CN1712497A - Fuel oil oxidative desulfurization - Google Patents
Fuel oil oxidative desulfurization Download PDFInfo
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- CN1712497A CN1712497A CN 200510017780 CN200510017780A CN1712497A CN 1712497 A CN1712497 A CN 1712497A CN 200510017780 CN200510017780 CN 200510017780 CN 200510017780 A CN200510017780 A CN 200510017780A CN 1712497 A CN1712497 A CN 1712497A
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Abstract
An oxidation sweetening process of fuel oil is carried out by reacting oxidant with fuel oil at 10-60 DEG C and 1-10atm for 1-30mins, oxidizing sulfide in fuel oil into sulfone and sulfoxide, removing sulfone and sulfoxide from extraction and adsorption, and obtaining low-sulfur fuel oil, which oxidant is ClO2 or mixture of hydrochloric acid and any substance in Ca(ClO)2, Ca(ClO3)2, KClO, KClO3, NaClO and NaClO3, and mol ratio for ClO2, Ca(ClO2), Ca(ClO3)2, KClO, KClO3, NaClO or NaClO3 and sulfur in fuel oil is 1-5:1. It achieves low temperature, short reaction time and less by products.
Description
Technical field
The invention belongs to the hydrocarbon oil refining field, relate to a kind of oxidative desulfurization of fuel oils and reduce the wherein technology of institute's sulfocompound.
Background technology
At present, vehicle exhaust has become the main source of atmospheric pollution.Contained sulphur compound is a kind of objectionable impurities in the oil fuel, and the burning back generates SOx and causes forming acid rain.In addition, SOx has obvious facilitation to the discharging of HC, CO, NOx and particulate matter in the vehicle exhaust, and the noble metal catalyst in the vehicle exhaust convertor is poisoned; SOx also can corrode engine, reduces the life-span of engine.In view of the harm of the sulphur compound in the oil fuel, strict oil fuel sulfur-bearing standard has been issued in each major country of the world, area in succession.
In the face of the restriction of strict content of sulphur compounds and the market great demand to the low-sulfur clean fuel, countries in the world are devoted to develop various desulfurization of fuel oil technology one after another.Desulfurization of fuel oil technology commonly used at present is divided into hydrogenating desulfurization (HDS) and non-hydrogenating desulfurization (NHDS) two big classes.Hydrodesulfurization reaction condition harshness, plant investment is big, and the process cost height causes the oil fuel cost significantly to rise.Non-hydrogenating desulfurization mainly comprises oxidation sweetening and biological desulphurization, oxidation sweetening is divided into chemical catalytic oxidation method, photocatalytic oxidation and ultrasonic wave catalytic oxidation etc. again, wherein the research of chemical catalytic oxidation method is more, and oxygenant commonly used has hydrogen peroxide, peroxycarboxylic acid, tert-butyl peroxide etc.United States Patent (USP) 20040007501 (application number) adopts Peracetic Acid and acetate to make oxygenant, after two hours the sulphur compound in the diesel oil is oxidized to sulfone or sulfoxide etc. in reaction about 60 ℃, adopts the absorption agent that contains zinc or nickel that sulfone or sulfoxide are separated again.United States Patent (USP) 6673236 adopts hydrogen peroxide, ethanol and metal oxide to make oxygenant, be generally 40～50 ℃ in temperature of reaction, reaction times is under 30 minutes～1 hour the condition, sulphur compound in the diesel oil is oxidized to sulfone or sulfoxide etc., adopts the methanol solvate extracting that sulfone is separated from diesel oil with sulfoxide again.United States Patent (USP) 6274785 adopts hydrogen peroxide and sulfuric acid or boric acid to make oxygenant, be generally 30～100 ℃ in temperature of reaction, preferred 60～90 ℃, reaction pressure is below the 10.2atm, under the condition below the preferred 2atm, after reacting more than 1 and a half hours, the sulphur compound in the gasoline is oxidized to sulfone or sulfoxide etc., adopts the dimethylsulfoxide solvent extracting that sulfone is separated from gasoline with sulfoxide again.The shortcoming that present oxidative desulfurization techniques mainly exists is: can produce by products such as some acid sludges in the oxygenant use, contaminate environment, aftertreatment trouble; Reaction times is long or temperature of reaction is higher, some in addition need special oxidation unit, be unfavorable for continuous large-scale industrialized.
Summary of the invention
The present invention be directed to the prior art oxygenant and in use can produce by products such as some acid sludges, contaminate environment, shortcomings such as aftertreatment trouble, and provide a kind of oxidation sweetening to reduce the production technique of sulphur content in the oil fuel, adopt this technology sulphur compound to be oxidized to sulfone or sulfoxide in lower temperature of reaction with in than the short reaction times, do not produce by products such as acid sludge, help continuous large-scale industrialized
Fuel oil oxidative desulfurization provided by the invention is: in temperature of reaction is 10～60 ℃, optimum temperature is 10～30 ℃, reaction pressure is under the condition of 1～10atm, oxygenant and oil fuel reaction 1～30 minute, the optimum reaction times is 1～20 minute, and the sulphur compound in the oil fuel is oxidized to sulfone and sulfoxide, removes the sulfone and the sulfoxide of generation then by solvent extraction or adsorbent method, obtain low sulphur fuel oil, wherein said oxygenant is ClO
2, or Ca (ClO)
2, Ca (ClO
3)
2, KClO, KClO
3, NaClO and NaClO
3In the mixture of arbitrary material and hydrochloric acid, ClO
2, Ca (ClO)
2, Ca (ClO
3)
2, KClO, KClO
3, NaClO or NaClO
3With the mol ratio of sulphur in the oil fuel be 1～5: 1, Ca (ClO)
2, Ca (ClO
3)
2, KClO, KClO
3, NaClO or NaClO
3With the mol ratio of hydrochloric acid be 1: 1～3.
Among the present invention in the fuel oil oxidative desulfurization, the using method of oxygenant is known in this area, when oxygenant is gas phase, employing is mode and the oil fuel contact reacts of oxygenant by oil fuel, or be dissolved in behind the organic solvent of routine again with oil fuel with blended mode contact reacts; When oxygenant is liquid phase, adopt oxygenant and oil fuel blended mode and oil fuel contact reacts.
The boiling range of indication oil fuel is generally 60 ℃～350 ℃ among the present invention, comprises the diesel oil behind gasoline and the diesel oil distillate, particularly hydrogenation.
The extraction solvent that utilizes during solvent extraction among the present invention is an extraction solvent commonly used in this area, as N, and N～dimethyl formamide or dioxane etc., extracting process adopts conventional solvent extraction method.
The sorbent material that the present invention adopts is a conventional sorbent material in this area, and as silica gel, aluminum oxide, 13X molecular sieve or carclazyte etc., adsorption method adopts conventional method.
The present invention compared with prior art because the oxygenant oxidation ability that adopts is suitable, good with the intermiscibility of hydrocarbon ils, so oxidizing reaction just can be finished smoothly in than demulcent temperature of reaction and short reaction times; Especially when oxygenant is gas phase, oxidation products except sulfone or/and remaining is still gas the sulfoxide, so use the inventive method not produce acid sludge.These characteristics make the present invention be particularly conducive to large-scale industrial production.
Embodiment
Describe the present invention in detail with specific embodiment below, but these embodiment do not limit the present invention:
Embodiment 1:
The content of sulphur compounds of straight-run spirit is 500ppm, and boiling range is 60～180 ℃.
Get 100 milliliters in above-mentioned straight-run spirit, with nitrogen with 45 milliliters of ClO
2Gas is brought in the straight-run spirit, and reaction is 20 minutes under room temperature, 1 normal atmosphere, uses 100 milliliters of N again, and N～dimethyl formamide extraction once can drop to 50ppm from 500ppm with the content of sulphur compounds in the gasoline.
Embodiment 2:
The content of sulphur compounds of straight-run spirit is 500ppm, and boiling range is 60～180 ℃.
With 150 milliliters of ClO
2Gas dissolves in 100 milliliters of hexanaphthenes, under agitation adds in 100 milliliters of above-mentioned straight-run spirit, and reaction is 1 minute under 50 ℃, 1 normal atmosphere, restrains 13X molecular sieve adsorption 1 hour with 50 again, the content of sulphur compounds in the gasoline can be dropped to 80ppm from 500ppm.
Embodiment 3:
The content of sulphur compounds of diesel oil is 450ppm behind the hydrogenation, and boiling range is 180～350 ℃.
With 30 gram NaClO
3Dissolve in 100 ml waters, under agitation be added drop-wise to simultaneously in 100 milliliters of above-mentioned catalytic cracking diesel oils with 30 milliliters of hydrochloric acid, reaction is 30 minutes under 10 ℃, 1 normal atmosphere, adsorbs 1 hour with 50 gram carclazytes again, the content of sulphur compounds in the diesel oil can be dropped to 50ppm from 450ppm.
Embodiment 4:
The content of sulphur compounds of catalytic cracking diesel oil is 4000ppm, and boiling range is 180～350 ℃.
20 gram NaClO are dissolved in 100 ml waters, under agitation be added drop-wise to simultaneously in 100 milliliters of above-mentioned catalytic cracking diesel oils with 30 milliliters of hydrochloric acid, reaction is 5 minutes under 40 ℃, 1 normal atmosphere, use 100 milliliters of N again, N～dimethyl formamide extracts once, the content of sulphur compounds in the diesel oil can be dropped to 1000ppm from 4000ppm.After three extractions, the content of sulphur compounds in the diesel oil can be dropped to below the 50ppm.
Embodiment 5:
The content of sulphur compounds of catalytic cracking diesel oil is 4000ppm, and boiling range is 180～350 ℃.
20 gram KClO are dissolved in 100 ml waters, under agitation be added drop-wise to simultaneously in 100 milliliters of above-mentioned catalytic cracking diesel oils with 30 milliliters of hydrochloric acid, reaction is 5 minutes under 30 ℃, 1 normal atmosphere, use 100 milliliters of N again, N～dimethyl formamide extracts once, the content of sulphur compounds in the diesel oil can be dropped to 1000ppm from 4000ppm.
Embodiment 6:
The content of sulphur compounds of straight-run diesel oil is 600ppm, and boiling range is 180～350 ℃.
With 20 gram Ca (ClO)
2Dissolve in 100 ml waters, under agitation be added drop-wise to simultaneously in 100 milliliters of straight-run diesel oils with 30 milliliters of hydrochloric acid, reaction is 8 minutes under room temperature, 1 normal atmosphere, once the content of sulphur compounds in the gasoline can be dropped to 60ppm from 600ppm with 100 milliliters of dioxane extractions again.
Embodiment 7:
The content of sulphur compounds of catalytically cracked gasoline is 2000ppm, and boiling range is 60～180 ℃.
With 10 gram Ca (ClO
3)
2Dissolve in 10 ml waters, be added drop-wise to simultaneously respectively in 100 milliliters of above-mentioned catalytically cracked gasolines with 15 milliliters of hydrochloric acid,, use 100 milliliters of N again in the reaction 5 minutes down of 60 ℃, 1 normal atmosphere, N～dimethyl formamide extracts once, the content of sulphur compounds in the gasoline can be dropped to 600ppm from 2000ppm.
Embodiment 8:
The content of sulphur compounds of catalytically cracked gasoline is 700ppm, and boiling range is 60～180 ℃.
With 5 gram NaClO
3Dissolve in 10 ml waters, be added drop-wise in the container respectively simultaneously with 20 milliliters of hydrochloric acid, with nitrogen the gas that produces is brought in 100 milliliters of above-mentioned catalytically cracked gasolines, in the reaction 5 minutes down of 60 ℃, 1 normal atmosphere, use 100 milliliters of N again, N～dimethyl formamide extracts once, the content of sulphur compounds in the gasoline can be dropped to 100ppm from 700ppm.
Embodiment 9
With embodiment 8, just pressure is 5 normal atmosphere, the content of sulphur compounds in the gasoline can be dropped to 80ppm from 700ppm.
Embodiment 10
With embodiment 8, just pressure is 9 normal atmosphere, the content of sulphur compounds in the gasoline can be dropped to 60ppm from 700ppm.
Claims (2)
1. fuel oil oxidative desulfurization, it is characterized in that: in temperature of reaction is 10～60 ℃, reaction pressure is under the condition of 1～10atm, oxygenant and oil fuel reaction 1～30 minute, sulphur compound in the oil fuel is oxidized to sulfone and sulfoxide, remove the sulfone and the sulfoxide of generation then by solvent extraction or adsorbent method, obtain low sulphur fuel oil, wherein said oxygenant is ClO
2, or Ca (ClO)
2, Ca (ClO
3)
2, KClO, KClO
3, NaClO and NaClO
3In the mixture of arbitrary material and hydrochloric acid, ClO
2, Ca (ClO)
2, Ca (ClO
3)
2, KClO, KClO
3, NaClO or NaClO
3With the mol ratio of sulphur in the oil fuel be 1～5: 1, Ca (ClO)
2, Ca (ClO
3)
2, KClO, KClO
3, NaClO or NaClO
3With the mol ratio of hydrochloric acid be 1: 1～3.
2. technology according to claim 1 is characterized in that: temperature of reaction is 10～30 ℃, and the reaction times of oxygenant and oil fuel is 1～20 minute.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100177801A CN1309805C (en) | 2005-07-12 | 2005-07-12 | Fuel oil oxidative desulfurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100177801A CN1309805C (en) | 2005-07-12 | 2005-07-12 | Fuel oil oxidative desulfurization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1712497A true CN1712497A (en) | 2005-12-28 |
| CN1309805C CN1309805C (en) | 2007-04-11 |
Family
ID=35718293
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|---|---|---|---|
| CNB2005100177801A Active CN1309805C (en) | 2005-07-12 | 2005-07-12 | Fuel oil oxidative desulfurization |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103387845A (en) * | 2013-07-26 | 2013-11-13 | 淮阴师范学院 | Persulfate-hydrochloric acid fuel oil oxidation desulfurizing agent and desulfurizing method thereof |
| WO2014138810A1 (en) * | 2013-03-15 | 2014-09-18 | Ultraclean Pty Ltd | Process for removing sulphur compounds from hydrocarbons |
| US8936719B2 (en) | 2006-03-22 | 2015-01-20 | Ultraclean Fuel Pty Ltd. | Process for removing sulphur from liquid hydrocarbons |
| US9441169B2 (en) | 2013-03-15 | 2016-09-13 | Ultraclean Fuel Pty Ltd | Process for removing sulphur compounds from hydrocarbons |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3227521B2 (en) * | 1992-04-06 | 2001-11-12 | 舟越 泉 | Method for recovering organic sulfur compounds from liquid oil |
| US6160193A (en) * | 1997-11-20 | 2000-12-12 | Gore; Walter | Method of desulfurization of hydrocarbons |
| CN1202209C (en) * | 2003-01-17 | 2005-05-18 | 石油大学(北京) | Desulfurizing method for petroleum product |
| CN1247294C (en) * | 2003-11-02 | 2006-03-29 | 华北电力大学 | Method and equipment of desulfurization and denitrogenation for purifying flue gas |
-
2005
- 2005-07-12 CN CNB2005100177801A patent/CN1309805C/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8936719B2 (en) | 2006-03-22 | 2015-01-20 | Ultraclean Fuel Pty Ltd. | Process for removing sulphur from liquid hydrocarbons |
| WO2014138810A1 (en) * | 2013-03-15 | 2014-09-18 | Ultraclean Pty Ltd | Process for removing sulphur compounds from hydrocarbons |
| JP2016514185A (en) * | 2013-03-15 | 2016-05-19 | ウルトラクリーン フューエル ピーティーワイ リミテッド | Process for removing sulfur compounds from hydrocarbons |
| US9441169B2 (en) | 2013-03-15 | 2016-09-13 | Ultraclean Fuel Pty Ltd | Process for removing sulphur compounds from hydrocarbons |
| US10214697B2 (en) | 2013-03-15 | 2019-02-26 | Ultraclean Fuel Pty Limited | Process for removing sulphur compounds from hydrocarbons |
| CN103387845A (en) * | 2013-07-26 | 2013-11-13 | 淮阴师范学院 | Persulfate-hydrochloric acid fuel oil oxidation desulfurizing agent and desulfurizing method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1309805C (en) | 2007-04-11 |
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Address after: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: China Petrochemical Group Corp. Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: China Petrochemical Group Corp. |
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Owner name: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORAT Free format text: FORMER OWNER: SINOPEC GROUP Effective date: 20130326 Free format text: FORMER OWNER: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORATION Effective date: 20130326 |
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Effective date of registration: 20130326 Address after: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Patentee before: China Petrochemical Group Corp. Patentee before: Luoyang Petrochemical Engineering Corporation /SINOPEC |