CN1054625C - Method of comprehensive utilization of condensed oil - Google Patents
Method of comprehensive utilization of condensed oil Download PDFInfo
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- CN1054625C CN1054625C CN92102254A CN92102254A CN1054625C CN 1054625 C CN1054625 C CN 1054625C CN 92102254 A CN92102254 A CN 92102254A CN 92102254 A CN92102254 A CN 92102254A CN 1054625 C CN1054625 C CN 1054625C
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Abstract
The present invention relates to a method for comprehensively preparing various hydrocarbon solvents, especially extraction solvent oil, by using condensed oil without proper purpose in petroleum production as raw materials in order to exploit the proper purpose of the condensed oil, increase the yield of the hydrocarbon solvents and realize the industrial production of high-quality narrow fraction extraction solvents No. 6-A, No . 6-B and No. 6-C. The present invention is characterized in that the processes of fractionating and refining are carried out at normal pressure and low temperature; gas-phase fractions obtained by the extraction solvents make a hydrogenation reaction in the reaction to remove unsaturated hydrocarbon and aromatic hydrocarbon; under the participation of a catalyst 'NI' with high activity and high selectivity, the unsaturated hydrocarbon and the aromatic hydrocarbon can be converted to cyclohexane 3H2 in the hydrogenation reaction; and the cyclohexane is washed to obtain a qualified product.
Description
The present invention is to be raw material with the condensate oil that does not still have proper purposes in the oil production, and comprehensive process becomes the working method of various solvent for extraction and other varsol oil in its contained fraction.
Condensate oil output in oil production is very big, and its fraction is many between 20 ℃-200 ℃.Component is by C
5Above lighter hydrocarbons, unsaturated hydrocarbons, aromatic hydrocarbons and other trace impurity are formed.It did not still have proper purposes in the past except that re-injection oil well and some improper purposes.
Extraction solvent in the varsol and other industrial solvent, former employing are raffinated oil or virgin oil forms with other industrial solvent processing and refining.It is produced under comparatively high temps and elevated pressures, and the complex process appointed condition requires high.The vegetables oil leaching agent fraction of being produced is wide, and the temperature better quality is also undesirable, more because of used raw material still has other important use, has limited the development of producing.
Purpose of the present invention just provides and a kind ofly utilizes condensate oil to be processed into it containedly to heat up in a steamer in one's duty serial varsol oil, especially as high-quality close-cut fraction extraction solvent oil (No. 6-A), (No. 6-B), (No. 6-C) processing method.Open up the proper outlet of condensate oil, for society provides more high-quality extraction solvent oil.
Concrete grammar of the present invention is: earlier condensate oil is delivered to water wash column washing (water temperature should below 20 ℃), to slough sulfide, acidic substance and other impurity, sending into moisture eliminator then dewaters, condensate oil after the dehydration is sent into still kettle and is distilled, to distill the gaseous phase materials that is obtained again and send into primary tower, again the product of primary tower is sent into rectifying tower rectifying, the gaseous substance after the rectifying carries out fractionation according to the requirement of product.Product fractionation situation is 30 ℃-60 ℃ and is sherwood oil; 80 ℃-140 ℃ is industrial solvent; 145 ℃-200 ℃ is No. 200 varnish makers' and painters' naphtha; The fraction of close-cut fraction solvent for extraction is: 60 ℃-80 ℃, 60 ℃-71 ℃, 60 ℃-90 ℃, be respectively: (No. 6-A), (No. 6-B), (No. 6-C) fraction of vegetables oil and perfume extraction solvent; 90 ℃-120 ℃ is the fraction of rubber solvent naphtha.
By after the rectifying isolating its quality of each fraction only meet the standard of general varsol oil.But for solvent for extraction especially close-cut fraction extraction solvent oil, work the mischief because of wherein still existing a spot of unsaturated hydrocarbons, aromatic hydrocarbons, alicyclic hydrocarbon that the people is known from experience, therefore it must be reduced to about 0.1%, sulphur content is less than 0.05%, and iodine number (gram iodine/100 grams) is less than 1; PH value neutrality does not have mechanical impurity, and alkane content is greater than 98%, and method is that the gas phase fraction is carried out hydrogenation reaction, and unsaturated hydrocarbons, aromatic hydrocarbons, alicyclic hydrocarbon are become hexanaphthene.Its reaction formula:
The method of hydrogenation reaction: when the rectifying fractionation, the gas phase thing of each fraction of solvent for extraction that will get is sent in the reactor, carries out hydrogenation reaction, and its pressure range is generally at 4-8Kg/cm, temperature is adjusted between 120 ℃-190 ℃, and the mol ratio of hydrogen and benzene should be 〉=10.Above technical qualification hydrogenation reaction is extremely slow, must be at high reactivity, selectivity could realize industrial production under the catalyzer condition of 95-98%, this catalyzer is to be the catalyzer that main component is made with nickel (Ni), participate in reaction, improve per pass conversion, this catalyzer is succeeded in developing by Catalyst Production producer and is gone on the market, code name is " NCG " type benzene hydrogenating catalyst, can make residual aromatics or unsaturated hydrocarbons drop to the ppm level.
More than after each product purification or the completion of processing, needing through condenser condenses be the liquid phase storage.Accompanying drawing is seen in its technical process.
The present invention makes that still not have the production of the condensate oil of proper purposes in the oil production be varsol oil, has also opened up vast raw material sources for the production of varsol oil.Production is carried out under normal pressure and lesser temps, and technology simple device cost is low, is easy to industrialization, has especially started close-cut fraction vegetables oil extraction solvent novel process, has created product innovation: " No. 6-A ", " No. 6-B ", " No. 6-C ".Do not have in the production " three wastes ".
Embodiment 1: 27 ℃-146 ℃ of condensate oil (Zhongyuan Oil Field) boiling ranges.With condensate oil from head tank＜1 suction water wash column＜3, water is by water cooling pond＜2〉supply with.After washing, send into moisture eliminator＜4〉send into still kettle＜5 after the drying〉distillation of heating.Thermal source is by medium heating furnace＜6〉supply with.The gaseous phase materials that fore-running gets is sent into rectifying tower＜7 〉, the gas phase fraction after the rectifying " 30 ℃-60 ℃ ", " 80 ℃-140 ℃ " are sent into condenser＜10 〉, send into basin＜11 after the condensation〉storage; Fraction to the close-cut fraction solvent for extraction should be sent into reaction＜8〉in carry out hydrogenation＜13 reaction, heat energy is by medium stove＜6〉supply with.Reacted product carries out condensation＜9 〉, water of condensation is by＜2〉supply with.Cold liquid phase thing " 60 ℃-71 ℃ ", " 60 ℃-80 ℃ ", " 60 ℃-90 ℃ " that get are close-cut fraction extraction solvent oil " No. 6-B ", " No. 6-A ", " No. 6-C ", and " 90 ℃-120 ℃ " are rubber solvent etc.Send into basin＜12〉storage.
Accompanying drawing: condensate oil complex processing technology schema.
＜1〉head tank,＜2〉water cooling pond,＜3〉water wash column,＜4〉moisture eliminator,＜5〉still kettle,＜6〉medium heating furnace,＜7〉rectifying tower,＜8〉reactor,＜9〉condenser,＜10〉condenser,＜11〉common solvent basins,＜12〉extracting (extraction) solvent tanker,＜13〉hydrogen jars.
Claims (1)
1. method of producing serial solvent by condensate oil, it is characterized in that this method comprises: earlier condensate oil is delivered to the water wash column washing, water temperature is below 20 ℃, to slough sulfide, acidic substance and other impurity, sending into moisture eliminator then dewaters, condensate oil after the dehydration is sent into still kettle and is distilled, to distill the gaseous phase materials that is obtained again and send into primary tower, again the product of primary tower is sent into rectifying tower rectifying, fractionate out desired product, the gas phase fraction that fractionation is obtained carries out hydrogenation reaction, hydrogenation conditions is: pressure 4-8Kg/cm, temperature 120-190 ℃, the mol ratio of hydrogen and benzene 〉=10, catalyst system therefor is a nickel catalyzator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN92102254A CN1054625C (en) | 1992-04-06 | 1992-04-06 | Method of comprehensive utilization of condensed oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN92102254A CN1054625C (en) | 1992-04-06 | 1992-04-06 | Method of comprehensive utilization of condensed oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1077213A CN1077213A (en) | 1993-10-13 |
| CN1054625C true CN1054625C (en) | 2000-07-19 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN92102254A Expired - Fee Related CN1054625C (en) | 1992-04-06 | 1992-04-06 | Method of comprehensive utilization of condensed oil |
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| Country | Link |
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| CN (1) | CN1054625C (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056870C (en) * | 1995-08-29 | 2000-09-27 | 巴陵石化长岭炼油化工总厂 | Process for producing extraction solvent oil by catalytic reforming device |
| EP2277980B1 (en) * | 2009-07-21 | 2018-08-08 | IFP Energies nouvelles | Method for selectively reducing the benzene and unsaturated compounds content of various hydrocarbon cuts |
| CN102876359B (en) * | 2011-07-15 | 2015-09-09 | 中国石油化工集团公司 | A kind of system and method processing condensate oil |
| CN103131457A (en) * | 2013-02-26 | 2013-06-05 | 宁夏易欣能源科技有限公司 | Condensate oil processing method |
| CN103113913B (en) * | 2013-02-26 | 2015-09-23 | 宁夏易欣能源科技有限公司 | Condensate oil treatment unit |
| CN103484152B (en) * | 2013-09-29 | 2016-06-01 | 东北农业大学 | Except the method for unsaturated hydrocarbons in solvent oil under a kind of supercritical state |
| CN104745225A (en) * | 2015-01-08 | 2015-07-01 | 库车中原石油化工有限公司 | Method and device for separating condensate oil |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU749818A1 (en) * | 1978-06-28 | 1980-07-23 | Всесоюзный научно-исследовательский институт углеводородного сырья | Method of purifying liquid saturated aliphatic hydrocarbons from sulfuric compounds |
| SU757510A1 (en) * | 1978-06-28 | 1980-08-23 | Vnii Uglevodorodnogo Syrya | Method of purifying liquid saturated aliphatic hydrocarbons from sulfuric compounds |
| SU1421760A1 (en) * | 1986-08-18 | 1988-09-07 | Уфимский Нефтяной Институт | Method of processing gas condensate |
-
1992
- 1992-04-06 CN CN92102254A patent/CN1054625C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU749818A1 (en) * | 1978-06-28 | 1980-07-23 | Всесоюзный научно-исследовательский институт углеводородного сырья | Method of purifying liquid saturated aliphatic hydrocarbons from sulfuric compounds |
| SU757510A1 (en) * | 1978-06-28 | 1980-08-23 | Vnii Uglevodorodnogo Syrya | Method of purifying liquid saturated aliphatic hydrocarbons from sulfuric compounds |
| SU1421760A1 (en) * | 1986-08-18 | 1988-09-07 | Уфимский Нефтяной Институт | Method of processing gas condensate |
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| Publication number | Publication date |
|---|---|
| CN1077213A (en) | 1993-10-13 |
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