CN116410774A - Reactor and catalytic cracking or catalytic cracking method for oil body - Google Patents
Reactor and catalytic cracking or catalytic cracking method for oil body Download PDFInfo
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- CN116410774A CN116410774A CN202111674856.3A CN202111674856A CN116410774A CN 116410774 A CN116410774 A CN 116410774A CN 202111674856 A CN202111674856 A CN 202111674856A CN 116410774 A CN116410774 A CN 116410774A
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- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 title claims description 17
- 238000006243 chemical reaction Methods 0.000 claims abstract description 164
- 239000003054 catalyst Substances 0.000 claims abstract description 80
- 239000007921 spray Substances 0.000 claims abstract description 68
- 239000002245 particle Substances 0.000 claims description 15
- 230000002035 prolonged effect Effects 0.000 claims description 8
- 239000002994 raw material Substances 0.000 abstract description 11
- 229910052799 carbon Inorganic materials 0.000 abstract description 8
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 8
- 238000005336 cracking Methods 0.000 description 12
- 230000000052 comparative effect Effects 0.000 description 10
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 6
- 239000005977 Ethylene Substances 0.000 description 6
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 6
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 6
- 238000012986 modification Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 238000000889 atomisation Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a reactor, which is suitable for catalytic cracking or catalytic cracking reaction of oil bodies and solves the problem of low yield of low-carbon olefin products in the traditional reactor; the reactor includes a body and a distributor. The body is provided with a vertically arranged reaction cavity, and is provided with a spray hole and a first outlet which are communicated with the reaction cavity and the outside; the spray hole of the body is positioned at one side of the reaction cavity downwards, and the first outlet of the body is positioned at the top of the body; the distributor is provided with an inlet and a plurality of second outlets which are communicated with each other and face the spray holes; the second outlets of the distributor are arranged in the reaction cavity, are positioned above the spray holes and are radially arranged by taking the axis of the reaction cavity as the center; the inlet of the distributor communicates with the outside and serves as an inlet for the catalyst. The reactor prolongs the contact time of the oil body and the catalyst, improves the raw material utilization rate of catalytic cracking or catalytic cracking reaction, and increases the yield of low-carbon olefin products.
Description
Technical Field
The invention belongs to the technical field of petrochemical reactors, and particularly relates to a catalytic cracking reactor and a catalytic cracking method of an oil body.
Background
The fluidized bed refers to a bed layer in which solid particles of the bed layer are separated from contact, the particles are suspended in fluid and move in all directions; fluidized bed reactors, also called ebullated bed reactors, refer to devices in which a gas undergoes a chemical reaction in an ebullated bed of solid material or catalyst. The fluidized bed reactor is widely applied to heterogeneous reaction systems in petrochemical production processes, wherein a reaction-regeneration system of a catalytic cracking/catalytic cracking device is a typical generalized circulating fluidization system and can be divided into bubbling bed fluidization, turbulent bed fluidization, rapid bed fluidization, dense-phase pneumatic conveying and dilute-phase pneumatic conveying.
Conventional catalytic cracking/catalytic cracking reactors feed the catalyst directly through the bottom of the reactor, which affects the yield of light olefins.
Disclosure of Invention
In order to solve the technical problems, the invention provides the reactor and the catalytic cracking or catalytic cracking method of the oil body, which improve the raw material utilization rate of catalytic cracking or catalytic cracking reaction and increase the yield of low-carbon olefin products.
The technical scheme of the invention is as follows:
in one aspect, the present invention provides a reactor suitable for catalytic cracking or catalytic cracking reactions of an oil body, the reactor comprising:
the device comprises a body, a first nozzle and a second nozzle, wherein the body is provided with a vertically arranged reaction cavity, and is provided with a spray hole and a first outlet which are communicated with the reaction cavity and the outside; the spray hole of the body is positioned at one side of the reaction cavity downwards, and the first outlet of the body is positioned at the top of the body;
a distributor provided with an inlet and a plurality of second outlets facing the spray holes, wherein the inlets are communicated with each other; the second outlets of the distributor are arranged in the reaction cavity, are positioned above the spray holes and are radially arranged with the axis of the reaction cavity as the center; the inlet of the distributor is communicated with the outside and serves as an inlet of the catalyst.
Further, the included angle between the axis of the spray hole of the body and the vertical direction is 10-80 degrees, and the included angle between the second outlet of the distributor and the vertical direction is 10-80 degrees.
Further, the included angle between the axis of the spray hole of the body and the vertical direction is 30-60 degrees, and the included angle between the second outlet of the distributor and the vertical direction is 30-60 degrees.
Further, the ratio of the distance between the spray hole and the bottom of the reaction cavity to the height of the reaction cavity is 0.1-0.6.
Further, the ratio of the distance between the second outlet of the distributor and the bottom of the reaction chamber to the height of the reaction chamber is 0.1-0.8.
Further, the projection of the spray orifice on the horizontal plane falls outside the projection of the second outlet of the dispenser on the horizontal plane.
Further, the number of the second outlets of the distributor is more than or equal to 3.
In another aspect, the present invention provides a catalytic cracking or catalytic cracking process for oil bodies, carried out in a reactor as described above, said process comprising,
atomized oil is sprayed into the reaction cavity of the body obliquely downwards from the spray hole of the body, and meanwhile, a catalyst enters from the inlet of the distributor and is sprayed into the reaction cavity of the body obliquely downwards from the second outlet of the distributor;
the oil body is mixed with the catalyst and then back mixed in the reaction cavity, and the oil body is discharged from the first outlet of the body after prolonged catalytic cracking or catalytic cracking.
Further, the temperature of the oil body in the reactor is 200-300 ℃, the temperature of the catalyst in the reactor is 650-850 ℃, and the particle size of the catalyst in the reactor is 20-100 mu m.
Further, the catalyst-to-oil ratio of the catalytic cracking or catalytic cracking reaction of the oil body is 6-30.
The beneficial effects of the invention at least comprise:
the invention provides a reactor which is suitable for catalytic cracking or catalytic cracking reaction of an oil body and comprises a body and a distributor. The body is provided with a vertically arranged reaction cavity, and is provided with a spray hole and a first outlet which are communicated with the reaction cavity and the outside; the spray hole of the body is positioned at one side of the reaction cavity downwards, and the first outlet of the body is positioned at the top of the body; the distributor is provided with an inlet and a plurality of second outlets which are communicated with each other and face the spray holes; the second outlets of the distributor are arranged in the reaction cavity, are positioned above the spray holes and are radially arranged by taking the axis of the reaction cavity as the center; the inlet of the distributor communicates with the outside and serves as an inlet for the catalyst. The oil body is sprayed into the reaction cavity in a mist form through the spray holes, and the spray holes are arranged on one side of the reaction cavity downwards, so that the oil body enters the lower part of the reaction cavity along the guide of the spray holes; the catalyst enters the inlet of the distributor from the outside and enters the reaction cavity from the second outlet of the distributor, and the second outlet of the distributor faces the spray hole at the lower part, so that the catalyst enters the lower part of the reaction cavity along the guide of the second outlet of the distributor, and then the catalyst and the oil body are back mixed at the lower part of the reaction cavity, and simultaneously are subjected to catalytic cracking or catalytic cracking reaction, and the oil body is high in temperature and atomized, and the catalyst is high in Wen Xifen, so that the oil body and the catalyst move back to the upper part of the reaction cavity after moving to the bottom of the reaction cavity until reaching the first outlet at the top of the reaction cavity. The oil body and the catalyst have long walking path and long residence time in the reaction cavity, so that the contact time of the oil body and the catalyst is prolonged, the utilization rate of raw materials of catalytic cracking or catalytic cracking reaction is improved, and the yield of low-carbon olefin products is increased.
Drawings
FIG. 1 is a schematic view showing the structure of a reactor according to the present embodiment;
fig. 2 is a top view of fig. 1.
Reference numerals illustrate: 1-a body, 101-a reaction cavity, 102-spray holes, 103-a first outlet; 2-dispenser, 201-inlet, 202-second outlet.
Detailed Description
In order to make the technical solution more clearly understood by those skilled in the art, the following detailed description is made with reference to the accompanying drawings.
Fig. 1 and 2 show the structure of a reactor, and in combination with fig. 1 and 2, in one aspect, an embodiment of the present invention provides a reactor suitable for catalytic cracking or catalytic cracking reaction of an oil body, the reactor comprising a body 1 and a distributor 2.
Wherein, the body 1 is provided with a reaction cavity 101 which is vertically arranged, and is provided with a spray hole 102 and a first outlet 103 which are communicated with the reaction cavity 101 and the outside; the spray hole 102 of the body 1 is positioned at one side of the reaction cavity 101 downwards, and the first outlet 103 of the body 1 is positioned at the top of the body 1; the dispenser 2 is provided with an inlet 201 and a plurality of second outlets 202 directed toward the nozzle holes 102, which are communicated with each other; a plurality of second outlets 202 of the distributor 2 are arranged in the reaction chamber 101, are positioned above the spray holes 102, and are radially arranged with the axis of the reaction chamber 101 as the center; the inlet 201 of the distributor 2 communicates with the outside and serves as the inlet 201 for the catalyst.
The oil body is sprayed into the reaction cavity 101 through the spray holes 102 in a mist form, and the spray holes 102 are positioned on one side of the reaction cavity 101 downwards, so that the oil body enters the lower part of the reaction cavity 101 along the guide of the spray holes 102; the catalyst enters the inlet 201 of the distributor 2 from the outside and enters the reaction cavity 101 from the second outlet 202 of the distributor 2, and the catalyst enters the lower part of the reaction cavity 101 along the direction of the second outlet 202 of the distributor 2 because the second outlet 202 of the distributor 2 faces the lower spray hole 102, so that the catalyst and the oil body are back mixed at the lower part of the reaction cavity 101 and simultaneously undergo catalytic cracking or catalytic cracking reaction, and the oil body is high in temperature and atomization, and the catalyst is high Wen Xifen, so that the oil body and the catalyst move back to the upper part of the reaction cavity 101 after moving to the bottom of the reaction cavity 101 until reaching the first outlet 103 at the top of the reaction cavity 101. Because the oil body and the catalyst travel along a long path in the reaction cavity 101, the residence time is long, and the contact time of the oil body and the catalyst is prolonged, so that the raw material utilization rate of catalytic cracking or catalytic cracking reaction is improved, and the yield of low-carbon olefin products is increased.
Preferably, in this embodiment, the axis of the nozzle 102 of the body 1 is inclined at an angle of 10-80 ° to the vertical, and the second outlet 202 of the dispenser 2 is inclined at an angle of 10-80 ° to the vertical.
If the included angle between the axis of the spray hole 102 of the body 1 and the vertical direction is too large, the oil body can be directly sprayed onto the distributor 2, and the oil body can be directly turned back when meeting the blocking of the distributor 2 and gradually moves upwards, so that the residence time of the oil body in the reaction cavity 101 is not prolonged; if the included angle between the axis of the spraying hole 102 of the body 1 and the vertical direction is too small, the oil will be sprayed out along the cavity wall, which affects the service life of the cavity wall of the reaction cavity 101. If the included angle between the second outlet 202 of the distributor 2 and the vertical direction is too large, the catalyst is flushed out horizontally and directly turns back upwards when encountering the cavity wall of the reaction cavity 101, which is not beneficial to prolonging the residence time of the catalyst in the reaction cavity 101; if the angle between the second outlet 202 of the distributor 2 and the vertical is too small, the residence time of the catalyst in the reaction chamber 101 is not greatly affected, but the mixing time with the oil body is delayed, thereby reducing the utilization rate of the raw materials.
More preferably, in this embodiment, the axis of the nozzle 102 of the body 1 is inclined at an angle of 30-60 ° to the vertical, and the second outlet 202 of the dispenser 2 is inclined at an angle of 30-60 ° to the vertical. The oil body and the catalyst can be contacted quickly within the angle range, and the contact time is long.
Further, in the present embodiment, the ratio of the distance between the nozzle 102 and the bottom of the reaction chamber 101 to the height of the reaction chamber 101 is 0.1-0.6. The distance between the spray hole 102 and the bottom of the reaction cavity 101 is too small, the oil body quickly reaches the bottom of the reaction cavity 101 and then starts to turn back upwards, and the residence time of the oil body in the reaction cavity 101 is short; the distance between the nozzle 102 and the bottom of the reaction chamber 101 is too large, the sprayed atomized oil body has a limited travel, and cannot reach the bottom of the reactor, so that the space of the reactor cannot be effectively utilized. Preferably, this ratio is between 0.15 and 0.3.
Further, in the present embodiment, the ratio of the distance between the second outlet 202 of the distributor 2 and the bottom of the reaction chamber 101 to the height of the reaction chamber 101 is 0.1-0.8. The distance between the second outlet 202 of the distributor 2 and the bottom of the reactor is too small, the catalyst quickly reaches the bottom of the reaction chamber 101, and then starts to turn back upwards, so that the residence time of the catalyst in the reaction chamber 101 is short; the second outlet 202 of the distributor 2 is too far from the bottom of the reaction chamber 101, and the distributed catalyst is limited in stroke, and cannot reach the bottom of the reactor, and thus the reactor space cannot be effectively utilized. Preferably, this ratio is between 0.15 and 0.3.
Further, in the present embodiment, the projection of the nozzle hole 102 on the horizontal plane falls outside the projection of the second outlet 202 of the dispenser 2 on the horizontal plane. Thus, the oil body and the catalyst can be prevented from entering the reaction cavity 101 to be in direct contact, and if the oil body and the catalyst are in direct collision contact, the kinetic energy of the oil body and the catalyst can be reduced, so that the oil body and the catalyst can directly rise after collision, and the reaction time of the oil body and the catalyst is not beneficial to being prolonged.
Preferably, in the present embodiment, the number of the second outlets 202 of the distributor 2 is equal to or greater than 3, the number of the spray holes 102 may be matched with the number of the distributors 2, for example, 4 second outlets 202 of the distributor 2 may be provided, 4 spray holes 102 may be provided, and the spray holes 102 are uniformly arranged in a radial shape with the axis of the reaction chamber 101 as the center. Of course, the dispenser 2 and the nozzle holes 102 may be provided in 5, or other numbers, without limitation.
In another aspect, the embodiment of the invention also provides a catalytic cracking or catalytic cracking method of an oil body, which is carried out in the fluidized bed reactor, and the method comprises the following steps of,
s1, atomized oil is sprayed into the reaction cavity 101 of the body 1 obliquely downwards from the spray hole 102 of the body 1, and meanwhile, a catalyst enters from the inlet 201 of the distributor 2 and is sprayed into the reaction cavity 101 of the body 1 obliquely downwards from the second outlet 202 of the distributor 2;
s2, after mixing the oil body and the catalyst, back mixing occurs in the reaction cavity 101, and after prolonged catalytic cracking or catalytic cracking, the oil body is discharged from the first outlet 103 of the body 1.
Further, in this example, the temperature of the oil body in the reactor was 200 to 300 ℃, the temperature of the catalyst in the reactor was 650 to 850 ℃, and the particle size of the catalyst in the reactor was 20 to 100 μm.
The oil body is a mixture of various organic matters, and if the temperature of the oil body in the reaction cavity 101 is too high, the oil body can react to generate coking; if the temperature of the oil in the reaction chamber 101 is too low, catalytic cracking or catalytic cracking reaction is not facilitated. The catalyst has over high temperature and over high thermal cracking reaction proportion, so that the yield of the low-carbon olefin is reduced; the catalyst temperature is too low, so that the oil body cannot be gasified completely, the contact area between the catalyst and the oil body is not improved, and the emergency stop of the reactor can be caused.
Further, in this embodiment, the catalyst-to-oil ratio of the catalytic cracking or catalytic cracking reaction of the oil body is 6 to 30.
The catalyst to oil ratio represents the ratio of the catalyst circulation amount to the total oil feed amount. The catalyst-oil ratio is too large, so that the catalyst in the reactor is easy to circulate; the catalyst-oil ratio is too small, the catalyst quantity is too small, and the catalytic cracking or catalytic cracking reaction of the oil body cannot be catalyzed sufficiently, so that the yield of the low-carbon olefin is reduced.
The reactor and reaction process provided herein will be further described with reference to specific examples.
Example 1
The embodiment 1 provides a catalytic cracking or catalytic cracking method for a reactor and an oil body, wherein 4 spray holes 102 are arranged in the reactor, the spray holes 102 are uniformly arranged in a radial manner by taking the axis of a reaction cavity 101 as the center, the included angle between the spray holes 102 and the vertical is 45 degrees, the distance between the spray holes 102 and the bottom of the reaction cavity 101 is 800mm, 4 uniformly distributed outlets are arranged in a distributor 2, the included angle between the outlets and the vertical is 45 degrees, and the distance between the outlets and the bottom of the reaction cavity 101 is 1000mm; the height of the reaction chamber 101 is 4000mm.
The oil body is sprayed into the reaction chamber 101 from the spray hole 102 of the reaction chamber 101 at a speed of 100m/s after atomization, the alpha-cracking catalyst is discharged into the reaction chamber 101 from the outlet of the distributor 2 at a speed of 10m/s, the atomized oil body and the catalyst are back mixed in the reaction chamber 101 and undergo catalytic cracking or catalytic cracking reaction, and then the alpha-cracking catalyst is discharged from the outlet of the body 1.
Wherein the temperature of the oil body is 220 ℃, the temperature of the catalyst is 680 ℃, the particle size of the catalyst is 20-100 mu m, and the average particle size is 60 mu m.
Example 2
The oil body is sprayed into the reaction chamber 101 from the spray hole 102 of the reaction chamber 101 at a speed of 80m/s after atomization, the beta-cracking catalyst is discharged into the reaction chamber 101 from the outlet of the distributor 2 at a speed of 6m/s, the atomized oil body and the catalyst are back mixed in the reaction chamber 101 and undergo catalytic cracking or catalytic cracking reaction, and then the oil body and the catalyst are discharged from the outlet of the body 1.
Wherein the temperature of the oil body is 240 ℃, the temperature of the catalyst is 690 ℃, the particle size of the catalyst is 20-95 mu m, and the average particle size is 58 mu m.
Example 3
Embodiment 3 provides a catalytic cracking or catalytic cracking method for a reactor and an oil body, wherein 3 spray holes 102 are arranged in the reactor, the spray holes 102 are uniformly arranged in a radial manner by taking the axis of a reaction cavity 101 as the center, the included angle between the spray holes 102 and the vertical is 60 degrees, the distance between the spray holes 102 and the bottom of the reaction cavity 101 is 600mm, 3 uniformly distributed outlets are arranged in a distributor 2, the included angle between the outlets and the vertical is 60 degrees, and the distance between the outlets and the bottom of the reaction cavity 101 is 800mm; the height of the reaction chamber 101 was 2500mm.
The oil body is sprayed into the reaction cavity 101 from the spray hole 102 of the reaction cavity 101 at a speed of 90m/s after being atomized, the gamma-cracking catalyst is discharged into the reaction cavity 101 from the outlet of the distributor 2 at a speed of 7.5m/s, the atomized oil body and the catalyst are back mixed in the reaction cavity 101 and undergo catalytic cracking or catalytic cracking reaction, and then the gamma-cracking catalyst is discharged from the outlet of the body 1.
Wherein the temperature of the oil body is 210 ℃, the temperature of the catalyst is 720 ℃, the particle size of the catalyst is 20-105 mu m, and the average particle size is 63 mu m.
Example 4
Embodiment 4 provides a catalytic cracking or catalytic cracking method for a reactor and an oil body, wherein 5 spray holes 102 are arranged in the reactor, the spray holes 102 are uniformly arranged in a radial manner by taking the axis of a reaction cavity 101 as the center, the included angle between the spray holes 102 and the vertical is 70 degrees, the distance between the spray holes 102 and the bottom of the reaction cavity 101 is 200mm, 5 uniformly distributed outlets are arranged in a distributor 2, the included angle between the outlets and the vertical is 75 degrees, and the distance between the outlets and the bottom of the reaction cavity 101 is 300mm; the reaction chamber 101 has a height of 1300mm.
The oil body is sprayed into the reaction chamber 101 from the spray hole 102 of the reaction chamber 101 at a speed of 85m/s after atomization, the gamma-cracking catalyst is discharged into the reaction chamber 101 from the outlet of the distributor 2 at a speed of 6m/s, the atomized oil body and the catalyst are back mixed in the reaction chamber 101 and undergo catalytic cracking or catalytic cracking reaction, and then the oil body and the catalyst are discharged from the outlet of the body 1.
Wherein the temperature of the oil body is 260 ℃, the temperature of the catalyst is 710 ℃, the particle size of the catalyst is 20-110 mu m, and the average particle size is 65 mu m. .
Example 5
Embodiment 5 provides a catalytic cracking or catalytic cracking method of a reactor and an oil body, wherein the number of spray holes 102 in the reactor is 5, the spray holes 102 are uniformly arranged in a radial manner by taking the axis of a reaction cavity 101 as the center, the included angle between the spray holes 102 and the vertical is 18 degrees, the distance between the spray holes 102 and the bottom of the reaction cavity 101 is 1000mm, the distributor 2 is provided with 5 uniformly distributed outlets, the included angle between the outlets and the vertical is 20 degrees, and the distance between the outlets and the bottom of the reaction cavity 101 is 1200mm; the reaction chamber 101 has a height of 6000mm.
The oil body is sprayed into the reaction cavity 101 from the spray hole 102 of the reaction cavity 101 at the speed of 120m/s after being atomized, the beta-cracking catalyst is discharged into the reaction cavity 101 from the outlet of the distributor 2 at the speed of 12m/s, the atomized oil body and the catalyst are back mixed in the reaction cavity 101 and undergo catalytic cracking or catalytic cracking reaction, and then the oil body and the catalyst are discharged from the outlet of the body 1.
Wherein the temperature of the oil body is 290 ℃, the temperature of the catalyst is 700 ℃, the particle size of the catalyst is 20-95 mu m, and the average particle size is 57 mu m.
Comparative example 1
Comparative example 1 with reference to example 3, comparative example 1 differs from example 3 in that: the angle between the spray hole 102 and the vertical direction is 5 degrees, and the angle between the outlet of the distributor 2 and the vertical direction is 82 degrees.
Comparative example 2
Comparative example 2 with reference to example 3, comparative example 1 differs from example 3 in that: the angle between the spray hole 102 and the vertical direction is 85 DEG, and the angle between the outlet of the distributor 2 and the vertical direction is 3 deg.
TABLE 1
| Numbering device | Feedstock conversion/% | Propylene yield/% | Ethylene yield/% |
| Example 1 | 82.44 | 17.71 | 4.52 |
| Example 2 | 82.67 | 17.92 | 4.62 |
| Example 3 | 83.35 | 18.16 | 5.35 |
| Example 4 | 83.11 | 18.02 | 5.15 |
| Example 5 | 82.15 | 17.52 | 4.17 |
| Comparative example 1 | 81.37 | 17.22 | 4.15 |
| Comparative example 2 | 81.21 | 17.08 | 4.16 |
As can be seen from the data in Table 1, the conversion rate of the raw material (oil body) is 82.15-83.35% by catalytic cracking or catalytic cracking reaction using the reactor provided by the invention, the yield of propylene obtained by the reaction is 17.52-18.16%, and the yield of ethylene obtained by the reaction is 4.52-5.35%. The reactor provided in comparative example 1 was used for catalytic cracking or catalytic cracking reaction, the conversion of the raw material (oil body) was 81.37%, the propylene yield was 17.22%, the ethylene yield was 4.15%, and the raw material conversion, the propylene yield and the ethylene yield were all lower than those in the present application; the reactor provided in comparative example 2 was used for catalytic cracking or catalytic cracking reaction, the conversion of the raw material (oil body) was 81.21%, the propylene yield was 17.08%, the ethylene yield was 4.16%, and the raw material conversion, the propylene yield and the ethylene yield were lower than those in the present application.
The invention provides a reactor and a catalytic cracking method of an oil body, wherein a distributor is arranged in a reaction cavity of a high-density bed reactor, and a catalyst is sprayed obliquely downwards; atomized oil drops are sprayed downwards obliquely from spray holes of the reactor, the oil body and the catalyst are sprayed downwards obliquely together to contact, mix and turn around in a high-density bed, so that intense back mixing occurs, the contact time of the oil body and the catalyst is prolonged, the contact probability of the oil agent is remarkably improved, the micro agent oil ratio and the macro agent oil ratio tend to be consistent, high-severity reaction occasions can be provided, the operation of the high agent oil ratio is adapted, and the yield and the selectivity of the target low-carbon olefin product are ensured; the mixture forms a high-severity reaction zone at the upper part of the distributor, which is beneficial to cracking of light components and gasification of extra heavy components, so that the cracking reaction further occurs in the rear riser, thus the high-density bed reactor completes the gasification of all raw materials, the cracking of light hydrocarbons and the partial cracking of heavy hydrocarbons, and the parallel sequential cracking reaction is continued in the rear riser plug flow reactor, thereby ensuring the yield and selectivity of light olefins.
While the preferred embodiments of the present application have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. It is therefore intended that the following claims be interpreted as including the preferred embodiments and all such alterations and modifications as fall within the scope of the application.
It will be apparent to those skilled in the art that various modifications and variations can be made in the present application without departing from the spirit or scope of the application. Thus, if such modifications and variations of the present application fall within the scope of the claims and the equivalents thereof, the present application is intended to cover such modifications and variations.
Claims (10)
1. A reactor suitable for catalytic cracking or catalytic cracking reactions of oil bodies, said reactor comprising:
the device comprises a body, a first nozzle and a second nozzle, wherein the body is provided with a vertically arranged reaction cavity, and is provided with a spray hole and a first outlet which are communicated with the reaction cavity and the outside; the spray hole of the body is positioned at one side of the reaction cavity downwards, and the first outlet of the body is positioned at the top of the body;
a distributor provided with an inlet and a plurality of second outlets facing the spray holes, wherein the inlets are communicated with each other; the second outlets of the distributor are arranged in the reaction cavity, are positioned above the spray holes and are radially arranged with the axis of the reaction cavity as the center; the inlet of the distributor is communicated with the outside and serves as an inlet of the catalyst.
2. The reactor of claim 1, wherein the axis of the orifice of the body is at an angle of 10-80 ° to the vertical and the second outlet of the distributor is at an angle of 10-80 ° to the vertical.
3. The reactor of claim 2, wherein the axis of the orifice of the body is at an angle of 30-60 ° to the vertical and the second outlet of the distributor is at an angle of 30-60 ° to the vertical.
4. The reactor of claim 1, wherein a ratio of a distance between the nozzle hole and a bottom of the reaction chamber to a height of the reaction chamber is 0.1 to 0.6.
5. The reactor according to claim 4, wherein a ratio of a distance between the second outlet of the distributor and the bottom of the reaction chamber to a height of the reaction chamber is 0.1 to 0.8.
6. The reactor of claim 1, wherein the projection of the orifice on the horizontal plane falls outside the projection of the second outlet of the distributor on the horizontal plane.
7. The reactor of claim 1, wherein the number of second outlets of the distributor is greater than or equal to 3.
8. A catalytic cracking or catalytic cracking process of an oil body, carried out in a reactor as claimed in any one of claims 1 to 7, characterized in that it comprises,
atomized oil is sprayed into the reaction cavity of the body obliquely downwards from the spray hole of the body, and meanwhile, a catalyst enters from the inlet of the distributor and is sprayed into the reaction cavity of the body obliquely downwards from the second outlet of the distributor;
the oil body is mixed with the catalyst and then back mixed in the reaction cavity, and the oil body is discharged from the first outlet of the body after prolonged catalytic cracking or catalytic cracking.
9. The catalytic cracking or catalytic cracking process of an oil body according to claim 8, wherein the temperature of the oil body in said reactor is 200-300 ℃, the temperature of the catalyst entering said reactor is 650-850 ℃, and the particle diameter of the catalyst entering said reactor is 20-100 μm.
10. The catalytic cracking or catalytic cracking method of an oil body according to claim 8, wherein the catalyst-to-oil ratio of the catalytic cracking or catalytic cracking reaction of the oil body is 6 to 30.
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| US4562046A (en) * | 1983-12-02 | 1985-12-31 | Phillips Petroleum Company | Catalytic cracking unit |
| US4883583A (en) * | 1985-07-16 | 1989-11-28 | Compagnie De Raffinage Et De Distribution Total France | Process for the catalytic cracking of hydrocarbons in a fluidized bed and their applications |
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| CN1840615A (en) * | 2005-03-31 | 2006-10-04 | 中国石油化工股份有限公司 | Process for catalytic cracking of petroleum hydrocarbon |
| CN1853768A (en) * | 2005-04-29 | 2006-11-01 | 中国石油化工股份有限公司 | Improved petroleum hydrocarbon catalytic cracking reactor |
| CN203507987U (en) * | 2013-09-27 | 2014-04-02 | 中国石油天然气股份有限公司 | High-efficiency contact fluidized bed reactor |
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2021
- 2021-12-31 CN CN202111674856.3A patent/CN116410774A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4562046A (en) * | 1983-12-02 | 1985-12-31 | Phillips Petroleum Company | Catalytic cracking unit |
| US4883583A (en) * | 1985-07-16 | 1989-11-28 | Compagnie De Raffinage Et De Distribution Total France | Process for the catalytic cracking of hydrocarbons in a fluidized bed and their applications |
| US20040124124A1 (en) * | 2002-12-30 | 2004-07-01 | Petroleo Brasileiro S.A. - Petrobras | Apparatus and process for downflow fluid catalytic cracking |
| CN1840615A (en) * | 2005-03-31 | 2006-10-04 | 中国石油化工股份有限公司 | Process for catalytic cracking of petroleum hydrocarbon |
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