CN102041092B - Method for widening catalytic reforming feedstock - Google Patents
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Abstract
The invention relates to method for widening catalytic reforming feedstock. The comprises the following steps: mixing FCC (fluid catalytic cracking) stabilized gasoline and straight-run naphtha in a ratio of (50:50) to (70:30), filtering the obtained mixture by a feedstock filter so as to remove impurities in the mixture, and then removing the water carried in the mixed naphtha by a coalescer; mixing the mixed naphtha with hydrogen, and heating the obtained mixture to a reaction temperature by a heating furnace, then feeding the obtained mixture into a hydrogenation reactor to contact with a hydrogenation catalyst so as to be subject to olefin saturation, desulphurization and denitrification reactions; and condensating and cooling the obtained hydrogenation effluent, then separating the obtained product so as to obtain hydrogen-rich gas and hydrogenated gasoline, recycling the hydrogen-rich gas, and feeding the hydrogenated gasoline into an evaporation tower to be subject to stripping fractionation, thereby obtaining a refined naphtha meeting the reforming feeding requirements. By utilizing the method provided by the invention, the mixed naphtha containing more than 50 percent of the FCC stabilized gasoline can be subject to hydroprocessing so as to obtain the refined naphtha, wherein the content of the impurities in the refined naphtha satisfies the reforming feeding requirements, thereby solving the shortage problem of the reforming feedstock, and widening the source of the reforming feedstock.
Description
Technical field
The present invention relates to a kind of processing method of producing treated oil (catalytic reforming feedstock) under the hydrogen environment of facing, more particularly, be in a kind of virgin naphtha blending at high proportion FCC (catalytic cracking) stable gasoline carry out the processing method that reformer feed is produced in hydrofining.
Background technology
Along with the increasingly stringent that requires of world's environmental regulation, production environment close friend's clean fuel becomes the theme of 21 century petroleum refining industry's development.China's gasoline products mainly be take FCC gasoline as main at present, and FCC gasoline is the main blend component of gasoline, has the characteristics of high-sulfur and high olefin, and the sulphur in gasoline product more than 90% comes from FCC gasoline.Therefore, the quality of improving catalytically cracked gasoline is the key of internal vapor oil quality upgrading.And catalytic reforming gasoline does not contain alkene substantially, its sulphur, nitrogen content are extremely low, and vapour pressure is little, and octane value is higher, is a kind of clean gasoline component of high-quality.If FCC gasoline is produced to reformed gasoline as reformer feed, so both can reduce sulphur in gasoline and the content of alkene, can improve gasoline octane rating again, can also provide cheap hydrogen source for hydrogenation unit simultaneously.
Catalytic reforming process is one of important technique of oil refining and petrochemical complex, and it take petroleum naphtha as raw material, reacts and generates the reformed oil that is rich in aromatic hydrocarbons by catalytic hydroprocessing, simultaneously by-product hydrogen and liquefied petroleum gas (LPG).Reformed oil can be directly as the blending component of gasoline, also can be through Aromatics Extractive Project or other conversions and separating technology preparing aromatic hydrocarbon product-benzene, toluene and dimethylbenzene, as the basic raw material of petrochemical complex, by-product hydrogen is the important sources of refinery with hydrogen.Reformer mainly be take virgin naphtha as raw material, and crude oil in China mostly is paraffinic base, and the virgin naphtha yield is low, simultaneously, virgin naphtha is again the main raw material of cracking ethylene preparation, and the development of ethylene industry makes the feed naphtha increase in demand, has restricted the development of catalytic reforming process.Therefore, widen reformer feed and become the matter of utmost importance that promotes China's catalytic reforming process development.
Catalytic reforming adopts platinum rhenium or platinum bimetallic ruthenium/tin catalyst, very strict to the requirement of the impurity such as the sulphur in raw material, nitrogen, requires sulphur, nitrogen content all to be less than 0.5 μ g/g, and especially nitrogen content requires to be less than as far as possible 0.1 μ g/g, and catalytic reforming feedstock impurity requires as table 1.At present, the petroleum naphtha hydrogenation unit (preprocessing part) of domestic reformer is all according to processing the virgin naphtha design and producing, because virgin naphtha sulphur, nitrogen content are lower, operational condition relatively relaxes, and hydrogenation reaction pressure generally just can be met the catalytic reforming feedstock of requirement at 2.0MPa (g).And the FCC content of olefin in gasoline is high, general 35 (v) % that surpasses, even reach 60 (v) %, sulphur content is at 100～1000 μ g/g, nitrogen content reaches 20～100 μ g/g, even mix the nitrogen content of petroleum naphtha after mixing with virgin naphtha also at 5～50 μ g/g, make nitrogen content in catalytic reforming feedstock be less than 0.5 μ g/g, the petroleum naphtha hydrogenation reaction pressure will be more than 4.0MPa (g).Simultaneously, the olefin(e) centent mixed in petroleum naphtha also has 10 (v) %～30 (v) %, because olefin hydrogenation is thermopositive reaction, can cause pre-hydrotreating reaction bed temperature runaway under the high olefin environment, make H2S again with olefine reaction, generate mercaptan, cause the catalytic reforming feedstock sulphur content to exceed standard.Therefore, the raw material ratio of the reformer petroleum naphtha hydrogenation cell processing blending FCC gasoline of Present Domestic is more difficult, can't guarantee the degree of depth of desulfurization removing nitric.
Patent EP0022883A1 discloses a kind of method of gasoline that sour gasoline is produced through catalytic cracking and hydrofining.Sour gasoline is first produced the high olefin gasoline of olefin(e) centent at 10%-60% through a stage catalytic cracking, then gets middle cut or last running or the two carries out saturation of olefins, desulfurization and denitrogenation through two stage catalytic crackings together again.Two sections products carry out under comparatively gentle condition that the low-sulphur oil blending component is produced in hydrofining or again as reformer feed.Can obtain by this kind of method the hydrofining product that sulphur, nitrogen all are less than 1 μ g/g, this product can be used as the charging of platinoiridita reforming catalyst, but can not meet platinum rhenium or platinum tin reforming catalyst charging requirement.And there is the flow process complexity in this technique, the problems such as investment operation expense height.
Application number CN200810118165.3 discloses a kind of in the situation that there is not hydrogen, and the light middle catalytically cracked gasoline cut of take is raw material, adopts the selective solvent extraction rectifying method to produce catalytic reforming raw material.Adopt this kind of method can obtain aromatic free, sulphur content is less than 20 μ g/g lighting ends as reformer feed.Adopt this kind of method can only reduce the sulphur content of catalytic gasoline, can't solve the problem that catalytic gasoline nitrogen and olefin(e) centent are high, must need to carry out further hydrotreatment before advancing reformer could be as the reformer charging.Need to increase a set of extraction plant simultaneously, greatly increased facility investment.
Application number CN200510089847.2, CN200510089848.7 disclose a kind of method that the hydrofining of secondary processing oil is produced to reformer feed.At first FCC gasoline is cut, be divided into light benzine cut, middle matter gasoline fraction and heavy gasoline cut, then chosen middle matter gasoline fraction as wanting hydrorefined raw material.CN200510089847.2 is mixed into the first reaction zone by middle matter gasoline fraction and hydrogen to react, and then is mixed into second reaction zone with low temperature virgin naphtha as quenching oil and is reacted.During patent CN200510089848.7 adopts, the matter gasoline fraction is mixed into the first reaction zone with hydrogen and reacts and carry out olefin saturated together with virgin naphtha, reaction product is carried out desulfurization removing nitric entering second reaction zone, and two kinds of methods all can obtain the product that sulphur, nitrogen content all are less than 0.5 μ g/g.The problem that this two method exists is: one, FCC gasoline is cut, and increase facility investment, increased energy consumption; Its two, the first hydrogenation one section outlet of middle matter gasoline fraction temperature is higher, and H easily occurs
2s reacts with olefin production mercaptan.And liquid easily occurs at the bed skewness with virgin naphtha as quenching oil, and produce channel, control the inlet amount of virgin naphtha amount by the second-stage reaction temperature out simultaneously, affected the processing power of device; Its three, without the chilling measure, be not suitable for matter gasoline fraction in the blending vast scale, otherwise the bed temperature out is too high in the method for middle matter gasoline fraction hydrogenation reaction together with virgin naphtha, the product sulphur content is defective.
Magnify Tianjin (refining of petroleum and chemical industry, 2004,35 (11), P48-51) introduced the industrial application that the straight-run spirit blend FCC gasoline is produced reformer feed, be subject to the pretreatment technology condition restriction, catalytic gasoline is mixed refining ratio maximum can only reach 18wt%, surpasses this ratio treated oil nitrogen content defective.
Summary of the invention
The purpose of this invention is to provide a kind of processing method that enlarges the reformer feed source.By optimization technological process and operational condition, make the ratio of blending FCC stable gasoline be not less than 50%, effectively enlarged the source of reformer feed.
The FCC stable gasoline is mixed with virgin naphtha, after filtration, poly-liquid removes catalyst dust that in mixing oil, FCC gasoline carries and the saturation water in mixing oil; Then enter the two-stage hydrogenation reactor and reacted together with hydrogen, reaction pressure is 2.0～5.0MPa (g), and average reaction temperature is 280～310 ℃, and volume space velocity (LHSV) is 2～8h
-1, hydrogen-oil ratio is 90～300Nm
3/ m
3.Reaction product, through heat exchange, is separated after condensing cooling, after the compressed machine of isolated hydrogen-rich gas boosts, recycles, and liquid is met the refining petroleum naphtha of catalytic reforming feedstock requirement after the fractionation of evaporator tower stripping imurity-removal.
FCC gasoline is initial boiling point～170 ℃, and virgin naphtha is initial boiling point～180 ℃.The FCC stable gasoline is 50: 50～70: 30 with the mixed weight ratio of virgin naphtha.
Hydrogenation catalyst adopts maximum denitrogenation-type catalyzer, is to take aluminum oxide as carrier, and metal Ni and Mo are active ingredient, and catalyzer is containing Ni 2～5 (wt) %, Mo 11～14 (wt) %.Catalyst shape is the extrusion cloverleaf pattern, and specification is 1.3-2.5mm, and packing density is 0.8-0.85t/m
3, one section is 20 with two sections catalyst loading part by weight: 80-50: 50.
Two reactor can adopt a reactor catalyst segmentation filling, and the method for establishing cold hydrogen dish between two beds, also can adopt two reactors in series, the method for establishing cold hydrogen decanting point between two reactors.Two-stage reaction all loads identical catalyzer, on first stage reactor top, adopts grading loading technology filling protection filler for slowing down olefinic polyreaction, and ant-scaling, reduce the reaction bed pressure drop.
The present invention has the following advantages:
(1) the mixing petroleum naphtha that mixing proportion can be surpassed to the 50%FCC stable gasoline carries out hydrotreatment, obtains the refining petroleum naphtha that foreign matter content all meets the catalytic reforming feedstock requirement, has solved the not enough problem of reformer feed, the source of having widened reformer feed.
(2) pre-hydrogenator adopts catalyst segments filling or two reactors in series, annotate the method for cold hydrogen between two beds or between reactor, effectively solved high bed temperature runaway and the uppity problem of bed temperature of causing of olefin(e) centent in pre-hydrogenation charging, guarantee that the bed temperature out is no more than 340 ℃, prevents alkene and H
2the S recombine generates mercaptan.
(3) one section bed top of pre-hydrogenator or the first reactor head adopt protective material grading loading technology; effectively slowed down olefinic polyreaction, made feed stream distribute more even, prevented that channel from occurring; and there is stronger ant-scaling ability, reduced the reaction bed pressure drop.
(4) raw material strainer and coalescer are set, filter out the impurity such as catalyst dust that mix in petroleum naphtha, remove the saturation water in stock oil, be conducive to reduce the pre-hydrotreating reaction pressure drop, prevent that catalyzer is subject to the efflorescence of water slug strength reduction, extended catalyzer work-ing life.
(5) technical process is simple, technology maturation, flexible operation.Both can process the FCC stable gasoline that mixing proportion is larger, also can process other secondary processing of gasoline of vast scale blending.This technique is applicable to newly-built Naphtha hydrofining unit, also is applicable to old device enlarging transformation.
The accompanying drawing explanation
Fig. 1 is the hydrofining technology method flow schematic diagram that blending FCC stable gasoline is produced reformer feed.
1-pipeline wherein, the 2-pipeline, 3-raw material strainer, the 4-pipeline, the 5-coalescer, 6-pipeline 7-surge tank, the 8-pipeline, the 9-fresh feed pump, the 10-pipeline, the 11-feed exchanger, the 12-pipeline, 13-charging process furnace, the 14-pipeline, the 15-hydrogenator, the 16-hydrogenator, the 17-pipeline, the 18-pipeline, 19-product air cooler, the 20-pipeline, 21-product water cooler, the 22-pipeline, the 23-gas-liquid separator, the 24-pipeline, the 25-circulating hydrogen compressor, the 26-pipeline, the 27-pipeline, the 28-pipeline, the 29-pipeline, 30-evaporator tower feed exchanger, the 31-pipeline, the 32-evaporator tower, the 33-pipeline, 34-evaporator tower head space cooler, the 35-pipeline, 36-evaporation tower top water cooler, the 37-pipeline, 38-evaporator tower return tank, the 39-pipeline, the 40-pipeline, the 41-light naphthar is through reflux pump, the 42-pipeline, the 43-pipeline, the 44-pipeline, the 45-pipeline, the 46-pipeline, the 47-column bottoms pump, the 48-pipeline, 49-evaporator tower reboiler furnace, the 50-pipeline
Embodiment
Method provided by the invention is so concrete enforcement:
(1) FCC stable gasoline and virgin naphtha are mixed, through the raw material strainer, remove by filter chip, degradation product and catalyst dust granule foreign wherein, then remove and mix the water carried in petroleum naphtha through coalescer;
(2) mix petroleum naphtha and enter hydrogenator with the hydrogen mixing after process furnace is heated to temperature of reaction and contact with hydrogenation catalyst, carry out olefin saturated, desulfurization and denitrification reaction;
(3) hydrogenation reaction effluent separates and obtains hydrogen-rich gas and hydrogenated gasoline after condensing cooling, and hydrogen-rich gas recycles, and hydrogenated gasoline enters evaporator tower and carries out the refining petroleum naphtha that the stripping fractionation is met the catalytic reforming feedstock requirement.
Control that stablize that the FCC stable gasoline does be 150 ℃～170 ℃ in step (1), higher than 170 ℃, be easy to cause reforming catalyst to tie carbon, shortened the production cycle.
The blending ratio that step (1) is stablized FCC stable gasoline and virgin naphtha is 0: 100～90: 10, preferably 50: 50～70: 30.The raw material strainer meets following the requirement: strainer adopts basket fabric, and filtering element is filter core, and filtering accuracy is less than or equal to 10 μ m, and filtration pressure is reduced to 20kPa; Coalescer meets following the requirement: coalescing element is filter element type, and the W/O decreasing ratio should be greater than 98 (v) %.
The described hydrogenation conditions of step (2) is that reaction pressure is 2.0～5.0MPa (g), the reaction temperature in is 280～320 ℃, the reaction temperature out is that 280～340 ℃ of average reaction temperature are 280～310 ℃, and volume space velocity (LHSV) is 2～8h
-1, hydrogen-oil ratio is 90～300Nm
3/ m
3.Catalyzer adopts the maximum denitrogenation-type catalyzer that Standard Co., Ltd's trade mark is DN3110, to take aluminum oxide as carrier, the metallic nickel molybdenum is active ingredient, be shaped as trefoil extruded catalyst, and wherein catalyzer is containing Ni 3.7 (wt) %, Mo 12.9 (wt) %.
Step (2) is carried out in two reactors, or carries out in a reactor.The catalyzer of the first reactor is for olefin saturated and partial desulfurization, denitrogenation, and the catalyzer of the second reactor is for desulfurization and denitrogenation.Cold hydrogen decanting point is set between two reactors, injects cold hydrogen when excessive for the bed temperature rise to reduce the bed temperature of reaction, guarantee that the reaction temperature out is not more than 340 ℃, prevents the H that alkene and hydrogenation reaction generate
2s, in conjunction with regenerating mercaptan, makes operation more flexible.If while using a reactor, hydrogenation catalyst adopts the segmentation filling, and two intersegmentally establish cold hydrogen dish.All load catalyzer of the same race in two reactors (or two sections beds), the filling ratio is 20: 80～50: 50, preferably 30: 70～50: 50.
Step (2) first hydrogenator tops adopt the grading loading technology, load successively from top to down the 834HC of Standard Co., Ltd and 815HC protective material.The activated iron protective material of 834HC tool; there is the hollow circular cylinder of catching the particle ability for a kind of; have wide aperture and be unlikely and accumulate in the hole that following catalyzer is less so that particle enters protective material itself; the generating rate of slow down coking and fouling, protection Primary Catalysts bed extending catalyst life-span.815HC is a kind of nickel molybdenum Hydrobon catalyst, for slowing down reactor pressure, falls and advances the speed, and its hydrogenation activity can slow down bed scaling rate and the olefinic polyreaction caused due to the coke deposition, reduces product of polymerization quantity.
Step (2) hydrogenation catalyst needs prevulcanized before use, and method for pre-sulphuration is identical with conventional petroleum naphtha hydrogenation catalyzer.Adopt virgin naphtha or refining petroleum naphtha as vulcanized oil, inject Methyl disulfide (DMDS), carry out cyclical operation under certain reaction pressure and hydrogen-oil ratio, curing temperature is 150 ℃～300 ℃, total cure time 24h.
Step (3) hydrogenated gasoline stripping adopts single tower flow process, is about to stripping tower and separation column and unites two into one, and a tower is realized stripping and fractional distillation functions, to reduce facility investment.Tower top arranges annotates the inhibiter measure, slows down equipment corrosion.Adopt the reboiler furnace heating at the bottom of tower.
To technology further instruction provided by the present invention, but not thereby limiting the invention below in conjunction with accompanying drawing.
Accompanying drawing is the Technology schematic diagram that reformer feed is produced in the FCC of blending at high proportion stable gasoline hydrofining provided by the invention.
This techniqueflow is as follows:
The FCC stable gasoline is through pipeline 1 and incoming stock strainer 3 after the virgin naphtha of pipeline 2 mixes, the solid impurity removed by filter in raw material enters coalescer 5 by pipeline 4, the water carried remove raw material in coalescer 5 in, meet the requirement of hydrogenation catalyst to water-content in raw material.After dehydration the mixing petroleum naphtha enter fresh feed pump 9 and boost through pipeline 6, surge tank 7, pipeline 8, again through pipeline 10 with after the recycle hydrogen of pipeline 26 mixes successively after feed exchanger 11, pipeline 12, charging process furnace 13, enter hydrogenator 15 and hydrogenator 16 and hydrogenation catalyst contact reacts through pipeline 14.Reaction product after pipeline 17 advances interchanger 11 heat exchange again through pipeline 18, product air cooler 19, pipeline 20, product water cooler 21 condensing coolings enter hydrogenation gas-liquid separator 23 by pipeline 22, separator 23 tops are isolated hydrogen-rich gas and are advanced circulating hydrogen compressor 25 compression rear portions through pipeline 24 and mix the petroleum naphtha mixing by feed exchanger 11 heat exchange as recycle hydrogen through pipeline 26 and pipeline 10, charging process furnace 13 is heated to after temperature of reaction and enters hydrogenator 15 and 16 and carry out hydrogenation reaction, another part enters decanting point between hydrogenator 15 and 16 as quenching hydrogen through pipeline 27.New hydrogen enters system to supplement hydrogen consumption in hydrogenation process through pipeline 28.Separator 23 bottom liquid phases enter evaporator tower 32 through pipeline 29,30 heat exchange of evaporator tower feed exchanger by pipeline 31, in evaporator tower 32, are removed H
2s, NH
3and H
20 operation and fractionation light naphthar.Evaporator tower 32 top gas are advanced evaporator tower head space cooler 34 and pipeline 35 through pipeline 33 and are advanced to evaporate tower top water cooler 36 condensing coolings and enter evaporator tower return tank 38 by pipeline 37, return tank 38 top sulfurous fuels gas go out device through pipeline 39,38 end of return tank light naphthar returns to evaporator tower 32 as refluxing through pipeline 42 through pipeline 40, reflux pump 41 rear portion of boosting, and rest part is through pipeline 43 carrying devices.32 end of evaporator tower,, a treated oil part was advanced evaporator tower feed exchanger 30 through pipeline 44, and the charging heat exchange is delivered to reformer as reformer feed by pipeline 45; Another part, after pipeline 46, column bottoms pump 47 boost, then returns to evaporator tower 32 through 49 heating of pipeline 48, evaporator tower reboiler furnace by pipeline 50.
The following examples will be further described technology provided by the present invention, but not thereby limiting the invention.
Embodiment 1
A kind of FCC stable gasoline and a kind of virgin naphtha are raw material, and its character is as table 2.The FCC stable gasoline is mixed by 20: 80 (wt%) with virgin naphtha, obtain mixing petroleum naphtha A, its character is as table 2.Mix petroleum naphtha C and contact in reactor and carry out hydrogenation reaction with hydrogenation catalyst DN3110, adopt two reactors, the catalyst loading ratio is 50: 50, does not annotate chilling hydrogen between reactor.Reaction conditions is: reaction pressure 2.5MPa (g), the first 280 ℃ of reactor inlet temperatures, volume space velocity (LHSV) 2.5h
-1, hydrogen to oil volume ratio 250Nm
3/ m
3.Reaction product obtains refining petroleum naphtha after the stripping fractionation.Operational condition and product property are as table 3.
As can be seen from Table 3, while mixing the low ratio FCC stable gasoline of refining, because olefin(e) centent is low, the bed temperature rise is not high, and sulphur, nitrogen, bromine index all meet the catalytic reforming feedstock requirement.
Embodiment 2
FCC stable gasoline identical in example 1 is mixed by 50: 50 (wt%) with virgin naphtha, obtain mixing petroleum naphtha B, its character is as table 2.Mix petroleum naphtha B and contact in reactor and carry out hydrogenation reaction with hydrogenation catalyst DN3110, reaction conditions is identical with example 1, and operational condition and product property are as table 3.
As can be seen from Table 3, when mixing refining FCC stable gasoline ratio while reaching 50wt%, mixing oil sulphur, nitrogen, olefin(e) centent are all higher, and nitrogen content reaches 27 μ g/g, and the bromine valency is 28gBr/100g.Under existing reaction conditions, the hydrogen dividing potential drop can't meet the requirement of denitrogenation, and the hydrogenated products nitrogen content exceeds standard.Simultaneously, in stock oil, olefin(e) centent is high, pre-hydrogenator bed temperature rise ratio is larger, the one anti-main olefin hydrogenation that occurs, in the situation that the catalyst loading ratio is 50: 50, an anti-bed temperature rise ratio is higher, temperature out reaches 352 ℃, in the situation that do not annotate cold hydrogen, two anti-temperature outs have reached 361 ℃, the H that hydrogenation reaction generates
2s and alkene generate mercaptan again, and the hydrogenated products sulphur content is defective.
Embodiment 3
Mixing petroleum naphtha B identical in example 2 is contacted and carries out hydrogenation reaction with hydrogenation catalyst DN3110 in reactor, and the catalyst loading ratio is 40: 60, annotates chilling hydrogen between reactor.Reaction conditions is: reaction pressure 3.6MPa (g), the first 280 ℃ of reactor inlet temperatures, volume space velocity (LHSV) 2.6h
-1, hydrogen to oil volume ratio 300Nm
3/ m
3.Operational condition and product property are as table 3.
As can be seen from Table 3, when reaction pressure being brought up to 3.6MPa (g), the catalyst loading ratio is 40: 60 and annotates in cold hydrogen situation, hydrogenated products sulphur nitrogen content all meets the catalytic reforming feedstock requirement, two anti-temperature outs are only 319 ℃, and the foreign matter contents such as hydrogenated products sulphur nitrogen all meet the catalytic reforming feedstock requirement.
Embodiment 4
FCC stable gasoline identical in example 1 is mixed by 70: 30 (wt%) with virgin naphtha, obtain mixing petroleum naphtha C, its character is as table 2.Mix petroleum naphtha C and contact in reactor and carry out hydrogenation reaction with hydrogenation catalyst DN3110, annotate chilling hydrogen between reactor.Reaction conditions is: reaction pressure 4.0MPa (g), the first 280 ℃ of reactor inlet temperatures, volume space velocity (LHSV) 2.8h
-1, hydrogen to oil volume ratio 300Nm
3/ m
3.Reaction product obtains refining petroleum naphtha after the stripping fractionation.Operational condition and product property are as table 3.
As can be seen from Table 3, mix while refining at high proportion the FCC stable gasoline, the bed temperature rise ratio is higher, needs cold hydrogen injection rate large, and sulphur, nitrogen, bromine index all can meet the catalytic reforming feedstock requirement.
The requirement of table 1 catalytic reforming feedstock foreign matter content
Table 2 feedstock property
Table 3 example 1-4 operational condition and product property
| Project | Example 1 | Example 2 | Example 3 | Example 4 |
| Processing condition | ||||
| The catalyst loading ratio | 50∶50 | 50∶50 | 40∶60 | 40∶60 |
| Working pressure, MPa (g) | 2.5 | 2.5 | 3.6 | 4.0 |
| The first reactor inlet temperature, ℃ | 280 | 280 | 280 | 280 |
| The first reactor outlet temperature, ℃ | 307 | 352 | 317 | 326 |
| The second reactor inlet temperature, ℃ | 307 | 352 | 308 | 315 |
| The second reactor outlet temperature, ℃ | 315 | 361 | 319 | 324 |
| Volume space velocity (LHSV), h -1 | 2.5 | 2.5 | 2.6 | 2.8 |
| Hydrogen-oil ratio (v), Nm 3/m 3 | 250 | 250 | 300 | 300 |
| Product property | ||||
| Sulphur, μ g/g | ＜0.5 | 4.3 | ＜0.5 | ＜0.5 |
| Nitrogen, μ g/g | ＜0.5 | 2 | ＜0.5 | ＜0.5 |
| H 20，μg/g | 0.5 | 1.3 | 0.8 | 0.6 |
| Bromine index, mgBr/100g | 0 | 6 | 0.2 | 0.5 |
Claims (5)
1. the method for a widening catalytic reforming feedstock is characterized in that:
(1) FCC stable gasoline and virgin naphtha are mixed, through the raw material strainer, remove by filter chip, degradation product and catalyst dust granule foreign wherein, then remove and mix the water carried in petroleum naphtha through coalescer; The FCC stable gasoline is initial boiling point～170 ℃, and virgin naphtha is initial boiling point～180 ℃; The FCC stable gasoline is 50:50～70:30 with the mixed weight ratio of virgin naphtha;
(2) mix petroleum naphtha and enter hydrogenator with the hydrogen mixing after process furnace is heated to temperature of reaction and contact with hydrogenation catalyst, carry out olefin saturated, desulfurization and denitrification reaction; Hydrogenation conditions is that reaction pressure is 2.0～5.0MPa, and the reaction temperature in is 280～320 ℃, and the reaction temperature out is 280～340 ℃, and average reaction temperature is 280～310 ℃, and volume space velocity is 2～8h
-1, hydrogen-oil ratio is 90～300Nm3
/m3
;catalyzer is to take aluminum oxide as carrier, and metallic nickel and molybdenum are active ingredient, Ni2～5wt%, Mo11～14wt%;
(3) hydrogenation reaction effluent separates and obtains hydrogen-rich gas and hydrogenated gasoline after condensing cooling, and hydrogen-rich gas recycles, and hydrogenated gasoline enters evaporator tower and carries out the refining petroleum naphtha that the stripping fractionation is met the catalytic reforming feedstock requirement.
2. the method for widening catalytic reforming feedstock according to claim 1 is characterized in that: strainer adopts basket fabric, and filtering element is filter core, and filtering accuracy is less than or equal to 10 μ m, and filtration pressure is reduced to 20kPa; The coalescer coalesces element is filter element type, and the W/O decreasing ratio should be greater than 98(v) %.
3. the method for widening catalytic reforming feedstock according to claim 1, it is characterized in that: hydrogenation reaction is carried out in one or two reactor; While using two reactors, the catalyzer of the first reactor is for olefin saturated and partial desulfurization, denitrogenation, and the catalyzer of the second reactor is for desulfurization and denitrogenation; Cold hydrogen decanting point is set between two reactors, injects cold hydrogen when excessive for the bed temperature rise to reduce the bed temperature of reaction, control the reaction temperature out and be less than or equal to 340 ℃; While using a reactor, hydrogenation catalyst adopts the segmentation filling, and two intersegmentally establish cold hydrogen dish; All load catalyzer of the same race in two reactors or two sections beds, charge weitght is than being 30:70～50:50.
4. the method for widening catalytic reforming feedstock according to claim 3 is characterized in that: the first reactor head adopts the grading loading technology, loads successively from top to down the activated iron protective material of tool and nickel molybdenum Hydrobon catalyst.
5. the method for widening catalytic reforming feedstock according to claim 1, it is characterized in that: step (3) hydrogenated gasoline stripping adopts single tower flow process, and stripping tower and separation column are united two into one, and adopts the reboiler furnace heating at the bottom of tower.
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| CN104232151B (en) * | 2013-06-20 | 2016-01-13 | 中国石油化工股份有限公司 | A kind of Benzin naphtha catalytic reforming method |
| CN106770891A (en) * | 2016-12-30 | 2017-05-31 | 神华集团有限责任公司 | Catalyst test apparatus and evaluation method |
| CN108795486B (en) * | 2017-05-04 | 2023-08-01 | 中国石油化工股份有限公司 | Coupling system of reforming generated oil liquid phase hydrogenation device and light component removing tower |
| CN107177370B (en) * | 2017-06-02 | 2018-10-02 | 钦州学院 | A method of being used for FCC gasoline removal of mercaptans |
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