CN106635127A - Method for removing organic sulfide from fuel oil through catalytic oxidation - Google Patents
Method for removing organic sulfide from fuel oil through catalytic oxidation Download PDFInfo
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- CN106635127A CN106635127A CN201611204416.0A CN201611204416A CN106635127A CN 106635127 A CN106635127 A CN 106635127A CN 201611204416 A CN201611204416 A CN 201611204416A CN 106635127 A CN106635127 A CN 106635127A
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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
- C10G27/00—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation
- C10G27/04—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen
- C10G27/12—Refining of hydrocarbon oils in the absence of hydrogen, by oxidation with oxygen or compounds generating oxygen with oxygen-generating compounds, e.g. per-compounds, chromic acid, chromates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/14—Phosphorus; Compounds thereof
- B01J27/186—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J27/188—Phosphorus; Compounds thereof with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum, tungsten or polonium
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method for removing organic sulfide from fuel oil through catalytic oxidation. The method comprises the following steps of mixing a catalyst with the fuel oil and reacting with an oxidizing agent to remove sulfur, wherein the catalyst is a porous material loaded with solid heteropolyacid and the load mass percentage of the solid heteropolyacid is 5 to 150 percent. The solid heteropolyacid is loaded on the porous material, the contact area of the oxidizing agent and oil phase is increased and the use amount of the oxidizing agent is greatly reduced; the catalyst is recovered through simple filtration or centrifugation and is reusable through washing and drying, and the activity of the catalyst is reduced non-obviously after the catalyst is used for many times; and after the desulfurization reaction is finished, dibenzothiophene can be removed through simple washing, a desulfurized oil product with extremely low sulfur content is obtained and loss is substantially avoided.
Description
Technical field
The invention belongs to desulfurization of fuel oil technical field, the specifically related to side of catalytic oxidative desulfurization Sulfur content in Fuel Oil compound
Method.
Background technology
With the fast development of social economy, the demand of fuel oil grows with each passing day, what is offered convenience to human lives
Meanwhile, the sulfur oxide produced during use also result in serious air pollution.For this phenomenon, countries in the world are
Jing is formulating stricter sulfur content of fuel oil control regulation.Therefore, the fuel oil for producing super-low sulfur and cleaning is mesh
Front petrochemical industry urgent problem.
At present, industrial the most frequently used petroleum sweetening technology is hydrodesulfurization, i.e., the catalytic hydrogenation under high-temperature and high-pressure conditions
The organic sulfur compound in oil is set to be converted into H2S.The technology is processing on a large scale thousand of ppm high-sulfurs oil products to hundreds of ppm timeliness
Fruit significantly, also there are problems that very big using hydrodesulfurization technology production super-low sulfur oil.In order to produce combustion of the sulfur content less than 10ppm
Material oil, hydrodesulfurization must greatly increase oil refining cost and equipment cost at high temperature under high pressure, using new catalyst.Cause
This, develops new and effective desulfurizing oil technology imperative.
The organosulfur compound such as thiophene-based occupies very big proportion in sulfide contained by fuel oil, especially in catalytic cracking
In gasoline, thiophene-type sulfide accounts for more than the 70% of its total sulfur content.The organic sulfur compounds such as thiophene-based are because boiling point is higher, phase
, stability larger to molecular mass is strong, and traditional hydrodesulfurization is difficult removing, therefore, the purpose of deep desulfuration is reached, it is most main
Wanting for task is to remove the thiophene-based organic sulfur compound that content in fuel oil is high and is difficult to remove.
Catalytic oxidation desulfurization technology is that just thiophene (BT) class that catalytic hydrogenation is difficult to remove can be vulcanized in a mild condition
The technique that thing reaches deep desulfuration.Traditional oxidation-desulfurizing catalyst mostly is liquid phase organic acid or inorganic acid catalyst, this kind of to urge
Agent separates after completion of the reaction difficulty, easy etching apparatus.Solid heteropoly acid as the new catalyst of a class, with composition
Simply, Stability Analysis of Structures, the advantages of catalysis activity is high, by the extensive concern of catalytic field researchers, is applied to deep oxidation
The existing many researchs report of desulfurization, but existing sulfur removal technology generally existing catalyst is difficult to recycle, catalysis activity is relatively low,
Oxidant consumption is big, extractant usage amount is excessive, and the low problem of economic benefit fundamentally limits industrial production.
The content of the invention
The present invention is directed to the deficiencies in the prior art, provides a kind of side of organic sulfur compound in catalytic oxidative desulfurization fuel oil
Method, is provided in particular in a kind of method of dibenzothiophenes class sulfide in catalysis oxidation fuel oil.
Technical scheme is as follows：
A kind of method of organic sulfur compound in catalytic oxidative desulfurization fuel oil, including step is as follows：
With oxidant reaction sulphur removal after catalyst is mixed with fuel oil, described catalyst is to be loaded with solid heteropoly acid
Porous material, the load quality percentage of solid heteropoly acid is 5%-150%.
, according to the invention it is preferred to, the quality of catalyst is 0.001-0.01g/mL with the volumetric mixture ratio of fuel oil, is entered
The preferred 0.005-0.008g/mL of one step.
, according to the invention it is preferred to, described oxidant is H2O2The aqueous solution, the H of further preferred 30wt%2O2It is water-soluble
Liquid；
Preferably, described oxidant and the mixed volume ratio of fuel oil are 1:50-500, further preferably (2-5):
500。
, according to the invention it is preferred to, the cation of described solid heteropoly acid is selected from 1- butyl -3- methylimidazole bromines, 1-
The methylimidazole acetic acid of butyl -3, the methylimidazole chlorine of 1- hexyls -3, the methylimidazole chlorine of 1- pi-allyls -3, the methylimidazole sulphur of 1- propyl group -3
One kind in hydrochlorate, shitosan, most preferably the methylimidazole bromide of 1- butyl -3；The anion of described solid heteropoly acid is phosphorus tungsten
Acid.
, according to the invention it is preferred to, described porous material is activated carbon, SiO 2 powder, meso-porous nano titanium dioxide
One kind in silicon, most preferably meso-porous nano silica；
Preferably, the load quality percentage of solid heteropoly acid is 20%-30%.
, according to the invention it is preferred to, the reaction temperature for reacting sulphur removal is 30-100 DEG C, and the reaction time is 20-180min.
, according to the invention it is preferred to, the organic sulfur compound in described fuel oil is thiophene-type sulfide, further preferably
Dibenzothiophenes sulfide；
Preferably, Sulfur content in Fuel Oil content is 100-1000ppm.
According to the present invention, the method for optimizing of organic sulfur compound in a kind of catalytic oxidative desulfurization fuel oil, including step is as follows：
(1) catalyst is added in fuel oil, is stirred, form mixture；The quality and fuel oil of catalyst
Volumetric mixture ratio be 0.001-0.01g/mL；
(2) oxidant H is added in said mixture2O2, the H of addition2O2It is (2- with the mol ratio of Sulfur content in Fuel Oil
12):1, under the conditions of temperature is for 30-100 DEG C, stirring reaction 20-180min；
(3) stop after reaction, take upper oil phase, the oil of the ultra low sulfur fuels after sulphur removal is obtained Jing after washing, extraction.
, according to the invention it is preferred to, H in step (2)2O2It is (4-6) with the mol ratio of Sulfur content in Fuel Oil：1, reaction temperature
For 65-80 DEG C, the reaction time is 90-120min；
Preferably, the extractant used by step (3) is water, methanol aqueous solution, N,N-Dimethylformamide, nitrogen nitrogen diformazan
One kind in yl acetamide, dimethyl sulfoxide (DMSO)；
Preferably, extractant and the mixed volume ratio of fuel oil are 5:1-1:10.
, according to the invention it is preferred to, step is additionally added acetic acid, H in reaction system in (2)2O2, in acetic acid and fuel oil
The mol ratio of sulphur is 1:1:6.
According to the present invention, described fuel oil can be 200#Solvent naphtha.Described catalyst uses rear recyclable recycling,
The mode of recovery can be i.e. reusable Jing after washing, drying using filtration or centrifugation.
In the present invention, catalyst is present at oil phase and water interfaces, adsorbs hydrogen peroxide, increases H2O2With fuel oil
The contact area of middle sulfide, substantially increases the service efficiency of oxidant.
Present invention advantage maximum compared with prior art is：
1st, solid heteropoly acid is loaded on the porous material, increases the contact area of oxidant and oil phase, is greatly reduced
The usage amount of oxidant.
2nd, catalyst is reclaimed by simply filtering or being centrifuged, and through washing, drying is reusable, and work is used for multiple times
Property reduce it is unobvious.
3rd, desulphurization reaction terminates, and can simply wash can just remove dibenzothiophenes, obtains the extremely low sweet oil of sulfur content
Product, and basic free of losses.
4th, the inventive method is simple, and operating condition is gentle, low cost, with great application prospect.
Specific embodiment
With reference to specific embodiment, the invention will be further described, but not limited to this.
In embodiment it is raw materials used if no special instructions, can market buy.
[BMIM]3The mesoporous SiO of HPW/2Can be obtained as follows：
Weigh 1g porous SiO2It is dissolved in 50ml deionized waters and forms suspension, 0.0557g [BMIM] the Br aqueous solution is slow
Slowly in instilling above-mentioned suspension, it is sufficiently stirred at 40 DEG C after 1.5h, is slowly added dropwise 30ml dissolved with 0.244g phosphotungstic acid aqueous solutions, it is raw
Into white precipitate, filter, washing obtains surface into oily solid, dries at 60 DEG C, obtains final product.In the same way, can be obtained
[BMIM]3HPW/ activated carbons, [HMIM]3HPW/SiO2、[BMIM]3The mesoporous SiO of HPW/2Deng.
Embodiment 1
Dibenzothiophenes is dissolved in into isooctane and is made into mould oil, its sulfur content is 200ppm.50ml mould oils are added
In the there-necked flask of 100ml, by [BMIM] that 0.07g load quality contents are 30%3The mesoporous SiO of HPW/2Add above-mentioned reactant
System, stirring.By 30wt%H2O2By O:S=4：1 mol ratio, adds reaction system, stirring reaction 100 minutes at 75 DEG C.Reaction
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content<1ppm.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 2.3ppm.
Embodiment 2
Dibenzothiophenes is dissolved in into isooctane and is made into mould oil, its sulfur content is 200ppm.50ml mould oils are added
In the there-necked flask of 100ml, by [BMIM] that 0.07g load quality contents are 30%3The mesoporous SiO of HPW/2Add above-mentioned reactant
System, stirring.By 30wt%H2O2By O:S=4：1 mol ratio, adds reaction system, stirring reaction 100 minutes at 70 DEG C.Reaction
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 13ppm.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 29.9ppm.
Embodiment 3
Dibenzothiophenes is dissolved in into isooctane and is made into mould oil, its sulfur content is 200ppm.50ml mould oils are added
In the there-necked flask of 100ml, by [BMIM] that 0.08g load quality contents are 30%3HPW/SiO2Above-mentioned reaction system is added,
Stirring.By 30wt%H2O2By O:S=5：1 mol ratio, adds reaction system, stirring reaction 100 minutes at 70 DEG C.Reaction knot
Beam takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 2.1ppm, the oil after oxidation and nitrogen nitrogen dimethyl
Formamide by volume 4:1 extracts once, sulfur content<1ppm, oil and methanol aqueous solution (methyl alcohol：Water=4:1) volume ratio=2；1
Extract once, sulfur content 1.37ppm.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 5.8ppm.
Embodiment 4
Dibenzothiophenes is dissolved in into isooctane and is made into mould oil, its sulfur content is 200ppm.50ml mould oils are added
In the there-necked flask of 100ml, by [BMIM] that 0.08g load quality contents are 50%3HPW/ activated carbons add above-mentioned reactant
System, stirring.By 30wt%H2O2By O:S=6：1 mol ratio, adds reaction system, stirring reaction 120 minutes at 70 DEG C.Reaction
End takes upper oil phase by DMF:Simulation oil=2:5 extractions once, are as a result determined, sulfur content 27ppm using microcoulomb instrument.
By catalyst [BMIM]3HPW/ activated carbon recyclings, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase by DMF:Simulation oil=2:5 extractions once, are as a result determined, sulfur content 34.5ppm using microcoulomb instrument.
Embodiment 5
Dibenzothiophenes is dissolved in into isooctane and is made into mould oil, its sulfur content is 200ppm.50ml mould oils are added
In the there-necked flask of 100ml, by [HMIM] that 0.07g load quality contents are 20%3HPW/SiO2Above-mentioned reaction system is added,
Stirring.By 30wt%H2O2By O:S=5：1 mol ratio, adds reaction system, stirring reaction 120 minutes at 60 DEG C.Reaction knot
Beam takes upper oil phase by DMF:Simulation oil=2:5 extractions once, are as a result determined, sulfur content 5.84ppm using microcoulomb instrument.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 11.7ppm.
Embodiment 6
Dibenzothiophenes is dissolved in into isooctane and is made into mould oil, its sulfur content is 200ppm.50ml mould oils are added
In the there-necked flask of 100ml, 0.1g chitosan phosphotungstates are added into above-mentioned reaction system, stirring.By 30wt%H2O2By O:S
=6：1 mol ratio, adds reaction system, stirring reaction 120 minutes at 60 DEG C.Reaction end takes upper oil phase by DMF:Simulation
Oil=1:2 extractions once, are as a result determined, sulfur content 23.1ppm using microcoulomb instrument.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase and washes three times, is as a result determined using microcoulomb instrument, sulfur content 38.3ppm.
Embodiment 7
It is the 200 of 180ppm by 50ml sulfur contents#Solvent naphtha is added in the there-necked flask of 100ml, by 0.08g load qualities
Content is 30% [BMIM]3The mesoporous SiO of HPW/2Above-mentioned reaction system is added, is stirred.By 30wt%H2O2The aqueous solution presses O:S=
6：1 mol ratio, adds reaction system, stirring reaction 120 minutes at 75 DEG C.Reaction end takes upper oil phase by DMF:Simulation oil
=1:2 extractions once, are as a result determined, sulfur content 21.9ppm using microcoulomb instrument.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase by DMF:Simulation oil=1:2 extractions once, are as a result determined, sulfur content 33.6ppm using microcoulomb instrument.
Embodiment 8
It is the 200 of 180ppm by 50ml sulfur contents#Solvent naphtha is added in the there-necked flask of 100ml, by 0.08g load qualities
Content is 30% [BMIM]3The mesoporous SiO of HPW/2Above-mentioned reaction system is added, is stirred.Acetic acid is introduced in reaction system, will
30wt%H2O2The aqueous solution, acetic acid press O:CH3COOH:S=1:1:6, add reaction system, 120 points of stirring reaction at 75 DEG C
Clock.Reaction end takes upper oil phase by DMF:Simulation oil=1:2 extractions once, are as a result determined using microcoulomb instrument, and as a result sulphur contains
Amount 1.3ppm.
By catalyst [BMIM]3The mesoporous SiO of HPW/2Recycling, after reusing 5 times aforesaid operations are carried out again, are reacted
End takes upper oil phase by DMF:Simulation oil=1:2 extractions once, are as a result determined, sulfur content 3.2ppm using microcoulomb instrument.
Claims (10)
1. in a kind of catalytic oxidative desulfurization fuel oil organic sulfur compound method, including step is as follows：
With oxidant reaction sulphur removal after catalyst is mixed with fuel oil, described catalyst is be loaded with solid heteropoly acid many
Porous materials, the load quality percentage of solid heteropoly acid is 5%-150%.
2. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, it is characterised in that catalysis
The quality of agent is 0.001-0.01g/mL, preferred 0.005-0.008g/mL with the volumetric mixture ratio of fuel oil.
3. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, it is characterised in that it is described
Oxidant be H2O2The aqueous solution, the H of preferred 30wt%2O2The aqueous solution；
Preferably, described oxidant and the mixed volume ratio of fuel oil are 1:50-500, further preferably (2-5):500.
4. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, it is characterised in that it is described
Solid heteropoly acid cation be selected from 1- butyl -3- methylimidazole bromines, the methylimidazole acetic acid of 1- butyl -3, the methyl of 1- hexyls -3
One kind in imidazoles chlorine, the methylimidazole chlorine of 1- pi-allyls -3, the methylimidazole sulfonate of 1- propyl group -3, shitosan, described solid
The anion of heteropoly acid is phosphotungstic acid.
5. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, it is characterised in that it is described
Porous material be activated carbon, SiO 2 powder, meso-porous nano silica in one kind；
Preferably, the load quality percentage of solid heteropoly acid is 20%-30%.
6. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, it is characterised in that reaction
The reaction temperature of sulphur removal is 30-100 DEG C, and the reaction time is 20-180min.
7. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, it is characterised in that it is described
Fuel oil in organic sulfur compound be thiophene-type sulfide, preferred dibenzothiophenes sulfide；
Preferably, Sulfur content in Fuel Oil content is 100-1000ppm.
8. in catalytic oxidative desulfurization fuel oil according to claim 1 organic sulfur compound method, including step is as follows：
(1) catalyst is added in fuel oil, is stirred, form mixture；The quality of catalyst and the body of fuel oil
Product mixing ratio is 0.001-0.01g/mL；
(2) oxidant H is added in the mixture described in step (1)2O2, the H of addition2O2It is with the mol ratio of Sulfur content in Fuel Oil
(2-12):1, under the conditions of temperature is for 30-100 DEG C, stirring reaction 20-180min；
(3) stop after reaction, take upper oil phase, the oil of the ultra low sulfur fuels after sulphur removal is obtained Jing after washing, extraction.
9. in catalytic oxidative desulfurization fuel oil according to claim 8 organic sulfur compound method, it is characterised in that step
(2) H in2O2It is (4-6) with the mol ratio of Sulfur content in Fuel Oil：1, reaction temperature is 65-80 DEG C, and the reaction time is 90-120min；
Preferably, the extractant used by step (3) is water, methanol aqueous solution, N,N-Dimethylformamide, nitrogen nitrogen dimethyl second
One kind in acid amides, dimethyl sulfoxide (DMSO)；
Preferably, extractant and the mixed volume ratio of fuel oil are 5:1-1:10.
10. in catalytic oxidative desulfurization fuel oil according to claim 8 organic sulfur compound method, it is characterised in that step
Suddenly acetic acid, H are additionally added in reaction system in (2)2O2, acetic acid and Sulfur content in Fuel Oil mol ratio be 1:1:6.
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| CN113976181A (en) * | 2021-09-29 | 2022-01-28 | 江苏大学 | Preparation of cobalt-based metal organic framework immobilized organic catalyst and application of catalyst in field of fuel oil desulfurization |
| CN113862026A (en) * | 2021-10-26 | 2021-12-31 | 山东圳谷新材料科技有限公司 | Method for catalyzing fuel oil by catalytic oxidation desulfurization catalyst and application thereof |
| CN114621782A (en) * | 2022-03-21 | 2022-06-14 | 中节能工程技术研究院有限公司 | Ultra-deep oxidation desulfurization reaction based on Pickering emulsion |
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