CN214485756U

CN214485756U - Continuous deamination recovery unit of amino nitrile reaction liquid

Info

Publication number: CN214485756U
Application number: CN202120068082.9U
Authority: CN
Inventors: 王永昌; 李亚飞; 刘顺领; 仝亚飞
Original assignee: Shandong Yisheng Industrial Co ltd
Current assignee: Shandong Yisheng Industrial Co ltd
Priority date: 2021-01-11
Filing date: 2021-01-11
Publication date: 2021-10-26
Anticipated expiration: 2031-01-11

Abstract

The utility model relates to a continuous deamination recovery unit of amino nitrile reaction liquid belongs to the technical field that the chemicals were retrieved. Comprises a primary deamination unit and a secondary deamination unit; the primary deamination unit comprises a primary deamination tower, a primary absorption tower and an ammonia water storage tank I; the primary deamination tower is connected with the primary absorption tower; the bottom of the primary absorption tower is connected with an ammonia water storage tank I; the ammonia water storage tank I is connected with the primary absorption tower; the secondary deamination unit comprises a secondary deamination tower, a secondary absorption tower and an ammonia water storage tank; the secondary deamination tower is connected with the primary deamination tower; the secondary deamination tower is connected with the secondary absorption tower; the bottom of the secondary absorption tower is connected with an ammonia water storage tank II; and the ammonia water storage tank I is connected with the secondary absorption tower. The utility model can separate the high-concentration ammonia gas from the reaction liquid and recover the ammonia gas. The recovered ammonia gas is changed into high-concentration ammonia water which is used as a production material for continuous use, so that the use amount of subsequent acid is reduced, and the production amount of a byproduct ammonium salt is also reduced.

Description

Continuous deamination recovery unit of amino nitrile reaction liquid

Technical Field

The utility model relates to a technical field that chemicals were retrieved, concretely relates to continuous deamination recovery unit of amino nitrile reaction liquid.

Background

Alpha-amino nitrile is an important intermediate for synthesizing various amino acids, and is widely applied to the fields of chemistry, biology, medicine and the like. The Strecker reaction, the most important method for synthesizing alpha-aminonitriles, requires the use of large amounts of ammonia in the synthesis process. After the reaction is finished, the excessive ammonia water can directly carry out the next acidolysis reaction along with the reaction solution, so that the acid consumption is increased during acidolysis. Therefore, it is necessary to recover the ammonia water during the reaction. Most of the existing recovery devices adopt the modes such as stripping, rectification, vacuum, flash evaporation and the like to recover ammonia, but the equipment can only remove low-content ammonia. The use of existing equipment is not conducive to ammonia removal due to the high ammonia content in the Strecker reaction.

SUMMERY OF THE UTILITY MODEL

To the problem that the higher reaction liquid of existing equipment is difficult to carry out ammonia recovery, the utility model provides a continuous deamination recovery unit of amino nitrile reaction liquid to solve above-mentioned problem.

A continuous deamination recovery device for aminonitrile reaction liquid comprises a primary deamination unit and a secondary deamination unit. The primary deamination unit comprises a primary deamination tower, a primary absorption tower, an ammonia water storage tank I and a primary spray pump; the primary deamination tower is connected with the primary absorption tower through a primary vacuum pump; the bottom of the primary absorption tower is connected with an ammonia water storage tank I; the ammonia water storage tank I is connected with the primary absorption tower through a primary spray pump; the secondary deamination unit comprises a secondary deamination tower, a secondary absorption tower, an ammonia water storage tank II and a secondary spray pump; the secondary deamination tower is connected with the primary deamination tower through a primary material transfer pump; the secondary deamination tower is connected with the secondary absorption tower through a secondary vacuum pump; the bottom of the secondary absorption tower is connected with an ammonia water storage tank II; the ammonia water storage tank I is connected with the secondary absorption tower through a secondary spray pump; and the secondary deamination tower is connected with the acidolysis kettle through a secondary material transferring pump.

Preferably, the recovery device further comprises a tail gas absorption unit; the tail gas absorption unit comprises a tail gas absorption tower, an ammonia water storage tank III and a tail gas spray pump; the tail gas absorption tower is respectively connected with the top of the primary absorption tower and the top of the secondary absorption tower; the bottom of the tail gas absorption tower is connected with an ammonia water storage tank III; and the ammonia water storage tank III is connected with the tail gas absorption tower through a tail gas spraying pump.

Preferably, the primary deamination tower is a falling film evaporator; the secondary deamination tower is a falling film evaporator.

Preferably, the primary vacuum pump is one of a screw vacuum pump, a reciprocating vacuum pump, a rotary vane vacuum pump and a roots vacuum pump; the secondary vacuum pump is one of a screw vacuum pump, a reciprocating vacuum pump, a rotary-vane vacuum pump and a Roots vacuum pump.

Preferably, the first-stage deamination tower and the second-stage deamination tower are made of corrosion-resistant materials; the corrosion-resistant material is graphite, silicon carbide, glass lining, glass or fluoroplastic.

Preferably, the vacuum degree of the first-stage deamination tower is less than or equal to-0.085 MPa. Because the ammonia content in the reaction liquid is relatively high after the ammoniation reaction, the most ammonia gas can be separated from the reaction liquid by controlling the vacuum degree to be less than or equal to-0.085 MPa. The ammonia content in the reaction liquid after the primary deamination is reduced to a lower level, so that the difficulty of the secondary deamination is reduced.

Preferably, the vacuum degree of the secondary deamination tower is less than or equal to-0.095 MPa. The content of ammonia in the reaction liquid is low, the vacuum degree is further increased, the separation effect of the ammonia and the reaction liquid can be ensured, and the content of the ammonia in the final material can meet the requirement.

Preferably, the first-stage absorption tower and the second-stage absorption tower are respectively provided with a cooling heat exchange device.

Preferably, the first-stage absorption tower and the second-stage absorption tower are both made of ammonia water-resistant and corrosion-resistant materials, and are selected from one of carbon steel, stainless steel, graphite, glass lining or glass fiber reinforced plastic.

The utility model discloses a theory of operation does: after the ammoniation reaction is finished, reaction liquid enters from the top of the primary deamination tower, forms an extremely thin liquid film under the action of a liquid distributor, flows down along the pipe wall of the primary deamination falling film tower, starts primary deamination, adjusts the feeding amount, maintains the vacuum degree of the primary falling film deamination system above-0.085 MPa, ensures the primary falling film deamination effect, and enables separated ammonia gas to enter a primary absorption tower. The ammonia gas is absorbed by the primary absorption tower through spraying dilute ammonia water, and the ammonia water after absorbing the ammonia gas flows into the ammonia water storage tank I and can be recycled. When the ammonia water reaches a certain concentration, the ammonia water is transferred out and can be used as a production material for continuous use. And the ammonia storage tank I is replaced with new dilute ammonia to absorb ammonia. The working principle of the secondary deamination unit and the tail gas absorption unit is the same as that of the primary deamination unit. And after the secondary deamination is finished, directly transferring the reaction liquid with qualified ammonia content into an acidolysis kettle for subsequent production.

The utility model has the advantages that:

the utility model discloses a continuous deamination is handled, can separate the ammonia and the reaction liquid of the high concentration in the ammoniation reaction liquid to retrieve. The recovered ammonia gas can be dissolved in the absorption liquid to be changed into high-concentration ammonia water to be continuously used as a production material. The utility model discloses can retrieve the ammonia in the ammoniation reaction liquid completely, the quantity of sour when having reduced follow-up acidolysis. Solves the problem that the existing equipment is not easy to recover ammonia from the reaction liquid with higher ammonia content.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without creative efforts.

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

In the figure, 1-a first-stage deamination tower, 2-a first-stage vacuum pump, 3-a first-stage absorption tower, 4-ammonia water storage tank I, 5-a first-stage spray pump, 6-a first-stage material transfer pump, 7-a second-stage deamination tower, 8-a second-stage vacuum pump, 9-a second-stage absorption tower, 10-ammonia water storage tank II, 11-a second-stage spray pump, 12-a second-stage material transfer pump, 13-acidolysis kettle, 14-a tail gas absorption tower, 15-ammonia water storage tank III and 16-a tail gas spray pump.

Detailed Description

In order to make the technical solutions in the present invention better understood, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, but not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts shall belong to the protection scope of the present invention.

Example 1

A continuous deamination recovery device for aminonitrile reaction liquid comprises a primary deamination unit, a secondary deamination unit and a tail gas absorption unit. The primary deamination unit comprises a primary deamination tower 1, a primary absorption tower 3, an ammonia water storage tank I4 and a primary spray pump 5; the primary deamination tower 1 is a falling film evaporator, receives the aminated reaction liquid and is made of graphite; the primary deamination tower 1 is connected with a primary absorption tower 3 through a primary vacuum pump 2; the vacuum degree of the primary deamination tower 1 is less than or equal to-0.085 MPa; the primary vacuum pump 2 is a reciprocating vacuum pump; the first-stage absorption tower 3 is provided with a cooling heat exchange device and is made of stainless steel. The bottom of the primary absorption tower 3 is connected with an ammonia water storage tank I4; the ammonia water storage tank I4 is connected with the primary absorption tower 3 through a primary spray pump 5; the top of the primary absorption tower 3 is connected with a tail gas absorption tower 14; the secondary deamination unit comprises a secondary deamination tower 7, a secondary absorption tower 9, an ammonia water storage tank II 10 and a secondary spray pump 11; the secondary deamination tower 7 is a falling film evaporator and is connected with the primary deamination tower 1 through a primary material transfer pump 6, and the material is graphite; the secondary deamination tower 7 is connected with a secondary absorption tower 9 through a secondary vacuum pump 8; the vacuum degree of the secondary deamination tower 7 is less than or equal to-0.095 MPa; the secondary vacuum pump 8 is a reciprocating vacuum pump; the secondary absorption tower 9 is provided with a cooling heat exchange device and is made of carbon steel; the bottom of the secondary absorption tower 9 is connected with an ammonia water storage tank II 10; the ammonia water storage tank I10 is connected with the secondary absorption tower 9 through a secondary spray pump 11; the top of the secondary absorption tower 9 is connected with a tail gas absorption tower 11; the secondary deamination tower 9 is connected with an acidolysis kettle 13 through a secondary material transfer pump 12; the bottom of the tail gas absorption tower 14 is connected with an ammonia water storage tank III 15; and the ammonia water storage tank III 15 is connected with the tail gas absorption tower 14 through a tail gas spraying pump 16.

Although the present invention has been described in detail by referring to the drawings in conjunction with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and substance of the present invention, and these modifications or substitutions are intended to be within the scope of the present invention/any person skilled in the art can easily conceive of changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.

Claims

1. A continuous deamination recovery device for aminonitrile reaction liquid is characterized by comprising a primary deamination unit and a secondary deamination unit; the primary deamination unit comprises a primary deamination tower, a primary absorption tower, an ammonia water storage tank I and a primary spray pump; the primary deamination tower is connected with the primary absorption tower through a primary vacuum pump; the bottom of the primary absorption tower is connected with an ammonia water storage tank I; the ammonia water storage tank I is connected with the primary absorption tower through a primary spray pump; the secondary deamination unit comprises a secondary deamination tower, a secondary absorption tower, an ammonia water storage tank II and a secondary spray pump; the secondary deamination tower is connected with the primary deamination tower through a primary material transfer pump; the secondary deamination tower is connected with the secondary absorption tower through a secondary vacuum pump; the bottom of the secondary absorption tower is connected with an ammonia water storage tank II; the ammonia water storage tank I is connected with the secondary absorption tower through a secondary spray pump; and the secondary deamination tower is connected with the acidolysis kettle through a secondary material transferring pump.

2. The continuous deamination recovery device of aminonitrile reaction liquid as claimed in claim 1, wherein the recovery device comprises a tail gas absorption unit; the tail gas absorption unit comprises a tail gas absorption tower, an ammonia water storage tank III and a tail gas spray pump; the tail gas absorption tower is respectively connected with the top of the primary absorption tower and the top of the secondary absorption tower; the bottom of the tail gas absorption tower is connected with an ammonia water storage tank III; and the ammonia water storage tank III is connected with the tail gas absorption tower through a tail gas spraying pump.

3. The continuous deamination and recovery device of aminonitrile reaction liquid as claimed in claim 1, wherein the primary deamination tower is a falling film evaporator; the secondary deamination tower is a falling film evaporator.

4. The continuous deamination and recovery device of claim 1, wherein the primary vacuum pump is one of a screw vacuum pump, a reciprocating vacuum pump, a rotary-vane vacuum pump and a roots vacuum pump; the secondary vacuum pump is one of a screw vacuum pump, a reciprocating vacuum pump, a rotary-vane vacuum pump and a Roots vacuum pump.

5. The continuous deamination and recovery device for aminonitrile reaction liquid as claimed in claim 1, wherein the primary deamination tower and the secondary deamination tower are made of corrosion-resistant materials; the corrosion-resistant material is graphite, silicon carbide, glass lining, glass or fluoroplastic.

6. The continuous deamination and recovery device of aminonitrile reaction liquid as claimed in claim 1, wherein the vacuum degree of the primary deamination tower is less than or equal to-0.085 MPa.

7. The continuous deamination and recovery device of aminonitrile reaction liquid as claimed in claim 1, wherein the vacuum degree of the secondary deamination tower is less than or equal to-0.095 MPa.

8. The continuous deamination and recovery device of aminonitrile reaction liquid as claimed in claim 1, wherein the primary absorption tower and the secondary absorption tower are respectively provided with a cooling and heat exchange device.

9. The continuous deamination and recovery device of aminonitrile reaction liquid as claimed in claim 1, wherein the first-stage absorption tower and the second-stage absorption tower are made of ammonia water resistant and corrosion resistant materials, and the materials are selected from one of carbon steel, stainless steel, graphite, glass lining and glass fiber reinforced plastic.