CN85108854A - Improved fluid charge catalytic cracking of hydrocarbon oils device and processing method - Google Patents
Improved fluid charge catalytic cracking of hydrocarbon oils device and processing method Download PDFInfo
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- CN85108854A CN85108854A CN85108854.6A CN85108854A CN85108854A CN 85108854 A CN85108854 A CN 85108854A CN 85108854 A CN85108854 A CN 85108854A CN 85108854 A CN85108854 A CN 85108854A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
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Abstract
The present invention is the processing method of the fluid catalytic cracking carried out of relevant hydrocarbon matter, comprising: hydrocarbon matter charging under cracking conditions in riser tube above stream mode contact with granules of catalyst; Used catalyzer separates with the downside of cracked charge in the upper end of above-mentioned riser tube; With the reflux type injecting gas used catalyzer is carried out stripping; Under the combustion conditions that is deposited on the coke on the catalyzer, above-mentioned catalyzer is regenerated; Above-mentioned riser tube is supplied with in the regenerated catalyst circulation.
According to the present invention, after standing above-mentioned stripping step and carry out before the above-mentioned regeneration step, in above-mentioned catalyzer, injects a kind of gas with stream mode altogether and limit to desorption manipulation.
Description
The catalytic cracking of the relevant hydrocarbon matter of the present invention charging.In the invention special improvements be in this type of processing method to using the regeneration of catalyzer later, and used in " feed riser " this type of processing method more in the past that adopts for short.
As everyone knows, applied catalysis cracking Technology usually in the petroleum industry.High molecular and high boiling hydrocarbon molecules are cracked into less molecule in this technological process, and these small molecule hydrocarbons can seethe with excitement in the lower temperature range that helps using.
For this purpose, fluid catalytic cracking process commonly used at present (English name Fluid Catalytic Cracking, or abbreviate the FCC Technology as).In these class methods, the charging of hydrocarbon matter promptly contacts with catalyzer under the high temperature in vaporization, and catalyzer is suspended state under the support of feed vapors.The size of hydrocarbon molecule reaches requirement after the cracking, and the also corresponding reduction of its boiling point separates catalyzer then with products therefrom.
In this type of technological process, the reduction of hydrocarbon product boiling point is the result of catalyzed reaction and thermal response.In a single day charging atomizes and contacts with catalyzer, and just moment takes place in above-mentioned reaction.Catalyzer contacts back rapid inactivation in very short time with charging.The absorption of hydrocarbon molecule and the deposition of coke all occur in the activity of such catalysts center basically.Thereby must carry out continuous stripping to used catalyzer, with the hydrocarbon molecule of deviating to be adsorbed.In order to make catalyzer continue on for catalyzed reaction and to keep its characteristic constant, at one section or divide several sections regeneration section STRENGTH ON COKE to control burning.This reaction should be carried out before catalyst recirculation is returned reaction zone.
In fact, the catalyzer of FCC technological process and the charging that will process enter the bottom of what is called " feed riser " under pressure and high temperature.Many technician are referred to as " riser " with English.Usually basin of coaxial with it arrangement on riser tube top wherein is equipped with isolating equipment, for example cyclonic separator.Catalyzer that the effect of cyclonic separator was to use and feed separation, the catalyzer after the separation are got back to the bottom and the stripping gas of basin and are met.For reducing the loss of catalyst dust, stripping gas such as water vapor inject the bottom of basin circlewise.The catalyzer that reclaims enters revivifier then.Be used for the incendiary air also injects revivifier with annular bottom.The cyclonic separator on revivifier top is used for making granules of catalyst to separate with combustion gases.Catalyzer after the separation drains into the revivifier bottom and circulates and enters the bottom of reaction tower that is riser tube.Charging is also just here injected usually, and the temperature of injection is between 80 and 400 ℃, and corresponding pressure is respectively 0.710
5With 3.5 * 10
5Crust.
FCC technology is to operate by the thermal equilibrium of cracking unit.That is the thermocatalyst after the regeneration should provide reactive moieties needed various heats, that is:
The preheating of-liquid feeding;
The vaporization of-liquid feeding;
-included needed the heat of reaction, total reaction is thermo-negative reaction;
The hear rate of-device.
The outlet temperature that RS Regenerator Section should reach is decided by to enter amount of coke and the regenerated mode on the catalyzer of RS Regenerator Section.The heat that the coke burning is given birth to also is used for making fluid (air and/or the oxygen) preheating of regeneration usefulness except the compensation hear rate, and its effect can also make burning gas and granules of catalyst separately.According to such operator scheme, as long as thermal equilibrium is not subjected to the influence of external disturbance, the amount of coke that cracking unit generated obviously will remain unchanged.
The difference △ coke of the amount of coke on amount of coke and the RS Regenerator Section entrance and exit place catalyzer is relevant, and the available relationship formula is expressed as follows:
Coke output=△ coke * C/O,
Wherein C/O represents the ratio of catalyzer and the charging that contacts with it in the conversion zone import.
On the other hand, regeneration temperature T
RegenerationWith conversion zone temperature out T
ReactorThe available following relational expression of difference represent:
T
Regeneration-T
Reactor=η * (△ coke * △ H burning)/(Cp catalyzer)
Wherein η is the exchange efficiency of the entrained combustion heat of catalyzer, and △ H is the combustion heat of coke, and Cp is the specific heat of catalyzer.
Obviously, when the △ coke increased, the internal circulating load that must dwindle catalyzer just can make the green coke amount remain unchanged.The increase of △ coke is corresponding to be that the regeneration temperature of catalyzer is higher, and this helps the vaporization of heavy feedstocks.
Therefore, in the unrestricted modern FCC cracking unit of regeneration temperature, the control of △ coke is one of basic variable of technological process.
At present, along with charging is more and more heavier, the operational condition of FCC process is more and more harsher, and the coke deposited on catalyst charcoal is also corresponding undoubtedly increases.From certain angle, this situation have its favourable aspect because at this moment the catalyzer in the conversion zone ingress will be in higher temperature, can make the vaporization ratio of charging more complete, and having promoted bitum may command heat cracking reaction, the activation evergy of catalyzer is also higher simultaneously.Yet the regeneration temperature of control and defined catalyst usually is desirable, because so more easily keep thermal equilibrium, and can reduce the harmful effect that some component such as stripped vapor and untreated residual oil causes.In addition, also wish sometimes to improve the C/O ratio that preamble has been addressed, also promptly improve the ratio between riser tube ingress catalyzer and contacted with it charging.For duration of contact that can change catalyzer and charging and the transformation efficiency that improves charging, require catalyzer to have more active centre.
The applicant confirms, before regeneration effective desorption is carried out in the absorption on the catalyzer, will help to satisfy above-mentioned requirements.
In the FCC of classics Technology used catalyzer is carried out stripping with a kind of gas, general used is water vapor, and hydro carbons is separated with granules of catalyst.From certain angle, be adsorbed on than the light-weight hydro carbons on the surface in hole of catalyzer.As is generally known if catalyzer does not carry out stripping well before regeneration, then the △ coke will increase, and the concentration of hydrogen will weigh greater than 7%(in the deposits of coke).
It is better that people know at high temperature steam stripped effect equally.
For further improving the regeneration of catalyzer, measure of the present invention is, after routinely catalyzer being carried out stripping, further carries out the desorption of a hydrocarbon product under at least than the high 25 ℃ temperature of the temperature of the granules of catalyst behind the stripping.This desorption is preferably by realizing in the fluid of handle from the burning gas injecting catalyst of one or more revivifiers.The injection of burning gas can be mentioned catalyzer and supply with the needed height of one or more revivifiers.Thereby the length of feed riser is compared and can be shortened with technology in the past.
With hydrocarbon feed fluid catalytic cracking process method is that the content of the present invention of target comprises: one, and under the cracked condition, charging of being addressed and cracking catalyst particle above stream mode in riser tube is in contact with one another; Its two, carry out at the downside position that is separated in riser tube upper end of used catalyzer and cracked charge; Its three, become injecting gas upstream with catalyzer, carry out the stripping of catalyzer with this; Its four, under the condition of the carbon deposit on the burning-off catalyzer, carry out the regeneration of catalyzer; They are five years old, riser tube is supplied with in the regenerated catalyst circulation, improvements are: catalyzer need carry out desorption one time after aforesaid stripping He before the aforesaid regeneration, its method is will to carry out desorption manipulation in the gas injecting catalyst stream under at least than the high 25 ℃ temperature of the temperature of the granules of catalyst behind the stripping, and the mixture that is produced then injects the fluidisation part of the RS Regenerator Section of dense phase fluidized bed top.
The desorption partly gas of usefulness is a kind of rare gas element or water vapor, and used in the present invention is the gas that catalyst regeneration provides.Favourable part with this gas is that its temperature is high than wanting the regenerated catalyzer.This gas can use separately, also can use after water vapor mixes.
Higher temperature and some benefits that desorption brought in the total stream of catalyzer are:
-shortened riser tube;
-can be easily just be separated when the fluidized-bed regeneration beginning from containing the formed water vapor of hydrogen partial in the water vapor of stripping stage and the coke, thus less to the influence of reactivation of catalyst;
-the metal that is deposited on the nickel, vanadium and so on of catalyst surface is very important part, and these metal variables become volatile components and become and be easy to separate, thereby have prolonged life of catalyst;
The gas that-desorption is used can be used for the lifting gas as the catalyzer behind the stripping, the particle of catalyzer can be sent to revivifier always, hereinafter will be than the benefit of introducing this injecting gas in more detail and being brought.
The present invention also relates to the device of hydrocarbon matter incoming flow fluidized catalytic cracking.The reactor that comprises the riser tube type; Some facilities that are used for feed cracking catalyst particle and the charging of hydrocarbon matter under pressure in this riser tube bottom; With a kind of gas granules of catalyst is carried out steam stripped facility in the space at riser tube top, this stripping gas is injected used catalyst in the mode of adverse current; By making the coke burning that is deposited on the catalyzer make above-mentioned catalyzer be able to the regenerated facility; And make regenerated catalyst circulation and be fed to the facility of above-mentioned each facility, described apparatus features is, between above-mentioned stripping and regeneration, make the product desorption that adsorbs in the granules of catalyst with second kind of gas, its method is that second kind of gas is injected stream of catalyst particles under pressure, the reinject fluidisation part of the RS Regenerator Section that is positioned at dense phase fluidized bed top of the mixture of catalyzer and gas.
One of benefit that above-mentioned desorption process brought is that the level attitude that carries out the device of this process is lower than aforesaid regenerating unit, therefore the above-mentioned gas that is injected in the total stream of catalyzer can be used as the gas that promotes granules of catalyst, thereby can use short riser tube.
The used gas of desorption can be same with gas phase with stripping, also can be different.Favourable part is that at least a portion can be from the gas of regenerating unit during it was formed.The use of desorption process has increased additional transfer pressure to granules of catalyst, and this pressure can change the position of each unit equipment in the cracking unit, especially riser tube and revivifier.In addition, can also help to improve steam stripped quality, when particularly using the gas from regenerating unit, the temperature of this gas can be higher than in the device about 25 ℃ of temperature, even may reach 100 ℃.Stripping will be more effective under higher temperature, thereby can reduce the △ coke of △ coke and limited reactions.The release of heat just reduces when regeneration like this, and is also less to the infringement of catalyzer, makes catalyzer keep stable.Corresponding therewith, the length of riser tube can be shortened, or heavier charging can be handled.At last, can control and regulate of the supply of used catalyzer well, in revivifier, have than controlled temperature preferably and limit focus, help keeping the stability of catalyzer, and provide the regenerated catalyst of greater activity revivifier.
What be worth pointing out emphatically is to the invention provides the possibility that shortens riser tube length.In fact, the length that shortens riser tube can improve the selectivity to the split product of gasoline and lightweight fraction oil type on the one hand, and being on the other hand can not increase gas volume and the △ coke is reduced when improving the temperature of riser tube.So the conversion of charging can reach optimizing, the octane value of products obtained therefrom can improve, and is can also processing treatment heavier and be difficult to the cracked charging.In addition, the riser tube of shortening makes the residence time of charging in riser tube shorten greatly.
To introduce in detail below, the present invention both had been applicable to a whole set of cracking unit that comprises two cover regenerating units, also was applicable to the cracking unit that has only a regenerating unit.
Accompanying drawing is several schemas, comprising the fluidized catalytic cracker and the various technical process used in the present invention of routine.These figure are:
-Fig. 1 is a fluid catalytic cracking common process flow process;
-Fig. 2 is the simulated technological process that constitutes by the present invention, comprises one one section catalyst regeneration device;
-Fig. 3 and Fig. 4 are that every cover all has one two sections catalyst regeneration device by the schema of two covering devices of the present invention's formation.
The FCC cracking unit that Fig. 1 represents is the known types of people.The major portion of device is the reactor that is called feed riser, that is " riser ", and the charging that process enters the riser tube bottom from pipeline 2, and the particle of cracking catalyst enters riser tube by pipeline 3.
The used catalyst particle is sent to revivifier 9 behind the 4 bottom strippings of chamber.Pass through interlude pipeline 10 therebetween, be equipped with variable valve 11 on the pipeline 10.In revivifier, the coke that is deposited on the granules of catalyst is burnt with air, is used for the incendiary coke and enters regenerator bottoms from pipeline 12, feeds the nozzle of arranging at regular intervals 13.Cyclonic separator 14 separates burning gas and granules of catalyst, and burning gas can be emitted from the pipeline 15 at cyclonic separator top, and catalyzer then flows to the bottom of revivifier 9, circulates through conduit 3.A variable valve 16 is arranged on the pipeline, use for riser tube 1.
The operational condition of such device and the characteristics of size specification are:
The height of-riser tube reactive moieties is 5～40 meters;
75～450 ℃ of the temperature of-cracked charge;
The flow of the charging of-supply riser tube 1 is 1,000～10,000 tons/day;
The flow of the catalyzer of-supply riser tube 1 is 3～50 tons/minute;
-charging is 0.1～10 second promoting intraductal retention time;
The regeneration temperature of-catalyzer is 650～900 ℃;
The residence time of-catalyzer in revivifier 9 is 5～20 minutes.
Fig. 2 represents device flow process of the present invention.The part described identical with Fig. 1 used the numerical code expression identical with Fig. 1.
In this device, the used catalyst particle is through pipeline 10 ' from the chamber 4 ' discharge at riser tube top, but pipeline 10 ' directly do not enter revivifier 9 ' and, a vertical part 101 is arranged, here after this again with pipeline 102 and revivifier 9 ' be connected.Pipeline 10 ' the lower end link to each other with vertical component.
Because the shortening of riser tube length significantly reduces the residence time of charging in riser tube.In the case, chamber 4 ' height needn't be too high because used granules of catalyst needn't lean on again simple gravity transfer to revivifier 9 and after regeneration the circulation flow to riser tube 1 '.At high temperature its temperature of desorption gas of Zhu Ruing is higher 25 ℃ than the temperature of catalyzer at least, enter pipeline 101 through pipeline 18 and carry out desorption, and the promotion granules of catalyst makes it to enter revivifier.
Change as follows by the operational condition of the improved cracking unit of the present invention and the characteristics of size specification:
1～30 meter of the height of-riser tube 1 ' reactive site;
-charging riser tube 1 ' the residence time be 0.05～5 second;
650～900 ℃ of the regeneration temperatures of-catalyzer;
-catalyzer revivifier 9 ' the residence time be 1～15 minute;
-catalyzer in the chamber 5 ' temperature out be 480～580 ℃;
-desorption gas is 500～900 ℃ in the temperature of pipeline 101 inlets.
Fig. 3 and Figure 3 shows that by other two kinds of fluid catalytic cracking process flow processs of the present invention uses two sections regenerated revivifiers in these two kinds of flow processs.In the drawings, the part identical with Fig. 1 and Fig. 2 be with identical numerical code expression, but add a and b respectively as countermark.
In the situation of Fig. 3, revivifier 9a presses the upflowing operation, comprises two RS Regenerator Section 91a and 91b.The steam stripped catalyzer of process in the chamber 4 is sent to the vertical component of pipeline 101a by pipeline 10a and is positioned at the horizontal pipeline 102a of revivifier 91a bottom.Desorption gas is injected the bottom of the vertical pipeline of 101a by pipeline 18a under pressure.This desorption gas bag is drawn together from the revivifier burning gas of pipeline 20a introducing and the water vapor of being introduced by pipeline 19a.
Air is sent into the bottom of first section burning 91a from the 12a pipeline, with there being the regularly arranged nozzle 13a of certain intervals to make air well distributed.In this burning zone, cyclonic separator 14a makes that the particle of the catalyzer of partial regeneration separates with burning gas.Burning gas is sent to pipeline 20a through pipeline 115a.Valve 116a on the pipeline 115a can switch portion gas inflow line 117a.
The particle of the catalyzer after first section regeneration is sent into second section regeneration by pipe core 110a, and the gas of conveying is supplied with by pipeline 111a.
Burning gas is supplied with pipeline 112a and nozzle 113a in the bottom of the second RS Regenerator Section 91b.The particle of regenerated catalyst enters surge chamber 118a from the side, and by pipeline 3a recycled back riser tube 1a.Row externally handles among the cyclonic separator 119a to the burning gas on 91b top, and the particle of catalyzer returns RS Regenerator Section 91b in the cyclonic separator bottom by pipeline 120a, and burning gas then is sent to pipeline 18a by pipeline 121a and 20a.Safety valve 122 is housed on the pipeline 121a, and switching valve 123a then can make the portion gas reversed flow to pipeline 124a.
The catalyst-assembly with two sections upflowing revivifiers of this form of the present invention, its superiority is:
The secondary recycling of-catalyzer can be implemented under the situation that does not change the catalyst characteristic coke is all burnt;
-the second section regenerated temperature is without any restriction, and can guarantee that catalyzer is reached is enough to make charging evaporation and cracked temperature.
Two sections revivifier 9b again of a downflow system have been comprised in the device of Fig. 4.
In the chamber 4b on riser tube 1b top, passed through steam stripped catalyzer by the vertical pipeline 101b of the pipeline 10b warp let-off, enter revivifier 92b upper strata through horizontal pipeline 102b again.Desorption gas injects vertical tube 101b by pipeline 18b under pressure.This desorption gas is by mixing through the water vapor of pipeline 19b introducing and the burning gas of introducing through pipeline 20b.
Combustion air injects the bottom of RS Regenerator Section 92b through pipeline 112b and nozzle 113b.Particles suspended is separated at cyclonic separator 14b in the burning gas, and burning gas is discharged through pipeline 121b, is equipped with switching valve 123b on this pipeline, portion gas can be switched to change auxiliary line 124b over to.
Granules of catalyst after first section 92b processing relies on gravity to be sent to second section 92a of revivifier through pipe 125, injects air in the revivifier bottom by pipeline 112b and nozzle 113b.Burning gas row is to external cyclone 119b, and granules of catalyst separates the back at this and sends RS Regenerator Section 92a back to by pipe 120b, and gas is sent to pipeline 20b through pipeline 115b and valve 116b.Switching valve 116b can be sent to auxiliary line 117b with the portion gas switching.
Catalyzer after the regeneration is discharged and is circulated through pipeline 3b from the bottom of RS Regenerator Section 92a and is sent to riser tube 1b.
By the catalytic cracking unit that comprises two sections revivifiers of a downflow system that the present invention constitutes, its superiority also has except that aforementioned each point:
Two stages of-regenerated are reflux type;
-cyclonic separator externally, its support does not need too high;
-revivifier is operated under higher temperature.Because revivifier is heavier and level attitude is lower, construction that can simplification device.
For the explanation the present invention be exemplified below, for embodiment do not have binding character.
Embodiment
With in the described device with two sections RS Regenerator Section types of Fig. 3, carrying out quadric catalysis agent test with a kind of hydrocarbon feed.With test for the first time differently, testing used for the second time is having the short riser tube and a device of streaming desorption equipment altogether by requirement of the present invention.
Feed properties
-proportion 0.903
-sulphur content 0.77%(is heavy)
-total nitrogen 0.19%(is heavy)
-vanadium 4ppm
-nickel 11ppm
-Conradson carbon residue 4.9%(is heavy)
-C/H is than 12.4
-600 ℃ do not distillate product 23%(volume)
Reaction conditions
Short riser tube of the test of no desorption and the test that desorption is arranged
Feeding temperature, ℃ 95 95
Riser temperature, ℃ 525 525
The outlet temperature of regenerated catalyst, ℃ 815 782
C/O is than 4.97 5.60
Coke, %(is heavy) 7.45 7.36
The △ coke, %(is heavy) 1.50 1.31
As can be seen, use short riser tube and used 595 ℃ resurgent gases to carry out desorption, can reduce the △ coke and reduce regeneration temperature to be total to stream mode.Thereby can improve the recycle ratio (C/O is 5.6) of catalyzer and the stability of catalyzer.For more great being changed to of cracking reaction:
-reduced dry gas;
-make the addition of live catalyst reduce 26%;
-improved transformation efficiency;
-improved the solution yield, see following table for details:
Short riser tube of the test of no desorption and the test that desorption is arranged
Dry gas, %(is heavy) 6.3 5.8
The charging of alkyl plant, %(is heavy) 17.6 18.0
Gasoline 42.8 45.2
Light diluent oil 16.5 15.7
Heavy thinning oil 9.3 8.0
Transformation efficiency in the time of 220 ℃, %(is heavy) 74.2 76.3
Transformation efficiency in the time of 355 ℃, %(is heavy) 90.7 92.0
Liquid yield, %(is heavy) 86.2 86.9
Claims (9)
1, the processing method of hydrocarbon matter incoming flow fluidized catalytic cracking, comprising: hydrocarbon matter charging under cracking conditions in riser tube above stream mode contact with granules of catalyst; Used catalyzer separates with the downside of cracked charge in above-mentioned riser tube upper end; With the reflux type injecting gas used catalyzer is carried out stripping; Under the combustion conditions of coke deposited on catalyst charcoal, above-mentioned catalyzer is regenerated; Above-mentioned riser tube is supplied with in the regenerated catalyst circulation, it is improved one's methods and is: after standing above-mentioned stripping step and carry out before the above-mentioned regeneration step, at least exceed in temperature under 25 ℃ the temperature than the granules of catalyst after standing above-mentioned stripping, a kind of gas is carried out desorption to be total to the stream mode injecting catalyst, and the used catalyzer of generation and the mixture of injecting gas are injected into the fluidisation position of the RS Regenerator Section of dense phase fluidized bed top.
2, by claim 1 described method, be characterized in, above-mentioned desorption gas to small part from gas that catalyst regeneration provided.
3, by each the described method in claim 1 and the claim 2, be characterized in that above-mentioned desorption gas is under certain pressure, be enough to be used as lift gas and catalyzer can be sent into one or more revivifiers.
4, the device of hydrocarbon matter charging fluidized catalytic cracking, comprising: the reactor of riser tube type; Can under pressure, be provided charging of hydrocarbon matter and the setting of cracking catalyst particulate what above-mentioned riser tube bottom connected for riser tube; With gas to used granules of catalyst in the chamber (4 ') carry out steam stripped setting (7 ', 8 '), chamber (4 ') are positioned at the top of above-mentioned riser tube and coaxial with it, steam stripped gas is injected in the above-mentioned used catalyzer with reflux type; Make the cell arrangement (9 ') of above-mentioned catalyst regeneration by the carbon deposit on the combustioncatalysts; And the setting that makes regenerated catalyst circulation and supply each part mentioned above, said apparatus is characterised in that: between above-mentioned stripping setting and regeneration unit device, also useful second kind of gas makes the device (13 ') of granules of catalyst desorption, this desorption method be under pressure with second kind of stripping gas with in the stream mode injecting catalyst grain flow altogether, the catalyzer that is produced and the mixture of gas inject the breeding blanket part that is positioned at the dense phase fluidized bed top.
5, by claim 4 described devices, in above-mentioned regeneration unit (9 '), has only a RS Regenerator Section, it is characterized in that above-mentioned desorption gas is injected in the vertical tube (101) of above-mentioned regeneration unit upstream, used catalyzer is sent into above-mentioned regeneration unit through this pipe.
6, by claim 5 described devices, it is characterized in that, comprising the feed line (18) of one section second kind of stripping gas that links to each other with the vent line (15 ') of the burning gas of regenerating unit (9 ').
7, by claim 4 described devices, at above-mentioned regeneration unit (9a, comprise two or upper reaches (91a 9b), 91b) or dirty (92a, RS Regenerator Section 92b) is characterized in that, desorption gas is injected into above-mentioned regeneration unit and RS Regenerator Section (91a, the vertical tube of upstream 91b) (101a, 101b) in, used catalyzer is sent into regeneration unit through this pipe.
8, by claim 7 described devices, it is characterized in that, comprise desorption gas feed line (18a, 18b), this pipeline and RS Regenerator Section (91a, upstream 92b) and/or RS Regenerator Section (91b, 92a) (20a's burning gas vent line in downstream 20b) is connected.
9, by each the described device in the claim 4～8, it is characterized in that, comprising the riser tube (1 ') that has highly shortened.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR8418706A FR2574422B1 (en) | 1984-12-07 | 1984-12-07 | IMPROVEMENTS TO METHODS AND DEVICES FOR CATALYTIC CRACKING IN A FLUID STATE OF HYDROCARBON FEEDSTOCKS |
| FR84.18706 | 1984-12-07 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN85108854A true CN85108854A (en) | 1986-05-10 |
| CN1006895B CN1006895B (en) | 1990-02-21 |
Family
ID=9310352
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN85108854A Expired CN1006895B (en) | 1984-12-07 | 1985-12-06 | Improved device and the production process for fluid charge catalytic cracking of hydrocarbon oils |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0184517B1 (en) |
| CN (1) | CN1006895B (en) |
| DE (1) | DE3562780D1 (en) |
| FR (1) | FR2574422B1 (en) |
| ZA (1) | ZA859374B (en) |
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| CN1078492C (en) * | 1998-09-25 | 2002-01-30 | 清华大学 | Dense-phase circulating fluidized bed reactor for strong exothermal reaction process |
| CN1109091C (en) * | 1997-12-23 | 2003-05-21 | 中国石油化工集团公司 | Lapping type two-stage regeneration technology of heavy oil fluidized catalystic cracking |
| CN102276402A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Combined reaction apparatus for producing low-carbon olefin |
| CN107271352A (en) * | 2017-06-30 | 2017-10-20 | 上海理工大学 | A kind of particle temperature and particle motion synchronous measuring apparatus and method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2624762B1 (en) * | 1987-12-21 | 1990-06-08 | Total France | METHOD AND DEVICE FOR REGENERATING A FLUIDIZED BED CATALYST |
| FR2624877B1 (en) * | 1987-12-22 | 1992-01-10 | Inst Francais Du Petrole | METHOD AND DEVICE FOR THE CATALYTIC CRACKING OF HEAVY LOADS COMPRISING A SECOND STRIPPING IN A FLUID BED |
| US5264115A (en) * | 1987-12-30 | 1993-11-23 | Compagnie De Raffinage Et De Distribution Total France | Process and apparatus for fluidized bed hydrocarbon conversion |
| FR2627187B1 (en) * | 1988-02-15 | 1993-01-22 | Inst Francais Du Petrole | FLUID CRACKING PROCESS OF A HYDROCARBON LOAD |
| US4973398A (en) * | 1988-05-25 | 1990-11-27 | Mobil Oil Corp. | Method of FCC spent catalyst stripping for improved efficiency and reduced hydrocarbon flow to regenerator |
| US5584986A (en) * | 1993-03-19 | 1996-12-17 | Bar-Co Processes Joint Venture | Fluidized process for improved stripping and/or cooling of particulate spent solids, and reduction of sulfur oxide emissions |
| CN1087647C (en) * | 1998-12-25 | 2002-07-17 | 中国石油化工集团公司 | Liquid-solid moving bed reactor |
| FR2791354B1 (en) | 1999-03-25 | 2003-06-13 | Inst Francais Du Petrole | PROCESS FOR THE CONVERSION OF HEAVY PETROLEUM FRACTIONS COMPRISING A STAGE OF HYDROCONVERSION IN BUBBLING BEDS AND A STAGE OF HYDROTREATMENT |
| FR2981659B1 (en) | 2011-10-20 | 2013-11-01 | Ifp Energies Now | PROCESS FOR CONVERTING PETROLEUM LOADS COMPRISING A BOILING BED HYDROCONVERSION STEP AND A FIXED BED HYDROTREATMENT STEP FOR THE PRODUCTION OF LOW SULFUR CONTENT |
| FR2983866B1 (en) | 2011-12-07 | 2015-01-16 | Ifp Energies Now | PROCESS FOR HYDROCONVERSION OF PETROLEUM LOADS IN BEDS FOR THE PRODUCTION OF LOW SULFUR CONTENT FIELDS |
| FR2999600B1 (en) | 2012-12-18 | 2015-11-13 | IFP Energies Nouvelles | METHOD FOR REFINING A HEAVY HYDROCARBONIC LOAD USING SELECTIVE DESASPHALTAGE |
| FR3000097B1 (en) | 2012-12-20 | 2014-12-26 | Ifp Energies Now | INTEGRATED PROCESS FOR THE TREATMENT OF PETROLEUM LOADS FOR THE PRODUCTION OF LOW SULFUR CONTENT FIELDS |
| FR3000098B1 (en) | 2012-12-20 | 2014-12-26 | IFP Energies Nouvelles | PROCESS WITH SEPARATING TREATMENT OF PETROLEUM LOADS FOR THE PRODUCTION OF LOW SULFUR CONTENT FIELDS |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2843460A (en) * | 1953-04-07 | 1958-07-15 | Standard Oil Dev Co | Contacting of gases with fluidized solids |
| NL105540C (en) * | 1954-02-09 | |||
| GB1293168A (en) * | 1969-12-08 | 1972-10-18 | Exxon Research Engineering Co | Two-stage countercurrent catalyst regenerator |
| WO1982004061A1 (en) * | 1981-05-13 | 1982-11-25 | Mckay William E Jr | Stripping hydrocarbons from catalyst with combustion gases |
-
1984
- 1984-12-07 FR FR8418706A patent/FR2574422B1/en not_active Expired
-
1985
- 1985-12-04 EP EP85402416A patent/EP0184517B1/en not_active Expired
- 1985-12-04 DE DE8585402416T patent/DE3562780D1/en not_active Expired
- 1985-12-06 ZA ZA859374A patent/ZA859374B/en unknown
- 1985-12-06 CN CN85108854A patent/CN1006895B/en not_active Expired
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056543C (en) * | 1996-08-20 | 2000-09-20 | 中国石油化工总公司 | Catalytic cracking riser reactor |
| CN1109091C (en) * | 1997-12-23 | 2003-05-21 | 中国石油化工集团公司 | Lapping type two-stage regeneration technology of heavy oil fluidized catalystic cracking |
| CN1078492C (en) * | 1998-09-25 | 2002-01-30 | 清华大学 | Dense-phase circulating fluidized bed reactor for strong exothermal reaction process |
| CN102276402A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Combined reaction apparatus for producing low-carbon olefin |
| CN102276402B (en) * | 2010-06-11 | 2013-12-04 | 中国石油化工股份有限公司 | Combined reaction apparatus for producing low-carbon olefin |
| CN107271352A (en) * | 2017-06-30 | 2017-10-20 | 上海理工大学 | A kind of particle temperature and particle motion synchronous measuring apparatus and method |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2574422B1 (en) | 1988-01-08 |
| EP0184517A1 (en) | 1986-06-11 |
| EP0184517B1 (en) | 1988-05-18 |
| CN1006895B (en) | 1990-02-21 |
| FR2574422A1 (en) | 1986-06-13 |
| DE3562780D1 (en) | 1988-06-23 |
| ZA859374B (en) | 1986-09-24 |
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