CN1912062A - Hydrogenation method for producing catalytic reforming raw material - Google Patents
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- CN1912062A CN1912062A CN 200510089847 CN200510089847A CN1912062A CN 1912062 A CN1912062 A CN 1912062A CN 200510089847 CN200510089847 CN 200510089847 CN 200510089847 A CN200510089847 A CN 200510089847A CN 1912062 A CN1912062 A CN 1912062A
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Abstract
The invention is a hydrogenating method for producing catalytic reforming raw materials, cutting secondary processed gasoline as light gasoline fractions, medium gasoline fractions and heavy gasoline fractions, where the medium gasoline fraction and hydrogen gas together enter in first reacting region to react by the action of hydrofining catalyst, the resultant effluent is not separated but directly mixes with virgin naphtha to enter in second reacting region so as to react by the action of hydrofining catalyst, the corresponding resultant effluent is cooled and separated, where the extracted hydrogen-rich gas is recycled and the extracted liquid enters in a distilling 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 hydrotreating 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 hydrotreating of producing catalytic reforming raw material.
Method provided by the invention is: the secondary processing of gasoline raw material is cut into the light benzine cut, middle matter gasoline fraction and heavy gasoline cut, middle matter gasoline fraction and hydrogen enter first reaction zone together, under the Hydrobon catalyst effect, react, reaction effluent enters second reaction zone without separating directly with after virgin naphtha mixes, under the effect of Hydrobon catalyst, react, the reaction effluent that generates cools off, separate, 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.
Description of drawings
Accompanying drawing is the method for hydrotreating schematic flow sheet of production catalytic reforming raw material provided by the present invention.
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, and 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 and hydrogen enter first reaction zone together, contacts with Hydrobon catalyst, and at reaction pressure 1.0～5.0MPa, preferred 1.5～3.2MPa, 220～380 ℃ of average reaction temperature, preferred 260～360 ℃, volume space velocity 2～10h
-1, preferred 3～6h
-1, hydrogen to oil volume ratio 50～500Nm
3/ m
3Preferred 100～300Nm
3/ m
3Condition under react; Reaction effluent enters second reaction zone without separating directly with after virgin naphtha mixes, under the effect of Hydrobon catalyst, react, reaction conditions is reaction pressure 1.0～5.0MPa, preferred 1.5～3.2MPa, 250～340 ℃ of average reaction temperature, preferred 270～320 ℃, volume space velocity 2～15h
-1, preferred 3～10h
-1, hydrogen to oil volume ratio 50～500Nm
3/ m
3Preferred 80～300Nm
3/ m
3, the reaction effluent of generation cools off, separates, and isolated hydrogen-rich gas recycles, and 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 and pyrolysis gasoline wherein any or several mixing oils.
The olefin(e) centent of secondary processing of gasoline such as catalytically cracked gasoline, coker gasoline is higher, with it as catalytic reforming raw material, in reformed pre-hydrogenated hydrodesulfurization process, alkene can and the H of hydrodesulfurization reaction generation
2S is in conjunction with regenerating mercaptan, and its reaction formula is:
。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.And discover that working as reaction bed temperature surpasses 320 ℃, and alkene and H will take place
2S is in conjunction with regenerating the reaction of mercaptan, thereby causes sulphur content in the hydrogenated products greater than 0.5 μ g/g, can not satisfy the requirement of catalytic reforming charging.Because the hydrogenation of olefins saturated reaction is strong exothermal reaction, so the high secondary processing of gasoline of olefin(e) centent must note the temperature rise of controlling reactor when carrying out reformed pre-hydrogenated reaction, wants the temperature of reaction bottom the controlling reactor to be no more than 320 ℃ when special.
The present invention's virgin naphtha that temperature is lower with mix in reactor chilling case from the higher resultant of reaction of first reaction zone (bed or first reactor) temperature, after making that the temperature of hybrid reaction material drops to required value, enter second reaction zone (two beds or second reactor) of reactor.According to the temperature of reaction of second reaction zone (two beds or second reactor), adjust the inlet amount and the feeding temperature of virgin naphtha, thereby the bed top temperature of controlling second reaction zone is no more than 320 ℃.The weight ratio of matter gasoline fraction and virgin naphtha is 99: 1～60: 40 among the present invention, preferred 90: 10～70: 30; The feeding temperature of virgin naphtha is 10～200 ℃, preferred 30～150 ℃.
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.
The preferred 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.
The present invention can adopt a reactor to divide two sections loading catalysts, and the method for chilling case and oil and gas distributor is set between the two-stage catalytic agent bed, also can adopt two reactors in series, injects the method for virgin naphtha between two reactors.The admission space ratio of first reaction zone (bed or first reactor) Hydrobon catalyst and second reaction zone (two beds or second reactor) Hydrobon catalyst is 40: 60～70: 30.
Hydrobon catalyst 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. the present invention adopts the method for the low charging of implantation temperature in the middle of two reaction zones of reactor, when having solved the high secondary processing of gasoline raw material of reformed pre-hydrogenated device processing olefin(e) centent preferably, the problem of reaction bed temperature control particularly can be controlled the outlet of two beds and be no more than 320 ℃.Suppress the H that alkene and hydrodesulfurization reaction generate effectively
2The S recombine generates mercaptan, and sulphur, nitrogen content are all less than 0.5 μ g/g in the charging of assurance catalytic reforming.
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.
Below in conjunction with accompanying drawing method provided by the present invention is further detailed.
Accompanying drawing is the method for hydrotreating schematic flow sheet of production catalytic reforming raw material provided by the present invention.
The method of hydrotreating flow process of production catalytic reforming raw material provided by the present invention is as follows:
The secondary processing of gasoline raw material enters separation column 2 through pipeline 1, and cat head is told the light benzine cut through pipeline 3 caterpillars, and side line is the matter gasoline fraction in pipeline 4 is extracted out, and the heavy gasoline cut at the bottom of the tower is through pipeline 5 caterpillars.From the incoming stock oil pump 6 of middle matter gasoline fraction of pipeline 4, through boosting the back with mix from the new hydrogen of pipeline 7 and from the recycle hydrogen of pipeline 20, enter interchanger 11 and the effusive resultant of reaction heat exchange in reactor 13 bottoms then.Material after the heat exchange enters process furnace 12, after being heated to temperature of reaction, enters first reaction zone (bed) of hydrogenator 13, carries out reactions such as hydrogenating desulfurization, hydrodenitrification and hydrogenation of olefins are saturated under the effect of Hydrobon catalyst.Virgin naphtha enters oil pump 9 through pipeline 8, virgin naphtha after boosting enters interchanger 15 and resultant of reaction heat exchange through pipeline 10, after heat exchange, enter the chilling case 14 that is positioned at reactor 13 middle parts, mix at this resultant of reaction with first reaction zone, the mixing oil that forms enters second reaction zone (two beds) of reactor 13, carries out reactions such as hydrogenating desulfurization, hydrodenitrification and a spot of hydrogenation of olefins are saturated under the effect of Hydrobon catalyst.The resultant of reaction of second reaction zone after interchanger 11, interchanger 15 heat exchange, behind air-cooler 16 and water recirculator 17 cooling condensations, enters high-pressure separator 18 and carries out gas-oil separation more successively.The hydrogen that is rich at high-pressure separator 18 tops enters circulating hydrogen compressor 19 and recycles as recycle hydrogen, and high-pressure separator 18 lower liquid and distillation dehydration tower 22 bottom streams after the heat exchange, enter distillation dehydration tower 22 in interchanger 21.The lighter hydrocarbons that cat head is told are through pipeline 25 caterpillars, and the petroleum naphtha that tower bottom flow goes out is divided into two portions, and a part is back to distillation dehydration tower 22 after reboiler furnace 23 heating; Another part is after interchanger 21 heat exchange, through pipeline 24 caterpillars.
The following examples will give further instruction to present method, but therefore not limit present method.
Used Hydrobon catalyst trade names are RS-1 in embodiment and the Comparative Examples, for Sinopec Chang Ling branch office catalyst plant is produced.Hydrobon catalyst adopts conventional method for pre-sulphuration, and vulcanized oil is the dithiocarbonic anhydride (CS that straight-run spirit is mixed 2 heavy %
2).The prevulcanized condition is, reaction pressure 2.5MPa, and vulcanized oil feed volume air speed is 3.0h
-1, the highest curing temperature is 290 ℃, curing time 8 hours.
Embodiment
A kind of catalytically cracked gasoline is carried out fractionation, extract wherein matter gasoline fraction (the boiling range scope is 79～175 ℃) out as stock oil A; A kind of virgin naphtha is as stock oil B, and stock oil character is as shown in table 1.
Reactor is divided into two beds in the present embodiment, be provided with chilling case and oil and gas distributor between two beds, one bed and the same Hydrobon catalyst of two beds filling, one bed Hydrobon catalyst and two bed Hydrobon catalyst admission space ratios are 55: 45, and reactor total catalyst admission space is 37.1m
3
Stock oil A and hydrogen enter reactor one bed after heating, carry out hydrofining reaction, 250 ℃ of bed temperature ins, and a bed temperature out is 370 ℃.Stock oil B is after heat exchange, and feeding temperature is 40 ℃ and enters reactor chilling case, generates oil with the reaction of a bed and mixes, and mixing oil enters reactor two beds, carries out hydrofining reaction, and wherein two bed temperature ins are 279 ℃, and temperature out is 281 ℃.The reaction effluent that two beds generate is after cooling, separating, and isolated hydrogen-rich gas recycles, and isolated liquid enters the distillation dehydration tower, obtains petroleum naphtha after removing impurity.The weight ratio of stock oil A and stock oil B is 75: 25.Reaction conditions and naphtha product character are as shown in table 2.Meet catalytic reforming unit charging requirement by sulphur, nitrogen content in the visible naphtha product of table 2 all less than 0.5 μ g/g.
Comparative Examples
Used reactor has only a beds in the Comparative Examples, but used Hydrobon catalyst is identical with embodiment, and the catalyst loading volume is identical with embodiment total catalyst admission space.Stock oil used in the Comparative Examples is identical with embodiment.
Stock oil A and stock oil B mix with hydrogen after mixing by weight 75: 25 again, enter reactor after the heating, carry out hydrofining reaction, and wherein the bed temperature in is 250 ℃, and temperature out reaches 340 ℃, 295 ℃ of average reaction temperature.The reaction effluent that generates cools off, separates, and isolated hydrogen-rich gas recycles, and isolated liquid enters the distillation dehydration tower, obtains petroleum naphtha after removing impurity.Reaction conditions and naphtha product character are as shown in table 3.By table 3 as seen, nitrogen content is less than 0.5 μ g/g in the naphtha product, and sulphur content is 1.0 μ g/g, can not satisfy the index of catalytic reforming unit charging＜0.5 μ g/g.
Table 1
| Material name | A | B |
| Density (20 ℃), g/cm 3 | 0.7612 | 0.7280 |
| Sulphur, μ g/g | 1390 | 82 |
| Nitrogen content, μ g/g | 39 | 5.1 |
| The bromine valency, gBr/100g | 46.9 | 0.21 |
| PONA analyzes, heavy % | ||
| Normal paraffin | 4.41 | 25.70 |
| Isoparaffin | 27.18 | 31.19 |
| Alkene | 25.01 | 0 |
| Naphthenic hydrocarbon | 9.07 | 25.47 |
| Aromatic hydrocarbons | 34.33 | 17.64 |
| Boiling range (ASTM D-86), ℃ | ||
| Initial boiling point | 79 | 60 |
| 50％ | 116 | 111 |
| Do | 175 | 168 |
Table 2
| Beds | One bed | Two beds |
| Reaction conditions | ||
| Reaction pressure, MPa | 2.5 | 2.5 |
| Volume space velocity, h -1 | 6.0 | 10.0 |
| The beds temperature in, ℃ | 250 | 279 |
| The beds temperature out, ℃ | 370 | 281 |
| Average reaction temperature, ℃ | 310 | 280 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | 202 | 90 |
| Naphtha product character: | ||
| Sulphur content, μ g/g | - | ＜0.5 |
| Nitrogen content, μ g/g | - | ＜0.5 |
| The bromine valency, gBr/100g | - | ＜0.1 |
Table 3
| Reaction conditions | |
| Reaction pressure, MPa | 2.5 |
| Volume space velocity, h -1 | 4.5 |
| The beds temperature in, ℃ | 250 |
| The beds temperature out, ℃ | 340 |
| Average reaction temperature, ℃ | 295 |
| Hydrogen to oil volume ratio | 150 |
| Naphtha product character: | |
| Sulphur content, μ g/g | 1.0 |
| Nitrogen content, μ g/g | ＜0.5 |
| The bromine valency, gBr/100g | 0.2 |
Claims (10)
1, a kind of method of hydrotreating of producing catalytic reforming raw material, the secondary processing of gasoline raw material is cut into the light benzine cut, middle matter gasoline fraction and heavy gasoline cut, matter gasoline fraction and hydrogen enter first reaction zone together in it is characterized in that, under the Hydrobon catalyst effect, react, reaction effluent enters second reaction zone without separating directly with after virgin naphtha mixes, under the effect of Hydrobon catalyst, react, the reaction effluent that generates cools off, separate, 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 and pyrolysis gasoline 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, in accordance with the method for claim 1, it is characterized in that the weight ratio of described middle matter gasoline fraction and virgin naphtha is 99: 1～60: 40, the feeding temperature of virgin naphtha is 10～200 ℃.
5, according to claim 1 or 4 described methods, it is characterized in that the weight ratio of described middle matter gasoline fraction and virgin naphtha is 90: 10～70: 30, the feeding temperature of virgin naphtha is 30～150 ℃.
6, in accordance with the method for claim 1, it is characterized in that the reaction conditions of first reaction zone is: reaction pressure 1.0～5.0MPa, 220～380 ℃ of average reaction temperature, volume space velocity 2～10h
-1, hydrogen to oil volume ratio 50～500Nm
3/ m
3The reaction conditions of second reaction zone is: reaction pressure 1.0～5.0MPa, 250～340 ℃ of average reaction temperature, volume space velocity 2～15h
-1, hydrogen to oil volume ratio 50～500Nm
3/ m
3
7, according to claim 1 or 6 described methods, it is characterized in that the reaction conditions of first reaction zone is: reaction pressure 1.5～3.2MPa, 260～360 ℃ of average reaction temperature, volume space velocity 3～6h
-1, hydrogen to oil volume ratio 100～300Nm
3/ m
3The reaction conditions of second reaction zone is: reaction pressure 1.5～3.2MPa, 270～320 ℃ of average reaction temperature, volume space velocity 3～10h
-1, hydrogen to oil volume ratio 80～300Nm
3/ m
3
8, in accordance with the method for claim 1, it is characterized in that described 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 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 the first reaction zone Hydrobon catalyst and the second reaction zone Hydrobon catalyst is 40: 60～70: 30.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009067893A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| CN101497806A (en) * | 2008-01-29 | 2009-08-05 | 丁冉峰 | System and method for preparing high quality petrol |
| WO2010083642A1 (en) * | 2009-01-21 | 2010-07-29 | 北京金伟晖工程技术有限公司 | System and process for producing high quality gasoline by recombination and subsequent hydrogenation of catalytic hydrocarbons |
| CN102268285A (en) * | 2011-07-08 | 2011-12-07 | 中国石油天然气股份有限公司 | Pre-hydrogenation treatment method for reforming raw material |
| CN102465020A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Combined hydrofining method |
| 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 |
| 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 |
| CN116064111A (en) * | 2021-10-31 | 2023-05-05 | 中国石油化工股份有限公司 | Process method for hydrodesiliconizing high-silicon naphtha |
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| DE2966422D1 (en) * | 1979-07-18 | 1983-12-29 | Exxon Research Engineering Co | Catalytic cracking and hydrotreating process for producing gasoline from hydrocarbon feedstocks containing sulfur |
| FR2807061B1 (en) * | 2000-03-29 | 2002-05-31 | Inst Francais Du Petrole | PROCESS FOR FUEL DESULFURIZATION COMPRISING DESULFURIZATION OF HEAVY AND INTERMEDIATE FRACTIONS FROM A FRACTIONATION IN AT LEAST THREE CUT |
| CN1210380C (en) * | 2002-04-30 | 2005-07-13 | 中国石油化工股份有限公司洛阳分公司 | Method of reducing sulfur content of catalytic cracking gasoline |
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| WO2009067893A1 (en) * | 2007-11-09 | 2009-06-04 | Ranfeng Ding | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| EA017164B1 (en) * | 2007-11-09 | 2012-10-30 | Жаньфэн Дин | A system and a process for recombining catalytic hydrocarbon to produce high quality gasoline |
| CN101497806A (en) * | 2008-01-29 | 2009-08-05 | 丁冉峰 | System and method for preparing high quality petrol |
| CN101497806B (en) * | 2008-01-29 | 2013-04-10 | 丁冉峰 | System and method for preparing high quality petrol |
| US8419930B2 (en) | 2009-01-21 | 2013-04-16 | Beijing Grand Golden-Bright Engineering & Technologies Co., Ltd. | System for preparing high-quality gasoline through component oil refining hydrocarbon recombination hydrogenation and method thereof |
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| EA019489B1 (en) * | 2009-01-21 | 2014-04-30 | Бейджин Гранд Голден-Брайт Инджиниринг Энд Текнолоджиз Ко., Лтд. | System and process for producing high quality gasoline by hydrogenation and recombination of oil refining hydrocarbon component |
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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 |
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| CN116064111A (en) * | 2021-10-31 | 2023-05-05 | 中国石油化工股份有限公司 | Process method for hydrodesiliconizing high-silicon naphtha |
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