CN112919444A - Method and device for co-processing organic fluorine and terpene residual liquid through plasma cracking - Google Patents
Method and device for co-processing organic fluorine and terpene residual liquid through plasma cracking Download PDFInfo
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Abstract
The invention belongs to the technical field of chemical waste treatment, and particularly discloses a method for cooperatively treating organic fluorine residual liquid and terpene residual liquid by adopting plasma cracking, and also discloses a device for treatment. The method for cooperatively treating the organic fluorine and terpene residual liquid by adopting the plasma cracking comprises the steps of mixing the organic fluorine residual liquid and the terpene residual liquid according to a ratio, and carrying out cracking in an oxygen-free environment under the action of plasma high-temperature electric arc, so that carbon black and hydrogen fluoride gas can be obtained through reaction. The method not only realizes the comprehensive synergistic treatment of the organic fluorine and the terpene residual liquid, but also prepares the carbon black product with high purity and obtains the byproduct hydrofluoric acid, thereby having good economic and environmental benefits.
Description
Technical Field
The invention relates to the technical field of chemical waste treatment, in particular to a method and a device for cooperatively treating organic fluorine residual liquid and terpene residual liquid by adopting plasma cracking.
Background
Organic fluorine raffinate and terpene raffinate are the main wastes generated in the fluoropolymer industry. The waste liquid generated in the process of producing the organic fluorine polymer is organic fluorine residual liquid, and the common method for treating the organic fluorine residual liquid at present is incineration treatment. The disadvantages of incineration treatment are incomplete incineration, high energy consumption, secondary pollution, and easy generation of dioxin. Plasma cracking has been reported to treat organic fluorine waste. For example, patent application publication No. CN109798531A discloses a method for treating organic fluorine raffinate by plasma cracking, in which the organic fluorine raffinate is mixed with compressed air to crack, and hydrogen fluoride gas is generated by cracking. However, due to the presence of compressed air, carbon dioxide gas and a small amount of nitrogen oxide are generated, which is harmful to the environment.
The terpene raffinate is derived from terpenes added to prevent polymerization of tetrafluoroethylene monomer. Since high-purity tetrafluoroethylene is easily self-polymerized, an effective method is to add a certain amount of polymerization inhibitor in order to prevent self-polymerization of tetrafluoroethylene monomer. For example, terpenoids are added as polymerization inhibitors to the rectification column and the tetrafluoroethylene storage tank. However, terpenes are only slightly soluble in tetrafluoroethylene, about 500ppm at 25 ℃ and 50ppm at-45 ℃, so that polymerization inhibitors are generally added from the top of the column, and the terpenes that are insoluble in tetrafluoroethylene settle at the bottom of the column during distillation, resulting in a residual terpene liquid. At present, the common method for treating the residual terpene liquid is incineration, but the defects of incomplete incineration, high energy consumption, secondary pollution, easy generation of dioxin and the like exist.
In addition, the organic fluorine residual liquid and the terpene residual liquid are treated as wastes in a harmless way at present, and no economic value is created.
Disclosure of Invention
The invention mainly solves the technical problem of providing a method for the plasma cracking synergistic treatment of organic fluorine and terpene residual liquid and also provides a device for treatment.
In order to solve the technical problems, the invention adopts a technical scheme that: a method for co-processing organic fluorine and terpene raffinate by plasma cracking comprises the following steps: mixing the organic fluorine residual liquid and the terpene residual liquid, cracking under the action of plasma high-temperature electric arc in an oxygen-free environment, and reacting to obtain carbon black and hydrogen fluoride gas.
In a preferred embodiment, the plasma high-temperature arc temperature is 2000-2500 ℃.
Preferably, the ratio of the organic fluorine residual liquid to the terpene residual liquid is 30-40 kg/h: 13-17 kg/h. The main component C of the organic fluorine residual liquid treated by the inventionnF2nThe weight percentage of the component (A) is 90-95%, and the component (B) mainly comprises octafluorocyclobutane, perfluoropropylene and a small amount of chlorodifluoromethane; the main component C in the treated terpene residual liquid10H16The weight percentage of the components is about 80 percent, and the others are heavy components and a small amount of water. The organic fluorine residual liquid can be tetrafluoroethylene residual liquid, hexafluoropropylene residual liquid and the like.
As a preferred embodiment, the cracking reaction is carried out in a cracking furnace, the pressure in the cracking furnace is-300 to-900 Pa, and the reaction temperature of the cracking section of the cracking furnace is controlled to be 1400 to 2000 ℃.
Preferably, the flow rate of the organic fluorine residual liquid entering the cracking furnace is controlled to be 30-40 kg/h, and the flow rate of the terpene residual liquid entering the cracking furnace is controlled to be 13-17 kg/h.
Further, the processing method provided by the invention comprises the following steps:
(1) heating the plasma arc to 2000-2500 ℃, and then introducing organic fluorine residual liquid and terpene residual liquid at the same time, wherein the ratio of the organic fluorine residual liquid to the terpene residual liquid is 30-40 kg/h and 13-17 kg/h; in an oxygen-free environment, mixing the organic fluorine residual liquid and the terpene residual liquid in a plasma arc high-temperature region for cracking, keeping the reaction temperature in a cracking section at 1400-2000 ℃, controlling the pressure in a cracking furnace at-300-900 Pa, and cracking to generate carbon black and hydrogen fluoride gas;
(2) discharging the carbon black generated by cracking from a discharge outlet at the bottom of the cracking furnace; and (4) discharging hydrogen fluoride gas generated by cracking from a tail gas outlet of the cracking furnace, and then washing and cooling to obtain a hydrofluoric acid product.
The invention also provides a device for the plasma cracking synergistic treatment of the organic fluorine and terpene residual liquid, which comprises a cracking furnace, wherein the cracking furnace is provided with a vertical cylindrical furnace body, and the furnace body comprises a high-temperature area arranged at the upper section of the furnace body and a low-temperature area arranged at the lower part of the high-temperature area; a plasma spray gun is vertically arranged at the center of the upper end surface of the furnace body, and the port of the plasma spray gun is arranged in a high-temperature area in the furnace body; the upper end surface of the furnace body is also respectively provided with an organic fluorine residual liquid feeding pipe and a terpene residual liquid feeding pipe, the organic fluorine residual liquid feeding pipe and the terpene residual liquid feeding pipe are arranged at two sides of the plasma spray gun and are symmetrically arranged, and the pipe orifices of the organic fluorine residual liquid feeding pipe and the terpene residual liquid feeding pipe face to the port of the plasma spray gun, so that the organic fluorine residual liquid and the terpene residual liquid are crossed and mixed in a plasma high-temperature arc area generated by the plasma spray gun; a tail gas outlet is arranged on the side wall of the furnace body positioned in the low-temperature region, and the tail gas outlet is sequentially connected with the water washing device and the alkali washing device in series; the bottom of furnace body is provided with the bin outlet, the bin outlet corresponds and is provided with material collecting device.
As a preferred embodiment, the organic fluorine residual liquid feeding pipe and the terpene residual liquid feeding pipe are respectively arranged at an included angle of 45 degrees with the side wall of the furnace body.
Preferably, the pipe diameter ratio of the organic fluorine raffinate feeding pipe to the terpene raffinate feeding pipe is 2.5: 1.
Preferably, the organic fluorine raffinate feeding pipe and the terpene raffinate feeding pipe are both made of common carbon steel.
The invention provides a method for cooperatively treating organic fluorine and terpene residual liquid by adopting plasma cracking. The method not only realizes the comprehensive synergistic treatment of the organic fluorine and the terpene residual liquid, but also prepares the carbon black product with high purity and obtains the byproduct hydrofluoric acid, thereby having good economic and environmental benefits.
The method of the invention is that under the oxygen-free environment, namely under the condition of not introducing compressed air, the main wastes of organic fluorine residual liquid and terpene residual liquid generated in the fluoropolymer industry are proportioned according to a proper proportion and then are directly cracked under the action of plasma high-temperature electric arc. The main component of the organic fluorine raffinate is CnF2nThe main component of the terpene residual liquid is C10H16The cracking is carried out at high temperature, chemical bonds of the organic matters can be completely broken, the organic fluorine residual liquid is cracked into carbon and fluorine, the terpene residual liquid is cracked into carbon and hydrogen, then the fluorine and the hydrogen rapidly react into hydrogen fluoride in a low-temperature area at the lower part of a cracking furnace under the anaerobic condition, and the simple substance carbon is separated out. The invention has the following advantages:
firstly, because compressed air is not required to be introduced, the high-temperature cracking is carried out in an oxygen-free environment, and the purity of the prepared carbon black is high;
the yield of the carbon black is high, the energy utilization efficiency can be greatly improved when the carbon black is produced by the method, and the carbon in the raw materials can be completely harvested under an ideal condition;
compared with the prior method for treating the organic fluorine residual liquid and the terpene residual liquid under the aerobic condition, the method for cracking the organic fluorine residual liquid and the terpene residual liquid under the anaerobic condition does not generate CO2And NOxGases, thus reducing the emission of greenhouse and harmful gases.
Carbon black is widely used in rubber, printing ink, paint, plastic, electronic components and other industrial fieldsApplication, and the demand for carbon black is steadily increasing year by year, it is expected that the annual demand for carbon black will exceed 1800 million tons by the year 2020. China is a large country for producing carbon black, and the yield of the carbon black accounts for 41 percent of the global yield. Furnace carbon black is now the most common mode of carbon black production, and this production process has been used for over 60 years. However, the furnace carbon black always has the problems of low yield and high energy consumption, and a large amount of CO exists2And NOxAnd (5) discharging. The plasma method has the characteristics of high temperature and high enthalpy, so that the heating efficiency is high, the advantage of the thermal efficiency is more obvious along with the rise of the reaction temperature, meanwhile, the method can break through the limitation of the reaction temperature of furnace carbon black, and has remarkable advantages in the preparation of novel carbon materials. In the current method for producing carbon black, raw materials account for a large part of the cost. The invention uses the waste organic fluorine residual liquid and terpene residual liquid generated in the fluoropolymer industry as raw materials, changes waste into valuable, does not generate greenhouse gases, dioxin and oxynitride polluting the environment, can be used as a new carbon black preparation way, and has good economic and environmental benefits.
Drawings
FIG. 1 is a schematic diagram of a plasma cracking co-processing apparatus for organic fluorine and terpene raffinate according to the present invention;
in the figure: 1-cracking furnace, 2-high temperature zone, 3-low temperature zone, 4-plasma spray gun, 5-organic fluorine raffinate inlet pipe, 6-terpene raffinate inlet pipe, 7-tail gas outlet, 8-first-stage water washing device, 9-second-stage water washing device, 10-alkali washing device, 11-discharge outlet and 12-material receiving device.
Detailed Description
The technical solution of the present invention will be explained in detail below.
Example 1
As shown in fig. 1, the device for co-processing organic fluorine and terpene residual liquid by plasma cracking provided in this embodiment includes a cracking furnace 1, the cracking furnace 1 has a vertical cylindrical furnace body, the furnace body includes a high temperature region 2 disposed at an upper section of the furnace body and a low temperature region 3 disposed at a lower section of the high temperature region; the center of the upper end surface of the furnace body is vertically provided with a plasma torch 4, and the port of the plasma torch 4 is arranged in the high-temperature area 2 in the furnace body. The plasma is generated by using a plasma torch or a plasma beam generated between electrodes to generate high temperature, the plasma torch or the plasma beam can be generated by using methods of alternating current, direct current, power frequency, high frequency and the like, the arc core temperature is very high, and the high temperature can be instantly realized. And starting a power supply, and striking an arc at the port of the plasma torch 4 by current to form a high-temperature arc region.
The upper end surface of the furnace body is also provided with an organic fluorine residual liquid feeding pipe 5 and a terpene residual liquid feeding pipe 6 respectively, the organic fluorine residual liquid feeding pipe 5 and the terpene residual liquid feeding pipe 6 are arranged at two sides of the plasma spray gun 4 and are symmetrically arranged, and the pipe orifices of the organic fluorine residual liquid feeding pipe 5 and the terpene residual liquid feeding pipe 6 face the port of the plasma spray gun 4, so that the organic fluorine residual liquid and the terpene residual liquid are mixed in a crossed manner in a plasma high-temperature arc area generated by the plasma spray gun.
A tail gas outlet 7 is arranged on the side wall of the furnace body positioned in the low-temperature zone 3, and the tail gas outlet 7 is sequentially connected with a water washing device and an alkali washing device 10 in series; the water washing device is divided into two stages and is formed by connecting a first-stage water washing device 8 and a second-stage water washing device 9 in series, wherein the first-stage water washing device 8 is connected with the tail gas outlet 7, and the second-stage water washing device 9 is connected with the alkali washing device 10 in series.
The bottom of the furnace body is provided with a discharge outlet 11, and the bottom of the furnace body is set to be a cone with a large opening upwards for discharging convenience. A material receiving device 12 is arranged corresponding to the discharge opening 11 and used for collecting carbon black products discharged from the discharge opening 11.
Wherein the organic fluorine residual liquid feeding pipe 5 and the terpene residual liquid feeding pipe 6 are preferably arranged to form an included angle of 45 degrees with the side wall of the furnace body, so that the organic fluorine residual liquid and the terpene residual liquid are more favorably intersected and mixed in a plasma high-temperature arc area generated by the plasma spray gun 4, the mixing is more sufficient, and the reaction is more thorough.
The pipe diameter ratio of the organic fluorine residual liquid feeding pipe 5 to the terpene residual liquid feeding pipe 6 is 2.5:1, the feeding amount can be controlled, and the complete cracking is ensured. The organic fluorine residual liquid feeding pipe 5 and the terpene residual liquid feeding pipe 6 are both made of common carbon steel.
The method for carrying out the plasma cracking synergistic treatment on the organic fluorine and the terpene raffinate by using the device of the embodiment comprises the following operations:
(1) starting a power supply, striking an arc at the port of the plasma spray gun 4 by current to form a high-temperature arc region, and simultaneously introducing organic fluorine residual liquid and terpene residual liquid through an organic fluorine residual liquid feeding pipe 5 and a terpene residual liquid feeding pipe 6 when the temperature of the plasma arc rises to 2000-2500 ℃; in an oxygen-free environment, mixing organic fluorine residual liquid and terpene residual liquid in a plasma arc high-temperature region 2 for cracking, keeping the reaction temperature in a cracking section (namely a high-temperature region) at 1400-2000 ℃, controlling the pressure in a cracking furnace at-300-900 Pa, cracking the organic fluorine residual liquid into carbon and fluorine, cracking the terpene residual liquid into carbon and hydrogen, then, in a low-temperature region at the lower part of the cracking furnace, rapidly reacting the fluorine and the hydrogen into hydrogen fluoride under the oxygen-free condition, and separating out simple substance carbon, namely, cracking to generate carbon black and hydrogen fluoride gas;
(2) discharging the carbon black generated by cracking from a discharge port 11 at the lower end of the cracking furnace, and collecting the carbon black in a material receiving device 12; hydrogen fluoride gas generated by cracking is discharged from a tail gas outlet 7 of the cracking furnace, and then is washed by a primary washing device 8 and a secondary washing device 9 in sequence, the cracking tail gas HF is absorbed by the washing devices to obtain hydrofluoric acid, and the washed tail gas is neutralized and absorbed by an alkaline washing device 10.
Example 2
The tetrafluoroethylene residual liquid and the terpene residual liquid are subjected to synergistic treatment, and the method specifically comprises the following steps:
the cooperative treatment is carried out in a cracking furnace, and the negative pressure of a hearth of the cracking furnace is controlled to be-300 Pa;
and starting a power supply, striking an arc at the port of the plasma spray gun by current to form a high-temperature arc region, and introducing tetrafluoroethylene residual liquid and terpene residual liquid simultaneously when the temperature of the plasma arc rises to above 2000 ℃, wherein the mass ratio of the introduction of the tetrafluoroethylene residual liquid to the introduction of the terpene residual liquid is 30kg/h to 13 kg/h. The tetrafluoroethylene residual liquid comprises the following components: 80-95% of octafluorocyclobutane, 5-10% of perfluoroisobutylene, about 5% of tetrafluoroethylene or a polymer thereof, a small amount of chlorodifluoromethane and the like; the main component of the terpene residual liquid is C10H16And the like with the content of about 80 percent, and the others are heavy components and a small amount of water, and the heavy components are fluorine-containing compounds.
In an anaerobic environment, mixing and fully cracking tetrafluoroethylene residual liquid and terpene residual liquid in a plasma high-temperature arc region, controlling the reaction temperature of a cracking section, namely a high-temperature region, of a cracking furnace within the range of 1400-2000 ℃, cracking to obtain carbon, fluorine and hydrogen, then rapidly reacting the fluorine and the hydrogen into hydrogen fluoride in a low-temperature region at the lower part of the cracking furnace under the anaerobic condition, completely converting active fluorine generated by cracking in the high-temperature region of a hearth into hydrogen fluoride gas, separating out elemental carbon to obtain carbon black and the hydrogen fluoride gas, and not generating greenhouse gas, dioxin and oxynitride polluting the environment;
discharging the cracked carbon black product from a lower discharge port 11, and collecting the carbon black product in a material receiving device 12; hydrogen fluoride gas generated by cracking is discharged from a tail gas outlet 7 of the cracking furnace, and then is sequentially sprayed and washed by a first-stage washing device 8 and a second-stage washing device 9 in two stages, the cracking tail gas HF is absorbed by the washing devices to obtain hydrofluoric acid, the washed tail gas is finally neutralized and absorbed by an alkaline washing device 10, sodium carbonate and/or sodium sulfite aqueous solution is adopted in the alkaline washing device 10 for spraying and absorption, and HF gas which is not absorbed by water is neutralized and removed.
The collected carbon black after cracking is 12-15 kg/h. The carbon conversion is 75-90%. Water and heavy components in the raffinate affect the carbon conversion. As the cracking process is carried out in an oxygen-free environment, the carbon black ash collected after cracking is not more than 5ppm, various metal impurities are not more than 20ppb, the coarse grain content is about 0.001 percent, and the purity is very high. Absorbing HF in the cracked gas by water to obtain hydrofluoric acid meeting the relevant product standards: the content of hydrofluoric acid is more than or equal to 40 percent.
The synergistic treatment method produces good economic benefits. The burning residue is less than or equal to 0.01 percent, the content of dust fluorine and gas fluorine in the flue gas is lower than the national standard, and the method has good social benefit.
Example 3
And (3) carrying out synergistic treatment on the hexafluoropropylene residual liquid and the terpene residual liquid, wherein the method comprises the following specific steps:
the cooperative treatment is carried out in a cracking furnace, and the negative pressure of a hearth of the cracking furnace is controlled to be-900 Pa;
starting a power supply, striking an arc at the port of the plasma torch by current to form a high-temperature arc region, and simultaneously heating the plasma arc to above 2000 DEG CIntroducing hexafluoropropylene residual liquid and terpene residual liquid, wherein the mass ratio of the hexafluoropropylene residual liquid to the terpene residual liquid is 40kg/h:17 kg/h. Wherein, the hexafluoropropylene raffinate comprises: perfluoroisobutylene about 90%, octafluorocyclobutane about 10%, and a small amount of hexafluoropropylene. The main component of the terpene residual liquid is C10H16And the like with the content of about 80 percent, and the others are heavy components and a small amount of water, and the heavy components are fluorine-containing compounds.
In an anaerobic environment, mixing and fully cracking hexafluoropropylene residual liquid and terpene residual liquid in a plasma high-temperature arc region, controlling the reaction temperature of a cracking section, namely a high-temperature region, of a cracking furnace within the range of 1400-2000 ℃, cracking to obtain carbon, fluorine and hydrogen, then rapidly reacting the fluorine and the hydrogen into hydrogen fluoride in a low-temperature region at the lower part of the cracking furnace under the anaerobic condition, completely converting active fluorine generated by cracking in the high-temperature region of a hearth into hydrogen fluoride gas, separating out elemental carbon to obtain carbon black and the hydrogen fluoride gas, and not generating greenhouse gas, dioxin and oxynitride polluting the environment;
discharging the cracked carbon black product from a lower discharge port 11, and collecting the carbon black product in a material receiving device 12; hydrogen fluoride gas generated by cracking is discharged from a tail gas outlet 7 of the cracking furnace, and then is sequentially sprayed and washed by a first-stage washing device 8 and a second-stage washing device 9 in two stages, the cracking tail gas HF is absorbed by the washing devices to obtain hydrofluoric acid, the washed tail gas is finally neutralized and absorbed by an alkaline washing device 10, sodium carbonate and/or sodium sulfite aqueous solution is adopted in the alkaline washing device 10 for spraying and absorption, and HF gas which is not absorbed by water is neutralized and removed.
The collected carbon black after cracking is 15-19 kg/h. The carbon conversion is 70-85%. As perfluoroisobutylene is a highly toxic substance, in order to ensure the complete cracking of perfluoroisobutylene, the residual terpene liquid is excessive. The cracking process is carried out in an oxygen-free environment, the collected carbon black ash after cracking is not more than 5ppm, various metal impurities are not more than 20ppb, the coarse grain content is about 0.001%, and the purity is very high. Absorbing HF in the cracked gas by water to obtain hydrofluoric acid meeting the relevant product standards: the content of hydrofluoric acid is more than or equal to 40 percent.
The synergistic treatment method produces good economic benefits. The burning residue is less than or equal to 0.01 percent, the content of dust fluorine and gas fluorine in the flue gas is lower than the national standard, and the method has good social benefit.
Claims (10)
1. A method for the synergistic treatment of organic fluorine and terpene raffinate by plasma cracking is characterized by comprising the following steps: mixing the organic fluorine residual liquid and the terpene residual liquid, cracking under the action of plasma high-temperature electric arc in an oxygen-free environment, and reacting to obtain carbon black and hydrogen fluoride gas.
2. The process of claim 1, wherein the plasma high temperature arc temperature is 2000 to 2500 ℃.
3. The method according to claim 1, wherein the ratio of the organic fluorine residual liquid to the terpene residual liquid is 30-40 kg/h: 13-17 kg/h.
4. The treatment method according to any one of claims 1 to 3, wherein the cracking reaction is carried out in a cracking furnace, the pressure in the cracking furnace is-300 to-900 Pa, and the reaction temperature of the cracking section of the cracking furnace is controlled to 1400 to 2000 ℃.
5. The method according to claim 4, wherein the flow rate of the organic fluorine residue entering the cracking furnace is controlled to be 30 to 40kg/h, and the flow rate of the terpene residue entering the cracking furnace is controlled to be 13 to 17 kg/h.
6. The process of claim 5, comprising the steps of:
(1) heating the plasma arc to 2000-2500 ℃, and then introducing organic fluorine residual liquid and terpene residual liquid at the same time, wherein the ratio of the organic fluorine residual liquid to the terpene residual liquid is 30-40 kg/h and 13-17 kg/h; in an oxygen-free environment, mixing the organic fluorine residual liquid and the terpene residual liquid in a plasma arc high-temperature region for cracking, keeping the reaction temperature in a cracking section at 1400-2000 ℃, controlling the pressure in a cracking furnace at-300-900 Pa, and cracking to generate carbon black and hydrogen fluoride gas;
(2) discharging the carbon black generated by cracking from a discharge outlet at the bottom of the cracking furnace; and (4) discharging hydrogen fluoride gas generated by cracking from a tail gas outlet of the cracking furnace, and then washing and cooling to obtain a hydrofluoric acid product.
7. The device for the plasma cracking synergistic treatment of the residual organic fluorine and terpene liquid is characterized by comprising a cracking furnace, wherein the cracking furnace is provided with a vertical cylindrical furnace body, and the furnace body comprises a high-temperature area arranged at the upper section of the furnace body and a low-temperature area arranged at the lower part of the high-temperature area; a plasma spray gun is vertically arranged at the center of the upper end surface of the furnace body, and the port of the plasma spray gun is arranged in a high-temperature area in the furnace body; the upper end surface of the furnace body is also respectively provided with an organic fluorine residual liquid feeding pipe and a terpene residual liquid feeding pipe, the organic fluorine residual liquid feeding pipe and the terpene residual liquid feeding pipe are arranged at two sides of the plasma spray gun and are symmetrically arranged, and the pipe orifices of the organic fluorine residual liquid feeding pipe and the terpene residual liquid feeding pipe face to the port of the plasma spray gun, so that the organic fluorine residual liquid and the terpene residual liquid are crossed and mixed in a plasma high-temperature arc area generated by the plasma spray gun; a tail gas outlet is arranged on the side wall of the furnace body positioned in the low-temperature region, and the tail gas outlet is sequentially connected with the water washing device and the alkali washing device in series; the bottom of furnace body is provided with the bin outlet, the bin outlet corresponds and is provided with material collecting device.
8. The apparatus of claim 7, wherein the organofluorine raffinate feed line and the terpene raffinate feed line are both angled at 45 ° to the side wall of the furnace body.
9. The apparatus of claim 7 or 8, wherein the organic fluorine raffinate feed line and the terpene raffinate feed line have a tube to tube ratio of 2.5: 1.
10. The apparatus of claim 9, wherein the organofluorine raffinate feed line and the terpene raffinate feed line are both made of plain carbon steel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911242346.1A CN112919444B (en) | 2019-12-06 | 2019-12-06 | Method and device for co-processing organic fluorine and terpene residual liquid through plasma cracking |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201911242346.1A CN112919444B (en) | 2019-12-06 | 2019-12-06 | Method and device for co-processing organic fluorine and terpene residual liquid through plasma cracking |
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