Multi-stage fluidized catalytic reaction process of petroleum hydrocarbons and an apparatus thereof

Abstract

A petroleum hydrocarbon multi-stage fluid catalytic reaction method and reactor are described. The method implements a sectional multi-stage reaction in one reactor and comprises primary-stage and secondary-stage catalytic cracking reactions of feedstock oil and primary-stage and secondary-stage catalytic cracking reactions of light hydrocarbons and/or cycle oil, which occur in different reaction regions of the reactor. The primary-stage reaction of the light hydrocarbon and/or circulation oil is carried out in an independent reaction region. The reactor comprises a first reaction section, a catalyst splitter, a third reaction section, a second reaction section and a settler.

Claims

1. A multi-stage fluidized catalytic reaction method of petroleum hydrocarbon, comprising: arranging a reactor with upper and lower partitions to realize a multi-stage catalytic reaction; wherein the multi-stage catalytic reaction includes primary-stage and secondary-stage catalytic cracking reactions of feedstock oil and primary-stage and secondary-stage catalytic cracking reactions of light hydrocarbons and/or cycle oil, which occur in different reaction regions of the reactor; wherein the reactor is provided with a first reaction section (110), a catalyst splitter (114), a third reaction section (121), a second reaction section (141) and a settler (151) from bottom to top; wherein the first reaction section (110) is a riser reactor, which is provided with a feedstock oil input (113) and upward first reaction region (115); the catalyst splitter (114) is disposed at the output of the first reaction region (115); a second reaction region (145) is arranged in the second reaction section (141), a third reaction region (125) is arranged in the third reaction section (121); a first reaction region output stream conveyor pipe (122) is arranged inside the third reaction section (121), and the output of the first reaction region output stream conveyor pipe (122) is located at the input of the second reaction region (145) which is at the top of the third reaction region (125); feeding a first catalyst (A1) into the first reaction section (110) under feedstock oil input (113), and then into the first reaction region (115) by pre-lifting medium (G); feeding a catalytic cracking feedstock oil (Y) into the first reaction region (115), carrying out the primary-stage reaction under the catalyst, then carrying out catalyst separation at output of the first reaction region; and entering oil gas upwards into the second reaction region (145) through the first reaction region output stream conveyor pipe (122) for the secondary-stage catalytic cracking reaction of deep cracking; the stream from the second reaction region enters the settler (151) for gas-solid separation; feeding a second catalyst (A2) into the third reaction region (125) in the third reaction section (121); feeding a light hydrocarbon and/or cycle oil into the third reaction region (125) to carrying out the independent primary-stage reaction under the second catalyst (A2), and then, introducing the catalyst and product from the third reaction region up to the second reaction region (145) to continue the secondary-stage catalytic cracking reaction continuously.

2. The method according to claim 1, wherein: the first catalyst (A1) is fed into pre-lifting section (112) of the first reaction section (110) through a first catalyst input pipe (118), fluidized by the pre-lifting medium (G) and conveyed to the first reaction region (115), the feedstock oil (Y) is atomized by steam through feedstock oil input (113) into the first reaction region (115) in the first reaction section (110), which is atomized and mixes and contacts with the first catalyst (A1), and then the primary-stage catalytic cracking reaction takes place; after the primary-stage catalytic cracking reaction, part of the catalyst is separated from catalyst splitter (114); separated catalyst flows out of the reactor through spent catalyst conveyor pipe after stripped in a first stripping section (131); oil gas is fed up to the second reaction region (145) through a first reaction region output stream conveyor pipe (134) for the secondary-stage catalytic cracking reaction; the second catalyst (A2) is fed into the third reaction region (125) in the third reaction section (121) which is installed between the first stripping section (131) and the second reaction section (141) through a second catalyst input pipe (128); the light hydrocarbon and/or cycle oil is fed into the third reaction region (125); independent primary-stage catalytic cracking reaction takes place in the surrounding of the second catalyst (A2), and then, catalyst and products (P3) of the third reaction region is fed up to the second reaction region (145), to continue the secondary-stage catalytic cracking reaction; in the third reaction region (125), catalyst is fluidized with steam, so that turbulent fluidized bed or circulating fluidized bed is formed in this area, and the steam enters the second reaction region (145) at the same time; the product gas and catalyst after reaction in the second reaction region are conveyed to the settler (151) for gas-solid separation, and reaction product (P) flows out of the settle; the catalyst after reaction in the second reaction region is fed to a first catalyst stripping region (133) installed in the first stripping section (131) from a catalyst reflux pipe (148) of the second reaction region, and stripped together with the catalyst separated from the first reaction region (115) through the catalyst splitter (114), and flows out of the reactor from the spent catalyst conveyor pipe (134) after stripping; or a second stripping section (143) is installed out of the second reaction region; a second spent catalyst (B2) flows out of the reactor through a catalyst output pipe (144) after stripping.

3. The method according to claim 1, wherein when there are multiple feedstock in the third reaction region (125), the feedstock is fed into the third reaction region (125) hierarchically according to the boiling point or final boiling point; components with low boiling point or final boiling point is fed into the third reaction region (125) in the lower layer, and the components with higher boiling point or final boiling point is fed into the third reaction region (125) in higher layer successively; when light hydrocarbon and light cycle oil react in the third reaction region (125) at the same time, the light hydrocarbon is fed into the reaction region below the third reaction region, and the light cycle oil is fed into the third reaction region (125) above the light hydrocarbon.

4. The method according to claim 1, wherein the first reaction region (115) adopts riser reactor, which is conveyor bed, the third reaction region (125) adopts turbulent fluidized bed or circulating fluidized bed, the second reaction region (145) adopts circulating fluidized bed or turbulent fluidized bed; optionally, the superficial velocity of the turbulent fluidized bed said is lower than 1.2 m/s, and the superficial velocity of circulating fluidized bed said is 1.2 to 4.0 m/s.

5. The method according to claim 1, wherein the third reaction section (121) mentioned is divided vertically into several independent sections which are clapboard region (125Y) and/or barrel region (125T) by vertical clapboards (126) and/or vertical barrels (127); the catalyst fed into the third reaction section (121) enters each region through the connected channel in the bottom of the clapboard region (125Y) and/or barrel region (125T); all or part of the said clapboard region (125Y) and/or barrel region (125T) is used as the third reaction region; the light hydrocarbon and/or cycle oil reacts in one or several or all of the said clapboard region (125Y) and/or barrel region (125T); when there are several kinds of feedstock in the third reaction region, different feedstock reacts in disparate clapboard region (125Y) and/or barrel region (125T) with respective reaction condition.

6. The method according to claim 1, wherein the amount of the feedstock fed into the third reaction region (125) which is the amount of the light hydrocarbon and/or cycle oil, is controlled by the carbon content of catalyst after reaction in the second reaction region; it could control the carbon content of catalyst after reaction in the second reaction region less than 0.8% weight ratio.

7. The method according to claim 1, wherein the amount of the feedstock fed into the third reaction region (125) which is the amount of the light hydrocarbon and/or cycle oil, is controlled by the carbon content of catalyst after reaction in the third reaction region; it could control the carbon content of catalyst after reaction in the third reaction region less than 0.4% weight ratio.

8. The method according to claim 1, wherein the reaction temperature of the second reaction region (145) is higher than or the same with the first reaction region (115); the reaction temperature of the second reaction region is higher than the first reaction region by 0° C. to 70° C., the reaction temperature of the second reaction region (145) is controlled by the amount of the second catalyst (A2).

9. The method according to claim 1, wherein a fourth reaction region (155) is installed between the second reaction region (145) and the shell of the second reaction section (141), which is used for the reaction of light hydrocarbon or cycle oil.

10. A multi-stage fluidized catalytic reactor of petroleum hydrocarbon, characterized in that, the reactor includes a first reaction section (110), a catalyst splitter (114), a third reaction section (121), a second reaction section (141) and a settler (151) from bottom to top; the first reaction section (110) is a riser reactor, including a first catalyst input pipe (118), a pre-lifting section (112), a feedstock input (113), a first reaction region (115) from bottom to top, which is used for the reaction of feedstock oil (Y); a first stripping section (131) is installed around the feedstock oil reaction region, which is the first reaction region (115), the catalyst splitter (114) is installed at the output of the first reaction region (115), which is also at the top of a first catalyst stripping region (133) in the first stripping section (131); there is a clapboard (116) installed between the first catalyst stripping region (133) and the third reaction section (121), and a first reaction region output stream conveyor pipe (122) is installed on the clapboard (116); a second reaction region (145) is installed in the second reaction section (141), a third reaction region (125) is installed inside the third reaction section (121), the output of first reaction region output stream conveyor pipe (122) is at the input of the second reaction region (145) which is at the top of the third reaction region (125), there are a light hydrocarbon or cycle oil input (124) and a second catalyst input pipe (128) installed in the third reaction section (121), which is used for the reaction of light hydrocarbon and cycle oil; a second clapboard (149) is installed between the third reaction section (121) and the outside of the second reaction region (145) which is in the second reaction section (141); a conveyor pipe (146) is installed between the second reaction region (145) and the gas-solid separator in the settler (151).

11. The reactor according to claim 10, wherein the first reaction section (110), catalyst splitter (114), the first stripping section (131), the third reaction section (121), the second reaction section (141), and settler (151) are installed coaxially up and down.

12. The reactor according to claim 10, wherein a porous plate (147) is installed between the third reaction section (121) and the second reaction region (145); stream from the first reaction region and catalyst and gas from the third reaction region is distributed to the second reaction region (145) through the porous plate (147).

13. The reactor according to claim 10, wherein a catalyst reflux pipe (148) is installed between the second reaction section (141) and the first stripping section (131); or a catalyst reflux pipe (148) is installed between the second reaction section (141) and the first stripping section (131), and a second stripping section (143) is arranged outside the second reaction region (145).

14. The reactor according to claim 10, wherein a fourth reaction region (155) is installed between the second reaction region (145) and the shell of the second reaction section (141), which is used for the reaction of cycle oil or recycle oil.

15. The reactor according to claim 10, wherein the district between the shell of the third reaction section (121) and the first reaction region output stream conveyor pipe (122) is divided into several isolated regions which are clapboard region (125Y) and/or barrel region (125T) by vertical clapboards (126) and/or vertical barrels (127), the vertical clapboards (126) or vertical barrels (127) are interconnected at the bottom; input of light hydrocarbon and steam is installed in the bottom of part or all of the clapboard region (125Y) and/or barrel region (125T).

16. The reactor according to claim 15, wherein the clapboards and barrels could be connected or supported to the shell of the third reaction section.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is the schematic structural diagram of the implementation case 1 of the petroleum hydrocarbon multi-stage fluidized catalytic reaction process in the present invention;

(2) FIG. 2 is the A-A view of FIG. 1, which is the schematic diagram of the distribution of the first reaction region output stream conveyor pipe.

(3) FIG. 3 is the A-A view of FIG. 1, which is the schematic diagram of the second type of distribution of the first reaction region output stream conveyor pipe.

(4) FIG. 4 is the schematic structural diagram of the implementation case 2 of the petroleum hydrocarbon multi-stage fluidized catalytic reaction process in the present invention. There is a porous plate (distribution plate) installed at the input of the second reaction region.

(5) FIG. 5 is the schematic structural diagram of the implementation case 3 of the petroleum hydrocarbon multi-stage fluidized catalytic reaction process in the present invention. The fourth reaction region is installed.

(6) FIG. 6 is the schematic structural diagram of the implementation case 4 of the petroleum hydrocarbon multi-stage fluidized catalytic reaction process in the present invention. The catalyst after reaction in the second reaction region refluxes to the first stripping section.

(7) FIG. 7 is the partial enlarged view of the third reaction section in FIG. 6.

(8) FIG. 8 is the B-B view of FIG. 7, which is the cross section diagram of the third reaction section divided into several isolated region.

DESCRIPTION OF THE REFERENCE NUMBERS IN THE FIGURES

(9) 110: The first reaction section, 112: Per-lifting section, 113: Feedstock oil input (nozzle), 114: Catalyst splitter, 115: The first reaction region, 116: Clapboards, 118: The first catalyst input pipe, 121: The third reaction section (light hydrocarbon and cycle oil reaction region), 122: The first reaction region output stream conveyor pipe, 123: The first steam distributor, 124: Light hydrocarbon and/or cycle oil input, 125: The third reaction region, 125Y: Clapboard region, 125T: Barrel region, 126: Vertical clapboard, 127: Vertical barrel, 128: The second catalyst input pipe, 131: The first stripping section, 132: The second steam distributor, 133: The first catalyst stripping section, 134: Spent catalyst conveyor pipe, 135: Stripping internals, 138: Catalyst reflux pipe, 141: The second reaction section, 142: The third steam distributor, 143: The third stripping section, 144: Catalyst (after reaction) output pipe, 145: The second reaction region, 146: Conveyor pipe, 147: Porous plate, 148: The second reaction region catalyst reflux pipe, 149: The second clapboard, 151: Settler, 152: Settler dilute phase, 153: The first gas-solid separator, 154: The second gas-solid separator, 155: The fourth reaction region (fluidized bed or turbulent fluidized bed reaction region), 156: Product output.

(10) Y: Feedstock oil, Y1: Light hydrocarbon feedstock, Y2: Light cycle oil feedstock, Y3: Heavy cycle oil or recycle oil, G: Pre-lifting medium, P: Reaction product, S: Steam, A1: The first catalyst (catalyst fed into the first reaction section), A2: The second catalyst (catalyst fed into the second reaction section), B1: Spent catalyst, B2: The second spent catalyst (catalyst after reaction in the second reaction region, the third reaction region and/or the fourth reaction region), P1: Stream after reaction in the first reaction region (fed into the second reaction region), P3: Stream after reaction in the third reaction region (fed into the second reaction region).

(11) FR: Flow recording instrument, FRC: Flow control instrument, TIC: Temperature control instrument.

DETAILED DESCRIPTION OF INVENTION

(12) The technical solution of the present invention will be described in detail with reference to the implementation methods and cases. The scope of protection for the present invention includes but not limited to the following implementation cases:

(13) The specific implementation process is as follows:

(14) Implementation Method 1:

(15) As shown in FIGS. 1 to 3,

(16) The multi-stage fluidized catalytic reaction process of petroleum hydrocarbon in the present invention, multi-stage reaction takes place in the same reactor, including the first order reaction of the feedstock oil, the second order reaction of the feedstock oil, light hydrocarbon and/or cycle oil cracking reaction process. In the process of the first and second order reaction of the catalytic cracking feedstock oil, the catalyst replacement and two-stage relay reaction takes place, and two-stage relay reaction of light hydrocarbon and/or cycle oil takes place too. The reaction mentioned takes place in different region of the same reactor. Light hydrocarbon and/or cycle oil reacts in independent region.

(17) From bottom up, the reactor consists of the first reaction section 110, catalyst splitter 114, the third reaction section 121, the second reaction section 141 and settler 151.

(18) The first reaction section 110 is riser reactor, which is adopting riser reaction condition. From bottom up, it includes the first catalyst input pipe 118, pre-lifting section 112, feedstock input 113, the first reaction region 115, which is used for the reaction of the feedstock oil Y. The first stripping section 131 is installed around the feedstock oil reaction region which is the first reaction region 115, and stripping internal 135 is installed in the first stripping section 131. Catalyst splitter 114 is installed at the output of the first reaction region 115, and at the top of the first catalyst stripping section which is in the first stripping section.

(19) Clapboard 116 is installed between the first catalyst stripping section 133 and the third reaction section. The first reaction region output stream conveyor pipe 122 is installed on clapboard 116. The first reaction region output stream conveyor pipe 122 is at the top of the third reaction region 125, and the input of the second reaction region 145. Light hydrocarbon and/or cycle oil input 124 and the second catalyst input pipe is installed in the third reaction section 121, which is used for the reaction of light hydrocarbon and cycle oil.

(20) The second reaction region 145 is installed inside the second reaction section 141. The second clapboard 149 is installed between the third reaction section and the outside of the second reaction region 145 which is installed inside the second reaction section 141. Conveyor pipe 146 is installed between the second reaction region and the gas-solid separator installed in settler 151.

(21) Stripping component is installed in the catalyst storage region after reaction in the second reaction region which is in the outside of the second reaction region. The storage region is used as the second stripping section 143. Catalyst (after reaction) output pipe 144 is installed in the second stripping section 143. The catalyst separated from the gas-solid separator is stripped by steam S which is fed by the third steam distributor 142 in the storage region. The second spent catalyst B2 flows out of the reactor through catalyst (after reaction) output pipe 144.

(22) When implementing, the first reaction section 110, catalyst splitter 114, the first stripping section 131, the third reaction section 121, the third reaction region 125, the second reaction section 141 and settler 151 are installed coaxially from top down. Catalyst splitter 114 is circumferential swirling. The first reaction region output stream conveyor pipe 122 may be installed inside the third reaction region. As shown in FIG. 2, a first reaction region output stream conveyor pipe 122 is installed in the center of the third reaction region, coaxially with the first reaction region. Or several first reaction region output stream conveyor pipe 122 is installed in the third reaction region, coaxially with the first reaction region, as shown in FIG. 3, four first reaction region output stream conveyor pipe 122 is installed side by side evenly.

(23) The following steps take place in the reaction process:

(24) The first catalyst A1 fed to the pre-lifting section 112 in the first reaction section 110 through the first catalyst input pipe 118 is conveyed to the first reaction region 115 by the pre-lifting medium G. Feedstock Y is fed to the first reaction region 115 in the first reaction section 110 through feedstock input 113 after atomized by steam. Feedstock Y and the first catalyst A1 is mixed and the first order catalytic cracking reaction takes place. After the first order catalytic cracking reaction, part of the catalyst is separated from catalyst splitter 114. The separated catalyst settles to the first catalyst stripping region 133 in the first stripping section 131. After stripped by steam S fed by the second steam distributor 132 in the first catalyst stripping section 133, spent catalyst B1 flows out of the reactor through spent catalyst conveyor pipe 134. Oil gas (included in the stream P1 after reaction in the first reaction region) is fed to the second reaction region 145 through the first reaction region output stream conveyor pipe 122, for the second order catalytic cracking reaction.

(25) The second catalyst A2 is fed into the third reaction region 125 in the third reaction section 121 which is installed between the first stripping section 131 and the second reaction section 141. Light hydrocarbon feedstock Y1 is fed into the third reaction region 125, and the first order catalytic cracking reaction takes place in the environment of the second catalyst A2 independently. And then the catalyst and product of the third reaction region which is stream P3 after reaction in the third reaction region, together with the oil gas of the first reaction region is fed to the second reaction region 145, the second order catalytic cracking reaction takes place. In the third reaction region 125, catalyst is fluidized by steam S fed by the first steam distributor 123, so that fluidized bed or turbulent fluidized bed condition forms in the region. All the steam is fed to the second reaction region 145.

(26) The gas and catalyst after reaction in the second reaction region is conveyed to settler 151 through conveyor pipe 146. Gas-solid separation takes place in the first order gas-solid separator 153 and the second order gas-solid separator 154. Product P flows out of the reactor through product output 156 (do not flow through settler dilute phase region 152).

(27) Catalyst after reaction in the second reaction region is stripped in the second stripping section 143. The second spent catalyst B2 flows out of the reactor through catalyst output pipe 144.

(28) In the present implementation method, specifically, after atomized by steam, the fresh catalytic feedstock oil Y is fed to the first reaction region through feedstock input 113, mixes with the first catalyst A1 which is the regenerated catalyst conveyed by the first catalyst conveyor pipe 118, and atomizes. After catalytic cracking reaction for about 1.2 seconds in the first reaction region, 85% of the catalyst is separated from the feedstock oil product by catalyst splitter 114 in the first reaction region output, and the oil gas flows into the first reaction region output stream conveyor pipe. Another catalyst the second catalyst A2 is fed to the bottom of the third reaction region through the second catalyst input pipe. Light hydrocarbon feedstock which is C4 and light gasoline is fed to the bottom of the third reaction region 125, and reacts in the environment of catalyst A2. The reaction gas and catalyst of the third reaction region together with the oil gas from the first reaction region output stream conveyor pipe 122 is fed to the second reaction region to continue reacting. Spent catalyst Blin the first reaction region flows out of the reactor through spent catalyst conveyor pipe 134. The second spent catalyst B2 after reaction in the second reaction region flows out of the reactor after stripped in the second stripping section 143 through catalyst output pipe 144.

(29) The first reaction region is designed by riser condition. The second reaction region is designed by circulating fluidized bed condition, and the gas apparent velocity is about 2.0 m/s. The third reaction region is designed by turbulent fluidized bed condition, and the gas apparent velocity is 0.6 m/s to 1.0 m/s, the catalyst space velocity is 4 to 6. The reaction temperature of the first reaction region is about 500° C. The reaction temperature of the 3nd reaction region is about 550° C. The reaction temperature of the third reaction region is about 590° C. to 610° C.

(30) The first catalyst A1 is regenerated catalyst. The second catalyst is catalyst with carbon content 0.1% to 0.2%.

(31) Steam is replenished in the third reaction region, which participate the reaction in the third reaction region, and then is fed to the second reaction region to decrease the partial pressure of oil gas.

(32) In the diagrams, FR is flow recording instrument, FRC is flow control instrument, and TIC is temperature control instrument.

(33) Implementation Method 2:

(34) As shown in FIG. 4, the multi-stage fluidized catalytic reaction process of petroleum hydrocarbon, porous plate 147 is installed in the second reaction region input which is between the third reaction region 121 and the second reaction region 145. Stream from the first reaction region and catalyst and gas from the third reaction region is fed to the second reaction region 145 through the porous plate 147.

(35) C4 component is first fed to the lower part of feedstock input 113. The first catalyst A1 contacts and reacts with C4 component first, and then flows up to contact and react with feedstock oil Y.

(36) The equipment structure of other parts is the same with implementation method 1.

(37) Implementation method 3:

(38) As shown in FIG. 5, the multi-stage fluidized catalytic reaction process of petroleum hydrocarbon, the second reaction region 145 is riser reaction region (the upper part of the riser is equivalent to the conveyor pipe in FIG. 1). The riser outlet is directly connected to the first stage gas-solid separator 153 of the settler. The second stripping section and the fourth reaction region 155 are arranged on the periphery of the riser reaction region. The fourth reaction region is installed upon the second stripping section. Light cycle oil feedstock Y2 and heavy cycle oil or recycle oil Y3 is fed into the fourth reaction region 155.

(39) Catalyst reflux pipe 138 is arranged between the third reaction region 125 and pre-lifting section 112 in the first reaction section. Part of the catalyst refluxes to pre-lifting section 112, to participate the catalytic reaction of feedstock oil Y.

(40) The equipment structure of other parts is the same with implementation method 1.

(41) Implementation Method 4:

(42) As shown in FIGS. 6 to 8, the multi-stage fluidized catalytic reaction process of petroleum hydrocarbon, the second reaction region catalyst reflux pipe 148 is installed between the second reaction section 141 and the first stripping section 131. After stripped in the second stripping section 143, the catalyst after reaction in the second reaction region, is fed to the first catalyst stripping region 133 in the first stripping section 131 through the second reaction region catalyst reflux pipe 148, to strip together with catalyst separated from the first reaction region 115 by catalyst splitter 114, and flows out of the reactor through spent catalyst conveyor pipe 134 after stripping.

(43) As shown in FIGS. 7 to 8, the interspace between the shell of the third reaction section and the first reaction region output stream conveyor pipe is divided by two vertical clapboards 126 and a vertical barrel 127 into three isolate regions, which are two clapboard regions 125Y and a barrel region 125T. Two vertical clapboards 126 are connected to the shell of the third reaction section 121, and the vertical barrel 127 is supported on the shell of the third reaction section 121. The bottom ends of the vertical clapboards 126 and the vertical barrel 127 are connected to each other to realize the flow of the catalyst in each region. Light hydrocarbon and steam input is arranged at the bottom input of the barrel region 125 T, barrel region 125 T is used as the third reaction region, and the light hydrocarbon reacts in barrel region 125 T. Steam input is installed at the bottom of two clapboard region. When implementing, the second catalyst A2 is fed to the bottom of the third reaction region 125 (which is barrel region 125T) through the second catalyst input pipe 128. Light hydrocarbon feedstock Y1 fed to barrel region 125T reacts in the environment of catalyst A2. The equipment structure of other parts is the same with implementation method 1.

(44) Implementation Case

(45) The equipment used in the implementation case is shown in FIG. 1.

(46) The feedstock oil is heavy oil. The processing capacity is 2 million tons/year. The character of the feedstock oil is shown in Table 1. The feedstock oil is pre-heated to 280° C. In the first reaction region, reaction time is 1.2 seconds, reaction temperature is 510° C., catalyst to oil ratio is 6.5, temperature of the regenerated catalyst A1 is 680° C. The amount of atomized steam is 5% of the feedstock oil;

(47) In the second reaction region, reaction temperature is 550° C., reaction time is 3.5 s, catalyst to oil ratio is 7.0, weight hourly space velocity of the catalyst is 8, carbon content of the spent catalyst is 0.6%, and the amount of replenishment steam is 12% of the feedstock oil;

(48) The separation ratio of the catalyst after reaction in the first reaction region is 85%, 15% of it remains in the oil gas. Catalyst A2 is half regenerated catalyst, temperature is 660° C., carbon content is 0.15%;

(49) In the third reaction region, the feedstock is self-produced light gasoline, the temperature is 40° C., the amount of light gasoline is 300000 tons/year, and the reaction temperature is 600° C.;

(50) The diameter of the first reaction region is 1.2 meters and the height of the reaction region is 14 meters;

(51) The diameter of the second reaction region is 3.8 meters and the height is 9 meters; The diameter of the third reaction region is 5 meters and the height is 4 meters, the diameter of the first reaction region output stream conveyor pipe 122 is 1.4 meters; The diameter of the first stripping section 131 is 4.8 meters, the diameter of the second stripping section 14 is 5 meters;

(52) The settler is designed according to the conventional technology, and the general technicians in this field master it.

(53) The reaction conditions and product distribution are shown in Table 2.

(54) Compare Case

(55) Adopting the prior catalytic cracking process, specifically, the equipment used consecutive reactor composes of riser reactor and fluidized bed reactor.

(56) The reaction conditions: the reaction temperature of the first reaction region is 580° C., the reaction temperature of the second reaction region which is the fluidized bed reaction region is 580° C., space velocity of catalyst in the fluidized bed reaction region is 4, superficial velocity of the gas in the fluidized bed reaction region is 1.0 m/s.

(57) The reaction conditions and product distribution are shown in Table 2. C4 mentioned in the present invention is hydrocarbon containing four carbon atoms, which is prior art.

(58) TABLE-US-00001 TABLE l Character of the feedstock oil Project Data Density, g/cm.sup.3 (20° C.) 0.9035 Residual carbon, w % 0.62 Hydrogen content, w % 12.56 Sulfur content, w % 0.31 Nitrogen content, w % 0.16 Distillation Range, ° C. 256~545

(59) TABLE-US-00002 TABLE 2 Reaction conditions and product distribution comparison of implementation case and compare case Imple- mentation Compare Project case case Temperature of the first 510 580 reaction region output, ° C. Reaction temperature of the 550 560 second reaction region, ° C. Reaction temperature of the 600 third reaction region, ° C. Regeneration temperature, ° C. 680 680 Ratio of the steam, % 17 24 Temperature of feedstock oil, 280 340 ° C. Temperature of the half 660 regenerated catalyst, ° C. Carbon content of the half 0.15 regenerated catalyst, % product distribution, % Dry gas (H~C2) 7.1 9.2 Liquefied gas (C3~C4) 36.8 35.33 Gasoline 28.2 28.81 Diesel 15.1 12.19 Heavy oil 3.6 4.28 Coke 8.8 9.73 Loss 0.4 0.46 Propylene 16.13 15.49 Propylene/Dry gas 2.272465 1.683696

(60) It can be seen from the comparison results in Table 2 that compared with the conventional catalytic process, the yield of low value products such as dry gas and coke is significantly reduced. High value products such as olefin, liquefied petroleum gas and gasoline yield increased significantly. A yield of dry gas decreases by 2.1 percentage points, the yield of coke decreases by 0.93 percentage points, the yield of propylene increases by 0.64 percentage points, the selectivity of propylene to dry gas increases by 0.589. It can be seen that, in the present invention, the selectivity of propylene increases greatly, and the yield of dry gas and coke decreases greatly.