CN114436761A - Method and system for feeding chlorine gas prepared by catalysis of fluorine-containing hydrogen chloride into methane chloride and polychlorinated methane for coproduction - Google Patents
Method and system for feeding chlorine gas prepared by catalysis of fluorine-containing hydrogen chloride into methane chloride and polychlorinated methane for coproduction Download PDFInfo
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- CN114436761A CN114436761A CN202111651233.4A CN202111651233A CN114436761A CN 114436761 A CN114436761 A CN 114436761A CN 202111651233 A CN202111651233 A CN 202111651233A CN 114436761 A CN114436761 A CN 114436761A
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- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/16—Preparation of halogenated hydrocarbons by replacement by halogens of hydroxyl groups
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Abstract
The invention provides a method and a system for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and throwing the chlorine gas into methane chloride and polychlorinated methane, which comprises the following steps: (1) the fluorine-containing hydrogen chloride is catalyzed and oxidized to prepare a mixed gas containing chlorine; (2) chlorine in the mixed gas and methane chloride from a hydrochlorination reaction system enter a thermal chlorination reaction unit to generate polychlorinated methane and hydrogen chloride, heavy components, namely the polychlorinated methane, are further refined, and light components enter the hydrochlorination reaction unit; (3) the hydrogen chloride in the light component reacts with methanol to generate methane chloride, and the methane chloride is degassed and refined to remove fluoride, so that pure methane chloride is prepared. The problem of high energy consumption in the separation of chlorine subsequent products prepared by the treatment of fluorine chemical by-product hydrogen chloride and the catalysis of hydrogen chloride is solved, the closed cycle of chlorine element in a system is realized, secondary pollutants are not generated, and a foundation is laid for promoting the energy conservation and emission reduction and the clean production of the fluorine chemical industry.
Description
Technical Field
The invention belongs to the field of chemical production, and relates to a method and a system for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and throwing the chlorine gas into monochloromethane and polychlorinated methane.
Background
Chlorine is an important chemical basic raw material for the industries of chemistry, metallurgy, medicine, synthetic materials and the like. With the increasing demand of chlorine-containing products, the shortage of chlorine supply by the development of chlor-alkali industry alone is not favorable for the balance of chlor-alkali consumption, and the search for a new source of chlorine becomes a strategy.
The hydrogen chloride is byproduct in the process of a plurality of processes taking chlorine as raw material, and the amount of the hydrogen chloride byproduct is enlarged while the chlorine demand is increased. The preparation of chlorine from hydrogen chloride is the key to solve the chlor-alkali consumption balance, and the methods for preparing chlorine from hydrogen chloride can be mainly classified into 3 types: electrolytic processes, direct oxidation processes and catalytic oxidation processes. The catalytic oxidation method with the advantages of strong adaptability of hydrogen chloride raw materials, low energy consumption, stable operation and the like becomes a hotspot for the development of the technology for preparing chlorine from hydrogen chloride at home and abroad. The method comprises the following steps:
2HCl+1/2O2→Cl2+H2OΔH＝-13.8kcal/mol；
the technology has developed catalytic oxidation catalysts and designed fluidized bed reactors suitable for the catalytic oxidation process at home at present, and the problem of how to reduce the separation energy consumption of subsequent product gas is the industrial maximization of the technology for preparing chlorine by catalytic oxidation of hydrogen chloride. The currently used methods mainly include a pressure swing adsorption method, a condensation method, a low-temperature rectification method, an absorption-desorption method, a membrane separation method and the like. Chinese patent document CN101128392A (CN200680005928.2) discloses a method for preparing chlorine gas, which utilizes a method combining a condensation method and a membrane separation method to recover chlorine gas in a hydrogen chloride catalytic oxidation mixed gas, and the purity of the obtained product chlorine gas is more than 95%. However, this method is high in energy consumption and complicated in process. Chinese patent document CN101663233A (CN200880012431.2) discloses a method for performing an optionally catalyst-assisted hydrogen chloride oxidation reaction by oxygen, comprising single-stage or multi-stage cooling of the process gas and separating unreacted hydrogen chloride and reaction water from the process gas, and drying the gaseous product. However, the method also has the defects of complex equipment and higher operation energy consumption. In conclusion, the purity of the chlorine gas obtained by the pressure swing adsorption method is not high, and the requirement that the purity of the chlorine gas for chemical production is more than 99 percent cannot be met. Although the purity requirement can be met by adopting a condensation method, an absorption method, a low-temperature distillation method, a membrane separation method and a coupling method thereof, the energy consumption is high, the process is complex, and the implementation of national strategy of energy conservation, emission reduction and sustainable development is not facilitated.
A large amount of fluorine-containing hydrogen chloride is generated in the production process of the fluorine chemical industry, the fluorine chemical industry is generally used for generating hydrochloric acid at present, the byproduct hydrochloric acid is analyzed to solve the mature recovery process of the byproduct hydrogen chloride, the hydrogen chloride in the byproduct hydrochloric acid can be recovered, and the comprehensive utilization of the byproduct hydrochloric acid is realized. Chinese patent document CN111499490A (202010342702.3) provides a method for producing methyl chloride by using fluorine-containing hydrogen chloride as a byproduct, which uses hydrogen chloride with a high fluoride content as a raw material for producing methyl chloride, and comprehensively treats the fluorine-containing hydrogen chloride to obtain a large amount of hydrogen chloride gas reaching reaction conditions, and after the hydrogen chloride gas reacts with methanol, the high-purity methyl chloride is obtained through chilling separation, water washing, alkali washing, compression condensation and degassing refining. However, this patent does not realize the recycle of chlorine element, and has disadvantages of high investment cost and high running cost.
Disclosure of Invention
In order to solve the problems of high recycling cost and easy generation of secondary pollutants of fluorine-containing hydrogen chloride in the prior art, the invention provides a method and a system for putting chlorine prepared by catalyzing fluorine-containing hydrogen chloride into a methane chloride and polychlorinated methane coproduction.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into the coproduction of monochloro methane and polychlorinated methane comprises the following steps:
(1) the fluorine-containing hydrogen chloride is catalyzed and oxidized to prepare a mixed gas containing chlorine;
(2) chlorine in the mixed gas and methane chloride from a hydrochlorination reaction system enter a thermal chlorination reaction unit to generate polychlorinated methane and hydrogen chloride, heavy components, namely the polychlorinated methane, are further refined, and light components enter the hydrochlorination reaction unit;
(3) the hydrogen chloride in the light component reacts with methanol to generate methane chloride, and the methane chloride is degassed and refined to remove fluoride, so that pure methane chloride is prepared. The light components can also be used for preparing chlorine in the step (1).
The content of fluoride in the byproduct hydrogen chloride of the fluorination industry is generally 2-5%, for example, when chloroform and HF are used to prepare trifluoromethane (R23), HCl and a byproduct of difluoromethane monochloride (R22) are generated. When the fluoride is in the range, the fluoride enters a monochloromethane and polychlorinated methane dual-production process system without influencing hydrochlorination and thermal chlorination reaction. When the HF content in the fluoride is too high, the activity of the catalyst in the catalytic oxidation is affected to some extent.
According to the invention, the fluorine chemical by-product hydrogen chloride contains 95-98 wt% of hydrogen chloride and 2-5 wt% of fluoride, and the fluoride is one or a combination of more of R22, R32, R125, R134a, R143a and HF.
The chlorine is prepared by the catalytic oxidation of fluorine-containing hydrogen chloride in the step (1), and the catalyst and the process adopt the prior art.
Preferably, the mixed gas in the step (1) has the following components: 70-85% of chlorine, 0.5-5% of fluoride and 15-25% of hydrogen chloride.
According to a preferred aspect of the present invention, the reaction conditions of step (2): the chlorine gas and the methane chloride react under the conditions of 395-405 ℃ and 0.55-0.65 MPa, the reaction is a strong exothermic reaction, and in order to control the reaction temperature, the mass ratio of the chlorine gas to the methane chloride is 2-2.5: 1.
And (3) performing secondary condensation and separation on the mixed gas after the reaction in the step (2), condensing methane chloride, dichloromethane and the like, feeding mixed condensate comprising methane chloride, dichloromethane, trichloromethane, carbon tetrachloride and a small amount of fluoride into a subsequent refining unit, feeding the mixed condensate into a recycling tower, a dichloro refining tower, a chloroform refining tower and a four-carbon refining tower to obtain corresponding qualified products, and feeding recycled and recycled part of the methane chloride into a reaction unit to participate in the reaction. The secondary condensation temperatures were 5 ℃ and-25 ℃ respectively.
According to the invention, the light component in the step (2) comprises the following components: 95-99% of hydrogen chloride, 0.2-3% of fluoride and 0-2% of other components (the other components are a small amount of non-condensable gas such as methane chloride, nitrogen and the like), and the light component enters the step (3) to react with methanol to generate methane chloride. The molar ratio of the hydrogen chloride to the methanol is 1-1.2: 1.
And (3) the chloromethane generated in the step (3) contains a small amount of water and a small amount of residual HCl and fluoride, the chloromethane is subjected to water washing, alkali washing, acid washing, drying and compression, and then enters a degassing and refining unit to remove the fluoride to obtain pure chloromethane, one part of which is sold as a product, and the other part of which is used as a raw material and enters a thermal chlorination reaction unit. The acid washing is to use concentrated sulfuric acid to absorb water, dimethyl ether and a small amount of entrained NaOH.
According to the invention, the degassing treatment tower pressure is preferably 0.8-1.6 MPa, and the temperature is preferably 30-45 ℃. The light component gas at the top of the degassing tower contains fluoride and a small amount of methane chloride component (the content of the fluoride is 90-98%); the heavy component liquid at the bottom of the tower contains methane chloride and a small amount of fluoride (the content of the methane chloride is 99 percent); wherein the light component gas at the top of the tower is sent to an incineration unit for treatment, and the heavy component liquid at the bottom of the tower is sent to a product refining unit.
According to the invention, the pressure of the refining rectifying tower is 0.7-1.0 MPa, the temperature is 35-45 ℃, and pure methane chloride is obtained after refining.
The invention also provides a system for putting chlorine gas prepared by catalyzing fluorine-containing hydrogen chloride into methane chloride and polychlorinated methane for coproduction, which comprises a catalytic oxidation unit, a thermal chlorination reaction unit and a hydrochlorination reaction unit which are connected in sequence;
a light component discharge port of the thermal chlorination reaction unit is connected with the hydrochlorination reaction unit, and a heavy component discharge port of the thermal chlorination reaction unit is connected with the polychlorinated methane rectifying tower;
the hydrochlorination reaction unit is connected with a lightness-removing tower and a methane chloride rectifying tower; and a discharge port of the methane chloride rectifying tower is connected with a thermal chlorination reaction unit.
Preferably, the thermal chlorination reaction unit is connected with the catalytic oxidation unit. The obtained fluorine-containing HCl can be recycled for preparing chlorine.
Preferably, the discharge port of the hydrogenation reaction unit is directly connected with the thermal chlorination reaction unit.
The working principle of the system of the invention is as follows: chlorine generated after the catalytic oxidation of the fluorine-containing hydrogen chloride enters a thermal chlorination reaction unit and is mixed with pure methane chloride from a hydrochlorination reaction system to generate polychlorinated methane and hydrogen chloride; wherein, the polychlorinated methane is refined to obtain a qualified product, fluorine-containing hydrogen chloride serving as a raw material enters a hydrochlorination reaction unit to generate fluorine-containing monochloromethane with methanol, and the fluorine-containing monochloromethane is subjected to light removal and refining to obtain a pure monochloromethane product. The hydrogen chloride generated by the thermal chlorination reaction unit can also be connected with the catalytic oxidation unit, and the obtained fluorine-containing HCl can be recycled for preparing chlorine. The components from the hydrogenation reaction unit mainly comprise methane chloride, a small amount of HCl and fluoride, and directly enter the thermal chlorination reaction unit, so that the components can be circulated in the system on the premise that the content of the fluoride does not influence the hydrochlorination reaction and the thermal chlorination reaction, and the treatment cost is reduced; when the fluoride content reaches a certain degree (the fluoride content is higher than 5 percent) and influences the hydrochlorination reaction and the thermal chlorination reaction, the product of the hydrochlorination reaction unit is dehydrogenated and refined.
The invention has the technical characteristics and beneficial effects that:
1. the invention puts the mixed gas such as chlorine and the like obtained by catalyzing the fluorine-containing hydrogen chloride into a chloromethane and polychlorinated methane co-production system, and greatly reduces the process investment and the operating cost compared with a method for generating hydrochloric acid by fluoride in a fluorine chemical industry and analyzing the byproduct hydrochloric acid.
2. According to the invention, the mixed gas such as chlorine and the like obtained by catalyzing fluorine-containing hydrogen chloride is compressed and then directly put into a chloromethane and polychlorinated methane co-production system, so that the purification and separation treatment such as subsequent liquefaction and the like of the catalyzed mixed gas are omitted; simultaneously, the subsequent product treatment is degassed and refined to remove fluorideAnd qualified products can be obtained, and economic and environmental benefits are achieved. The invention removes fluoride after reaction of fluorine-containing hydrogen chloride and methanol, but does not remove fluoride in other processes because the boiling point of monochloromethane is higher than that of other fluorides except HF, but hydrogen fluoride is soluble in water and is easy to remove. The products chlorine and hydrogen chloride of other reaction units have low boiling points and are difficult to remove fluoride through dehydrogenation. In addition, the reason for selecting the fluoride removal in this step is that the unit does not produce new HCl, the HCl content in the light components is minimal, and the chlorine element can be utilized to the maximum extent; if fluoride is removed in the thermal chlorination reaction unit, as part of HCl is newly generated in the thermal chlorination reaction, the content of HCl in the light component is the same as that in byproduct HCl, the content is higher, resource waste is caused, and the treatment process is increased. If fluoride is removed after the catalytic oxidation unit, then Cl2The content is high, the difference between the boiling point of chlorine and the boiling point of fluoride is not large, the chlorine is not easy to separate, and the treatment cost is increased.
3. According to the invention, the chlorine gas and the methane chloride generate the polychlorinated methane and the hydrogen chloride, the generated hydrogen chloride is used as a raw material and enters the hydrochlorination reaction unit, and the chlorine element and the methanol generate the methane chloride, so that the closed cycle of the chlorine element in a system is realized, secondary pollutants are not generated, and a foundation is laid for promoting the energy conservation, emission reduction and clean production of the fluorine chemical industry.
Drawings
FIG. 1 is a schematic diagram of a process system for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into chloromethane and polychlorinated methane.
Detailed Description
The present invention will be further described with reference to the following examples, but is not limited thereto.
Example 1
A method for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into a monochloromethane and polychlorinated methane two-coproduction process comprises the following steps:
(1) fluorine-containing hydrogen chloride (the hydrogen chloride content is 96.5 percent, and the R125 content is 3.5 percent) is reacted at the temperature of 400 ℃ and under the reaction pressure of 0.4MPa by adopting a fixed bed reactor, and copper-lanthanum-potassium is addedOxygen/alumina as catalyst, space velocity 2200h-1Carrying out catalytic oxidation to obtain a chlorine-containing mixed gas, and deoxidizing and drying the mixed gas to obtain the following gas components: 73.1% of chlorine, 3.5% of R125 and 23.4% of hydrogen chloride.
(2) The mixed gas compressed to 1.0MPa is added into a thermal chlorination reaction unit, and generates dichloromethane, trichloromethane, carbon tetrachloride and hydrogen chloride (the content of fluoride in light components is 1.4 percent, the content of hydrogen chloride is 98.1 percent, and the content of monochloromethane is 0.5 percent) with monochloromethane from a hydrochlorination reaction unit, and the light components enter a hydrochlorination reaction system, wherein the monochloromethane is a product of the hydrochlorination reaction system, so the reaction is not influenced.
Chlorine (Cl)2) And monochloromethane (CH)3Cl) is reacted at 400 ℃ and 0.55MPa to generate polychlorinated methane, wherein the mass ratio of chlorine to monochloromethane is 2.2: 1.
and separating the polychlorinated methane products according to the boiling points of dichloromethane, trichloromethane and carbon tetrachloride, wherein the tower temperature of a dichloro tower is 125 ℃, the tower pressure is 0.45MPa, the tower temperature of a chloroform tower is 110 ℃, the tower pressure is 0.1MPa, the tower temperature of a four-carbon tower is 75 ℃, and the tower pressure is 0.01MPa, so that the corresponding polychlorinated methane products can be obtained.
(3) And (3) allowing the light components (with the feeding pressure of 0.35-0.45 MPa, ensuring that the light components can enter a reaction) in the step (2) to enter a hydrochlorination reaction system, respectively overheating the light components and methanol (with the feeding pressure of 0.5MPa after the methanol is vaporized and overheated) to 210 ℃, and then entering a reactor for reaction. The catalyst is active alumina, the reaction temperature is 230 ℃, the reaction pressure is 0.25Mpa, and the products in the reactor are methane chloride, water and excessive HCl (in order to reduce by-products and obtain better CH3OH conversion, control of HCl and CH3The molar ratio of OH is 1.15: 1, if CH3Excessive OH can generate more gas-liquid mixtures of dimethyl ether, fluoride (R125) and the like, and the mixed gas is obtained by acid washing, alkali washing, drying and compressing to 0.8MPa, wherein the mixed gas comprises the following components in percentage by mass: 97.7% methyl chloride, 2.2% R125 and 0.01% moisture; the mixed gas enters a degassing unit, the tower pressure is 1.0MPa, the temperature is 38 ℃, and the light component gas at the top of the tower contains fluoride (96.5%) and a small amount of methane chloride component (3.5%); the bottoms heavies liquid contained monochloromethane (98.5%) And a minor amount of fluoride; wherein the light component gas at the top of the tower is sent to an incineration unit for treatment, and the heavy component liquid at the bottom of the tower is sent to a product refining unit; the pressure of the methane chloride rectifying tower is 0.9MPa, the temperature is 40 ℃, and methane chloride with the content of 99.9 percent is obtained after refining.
The fluorine-containing hydrogen chloride is treated according to the method, and the yield of the treatment of 1t of fluorine-containing hydrogen chloride is about 100 yuan/t. The prior treatment method for preparing the fluorine-containing hydrogen chloride into the hydrochloric acid needs to be about 300 yuan/t for treating 1t of hydrogen chloride. The method of the invention produces higher economic benefit.
Example 2
A method for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into a monochloromethane and polychlorinated methane two-coproduction process comprises the following steps:
(1) catalytic oxidation of fluorine-containing hydrogen chloride (the hydrogen chloride content is 95.5%, and the R125 and R32 contents are 4.5%) (the reaction temperature is 400 ℃, the reaction pressure is 0.4MPa, the reactor is a fixed bed reactor, the catalyst is copper-lanthanum-potassium-oxygen/alumina, and the space velocity is 2200h-1) Obtaining mixed gas containing chlorine, and deoxidizing and drying the mixed gas to obtain the following gas components: 72% of chlorine, 3.6% of R125 and R32 and 24.4% of hydrogen chloride.
(2) Adding the mixed gas compressed to 1.0MPa into a thermal chlorination reaction unit, and reacting with monochloromethane from a hydrochlorination reaction unit to generate dichloromethane, trichloromethane, carbon tetrachloride and hydrogen chloride (the content of fluoride is 1.6%, the content of hydrogen chloride is 97.9%, and the content of monochloromethane is 0.5%),
chlorine (Cl)2) And monochloromethane (CH)3Cl) is reacted at 400 ℃ and 0.55MPa to generate polychlorinated methane, and the mass ratio of chlorine to monochloromethane is 2.2: 1; the tower temperature of the dichloro tower is 125 ℃, the tower pressure is 0.45MPa, the tower temperature of the chloroform tower is 110 ℃, the tower pressure is 0.1MPa, the tower temperature of the four-carbon tower is 75 ℃, and the tower pressure is 0.01 MPa.
(3) And (3) allowing the light component in the step (2) to enter a hydrochlorination reaction system, respectively overheating the light component and methanol (with the pressure of 0.5MPa after vaporization) to 210 ℃, and then allowing the light component and the methanol to enter a reactor for reaction. The catalyst is active alumina, the reaction temperature is 220 ℃, the reaction pressure is 0.25Mpa, methane chloride is generated in the reactor, and at the moment, the components in the reactor are methane chloride, water and excessive HCl (in order to reduce side effects)The product is obtained and better CH is obtained3OH conversion, control of HCl and CH3The molar ratio of OH is 1.1: 1, if CH3Excessive OH can generate more gas-liquid mixtures such as dimethyl ether and fluoride (R125 and R32), and the gas-liquid mixtures are subjected to acid washing, alkali washing, drying and compression to 0.8MPa to obtain mixed gas, wherein the mixed gas comprises the following components in percentage by mass: 97.2% methyl chloride, 2.6% R125 and R32 and 0.02% moisture; the mixed gas enters a degassing unit, the tower pressure is 1.0MPa, the temperature is 38 ℃, and the light component gas at the top of the tower contains 96.5 percent of fluoride and a small amount of 3.5 percent of methane chloride; the bottoms heavies liquid contained methyl chloride (98.3%) and a small amount of fluoride; wherein the light component gas at the top of the tower is sent to an incineration unit for treatment, and the heavy component liquid at the bottom of the tower is sent to a product refining unit; the pressure of the methane chloride rectifying tower is 0.9MPa, the temperature is 40 ℃, and methane chloride with the content of 99.9 percent is obtained after refining.
Comparative example 1
A method for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into a monochloromethane and polychlorinated methane two-coproduction process comprises the following steps:
chlorine gas obtained by catalyzing fluorine-containing hydrogen chloride as described in example 1 is fed into a monochloromethane and polychlorinated methane co-production system, which is different from example 1 in that: degassing and refining are omitted; the other steps and conditions were in accordance with example 1, and the content of the resulting monochloromethane product was 97.5%, whereby a qualified product could be obtained by the process of the present invention as compared with example 1, and also recycling of chlorine was achieved.
The monochloromethane which is not subjected to degassing and refining treatment can enter a thermal chlorination reaction system to prepare polychlorinated methane, but when the fluoride content is high, the reaction efficiency is affected, and the consumption of a refining unit is increased.
Claims (10)
1. A method for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into methane chloride and polychlorinated methane for coproduction is characterized by comprising the following steps:
(1) the fluorine-containing hydrogen chloride is catalyzed and oxidized to prepare a mixed gas containing chlorine;
(2) chlorine in the mixed gas and methane chloride from a hydrochlorination reaction system enter a thermal chlorination reaction unit to generate polychlorinated methane and hydrogen chloride, heavy components, namely the polychlorinated methane, are further refined, and light components enter the hydrochlorination reaction unit;
(3) the hydrogen chloride in the light component reacts with methanol to generate methane chloride, and the pure methane chloride is prepared after degassing and refining and fluoride removal.
2. The method according to claim 1, wherein the fluorine-containing hydrogen chloride contains 2 to 5% of fluoride;
preferably, the fluoride is one or more of R22, R32, R125, R134a, R143a and HF.
3. The method of claim 1, wherein the composition of the mixed gas of step (1): 70-85% of chlorine, 0.5-5% of fluoride and 15-25% of hydrogen chloride.
4. The method according to claim 1, wherein the reaction conditions of step (2): reacting chlorine gas and methane chloride at 395-405 ℃ and 0.55-0.65 MPa, wherein the mass ratio of the chlorine gas to the methane chloride is 2-2.5: 1.
5. The method of claim 4, wherein the light fraction of step (2) has a composition of: 95-99% of hydrogen chloride, 0.2-3% of fluoride and 0-2% of the rest.
6. The method according to claim 1, wherein the molar ratio of hydrogen chloride to methanol in the step (3) is 1-1.2: 1.
7. The method of claim 1, wherein the monochloromethane produced in step (3) is passed through water washing, alkali washing, acid washing, drying, compression, and then to a degassing and refining unit.
8. The method according to claim 1, wherein the degassing treatment in the step (3) has a column pressure of 0.8 to 1.6MPa and a temperature of 30 to 45 ℃;
the pressure of the refining rectification tower is 0.7-1.0 MPa, and the temperature is 35-45 ℃.
9. A system for preparing chlorine gas by catalyzing fluorine-containing hydrogen chloride and putting the chlorine gas into the methane chloride and the polychlorinated methane, which is characterized by comprising a catalytic oxidation unit, a thermal chlorination reaction unit and a hydrochlorination reaction unit which are connected in sequence;
a light component discharge port of the thermal chlorination reaction unit is connected with the hydrochlorination reaction unit, and a heavy component discharge port of the thermal chlorination reaction unit is connected with the polychlorinated methane rectifying tower;
the hydrochlorination reaction unit is connected with a lightness-removing tower and a methane chloride rectifying tower; and a discharge port of the methane chloride rectifying tower is connected with a thermal chlorination reaction unit.
10. The system of claim 9, wherein the thermal chlorination reaction unit is coupled to a catalytic oxidation unit.
Preferably, the discharge port of the hydrogenation reaction unit is directly connected with the thermal chlorination reaction unit.
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