into a reaction zone, a curing zone and a liquid storage zone from top to bottom in sequence;
a plurality of tower trays are fixedly arranged in the reaction zone; one end of the tower tray is provided with a liquid receiving disc, and the other end of the tower tray is provided with a down-extending down-flow plate; the tower tray divides the reaction area into a plurality of reaction chambers, and the down-flow plates in the adjacent reaction chambers are arranged oppositely; a first feeding pipe and a first condensing pipe are arranged in each reaction chamber; the first feeding pipe is communicated with a main feeding pipe arranged outside the tower reactor; the first condenser pipe is communicated with a water circulation system arranged outside the tower reactor; a second feeding pipe is also arranged in the reaction chamber at the top of the reaction zone;
the curing zone is positioned below the reaction zone; a plurality of tower trays are also arranged in the curing area, and the tower tray structure of the curing area is the same as that of the reaction area; the tower tray divides the curing area into a plurality of curing chambers, each curing chamber is internally provided with a first heating pipe, and the first heating pipes are communicated with a heat supply pipeline arranged outside the tower reactor;
the liquid storage area is positioned at the bottom of the tower reactor; a second heating pipe is arranged in the liquid storage area; the second heating pipe is communicated with a heating device arranged outside the tower reactor; an air inlet pipe is also arranged in the liquid storage area; the air inlet pipe is positioned below the second heating pipe;
the condensate circulating system comprises a vacuum pump, a condenser, a condensation liquid storage tank and a connecting pipeline; a gas phase pipeline at the top of the tower reactor is communicated with a vacuum pump through a condenser, and gas in the tower reactor enters the vacuum pump after being cooled by the condenser; the condenser is communicated with the condensation liquid storage tank through a liquid discharge pipe, and condensate in the condenser enters the condensation liquid storage tank through the liquid discharge pipe; a main liquid outlet pipe is arranged at the bottom of the condensation liquid storage tank, and a liquid outlet pump is arranged on the main liquid outlet pipe; a liquid return pipe is arranged on the main liquid outlet pipe, and the end part of the liquid return pipe far away from the main liquid outlet pipe extends into the tower reactor;
a plurality of on-line detection devices are arranged on the tower reactor and the condensate circulating system; the online monitoring device comprises a pressure gauge, a thermometer, a flowmeter and a liquid level meter.
2. A novel adipic acid reaction apparatus according to claim 1, wherein: a first feed liquid backflow pipeline and a second feed liquid backflow pipeline are arranged on the main discharge pipe; the end part of the first feed liquid backflow pipeline, which is far away from the main discharge pipe, extends into a liquid storage area of the tower reactor; the end part of the second feed liquid reflux pipeline far away from the main discharge pipe extends into the top of the reaction zone of the tower reactor.
3. A novel adipic acid reaction apparatus according to claim 2, wherein: a crystallization point measuring branch is arranged on the tower reactor; one end of the crystallization point measuring branch is communicated with the first feed liquid return pipeline or the second feed liquid return pipeline; the other end of the crystallization point measuring branch extends into a liquid storage area of the tower reactor; and a detection device for determining the crystallization point is arranged on the crystallization point measurement branch.
4. A novel adipic acid reaction apparatus according to claim 1, wherein: a plurality of feed ports are opened to the lateral wall of first inlet pipe and second inlet pipe.
5. A novel adipic acid reaction apparatus according to claim 1, wherein: the horizontal position of the liquid receiving plate is lower than that of the tray, so that a liquid receiving groove for containing reaction liquid is formed above the liquid receiving plate; the bottom end of the down-flow plate on the upper tower tray extends into the liquid receiving tank, so that the bottom of the down-flow plate is positioned below the reaction liquid level in the reaction process; and an overflow plate extending upwards is arranged at the joint of the downcomer plate and the tray.
6. A novel adipic acid reaction apparatus according to any one of claims 1 to 5, wherein: sieve pores are arranged on the tower tray.
7. A novel adipic acid reaction apparatus according to claim 1, wherein: the condensation liquid storage tank is filled with liquid with a certain height; the end part of the liquid discharge pipe extends into the condensation liquid storage tank and below the liquid level surface, and the negative pressure environment of the condenser during working is ensured through liquid seal.
8. A novel adipic acid reaction apparatus according to claim 7, wherein: the bottom of the condensation liquid storage tank is provided with a vertical partition plate, the vertical partition plate divides the condensation liquid storage tank into a left cavity and a right cavity, and the tops of the left cavity and the right cavity are communicated; the end part of the liquid discharge pipe extends into the position below the liquid level of the left chamber; the total liquid outlet pipe is positioned at the bottom of the right cavity.
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| CN202022923276.0U CN213803579U (en) | 2020-12-09 | 2020-12-09 | Novel adipic acid reaction device |
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| CN202022923276.0U CN213803579U (en) | 2020-12-09 | 2020-12-09 | Novel adipic acid reaction device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112239403A (en) * | 2020-12-09 | 2021-01-19 | 河南神马尼龙化工有限责任公司 | Novel adipic acid reaction device and synthesis process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112239403A (en) * | 2020-12-09 | 2021-01-19 | 河南神马尼龙化工有限责任公司 | Novel adipic acid reaction device and synthesis process |
| CN112239403B (en) * | 2020-12-09 | 2023-10-13 | 河南神马尼龙化工有限责任公司 | Adipic acid reaction device and synthesis process |
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