CN1912063A - Method of producing catalytic reforming raw material - Google Patents
Method of producing catalytic reforming raw material Download PDFInfo
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- CN1912063A CN1912063A CN 200510089848 CN200510089848A CN1912063A CN 1912063 A CN1912063 A CN 1912063A CN 200510089848 CN200510089848 CN 200510089848 CN 200510089848 A CN200510089848 A CN 200510089848A CN 1912063 A CN1912063 A CN 1912063A
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Abstract
The invention is a method for producing catalytic reforming raw material, cutting secondary gasoline raw material into light gasoline fraction, medium gasoline fraction and heavy gasoline fraction, where the medium gasoline fraction, optional virgin naphtha and hydrogen gas contact with first hydrofining catalyst to make alkene saturated reaction, the resultant effluent is not separated but directly contacts with second hydrofining catalyst to make hydrodesulfurization and hydro- denitrogenation reactions, and the extracted hydrogen-enriched gas is recycled and the extracted liquid enters a distillation dehydrating tower and is purified to obtain naphtha. And it can process secondary gasoline with high sulfur, nitrogen and alkene contents, and provides qualified raw material with sulfur and nitrogen contents both less than 0.5 mug/g for catalytic reforming.
Description
Technical field
The invention belongs in the method that has refining hydrocarbon ils under the situation of hydrogen, more particularly, is a kind of method of producing catalytic reforming raw material.
Background technology
According to the difference in its source, gasoline can roughly be divided into two big classes, i.e. straight-run spirit and secondary processing of gasoline, and secondary processing of gasoline mainly comprises catalytically cracked gasoline, coker gasoline, hydrocracking gasoline, pyrolysis gasoline and reformed gasoline.In China, the component in the gasoline pool more than the 80 heavy % is from catalytically cracked gasoline, and it is catalytically cracked gasolines that some refinerys even 100 heavy % are arranged.Therefore the sulphur and the olefin(e) centent that how to reduce catalytically cracked gasoline are the clean gasoline key points that refinery production meets new environmental protection standard.Reformed gasoline does not have sulphur, no nitrogen, no alkene substantially, and the octane value height, is fine gasoline blend component.If catalytically cracked gasoline is carried out fractionation, cut section in the middle of it is cut out as reformer feed, produce reformed gasoline by reforming process again, can in the higher octane value of maintenance, reduce sulfur in gasoline and olefin(e) centent effectively.
Catalytic reforming process is one of important technology of oil refining and petrochemical complex, and it is with C
6～C
11Naphtha fraction is a raw material, generates the reformed oil that is rich in aromatic hydrocarbons by the catalytic hydroprocessing reaction, simultaneously by-product hydrogen.Reformed oil can also can be produced low molecule aromatic hydrocarbon product, as the basic raw material of petrochemical complex directly as the blend component of stop bracket gasoline; By-product hydrogen is the important source of refinery with hydrogen.The raw material of catalytic reforming mainly is a virgin naphtha at present, but crude oil in China mostly is heavy crude, and the virgin naphtha extracting rate is lower, and virgin naphtha is a main raw material of producing preparing ethylene by steam cracking.Therefore, the raw material sources deficiency just becomes a principal element of restriction China catalytic reforming technical development.
Catalytic reforming process adopts two (many) noble metal catalysts such as platinum-rhenium and platinum-iridium usually, for preventing the catalytic reforming catalyst poisoning, requires sulphur, nitrogen content in its charging all less than 0.5 μ g/g.Therefore catalytic reforming process comprises that all petroleum naphtha hydrogenation makes with extra care (reformed pre-hydrogenated) unit, to remove in the stock oil to the deleterious impurity of catalytic reforming catalyst, comprising sulphur, nitrogen, alkene and arsenic, lead, copper and moisture etc.
At present, reformed pre-hydrogenated unit all designs to handle the virgin naphtha raw material, because the nitrogen content in the virgin naphtha raw material is usually less than 1 μ g/g, so the design pressure of hydrogenator is usually about 2MPa or lower.And the nitrogen content of catalytically cracked gasoline is higher than virgin naphtha far away, reaches 10～100 μ g/g usually.Even advance pre-hydrogenator after virgin naphtha mixes, the nitrogen content of mixing oil also has 2～20 μ g/g, if high-load like this nitrogen is dropped to below the 0.5 μ g/g, required pressure should be higher than 3MPa usually.In addition, different with virgin naphtha also has, and the catalytic gasoline olefin(e) centent is higher, even mix with virgin naphtha, the olefin(e) centent of mixing raw material also has 5 volume %～20 volume %, because the H that generates in the reaction
2S can regenerate mercaptan with alkene, so the too high meeting of olefin(e) centent causes the sulphur content of product to exceed standard.Therefore present secondary processing of gasoline such as reformed pre-hydrogenated device processing catalytically cracked gasoline are all very difficult, and particularly the hydrodenitrification reaction depth is not enough.
Disclose a process of producing stop bracket gasoline among the EP0022883, sulfur-bearing last running raw material generates the catalytically cracked gasoline that olefin(e) centent accounts for 10～60 heavy % after first cracking zone carries out catalytic cracking reaction; The catalytically cracked gasoline of extracting out is carried out cracking reaction again at second cracking zone, to remove the alkene of its part sulphur impurity and saturated 50 heavy %; Product to second cracking zone carries out hydrotreatment, further removes sulphur impurity and falls alkene, and this hydrofining product can be used as the material of reforming.It distills out the boiling range scope for example from catalytically cracked gasoline be 93～177 ℃ cut, adopts Co-Mo/Al
2O
3Catalyzer and suitable operational condition obtain sulphur, nitrogen all less than 1 μ g/g, and bromine index is less than 1 hydrofining product, and this product can be used as the charging of platinoiridita reforming catalyst.Because produce the material of reforming with this method, catalytically cracked gasoline will be through catalytic cracking once more, hydrorefined then process, so flow process complexity, investment operation expense height, and yield is low.
CN1319644A discloses a kind of gasoline desulfating method, this method is at first carried out removing alkadiene by selective hydrogenation to full distillation gasoline (preferred catalytic pressure gasoline), then this gasoline is separated into four cuts, wherein second cut and the 4th cut (last running) carry out selective hydrodesulfurization after mixing; The 3rd cut then carries out catalytic reforming after hydrofining.It is mentioned and will extract out the full distillation gasoline of the cut of boiling range scope between 95～150 ℃ behind dialkene removal in giving an example, at 300 ℃ of temperature of reaction, hydrogen dividing potential drop 3.5MPa, hydrogen to oil volume ratio 150Nm
3/ m
3And volume space velocity 3h
-1Condition under, adopt the HR306 catalyzer (Co-Mo/Al of Procatalyse company
2O
3) this cut is carried out hydrofining, sulphur content is less than 1 μ g/g in the product, and olefin(e) centent is 0.9 volume %, and nitrogen content does not provide data.This product can be used as the charging of platinum-Xi continuous reforming catalyst.Obtaining reforming material with this method must be through the process of two hydrotreatments, therefore have problems such as flow process complexity, investment operation expense height.
Summary of the invention
The present invention seeks to provide on the basis of existing technology a kind of method of producing catalytic reforming raw material.
Method provided by the invention is: the secondary processing of gasoline raw material is cut into light benzine cut, middle matter gasoline fraction and heavy gasoline cut; Middle matter gasoline fraction, optional virgin naphtha contact with first Hydrobon catalyst together with hydrogen, at 200～380 ℃ of average reaction temperature, reaction pressure 1.2～4.0MPa, volume space velocity 2～25h
-1, hydrogen to oil volume ratio is 90～200Nm
3/ m
3Condition under react, reaction effluent directly contacts with second Hydrobon catalyst without separating, at 200～380 ℃ of average reaction temperature, reaction pressure 1.2～4.0MPa, volume space velocity 2.5～25h
-1, hydrogen to oil volume ratio is 90～200Nm
3/ m
3Condition under react, the reaction effluent of generation cools off, separates, isolated hydrogen-rich gas recycles, isolated liquid enters the distillation dehydration tower, obtains petroleum naphtha after removing impurity.
Use this method, can under the low pressure condition, handle the secondary processing of gasoline that high sulfur-bearing is nitrogenous and olefin(e) centent is high, for catalytic reforming provides sulphur, nitrogen content all less than the acceptable material of 0.5 μ g/g.
Embodiment
Method provided by the invention is so concrete enforcement:
The secondary processing of gasoline raw material is cut into light benzine cut, middle matter gasoline fraction and heavy gasoline cut.The initial boiling point of middle matter gasoline fraction is 65～100 ℃, and doing is 150～180 ℃.The light ends that is lower than initial boiling point contains more alkene, if enter reformed pre-hydrogenated reactor, can increase the hydrogen consumption, and influential to the sulphur content in the product.Be easy to carbon deposit on reforming catalyst greater than 180 ℃ heavy endss, the production cycle is shortened.
Middle matter gasoline fraction, optional virgin naphtha contact with first Hydrobon catalyst together with hydrogen, 200～380 ℃ of average reaction temperature, and preferred 280～350 ℃, reaction pressure 1.2～4.0MPa, preferred 1.5～2.5MPa, volume space velocity 2～25h
-1, preferred 3～16h
-1, hydrogen to oil volume ratio is 90～200Nm
3/ m
3Condition under, mainly carry out olefin saturation and a spot of hydrogenating desulfurization, hydrodenitrification reaction, reaction effluent directly contacts with second Hydrobon catalyst without separating, 200～380 ℃ of average reaction temperature, preferred 280～350 ℃, reaction pressure 1.2～4.0MPa, preferred 1.5～2.5MPa, volume space velocity 2.5～25h
-1, preferred 3～12h
-1, hydrogen to oil volume ratio is 90～200Nm
3/ m
3Condition under, carry out hydrogenating desulfurization and hydrodenitrification the reaction, the reaction effluent of generation cools off, separates, isolated hydrogen-rich gas recycles, isolated liquid enters the distillation dehydration tower, through removing H
2S, NH
3With obtain petroleum naphtha behind the impurity such as moisture, this petroleum naphtha is the acceptable material that meets catalytic reforming charging requirement.
Described secondary processing of gasoline raw material is catalytically cracked gasoline, coker gasoline, pyrolysis gasoline, hydrogenation coker gasoline and hydrocracking petroleum naphtha wherein any or several mixing oils.The weight ratio of matter gasoline fraction and virgin naphtha is 5: 95～90: 10 in described.
The olefin(e) centent of secondary processing of gasoline such as catalytically cracked gasoline, coker gasoline is higher, during as catalytic reforming raw material, and must this part alkene is saturated.This be because, in the catforming process because degree of depth dehydrogenation and aromatic hydrocarbons condensation reaction, can produce carbon deposit inevitably on catalyzer, the increase of olefin(e) centent can make carbon deposit speed up in the raw material, and cycloolefin especially the existence of cyclopentadiene hydrocarbon more can cause carbon deposit aggravation.In addition, in reformed pre-hydrogenated hydrodesulfurization process, the H that alkene meeting and hydrodesulfurization reaction generate
2S is in conjunction with regenerating mercaptan, and its reaction formula is:
。And the amount of mercaptan and the amount of alkene in the raw material have substantial connection in the hydrogenated products, promptly increase along with the increase of olefin(e) centent.
The first preferred Hydrobon catalyst of the present invention is a kind of metal load type catalyst, and carrier is an aluminum oxide, and metal component is molybdenum and/or tungsten and the basic metal that is selected from group VIII cobalt and/or nickel, group vib.In oxide compound and with the catalyzer is benchmark, and it consists of nickel 1～6 heavy %, molybdenum and/or tungsten 4～12 heavy %, and basic metal 2～8 heavy %, surplus is an aluminum oxide.This catalyzer is the higher hydrogenation catalyst of olefine selective, especially the selectivity to diolefine is higher, most alkene in can the saturated stock oil of hydrogenation, thus can reduce the olefin(e) centent in the hydrogenated products effectively and prevent alkene and H that hydrodesulfurization reaction generates
2The S recombine generates mercaptan.
Sulphur, nitrogen impurity content are far above virgin naphtha in secondary processing of gasoline such as catalytically cracked gasoline, the coker gasoline, satisfy the requirement of catalytic reforming charging, just must improve the severity of reformed pre-hydrogenated unit process, especially to improve the degree of depth of hydrodenitrification reaction, sulphur, nitrogen content in the hydrogenated products are dropped to below the 0.5 μ g/g.
Preferred second Hydrobon catalyst of the present invention is a kind of metal load type catalyst, and carrier is an aluminum oxide, and active ingredient is the tungsten that is selected from group VIII nickel and cobalt and group vib, and cocatalyst component is the arbitrary element that is selected from magnesium, zinc, iron, the calcium.In oxide compound and with the catalyzer is benchmark, and it consists of nickel 1～7 heavy %, cobalt 0.01～1.0 heavy %, and tungsten 10～30 heavy %, cocatalyst component 0.1～10 heavy %, surplus is an aluminum oxide.This catalyzer has good hydrogenating desulfurization and hydrodenitrification performance, can remove impurity such as sulphur in the secondary processing of gasoline raw material inferior, nitrogen effectively.The major metal active ingredient that this catalyzer is selected for use is nickel and tungsten, because its hydrogenation activity height, help the carrying out of hydrodenitrification reaction, can under lower reaction pressure, nitrogenous impurity higher in the secondary processing of gasoline raw material be taken off to 0.5 μ g/g, satisfy the requirement of catalytic reforming charging.
First Hydrobon catalyst among the present invention and second Hydrobon catalyst can fill in respectively in two reactors, also first Hydrobon catalyst can be placed the top of second catalyzer and be seated in a reactor to implement.The admission space ratio of first Hydrobon catalyst and second Hydrobon catalyst is 20: 80～80: 20, preferred 30: 70～60: 40.
Two catalyzer all need carry out prevulcanized before use, and the method for the conventional Hydrobon catalyst prevulcanized of reporting in vulcanization process and the document is identical.For example, under certain reaction pressure and certain hydrogen flowing quantity, add dithiocarbonic anhydride (CS with virgin naphtha
2) or Methyl disulfide (CH
3-S-S-CH
3, be called for short DMDS) and as vulcanized oil, curing temperature is 230～370 ℃, curing time is 8～24 hours.
The advantage of the inventive method is:
1. adopt two kinds of Hydrobon catalyst combination loadings with different activities metal component, first Hydrobon catalyst is the olefine selective hydrogenation catalyzer, the alkene of the overwhelming majority in can the saturated stock oil of hydrogenation, thus can reduce the content of alkene in the product effectively and prevent alkene and the H of hydrodesulfurization reaction generation
2The S recombine generates mercaptan.Second Hydrobon catalyst has very high hydrodenitrogenationactivity activity, can under the low pressure condition nitrogen content in the stock oil be taken off to 0.5 μ g/g.Adopt method of the present invention can under the low pressure condition, handle the secondary processing of gasoline that high sulfur-bearing is nitrogenous and olefin(e) centent is high, for catalytic reforming provides sulphur, nitrogen content all less than the acceptable material of 0.5 μ g/g.
2. adopt method of the present invention, can remedy the deficiency of raw materials for catalytic reforming device, or replace out virgin naphtha and be used for steam crack material and produce Chemicals such as ethene.The hydrogen that produces in catforming process can be used for hydrogenation unit, reduces the cost of refinery's hydrogenation unit hydrogen consumption.
3. the present invention adopts single hop connect one-pass flow process and non-precious metal catalyst, and technical process is simple, technology maturation, invest cheap, flexible operation.This method is applicable to builds and at the reformed pre-hydrogenated device of building, also is applicable to old plant modification.This invention can be implemented under lower reaction pressure, has reduced facility investment and process cost.
The following examples will give further instruction to present method, but therefore not limit present method.
The trade names of used Hydrobon catalyst G are RGO-2 in embodiment and the Comparative Examples, and the trade names of Hydrobon catalyst S are RS-1, are the catalyst plant production of Sinopec Chang Ling branch office.Contrast Hydrobon catalyst O is the catalyst used for hydrogenation of distilled oil fraction of a kind of Co-Mo of containing.
Hydrobon catalyst G, Hydrobon catalyst S and contrast Hydrobon catalyst O adopt conventional method for pre-sulphuration, and vulcanized oil is the dithiocarbonic anhydride (CS that straight-run spirit is mixed 2 heavy %
2) mixing oil.The prevulcanized condition is reaction pressure 2.0MPa, vulcanized oil volume space velocity 3.0h
-1, the highest curing temperature is 290 ℃, curing time 8 hours.
Comparative Examples 1
A kind of catalytically cracked gasoline obtains wherein matter gasoline fraction (the boiling range scope is 95～163 ℃) after fractionation, matter gasoline fraction in this is mixed with 20: 80 weight ratios with a kind of virgin naphtha, obtains stock oil A, and its character is as shown in table 1.Stock oil A contacts with Hydrobon catalyst S, at reaction pressure 3.2MPa, and 300 ℃ of average reaction temperature, volume space velocity 3.5h
-1, hydrogen to oil volume ratio 150Nm
3/ m
3Condition under react, reaction generates oil and obtains naphtha product after cooling off, separate, removing impurity, its processing condition and product property are as shown in table 2.
By table 2 as seen, nitrogen content meet catalytic reforming unit charging requirement, and sulphur content is 6.3 μ g/g, is higher than far away＜index of 0.5 μ g/g less than 0.5 μ g/g in the naphtha product.Sulfocompound type of listing from table 2 and analysis on Content result, sulfocompound all is a thio-alcohol in the naphtha product, the H that this explanation alkene and hydrodesulfurization reaction generate
2The S reaction has regenerated mercaptan.
Embodiment 1
The used stock oil A of the used raw material of present embodiment and Comparative Examples 1 is identical.Stock oil A contacts with Hydrobon catalyst S with Hydrobon catalyst G successively, carries out that alkene is saturated, hydrogenating desulfurization and hydrodenitrification reaction, reaction effluent through cooling, separate and remove impurity after obtain naphtha product.The admission space ratio of Hydrobon catalyst G and Hydrobon catalyst S is 40: 60.Average reaction temperature, volume space velocity and hydrogen to oil volume ratio are identical with Comparative Examples 1 in embodiment 1 reaction conditions, and reaction pressure drops to 2.0MPa, and its reaction conditions and product property are as shown in table 2.
By table 2 as seen, sulphur, nitrogen content meet catalytic reforming unit charging requirement all less than 0.5 μ g/g in the naphtha product oil.
Embodiment 2
A kind of catalytically cracked gasoline and a kind of hydrogenation coker gasoline mix with 66: 34 weight ratios, after fractionation, obtain wherein matter gasoline fraction (the boiling range scope is 70～168 ℃), then matter gasoline fraction in this is mixed with 50: 50 weight ratios with a kind of virgin naphtha, obtain stock oil B, its character is as shown in table 1.By table 1 as seen, nitrogen content is higher among the stock oil B, reaches 17 μ g/g.
Stock oil B contacts with Hydrobon catalyst S with Hydrobon catalyst G successively, at reaction pressure 1.8MPa, and 300 ℃ of average reaction temperature, volume space velocity 3.0h
-1, hydrogen to oil volume ratio 150Nm
3/ m
3Condition under carry out that alkene is saturated, hydrogenating desulfurization and hydrodenitrification reaction, reaction effluent through the cooling, separate and remove impurity after obtain naphtha product, the admission space ratio of Hydrobon catalyst G and Hydrobon catalyst S is 40: 60, and its reaction conditions and product property are as shown in table 3.
By table 3 as seen, sulphur, nitrogen content meet catalytic reforming unit charging requirement all less than 0.5 μ g/g in the naphtha product.
Comparative Examples 2
The used stock oil B of the used raw material of this Comparative Examples and embodiment 2 is identical.Stock oil B contacts with contrast Hydrobon catalyst O with Hydrobon catalyst G successively, carry out that alkene is saturated, hydrogenating desulfurization and hydrodenitrification reaction, reaction effluent through the cooling, separate and remove impurity after obtain naphtha product, the admission space ratio of Hydrobon catalyst G and contrast Hydrobon catalyst O is 40: 60, reaction conditions is identical with embodiment 2 in this Comparative Examples, and its reaction conditions and product property are as shown in table 3.
By table 3 as seen, sulphur content is 0.6 μ g/g in the naphtha product, and nitrogen content is 2 μ g/g, so sulphur, nitrogen content all do not meet catalytic reforming unit charging requirement in the naphtha product of this Comparative Examples.
Table 1
| Stock oil A | Stock oil B | |
| Density (20 ℃), g/cm 3 | 0.7194 | 0.7432 |
| Sulphur, μ g/g | 402 | 523 |
| Nitrogen, μ g/g | 3 | 17 |
| The bromine valency, gBr/100g | 11.7 | 20.6 |
| Alkene, heavy % | 7.9 | 7.3 |
| Boiling range ASTM D-86, ℃ | ||
| Initial boiling point | 55 | 53 |
| 50％ | 120 | 110 |
| Do | 177 | 158 |
Table 2
| Comparative Examples 1 | Embodiment 1 | |
| Catalyst type | S | G/S |
| The catalyst loading volume ratio | 100 | 40/60 |
| Processing condition: | ||
| Reaction pressure, MPa | 3.2 | 2.0 |
| Average reaction temperature, ℃ | 300 | 300 |
| Volume space velocity, h -1 | 3.5 | 3.5 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 150 | 150 |
| Naphtha product character: | ||
| Sulphur, μ g/g | 6.3 | ＜0.5 |
| Nitrogen, μ g/g | ＜0.5 | ＜0.5 |
| Sulfide analysis, μ g/g | ||
| Thiomethyl alcohol | 1.1 | - |
| Sulfur alcohol | 1.4 | - |
| Tert.-butyl mercaptan | 0.5 | - |
| Propane thiol | 2.8 | - |
| Isopentyl mercaptan | 0.5 | - |
Table 3
| Embodiment 2 | Comparative Examples 2 | |
| Catalyst type | G/S | G/O |
| The catalyst loading volume ratio | 40/60 | 40/60 |
| Processing condition: | ||
| Reaction pressure, MPa | 1.8 | 1.8 |
| Average reaction temperature, ℃ | 300 | 300 |
| Volume space velocity, h -1 | 3.0 | 3.0 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 150 | 150 |
| Naphtha product character: | ||
| Sulphur, μ g/g | ＜0.5 | 0.6 |
| Nitrogen, μ g/g | ＜0.5 | 2.1 |
Claims (10)
1, a kind of method of producing catalytic reforming raw material, the secondary processing of gasoline raw material is cut into light benzine cut, middle matter gasoline fraction and heavy gasoline cut, matter gasoline fraction, optional virgin naphtha contact with first Hydrobon catalyst together with hydrogen in it is characterized in that, 200～380 ℃ of average reaction temperature, reaction pressure 1.2～4.0MPa, volume space velocity 2～25h
-1, hydrogen to oil volume ratio is 90～200Nm
3/ m
3Condition under react, reaction effluent directly contacts with second Hydrobon catalyst without separating, at 200～380 ℃ of average reaction temperature, reaction pressure 1.2～4.0MPa, volume space velocity 2.5～25h
-1, hydrogen to oil volume ratio is 90～200Nm
3/ m
3Condition under react, the reaction effluent of generation cools off, separates, isolated hydrogen-rich gas recycles, isolated liquid enters the distillation dehydration tower, obtains petroleum naphtha after removing impurity.
2, in accordance with the method for claim 1, it is characterized in that described secondary processing of gasoline raw material is catalytically cracked gasoline, coker gasoline, pyrolysis gasoline, hydrogenation coker gasoline and hydrocracking petroleum naphtha wherein any or several mixing oils.
3, in accordance with the method for claim 1, it is characterized in that the initial boiling point of described middle matter gasoline fraction is 65～100 ℃, doing is 150～180 ℃.
4,, it is characterized in that the weight ratio of described middle matter gasoline fraction and virgin naphtha is 5: 95～90: 10 according to claim 1 or 3 described methods.
5, in accordance with the method for claim 1, it is characterized in that hydrorefined reaction conditions is: 280～350 ℃ of average reaction temperature, reaction pressure 1.5～2.5MPa, the volume space velocity 3～16h of first Hydrobon catalyst
-1, the volume space velocity 3～12h of second Hydrobon catalyst
-1
6, in accordance with the method for claim 1, it is characterized in that described first Hydrobon catalyst is a kind of metal load type catalyst, carrier is an aluminum oxide, and metal component is molybdenum and/or tungsten and the basic metal that is selected from group VIII cobalt and/or nickel, group vib.
7, according to claim 1 or 6 described methods, it is characterized in that described first Hydrobon catalyst, is benchmark in oxide compound and with the catalyzer, and it consists of nickel 1～6 heavy %, molybdenum and/or tungsten 4～12 heavy %, and basic metal 2～8 heavy %, surplus is an aluminum oxide.
8, in accordance with the method for claim 1, it is characterized in that described second Hydrobon catalyst is a kind of metal load type catalyst, carrier is an aluminum oxide, active ingredient is the tungsten that is selected from group VIII nickel and cobalt and group vib, and cocatalyst component is the arbitrary element that is selected from magnesium, zinc, iron, the calcium.
9, according to claim 1 or 8 described methods, it is characterized in that described second Hydrobon catalyst, is benchmark in oxide compound and with the catalyzer, it consists of nickel 1～7 heavy %, cobalt 0.01～1.0 heavy %, tungsten 10～30 heavy %, cocatalyst component 0.1～10 heavy %, surplus is an aluminum oxide.
10, in accordance with the method for claim 1, the admission space ratio that it is characterized in that first Hydrobon catalyst and second Hydrobon catalyst is 20: 80～80: 20.
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| CN102051228A (en) * | 2011-01-28 | 2011-05-11 | 赵丽 | Method for producing aromatic hydrocarbon by catalytically reforming hydrogenation naphtha |
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| CN102268285B (en) * | 2011-07-08 | 2013-12-04 | 中国石油天然气股份有限公司 | Pre-hydrogenation treatment method for reforming raw material |
| CN103074107A (en) * | 2011-10-25 | 2013-05-01 | 中国石油化工股份有限公司 | Production method for full-fraction gasoline product with ultralow sulfur |
| CN103074106B (en) * | 2011-10-25 | 2016-01-13 | 中国石油化工股份有限公司 | A kind of method reducing content of sulfur in gasoline |
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| CN103074106A (en) * | 2011-10-25 | 2013-05-01 | 中国石油化工股份有限公司 | Method for reducing sulfur content in gasoline |
| CN112745894A (en) * | 2019-10-30 | 2021-05-04 | 中国石油化工股份有限公司 | Method for producing catalytic reforming raw material by hydrofining inferior raw oil |
| CN112745894B (en) * | 2019-10-30 | 2022-12-13 | 中国石油化工股份有限公司 | Method for producing catalytic reforming raw material by hydrofining inferior raw oil |
| CN116064110A (en) * | 2021-10-31 | 2023-05-05 | 中国石油化工股份有限公司 | Process for producing reforming feed and ethylene cracking raw material |
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