CN1626622A - Method of combined catalytic cracking regeneration technology and equipment - Google Patents
Method of combined catalytic cracking regeneration technology and equipment Download PDFInfo
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- CN1626622A CN1626622A CN 200410030876 CN200410030876A CN1626622A CN 1626622 A CN1626622 A CN 1626622A CN 200410030876 CN200410030876 CN 200410030876 CN 200410030876 A CN200410030876 A CN 200410030876A CN 1626622 A CN1626622 A CN 1626622A
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- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000008929 regeneration Effects 0.000 title description 32
- 238000011069 regeneration method Methods 0.000 title description 32
- 238000004523 catalytic cracking Methods 0.000 title description 6
- 238000005516 engineering process Methods 0.000 title description 5
- 239000007789 gas Substances 0.000 claims abstract description 58
- 239000003054 catalyst Substances 0.000 claims abstract description 52
- 230000003197 catalytic effect Effects 0.000 claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000000571 coke Substances 0.000 claims abstract description 16
- 239000007787 solid Substances 0.000 claims description 46
- 238000000926 separation method Methods 0.000 claims description 41
- 239000003546 flue gas Substances 0.000 claims description 31
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 26
- 239000001301 oxygen Substances 0.000 claims description 26
- 229910052760 oxygen Inorganic materials 0.000 claims description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 25
- 238000003672 processing method Methods 0.000 claims description 11
- 239000001257 hydrogen Substances 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 239000008247 solid mixture Substances 0.000 claims description 6
- 230000008569 process Effects 0.000 abstract description 19
- 239000003517 fume Substances 0.000 abstract 2
- 238000006243 chemical reaction Methods 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 6
- 230000009849 deactivation Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000003610 charcoal Substances 0.000 description 5
- 230000005587 bubbling Effects 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000002411 adverse Effects 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000007812 deficiency Effects 0.000 description 3
- 230000008439 repair process Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 125000001183 hydrocarbyl group Chemical group 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
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- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
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Abstract
A combined catalytic cracking-regenrating process for the used catalyst includes using O2-contained gas to burn said catalyst for removing H2 and part of coke and generating the fume containing CO2, CO and water vapour and the semi-regenerated catalyst, and using the O2-contained gas to further burn it for generating the fume containing Co2, Co and excessive O2 and the regenerated catalyst. Its apparatus is composed of a conventional turbulent-bed regenerator and post-burning unit.
Description
Technical field
The present invention relates to a kind of catalytic cracked regenerated processing method and equipment, catalytic cracked regenerated processing method of especially a kind of built-up type and equipment make because of the deactivated catalyzer of carbon deposit and recover active again; Belong to the petrochemical technology field.
Background technology
Catalytically cracked stock resolves into light constituents such as gas, gasoline, diesel oil on the one hand under the situation that catalytic cracking catalyst exists, condensation reaction also takes place on the other hand generate coke.The major ingredient of coke is a charcoal, also contains part hydrogen.Its hydrocarbon atom is higher than very, is about 1: 0.3 to 1: 1.Sedimentation of coke can not go out as product separation on the surface of catalyzer in reaction process.Along with the carrying out of reaction, the carbon deposit of catalyst surface is more and more, activity of such catalysts is descended or completely loses.Therefore, must recover activity of such catalysts and selectivity with oxygen-containing gas with the coke burning-off.Process with oxygen-containing gas burning-off coke is called regeneration.Surface deposition has the catalyzer of coke to be called spent agent, and the catalyzer of burning-off coke is called regenerator.Regenerator can recycle by Returning reacting system.
Oxygen-containing gas contacts with reclaimable catalyst under the hot conditions more than 600 ℃ and burns, because the combustionvelocity of hydrogen approximately is 10 times of charcoal, therefore, during burning-off part charcoal, the hydrogen in the coke is just all burnt.The charcoal burning generates CO
2And CO, hydrogen burning generates water.At high temperature, particularly have under the condition of water vapour existence, the surface tissue of catalyzer changes, and causes activity of such catalysts and selectivity to descend, and is called hydrothermal deactivation.For improving scorching speed, take to improve the way of burning temperature usually.Yet, the raising of temperature, catalyzer is easy to take place hydrothermal deactivation under the situation that water vapour exists.Initial revivifier of FCC regenerated employing is once finished burning process, is called single hop regeneration.Although equipment is fairly simple, scorching speed is low, burns weak effect, and the regenerator carbon residue is higher, and the catalyzer hydrothermal deactivation is serious.Therefore, must in time remove the water vapour that burning generates.For addressing this problem, people are divided into two sections with catalytic cracked regenerated, one section most of coke of first burning-off and whole hydrogen, and steam-laden flue gas is discharged revivifier immediately.Then, catalyzer enters two sections, because there is not the influence of water vapour in the whole burning-off of hydrogen, therefore, two sections can burn under higher temperature, and scorching speed improves greatly, and the carbon residue of regenerator is further reduction thereupon also.
The scorching speed of reclaimable catalyst is also burnt the influence of gas speed, and when gas speed was low, gas-solid ratio was low, and oxygen is delivered to the CO of catalyst surface and burning generation from the air-flow main body
2The resistance to mass transfer that is delivered to the air-flow main body with CO is big.Therefore, mass transfer process has just become the controlling factor of scorching speed.Reach by reaction kinetics control for making to burn to react, resurgent gases speed constantly promotes.The regenerator bed laminar-type also develops into turbulent bed by the bubbling bed, and then fast bed occurred or even carried bed.Gas speed surpasses 3m/s, and burning process can be realized being controlled by reaction kinetics fully.
Regenerative process can be recovered catalytic cracking reaction activity of such catalysts and selectivity by the burning-off coke on the one hand.It simultaneously is again power consumption part maximum in the catalytic cracking unit.Therefore, be subjected to people's attention always.Along with the change day by day of raw material is heavy, the coke that generates in the reaction process is multiplied, and the carbon-burning load of revivifier increases, and temperature raises.Particularly applying of super steady zeolitic cracking catalyst proposed harsher requirement to regeneration techniques, thereby industrial priority has been designed dissimilar revivifiers, concludes and gets up to mainly contain single hop regeneration, two-stage regeneration and fast bed regeneration.Different according to catalyzer with the flow process of burning gas, can be divided into: single hop or two sections and stream, cross-flow or adverse current; According to the fluid bed type difference, can be divided into: bubbling bed, turbulent bed, fast bed or conveying bed; According to burning the degree difference, can be divided into: part is burnt or is burnt fully; Difference according to processing condition such as temperature, bed gas speed, oxygen concns is combined into diversified regeneration.
Single hop regeneration is fluidisation reconstituted form the earliest, just is to use a revivifier once to finish the burning process of catalyzer.Two-stage regeneration is divided into two sections to regenerative process, and first section burning-off part of coke remaining enter second section and continue to burn.Two-stage regeneration is divided into single device cross-flow two-stage regeneration, single device adverse current two-stage regeneration, two device cross-flow two-stage regeneration, two device adverse current two-stage regeneration again.All the time, for eliminating the resistance to mass transfer of burning carbon, resurgent gases speed improves constantly, and the bed flow pattern develops into fast bed from bubbling bed, turbulent bed.Initial fast bed regeneration is feature to burn jar, therefore the domestic jar technology of burning that also is commonly called as.Its technology pattern is divided into preposition regeneration and the postposition of burning jar and burns and jar regenerate two kinds.
Therefore single hop and two-stage regeneration belong to bubbling bed and turbulent bed mostly, and the gas-solid resistance to mass transfer is big, and back-mixing is serious, and it is low to burn intensity, burns weak effect.Further improved gas speed though burn jar regeneration techniques, entered the fast bed zone, burning process has been reached fully by reaction kinetics control.And coke-burning riser regeneration belongs to a conveying bed operating area, as a kind of efficient, no bubble gas-solid contact technique, can eliminate the influence of resistance to mass transfer fully, and burning process is controlled by reaction kinetics fully.It is big that coke-burning riser regeneration not only has the intensity of burning, and the regenerated catalyst carbon residue is reduced greatly, to satisfy the requirement of residual oil catalytic cracking reaction.Coke-burning riser is survived again in addition, and to have the incomparable occupations of land of other regeneration patterns little, advantages such as less investment.Therefore, coke-burning riser regeneration is the inexorable trend of catalytic cracked regenerated pattern.
Yet tubular type regeneration also has the weakness of oneself.Adopt coke-burning riser regeneration separately, because the raising of gas-solid ratio is opened the combustion temperature and is difficult to meet the demands.If under higher temperature, burn, also can there be problem of catalyzer hydrothermal deactivation or the like.
Summary of the invention
Technical problem to be solved by this invention is, at the deficiencies in the prior art, provide a kind of built-up type catalytic cracked regenerated processing method, this method adopts rearmounted coke-burning riser to add the regeneration of turbulent bed revivifier built-up type, avoided the generation of catalyzer hydrothermal deactivation in the follow-up burning process, scorching speed is fast, burns effective.
Technical problem to be solved by this invention also is, at the deficiencies in the prior art, provides a kind of built-up type catalytic cracked regenerated equipment, tubular type is burnt with turbulent bed burn effective combination, catalytic cracking unit is expanded can and improve intermingled dregs ratio.This occupation area of equipment is little, less investment, and flexible operation, elasticity are big, both can be used for new device, also can be used for the transformation to old device, can effectively realize expanding the purpose that can and improve intermingled dregs ratio, thereby increase economic efficiency.
Technical problem solved by the invention is achieved by the following technical solution:
A kind of catalytic cracked regenerated processing method, this method comprises the steps:
Step 1: reclaimable catalyst is mixed with oxygen-containing gas, is 650-730 ℃ burning temperature, and the revivifier top pressure is under the condition of 0.12-0.2Mpa (gauge pressure), and the coke of burning-off 60-80% and whole hydrogen generate half regenerated catalyst; What generate contains CO
2, CO and water vapour mixed flue gas, immediately with catalyst separating.
Step 2: half regenerated catalyst is continued to mix with oxygen-containing gas, and burning temperature is 680-750 ℃, continues to burn, and generates and contains CO
2, a small amount of CO and excess oxygen mixed flue gas and regenerator.
Gas-operated linear speed scope in the step 1 is 0.5-1.2m/s; Gas-operated linear speed scope in the step 2 is 4-16m/s.
The catalytic cracked regenerated processing unit of a kind of built-up type, comprise conventional turbulent bed revivifier, on the turbulent bed revivifier, increase postposition and burn device, this burns device and mainly comprises: coke-burning riser, inclined tube and gas-solid separation member, turbulent bed revivifier bottom is connected with inclined tube with the coke-burning riser bottom, the coke-burning riser top exit is connected with the gas solid separation part, reclaimable catalyst at first enters the turbulent bed revivifier and partly burns, the containing water vapor flue gas rises to the revivifier dilute phase, after cyclonic separation, discharge, half regenerated catalyst enters rearmounted coke-burning riser to be continued to burn, and the gas solid separation part of coke-burning riser outlet separates catalyzer with flue gas, generate regenerator and Returning reacting system.
For the flow of control catalyst better, inclined tube is provided with pneumavalve.
The close dividing plate of setting up mutually of turbulent bed revivifier partly burns half regenerated catalyst that the back generates in dividing plate one side, enters to burn generation regenerator in back in the coke-burning riser, and regenerator enters the opposite side Returning reacting system of dividing plate.
A surge tank is set up in the below of coke-burning riser, by the isolated regenerator of gas solid separation part of coke-burning riser outlet through the surge tank Returning reacting system.
Set up second cyclonic separator after the coke-burning riser outlet gas-solid separation member, be used to alleviate the load of first cyclonic separator in the revivifier, two strands of flue gases separating from first and second cyclonic separator converge outside revivifier.
The gas solid separation part is an arched door shape housing, the arched door two ends are respectively gas-solid mixture inlet and solid outlet, with the concentric pipe core that is provided with of arched door circular arc, this pipe core is a pneumatic outlet, it is contained in the intravital body of shell and has two vertical narrow slits vertically, the aperture of narrow slit is respectively α angle and β angle, and the size at α angle and β angle can equate or be unequal.Article two, the angle of offering of narrow slit is the γ angle, it is identical with the housing width to offer length, according to the flow of catalyzer and the requirement of separation efficiency, the size at α, β angle is 15 °-35 °, the γ angle is 20 °-60 °, the arc radius of pipe core and arched door housing is than r: R=1/2-2/3, the R of arched door height H=(0.5-3).
In sum, the present invention regenerates tubular type regeneration and combines with turbulent bed, catalytic cracked regenerated processing method of the built-up type of formation and equipment, and it is big to burn intensity, burns effectively, and treatment capacity is big, and floor space is little, less investment, flexible operation, elasticity is big; Both can be used for new device, also can be used for transformation, and can effectively realize expanding the purpose that can and improve intermingled dregs ratio, thereby increase economic efficiency old device.
Description of drawings
Fig. 1 is the structural representation of the embodiment of the invention one regeneration processing unit;
Fig. 2 is the structural representation of the embodiment of the invention two reclaiming process equipment;
Fig. 3 is the structural representation of the embodiment of the invention three reclaiming process equipment;
Fig. 4 is the structural representation of the embodiment of the invention four reclaiming process equipment;
Fig. 5 is the front view of gas solid separation part;
Fig. 6 is the right view of gas solid separation part.
Embodiment
Below in conjunction with the drawings and specific embodiments technical scheme of the present invention is described in detail.
The catalytic cracked regenerated processing method of built-up type provided by the present invention comprises the steps:
Step 1: reclaimable catalyst is mixed with oxygen-containing gas, is 650-730 ℃ in temperature, and the revivifier top pressure is under the condition of 0.12-0.2Mpa (gauge pressure), and the coke of burning-off 60-80% and whole hydrogen generate half regenerated catalyst; What generate contains CO
2, CO and water vapour mixed flue gas, immediately with catalyst separating.
Step 2: half regenerated catalyst is continued to mix with oxygen-containing gas, under 680-750 ℃ of condition, continue to burn, generate and contain CO
2, a small amount of CO and excess oxygen mixed flue gas and regenerator.
Gas-operated linear speed scope in the step 1 is 0.5-1.2m/s, and the gas-operated linear speed scope in the step 2 is 4-16m/s.
Above-mentioned step 1 is the oxygen deprivation incomplete regen-eration, can contain a certain amount of CO in the flue gas that generates, and step 2 is rich oxygen containing regenerative process, has a certain amount of excess oxygen in the flue gas after the regeneration, as not controlled tail combustion phenomenon can take place when two strands of flue gases mix.Control method can adopt the mode that adds the CO ignition dope in the turbulent bed revivifier of step 1, reduces the CO content in the flue gas as far as possible; Also can be by excess oxygen content in the strict controlled step two of method of heat balance.
The equipment that adopts aforesaid method to carry out catalytic cracked regenerated technological process can be realized by multiple array configuration.
Embodiment one:
As shown in Figure 1, the catalytic cracked regenerated processing unit of this built-up type provided by the present invention, comprise conventional turbulent bed revivifier 1, on turbulent bed revivifier 1, set up one and burn device 2, this burns device 2 and mainly comprises: coke-burning riser 21, inclined tube 22 and gas-solid separation member 23, turbulent bed revivifier 1 bottom is connected with inclined tube 22 with coke-burning riser 21 bottoms, coke-burning riser 21 top exits with link to each other with turbulent bed revivifier 1 again after gas solid separation part 23 is connected.
Control for the flow to catalyzer better, inclined tube 22 is provided with pneumavalve 221.
As shown in Figure 1, reclaimable catalyst at first enters turbulent bed revivifier 1, oxygen-containing gas enters revivifier 1 by gas distributor 11, burn with the spent agent contact part, the containing water vapor regenerated flue gas rises to revivifier 1 dilute phase, discharge revivifier 1 after cyclonic separator 12 separates, the catalyzer that separates returns revivifier 1 close phase.Half regenerated catalyst enters the rearmounted bed coke-burning riser 21 of carrying through inclined tube 22, and its flow is by pneumavalve 221 controls.Oxygen-containing gas enters from coke-burning riser 21 bottoms, owing to eliminated the influence of water vapour, half regenerated catalyst can continue to burn under higher temperature in coke-burning riser 21.Coke-burning riser 21 outlet gas-solid separation members 23 place the revivifier dilute phase, and the catalyzer that separates turns back to the close phase of revivifier 1, and flue gas and revivifier 1 flue gas converge.The coke-burning riser 21 outlet gas-solid separation members 23 of this scheme also can be placed on revivifier 1 outside, but need to consider the problem of insulation, if enough spaces are arranged in the revivifier dilute phase, the gas solid separation part preferably is placed on revivifier 1 dilute phase.
Embodiment two:
As shown in Figure 2, be the structural representation of the embodiment of the invention two reclaiming process equipment.As we know from the figure, at revivifier 1 close addition one dividing plate 13, catalyzer and revivifier 1 dense-phase catalyst that gas solid separation part 23 is separated separate.Spent agent enters a side of revivifier 1 close phase dividing plate, and oxygen-containing gas enters revivifier by gas distributor 14, burns with the spent agent contact part.Flue gas rises to revivifier 1 dilute phase, discharges revivifier 1 after cyclonic separator 12 separates, and the catalyzer that separates returns revivifier 1 close phase.Half regenerated catalyst enters rearmounted coke-burning riser 21, oxygen-containing gas is entered by coke-burning riser 21 bottoms, contact with half regenerated catalyst, under higher temperature, continue to burn, the catalyzer that is separated by coke-burning riser 21 outlet gas-solid separation members 23 enters the opposite side of dividing plate 13, fluidized wind is entered by gas distributor 15, keeps the bed fluidisation.Gas solid separation part 23 flue gases turn back to the dilute phase of revivifier 1.Equally, the coke-burning riser 21 outlet gas-solid separation members 23 of this scheme also can be selected to be placed on revivifier 1 dilute phase or to place outside the revivifier 1.The pipe connecting of revivifier 1 bottom and coke-burning riser 21 bottoms is an inclined tube 22, and pneumavalve 221 is installed on it, is used for the flow of control catalyst.
Embodiment three:
As shown in Figure 3, be the structural representation of the embodiment of the invention three reclaiming process equipment.As we know from the figure, reclaimable catalyst at first enters turbulent bed revivifier 1, oxygen-containing gas enters revivifier 1 by gas distributor 11, burn with the spent agent contact part, the containing water vapor flue gas rises to revivifier 1 dilute phase, discharge revivifier 1 after cyclonic separator 12 separates, the catalyzer that separates returns revivifier 1 close phase.Half regenerated catalyst enters the rearmounted bed coke-burning riser 21 of carrying through inclined tube 22, and its flow is by 221 controls of the pneumavalve on the inclined tube 22.Oxygen-containing gas is entered by coke-burning riser 21 bottoms, owing to got rid of the influence of water vapour, half regenerated catalyst can continue to burn under higher temperature in coke-burning riser 21.The catalyzer that separates through coke-burning riser 21 outlet gas-solid separation members 23 is through surge tank 3 Returning reacting systems.Flue gas then turns back to the dilute phase of revivifier 1, converges outside the displacer with the flue gas of revivifier 1.
Embodiment four:
As shown in Figure 4, be the structural representation of the embodiment of the invention four reclaiming process equipment.As we know from the figure, reclaimable catalyst at first enters turbulent bed revivifier 1, oxygen-containing gas enters revivifier 1 by gas distributor 11, burn with the reclaimable catalyst contact part, the containing water vapor flue gas rises to revivifier 1 dilute phase, discharge revivifier 1 after cyclonic separator 16 separates, the catalyzer that separates returns revivifier 1 close phase.Half regenerated catalyst enters rearmounted coke-burning riser 21 through inclined tube 22, and its flow is by 221 controls of the pneumavalve on the inclined tube 22.Oxygen-containing gas is entered by coke-burning riser 21 bottoms, do not have water vapour in the presence of, can under higher temperature, continue to burn.Gas-solid mixture is after coke-burning riser 21 outlet gas-solid separation members 23 separate, catalyzer returns the riser tube reactive system through surge tank 3, flue gas separates through one group of cyclonic separator 24 again, the catalyzer that separates returns revivifier 1 dense bed, and whirlwind 24 flue gases and revivifier 1 flue gas converge outside revivifier 1.
In sum, embodiment two is with the difference of embodiment one:
Embodiment one, and catalyzer is cyclic char between revivifier 1 and coke-burning riser 21, reaches and decides to get back to riser reactor after the charcoal index; Embodiment two, and revivifier 1 emulsion zone is welded with a plane or arcual vertical clapboard 13, can reduce the back-mixing between the catalyzer, further reduces the carbon content of regenerated catalyst.Catalyzer after coke-burning riser 21 burns no longer mixes with dense-phase catalyst in the revivifier 1, directly returns riser reactor.
In addition, embodiment three is with the difference of embodiment two:
Embodiment three has cancelled the dividing plate 13 of revivifier 1 close phase, has set up a catalyzer surge tank 3, and the catalyzer that is separated by coke-burning riser 21 outlet gas-solid separation members 23 returns riser reactor through surge tank 3.Surge tank 3 can guarantee the circulation that catalyzer is stable, improves the stability of device operation.
And the difference of embodiment four and embodiment three is:
Embodiment four has set up one group of cyclonic separator 24 after coke-burning riser 21 outlet gas-solid separation members 23, divide 16 load to alleviate revivifier 1 inward turning.Last two strands of flue gases converge outside revivifier 1.
Therefore, processing method provided by the present invention, essence also are two-stage regenerations.Reclaimable catalyst is the whole hydrogen of burning-off in the turbulent bed revivifier earlier, and steam-laden flue gas is in time discharged, and has avoided the generation of catalyzer hydrothermal deactivation in the follow-up burning process.Coke-burning riser places after the revivifier, and half regenerated catalyst enters with very high temperature, is well positioned to meet the tubular type regenerated and opens the combustion temperature requirement.And tubular type regeneration to have a scorching speed fast, burn effectively, floor space is little, less investment a bit.Give full play to the empyreumatic advantage of tubular type, avoided its deficiency.
Rearmounted coke-burning riser built-up type regenerated realizes depending on two key equipments: gas solid separation part and pneumavalve.The catalyzer of coke-burning riser outlet is sharp separation efficiently, and pressure drop is little, so the present invention adopts a kind of gas solid separation part 23, and its structure is shown in Fig. 5,6.Gas solid separation part 23 is an arched door shape housing, the arched door two ends are respectively gas-solid mixture inlet 231 and solid outlet 232, with the concentric pipe core 233 that is provided with of arched door circular arc, this pipe core 233 is a pneumatic outlet, it is contained in the intravital body of shell and has two vertical narrow slits 2331 and 2332 vertically, narrow slit 2331 and 2332 aperture are respectively α angle and β angle, and two narrow slits 2331 and 2332 the angle of offering are the γ angle.It is identical with the housing width D that narrow slit is offered length, according to the flow of catalyzer and the requirement of separation efficiency, the size at α, β angle is 15 °-35 °, the size at α angle and β angle can equate or be unequal, the γ angle is 20 °-60 °, the arc radius of pipe core and arched door housing is than r: R=1/2-2/3, the R of arched door height H=(0.5-3).
Gas-solid mixture inlet 231 links to each other with coke-burning riser 21 outlets, and solid particulate outlet 232 connects gas solid separation part 23 diplegs, and gas is discharged by pipe core 233.After gas-solid mixture to be separated enters gas solid separation part 23, do half circular motion along housing, because the inertia of solid particulate is greater than the inertia of gas, through narrow slit 2331 and 2332 o'clock, gas flow direction takes place sharply to change, and enters pipe core 233 by narrow slit, and solid particulate then continues to do half circular motion along housing, enter gas solid separation part 23 diplegs by solid particulate outlet 232, thereby realize gas solid separation.The flow of catalyzer adopts pneumavalve 221 controls in the inclined tube.The pneumavalve resistance is little, and is simple to operate.
In conjunction with Fig. 1-shown in Figure 4, the gas in the equipment and the flow direction of solid particulate in the burning process are represented in the sensing of arrow among the figure, and wherein, A represents that spent agent, B represent to burn the regenerator that the back generates.
Need to prove at last, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although the present invention is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement technical scheme of the present invention, and not breaking away from the spirit and scope of technical solution of the present invention, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (10)
1, the catalytic cracked regenerated processing method of a kind of built-up type, it is characterized in that: this method comprises the steps:
Step 1: reclaimable catalyst is mixed with oxygen-containing gas, is 650-730 ℃ burning temperature, and the revivifier top pressure is under the condition of 0.12-0.2Mpa, and the coke of burning-off 60-80% and whole hydrogen generate half regenerated catalyst; What generate contains CO
2, CO and water vapour mixed flue gas, immediately with catalyst separating.
Step 2: half regenerated catalyst is continued to mix with oxygen-containing gas, and burning temperature is 680-750 ℃, continues to burn, and generates and contains CO
2, a small amount of CO and excess oxygen mixed flue gas and regenerator.
2, the catalytic cracked regenerated processing method of built-up type according to claim 1 is characterized in that: the gas-operated linear speed scope in the described step 1 is 0.5-1.2m/s.
3, the catalytic cracked regenerated processing method of built-up type according to claim 1 is characterized in that: the gas-operated linear speed scope in the described step 2 is 4-16m/s.
4, the catalytic cracked regenerated processing unit of a kind of built-up type, comprise conventional turbulent bed revivifier, it is characterized in that: on described turbulent bed revivifier, increase postposition and burn device, this burns device and mainly comprises: coke-burning riser, inclined tube and gas-solid separation member, turbulent bed revivifier bottom is connected with inclined tube with the coke-burning riser bottom, the coke-burning riser top exit is connected with the gas solid separation part, reclaimable catalyst at first enters the turbulent bed revivifier and partly burns, the containing water vapor flue gas rises to the revivifier dilute phase, after cyclonic separation, discharge, half regenerated catalyst enters rearmounted coke-burning riser to be continued to burn, the gas solid separation part of coke-burning riser outlet separates catalyzer with flue gas, generate regenerator and Returning reacting system.
5, the catalytic cracked regenerated processing unit of built-up type according to claim 4, it is characterized in that: described inclined tube is provided with pneumavalve, is used for the flow of control catalyst.
6, the catalytic cracked regenerated processing unit of built-up type according to claim 4, it is characterized in that: the close dividing plate of setting up mutually of described turbulent bed revivifier, partly burn half regenerated catalyst that the back generates in dividing plate one side, enter and burn generation regenerator in back in the coke-burning riser, regenerator enters the opposite side Returning reacting system of dividing plate.
7, the catalytic cracked regenerated processing unit of built-up type according to claim 4, it is characterized in that: a surge tank is set up in the below of described coke-burning riser, by the isolated regenerator of gas solid separation part of coke-burning riser outlet through the surge tank Returning reacting system.
8, the catalytic cracked regenerated processing unit of built-up type according to claim 7, it is characterized in that: set up second cyclonic separator after the described coke-burning riser outlet gas-solid separation member, be used to alleviate the load of first cyclonic separator in the revivifier, two strands of flue gases separating from first and second cyclonic separator converge outside revivifier.
9, according to the catalytic cracked regenerated processing unit of each described built-up type of claim 4-8, it is characterized in that: described gas solid separation part is an arched door shape housing, the arched door two ends are respectively gas-solid mixture inlet and solid particulate outlet, with the concentric pipe core that is provided with of arched door circular arc, this pipe core is a pneumatic outlet, it is contained in the intravital body of shell and has two vertical narrow slits vertically, the aperture of narrow slit is respectively α angle and β angle, article two, the angle of offering of narrow slit is the γ angle, it is identical with the housing width to offer length, according to the flow of catalyzer and the requirement of separation efficiency, α, the size at β angle is 15 °-35 °, the γ angle is 20 °-60 °, and the arc radius of pipe core and arched door housing is than r: R=1/2-2/3, the R of arched door height H=(0.5-3).
10, the catalytic cracked regenerated processing unit of built-up type according to claim 9 is characterized in that: described α angle and β angle equate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410030876 CN1253534C (en) | 2004-04-07 | 2004-04-07 | Method of combined catalytic cracking regeneration technology and equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410030876 CN1253534C (en) | 2004-04-07 | 2004-04-07 | Method of combined catalytic cracking regeneration technology and equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1626622A true CN1626622A (en) | 2005-06-15 |
| CN1253534C CN1253534C (en) | 2006-04-26 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 200410030876 Expired - Lifetime CN1253534C (en) | 2004-04-07 | 2004-04-07 | Method of combined catalytic cracking regeneration technology and equipment |
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| CN (1) | CN1253534C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101875858A (en) * | 2009-04-30 | 2010-11-03 | 中国石油化工股份有限公司 | Method for treating solid particles of deposited carbon-containing compound |
| CN103721761A (en) * | 2012-10-12 | 2014-04-16 | 中国石油化工股份有限公司 | Catalyst regeneration method capable of reducing carbon dioxide discharge and improving selectivity |
| CN104099126A (en) * | 2013-04-08 | 2014-10-15 | 中石化洛阳工程有限公司 | Catalytic cracking unit |
| CN104974783A (en) * | 2014-04-08 | 2015-10-14 | 中石化洛阳工程有限公司 | Catalytic cracking method |
| CN105396518A (en) * | 2015-11-10 | 2016-03-16 | 清华大学 | Coal gasification ash oxidation decarburization combined circulating fluidized bed reactor |
| CN106890681A (en) * | 2017-04-20 | 2017-06-27 | 上海蓝科石化环保科技股份有限公司 | A kind of catalytic cracked regenerated system and method |
-
2004
- 2004-04-07 CN CN 200410030876 patent/CN1253534C/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101875858A (en) * | 2009-04-30 | 2010-11-03 | 中国石油化工股份有限公司 | Method for treating solid particles of deposited carbon-containing compound |
| CN101875858B (en) * | 2009-04-30 | 2014-03-26 | 中国石油化工股份有限公司 | Method for treating solid particles of deposited carbon-containing compound |
| CN103721761A (en) * | 2012-10-12 | 2014-04-16 | 中国石油化工股份有限公司 | Catalyst regeneration method capable of reducing carbon dioxide discharge and improving selectivity |
| CN103721761B (en) * | 2012-10-12 | 2015-10-28 | 中国石油化工股份有限公司 | A kind of reduction CO2 emission also improves optionally catalyst recovery process |
| CN104099126A (en) * | 2013-04-08 | 2014-10-15 | 中石化洛阳工程有限公司 | Catalytic cracking unit |
| CN104974783A (en) * | 2014-04-08 | 2015-10-14 | 中石化洛阳工程有限公司 | Catalytic cracking method |
| 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 |
| CN106890681A (en) * | 2017-04-20 | 2017-06-27 | 上海蓝科石化环保科技股份有限公司 | A kind of catalytic cracked regenerated system and method |
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| Publication number | Publication date |
|---|---|
| CN1253534C (en) | 2006-04-26 |
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