CN104277877A - Adsorption desulfurization process of cracked gasoline - Google Patents
Adsorption desulfurization process of cracked gasoline Download PDFInfo
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- CN104277877A CN104277877A CN201310292089.9A CN201310292089A CN104277877A CN 104277877 A CN104277877 A CN 104277877A CN 201310292089 A CN201310292089 A CN 201310292089A CN 104277877 A CN104277877 A CN 104277877A
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- adsorption
- desulfuration adsorbent
- adsorbent
- desulfurization
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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
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
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- Chemical & Material Sciences (AREA)
- 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)
Abstract
The invention discloses an adsorption desulfurization process of a cracked gasoline. The adsorption desulfurization process is a method for producing clean gasoline meeting the European V sulfur index requirement (less than 10 micrograms/gram of sulfur content) by combining non-hydrogenation physical adsorption desulfurization and a hydrogenation treatment adsorbent. The adsorption desulfurization process is characterized in that the catalytic gasoline (less than 150 micrograms/gram of sulfur content) treated by selective hydrodesulfurization is selected as the raw material and goes into a fixed bed reactor to contact with a desulfurization adsorbent, the catalytic gasoline desulfurized by adsorption goes out of the fixed bed reactor, the feeding of the raw material oil is stopped until saturated adsorption of the desulfurization adsorbent, the hydrogen gas is introduced to pass through the bed layer of the desulfurization adsorbent to perform hydrogenation treatment on the desulfurization adsorbent, and the hydrogenated desulfurization adsorbent can be continuously used for adsorbing sulfides in the catalytic gasoline. The adsorption desulfurization process of the cracked gasoline can be joined with the existing selective hydrodesulfurization process to produce the clean gasoline meeting the European V sulfur index requirement; the adsorption desulfurization process is low in equipment investment, convenient in desulfurization adsorbent loading, high in desulfurization rate, simple in process procedure, free of loss of octane number, and suitable for industrial application.
Description
Technical field
The present invention relates to a kind of method of adsorbing and desulfurizing catalytic cracking gasoline, belong to Petroleum Processing Technology field.
Background technology
The subject matter of China's quality of gasoline is that sulphur content and olefin(e) centent are high, and reason is that the ratio accounted in gasoline pool due to catalytically cracked gasoline is too high.In China, catalytically cracked gasoline is the main blend component of gasoline, accounts for more than 75%.Use catalytic cracking olefine lowering catalyst, auxiliary agent and new catalytic cracking technology, the olefin(e) centent in catalytic gasoline can be made to be down to
after traditional selective hydrogenation desulfurization process, olefin(e) centent can reduce further, then oil refinery gasoline can be made to reach olefin(e) centent by allotment and be less than
target.But sulphur content is less than 50 μ g/g or is less than that the requirement of 10 μ g/g is just more difficult to be reached further, and when deep hydrodesulfurizationof, the hydrogenation reaction of unsaturated hydrocarbons is violent, and hydrogen consumption increases considerably, and the loss of octane number of gasoline is larger.Oil refining enterprise and scientific research institution carry out the research of Novel desulphurization technology one after another, and gasoline absorbing desulfurization technique is paid attention to gradually.Adsorption desulfurize can be divided into chemisorption and physical adsorption two class, and chemisorption is generally carried out under hydro condition, there is olefin saturated, loss of octane number, and physical adsorption is generally carried out under conditions of non-hydrogen, there is not loss of octane number.
Patent WO03/084656(S-zorb technique) disclose a kind of hydrocarbon sweetening system using renewable Solid desulfuration adsorbent particle in fluid-bed sweetening reactor.This technique adopts fluidized-bed reactor, and desulfuration adsorbent particle being circulated in reactor, regeneration system rapidly and reducer, achieves the continuous desulfurization of catalytically cracked gasoline and the cyclic regeneration of desulfuration adsorbent, is the Typical Representative of chemisorption desulfurization.
Patent US5730860(IRVAD technique) adopt a kind of solid aluminum based selective sorbent material through inorganic accelerator modification, in multi-stage absorption tower, sorbent material and gasoline counter current contact (moving bed process), adsorbing and removing sulfocompound wherein, desulfurization degree reaches more than 90%.The sorbent material of inactivation regenerates in the activator of atmosphere of hydrogen, and being recycled to adsorption tower and continuing to use, is the Typical Representative of physical adsorption desulfurization.
The LADS technique of patent CN200410010353.6(Sinopec Luoyang Petrochemical engineering corporation exploitation, belongs to physical adsorption) inferior patrol is heated to 20 ~ 220 DEG C, be 0.1 ~ 10h at volume space velocity
-1pressure is contact with desulfuration adsorbent under the condition of normal pressure ~ 0.5MPa, gasoline after desulfurization goes out device, after desulfuration adsorbent absorption is saturated, desorbing agent is utilized to carry out desorption process to desulfuration adsorbent, after carrying out adsorption and desorption process 1 ~ 1000 time afterwards again, adopt regenerator to regenerate desulfuration adsorbent, the sorbent circulation after regeneration uses.Described desorbing agent is one or more mixture of water vapour, purification dry gas, nitrogen or air, and described regenerator is C
1~ C
5small molecules aliphatic alcohols, C
2~ C
8ethers, C
3~ C
5ketone or C
6~ C
8arene compounds in one or more mixture.This technique can be down to 800 ~ 400 μ g/g the sulphur content in gasoline from 1290 μ g/g.
Although adsorption desulfurize has good removal effect for the sulfide in gasoline, no matter be chemisorption or physical adsorption, the sulfur capacity of desulfuration adsorbent is limited, needs frequent regeneration.Therefore S-zorb adopts fluidized-bed process, and IRVAD adopts moving bed process.But adopt fluidized-bed or moving-burden bed reactor to have higher requirement to parameters such as the intensity of desulfuration adsorbent, the reaction of S-Zorb technique, regeneration and reduction are carried out in different reactors, and investment is large, and energy consumption is high.Absorption and the regeneration of IRVAD technique are also carried out in different reactors, and desulfuration adsorbent is also very short for work-ing life in addition.Adsorption and desorption and the regeneration of LADS technique can be carried out in same reactor, but its sweetening effectiveness is poor, is difficult to realize industrial application.
Summary of the invention
The present invention is with the catalytic gasoline after selective hydrodesulfurization for raw material, and object is to provide a kind of method adopting fixed-bed process non-hydrogen physical adsorption desulfurization production to meet Europe V sulphur index request (being less than 10 μ g/g) clean gasoline.
The present invention is realized by following steps:
1. heating raw materials is to 20 ~ 400 DEG C, at volume space velocity 0.2 ~ 10h
-1, enter fixed-bed reactor under the condition of working pressure 0.1 ~ 3MPa and contact with desulfuration adsorbent, the catalytic gasoline after adsorption desulfurize goes out fixed-bed reactor.Preferred processing condition be heating raw materials to 100 ~ 350 DEG C, volume space velocity is 0.5 ~ 5h
-1, working pressure is 0.5 ~ 2MPa.
2. the incoming stock oil of the desulfuration adsorbent saturated rear stopping of absorption, in temperature higher than adsorption temp 0 ~ 50 DEG C, volume space velocity is 10 ~ 2000h
-1, under the condition of working pressure 0.1 ~ 3MPa, make hydrogen by desulfuration adsorbent bed, hydrogen process faced to desulfuration adsorbent.Preferred processing condition be temperature higher than adsorption temp 30 ~ 50 DEG C, volume space velocity is 500 ~ 1000h
-1, working pressure 0.5 ~ 2MPa.
3., after carrying out the absorption of step 1 and step 2, facing hydrogen treating processes 5-20 time, desulfuration adsorbent needs regeneration and reduction.Regeneration condition is: regeneration temperature 300 ~ 600 DEG C, regeneration pressure 0.1 ~ 2.0MPa, regeneration gas comprises oxygen, such as, can be oxygen volume content be the oxygen of 0.1% ~ 21.0% and the mixed gas of rare gas element, can be more specifically the mixed gas of oxygen and nitrogen.Desulfuration adsorbent after regeneration and reducing gas react and realize desulfuration adsorbent and reduce, reductive condition is: reduction temperature 260 ~ 600 DEG C, reduction pressure 0.1 ~ 2.0MPa, reducing gas is the gas that hydrogen volume content is at least 40%, the mixed gas of the mixed gas of such as hydrogen and nitrogen or hydrogen and other gas.Desulfuration adsorbent after reduction continues to recycle.
Desulfuration adsorbent of the present invention with nickel, zinc for active ingredient, can commodity in use desulfuration adsorbent, or by desulfuration adsorbent prepared by prior art, as prepared according to method described in ZL03139159.1 claim 1.
Desulfuration adsorbent of the present invention is primarily of zinc oxide and reduced state nickel composition, and wherein zinc oxide accounts for 15% ~ 90%, and reduced state nickel accounts for 2% ~ 85%.Not specified " % " of the present invention all refers to mass percent.
Also silicon oxide, aluminum oxide etc. is comprised in described desulfuration adsorbent.
Present invention also offers the preferred composition of described desulfuration adsorbent, its weight percent consists of: the nano zine oxide 30% ~ 85% that particle diameter is 100 ~ 500 μm, silicon oxide 5% ~ 60%, aluminum oxide 5% ~ 30%, reduced state nickel 3% ~ 60%.
By the non-hydrogen physical adsorption process of step 1, the sulfocompound in catalytic gasoline is made to be attracted to the surface of desulfuration adsorbent, see Fig. 1-a non-hydrogen physical adsorption schematic diagram, owing to being non-hydrogen physical adsorption process, alkene in catalytic gasoline can not by hydrotreated lube base oil, and octane value also can not lose.When the sulfocompound of non-hydrogen physical adsorption reach a certain amount of after, desulfurization degree can decline to a great extent, and stops adding catalytic gasoline raw material, makes hydrogen by desulfuration adsorbent bed, faces hydrogen process to desulfuration adsorbent.It is as follows that this faces hydrogen treating processes principle: in hydrogen and desulfuration adsorbent nickel effect under, the zinc oxide of sulphur atom in the sulfocompound of adsorbent surface in sorbent material is combined generation zinc sulphide and transfers to absorbent interior, and the hydrocarbon compound desorption losing sulphur atom diffuses out sorbent material, see Fig. 1-b.The room of adsorbent surface is released the non-hydrogen physical adsorption that can repeat step 1.After repeating step 1 and step 2 many times, the solid sulphur component zinc oxide major part in sorbent material is occupied, and sees Fig. 1-c.After regenerating desulfuration adsorbent and reducing, sorbent material can recycle, and sees Fig. 1-d.Adopt desulfuration adsorbent of the present invention and Adsorption Desulfurization process, desulfurization degree can reach more than 80%, and whole technological process can complete in fixed-bed reactor.
The present invention can be connected mutually with existing selective hydrogenation desulfurization process, and produce the clean gasoline meeting Europe V sulphur index request, facility investment is few, and desulfuration adsorbent is loaded convenient, and desulfurization degree is high, and technological process is simple, does not lose octane value, is easy to industrial application.
Accompanying drawing explanation
Fig. 1-a is non-hydrogen physical adsorption schematic diagram.
Fig. 1-b is for facing hydrogen process schematic diagram.
Fig. 1-c is repeatedly non-hydrogen physical adsorption-face hydrogen process schematic diagram.
Fig. 1-d is schematic diagram after the regeneration-reduction of non-hydrogen physical adsorption schematic diagram.
In figure, zero represents ZnO; o represents Ni; ● represent ZnS;
represent sulfide;
represent hydrocarbon.
Fig. 2 is pressure gasoline process for adsorption desulfuration schematic flow sheet of the present invention.
1-catalytic gasoline in figure, 2-process furnace, 3-enters fixed bed logistics, 4-fixed bed, and 5-flows out fixed bed logistics, 6-high-pressure separator, 7-high-pressure separator overhead stream, 8-high-pressure separator bottoms, 9-hydrogen, 10-regeneration gas.
Embodiment
Adsorption desulfurize process:
Catalytic gasoline 1 enters fixed-bed reactor 4 after process furnace 2 heats, and after adsorption desulfurize, product 5 is after high-pressure separator 6 is separated, and logistics 7 is mainly containing minute quantity lighter hydrocarbons, and can recycle, logistics 8 is super low sulfur catalytic gasoline product.
Face hydrogen treating processes
Catalytic gasoline 1 stops charging, hydrogen 9 enters fixed-bed reactor 4 after process furnace 2 heats, from adsorbent surface desorption after the sulfide on desulfuration adsorbent surface removes sulphur atom under the effect of hydrogen, after high-pressure separator 6 is separated, the main hydrogen of logistics 7, logistics 8 is also super low sulfur catalytic gasoline product.
Regeneration-reduction process:
Catalytic gasoline 1 stops charging, and regeneration gas 10 enters fixed-bed reactor 4 after heating, and after the sulphur content in regeneration tail gas 8 is lower than 20 μ g/g, stop entering regeneration gas 10, hydrogen 9 enters fixed-bed reactor 4 and realizes desulfuration adsorbent reduction reaction.
The following examples will be further described method provided by the invention, but therefore not be limited to the present invention, and those skilled in the art can according to the product of raw material of different nature and different index, concrete optimize needed for condition.
Embodiment 1:
With the catalytic gasoline A through selective hydrodesulfurization for raw material, in table 1, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 3, adopts method of the present invention, processing condition and product property as shown in table 2.As can be seen from Table 2, the sulphur content of product is 9.7 μ g/g, and RON octane value does not lose.
Comparative example 1:
With the catalytic gasoline A through selective hydrodesulfurization for raw material, in table 1, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 3, adopts and faces the method for H chemisorption, process for adsorption desulfuration condition and product property as shown in table 3.As can be seen from Table 3, the sulphur content of product is 9.5 μ g/g, RON loss of octane number 0.9 unit.
Embodiment 2:
When identical with embodiment 1 raw material, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 5, adopts method of the present invention, process for adsorption desulfuration condition and product property as shown in table 2.As can be seen from Table 2, the sulphur content of product is 12.1 μ g/g, and RON octane value does not lose.
Comparative example 2:
With the catalytic gasoline A through selective hydrodesulfurization for raw material, in table 1, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 3, adopts and faces the method for H chemisorption, process for adsorption desulfuration condition and product property as shown in table 3.As can be seen from Table 3, the sulphur content of product is 22.1 μ g/g, RON loss of octane number 0.6 unit.
Embodiment 3:
With the catalytic gasoline B through selective hydrodesulfurization for raw material, in table 1, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 3, adopts method of the present invention, process for adsorption desulfuration condition and product property as shown in table 2.As can be seen from Table 2, the sulphur content of product is 9.8 μ g/g, RON loss of octane number 0.1 unit.
Comparative example 3:
With the catalytic gasoline A through selective hydrodesulfurization for raw material, in table 1, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 3, adopts and faces the method for H chemisorption, process for adsorption desulfuration condition and product property as shown in table 3.As can be seen from Table 3, the sulphur content of product is 20.9 μ g/g, RON loss of octane number 0.3 unit.
Embodiment 4:
When identical with embodiment 3 raw material, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 5, adopts method of the present invention, process for adsorption desulfuration condition and product property as shown in table 2.As can be seen from table 2, the sulphur content of product is 7.9 μ g/g, and RON octane value does not lose.
Comparative example 4:
With the catalytic gasoline A through selective hydrodesulfurization for raw material, in table 1, desulfuration adsorbent is prepared by ZL03139159.1 embodiment 3, adopts and faces the method for H chemisorption, process for adsorption desulfuration condition and product property as shown in table 3.As can be seen from Table 3, the sulphur content of product is 7.7 μ g/g, and RON loss of octane number loses 1.2 units.
The gasoline stocks main character that table 1 embodiment uses
| Project | Raw material A | Raw material B |
| Density (20 DEG C)/g/cm 3 | 0.7175 | 0.7280 |
| Total sulfur/μ g/g | 93.2 | 70.7 |
| Alkene/w% | 26.3 | 28.7 |
| Boiling range/DEG C | ? | ? |
| Initial boiling point | 36.0 | 38.9 |
| 10% | 50.0 | 52.0 |
| 30% | 66.2 | 67.6 |
| 50% | 88.9 | 91.9 |
| 70% | 119.9 | 123.6 |
| 90% | 165.2 | 170.5 |
| Final boiling point | 188.0 | 198.2 |
| RON | 90.6 | 91.1 |
Table 2 embodiment 1 ~ embodiment 4 operational condition and product property
Table 3 comparative example 1 ~ comparative example 4 operational condition and product property
。
Claims (10)
1. a pressure gasoline process for adsorption desulfuration, is characterized in that comprising the following steps:
1) non-hydrogen physical adsorption: cracking gasoline feedstock is heated to 20 ~ 400 DEG C, at volume space velocity 0.2 ~ 10h
-1, enter fixed-bed reactor under the condition of working pressure 0.1 ~ 3MPa and contact with desulfuration adsorbent, the catalytic gasoline after adsorption desulfurize goes out fixed-bed reactor;
2) hydrogen process desulfuration adsorbent is faced: the incoming stock oil of the desulfuration adsorbent saturated rear stopping of absorption, in temperature higher than adsorption temp 0 ~ 50 DEG C, volume space velocity is 10 ~ 2000h
-1, under the condition of working pressure 0.1 ~ 3MPa, make hydrogen by desulfuration adsorbent bed, hydrogen process faced to desulfuration adsorbent.
2. technique as claimed in claim 1, is characterized in that carrying out described step 1) and step 2) process 5-20 time after, desulfuration adsorbent is regenerated and reduces.
3. technique as claimed in claim 2, is characterized in that carrying out described regeneration condition is: regeneration temperature 300 ~ 600 DEG C, regeneration pressure 0.1 ~ 2.0MPa, regeneration gas comprises oxygen.
4. technique as claimed in claim 2, it is characterized in that the desulfuration adsorbent after regenerating and reducing gas react to realize desulfuration adsorbent and reduce, reductive condition is: reduction temperature 260 ~ 600 DEG C, and reduction pressure 0.1 ~ 2.0MPa, reducing gas is the gas that hydrogen volume content is at least 40%.
5. technique as claimed in claim 1, is characterized in that described desulfuration adsorbent is primarily of zinc oxide and reduced state nickel composition.
6. technique as claimed in claim 1, is characterized in that described desulfuration adsorbent comprises the zinc oxide of 15% ~ 90% and the reduced state nickel of 2% ~ 85%.
7. technique as claimed in claim 1, is characterized in that described desulfuration adsorbent comprises silicon oxide and aluminum oxide.
8. technique as claimed in claim 1, is characterized in that described desulfuration adsorbent weight percent consists of: the nano zine oxide 30% ~ 85% that particle diameter is 100 ~ 500 μm, silicon oxide 5% ~ 60%, aluminum oxide 5% ~ 30%, reduced state nickel 3% ~ 60%.
9. technique as claimed in claim 1, it is characterized in that step 1) Raw is heated to 100 ~ 350 DEG C, volume space velocity is 0.5 ~ 5h
-1, working pressure is 0.5 ~ 2MPa.
10. technique as claimed in claim 1, is characterized in that step 2) in temperature higher than adsorption temp 30 ~ 50 DEG C, volume space velocity is 500 ~ 1000h
-1, under the condition of working pressure 0.5 ~ 2MPa, make hydrogen by desulfuration adsorbent bed, hydrogen process faced to desulfuration adsorbent.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1583962A (en) * | 2003-08-22 | 2005-02-23 | 中国石油化工股份有限公司齐鲁分公司 | Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof |
| CN1594505A (en) * | 2004-06-18 | 2005-03-16 | 中国石油化工集团公司 | Process for adsorption desulfurization of gasoline |
-
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1583962A (en) * | 2003-08-22 | 2005-02-23 | 中国石油化工股份有限公司齐鲁分公司 | Absorbing desulfurizing catalyst for catalytic cracking petroleum and preparing method thereof |
| CN1594505A (en) * | 2004-06-18 | 2005-03-16 | 中国石油化工集团公司 | Process for adsorption desulfurization of gasoline |
Non-Patent Citations (1)
| Title |
|---|
| 徐文清等: "Ni/ZnO吸附剂脱除催化裂化汽油中的硫", 《石油学报（石油加工）》, vol. 24, no. 6, 31 December 2008 (2008-12-31) * |
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