CN111686556A - Industrial treatment system and treatment method for solid light tail gas in process of synthesizing fluorinated phase transfer catalyst - Google Patents

Abstract

The invention relates to the technical field of tail gas treatment, in particular to an industrial treatment system and treatment method for solidifying tail gas in the process of synthesizing a fluorinated phase transfer catalyst. components, end-stage flushing tanks, water absorption components, and alkali absorption components; the front-end buffer tanks, the multi-stage external circulation absorption components, and the end-stage flushing tanks can be used for the individual absorption of phosgene tail gas or the successive absorption of the phosgene tail gas; The downstream of the alkali absorption component is connected with an induced draft fan, and the treated gas is introduced into the RTO combustion process through the induced draft fan. After the external circulation three-stage absorption of the mixed liquid of DMI (or DMF, NMP) and dichloroethane in this device, and then two-stage water absorption and two-stage alkali absorption to complete the harmless treatment of phosgene tail gas, it can be recycled and applied in During the reaction, the output of the waste brine and the aqueous hydrochloric acid solution is almost zero, which greatly reduces the pressure of the subsequent treatment process of the waste brine, reduces the alkali consumption, and improves the economic benefit.

Description

Industrial treatment system and treatment of solid-light tail gas in the process of synthesizing fluorinated phase transfer catalysts management method

technical field

The invention relates to the technical field of tail gas treatment, in particular to an industrial treatment system and a treatment method for solidifying tail gas in the process of synthesizing a fluorinated phase transfer catalyst.

Background technique

Phosgene, also known as phosgene, is a colorless and extremely toxic gas at room temperature and pressure, with high chemical reactivity and strong corrosiveness when it encounters water. However, in the process of production and use of solid light, due to the constraints of production methods, production capacity and technological development level, it is difficult to completely and completely remove phosgene tail gas. When synthesizing pesticides or medicines with solid light as raw materials, the exhaust gas discharged contains unreacted excess phosgene, but the depth of phosgene contained in the exhaust gas recovered by cryogenic method or solvent absorption method is generally much higher than that of the emission. The depth specified by the standard must be destructively treated before being released into the atmosphere. At present, the commonly used phosgene-containing waste gas treatment methods in industry include lye method, ammonia method, incineration method and catalytic hydrolysis method.

The reaction principle of the lye method is as follows:

Usually in emergency situations, phosgene is destroyed by alkaline washing. The lye method generally has a treatment effect of about 80% on phosgene, and the highest can reach 90%. Advantages: The equipment is relatively simple, and the operation is stable and reliable. Disadvantages: When this method is applied in production, a large amount of sodium hydroxide will be consumed, and a large amount of white sodium salt will be produced, which greatly reduces the damage to the phosgene tail gas. More importantly, the long-term continuous operation cost is high, and the phosgene with high content in the exhaust gas is not completely destroyed, and there will be very pungent phosgene running out.

The principle of ammonia reaction is:

The principle of the ammonia method is basically similar to that of the lye method, and this method is rarely used in industrial production. Advantages: The equipment is simple, the contact reaction speed of phosgene and ammonia is faster, the destruction is more thorough, and the removal efficiency can be as high as 90% or more. At the same time, when the ammonia chloride and urea generated during the reaction reach a certain amount, they can be recycled. Disadvantages: Due to the high price of ammonia, it is not suitable to be used alone, but as an auxiliary treatment measure, such as after hot water and lye method, or as emergency ammonia treatment in the event of an accident.

The steam method reaction principle is:

The steam method is an older traditional method. After the phosgene is contacted with steam, a hydrolysis reaction occurs, and the HCl generated by the hydrolysis, together with the water vapor, is condensed to recover the hydrochloric acid, and the hydrolysis reaction speed increases with the increase of temperature. Advantages: In order to speed up the reaction in the industry, superheated steam is often used, and the general destruction rate can reach more than 95%. The equipment used is usually a steam jet pump. Disadvantages: Hydrogen chloride, a domestic product, becomes hydrochloric acid after absorbing water, which is highly corrosive. Therefore, the jet pump and the receiving tank should be made of heat-resistant and hydrochloric acid-resistant materials, and the equipment material requirements are high. In addition, this method requires a large amount of steam and cooling water, and the treatment cost is high, so it is rarely used in industry.

The reaction principle of the catalytic hydrolysis method is as follows:

Phosgene and water undergo a hydrolysis reaction at a suitable temperature through a catalyst in a packed column. If the tail gas contains organic solvent, the organic solvent in the tail gas is generally condensed by the condenser first, and the tail gas containing phosgene undergoes hydrolysis reaction through the catalyst in the packed tower, so as to achieve the purpose of destroying the phosgene. Advantages: The process is simple, the destruction efficiency can reach more than 95%, and the operation is convenient. Disadvantages: The catalysts used in this method are mainly activated carbon and SN-7501. The investment is relatively expensive, and hydrochloric acid is produced.

Comparing the above four phosgene tail gas treatment technologies, the lye method, ammonia method, steam method, and catalytic hydrolysis method are decomposed and destroyed, which not only consumes a large amount of chemical raw materials, but also produces a large amount of waste brine and hydrochloric acid aqueous solution, which increases production costs. The effect is not ideal, and generally the real industrialization cannot meet the emission requirements.

SUMMARY OF THE INVENTION

In order to solve one of the above-mentioned technical problems, the technical scheme adopted in the present invention is: an industrial treatment system for solidifying tail gas in the process of synthesizing a fluorinated phase transfer catalyst, comprising a front-end buffer tank, a multi-stage buffer tank connected in series through pipelines from upstream to downstream sequentially Stage external circulation absorption assembly, end-stage flushing tank, water absorption assembly, alkali absorption assembly; the multi-stage outer circulation absorption assembly is used for individual absorption of phosgene tail gas or step-by-step sequential absorption; the downstream connection of the alkali absorption assembly The treated gas is introduced into the RTO combustion process through the induced draft fan.

Preferably, the multi-stage external circulation absorption assembly comprises a first-stage absorption still, a second-stage absorption still, and a third-stage absorption still connected in series through pipelines; the first-stage absorption still, the second-stage absorption still, the A mixed solution of dipolar solvent and ethylene dichloride is arranged inside the three-stage absorption kettle.

Preferably, the dipolar solvent is one of DMI, DMF or NMP.

Preferably, the first-stage absorption still, the second-stage absorption still, and the third-stage absorption still are connected with their respective matching graphite shell-and-tube condensers.

The graphite tubular condensers of 20 square meters each are used to prevent dichloroethane from entering the next-stage recovery kettle.

Preferably, the front-end buffer tank and the end-stage flushing tank are connected with their respective matching 20 square front-end graphite tubular condensers and end graphite tubular condensers;

Preferably, the front-end graphite tubular condensers are all condensed with water at 5°C, and the front-end graphite tubular condenser of 20 square meters on the front-end buffer tank is used to prevent other organic solvents in the synthetic fluorination catalyst from entering the exhaust gas treatment device ;

Preferably, the 20 square terminal graphite tubular condenser on the terminal buffer tank is used to prevent dichloroethane from entering the downstream water absorption components and alkali absorption components.

Preferably, the water absorption assembly is a two-stage water absorption structure, which specifically includes two water spray primary water absorption towers and water spray secondary water absorption towers connected in series. In order to receive the gas from the upstream, the water spray secondary water absorption tower is used to transport the gas to the alkali absorption component.

Preferably, the alkali absorption component is a two-stage alkali absorption structure, and specifically includes two liquid alkali spraying primary alkali absorption towers and liquid alkali spraying secondary alkali absorption towers connected in series, the liquid alkali spraying primary alkali absorption towers The absorption tower is used to receive the gas discharged from the upstream water spray secondary water absorption tower, and the liquid alkali spray secondary alkali absorption tower is used to transport the gas to the induced draft fan.

Preferably, in the absorption process of phosgene tail gas absorption, the mixed liquid of DMI (or DMF, NMP) and dichloroethane in each stage of absorption kettle is heated to above 70°C, which can maximize the absorption of phosgene tail gas.

Allow unreacted DMI and dichloroethane to fully dissolve the white solid of Vilsmeier reagent 1.

Preferably, each absorption kettle is a 2000L or 3000L enamel reaction kettle, and a tetrafluoro tube is connected to the bottom of each enamel reaction kettle, and the upper end of each tetrafluoro tube is connected by the upper port of the enamel reaction kettle at the corresponding position. It is introduced into the interior of the enamel reaction kettle to form a circulation, and a centrifugal pump or a diaphragm pump is installed on the pipeline of each tetrafluoro tube, and both ends of each tetrafluoro tube are connected to the corresponding enamel reaction kettle through steel-lined tetrafluoro tubes. , a shower nozzle with a number of honeycomb holes is arranged on the pipeline of the steel-lined PTFE tube located at the upper end.

Preferably, each honeycomb hole on the shower head is used to spray and return the unreacted mixed solution in the corresponding reaction kettle to the current reaction kettle, and the exhaust port of the inner air inlet pipeline for passing the phosgene tail gas into the reaction kettle There is a grid plate with several mesh holes on the surface for dispersing it into small bubbles, and the end of each air inlet pipeline extends below the liquid level inside the reactor.

Preferably, the mesh plate can disperse the exhaust gas discharged into the reactor into small bubbles and DMI (or DMF, NMP) for sufficient contact reaction; DMI (or DMF, NMP) and DMI (or DMF, NMP) and DMI (or DMF, NMP) and The mixed solution of dichloroethane is circulated back to the reaction kettle, and at the same time, it is dispersed into mist or spray through the shower head, and then fully contacted and reacted with the unreacted phosgene tail gas emerging from the bottom of the kettle.

An industrial treatment method for solidification tail gas in the process of synthesizing a fluorinated phase transfer catalyst, the industrial treatment method adopts the above-mentioned industrial treatment system to realize the treatment of the solidification tail gas, comprising the following specific steps:

S1: The above system receives the phosgene tail gas emitted from the outside;

S2: the phosgene tail gas enters the interior of the multi-stage external circulation absorption assembly to complete the three-stage continuous chlorination absorption and forms a white solid of Vilsmeier reagent 1 in each reactor;

S3: The above-mentioned treated phosgene continues to undergo two-stage water absorption and two-stage alkali absorption in sequence, and then is outputted by the induced draft fan and then introduced into RTO combustion treatment.

Preferably, the molar ratio of phosgene tail gas, dipolar solvent (DMI or DMF or NMP) and dichloroethane in the S1 is 0.1-1:1:1.0-4.

The above specific ratio is determined according to the amount of phosgene tail gas emerging from each batch. The purpose is to make phosgene react with DMI (or DMF, NMP) to generate a white solid of Vilsmeier reagent 1 that is completely dissolved in unreacted DMI (or DMF, NMP). and dichloroethane.

Preferably, in each enamel reaction kettle of the multi-stage external circulation absorption assembly in the S2, the tail gas absorption temperature is raised to above 70° C. to prevent the phenomenon of crystal insolubility.

Preferably, after the internal reaction and absorption of each of the enamel reaction kettles, the internal substances are injected into the external reaction kettle for synthesizing the fluorination catalyst, and the Vilsmeier reagent generated by distillation is continued to be recovered after the dichloroethane is distilled off.

The beneficial effects of the present invention are embodied in:

After the external circulation of the mixed liquid of DMI (or DMF, NMP) and dichloroethane in this device is three-stage absorption, and then two-stage water absorption and two-stage alkali absorption to complete the harmless treatment of phosgene tail gas, the main product is Vilsmeier The white solid of reagent 1 can be recycled in the reaction.

The output of waste brine and hydrochloric acid aqueous solution is almost zero, which greatly reduces the pressure of the subsequent treatment process of waste brine, reduces alkali consumption and improves economic benefits.

Description of drawings

In order to illustrate the specific embodiments of the present invention or the technical solutions in the prior art more clearly, the following briefly introduces the accompanying drawings that are required to be used in the description of the specific embodiments or the prior art. Similar elements or components are generally identified by similar reference numerals throughout the drawings. In the drawings, each element or component is not necessarily drawn to actual scale.

FIG. 1 is a schematic diagram of a system connection relationship of the present invention.

In the figure, 1. Front-end buffer tank; 101. Front-end graphite tubular condenser; 2. Multi-stage external circulation absorption assembly; 201, Primary absorption kettle; 202, Secondary absorption kettle; 203, Tertiary absorption kettle; 204 , graphite shell and tube condenser; 3, end stage flushing tank; 301, end graphite shell and tube condenser; 4, water absorption component; 401, water spray primary water absorption tower; 402, water spray secondary water Absorption tower; 5. Alkali absorption component; 501. Liquid alkali spraying primary alkali absorption tower; 502. Liquid alkali spraying secondary alkali absorption tower; 6. Induced draft fan; 7. RTO; 8. PTFE pipe; 9. Circulating pump; 10, shower head; 11, grid plate; 12, liquid level; 13, spray pump; 14, spray pipeline.

Detailed ways

Embodiments of the technical solutions of the present invention will be described in detail below with reference to the accompanying drawings.

The following examples are only used to more clearly illustrate the technical solutions of the present invention, and are therefore only used as examples, and cannot be used to limit the protection scope of the present invention.

As shown in Figure 1, the industrial treatment system for solid-light tail gas in the process of synthesizing a fluorinated phase transfer catalyst includes a front-end buffer tank 1, a multi-stage external circulation absorption assembly 2, and an end stage sequentially connected in series from upstream to downstream through pipelines. The flushing tank 3, the water absorption component 4, the alkali absorption component 5; the front-end buffer tank 1, the multi-stage external circulation absorption component 2, and the end-stage flushing tank 3 can be used for the individual absorption of phosgene tail gas or step by step. Absorption; the downstream of the alkali absorption component 5 is connected to the induced draft fan 6 and the treated gas is introduced into the RTO7 through the induced draft fan 6 for combustion processing.

Preferably, the multi-stage external circulation absorption assembly 2 comprises a first-stage absorption still 201, a second-stage absorption still 202, and a third-stage absorption still 203 connected in series through pipelines; the first-stage absorption still 201, the second-stage absorption still Both the absorption kettle 202 and the three-stage absorption kettle 203 are provided with a mixed solution of dipolar solvent and dichloroethane.

Corresponding control valves are set on each pipeline as required.

Preferably, the dipolar solvent is one of DMI, DMF or NMP.

The chlorination reaction principle of the industrial treatment method of solid light tail gas adopted in this application is as follows:

The reaction of phosgene tail gas with DMI (or DMF, NMP) is easy to generate Vilsmeier reagent 1, that is, compared with water absorption or alkali absorption, DMI (or DMF, NMP) absorbs phosgene tail gas particularly well,

The first-stage absorption kettle 201 can reach more than 99% through the external circulation of the mixed liquid of DMI (or DMF, NMP) and dichloroethane, and the reaction itself is exothermic, and the generated Vilsmeier reagent 1 (ie: active intermediate chloride salt 1) can reach more than 99%. ) just dissolved in the unreacted DMI (or DMF, NMP) and the polar solvent dichloroethane, in the form of a homogeneous liquid.

Preferably, the first-stage absorption stills 201, the second-stage absorption stills 202, and the third-stage absorption stills 203 are all connected with their respective matching graphite shell-and-tube condensers 204.

The graphite tubular condensers 204 of 20 square meters each are used to prevent dichloroethane from entering the next-stage recovery kettle.

Preferably, the front-end buffer tank 1 and the end-stage flushing tank 3 are connected with their respective matching 20 square front-end graphite tubular condensers 101 and end graphite tubular condensers 301;

Preferably, the front-end graphite tubular condenser 101 is condensed with water at 5°C, and the front-end graphite tubular condenser 101 of 20 square meters on the front-end buffer tank 1 is used to prevent the synthesis of other organic solvents in the fluorination catalyst. Enter the subsequent exhaust gas treatment device;

Preferably, the 20 square terminal graphite tubular condenser 301 on the terminal buffer tank is used to prevent dichloroethane from entering the downstream water absorption component 4 and alkali absorption component 5 .

Preferably, the water absorption assembly 4 is a two-stage water absorption structure, and specifically includes two water spray primary water absorption towers 401 and water spray secondary water absorption towers 402 connected in series. The absorption tower 401 is used to receive the gas from the upstream, and the water spray secondary water absorption tower 402 is used to deliver the gas to the alkali absorption component 5 .

Preferably, the alkali absorption component 5 is a two-stage alkali absorption structure, and specifically includes two liquid alkali spraying primary alkali absorption towers 501 and liquid alkali spraying secondary alkali absorption towers 502 connected in series. The primary alkali absorption tower 501 is used to receive the gas discharged from the upstream water spray secondary water absorption tower 402 , and the liquid alkali spray secondary alkali absorption tower 502 is used to transport the gas to the induced draft fan 6 .

On the spray pipelines 14 of the liquid alkali spray primary alkali absorption tower 501, the liquid alkali spray secondary alkali absorption tower 502, the water spray primary water absorption tower 401, and the water spray secondary water absorption tower 402 A spray pump 13 is installed.

Preferably, in the absorption process of phosgene tail gas absorption, the mixed liquid of DMI (or DMF, NMP) and dichloroethane in each stage of absorption kettle is heated to above 70°C, which can maximize the absorption of phosgene tail gas.

Allow unreacted DMI and dichloroethane to fully dissolve the white solid of Vilsmeier reagent 1.

Preferably, each absorption kettle is a 2000L or 3000L enamel reaction kettle, and a tetrafluoro tube 8 is connected to the bottom of each enamel reaction kettle, and the upper end of each tetrafluoro tube 8 is connected by the enamel reaction kettle at the corresponding position. The upper port is introduced into the interior of the enamel reaction kettle to form an external circulation, and a circulating pump 9 (the circulating pump is a centrifugal pump or a diaphragm pump) is installed on the pipeline of each of the tetrafluoro tubes 8. Both ends are connected to the corresponding enamel reaction kettles through steel-lined PTFE tubes 8, and a shower head 10 with several honeycomb holes is provided at the pipeline return ports of the steel-lined PTFE tubes 8 at the upper ends.

Preferably, each honeycomb hole on the shower head 10 is used to spray and return the unreacted mixed solution in the corresponding reaction kettle to the current reaction kettle, and exhaust the phosgene tail gas into the inner air inlet pipeline of the reaction kettle. A mesh plate 11 with several mesh holes on the surface for dispersing it into small bubbles is arranged at the mouth, and the ends of each air inlet pipe extend below the liquid level 12 inside the reactor.

Preferably, the grid plate 11 can disperse the exhaust gas discharged into the reactor into small bubbles and DMI (or DMF, NMP) for sufficient contact reaction; DMI (or DMF, NMP) The mixed solution with ethylene dichloride is circulated back to the reaction kettle, and is dispersed into mist or spray through the shower head 10 at the same time, and then fully contacts and reacts with the unreacted phosgene tail gas that emerges from the bottom of the kettle.

The national environmental protection laws and regulations are becoming more and more perfect, and the requirements are becoming more and more strict. Not only are there clear regulations on the emission concentration of phosgene-containing tail gas of existing installations, but also strict restrictions on new construction and reconstruction, which force the production enterprises of phosgene-containing tail gas to consider how to Effectively treat exhaust gas and meet national emission requirements.

The phosgene is absorbed by the phosgene and the mixed solution is circulated outside the liquid level below 12 in the system at all levels. The phosgene is basically absorbed by DMI (or DMF, NMP) and dichloroethane. The first-stage absorption kettle 201 of the external circulation of the mixed liquid is completely absorbed.

After the first-level kettle is fully absorbed, it can be pumped into the corresponding fluorinated phase transfer catalyst synthesis kettle for recycling, which reduces the amount of solid light and avoids the generation of a large amount of hydrochloric acid aqueous solution and waste brine from water absorption and alkali absorption.

An industrial treatment method for solidification tail gas in the process of synthesizing a fluorinated phase transfer catalyst, the industrial treatment method adopts the above-mentioned industrial treatment system to realize the treatment of the solidification tail gas, comprising the following specific steps:

S1: The above system receives the phosgene tail gas emitted from the outside;

S2: The phosgene tail gas enters the multi-stage external circulation absorption component 2 to complete the three-stage continuous chlorination absorption, and the Vilsmeier reagent 1 formed in each reaction kettle (the Vilsmeier reagent 1 is dissolved in the reaction kettle at above 70°C) in a mixture of unreacted dipolar solvent and dichloroethane);

S3: The above-mentioned treated phosgene continues to undergo two-stage water absorption and two-stage alkali absorption in sequence, and then is outputted by induced draft fan 6 and then introduced into RTO7 for combustion treatment.

Preferably, the molar ratio of phosgene tail gas, dipolar solvent (DMI or DMF or NMP) and dichloroethane in the S1 is 0.1-1:1:1.0-4.

The above specific ratio is determined according to the amount of phosgene tail gas emerging from each batch. The purpose is to make phosgene react with DMI (or DMF, NMP) to generate a white solid of Vilsmeier reagent 1 that is completely dissolved in unreacted DMI (or DMF, NMP). and dichloroethane.

Preferably, in each enamel reaction kettle of the multi-stage external circulation absorption assembly 2 in the S2, the exhaust gas absorption temperature is raised to above 70° C. to prevent the phenomenon of crystal insolubility.

Preferably, after the internal reaction and absorption of each of the enamel reaction kettles, the internal substances are injected into the external reaction kettle for synthesizing the fluorination catalyst, and the Vilsmeier reagent generated by distillation is continued to be recovered after the dichloroethane is distilled off.

The invention adopts three-stage continuous chlorination absorption, two-stage water absorption and two-stage alkali absorption method to absorb the phosgene tail gas into another available product Vilsmeier reagent 1, avoiding the neutralization method of some manufacturers with water or liquid alkali, It consumes a large amount of water or liquid caustic soda, and the hydrochloric acid water or saline wastewater produced is difficult to treat, consumes high energy, and has high operating costs. The phosgene tail gas emission is more stable, and the production process is safer, more economical, more environmentally friendly, scientific and reasonable.

The above embodiments are only used to illustrate the technical solutions of the present invention, but not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that the foregoing embodiments can still be used for The technical solutions described in the examples are modified, or some or all of the technical features thereof are equivalently replaced; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention, and all of them should cover Within the scope of the claims and description of the present invention; for those skilled in the art, any alternative improvements or transformations made to the embodiments of the present invention fall within the protection scope of the present invention.

The parts that are not described in detail in the present invention are the well-known technologies of those skilled in the art.

Claims (9)

1. The industrial treatment system for the solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst is characterized in that: comprises a front-end buffer tank, a multi-stage external circulation absorption assembly, a tail-end flushing tank, a water absorption assembly and an alkali absorption assembly which are sequentially connected in series through pipelines from upstream to downstream; the multistage external circulation absorption assembly is used for separately absorbing phosgene tail gas or sequentially absorbing phosgene tail gas stage by stage; and the downstream of the alkali absorption assembly is connected with an induced draft fan, and treated gas is introduced into the RTO for combustion treatment through the induced draft fan.

2. The industrial treatment system for solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst according to claim 1, characterized in that: the multistage external circulation absorption assembly comprises a first-stage absorption kettle, a second-stage absorption kettle and a third-stage absorption kettle which are sequentially connected in series through pipelines; mixed liquid of dipolar solvent and dichloroethane is arranged in the primary absorption kettle, the secondary absorption kettle and the tertiary absorption kettle; the dipolar solvent is one of DMI or DMF or NMP.

3. The industrial treatment system for solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst according to claim 2, characterized in that: and the primary absorption kettle, the secondary absorption kettle and the tertiary absorption kettle are respectively connected with graphite shell and tube condensers which are respectively matched with the primary absorption kettle, the secondary absorption kettle and the tertiary absorption kettle.

4. The industrial treatment system for solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst according to claim 3, characterized in that: the front end buffer tank and the tail end level flushing tank are respectively connected with a front end graphite tubular condenser and a tail end graphite tubular condenser which are respectively matched with the front end buffer tank and the tail end level flushing tank and have a square diameter of 20.

5. The industrial treatment system for solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst according to claim 4, characterized in that: the water absorption component is of a two-stage water absorption structure and specifically comprises a water spraying primary water absorption tower and a water spraying secondary water absorption tower which are connected in series, wherein the water spraying primary water absorption tower is used for receiving gas from the upstream, and the water spraying secondary water absorption tower is used for conveying the gas to the alkali absorption component.

6. The industrial treatment system for solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst according to claim 5, characterized in that: the alkali absorption component is two-stage alkali absorption structure, specifically includes that two series connection's liquid alkali sprays one-level alkali absorption tower, liquid alkali sprays second grade alkali absorption tower, liquid alkali sprays one-level alkali absorption tower and is used for receiving the water that comes from the upper reaches and sprays second grade water absorption tower combustion gas, liquid alkali spray second grade alkali absorption tower be used for to draught fan conveying gas.

7. The industrial treatment method for the solid light tail gas in the process of synthesizing the fluorinated phase transfer catalyst adopts the industrial treatment system to realize the treatment of the solid light tail gas, and is characterized in that: the method comprises the following specific steps:

s1: the system receives phosgene tail gas emitted from the outside;

s2: phosgene tail gas enters the multistage external circulation absorption assembly to complete three-stage continuous chlorination absorption, and Vilsmeier reagent 1 is formed in each reaction kettle (the Vilsmeier reagent 1 is dissolved in the mixed solution of unreacted dipolar solvent and dichloroethane in the reaction kettle at the temperature of more than 70 ℃);

s3: and the treated phosgene tail gas is continuously subjected to two-stage water absorption and two-stage alkali absorption in sequence, and then is output by a draught fan and introduced into RTO combustion treatment.

8. The industrial treatment method of solid light tail gas in the process of synthesizing fluorinated phase transfer catalyst according to claim 7, characterized in that: the molar ratio of the phosgene tail gas, the dipolar solvent (DMI or DMF or NMP) and the dichloroethane in the S1 is 0.1-1: 1: 1.0-4.

9. The industrial treatment method of solid light tail gas in the process of synthesizing fluorinated phase transfer catalyst according to claim 7, characterized in that: and the tail gas absorption temperature in each enamel reaction kettle of the multistage external circulation absorption assembly in the S2 is raised to be above 70 ℃ so as to prevent the phenomenon of crystal insolubility.

Images