CN114618578A - Catalyst for preparing vinyl chloride by cracking 1, 2-dichloroethane, preparation method and regeneration method - Google Patents

Abstract

The invention relates to a catalyst for preparing vinyl chloride by cracking 1, 2-dichloroethane, a preparation method and a regeneration method. The catalyst is a supported phosphorus-aluminum molecular sieve catalyst, and is a catalyst which takes a nitrogen-containing material as a catalyst active component and is loaded on the surface of a phosphorus-aluminum molecular sieve. The preparation method of the catalyst comprises the steps of loading a nitrogen-containing material on a phosphorus-aluminum molecular sieve, and then calcining and pyrolyzing the phosphorus-aluminum molecular sieve at high temperature for activation. The regeneration method of the catalyst comprises the steps of roasting the catalyst with carbon deposit inactivated in an oxidizing atmosphere to remove all carbon parts on the surface, and then repeating the preparation process of the catalyst. Compared with the existing thermal cracking technology, the catalyst is simple to prepare; the reaction temperature can be reduced, the yield of the chloroethylene is high, and the stability of the whole reaction process is good; the catalyst is cheap and renewable, has long service life and is beneficial to reducing industrial cost.

Description

A kind of 1,2-dichloroethane cracking to produce vinyl chloride catalyst, preparation method and regeneration method

technical field

The invention relates to a catalyst for preparing vinyl chloride by cracking 1,2-dichloroethane, in particular to a supported phospho-aluminum molecular sieve catalyst, a preparation method and a regeneration method, and belongs to the technical field of vinyl chloride monomer preparation.

Background technique

Vinyl chloride is an important polymerized monomer used in polymer chemical industry. At present, there are two main production processes of vinyl chloride in industry: ethylene method and acetylene method. The mercuric chloride catalyst generally used in the production of PVC by the calcium carbide acetylene method will not only generate a large amount of calcium carbide slag and waste water and increase the investment cost, but also cause pollution to the environment and pose a hazard to human health. The ethylene method mainly has three processes. The first step is to obtain ethylene by cracking light diesel oil or chemical light oil in crude oil. The second step is to generate 1,2-dichloroethane by direct chlorination or oxychlorination of ethylene. The first step is to crack 1,2-dichloroethane in a high temperature tubular cracking furnace to prepare vinyl chloride. Therefore, the cracking of 1,2-dichloroethane is a crucial step in the ethylene process. In industry, the reaction temperature is usually 500-600 °C for thermal cracking. At this time, the conversion rate of 1,2-dichloroethane is controlled at 50%. about. Due to the high reaction temperature of high-temperature thermal cracking, high energy consumption, and easy coking, the cracking furnace and subsequent separation process equipment are blocked by coke particles, requiring frequent coke cleaning, and a series of problems such as short production cycle.

Judging from the reported catalysts, the common catalysts for catalytic cracking of 1,2-dichloroethane to produce vinyl chloride are mainly based on carbon materials, which are used for catalytic cracking of 1,2-dichloroethane by loading other species as active centers. Ethane produces vinyl chloride, but the process of cracking 1,2-dichloroethane to produce vinyl chloride with carbon materials as catalysts has disadvantages such as high cost, short life and difficult regeneration, and does not meet the sustainable development strategy , and thus failed to achieve industrial application.

SUMMARY OF THE INVENTION

The purpose of the present invention is to overcome the deficiencies of the prior art and provide a catalyst for catalyzing the cracking of 1,2 dichloroethane to produce vinyl chloride. The catalyst is applied to the reaction of 1,2-dichloroethane cracking to prepare vinyl chloride, and has high 1,2-dichloroethane conversion rate, high vinyl chloride yield and good stability. And after the molecular sieve is deactivated during use, the carbonaceous part on the surface of the carrier can be removed by calcination, and the active components can be reloaded to restore the catalyst activity. In addition, the molecular sieve can be regenerated and reused, thereby greatly reducing the cost of the catalyst, making the catalyst very promising for industrial application.

According to one aspect of the present application, there is provided a catalyst for preparing vinyl chloride by cracking 1,2-dichloroethane, the catalyst is a supported catalyst, and includes a nitrogen-containing active component and a carrier; the carrier is selected from silicon-phosphorus-aluminum At least one of molecular sieves or phosphorus-aluminum molecular sieves; the nitrogen-containing active component is obtained by loading a nitrogen source on the carrier and subjecting it to heat treatment in an oxygen-containing atmosphere or a nitrogen-containing atmosphere.

Those skilled in the art can select a suitable nitrogen source according to the specific situation. Optionally, the nitrogen source is selected from at least one of nitrogen-containing organics and ammonium salts.

Preferably, the nitrogen source is selected from ammonia (including ammonia water and ammonia gas), hydrazine, acetonitrile, cyanamide, pyridine, pyrrole, ethylenediamine, methylamine, tetramethylammonium hydroxide, tetraethylammonium hydroxide, Tetrapropylammonium Hydroxide, Tetrabutylammonium Hydroxide, Ammonium Chloride, Ammonium Persulfate, Ammonium Dimolybdate, Ammonium Lactate, Ferric Ammonium Oxalate, Ammonium Heptamolybdate, Ammonium Chloroplatinite, Ammonium Viuronate, Chloroplatinum Ammonium acid, ammonium chromate, ammonium fluoroborate, ammonium metavanadate, ammonium formate, ammonium sulfamate, ammonium tetrachloroaurate, ammonium hexabromoplatinate, water-soluble ammonium polyphosphate, ammonium phosphomolybdate, ammonium oxalate, Ammonium dihydrogen arsenate, ferrous amine sulfate, ammonium phosphate hexahydrate, ammonium phosphomolybdate, ammonium fluorotitanate, sodium ammonium phosphate, monoammonium glycyrrhizinate, ammonium bicarbonate, ammonium stearate, ammonium dichromate , ammonium tellurate, ammonium octamolybdate, ammonium chloropalladate, ammonium lignosulfonate, ammonium trifluoroacetate, ammonium phthalate, ammonium hexafluorogermanate, ammonium paratungstate, ammonium chloroiridate, ammonium chloroosmate, Ammonium chlororuthenate, ammonium carbonate, diammonium arsenate, ammonium polyacrylate, ammonium sulfate, ammonium tetrathiomolybdate, ammonium succinate, ammonium iodate, ammonium perrhenate, hydrated ammonium ferrocyanide, ammonium molybdate, Ammonium titanyl oxalate, ammonium phosphotungstate, ammonium nitrate, ammonium chlororhodium, ammonium oxalate, iron salt diammonium glycyrrhizate, ammonium hexachloroiridate, ammonium oxalate, ammonium chlororuthenate, ammonium dodecanoate, ammonium hydrogen borate Ammonium, tetrahydrate ammonium sebacate, ammonium polyphosphate, ammonium chloride phosphate, ammonium tetramolybdate, ammonium polyphosphate, ammonium tetrathiotungstate, ammonium purple urate, food grade ammonium acetate, ammonium molybdate solution, Monoammonium glycyrrhizinate, ammonium hydrogen oxalate, ammonium lactate, ammonium bissebacate, ammonium phosphotungstate, ammonium acetate or hydroxylammonium hydrochloride nitrogen-containing substances, or at least one of the derivatives of any of the above nitrogen-containing substances.

Optionally, the carrier is selected from SAPO-5, SAPO-11, SAPO-18, SAPO-31, SAPO-34, SAPO-35, SAPO-37, SAPO-39, SAPO-41, SAPO-47, MgAPSO -31, at least one of MnAPSO-11, CoAPO-50, ZnAPSO-39, CoAPSO-47, AlPO-5, AlPO-11, AlPO-14, AlPO-16 and AlPO-20.

Optionally, in the supported catalysis, the mass percentage of the active component to the carrier is 0.01-100%.

Another object of the present invention is to provide a method for preparing a supported catalyst, which comprises the following steps: firstly, a nitrogen source is supported on a carrier, and then heat treatment is performed in a nitrogen-containing atmosphere or an oxygen-containing atmosphere; Supported catalyst; the temperature of the heat treatment is 200-1000°C, and the heat treatment time is 2-48 hours.

Optionally, the loading method is direct impregnation, ion exchange or spraying liquid nitrogen-containing material or solution of nitrogen-containing material onto the carrier.

Optionally, the pyrolysis temperature is 600-850°C; and the time is 3-20 hours.

Optionally, the nitrogen-containing compound atmosphere refers to nitrogen-containing gas or a mixture of nitrogen-containing gas and inert atmosphere gas. The nitrogen-containing gas is selected from at least one of ammonia gas, nitrogen gas, and organic amine gas.

Optionally, the oxygen-containing atmosphere is an oxygen-containing gas or a mixture of an oxygen-containing gas and nitrogen or an inert gas. The oxygen-containing compound atmosphere is selected from the group consisting of air and oxygen.

Optionally, the inert atmosphere gas is a mixture of one or more of argon or helium; if a mixture of nitrogen-containing gas and inert gas is used, the mass content of the nitrogen-containing gas in the mixture is greater than Equal to 0.1% to less than 100%; if a mixture of oxygen-containing gas and inert gas is used, the mass content of oxygen-containing gas in the mixture is greater than or equal to 0.1% to less than 100%.

Optionally, the nitrogen source is dissolved in a solution and then loaded onto a carrier, and the solvent in the solution is water, hydrocarbons with 1 to 18 carbon atoms, halogenated hydrocarbons, alcohols, ethers, esters, ketones, amines, acids , one or both of phenol, nitrile, furan, pyridine or pyrrole.

Another object of the present application is to provide a method for regenerating a supported catalyst, wherein the deactivated catalyst is obtained after the catalyst is deactivated in the reaction of catalyzing the cracking of 1,2-dichloroethane to prepare vinyl chloride; the deactivated supported catalyst is in The charcoal of the inorganic porous material is removed by calcination in an oxidizing atmosphere and used as a carrier, and then the regenerated catalyst is prepared according to the above-mentioned method.

Optionally, the oxidizing atmosphere is oxygen, a mixture of oxygen and nitrogen or inert atmosphere gas or air; the inert atmosphere gas is one or more mixtures of argon or helium; in the oxidizing atmosphere The mass content of oxygen is 1-100% by mass.

Optionally, the calcination temperature is 300-1000° C.; the treatment time is 2-48 hours.

Another object of the present application is to further provide the application of the supported catalyst in catalyzing the cracking of 1,2-dichloroethane to prepare vinyl chloride. Specifically, 1,2-dichloroethane is vaporized and passed into the reactor equipped with the catalyst, wherein the mass space velocity (WHSV) of the reaction is 0.01-100 h ^-1 , and the cracking temperature is 200-450°C.

The beneficial effects of this application include but are not limited to:

(1) The catalyst provided by the application has simple preparation steps and good regeneration effect;

(2) the catalyst prepared by the application is used for the cracking of ethylene dichloride to produce vinyl chloride, the vinyl chloride yield is high, and the stability of the whole reaction process is good;

(3) The catalyst prepared by the present application is cheap and regenerable, and has a long service life; the energy consumption of the whole reaction process is low, which is conducive to reducing industrial costs and has a good industrial application prospect.

Detailed ways

The technical solutions of the present invention will be described in detail below through specific embodiments. The following embodiments are only some preferred embodiments of the present invention, and the present invention is not limited to the contents of the embodiments. For those skilled in the art, various changes and modifications can be made within the scope of the technical solution of the present invention, and any changes and modifications made are within the protection scope of the present invention.

Unless otherwise specified, the raw materials in the examples of this application are all purchased through commercial channels.

In the embodiment of the application, conversion rate and selectivity calculation results are as follows when reacting for one hour:

Example 1

It was sprayed into 15 mL of SAPO-34 in 40 mL of 10% acetonitrile solution at room temperature, heated to 120° C. and then dried. Put the dried SAPO-34 into a quartz tube, heat it up to 450°C under nitrogen protection in a tube furnace, keep the temperature constant for 3 hours, switch to an ammonia gas atmosphere, heat it up to 700°C at 10°C/min, and keep it at a constant temperature for 3 hours. The activation process yields a catalyst.

For the application of the catalyst, the 1,2-dichloroethane liquid is pumped into the fixed-bed reactor of the 1,2-dichloroethane cracking catalyst prepared in this example, the reactor temperature is 450°C, and the space velocity is 80h ^-1 .

The deactivated catalyst was calcined in the air at 750° C. for 3 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 2

In 40 mL of aqueous solution at room temperature, 20 g of ammonium nitrate was added under stirring, and after dissolving, 60 mL of CoAPO-50 was added to the beaker for ion exchange for 6 hours, washed to remove excess liquid, and heated to 100 ° C for drying. The dried CoAPO-50 was put into a muffle furnace, and the temperature in the muffle furnace was heated to 750° C. under an air atmosphere, and the activation process was carried out at a constant temperature for 6 hours to obtain a catalyst.

The application of the catalyst, the 1,2-dichloroethane is brought into the fixed bed reactor of the 1,2-dichloroethane cracking catalyst by means of nitrogen carrying the saturated steam of dichloroethane, the reactor temperature is 220 ℃, the space velocity 0.1h ^-1 .

The deactivated catalyst was calcined in air at 400° C. for 32 hours, and the obtained phospho-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 3

Add 20 g of ammonium oxalate to 50 mL of aqueous solution at room temperature, add 20 g of ammonium oxalate under stirring, dissolve and then immerse it into 10 mL of AIPO-5, filter and wash to remove excess liquid, and heat up to 110 ° C for drying. The dried AIPO-5 was put into a muffle furnace, and the temperature in the muffle furnace was heated to 850° C. under a nitrogen atmosphere, and the activation process was carried out at a constant temperature for 3 hours to obtain a catalyst.

Application of catalyst, 1,2-dichloroethane is brought into the fixed-bed reactor of 1,2-dichloroethane cracking catalyst by means of saturated steam carried by helium gas, the reactor temperature is 300℃, and the space velocity is 40h ^{- 1} .

The deactivated catalyst was calcined in the air at 550° C. for 8 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 4

Spray 40 mL of 25% tetramethyl ammonium hydroxide into 40 mL of SAPO-47, and heat up to 140°C for drying. The dried SAPO-47 was put into a quartz tube, heated to 650°C under nitrogen protection in a tube furnace, kept at a constant temperature for 7 hours, heated to 700°C at 10°C/min, and was activated at a constant temperature for 8 hours to obtain a catalyst.

The application process is the same as that in Example 1, except that the reactor temperature is 350°C and the space velocity is 0.5h ^-1 .

The deactivated catalyst was calcined in air at 800° C. for 16 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 5

30 mL of 25% monoammonium glycyrrhizate solution was prepared, ion-exchanged into 22 mL of AlPO ₄ -11, washed and filtered to remove excess liquid, and the temperature was raised to 130° C. for drying. Put the dried AlPO ₄ -11 into a quartz tube, heat up to 550°C under nitrogen protection in a tube furnace, keep the constant temperature for 3 hours, switch to an ammonia gas atmosphere, heat up to 800°C at 20°C/min, and keep the constant temperature for 4 hours The activation process is carried out to obtain a catalyst. .

The application process is the same as that in Example 2, except that the reactor temperature is 350°C and the space velocity is 50h ^-1 .

The deactivated catalyst was calcined in air at 600° C. for 9 hours, and the obtained phospho-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 6

10mL of 25% hydroxylamine hydrochloride aqueous solution was prepared, ion-dipped into 50mL of ZnAPSO-39, filtered to remove excess liquid, and heated to 110°C for drying. The dried ZnAPSO-39 was put into a muffle furnace, and the temperature in the muffle furnace was heated to 450° C. under an air atmosphere, and the activation process was carried out at a constant temperature for 3.5 hours to obtain a catalyst.

The application process is the same as that in Example 3, except that the reactor temperature is 250°C and the space velocity is 15h ^-1 .

The deactivated catalyst was calcined in the air at 300° C. for 40 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 7

Configure 10 mL of 15% ammonium chloroiridate, spray it into 40 mL of SAPO-5, and heat up to 140°C for drying. The dried SAPO-5 was put into a muffle furnace, and the temperature in the muffle furnace was raised to 350° C. under a nitrogen atmosphere, and the activation process was carried out at a constant temperature for 3 hours to obtain a catalyst.

The application process is the same as that in Example 1, except that the reactor temperature is 350°C and the space velocity is 0.5h ^-1 .

The deactivated catalyst was calcined in air at 800° C. for 16 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 8

Prepare 30 mL of 25% ammonium uric acid solution, ion-exchange into 22 mL of SAPO-11, heat up to 110° C. and then dry. Put the dried SAPO-11 into a quartz tube, heat up to 550°C under nitrogen protection in a tube furnace, keep the temperature constant for 3 hours, switch to an ammonia gas atmosphere, heat up to 800°C at 30°C/min, and keep the temperature constant for 3 hours. The activation process yields a catalyst.

The application process is the same as that in Example 2, except that the reactor temperature is 360°C and the space velocity is 43h ^-1 .

The deactivated catalyst was calcined in air at 440° C. for 18 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier after regeneration according to the above catalyst preparation process, and the activity did not decrease.

Example 9

Prepare 40 mL of 25% ammonium sulfate solution, spray it into 40 mL of AIPO-14, heat it up to 100°C, and then dry it. The dried AIPO-14 was put into a quartz tube, heated to 350°C under nitrogen protection in a tube furnace, kept at a constant temperature for 4 hours, heated to 500°C at 1°C/min, and was activated at a constant temperature for 6 hours to obtain a catalyst.

The application process is the same as that in Example 3, except that the reactor temperature is 370°C and the space velocity is 45h ^-1 .

The deactivated catalyst was calcined in the air at 750° C. for 12 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 10

33mL of 25% pyrrole solution was prepared, ion-exchanged into 22mL of SAPO-35, heated to 110°C and then dried. Put the dried SAPO-35 into a quartz tube, heat it up to 650°C under nitrogen protection in a tube furnace, keep the temperature constant for 4 hours, switch to an ammonia gas atmosphere, heat it up to 500°C at 3°C/min, and keep it at a constant temperature for 10 hours. The activation process yields a catalyst.

The application process is the same as that in Example 1, except that the reactor temperature is 400°C and the space velocity is 86h ^-1 .

The deactivated catalyst was calcined at 600° C. for 8 hours in the air, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 11

The preparation method was the same as that of Example 1, except that 58 mL of 25% sodium ammonium phosphate solution was sprayed into 40 mL of SAPO-18.

The application process is the same as that in Example 2, except that the reactor temperature is 245°C and the space velocity is 77h ^-1 .

The deactivated catalyst was calcined at 400° C. for 12 hours in the air, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 12

47 mL of 25% ammonium lactate solution was prepared, and ion exchanged into 22 mL of SAPO-31. The preparation method was the same as that of Example 2.

The application process is the same as that in Example 3, except that the reactor temperature is 270°C and the space velocity is 83h ^-1 .

The deactivated catalyst was calcined at 300° C. for 10 hours in the air, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 13

The preparation method was the same as in Example 3, except that 18 mL of 25% ammonium dichromate solution was sprayed into 40 mL of SAPO-37.

The application process is the same as that in Example 1, except that the reactor temperature is 290°C and the space velocity is 30h ^-1 .

The deactivated catalyst was calcined in the air at 450° C. for 11 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above-mentioned catalyst preparation process, and the activity did not decrease.

Example 14

13mL of 25% ammonium bicarbonate solution was prepared and ion-exchanged into 22ml of MgAPSO-31. The preparation method was the same as that of Example 4.

The application process is the same as that in Example 2, except that the reactor temperature is 270°C and the space velocity is 4h ^-1 .

The deactivated catalyst was calcined at 700° C. for 8 hours in the air, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 15

The preparation method was the same as in Example 5, except that it was sprayed into 40 mL of AIPO-16 in 40 mL of 8% ammonium octamolybdate solution.

The application process is the same as that of Example 3, except that the reactor temperature is 260°C and the space velocity is 1.5h ^-1 .

The deactivated catalyst was calcined in the air at 350° C. for 16 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 16

10 mL of 27% monoammonium glycyrrhizate solution was prepared, and ion exchanged into 22 mL of AlPO-20. The preparation method was the same as that of Example 6.

The application process is the same as that in Example 1, except that the reactor temperature is 310°C and the space velocity is 6h ^-1 .

The deactivated catalyst was calcined in air at 650° C. for 9 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 17

The preparation method was the same as in Example 7, except that 23 mL of 33% hydrated ammonium ferrocyanide solution was sprayed into 40 mL of MnAPSO-11.

The application process is the same as that in Example 2, except that the reactor temperature is 320°C and the space velocity is 0.9h ^-1 .

The deactivated catalyst was calcined in the air at 550° C. for 5 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

Example 18

34 mL of 5% ammonium succinate solution was prepared and ion exchanged into 22 mL of SAPO-39. The preparation method was the same as that of Example 8.

The application process is the same as that of Example 3, except that the reactor temperature is 220°C and the space velocity is 17h ^-1 .

The deactivated catalyst was calcined in air at 800° C. for 2 hours, and the obtained phosphorus-aluminum molecular sieve was used as a carrier and then regenerated according to the above catalyst preparation process, and the activity did not decrease.

The above are only a few embodiments of the present application, and are not intended to limit the present application in any form. Although the present application is disclosed as above with preferred embodiments, it is not intended to limit the present application. Without departing from the scope of the technical solution of the present application, any changes or modifications made by using the technical content disclosed above are equivalent to equivalent implementation cases and fall within the scope of the technical solution.

Claims (10)

1. The catalyst for preparing vinyl chloride by cracking 1, 2-dichloroethane is characterized in that the catalyst is a supported catalyst and comprises a nitrogen-containing active component and a carrier;

the carrier is selected from at least one of a silicon-phosphorus-aluminum molecular sieve or a phosphorus-aluminum molecular sieve;

the nitrogen-containing active component is obtained by loading a nitrogen source on the carrier and carrying out heat treatment in an oxygen-containing atmosphere or a nitrogen-containing atmosphere.

2. The catalyst for cracking 1, 2-dichloroethane to produce vinyl chloride according to claim 1, characterized in that said nitrogen source is at least one selected from the group consisting of organic substances containing nitrogen elements and ammonium salts;

preferably, the nitrogen source is selected from the group consisting of ammonia, hydrazine, acetonitrile, cyanamide, pyridine, pyrrole, ethylenediamine, methylamine, tetramethylammonium hydroxide, tetraethylammonium hydroxide, tetrapropylammonium hydroxide, tetrabutylammonium hydroxide, ammonium chloride, ammonium persulfate, ammonium dimolybdate, ammonium lactate, ferric ammonium oxalate, ammonium heptamolybdate, ammonium chloroplatinate, ammonium ureanate, ammonium chloroplatinate, ammonium chromate, ammonium fluoroborate, ammonium metavanadate, ammonium formate, ammonium sulfamate, ammonium tetrachloroaurate, ammonium hexabromoplatinate, water-soluble ammonium polyphosphate, ammonium phosphomolybdate, ammonium oxalate, ammonium dihydrogenate, ferric ammonium ferrocyanide sulfate, ammonium hexahydrate, ammonium phosphomolybdate, ammonium fluorotitanate, sodium ammonium phosphate, monoammonium glycyrrhizinate, ammonium bicarbonate, ammonium stearate, ammonium dichromate, ammonium tellurate, ammonium octamolybdate, ammonium palladate, ammonium lignosulfonate, ammonium trifluoroacetate, ammonium orthophthalate, ammonium phosphate, ammonium hydrogen phosphate, ammonium fluotitanate, ammonium hydrogen phosphate, ammonium glycyrrhizinate, ammonium hydrogen carbonate, ammonium stearate, ammonium dichromate, ammonium molybdate, ammonium octamolybdate, ammonium chloride, ammonium lignosulfonate, ammonium trifluoroacetate, ammonium phthalate, Ammonium hexafluorogermanate, ammonium paratungstate, ammonium chloroiridate, ammonium chloroosmium, ammonium chlororuthenate, ammonium carbonate, diammonium arsenate, ammonium polyacrylate, ammonium tetrathiomolybdate, ammonium succinate, ammonium iodate, ammonium perrhenate, ammonium ferrocyanide hydrate, ammonium molybdate, ammonium sulfate, ammonium titanyl oxalate, ammonium phosphotungstate, ammonium nitrate, ammonium chlororhodate, ammonium oxalate, diammonium glycyrrhizinate, ammonium hexachloroiridate, ammonium oxalate, ammonium chlorotaurinate, ammonium dodecaborate, ammonium sebacate tetrahydrate, ammonium polyphosphate, chlorphenamine phosphate, ammonium tetramolybdate, ammonium polyphosphate, ammonium tetrathiotungstate, ammonium violate, food grade ammonium acetate, ammonium molybdate solution, monoammonium glycyrrhizinate, ammonium hydrogen lactate, ammonium bicecanate, ammonium phosphotungstate, ammonium acetate, or ammonium hydroxylammonium hydrochloride, or at least one nitrogen-containing substance of any of the foregoing nitrogen-containing substance derivatives.

3. The catalyst for preparing vinyl chloride by cracking 1, 2-dichloroethane according to claim 1, wherein the carrier is at least one selected from the group consisting of SAPO-5, SAPO-11, SAPO-18, SAPO-31, SAPO-34, SAPO-35, SAPO-37, SAPO-39, SAPO-41, SAPO-47, MgAPSO-31, MnAPSO-11, CoAPO-50, ZnAPSO-39, CoAPSO-47, AlPO-5, AlPO-11, AlPO-14, AlPO-16 and AlPO-20.

4. A process for preparing a catalyst for vinyl chloride production by cracking 1, 2-dichloroethane according to any one of claims 1 to 3, comprising the steps of:

firstly, loading a nitrogen source on a carrier, and then carrying out heat treatment in a nitrogen-containing atmosphere or an oxygen-containing atmosphere; thus obtaining the supported catalyst;

the heat treatment temperature is 200-1000 ℃, and the heat treatment time is 2-48 hours.

5. The method according to claim 4, wherein the supporting is carried out by dipping, ion exchange or spraying.

6. The method according to claim 4, wherein the oxygen-containing atmosphere is an oxygen-containing gas or a mixture of an oxygen-containing gas and nitrogen or an inert gas; the oxygen-containing gas is selected from air and oxygen;

the nitrogen-containing atmosphere is a nitrogen-containing gas or a mixture of a nitrogen-containing gas and an inert gas; the nitrogen-containing gas is at least one of ammonia gas, nitrogen gas and organic amine gas.

7. The process for regenerating a catalyst for the preparation of vinyl chloride by cracking 1, 2-dichloroethane according to any one of claims 1 to 3, wherein the catalyst is used to obtain a deactivated catalyst after deactivation of the reaction for preparing vinyl chloride by cracking 1, 2-dichloroethane;

the deactivated catalyst is calcined in an oxidizing atmosphere and used as a carrier to prepare a regenerated catalyst according to the method of any one of claims 4 to 6.

8. The regeneration process according to claim 7, wherein the oxidizing atmosphere is oxygen, a mixture of oxygen and nitrogen or an inert atmosphere gas, or air; the inert atmosphere gas is one or more than two of argon or helium; the oxygen content in the oxidizing atmosphere is 1-100% by mass.

9. The regeneration method according to claim 7, wherein the roasting temperature is 300 ℃ to 1000 ℃; the treatment time is 2-48 hours.

10. Use of the catalyst for the cracking of 1, 2-dichloroethane to produce vinyl chloride according to any one of claims 1 to 3 for catalyzing the cracking of 1, 2-dichloroethane to produce vinyl chloride.