CN101993712B - Method for flexibly adjusting catalytic cracking reaction-regeneration system heat balance - Google Patents
Method for flexibly adjusting catalytic cracking reaction-regeneration system heat balance Download PDFInfo
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- CN101993712B CN101993712B CN 200910162649 CN200910162649A CN101993712B CN 101993712 B CN101993712 B CN 101993712B CN 200910162649 CN200910162649 CN 200910162649 CN 200910162649 A CN200910162649 A CN 200910162649A CN 101993712 B CN101993712 B CN 101993712B
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Abstract
The invention relates to a method for flexibly adjusting catalytic cracking reaction-regeneration system heat balance. A conventional regenerated catalyst heat remover which is arranged beside a regenerator and a regenerated catalyst cooler which is arranged on a regenerated catalyst conveying pipe are coupled and linked so that the catalyst bed temperature in the regenerator is controlled in one aspect to solve the problem of catalyst inactivation because of overhigh temperature caused by great scorching amount in a traditional heavy oil catalytic cracking device and too much heat in the regenerator, and the carried heat and the temperature of the regenerated catalyst entering a lifting pipe reactor are adjusted in the other aspect to adjust ratios of different catalyst and oil needed for raw materials with different properties in cracking reactions. The invention takes heat and adjusts the temperatures of high-temperature regenerated catalysts in different positions in a traditional heavy oil catalytic cracking device and flexibly adjusts the reaction-regeneration system heat balance so as to optimize heavy oil catalytic cracking process conditions and remarkably improve the yield of light oil and liquid.
Description
Technical field
The present invention relates to a kind of method of adjusting heavy oil catalytically cracking equipment reaction-regeneration system heat balance, belong to the Petroleum Processing Technology field.
Background technology
In catalytic cracking unit, catalyzer coke burning regeneration process discharges amount of heat, because catalyzer circulating between revivifier-reactor, the heat energy of high potential temperature is carried and enters the needs that riser reactor satisfies the cracking reaction of lower temperature position, thereby keep the temperature that regeneration and cracking process all reach to be needed, realize the heat balance of heavy oil catalytically cracking equipment reaction-regeneration system.Yet, the catalytically cracked material heaviness is on the rise in recent years, its density, carbon residue and colloid, bitum content increase gradually, consequently coke yield rises in the reaction process, revivifier inner catalyst burning process liberated heat is greater than reaction-regeneration system institute heat requirement, causes that heat is superfluous, regeneration temperature is too high.Therefore, on the revivifier of heavy oil catalytically cracking equipment the heat-obtaining facility must be installed, take out superfluous heat, the guarantee regeneration temperature is not too high, prevents the catalyzer hydrothermal deactivation, can keep the heat balance of reaction-regeneration system simultaneously.In addition on the one hand, in riser reactor, the heavy oil catalytic cracking reaction process is typical gas-liquid-solid heterogeneous thermo-negative reaction process, regenerated catalyst carries sufficient heat and contacts with stock oil, promote the macromolecular vaporization of heavy oil and cracking reaction further occurs, wherein contact fully fast, mix the matter and energy transmission that can effectively promote between the two between oil, the agent, this is most important for improving heavy-oil catalytic reaction transformation efficiency.But, for present heavy oil catalytically cracking equipment, because the excess Temperature (up to 690～710 ℃) of regenerated catalyst, the catalytic amount that enters riser reactor is controlled in the less scope (be generally stock oil inlet amount 5～7 times) just can carry enough heats, satisfies the needs that heavy oil cracking is reacted in the riser reactor.If the internal circulating load of regenerated catalyst is too high, will cause the riser reactor interior reaction temperature too high, the thermally splitting side reaction rolls up, product distribution variation-particularly coke yield increases thereby make, and this burns the further burden that increased to revivifier again.
For the heat balance of adjusting catalytic cracking reaction-regeneration system rapidly, at present conventional method is that revivifier at heavy oil catalytically cracking equipment arranges inside and outside heat collector, for example the patent of Chinese patent 901010480,901034134,921015321 discloseder inside and outside heat collector aspects.The common feature of these patents is that the heat that produces in, the revivifier high when coke yield is when superfluous, thereby take the heat balance that a part of heat is kept reaction-regeneration system away by heat collector, key is to guarantee not superelevation of revivifier reaction bed temperature, to prevent catalyzer serious hydrothermal deactivation occurs in regenerative process.These methods have played positive effect for the reaction-regeneration system heat balance of keeping heavy oil catalytically cracking equipment, but in order to guarantee to burn fully, recover catalyst activity, the revivifier reaction bed temperature must maintain 680～710 ℃, otherwise will affect catalyzer regeneration effect, the carbon of deciding on the regenerated catalyst is increased.Because the catalyst temperature too high (up to 690～720 ℃) after the regeneration, this has just seriously limited the catalyst recirculation amount that enters riser reactor, otherwise the too much heat that high temperature catalyst carries can make the heat cracking reaction in the reactor increase, and the catalytic cracking reaction environment is worsened.
Yet, if under the prerequisite that guarantees the suitable regeneration temperature of revivifier inner catalyst, by appropriate means heat and temperature thereof that the regenerated catalyst that enters riser reactor carries are regulated, then can need heat to adjust flexibly the catalyst recirculation amount that enters riser reactor in the situation that satisfy cracking reaction, this will create good environment for heavy oil catalytic cracking reaction in riser reactor, be mainly manifested in: the raising of (1) regenerated catalyst internal circulating load means that riser reactor unit space catalyst particles number increases, distance reduces between the particle, this will make the probability of collision of granules of catalyst and heavy oil atomizing liquid grain significantly increase, thereby strengthened stock oil, heat transmission between the granules of catalyst is conducive to fast vaporizing and the cracking reaction of heavy oil.(2) the regenerated catalyst internal circulating load improves the catalyst active center's number that makes riser reactor participate in catalytic cracking reaction increases, catalyzer overall activity in the reactor is improved, this is a significant benefit to the raising reaction preference, the product that improves heavy oil fluid catalytic cracking distributes, and obtains higher yield of light oil and liquid yield.
In order to improve catalyst recirculation amount or the agent-oil ratio of reaction process (participating in the catalyst recirculation amount of reaction and the mass ratio of stock oil inlet amount) in the FCC riser, Chinese patent CN99120529 discloses a kind of method of cooling of regenerated catalyst, the method is that the cooled catalyzer of the part in the revivifier heat collector is introduced riser reactor to improve the catalyst recirculation amount in the FCC riser, and a part of cooled catalyzer returns revivifier to regulate the revivifier reaction bed temperature in addition.But, in riser reactor, realize the suitable temperature of reaction under the high catalyst internal circulating load, the revivifier reaction bed temperature that requires simultaneously to keep higher is to guarantee the regeneration effect of catalyzer, only rely on the independent regenerated catalyst interior heat collecting device of the use of describing in the above-mentioned patent to realize that two-ways regulation is difficult to realize in engineering, need the heat-obtaining load of revivifier heat collector to increase substantially because improve riser reactor inner catalyst internal circulating load, this must disturb the revivifier reaction bed temperature.
Chinese patent CN99120517 discloses a kind of heavy oil fluid catalytic cracking regenerated catalyst method of cooling, this method only relies on the regenerated catalyst water cooler of installing on the regenerator line of pipes to reduce regenerated catalyst temperature, to improve the catalyst recirculation amount in the FCC riser, but the method does not consider to regulate heat collector inner catalyst material level to realize the flexible of heat-obtaining load, has therefore that the heat-obtaining load is relatively fixing, the poor shortcoming of adjustable elastic.If the fcc raw material character of riser reactor becomes heavy and difficult gasification, material gasification needs higher regenerated catalyst temperature, and then this technology must improve and burns temperature in the revivifier and realize, consequently will make the hydrothermal deactivation aggravation of revivifier inner catalyst; If do not improve regenerated catalyst temperature, can cause material gasification poor, dry gas and coke yield rise in the reaction process, and yield of light oil descends.
Chinese patent CN 200710054737.1, Chinese patent CN200710054739.0, Chinese patent CN200710054738.6, Chinese patent 200710054772.3 disclose the regenerated catalyst thermoregulation equipment of catalytic cracking unit, this equipment is mainly by regulating the fluidisation air quantity in the temperature equipment, change beds density and height, realize the adjusting of heat transfer coefficient and heat-obtaining area, thereby reach the adjusting of the regenerated catalyst temperature that enters riser reactor and the raising of reaction process agent-oil ratio.But, rely on the temperature equipment of describing in the above-mentioned patent to realize that heat-obtaining load and the two-way raising of agent-oil ratio are implemented difficulty in engineering large.For example, when requiring to increase the heat-obtaining load, must temperature equipment inner catalyst bed expansion (increase heat transfer area), raising catalyzer less turbulence (raising heat transfer coefficient) be realized by improving the fluidisation air quantity, but after expanding, beds makes beds mean density decrease, this can cause catalyzer to enter the reduction of riser reactor impellent, make simultaneously to enter riser reactor and get the catalyst entrainment gas volume and increase, these have all directly affected the raising of reaction process agent-oil ratio.Simultaneously, the thermoregulation range that these patents propose regenerated catalyst is 630～660 ℃, but this temperature range is not all feasible to any device, particularly when the coke yield of device is hanged down, the heat-obtaining amount that regenerated catalyst is cooled to 630～660 ℃ of needs is too large, cause regeneration temperature excessively low, affect the catalyzer coke burning regeneration.And 630～660 ℃ of these temperature ranges are obviously on the low side to the large raw material of catalytic cracking unit processing carbon residue, can cause high boiling component to be difficult to gasification; And for the raw material of carbon residue less than 4.0wt%, 630～660 ℃ of these temperature ranges are obviously higher again, can cause the heat cracking reaction inhibition poor.
Chinese patent CN2005100585695.4 discloses a kind of method for catalytic conversion of heavy oil and device thereof, the method has proposed two riser tube reactive systems, or riser reactor is divided into two reaction zones and carries out two strands of cooled catalysts and participate in reaction, the operation of rising agent oil ratio, the method does not illustrate how to realize heat-obtaining burden apportionment and adjusting between revivifier and the reactor when cooling off respectively two strands of catalyzer, the method is non-for the present conventional catalytic cracking riser reaction decorum simultaneously, and those skilled in the art can not be pushed into the conventional riser tube reaction decorum with its invention according to this instruction.
Comprehensive above-mentionedly can find out, previous patent is when emphasizing that the regenerated catalyst before entering riser reactor carried out the invention of heat-obtaining cooling, do not relate to revivifier operation and the device heat balance keep the particularly adjustment of conventional heat collector and matching operation.
Summary of the invention
The method that the purpose of this invention is to provide flexible adjustment heavy oil catalytic cracking reaction-regeneration system rapidly heat balance.For heavy oil catalytically cracking equipment, reaction process green coke amount is larger, for fully recovering catalyst activity, must in revivifier, the carbon of deciding on the catalyzer be down to very low level (as below 0.1%), this need to keep higher revivifier reaction bed temperature, will prevent also that simultaneously excess Temperature from causing the catalyzer hydrothermal deactivation; Yet higher regenerated catalyst temperature has restricted again the required high catalyst internal circulating load of riser reactor.Therefore, the heat balance of adjusting flexibly the heavy oil catalytically cracking equipment reaction-regeneration system need to be from taking into account the consideration that needs of reaction-regeneration two aspects, need on the one hand to utilize the conventional inside and outside heat collector of revivifier that the superfluous heat that revivifier burns rear generation is taken out, cooled catalyzer returns revivifier, reaches the purpose that satisfies heat balance, keeps suitable regeneration temperature; On the other hand, by different regenerated catalyst water cooler decoration forms and the control mode of heat-obtaining amount thereof, the high-temperature regenerated catalyst that will participate in catalytic cracking reaction according to the characteristics of feedstock property carries out flexible heat-obtaining, then enter riser reactor, to improve catalyst recirculation amount and agent-oil ratio, realize the purpose that optimizing product distributes.This heat regulation mode of carrying out heat-obtaining for different " position ", objectively satisfy reactive system and improved the catalyst recirculation amount to regulating regenerated catalyst temperature, regeneration system rapidly burns this two aspect of recovery catalyst activity to the different demands of service temperature to keeping higher optimal temperature, can be in improving riser reactor in the agent-oil ratio, keep relatively high regeneration temperature, decide carbon thereby process higher regeneration temperature relatively independently to satisfy the reduction regenerator, recover regeneration requirement and the rising agent oil ratio of catalyst activity, improving product distributes, contradiction between the reactive system that improves the quality of products requires.
To achieve these goals, flexible adjustment heavy oil catalytic cracking reaction provided by the invention-regeneration system rapidly heat balance method comprises the steps:
Revivifier at heavy oil catalytically cracking equipment arranges the conventional catalyst heat collector, to enter a part of high temperature catalyst behind the revivifier coke burning regeneration (account for revivifier catalyst inventory 1%～20%) by catalyst transport introduces the conventional catalyst heat collector and carries out heat-obtaining, low temperature catalyst behind the heat-obtaining returns revivifier by catalyst transport and catalyst stream control valve, high temperature catalyst in the low temperature catalyst that returns and the revivifier mixes, thereby realize the adjusting of revivifier inner catalyst bed temperature, the regulation range of revivifier reaction bed temperature is 680～700 ℃.The catalyst recirculation amount that enters the conventional catalyst heat collector is regulated by the catalyst stream control valve on the catalyst transport, and the heat-obtaining amount is regulated by the catalyst recirculation amount that enters heat collector and heat-eliminating medium (water or low-pressure water steam) flow.
Simultaneously, with the other regenerated catalyst water cooler that arranges of the revivifier of the heavy oil catalytically cracking equipment of conventional catalyst heat collector, the high-temperature regenerated catalyst that revivifier comes is suitably lowered the temperature by transfer lime and the part or all of regenerated catalyst water cooler of newly establishing of introducing of catalyst stream control valve, regenerated catalyst water cooler heat-obtaining amount is regulated by the catalyzer material level (being the reserve of water cooler inner catalyst) in the control water cooler and the flow of heat-eliminating medium (water or low-pressure water steam), and the character adjustment that the cooled temperature range of regenerated catalyst processes raw material according to device, then introduce riser reactor and stock oil contact reacts, enter the regenerated catalyst internal circulating load of riser reactor by regulating the control of regenerated catalyst flowrate control valve, with control regenerated catalyst and stock oil in riser reactor the initial mixing temperature and agent-oil ratio in optimum range, to realize the optimization of product distribution.
In the above-mentioned steps, in order to realize the different agent-oil ratio operations of riser reactor, keeping under 680～700 ℃ of conditions of regenerator temperature, total heat-obtaining amount of device is born simultaneously by conventional catalyst heat collector on the revivifier and regenerated catalyst water cooler and is regulated;
In the above-mentioned steps, the regenerated catalyst water cooler is a cylindrical tube, inner barrel is provided with some heat removing tubes and carries out heat exchange to pass into heat-eliminating medium (water or low-pressure water steam), cylinder body bottom arranges a gas distribution tube, fluidizing agent (air or water vapour) enters in the regenerated catalyst water cooler by gas distribution tube, thereby by beds density and reserve in the flow adjusting regenerated catalyst water cooler of adjustments of gas.The top of regenerated catalyst water cooler, top, bottom respectively be equipped with catalyst transport respectively revivifier be connected with riser reactor.High-temperature regenerated catalyst enters the regenerated catalyst water cooler by the catalyst transport that links to each other with regenerated catalyst water cooler top, enter riser reactor by the catalyst transport that links to each other with regenerated catalyst water cooler bottom after the heat exchange, and a part of catalyzer after the heat exchange also can return revivifier by the catalyst transport that links to each other with regenerated catalyst water cooler top in the regenerated catalyst water cooler under the effect of fluidizing agent;
In the above-mentioned steps, for different heavy oil feedstocks, regenerated catalyst before entering riser reactor and the stock oil contact mixing need to keep different optimum tempss, to guarantee effective gasification of heavy oil feedstock, that is: when the heavy oil feedstock carbon residue greater than 5.0w%, the regenerated catalyst optimum temps is 660～670 ℃; When the heavy oil feedstock carbon residue is 4.0～5.0w%, the regenerated catalyst optimum temps is 640～660 ℃; When the heavy oil feedstock carbon residue less than 4.0w%, the regenerated catalyst optimum temps is 610～640 ℃;
In the above-mentioned steps, for different heavy oil feedstocks, there is optimum range in regenerated catalyst and stock oil initial mixing temperature and the agent-oil ratio in riser reactor, to guarantee to reduce the generation of heat cracking reaction, optimizing product distributes, and will keep different agent-oil ratios when namely regenerated catalyst mixes from stock oil in riser reactor, when the heavy oil feedstock carbon residue greater than 5.0w%, 550～580 ℃ of best finish mixing temperatures, best agent-oil ratio is 8～9; When the heavy oil feedstock carbon residue is 4.0～5.0w%, 540～570 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8; When the heavy oil feedstock carbon residue less than 4.0w%, 530～560 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8;
The below is described in detail technical scheme of the present invention with reference to the accompanying drawings and specific embodiment.
Description of drawings
Fig. 1, Fig. 2 and Fig. 3 are the schematic diagram of the embodiment of the invention.
Embodiment 1
The visible Fig. 1 of flow process of the present invention, be summarized as follows: the revivifier 1 at heavy oil catalytically cracking equipment arranges conventional catalyst heat collector 4, a part of high temperature catalyst in the revivifier 1 (account for revivifier catalyst inventory 1%～20%) returns revivifier by catalyst transport 18 and catalyst stream control valve 19 after entering conventional catalyst heat collector 4 and heat-eliminating medium 13 (water or low-pressure water steam) heat-shift, the catalyst recirculation amount that enters conventional catalyst heat collector 4 is regulated by the aperture of control catalyst stream control valve 19, and the heat-obtaining amount is regulated by the flow of the internal circulating load that enters the heat collector inner catalyst and heat-eliminating medium 13 (water or low-pressure water steam).The low temperature catalyst (560～660 ℃) that returns in the revivifier mixes with high temperature catalyst in the revivifier, thus the adjusting of realization revivifier inner catalyst bed temperature, and the regulation range of revivifier reaction bed temperature is 680～700 ℃.
Simultaneously on revivifier 1 next door regenerated catalyst water cooler 3 is set, regenerated catalyst water cooler 3 is cylindrical tubes, inner barrel arranges some heat removing tubes and carries out heat exchange to pass into heat-eliminating medium 12 (water or low-pressure water steam), the cylindrical shell inner bottom part arranges a gas distribution tube 18, fluidizing agent 14 (air or water vapour) enters in the regenerated catalyst water cooler 3 by gas distribution tube 18, thereby by beds density and reserve in the flow adjusting regenerated catalyst water cooler 3 of adjustments of gas 14.The top of regenerated catalyst water cooler 3, top, bottom respectively are equipped with catalyst transport and are connected with riser reactor 2 with revivifier 1 respectively.High-temperature regenerated catalyst enters regenerated catalyst water cooler 3 by the catalyst transport 6 that links to each other with regenerated catalyst water cooler 3 tops, enter riser reactor 2 by the catalyst transport 17 that links to each other with regenerated catalyst water cooler 3 bottoms after the heat exchange, and a part of catalyzer after the 3 interior heat exchange of regenerated catalyst water cooler also can return revivifier 1 by the catalyst transport 15 that links to each other with regenerated catalyst water cooler 3 tops under the effect of fluidizing agent 14.
From revivifier 1 high-temperature regenerated catalyst out by transfer lime 6 enter regenerated catalyst water cooler 3 by heat transferring medium 12 suitably lower the temperature (when the heavy oil feedstock carbon residue greater than 5.0w%, the regenerated catalyst optimum temps is 660～670 ℃; When the heavy oil feedstock carbon residue is 4.0～5.0w%, the regenerated catalyst optimum temps is 640～660 ℃; When the heavy oil feedstock carbon residue less than 4.0w%, the regenerated catalyst optimum temps is 610～640 ℃), regenerated catalyst water cooler heat-obtaining amount and cooled regenerator temperature are regulated by the catalyzer material level in the regenerated catalyst water cooler 3 and the flow of heat-eliminating medium 12 (water or low-pressure water steam).When for example increasing the heat-obtaining amount and requiring cooled regenerator temperature low, can by the flow that increases heat-eliminating medium 12 or the aperture of turning the catalyst stream control valve 8 on the catalyst transport 17 down, the catalyzer material level in the regenerated catalyst water cooler 3 be improved.Cooled regenerated catalyst is through regenerated catalyst guiding valve 8 and catalyst transport 17 enters riser reactor 2 and make progress under the castering action of lift gas 10 mobile and stock oil contact reacts, and the temperature of reaction in the riser reactor 2 are controlled by the regenerated catalyst internal circulating load that enters riser reactor 2 by regulating regenerated catalyst guiding valve 8 apertures; Control catalyzer and initial mixing temperature and the agent-oil ratio of stock oil in heavy oil riser reactor 2 are in the optimized scope, (when the heavy oil feedstock carbon residue greater than 5.0w%, 550～580 ℃ of best finish mixing temperatures, best agent-oil ratio are 8～9; When the heavy oil feedstock carbon residue is 4.0～5.0w%, 540～570 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8; When the heavy oil feedstock carbon residue less than 4.0w%, 530～560 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8), the heavy oil feedstock preheating temperature is 200～300 ℃.After reacted catalyzer and oil gas separated through oil and gas separating system 9, oil gas went out catalytic cracking unit and catalyzer enters stripping stage 5 strippings, after enter revivifier 1 through catalyst transport 7 and contact coke burning regeneration with main air 11.
Flow process of the present invention is visible Fig. 2 also, be summarized as follows: the revivifier 1 at heavy oil catalytically cracking equipment arranges conventional catalyst heat collector 4, a part of high temperature catalyst in the revivifier 1 (account for revivifier catalyst inventory 1%～20%) returns revivifier by catalyst transport 18 and catalyst stream control valve 19 after entering conventional catalyst heat collector 4 and heat-eliminating medium 13 (water or low-pressure water steam) heat-shift, the catalyst recirculation amount that enters conventional catalyst heat collector 4 is regulated by the aperture of control catalyst stream control valve 19, and the heat-obtaining amount is regulated by the flow of the internal circulating load that enters the heat collector inner catalyst and heat-eliminating medium 13 (water or low-pressure water steam).The low temperature catalyst (550～660 ℃) that returns in the revivifier mixes with high temperature catalyst in the revivifier, thus the adjusting of realization revivifier inner catalyst bed temperature, and the regulation range of revivifier reaction bed temperature is 680～700 ℃.
Simultaneously on revivifier 1 next door regenerated catalyst water cooler 3 is set, regenerated catalyst water cooler 3 is cylindrical tubes, inner barrel arranges some heat removing tubes and carries out heat exchange to pass into heat-eliminating medium 12 (water or low-pressure water steam), cylinder body bottom arranges a gas distribution tube 18, fluidizing agent 14 (air or water vapour) enters in the regenerated catalyst water cooler 3 by gas distribution tube 18, thereby by beds density and reserve in the flow adjusting regenerated catalyst water cooler 3 of adjustments of gas 14.The top of regenerated catalyst water cooler 3, top, bottom respectively are equipped with catalyst transport and are connected with riser reactor 2 with revivifier 1 respectively.High-temperature regenerated catalyst enters regenerated catalyst water cooler 3 by the catalyst transport 6 that links to each other with regenerated catalyst water cooler 3 tops, enter riser reactor 2 by the catalyst transport 17 that links to each other with regenerated catalyst water cooler 3 bottoms after the heat exchange, and a part of catalyzer after the 3 interior heat exchange of regenerated catalyst water cooler also can return revivifier 1 by the catalyst transport 15 that links to each other with regenerated catalyst water cooler 3 tops under the effect of fluidizing agent 14.
Draw respectively the two-way regenerated catalyst from revivifier 1, one road high-temperature regenerated catalyst (account for enter riser reactor catalyzer total amount 10～90%) enters the bottom of riser reactor 2 by catalyst transport 20 and catalyst stream control valve 21; A part of high-temperature regenerated catalyst (account for enter riser reactor catalyzer total amount 10～90%) enters regenerated catalyst water cooler 3 by transfer lime 6 and suitably lower the temperature by heat-eliminating medium 12 in addition, and regenerated catalyst water cooler heat-obtaining amount and cooled regenerator temperature are regulated by the interior catalyzer material level of regenerated catalyst water cooler 3 and the flow of heat-eliminating medium 12 (water or low-pressure water steam).When for example increasing the heat-obtaining amount and requiring cooled regenerator temperature low, can by the flow that increases heat-eliminating medium 12 or the aperture of turning the catalyst stream control valve 8 on the catalyst transport 17 down, the catalyzer material level in the regenerated catalyst water cooler 3 be improved.Cooled regenerated catalyst enters riser reactor 2 bottoms through regenerated catalyst guiding valve 8 and catalyst transport 17.
Above-mentioned two-way regenerated catalyst of drawing from revivifier 1 enters the catalyst mix device 22 of riser reactor 2 bottoms and fully mixes, and under the castering action of lift gas 10, upwards flow and the stock oil contact reacts, regulate the heat-obtaining amount of regenerated catalyst water cooler and the blending ratio of cold and hot two strands of regenerated catalysts, make enter the regenerated catalyst temperature of riser reactor before contacting with stock oil be in optimum range (when the heavy oil feedstock carbon residue greater than 5.0w%, the regenerated catalyst optimum temps is 660～670 ℃; When the heavy oil feedstock carbon residue is 4.0～5.0w%, the regenerated catalyst optimum temps is 640～660 ℃; When the heavy oil feedstock carbon residue less than 4.0w%, the regenerated catalyst optimum temps is 610～640 ℃), the temperature of reaction in the riser reactor 2 is controlled by the regenerated catalyst internal circulating load that enters riser reactor 2 by the aperture of regulating regenerated catalyst flow valve 8 and regenerated catalyst flow valve 21; Control catalyzer and initial mixing temperature and the agent-oil ratio of stock oil in heavy oil riser reactor 4 are in the optimized scope, (when the heavy oil feedstock carbon residue greater than 5.0w%, 550～580 ℃ of best finish mixing temperatures, best agent-oil ratio are 8～9; When the heavy oil feedstock carbon residue is 4.0～5.0w%, 540～570 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8; When the heavy oil feedstock carbon residue less than 4.0w%, 530～560 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8), the heavy oil feedstock preheating temperature is 200～300 ℃.After reacted catalyzer and oil gas separated through oil and gas separating system 9, oil gas went out catalytic cracking unit and catalyzer enters stripping stage 5 strippings, after enter revivifier 1 through catalyst transport 7 and contact coke burning regeneration with main air 11.
Embodiment 3
Flow process of the present invention is visible Fig. 3 also, be summarized as follows: the revivifier 1 at heavy oil catalytically cracking equipment arranges conventional catalyst heat collector 4, a part of high temperature catalyst in the revivifier 1 (account for revivifier catalyst inventory 1%～20%) returns revivifier by catalyst transport 18 and catalyst stream control valve 19 after entering conventional catalyst heat collector 4 and heat-eliminating medium 13 (water or low-pressure water steam) heat-shift, the catalyst recirculation amount that enters conventional catalyst heat collector 4 is regulated by the aperture of control catalyst stream control valve 19, and the heat-obtaining amount is regulated by the flow of the internal circulating load that enters the heat collector inner catalyst and heat-eliminating medium 13 (water or low-pressure water steam).The low temperature catalyst (550～660 ℃) that returns in the revivifier mixes with high temperature catalyst in the revivifier, thus the adjusting of realization revivifier inner catalyst bed temperature, and the regulation range of revivifier reaction bed temperature is 680～700 ℃.
On revivifier 1 next door regenerated catalyst water cooler 3 is set, regenerated catalyst water cooler 3 is cylindrical tubes, inner barrel arranges some heat removing tubes and carries out heat exchange to pass into heat-eliminating medium 12 (water or low-pressure water steam), cylinder body bottom arranges a gas distribution tube 18, fluidizing agent 14 (air or water vapour) enters in the regenerated catalyst water cooler 3 by gas distribution tube 18, thereby by beds density and reserve in the flow adjusting regenerated catalyst water cooler 3 of adjustments of gas 14.The top of regenerated catalyst water cooler 3, top, bottom respectively are equipped with catalyst transport and are connected with riser reactor 2 with revivifier 1 respectively.High-temperature regenerated catalyst enters regenerated catalyst water cooler 3 by the catalyst transport 6 that links to each other with regenerated catalyst water cooler 3 tops, enter riser reactor 2 by the catalyst transport 17 that links to each other with regenerated catalyst water cooler 3 bottoms after the heat exchange, and a part of catalyzer after the 3 interior heat exchange of regenerated catalyst water cooler also can return revivifier 1 by the catalyst transport 15 that links to each other with regenerated catalyst water cooler 3 tops under the effect of fluidizing agent 14.
Simultaneously on revivifier 1 next door regenerated catalyst water cooler 23 is set, regenerated catalyst water cooler 23 is cylindrical tubes, inner barrel arranges some heat removing tubes and carries out heat exchange to pass into heat-eliminating medium 26 (water or low-pressure water steam), cylinder body bottom arranges a gas distribution tube 25, fluidizing agent 24 (air or water vapour) enters in the regenerated catalyst water cooler 23 by gas distribution tube 25, thereby by beds density and reserve in the flow adjusting regenerated catalyst water cooler 23 of adjustments of gas 24.The top of regenerated catalyst water cooler 23, bottom respectively are equipped with catalyst transport and are connected with riser reactor 2 with revivifier 1 respectively.High-temperature regenerated catalyst enters regenerated catalyst water cooler 23 by the catalyst transport 20 that links to each other with regenerated catalyst water cooler 3 tops, enters riser reactor 2 by the catalyst transport 27 that links to each other with regenerated catalyst water cooler 23 bottoms after the heat exchange.
Draw respectively the two-way regenerated catalyst from revivifier 1, part high-temperature regenerated catalyst (account for enter riser reactor catalyzer total amount 10～90%) enters regenerated catalyst water cooler 3 by transfer lime 6 suitably lower the temperature by heat transferring medium 12, and regenerated catalyst water cooler heat-obtaining amount and cooled regenerator temperature are regulated by the interior catalyzer material level of regenerated catalyst water cooler 3 and the flow of heat-eliminating medium 12 (water or low-pressure water steam).When for example increasing the heat-obtaining amount and requiring cooled regenerator temperature low, can by the flow that increases heat-eliminating medium 12 or the aperture of turning the catalyst stream control valve 8 on the catalyst transport 17 down, the catalyzer material level in the regenerated catalyst water cooler 3 be improved.Cooled regenerated catalyst enters riser reactor 2 bottoms through regenerated catalyst guiding valve 8 and catalyst transport 17.
Above-mentioned other one road high-temperature regenerated catalyst of drawing from revivifier 1 (account for enter riser reactor catalyzer total amount 10～90%) enters regenerated catalyst water cooler 23 by catalyst transport 20 and suitably is cooled to 550～660 ℃ by heat-eliminating medium 26, and regenerated catalyst water cooler 23 heat-obtaining amounts and cooled regenerator temperature are regulated by the flow of heat-eliminating medium 26 (water or low-pressure water steam).When for example increasing the heat-obtaining amount and requiring cooled regenerator temperature low, can be by increasing the flow of heat-eliminating medium 26.Cooled regenerated catalyst enters riser reactor 2 bottoms through regenerated catalyst guiding valve 21 and catalyst transport 27.
Above-mentioned two-way regenerated catalyst of drawing respectively from revivifier 1 enters after cooling the catalyst mix device 22 of riser reactor 2 bottoms and upwards flows and the stock oil contact reacts under the fully mixed castering action that is incorporated in lift gas 10, regulate the heat-obtaining amount of regenerated catalyst and the blending ratio of cold and hot two strands of regenerated catalysts, make enter the regenerated catalyst temperature of riser reactor before contacting with stock oil be in optimum range (when the heavy oil feedstock carbon residue greater than 5.0w%, the regenerated catalyst optimum temps is 660～670 ℃; When the heavy oil feedstock carbon residue is 4.0～5.0w%, the regenerated catalyst optimum temps is 640～660 ℃; When the heavy oil feedstock carbon residue less than 4.0w%, the regenerated catalyst optimum temps is 610～640 ℃), the temperature of reaction in the riser reactor 2 is controlled by the regenerated catalyst internal circulating load that enters riser reactor 2 by the aperture of regulating regenerated catalyst flow valve 8 and regenerated catalyst flow valve 21; Control catalyzer and initial mixing temperature and the agent-oil ratio of stock oil in heavy oil riser reactor 4 are in the optimized scope, (when the heavy oil feedstock carbon residue greater than 5.0w%, 550～580 ℃ of best finish mixing temperatures, best agent-oil ratio are 8～9; When the heavy oil feedstock carbon residue is 4.0～5.0w%, 540～570 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8; When the heavy oil feedstock carbon residue less than 4.0w%, 530～560 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8), the heavy oil feedstock preheating temperature is 200～300 ℃.After reacted catalyzer and oil gas separated through oil and gas separating system 9, oil gas went out catalytic cracking unit and catalyzer enters stripping stage 5 strippings, after enter revivifier 1 through catalyst transport 7 and contact coke burning regeneration with main air 11.
The method of a kind of flexible adjustment heavy oil catalytic cracking reaction provided by the present invention-regeneration system rapidly heat balance, its advantage is, by the regenerated catalyst heat-obtaining to different positions, the catalyzer that namely the revivifier inner catalyst is carried out being about to enter after heat-obtaining and the regeneration riser reactor carries out heat-obtaining, thereby to satisfy effectively reactive system require to reduce regenerated catalyst temperature to improve the catalyst recirculation amount, regeneration system rapidly requires to keep comparatively high temps to guarantee to burn effect to the different demands of service temperature separately, and this provides a kind of relative flexible for optimizing the riser reactor operational condition with the regeneration effect of guaranteeing the revivifier inner catalyst, control method independently.
Advantage of the present invention is by different positions high-temperature regenerated catalyst in the heavy oil catalytically cracking equipment being carried out the heat-obtaining temperature adjustment, adjust flexibly the reaction-regeneration system heat balance, thereby the problem that solves that the catalyst recirculation amount is subjected to the restriction of two device thermal equilibrium and can't flexible, the optimization of heavy oil catalytic cracking process condition be can realize, lightweight oil and liquid yield significantly improved.
Need to prove at last, above embodiment only is used for technical scheme of the present invention is described and unrestricted, although with reference to preferred embodiment the present invention is had been described in detail, 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 break away from the spirit and scope of technical solution of the present invention.
Embodiment 1
For verifying effect of the present invention, adopt technical process shown in Figure 2, carry out commerical test at 400,000 ton/years of heavy oil catalytically cracking equipments of certain refinery, test-results is listed in table 1.
After adopting this invention, in the situation that keep the revivifier reaction bed temperature at 690 ℃, the regenerated catalyst that enters riser reactor is cooled to 660 ℃, 560 ℃ of finish mixing temperatures, agent-oil ratio brings up to 9 from 6, temperature of reaction remains on 490 ℃, thereby makes yield of light oil improve 2.3 percentage points, and dry gas and coke yield obviously reduce.Can see Table 1 in detail.
Table 1 heavy oil feedstock character
| Project | Data | Project | Data |
| Density (20 ℃) kg/m 3 | 945 | Nitrogen content, ppm | 2000 |
| Carbon residue, wt% | 5.4 | Hydrocarbon group composition analysis | |
| Ultimate analysis | Stable hydrocarbon, wt% | 54.61 | |
| Hydrogen richness, wt% | 12.61 | Aromatic hydrocarbons, wt% | 24.96 |
| Carbon content, wt% | 86.82 | Colloid, wt% | 16.34 |
| Sulphur content, wt% | 0.3 | Bituminous matter, wt% | 4.09 |
Table 2 technological condition
| Project | The prior art scheme | The present invention program |
| The riser reactor temperature out, ℃ | 510 | 490 |
| Regenerator temperature, ℃ | 700 | 700 |
| The finish mixing temperature, ℃ | 550 | 560 |
| Enter the catalyst temperature of riser reactor, ℃ | 690 | 660 |
| The fuel oil preheating temperature, ℃ | 180 | 260 |
| Reaction times, s | 3.0 | 2.7 |
| Catalyst/feed oil, weight by weight | 6 | 9 |
Table 3 main products distributes
| Product distributes and character | The prior art scheme | The present invention program |
| H 2S | 0.5 | 0.7 |
| Fuel gas | 4.2 | 3.1 |
| Liquefied gas | 15.5 | 15.9 |
| Gasoline | 44.1 | 46.3 |
| Diesel oil | 25.3 | 25.4 |
| Clarified oil | 1.8 | 1.0 |
| Coke | 8.6 | 7.6 |
| Add up to | 100.0 | 100.0 |
Claims (5)
1. method of adjusting flexibly heavy oil catalytic cracking reaction-regeneration system rapidly heat balance, it is characterized in that: the revivifier at heavy oil catalytically cracking equipment arranges the conventional catalyst heat collector, realizes the adjusting of revivifier inner catalyst bed temperature by the circulating cooling of catalyzer; The regenerated catalyst water cooler is set between revivifier and riser reactor simultaneously, enter the regenerated catalyst water cooler from revivifier all or part of high-temperature regenerated catalyst out by transfer lime and suitably lower the temperature, then enter riser reactor by transfer lime and regenerated catalyst guiding valve; Regulate the heat-obtaining amount of conventional catalyst heat collector, regenerated catalyst water cooler by coupling linkage, realize the flexible of the heat balance of heavy oil catalytically cracking equipment reaction-regeneration system guaranteeing to improve under the good condition of revivifier inner catalyst reproduction condition the catalyst recirculation amount that enters riser reactor or agent-oil ratio.
2. the method for a kind of flexible adjustment heavy oil catalytic cracking reaction according to claim 1-regeneration system rapidly heat balance, it is characterized in that: in order to realize the different agent-oil ratio operations of riser reactor, keeping under 680～700 ℃ of conditions of regenerator temperature, total heat-obtaining amount of device is born simultaneously by revivifier conventional catalyst heat collector and regenerated catalyst water cooler and is regulated.
3. the method for a kind of flexible adjustment heavy oil catalytic cracking reaction according to claim 1-regeneration system rapidly heat balance, it is characterized in that: the regenerated catalyst water cooler is a cylindrical tube, inner barrel arranges some heat removing tubes and carries out heat exchange to pass into heat-eliminating medium, the cylindrical shell inner bottom part arranges a gas distribution tube, fluidizing agent enters in the regenerated catalyst water cooler by gas distribution tube, thereby by beds density and reserve in the flow adjusting regenerated catalyst water cooler of adjustments of gas; The top of regenerated catalyst water cooler, top, bottom respectively are equipped with catalyst transport and are connected with riser reactor with revivifier respectively; High-temperature regenerated catalyst enters the regenerated catalyst water cooler by the catalyst transport that links to each other with regenerated catalyst water cooler top, enter riser reactor by the catalyst transport that links to each other with regenerated catalyst water cooler bottom after the heat exchange, and a part of catalyzer after the heat exchange also can return revivifier by the catalyst transport that links to each other with regenerated catalyst water cooler top in the regenerated catalyst water cooler under the effect of fluidizing agent.
4. the method for a kind of flexible adjustment heavy oil catalytic cracking reaction according to claim 1-regeneration system rapidly heat balance, it is characterized in that: for different heavy oil feedstocks, regenerated catalyst before entering riser reactor and the stock oil contact mixing need to keep different optimum tempss, to guarantee effective gasification of heavy oil feedstock, that is: when the heavy oil feedstock carbon residue greater than 5.0w%, the regenerated catalyst optimum temps is 660～670 ℃; When the heavy oil feedstock carbon residue is 4.0～5.0w%, the regenerated catalyst optimum temps is 640～660 ℃; When the heavy oil feedstock carbon residue less than 4.0w%, the regenerated catalyst optimum temps is 610～640 ℃.
5. the method for a kind of flexible adjustment heavy oil catalytic cracking reaction according to claim 1-regeneration system rapidly heat balance, it is characterized in that: for different heavy oil feedstocks, there is optimum range in regenerated catalyst and stock oil initial mixing temperature and the agent-oil ratio in riser reactor, when the heavy oil feedstock carbon residue greater than 5.0w%, 550～580 ℃ of best finish mixing temperatures, best agent-oil ratio is 8～9; When the heavy oil feedstock carbon residue is 4.0～5.0w%, 540～570 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8; When the heavy oil feedstock carbon residue less than 4.0w%, 530～560 ℃ of best finish mixing temperatures, best agent-oil ratio are 7～8.
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