Continuous preparation system for hydrogen chloride alcohol

Abstract

The utility model belongs to the technical field of chemical engineering, and particularly relates to a hydrogen chloride alcohol continuous preparation system which comprises a chlorination reactor, a tail gas condenser and a falling film absorption tower, the chlorination reactor is connected with a chloroacetic acid storage tank and the tail gas condenser, and the gas phase output end of the tail gas condenser is connected with the input end of the falling film absorption tower. The gas phase output end of the tail gas condenser is further connected with the gas phase input end of the isopropanol absorption tower, the liquid phase input end of the isopropanol absorption tower is connected with the output end of the isopropanol raw material tank, and the liquid phase output end of the isopropanol absorption tower is connected with the hydrochloric acid isopropanol storage tank. According to the utility model, isopropanol is adopted to absorb hydrogen chloride, so that a cold source consumed by heat release of absorbed hydrochloric acid is reduced, a large amount of wastewater generated by absorbing washing alkali liquor by hydrogen chloride tail gas is effectively reduced, and compared with the traditional falling film absorption process, the new process reduces the generation of hydrochloric acid, reduces energy consumption, greatly reduces the consumption of absorbed alkali, and reduces the production cost. And a hydrochloric acid alcohol solution product with good quality is obtained.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the field of chemical technology, more particularly to a hydrogen chloride alcohol continuous preparation system. BACKGROUND

[0002] In the production process of chloroacetic acid, a large amount of hydrogen chloride tail gas is produced. At present, the chloroacetic acid tail gas absorption system mostly adopts water absorption to produce hydrochloric acid process. This process has many drawbacks. On the one hand, a large amount of absorption water and absorption alkali are consumed to produce hydrochloric acid, and a large amount of circulating water is also needed for cooling and heat removal, which undoubtedly increases the production cost and resource consumption. On the other hand, the reaction impurities carried in the chlorination tail gas will affect the quality of hydrochloric acid, and a large amount of waste water will be produced in the recovery process, causing resource waste. More seriously, if the tail gas is not completely purified before being discharged, it will pollute the environment and even harm human health.

[0003] In addition, the current market supply of hydrochloric acid is greater than the demand, and the economic benefits brought by hydrochloric acid to enterprises are low, which to a large extent limits the development of enterprises. Therefore, developing a new hydrogen chloride tail gas treatment system that can effectively treat tail gas and improve economic benefits has become a problem to be solved in the chemical field. CONTENT OF THE UTILITY MODEL

[0004] In order to solve the problems existing in the prior art, the utility model provides a hydrogen chloride alcohol continuous preparation system, which uses isopropyl alcohol to absorb hydrogen chloride, reduces the consumption of cold source of absorption of hydrochloric acid heat, effectively reduces a large amount of waste water produced by washing alkali liquid of hydrogen chloride tail gas absorption, compared with the traditional falling film absorption process, the new process reduces the generation of hydrochloric acid, reduces the energy consumption, and greatly reduces the consumption of absorption alkali, and obtains good hydrochloric acid alcohol solution product.

[0005] The utility model adopts the specific technical scheme of:

[0006] A hydrogen chloride alcohol continuous preparation system, including chlorination reactor, tail gas condenser and falling film absorption tower, the liquid phase output end of chlorination reactor is connected with chloroacetic acid storage tank, the tail gas end of chlorination reactor is connected with the input end of tail gas condenser, the gas phase output end of tail gas condenser is connected with the input end of falling film absorption tower, the gas phase output end of tail gas condenser is also connected with the gas phase input end of isopropyl alcohol absorption tower, the liquid phase input end of isopropyl alcohol absorption tower is connected with the output end of isopropyl alcohol raw material tank, and the liquid phase output end of isopropyl alcohol absorption tower is connected with hydrochloric acid isopropyl alcohol storage tank.

[0007] Further, the tail gas condenser comprises a first condenser and a second condenser, an input end of the first condenser is formed as an input end of the tail gas condenser, a gas phase output end of the first condenser is connected with an input end of the second condenser, a gas phase output end of the second condenser is formed as a gas phase output end of the tail gas condenser, and a liquid phase output end of the first condenser and a liquid phase output end of the second condenser are connected with an input end of the chlorination reactor respectively.

[0008] Further, a cooler is arranged between the gas phase output end of the tail gas condenser and the gas phase input end of the isopropanol absorption tower, and hydrogen chloride is cooled by the cooler and then is transported into the isopropanol absorption tower.

[0009] Further, an acetic acid washing tower is arranged between the cooler and the isopropanol absorption tower, an output end of the cooler is connected with a gas phase input end of the acetic acid washing tower, a gas phase output end of the acetic acid washing tower is connected with the gas phase input end of the isopropanol absorption tower, a liquid phase output end of the acetic acid washing tower is connected with a circulating pump and an output pump in parallel, an output end of the circulating pump is connected with a liquid phase input end of the acetic acid washing tower, and an output end of the output pump is connected with an input end of a dilute hydrochloric acid tank.

[0010] Further, a dechlorination absorption tower and a concentrated sulfuric acid absorption tower are further arranged between the acetic acid washing tower and the isopropanol absorption tower, a gas phase output end of the acetic acid washing tower is connected with a gas phase input end of the dechlorination absorption tower, a gas phase output end of the dechlorination absorption tower is connected with a gas phase input end of the concentrated sulfuric acid absorption tower, and a gas phase output end of the concentrated sulfuric acid absorption tower is connected with the gas phase input end of the isopropanol absorption tower.

[0011] The utility model discloses the beneficial effect is:

[0012] 1, the utility model discloses a hydrogen chloride adopts isopropanol absorption, reduces the heat -releasing consumption of absorption hydrochloric acid cold source, effectively reduces the large amount of waste water of hydrogen chloride tail gas absorption lye production, compared with traditional falling film absorption process, new technology reduces the generation of hydrochloric acid, reduces the energy consumption, and greatly reduces the consumption of absorption alkali, obtains good quality hydrochloric acid alcohol solution product.

[0013] The utility model solves the problem of chlorination tail gas treatment, and realizes the continuous production of high-purity hydrogen chloride isopropanol solution.

[0014] 2, the utility model discloses simple process, easy operation, saves manpower, improves product added value, and product and byproduct application is wide, realizes the recovery of most organic matters in tail gas, reduces product consumption.

[0015] 3, the utility model solves the product quality problem of hydrochloric acid alcohol solution, and the recycling use of absorption liquid of recovery tail gas slows down the problem of waste water production. Compared with the traditional method of absorbing hydrogen chloride tail gas device with lye, a large amount of water and lye are saved, and the amount of waste liquid is small.BRIEF DESCRIPTION OF DRAWINGS BRIEF DESCRIPTION OF DRAWINGS

[0016] Figure 1 A process flow chart of the present application. DETAILED DESCRIPTION

[0017] The present application will be further described below in conjunction with the drawings and specific embodiments:

[0018] Specific embodiments, such as Figure 1 The present application provides a kind of hydrogen chloride alcohol continuous preparation system, including chlorination reactor, tail gas condenser and falling film absorption tower, the liquid phase output end of chlorination reactor is connected with chloroacetic acid storage tank, the tail gas end of chlorination reactor is connected with the input end of tail gas condenser, the gas phase output end of tail gas condenser is connected with the input end of falling film absorption tower, the gas phase output end of the tail gas condenser is also connected with the gas phase input end of isopropyl alcohol absorption tower, the liquid phase input end of the isopropyl alcohol absorption tower is connected with the output end of isopropyl alcohol raw material tank, the liquid phase output end of isopropyl alcohol absorption tower is connected with hydrochloric acid isopropyl alcohol storage tank.

[0019] At present, chloroacetic acid tail gas absorption system mostly uses water absorption to produce hydrochloric acid process. This process has many drawbacks, on the one hand, a large amount of absorption water and absorption alkali are consumed to produce hydrochloric acid, and a large amount of circulating water is also needed for cooling and heat removal, which undoubtedly increases the production cost and resource consumption; on the other hand, the reaction impurities carried in the chlorination tail gas will affect the quality of hydrochloric acid, and a large amount of waste water will be produced in the recovery process, causing resource waste. More seriously, if the tail gas is not completely purified before being discharged, it will pollute the environment and even harm human health.

[0020] In the process of the present application, the hydrogen chloride gas produced by chloroacetic acid is partly used to produce 31% by-product hydrochloric acid under the action of the falling film absorption tower; the other part of the hydrogen chloride tail gas is used to absorb and produce hydrochloric acid isopropyl alcohol solution by using the isopropyl alcohol absorption tower.

[0021] Hydrogen chloride isopropyl alcohol solution is widely used in chemical analysis, organic synthesis reaction, extraction and separation, etc. Due to its excellent chemical reaction properties, it can be used as a catalyst, reaction medium and dehydrating agent in the process of organic synthesis. This process provides a practical solution for a large amount of hydrogen chloride downstream product, reduces the total amount of industrial hydrochloric acid from the source, broadens the application field, and improves the economic benefit of by-product hydrogen chloride.

[0022] In the present application, hydrogen chloride is absorbed by isopropyl alcohol, which reduces the cooling source for absorbing heat generated by hydrochloric acid, effectively reduces a large amount of waste water produced by washing alkali solution of hydrogen chloride tail gas, compared with the traditional falling film absorption process, the new process reduces the generation of hydrochloric acid, reduces energy consumption, and greatly reduces the consumption of absorption alkali, and obtains high-quality hydrochloric acid alcohol solution product.

[0023] The tail gas condenser includes a primary condenser and a secondary condenser. The input end of the primary condenser is formed as the input end of the tail gas condenser. The gas phase output end of the primary condenser is connected to the input end of the secondary condenser. The gas phase output end of the secondary condenser is formed as the gas phase output end of the tail gas condenser. The liquid phase output ends of the primary condenser and the liquid phase output ends of the secondary condenser are respectively connected to the input end of the chlorination reactor.

[0024] The hydrogen chloride tail gas generated during the chloroacetic acid production process is discharged from the chlorination reactor and enters the tail gas condenser. After condensation in the primary and secondary condensers, impurities such as chloroacetic acid and dichloroacetic acid are condensed into liquid phase and recycled back to the chlorination reactor. The uncondensed gaseous hydrogen chloride enters the falling film absorption tower or isopropanol absorption tower for further treatment.

[0025] A cooler is installed between the gas phase output end of the tail gas condenser and the gas phase input end of the isopropanol absorption tower. Hydrogen chloride is cooled by the cooler and then transported into the isopropanol absorption tower. The cooled hydrogen chloride gas is more conducive to reacting with isopropanol in the absorption tower, producing an isopropanol hydrochloride solution. Furthermore, the cooler lowers the temperature of the hydrogen chloride to a suitable range, protecting subsequent equipment such as the acetic acid scrubbing tower, dechlorination absorption tower, and concentrated sulfuric acid drying tower, preventing equipment failure due to high temperatures.

[0026] An acetic acid scrubbing tower is installed between the cooler and the isopropanol absorption tower. The output end of the cooler is connected to the gas phase input end of the acetic acid scrubbing tower, and the gas phase output end of the acetic acid scrubbing tower is connected to the gas phase input end of the isopropanol absorption tower. A circulation pump and an output pump are connected in parallel to the liquid phase output end of the acetic acid scrubbing tower. The output end of the circulation pump is connected to the liquid phase input end of the acetic acid scrubbing tower, and the output end of the output pump is connected to the input end of the dilute hydrochloric acid tank. The acetic acid scrubbing tower can remove impurities from hydrogen chloride gas. The scrubbing liquid is recycled through the circulation pump to ensure the scrubbing effect. As impurities in the scrubbing liquid increase, unqualified scrubbing liquid is transported to the dilute hydrochloric acid tank through the output pump, and new scrubbing liquid is replenished to the acetic acid scrubbing tower.

[0027] A dechlorination absorption tower and a concentrated sulfuric acid absorption tower are also installed between the acetic acid washing tower and the isopropanol absorption tower. The gas phase output end of the acetic acid washing tower is connected to the gas phase input end of the dechlorination absorption tower, the gas phase output end of the dechlorination absorption tower is connected to the gas phase input end of the concentrated sulfuric acid absorption tower, and the gas phase output end of the concentrated sulfuric acid absorption tower is connected to the gas phase input end of the isopropanol absorption tower. The dechlorinating agent in the dechlorination absorption tower removes chlorine from the hydrogen chloride gas; the concentrated sulfuric acid absorption tower removes moisture from the hydrogen chloride gas. Both methods improve the purity of the hydrogen chloride gas, reduce the impurity content in the subsequent product, isopropanol hydrochloride, and improve the purity of isopropanol hydrochloride.

Claims

1. A continuous preparation system for hydrochlorohydrin, comprising a chlorination reactor, a tail gas condenser, and a falling film absorption tower, wherein the liquid phase output end of the chlorination reactor is connected to a chloroacetic acid storage tank, the tail gas end of the chlorination reactor is connected to the input end of the tail gas condenser, and the gas phase output end of the tail gas condenser is connected to the input end of the falling film absorption tower, characterized in that, The gas phase output end of the tail gas condenser is also connected to the gas phase input end of the isopropanol absorption tower, the liquid phase input end of the isopropanol absorption tower is connected to the output end of the isopropanol raw material tank, and the liquid phase output end of the isopropanol absorption tower is connected to the hydrochloric acid isopropanol storage tank.

2. The continuous preparation system for hydrogen chloride alcohol according to claim 1, characterized in that, The tail gas condenser includes a primary condenser and a secondary condenser. The input end of the primary condenser is formed as the input end of the tail gas condenser. The gas phase output end of the primary condenser is connected to the input end of the secondary condenser. The gas phase output end of the secondary condenser is formed as the gas phase output end of the tail gas condenser. The liquid phase output ends of the primary condenser and the liquid phase output ends of the secondary condenser are respectively connected to the input end of the chlorination reactor.

3. The continuous preparation system for hydrogen chloride alcohol according to claim 1, characterized in that, A cooler is installed between the gas phase output end of the tail gas condenser and the gas phase input end of the isopropanol absorption tower. Hydrogen chloride is cooled by the cooler and transported to the isopropanol absorption tower.

4. The continuous preparation system for hydrogen chloride alcohol according to claim 3, characterized in that, An acetic acid scrubbing tower is installed between the cooler and the isopropanol absorption tower. The output end of the cooler is connected to the gas phase input end of the acetic acid scrubbing tower, and the gas phase output end of the acetic acid scrubbing tower is connected to the gas phase input end of the isopropanol absorption tower. A circulation pump and an output pump are connected in parallel to the liquid phase output end of the acetic acid scrubbing tower. The output end of the circulation pump is connected to the liquid phase input end of the acetic acid scrubbing tower, and the output end of the output pump is connected to the input end of the dilute hydrochloric acid tank.

5. The continuous preparation system for hydrogen chloride alcohol according to claim 4, characterized in that, A dechlorination absorption tower and a concentrated sulfuric acid absorption tower are also provided between the acetic acid washing tower and the isopropanol absorption tower. The gas phase output end of the acetic acid washing tower is connected to the gas phase input end of the dechlorination absorption tower, the gas phase output end of the dechlorination absorption tower is connected to the gas phase input end of the concentrated sulfuric acid absorption tower, and the gas phase output end of the concentrated sulfuric acid absorption tower is connected to the gas phase input end of the isopropanol absorption tower.

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