CN102051230B - Process method for producing aromatic hydrocarbon by moving bed continuous reforming - Google Patents
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Abstract
The invention discloses a process method for producing aromatic hydrocarbon by moving bed continuous reforming. The process method comprises the following steps: carrying out prehydrogenation on a naphtha raw material; carrying out catalytic reforming on prehydrogenation generating oil so as to convert at least partial alkane and cycloparaffin into the aromatic hydrocarbon; and separating the aromatic hydrocarbon from the catalytic reforming generating oil, wherein a moving bed continuous reforming technology is adopted in the catalytic reforming process, four reaction areas are arranged, reaction raw materials successively pass through the four reaction areas, the aromatic hydrocarbon product is separated from reaction effluent in the fourth reaction area, a catalyst discharged from the fourth reaction area is recycled, and the recycled catalyst respectively enters the first reaction area and the fourth reaction area. Compared with the prior art, the process method disclosed by the invention has the advantages of high reaction efficiency, high aromatic hydrocarbon yield, prominent device economy and the like.
Description
Technical field
The present invention relates to a kind ofly take the material that contains paraffinic hydrocarbons and/or naphthenic hydrocarbon as raw material, adopt the catalytic reforming technology to produce the processing method of aromatic hydrocarbons, particularly adopt the processing method of producing aromatic hydrocarbon by moving bed continuous reforming.
Background technology
Along with the continuous increase of market to the petrochemicals demand, the demand rapid growth of the aromatic hydrocarbon products such as benzene, toluene and dimethylbenzene (being referred to as BTX).At present, take the petroleum naphtha that contains paraffinic hydrocarbons and/or naphthenic hydrocarbon as raw material, producing BTX with catalytic reforming process is the important means that obtains aromatic hydrocarbons.
Generally comprise the pre-hydrogenation of feed naphtha take petroleum naphtha as raw material production BTX technological process, hydrogenated oil carries out catalytic reforming, and reformate carries out the technical processes such as Aromatics Extractive Project.Feed naphtha generally comprises virgin naphtha and secondary processing petroleum naphtha.Therefore catalytic reforming generally comprises semi-regenerating catalytic reforming technology and continuous regenerative catalytic reforming technology, and two kinds of technology are all used noble metal catalyst, is essentially identical to the requirement of the pre-hydrogenation of raw material, requires sulphur in raw material and nitrogen all lower than 0.5 μ g/g.Therefore, for the source various, quality differs, the ever-increasing feed naphtha of impurity, adopting suitable pre-hydrogen addition technology is vital to the stable operation of catalytic reforming.
Along with improving constantly that device maximizes, mass-producing requires, the application of fixed bed half-regeneration reformer is restricted, and quality product is high, the continuous reformer that requires that is suitable for maximizing is used more and more extensive.At present 600,000 tons of annual working abilities even the Large Scale and Continuous reformer more than 1,000,000 tons be the emphasis of industrial application, be generally the annual working ability of 180～2,200,000 tons as the reformer in the ten-million-ton scale oil refining enterprise.Catalytic reforming reaction needs to carry out under hot conditions, and because reaction is strong endothermic reaction, therefore at conversion zone, a plurality of process furnace just need to be set reaction mass is heated (general reforming reaction is established 4 reactors, and each reactor inlet all need arrange process furnace).
In continuous reforming process, petroleum naphtha is in the situation that there is the hydrogen existence contact and react with the catalyzer that moves.Simultaneously, produce coke on the surface of catalyzer, the activity of catalyzer is reduced gradually.Catalyzer by reactive system is transported in the continuous catalyst regenerating system regenerates, and the catalyzer after regeneration is sent back to reactive system, begins next circulation.CN1042559A discloses a kind of CONTINUOUS REFORMER technology, and reaction mass is full of catalyzer and moves down by gravity successively by several reaction zones side by side in each reaction zone.According to the reagent flow direction, the catalyzer in previous reaction zone is transported to the top of next reaction zone from reaction zone bottom taking-up with hydrogen.The catalyzer of last reaction zone is transported to regeneration system rapidly with nitrogen and regenerates, and is transported to the top of first reaction zone with nitrogen through the catalyzer of regenerating.CN85103262A discloses a kind of continuous reforming process that adopts the eclipsed form reaction zone, and four reaction areas overlaps from top to bottom.Catalyzer is all by gravity flowage from first reaction zone to last reaction zone; The catalyzer of discharging from last reaction zone rises to regeneration system rapidly with nitrogen and regenerates, and rises to the top of first reaction zone with hydrogen through the catalyzer of regeneration.
In 4 reactors of continuous reformer, along the mobile direction of reaction mass, the volume of each reactor increases successively, is generally the ratio setting by catalyst loading volume 10:15:25:50.Also successively by first reactor to the four reactors, generally, the temperature in of four reactors is basic identical or close for continuous reforming catalyst, but due to the impact of reacting temperature drop, the average reaction temperature of four reactors increases successively.Because the catalyst activity of third and fourth reactor obviously reduces, the 4th reactor particularly, its catalyzer is through three reactors, activity has certain decline, and the 4th reactor average reaction temperature is high simultaneously, long reaction time, carbon deposit is many, and the overall activity of catalyzer is obviously lower.In the longest the 4th reactor of reaction times, the renewal speed of catalyzer slow (because reactor volume is large), catalyst activity is low, so reaction efficiency is low.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of processing method of producing aromatic hydrocarbon by moving bed continuous reforming, by optimizing the performance of each catalyst reactor, improve reaction efficiency, and then improve the economy of device.
The processing method of producing aromatic hydrocarbon by moving bed continuous reforming of the present invention comprises following content: feed naphtha carries out pre-hydrotreating, pre-hydrotreating generation oil carries out catalytic reforming at least part of paraffinic hydrocarbons and naphthenic hydrocarbon is converted into aromatic hydrocarbons, generates aromatics separation oil from catalytic reforming.wherein catalytic reforming adopts moving-bed CONTINUOUS REFORMER technology, four reaction areas is set: the first reaction zone, second reaction zone, the 3rd reaction zone and the 4th reaction zone, reaction raw materials passes through four reaction areas successively, isolate aromatic hydrocarbon product from the 4th reaction zone reaction effluent, the catalyzer that the 4th reaction zone is discharged is regenerated, catalyzer after regeneration enters respectively the first reaction zone and the 4th reaction zone, the catalyzer that the first reaction zone is discharged enters second reaction zone, the catalyzer that second reaction zone is discharged enters the 3rd reaction zone, the catalyzer that the 3rd reaction zone is discharged enters the 4th reaction zone.
In the inventive method, the four reaction areas of CONTINUOUS REFORMER can be set up in parallel, and also can overlap.Also can the first reaction zone and second reaction zone overlap, the 3rd reaction zone and the 4th reaction zone overlap, above-mentioned two overlapping reaction zones are set up in parallel.Also can the first reaction zone, second reaction zone and the 3rd reaction zone overlap, then be set up in parallel with the 4th reaction zone.Each reaction zone entrance reaction mass enters respective reaction zones after heating through process furnace.
In the inventive method, the catalytic reforming reaction temperature is 400～600 ℃, and reaction pressure is 0.1～1MPa(gauge pressure), during feeding liquid, the volume space velocity degree is 0.5～10h
-1, hydrogen to oil volume ratio is 100～2500Nm
3/ m
3Reforming catalyst generally uses platinum-Xi/aluminium oxide catalyst, and catalytic reforming catalyst can use the commercial goods, also can be by the conventional knowledge preparation in this area.
In the inventive method, the volume ratio that regenerated catalyst enters the first reaction zone and the 4th reaction zone is 2:1～15:1, is preferably 4:1～10:1.The processing power of catalyst regeneration system can not need increase, and namely total catalyst recirculation amount can not increase, and only regenerated catalyst is divided into two portions, and major part enters the first reaction zone, and small part enters the 4th reaction zone, can improve the combined reaction performance.Certainly, in order further to improve the reactivity worth of reactive system, can improve in right amount the catalyst treatment amount of regeneration system rapidly.
In the inventive method, the feed naphtha pre-hydrotreating can adopt first fractionation process, also can adopt the aftercut flow process, and first fractionation process is that feed naphtha first carries out fractionation, and the cut that boiling range is suitable carries out pre-hydrogenation, and pre-hydrogenated oil carries out catalytic reforming; The aftercut flow process is that feed naphtha first carries out pre-hydrogenation, and pre-hydrogenated oil carries out fractionation and obtains suitable cut and carry out catalytic reforming.The preferred aftercut flow process of the inventive method.
In the inventive method, the pre-hydrogenation of feed naphtha can adopt the method for this area routine, and as under suitable hydroconversion condition, feed naphtha and hydrogen make sulphur, nitrogen impurity content in raw material be reduced to below 0.5 μ g/g by the hydrotreating catalyst bed.The feed naphtha catalyst for pre-hydrogenation is non-precious metal catalyst, and catalyzer vulcanizes before use, and under state, active ingredient is sulphided state using, and the vulcanization process of catalyzer is well known to those skilled in the art.
In the inventive method, the pre-hydrogenation technique condition of feed naphtha is generally: 200～400 ℃ of average reaction temperature, reaction pressure 1.0～8.0MPa, volume space velocity 1.5～20h
-1, hydrogen to oil volume ratio is 50～500Nm
3/ m
3, the concrete technology condition can be adjusted according to feedstock property.
The pre-hydrotreating process that is preferably as follows: feed naphtha and hydrogen are under the hydroprocessing technique condition, successively by comprising following two hydrotreating catalyst beds, Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst mixed catalyst bed, and W-Mo-Ni-Co/ aluminium oxide catalyst bed.In the inventive method, the feed naphtha catalyst for pre-hydrogenation is non-precious metal catalyst, catalyzer vulcanizes before use, under state, active ingredient is sulphided state using, the vulcanization process of catalyzer is well known to those skilled in the art, by the outer sulfuration of sulfuration or device in device, active metal component is converted into sulphided state from oxidation state as the oxidation state active metal component for preparing.The Mo-Ni/ aluminium oxide catalyst refers to take Mo and Ni as active ingredient, the catalyzer take aluminum oxide as carrier, and general active ingredient is oxidation state when catalyzer prepares, and is sulphided state in use.Active ingredient is in oxide weight, and in the Mo-Ni/ aluminium oxide catalyst, molybdenum oxide content is 10%～25%, and nickel oxide content is 2%～8%; In the Mo-Co/ aluminium oxide catalyst, molybdenum oxide content is 10%～25%, and cobalt oxide content is 1%～8%; In the W-Mo-Ni-Co/ aluminium oxide catalyst, tungsten oxide content is 5%～15%, and molybdenum oxide content is 5%～15%, and nickel oxide content is 1%～6%, and cobalt oxide content is 1%～6%.In above-mentioned catalyzer, the pore volume of general requirement catalyzer is at 0.3～0.6ml/g, and specific surface area is at 180～350m
2/ g can contain suitable auxiliary agent in catalyzer.Concrete catalyzer can be selected satisfactory commercial catalyst, also can prepare by state of the art.In Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst mixed catalyst bed, the volume ratio of Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst is generally 5:1～1:5, is preferably 2:1～1:2.Total consumption of Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst be pre-hydrogenation use all catalyst volumes 30%～70%.W-Mo-Ni-Co/ aluminium oxide catalyst consumption be pre-hydrogenation use all catalyst volumes 30%～70%.Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst mixed catalyst bed have the various raw materials of adaptation, and the characteristic of quick removing impurities matter, for the high raw material of sulphur content, or the high raw material of nitrogen content, or the equal high raw material of sulphur, nitrogen content, the effect that all has quick removing impurities matter, the W-Mo-Ni-Co/ aluminium oxide catalyst is conducive to the degree of depth removing impurities qualitative response of foreign matter content when low, therefore above-mentioned catalyzer coordinates system, the hydrogenation process that can adapt to various character raw materials all can obtain qualified catalytic reforming raw material.
In the inventive method, catalytic reforming generates the method aromatics separation that oil can adopt this area routine, as adopting the solvent extraction method, perhaps adopts extraction rectifying method etc.After catalytic reforming generation oil can be gone and be carried out selective hydrogenation and removing a small amount of rare hydrocarbon wherein, then aromatics separation.
Compared with prior art, the inventive method has following advantage:
(1) adopt the catalytic reforming technology to produce aromatic hydrocarbons, have raw material sources wide, the advantage such as industrial scale is large, and is good in economic efficiency;
(2) the regenerated catalyst small part enters the 4th reaction zone, can effectively improve the catalyst updating speed of the 4th reaction zone, improves the overall activity of the 4th reaction zone catalyzer, is conducive to improve catalytic reforming reaction entire system reactivity worth.In the situation that the catalyst regeneration system processing power is constant, the combined reaction effect that all enters the first reaction zone than all regenerated catalysts is significantly improved;
(3) the pre-hydrogenation of raw material adopts the hydrogen system that adds of optimizing, and can adapt to multiple feed naphtha of different nature, all can obtain qualified catalytic reforming charging.As being adapted to all virgin naphthas, also can be adapted to some secondary processing petroleum naphthas, as the coking naphtha by simple hydrogenation, cracking naphtha, hydrocracking petroleum naphtha etc., perhaps mix petroleum naphtha etc.Improved market adaptability and the adaptability to changes of production equipment, be conducive to increase economic efficiency.
Description of drawings
Fig. 1 is process flow diagram of the present invention.
Wherein: 1-the first reactor, 2-the second reactor, 3-the 3rd reactor, 4-the 4th reactor, 5-catalyst regeneration system, 6-the first reactor process furnace, 7-the second reactor process furnace, 8-the 3rd reactor process furnace, 9-the 4th reactor process furnace.
Embodiment
Further illustrate the solution of the present invention and effect below in conjunction with drawings and Examples.
As shown in Figure 1, CONTINUOUS REFORMER arranges four reactors arranged side by side, reaction mass is successively by the first reaction heating furnace 6, the first reactor 1, the second reactor process furnace 7, the second reactor 2, the 3rd reactor process furnace 8, the 3rd reactor 3, the 4th reactor process furnace 9 and the 4th reactor 4, the 4th reactor 4 reaction effluents enter separation system through after heat exchange, obtain recycle hydrogen and reformed oil, reformed oil further separation obtains the purpose product.Catalyzer is successively by the first reactor 1, the second reactor 2, the 3rd reactor 3 and the 4th reactor 4, the catalyzer that the 4th reactor 4 is discharged enters catalyst regeneration system 5, catalyzer major part after regeneration enters the first reactor 1, and small part enters the 4th reactor 4.
In embodiment, keep the regenerated catalyst system throughput identical, namely the catalyst recirculation amount is constant.
Embodiment 1
In embodiment, the catalyzer that uses in the pre-hydrogenation of feed naphtha is as follows: the Mo-Ni/ aluminium oxide catalyst uses the FH-40A catalyzer of Fushun Petrochemical Research Institute's development, the Mo-Co/ aluminium oxide catalyst uses the FDS-4A catalyzer of Fushun Petrochemical Research Institute's development, and the W-Mo-Ni-Co/ aluminium oxide catalyst uses the FH-40C catalyzer of Fushun Petrochemical Research Institute's development.The catalyzer main character sees Table 1.The FH-40A catalyzer mixes formation the first beds (bed I) with the FDS-4A catalyst by proportion, the FH-40C catalyzer consists of the second beds (bed II), and reaction mass is successively by bed I and bed II.The feed naphtha that uses mainly contains three kinds, and specific nature sees Table 2.Raw material 1 is the virgin naphtha of domestic certain crude oil, and raw material 2 is the virgin naphtha of imported crude oil, the mixing raw material of the mass ratio 1:1 of imported crude oil virgin naphtha and hydrogenation coking naphtha in raw material 3.
Table 1 catalyzer main character.
| Catalyzer | FH-40A | FDS-4A | FH-40C |
| Active metal component | Mo-Ni | Mo-Co | W-Mo-Ni-Co |
| Pore volume/cm 3.g -1 | ≮0.40 | ≮0.40 | ≮0.42 |
| Surface-area/m 2.g -1 | ≮200 | ≮200 | ≮220 |
| Compressive strength/N.cm -1 | ≮150 | ≮150 | ≮150 |
Table 2 feed naphtha main character.
| The raw material numbering | Raw material 1 | Raw material 2 | Raw material 3 |
| The source | Virgin naphtha | Virgin naphtha | Mix petroleum naphtha |
| Density (20 ℃)/g.cm -3 | 0.7313 | 0.7242 | 0.7348 |
| Sulphur content/μ g.g -1 | 400 | 2600 | 800 |
| Nitrogen content/μ g.g -1 | 1.3 | 1.0 | 2.8 |
Embodiment 1～3
Adopt the inventive method, successively by bed I and bed II, the bed I is the mixed catalyst bed of Mo-Ni type catalyzer and Mo-Co type catalyzer under hydroconversion condition for raw material and hydrogen, and the bed II is W-Mo-Ni-Co type catalyzer.
Adopt different catalyst proportions, can effectively process dissimilar raw material, make hydrogenated oil meet the requirement of catalytic reforming charging.Concrete technology condition and reaction result see Table 3.
Table 3 embodiment 1～3 technological condition and hydrogenated oil character.
| Embodiment | 1 | 2 | 3 |
| Stock oil | Raw material 1 | Raw material 2 | Raw material 3 |
| Beds | ? | ? | ? |
| FH-40A and FDS-4A volume ratio | 1：1 | 1：3 | 2：1 |
| Bed I/bed II volume ratio | 1：1 | 2：1 | 1：2 |
| Processing condition | ? | ? | ? |
| Reaction pressure/MPa | 1.6 | 1.6 | 1.6 |
| Temperature of reaction/℃ | 270 | 300 | 300 |
| Volume space velocity/h -1 | 10.0 | 10.0 | 10.0 |
| Hydrogen-oil ratio/Nm 3.m -3 | 100 | 100 | 100 |
| Oil property | Treated oil | Treated oil | Treated oil |
| Sulphur content/μ g.g -1 | <0.5 | <0.5 | <0.5 |
| Nitrogen content/μ g.g -1 | <0.5 | <0.5 | <0.5 |
Embodiment 4
According to the catalyzer coordinated scheme of embodiment 1, process different raw materials under higher air speed, all can obtain up-to-standard catalytic reforming raw material, actual conditions and the results are shown in Table 4.
Use single catalyst, adopt the reaction conditions identical with embodiment 4, use different material to test, result shows, under higher space velocity, single catalyst can reach catalytic reforming charging requirement to some raw material, but can't obtain qualified catalytic reforming raw material to some raw material, and the adaptability of raw material is relatively poor.Actual conditions and the results are shown in Table 5.
Table 4-1 embodiment 4-5 technological condition.
| Embodiment | 4 | 5 |
| Beds | ? | ? |
| FH-40A and FDS-4A volume ratio | 1：1 | / |
| Bed I/bed II volume ratio | 1：1 | Single FH-40A catalyzer |
| Processing condition | ? | ? |
| Reaction pressure/MPa | 1.6 | 1.6 |
| Temperature of reaction/℃ | 300 | 300 |
| Volume space velocity/h -1 | 12.5 | 12.5 |
| Hydrogen-oil ratio/Nm 3.m -3 | 100 | 100 |
Table 4-2 embodiment 4-5 hydrogenated oil character.
| Embodiment | 4 | 4 | 4 | 5 | 5 | 5 |
| Stock oil | Raw material 1 | Raw material 2 | Raw material 3 | Raw material 1 | Raw material 2 | Raw material 3 |
| Oil property | Treated oil | Treated oil | Treated oil | Treated oil | Treated oil | Treated oil |
| Sulphur content/μ g.g -1 | <0.5 | <0.5 | <0.5 | <0.5 | 0.8 | 0.9 |
| Nitrogen content/μ g.g -1 | <0.5 | <0.5 | <0.5 | <0.5 | <0.5 | 0.6 |
Embodiment 6-8
Hydrogenation products with 4 three kinds of raw materials of embodiment carries out catalytic reforming, and wherein at least part of paraffinic hydrocarbons and naphthenic hydrocarbon are converted into aromatic hydrocarbons.Catalytic reforming is the CONTINUOUS REFORMER experimental installation, and CONTINUOUS REFORMER is used four moving-burden bed reactors and catalyst regeneration system, and the treatment capacity of catalyst regeneration system remains unchanged.Catalytic reforming catalyst is the RC-011 continuous reforming catalyst of Sinopec Research Institute of Petro-Chemical Engineering development, and the effecting reaction volume of four reactors is 10:15:25:50.Reaction pressure 0.35MPa, hydrogen-oil ratio 700Nm
3.m
-3, volume space velocity 2.0h
-1, average bed temperature of reaction is 508 ℃, the reaction result of different material sees Table 5.
Comparative example 1-3
Identical with embodiment 6-8 operational condition, adopt conventional operating method, reaction result sees Table 5.As can be seen from Table 5, the inventive method can effectively improve aromatics yield and the liquid product yield of continuous reforming process.
Table 5 embodiment 6-8 and comparative example 1-3 experimental result.
| Embodiment | Embodiment 6 | Comparative example 1 | Embodiment 7 | Comparative example 2 | Embodiment 8 | Comparative example 3 |
| Raw material | Raw material 1 | Raw material 1 | Raw material 2 | Raw material 2 | Raw material 3 | Raw material 3 |
| Enter the volume ratio of the first reactor and the 4th reactor regenerated catalyst | 5：1 | / | 10：1 | / | 3：1 | / |
| Liquid receipts/quality % | 87.43 | 85.32 | 84.17 | 82.76 | 84.53 | 83.48 |
| Aromatics yield/quality % | 66.35 | 63.48 | 66.03 | 64.52 | 63.84 | 62.79 |
Catalytic reforming generates oil and adopts the method for Sulfolane Extraction and further rectifying to obtain various aromatic hydrocarbon products, and the product of whole Technology comprises p-Xylol, o-Xylol, benzene, toluene, light naphthar (solvent oil), liquefied gas, hydrogen etc.
Claims (11)
1. the processing method of a producing aromatic hydrocarbon by moving bed continuous reforming, comprise following content: feed naphtha carries out pre-hydrotreating, pre-hydrotreating generation oil carries out catalytic reforming at least part of paraffinic hydrocarbons and naphthenic hydrocarbon is converted into aromatic hydrocarbons, generates aromatics separation oil from catalytic reforming, wherein catalytic reforming adopts moving-bed CONTINUOUS REFORMER technology, four reaction areas is set: the first reaction zone, second reaction zone, the 3rd reaction zone and the 4th reaction zone, reaction raw materials passes through four reaction areas successively, isolate aromatic hydrocarbon product from the 4th reaction zone reaction effluent, the catalyzer that the 4th reaction zone is discharged is regenerated, it is characterized in that: the catalyzer after regeneration enters respectively the first reaction zone and the 4th reaction zone, the catalyzer that the first reaction zone is discharged enters second reaction zone, the catalyzer that second reaction zone is discharged enters the 3rd reaction zone, the catalyzer that the 3rd reaction zone is discharged enters the 4th reaction zone, the volume ratio that regenerated catalyst enters the first reaction zone and the 4th reaction zone is 2:1～15:1, four reaction areas is four reactors, and along the mobile direction of reaction mass, four reactor catalyst admission spaces are 10:15:25:50.
2. it is characterized in that in accordance with the method for claim 1: the four reaction areas of CONTINUOUS REFORMER is set up in parallel; Perhaps overlap; Perhaps the first reaction zone and second reaction zone overlap, and the 3rd reaction zone and the 4th reaction zone overlap, and above-mentioned two overlapping reaction zones are set up in parallel; Perhaps the first reaction zone, second reaction zone and the 3rd reaction zone overlap, and then are set up in parallel with the 4th reaction zone.
3. according to the described method of claim 1 or 2, it is characterized in that: each reaction zone entrance reaction mass enters respective reaction zones after heating through process furnace.
4. in accordance with the method for claim 1, it is characterized in that: the catalytic reforming reaction temperature is 400～600 ℃, and reaction pressure is 0.1～1MPa, and during feeding liquid, the volume space velocity degree is 0.5～10h
-1, hydrogen to oil volume ratio is 100～2500Nm
3/ m
3
5. it is characterized in that in accordance with the method for claim 1: the volume ratio that regenerated catalyst enters the first reaction zone and the 4th reaction zone is 4:1～10:1.
6. in accordance with the method for claim 1, it is characterized in that: the feed naphtha pre-hydrotreating can adopt first fractionation process, perhaps adopts the aftercut flow process.
7. according to the described method of claim 1 or 6, it is characterized in that: the pre-hydrogenation of feed naphtha is under suitable hydroconversion condition, and feed naphtha and hydrogen make sulphur, nitrogen impurity content in raw material be reduced to below 0.5 μ g/g by the hydrotreating catalyst bed; The pre-hydrogenation technique condition of feed naphtha is: 200～400 ℃ of average reaction temperature, reaction pressure 1.0～8.0MPa, volume space velocity 1.5～20h
-1, hydrogen to oil volume ratio is 50～500Nm
3/ m
3
8. in accordance with the method for claim 7, it is characterized in that: feed naphtha pre-hydrotreating process is that feed naphtha and hydrogen are under the hydroprocessing technique condition, successively by comprising following two hydrotreating catalyst beds, Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst mixed catalyst bed, and W-Mo-Ni-Co/ aluminium oxide catalyst bed; Active ingredient is in oxide weight, and in the Mo-Ni/ aluminium oxide catalyst, molybdenum oxide content is 10%～25%, and nickel oxide content is 2%～8%; In the Mo-Co/ aluminium oxide catalyst, molybdenum oxide content is 10%～25%, and cobalt oxide content is 1%～8%; In the W-Mo-Ni-Co/ aluminium oxide catalyst, tungsten oxide content is 5%～15%, and molybdenum oxide content is 5%～15%, and nickel oxide content is 1%～6%, and cobalt oxide content is 1%～6%.
9. in accordance with the method for claim 8, it is characterized in that: in Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst mixed catalyst bed, the volume ratio of Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst is 5:1～1:5; Total consumption of Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst be pre-hydrogenation use all catalyst volumes 30%～70%; W-Mo-Ni-Co/ aluminium oxide catalyst consumption be pre-hydrogenation use all catalyst volumes 30%～70%.
10. in accordance with the method for claim 1, it is characterized in that: catalytic reforming generates oil and adopts the solvent extraction method, perhaps adopts the extraction rectifying method aromatics separation; After perhaps catalytic reforming generation oil carries out selective hydrogenation and removing a small amount of rare hydrocarbon wherein, then aromatics separation.
11. in accordance with the method for claim 9, it is characterized in that: in Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst mixed catalyst bed, the volume ratio of Mo-Ni/ aluminium oxide catalyst and Mo-Co/ aluminium oxide catalyst is 2:1～1:2.
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| CN1247886A (en) * | 1998-09-11 | 2000-03-22 | 中国石化北京设计院 | Catalytic conversion process in counter-flow moving bed with several reactors |
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| CN1746268A (en) * | 2004-09-07 | 2006-03-15 | 白跃华 | Continuous reforming process of non-locking hopper |
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