CN104388120B - Organic heat carrier recycling process for selective hydrogenation - Google Patents
Organic heat carrier recycling process for selective hydrogenation Download PDFInfo
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- CN104388120B CN104388120B CN201410351574.3A CN201410351574A CN104388120B CN 104388120 B CN104388120 B CN 104388120B CN 201410351574 A CN201410351574 A CN 201410351574A CN 104388120 B CN104388120 B CN 104388120B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses organic heat carrier recycling process for selective hydrogenation, belong to organic heat carrier application.Including four technological processes, it is dewatering and filtering flow process, molecular clock flow process, hydrofinishing flow process and fraction seperation flow process successively.First higher boiling waste oil enters oil water separator, under non-homogeneous phase filling effect, carry out dehydration and solid impurity removes, then enter molecular clock stream device, hydro-refining unit fraction seperation stream device by delivery pump, after fractionation, respectively enter different collecting tanks.Finally restructuring lease making delivery pump enters molecular clock evaporimeter, separates and produces distillate and residue.This technology can not only save limited national oil resource; and surrounding environment protection is also made that contribution; project has preferable market prospects simultaneously, it is possible to producing good Social benefit and economic benefit, also the development in pluralism to the sector serves active promoting function.
Description
Technical field
The present invention relates to organic heat carrier recycling process for selective hydrogenation, belong to organic heat carrier application.
Background technology
In productive life of today, the application of organic heat carrier is the most quite varied, and the thing followed is the pollution problem brought to after date service life.The conduction oil in market, is in for a long time under the condition of high temperature and all can deteriorate (such as thermal decomposition, polycondensation pollution etc.) now, and the greatest problem thus brought is that, the recycling of waste oil.The recycling of waste oil, reduces energy loss while reducing environmental pollution.
Waste oil recycles one of most important process for purification, it is simply that hydrofinishing.Organic heat carrier hydrofining technology involved by the technology contents of the present invention, it is simply that in order to solve this technical barrier, after making waste oil recycling, quality is higher, and product stability is more preferable.
Summary of the invention
The technical problem to be solved is to provide organic heat carrier recycling process for selective hydrogenation, can effectively improve the product quality after higher boiling waste oil recycling and quality stability.
The technical solution adopted for the present invention to solve the technical problems is: provide organic heat carrier recycling process for selective hydrogenation, including four technological processes, it is dewatering and filtering flow process, molecular clock flow process, hydrofinishing flow process, fraction seperation flow process successively, it is characterised in that:
During dewatering and filtering flow process, higher boiling waste oil enters oil water separator, oil water separator arranges non-homogeneous phase filling, make oil water mixture through out-of-date, dispersion phase is gradually assembled by droplet at filling surface, after forming big drop, shifts to the upper surface of liquid along filling surface, and the solid impurity in oil water mixture is separated simultaneously, thus reach the purpose of two-phase laminated flow；
During molecular clock flow process, after dehydration, component enters molecular clock evaporimeter through delivery pump, blending ingredients is heated during flowing along heating plate simultaneously, gently, weight molecule can escape liquid level and enter gas phase, owing to molecular tools light, weight molecule is different, then light molecule separates with weight molecule, and distillate and residue respectively enter collecting tank D and collecting tank E；
During hydrofinishing flow process, molecular clock distillates part and enters hydro-refining unit by delivery pump, removes that sulfur-bearing in cut is nitrogenous, the non-hydrocarbon component of oxygen and organo-metallic compound under the effect of catalyst and hydrogen, thus improves oil quality；
During fraction seperation flow process, the overhead condenser that hydrogenated oil respectively enters light ends tower and midbarrel knockout tower through delivery pump carries out heat exchange, first in light ends tower, light fraction is separated, the light fraction that tower top goes out enters collecting tank A, midbarrel enters collecting tank B, by Liquid level feed supplement in light ends tower still, midbarrel is injected midbarrel knockout tower by delivery pump, the middle distillate that tower top goes out enters collecting tank B after cooling down via water cooler, by the feed supplement of Liquid level distillate drum in still, the heavy constituent of evaporation is not had to enter collecting tank C.
During fraction seperation flow process, the vacuum system of light ends tower is made up of water ring and lobe pump group, and operation pressure is 100Pa, and operation temperature is 120-150 degree Celsius.
During fraction seperation flow process, the vacuum system of midbarrel knockout tower is made up of blade and lobe pump group, and operation pressure is 30Pa, and operation temperature is 180-200 degree Celsius.
During molecular clock flow process, the vacuum system of molecular distillation apparatus is made up of blade and lobe pump group, and operation pressure is 1Pa, and operation temperature is 200-240 degree Celsius.
Whole operating process uses DCS control system, it is achieved Automated condtrol.
Compared with prior art, the invention has the beneficial effects as follows:
1, organic heat carrier recycling process for selective hydrogenation, uses dewatering and filtering flow process, molecular clock flow process, hydrofinishing flow process, and four process procedures of fraction seperation flow process complete.Technological process arranges rationally, easy and simple to handle, it is simple to the actual application of this technology and popularization.
2, in fraction seperation flow process and molecular clock flow process, set particular job condition and equipment, be more accurately controlled the realization of whole technique.
3, the hydrofining technology described by this patent; limited national oil resource can not only be saved; and surrounding environment protection is also made that contribution; project has preferable market prospects simultaneously; can produce good Social benefit and economic benefit, also the development in pluralism to the sector serves active promoting function.
Detailed description of the invention:
Organic heat carrier recycling process for selective hydrogenation, including four technological processes, it is dewatering and filtering flow process successively, molecular clock flow process, hydrofinishing flow process, fraction seperation flow process, during dewatering and filtering flow process, higher boiling waste oil enters oil water separator, oil water separator arranges non-homogeneous phase filling, make oil water mixture through out-of-date, dispersion phase is gradually assembled by droplet at filling surface, after forming big drop, the upper surface of liquid is shifted to along filling surface, and the solid impurity in oil water mixture is removed simultaneously, thus reach the purpose of two-phase laminated flow.
During molecular clock flow process, after dehydration, component enters molecular clock evaporimeter through delivery pump, and the vacuum system of molecular distillation apparatus is made up of blade and lobe pump group, and operation pressure is 1Pa, and operation temperature is 200-240 degree Celsius.Blending ingredients is heated during flowing along heating plate simultaneously, gently, weight molecule can escape liquid level and enter gas phase, owing to molecular tools light, weight molecule is different, then light molecule separates with weight molecule, and distillate and residue respectively enter collecting tank D and collecting tank E.Appliance arrangement involved in whole technological process, uses DCS control system, it is achieved the Automated condtrol of a complete set of flow process.
During hydrofinishing flow process, molecular clock distillates part and enters hydro-refining unit by delivery pump, removes that sulfur-bearing in cut is nitrogenous, the non-hydrocarbon component of oxygen and organo-metallic compound under the effect of catalyst and hydrogen, thus improves oil quality.
During fraction seperation flow process, the overhead condenser that hydrogenated oil respectively enters light ends tower and midbarrel knockout tower through delivery pump carries out heat exchange.First light fraction being separated in light ends tower, the light fraction that tower top goes out enters collecting tank A, and midbarrel enters collecting tank B, by Liquid level feed supplement in light ends tower still.The vacuum system of light ends tower is made up of water ring and lobe pump group, and operation pressure is 100Pa, and operation temperature is 120-150 degree Celsius.Midbarrel is injected midbarrel knockout tower by delivery pump, and the middle distillate that tower top goes out enters collecting tank B, by the feed supplement of Liquid level distillate drum in still after cooling down via water cooler.The vacuum system of midbarrel knockout tower is made up of blade and lobe pump group, and operation pressure is 30Pa, and operation temperature is 180-200 degree Celsius.The heavy constituent not having evaporation enters collecting tank C.
The above, be only presently preferred embodiments of the present invention, is not the restriction that the present invention makees other form, and any those skilled in the art are combined possibly also with the technology contents of the disclosure above, change or retrofit and are the Equivalent embodiments of the present invention.Every without departing from technical solution of the present invention content, any simple modification, equivalent variations and remodeling above example made according to the technical spirit of the present invention, still fall within the protection domain of technical solution of the present invention.
Claims (2)
1. organic heat carrier recycling process for selective hydrogenation, including four technological processes, is dewatering and filtering flow process successively, divides
Son distillation flow process, hydrofinishing flow process and fraction seperation flow process, it is characterised in that:
During dewatering and filtering flow process, higher boiling waste oil enters oil water separator, arranges non-homogeneous phase filling in oil water separator, makes profit mix
Compound, through out-of-date, be dispersed in phase filling surface and gradually assembled by droplet, after forming big drop, floating along phase filling surface
Rise to the upper surface of liquid, and the solid impurity in oil water mixture is separated simultaneously, thus reach the purpose of two-phase laminated flow；
During molecular clock flow process, after dehydration, component enters molecular clock evaporimeter, the process that blending ingredients flows along heating plate through delivery pump
Middle being heated, light, weight molecule can escape liquid level and enter gas phase, due to light, the molecular tools of weight molecule simultaneously
Difference, then light molecule separates with weight molecule, and distillate and residue respectively enter collecting tank D and collecting tank E；
During hydrofinishing flow process, molecular clock distillates part and enters hydro-refining unit by delivery pump, under catalyst and hydrogen effect
In removing cut, sulfur-bearing is nitrogenous, the non-hydrocarbon component of oxygen and organo-metallic compound, thus improves oil quality；
During fraction seperation flow process, the overhead condenser that hydrogenated oil respectively enters light ends tower and midbarrel knockout tower through delivery pump enters
Row heat exchange, first separates light fraction in light ends tower, and the light fraction that tower top goes out enters collecting tank A, and centre evaporates
Dividing and enter collecting tank B, by Liquid level feed supplement in light ends tower still, midbarrel is injected midbarrel by delivery pump and is separated
Tower, the middle distillate that tower top goes out enters collecting tank B, by the benefit of Liquid level distillate drum in still after cooling down via water cooler
Material, does not has the heavy constituent of evaporation to enter collecting tank C；
During described fraction seperation flow process, the vacuum system of light ends tower is made up of water ring and lobe pump group, and operation pressure is
100Pa, operation temperature is 120-150 degree Celsius；
During described fraction seperation flow process, the vacuum system of midbarrel knockout tower is made up of blade and lobe pump group, and operation pressure is
30Pa, operation temperature is 180-200 degree Celsius；
During described molecular clock flow process, the vacuum system of molecular distillation apparatus is made up of blade and lobe pump group, and operation pressure is
1Pa, operation temperature is 200-240 degree Celsius.
2., according to the organic heat carrier recycling process for selective hydrogenation described by claim 1, its feature also includes: whole
Operating process uses DCS control system, it is achieved Automated condtrol.
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| CN201410351574.3A CN104388120B (en) | 2014-07-23 | 2014-07-23 | Organic heat carrier recycling process for selective hydrogenation |
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| CN201410351574.3A CN104388120B (en) | 2014-07-23 | 2014-07-23 | Organic heat carrier recycling process for selective hydrogenation |
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| CN104388120B true CN104388120B (en) | 2016-08-17 |
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| CN111253918A (en) * | 2020-03-19 | 2020-06-09 | 中化泉州石化有限公司 | Method for directly producing organic heat carrier by mineral oil |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2155209C2 (en) * | 1998-11-13 | 2000-08-27 | Сафин Ришат Рафилович | Process for production of base components for low-freezing lubrication oils |
| CN101575537A (en) * | 2008-05-06 | 2009-11-11 | 牟艳春 | Process for producing light and heavy fuel oil and high-quality asphalt by hydrogenating coal tar at medium and low temperature |
| CN102989468A (en) * | 2012-12-20 | 2013-03-27 | 抚顺新瑞催化剂有限公司 | Catalyst for waste heat conduction oil hydrogenation and preparation method as well as application thereof |
-
2014
- 2014-07-23 CN CN201410351574.3A patent/CN104388120B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2155209C2 (en) * | 1998-11-13 | 2000-08-27 | Сафин Ришат Рафилович | Process for production of base components for low-freezing lubrication oils |
| CN101575537A (en) * | 2008-05-06 | 2009-11-11 | 牟艳春 | Process for producing light and heavy fuel oil and high-quality asphalt by hydrogenating coal tar at medium and low temperature |
| CN102989468A (en) * | 2012-12-20 | 2013-03-27 | 抚顺新瑞催化剂有限公司 | Catalyst for waste heat conduction oil hydrogenation and preparation method as well as application thereof |
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| CN104388120A (en) | 2015-03-04 |
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Effective date of registration: 20170907 Address after: 255300, No. 1, outer ring road, northwest of Zhoucun District, Shandong, Zibo Patentee after: Shandong Hengli heat carrier Engineering Co. Ltd. Address before: 255300 Shandong Province, Zibo city Zhoucun District North Ring Road No. 1 (new material in Chemical Industry Park) Patentee before: SHANDONG HENGDAO OIL CHEMICAL CO., LTD. |