CN1185477A - Fluid catalytic cracking to hydrocarbon by comprehensive equipment of separating and stripping catalyst - Google Patents
Fluid catalytic cracking to hydrocarbon by comprehensive equipment of separating and stripping catalyst Download PDFInfo
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- CN1185477A CN1185477A CN96121397A CN96121397A CN1185477A CN 1185477 A CN1185477 A CN 1185477A CN 96121397 A CN96121397 A CN 96121397A CN 96121397 A CN96121397 A CN 96121397A CN 1185477 A CN1185477 A CN 1185477A
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Abstract
The effective utilization of available stripping medium in an FCC process is increased by using a cyclonic separation method and apparatus to discharge particulate solids and gaseous fluids into a separation vessel from a discharge opening of a central conduit and to withdraw separated gaseous fluids from the separation vessel by contacting the catalyst in the separation vessel with redistributed gases from outside the separation vessel, at least a portion of which enter the separation vessel through a plurality of restricted openings around the bottom of said separation vessel.
Description
The present invention relates to use from gas solid catalyst particle and gas is carried hydrocarbon from catalyzer novel appts carries out the method for fluid catalystic cracking (" FCC ") to hydrocarbon.The invention still further relates in the cyclonic separator of FCC method catalyzer is separated from its mixture with the gaseous state material.
The known and common application of the cyclone separation method of separate solid from gas.An application that is widely known by the people especially of this method is in hydrocarbon processing industry, wherein beaded catalyst contact with the hydrocarbon gas reactant chemical conversion that realizes the air-flow component or with the contacted particulate physical change of air-flow.
For making air-flow contact and realize gas and the contacted method of particle with final isolating granules of catalyst logistics, the FCC method is its example being familiar with.FCC method and use therein tripping device have comprehensive narration in US-A-4701307 and US-A-4792437.
What the most general method of separate solid particles was used from air-flow is cyclonic separation.Cyclonic separator is known, and its operating method is by giving the speed of a tangential direction of entrained solids particulate gas, make heavier solid outwards leave away, also collecting solid downwards thereby upwards discharge gas.Cyclonic separator generally includes the less swirler of diameter, and the latter has the tangent line inlet in drum ladle outside, garden, and the described garden molten device of tubular has constituted the shell of swirler.
For the technician in FCC method field, be used for that the cyclonic separator of separating granular material is known from the gaseous state material.In the operation of FCC cyclonic separator, the tangential direction of gaseous state material and catalyzer enters, produced a volution flow path, this sets up a vortex configuration in cyclonic separator, make the entad booster action relevant with outside vortex cause granules of catalyst to move and the gaseous state material enters inner vortex finally to discharge from top exit to the outside of garden tube container.Heavier granules of catalyst is accumulated on the sidewall of cyclonic separator garden drum ladle and is finally dropped down onto cyclonic separator bottom and through outlet be used for discharging through FCC apparatus round-robin dipping tube.US-A-4670410 and US-A-2535140 general description cyclone separator means and its modification.
The FCC method is to seek when the representative with many approach of the method for their sharp separation when pipeline is discharged of gaseous fluid and solid.In the FCC method, a kind of way that reaches this initial stage snap-out release is that the pipeline that will contain reaction-ure fluid and catalyzer directly is connected with traditional cyclonic separator.Improving the isolating while, the shortcoming of its existence is directly to connect the pipeline of discharging solid and gaseous fluid mixture to cyclonic separator.And the mixture that enters cyclonic separator contains the high-load solid, and directly discharging needs big cyclonic separator.In addition, the unstable that mixture is carried also can cause the cyclonic separator function to worsen, and is had unacceptable solid to take out of in the isolating hydrocarbon vapour of cyclonic separator to have destroyed described method owing to pressure pulsation causes.In the method for for example fluid catalystic cracking, often run into this class problem.Thereby, usually seek the low restricted initially-separate that realizes between solid particulate and the gaseous state fluidic mixture.
US-A-4397738 and US-A-4482451 divide the another kind of decoration form of having opened cyclonic separation, wherein are expelled to the container with tangential direction from the mixture of central duct with gas and solid particulate.This container has bigger diameter, provides solid to be separated by the first step in the gas generally.The difference that such layout and common cyclonic separator are arranged is to discharge solid and use larger-diameter container to be used as container from central duct.In these are arranged, just separate usually follow-up have than the better second stage of traditional cyclonic separation container from gas, isolate solid.
Except that solid catalyst from appropriate hydrocarbon gas, the valid function of FCC method also require when solid catalyst when reactor is delivered to revivifier from this solid catalyst gas carry hydrocarbon.Gas is carried general use steam and is realized that described steam replaces adsorbed hydrocarbons in solid catalytic material surface and hole.Importantly want as much as possible from catalyst surface gas carry hydrocarbon with the recovery product of maximum and make that the burning of hydrocarbon reduces to minimum revivifier, if not the burning meeting of described hydrocarbon produces excessive temperature in the breeding blanket.
US-A-4689206 discloses the gentle layout of putting forward of a kind of separation of FCC method, wherein enter in the separation vessel, and make gas carry the district upwards to flow into a series of baffle plates to replace hydrocarbon the catalyzer in separation vessel from bottom gas with the mixture of tangential direction with catalyzer and gas.Though the layout shown in this piece patent can be implemented in the separation vessel appropriate hydrocarbon gas and carry from catalyzer gas to a certain degree, but this layout is not utilized and be used for utilized gas whole that gas is carried hydrocarbon in separation vessel, and and comes with by guaranteeing that in the mutually inner good distribution of catalyzer the mode of effectively using distributes the gas stripping gas body that enters in the separation vessel.
Though from the FCC catalyzer as far as possible at utmost gas carry and maximum to reclaim hydrocarbon be useful, be engaged in the purified personnel and under the increasing pressure, reduced and be used for realizing that traditional gas that gas is carried recommends the quantity of matter.Above-mentioned pressure is to produce by put forward in the operation difficulty that the acidic aqueous stream that contacted with steam by catalyzer and produce handles at general gas.Thereby though the more efficient operation method requires the more effective hydrocarbon that removes from the FCC catalyzer, the quantity that preferred gas is recommended matter is restricted.
Have now found that, by can improve the gas stripping efficiency of discharging the particulate cyclonic separation by middle mind-set separate chamber unexpectedly with ad hoc fashion operant response device container, described ad hoc fashion is, whole passages of available gas stripping gas body are entered separation vessel, distribute this gas to be increased in the separate chamber mode of gas stripping efficiency simultaneously.According to this discovery, the pressure of gaseous fluid in reactor vessel in the reactor vessel of separate chamber is kept above the pressure in the separate chamber.Higher pressure has produced from a large amount of pure qi (oxygen) body to separation vessel of reactor vessel around the separate chamber.Some or its of this gas all passed a plurality of air-flow air throttles to import on the position that is higher than the bottom, separate chamber in the catalyst bed in the separate chamber and can improve gas stripping efficiency.The gas distribution that described air-flow air throttle assurance enters the separate chamber is even, and this makes gas can effectively use as the stripping medium.
Corresponding, a method that specific embodiments is the charging of a kind of fluid catalystic cracking hydrocarbon of the present invention.This method comprises the standpipe zone of transformation of a conduit to produce solid particulate and gas fluidic mixture with hydrocarbon charging and solid catalyst particle feeding.This mixture flows into separation vessel through pipeline, and wherein pipeline occupies the middle body of separation vessel, and separation vessel is positioned at reactor vessel.This pipeline enters separation vessel by discharge outlet with tangential direction with described mixture.Granules of catalyst flows into first catalyst bed that is positioned at the separation vessel lower section, and granules of catalyst contacts with the first gas stripping gas body at this first.Granules of catalyst is positioned at second of separation vessel under first catalyst bed by this first inflow.Granules of catalyst contacts with the second gas stripping gas body, and the second gas stripping gas body flows into first catalyst bed so that a part of first gas stripping gas body to be provided.Granules of catalyst by second flow into gas carry the district and this gas carry the district contact with the 3rd gas stripping gas body.The 3rd gas stripping gas body flows into second catalyst bed to provide at least a portion the second gas stripping gas body.Cleaning medium inflow reactor container top part, and at least a portion purge gas be passed in first catalyst bed bottom along a plurality of solar term mouths of separation vessel outer setting so that a part of first gas stripping gas body to be provided.Carry the district from first gas and reclaim the granules of catalyst of being carried by gas.Enter an outlet from the top of separation vessel and from separation vessel discharge gaseous fluid by the gaseous fluid that comprises the first gas stripping gas body and granules of catalyst that will collect of outlet.
Another specific embodiments of the present invention be a kind of from the logistics that comprises gaseous fluid and solid particle mixture the device of separate solid particles.This device comprises a reactor vessel; A separation vessel that is positioned at this reactor vessel; With the mixture conduit that stretches in the separation vessel and constitute the discharge gate that is positioned at this container.The discharge gate orientation that is oriented in a tangential direction is used for that logistics entered container and gives the speed of this logistics tangential direction.Discharge particle by the particle outlet that separation vessel constitutes from the bottom part of this container.One gas carry container be positioned at separation vessel below.A gas recovery conduit formation is discharged an outlet of gaseous state fluidic and a cyclonic separator and this gas recovery conduit from separation vessel inside and is linked.Have a plurality of nozzles to be positioned on the separation vessel bottom, and along separation vessel garden Zhou Yanshen so that separation vessel be communicated with reactor vessel.
Carry fluid by in separation vessel, keeping catalyst bed and the position on the separation vessel bottom to inject gas to the dense bed of separation vessel, make all in reactor vessel available gas all be used as gas and recommend matter from reactor vessel.This class gas comprise enter the reactor vessel top with the purge gas of the hydrocarbon that is substituted in this container top and collects and come from the cyclonic separator dipping tube cracking appropriate hydrocarbon gas.Cracked gas from the cyclonic separator dipping tube is effective especially as the gas stripping gas body, and this is because because long in the residence time of cyclonic separator dipping tube, the cracking of their experience has reached and has been the inert degree substantially.Recommend matter as the gas that flows through separation vessel and can reduce and reach that required gas is put forward degree and the gas of needs is put forward total demand of steam being present in all gas in the reactor vessel.Handle the relevant more and more higher purifier of processing costs for facing with the sour water that is produced, the demand of eliminating steam is useful especially.
In addition, by with the past utilize mode to compare more effective mode to use available gas stripping gas body, method and apparatus of the present invention can further reduce the demand to steam.Prior art decoration form of stripping catalyst in separation vessel is that the general bigger bottom opening from separation vessel receives the gas stripping gas body.The gas that enters this opening generally can be uneven, mainly trends towards flowing on one side or the other side.Inject gas stripping gas body from reactor vessel to the tight bed of separation vessel through a plurality of nozzles, the distribution mode that makes the gas stripping gas body is for to inject the gas stripping gas body equably along the garden week of container.Can effectively recommend matter with this distribution mode gas as gas.
Accompanying drawing is the sectional view of FCC reactor vessel 10, has wherein illustrated the separation vessel 11 arranged according to the present invention.
The inventive system comprises a separation vessel, the mixture conduit that contains the solid particle mixture of being carried by gaseous fluid is discharged the mixture of particle and gaseous fluid in described separation vessel.Separation vessel is preferably a garden drum ladle.When gaseous fluid and solid when the discharge outlet of mixture conduit enters separation vessel with tangential direction, the garden drum ladle can promote their turning effort.Separation vessel preferably has unlimited inside under discharge outlet, when having some obstacles that pass separation vessel such as conduit or miscellaneous equipment, this still can provide satisfied operation.
The duct portion of discharge outlet and discharge outlet upstream is configured to provide the speed of tangential direction to the gaseous fluid that disengages and solid mixture.Can use blade or baffle plate to come the limiting emission mouth to give the speed of the required tangential direction of the gaseous fluid that disengages and solid.Exhaust outlet is preferably by constituting from outward extending conduit of central mixture conduit or arm.A crooked tube portion is provided in the discharge tube upstream, when gaseous fluid and solid disengage discharge outlet, can gives the momentum that provides essential to continue tangentially to pass separation vessel.Separation vessel is arranged to shift out granules of catalyst from the bottom of container, makes that heavier solid particulate breaks away from from lighter gaseous fluid downwards.Bottom at the separation vessel that extends to separation vessel keeps granular bed.The gas that comes from the separation of separation vessel will contain the entrained catalyst of additional content, and they generally separate in cyclonic separator.Preferred cyclonic separator is the type that has with the direct-connected inlet of outlet of separation vessel.The additional detail of such apart arrangement is shown among the US-A-4482451.
An essential feature of the present invention is that a plurality of solar term mouths are positioned at garden along separation vessel outside on week.Outlet is positioned on the separation vessel outlet at bottom and is under the top of tight catalyzer phase of separation vessel maintenance.Well distributed for protecting, the pressure drop that the solar term mouth produces is at least 1.7KPa (.25psi).The solar term mouth preferably is nozzle shape, and the aperture of the tight catalyzer that air-flow is imported separation vessel in mutually is provided.The preferred orifice diameter of this nozzle is 25.4mm (1 inch or less slightly), interval along separation vessel garden week is less than 305mm (12 inch), in order to obtain uniform pressure drop, all the solar term mouth preferably is being positioned on the identical height on the separation vessel wall more preferably less than 152mm (6 inch).
Can enter separation vessel solar term mouth and recommend the gas of inflow reactor container of matter from multiple source as gas.Main source is the cleaning medium that enters reactor vessel.When not cleaning, in the reactor operating process relative non-activity around the reactor vessel volume of separate chamber and direct-connected cyclone separator means.The necessary function that cleaning medium provides the removing hydrocarbon for not so the zone of non-activity relatively, otherwise described hydrocarbon can cause generating coke in container.Because this cleaning medium is generally steam, it can easily provide a kind of gas stripping gas body that might utilize.Another kind of gas is recommended matter and can be obtained by the catalyst outlet of cyclonic separator.The catalyzer that is recovered that cyclonic separator disengages contains the gas-entrained of additional content, and this gas enters reactor vessel.The heavy constituent cracking is disappeared these gases are become be inertia relatively by being trapped in the cyclonic separator dipleg for a long time.
By mode of the present invention to effective utilization of the gas stripping gas stream that comes from reactor vessel also be to have adopted separation vessel, around reactor around, and the solar term mouth between pressure equilibrium.Pressure equilibrium of the present invention keeps reactor vessel pressure to be higher than separation vessel.The pressure equilibrium that keeps necessary is asked tight catalyzer to be higher than the bottom in reactor and is extended upward and enter separation vessel.Being defined as density of catalyst mutually according to the tight catalyzer of purpose of the present invention is 320kg/m at least
3(20lb/ft
3).Closely catalyzer upwards extends to the height that exceeds the solar term mouth in the part of the bottom of separation vessel.The height that tight catalyzer exceeds the solar term mouth mutually falls restriction by export the peak pressure that passes cyclonic separator from cyclone inlet to dipping tube.Can increase by the length that prolongs the cyclonic separator dipping tube and to pass the cyclonic separator peak pressure and fall.
Solar term mouth or nozzle on separation vessel bottom with a top keeping tight catalyzer between solar term mouth and separation vessel bottom.The gas that this catalyzer top forces at least a portion to go out autoreactor flows into separation vessel through solar term mouth rather than separation vessel bottom opening, because always surpass the pressure at separation vessel solar term mouth place according to the pressure of reactor vessel of the present invention.The pressure that the catalyzer top that preferably is lower than the solar term mouth in separation vessel is kept above through the solar term mouth falls, make the gas stream that all comes from reactor vessel through the solar term mouth and before gas is carried catalyzer in the separation vessel through distributing again.
Referring to accompanying drawing, this synoptic diagram has illustrated the apart arrangement in reactor vessel 10.The center conduit that is reactor standpipe 12 forms extends upward from the bottom part of reactor vessel 10 typical FCC arranges.Center conduit or standpipe preferred vertical orientation and extend upward from the bottom of reactor vessel or extend downwards in reactor vessel 10 from the top of reactor vessel.The terminal of standpipe 12 is at the top section of separation vessel 11 and have the bending conduit that is arm shape 14.Arm 14 is discharged gaseous fluid and the mixture that comprises rigid granules.
Produced the vortex helicoidal configuration that is lower than relief outlet 16 around separation vessel 11 inside from relief outlet 16 with tangential direction discharge gas and catalyzer.The entad booster action relevant with spiral motion forces the part of heavier granules of catalyst trend separation vessel 11 than the outside.The catalyzer that comes from relief outlet 16 is collected in the bottom of separation vessel 11 to form dense catalyst bed 17.
Density is lower than solid gas and is easier to change direction and begins upwards to spiral, the final gas recovery pipe 18 that flows into of gas with import 20, and import 20 is as the pneumatic outlet of separation vessel 11.Import 20 is positioned under the relief outlet 16 in preferred form of the present invention (not shown in figures).The gas that enters gas recovery pipe 18 through import 20 contains lighter granules of catalyst load usually.Import 20 is reclaimed gas and this paper back gas stripping gas body with narration from discharge tube.The load that enters granules of catalyst in the gas of conduit 18 is usually less than 16kg/m
3(1lb/ft
3), be typically and be lower than 1.6kg/m
3(.1lb/ft
3).
Gas recovery pipe 18 imports cyclonic separator 22 with gas separated, further removes granule materials the gas of this place in gas recovery pipe.Cyclonic separator 22 is the same with common direct-connected cyclonic separator in general manner to be operated, wherein gas enters with tangential direction, produces swirling action to set up known internal layer and outer vortex separating catalyst from gas thus in cyclonic separator inside.The product logistics that does not contain catalyzer comparatively speaking flows out from reactor vessel 10 through outlet 24.
The catalyzer that reclaims by cyclonic separator 22 disengages and flows through the bottom part of reactor vessel 10 through dipping tube conduit 23 from the cyclonic separator bottom, be collected in the part that is formed on separation vessel 11 outsides at this place with the catalyzer that disengages separation vessel 11 through the bottom of opening wide 19 and have top surface 28 ' reach have top surface 28 in separation vessel 11 " dense catalyst bed 28.The catalyzer that comes from catalyst bed 28 is downward through gas and carries container 30.Gas is carried fluid, is typically steam, enters the bottom part that gas is carried container 30 through divider 31, and when catalyzer continued to be passed down through gas and carries container, catalyzer and gas were carried fluid and carried out counter current contact through a series of baffle plates, have replaced product gas from catalyzer.Fluidizing agent or additional gas are recommended matter and can be added at the top of catalyst bed 28 by divider 29.
The catalyzer of being carried by gas is carried container 30 from gas and is flowed through conduit 15 to catalyst regenerator 34, and this revivifier is by contacting regenerated catalyst with oxygen-containing gas.Oxygen-containing gas contacts from the oxidized deposits of coke of catalyst surface with the high temperature of catalyzer.After the regeneration, granules of catalyst enters the bottom of reactor standpipe 12 through conduit 33, from the fluidizing agent of conduit 35 the granules of catalyst pneumatic transfer that makes progress is passed standpipe at this place.When catalyzer and transport gas mixture continue to rise in standpipe, nozzle 36 injecting feeding in catalyzer, contact makes the charging gasification so that the additional gas that disengages through discharge outlet 16 by aforementioned manner to be provided between them.
By adding cleaning medium to the top of container, make with respect to cyclonic separator internal pressure P through nozzle 37
3With separation vessel internal pressure P
1, keep being called outer space 38, the space reactor outside cyclonic separator 22 and separation vessel 11 is in a positive pressure P
2Down.Cleaning medium typically comprises steam, is used in outer space 38 keeping low hydrocarbon partial pressure to prevent coking problem as the aforementioned.
The present invention has added the solar term mouth that is nozzle 40 forms, makes the whole cleaning mediums enter nozzle 37 have the place of production to be used as that gas is carried or pre-gas is recommended matter in the top section 41 of dense catalyst bed 17.Minimum positive pressure P
2Equal pressure P at outlet 16 place's reactants
RX, the top of this pressure drop and catalyzer on nozzle 40 and relevant through any parasitic pressure drop of nozzle 40.If ignore the pressure drop through nozzle 40, then minimum positive pressure equals P
1Being designated as height X, dense catalyst bed part 41 in the accompanying drawings is necessary for operation of the present invention, utilize available gas to recommend the position of matter fully because it provides, this utilization fully when catalyzer enters separation vessel by most catalyzer being carried out preliminary gas carried and being realized.Height X extends upward 30cm (1ft) usually at least.As discussed earlier, height X is subjected to dipleg 23 can utilize limitation of length.When height X increased, pressure P had been improved at additional catalyzer top
1And P
2The numerical value of minimum pressure.Because pressure P
3Equal pressure P
RXWith the difference of cyclonic separator pressure drop, with respect to P
RXPressure in cyclonic separator top part keeps constant.Thereby, the pressure P in dipleg 23 bottoms
2Rising make in the dipleg 23 closely that the height of catalyzer rises.So height X must keep below and make tight catalyzer plane 42 enter the height of cyclonic separator 22 barrel 43.Thereby in a preferred form of the invention, regulate pressure P according to the height of catalyzer in separation vessel 11
1
With respect to pressure P
1, pressure P
2Maximum value also be subjected to distance that bed 17 bottom part 44 extends with restriction under nozzle.In case pressure P
2Exceed pressure P
1Quantity equal catalyzer drop on height Y, the gas that then comes from outer space 38 can flow under the separation vessel bottom and enter its inside through opening 19.Thereby height Y is used for limiting the pressure drop through nozzle 40, and this pressure drop will never surpass the pressure that is produced by catalyzer drop on height Y.So, to can through nozzle 37 enter the quantity of this process cleaning medium and enter that gas that regenerator vessel flows into separators through bottom opening 19 is carried or any additives amount of purge gas without limits.Catch available gas and recommend matter and be used in separation vessel 11 gentle the carrying of reallocation for as much as possible, height Y provides the minor increment of corresponding required pressure drop through nozzle 40 to enter the air-flow of bottom opening 19 with removing.When the pressure drop through nozzle 40 is reduced to when preventing to pass the numerical value of air-flow of bottom opening 19 from outer space 38, the top of bed 28 will be in a plane 28 ' and nozzle 40 height between certain position.Purge flow further reduces to make bed 28 top plan near nozzle 40.The preferred catalyzer height Y that keeps makes the whole gaseous state streams in outer space 38 cross nozzle 40 and be provided with gas through opening 19 inflow separation vessels 11.Arrange that at great majority middle distance Y equals 30cm (12in) at least.Like this, in preferred the layout, the whole gas stripping gas bodies that come from bed 28 flow in the bed parts 44, and the whole gas stripping gas bodies that come from a part 44 are recommended matter with the part 41 of flowing through from the gas in outer space 38 as gas.
Claims (1)
1 one kinds of FCC methods that are used for the charging of fluid catalystic cracking hydrocarbon comprise:
(a) hydrocarbon charging and solid catalyst particle feeding are comprised that the standpipe zone of transformation of conduit (12) is to produce the mixture of solid particulate and gaseous fluid;
(b) through described conduit (12) described granules of catalyst and the described mixture of gaseous state fluidic are fed in the separation vessel (11), wherein said conduit (12) occupies the middle body of described separation vessel (11), and described separation vessel (11) is positioned at the inside of reactor vessel (10);
(c) from described conduit described mixture is entered described separation vessel (11) with tangential direction through discharge outlet (16);
(d) the granules of catalyst feeding is arranged in first catalyst bed (17) of described separation vessel (11) bottom part, and described granules of catalyst is contacted in described first (17) with the first gas stripping gas body;
(e) from described first (17) described granules of catalyst is fed second (28) that are arranged in described reactor vessel (10) under described first catalyst bed (17), described granules of catalyst is contacted with the second gas stripping gas body and the described second gas stripping gas body is fed in described first catalyst bed (17) so that a part of described first gas stripping gas body to be provided;
(f) described granules of catalyst being fed gas from described second (28) carries the district (30), carry at institute's gas described particle is contacted with the 3rd gas stripping gas body, and described the 3rd gas stripping gas body is fed described second catalyst bed (28) to provide at least a portion the described second gas stripping gas body;
(g) cleaning medium (through nozzle 37) is fed the top part of described reactor vessel (10);
(h) make the described cleaning medium of at least a portion be passed in described first catalyst bed (17) bottom along centering on all a plurality of solar term mouths (40) that are provided with in the outside garden of described separation vessel (11) to provide a part the described first gas stripping gas body;
(i) carry district (30) from described gas and reclaim the granules of catalyst (through conduit 15) that gas was carried; And
(j) gaseous fluid that will comprise described first gas stripping gas body and catalyzer from the top part of described separation vessel (11) collect enter outlet (20) and from described separation vessel (11) the discharge gaseous fluid be used for recovery.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96121397 CN1128854C (en) | 1996-12-16 | 1996-12-16 | Fluid catalytic cracking to hydrocarbon by comprehensive equipment of separating and stripping catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96121397 CN1128854C (en) | 1996-12-16 | 1996-12-16 | Fluid catalytic cracking to hydrocarbon by comprehensive equipment of separating and stripping catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1185477A true CN1185477A (en) | 1998-06-24 |
| CN1128854C CN1128854C (en) | 2003-11-26 |
Family
ID=5126863
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96121397 Expired - Lifetime CN1128854C (en) | 1996-12-16 | 1996-12-16 | Fluid catalytic cracking to hydrocarbon by comprehensive equipment of separating and stripping catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1128854C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102348500A (en) * | 2009-03-13 | 2012-02-08 | 犹德有限公司 | Method and apparatus for a constant steam generation from the waste heat of an alkane dehydrogenation |
| US8435401B2 (en) | 2009-01-06 | 2013-05-07 | Process Innovators, Inc. | Fluidized catalytic cracker with active stripper and methods using same |
-
1996
- 1996-12-16 CN CN 96121397 patent/CN1128854C/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8435401B2 (en) | 2009-01-06 | 2013-05-07 | Process Innovators, Inc. | Fluidized catalytic cracker with active stripper and methods using same |
| CN102348500A (en) * | 2009-03-13 | 2012-02-08 | 犹德有限公司 | Method and apparatus for a constant steam generation from the waste heat of an alkane dehydrogenation |
| CN102348500B (en) * | 2009-03-13 | 2013-12-18 | 犹德有限公司 | Method and apparatus for constant steam generation from waste heat of alkane dehydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1128854C (en) | 2003-11-26 |
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