阅读说明：本技术 一种dmac反应液的蒸馏处理方法 (Distillation treatment method of DMAC reaction solution ) 是由 夏家信 许传久 杨涛 于 2020-11-30 设计创作，主要内容包括：本发明涉及一种DMAC反应液的蒸馏处理方法,其特征在于：(1)将反应液中转槽内的物料以0.5-0.8m～3/h的量送入蒸馏釜,控制蒸馏釜内压力为-88～-96KPa、温度为100～110℃,蒸馏釜顶出来的气相冷凝后进入接收槽,当接受槽内有30%～40%体积的液位时,将液体送至DMF精馏塔,蒸馏釜内釜底液采出送去残液槽,作为燃料处理。本发明优点：设备投资费用低、工艺简单、操作方便；降低能耗、设备的磨损,减少了操作的劳动量；节约了成本,保护了环境；可有效减少DMAC反应液中的糖渣、二甲胺盐、醋酸盐等,管线的清理周期由原来的1-2天/次延长至10-15天/次。(The invention relates to a distillation treatment method of DMAC reaction liquid, which is characterized by comprising the following steps: (1) the material in the reaction liquid transfer tank is added by 0.5-0.8m 3 The volume of the liquid/h is sent into a distillation kettle, the pressure in the distillation kettle is controlled to be-88 to-96 KPa, the temperature is controlled to be 100 to 110 ℃, the gas phase from the top of the distillation kettle is condensed and then enters a receiving tank, when the receiving tank has a liquid level of 30 to 40 percent of the volume, the liquid is sent into a DMF (dimethyl formamide) rectifying tower, and the bottom liquid in the distillation kettle is extracted and sent to a residual liquid tank to be treated as fuel. The invention has the advantages that: the equipment investment cost is low, the process is simple, and the operation is convenient; the energy consumption and the equipment abrasion are reduced, and the operation labor amount is reduced; the cost is saved, and the environment is protected; sugar residue, dimethylamine salt, acetate and the like in the DMAC reaction solution can be effectively reduced, and the cleaning period of the pipeline is prolonged from 1-2 days to 10-15 days.)

1. A distillation treatment method of DMAC reaction liquid comprises a primary separation tower, a dimethylamine absorption tank, a dimethylamine reactor, a reaction liquid transfer tank, a residual liquid tank, a DMF (dimethyl formamide) rectifying tower, a DMAC rectifying tower and a DMAC finished product tank; the method is characterized in that: the reaction liquid transfer tank is connected with the distillation still through a pipeline, the outlet at the top of the distillation still is connected with the receiving tank through a pipeline, the receiving tank is connected with the DMF rectifying tower through a pipeline, and the outlet at the bottom of the distillation tower is connected with the raffinate tank through a pipeline;

the method comprises the following steps:

(1) the material in the reaction liquid transfer tank is added by 0.5-0.8m³The volume of the liquid/h is sent into a distillation kettle, the pressure in the distillation kettle is controlled to be-88 to-96 KPa, the temperature is controlled to be 100 to 110 ℃, the gas phase from the top of the distillation kettle is condensed and then enters a receiving tank, when the receiving tank has a liquid level of 30 to 40 percent of the volume, the liquid is sent into a DMF rectification tower, and the bottom liquid in the distillation kettle is extracted and sent to a residual liquid tank.

Technical Field

The invention belongs to a method for treating a solvent in a sucralose production process, and relates to a method for distilling a DMAC reaction solution.

Background

In the sucralose DMF recovery working section, after purification and recovery, residual acidic DMF is difficult to treat, and in order to save energy, protect environment and protect environment, the currently adopted method is mainly as follows: firstly, primarily extracting DMF in acidic DMF, then reacting dimethylamine with acetic acid in the acidic DMF to generate DMAC, further extracting the DMF in the acidic DMF completely, and finally rectifying the DMAC. Under the process flow, the DMAC reaction solution contains 3-5% of sucralose sugar residues, 5-8% of dimethylamine salt, 2-5% of acetate, 45-55% of DMAC and the like, which easily causes blockage of a DMF rectifying tower, a DMAC rectifying tower and pipelines of a rear section, influences the continuity and stability of production and is not beneficial to the smooth production.

Disclosure of Invention

The invention aims to solve the problems that DMAC residual liquid contains sucralose sugar residues, dimethylamine salt, acetate and other substances, so that subsequent pipelines are easily blocked and production is influenced under the existing process conditions, and provides a distillation treatment method for DMAC reaction liquid.

In order to achieve the purpose, the technical scheme adopted by the invention is as follows:

a distillation treatment method of DMAC reaction liquid comprises a primary separation tower, a dimethylamine absorption tank, a dimethylamine reactor, a reaction liquid transfer tank, a residual liquid tank, a DMF (dimethyl formamide) rectifying tower, a DMAC rectifying tower and a DMAC finished product tank; the method is characterized in that: the reaction liquid transfer tank is connected with the distillation still through a pipeline, the outlet at the top of the distillation still is connected with the receiving tank through a pipeline, the receiving tank is connected with the DMF rectifying tower through a pipeline, and the outlet at the bottom of the distillation tower is connected with the raffinate tank through a pipeline;

the method comprises the following steps:

(1) adding the material (DMAC reaction solution) in the reaction solution transfer tank at a distance of 0.5-0.8m³The amount of the methanol/ethanol/water is fed into a distillation kettle, the pressure in the distillation kettle is controlled to be-88 to-96 KPa, the temperature is controlled to be 100 to 110 ℃, gas phase (DMAC, tetramethylurea and acetic acid) from the top of the distillation kettle is condensed (30 to 50 ℃) and then enters a receiving tank, when the receiving tank has a liquid level of 30 to 40 percent of the volume, the liquid is fed into a DMF (dimethyl formamide) rectifying tower, and bottom liquid in the distillation kettle is extracted and fed into a residual liquid tank (sugar residue, dimethylamine salt, acetate and the like) to be treated as fuel.

The invention has the advantages that: the equipment investment cost is low, the process is simple, and the operation is convenient; the energy consumption and the equipment abrasion are reduced, and the operation labor amount is reduced; the cost is saved, and the environment is protected; sugar residues, dimethylamine salts, acetate and the like in the DMAC reaction liquid can be effectively reduced (the sucralose sugar residues are reduced to below 1% from 3-5% before treatment, the dimethylamine salts are reduced to below 0.5% from 5-8% before treatment, and the acetate is reduced to below 1% from 2-5% before treatment), the cleaning period of the pipeline is prolonged to 10-15 days/time from the original 1-2 days/time, and the stable operation of the subsequent working sections is greatly ensured.

Drawings

FIG. 1 is a schematic diagram of a process for the distillation treatment of a DMAC reaction solution.

Detailed Description

The invention is further illustrated with reference to fig. 1:

a distillation treatment device for DMAC reaction liquid comprises the following devices: the primary separation tower is sequentially connected with a dimethylamine absorption tank, a dimethylamine reactor, a reaction liquid transfer tank, a distillation kettle (containing a condenser), a receiving tank, a DMF (dimethyl formamide) rectifying tower, a DMAC rectifying tower and a DMAC finished product tank through pipelines, and an outlet at the bottom of the distillation tower is connected with a residue tank through a pipeline.

A distillation treatment method of DMAC reaction liquid comprises the following specific implementation steps:

example 1

(1) The liquid from the bottom of the primary separation tower enters a dimethylamine absorption tank, dimethylamine is circularly absorbed until the acid value is below 5, the absorbed absorption liquid is pumped into a dimethylamine reactor for reaction, the temperature of the reactor is controlled to be 190 ℃, the pressure is 0.95MPA, the content of acetic acid after the reaction is measured to be below 5 percent, and the reaction liquid is sent into a reaction liquid transfer tank;

(2) DMAC reaction solution in the reaction solution transfer tank is 0.5m³The amount of the distillate is fed into a distillation still, the pressure in the distillation still is controlled to be-92 KPa, the temperature is controlled to be 105 ℃, the gas phase (DMAC, tetramethylurea and acetic acid) from the top of the distillation still is condensed by a condenser (35 ℃) and then enters a receiving tank, and the bottom liquid in the distillation still is extracted and sent to a residual liquid tank (sugar residue, dimethylamine salt, acetate and the like) to be treated as fuel;

(3) when the liquid level in the receiving tank is 35% by volume, the liquid is added at 0.9m³The amount of the catalyst is fed into a DMF rectifying tower, the temperature in the DMF rectifying tower is controlled to be 115 ℃, the pressure is controlled to be minus 86KPa, DMThe liquid phase (DMAC) from the rectifying tower F enters a DMAC rectifying tower for rectification;

(4) controlling the temperature in the DMAC rectifying tower at 110 ℃ and the pressure at-90 KPa, and enabling the gas phase coming out of the DMAC rectifying tower to enter a DMAC finished product tank (the content is 99.5%).

Example 2

(1) Liquid from the bottom of the primary separation tower enters a dimethylamine absorption tank, dimethylamine is absorbed in a circulating manner until the acid value is below 5, the absorbed absorption liquid is injected into a dimethylamine reactor for reaction, the temperature of the reactor is controlled to be 200 ℃, the pressure is 0.95MPA, the content of acetic acid after the reaction is measured to be below 5%, and the reaction liquid is fed into a reaction liquid transfer tank;

(2) DMAC reaction solution in the reaction solution transfer tank is 0.6m³The amount of the distillate is fed into a distillation still, the pressure in the distillation still is controlled to be-92 KPa, the temperature is controlled to be 105 ℃, the gas phase (DMAC, tetramethylurea and acetic acid) from the top of the distillation still is condensed by a condenser (35 ℃) and then enters a receiving tank, and the bottom liquid in the distillation still is extracted and sent to a residual liquid tank (sugar residue, dimethylamine salt, acetate and the like) to be treated as fuel;

(3) when the liquid level in the receiving tank is 35% by volume, the liquid is filled at 1.1m³Feeding the volume of the solution/h into a DMF (dimethyl formamide) rectifying tower, controlling the temperature in the DMF rectifying tower to be 116 ℃ and the pressure to be-86 KPa, and feeding a liquid phase (DMAC) from the DMF rectifying tower into the DMAC rectifying tower for rectifying;

(4) controlling the temperature in the DMAC rectifying tower to be 111 ℃ and the pressure to be-90 KPa, and enabling the gas phase discharged from the DMAC rectifying tower to enter a DMAC finished product tank (the content is 99.5%).

Example 3

(1) Liquid from the bottom of the primary separation tower enters a dimethylamine absorption tank, dimethylamine is absorbed in a circulating manner until the acid value is below 5, the absorbed absorption liquid is injected into a dimethylamine reactor for reaction, the temperature of the reactor is controlled to be 195 ℃, the pressure is controlled to be 0.95MPA, the content of acetic acid after the reaction is measured to be below 5%, and the reaction liquid is sent into a reaction liquid transfer tank;

(2) DMAC reaction solution in the reaction solution transfer tank is 0.8m³The amount of the components is fed into a distillation still, the pressure in the distillation still is controlled to be-92 KPa, the temperature is controlled to be 105 ℃, and the gas phase (DMAC, tetramethylmethane) from the top of the distillation still is controlledUrea and acetic acid) is condensed by a condenser (at 35 ℃) and then enters a receiving tank, and bottom liquid in a distillation kettle is extracted and sent to a residual liquid tank (sugar residue, dimethylamine salt, acetate and the like) to be treated as fuel;

(3) when the liquid level in the receiving tank is 35% by volume, the liquid is filled at 1.2m³Feeding the amount of the solid phase/h into a DMF (dimethyl formamide) rectifying tower, controlling the temperature in the DMF rectifying tower to be 118 ℃ and the pressure to be 86KPa, and feeding a liquid phase (DMAC) from the DMF rectifying tower into the DMAC rectifying tower for rectifying;

(4) controlling the temperature in the DMAC rectifying tower to be 113 ℃ and the pressure to be-90 KPa, and enabling the gas phase discharged from the DMAC rectifying tower to enter a DMAC finished product tank (the content is 99.5%).