CN100450983C - Single-tube multiple rotary static and mixed-piping reacotr with vinyl chlorination and method thereof - Google Patents
Single-tube multiple rotary static and mixed-piping reacotr with vinyl chlorination and method thereof Download PDFInfo
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- CN100450983C CN100450983C CNB2006100461198A CN200610046119A CN100450983C CN 100450983 C CN100450983 C CN 100450983C CN B2006100461198 A CNB2006100461198 A CN B2006100461198A CN 200610046119 A CN200610046119 A CN 200610046119A CN 100450983 C CN100450983 C CN 100450983C
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- ethene
- chlorine
- ethylene dichloride
- chlorination
- ethylene
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Abstract
The present invention relates to a device and a method for producing chemical engineering products, particularly to a device and a method for generating dichloroethane by ethylene chlorination reaction in the process of preparing dichloroethane. The production device comprises a dichloroethane cycling and chlorine gas inlet pipeline, a pipe chlorine gas instant mixer, a chlorine gas solution outlet pipeline, a chlorine gas solution and ethylene mixed liquor merging pipeline, a pipe ethylene chlorination reactor, a dichloroethane outlet line, etc., and a production method of single pipe multicycle static mixing pipe ethylene chlorination reaction used for preparing dichloroethane by ethylene chlorination is provided. Channelization of the production process can be realized, the investment is little, and the production capacity is great; in the reaction process, circulating dichloroethane is used for predissolving chlorine gas and ethylene, no gas-phase contact between the chlorine gas and the ethylene occurs, few by-products are generated, and the purity of the products is high; in the present invention, low temperature chlorination, moderate temperature chlorination and high temperature chlorination can be used, and the present invention can be used for the operation of liquid phase discharge, gas phase discharge and gas-liquid mixed discharge.
Description
Technical field
The present invention relates to the production equipment and the production method of Chemicals, what be specifically related to is production equipment and the production method that vinyl chlorination is produced ethylene dichloride.
Technical background
Ethylene dichloride is an important source material of producing vinyl chloride monomer.Directly contacting the production ethylene dichloride with ethene and chlorine in the presence of catalyzer is comparatively general in the world technology.
The vinyl chlorination device can be divided into tower reactor, U type reactor, tubular reactor.Ethylene chlorination technology can be divided into and is being lower than the low temperature chlorination operated under the ethylene dichloride boiling temperature and is being higher than the high-temp chlorination of operating under the ethylene dichloride boiling temperature.Its difference is that low temperature chlorination adopts the liquid phase discharging, and high-temp chlorination adopts the gas phase discharging.Also have and adopt the gas-liquid mixture discharging, warm chlorination in being called.The low temperature chlorination fado adopts tower reactor, as Fig. 1.The chlorination reaction of ethene and chlorine is carried out in the tower reactor that is filled with the circulation chlorated liquid in advance.The circulation chlorated liquid before entering reactor through Wen's nozzle with raw material chlorine drawing-in system, the chlorated liquid that is dissolved with chlorine enters tower reactor with raw material ethene and carries out chlorination reaction near reactor inlet.The used chlorination reactor of high-temperature chlorination has multiple.Fig. 2 is the U type chlorination reactor that is used for high-temp chlorination, and it is the molectron that reactor design is become a U type pipe and a separator.Raw material ethene and chlorine join the U type tube portion of separator by spray gun.Two kinds of reactant gasess enter to be dissolved in to react in the ethylene dichloride liquid phase behind the reactor and are transformed into ethylene dichloride, be in the bottom of reactor this moment, because the hydrostatic pressure of liquid boiling can not occur, when being positioned at the last position of U type pipe, the reaction of ethene and chlorine is finished substantially, when liquid continued to rise, owing to static pressure reduces to occur boiling, formed gas-liquid mixture entered the gas-liquid separator on top, gas phase is as discharging, and liquid phase relies on syphonic effect at U type pipe reactor internal recycle.
At present, it is the high temperature direct chlorination technology of catalyzer that German a company has developed with titanium tetrachloride acid sodium, and reactor used is bubbling column reactor, and this reactor mass transfer effect is poor, and throughput is low, and quality product is difficult for guaranteeing; Japan a company has developed a kind of tower chlorination reactor of bubbling with special gas sparger and packing layer, and the major defect of this technology is that turndown ratio is little, and gas distributor easily stops up; Domesticly once announced a kind of technology that the pipeline reactor that mixes inner member directly carries out ethylene chlorination that has, technical process such as Fig. 3, structure of reactor such as Fig. 4, the mentality of designing of this technology and structure of reactor are all novel, the data of announcing are 83～90 ℃ of temperature of reaction, warm chlorination in the genus, shortcoming are that reactant purity is not high enough.
Present ethene direct chlorination is produced the production technology of ethylene dichloride and produces equipment all not ideal enough, and therefore, it is very significant that a kind of novel, efficient ethylene dichloride production equipment and production method are provided.
Summary of the invention
The object of the present invention is to provide a kind of less investment, simple in structure, output wide ranges, can make chlorine and ethene not have gas phase and contact, by product is few, product purity is high, the ethylene dichloride production of easy handling tubular type vinyl chlorination device.
Another object of the present invention provides the production method that a kind of new ethylene chlorination is produced ethylene dichloride, with the technical progress that advances ethylene dichloride and subsequent product vinylchlorid to produce.
The technical scheme that adopts is:
The single tube multi-spiral static mixes tubular type vinyl chlorination method, circulation ethylene dichloride and chlorine enter through circulation ethylene dichloride and chlorine inlet tube that flow in tubular chlorine quick dissolving mixing tank back, mix on the limit, dissolve on the limit, and the chlorine leach liquid of formation flows out through chlorine leach liquid outlet line; Ethene and circulation ethylene dichloride enter through ethene and circulation ethylene dichloride source line that flow in ethene dispersing and mixing pipe back, mix on the limit, and the ethene mixed solution of formation is flowed out by ethene mixture export pipeline; Chlorine leach liquid and ethene mixed solution converge pipeline through chlorine leach liquid and ethene mixed solution and enter that flow in tubular type vinyl chlorination device limit, mix on the limit, react on the limit, the ethylene dichloride that generates is flowed out by the ethylene dichloride outlet line, ethene directly and chlorine leach liquid converge and converge pipeline through chlorine leach liquid and ethene mixed solution and enter tubular type vinyl chlorination device; Circulation ethylene dichloride and chlorine meet, circulation ethylene dichloride and ethene meet, chlorine leach liquid and mixture of ethylene or ethene meet adopt injector to aspirate another strand material by one material; Circulation ethylene dichloride and chlorine enter tubular type vinyl chlorination device, circulation ethylene dichloride and ethene and enter the impellent that ethene dispersing and mixing pipe, chlorine leach liquid and ethene mixed solution or ethene enters tubular type vinyl chlorination device and provided by pump, potential difference or pressure difference.
The single tube multi-spiral static mixes tubular type vinyl chlorination method, and circulation ethylene dichloride and chlorine directly enter the tubular chlorine quick dissolving mixing tank without circulation ethylene dichloride and chlorine source line; Ethene and circulation ethylene dichloride are without ethene and circulation ethylene dichloride source line and directly enter ethene dispersing and mixing pipe; Ethene directly and chlorine leach liquid converge and enter tubular type vinyl chlorination device; Chlorine leach liquid and ethene mixed solution or ethene converge pipeline and directly enter tubular type vinyl chlorination device without chlorine leach liquid and ethene mixed solution.
The present invention has following advantage and effect:
1. production process has realized canalization, and facility investment is few, throughput is big, and turndown ratio is big;
2. in the vinyl chlorination process, chlorine does not have gas phase with ethene and contacts, vinyl chlorination device outlet ethylene dichloride purity height, and by product is few;
3. the material that participates in reaction has only radially mixing, no axial backmixing in reactor;
4. the residence time of material in reactor that participates in reaction is even, has realized the plug flow reaction;
5. the raw materials components mole ratio of ethene and chlorine can be near theoretical value;
6. the no moving member of device is difficult for breaking down, and can increase the effective production time;
7. this production equipment and production method can apply to low temperature chlorination, middle temperature chlorination and high-temp chlorination; Can be used for adopting the operation of liquid phase discharging, the operation of gas phase discharging and the operation of gas-liquid mixture discharging.
Description of drawings
Fig. 1 is existing tower reactor ethylene chlorination system ethylene dichloride process flow sheet;
Fig. 2 is existing U type reactor ethylene chlorination system ethylene dichloride process flow sheet;
Fig. 3 is existing domestic ethylene chlorination technological process of production figure;
Fig. 4 is the existing domestic pipeline vinyl chlorination device that mixes inner member that has;
Fig. 5 is the ethylene dichloride production single tube multi-spiral static mixing tubular type vinyl chlorination device that the present invention has tubular chlorine quick dissolving mixing tank and ethene dispersing and mixing pipe;
Fig. 6 is the ethylene dichloride production single tube multi-spiral static mixing tubular type vinyl chlorination device that the present invention has the tubular chlorine quick dissolving mixing tank;
Fig. 7 is that single tube multi-spiral static of the present invention mixes in the tubular type vinyl chlorination device, and tubular chlorine quick dissolving mixing tank, tubular type vinyl chlorination device, ethene dispersing and mixing tubular axis are to sectional view;
Fig. 8 is that single tube multi-spiral static of the present invention mixes in the tubular type vinyl chlorination device tubular chlorine quick dissolving mixing tank, tubular type vinyl chlorination device, the instant mixing tube transverse cross-sectional view of ethene;
Fig. 9 is the left-handed flight synoptic diagram of the present invention;
Figure 10 is a right-hand(ed)screw sheet synoptic diagram of the present invention.
Embodiment
Embodiment one
Ethylene dichloride production mixes tubular type vinyl chlorination production equipment with the single tube multi-spiral static, shown in Fig. 5,6,7,8,9,10, comprise that circulation ethylene dichloride and chlorine source line 1, tubular chlorine quick dissolving mixing tank 2, chlorine leach liquid outlet line 3, chlorine leach liquid and ethene mixed solution converge pipeline 4, tubular type vinyl chlorination device 5, ethylene dichloride outlet line 6, ethene mixture export pipeline 7, ethene dispersing and mixing pipe 8, ethene and circulation ethylene dichloride source line 9.In above-mentioned tubular chlorine quick dissolving mixing tank 2, tubular type vinyl chlorination device 5, the ethene dispersing and mixing pipe 8 hollow core shaft and flight are set, along cross section every group of three flights are set, angle α=120 between flight °, the flight that two groups of axially adjacent rotation directions are different is end to end, and ° angle, β=60 of along the circumferential direction staggering is arranged.Flight 10 and dextral flight 11 left-handed shown in Fig. 8,9 are end to end, are that the axle center is the radial distribution shape with mandrel 12.
Concrete mounting means: circulation ethylene dichloride and chlorine source line 1 link with tubular chlorine quick dissolving mixing tank 2 inlets, 2 outlets of tubular chlorine quick dissolving mixing tank link with chlorine leach liquid outlet line 3, propylene and circulation ethylene dichloride source line 9 link with ethene dispersing and mixing pipe 8 inlets, 8 outlets of ethene dispersing and mixing pipe link with ethene mixture export pipeline 7, chlorine leach liquid outlet line 3 and ethene mixture export pipeline 7 converge pipeline 4 with chlorine leach liquid and ethene mixed solution and link, the inlet that chlorine leach liquid and ethene mixed solution converge pipeline 4 and tubular type vinyl chlorination device 5 links, and the outlet and the ethylene dichloride outlet line 6 of tubular type vinyl chlorination device 5 link.
Embodiment two
Embodiment two and embodiment one are basic identical, and difference is that the hybrid component that is provided with in tubular chlorine quick dissolving mixing tank 2, tubular type vinyl chlorination device 5, the ethene dispersing and mixing pipe 8 is the chemical filler Pall ring.
Embodiment three
Embodiment three and embodiment one are basic identical, and difference is that the hybrid component that is provided with in tubular chlorine quick dissolving mixing tank 2, tubular type vinyl chlorination device 5, the ethene dispersing and mixing pipe is a chemical filler Lamb wave line.
Embodiment four
Embodiment four and embodiment one are basic identical, difference be chlorine leach liquid outlet line 3 and ethene mixture export pipeline 7 directly and tubular type vinyl chlorination device 5 link, need not chlorine leach liquid and the ethene mixed solution converges pipeline 4.
Embodiment five
Embodiment five and embodiment one are basic identical, and difference is no ethene dispersing and mixing pipe 8 in the device, and the direct and ethene mixed export pipeline 7 of propylene and circulation ethylene dichloride source line 9 is linked into the ethene source line.
Embodiment six
Ethylene dichloride production mixes tubular type vinyl chlorination production method with the single tube multi-spiral static, comprises that circulation ethylene dichloride and chlorine enter tubular chlorine quick dissolving mixing tank 2 through circulation ethylene dichloride and chlorine source line 1, forms chlorine leach liquid; Ethene and circulation ethylene dichloride enter ethene dispersing and mixing pipe 8 formation ethene mixed solutions through ethene and circulation ethylene dichloride source line 9; By chlorine leach liquid outlet line 3 effusive chlorine leach liquid, with by ethene mixture export pipeline 7 effusive ethene mixed solutions, converge at chlorine leach liquid and ethene mixed solution and to enter tubular type vinyl chlorination device 5 after pipeline 4 converges, the ethylene dichloride that reaction generates is flowed out by ethylene dichloride outlet line 6.
Embodiment seven
Embodiment seven and embodiment six are basic identical, and difference is that no circulation ethylene dichloride disperses the propylene operation in the operation, and propylene can directly enter tubular type vinyl chlorination device 5 after pipeline 7 and chlorine leach liquid converge.
Embodiment eight
Embodiment eight and embodiment six are basic identical, and difference be to circulate ethylene dichloride and chlorine directly enters tubular chlorine quick dissolving mixing tank 2 respectively without circulation ethylene dichloride and chlorine source line 1; Ethene and circulation ethylene dichloride are without ethene and circulation ethylene dichloride source line 9 and enter ethene dispersing and mixing pipe 8 respectively; Chlorine leach liquid and ethene mixed solution converge pipeline 4 without chlorine leach liquid and ethene mixed solution, and directly enter tubular type vinyl chlorination device 5 respectively.
Apparatus and method of the present invention can be used for low temperature chlorination, middle temperature chlorination and high-temp chlorination, are used for liquid phase discharging, gas-liquid mixed discharging and gas phase discharging.
Claims (1)
1. the single tube multi-spiral static mixes tubular type vinyl chlorination method, circulation ethylene dichloride and chlorine enter through circulation ethylene dichloride and chlorine inlet tube (1) that flow in tubular chlorine quick dissolving mixing tank (2) back, mix on the limit, dissolve on the limit, and the chlorine leach liquid of formation flows out through chlorine leach liquid outlet line (3); Ethene and circulation ethylene dichloride enter through ethene and circulation ethylene dichloride source line (9) that flow in ethene dispersing and mixing pipe (8) back, mix on the limit, and the ethene mixed solution of formation is flowed out by ethene mixture export pipeline (7); Chlorine leach liquid and ethene mixed solution converge pipeline (4) through chlorine leach liquid and ethene mixed solution and enter that flow in tubular type vinyl chlorination device limit, mix on the limit, react on the limit, the ethylene dichloride that generates is flowed out by ethylene dichloride outlet line (6), it is characterized in that: ethene directly and chlorine leach liquid converge and converge pipeline (4) through chlorine leach liquid and ethene mixed solution and enter tubular type vinyl chlorination device (5); Circulation ethylene dichloride and chlorine meet, circulation ethylene dichloride and ethene meet, chlorine leach liquid and mixture of ethylene or ethene meet adopt injector to aspirate another strand material by one material; Circulation ethylene dichloride and chlorine enter tubular type vinyl chlorination device (5), circulation ethylene dichloride and ethene and enter the impellent that ethene dispersing and mixing pipe (8), chlorine leach liquid and ethene mixed solution or ethene enters tubular type vinyl chlorination device and provided by pump, potential difference or pressure difference.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100461198A CN100450983C (en) | 2006-03-20 | 2006-03-20 | Single-tube multiple rotary static and mixed-piping reacotr with vinyl chlorination and method thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CNB2006100461198A CN100450983C (en) | 2006-03-20 | 2006-03-20 | Single-tube multiple rotary static and mixed-piping reacotr with vinyl chlorination and method thereof |
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| CN1817831A CN1817831A (en) | 2006-08-16 |
| CN100450983C true CN100450983C (en) | 2009-01-14 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101642689B (en) * | 2009-08-24 | 2012-07-25 | 天津长芦海晶集团有限公司 | Combined static mixing device |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100425938C (en) * | 2006-09-08 | 2008-10-15 | 沈阳化工学院 | Pipe type fluid turbulence device capable of strengthening mass and heat transfer and operation method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1155588C (en) * | 2001-12-18 | 2004-06-30 | 锦化化工（集团）有限责任公司 | Chlorohydrination process of producing epoxypropane and its production equipment |
| CN1208123C (en) * | 2000-03-02 | 2005-06-29 | 陶氏环球技术公司 | Tubular reactor, process for conducting liquid/liquid multiphase reactions in a tubular reactor, and a process for ring-nitrating aromatic compounds |
| CN1211329C (en) * | 2000-11-22 | 2005-07-20 | 弗纳技术股份有限公司 | Dehydrogenation method |
| CN1680346A (en) * | 2005-01-05 | 2005-10-12 | 沈阳化工学院 | Apparatus and method for monotubular multi-spiral static mixed tube style chlorohydrination of propene for production of epoxypropane |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1208123C (en) * | 2000-03-02 | 2005-06-29 | 陶氏环球技术公司 | Tubular reactor, process for conducting liquid/liquid multiphase reactions in a tubular reactor, and a process for ring-nitrating aromatic compounds |
| CN1211329C (en) * | 2000-11-22 | 2005-07-20 | 弗纳技术股份有限公司 | Dehydrogenation method |
| CN1155588C (en) * | 2001-12-18 | 2004-06-30 | 锦化化工（集团）有限责任公司 | Chlorohydrination process of producing epoxypropane and its production equipment |
| CN1680346A (en) * | 2005-01-05 | 2005-10-12 | 沈阳化工学院 | Apparatus and method for monotubular multi-spiral static mixed tube style chlorohydrination of propene for production of epoxypropane |
Non-Patent Citations (2)
| Title |
|---|
| 二氯乙烷生产装置的技术探讨. 邴涓林.聚氯乙烯，第3期. 2000 |
| 二氯乙烷生产装置的技术探讨. 邴涓林.聚氯乙烯，第3期. 2000 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101642689B (en) * | 2009-08-24 | 2012-07-25 | 天津长芦海晶集团有限公司 | Combined static mixing device |
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| CN1817831A (en) | 2006-08-16 |
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