REGENERATION METHOD FOR CATALYTIC CRACKING REACTION

Abstract

A regeneration method for catalytic cracking reaction, the method is applied in a catalytic reaction process of petroleum hydrocarbon materials, and the method comprises: feeding the regenerated and semi-regenerated catalyst from a regenerator separately into different positions of a reactor for reaction. A part of the semi-regenerated catalyst is firstly processed in a purification cooler for removing carried nitrogen, oxygen, carbon dioxide and impurity gases before being fed into the reactor. Spent catalyst or the purified and cooled semi-regenerated catalyst is fed into a catalyst mixing section of the reactor for controlling the temperature of the catalyst being contact with the oil material to be gasified, thereby achieving a three stage cycle of the catalyst in the reactor and a three stage control for the reaction outlets of the oil material gasification zone and the cracking reaction zone and the catalyst taking part in the reaction.

Claims

1-19. (canceled)

20. A reaction-regeneration method for catalytic cracking reaction, for use in the process of catalytic reaction of petroleum hydrocarbon-based feedstock, comprising: arranging a regenerator, a reactor, and a catalyst purifying or stripping and cooling device in parallel, wherein: the regenerator is used for coke-burning regeneration of the spent catalyst fed from the reactor, and according to the flow direction of the fed spent catalyst and the coke-burning degree, the coke-burning zone of the regenerator is divided into a semi-regenerated catalyst section for semi-regenerated catalyst and a regenerated catalyst section for regenerated catalyst, wherein the regenerated catalyst section is located below the semi-regenerated catalyst section, and wherein the regenerator is provided with a returning pipe which introduces the semi-regenerated catalyst from the semi-regenerated catalyst section of the coke-burning zone into the regenerated catalyst section; the reactor has a riser reaction section as the main part, a catalyst mixing section with a enlarged diameter provided at the bottom, and feedstock oil inlets of the reactor located between the catalyst mixing section and the riser reaction section, wherein above the feedstock oil inlets are a feedstock oil vaporization zone and a catalytic cracking reaction zone in this order, and a settler is provided downstream of the catalytic cracking reaction zone; the spent catalyst from the reactor enters the semi-regenerated catalyst section of the coke-burning zone of the regenerator, and goes into contact and reacts with the oxygen-containing gas from below, to form semi-regenerated catalyst which then enters the regenerated catalyst section of the coke-burning zone via the returning pipe and goes into contact and reacts with the oxygen-containing gas from the bottom of the coke-burning zone to accomplish the regeneration and form regenerated catalyst; the regenerated catalyst is introduced into the catalyst mixing section of the reactor; a part of the semi-regenerated catalyst is drawn out of the regenerator; this part of the semi-regenerated catalyst first enters the catalyst purifying or stripping and cooling device wherein it is cooled to a required temperature and the gaseous medium carried by the catalyst is released or stripped by displacement, and then: enters the reactor from location above the feedstock oil inlet of the reactor to participate in the catalytic cracking reaction, or enters the catalyst mixing section at the bottom of the reactor to be mixed with the regenerated catalyst, and participates in the vaporization and catalytic cracking reaction of the feedstock oil, or is split into two streams, one of which enters the reactor from location above the feedstock oil inlets of the reactor, the other one of which enters the catalyst mixing section at the bottom of the reactor; the feedstock oil enters the reactor to contact with the catalyst so as to complete vaporization and catalytic cracking reaction; and after the reaction, the spent catalyst is subjected to gas-solid separation in the settler, then enters the steam stripping section for steam stripping, and then enters the regenerator for regeneration.

21. The method according to claim 20, wherein a dilute phase section is provided above the coke-burning zone of the regenerator, the coke-burning zone and the dilute phase section are vertically coaxially arranged, the flue gas in the coke-burning zone after the reaction moves upwards and enters the dilute phase section, the semi-regenerated catalyst carried by the flue gas is separated in the gas-solid separator, and the flue gas is discharged through a flue gas pipe.

22. The method according to claim 20, wherein a first distribution plate is provided in the coke-burning zone of the regenerator and below the inlet of the spent catalyst, and divides the coke-burning zone into a semi-regenerated catalyst section above the first distribution plate and a regenerated catalyst section below the first distribution plate.

23. The method according to claim 22, wherein a second distribution plate is further provided in the semi-regenerated catalyst section of the coke-burning zone of the regenerator, the second distribution plate placed above the inlet of the spent catalyst, and further clearly divides the semi-regenerated catalyst section into an upper sub-section and a lower sub-section, i.e., the first and second half-regeneration sections, wherein the first half-regeneration section is below the second half-regeneration section.

24. The method according to claim 22, wherein in the regenerator a part of oxygen-containing gas is introduced by a first gas distributor to enter the semi-regenerated catalyst section; preferably, the flux of the oxygen-containing gas that enters the semi-regenerated catalyst section is 30% to 40% of the total flux of the oxygen-containing gas into the regenerator.

25. The method according to claim 23, wherein a part of oxygen-containing gas is introduced by a second gas distributor to directly enter the upper section of the semi-regenerated catalyst section; preferably, the flux of this part of oxygen-containing gas is less than or equal to 10% of the total flux of the oxygen-containing gas into the regenerator.

26. The method according to claim 24, wherein a part of oxygen-containing gas is introduced by a second gas distributor to directly enter the upper section of the semi-regenerated catalyst section; preferably, the flux on this part of oxygen-containing gas is less than or equal to 10% of the total flux of the oxygen-containing gas into the regenerator.

27. The method according to claim 20, wherein the inside of the catalyst mixing section of the reactor is designed as a dense phase fluidized bed, and the gas apparent velocity of the catalyst fluidized bed is 0.2 to 0.6 m/s; and an internal catalyst-circulating and mixing conduit is provided inside the catalyst mixing section, so that the catalyst in the mixing section is circulated between the conduit and the fluidized bed in the mixing section.

28. The method according to claim 20, wherein a spent-catalyst returning pipe is provided between the steam stripping section of the reactor and the catalyst mixing section at the bottom of the reactor to return part of the spent catalyst to the catalyst mixing section.

29. The reaction-regeneration method for catalytic cracking reaction according to claim 20 is for the use in the process of catalytic reaction of petroleum hydrocarbon-based feedstock, comprising a regenerator, a reactor, and a catalyst purifying and cooling device in parallel, wherein double catalyst circulation of regenerated catalyst and semi-regenerated catalyst is formed between the reactor and the regenerator; according to the requirements of reaction, the regenerator simultaneously provides differently regenerated catalysts for the reactor, so that the thermal cracking reaction, especially in the vaporization and cracking reaction zones, can be reduced, the thermal equilibrium between vaporization and the reaction can be regulated, and multi-site control of the catalyst in each reaction zone can be conveniently and flexibly achieved; the reaction-regeneration method for catalytic cracking reaction is implemented in the following processes: 1) the regenerator is configured in a three-section regeneration form wherein the first section is set at the middle part of the coke-burning zone, the second section is set at the upper part of the coke-burning zone, and the third section of the regenerator is set at the bottom part of the coke-burning zone; the regenerator supplies the catalyst to the reactor in such a manner that the regenerated catalyst in regenerated catalyst section enters the catalyst mixing section below the feedstock oil inlet of the reactor; the semi-regenerated catalyst from the first or second section set in the coke-burning zone of the regenerator enters the catalyst purifying and cooling device first, where it is cooled to a required temperature and the gaseous medium carried by the catalyst is released or stripped by displacement, and then the catalyst enters the reactor from location above the feedstock oil atomizing nozzle to participate in the catalytic cracking reaction, or the semi-regenerated catalyst enters the catalyst mixing sect at the bottom of the reactor, is mixed with the regenerated catalyst to form a catalyst colder than the regenerated catalyst, and then the formed catalyst participates in the vaporization and reaction of the feedstock oil, or alternatively, the semi-regenerated catalyst from the first or second section in the coke-burning zone of the regenerator enters the catalyst purifying and cooling device first, where it is cooled to a required temperature and the gaseous medium carried by the catalyst is released or stripped by displacement, and then the resultant is split into two streams to respectively enter the reactor from location above the feedstock oil atomizing nozzle immediately after vaporization of the feedstock oil and enter the catalyst mixing section at the bottom of the reactor, to participate in the vaporization and the catalytic cracking reaction of the feedstock oil; the regenerated and semi-regenerated catalysts after undergoing the reaction in the reactor, i.e. the spent catalysts, are subjected to gas-solid separation in the settler, then enter the steam stripping section to undergo steam stripping, and then enter the semi-regenerated section of the regenerator for regeneration and reactivation; 2) a part of the spent catalyst in the steam stripping section returns to the catalyst mixing section at the bottom of the reactor via a spent-catalyst returning pipe, or the semi-regenerated catalyst from the first or second section in the coke-burning zone of the regenerator enters the catalyst purifying and cooling device first, where it is cooled to a required temperature and the gaseous medium carried by the catalyst is released or stripped by displacement, and then the resultant enters the catalyst mixing section at the bottom of the reactor; the returned spent catalyst or the purified cooled semi-regenerated catalyst is mixed with the regenerated catalyst fed from a regenerated-catalyst standpipe to form a catalyst colder than the regenerated catalyst, and the formed catalyst flows upwards under the action of a pre-lift medium to contact and vaporize the feedstock oil and catalyze the catalytic cracking reaction after the vaporization, and then the catalyst is subjected to gas-solid separation in the settler and enters the steam stripping section; the amount of the returned spent catalyst or the purified cooled semi-regenerated catalyst is controlled according to the required catalyst mixing temperature in the mixing section; 3) the reaction feedstock is atomized via the atomizing nozzle, then enters the vaporization zone of the reactor, comes into contact with the catalyst mixture from the catalyst mixing section at bottom, and is vaporized by absorbing the heat from the catalyst; the vaporized oil vapor and the catalyst are immediately and selectively mixed with the semi-regenerated catalyst from the purifying and cooling device to undergo gas-phase cracking reaction in a new catalytic environment; 4) at the bottom of the reactor is provided a catalyst mixing section having a diameter greater than that of the cracking reaction section of the riser to thoroughly mix the catalyst coming from the regenerated-catalyst standpipe and the spent-catalyst returning pipe or the purifying and cooling device; the inside of the catalyst mixing section is designed as a dense phase fluidized bed, and the gas apparent velocity of the catalyst fluidized bed is 0.2 to 0.6 m/s; the pre-lift medium enters the reactor at the bottom the catalyst mixing section to thoroughly mix the catalyst and meanwhile transport the catalyst; 5) preferably, the catalyst purifying and cooling device includes a catalyst cooling portion and a carried-gas stripping portion; a heat-exchange tube is provided within the catalyst cooling portion, so that the cooling medium is circulated inside the tube and the catalyst is outside the tube; the catalyst enters the purifying and cooling device from the inlet pipe and is discharged to the reactor via a transporting pipe; steam or nitrogen gas serves as the stripping medium which enters the purifying and cooling device at the bottom, and the stripping medium and the gas carried by the catalyst are discharged from gas-discharge pipe; 6) after reaction, the catalyst and the product gas of reaction in the reactor are separated by a gas-solid separator, the product gas of reaction enters a fractionation column, and the catalyst enters the steam stripping section for stripping, the stripped spent catalyst returns to the regenerator via the spent-catalyst standpipe to undergo regeneration, and turns to regenerated catalyst and semi-regenerated catalyst which then returns to the reactor to participate in the reaction; 7) after the carried hydrocarbons is stripped off in the steam stripping section, via the spent-catalyst standpipe the spent catalyst enters the inlet provided above the regenerated-catalyst outlet and enters the first section of the coke-burning zone of the regenerator, and reacts with the oxygen-containing gas coming from below, to form semi-regenerated catalyst in the first and second sections; the semi-regenerated catalyst in the second section returns to the lowest third section of the regenerator via a semi-regenerated catalyst returning pipe to continue to be regenerated into regenerated catalyst; the regenerated catalyst is directed out of the outlet below the spent catalyst inlet, and enters the catalyst mixing section at the bottom of the reactor via the regenerated-catalyst standpipe; a part of the semi-regenerated catalyst is directed out of the regenerator from outlet above the spent catalyst inlet, and enters the reactor after being processed in the catalyst purifying and cooling device; and the flue gas in the regenerator moves upwards and enters the dilute phase section, and is discharged via the flue gas pipe after the catalyst is separated by a gas-solid separator.

30. The method according to claim 20, wherein a heat exchange tube is installed in the upper part in the catalyst zone of the catalyst purifying and cooling device, the reactants are heated in the heat exchange tube while the catalyst is cooled, and the heated reactants enter the reactor; or, steam is generated in the heat exchange tube; a displacement or stripping zone for the gas carried by the catalyst is provided at the lower part in the catalyst purifying and cooling device.

31. The method according to claim 20, wherein after the feedstock oil is vaporized, the entire gas-phase reaction zone of the reactor serves as a riser reactor, or a reaction section with an enlarged diameter is provided above the inlet of the cooled purified catalyst where the cracking of the feedstock oil has lasted over a reaction period of 0.8 to 1.5 seconds; in the reaction section with an enlarged diameter, the gas phase flow velocity is 1.8 m/s to 4.0 m/s, and the reaction time is 3.0 to 5.5 seconds.

32. The method according to claim 20, wherein the semi-regenerated catalyst that enters the reactor has a carbon content of 0.10 to 0.5 wt %.

33. The method according to claim 20, wherein the carbon content of the semi-regenerated catalyst in the upper part of the coke-burning zone of the regenerator is controlled at 0.15 to 0.4 wt %.

34. The method according to claim 20, wherein each section of the coke-burning zone of the regenerator is at the condition of a fast fluidized bed, the gas superficial velocity in the semi-regenerated catalyst section is 0.6 to 2.5 m/s, and the gas superficial velocity in the regenerated catalyst section of the coke-burning zone is 0.6 to 1.2 m/s; preferably, the gas superficial velocity in the lower half of the semi-regenerated catalyst section is 1.2 to 2.5 m/s, and the gas superficial velocity in the upper half of the semi-regenerated catalyst section is 0.6 to 1.2 m/s.

35. The method according to claim 20, wherein the temperature of the semi-regenerated catalyst section of the coke-burning zone of the regenerator is controlled between 650° C. and 720° C., and the temperature of the regenerated catalyst section is controlled between 640° C. and 700° C.; preferably, the temperature of the lower half of the semi-regenerated catalyst section is controlled between 650° C. and 690° C., and the temperature of the upper half of the semi-regenerated catalyst section is controlled between 660° C. and 720° C.

36. The method according to claim 20, wherein the amount of the semi-regenerated catalyst or spent catalyst that enters the catalyst mixing section of the reactor is 10% to 100%, preferably 20% to 100% of the amount of the regenerated catalyst.

37. The method according to claim 20, wherein the amount of the semi-regenerated catalyst that enters the reactor from above the feedstock oil inlet of the reactor is 10% to 50% of the amount of the regenerated catalyst that enters the reactor.

38. The method according to claim 20, wherein a catalyst mixing circulation tube is provided within the catalyst mixing section, the flux section area of this tube is 10% to 40%, preferably 10% to 30% of the flux section area of the catalyst mixing section; the gas apparent velocity in the inner circulation tube is between 1.5 m/s and 5.0 m/s.

39. An apparatus for implementing the reaction-regeneration method for catalytic cracking reaction according to claim 20, including a regenerator, a reactor, and a catalyst purifying and cooling device, arranged in parallel, wherein: the regenerator is used for coke-burning regeneration of the spent catalyst fed from the stripping section, and according to the inlet position and flow direction or distribution of the fed spent catalyst and the coke-burning degree, the coke-burning zone of the regenerator is divided into a semi-regenerated catalyst section and a regenerated catalyst section, wherein the regenerated catalyst section is located below the semi-regenerated catalyst section, and a spent catalyst inlet is provided in the lower part of the semi-regenerated catalyst section; and wherein the regenerator is provided with a returning pipe which introduces the semi-regenerated catalyst from the semi-regenerated catalyst section of the coke-burning zone to the regenerated catalyst section; the reactor has a riser reaction section as the main part, a catalyst mixing section with a enlarged diameter is provided at the bottom of the reactor, and feedstock oil inlets of the reactor are provided between the catalyst mixing section and the riser reaction section, wherein above the feedstock oil inlet are a feedstock oil vaporization zone and a catalytic cracking reaction zone in this order, and a settler is provided downstream of the catalytic cracking reaction zone; between the reactor and the regenerator, a spent-catalyst standpipe is provided to introduce the spent catalyst from the reactor to lower portion of the semi-regenerated catalyst coke-burning zone of the regenerator, and a regenerated-catalyst standpipe is provided to introduce the regenerated catalyst from the regenerator to the catalyst mixing section of the reactor; between the regenerator and the catalyst purifying and cooling device, a semi-regenerated-catalyst transporting pipe is provided to introduce the semi-regenerated catalyst from the regenerator to the catalyst purifying and cooling device; between the catalyst purifying and cooling device and the reactor, a semi-regenerated-catalyst feeding pipe is provided to feed the semi-regenerated catalyst in the catalyst purifying and cooling device to the reactor from above the reaction feedstock oil inlets, and another semi-regenerated-catalyst feeding pipe is provided to feed the semi-regenerated catalyst in the catalyst purifying and cooling device to the catalyst mixing section at the bottom of the reactor.

Description

DESCRIPTION OF DRAWINGS

[0070] FIG. 1 is a structure schematic representation of the part of the reactor-regenerator for the catalytic cracking reaction process according to one embodiment of the present invention;

[0071] FIG. 2 is a structure schematic representation of the part of the reactor-regenerator according to another embodiment of the present invention;

[0072] FIG. 3 is a structure schematic representation of the part of the reactor-regenerator according to another embodiment of the present invention;

[0073] FIG. 4 is a structure schematic representation of one embodiment of the distribution plate in the coke-burning zone according to the present invention; and

[0074] FIG. 5 is a structure schematic representation of another embodiment of the distribution plate in the coke-burning zone according to the present invention.

DESCRIPTION OF THE REFERENCE NUMBERS IN THE FIGURES

[0075] I: Vaporization zone of reactor where feedstock and catalyst contact; II: Gas-phase catalytic cracking reaction zone of reactor; IIA: Reaction zone with enlarged diameter; 1: Regenerator; 2: Catalyst purifying or stripping and cooling device; 3: Reactor; 5: External catalyst cooler; 1A: Semi-regenerated catalyst section; 1B: Regenerated catalyst section; 10: First section of regenerator (Middle section of coke-burning zone, First half-regeneration section,); 10A: First distribution plate (perforated partitioning plate); 10B and 11B: Gas and catalyst rising holes; 11: Second section of regenerator (Upper section of coke-burning zone, Second half-regeneration zone); 11A: Second distribution plate (perforated partitioning plate); 10C and 11C: Hole lids of distribution plate; 12: Third section of regenerator (Lower section of coke-burning zone); 13: Dilute phase section of regenerator; 14: Flue gas outlet; 15: Semi-regenerated catalyst returning pipe (Returning pipe); 16: Slide valve of semi-regenerated catalyst returning pipe; 17: Semi-regenerated catalyst outlet; 18: Spent-catalyst inlet; 19: Regenerated-catalyst outlet; 51: Gas outlet tube of external catalyst cooler; 52: Gas distributor; 53: Catalyst outlet tube of external catalyst cooler; 54: Slide valve; 21: Water-steam separator; 22: Gas distributor for gas carried by the catalyst purifying or stripping in catalyst purifying or stripping and cooling device; 23 and 23A: Catalyst transporting pipes; 25: Slide valve of catalyst transporting pipe of purifying or stripping and cooling device; 26: Fluidizing gas distributor for catalyst temperature control in catalyst purifying and cooling device; 27: Steam stripping section of catalyst purifying and cooling device; 28: Cooling zone of catalyst purifying and cooling device; 29: Gas-discharge pipe of catalyst purifying and cooling device; 30: Catalyst mixer and riser (Catalyst mixing section); 30A: Catalyst mixing and circulating pipe; 30B: Pre-lift medium inlet; 31: Feedstock nozzle; 32: Catalyst distributor; 33: Regenerated-catalyst standpipe; 34: Spent-catalyst standpipe; 35: Steam stripping section; 36: Cyclone separator; 37: Settler; 39: Reaction product outlet; 38: Regeneration slide valve; 41: Spent-catalyst returning pipe; 42: Slide valve; 43: Fluidizing gas of purifying and cooling device; 61: Third gas distributor; 62: First gas distributor; 63: Second gas distributor; 80: Temperature of catalyst at outlet of catalyst purifying and cooling device; 83: Temperature of catalyst mixture in catalyst mixing section; 84: Temperature of vaporized feedstock oil; 85: Temperature at reactor outlet; 81: Temperature difference; A: Compressed air; C: Catalyst; F: Flue gas; S: Steam; G: Pre-lift medium; O: Feedstock oil for reaction; N: Nitrogen gas.

DETAILED DESCRIPTION OF INVENTION

[0076] The technical solutions according to the present invention will be described in detail in conjunction with the figures and Examples. However, the scope of protection of the present invention is not limited thereto. All apparatus configurations not fully described herein can be those conventional in the art.

[0077] With reference to FIGS. 1 to 3, the apparatus for implementing the reaction-regeneration method of the present invention includes a regenerator 1, a catalyst purifying and cooling device 2 and a reactor 3 arranged in parallel, wherein: the regenerator 1 is used for coke-burning regeneration of the spent catalyst from the reactor 3, a first distribution plate 10A is provided below the spent-catalyst inlet 18 in the coke-burning zone of the regenerator 1, to divide the coke burning zone into a semi-regenerated catalyst section 1A above the first distribution plate and a regenerated catalyst section 1B beneath the first distribution plate. The spent-catalyst inlet 18 is typically located in the lower part of the semi-regenerated catalyst section. The position of the first distribution plate 10A in the coke-burning zone may be adjusted according to the coke-burning degree and the catalyst bed level in the semi-regenerated and regenerated catalyst sections, and may be set at above the mid-level of the coke-burning zone (as shown in FIG. 1) or at below the mid-level of the coke-burning zone (as shown in FIGS. 2 and 3). Furthermore, as shown in FIGS. 2 and 3, in the semi-regenerated catalyst section of the coke-burning zone of the regenerator, a second distribution plate 11A may be provided above the spent-catalyst inlet 18 to further divide the semi-regenerated catalyst section clearly into two sub-sections one atop another, i.e. the first half-regeneration section 10 and the second half-regeneration section 11 above the first half-regeneration section 10. In addition, in the regenerator a returning pipe 15 is provided to introduce the semi-regenerated catalyst from the semi-regenerated catalyst section of the coke-burning zone to the regenerated catalyst section.

[0078] The regenerator based on three-section coke-burning regeneration as shown in FIGS. 2 and 3 will be exemplarily described below. With reference to the catalytic cracking reactor-regenerator apparatus shown in FIGS. 2 and 3, the regenerator works by three-section coke-burning regeneration, wherein the three sections refer to the upper, middle and lower sections resulting from spatial dividing of the coke-burning zone of the regenerator, and are partitioned with distribution plates between one another. The first and second distribution plates 10A and 11A are provided in the coke-burning zone. The part of the coke-burning zone below the first distribution plate 10A may be defined as the lower section or the regenerated catalyst section, the part of the coke-burning zone above the second distribution plate may be defined as the upper section or the upper half-regeneration section, and the part of the coke-burning zone between the first and second distribution plates 10A and 11A may be defined as the medium section or the lower half-regeneration section. The detailed structure of the first and second distribution plates 10A and 11A can be seen in FIGS. 4 and 5, and they may be a normal perforated partitioning plate as shown in FIG. 4 where a number of gas and catalyst rising holes 10B and 11B serving as flowing channels for flue gas F and catalyst C are provided in the partitioning plate, or may be as shown in FIG. 5 wherein hole lids 10C and 11C of distribution plates are further provided over the gas and catalyst rising holes 10B and 11B so as to adjust the distribution of the gas and catalyst.

[0079] With reference to FIGS. 2 and 3 again, the three-section regenerator and the dilute phase section 13 of the regenerator are coaxially arranged one atop another, and according to the inlet position and flowing direction or distribution of the spent catalyst in the regenerator, the first section 10 of regenerator is set at the middle section of the coke-burning zone, the second section 11 of regenerator is set at the upper part of the coke-burning zone, and the third section 12 of regenerator is set at the lower part of the coke-burning zone. Spent catalyst enters the first section of regenerator to react with the oxygen-containing gas from the third section and the first gas distributor 62. The catalyst and the gas are together transported upwards through the second distribution plate to the second section of regenerator to continue the regeneration, and the catalyst in the second section enters the third section of regenerator via a catalyst returning pipe. Oxygen-rich fresh air enters the third section from the bottom via the third gas distributor 61, and reacts with the low-carbon semi-regenerated catalyst from the semi-regenerated catalyst coke-burning zone, generally the third section of regenerator, to complete the regeneration of catalyst. About 50% to 60% of the compressed air enters the third section via the third gas distributor 61 to participate in the reaction in the third section of regenerator, about 30% to 40% of the compressed air enters the first section via the first gas distributor 62 to participate in the reaction, and 0% to 10% of the compressed air enters the second section of regenerator via the second gas distributor 63. The third section of regenerator operates in a dense-phase fluidized bed state (optimally, the gas superficial velocity of the dense-phase fluidized bed is 0.5 m/s to 1.2 m/s).

[0080] The reaction-regeneration method of the present invention provides differently generated catalysts for the reactor. Regenerated catalyst exits the third section 12 of regenerator (i.e. the coke-burning zone of regenerated catalyst), and enters the catalyst mixing section 30 at the bottom of the reactor via a regenerated-catalyst standpipe 33 right below the reaction feedstock inlet (feedstock nozzle 31) of the reactor 3; meanwhile, spent catalyst, or purified and cooled semi-regenerated catalyst from the second section of regenerator, enters the catalyst mixing section 30. The catalyst mixing section 30 has a diameter 1.5 to 2.5 times the diameter of the cracking section of the reactor, operates under a dense-phase fluidized bed condition to uniformly fluidize catalyst, and has a catalyst mixing and circulating pipe 30A provided inside it and having a cross-section area 10% to 40%, preferably 10% to 30% of that of the catalyst mixing section. Catalyst is internally circulated inside the catalyst mixer to be uniformly mixed. The catalyst in the catalyst mixing section provides all the vaporization heat and part of the reaction heat for feedstock, and the amount of the catalyst is used to adjust the reaction temperature in the reactor. A spent catalyst returning pipe 41 may be provided between the steam stripping section 35 and the catalyst mixing section 30 at the bottom of the reactor, so that a part of spent catalyst is returned to the catalyst mixing section to be mixed with regenerated catalyst. Because this spent catalyst's temperature is much lower than the temperature of regenerated catalyst, the returned amount of the spent catalyst can be used to adjust the catalyst temperature before contact with feedstock oil and the temperature difference between catalyst and feedstock oil upon their contact. The returned spent catalyst is only circulated in the reaction system, and does not alter the catalyst circulation between the reactor 3 and regenerator 1.

[0081] According to the present invention, the semi-regenerated catalyst from the second section 11 of regenerator is cooled in the catalyst purifying and cooling device 2, and after its temperature is controlled as required (generally 480° C. to 570° C. in the present invention) and the carried gas medium is released by displacement or stripping, enters the reactor 3 at a position where feedstock oil has been vaporized to participate in the reaction in the cracking reaction zone, so that the reaction catalyst-to-oil ratio in the reaction zone of the reactor can be further increased and independently controlled.

[0082] The present invention employs a short reaction time of 1.5 to 2.5 seconds, about a temperature of 300° C. to 360° C. for pre-heating the feedstock oil, and a catalyst-to-oil ratio of 9 to 15, so as to maximize the yield of gasoline and minimize the yield of dry gas and coke.

[0083] Furthermore, as shown in FIG. 3, the regenerator of the present invention may be provided with an external catalyst cooler 5 including related facilities such as a gas outlet tube 51 of external catalyst cooler, a gas distributor 52, a catalyst outlet tube 53 of external catalyst cooler, a slide valve 54, etc. The settings of the external catalyst cooler can be made according to conventional operations in the art and the description thereof will be omitted here.

[0084] In the present invention, an independent catalyst purifying and cooling device 2 is provided between the reactor 3 and the regenerator 1, which includes a catalyst cooling portion, a carried-gas stripping portion, a catalyst temperature controller, stripping gas adjusting and stripped gas-discharging pipelines, and catalyst inlet and outlet pipelines. The catalyst cooling portion is Installed in the upper and the stripping portion is provided below. Catalyst enters the device via one inlet pipeline, is discharged via a transportation pipe and fed into the reactor. Steam or nitrogen gas enters the device from below the stripping area, and the stripping medium and the gas carried by regenerated catalyst are discharged from gas-discharging pipelines. Then the steam or nitrogen gas enters through a regulatory valve provided in the pipeline, and the regulatory value is acted by the catalyst temperature in the catalyst purifying and cooling device or by the difference between the temperature of corresponding position in the reaction zone and the catalyst temperature in the catalyst purifying and cooling device.

[0085] In the present invention, the catalyst temperature in the catalyst purifying and cooling device is controlled according to the temperature of the vaporized stream above the feedstock inlet of the reactor, so that the catalyst entering the cracking reaction zone fits the reaction condition in the cracking reaction zone. To meet the requirements, thermometric points are set in the vaporization zone between the catalyst inlet and the reaction feed stock inlet in the cracking reaction zone of the reactor and in the catalyst purifying and cooling device. The temperature difference between these two points is taken as an indicator to control the opening degree of the control (regulatory) valve in the operation medium pipeline of the catalyst purifying and cooling device, or the temperature difference between the outlet of the reactor and the catalyst purifying and cooling device is taken as an indicator to control the opening degree of the control (regulatory) valve in the operation medium pipeline of the catalyst purifying and cooling device. The regulatory valve in turn controls the amount of operation medium entering the catalyst purifying and cooling device, to achieve interconnected control of the catalyst temperature in the catalyst purifying and cooling device and the reaction temperature in the reactor, so that the catalyst entering the cracking reaction zone of the reactor always fits the conditions in the reactor. Alternatively, the temperature in the catalyst purifying and cooling device is used as an indicator to control the opening degree of the control valve in the operation medium pipeline of the catalyst purifying and cooling device, to adjust the amount of the introduced fluidized medium and to control the outlet temperature of the catalyst purifying and cooling device.

[0086] The catalyst purifying and cooling device of the present invention uses steam or nitrogen gas as the operation medium to achieve displacement of the flue gas carried by the catalyst and to control the catalyst temperature. Alternatively, it may use air and steam as two operation media with the steam entering the catalyst purifying and cooling device below the air, wherein adjustment of the air amount may change the catalyst temperature and adjustment of the steam amount may control the catalyst temperature and the displacement effect (stripping efficiency) of the carried gas.

[0087] The catalyst from the catalyst purifying and cooling device of the present invention enters the reactor at a position above the reaction feedstock inlet with a distance over which it takes 0.1 to 0.5 seconds for the vaporized gas equivalent to flow, or at a position 1.0 to 6 meters above the reaction feedstock inlet, to participate in the reaction in the cracking reaction zone of the reactor.

[0088] A heat exchange tube is provided at the upper part inside the catalyst purifying and cooling device of the present invention. While the catalyst is cooled, the reaction feedstock is heated in the heat exchange tube and then enters the reactor; or steam is generated in the heat exchange tube. A catalyst-carried gas displacement zone is provided at the lower part inside the catalyst purifying and cooling device.

[0089] The reactor of the present invention as a whole can work as a riser reactor, or as shown in FIG. 2, a reaction section with an enlarged diameter IIA may be provided downstream of the reactor and above the inlet of the catalyst purifying and cooling device. Preferably, in the section with an enlarged diameter, the gas phase flow velocity is 1.8 m/s to 4.0 m/s, and the reaction time is 3.0 to 5.5 seconds. The reaction section with an enlarged diameter IIA is provided mainly according to the requirement for olefin conversion of gasoline.

[0090] With reference to FIG. 2 again, in the reaction and regeneration method for catalytic cracking reaction according to the present invention, the regenerated catalyst in the third section 12 of regenerator and the semi-regenerated catalyst in the second section 11 of regenerator are introduced into the reactor 3 from the regenerated-catalyst outlet 19 and the semi-regenerated catalyst outlet 17, respectively; the regenerated catalyst from the third section 12 of the regenerator 1 directly enters the catalyst mixing section 30 at the bottom of the reactor 3 via the regenerated-catalyst standpipe 33 from the regenerated-catalyst outlet 19, and flows upwards under the action of the pre-lift medium that enters via the pre-lift medium inlet 30B, so as to contact the feedstock oil to vaporize it and then complete the catalytic cracking reaction; after the reaction is completed, the hydrocarbons carried is stripped in the steam stripping section 35, and the catalyst is returned to the first section 10 of regenerator via the spent-catalyst standpipe 34. The semi-regenerated catalyst from the second section 11 of regenerator is treated in the catalyst purifying and cooling device 2, and then is fed by gravity via the catalyst transporting pipe 23 into the reactor 3 at a position of the reactor where the feedstock oil is vaporized, to participate in the cracking reaction; after the reaction is completed, the hydrocarbons carried is stripped in the steam stripping section 35, and then the catalyst is returned to the first section 10 of regenerator from the spent-catalyst inlet 18 via the spent-catalyst standpipe 34. A part of the spent catalyst in the steam stripping section 35 is returned to the catalyst mixing section 30 via the spent-catalyst returning pipe 41.

[0091] Alternatively, as shown in FIG. 3, the semi-regenerated catalyst from the second section 11 of regenerator is treated in the catalyst purifying and cooling device 2, then enters the catalyst mixing section 30 via the catalyst transporting pipe 23A, and is mixed with the regenerated catalyst to lower the temperature of the regenerated catalyst.

[0092] In the present invention, based on the temperature 83 of the catalyst mixture mixed in the catalyst mixing section below the feedstock inlet of the reactor, the slide valve 42 of the spent-catalyst returning pipe is adjusted to control the amount of the returning spent catalyst, as shown in FIGS. 1 and 2; or the slide valve 42 is adjusted to control the amount of the low-temperature semi-regenerated catalyst that enters from the catalyst purifying and cooling device, as shown in FIG. 3, so as to regulate the catalyst temperature in the catalyst mixing section. A catalyst mixing pipe 30A is provided in the catalyst mixing section to circulate the catalyst within the catalyst mixing section and improve the mixing of catalyst. The catalyst in the catalyst transporting pipe 23 of the catalyst purifying and cooling device moves downwards by gravity into the cracking reaction zone II of reactor above the feedstock oil inlet; according to the temperature difference 81 between (i) the temperature at a point between the catalyst inlet and the reaction feedstock inlet of the reactor (i.e. the temperature 84 of the vaporized feedstock oil) and (ii) the catalyst temperature 80 at the outlet of the catalyst purifying and cooling device, the operation medium 43 or steam S or nitrogen gas N in the catalyst purifying and cooling device 2 is regulated to control the catalyst temperature 80 at the outlet of the catalyst purifying and cooling device, and supply catalyst that meets the requirements to the cracking reaction zone II of reactor. Steam or nitrogen gas enters the catalyst purifying and cooling device 2 at the bottom of the catalyst purifying and cooling device 2 via the gas distributor 22, moves upwards through the stripping section 27 of catalyst purifying and cooling device and the cooling zone 28 of catalyst purifying and cooling device, and is discharged through the top gas-discharge pipe 29 of catalyst purifying and cooling device. The temperature 84 of the vaporized feedstock oil in the reactor or the outlet temperature 85 of reactor is controlled by regulating the flow of regenerated catalyst by the regeneration slide valve 38. Feedstock oil is heated upon heat exchange, then is atomized via the feedstock nozzle 31, and then enters the reactor. The semi-regenerated catalyst in the second section of the regenerator enters the third section 12 of regenerator via the returning pipe 15. Air A enters the third section 12 of regenerator, the second section 11 of regenerator and the external catalyst cooler 5, respectively. The pre-lift medium G enters the catalyst mixing section. Feedstock oil O enters the reactor via the feedstock nozzle 31. Steam S enters the steam stripping section.

EXAMPLES

[0093] The apparatus used in this example for controlling the catalyst in the reaction zone and performing the cooling method on the regenerated catalyst is shown in FIG. 3.

[0094] A petroleum hydrocarbon catalytic cracking apparatus with a capacity of 150×10.sup.4 t/a performs regeneration with a coke-burning tank and with parallel reactor and regenerator. The riser reactor 3 and catalyst purifying and cooling device 2 produce mid-pressure steam. The catalyst purifying and cooling device 2 is equipped with a gas-liquid separator which is directly attached to the catalyst purifying and cooling device 2 and has the same diameter as the catalyst purifying and cooling device 2. The reactant materials and reaction conditions of the examples versus comparative examples representing the prior art are shown in the table below.

TABLE-US-00001 Comparative Examples Examples Items Unit Value Unit Value Amount of feedstock oil O t/h 180 t/h 180 Density Kg/m.sup.3 0.91 Kg/m.sup.3 0.91 Residual carbon W % 0.5 W % 0.5 Feed temperature of feedstock oil O ° C. 330 ° C. 230 Precooling medium G Kg/h 4500 Kg/h 4500 Temperature at reaction outlet 85 ° C. 515 ° C. 500 Dense phase temperature of regenerator ° C. ° C. 695 Regeneration temperature of the second section ° C. 675 ° C. Coke content in the semi-regenerated catalyst in % 0.2 the second section Regeneration temperature of the third section ° C. 695 ° C. Gas apparent velocity in the third section of m/s 0.9 regenerator Gas apparent velocity in the first section of m/s 1.55 regenerator Average gas superficial velocity in the m/s 1.0 second section of regenerator Carbon content in the regenerated catalyst % 0.05 % 0.05 Catalyst temperature in catalyst mixing ° C. 630 ° C. 690 section 30 Temperature at the thermometric point for ° C. 535 ° C. 540 catalyst feed in the cracking reaction zone II (the temperature 84 of the vaporized feedstock oil) Temperature difference 81 between the ° C. 0 temperature of the second outlet of the purifying and cooling device 2 and the temperature at the thermometric point for catalyst feed in the cracking reaction zone II (the temperature 84 of the vaporized feedstock oil) Distance from the feedstock inlet to the m 2.0 catalyst feed inlet of the cracking reaction zone II Total reaction time s 2.2 s 2.8 Circulating amount of regenerated catalyst t/h 900 t/h 1224 Amount of catalyst from the spent-catalyst t/h 450 t/h 0 returning pipe 41 Amount of catalyst entering the cracking t/h 600 t/h 0 reaction zone II Overall reaction catalyst-to-oil ratio 10.8 6.67 Amount of steam used in the catalyst Kg/h 980 Kg/h 0 purifying and cooling device

[0095] Specifications of the reaction apparatus of the examples according to the invention and comparative examples according to the prior art are shown in the table below.

TABLE-US-00002 Comparative Examples Examples Items Unit Value Unit Value Diameter of the third section 12 of mm 5600 mm regenerator Height of the third section of regenerator mm 7000 mm Diameter of the first section of regenerator mm 5600 mm Height of the first section of regenerator mm 9000 mm 16000 Diameter of the second section of mm 6800 mm regenerator Height of the second section of mm 5000 regenerator Diameter of the dilute phase section of mm 9500 mm 9800 regenerator Diameter of the catalyst mixer and mm 2000 mm 1600 pre-riser 30 of the reactor Diameter of the cracking reaction zone mm 1150 mm 1100 II of reactor Diameter of the catalyst distributor 32 of mm 2200 the cracking reaction zone II of reactor Diameter of the semi-regenerated catalyst mm 500 returning pipe Diameter of the catalyst purifying and mm 2000 cooling device 2 Area of the heat exchange tube of the m.sup.2 90 catalyst purifying and cooling device 2 Diameter of the regenerated catalyst inlet mm 1100 tube of the catalyst purifying and cooling device 2 Diameter of the catalyst transporting pipe mm 500 23 of the catalyst purifying and cooling device Diameter of the gas-discharge pipe 29 of mm 250 the catalyst purifying and cooling device Diameter of the steam inlet pipe of the mm 200 catalyst purifying and cooling device 2

[0096] Reaction product profiles of the examples and the comparative examples according to the prior art are shown in the table below.

TABLE-US-00003 Comparative Examples Examples Components Unit Value Unit Value Dry gas W % 2.2 W % 3.6 Liquefied gas W % 12 W % 11.9 Gasoline W % 52.4 W % 50.9 Diesel W % 25.4 W % 25.4 Heavy oil W % 1.6 W % 1.6 Coke W % 6 W % 6.2 Loss W % 0.4 W % 0.4 Total W % 100 W % 100