CN85104806A - Fluid catalytic cracking process and device - Google Patents
Fluid catalytic cracking process and device Download PDFInfo
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- CN85104806A CN85104806A CN85104806.4A CN85104806A CN85104806A CN 85104806 A CN85104806 A CN 85104806A CN 85104806 A CN85104806 A CN 85104806A CN 85104806 A CN85104806 A CN 85104806A
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Abstract
The present invention relates to the fluid catalystic cracking of hydrocarbon feed and the reclaiming process of catalyzer.The top of (1) contacts with the liquid starting material of sending forth that will process the granules of catalyst of heat in the zone of cracking, and (a) raw material is vaporized in pipeline 10, and (b) raw material and granules of catalyst mix closely.Granules of catalyst is discharged from the bottom of cracking case (1) then, separate with reaction effluent, stripping in reactor (17), and carry out two-stage regeneration in zone (22) and (37) respectively successively, zone (37) is a tubular reactor, and granules of catalyst is boosted by carrier gas at tubular reactor.
Description
The present invention relates to a kind of catalytic cracking of new (a) catalytic cracking, particularly heavy-hydrocarbon oil and (b) reclaiming process of catalyzer, and relate to the device of realizing this technology.
Because the variation of natural crude oil supply side and the requirement of purified product and oil fuel reduced, the requirement than light product to gasoline-type increases, this just makes petroleum refining industry will develop various novel procesies, to improve the quality of natural heavy oil and residual oil (for example straight run residue or vacuum residuum).
About handling the catalytic cracking process of such raw material, seeming main difficulty is to be caused by following reason: contain the such organic substance of polycyclic aromatic hydrocarbons that resembles bituminous matter and condensation in these raw materials, these materials are to be difficult to be cracked into less molecule to obtain quite a large amount of low boiler cuts, these materials will interosculate and produce a large amount of coke, be deposited on the used catalyzer, therefore reduced activity of such catalysts.And, in these heavy oil, there is a large amount of heavy metals, resemble Ni-V-Fe etc., these heavy metals are considered to deleterious, because these metals will make general zeolite catalyst used in fluid catalytic cracking process poison or inactivation at least.The back, fluid catalystic cracking is called F.C.C..
But there are many basic factors to keep the coke of formation minimum simultaneously so that may transform heavy product highly selective or lighter cut.
In these factors, one of most important factor is that the regenerated catalyzer of the heat that will guarantee that hydrocarbon feed (generally be preheating and with the steam annexation) and catalytic cracking unit are used well mixes in the zone that contacts, so that the heat passage generation between raw material and the catalyzer is fast and regular as far as possible.The charge level of introducing at the raw material of conversion zone, also be very important with effectively upgrading the regenerated catalyzer enduringly particularly by avoiding air-teturning mixed phenomenon, air-teturning mixed phenomenon increases duration of contact and the lighting end of generation is significantly reduced, and has increased the weight ratio of the coke that forms on granules of catalyst simultaneously.
Also be harmful to the smooth operation of F.C.C. device, especially specifying another important phenomenon of the smooth operation in the time of will handling heavier feedstocks is the warp-wise homogeneity that is difficult to reach good catalyzer, not only at inlet, and in the radially homogeneity that all will reach good catalyzer by reaction zone.
About the selectivity of cracking reaction, it is generally acknowledged that fluidic flows, and to approach piston flow more good more.It is difficult especially will reaching piston flow at general F.C.C. 〃 device.
The objective of the invention is to reach best condition simultaneously: do not have back mixing, radially homogeneity and resemble piston flow with above-mentioned three kinds of favorable factors.Spray with a kind of novel raw material simultaneously and can reach these purposes, at conversion zone raw material and catalyzer and flow to current downflow with mixing device, conversion zone and the quick disconnector of catalyzer.
Reach in the middle of the F.C.C. technology of the reactor under the conversion zone usefulness and the flow direction disclosed, some is to specify the common raw material that will handle resemble the vacuum gas oil.United States Patent (USP) 2,420,558 disclose a kind of like this method, still with a kind of general raw material injection system and single catalyst regeneration zone.United States Patent (USP) 2,965,454 disclose a kind of device, and its conversion zone is made up of many standpipes, passes through reaction zone under raw material and catalyzer and the flow direction.United States Patent (USP) 3,835,029 also mentions the F.C.C. technology under a kind of and the flow direction, it only is used for handling light raw material (can vaporize fully at 510～550 ℃), when the speed of catalyzer was 9～30m/s, raw material was introduced from the bottom of conversion zone catalyst inlet and gas/solid separation system fast not.
It is inappropriate that these methods are used to process heavier hydrocarbon feed, and such raw material needs special vaporization and jet apparatus, for ease of regenerated catalyst, normally uses two-step catalysis agent reclaiming process.
United States Patent (USP) 4,385,985 disclose a kind of improved catalytic cracking process, it is that downflow system is handled heavier feedstocks, raw material do greater than 560 ℃ Conradson carbon residue at least 3%.But in the system of introducing, mixture about regenerated catalyzer and raw material, wherein catalyzer is to introduce by a porous screen, raw material is to introduce by the general system of being made up of several injectors, injector is positioned at the bottom at the position of introducing the regenerated catalyzer, can not make raw material sharply be vaporized into uniform mixture by whole reactor.United States Patent (USP) 4,411, the 773 disclosed systems that in fact same apparatus is arranged at least with regard to essential part, particularly are identical with regard to jet-mixing system.
The special technique of much introducing heavy hydrocarbon feeds at the conversion zone of catalyst cracker is disclosed already.For example, United States Patent (USP) 4,097,243 disclose a kind of feed distribution system, and this system comprises many nozzles, and these nozzles are contained on the bigger cross section of frustum cone, and several nozzle arrangements is parallel with reactor axis, and other nozzles favour reactor axis.The regenerated catalyzer provides in the direction that favours reactor axis on the system that introduces raw material.United States Patent (USP) 4,427,737 disclose the method for a kind of preparation and dispersion heavier feedstocks.This method is: earlier raw material is formed a kind of emulsion in water, the emulsion preheating, be sprayed into 100～500 microns droplet then, carry out such spray with diluent for gases in the outside of conversion zone.Be implemented in the injection of conversion zone by many nozzles that are distributed on the conical surface sparger of frustum garden, the area of sparger only is a reactor " area 20～40%.According to the method, the regenerated catalyzer is at the underfeed of raw material injection system, and raw material is introduced with the speed greater than 90m/s.United States Patent (USP) 3,152,065 and 3,246,960 introduced a kind of at the bottom of " reactor " hydrocarbon injection raw material, so that introduce the method for raw material and steam mixture, raw material carries out screw type motion, and then with vapor mixing, whole mixture is by an aperture that limits sectional area, the regenerated catalyzer is supplied with in the bottom of reactor in the bottom of injection system.
Yet, above-mentioned device does not have a kind of injection easily that may be implemented in the catalytic cracking reaction zone territory, and simultaneously apace (preferably less than 0.5 second) catalyzer is mixed with the raw material of vaporization, and fine along the radially homogeneity of surperficial this mixture of whole reactor.
In addition, these devices are to be used for introducing raw material at the F.C.C. of up parallel flow type reactor, are not suitable for the downward parallel flow type of raw material and catalyzer.
The invention relates to a kind of new F.C.C.(fluid catalytic cracking) technology, in particular for transforming heavy-hydrocarbon oil.In fact these raw materials both can be general raw materials, promptly for example do to be about 400 ℃ raw material, and as vacuum gas oil, also can be heavier hydrocarbon ils, as rough and/or stripped oil plant, straight run or vacuum residuum.These raw materials can optionally carry out pre-treatment, for example carry out hydrotreatment with cobalt-molybdenum or nickel-molybdenum type catalyzer.According to the present invention, reasonable raw material be normal boiling point up to 700 ℃ or higher cut, randomly contain a high proportion of asphaltene product and Conradson carbon residue content up to 4% or higher raw material.These raw materials can with or lighter distillate dilution that need not be general, these benzolines can comprise carries out the cracked hydrocarbon-fraction, these hydrocarbon-fractions are turning oil, for example light cycle oil (LCO) or heavy cycle oil (HCO).According to an embodiment preferably of the present invention, these raw materials will be 300～450 ℃ of preheatings before handling.
Or rather, the present invention includes: raw material is introduced on the top of vertical basically conversion zone, utilize the system of injection and raw material dispersion, usually use additional steam, raw material is sprayed into the drop of mean size, and the big or small reasonable of drop is to be no more than 100 microns, and is more preferably about 50 microns, at the charge level that sprays, the speed of raw material is 10～100m/s preferably.The inventive system comprises many nozzles; each nozzle all is placed on the top of regenerated thermocatalyst vent pipe; and it is coaxial with this pipe; so that make top at vent pipe; the material jet of part vaporization flows with the granules of catalyst of heat is substantially parallel on the one hand; on the other hand, help like this carrying out heat exchange at this by radiation between these two kinds of logistics, raw material is vaporized fully in the bottom of above-mentioned catalyzer vent pipe.According to this device, generally be no more than 0.5 second the duration of contact of raw material and catalyzer, and generally be approximately 0.1 second.Raw material (vaporization) and catalyzer and stream, then to dirty, by conversion zone, the temperature of conversion zone is generally 450～700 ℃, 0.1～10 second residence time, preferably 0.2～4 second.At reactor lower part, the reaction effluent of the catalyzer of stream and process cracking processing is accelerated altogether, then by an initial Quick Separation System (seeing below the explanation of Fig. 3), in less than 1 second time, reach separating of granules of catalyst and steam for the first time; So 50～90% granules of catalyst separates with the gas-phase reaction effluent, finish this separation with one or several general cyclonic separator.Therefore, the present invention guarantees quick and complete the separating of catalyzer and gaseous stream (cyclonic separator (answering) of the so-called reverse direction flow ejector half of the reverse screw that the available motion that has by logistics obtains), and assurance catalyzer and logistics sharp separation, because very short with at least one above-mentioned residence time before separating more fully, gained steam that has helicoidal flow and the single current cyclonic separator that does not have reverse screw are by the granules of catalyst of isolating 50～90% in the gaseous stream.Isolate after the effluent gas, catalyzer is by a stripping zone, at stripping zone, catalyzer with resemble steam and/or rare gas element (as CO, CO
2), the such gas of burning gas or fuel oil gas is handled, and hydro carbons and stripping gas are discharged, and stripped like this catalyzer is transported to first vertical basically breeding blanket with the fluidic form then, and the temperature of this breeding blanket is maintained at about 500～700 ℃.In above-mentioned first breeding blanket, introduce oxygen and/or oxygen containing gas, air preferably, the introducing amount of gas will make the hydrogen product perfect combustion basically that is deposited on the catalyzer, or 90%(is heavy at least) burning.Only a part of carbon product that is deposited on the catalyzer is also oxidized, and 10～60%(of the carbon of embryo deposit is heavy as a result) oxidized, be oxidized to CO basically; By the effusive logistics gas in first breeding blanket in cyclonic separator with the catalyst separating of partial regeneration, thereby, and the temperature of operating relatively low in view of the amount of used oxygen, the content of CO is high especially in the gas.The catalyzer of partial regeneration is transported to second regeneration zone with the anhydrous oxygen-containing gas (as dry air) that provides in addition then.
Second breeding blanket is a vertical reactor basically, and its length L is much larger than its diameter phi, and making length (L/ φ) is 3～90, its inside refractory liner.Introduce the catalyzer of partial regeneration in the bottom of second breeding blanket.The regeneration temperature of second breeding blanket usually above 65 ℃, can reach 1000 ℃ than the first breeding blanket height.Above-mentioned second process catalyst regeneration step is carried out CO in the gas of formation under the situation that excess of oxygen (preferably dry air) exists greatly
2Content high especially.The catalyzer that obtains thus, it is deposited on lip-deep most of carbon and has all removed, because the weight ratio of carbon deposit and catalyzer generally is lower than 0.04%.Cyclonic separator with outside, second breeding blanket separates such regenerated catalyzer with the gas phase steam flow; Then generally 600 ℃ (or average 700 ℃)～950 ℃, the pipe racks of the dirty extension of catalyzer by control valve for fluids is housed is got back in contactor one mixing tank.
F.C.C. technology of the present invention can be used general catalyzer any commonly used used in this technology; But zeolite based catalysts is better.For the dual catalyst regeneration system, though at high temperature, thermostability is not a underlying condition under the situation that moisture exists, zeolite based catalysts Heat stability is good, particularly Heat stability is good under the situation that steam exists.In fact the regeneration of second step is at high temperature, under anhydrous basically condition, carry out, in light of this situation, in the cracking reaction process, be deposited in the first step regenerative process that hydrogen contained in the hydrocarbon molecule very heavy on the catalyzer carries out under temperature condition relatively stably and almost all change into steam.Usually, the ratio of the contained carbon deposit of catalyzer of the first step regeneration output is that 0.8～5.4%(is heavy), in this step, the ratio of last hydrogen in fact often is zero.
According to special embodiment of the present invention, if necessary, can be at multi-point injection dry oxidation gas (generally being dry air) along the combustion zone that forms by the second revivifier high temperature, so that keep and want the incendiary carbon ratio always, oxygen is excessive greatly.
According to the present invention, the various devices of Shi Yonging promptly simultaneously: spray on the plane of the regenerated catalyzer feed of heat and the system of raw material dispersion oil, catalyzer and raw material also flow to the conversion zone that passes through down, the fast separation device of catalyzer and product, with two sections catalyst regenerators, to guarantee to increase significantly the productive rate of benzoline, particularly increase the productive rate of stop bracket gasoline.
Improve the radial distribution of catalyzer, do not have back-mixing, the mobile comparing class of fluidic is similar to plug flow, the sharp separation of catalyzer and product, just can increase selectivity, reduce the generation of charcoal and gas and can make its volume that reduces reaction zone, thereby reduce investment cost and catalyzer investment.
Brief description of drawings
Fig. 1 schematically illustrates a possible embodiment of the F.C.C. device according to the present invention.
Fig. 2 is spray and raw material dispersion oil one of the device more detailed figure of embodiment preferably.
Fig. 3 is at the stripping reactor of the outlet of cyclonic separator and the detail drawing of quick drain device, and cyclonic separator is used for separating the gas and the granules of catalyst of the mixture that the F.C.C. reactor discharges.
The present invention relates to (a) in the fluid catalytic cracking of reaction zone (1) hydrocarbon feed with (b) in the reclaiming process of two breeding blankets (22) and (37) catalyzer, under reaction zone (1) raw material and the catalyzer and the flow direction.
Technology of the present invention comprises the steps (seeing Fig. 1 or 2):
By at least one pipe (2) at the top of reaction zone atomizing of liquids raw material, pipe (2) is subdivided into the conduit (9) of many independent perpendicular, a kind of equipment (Fig. 2 114) is housed raw material be sprayed into mean size, be preferably 100 microns in the lower end of conduit (9), better be about 50 microns droplet, in spray site, the speed of raw material better is 10～100m/s;
Material district on reaction zone (1) top, according to introducing the back, by breeding blanket (37), by at least one pipe (3) or (4), beginning is introduced granules of catalyst at 600～950 ℃, so that at last catalyst fluidized bed of material district formation of crossing;
Feed the air-flow that one makes progress, by above-mentioned beds, with this so that promote the granules of catalyst vent pipe (10) by many perpendicular downwards, thus catalyst transport is arrived reaction zone, the standpipe (9) of each injection raw material is all coaxial with catalyzer vent pipe (10), the equipment of each atomizing of liquids raw material all be contained in vent pipe upper end near, so that form feedstream and catalyst stream at above-mentioned vent pipe (10), and complete gasifying liquid raw material, raw material is closely mixed with catalyzer, better be less than 1/2 second the duration of contact of raw material and catalyzer in vent pipe, is preferably less than 0.1 second;
At reaction zone,, keep raw material to contact 0.1～10 second residence time of raw material, best 0.2～4 second with catalyzer at 450～700 ℃;
Be increased in the catalyzer of bottom (12) of reaction zone and the speed of reactant flow, the bottom of above-mentioned reaction zone is made up of at least one shrinkage cavity pipe, and its shape resembles frustum cone or bodies such as four sides cone or any other, and it top down, 5～30 ° of semiapex angles, best 7～15 °;
From reaction effluent, isolate 50～90% catalyzer at least one first disengaging zone (13), provide the residence time less than 1 second, speed at the inlet gas phase effluent of above-mentioned disengaging zone is 10～40 meter per seconds, to produce a kind of screw type vapour stream that reverse screw does not take place, remaining most of catalyzer is along with gaseous stream moves, separate with reactant flow at least one other disengaging zone (14) then, disengaging zone (14) is anti-flow pattern, promptly has the reverse screw that produces by spraying into gas stream in above-mentioned other disengaging zone;
Use the gas stripping, from catalyzer, remove most of hydro carbons;
Use gas, granules of catalyst is upwards carried (at least 450 ℃ of this Buwen's degree),, these catalyzer are delivered to first breeding blanket (22) by pipe (23) at 150～300 ℃;
With fluidizing (or close phase) bed form, in temperature T
1(about 500～700 ℃), in the presence of hydrogen or oxygen containing gas, finish the first step catalyst regeneration, so that be deposited in the product on the catalyzer contained at least 90% hydrogen, preferably whole basically hydrogen burnings fall, and being deposited on the catalyzer, with the carbon that the carbide form exists, 10～60%(is heavy) all oxidations, major part is oxidized to-carbonoxide;
Most of gas at first catalyst regeneration zones is removed;
From the first breeding blanket recovery part regenerated catalyzer, and with oxygen base load gas or oxygen containing gas, basically there is not steam, the catalyzer of partial regeneration is upwards carried, by the top of pipeline (36) to second breeding blanket, the shape of second breeding blanket resembles a basic vertical also tubular zone (37) of elongation, and its L/ φ (L is a pipe range, and φ is a caliber) is 3～90.In second breeding blanket, with contain oxygen, anhydrous resurgent gases is 650～1000 ℃ temperature T basically
2, T
2＞T
1, handle above-mentioned catalyzer, to obtain the regenerated catalyzer, it is heavy that its carbon content is not more than 0.04%(), produce high CO simultaneously
2The gas of content.In the above-mentioned second step regenerated process, use above-mentioned carrier gas, catalyzer is upwards carried by breeding blanket (37);
Reclaim gas-catalyst mixture from second breeding blanket (37), from gas, isolate catalyzer, and above-mentioned regenerated catalyzer is sent back to catalytic cracking reaction zone (1) by at least one conduit (3) or (4).
The present invention also relates to a kind of catalytic cracking and catalyst regeneration device, it comprises as lower section (seeing Fig. 1 and 2):
An elongation, the reactor of perpendicular (1);
On the top of reactor, has the pipeline (2) of a feeding liquid raw material at least.Pipeline (2) is subdivided into conduit many perpendicular, separated from each other (9) again.There is the nozzle that sprays above-mentioned raw materials oil (Fig. 2 114) lower end in conduit (9);
At least two vertical substantially arms (3) and (4), general valve (7) and (8) of being equipped with, horizontal wall (113-a of Fig. 2) is above so that granules of catalyst is incorporated into, the storage tank on reactor (1) top or material district;
Near the divider of at least one fluidizing agent horizontal wall (113-a of Fig. 2) (Fig. 2 113);
The pipe of many discharge granules of catalyst (10), granules of catalyst in the above-mentioned storage tank is discharged into reactor, the arrangement of above-mentioned vent pipe will be managed each raw material, and to enter conduit (9) coaxial with delivery pipe (10), and make each raw material nozzle near delivery pipe (10) upper end, therefore, the nozzle of assembling forms contacting and the mixing zone of a raw material and catalyzer with vent pipe (10);
The bottom of reactor (1) has a funnel at least, and its shape resembles a tack cone or pyramid or any similar shape, its top down, semiapex angle is 5～30 °, best 7～15 °;
At least one is disengaging zone (13) just, it comprises that one or more lists dredge cyclonic separator, directly pass through, react effusive granules of catalyst and oppositely do not spiral, the first above-mentioned disengaging zone is in the reactor outside, reclaim granules of catalyst by at least one vertical substantially pipe (15) from above-mentioned first disengaging zone;
At least one second disengaging zone (14), its separating reaction effluent, most of remaining granules of catalyst is fed forward again, granules of catalyst reclaims granules of catalyst by at least one pipe (16) (preferably perpendicular) by above-mentioned second disengaging zone, reclaims reaction effluent by at least one pipe (16-a);
A reactor, promptly district (17) introduces gas by at least one pipeline (among Fig. 3 221), by pipe (16) and (15) catalyzer is sent into this district (17);
Pipe (20) is used for granules of catalyst is discharged into the outside of district (17) managing (20) valve (21) generally being housed;
The pipeline of perpendicular (23) is used for promoting the granules of catalyst that replenishes by pipe (20), and it is to promote with the lifting gas of introducing by pipeline (23a), so just granules of catalyst is transported to first regeneration reactor (22);
First regeneration reactor (22), it is equipped with a screen or any other equivalent of the apparatus (27a), with support catalyst bed (25), a feeding line (26) is arranged, and is used for supplemental oxygen or oxygen-containing gas.A device (28) is arranged, and it is equipped with a cyclonic separator at least, with divided gas flow and granules of catalyst;
Gas discharge line (29) generally is equipped with a valve (30) and conduit (33), is used for catalyzer is drawn from district (22);
Pipe (34) communicates with conduit (33), and valve (35) generally is housed, and is used for making catalyzer to flow downward;
Vertical and on catalyzer conduit (36), sending conduit (36) to by the conveying gas (promptly promoting gas) of pipeline (36a) introducing;
The tubular type catalyst regeneration reactor (3) of perpendicular, its L/ φ is than being that 3～90(L is the length of tubular reactor, φ is its diameter), reactor is equipped with a nozzle at least, to spray into regeneration gas;
Gas-catalyst mixture outfall pipeline (38);
Device (5 and 6), be used for separating catalyst and gas, it has two cyclonic separators at least, generally is placed on the outside of regeneration reactor (37) and reactor (1), catalyzer is told from above-mentioned separator, adds in the reactor by feed conduit (3) and (4).
According to an explanation possible enforcement illustration (1) of the present invention, hydrocarbon feed, as gas oil or high boiling hydrocarbon, be to introduce by pipeline (2) on the top of vertical reactor, at high temperature the catalyzer after the regeneration is also introduced on the top of reactor (1) by pipe (3) and (4) of the downward extension of outside cyclonic separator (5) and (6), pipe (3) and (4) is equipped with valve (7) and (8), with the control flow velocity, hydrocarbon feed is sent forth at many nozzles injection system (9), and the part vaporization, introduced this embodiment among Fig. 2 in more detail.Raw material promptly disperses preferably among the embodiment at one, and contacts fast at the many nozzles that extend downwards-mix with thermocatalyst in many drainage conduit (10) of mixing tank (11).Such embodiment has been described among Fig. 2 in more detail.Outlet in contact mixer (11), regenerated catalyzer and raw material carry out the utmost point and conduct heat rapidly under the high temperature, and the latter vaporizes fully, and last running owing to being subjected to so anxious heat thermo-cracking takes place.In this common rapid mixing device, general maximum 0.5 second of the duration of contact of raw material-catalyzer was most preferably less than 0.1 second.
After the mixing, the temperature that hydrocarbon vapours/the catalyzer suspended substance is reached can be 450～700 ℃, and its composition with desired transformation efficiency and raw material is relevant.Hydrocarbon vapours/catalyzer suspended substance flows through reactor (1) vertically downward then, and according to conditions such as the required service temperature and the residence time, the cross-sectional area of reactor (1) can gradually change.The high temperature suspended substance contains steam, diluent gas and the mobile catalyzer of generation.The speed that suspended substance flows through reactor is corresponding to the speed near the flow condition of piston flow.The downflow system particularly advantageous, it makes catalyzer significantly reduce with respect to the relatively sliding of carrier gas.Hydrocarbon feed is approximately 0.1～10 second in the residence time of reaction zone (1), best 0.2～4 second.In order further to increase the viscous flow of catalyzer, to reduce total reaction volume, plate washer or filling material (not shown) can be equipped with in the inside of reactor (1), as Raschig ring, saddle packing, Intelux filling etc.
Then, hydrocarbon steam/catalyzer suspended substance quickens in the convergent system (12) of one or more cones or prism or equivalent shapes, the semiapex angle of cone is 5～30 °, be preferably 7～15 °, suspended substance enters the separator of separator 13(or several parallel connections thus), make the residence time be less than 1 second, with a cyclonic separator (or cyclonic separator of several parallel connections), employing is directly passed through, and does not have the reverse spiral of so-called single current, can reach the purpose of sharp separation preferably.Fig. 3 at length expresses these possible embodiment, and wherein, the cyclonic separator of single current is horizontal.In this section, separate (but efficient is higher than 50%) (less than 1 second) more rough first time in a short period of time.This effluent is by the single current cyclonic separator, do not produce reverse screw, effluent flows out, one or more snippets second disengaging zone that enters in parallel or placed in-line, it is by general so-called reversed flow cyclonic separator (it is known technology), and catalyzer is separated fully.Effluent still moves with the effluent that the first sharp separation section (13) is come.Reaction effluent is discharged from pipeline (16) (two).Catalyzer passes through the tube drainage of first separator (15) and second separator (16) extension downwards to the reactor the inside, with the hydro carbons that solid powder moves, generally uses steam stripped at this stripping.The device of this structure can all externally be installed reactor (1), and reactive moieties is easy to maintenance.
The general diameter in bottom of reactor (17) is little than top, and stripping zone (18) is arranged at the bottom, introduces stripping gas in the bottom of stripping zone, as steam, rare gas element (CO, CO
2...), burning gas or fuel gas.Be generally the top that first and second separation systems (19) are used for reactor, from granules of catalyst, to isolate steam stripped hydrocarbon product and stripping gas.Stripping gas and steam stripped hydro carbons flow out separator (19) by outlet line (representing on the figure).According to another possible embodiment, when the top of stripping reactor (17) too little, so that in the time of can not including an additional separation system (19), the stripping effluent can be at independent separator row (14), serial or parallel connection, directly use the effluent processing of flowing out from this reactor, the direct coupling device between first separator (13) and the above-mentioned separator row (14) can omit arbitrarily.This stripping operation is general technology, does not need further introduction at this.
After the stripping, catalyzer is topped by carbon deposit, and it, is emitted by the drainage conduit (20) that valve (21) are housed from the bottom of stripping reactor (17) at least 450 ℃, and dress valve (21) is in order to control the flow velocity of solid particulate.Almost the drainage conduit of being filled up by solid particulate (20) wants enough high, so that the solid tamper that forms plays connection, and makes the pressure equilibrium separately of conversion zone and RS Regenerator Section thereafter.
After the stripping, still by deposits of coke topped catalyzer be transported to the bottom of first RS Regenerator Section (22) by means of feeding gas from unloading dipleg (20), to the bottom of heavy straight lifter (23) basically.Can clean by valve (39).The feeding gas here (pipeline 23a) can be made up of the oxygen annexation of the air that gives heat, superheated vapour and heat, and temperature is 150 to 300 ℃, the about 2-3 crust of pressure.Gu introducing the amount of the feeding gas of above-mentioned lifter should be enough to form with catalyzer-/the gas suspension thing, its density should make catalyzer have to upwards flow along pipeline (23), is discharged into the bottom of first RS Regenerator Section (22) thus.
First RS Regenerator Section of catalyzer is made up of for bed (25) a solid stream, and it is known technology, must not do to describe with regard to details here more.
The bottom that the required oxygen rich gas of catalyst regeneration is introduced fluidized-bed by pipeline (23) and/or the pipeline (26) that links to each other with gas distributor (grid or porous tube wall 27a) (hole 27).
The top (31) that elementary and auxiliary (28) cyclone separation system is contained in reactor (22) expansion is to separate from the burning gas that is rich in CO and by the granules of catalyst of its conveying.The resurgent gases that is rich in Co is discharged by pipeline (29) from reactor (22), a valve (30) is housed on the pipeline (29) comes control pressure.
First regeneration step of carrying out in reactor (22) is being lower than under the lower condition of the concentration of 750 ℃ relatively mild temperature and oxygen to be finished, and selecting like this is in order to make the contained hydrogen of deposits of coke that forms on catalyzer have 50%(preferably basically 100% at least) obtain burning and a part of carbon that burns (weight with carbon is expressed as 10～60%).The concentration of operational condition and oxygen is enough to temperature maintenance with intensive fluidized-bed (25) within about 500～750 ℃.Using this comparatively gentle regeneration condition is steam to occur for fear of combustion of hydrogen, because it can reduce activity of such catalysts greatly.Like this, first RS Regenerator Section that is positioned under the lesser temps has just produced the very high combustion gases of Co content.This has just been avoided Co in discharge region and the subsequent combustion in cyclonic separator (28) of solid stream for bed (25).In the dirty well heater (not shown) of being furnished with a Co of discharging pipeline (29), so that change into CO at Co
2The time produce pressurised steam.Before above-mentioned Co combustion step, also can be equipped with a powder recovering device, it is a known technology.
Thereby first RS Regenerator Section can be at the O of such temperature, pressure and reduction
2Carry out under the concentration,, finally burn in pyritous second RS Regenerator Section then so that the coke of a certain proportion of low hydrogen content is stayed on the catalyzer.Suggestion will the burning of carbon reduce to the quantity that the most of burning of hydrogen just in time needs in first RS Regenerator Section under being lower than 750 ℃ lesser temps.
In fact its residual coke does not have hydrogen or only contains the catalyzer of the partial regeneration of a small amount of hydrogen, discharge from concentrated type fluidized-bed (25) by the drainage conduit (33) that is connected with the descending extension leg (34) of an outer bend, this extension leg (34) is furnished with a valve (35) and flows with the control solid.This descending extension leg that keeps intensive pulverulent solids stream to pass through finishes in the vertical tube of a rising (36), feeding gas enters this vertical tube bottom with appropriate flow, and its amount is advisable along pipe (36) is upwards mobile so that the density difference in pipeline (36) and (34) can cause solid materials.This feeding gas is an oxygen containing incombustible gas, is generally air.It preferably must not have steam fully.
When fluidized-bed is promoted by oxygen containing feeding gas, catalyzer enters separate reactor (37), it preferably should be furnished with in the high temperature-resistant liner, here, and at high temperature, promptly be higher than the separation regeneration of carrying out subordinate phase under 650 ℃ and the situation that do not have steam to exist basically.The amount of oxygen should be enough to burn by coke and keep regenerative response at high temperature to carry out, make simultaneously CO basically perfect combustion generate CO
2For the high temperature regeneration that is undertaken by the burning of whole residue carbon limiting temperature not, it can reach 1000 ℃.Like this, the temperature of second RS Regenerator Section just reaches almost easily removes needed temperature with all sedimentary residue charcoals on the granules of catalyst, so that reduce the coke content on the catalyzer, makes it to compare less than 0.04% with the weight of catalyzer.The second separation regeneration stage at high temperature finishes in the vertical tube type reactor (37) that rises.Employed catalyzer, is sent into 0.5 to 10m/s-best 1 to 5m/s surface velocity as the suspended substance in the such resurgent gases of air by this quick revivifier.The height/diameter of revivifier is than must be in 3～90 scope, and best 10～25.This quick revivifier is furnished with the nozzle (not shown) of the resurgent gases of spraying in the bottom, also be furnished with to spray into secondary recycling gas-the be generally nozzle of dry air-usefulness on whole height.
With respect to the total volume and the capacity of revivifier, owing to saved needed volumes such as being generally used for the descending extension leg of bellows, sparger, discharge region and whirlwind.The present invention has significant big available space.Because the result of the high passage flow velocity and/or the height/diameter ratio of reactor (37) has also improved the contact efficiency between resurgent gases and the catalyzer, improved distribution and reduced channel and air-teturning mixed phenomenon.
And, become and be similar to mobile oarse-grained separation and the local particle that not holomorphosis occurs avoided in the form of piston more.This makes the control of subsequent combustion in the second regeneration stage be more prone to, no longer need to resemble the refrigerating unit that uses steam or water traditional flow process, thereby no longer lose catalyzer and reduce their activity, and make refractory materials and shell be subjected to major injury.
Be suspended in the catalyzer of the regeneration in the combustion gases, by being positioned at a little less than the vertical pipe (38) at the top of reactor (37) to come out, so that the wearing and tearing that make described flow direction change 90 ° zone are reduced to minimum value by side discharge.Suspended substance is accelerated in pipe (38) and is separated at first segregation section of being made up of one or several cyclonic separator in parallel, and resurgent gases is separated with the catalyzer of at high temperature having regenerated in cyclonic separator.Pressurized gas leads to second segregation section (6) efficiently then, and it has one or several cyclonic separator, but serial or parallel connection, and method is a known technology.
Cyclonic separator (5) and (6) can be installed in outside the reactor (37) that is used for second RS Regenerator Section, to avoid the difficulty of pyrometallurgy.CO
2The burning gas that content is very high, each valve by keeping this device pressure is discharged from cyclonic separator (5) and (6), then can be in a well heater (not marking) be used for production process steam.
Granules of catalyst is discharged from second RS Regenerator Section of high temperature and low carbon content, and its carbon content is preferably lower than the weight of 0.04%(by catalyzer).Temperature is higher than descending extension leg (3) and (4) adding mixing-contactor (11) of catalyzer by separating series (5) and (6) of regeneration of the pseudocritical temperature of charging.Inner have enough height by means of flowrate control valve (7) and (8) the maintenance intensive mobile supporting legs of powder solid (3) and (4), with the pressure equilibrium of assurance device.
In contact-mixing tank (11), the catalyzer of the regeneration of heat does not remain on fluidized state by spray into (the marking among Fig. 1) of ventilation gas, and this ventilation gas is the hydro carbons that is less than 4 carbon atoms, or other available gas, as rare gas element etc.Temperature is higher than the catalyzer of regeneration of heat of the pseudocritical temperature of charging and discharges by the drainage conduit (10) that can directly contact with hydrocarbon material.A catalyzer take-off pipe (39) is equipped with in the bottom of stripping zone (18); Consistent with traditional device, the live catalyst that replenishes adds by the charge level that adds of pipeline (40) in first RS Regenerator Section (25).
Fig. 2 has represented to be positioned at the device concrete equipment in the present invention that is used to spray and disperse the hydrocarbon charging at the vertical reactor of descending extension (101) top in further detail.As described, descending extension supporting leg (103) and (104) of the catalyzer of at high temperature regenerating, being flowed into by second RS Regenerator Section (132) that forms hoisting type vertical transport circuit by one (or parallel connection is several) series of separate device reach the top of reactor (101), the tripping device here is made up of cyclonic separator (105) and (106) of outside, and are equipped with valve (107) and (108) to control solid flow.The catalyzer of the regeneration of heat is collected in the bank and (is positioned on the water wall 113a), forms one by spraying into the beds that ventilating gas keeps intensive fluidized state by a sparger (113) at least at this.This sparger (113) is made up of for example a screen or one group of water jet standpipe, and it is a traditional way.Form by rare gas element or from cut series distilled lighter hydrocarbons (oil fuel) or other any making in for example this device downstream by the ventilation gas that above-mentioned sparger (113) sprays in fluidized mixture or gas phase media.A kind of selectable steam according to the present invention sprays in the limit that can allow at the hydrothermal stability of the catalyzer that high temperature regeneration is crossed and carries out.The catalyzer of this heat and fluidized gas flow out downwards by some material pipes (110).
Give hot upper reaches (in the system that does not mark) and can add that the liquid hydrocarbon of a certain amount of dispersion steam is material bed to be divided into some charging slide units (102) addings of leading to the feed-pipe (109) discharge tube (110) in by one.Tail end at these feed-pipes (109) is equipped with some nozzles (114), and its type is general.Hydrocarbon material sprays into the dispersion steam of suitably replenishing in many nozzles injection system as far as possible carefully, and its drop size that is to say less than the average grain of regenerated catalyzer, usually less than 100 microns, preferably less than 90 or even less than 50 microns.Spray with 10 to 100m/S speed and begin vaporization from nozzle (114) through drop at this.
Form a center circle cone jet on the top (A district) of each discharge tube (110), the gob that its disperses the ring by the catalyzer circulation of high temperature regeneration to water, catalyzer is carried along each discharging tube wall by fluidized gas.Two almost parallel flowing are formed simultaneously at the top (A district) in each discharge tube (110), are respectively coaxial the flowing of catalyzer that drop and high temperature regeneration are crossed.The contact of two materials flows is limited to above-mentioned A district relatively, and the heat transfer between granules of catalyst and the drop carries out with radiation mode basically, but the advantage of two sections high temperature regenerations just is to make above-mentioned A district flash heat transfer.Main part vaporization is finished immediately in nozzle (114) exit.With this special type of heating make drop and at high temperature mobile solid (granules of catalyst) spray together, the temperature of droplets of feed rises rapidly, is unfavorable for burnt generation reaction like this with regard to helping scission reaction.Importantly make drop as far as possible little, so that make heat exchanging process not be subjected to from the restriction of drop external-to-internal thermodiffusion.Though heat exchange is mainly finished by the radiation in above-mentioned A district, do not get rid of other heat exchange mode yet, promptly conduct heat by heat conduction and/or convection current.
Yet said, radiation heat transfer is occupied an leading position in this jet apparatus, 1 is like this in zone as defined above at least.This may make and be significantly reduced by the caused heap phenomenon of the direct contact of the catalyst particles intergranular of heat.This heap can play the solid thermophore and the liquid gob of not vaporizing.
Bottom (B district) in each discharge tube (110), these the two bursts of materials flows of raw material and catalyzer mix under the influence of dispersion and part vaporization closely, vaporize substantially at the drop of A district hydrocarbon in fact in the past.Contact between desirable catalyzer in B district and hydrocarbon feed and mixing closely, more effective than the influence that basic vaporization produced of former A district drop.In the B district of each discharge tube (110) and since the close mixing between drop and the catalyzer that high temperature regeneration is crossed with contact, and finish the vaporization of drop.For realizing the flash heat transfer in above-mentioned B district, such mixing is essential with contacting closely.On the other hand, flow downward and to avoid the back-mixing of catalyzer, help the renewal of catalyzer around nozzle, can avoid, can avoid suspended substance nozzle injection place and near the intensive phase of formation, as if in the up reactor of general feed system with F.C.C., taken place such.By with this structure with because the result that flows downward reduces to minimum value with the back-mixing of nozzle injection place, the formation of coke and caking phenomenon and coke build-up also significantly reduce on the catalyzer.All feed systems that are deposited in the up reactor that generally is used for F.C.C. of this caking phenomenon and carbon are very deleterious but are unavoidable.
In regional A and B, heat passage can extremely promptly realization the between the catalyzer that high temperature regeneration is crossed and the drop of segmentation.The length of discharge tube should make and be no more than 0.5 second the duration of contact of feed/catalyst and be advisable, and preferably is shorter than 0.1 second.This extremely fast heat passage in mixing device easily, on the surface of drop, caused an initial thermal shock, this makes the light constituent of raw material vaporize fully and contained last running and bituminous matter structure thermo-cracking.So initial thermal shocking needs, and the raw material that contains a great deal of last running and/or bituminous matter structure for processing is favourable.And then see that the cracking of this light constituent is good, it is unfavorable for tying the charcoal reaction.The present invention has many nozzles of downflow system short mix-contactor and not only is applicable to the processing heavier feedstocks owing to producing initial thermal shock, and can significantly reduce air-teturning mixed phenomenon.
Outlet in descending extension tube (110), hydrocarbon steam/catalyzer suspended substance flows through reactor (101) vertically downward, the cross section of this reactor can gradually change, and obtaining operational condition such as temperature required and residence time, and makes flow state approach piston flow.
Fig. 3 represents the tripping device of a catalyzer and reacting fluid.Hydrocarbon steam/the catalyzer that suspends is 5 to 30 ° at a semiapex angle, be preferably 7 to 15 ° by being accelerated in the body (212) that contracts, enter an initial separator (213) then.In Fig. 3, the primary separation device only comprises a cyclonic separator that has straight channel (213), and cyclone is single current and has the tangent line outlet, here installs for level.Other possible equipment of selecting for use of the present invention can comprise a series of above-mentioned cyclonic separators, side by side level or vertical the installation.In the single current cyclonic separator of this class band straight channel, steam is done spiral flowing around drum just as shaft centre line (211), said effluent enters by inlet (210) tangent line and has the not reverse characteristic that produces of spiral-line, and these are different with traditional anti-stream cyclonic separator.The speed that air communication is crossed inlet (210) must be controlled at 10 in the scope of 40m/S, flows so that produce genuine spiral-line under the centrifugal action that is produced, and granules of catalyst is flattened under the effect of shell.Cross coaxial pipe core (209) discharge that runs through inside and outside shell (213) with the air communication that solid particulate separates.Solid is down by vertical bottom tube (215) discharge substantially.The residence time of this class cyclonic separator may be shorter relatively, only less than one second, is suitable for elementary roughing out, and however, efficient then is higher than 50%, can reach 90%.In order to improve the efficient of above-mentioned primary separation, must supply with a certain amount of air-flow to the solid particulate that flows downward by bottom tube (215), this amount can reach 10% of this air-flow total flux.Be connected to the helicoidal flow of not swinging in the cyclonic separator of straight channel in this class, not only can provide the residence time to be shorter than 1 second sharp separation, and since spiral-line do not swing to and air-teturning mixed phenomenon reduced to Schwellenwert.This primary separation fast might reduce can produce dysgenic overcracking to the selectivity of cracking reaction.On the other hand, this cyclonic separator that is used for primary separation (213) can only partly run through stripping zone inside (217); Take this arrangement to help the complete location, outside of reactor (201), have the advantage of easy maintenance reaction zone.
Outlet (209) can be opened in stripping reactor or zone (217), but preferably directly is connected in the ingress of second separation system (214) by pipe (224).Second separation system is formed to several segregation sections by one, each section is the general reversed flow cyclonic separator of some serial or parallel connections, this just provides catalyst separating very completely, and catalyzer also can be transported to the outlet (209) of the first sharp separation section once more by air-flow.Here, outlet (209) directly by pipeline (224)-preferably essentially horizontally-inlet part that separates series (214) with the second stage is connected.Generally be equipped with one on the top of stripping reactor and separate level to several by what known general reversed flow cyclonic separator was formed by one to the device (219) of several separation and stripping effluent they each, at different levels for arranged side by side and/or be connected in series.
Here the outlet (208) of tripping device (214) is only from reaction zone (201) ejecta materials flow, and the outlet of tripping device (219) is then only from stripping zone (217) ejecta materials flow.These gas material outlets (207) and (208) are equipped with regulated valve (237) and (238) to jointly control the pressure equilibrium of reactor plane or stripping zone (217).
Stripping reactor (217) opens usually gradually on top, is furnished with plate washer (220) in its bottom (218) to improve the efficient of stripping operation.A kind of such as steam, rare gas element (CO, CO
2, N ...) stripping gas of combustion gases or burning gas and so on sprays into by a suitable sparger (221) (grid or jet pipe) in the bottom of stripping zone.
Stripped catalyzer is discharged by following drainage conduit (239) adverse current from reactor (217).
Errata
Errata
Errata
Errata
Claims (9)
1,--one (a) is used at hydrocarbon feed catalytic pyrolysis and the technological process that (b) is used in two breeding blankets (22) and (37) regenerated catalyst the fluidized-bed of reaction zone (1) and the downward also stream of catalyst stream, this process by (seeing Fig. 1 and Fig. 2) liquid material on the top of reaction zone (1) step such as spray into of the pipe (2) by at least one arm (9) that is divided into some perpendicular form, the injection apparatus (among Fig. 2 114) of droplet material liquid is equipped with in the lower end of arm
--temperature range is the bank that 600 to 950 ℃ granules of catalyst enters reaction zone (1) top, as after this will illustrating, catalyzer from the breeding blanket (37) by at least one conduit (3) or (4), so that in above-mentioned bank, form a catalyst stream movable bed layer
--be the downward drainage conduit pipe of the granules of catalyst that makes bed by a series of perpendicular, (10) flow, and to the greatest extent upwards being circulated by above-mentioned catalyst bed, a kind of gas therefore granules of catalyst is sent into reaction zone itself, be used for each vertical tube that feed liquid is sprayed, (9) all have and the catalyzer drainage conduit, (10) identical axis, each feed liquid is sprayed apparatus and all is positioned near the drainage conduit upper end, with at above-mentioned material pipe, (10) obtain one feedstream and one granules of catalyst materials flow in and the feed liquid and mix closely of vaporizing fully with granules of catalyst
--in above-mentioned temperature is 450～700 ℃ reaction zone inner sustain raw material and the contact between the catalyzer, and the residence time of material is 0.1 to 10 second, is preferably 0.2 to 4 second,
--be increased in the catalyzer of reaction zone bottom (12) and the flow velocity of reaction mass, said bottom resembles frustum of a cone by at least one shape or butt funnel prismatic or any other respective shapes is formed, the tip is 5 to 30 ° with semiapex angle down, is preferably 7 to 15 °
--at least one first disengaging zone, (13) in the granules of catalyst of reacting material flow is isolated 50% to 90%, the residence time was less than one second, the speed of air-flow in ingress, above-mentioned disengaging zone is 10 to 40 meters of per seconds, so that do not having to produce the spiral mobile of steam under the mobile situation of swinging to, the major portion of remaining granules of catalyst is wrapped up in by air-flow to be taken and other the separator of swinging to types of flow at least one, (14) from reaction mass, separate in, separator for example by helical flow being swung in above-mentioned disengaging zone jet flow stream
--remove the most of hydrocarbon flow that promotes by stripping gas in the granules of catalyst,
--the air-flow that by means of one temperature is 150～300 ℃ is upwards delivered to one first breeding blanket (22) by a conduit (23) with granules of catalyst (in this stage, at least 450 ℃ of temperature),
-in fluidized-bed, in temperature T
1Finish first regeneration step of catalyzer, temperature T
1From 500 to 750 ℃ of scopes, the gas that oxygen is arranged or contain molecular oxygen exists so that make the hydrogen at least 90% that exists in the catalyzer, preferably all burnings, and make 10～60% (W) of the carbon that exists with the carbide form on the catalyzer mainly be oxidized to CO,
--remove most of gas from first catalyst regeneration zones,
--the catalyzer of regenerating from discharge section ground, said first breeding blanket, in order to the gas of oxygen or molecule-containing keto is carrier gas-do not have the basically steam-it is upwards delivered to the bottom of second breeding blanket by pipeline (36) of matrix, this district is shaped as vertical substantially long tube (37), (L is a pipe range to L/ φ, φ is the diameter of pipe) ratio ranges from 3 to 90, catalyzer in second breeding blanket with the gas of molecule-containing keto-do not have basically water-processing, temperature T
2Be 650 to 1000 ℃, T
2Be higher than T
1, in order to produce CO
2Make catalyzer contain the coke of no more than 0.04% (W) after the very high gas of content, and by means of said carrier gas, through said second breeding blanket (37), with catalyzer upwards sent breeding blanket (37) and
--discharge gas-catalyst mixture from second breeding blanket (37), from gas, isolate granules of catalyst and will be that the catalyzer of 600 to 950 ℃ regeneration is delivered to catalytic cracking reaction zone (1) by at least one conduit (3) or (4) in this phase temperature.
2 ,-and according to the technological process of claim 1, it is characterized by: material gives heat before entering reaction zone (1) under from 350 to 450 ℃ temperature.
3 ,-and according to the technological process of claim 1 or 2, it is characterized by: catalyzer has a zeolite matrix at least.
4 ,-according to the technological process one of in the claim 1 to 3, it is characterized by: the resurgent gases of using in second breeding blanket is dry air.
5 ,-and finish the device of catalytic cracking and catalyst regeneration process according to claim 1, it comprises (seeing Fig. 1 and Fig. 2):
The reactor (1) of-one perpendicular elongation,
-at least one pipe in the receiving fluids charging of reactor top (2), said pipe are subdivided into the arm (9) that a series of each comfortable lower end are furnished with the perpendicular of the nozzle (Fig. 2 114) that is used for spraying said charging,
-at least two are used for granules of catalyst is introduced in the container that forms on the horizontal wall (113a) on reactor (1) top or conduit (3) and (4) of bank,
-at least one is arranged near the gas distributor (Fig. 2 113) the horizontal wall (Fig. 2 113a),
The granules of catalyst drainage conduit (10) that-a series of and said container is connected with reactor itself, said drainage conduit is so assembled, so that each feed-pipe (9) has identical axis with drainage conduit (10), so that each charging nozzle is positioned near the upper end of drainage conduit (10), all nozzles (9) and drainage conduit (10) just formed raw material and catalyzer connect can and the mixing zone
-one reactor bottom that resembles frustum of a cone or truncated pyramid or form by at least one shape by the funnel of other respective shapes, the funnel pinnacle is 5 to 30 ° with semiapex angle down, preferably from 7 to 15 °,
-at least one primary separation district (13) is furnished with one to several cyclonic separators that have straight channel, does not have swinging to of spiral-line here, and granules of catalyst is discharged from the reaction product separation and from above-mentioned primary separation district through at least one conduit (15),
-at least one secondary disengaging zone (14), reacting fluid is separated at this and the most of remaining granules of catalyst that is carried by said fluid, granules of catalyst is discharged through at least one conduit (16) by said secondary disengaging zone, reacting fluid is also discharged by at least one conduit (16a)
-one reactor or by the stripping of catalyst with gas particulate reaction zone (17) to send into by at least one pipe (among Fig. 3 221), said zone (17) be by (16) and (15) this class conduit supply catalyzer,
-conduit (20) of discharging granules of catalyst from zone (17),
-vertical basically pipe (23) that is used for promoting the granules of catalyst of being supplied with by conduit (20) utilizes the lifting gas that is entered by pipe (23-a), granules of catalyst can be transported in first regeneration reactor (22),
-one comprises a grid or other is used for the equipment (27a) of support catalyst bed arbitrarily, the inlet pipe (26) of the gas of oxygen or molecule-containing keto and one are at least by first regeneration reactor (22) that is used for the device that the cyclonic separator of divided gas flow is formed from granules of catalyst (28)
-conduit (29) and conduit (33) of discharging catalyzer from zone (22) of discharging gas,
-conduit (34) that catalyzer is flowed downward that is connected with said pipe (33),
The upward vertical tube of-catalyzer (36) comes feed by carrier gas or the rising gas introduced by pipe (36-a),
-tubular reactor (37) that is used for the perpendicular of catalyst regeneration, the scope of its L/ φ (L is a tubular reactor length, and φ is its diameter) ratio is 3 to 90, this reactor is equipped with at least one and is used for the nozzle of jet regeneration gas,
-pipe (38) that is used to discharge gas-catalyst mixture,
-the device of separating catalyst (5) and (6) from gas are made up of at least two cyclonic separators, and the catalyzer of discharging from these separators is delivered to reactor (1) by conduit (3) and (4).
6 ,-and according to the device of claim 5, it is characterized by: on different planes, be distributed with some regeneration gas spray site along regeneration reactor (37).
7 ,-and according to the device of claim 5 or 6, it is characterized by: sparger (113 among Fig. 2) is made up of a grid or the gas ejector pipe of uniting assembling.
8 ,-according to the device one of in the claim 5 to 7, it is characterized by: granules of catalyst primary separation district (13) comprises the cyclonic separator of a horizontal positioned and the segregation section that secondary disengaging zone (14) comprise some parallel connections or arranged in series at least, and is at different levels by the so-called cyclonic separator composition that flows of swinging to.
9,-according to the device of claim 8, it is characterized by: the reactor (217) that is used for the reactor (17) of Fig. 1 of the granules of catalyst that stripping separates or figure (3) from the reacting fluid of reactor (1) (or Fig. 3 201) also contains an isolating auxiliary disengaging zone of granules of catalyst (among Fig. 1 14) in addition in the bottom expansion and on top, this district (among Fig. 1 14) is by a series of two-stages at least, the cyclonic separator of horizontal positioned (213) is formed, these cyclonic separators are opened on reactor (217) inside, outlet links to each other by the ingress of pipe (224) and so-called auxiliary separation system (214) (among Fig. 1 14), (214 outlet (208) ejects the gaseous fluid of autoreactor (201) to separation system, and reactor (217) includes the separation system (219) that an outlet (207) ejects the gas of removing from the fluid of stripping gas with from granules of catalyst in the top, the pressure equilibrium of whole reactor (217) by valve (237 and (238) regulate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 85104806 CN1009659B (en) | 1985-06-24 | 1985-06-24 | Process and equipment for fluidized bed catalytic cracking |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 85104806 CN1009659B (en) | 1985-06-24 | 1985-06-24 | Process and equipment for fluidized bed catalytic cracking |
| FR8516817A FR2589875B1 (en) | 1985-11-12 | 1985-11-12 | CATALYTIC FLUID BED CRACKING METHOD AND APPARATUS WITH HYDROCARBON CHARGE PRETREATMENT |
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|---|---|
| CN85104806A true CN85104806A (en) | 1987-01-07 |
| CN1009659B CN1009659B (en) | 1990-09-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 85104806 Expired CN1009659B (en) | 1985-06-24 | 1985-06-24 | Process and equipment for fluidized bed catalytic cracking |
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| CN (1) | CN1009659B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1035773C (en) * | 1990-11-15 | 1997-09-03 | 环球油品公司 | Disengager stripper containing dissipation plates for use in an FCC process |
| CN1090530C (en) * | 2000-04-28 | 2002-09-11 | 清华大学 | Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor |
| CN101928589B (en) * | 2009-06-25 | 2013-07-31 | 中国石油化工股份有限公司 | Catalytic cracking method of hydrocarbon oil |
| CN104602803A (en) * | 2012-08-30 | 2015-05-06 | 霍尼韦尔国际公司 | Improved internal cyclone for fluidized bed reactor |
| CN105396518A (en) * | 2015-11-10 | 2016-03-16 | 清华大学 | Coal gasification ash oxidation decarburization combined circulating fluidized bed reactor |
| CN105461497A (en) * | 2014-09-09 | 2016-04-06 | 中国石油化工股份有限公司 | Two-stage regenerating reaction device for preparing low-carbon olefins and aromatic hydrocarbon by converting methanol and/or dimethyl ether and reaction method for two-stage regenerating reaction device |
| CN109195697A (en) * | 2016-06-17 | 2019-01-11 | 陶氏环球技术有限责任公司 | The system component of fluid catalyst reactor assembly |
| CN110678253A (en) * | 2017-05-01 | 2020-01-10 | 法语天主教鲁汶大学 | Apparatus for treating particles in a rotating fluidized bed |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN100345622C (en) * | 2006-05-10 | 2007-10-31 | 中国石油大学(北京) | Method and device for solid alkylation reaction |
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1985
- 1985-06-24 CN CN 85104806 patent/CN1009659B/en not_active Expired
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1035773C (en) * | 1990-11-15 | 1997-09-03 | 环球油品公司 | Disengager stripper containing dissipation plates for use in an FCC process |
| CN1090530C (en) * | 2000-04-28 | 2002-09-11 | 清华大学 | Catalyst inlet device adaptable to gas-solid cocurrent flow descending bed reactor |
| CN101928589B (en) * | 2009-06-25 | 2013-07-31 | 中国石油化工股份有限公司 | Catalytic cracking method of hydrocarbon oil |
| CN104602803A (en) * | 2012-08-30 | 2015-05-06 | 霍尼韦尔国际公司 | Improved internal cyclone for fluidized bed reactor |
| CN104602803B (en) * | 2012-08-30 | 2017-05-03 | 霍尼韦尔国际公司 | Improved internal cyclone for fluidized bed reactor |
| CN105461497A (en) * | 2014-09-09 | 2016-04-06 | 中国石油化工股份有限公司 | Two-stage regenerating reaction device for preparing low-carbon olefins and aromatic hydrocarbon by converting methanol and/or dimethyl ether and reaction method for two-stage regenerating reaction device |
| CN105396518A (en) * | 2015-11-10 | 2016-03-16 | 清华大学 | Coal gasification ash oxidation decarburization combined circulating fluidized bed reactor |
| CN105396518B (en) * | 2015-11-10 | 2018-11-23 | 清华大学 | A kind of combination circulating fluid bed reactor of coal gasification lime-ash oxidation and decarbonization |
| CN109195697A (en) * | 2016-06-17 | 2019-01-11 | 陶氏环球技术有限责任公司 | The system component of fluid catalyst reactor assembly |
| CN110678253A (en) * | 2017-05-01 | 2020-01-10 | 法语天主教鲁汶大学 | Apparatus for treating particles in a rotating fluidized bed |
| CN110678253B (en) * | 2017-05-01 | 2022-04-08 | 法语天主教鲁汶大学 | Apparatus for treating particles in a rotating fluidized bed |
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| CN1009659B (en) | 1990-09-19 |
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