CN101928589B - Catalytic cracking method of hydrocarbon oil - Google Patents
Catalytic cracking method of hydrocarbon oil Download PDFInfo
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- CN101928589B CN101928589B CN 200910148616 CN200910148616A CN101928589B CN 101928589 B CN101928589 B CN 101928589B CN 200910148616 CN200910148616 CN 200910148616 CN 200910148616 A CN200910148616 A CN 200910148616A CN 101928589 B CN101928589 B CN 101928589B
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Abstract
The invention relates to a catalytic cracking method of hydrocarbon oil. The processes are carried out in a riser tube or a fluidized bed reactor at least comprising upper and lower reaction zones. The method comprises the following steps: leading raw gasoline and a spent catalyst and/or a semi-regenerated catalyst in the lower reaction zone to carry out contact reaction; and leading heavy raw materials and a regenerated catalyst in the upper reaction zone to carry out contact reaction with the oil and gas and the catalyst from the lower reaction zone. The method can increase the yield of the liquid and simultaneously improve the quality of the gasoline.
Description
Technical field
The present invention relates to a kind of catalyst cracking method of hydrocarbon ils.
Background technology
Catalytic cracking is one of important means of oil secondary processing, is used for producing gasoline, diesel oil, liquefied gas etc. from heavy raw oil.Modern catalytic cracking process adopts molecular sieve catalyst, and reaction/regenerative process is carried out continuously.The steam atomizing of stock oil water also sprays in the riser reactor, contacts with high temperature catalyst (550～700 ℃) from revivifier therein, carries out catalytic cracking reaction immediately.The residence time of oil gas in riser reactor that catalytic cracking reaction generates is very short, generally has only several seconds.The reaction product of leaving riser reactor is through isolating the catalyzer of carrying secretly in settling vessel, after go separation column to carry out product separation.Long-pending have the catalyzer of coke to fall into following stripping stage by settling vessel, in stripping stage the oil gas that adsorbs on the catalyzer removed, and obtains reclaimable catalyst.Reclaimable catalyst behind the stripping enters revivifier, and the carbon deposit that generates because of reaction on the burning-off catalyzer is recovered activity of such catalysts.Catalyzer after the regeneration returns riser reactor and recycles.
Catalytic cracking is raw material in early days with the vacuum distillate, along with crude oil becomes heavy and poor qualityization day by day, and the light-end products demand increased day by day, the raw material sources of catalyzed cracking processing also enlarge day by day, as mix refining vacuum residuum and hot-work product such as wax tailings, viscosity breaking distilled oil, and the intermingled dregs ratio example is also improving constantly, catalytically cracked material character variation, cause the catalyzed reaction green coke to increase, the corresponding raising of regeneration temperature, heat cracking reaction increases, and dry gas yied and coke yield increase, product distribution variation.Environmental regulation is to the restriction increasingly stringent of Fuel Petroleum composition simultaneously, and market is to diesel oil fuel, liquefied gas increase in demand.
Improve existing heavy oil fluid catalytic cracking technology by contact environment and the gasoline freshening that improves stock oil and catalyzer, certain effect is arranged improving the distribution of catalytic cracking product, reduction content of sulfur in gasoline and olefin(e) centent.
For improving the contact environment of catalytic cracking catalyst and raw material, CN1114676C, CN1114677C discloses cool method of the regenerated catalyst of optimizing the reactive system operation in the heavy oil catalytic cracking process, chilled low-temp recovery agent is mixed in regenerator sloped tube or riser reactor pre lift zone with high temperature regeneration agent from revivifier, create a kind of high regeneration temperature, high solvent-oil ratio (weight ratio of catalyzer and stock oil), " three height " operational condition of high raw material preheating temperature, can improve the intermingled dregs ratio of device, improve transformation efficiency and light oil yield, improve product and distribute, but the high regeneration temperature of this method is to keeping activity of such catalysts unfavorable.US5451313 has developed reclaimable catalyst and regenerated catalyst hybrid technology, and US6059958 has developed regenerated catalyst and cooled regenerated catalyst hybrid technology.
CN1340593A discloses a kind of contact method for catalytic cracking of oil, locate the finish sparger to be set in the pre-lifting medium inlet of riser reactor inside between the main raw material ingress, the lower section of riser reactor is divided into is parallel to 2～4 axial reaction zones, and corresponding catalyst inlet and pre-upgrading raw material nozzles are set at each reaction zone; Enter different reaction zones respectively from the high temperature regeneration agent of revivifier, cooled half regenerator and/or from the spent agent of stripping stage; Pre-upgrading raw material injects 1,2 or 3 reaction zones wherein, contacts with catalyzer in the reaction zone and reacts; It is up along riser reactor in reaction zone separately to have neither part nor lot in catalyst for reaction in reacted logistics and other reaction zone, converges in finish sparger exit, contacts with main raw material through steam atomizing and reacts; Reaction product isolated, and spent agent is carried out gas carry and regenerate, above-mentioned finish contact process circulation is carried out.This method enters each reaction zone catalyzer different with carbon content with temperature respectively with raw material of different nature and contacts and carry out upgrading, and heavy feed stock is played pretreated effect, can improve product and distribute.But the liquid yield of this method is lower.
Zhong Xiaoxiang etc. have introduced on common catalytic cracking unit small-sized, medium-sized test and the Commercial application in the reaction principle, this process exploitation process of voluminous liquefied gas and diesel oil Technology (MGD technology) simultaneously in " refining of petroleum and chemical industry " calendar year 2001 32 volume 11 phase P1～5 " exploitation and the application of catalytic cracking fecund liquefied gas and diesel oil Technology ".Commercial application shows: adopt the MGD technology on catalytic cracking unit, liquefied gas yield can increase by 1.3～5.0 percentage points, diesel yield can increase by 3.0～5.0 percentage points, the olefin(e) centent of gasoline is when reducing by 9～11 percentage points, and RON and MON can improve 0.2～0.7 and 0.4～0.9 unit respectively.This technology has the flexibility of operation and the product flexibility of height, can select different production decisions according to the market requirement, adjust the product mix flexibly, and the adjustment time is short, but dry gas and coke yield increases to some extent.
Summary of the invention
The invention provides a kind of catalyst cracking method of hydrocarbon ils, the liquid yield height of this method, and can improve gasoline products character.
Method provided by the present invention is to carry out in riser tube that comprises upper and lower two reaction zones at least or fluidized-bed reactor, may further comprise the steps:
(1) will promote in advance medium, introduce lower reaction zone through the gasoline stocks of steam atomizing, contact with reclaimable catalyst and/or half regenerated catalyst, the oil gas of generation and reacted catalyzer upwards enter the top reaction zone;
(2) will introduce the top reaction zone through the heavy feed stock of steam atomizing, with regenerated catalyst, contact with catalyzer from the oil gas of lower reaction zone, the oil gas of generation carries out finish with reacted catalyzer to be separated;
(3) oil gas removes subsequent separation system separating reaction product, catalyzer obtains reclaimable catalyst behind stripping, reclaimable catalyst obtains half regenerated catalyst, regenerated catalyst behind coke burning regeneration, the reclaimable catalyst of part and/or half regenerated catalyst of part are returned lower reaction zone, regenerated catalyst is returned the top reaction zone.
The present invention carries out catalytic cracking reaction with gasoline stocks with heavy feed stock in different reaction zones, gasoline stocks and reclaimable catalyst and/or half regenerated catalyst contact reacts, help gasoline and reduce sulphur content and olefin(e) centent, gasoline fraction is produced liquefied gas by partial cracking, avoid gasoline stocks and high-temperature regenerated catalyst contact reacts simultaneously, make dry gas and coke yield too high.For heavy feed stock, oil gas that lower reaction zone is come and catalyst mixture by with the mixing of regenerated catalyst, reduced the contact temperature of heavy feed stock with catalyzer, reduced the hydrocarbon ils overcracking, further reduce the generation of dry gas and coke.
Description of drawings
Accompanying drawing is the structural representation of the riser reactor among the present invention.
Embodiment
Below elaborate the present invention.
Method provided by the present invention is to carry out in riser tube that comprises upper and lower two reaction zones at least or fluidized-bed reactor, may further comprise the steps:
(1) will promote in advance medium, introduce lower reaction zone through the gasoline stocks of steam atomizing, contact with reclaimable catalyst and/or half regenerated catalyst, the oil gas of generation and reacted catalyzer upwards enter the top reaction zone;
(2) will introduce the top reaction zone through the heavy feed stock of steam atomizing, with regenerated catalyst, contact with catalyzer from the oil gas of lower reaction zone, the oil gas of generation carries out finish with reacted catalyzer to be separated;
(3) oil gas removes subsequent separation system separating reaction product, catalyzer obtains reclaimable catalyst behind stripping, reclaimable catalyst obtains half regenerated catalyst, regenerated catalyst behind coke burning regeneration, the reclaimable catalyst of part and/or half regenerated catalyst of part are returned lower reaction zone, regenerated catalyst is returned the top reaction zone.
Described gasoline stocks is that boiling range is 20～250 ℃ a hydrocarbon raw material, is preferably in coker gasoline, straight-run spirit, catalytic gasoline, pressure gasoline and the reforming raffinate oil one or more.
Described heavy feed stock is that boiling range is 250～550 ℃ distillate or boiling range greater than 350 ℃ residual oil raw material, is preferably in straight-run gas oil, vacuum gas oil, hydrocracking tail oil, solvent-deasphalted oils, hydrofined oil, wax tailings, long residuum and the vacuum residuum one or more.
The weight ratio of gasoline stocks and heavy feed stock is 1: 1～20, be preferably 1: 5～and 10.
Described pre-lifting medium is a various pre-lifting medium well known to those skilled in the art, as in water vapor, refinery dry gas, light paraffins, the light olefin one or more.The pre-effect that promotes medium is to make catalyzer quicken to rise, and forms density uniform catalyst piston flow in the riser reactor bottom.The pre-consumption that promotes medium is known by those skilled in the art.In general, the consumption that promotes medium in advance accounts for 1～30 weight % of hydrocarbon ils total amount, preferred 2～15 weight %.
Described catalyzer is a catalytic cracking catalyst, as the amorphous silicon aluminium catalytic cracking catalyst or contain the catalytic cracking catalyst of zeolite.The composition of catalytic cracking catalyst is well known to those skilled in the art, and for example catalytic cracking catalyst generally includes one or more molecular sieves and heat-resistant inorganic oxide, optionally contains clay.Molecular sieve is optional self-contained or do not contain in the y-type zeolite of rare earth element, the ultrastable Y that contains or do not contain rare earth element, the supersiliceous zeolite with five-membered ring structure, β zeolite, mordenite, the omega zeolite one or more, and the supersiliceous zeolite with five-membered ring structure can be ZSM-5 zeolite and/or ZRP zeolite.In the optional self-alumina of heat-resistant inorganic oxide, silicon oxide, amorphous silicon aluminium, zirconium white, titanium oxide, boron oxide and the alkaline earth metal oxide one or more.Clay can be selected from kaolin, halloysite, polynite, diatomite, halloysite, saponite, tiredly take off in soil, sepiolite, attapulgite, hydrotalcite and the boron-moisten soil one or more.
Among the present invention, the cracking reaction condition of each reaction zone all can adopt conventional cracking reaction condition.When adopting riser reactor, the preferred reaction conditions of lower reaction zone is: gasoline stocks is 300～550 ℃ with the temperature that contacts of reclaimable catalyst and/or half regenerated catalyst, preferred 350～500 ℃; Contact pressure is 130～450 kPas, preferred 200～400 kPas; The weight ratio of reclaimable catalyst and/or half regenerated catalyst and gasoline stocks is 2～25: 1, preferred 8～15: 1, and the residence time is 0.8～8 second, preferred 2～5 seconds; The pre-weight ratio that promotes medium and gasoline stocks is 0.01～0.1: 1, preferred 0.03～0.08: 1, and the weight ratio of atomizing steam and gasoline stocks is 0.01～0.1: 1, is preferably 0.02～0.05: 1; The preferred reaction conditions of top reaction zone is: heavy feed stock is 400～650 ℃ with the temperature that contacts of regenerated catalyst, preferred 500～630 ℃; Contact pressure is 130～450 kPas, preferred 150～250 kPas; Heavy feed stock is 2～15: 1 with the agent weight of oil ratio of regenerated catalyst, preferred 3～10: 1; The residence time is 0.5～8 second, preferred 1～5 second; The weight ratio of atomizing steam and heavy feed stock is 0.01～0.1: 1, is preferably 0.03～0.06: 1.
When adopting fluidized-bed reactor, the preferred reaction conditions of lower reaction zone is: gasoline stocks is 300～550 ℃ with the temperature that contacts of reclaimable catalyst and/or half regenerated catalyst, preferred 350～500 ℃; Contact pressure is 130～450 kPas, preferred 200～400 kPas; The weight ratio of reclaimable catalyst and/or half regenerated catalyst and gasoline stocks is 2～25: 1, preferred 8～15: 1; The weight hourly space velocity of gasoline stocks is 1～120 hour
-1, preferred 2～80 hours
-1The pre-weight ratio that promotes medium and gasoline stocks is 0.01～0.1: 1, preferred 0.03～0.08: 1, and the weight ratio of atomizing steam and gasoline stocks is 0.01～0.1: 1, is preferably 0.02～0.05: 1.The preferred reaction conditions of top reaction zone is: heavy feed stock is 400～650 ℃ with the temperature that contacts of regenerated catalyst, preferred 500～630 ℃; Contact pressure is 130～450 kPas, preferred 150～250 kPas; Heavy feed stock is 2～15: 1 with the agent weight of oil ratio of regenerated catalyst, preferred 3～10: 1; The weight hourly space velocity of heavy feed stock is 1～120 hour
-1, preferred 2～60 hours
-1The weight ratio of atomizing steam and heavy feed stock is 0.01～0.1: 1, is preferably 0.03～0.06: 1.
The condition of riser reactor outlet area is conventional condition, and these conditions comprise that temperature is 460～590 ℃, and preferred 470～530 ℃, pressure is 130～400 kPas, is preferably 150～350 kPas, and be 0.1～1 second duration of contact, is preferably 0.1～0.8 second.The condition of riser reactor outlet area is conventionally known to one of skill in the art.
Among the present invention, in stripper, adopt water vapor to carry out stripping, its effect be with between the granules of catalyst and the oil gas that is full of in the particle hole cement out, improve the oil product productive rate.The consumption of water stripping steam is known by those skilled in the art.In general, the consumption that is used for water stripping steam accounts for 0.1～0.8 weight % of catalyst recirculation amount, is preferably 0.2～0.4 weight %.
Among the present invention, described reclaimable catalyst be after catalytic cracking reaction is finished through the catalyzer behind the stripping stage stripping, the reclaimable catalyst carbon content is about 0.8～1.2 weight %.Half regenerated catalyst is a kind of catalyzer of incomplete regen-eration, and carbon content is about the catalyzer of 0.16～0.48 weight % after referring to regenerate, as the catalyzer that obtains from one section revivifier in the two-stage regeneration device.Regenerated catalyst is the catalyzer of holomorphosis, and this coke on regenerated catalyst is about 0.01～0.05 weight %, as the catalyzer that obtains from two sections revivifiers in the two-stage regeneration device.The refrigerative regenerator is the regenerator regenerator that temperature reduces after the external warmer heat exchange.
The method that obtains half regenerated catalyst and regenerated catalyst is conventionally known to one of skill in the art, for example, can adopt among the CN1221022A disclosed two-stage regeneration system to regenerate.
Among the present invention, at least two reaction zones to be set in vertical direction, could realize purpose of the present invention.Certainly, the present invention also can be set to according to the number of concrete needs reaction zone＞and 2, as when the heavy feed stock that needs processing is two or more, 3 or 3 above reaction zones can be set, so that the heavy feed stock of different properties and different sources contacts with catalyzer respectively.When concrete example is wax tailings and long residuum as the heavy feed stock of processing, 3 reaction zones can be set, introduce gasoline stocks, long residue feed and wax tailings raw material from bottom to top respectively, the benefit one that topmost is introduced wax tailings is to reduce the toxication of wax tailings to catalyzer, improve the long residue feed cracking effect that introduce at the middle part, the 2nd, wax tailings is carried out upgrading, the wax tailings behind the upgrading carries out cracking again by freshening.
Among the present invention, the volume ratio of lower reaction zone and top reaction zone is 1: 1～10, be preferably 1: 2～and 6.The diameter of lower reaction zone and top reaction zone can be identical, also can be different.When the diameter of each reaction zone of riser reactor is identical, then the aspect ratio of lower reaction zone and top reaction zone is volume ratio, therefore, and when the diameter of each reaction zone of riser reactor is identical, the aspect ratio of lower reaction zone and top reaction zone is preferably 1: 1～and 10, be preferably 1: 2～6.
First kind of preferred implementation of the present invention is to adopt one section regeneration.Gasoline stocks after the preheating is introduced lower reaction zone by atomizing nozzle, with reclaimable catalyst contact reacts from stripper, under the effect of pre-lifting medium, reaction oil gas and catalyzer rise along riser reactor, enter the top reaction zone, with mix from the high-temperature regenerated catalyst of revivifier and the heavy feed stock after the preheating, and contact, reaction, reaction oil gas and catalyzer rise along riser reactor, to the riser reactor outlet, enter settling vessel, separating catalyst and reaction product, reaction product enter the subsequent separation system product separation, and catalyzer obtains reclaimable catalyst behind the stripper stripping, part reclaimable catalyst returns lower reaction zone and recycles, another part reclaimable catalyst enters the revivifier coke burning regeneration, obtains regenerated catalyst, regenerated catalyst is returned the top reaction zone recycle.
Second kind of preferred implementation of the present invention is to adopt the two-stage regeneration mode of CN1221022A.Gasoline stocks after the preheating is introduced lower reaction zone by atomizing nozzle, with from the reclaimable catalyst of stripper with from half regenerated catalyst contact reacts of one section revivifier, under the effect of pre-lifting medium, reaction oil gas and catalyzer rise along riser reactor, enter the top reaction zone, with mix from the high-temperature regenerated catalyst of two sections revivifiers and the heavy feed stock after the preheating, and contact, reaction, reaction oil gas and catalyzer rise along riser reactor, to the riser reactor outlet, enter settling vessel, separating catalyst and reaction product, reaction product enters the subsequent separation system product separation, catalyzer obtains reclaimable catalyst behind the stripper stripping, part reclaimable catalyst returns lower reaction zone and recycles, another part reclaimable catalyst enters one section revivifier coke burning regeneration, obtain half regenerated catalyst, a part half regenerated catalyst returns lower reaction zone and recycles, another part half regenerated catalyst enters two sections revivifier coke burning regenerations, obtain regenerated catalyst, regenerated catalyst is returned the top reaction zone recycle.
The third preferred implementation of the present invention is to adopt the two-stage regeneration mode of CN1221022A.Gasoline stocks after the preheating is introduced lower reaction zone by atomizing nozzle, with half regenerated catalyst contact reacts from one section revivifier, under the effect of pre-lifting medium, reaction oil gas and catalyzer rise along riser reactor, enter the top reaction zone, with mix from the high-temperature regenerated catalyst of two sections revivifiers and the heavy feed stock after the preheating, and contact, reaction, reaction oil gas and catalyzer rise along riser reactor, to the riser reactor outlet, enter settling vessel, separating catalyst and reaction product, reaction product enters the subsequent separation system product separation, catalyzer obtains reclaimable catalyst behind the stripper stripping, reclaimable catalyst enters one section revivifier coke burning regeneration, obtains half regenerated catalyst, a part half regenerated catalyst returns lower reaction zone and recycles, another part half regenerated catalyst enters two sections revivifier coke burning regenerations, obtains regenerated catalyst, regenerated catalyst is returned the top reaction zone recycle.
The 4th kind of preferred implementation of the present invention is to adopt the two-stage regeneration mode of CN1221022A.Gasoline stocks after the preheating is introduced lower reaction zone by atomizing nozzle, with half regenerated catalyst contact reacts from one section revivifier, under the effect of pre-lifting medium, reaction oil gas and catalyzer rise along riser reactor, enter the top reaction zone, with mix from the high-temperature regenerated catalyst of two sections revivifiers and the heavy feed stock after the preheating, and contact, reaction, reaction oil gas and catalyzer rise along riser reactor, to the riser reactor outlet, enter settling vessel, separating catalyst and reaction product, reaction product enters the subsequent separation system product separation, catalyzer obtains reclaimable catalyst behind the stripper stripping, reclaimable catalyst enters one section revivifier coke burning regeneration, obtains half regenerated catalyst, a part half regenerated catalyst returns lower reaction zone and recycles, another part half regenerated catalyst enters two sections revivifier coke burning regenerations, obtains regenerated catalyst, and regenerated catalyst returns the top reaction zone and recycles after the external warmer cooling.
In all preferred implementations of the present invention, all can external warmer be set, the refrigerative regenerated catalyst be returned the top reaction zone recycle, and be not limited only to the 4th kind of preferred implementation at revivifier.
Further set forth the present invention below in conjunction with drawings and Examples.Except that specifying, the interchanger among the embodiment is tube and shell heat exchanger, and revivifier is the two-stage regeneration device, and wherein two sections revivifiers are provided with external warmer, obtain the refrigerative regenerated catalyst from two sections revivifiers.The consumption that is used for steam stripped water vapor accounts for about 0.4 weight % of catalyst recirculation amount.The pre-medium that promotes adopts water vapor.
Embodiment 1
Present embodiment adopts medium-sized riser reactor, and this riser reactor is that total height is 10 meters, and diameter is 25 centimetres a cylindrical structure, and the aspect ratio of its middle and lower part, top reaction zone is 1.8: 7.5, and this riser tube foot is a pre lift zone.
The stock oil of device processing is that the gasoline stocks of introducing from lower reaction zone is a catalytically cracked gasoline; The heavy feed stock of introducing from the top reaction zone is wax oil (vacuum gas oil).The inlet amount of catalytically cracked gasoline is 15 weight % of wax oil.Various raw material oil propertiess are listed in table 1, and the trade mark of catalyzer is LV-23, are produced by Sinopec group Shandong catalyst plant, and catalyzer LV-23 is the cracking catalyst that contains y-type zeolite, ultrastable Y.
Concrete steps are, as shown in drawings, gasoline stocks after the preheating enters lower reaction zone 1 by atomizing nozzle 5, reclaimable catalyst from stripper enters lower reaction zone 1 through catalyst inlet 3, the gasoline fraction raw material contacts with reclaimable catalyst, under the effect of the pre-lifting medium that enters the riser reactor bottom through pipeline 7, rise along riser reactor, enter top reaction zone 2.
Wax oil after the preheating enters top reaction zone 2 by atomizing nozzle 6, enters top reaction zone 2 from the regenerated catalyst of revivifier through catalyst inlet 4, wax oil with contact, react from the logistics of lower reaction zone, the mixture flow of regenerated catalyst; Catalyzer and reaction mass from lower reaction zone, top reaction zone continue to rise along riser reactor, to the riser reactor outlet, enter settling vessel, separating catalyst and reaction product, reaction product enters the subsequent separation system product separation, catalyzer obtains reclaimable catalyst through the stripper stripping, method according to above-mentioned patent CN1221022A obtains half regenerated catalyst and regenerated catalyst, part reclaimable catalyst returns lower reaction zone and recycles, and regenerated catalyst returns the top reaction zone and recycles.
Concrete operational condition, product distribute and gasoline products character is listed in table 2, table 3, table 4 respectively.
Repeat the method for embodiment 1, different is that the catalyzer that enters lower reaction zone is half regenerated catalyst from first section revivifier in the two-stage regeneration device.
Concrete operational condition, product distribute and gasoline products character is listed in table 2, table 3, table 4 respectively.
Comparative Examples 1
This Comparative Examples adopts the medium-sized riser reactor of the successive reaction regenerative operation identical with the foregoing description 1 and embodiment 2, and stock oil is wax oil shown in the table 1.
Concrete testing sequence is: the wax oil stock oil after the preheating enters the top of riser reactor by atomizing nozzle 6, contact, mix with regenerated catalyst from revivifier through pipeline 4, reaction, catalyzer and reaction mass are under the effect of pre-lifting medium, rise along riser reactor, to the riser reactor outlet, enter settling vessel, separating catalyst and reaction product, reaction product enters the subsequent separation system product separation, and catalyzer recycles after stripper stripping, revivifier burn.
Concrete operational condition, product distribute and gasoline products character is listed in table 2, table 3, table 4 respectively.
Repeat the step of embodiment 1, different is that the catalyzer that enters the top reaction zone is the cooling regenerated catalyst from second section revivifier external warmer in the two-stage regeneration device.
Concrete operational condition, product distribute and gasoline products character is listed in table 5, table 6, table 7 respectively.
Embodiment 4
Repeat the step of embodiment 3, different is that the catalyzer that enters lower reaction zone is half regenerated catalyst from first section revivifier in the two-stage regeneration device.
Concrete operational condition, product distribute and gasoline products character is listed in table 5, table 6, table 7 respectively.
Comparative Examples 2
Repeat the step of Comparative Examples 1, different is that the catalyzer that enters the top reaction zone is the cooling regenerated catalyst from second section revivifier external warmer in the two-stage regeneration device.
Concrete operational condition, product distribute and gasoline products character is listed in table 5, table 6, table 7 respectively.
From table 3, table 6 data as can be seen, adopt hydrocarbon oil catalytic cracking method of the present invention after, dry gas and coke yield descend, liquid product yield (liquefied gas+gasoline+diesel oil) improves.Simultaneously from table 4, table 7 data as can be seen, olefin(e) centent descends in the gasoline products, and aromatic hydrocarbons and isoparaffin content increase, and the gasoline products quality improves.
Table 1
Table 2
Table 3
Table 4
Table 5
Table 6
Table 7
Claims (10)
1. the catalyst cracking method of a hydrocarbon ils is to carry out in riser tube that comprises upper and lower two reaction zones at least or fluidized-bed reactor, may further comprise the steps:
(1) will promote in advance medium, introduce lower reaction zone through the gasoline stocks of steam atomizing, contact with reclaimable catalyst and/or half regenerated catalyst, the oil gas of generation and reacted catalyzer upwards enter the top reaction zone;
(2) will introduce the top reaction zone through the heavy feed stock of steam atomizing, with regenerated catalyst, contact with catalyzer from the oil gas of lower reaction zone, the oil gas of generation carries out finish with reacted catalyzer to be separated;
(3) oil gas removes subsequent separation system separating reaction product, catalyzer obtains reclaimable catalyst behind stripping, reclaimable catalyst obtains half regenerated catalyst, regenerated catalyst behind coke burning regeneration, the reclaimable catalyst of part and/or half regenerated catalyst of part are returned lower reaction zone, regenerated catalyst is returned the top reaction zone;
When adopting riser reactor, the reaction conditions of lower reaction zone is: gasoline stocks is 300～550 ℃ with the temperature that contacts of reclaimable catalyst and/or half regenerated catalyst, contact pressure is 130～450 kPas, the weight ratio of reclaimable catalyst and/or half regenerated catalyst and gasoline stocks is 2～25: 1, the residence time is 0.8～8 second, the pre-weight ratio that promotes medium and gasoline stocks is 0.01～0.1: 1, and the weight ratio of atomizing steam and gasoline stocks is 0.01～0.1: 1; The reaction conditions of top reaction zone is: heavy feed stock is 400～650 ℃ with the temperature that contacts of regenerated catalyst, contact pressure is 130～450 kPas, heavy feed stock is 2～15: 1 with the agent weight of oil ratio of regenerated catalyst, the residence time is 0.5～8 second, and the weight ratio of atomizing steam and heavy feed stock is 0.01～0.1: 1;
When adopting fluidized-bed reactor, the reaction conditions of lower reaction zone is: gasoline stocks is 300～550 ℃ with the temperature that contacts of reclaimable catalyst and/or half regenerated catalyst, contact pressure is 130～450 kPas, the weight ratio of reclaimable catalyst and/or half regenerated catalyst and gasoline stocks is 2～25: 1, and the weight hourly space velocity of gasoline stocks is 1～120 hour
-1, the weight ratio that promotes medium and gasoline stocks in advance is 0.01～0.1: 1, the weight ratio of atomizing steam and gasoline stocks is 0.01～0.1: 1; The reaction conditions of top reaction zone is: heavy feed stock is 400～650 ℃ with the temperature that contacts of regenerated catalyst, contact pressure is 130～450 kPas, heavy feed stock is 2～15: 1 with the agent weight of oil ratio of regenerated catalyst, and the weight hourly space velocity of heavy feed stock is 1～120 hour
-1, the weight ratio of atomizing steam and heavy feed stock is 0.01～0.1: 1.
2. in accordance with the method for claim 1, it is characterized in that described gasoline stocks is one or more in coker gasoline, straight-run spirit, catalytic gasoline, pressure gasoline and the reforming raffinate oil.
3. in accordance with the method for claim 1, it is characterized in that described heavy feed stock is one or more in straight-run gas oil, vacuum gas oil, hydrocracking tail oil, solvent-deasphalted oils, hydrofined oil, wax tailings, long residuum and the vacuum residuum.
4. in accordance with the method for claim 1, it is characterized in that the weight ratio of gasoline stocks and heavy feed stock is 1: 1～20.
5. in accordance with the method for claim 4, it is characterized in that the weight ratio of gasoline stocks and heavy feed stock is 1: 5～10.
6. in accordance with the method for claim 1, it is characterized in that, when adopting riser reactor, the reaction conditions of lower reaction zone is: gasoline stocks is 350～500 ℃ with the temperature that contacts of reclaimable catalyst and/or half regenerated catalyst, contact pressure is 200～400 kPas, the weight ratio of reclaimable catalyst and/or half regenerated catalyst and gasoline stocks is 8～15: 1, the residence time is 2～5 seconds, the pre-weight ratio that promotes medium and gasoline stocks is 0.03～0.08: 1, and the weight ratio of atomizing steam and gasoline stocks is 0.02～0.05: 1; The reaction conditions of top reaction zone is: heavy feed stock is 500～630 ℃ with the temperature that contacts of regenerated catalyst, contact pressure is 150～250 kPas, heavy feed stock is 3～10: 1 with the agent weight of oil ratio of regenerated catalyst, the residence time is 1～5 second, and the weight ratio of atomizing steam and heavy feed stock is 0.03～0.06: 1.
7. in accordance with the method for claim 1, it is characterized in that, when adopting fluidized-bed reactor, the reaction conditions of lower reaction zone is: gasoline stocks is 350～500 ℃ with the temperature that contacts of reclaimable catalyst and/or half regenerated catalyst, contact pressure is 200～400 kPas, the weight ratio of reclaimable catalyst and/or half regenerated catalyst and gasoline stocks is 8～15: 1, and the weight hourly space velocity of gasoline stocks is 2～80 hours
-1, the weight ratio that promotes medium and gasoline stocks in advance is 0.03～0.08: 1, the weight ratio of atomizing steam and gasoline stocks is 0.02～0.05: 1; The reaction conditions of top reaction zone is: heavy feed stock is 500～630 ℃ with the temperature that contacts of regenerated catalyst, contact pressure is 150～250 kPas, heavy feed stock is 3～10: 1 with the agent weight of oil ratio of regenerated catalyst, and the weight hourly space velocity of heavy feed stock is 2～60 hours
-1, the weight ratio of atomizing steam and heavy feed stock is 0.03～0.06: 1.
8. in accordance with the method for claim 1, it is characterized in that the volume ratio of lower reaction zone and top reaction zone is 1: 1～10.
9. in accordance with the method for claim 8, it is characterized in that the volume ratio of lower reaction zone and top reaction zone is 1: 2～6.
10. in accordance with the method for claim 1, it is characterized in that regenerated catalyst returns the top reaction zone after the external warmer cooling.
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| CN 200910148616 CN101928589B (en) | 2009-06-25 | 2009-06-25 | Catalytic cracking method of hydrocarbon oil |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85104806A (en) * | 1985-06-24 | 1987-01-07 | 法国石油公司 | Fluid catalytic cracking process and device |
| CN1083092A (en) * | 1992-08-27 | 1994-03-02 | 中国石油化工总公司石油化工科学研究院 | The catalytic thermocracking process of petroleum hydrocarbon |
| CN1221022A (en) * | 1997-12-23 | 1999-06-30 | 中国石油化工总公司 | Lapping type two-stage regeneration technology of heavy oil fluidized catalystic cracking |
-
2009
- 2009-06-25 CN CN 200910148616 patent/CN101928589B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85104806A (en) * | 1985-06-24 | 1987-01-07 | 法国石油公司 | Fluid catalytic cracking process and device |
| CN1083092A (en) * | 1992-08-27 | 1994-03-02 | 中国石油化工总公司石油化工科学研究院 | The catalytic thermocracking process of petroleum hydrocarbon |
| CN1221022A (en) * | 1997-12-23 | 1999-06-30 | 中国石油化工总公司 | Lapping type two-stage regeneration technology of heavy oil fluidized catalystic cracking |
Non-Patent Citations (4)
| Title |
|---|
| 《催化热裂解工艺机理及影响因素》;侯典国等;《乙烯工业》;20021231;第14卷(第4期);第1-5页 * |
| 《催化裂化过程中的热裂化与催化裂化》;高永灿等;《化工学报》;20020531;第53卷(第6期);第469-472页 * |
| 侯典国等.《催化热裂解工艺机理及影响因素》.《乙烯工业》.2002,第14卷(第4期),第1-5页. |
| 高永灿等.《催化裂化过程中的热裂化与催化裂化》.《化工学报》.2002,第53卷(第6期),第469-472页. |
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