CN210963956U

CN210963956U - Evaporator for NVP continuous crystallization

Info

Publication number: CN210963956U
Application number: CN201921595926.4U
Authority: CN
Inventors: 孙旭东; 张森林; 方鄂
Original assignee: BOAI NKY PHARMACEUTICALS Ltd
Current assignee: Boai Xinkaiyuan Pharmaceutical Co.,Ltd.
Priority date: 2019-09-24
Filing date: 2019-09-24
Publication date: 2020-07-10
Anticipated expiration: 2029-09-24

Abstract

The utility model belongs to the technical field of evaporative crystallization, and discloses an NVP (non-volatile semiconductor) continuous crystallization evaporator, which comprises a heater, an evaporation chamber, a separation chamber, a stirring box and a preheating box, wherein the stirring box and the preheating box are communicated up and down; a snake-shaped heating pipe is arranged outside the stirring box; a preheating interlayer is arranged outside the preheating box; the evaporation chamber is communicated with the separation chamber up and down, an inlet of the serpentine heating pipe is communicated with a steam discharge pipe of the evaporation chamber, the preheating interlayer is communicated with a medium outlet of the heater, a discharge hole of the preheating box is respectively communicated with a reflux port of the separation chamber and a feed pipe of the heater, and a discharge pipe of the heater is communicated with a material inlet of the evaporation chamber. The utility model improves the utilization rate of the reaction raw materials and reduces the waste; continuous circulation evaporation crystallization improves the reaction yield and the crystallization quality; the heat in the reaction production is secondarily utilized, so that the heat waste is reduced, the energy utilization rate is improved, the use amount of cooling water is reduced, and the production cost is reduced; the evaporation crystallization is continuous and uninterrupted, and the production efficiency is improved.

Description

Evaporator for NVP continuous crystallization

Technical Field

The utility model relates to an evaporation crystallization technical field especially relates to an NVP is evaporimeter for continuous crystallization.

Background

Polymers of N-vinylpyrrolidone (NVP for short) are widely used in the fields of medicines, daily chemicals, foods and the like. In general, 2-pyrrolidone and acetylene are subjected to vinylation reaction under the action of a catalyst in industry to produce N-vinylpyrrolidone, and a reaction mixture contains the unreacted 2-pyrrolidone and acetylene besides the N-vinylpyrrolidone, so that waste of production raw materials is caused; the produced N-vinyl pyrrolidone contains impurities such as a catalyst, and the purity of the N-vinyl pyrrolidone is different due to different applications, and the N-vinyl pyrrolidone is generally purified by adopting an evaporator evaporation crystallization mode, but the process steps are various, and in the evaporation crystallization process of the evaporator, steam from a heater and an evaporation chamber still has high temperature and is directly cooled, so that the waste of heat is caused, a large amount of cooling water is consumed in the cooling process, and the production cost is increased. Therefore, an evaporator for NVP continuous crystallization, which has the advantages of more complete reaction, full utilization of raw materials and resource and energy conservation, is urgently needed.

SUMMERY OF THE UTILITY MODEL

The utility model aims at overcoming current technical problem, provide an evaporimeter is used in continuous crystallization of NVP.

In order to achieve the purpose, the utility model is implemented according to the following technical scheme:

an evaporator for NVP continuous crystallization comprises a heater, an evaporation chamber and a separation chamber; the device also comprises a stirring box and a preheating box;

a stirring paddle is arranged in the stirring box, and a serpentine heating pipe is fixedly arranged on the outer wall of the stirring box; a feed inlet of the preheating box is communicated with a discharge outlet of the stirring box, and a preheating interlayer is fixedly arranged on the outer wall of the preheating box; the heater comprises a heater body, a steam heating layer is arranged outside the heater body, a medium inlet and a medium outlet are arranged on the steam heating layer, a feeding hole of the heater body is fixedly connected with a feeding pipe, and a conveying pump is arranged on the feeding pipe; the evaporation chamber is fixedly arranged above the separation chamber and is communicated with the separation chamber up and down, a steam discharge pipe is arranged at the top end of the evaporation chamber, a material inlet is arranged at the bottom of the evaporation chamber, a crystal outlet is arranged at the lower part of the separation chamber, and a reflux port is arranged at the upper part of the separation chamber;

the import and the steam discharge pipe intercommunication of serpentine heating pipe, preheat the intermediate layer import and pass through the medium export intercommunication of pipe and steam heating layer, the discharge gate of preheating cabinet passes through pipeline one and the backward flow mouth intercommunication of separation chamber, the middle part of pipeline one and the inlet pipe intercommunication of heater body, the discharging pipe of heater body passes through pipeline two and the material import intercommunication of evaporating chamber.

The utility model discloses in the collaborative relationship between each subassembly as follows: the stirring box fully stirs the reaction mixture to promote the unreacted raw materials to fully react again, and the serpentine heating pipe on the outer wall of the stirring box plays a role in primary preheating of the reaction mixture, so that the secondary reaction of the unreacted raw materials is facilitated, the utilization rate of the reaction raw materials is improved, and the waste is reduced; the mixed liquid fully reacted enters the preheating box, the heat-conducting medium in the preheating interlayer preheats the mixed liquid for the second time, then the mixed liquid enters the heater for full heating and then enters the evaporation chamber for evaporation, the saturated solution enters the separation chamber, the qualified crystals after the crystallization of the saturated solute are discharged from the crystal outlet, the micro crystals and the mother liquid flow into the preheating box from the backflow port and enter the heater again with the mixed liquid in the preheating box for repeated evaporation and crystallization, so that the qualified crystals are prevented from being generated, and the reaction yield and the crystallization quality are improved. In the process, hot steam exhausted from a steam exhaust pipe of the evaporation chamber is introduced into the serpentine heating pipe, and secondary utilization is carried out on the heat; the heat conducting medium in the preheating interlayer is hot steam exhausted from the outlet of the steam heating layer of the heater, the heat is secondarily utilized, the energy utilization rate is improved, and when the hot gas exhausted from the outlet of the serpentine heating pipe and the outlet of the preheating interlayer is cooled, the use amount of cooling water is reduced due to the heat reutilization, and the production cost is reduced.

Preferably, the discharge port of the stirring box is provided with a switch valve, and after the reaction mixture in the stirring box is fully mixed and reacted, the switch valve is opened to enable the reaction mixture to flow into the preheating box, so that the unreacted raw materials in the reaction mixture are ensured to be as little as possible, and the crystallization precision is improved.

Preferably, a filter screen is arranged at the discharge port of the stirring box, and insoluble substances in the reaction mixture can be filtered at the filter screen, so that the crystallization precision is improved.

The utility model discloses in still including other subassemblies that can make the device normal use, it all belongs to the conventional selection in this field, like the control assembly of stirring rake, the control assembly that steam heating zone hot steam circulation flows, the subassembly that evaporating chamber and separation chamber normally worked etc.. In addition, the device or the assembly which is not limited in the utility model adopts the conventional means in the field, for example, the equipment such as the evaporation chamber, the separation chamber, the transfer pump and the like adopts the conventional structure.

The utility model discloses a theory of operation: the stirring box fully stirs the reaction mixture to promote the unreacted raw materials to fully react again, and the serpentine heating pipe on the outer wall of the stirring box plays a role in primary preheating of the reaction mixture, so that the secondary reaction of the unreacted raw materials is facilitated, the utilization rate of the reaction raw materials is improved, and the waste is reduced; the mixed liquid fully reacted enters the preheating box, the heat-conducting medium in the preheating interlayer preheats the mixed liquid for the second time, then the mixed liquid enters the heater for full heating and then enters the evaporation chamber for evaporation, the saturated solution enters the separation chamber, the qualified crystals after the crystallization of the saturated solute are discharged from the crystal outlet, the micro crystals and the mother liquid flow into the preheating box from the backflow port and enter the heater again with the mixed liquid in the preheating box for repeated evaporation and crystallization, so that the qualified crystals are prevented from being generated, and the reaction yield and the crystallization quality are improved. In the whole process, according to the crystallization progress, the reaction mixture can be continuously added into the stirring box, so that evaporative crystallization is continuous and uninterrupted, and the production efficiency is improved; hot steam discharged from a steam discharge pipe of the evaporation chamber is introduced into the serpentine heating pipe, and the heat is secondarily utilized; the heat conducting medium in the preheating interlayer is hot steam exhausted from the outlet of the steam heating layer of the heater, the heat is secondarily utilized, the energy utilization rate is improved, and when the hot gas exhausted from the outlet of the serpentine heating pipe and the outlet of the preheating interlayer is cooled, the use amount of cooling water is reduced due to the heat reutilization, and the production cost is reduced.

The utility model discloses following beneficial effect has been reached: the method is favorable for fully reacting the unreacted raw materials again, improves the utilization rate of the reaction raw materials and reduces waste; continuous circulation evaporation crystallization improves the reaction yield and the crystallization quality; the heat in the reaction production is secondarily utilized, so that the heat waste is reduced, the energy utilization rate is improved, and the use amount of cooling water is reduced and the production cost is reduced due to the reutilization of the heat; according to the crystallization progress, the reaction mixture can be continuously added into the stirring box, so that evaporative crystallization is continuous and uninterrupted, and the production efficiency is improved; the whole structure is simple and the maintenance is convenient.

Drawings

Fig. 1 is a schematic structural diagram of the present invention.

In the figure: 1. a separation chamber; 2. an evaporation chamber; 3. a heater; 4. a stirring box; 5. a stirring paddle; 6. a feeding port; 7. a preheating box; 8. preheating the interlayer; 9. preheating an outlet of the interlayer; 10. a conduit; 11. a first pipeline; 12. a feed pipe; 13. a delivery pump; 14. a serpentine heating tube; 15. a crystal outlet; 16. a second pipeline; 17. A steam discharge pipe; 18. a media inlet.

Detailed Description

The invention will be further described with reference to the drawings and specific embodiments, illustrative embodiments and description of which are provided herein to explain the invention, but not as a limitation thereof.

Example (b):

an evaporator for NVP continuous crystallization shown in fig. 1 comprises a heater 3, an evaporation chamber 2 and a separation chamber 1; the device also comprises a stirring box 4 and a preheating box 7;

a stirring paddle 5 is arranged in the stirring box 4, and a serpentine heating pipe 14 is fixedly arranged on the outer wall of the stirring box 4; a feed inlet of the preheating box 7 is communicated with a discharge outlet of the stirring box 4, and a preheating interlayer 8 is fixedly arranged on the outer wall of the preheating box 7; the heater 3 comprises a heater body, a steam heating layer is arranged outside the heater body, a medium inlet 18 and a medium outlet are arranged on the steam heating layer, a feeding hole of the heater body is fixedly connected with a feeding pipe 12, and a conveying pump 13 is arranged on the feeding pipe 12; the evaporation chamber 2 is fixedly arranged above the separation chamber 1 and is communicated with the separation chamber 1 up and down, a steam discharge pipe 17 is arranged at the top end of the evaporation chamber 2, a material inlet is arranged at the bottom of the evaporation chamber, a crystal outlet 15 is arranged at the lower part of the separation chamber 1, and a reflux port is arranged at the upper part of the separation chamber;

the import and the steam discharge pipe 17 intercommunication of snakelike heating pipe 14, preheat the import of intermediate layer 8 and pass through the medium export intercommunication of pipe 10 with the steam heating layer, the discharge gate of preheating cabinet 7 passes through the backward flow mouth intercommunication of pipeline 11 and separation chamber 1, the middle part of pipeline 11 and the inlet pipe 12 intercommunication of heater body, the discharging pipe of heater body passes through the material import intercommunication of pipeline two 16 and evaporating chamber 2.

The discharge gate department of agitator tank 4 is provided with the ooff valve, and this department sets up and to be able to make it flow in preheating cabinet 7 in opening the ooff valve after the reaction mixture intensive mixing reaction in agitator tank 4, ensures that the unreacted raw materials in the reaction mixture is as little as possible, improves the precision of crystallization.

The discharge gate department of agitator tank 4 is provided with the filter screen, and this department sets up and can filters the insoluble material in the reaction mixture, improves the precision of crystallization.

When the reaction kettle is used, firstly, a reaction mixture is added into the stirring box 4 through the feeding port 6 of the stirring box, the stirring paddle 5 fully stirs the reaction mixture to promote the unreacted raw materials to fully react again, and meanwhile, the snake-shaped heating pipe 14 on the outer wall of the stirring box 4 has a primary preheating effect on the reaction mixture, so that the secondary reaction of the unreacted raw materials is facilitated, the utilization rate of the reaction raw materials is improved, and the waste is reduced; and then opening a switch valve to enable the fully reacted mixed liquid to enter a preheating box 7, preheating the fully reacted mixed liquid for the second time by a heat-conducting medium in a preheating interlayer 8, finally enabling the mixed liquid to enter a heater 3 through a pipeline I11 and a feeding pipe 12, enabling hot steam to enter a steam heating layer from a medium inlet 18 of the steam heating layer, fully heating the mixed liquid in the heater body, enabling the mixed liquid to enter an evaporation chamber 2 through a guide pipe 10 to be evaporated, enabling the evaporated saturated solution to enter a separation chamber 1, discharging qualified crystals after the crystallization of saturated solute from a crystal outlet 15, enabling the micro crystals and mother liquid to flow into the preheating box 7 from a backflow port, enabling the mixed liquid in the preheating box 7 to enter the heater 3 again to repeat the evaporation and crystallization steps to prevent the generation of qualified crystals, and improving the reaction yield and the crystallization quality. In the whole process, according to the crystallization progress, the reaction mixture can be continuously added into the stirring box 4, so that evaporative crystallization is continuous and uninterrupted, and the production efficiency is improved; hot steam discharged from a steam discharge pipe 17 of the evaporation chamber 2 is introduced into the serpentine heating pipe 14, and secondary utilization is carried out on the heat; the heat conducting medium in the preheating interlayer is hot steam exhausted from the steam heating layer outlet of the heater 3, the heat is secondarily utilized, the energy utilization rate is improved, and when the outlet of the serpentine heating pipe 14 and hot gas exhausted from the outlet of the preheating interlayer are cooled, the use amount of cooling water is reduced due to the heat reutilization, and the production cost is reduced.

The technical scheme of the utility model is not limited to the restriction of above-mentioned specific embodiment, all according to the utility model discloses a technical scheme makes technical deformation, all falls into within the protection scope of the utility model.

Claims

1. An evaporator for NVP continuous crystallization comprises a heater, an evaporation chamber and a separation chamber; the method is characterized in that: the device also comprises a stirring box and a preheating box;

2. An evaporator for NVP continuous crystallization according to claim 1, characterized in that: and a switch valve is arranged at the discharge port of the stirring box.

3. An evaporator for NVP continuous crystallization according to claim 2, characterized in that: and a filter screen is arranged at the discharge port of the stirring box.