CN106398746A - Gasoline desulfurization method - Google Patents
Gasoline desulfurization method Download PDFInfo
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- CN106398746A CN106398746A CN201611064621.1A CN201611064621A CN106398746A CN 106398746 A CN106398746 A CN 106398746A CN 201611064621 A CN201611064621 A CN 201611064621A CN 106398746 A CN106398746 A CN 106398746A
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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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/003—Specific sorbent material, not covered by C10G25/02 or C10G25/03
-
- 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
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
- B01J20/0211—Compounds of Ti, Zr, Hf
-
- 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
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
- B01J20/0225—Compounds of Fe, Ru, Os, Co, Rh, Ir, Ni, Pd, Pt
-
- 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
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/06—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04
-
- 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
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
- C10G25/12—Recovery of used adsorbent
-
- 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
- C10G2300/1037—Hydrocarbon fractions
-
- 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)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a gasoline desulfurization method which comprises the following steps: heating the raw material gasoline to 20-400 DEG C, feeding the gasoline into a fixed-bed reactor to contact an adsorbent at the volumetric space velocity of 0.2-10 h<-1> under the operating pressure of 0.1-3 MPa; and after the desulfurizer is saturated, stopping feeding the raw material gasoline, and passing hydrogen through a desulfurization adsorbent bed layer at the temperature of 0-50 DEG C higher than adsorbent temperature at the volumetric space velocity of 10-2000 h<-1> under the operating pressure of 0.1-3 MPa, thereby performing desulfurization treatment on the desulfurization adsorbent. The desulfurization adsorbent comprises the following raw materials in parts by weight: 75-85 parts of ZnO, 2-10 parts of reduced-state Ni and 3-8 parts of TiC. The method can implement gasoline deep desulfurization under the condition of keeping lower loss of octane number.
Description
Technical field
The invention belongs to Petroleum Processing Technology field is and in particular to a kind of sulfur method of gasoline.
Background technology
With economic fast development in world wide, the consumption of motor petrol grows with each passing day, because people are to environmental protection
The continuous improvement requiring, the atmosphere polluting problem that vehicle exhaust causes has caused the close attention of people.Motor vehicle exhaust emission reaches
Target it is critical only that the quality improving vehicle fuel oil, and therefore, America and Europe has promulgated automobile exhaust emission standard, restricting vehicle in succession
CO, SO in tail gasX、NOX, the content of the noxious pollutant such as particulate matter and soot.Research shows, if the sulfur content in gasoline is from 50 μ
G/g increases to 450 μ g/g, then in vehicle exhaust, hydrocarbon emission amount can increase by 18%, and carbon monoxide can increase by 19%, nitrogen
Oxygen compound can increase by 9%.As can be seen here, its sulfur content in gasoline is conducive to controlling the row of noxious pollutant in vehicle exhaust
Put.
With the attention to environmental problem for the countries in the world, the pollution problem caused by sulphur in motor petrol is increasingly subject to
To concern.Many countries have formulated strict standard and have limited the sulfur content in gasoline.The Europe IV standard specifies, sulfur in gasoline quality is divided
Number will be less than 50 μ g/g；Sulfur in gasoline mass fraction is down to below 30 μ g/g in June, 2006 by the U.S.；China has also formulated
Corresponding content of sulfur in gasoline standard.Beijing has begun to carry out the Europe IV standard, and plans in comprehensively in line with international standards, vapour in 2010
Sulfur nutrient in oil will be limited in below 10 μ g/g.
For China's gasoline product, the 90～95% of sulfide contained therein carrys out catalytic cracking (FCC) gasoline,
The content of wherein thiophene-type sulfide accounts for more than the 60% of total sulfur content, and the content of thioether sulphur and thiophenic sulfur accounts for the 85% of total sulfur
More than.Hydrodesulfurization is traditional sulfur method, but the method condition is harsh, needs high temperature, high pressure, high to equipment requirement, with
When expend mass energy, also by substantial amounts of alkene saturation while desulfurization, cause octane number loss excessive.Absorption desulfurization
Technology is the method using absorption, is same as and being fully contacted of adsorbent, by sulfur compounds adsorptions all kinds of in gasoline to adsorbent,
Thus reducing the sulfur content of gasoline.But there is the defect of adsorption efficiency difference in adsorbent desulfurization.
Content of the invention
The technical problem to be solved in the present invention is to provide one kind to enable vapour in the case of keeping relatively low loss of octane number
The process for deep desulphurization of oil.
The technical scheme that the present invention provides is a kind of sulfur method of gasoline, and feed gasoline is heated to 20～400 DEG C,
Volume space velocity 0.2～10h-1, enter fixed bed reactors under conditions of operating pressure 0.1～3MPa and contact with adsorbent, desulfurization
Stop after agent adsorption saturation entering feedstock oil, be higher than 0～50 DEG C of adsorption temp in temperature, volume space velocity is 10～2000h-1, behaviour
Under conditions of making pressure 0.1～3MPa, make hydrogen pass through desulfuration adsorbent bed, desulfurization process are carried out to desulfuration adsorbent；
Described desulfuration adsorbent includes the raw material composition of following weight portion：75～85 parts of ZnO, reduction-state Ni2～10 part,
3～8 parts of TiC.
ZnO structure interval is big, and zinc easily enters gap, forms zinc interstitial atom and room, and interstitial zinc ions free energy is high, holds
Easily cross crystal boundary, lead to crystal boundary migration, thus causing crystal grain to grow up it is well known that the quantity of interstitial zinc ions determines
ZnO grain size, interstitial zinc ions quantity is more, and ZnO free energy is higher, and crystal grain is more easily reunited, and leads to particle diameter to increase.
And the interpolation of TiC, Ti can replace zinc atom and carry out gap titanium, but the free energy of titanium is low, therefore can effectively suppress ZnO brilliant
The reunion of grain, substantially reduces the size of ZnO crystal grain.
The desulphurizing activated of desulfuration adsorbent is limited to decomposition rate on metallic nickel for the thiophene in the starting stage, when ZnO quilt
After partial vulcanization, diffusion velocity in ZnO for the element sulphur becomes desulphurizing activated decisive factor, and the surface area of ZnO is bigger, particle
Less, Ni/ZnO's is desulphurizing activated higher.Therefore, on the basis of Ni/ZnO adsorbent, add TiC and can significantly reduce ZnO grain
The size of son, thus improve desulfurized effect
According to the experimental data of applicant, ZnO particle size can be reduced to below 6nm, desulfurization by the interpolation of TiC
The apparent activation energy of reaction is remarkably decreased, and the desulfurization performance of adsorbent increases substantially.
Described desulfuration adsorbent also includes MgO 1～3 weight portion.It is common that the interpolation of MgO can work in coordination with TiC solute retardation
Suppression ZnO crystal grain is grown up.
Described desulfuration adsorbent also includes Y2O30.5～2 weight portion.Y2O3The effect of cyrystal boundary segregation can be played, thus pressing down
ZnO crystal grain processed is grown up.
The preparation method of described desulfuration adsorbent is：By Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in deionized water respectively
In, then three kinds of solution are mixed, heat up precipitation, washing is filtered, filter cake dried, adds TiC, at 400～500 DEG C
Carry out roasting, the as adsorbent of oxidation state, NiO hydrogenating reduction is become Ni, as desulfuration adsorbent.
The preparation method of described desulfuration adsorbent is：By Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in deionized water respectively
In, then three kinds of solution are mixed, heat up precipitation；By precipitation washing, filter, filter cake is dried, adds TiC and MgO,
Carry out roasting, the as adsorbent of oxidation state at 400～500 DEG C, NiO hydrogenating reduction is become Ni, as desulfuration adsorbent.
The preparation method of described desulfuration adsorbent is：By Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in deionized water respectively
In, then three kinds of solution are mixed, heat up precipitation, washing is filtered, filter cake dried, adds TiC, MgO and Y2O3, 400
Carry out roasting, the as adsorbent of oxidation state at～500 DEG C, NiO hydrogenating reduction is become Ni, as desulfuration adsorbent.
Described desulfuration adsorbent particle diameter be 100～500 μm.
Compared with prior art, the invention has the advantages that：
1) add, in Ni/ZnO, the reunion that TiC can effectively suppress ZnO crystal grain, substantially reduce the size of ZnO crystal grain, from
And improve the desulfurized effect of adsorbent.
2) it is also added with MgO in Ni/ZnO and can work in coordination with TiC solute retardation jointly suppressing ZnO crystal grain to grow up, further
Improve the desulfurized effect of adsorbent.
3) being also added with the effect that Y2O3 can play cyrystal boundary segregation in Ni/ZnO, thus suppressing ZnO crystal grain to grow up, more entering one
Step improves the desulfurized effect of adsorbent.
Specific embodiment
The present invention is further elaborated for specific examples below, but not as a limitation of the invention.
Embodiment 1
1) by Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up
Precipitated to 90 DEG C, kept 12h.After the completion of precipitation, wash with water and precipitate three times, filter, obtain filter cake.Filter cake is positioned over baking
In case, dry at 120 DEG C, then the powder being dried is mixed with TiC, carry out roasting, the as suction of oxidation state at 400 DEG C
Attached dose.It is passed through H in the adsorbent of the most backward oxidation state2Reduced, reduction temperature is 370 DEG C, reduced pressure 0.5MPa, reduction
Hydrogen flowrate 40ml/min, recovery time 1h, NiO is reduced into Ni, is crushed to particle diameter and is 100 μm, as desulfuration adsorbent.Desulfurization
In adsorbent, ZnO 75 weight portion, reduction-state Ni2 weight portion, TiC 3 weight portion.
2) feed gasoline A is heated to 20 DEG C, in volume space velocity 0.2h-1, enter solid under conditions of operating pressure 0.1MPa
Fixed bed reactor is contacted with adsorbent, stops entering feedstock oil after desulfurizing agent adsorption saturation, is higher than 10 DEG C of adsorption temp in temperature,
Volume space velocity is 10h-1, under conditions of operating pressure 0.1MPa, make hydrogen pass through desulfuration adsorbent bed, desulfuration adsorbent entered
Row desulfurization process.In gasoline after desulfurization process, sulfur content is 6.2 μ g/g after testing, and octane number does not lose.
Comparative example 1
1) by Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up
Precipitated to 90 DEG C, kept 12h.After the completion of precipitation, wash with water and precipitate three times, filter, obtain filter cake.Filter cake is positioned over baking
In case, dry at 120 DEG C, then the powder being dried is carried out roasting, the as adsorbent of oxidation state at 400 DEG C.Finally
It is passed through H in the adsorbent of oxidation state2Reduced, reduction temperature is 370 DEG C, reduced pressure 0.5MPa, reduced hydrogen flowrate
40ml/min, recovery time 1h, NiO is reduced into Ni, is crushed to particle diameter and is 100 μm, as desulfuration adsorbent.Desulfuration adsorbent
In, ZnO 75 weight portion, reduction-state Ni2 weight portion, TiC 3 weight portion.
2) feed gasoline A is heated to 20 DEG C, in volume space velocity 0.2h-1, enter solid under conditions of operating pressure 0.1MPa
Fixed bed reactor is contacted with adsorbent, stops entering feedstock oil after desulfurizing agent adsorption saturation, is higher than 10 DEG C of adsorption temp in temperature,
Volume space velocity is 10h-1, under conditions of operating pressure 0.1MPa, make hydrogen pass through desulfuration adsorbent bed, desulfuration adsorbent entered
Row desulfurization process.In gasoline after desulfurization process, sulfur content is 19.1 μ g/g after testing, and octane number does not lose.
Embodiment 2
1) by Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up
Precipitated to 90 DEG C, kept 12h.After the completion of precipitation, wash with water and precipitate three times, filter, obtain filter cake.Filter cake is positioned over baking
In case, dry at 120 DEG C, then the powder being dried is mixed with TiC, carry out roasting, the as suction of oxidation state at 500 DEG C
Attached dose.It is passed through H in the adsorbent of the most backward oxidation state2Reduced, reduction temperature is 370 DEG C, reduced pressure 0.5MPa, reduction
Hydrogen flowrate 40ml/min, recovery time 1h, NiO is reduced into Ni, is crushed to particle diameter and is 500 μm, as desulfuration adsorbent.Desulfurization
In adsorbent, ZnO 85 weight portion, reduction-state Ni 10 weight portion, TiC 8 weight portion.
2) feed gasoline A is heated to 400 DEG C, in volume space velocity 10h-1, enter under conditions of operating pressure 3MPa and fix
Bed reactor is contacted with adsorbent, stops entering feedstock oil after desulfurizing agent adsorption saturation, is higher than 50 DEG C of adsorption temp in temperature, body
Long-pending air speed is 2000h-1, under conditions of operating pressure 3MPa, make hydrogen pass through desulfuration adsorbent bed, desulfuration adsorbent carried out
Desulfurization process.In gasoline after desulfurization process, sulfur content is 5.9 μ g/g after testing, and octane number does not lose.
Embodiment 3
1) by Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up
Precipitated to 90 DEG C, kept 12h.After the completion of precipitation, wash with water and precipitate three times, filter, obtain filter cake.Filter cake is positioned over baking
In case, dry at 120 DEG C, then the powder being dried is mixed with TiC, carry out roasting, the as suction of oxidation state at 450 DEG C
Attached dose.It is passed through H in the adsorbent of the most backward oxidation state2Reduced, reduction temperature is 370 DEG C, reduced pressure 0.5MPa, reduction
Hydrogen flowrate 40ml/min, recovery time 1h, NiO is reduced into Ni, is crushed to particle diameter and is 300 μm, as desulfuration adsorbent.Desulfurization
In adsorbent, ZnO 80 weight portion, reduction-state Ni 8 weight portion, TiC 5 weight portion.
2) feed gasoline A is heated to 200 DEG C, in volume space velocity 5h-1, under conditions of operating pressure 3MPa, enter fixed bed
Reactor is contacted with adsorbent, stops entering feedstock oil after desulfurizing agent adsorption saturation, is higher than 25 DEG C of adsorption temp in temperature, volume
Air speed is 1000h-1, under conditions of operating pressure 1.5MPa, make hydrogen pass through desulfuration adsorbent bed, desulfuration adsorbent carried out
Desulfurization process.In gasoline after desulfurization process, sulfur content is 5.5 μ g/g after testing, 0.1 unit of loss of octane number.
Embodiment 4
1) by Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up
Precipitated to 90 DEG C, kept 12h.After the completion of precipitation, wash with water and precipitate three times, filter, obtain filter cake.Filter cake is positioned over baking
In case, dry at 120 DEG C, then the powder being dried is mixed with TiC, carry out roasting, the as suction of oxidation state at 400 DEG C
Attached dose.It is passed through H in the adsorbent of the most backward oxidation state2Reduced, reduction temperature is 370 DEG C, reduced pressure 0.5MPa, reduction
Hydrogen flowrate 40ml/min, recovery time 1h, NiO is reduced into Ni, is crushed to particle diameter and is 500 μm, as desulfuration adsorbent.Desulfurization
In adsorbent, ZnO 75 weight portion, reduction-state Ni 10 weight portion, TiC 3 weight portion.
2) feed gasoline A is heated to 400 DEG C, in volume space velocity 0.2h-1, enter under conditions of operating pressure 3MPa and fix
Bed reactor is contacted with adsorbent, stops entering feedstock oil after desulfurizing agent adsorption saturation, is higher than 0 DEG C of adsorption temp in temperature, body
Long-pending air speed is 2000h-1, under conditions of operating pressure 0.1MPa, make hydrogen pass through desulfuration adsorbent bed, desulfuration adsorbent entered
Row desulfurization process.In gasoline after desulfurization process, sulfur content is 5.6 μ g/g after testing, and octane number does not lose.
In the desulfuration adsorbent that embodiment 1～4 and comparative example 1 are obtained, the granularity of ZnO is detected, result see table 1：
The size of ZnO crystal grain in table 1 each group desulfuration adsorbent
With the catalytic gasoline A of selective hydrodesulfurization as feed gasoline, its property see table 2：
Table 2：The main character of the used feed gasoline of embodiment
Claims (7)
1. gasoline sulfur method it is characterised in that：Feed gasoline is heated to 20～400 DEG C, in volume space velocity 0.2～10h-1, enter fixed bed reactors under conditions of operating pressure 0.1～3MPa and contact with adsorbent, stop after desulfurizing agent adsorption saturation
Enter feedstock oil, be higher than 0～50 DEG C of adsorption temp in temperature, volume space velocity is 10～2000h-1, operating pressure 0.1～3MPa's
Under the conditions of, make hydrogen pass through desulfuration adsorbent bed, desulfurization process are carried out to desulfuration adsorbent；
Described desulfuration adsorbent includes the raw material composition of following weight portion：75～85 parts of ZnO, reduction-state Ni2～10 part, TiC 3
～8 parts.
2. gasoline according to claim 1 sulfur method it is characterised in that：Described desulfuration adsorbent also includes MgO 1
～3 weight portions.
3. gasoline according to claim 2 sulfur method it is characterised in that：Described desulfuration adsorbent also includes Y2O3
0.5～2 weight portion.
4. gasoline according to claim 1 sulfur method it is characterised in that：The preparation method of described desulfuration adsorbent
For：By Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up precipitation, water
Wash, filter, filter cake is dried, adds TiC, carry out roasting, the as adsorbent of oxidation state at 400～500 DEG C, by NiO
Hydrogenating reduction becomes Ni, as desulfuration adsorbent.
5. gasoline according to claim 2 sulfur method it is characterised in that：The preparation method of described desulfuration adsorbent
For：By Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up precipitation；Will
Precipitation washing, filters, filter cake is dried, adds TiC and MgO, carry out roasting, the as suction of oxidation state at 400～500 DEG C
Attached dose, NiO hydrogenating reduction is become Ni, as desulfuration adsorbent.
6. gasoline according to claim 3 sulfur method it is characterised in that：The preparation method of described desulfuration adsorbent
For：By Zn (NO3)2、Ni(NO3)2And urea, it is dissolved in respectively in deionized water, then three kinds of solution is mixed, heat up precipitation, water
Wash, filter, filter cake is dried, adds TiC, MgO and Y2O3, carry out roasting, the as absorption of oxidation state at 400～500 DEG C
Agent, NiO hydrogenating reduction is become Ni, as desulfuration adsorbent.
7. the gasoline according to any one of claim 1～6 sulfur method it is characterised in that：Described desulfuration adsorbent
Particle diameter be 100～500 μm.
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| CN201611064621.1A CN106398746B (en) | 2016-11-28 | 2016-11-28 | The sulfur method of gasoline |
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| CN201611064621.1A CN106398746B (en) | 2016-11-28 | 2016-11-28 | The sulfur method of gasoline |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6150300A (en) * | 1996-08-14 | 2000-11-21 | Phillips Petroleum Company | Process to produce sorbents |
| CN101205478A (en) * | 2006-12-22 | 2008-06-25 | 中国科学院大连化学物理研究所 | Adsorbent used for desulfuration-deodorization of solvent oil and preparation thereof |
| CN101844067A (en) * | 2009-03-23 | 2010-09-29 | 通用电气公司 | Surface modified sorbent |
| CN102527322A (en) * | 2012-02-20 | 2012-07-04 | 天津大学 | Method for preparing gasoline deeply desulfurized adsorbent and application of adsorbent |
-
2016
- 2016-11-28 CN CN201611064621.1A patent/CN106398746B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6150300A (en) * | 1996-08-14 | 2000-11-21 | Phillips Petroleum Company | Process to produce sorbents |
| CN101205478A (en) * | 2006-12-22 | 2008-06-25 | 中国科学院大连化学物理研究所 | Adsorbent used for desulfuration-deodorization of solvent oil and preparation thereof |
| CN101844067A (en) * | 2009-03-23 | 2010-09-29 | 通用电气公司 | Surface modified sorbent |
| CN102527322A (en) * | 2012-02-20 | 2012-07-04 | 天津大学 | Method for preparing gasoline deeply desulfurized adsorbent and application of adsorbent |
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| CN106398746B (en) | 2018-06-19 |
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