CN105647581B - Gasoline hydrogenation method - Google Patents
Gasoline hydrogenation method Download PDFInfo
- Publication number
- CN105647581B CN105647581B CN201410645062.8A CN201410645062A CN105647581B CN 105647581 B CN105647581 B CN 105647581B CN 201410645062 A CN201410645062 A CN 201410645062A CN 105647581 B CN105647581 B CN 105647581B
- Authority
- CN
- China
- Prior art keywords
- gasoline
- reaction
- stabilizer
- heat exchange
- octane value
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The present invention provides a kind of gasoline hydrogenation method.The gasoline hydrogenation method comprises the following steps：Full cut catalytic gasoline (1) enters pre-hydrogenator (9), and reaction product enters fractionating column (10) and carries out light, heavy distillat gasoline segmentation；Fractionator Bottom heavy distillat gasoline enters hydrodesulphurisatioreactors reactors (14) after heat exchange, and reaction product is fed after heating furnace (16) is heated through octane value recovering reaction feed heat exchanger (15) heat exchange and octane value recovering enters octane value recovering reactor (17)；Octane value recovering reactor (17) outlet reaction product enters stabilizer reboiler (25), then enters hot knock-out pot (18) after octane value recovering feed exchanger (15) and hydrodesulfurization feed exchanger (13) heat exchange successively；Hot knock-out pot bottom liquid phase removes stabilizer (24), and tank deck gas phase enters cold knockout drum (20) after heat exchange, cooling, and cold separation tank bottom liquid phase enters stabilizer (24) after heat exchange.
Description
Technical field
The present invention relates to a kind of gasoline hydrogenation method.
Background technology
To improve air quality, the ability of automobile tail gas purification system is further improved, Exhaust emission is reduced,
In December, 2013, China issues and comes into effect the 5th stage motor petrol national standard (GB17930-2013), and the transitional period is extremely
Supply country V standards motor petrol in China from the end of the year 2017,1 day January in 2018, it is desirable to which sulfur content is not more than 10ppm.
Catalytic gasoline accounts for more than the 70% of gasoline concoction pond, therefore reduction as the main blending component of China's clean vehicle gasoline
Sulfur content in catalytic gasoline is the key for producing super low-sulfur oil.Gasoline hydrogenation is that one kind uses bed technology to urging
Change cracking gasoline and carry out hydrotreating so that the method that its sulfur content meets national motor petrol discharge standard, because of its operating condition
The advantages of mitigation, high desulfurization degree, hydrogen consumption low and small loss of octane number, it is widely used in major oil plants.The technique is generally adopted
With the technological process of full distillation gasoline pre-hydrotreating-light and heavy fractions gasoline segmentation-heavy distillat gasoline hydrodesulfurizationmethod, reaction product
Enter knockout drum after reaction feed heat exchange, after being cooled down through air cooling and carry out gas-liquid separation, separation tank bottom liquid is again after heat exchange heating
Hydrogen sulfide and lighter hydrocarbons are removed into stabilizer, the treated gasoline product for meeting and requiring is finally given.Such a technological process, it is most of
Heat of reaction can not be fully utilized, and cooled away by reaction product air cooler, cause energy loss.While liquid-phase reaction product
Repeatedly through cooling, enter stabilizer after heat exchange heating, add the exergy destruction in heat transfer process, cause energy loss, lead
Cause the energy consumption increase that gasoline hydrogenation device is unnecessary so that gasoline hydrogenation plant energy consumption is universal higher.Energy-saving and emission-reduction, raising
ERM utilization rate, reduction energy consumption, reduce pollution be enterprise existence this, realize the maximized key of enterprise profit.
Further, since China's catalytic gasoline olefin(e) centent is high, generally higher than 40v%, using gasoline hydrofinishing technology hydrodesulfurization
Meanwhile, a large amount of alkene are hydrogenated saturation, cause loss of octane number to increase.Therefore, it is necessary to which developing a kind of country that is adapted to is catalyzed vapour
Oil production sulfur content is less than 10ppm super-low sulfur clean gasoline, and can effectively reduce energy consumption, and what is recovered energy to greatest extent is new
Technology.
CN 102167985B provide a kind of hydro-upgrading method for ungraded gasoline, the characteristics of for China's catalytic gasoline, adopt
With selective hydrodesulfurization, Olefin decrease, the method for modifying for recovering octane number, two sections, two device flows, gasoline is without weight point
From full cut directly carries out hydro-upgrading.Sulphur and alkene can be greatly reduced in this method, and loss of octane number is small, but gasoline products
Sulfur content is only capable of meeting state IV motor petrol standards.
CN 102010751A relate to a kind of combination production method of ultra-low sulfur and high-octane number gasoline, full distillation gasoline
First be oriented sulphur transfer, then carry out weight segmentation, heavy distillat gasoline carries out hydrodesulfurization and isomery, aromatisation, then with gently
Gasoline products are obtained after distillation gasoline mixing.This method can produce the gasoline products that sulfur content is less than 10ppm, but reaction condition
Harshness, reaction product only exchanges heat with untreated heavy distillat gasoline, and heat exchange process is unreasonable, and high-temperature position heat energy can not be fully sharp
With heat utilization ratio is low.
CN 103059957A disclose a kind of Low-energy consumption catalytic gasoline hydrodesulfurizationmethod method, by taking adjustment catalysis to split
Fractionating column operation is put in makeup, and former full cut catalytic gasoline is extracted out and is adjusted to extract light fraction gasoline and middle gasoline out, and increases weight
Distillation gasoline extracts line out, and light fraction gasoline and middle gasoline, which face, is divided into light, middle gasoline after hydrogen removal of mercaptans, then middle gasoline and double distilled
Hydrodesulfurization is carried out after dividing gasoline mixing.The method can meet gasoline product quality the quality requirement that sulfur content is less than 10ppm,
And energy consumption is relatively low.It is not truly but the method is transferred to catalytic unit equivalent to by the energy consumption of gasoline hydrogenation device
Low power technology.
CN 103059946A disclose a kind of Low-energy consumption catalytic gasoline hydrodesulfurizationmethod method, the method with
CN103059957A almost all fours, simply in gasoline and heavy distillat gasoline carried out hydrodesulfurization respectively.
The content of the invention
Goal of the invention
It is an object of the invention to provide a kind of gasoline hydrogenation method, catalytic gasoline product sulfur content can be greatly reduced,
And loss of octane number is small, and energy consumption can be effectively reduced, recovered energy to greatest extent.
Summary of the invention
The gasoline hydrogenation method comprises the following steps：
Full cut catalytic gasoline enters pre- after pre- hydrogenation feed exchanger and pre- hydrogenation feed preheater heat exchange and heating
Hydrogenation reactor, reaction product enters fractionating column and carries out light, heavy distillat gasoline segmentation, and fractionation cut point is 50~70 DEG C；
Enter hydrodesulphurisatioreactors reactors, reaction production after the hydrogenated desulphurised feed heat exchanger heat exchange of Fractionator Bottom heavy distillat gasoline
It is anti-that thing enters octane value recovering after the heat exchange of octane value recovering reaction feed heat exchanger and octane value recovering charging heating stove heat
Answer device；
Octane value recovering reactor outlet reaction product enters stabilizer reboiler, and thermal source, Ran Houyi are provided for stabilizer
It is secondary to enter hot knock-out pot at 175~215 DEG C after octane value recovering feed exchanger and the heat exchange of hydrodesulfurization feed exchanger
Hot gas-liquid separation；
Hot knock-out pot bottom liquid phase goes stabilizer to carry out product stabilization, and tank deck gas phase warp is hydrogenated with feed exchanger heat exchange in advance, then
Enter the cold gas-liquid separation at 40~55 DEG C of cold knockout drum after cooling, cold separation tank bottom liquid phase is changed through stabilizer feed exchanger
Enter stabilizer after heat and carry out product stabilization；Stabilizer bottom gasoline, which exchanges heat through stabilizer feed exchanger and is used as after cooling, to be added
Hydrogen heavy distillat gasoline products.
By the control for being fractionated cut point, it can be ensured that gained light fraction mercaptan from gasoline and total sulfur content no more than
10ppm, meets state V gasoline standard requirements, such light fraction gasoline can directly with it is refined after hydrodesulfurization and octane value recovering
Heavy distillat gasoline is mixed, and obtains super-low sulfur clean gasoline product, also can be directly as ether-based device raw material.Settable light fraction vapour
Oily online sulphur content analyzer, on-line analysis light fraction mercaptan from gasoline and total sulfur content, convenient and swift regulation and control light fraction gasoline are cut
Cutpoint and quality.
Preferably, pre-hydrotreating reaction use Ni-Mo catalyst, it is ensured that removing feedstock oil in alkadienes and
Colloid, extends the downstream reaction operation cycle, and ensures light fraction mercaptan from gasoline and total sulfur no more than 10ppm, meets state's V vapour
Oil ga(u)ge alignment request.Operation condition is：2~2.4MPa of reaction pressure, 95~190 DEG C of reaction temperature, reaction velocity 2.5~
4.0h-1, hydrogen-oil ratio 3~6.
Preferably, hydrodesulfurization reaction uses Co -- Mo catalyst, for removing in heavy distillat gasoline larger point
The sulfide of son.Operation condition is：1.9~2.1MPa of reaction pressure, 185~260 DEG C of reaction temperature, reaction velocity 3~
6h-1, hydrogen-oil ratio 200~300；Octane value recovering reaction uses Co~Mo catalyst using molecular sieve as carrier, for heavy distillat
Removed in gasoline compared with small molecule sulfur-containing compound, it is to avoid hydrogen sulfide and alkene recombine generation mercaptan, and carry out isomerization and
Aromatization, makes up the loss of octane number caused by alkene saturation.Operation condition is：1.5~1.7MPa of reaction pressure,
250~370 DEG C of reaction temperature, 2~6h of reaction velocity-1, hydrogen-oil ratio 200~300.
Reaction temperature of the present invention is reacting initial temperature, i.e., each elementary reaction material enters entering for respective reaction device
Mouth temperature.Because the pre-hydrotreating reaction, hydrodesulfurization reaction, octane value recovering reaction are exothermic reaction, reactor outlet
Temperature can be slightly above inlet temperature.The difference of reactor outlet temperature and inlet temperature is referred to as temperature rise.For example, in above-mentioned preferred scheme
In, the reaction temperature of pre-hydrotreating reaction is 95~190 DEG C, and temperature rise is 2~10 DEG C, pre-hydrogenator outlet temperature is 97~
200℃；The reaction temperature of hydrodesulfurization reaction is 185~260 DEG C, and temperature rise is 5~20 DEG C, the outlet temperature of hydrodesulphurisatioreactors reactors
Spend for 190~280 DEG C；The reaction temperature of octane value recovering reaction is 250~370 DEG C, and temperature rise is 20~30 DEG C, octane value recovering
The outlet temperature of reactor is 270~400 DEG C.The change of reaction temperature and temperature rise is main by reaction raw materials composition and catalyst performance
The influence of energy, for example, with the degeneration of catalyst performance, reaction temperature needs to improve, and this is ripe for those skilled in the art
Know.
Preferably, hot knock-out pot bottom liquid phase and cold separation tank bottom liquid phase respectively enter stabilizer different feeds position
Put, reduce sub-thread charging cooling caused by cold and hot material is remixed, heating up repeats, and reduces energy loss (tradition
Flow only sets a cold knockout drum, and one material of tank bottom liquid enters stabilizer after heat exchange, therefore stabilizer only one of which is entered
Discharge position).
Preferably, the hot gas liquid separation temperature is 180~190 DEG C.So-called hot gas-liquid separation refers to after heat exchange
Reaction product directly carry out gas-liquid two-phase separation without further cooling, improve the utilization of heat to economize on resources.Application
People it has been investigated that, hot gas liquid separation temperature involved in the present invention can not be too high, too it is high can cause it is pre- hydrogenation charging coking (hot gas
Liquid separation temperature should control to be no more than 215 DEG C, to prevent from heating diene polymerization coking therein when pre- hydrogenation is fed), and dodge
Steaming liquid phasor is few, and gas phase carries heat surplus, increase cooling load, unfavorable energy-conservation；Hot gas liquid separation temperature can not be too low, too
Low flashed vapour phasor is few, it is impossible to pre- hydrogenation charging is heated to high enough temp, can increase the amount of extraneous input heating medium, no
Beneficial to energy-conservation.Calculated through applicant's repetition test, effect is ideal when hot gas liquid separation temperature is 180~190 DEG C, both will not
The material of reaction system is adversely affected, good energy-saving effect can be reached again.
Preferably, cold separation head space gas mutually remove after hydrogen sulfide recycled as recycle hydrogen it is anti-in hydrodesulfurization
Should.Recycle hydrogen sets the hydrogen sulfide in depriving hydrogen sulphide facility, removing recycle hydrogen, prevents hydrogen sulfide and the alkene in heavy distillat gasoline
Restructuring generation sulfide, improves hydrodesulfurization reaction selectivity, reduction reaction severity.
The present invention uses two sections of combined hydrogenation technologies of pre- hydrogenation, hydrodesulfurization and octane value recovering, and full distillation gasoline enters
Di-olefins are monoolefine, reduce downstream hydrogenation desulphurization reaction system coking, it is ensured that device long period by row pre-hydrotreating reaction
Operation, while also carry out the small molecule trechmannite compounds such as mercaptan tautomerizes to active monoene to heavy sulfide transfer and nonactive monoolefine
Hydrocarbon etc. reacts；Hydrodesulfurization and octane value recovering reaction, then carry out desulfurization, aromatisation and isomerization reaction, be conducive to depth to take off
Sulphur and reduction loss of octane number.The pre-hydrotreating reaction, hydrodesulfurization reaction and octane value recovering reaction are prior art, institute
The material for being common used to the reaction is also known in the art with catalyst, those skilled in the art can select excellent according to actual conditions
The catalyst and reaction condition of choosing.
Octane value recovering reaction product heat is utilized step by step from high temperature to low temperature.Reaction product is to stablize tower weight first
Boil device and thermal source is provided, it is to avoid the energy input of outside thermal medium, reduce energy expenditure；Again, preheating octane number is carried out extensive
Multiple reaction feed, reduces the thermic load of octane value recovering reaction feed heating furnace, reduces fuel consumption；Then it is anti-with hydrodesulfurization
It should feed and be exchanged heat, charging is met the reaction temperature requirement of hydrodesulphurisatioreactors reactors；Finally utilize the gas of thermal release tank deck
Heat phase pre-hydrotreating reaction is fed, and realizes that heat is utilized step by step.The liquid phase at hot knock-out pot bottom directly enters stabilizer simultaneously, reduces anti-
Answer liquid product cooling, heating repeat, reduce energy loss.
Compared with prior art, the present invention has advantages below：
1. sulfur content no more than 2000ppm can be handled, olefin(e) centent is not more than 45v% catalytic gasoline inferior, produces sulphur
Content is less than 10ppm state's V gasoline components, and product liquid yield is not less than 99wt% and loss of octane number is small.
2. fractionating column light and heavy fractions gasoline cut point can be regulated and controled online and light according to feedstock property and sulfur content characteristic distributions
Distillation gasoline quality.
3. it is extensive to pre- hydrogenation, hydrodesulfurization and octane number on the premise of the sulfur content and octane number of gasoline products is ensured
The condition reacted again optimizes matching, to reduce energy consumption.
4. hydrodesulfurization reaction product heat is utilized step by step from high temperature to low temperature.Reaction product is to stablize tower weight first
Boil device and thermal source is provided, it is to avoid the energy input of outside thermal medium, reduce energy expenditure；Again, preheating octane number is carried out extensive
Multiple reaction feed, reduction octane value recovering feeds the thermic load of heating furnace, reduces fuel consumption；Then enter with hydrodesulfurization reaction
Material is exchanged heat, and charging is met the reaction temperature requirement of hydrodesulphurisatioreactors reactors；Finally added using the gas phase of thermal release tank deck
Hot pre-hydrotreating reaction charging, realizes that heat is utilized step by step.
5. compared with conventional catalyst gasoline hydrogenation device, unique distinction of the invention is to set that reaction product is hot, cold separation
Tank, octane value recovering reaction product first carries out hot gas, liquid separation, and hot knock-out pot top gas is mutually used to heat pre-hydrotreating reaction charging,
Enter gas-liquid separation in cold knockout drum after air cooling cooling again, cold separation head space gas is mutually that recycle hydrogen is used through desulfurization Posterior circle, cold
Separation tank bottom liquid phase after the heat exchange of stabilizer base oil with entering stabilizer；Hot knock-out pot bottom liquid phase directly enters stabilizer.Reduce anti-
Answer liquid product cooling, heating repeat, reduce energy loss.Hot knock-out pot is vertical vessel, charging aperture and canister
Wall is tangential, the gas phase flashed off is increased in tank inside spin, centrifugal action is produced, under the positive action of centrifugal force, in gas
The drop of carrying is thrown toward container inner wall, and is settled down to tank bottom along container inner wall progress by self gravitation.With traditional knockout drum
Compare, liquid separative efficiency is higher, required container casing is smaller, save equipment investment.
6. compared with conventional catalyst gasoline hydrogenation device, plant energy consumption can reduce by 4~7 kgoe/t chargings.
Brief description of the drawings
Fig. 1 is low energy consumption gasoline hydrogenation device technique schematic flow sheet of the present invention.
Wherein：1 is catalytic gasoline charging, 2 supplement fresh hydrogens (hereinafter referred to as new hydrogen), and 3 be charge filter, 4 be into
Expect that surge tank, 5 are pre- hydrogenation feed pump, 6 be make-up hydrogen compressor, and 7 be pre- hydrogenation feed exchanger, and 8 be pre- hydrogenation feeding preheating
Device, 9 be pre-hydrogenator, and 10 be fractionating column, and 11 be fractionating column reboiler furnace, and 12 be hydrodesulfurization feed pump, and 13 is de- for hydrogenation
Sulphur feed exchanger, 14 be hydrodesulphurisatioreactors reactors, and 15 be octane value recovering feed exchanger, and 16 be that octane value recovering charging adds
Hot stove, 17 be octane value recovering reactor, and 18 be reaction product hot knock-out pot, and 19 be reaction product air cooler, and 20 be reaction production
The cold knockout drum of thing, 21 be desulphurization of recycle hydrogen system, and 22 be circulating hydrogen compressor, and 23 be stabilizer feed exchanger, and 24 be stable
Tower, 25 be stabilizer reboiler, and 26 be gasoline products air cooler, and 27 be gasoline products water cooler, and 28 be note vulcanizing agent facility, 29
It is hydrogenation heavy distillat gasoline products for note corrosion inhibiter facility, 30,31 be light fraction gasoline products.
Embodiment
The inventive method will be described in detail for the following examples, but the present invention and should not be limited by the examples.
The technological process of example 1 below~3 is described with reference to the drawings：
As shown in figure 1, full cut catalytic gasoline 1 is filtered through charge filter 3, into feed surge tank 4, through it is pre- be hydrogenated with into
Material pump 5 is mixed with coming from the new hydrogen 2 of make-up hydrogen compressor 6, is changed through pre- hydrogenation feed exchanger 7 and pre- hydrogenation feed preheater 8
Heat and it is heated to after suitable reaction temperature enter pre-hydrogenator 9, progresss di-olefins are the trechmannite such as monoolefine, mercaptan
Compound is converted into the reaction of heavy sulfide.New hydrogen is supplemented to be pressurized through make-up hydrogen compressor 6.Reaction product is carried out into fractionating column 10
Gently, heavy distillat gasoline is split, and mercaptan and total sulfur content meet state V gasoline standard requirements in light fraction gasoline 31, can be directly as
Gasoline blending component, also can remove deep hydrodesulfurizationof, fractionating column directly as ether-based device raw material carrying device, heavy distillat gasoline
10 are heated by fractionating column reboiler furnace 11.The hydrogenated desulphurised feed pump 12 of Fractionator Bottom heavy distillat gasoline is mixed with recycle hydrogen,
Hydrogenated desulphurised feed heat exchanger 13 exchanges heat to after reaction temperature and carries out hydrodesulfurization and part into hydrodesulphurisatioreactors reactors 14
Olefin saturation, reaction product is heated through the heat exchange of octane value recovering feed exchanger 15 and octane value recovering charging heating furnace 16
Enter octane value recovering reactor 17 after to reaction temperature, carry out removal of mercaptans, aromatisation and isomerization reaction, realization meets product
Less loss of octane number is kept while desulfurization requirement.The outlet of octane number reactor 17 reaction product enters stabilizer reboiler
25, it is that stabilizer 24 provides thermal source, then successively through octane value recovering feed exchanger 15 and hydrodesulfurization feed exchanger 13
Enter the hot gas-liquid separation of reaction product hot knock-out pot 18 after heat exchange.Hot knock-out pot bottom liquid phase removes stabilizer 24, and tank deck gas phase is through pre-
Hydrogenation feed exchanger 7, which exchanges heat again after the reacted condensation of product air cooler 19 is cooled down, enters the cold knockout drum 20 of reaction product, cold point
It is to be mixed after recycle hydrogen removes hydrogen sulfide through desulphurization of recycle hydrogen system 21 with the new hydrogen 2 of supplement and through circulation from tank deck gas phase
The compression boosting Posterior circle of hydrogen compressor 22 is used.Cold separation tank bottom liquid phase enters stable after being exchanged heat through stabilizer feed exchanger 23
It is stable that tower 24 carries out product.Conduct after bottom of towe gasoline exchanges heat and cooled down through gasoline products air cooler 26 and gasoline products water cooler 27
Hydrogenation heavy distillat gasoline products 30 deliver to storage tank.Device sets note vulcanizing agent facility 28, and the catalyst that initially gone into operation for device is pre-
Vulcanization.Note corrosion inhibiter facility 29 is set on the top of stabilizer 24, to reduce equipment corrosion.
Embodiment 1
Using catalytic gasoline A as raw material, its property such as table 1.Catalyst is commercial goods, and composition is shown in Table 2.Being fractionated cut point is
70℃.Operating condition is shown in Table 3, and product property is shown in Table 4, and plant energy consumption is shown in Table 5.Production can be made using the technology as can be seen from Table 4
Sulfur content is less than 10ppm in product, and 1.0 units of loss of octane number are found out by table 5, and plant energy consumption feeds for 15.76kgoe/t,
Than 1 low 5.99 unit of comparative example, than 2 low 3.84 units of comparative example.
Embodiment 2
Using catalytic gasoline B as raw material, its property such as table 1.Catalyst is commercial goods, and composition is shown in Table 2.Being fractionated cut point is
65℃.Operating condition is shown in Table 3, and product property is shown in Table 4, and plant energy consumption is shown in Table 5.Production can be made using the technology as can be seen from Table 4
Sulfur content is less than 10ppm in product, and 0.5 unit of loss of octane number is found out by table 5, and plant energy consumption feeds for 14.95kgoe/t,
Than 1 low 6.8 unit of comparative example, than 2 low 4.65 units of comparative example.
Embodiment 3
Using catalytic gasoline C as raw material, its property such as table 1.Catalyst is commercial goods, and composition is shown in Table 2.Being fractionated cut point is
60℃.Operating condition is shown in Table 3, and product property is shown in Table 4, and plant energy consumption is shown in Table 5.Production can be made using the technology as can be seen from Table 4
Sulfur content is less than 10ppm in product, and 1.2 units of loss of octane number are found out by table 5, and plant energy consumption feeds for 15.32kgoe/t,
Than 1 low 6.43 unit of comparative example, than 2 low 4.28 units of comparative example.
Comparative example 1
Using catalytic gasoline A as raw material, pre- hydrogenation dialkene removal first is carried out to raw material and sulphur is shifted, is then entered in fractionating column
Row light and heavy fractions are cut, and cut point is 70 DEG C, after heavy distillat gasoline is mixed with recycle hydrogen, are exchanged heat with octane value recovering reaction product
Enter hydrodesulphurisatioreactors reactors after to 240 DEG C and carry out desulphurization reaction, reaction product is heated through octane value recovering reaction heating furnace again
Progress removal of mercaptans, isomerization and aromatisation are contacted with octane value recovering catalyst into octane value recovering reactor after to 340 DEG C
Reaction, octane value recovering reaction product is cooled down through air cooling again with hydrodesulfurization reaction charging, pre-hydrotreating reaction charging heat exchange successively
Enter the progress gas-liquid separation of reaction product knockout drum afterwards, liquid is stable with entering stabilizer after the heat exchange of stabilizer base oil, after stabilization
Heavy distillat gasoline and light fraction gasoline be mixed to get gasoline products.Catalyst is commercial goods, and composition is shown in Table 2.Operating condition
3 are shown in Table, product property is shown in Table 4, and plant energy consumption is shown in Table 5.Can be less than sulfur content in product using the technology as can be seen from Table 4
10ppm, 1.5 units of loss of octane number, is found out by table 5, and plant energy consumption feeds for 21.75kgoe/t, higher than embodiment about 6-7
Individual unit.
Comparative example 2
Using catalytic gasoline A as raw material, pre- hydrogenation dialkene removal first is carried out to raw material and sulphur is shifted, is then entered in fractionating column
Row light and heavy fractions cut, cut point be 70 DEG C, after heavy distillat gasoline is mixed with recycle hydrogen, with hydrodesulfurization reaction product exchange heat to
Enter hydrodesulphurisatioreactors reactors after 240 DEG C and carry out desulphurization reaction, the heated stove heat of reaction product is to entering stabilizer after 355 DEG C
Reboiler exchanges heat to entering hydrogenation post processing reactor after 330 DEG C and carries out sweetening reaction, and hydrogenation post processing reaction product is successively
Enter reaction product knockout drum after being cooled down again through air cooling with hydrodesulfurization reaction charging, pre-hydrotreating reaction charging heat exchange and carry out gas-liquid
Separation, liquid is stable with entering stabilizer after the heat exchange of stabilizer base oil, and stable gasoline is mixed to get gasoline production with light fraction gasoline
Product heavy distillat gasoline.Catalyst is commercial goods, and composition is shown in Table 2.Operating condition is shown in Table 3, and product property is shown in Table 4, plant energy consumption
It is shown in Table 5.Using the technology sulfur content can be made to be less than 10ppm in product as can be seen from Table 4,1.2 units of loss of octane number, by
Table 5 finds out that plant energy consumption feeds for 19.6kgoe/t, higher than about 4-5 unit of embodiment.
The feedstock property of table 1
| Project | Catalytic gasoline A | Catalytic gasoline B | Catalytic gasoline C |
| Proportion | 0.731 | 0.725 | 0.71 |
| Boiling range, DEG C | 37~185 | 36~202 | 40~205 |
| Sulfur content, ppm | 400 | 200 | 624 |
| Alkene, v% | 45 | 29 | 39.9 |
| Octane number (RON) | 89.7 | 90 | 90.8 |
The catalyst of table 2 constitutes wt%
The operating condition of table 3
The product property of table 4
The device of table 5 is consumed
Claims (7)
1. gasoline hydrogenation method, it is characterised in that comprise the following steps：
Full cut catalytic gasoline (1) is through pre- hydrogenation feed exchanger (7) and pre- hydrogenation feed preheater (8) heat exchange and heats laggard
Enter pre-hydrogenator (9), reaction product enters fractionating column (10) and carries out light, heavy distillat gasoline segmentation, and fractionation cut point is 50
~70 DEG C；
Enter hydrodesulphurisatioreactors reactors (14) after hydrogenated desulphurised feed heat exchanger (13) heat exchange of Fractionator Bottom heavy distillat gasoline, instead
Product is answered to enter after feeding heating furnace (16) heating through octane value recovering reaction feed heat exchanger (15) heat exchange and octane value recovering
Octane value recovering reactor (17)；
Octane value recovering reactor (17) outlet reaction product enters stabilizer reboiler (25), is that stabilizer (24) provides heat
Source, then enters thermal release after octane value recovering feed exchanger (15) and hydrodesulfurization feed exchanger (13) heat exchange successively
Tank (18) hot gas-liquid separation at 175~215 DEG C；
Hot knock-out pot bottom liquid phase goes stabilizer (24) to carry out product stabilization, and tank deck gas phase is hydrogenated with feed exchanger (7) heat exchange through pre-,
Enter cold knockout drum (20) cold gas-liquid separation at 40~55 DEG C after cooling again, cold separation tank bottom liquid phase is changed through stabilizer charging
Enter stabilizer (24) after hot device (23) heat exchange and carry out product stabilization；Stabilizer bottom gasoline is changed through stabilizer feed exchanger (23)
Heat is simultaneously used as hydrogenation heavy distillat gasoline products (30) after cooling.
2. gasoline hydrogenation method as claimed in claim 1, it is characterised in that pre-hydrotreating reaction is catalyzed using Ni-Mo
Agent, 2~2.4MPa of reaction pressure, 95~190 DEG C of reaction temperature, 2.5~4.0h of reaction velocity-1, hydrogen-oil ratio 3~6.
3. gasoline hydrogenation method as claimed in claim 1, it is characterised in that hydrodesulfurization reaction is catalyzed using Co-Mo
Agent, 1.9~2.1MPa of reaction pressure, 185~260 DEG C of reaction temperature, 3~6h of reaction velocity-1, hydrogen-oil ratio 200~300；Octane
Value recovers reaction and uses Co~Mo catalyst using molecular sieve as carrier, 1.5~1.7MPa of reaction pressure, and reaction temperature 250~
370 DEG C, 2~6h of reaction velocity-1, hydrogen-oil ratio 200~300.
4. gasoline hydrogenation method as claimed in claim 1, it is characterised in that hot knock-out pot bottom liquid phase and cold separation tank bottom
Liquid phase respectively enters stabilizer different pelverized coal feeder positions.
5. gasoline hydrogenation method as claimed in claim 1, it is characterised in that cold separation head space gas is mutually removed after hydrogen sulfide
Recycled as recycle hydrogen in hydrodesulfurization reaction.
6. gasoline hydrogenation method as claimed in claim 1, it is characterised in that hot gas liquid separation temperature is 180~190
℃。
7. gasoline hydrogenation method as claimed in claim 1, it is characterised in that fractionation cutting gained light fraction sulfur in gasoline
Alcohol and total sulfur content are no more than 10ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410645062.8A CN105647581B (en) | 2014-11-12 | 2014-11-12 | Gasoline hydrogenation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410645062.8A CN105647581B (en) | 2014-11-12 | 2014-11-12 | Gasoline hydrogenation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105647581A CN105647581A (en) | 2016-06-08 |
| CN105647581B true CN105647581B (en) | 2017-09-15 |
Family
ID=56478904
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410645062.8A Active CN105647581B (en) | 2014-11-12 | 2014-11-12 | Gasoline hydrogenation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105647581B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI739933B (en) | 2016-10-21 | 2021-09-21 | 大陸商中國石油化工科技開發有限公司 | Method for processing gasoline |
| CN108359495B (en) * | 2018-02-08 | 2020-04-21 | 中国石油大学(北京) | Method for modifying high-olefin catalytic cracking gasoline |
| CN108359493B (en) * | 2018-02-08 | 2020-05-26 | 中国石油大学(北京) | Method for modifying catalytic cracking gasoline |
| CN108315053B (en) * | 2018-02-08 | 2020-04-21 | 中国石油大学(北京) | Method for upgrading quality of catalytic cracking gasoline |
| CN111534327B (en) * | 2020-05-11 | 2022-02-22 | 中国石油化工股份有限公司 | Reforming pretreatment system, reforming pretreatment method and application |
| RU2753602C1 (en) * | 2021-05-17 | 2021-08-18 | Роман Николаевич Демин | Method for catalytic processing of light hydrocarbon fractions and installation for its implementation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102071058A (en) * | 2011-01-31 | 2011-05-25 | 中国石油工程建设公司 | Special selective processing method of FCC heavy gasoline |
| CN102234541A (en) * | 2010-05-07 | 2011-11-09 | 中国石油化工集团公司 | Energy-saving pyrolysis gasoline full-cut hydrogenation method and device |
| CN203451400U (en) * | 2013-08-18 | 2014-02-26 | 河南永胜能源化工集团有限公司 | Quick cyclic heating device in aromatization startup reaction system |
-
2014
- 2014-11-12 CN CN201410645062.8A patent/CN105647581B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102234541A (en) * | 2010-05-07 | 2011-11-09 | 中国石油化工集团公司 | Energy-saving pyrolysis gasoline full-cut hydrogenation method and device |
| CN102071058A (en) * | 2011-01-31 | 2011-05-25 | 中国石油工程建设公司 | Special selective processing method of FCC heavy gasoline |
| CN203451400U (en) * | 2013-08-18 | 2014-02-26 | 河南永胜能源化工集团有限公司 | Quick cyclic heating device in aromatization startup reaction system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105647581A (en) | 2016-06-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105647581B (en) | Gasoline hydrogenation method | |
| CN100371423C (en) | Hydrocarbons hydrocracking method | |
| CN104140847B (en) | A kind of F-T synthesis petroleum naphtha upgrading produces the method for stop bracket gasoline | |
| CN103864564B (en) | Technique for processing methanol-to-propylene by-products | |
| CN112322343B (en) | Method and device for producing high-aromatic-content gasoline by MTP byproduct mixed aromatic hydrocarbon modification, high-aromatic-content gasoline and application thereof | |
| CN103937527B (en) | Bio-oil hydrofining-isomerization-visbreaking prepares the method for low freezing point diesel fuel component | |
| CN210560278U (en) | Hydrocracking and hydrodesulfurization integrated unit | |
| CN102559260A (en) | Rear inferior gasoline fraction hydrotreating method for heating furnace | |
| CN204369817U (en) | A kind of gasoline hydrogenation system | |
| CN103450933A (en) | Diesel oil hydroupgrading combination method | |
| RU128612U1 (en) | ENGINE FOR FUEL FUELS | |
| CN105713647B (en) | A kind of utilization coal tar maximization prepares the method and device of carbolic oil and diesel oil | |
| CN103059955B (en) | Method for producing clean gasoline from catalytic cracking gasoline | |
| CN210560277U (en) | Hydrocracking-condensate oil hydrodesulfurization coupled system | |
| CN104531211B (en) | A kind of coal tar hydrogenating produces technique and the process matched therewith system of fuel or industrial oil | |
| CN103059949B (en) | Catalytic cracking gasoline desulfurization method | |
| CN207749076U (en) | A kind of refinery product's upgrading synergy and hydrogen recovery system | |
| CN102226102A (en) | Method for producing gasoline blended component with high octane number from refinery gas and light hydrocarbons | |
| CN112877090A (en) | Coal direct liquefaction circulating solvent and preparation method and system thereof | |
| CN103059951B (en) | Catalytic cracking and catalytic gasoline hydrogenation combined technological method | |
| CN102559259A (en) | Method for hydrotreatment of secondary processed inferior gasoline fraction | |
| CN102559258A (en) | Method for hydrotreatment of inferior gasoline fraction | |
| CN104611028A (en) | Coking full-distillate oil hydrocracking method | |
| CN204400920U (en) | A kind of coal tar hydrogenating produces the process system of fuel or industrial oil | |
| CN102559261A (en) | Dialkene-containing gasoline fraction hydrotreating method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Co-patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee after: PetroChina Co.,Ltd. Address before: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Co-patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee before: PetroChina Co.,Ltd. |
|
| CP01 | Change in the name or title of a patent holder | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190523 Address after: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Co-patentee after: CNPC EAST CHINA DESIGN INSTITUTE CO.,LTD. Patentee after: PetroChina Co.,Ltd. Address before: 100007 Oil Mansion, Oil Mansion, 9 Dongzhimen North Street, Dongcheng District, Beijing. Co-patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Patentee before: PetroChina Co.,Ltd. |
|
| TR01 | Transfer of patent right |