CN202786058U - Industrial production device of tetrachloroethylene - Google Patents
Industrial production device of tetrachloroethylene Download PDFInfo
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- CN202786058U CN202786058U CN 201220399330 CN201220399330U CN202786058U CN 202786058 U CN202786058 U CN 202786058U CN 201220399330 CN201220399330 CN 201220399330 CN 201220399330 U CN201220399330 U CN 201220399330U CN 202786058 U CN202786058 U CN 202786058U
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Abstract
The utility model provides an industrial production device of tetrachloroethylene, which comprises a methane chloride/natural gas storage tank (11), a chlorinated methane storage tank (12) and a first chlorine gas storage tank (13) which are connected with a material feeding opening of a reactor (1) through pipelines, wherein a material outlet of the reactor (1) is connected with a quench tower (2); a lower part outlet end of the quench tower (2) is connected with a heavy component recovery system, a middle side part outlet end of the quench tower (2) is connected with a rough tetrachloroethylene storage tank (3), and an upper part outlet end of the quench tower (2) is connected with an inlet end of a condenser (4); an outlet end of the condenser (4) is connected with an inlet end of a separator (5); and inlet ends of a carbon tetrachloride storage tank (6), a second chlorine gas storage tank (7), and a methane chloride reactor (8) connected with a methanol storage tank (10) are respectively connected with an outlet end of the separator (5); and an outlet end of the methane chloride reactor (8) is connected with a methane chloride storage tank (9). The industrial production device has the advantages of high chlorine resource conversion rate.
Description
Technical field
The utility model relates to the chlor-alkali field, is specifically related to a kind of industrial production device of zellon.
Background technology
Tetracol phenixin is the controlled ODS material of Montreal Protocol on Substances that Deplete the Ozone Layer regulation.Begun to eliminate gradually and limit the use tetracol phenixin in China, the tetracol phenixin of domestic methane chloride device by-product need effectively be processed and just allow to produce, and is reasonable outlet so tetracol phenixin is converted into zellon.
Zellon is the material of environmental sound, used as clean-out system for a long time in the past, along with the quickening of eliminating the HCFC-22 process, pentafluoride ethane (HFC-125) demand rapid growth, zellon develops as the main production raw material purposes of pentafluoride ethane, and its market outlook are good.
The by-product tetracol phenixin of methane chloride production can generate zellon by pyrolysis, because the increase of zellon demand, can use methylene dichloride, trichloromethane pyrolysis to generate zellon, needs with satisfying the market, also further widened simultaneously the purposes of methylene dichloride and trichloromethane, adjust the chlorine products structure, reply methane chloride keen competition market reduces the market risk of methane chloride enterprise.
US Patent No. 1930350 is at 600-1500 ℃, US Patent No. 3364272 pyrolysis generation zellon under 800 ℃ of conditions, and its high temperature pyrolysis method will have a large amount of restructuring to divide generation, and difficult treatment is not suitable for suitability for industrialized production.
Mentioned under the condition of any one existence in monochloro methane, methane and the Sweet natural gas among the Chinese patent CN101348414A and tetracol phenixin on-catalytic method generates the method for zellon, temperature of reaction is that 500-700 ℃ of pressure is 0.1-2kg/cm
2, the method has higher transformation efficiency, and restructuring minute generation is few, but still has the HCl of a large amount of by-products to process.
Therefore, need to provide a kind of industrial production device of zellon to address the above problem.
The utility model content
The purpose of this utility model is for providing the industrial production device of the high zellon of a kind of chlorine resource utilization.
For realizing above-mentioned purpose of the present utility model, the utility model has adopted following technical proposals.
The industrial production device of zellon of the present utility model, it comprises: monochloro methane/Sweet natural gas storage tank 11, methane chloride storage tank 12 links to each other by the opening for feed of pipeline with reactor 1 with the first chlorine storage tank 13, the discharge port of described reactor 1 links to each other with quench tower 2, the lower part outlet end of described quench tower 2 links to each other with the heavy component recovery system, the middle sidepiece exit end of described quench tower 2 links to each other with thick zellon storage tank 3, the top exit end of described quench tower 2 links to each other with the inlet end of condenser 4, the exit end of described condenser 4 links to each other with the inlet end of separator 5, tetracol phenixin storage tank 6, the second chlorine storage tank 7, the inlet end of the monochloro methane reactor 8 that links to each other with methyl alcohol storage tank 10 links to each other with the exit end of described separator 5 respectively, the exit end of described monochloro methane reactor 8 links to each other with monochloro methane storage tank 9, tetracol phenixin in the described tetracol phenixin storage tank 6 can add to methane chloride storage tank 12 and recycle, and the chlorine in described the second chlorine storage tank 7 can add to the first chlorine storage tank 13 and recycle.
Wherein, tetracol phenixin storage tank 6 can be linked to each other with methane chloride storage tank 12, the second chlorine storage tank 7 links to each other with the first chlorine storage tank 13.
The method of utilizing the industrial production device of the zellon that the utility model provides to produce zellon is: adopt monochloro methane or Sweet natural gas and excessive chlorine and methane chloride: several methane chlorides of wherein any one or arbitrary proportion in methylene dichloride, trichloromethane, the tetracol phenixin are raw material, reaction production zellon.
The mixture that also can contain in a small amount of trieline, ethylene dichloride, pentaline, hexachloroethane and the hexachlorobutadiene any one or a few in the described methane chloride.
Reaction process is: with Sweet natural gas (or monochloro methane), chlorine and methane chloride are sent in the reactor 1 after mixing, temperature of reaction maintains 560-620 ℃, reaction pressure is 0.05-0.22Mpa, reaction generates zellon, reaction mixture is shifted out reactor 1 rapidly to quench tower 2, the light constituent tetracol phenixin, hydrogenchloride and chlorine are discharged from quench tower 2 tops, wherein tetracol phenixin and excessive chlorine loop back reactor 1, hydrogen chloride absorption can be used for synthetic monochloro methane after becoming hydrochloric acid, as the raw material of synthetic PCE or as the raw material of producing methylene dichloride and trichloromethane.Thick zellon rectification and purification again after sidepiece is discharged from quench tower 2.Heavy component loops back reactor 1 regeneration zellon after vaporization, but the waste residue barrelling is taken out.
Several large important factor of impact reaction is: the excessive amount of temperature of reaction, reaction pressure, the residence time and chlorine.
The height of temperature of reaction can determine the transformation efficiency of zellon growing amount, restructuring minute growing amount and methane chloride.Reaction temperature is spent low, the low conversion rate of methane chloride, and namely the growing amount of zellon is few; Temperature of reaction is too high, and the growing amount of heavy component is large; When temperature of reaction (hottest point) maintained 560-620 ℃, the transformation efficiency of methane chloride was the highest, and the zellon that namely generates is maximum, and the by product growing amount is minimum.
The excessive amount of chlorine also can affect the transformation efficiency of tetracol phenixin, and chlorine is excessive too large, and the amount that methane chloride changes into zellon is just few, and chlorine is crossed quantity not sufficient, generates easily carbon black.The volume percent of chlorine is that 3%-7% is comparatively suitable in reaction mixture gas.
Reaction pressure is lower, and is more favourable to reaction, more is conducive to the generation of zellon.
The residence time determines by producing load, more is conducive to the generation of zellon when the residence time is 15s.
Reaction mechanism when using monochloro methane is:
CH
3Cl+3Cl
2 →CCl
4 +3HCl （1）
2CCl
4 C
2Cl
4 +2Cl
2 （2）
CH
3Cl+Cl
2 +CCl
4 → C
2Cl
4 +3HCl （3）
Reaction mechanism when using Sweet natural gas (methane) is:
CH
4+4Cl
2 → CCl
4 + 4HCl （1）
2CCl
4 C
2Cl
4 + 2Cl
2 （2）
CH
3Cl+Cl
2 +CCl
4 → C
2Cl
4 + 4HCl （3）
The mechanism that generates zellon take methylene dichloride or trichloromethane as raw material reaction as:
CH3Cl+CH2Cl2+3Cl2→C2Cl4+5HCl （1）
CH3Cl+CHCl3+2Cl2→C2Cl4+4HCl （2）
2CCl
4 C
2Cl
4 + 2Cl
2 （3）
The transformation mechanism that restructuring divides is:
The useful component such as zellon will be regenerated after the restructuring lease making vaporization in the useful component Returning reactors such as pentaline, hexachloroethane and hexachlorobutadiene.
C
2H
4Cl
2 + 4 Cl
2 C
2Cl
6 + 4 HCl
C
2Cl
6 C
2Cl
4 + Cl
2
C
4Cl
6 + 5 Cl
2 4 CCl
4
2 C
2H
4Cl
2 + 5 Cl
2 C
4Cl
6 + 8 HCl
C
2HCl
3+ Cl
2 → C
2HCl
5 + HCl
C
2HCl
5 → CCl
4 + HCl
The industrial production device of zellon of the present utility model can synthesize zellon under high temperature, low pressure, the transformation efficiency of raw material is high, the restructuring lease making that generates is crossed decomposition can generate zellon by Returning reactor, the hydrogenchloride of by-product can be converted into monochloro methane and supply with methane chloride device or synthetic zellon device as raw material, has realized the maximum utilization of chlorine resource.
Description of drawings
Fig. 1 is the synoptic diagram of the industrial production device of zellon of the present utility model.
Reference numeral
Embodiment
Below by exemplary embodiments, the utility model is further specified, but the utility model is not limited to described embodiment.
Referring to Fig. 1, the industrial production device of zellon of the present utility model, wherein: monochloro methane/Sweet natural gas storage tank 11, methane chloride storage tank 12 links to each other by the opening for feed of pipeline with reactor 1 with the first chlorine storage tank 13, the discharge port of described reactor 1 links to each other with quench tower 2, the lower part outlet end of described quench tower 2 links to each other with the heavy component recovery system, the middle sidepiece exit end of described quench tower 2 links to each other with thick zellon storage tank 3, the top exit end of described quench tower 2 links to each other with the inlet end of condenser 4, the exit end of described condenser 4 links to each other with the inlet end of separator 5, tetracol phenixin storage tank 6, the second chlorine storage tank 7, the inlet end of the monochloro methane reactor 8 that links to each other with methyl alcohol storage tank 10 links to each other with the exit end of described separator 5 respectively, the exit end of described monochloro methane reactor 8 links to each other with monochloro methane storage tank 9, tetracol phenixin in the described tetracol phenixin storage tank 6 can add to methane chloride storage tank 12 and recycle, and the chlorine in described the second chlorine storage tank 7 can add to the first chlorine storage tank 13 and recycle.
Adopt the embodiment of the industrial production device production zellon of zellon of the present utility model to be:
Embodiment 1: the embodiment when using Sweet natural gas.
With Sweet natural gas (normal temperature) 130Nm
3/ h, excessive chlorine (85 ℃) 0.9-1.1t/h, overheated tetracol phenixin steam (240 ℃) 2.5-3.0 t/h, introduce reactor 1, make temperature of reaction maintain 550-600 ℃, reaction generates zellon under the condition of reaction pressure 0.1-0.15Mpa, and product is the thick zellon of about 1.18 t/h and 520 Nm
3/ h hydrogenchloride, reaction mixture are shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, the restructuring after separating divides from quench tower 2 shifts out, and loops back reactor 1 after the recovery.
Embodiment 2: the embodiment take monochloro methane, tetracol phenixin and chlorine as raw material.
With monochloro methane (20-40 ℃) 180Nm
3/ h, excessive chlorine (85 ℃) 0.9-1.1t/h, overheated tetracol phenixin steam (240 ℃) 2.5-3.0 t/h, introduce reactor 1, make temperature of reaction maintain 550-620 ℃, under the condition of reaction pressure 0.1-0.15Mpa, reaction generates zellon, and product is the thick zellon of about 1.21 t/h and 540 Nm
3/ h hydrogenchloride, reaction mixture is shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, after reaction gas cools off in quench tower 2, light constituent hydrogenchloride and tetracol phenixin are gone out from the cat head of quench tower 2, and thick zellon goes rectification and purification again from quench tower 2 side line extraction, restructuring divides shifts out from quench tower 2, loops back reactor 1 after existing the recovery.
Embodiment 3: the embodiment take monochloro methane, methylene dichloride and chlorine as raw material.
With the monochloro methane 40Nm that is heated to 20 ℃～40 ℃
3/ h, 85 ℃ of chlorine 0.9-1.1t/h, heating vaporization are to about 50 ℃ methylene dichloride 210 Nm
3/ h passes into reactor 1.Reactor 1 temperature is controlled between 560 ℃～620 ℃, and reaction pressure is to generate zellon under the condition of 0.1-0.15Mpa, and product is about the thick zellon of 0.62 t/h and 540 Nm
3The hydrogenchloride of/h, reaction mixture are shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, the restructuring after separating divides from quench tower 2 shifts out, and loop back reactor 1 after the recovery and generate zellon.
Embodiment 4: the embodiment take monochloro methane, trichloromethane and chlorine as raw material.
With the monochloro methane 40Nm that is heated to 20 ℃～40 ℃
3/ h, 85 ℃ of chlorine 0.9-1.1t/h, heating vaporization are to about 70 ℃ trichloromethane 420 Nm
3/ h passes into reactor 1.Reactor 1 temperature is controlled between 560 ℃～620 ℃, and reaction pressure is to generate zellon under the condition of 0.1-0.15Mpa, and product is about the thick zellon of 0.96 t/h and 540 Nm
3The hydrogenchloride of/h, reaction mixture are shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, the restructuring after separating divides from quench tower 2 shifts out, and loop back reactor 1 after the recovery and generate zellon.
Embodiment 5: the embodiment take monochloro methane, methylene dichloride, trichloromethane, tetracol phenixin and chlorine as raw material.
With the monochloro methane 100Nm that is heated to 20 ℃～40 ℃
3/ h, 85 ℃ of chlorine 0.9-1.1t/h, heating vaporization be to about 200 ℃, and volume ratio is 15% methylene dichloride, 15% trichloromethane and 70% carbon tetrachloride mixture 550 Nm
3Methylene dichloride and trichloromethane that/h passes in the reactor 1(tetracol phenixin can be arbitrary proportions).Reactor 1 temperature is controlled between 560 ℃～620 ℃, and reaction pressure is to generate zellon under the condition of 0.1-0.15Mpa, and product is about the thick zellon of 1.09 t/h and 536 Nm
3The hydrogenchloride of/h, reaction mixture are shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, the restructuring after separating divides from quench tower 2 shifts out, and loop back reactor 1 after the recovery and generate zellon.
Embodiment 6: the embodiment take monochloro methane, methylene dichloride, tetracol phenixin and chlorine as raw material.
With the monochloro methane 80Nm that is heated to 20 ℃～40 ℃
3/ h, 85 ℃ of chlorine 0.9-1.1t/h, heating vaporization are to about 200 ℃ methylene dichloride and carbon tetrachloride mixture (mixture that the two can arbitrary proportion, both volume ratios are in this example: methylene dichloride 30%, tetracol phenixin 70%) 500 Nm
3/ h passes into reactor 1.Reactor 1 temperature is controlled between 560 ℃～620 ℃, and reaction pressure is to generate zellon under the condition of 0.1-0.15Mpa, and product is the thick zellon of about 1.01 t/h and 540 Nm
3/ h hydrogenchloride, reaction mixture are shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, the restructuring after separating divides from quench tower 2 shifts out, and loop back reactor 1 after the recovery and generate zellon.
Embodiment 7: the embodiment take monochloro methane, trichloromethane, tetracol phenixin and chlorine as raw material.
With the monochloro methane 130Nm that is heated to 20 ℃～40 ℃
3/ h, 85 ℃ of chlorine 0.9-1.1t/h, heating vaporization are to about 200 ℃ trichloromethane and carbon tetrachloride mixture (mixture that the two can arbitrary proportion, both volume ratios are in this example: methylene dichloride 30%, tetracol phenixin 70%) 500 Nm
3/ h passes into reactor 1.Reactor 1 temperature is controlled between 560 ℃～620 ℃, and reaction pressure is to generate zellon under the condition of 0.1-0.15Mpa, and product is the thick zellon of about 1.06 t/h and 540 Nm
3/ h hydrogenchloride, reaction mixture are shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, the restructuring after separating divides from quench tower 2 shifts out, and loop back reactor 1 after the recovery and generate zellon.
Embodiment 8: the embodiment take the mixture of monochloro methane, methylene dichloride and trichloromethane arbitrary proportion, chlorine as raw material.
With the monochloro methane 80Nm that is heated to 20 ℃～40 ℃
3/ h, heating vaporization is to about 200 ℃ methylene dichloride 250Nm
3/ h and trichloromethane 220Nm
3/ h, 85 ℃ of chlorine 0.9-1.1t/h pass into reactor 1.Reactor 1 temperature is controlled between 560 ℃～620 ℃, and reaction pressure is that the condition of 0.1-0.15Mpa generates zellon, and product is the thick zellon of about 0.85 t/h and 720 Nm
3/ h hydrogenchloride, reaction mixture is shifted out reactor 1 rapidly to quench tower 2, so that reaction is more complete, after reaction gas cools off in quench tower 1, light constituent hydrogenchloride and tetracol phenixin are gone out from the cat head of quench tower 2, and thick zellon goes rectification and purification again from quench tower 2 side line extraction, restructuring divides shifts out from quench tower 2, loops back reactor 1 after the recovery.
Embodiment 9: byproduct hydrogen chloride synthesizes monochloro methane
By-product hydrogen chloride 540Nm of the present utility model
3/ h and methyl alcohol 540Nm
3/ h is preheating to 100-160 ℃, enters monochloro methane reactor 8 after the mixing and reacts generation monochloro methane 540Nm
3/ h can be used as the raw material that the utility model synthesizes the raw material of zellon or produces methylene dichloride, trichloromethane as the downstream.
The above, it only is preferred embodiment of the present utility model, be not to be the restriction of the utility model being made other form, any those skilled in the art may utilize the technology contents of above-mentioned announcement to be changed or be modified as the equivalent embodiment of equivalent variations.But every technical solutions of the utility model content that do not break away to any simple modification, equivalent variations and remodeling that above embodiment does, still belongs to the protection domain of technical solutions of the utility model according to technical spirit of the present utility model.
Claims (1)
1. the industrial production device of a zellon, it is characterized in that comprising: monochloro methane/Sweet natural gas storage tank (11), methane chloride storage tank (12) links to each other by the opening for feed of pipeline with reactor (1) with the first chlorine storage tank (13), the discharge port of described reactor (1) links to each other with quench tower (2), the lower part outlet end of described quench tower (2) links to each other with the heavy component recovery system, the middle sidepiece exit end of described quench tower (2) links to each other with thick zellon storage tank (3), the top exit end of described quench tower (2) links to each other with the inlet end of condenser (4), the exit end of described condenser (4) links to each other with the inlet end of separator (5), tetracol phenixin storage tank (6), the second chlorine storage tank (7), the inlet end of the monochloro methane reactor (8) that links to each other with methyl alcohol storage tank (10) links to each other with the exit end of described separator (5) respectively, the exit end of described monochloro methane reactor (8) links to each other with monochloro methane storage tank (9), tetracol phenixin in the described tetracol phenixin storage tank (6) can add to methane chloride storage tank (12) and recycle, and the chlorine in described the second chlorine storage tank (7) can add to the first chlorine storage tank (13) and recycle.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220399330 CN202786058U (en) | 2012-08-13 | 2012-08-13 | Industrial production device of tetrachloroethylene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220399330 CN202786058U (en) | 2012-08-13 | 2012-08-13 | Industrial production device of tetrachloroethylene |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288588A (en) * | 2013-05-24 | 2013-09-11 | 陕西科技大学 | One-step method synthesis system and process for co-production of trichloroethylene and tetrachloroethylene |
| CN103588615A (en) * | 2013-11-01 | 2014-02-19 | 聊城市鲁西化工工程设计有限责任公司 | Device and technology for recovery of tetrachloroethylene |
| CN106187675A (en) * | 2016-06-28 | 2016-12-07 | 乳源东阳光电化厂 | A kind of method producing tetrachloroethylene |
| CN109627142A (en) * | 2018-12-12 | 2019-04-16 | 山东东岳氟硅材料有限公司 | A kind of processing method and processing system producing tetrachloro-ethylene by-product tail gas |
-
2012
- 2012-08-13 CN CN 201220399330 patent/CN202786058U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103288588A (en) * | 2013-05-24 | 2013-09-11 | 陕西科技大学 | One-step method synthesis system and process for co-production of trichloroethylene and tetrachloroethylene |
| CN103588615A (en) * | 2013-11-01 | 2014-02-19 | 聊城市鲁西化工工程设计有限责任公司 | Device and technology for recovery of tetrachloroethylene |
| CN103588615B (en) * | 2013-11-01 | 2014-12-10 | 聊城市鲁西化工工程设计有限责任公司 | Device and technology for recovery of tetrachloroethylene |
| CN106187675A (en) * | 2016-06-28 | 2016-12-07 | 乳源东阳光电化厂 | A kind of method producing tetrachloroethylene |
| CN106187675B (en) * | 2016-06-28 | 2018-09-07 | 乳源东阳光电化厂 | A method of producing tetrachloro-ethylene |
| CN109627142A (en) * | 2018-12-12 | 2019-04-16 | 山东东岳氟硅材料有限公司 | A kind of processing method and processing system producing tetrachloro-ethylene by-product tail gas |
| CN109627142B (en) * | 2018-12-12 | 2021-10-22 | 山东东岳氟硅材料有限公司 | Treatment method and treatment system for byproduct tail gas in tetrachloroethylene production |
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