CN100510016C - Process for catalytic cracking of petroleum hydrocarbon - Google Patents
Process for catalytic cracking of petroleum hydrocarbon Download PDFInfo
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- CN100510016C CN100510016C CNB2005100597738A CN200510059773A CN100510016C CN 100510016 C CN100510016 C CN 100510016C CN B2005100597738 A CNB2005100597738 A CN B2005100597738A CN 200510059773 A CN200510059773 A CN 200510059773A CN 100510016 C CN100510016 C CN 100510016C
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Abstract
The catalytic cracking method for petroleum hydrocarbon comprises: injecting material with injection angle in 90-180deg into reaction to contact with catalyst and react, separating oil and catalyst to send oil into successive system and recover the catalyst. This invention can improve product distribution and performance.
Description
Technical field
The invention belongs to the catalyst cracking method of petroleum hydrocarbon under the situation that does not have hydrogen.
Background technology
In catalytic cracking process, heavy macromole petroleum hydrocarbon is the small molecules petroleum hydrocarbon by cracking.Generally, be injected in one or more reaction zones after the hydrocarbon raw material process atomizing through preheating, contact and be gasificated into oil gas with the fluidized catalyst particle flux therein, cracking reaction takes place in the oil gas molecule under the effect of catalyzer subsequently.In the reaction process, coke loses activity catalyzer at the catalyst particle surface deposition as one of reaction product gradually gradually, contain Pd/carbon catalyst after stripping oil gas in the oxygen enrichment hot environment of breeding blanket the burning-off coke, recover active, circulation turns back to reaction zone then, carries out contact reacts with hydrocarbon raw material again.Reaction product enters separation system and forms product or partial reflux to reaction zone.
Discover that the way of contact of hydrocarbon feed and fluidized catalyst particle flux is very big to the performance impact of catalytic cracking reaction in the riser reaction zone.Along with the heaviness day by day of catalytically cracked material, byproduct such as coke and dry gas productive rate increases gradually in the product.The instantaneous uniform contact of hydrocarbon feed and fluidized catalyst particle flux can reduce the side reaction in the cracking process in theory, reduces the productive rate of coke and dry gas.The instantaneous uniform contact of hydrocarbon raw material and fluidized catalyst particle flux requires on the riser cross-section of feed entrance point, and the hydrocarbon raw material whole catalyst particle streams on the cross section therewith carries out instantaneous contact.But accomplish that on instantaneous cross section therewith all the catalyzer contact is impossible in actual applications, non-instantaneous uniform contact exist in the character that has influenced reaction product to a certain extent, for example productive rate of dry gas and coke.
Traditional catalytic cracking nozzle direction flow direction general and catalyst particle stream is the Small angle angle, be generally 40 °～65 °, the motion linear speed of going up mutually that the hydrocarbon feed drop has is between 13～27m/s, and moves upward along riser tube is parallel with catalyst particle.And catalyst particle flowed before entering intake zone, and its upward speed is generally 10～15m/s.Above-mentioned velocity contrast between the two causes the speed of relative movement between the two very little, needs the regular hour thereby contact with each other, so can not accomplish instantaneous uniform contact in this case.
The abundant atomizing of hydrocarbon feed can improve the effect that contacts between hydrocarbon feed and catalyst particle.The uniform contact degree of hydrocarbon feed and catalyst particle stream depends in part on the drop size of hydrocarbon feed.When enough hour of charging drop (usually less than 100 microns), just can think approx that hydrocarbon feed has just fully been atomized before the contact catalyst particle.Fully atomizing can increase the total surface area of charging drop, thereby increases the probability that the hydro carbons drop contacts with catalyst particle, impels feed liquid to enter in the duct of catalyst pellets sub-surface simultaneously and carries out catalytic cracking reaction, thermal responses such as minimizing condensation.US3,547, thus 805 disclosed by the method that hydrocarbon raw material is atomized of mixing of water vapor with hydrocarbon raw material.US3,152,065 describe feed nozzle is made up of the sleeve pipe of the different design of a Gent, hydrocarbon raw material by the telescopic outer tube and water vapour by pipe in the telescopic, two media collided and atomizes in terminal mixing of telescopic.Similar US4, methods such as 523,987, US5,622,677, US4,578,183 and US5,318,691 or equipment adopt undergauge or Venturi effect, vortex effect, vapour-liquid two-phase to mix the atomizing that promotes hydrocarbon feed usually.This requires the hydro carbons drop to have higher speed when leaving nozzle, is not less than 30m/s usually, and is to realize by increasing feed pressure at a high speed.Generally, this needs additional pump or other equipment to provide, thereby has increased the energy consumption and the maintenance cost of catalytic cracking unit.And, just reaching fully before contact catalyst, atomizing also exists shortcoming, promptly the droplet dia owing to hydrocarbon feed diminishes, himself kinetic energy also reduces thereupon, thereby reduced the penetration power of hydrocarbon feed on riser cross-section, can not touch all catalyst particles of mobile on this cross section fully.
The movement velocity of raising catalyst particle stream also can be improved the effect that contacts between hydrocarbon feed drop and catalyst particle stream.Generally speaking by use pre-promote the medium accelerator activator in riser tube on mobile speed, impel catalyst particle stream to quicken gradually, near the even flow effect of piston flow, hydrocarbon feed can be injected on the catalyst particle equably; Simultaneously pre-lift technique is by improving the upwards flow velocity of catalyst particle, makes it keep high momentum with bump is not atomized fully and diameter is bigger hydrocarbon feed drop when the contact hydrocarbon feed.US4,479,870 have disclosed method or the equipment that the using gas medium promotes catalyzer in advance.Yet the movement velocity of catalyst particle must be limited within the specific scope of catalytic cracking process needs.Because the movement velocity of catalyst particle also has influence on the residence time of hydrocarbon raw material in riser reactor; Simultaneously, in actual applications, landing, the back mixing phenomenon of catalyst particle in riser reactor also makes catalyst particle stream be difficult to reach piston flow mobile perfect condition.
The direction that sprays into of hydrocarbon feed also has a significant impact solid-liquid contact effect.US4,717,467 have disclosed the method and apparatus that non-radial direction sprays into hydrocarbon feed.US5,554,341, US5,173,175, US3,654,140 and US5139748 disclosed method or the equipment that radially sprays into hydrocarbon feed, series of spray nozzles is disposed on the circumferential plane of riser tube tube wall, they point to the radial center of riser tube simultaneously.Such technology or equipment make hydrocarbon feed drop formation curtain on the one hand, strengthen the effect that contacts between hydrocarbon feed drop and catalyst particle stream; Can not make the bigger hydrocarbon feed drop of atomizing fully, diameter at riser tube center bump on the other hand yet, reach the effect of atomizing fully to impel it to be split into the littler drop of diameter.
The angle of feed nozzle also is to influence hydrocarbon feed to contact one of influence factor of effect with catalyst particle stream.US6,613,290 point out hydrocarbon raw material spray into angle should with axially vertically upward direction be 40 °～65 °, surpass 65 ° and may cause hydrocarbon raw material to be sprayed onto on the riser tube inwall.This angle that sprays into of hydrocarbon feed can promote that on the one hand oil gas forms the short residence time, can prevent the landing back-mixing of catalyst particle on the other hand, thereby prevent cracking reaction.Yet the flow direction that sprays into direction and fluidized catalyst particle flux of hydrocarbon raw material is identical or be Small angle disadvantageous aspect is also arranged.The speed that sprays into of hydrocarbon raw material is generally between 30m/s-120m/s, to spray into speed 30m/s is example (the vertical direction component is between the 13-23m/s), and catalyzer linear speed before the hydrocarbon feed nozzle in riser tube is generally about 10-12m/s, maximum is no more than 15m/s, and the velocity contrast between the two causes the long time of catalyzer and hydrocarbon feed parallel motion just can contact and carry out the heat transmission fully.US5,139,748 have disclosed the hydrocarbon raw material horizontal direction or have been 25 ° of method or equipment that spray into riser tube with horizontal direction; US6,042,717 and US6,627,161 have disclosed hydrocarbon raw material sprays into riser tube by some little atomizing nozzle levels by special equipment method.The level of hydrocarbon feed sprays into, and avoid hydrocarbon feed to be directly injected on the riser tube inwall as far as possible.US5,139,748 are provided with particular component allowing the hydrocarbon raw material bump at riser tube axle center place, thereby prevent that hydrocarbon feed is directly injected on the riser tube inwall.US6,042,717 and US6,627,161 have adopted the special construction small nozzle, spray into velocity level's durection component to reduce hydrocarbon feed, thereby prevent that hydrocarbon feed is directly injected on the riser tube inwall.
In sum, in order to improve the effect that contacts of petroleum hydrocarbon raw material and catalyzer, for decades, the researchist is carrying out unremitting effort aspect petroleum hydrocarbon feeding equipment and the feeding manner improving always.But up to now, petroleum hydrocarbon raw material injects the implant angle of FCC reactor, and promptly the axial angle that direction is vertically upward of feedstock direction and reactor does not appear in the newspapers as yet greater than 90 ° feeding manner.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of improved petroleum hydrocarbon catalytic cracking process, to improve contacting effect, obtaining even more ideal product and distribute and product property of petroleum hydrocarbon raw material and catalyzer.
Petroleum hydrocarbon catalytic cracking process provided by the invention is as follows: make to contact with catalyzer in petroleum hydrocarbon raw material injecting lift pipe reactor or the riser tube+fluidized-bed reactor and react under the catalytic cracking reaction condition, oil gas behind the separating reaction and catalyzer, reaction oil gas is sent into subsequent separation system, the catalyzer of reaction back carbon deposit recycles after regeneration, wherein, the central axis of the central axis of the nozzle of described petroleum hydrocarbon raw material injecting lift pipe reactor or riser tube+fluidized-bed reactor and riser reactor vertically upward the formed angle of direction be 90 °＜α＜180 °.
Compared with prior art, petroleum hydrocarbon catalytic cracking process provided by the invention has adopted the feeding manner that is different from prior art, has improved the contact effect of petroleum hydrocarbon raw material with granules of catalyst greatly.At first, according to the method for the invention, behind the hydrocarbon feed injecting reactor, the hydrocarbon feed small droplets on direction of motion, have vertically downward component and the component of tangential movement, and catalyst particle stream has the component of motion vertically upward, catalyst particle stream mainly clashes at place, reactor axle center with the hydrocarbon feed drop, thereby impels the hydrocarbon feed drop further to split into the littler drop of diameter.Simultaneously, after hydrocarbon feed drop and the catalyst particle head-on collision, make hydrocarbon feed drop division and gasification rapidly by momentum exchange and thermal exchange, thereby increased the chance that the catalyst in reactor particle contacts with hydrocarbon feed greatly.Because the head-on collision effect between hydrocarbon feed small droplets and catalyst particle, make the hydrocarbon feed small droplets split into the littler drop of diameter, thereby increased hydrocarbon feed total surface area, quickened the thermal exchange process, make the instantaneous possibility that is gasificated as of hydrocarbon feed drop.
Because employing the method for the invention can make the gasification of hydrocarbon feed instantaneous height and mix with catalyst particle, thereby realize the instantaneous uniform contact of hydrocarbon feed and catalyst particle.The improvement of this finish contact effect makes the shortening of length of mixing of catalyst in reactor and hydrocarbon feed become possibility, thereby has created condition for reduction reactor absolute altitude, compression set construction investment.
Description of drawings
Fig. 1 is the catalytic cracking reaction part-structure synoptic diagram that adopts the method for the invention.
Petroleum hydrocarbon raw material implant angle synoptic diagram after Fig. 2 amplifies.
Embodiment
In the method for the invention, the implant angle α of described petroleum hydrocarbon raw material is meant the central axis of petroleum hydrocarbon feed nozzle and the catalyst cracker central axis formed angle of direction vertically upward, sees accompanying drawing 2.For the present invention, the central axis of feed nozzle and reactor center axis normal be upward to 90 °＜α of formed angle＜180 °, preferred 110 °＜α＜160 °, further preferred 130 °＜α＜155 °.Generally speaking, feed nozzle of the present invention is fixedly connected with catalyst cracker and be connected.The present invention does not have particular restriction for the structural shape of feed nozzle and catalyst cracker, the any feed nozzle of catalytic cracking or catalytic conversion process and reactor of being applicable to all is applicable to the present invention, for example, described riser reactor can be selected this area riser reactor commonly used, reducing riser reactor etc. for use; And feed nozzle can be selected this area wikipedia type nozzle commonly used, y-type nozzle, target spray nozzle, effervescent atomizer, BWJ-I type nozzle etc. for use.The present invention does not have particular requirement for the pattern of catalytic cracking or catalytic convention design yet, the FCC apparatus of interior riser tube, outer riser tube, anti-coaxial-type again or on the said apparatus basis improved device type etc. all be suitable for the present invention.
The present invention does not have particular requirement for the position that is provided with of number that is arranged on the feed nozzle on the reactor and feed nozzle.Feed nozzle can be provided with individual layer, also multilayer can be set; And every layer can be provided with feed nozzle 2-20, preferred 4-18, and further preferred 4-16; As long as help the uniform contact of petroleum hydrocarbon raw material and catalyzer.For example, for the riser reactor that this area is used always, petroleum hydrocarbon feed nozzle of the present invention can be arranged on the position that any needs are provided with feed nozzle, promptly, can implement the single hop charging by the individual layer feed nozzle is set, also can implement sectional feeding, thereby make the operation of FCC apparatus more flexible, help the production of high value purpose product more by the multilayer feed nozzle is set.As known to persons of ordinary skill in the art, can 1-8 layer feed nozzle be set on riser reactor, preferred 1-4 layer, further preferred 1-3 layer according to the characteristics of catalytic cracking unit raw material and the requirement of purpose product; When every layer of feed nozzle that is provided with more than 2 or 2, the central axis of each feed nozzle preferably equates with the formed angle of the central axis of riser reactor, so that the central axis of feed nozzle is converged to a bit on the central axis of riser reactor.
In the method for the invention, petroleum hydrocarbon raw material for example, injects in the catalyst cracker after being preheated to 150-280 ℃ preferably after preheating, contacts, reacts with catalyzer.Described catalytic cracking reaction condition is including, but not limited to following processing parameter: temperature of reaction 460-580 ℃, preferred 480-550 ℃; Reaction pressure (absolute pressure) 0.1-0.6MPa, preferred 0.2-0.4MPa; Agent-oil ratio 3-20, preferred 4-15; Finish duration of contact is 0.5-20 second, preferred 1.0-10 second; Preferred 650-700 ℃; The heavy % (accounting for raw material) of atomizing steam 1-15, the heavy % of preferred 2-10.
The catalyzer that the present invention uses can be any catalyzer that is applicable to catalytic cracking process, its active ingredient can be selected from: contain or do not contain Y type or HY type zeolite, the ultrastable Y that contains or do not contain rare earth and/or phosphorus, the ZSM-5 series zeolite of rare earth and/or phosphorus or have in the supersiliceous zeolite, β zeolite, ferrierite of five-membered ring structure a kind of, two or three, also can be the amorphous silicon aluminium catalyzer.
Petroleum hydrocarbon raw material of the present invention can be selected from: the mixture of one or more in time processing gasoline fraction, secondary processing of gasoline cut, time processing diesel oil distillate, secondary processing diesel oil cut, straight-run gas oil, wax tailings, deasphalted oil, hydrofined oil, hydrocracking tail oil, decompressed wax oil, vacuum residuum, long residuum or the crude oil; Preferably: the mixture of one or more in straight-run gas oil, wax tailings, deasphalted oil, hydrofined oil, hydrocracking tail oil, decompressed wax oil, vacuum residuum, the long residuum.
In the method for the invention, reacted oil gas separates through gas-solid separation equipment with mixture of catalysts, wherein, reaction oil gas is delivered to subsequent separation system and further is separated into products such as gasoline, diesel oil, liquefied gas, and the catalyzer of reaction back carbon deposit is delivered to stripper, at the stripping medium, under the effect as stripped vapor, the hydro carbons oil gas of being carried secretly is stripped as much as possible, deliver to the revivifier coke burning regeneration then, the catalyzer Returning reactor after the regeneration recycles.
Further specify method provided by the present invention below in conjunction with accompanying drawing, but therefore the present invention is not subjected to any restriction.
As shown in Figure 1, the catalyzer after the regeneration is circulated to the pre lift zone 6 of riser reactor 7 bottoms through regeneration pipeline 9, promotes medium 3 in advance and sprays into the riser tube pre lift zone 6 from nozzle 5, drives catalyst particle and quickens to move upward.2-20 feed nozzle that is symmetrically distributed along the riser tube even tube wall is set on the top of pre lift zone, the angle α of the central axis of feed nozzle and the central axis of riser reactor〉90 ° and＜180 °, and the central axis of feed nozzle crosses to the riser tube central axis.Hydrocarbon feed 2 and atomizing steam 1 are injected in the riser tube by feed nozzle 4 after pressurizeing.Hydrocarbon raw material after the abundant atomizing of quilt clashes into, mixes with the mobile catalyst particle that makes progress under the effect of pre-lifting medium, generate gasiform reaction oil gas and mixture of catalysts stream, and continuation moves upward along riser tube.Catalytic cracking reaction under the effect of catalyzer, takes place in reaction oil gas in the process that moves upward along riser tube 7, coke produces and gradually at the catalyst particle surface deposition simultaneously.Oil gas and catalyst motion to riser tube 7 tops after sparger 13 enters reactor settling vessel 19.In settling vessel 19, oil gas and catalyst particle are by the centrifugation of primary cyclone 15 and secondary cyclone 16, and oil gas enters into collection chamber 17 and enters into follow-up separation system by transfer line 18; Catalyst particle is delivered to the stripper 11 that is arranged in settling vessel 19 bottoms from cyclone dip-leg 14 under the centrifugation of a series of cyclonic separators.Stripped vapor 8 enters into stripper through the sparger 10 of stripper 11 bottoms, and through the catalyst particle contact that chevron shaped baffle plate 12 upwards flows and flows downward together, the oil gas that catalyst particle is entrained strips.Enter in the regeneration system rapidly from inclined tube 20 to be generated through steam stripped catalyst particle, coke burning regeneration under the effect of oxygen-containing gas, the catalyzer Returning reactor after the regeneration recycles.
Fig. 2 is the petroleum hydrocarbon raw material implant angle synoptic diagram after amplifying.As can be seen from Figure, the central axis of feed nozzle 25 is α with the angle of the central axis 23 of riser reactor, α〉90 ° and＜180 °.The central axis of feed nozzle crosses to the riser tube central axis.
The following examples will give further instruction to petroleum hydrocarbon feeding equipment provided by the invention, but not thereby limiting the invention.
Embodiment 1
Present embodiment explanation: the implementation result that adopts method provided by the present invention.
On catalytic cracking middle-scale device as shown in Figure 1, test.Main testing sequence is as follows: promote steam in advance and inject from the bottom of riser reactor, raw material A (its character is as shown in table 1) is in nozzle 4 injecting lift pipe reactors.The central axis of nozzle 4 and the formed angle of the central axis of riser reactor are 135 °.Stock oil with regeneration after catalyzer MLC-500 (its character is as shown in table 2) contact, react, the oil gas of generation and reacted catalyzer upwards enter settling vessel; Separating reaction oil gas and reacted catalyzer, reaction oil gas is sent into subsequent separation system, further is separated into various products; And reacted catalyzer is sent into the revivifier coke burning regeneration behind stripping; Catalyzer after the regeneration returns riser reactor and recycles.
Comparative Examples 1
For implementation result of the present invention is described, in Comparative Examples 1, adopt stock oil identical and catalyzer and identical reaction conditions to compare test with embodiment 1.The angle of the central axis of the hydrocarbon oil feed nozzle that this simultaneous test adopted and the central axis of riser reactor is 45 °.Main operational condition and test-results see Table 3.As can be seen from Table 3, behind employing the present invention, the productive rate of light naphthar, liquefied gas is greatly improved than Comparative Examples 1, has increased by 3.9 heavy % and 1.2 heavy % respectively, and heavy oil has reduced by 1.9 heavy %.
Present embodiment explanation: the implementation result that adopts method provided by the present invention.
On catalytic cracking middle-scale device as shown in Figure 1, test.Main testing sequence is as follows: promote steam in advance and inject from the bottom of riser reactor, raw material A (its character is as shown in table 1) is in nozzle 4 injecting lift pipe reactors.The central axis of nozzle 4 and the formed angle of the central axis of riser reactor are 155 °.Stock oil with regeneration after catalyzer MLC-500 (its character is as shown in table 2) contact, react, the oil gas of generation and reacted catalyzer upwards enter settling vessel; Separating reaction oil gas and reacted catalyzer, reaction oil gas is sent into subsequent separation system, further is separated into various products; And reacted catalyzer is sent into the revivifier coke burning regeneration behind stripping; Catalyzer after the regeneration returns riser reactor and recycles.
Comparative Examples 2
Adopt US6,613,290 described methods, and utilize petroleum hydrocarbon raw material described in the embodiment 1 and catalyzer to test resulting result.Main operational condition and product distribution situation are referring to table 4.As can be seen from Table 4, the productivity ratio US6 of light naphthar of the present invention and liquefied gas, 613,290 described methods are greatly improved, and have increased by 3.8 heavy % and 1.0 heavy % respectively, and heavy oil has reduced by 2.52 heavy %.Therefore, the economic benefit that the present invention brought will be very significant.
Table 1
| The stock oil title | A |
| Density, g/cm 3 | 0.8764 |
| Kinematic viscosity, mm 2/s80℃ | 20.39 |
| 100℃ | 12.06 |
| Condensation point, ℃ | >50 |
| Elementary composition, heavy % | |
| C | 86.70 |
| H | 13.48 |
| S | 0.13 |
| N | 0.13 |
| Group composition, heavy % | |
| Stable hydrocarbon | 75.0 |
| Aromatic hydrocarbons | 19.8 |
| Colloid | 5.2 |
| Bituminous matter | <0.1 |
| Boiling range, ℃ | |
| Initial boiling point | 246 |
| 5％ | 402 |
| 10％ | 430 |
| 30％ | 482 |
| 50％ | 519 |
| 70％ | 573(75.2％) |
| Distillation yield (350 ℃), % | 1.5 |
| Distillation yield (500 ℃), % | 39.4 |
| The liquid temperature〉400 ℃, % | 61.6(538℃) |
Table 2
| Catalyzer | MLC-500 * |
| Chemical constitution, heavy % | |
| Al 2O 3 | 44.7 |
| Fe 2O 3 | 0.38 |
| Physical properties | |
| Specific surface area, m2/g | 203 |
| Pore volume, cm 3/g | 2.14 |
| Apparent density, g/cm 3 | 0.7921 |
| Size composition, % | |
| 0～40 micron | 8.5 |
| 0～80 micron | 66.3 |
| 0～110 micron | 87.2 |
| 0～150 micron | 95.9 |
*MLC-500 is trade names, by Sinopec Shandong catalyst plant industrial production, MA=60.
Table 3
| Comparative Examples 1 | Embodiment 1 | |
| The angle of nozzle centre axis and riser tube central axis | 45° | 135° |
| Temperature of reaction, ℃ | 510 | 510 |
| Reaction times, second | 4 | 4 |
| Agent- |
6 | 6 |
| Reaction pressure, kPa | 180 | 180 |
| Material balance, heavy % | ||
| Dry gas | 3.2 | 3.4 |
| Liquefied gas | 12.5 | 13.7 |
| Light naphthar | 30.3 | 34.2 |
| Heavy naphtha | 10.8 | 9.5 |
| Diesel oil | 17.2 | 15.5 |
| Heavy oil | 19.7 | 17.8 |
| Coke | 6.3 | 5.9 |
| Transformation efficiency, heavy % | 63.1 | 66.7 |
| Main products character: | ||
| Light naphthar MON | Benchmark | +1.1 |
| Light naphthar RON | Benchmark | +2.4 |
| Heavy naphtha MON | Benchmark | +3.6 |
| Heavy naphtha RON | Benchmark | +4.2 |
Table 4
| Comparative Examples 2 | |
|
| The angle of nozzle centre axis and riser tube central axis | / | 155° |
| Temperature of reaction, ℃ | 520 | 520 |
| Reaction times, second | 5 | 5 |
| Agent- |
6 | 6 |
| Reaction pressure, kPa | 200 | 200 |
| Material balance, heavy % | ||
| Dry gas | 3.6 | 3.72 |
| Liquefied gas | 13.1 | 14.1 |
| Light naphthar | 29.3 | 33.1 |
| Heavy naphtha | 11.8 | 9 |
| Diesel oil | 16.6 | 16.4 |
| Heavy oil | 18.8 | 16.28 |
| Coke | 6.8 | 7.4 |
| Transformation efficiency, heavy % | 64.6 | 67.32 |
| Main products character: | ||
| Light naphthar MON | Benchmark | +0.9 |
| Light naphthar RON | Benchmark | +2.1 |
| Heavy naphtha MON | Benchmark | +3.3 |
| Heavy naphtha RON | Benchmark | +3.9 |
Claims (13)
1, a kind of petroleum hydrocarbon catalytic cracking process, be to make to contact with catalyzer in petroleum hydrocarbon raw material injecting lift pipe reactor or the riser tube+fluidized-bed reactor and under the catalytic cracking reaction condition, react, oil gas behind the separating reaction and catalyzer, reaction oil gas is sent into subsequent separation system, the catalyzer of reaction back carbon deposit recycles after regeneration, and the central axis that it is characterized in that the central axis of nozzle of described petroleum hydrocarbon raw material injecting lift pipe reactor or riser tube+fluidized-bed reactor and the riser reactor formed angle of direction vertically upward is 90 °＜α＜180 °.
2, according to the method for claim 1, the central axis that it is characterized in that the central axis of injection nozzle of described petroleum hydrocarbon raw material and the riser reactor formed angle of direction vertically upward is 110 °＜α＜160 °.
3, according to the method for claim 2, the central axis that it is characterized in that the central axis of injection nozzle of described petroleum hydrocarbon raw material and the riser reactor formed angle of direction vertically upward is 130 °＜α＜155 °.
4, according to the method for claim 1, it is characterized in that described riser reactor is selected from: a kind of in the commonly used riser reactor in this area, the reducing riser reactor or the reactor that forms by more than one combination of reactors.
5,, it is characterized in that being provided with on the described riser reactor 1-8 layer feed nozzle according to the method for claim 4.
6,, it is characterized in that being provided with on the described riser reactor 1-5 layer feed nozzle according to the method for claim 5.
7,, it is characterized in that being provided with on the described riser reactor 1-3 layer feed nozzle according to the method for claim 6.
8, according to claim 5, one of 6 or 7 method, it is characterized in that described every layer comprises 2-20 feed nozzle.
9,, it is characterized in that described every layer comprises 4-18 feed nozzles according to the method for claim 8.
10,, it is characterized in that described every layer comprises 4-16 feed nozzles according to the method for claim 9.
11, according to claim 5,6,7,8, one of 10 method, it is characterized in that described feed nozzle along and the outer of the perpendicular cross section of riser reactor central axis be provided with symmetrically.
12, according to the method for claim 1, it is characterized in that described catalytic cracking reaction condition is as follows: temperature of reaction 460-580 ℃, reaction pressure 0.1-0.6MPa, agent-oil ratio 3-20, finish duration of contact are 0.5-20 second.
13, according to the method for claim 12, it is characterized in that described catalytic cracking reaction condition is as follows: temperature of reaction 480-550 ℃, reaction pressure 0.2-0.4MPa, agent-oil ratio 4-15, finish 1.0-10 duration of contact second.
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