CN109385302B - Catalytic conversion method for increasing yield of gasoline and low-carbon olefin - Google Patents
Catalytic conversion method for increasing yield of gasoline and low-carbon olefin Download PDFInfo
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- CN109385302B CN109385302B CN201710670322.0A CN201710670322A CN109385302B CN 109385302 B CN109385302 B CN 109385302B CN 201710670322 A CN201710670322 A CN 201710670322A CN 109385302 B CN109385302 B CN 109385302B
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Images
Classifications
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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
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
-
- 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
-
- 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
- C10G11/182—Regeneration
-
- 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
- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
-
- 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
- C10G2300/1088—Olefins
- C10G2300/1092—C2-C4 olefins
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/20—C2-C4 olefins
Landscapes
- 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 relates to a catalytic conversion method for increasing the yield of gasoline and low-carbon olefin, which mainly solves the problems of low gasoline yield and complex process in the existing catalytic cracking process or catalytic cracking coupling hydrogenation process. Introducing two regenerant conveying pipes from a regenerator to respectively convey the regenerated catalyst to a diameter-expanded light hydrocarbon reaction zone I and a heavy hydrocarbon reaction zone in a riser reactor reaction zone, simultaneously and respectively spraying preheated light hydrocarbon and heavy hydrocarbon into the light hydrocarbon reaction zone I and the heavy hydrocarbon reaction zone from an integrated nozzle, and carrying out contact reaction with the high-temperature regenerated catalyst from the regenerator and moving upwards together; the reaction product and the catalyst containing carbon deposit flow out of the reactor from a top outlet and enter a cyclone separation system for separation, and the separated reaction product enters a fractionating tower through an oil-gas pipeline for fractionation to obtain a corresponding product; the catalytic conversion method provided by the invention has the characteristic of increasing the yields of gasoline and low-carbon olefin.
Description
Technical Field
The invention relates to a catalytic conversion method of petroleum hydrocarbons, in particular to a catalytic conversion method of heavy diesel oil and poor heavy oil for increasing the yield of gasoline and low-carbon olefins under the condition of no hydrogen.
Background
Under the new economic normal state, the consumption of the Chinese main product oil still shows a growing trend, the rigidity demand of gasoline is increased rapidly, the speed increase of diesel oil demand is greatly reduced, and the speed increase of the gasoline demand of China is generally faster than that of the diesel oil before 2020; meanwhile, the chemical industry market has more and more vigorous demand for low-carbon olefins such as ethylene, propylene, butadiene and the like. Because crude oil in China is generally heavier and naphtha fraction with the boiling point of less than 200 ℃ has lower yield, less than 50 percent of steam cracking raw material can be provided for producing low-carbon olefins. The catalytic cracking device is one of the main means for producing gasoline and byproduct low-carbon olefin in refinery, provides 75% of gasoline component in commercial gasoline pool and 32% of propylene component in propylene product pool in China, and plays a significant role in oil refinery.
In recent years, with the gradual decline of the diesel-gasoline ratio consumed in China, the market of finished products is changed, the diesel stock is increased rapidly, the problem of diesel surplus is obvious, the normal operation of a refinery is influenced, and the reduction of the diesel stock and the increase of the gasoline yield are urgently needed. The historical data research at home and abroad shows that: the economic development stage and the development level of the automobile industry are decisive factors influencing the trend of consuming diesel-gasoline ratio. Before 2020, the gasoline demand in China is increased faster than that of diesel oil; the influence of alternative energy sources on the change trend of gasoline and diesel oil requirements is limited. The consumption ratio of diesel and gasoline in China is predicted to be reduced to about 1.0 in 2020.
CN1382776 discloses a combined method of residual oil hydrotreating and heavy oil catalytic cracking, which proposes that heavy cycle oil produced by a catalytic cracking device and clarified oil in slurry oil are mixed together to be used as a part of residual oil device feeding, and the stream is returned to the catalytic cracking device together with other feeding materials for processing after being subjected to hydro-upgrading, so that the yield of gasoline and diesel oil of the catalytic cracking device can be improved. Although the gasoline yield is increased by 2.8-3 units, compared with the high cost of a hydrogenation device and the large hydrogen consumption and corresponding energy consumption, the increase of the gasoline yield is not ideal.
CN1422327A discloses a method for increasing the production of small molecular olefins and gasoline by hydrotreating HCO produced by a catalytic cracking unit or mixing with naphtha, and processing by an external independent catalytic cracking unit. Although the yield of the low-carbon olefin is improved to a certain extent, the technology for treating the relatively light naphtha by adopting the two-riser combined hydrogenation technology is complex, the investment cost is high, and the technology economy is not high.
CN103540359A discloses an inferior heavy oil catalytic conversion process for improving the yield of low-carbon olefins and gasoline, the patent proposes that a riser reactor is divided into two reaction zones, the first reaction zone is a zone for the reaction of inferior heavy oil and a catalyst, the second reaction zone is a zone for the reaction of catalytic wax oil and diesel oil and the catalyst, slurry oil generated by the reaction of the riser enters a vacuum distillation tower, and a lower carbon residue light fraction material at an upper outlet of the vacuum distillation tower and a higher carbon residue heavy fraction material at a middle outlet of the vacuum distillation tower enter a hydrogenation device together for hydrogenation treatment; the bottom ultrahigh carbon residue slurry oil enters a delayed coking device after being treated by a slurry oil filter; the low carbon residue easy cracking material from the hydrogenation device enters the first reaction zone of the lift pipe for reaction again. The patent utilizes the combined process of catalytic cracking, a pressure reduction device and hydrogenation to carry out combined operation, can simultaneously improve the yield of gasoline and low-carbon olefin to a certain extent, but has more complex process, needs to carry out greater transformation on the prior catalytic cracking device, has high investment cost and is difficult to implement.
CN 204981765U discloses an inferior light oil and heavy oil processingequipment, characterized by: a dense phase conversion reactor is arranged below the heavy oil feeding nozzle, and an inferior light oil or/and olefin gas phase feeding distributor is arranged inside the dense phase conversion reactor, or an inferior light oil or/and olefin gas phase feeding nozzle is arranged at the middle lower part of the pre-lifting section or the pre-lifting section; the inferior light oil or/and olefin vaporizer is provided, the lower part of the inferior light oil or/and olefin vaporizer is provided with a liquid phase inlet, and the upper part of the inferior light oil or/and olefin vaporizer is provided with a gas phase outlet and is connected with a gas phase feeding distributor or a gas phase feeding nozzle of the dense phase conversion reactor. The device is used for modifying coking gasoline, naphtha, olefin and the like to increase the yield of propylene, and simultaneously improves the oil ratio of heavy oil cracking reactants, improves the product distribution and improves the economic efficiency. However, the patent has no examples, and the specific effects are unknown. From the analysis of the catalytic cracking principle, because the light hydrocarbons adopted by the device are the coking gasoline, naphtha and olefin, and after the dense phase conversion reactor is adopted, the high-temperature regenerated catalyst contacts and reacts with the light hydrocarbons under the condition of a larger catalyst-oil ratio, the light hydrocarbons are cracked excessively, and the byproduct dry gas is greatly increased.
CN102746880A discloses a method for coupling light hydrocarbon and heavy oil with catalytic cracking gasoline, diesel oil, ethylene and propylene, wherein a parallel or coaxial composite riser tube circulating reaction-regeneration device is adopted; the preheated light hydrocarbon enters the embedded riser reactor and contacts with the catalyst I to generate a product containing low-carbon olefin and form a carbon-deposited catalyst II; the preheated heavy oil enters an external riser reactor and contacts with a catalyst I to generate a product containing gasoline and diesel oil, a carbon deposition catalyst III is formed, carbon deposition catalysts II and III enter a regenerator, and the regenerated catalyst I returns to the reactor. The patent adopts two riser reactors, the embedded riser adopts mixed C4, FCC light gasoline, light naphtha and light diesel oil as raw materials, the external embedded riser adopts Daqing mixed oil or Daqing vacuum residue oil as raw materials, the gasoline yield is lower, the process is more complex, and the implementation difficulty is high.
Therefore, how to convert heavy diesel oil and poor heavy oil into gasoline and low-carbon olefins more by using a catalytic cracking unit becomes a focus of attention of researchers and a key problem to be solved.
Disclosure of Invention
The invention aims to provide a catalytic conversion method which takes heavy diesel oil and poor-quality heavy oil as raw materials and simultaneously improves the yield of gasoline and low-carbon olefin on the basis of the prior art.
The invention provides a catalytic conversion method for increasing yields of gasoline and low-carbon olefins, which comprises the following steps: the reaction zone is a light hydrocarbon reaction zone I, a heavy hydrocarbon reaction zone and a light hydrocarbon reaction zone II which are expanded in diameter from bottom to top along the vertical direction of the riser reactor; introducing two regenerant conveying pipes from a regenerator to respectively convey the regenerated catalyst to a light hydrocarbon reaction zone I and a heavy hydrocarbon reaction zone with expanded diameters, simultaneously and respectively spraying preheated light hydrocarbon and heavy hydrocarbon into the light hydrocarbon reaction zone I and the heavy hydrocarbon reaction zone from an integrated nozzle, and contacting the preheated light hydrocarbon and heavy hydrocarbon with the catalyst from the regenerator to perform catalytic cracking reaction; the light hydrocarbon is petroleum hydrocarbon fraction with the distillation range of 140-320 ℃, the heavy hydrocarbon is petroleum hydrocarbon fraction with the initial boiling point of more than or equal to 245 ℃ and/or animal and vegetable oil and/or coal liquefaction products containing hydrocarbon, and the mass ratio of the light hydrocarbon to the heavy hydrocarbon is 0.001: 1-0.55: 1; the catalyst is a catalytic cracking catalyst, and the method comprises the following steps:
(1) the pre-lifting medium is sprayed upwards from the bottom of the riser reactor, light hydrocarbon is sprayed out from a light hydrocarbon spray head in the integrated spray nozzle, and is contacted and reacted with the high-temperature regenerated catalyst from the regenerator in the expanded light hydrocarbon reaction zone I, and the generated reaction product and the reacted carbon-deposited catalyst move upwards and enter the heavy hydrocarbon reaction zone;
(2) the heavy hydrocarbon is sprayed out of a heavy hydrocarbon outer spray head in the integrated nozzle, enters the reactor from the bottom of the heavy hydrocarbon reaction zone, is contacted and reacted with the high-temperature regenerated catalyst from the regenerator and the carbon deposit catalyst moving upwards from the expanded light hydrocarbon reaction zone I, and the generated reaction product and the reacted catalyst move upwards and enter a light hydrocarbon reaction zone II;
(3) the generated reaction product and the catalyst enter a cyclone separation system after leaving the light hydrocarbon reaction zone II;
(4) after the reaction products are separated, the catalyst to be generated enters a stripper for steam stripping, the catalyst after steam stripping enters a regenerator, and the catalyst after steam stripping enters a light hydrocarbon reaction zone I with the diameter expanded by a riser or a heavy hydrocarbon reaction zone for recycling after being burnt by the regenerator; and the reaction product enters a fractionating tower through an oil-gas pipeline to be fractionated to obtain a corresponding product.
The invention relates to a catalytic cracking conversion method for increasing production of gasoline and reducing slurry oil, wherein an integrated nozzle comprises a light hydrocarbon nozzle, a light hydrocarbon sleeve, a heavy hydrocarbon nozzle and a heavy hydrocarbon sleeve, wherein the light hydrocarbon nozzle is provided with a light hydrocarbon spray head, the heavy hydrocarbon nozzle is provided with a heavy hydrocarbon outer spray head, and the light hydrocarbon spray head and the heavy hydrocarbon outer spray head can simultaneously and respectively spray light hydrocarbon and heavy hydrocarbon; the light hydrocarbon sleeve in the integrated nozzle is coaxial with the heavy hydrocarbon outer sleeve, and the outer pipe wall of the heavy hydrocarbon outer sleeve and the inner pipe wall of the light hydrocarbon sleeve form a light hydrocarbon annular atomizing chamber; 1-5 heavy hydrocarbon outer spray holes are uniformly formed in the heavy hydrocarbon outer spray head, 4-10 light hydrocarbon spray holes are uniformly formed in the light hydrocarbon spray head, the ratio of the outer diameter of the light hydrocarbon sleeve to the outer diameter of the heavy hydrocarbon outer sleeve is 2.20: 1-2.28: 1, and the ratio of the aperture of a single light hydrocarbon spray hole in the light hydrocarbon spray head to the aperture of a single heavy hydrocarbon outer spray hole in the heavy hydrocarbon outer spray head is 0.1: 1-2.0: 1.
According to the catalytic cracking conversion method for increasing the yield of gasoline and reducing the slurry oil, the ratio of the inner diameter of the riser reactor of the diameter-expanded light hydrocarbon reaction zone I to the inner diameter of the riser reactor of the heavy hydrocarbon reaction zone is 1.1: 1-3: 1.
According to the catalytic cracking conversion method for increasing the yield of gasoline and reducing the slurry oil, the heights of the expanded light hydrocarbon reaction zone I, the heavy hydrocarbon reaction zone and the light hydrocarbon reaction zone II respectively account for 1-15%, 1-40% and 1-60% of the total height of the riser reactor.
The catalytic cracking conversion method for increasing the yield of gasoline and reducing the slurry oil of the invention has the pre-lifting medium selected from one or a mixture of more than two of nitrogen, helium, catalytic cracking dry gas and water vapor.
According to the catalytic cracking conversion method for increasing the yield of gasoline and reducing the slurry oil, light hydrocarbon in the expanded light hydrocarbon reaction zone I is distillate oil with the boiling point range of 140-320 ℃, the sulfur content of 0.03-0.27 weight percent and the cetane number of 55-65, and the distillate oil is one or a mixture of more than two of straight-run diesel oil, vacuum diesel oil, hydrogenated diesel oil, residual hydrogenated diesel oil, coked diesel oil, catalytic diesel oil and light/heavy cycle oil of a catalytic cracking unit.
The heavy hydrocarbon in the heavy hydrocarbon reaction zone is petroleum hydrocarbon fraction with an initial boiling point of more than or equal to 245 ℃ and/or animal and vegetable oil containing hydrocarbon and/or coal liquefaction products, and specifically is one or a mixture of more than two of atmospheric gas oil, vacuum residual oil, atmospheric residual oil, inferior diesel oil, coal tar, residual oil hydrogenation tail oil, solvent deasphalted oil, raffinate oil, coker wax oil, shale oil, oil sand asphalt, heavy crude oil, animal and vegetable oil containing hydrocarbon and coal liquefaction products.
According to the catalytic cracking conversion method for increasing the yield of gasoline and reducing the slurry oil, the contact temperature of the light hydrocarbon oil agent in the expanded light hydrocarbon reaction zone I is 450-710 ℃, and preferably 590-650 ℃; the reaction pressure is normal pressure to 320 kPa, preferably 100-270 kPa; the retention time is 0.05-3 s, preferably 0.1-0.7 s; the catalyst-to-light hydrocarbon solvent-to-oil ratio is 5: 1-160: 1, preferably 15: 1-130: 1; the mass ratio of the light hydrocarbon to the heavy hydrocarbon is 0.001: 1-0.55: 1, preferably 0.05: 1-0.15: 1; the temperature of the regenerated catalyst is 570-755 ℃, preferably 630-720 ℃.
According to the catalytic cracking conversion method for increasing the yield of gasoline and reducing the slurry oil, the contact temperature of the heavy hydrocarbon oil agent in the heavy hydrocarbon reaction zone is 450-640 ℃, and preferably 500-600 ℃; the catalyst-to-raw material catalyst-to-oil ratio is 5: 1-25: 1, preferably 6: 1-18: 1; the residence time of oil gas molecules is 0.05-2.5 s, preferably 0.5-1.5 s; the reaction pressure is normal pressure to 320 kPa, preferably 100 to 270 kPa.
The method provided by the invention can be carried out after a conventional catalytic cracking device is properly modified.
The theoretical basis of the method provided by the invention is as follows: because the acid B in the catalyst is mainly provided by the molecular sieve, and the pore canal diameter of the molecular sieve is small, in the conventional catalytic cracking reaction, heavy hydrocarbon macromolecules are difficult to enter the molecular sieve to contact with an acid center to react when the heavy hydrocarbon macromolecules are contacted with the molecular sieve at the bottom of a riser reactor, the temperature of the regenerated catalyst circulating from a regenerator is about 680 ℃, and at the moment, the heavy hydrocarbon macromolecules are easy to coke outside the pore canal of the molecular sieve instantly, so that the pore canal of the molecular sieve is blocked, and the cracking effect is influenced. According to the invention, a high-temperature regenerated catalyst circulated to a riser reactor from a regenerator firstly contacts and reacts with light hydrocarbon (such as straight-run diesel oil) in an expanded light hydrocarbon reaction zone I, on one hand, the inner diameter of the riser reactor in the expanded light hydrocarbon reaction zone I is larger than that of the heavy hydrocarbon reaction zone, and the reaction time of the light hydrocarbon (such as straight-run diesel oil) in the expanded light hydrocarbon reaction zone I is prolonged, so that the time for the light hydrocarbon (such as straight-run diesel oil) to be rapidly cracked at high temperature to generate a large amount of small molecular olefins is prolonged, the acid B center on the regenerated catalyst and the small molecular olefins undergo catalytic reaction to generate a large amount of carbonium ions, and the carbonium ions move upwards to the heavy hydrocarbon reaction zone to initiate the chain reaction of the large heavy hydrocarbon macromolecules, promote the rapid cracking of; on the other hand is owing to introduce a regenerant conveyer pipe from the regenerator and carry the regenerated catalyst to the heavy hydrocarbon reaction zone of riser reactor for the average activity of catalyst in heavy hydrocarbon reaction zone improves, has strengthened the high-efficient conversion of heavy hydrocarbon, thereby reaches the multiple effect of output increasing gasoline and low carbon olefin.
The invention has the beneficial effects that: (1) because the integrated nozzle is adopted, heated light hydrocarbon (such as straight-run diesel) is sprayed out from a plurality of light hydrocarbon spray holes which are uniformly distributed on the light hydrocarbon spray head to form uniformly dispersed light hydrocarbon (such as straight-run diesel) oil drops, the catalyst is ensured to be uniformly contacted with the light hydrocarbon (such as straight-run diesel) oil drops, and the light hydrocarbon (such as straight-run diesel) is prevented from forming channeling with the catalyst; the heated heavy hydrocarbon is sprayed out of a plurality of heavy hydrocarbon outer spray holes uniformly distributed on the heavy hydrocarbon outer spray head to form uniformly dispersed heavy hydrocarbon oil drops, so that the catalyst is ensured to be uniformly contacted with the heavy hydrocarbon oil drops; (2) the inner diameter of a riser reactor of the expanded light hydrocarbon reaction area I is larger than that of the heavy hydrocarbon reaction area, the reaction time of the light hydrocarbon (such as straight-run diesel oil) in the expanded light hydrocarbon reaction area I is prolonged, the light hydrocarbon (such as straight-run diesel oil) is rapidly cracked at high temperature to generate a large amount of micromolecule olefin, the acid B center on the regenerated catalyst and the micromolecule olefin generate catalytic reaction to generate a large amount of carbonium ions, and the carbonium ions move upwards to the heavy hydrocarbon reaction area to initiate the chain reaction of heavy hydrocarbon macromolecules, promote the rapid cracking of the heavy hydrocarbon macromolecules, generate more carbonium ions and accelerate the cracking of the heavy hydrocarbon; (3) the regenerated catalyst is conveyed to the heavy hydrocarbon reaction area of the riser reactor by introducing a regenerant conveying pipe from the regenerator, so that the average activity of the catalyst in the heavy hydrocarbon reaction area is improved, the high-efficiency conversion of the heavy hydrocarbon is enhanced, and the multiple effects of increasing the yield of gasoline and the low-carbon olefin are achieved.
Drawings
FIG. 1 is a flow chart of the apparatus used in the catalytic cracking conversion method for increasing the yield of gasoline and light olefins according to the present invention;
FIG. 2 is an enlarged schematic view of the integral nozzle;
FIG. 3 is a flow chart of the apparatus in the case of an experiment using a conventional nozzle;
wherein: 1-pre-lifting medium, 2-light hydrocarbon, 3-heavy hydrocarbon, 4-riser reactor, 5-stripper, 6-spent agent conveying pipe, 7-regenerator, 8-first regenerant conveying pipe, 9-second regenerant conveying pipe, 10-oil gas pipeline, 11-fractionating tower and 12-integrated nozzle.
13-light hydrocarbon inlet, 14-heavy hydrocarbon inlet, 15-light hydrocarbon nozzle, 16-light hydrocarbon spray head, 17-heavy hydrocarbon nozzle, 18-heavy hydrocarbon outer spray head, 19-heavy hydrocarbon outer sleeve pipe, 20-light hydrocarbon sleeve pipe, 21-annular atomizing chamber, 32-light hydrocarbon spray hole and 33-heavy hydrocarbon outer spray hole.
22-pre-lifting medium, 23-mixed raw material, 24-riser reactor, 25-stripper, 26-spent agent conveying pipe, 27-regenerator, 28-regenerant conveying pipe, 29-oil gas pipeline, 30-fractionating tower and 31-conventional nozzle.
Detailed Description
The method according to the invention is further illustrated with reference to the following figures and examples, which should not be construed as limiting the invention.
The main analysis method comprises the following steps:
in each example, Na2O、Al2O3Chemical compositions such as these were measured by X-ray fluorescence (see "analytical methods of petrochemical industry (RIPP methods of experiments)", ed. Yang Cui et al, ed. science publishers, published in 1990). The phase was determined by X-ray diffraction. Specific surface area and pore volume are measured by low-temperature nitrogen adsorption-desorption method(ii) a The particle size distribution is analyzed by laser particle size (analysis method GB/T19077.1-2008); the abrasion index is determined by the abrasion index (straight tube method) (analytical method GB/T15458-; evaluation of Microreflective Activity (MA): the method of ASTM-D3907 was used. The catalyst is treated for 17 hours at 800 ℃ under the condition of 100 percent of water vapor in advance, and Hongkong light diesel oil is used as reaction raw oil. The reaction temperature is 460 ℃, the oil inlet time is 70s, the catalyst loading is 2.5-5 g, and the yield of gasoline after reaction is analyzed by GC 7890.
The main raw materials and sources are as follows:
LDO-70 fresh catalyst, produced by catalyst factory of petrochemical company, Lanzhou, is subjected to hydrothermal deactivation treatment for 10 hours at the temperature of 800 ℃ and with the water vapor of 100 percent before evaluation, and the physicochemical properties of the aged LDO-70 are shown in Table 1.
TABLE 1 physicochemical Properties of the catalyst
The light hydrocarbon is normal third line diesel oil (the properties are shown in table 2) of 500 ten thousand tons/year normal pressure reduction device of Lanzhou petrochemical company; the heavy hydrocarbon is taken from a fresh catalytic raw material (properties are shown in a table 3) of a 300 ten thousand ton/year catalytic cracking device of Lanzhou petrochemical company, the mass ratio of vacuum wax oil to vacuum residue in the fresh catalytic raw material is (6:4), the vacuum wax oil is the vacuum wax oil from a 550 ten thousand ton atmospheric and vacuum device of the Lanzhou petrochemical company, and the vacuum residue is the vacuum residue from a 550 ten thousand ton atmospheric and vacuum device of the Lanzhou petrochemical company.
The evaluation device adopts a flexible reaction mode type catalytic cracking riser test device produced by the Luoyang petrochemical engineering company.
TABLE 2 Properties of light hydrocarbons
TABLE 3 Properties of heavy hydrocarbons
| Item | Test data | Item | Test data |
| Molecular weight/(g. mol)-1) | 432 | w (saturated hydrocarbons)/%) | 61.6 |
| Density/(kg. m) at 20 DEG C-3) | 877.9 | w (aromatics)/%) | 24.9 |
| Kinematic viscosity at 100 ℃/(mm)2·s-1) | 17.08 | w (colloid + asphaltene)/% | 13.5 |
| w (carbon residue)/%) | 5.04 | w (heavy metals)/(μ g)-1) | |
| Flash point/. degree.C | 224 | Fe | 60.50 |
| w (element)/%) | Ni | 9.14 | |
| S | 0.61 | V | 22.12 |
| N | 0.29 | Na | 9.00 |
Example 1
Tests were carried out using the apparatus shown in figure 1 and the integrated nozzle shown in figure 2.
The heights of the expanded light hydrocarbon reaction zone I, the heavy hydrocarbon reaction zone and the light hydrocarbon reaction zone II respectively account for 5 percent, 35 percent and 55 percent of the total height of the riser reactor. The ratio of the inner diameter of the riser reactor of the expanded light hydrocarbon reaction zone I to the inner diameter of the riser reactor of the heavy hydrocarbon reaction zone is 1.5: 1. The ratio of the outer diameter of the light hydrocarbon sleeve 20 of the integrated nozzle 12 to the outer diameter of the heavy hydrocarbon outer sleeve 19 is 2.20:1, and the ratio of the aperture of a single light hydrocarbon spray hole on the light hydrocarbon spray head 16 to the aperture of a single heavy hydrocarbon spray hole on the heavy hydrocarbon outer spray head 18 is 1.429: 1. The pre-lift medium is nitrogen.
The 500 ten thousand normal three-way diesel oil with the mass flow rate of 150g/h is sprayed out from 4 light hydrocarbon spray holes 32 on a light hydrocarbon spray head 16 of an integrated nozzle 12, a light hydrocarbon reaction area I with the diameter expanded in a riser reactor 4 is contacted and reacted with a regenerated catalyst conveyed by a first regenerant conveying pipe 8, and the reacted catalyst continues to move upwards under the conditions that the contact temperature of a light hydrocarbon oil agent is 620 ℃, the agent-oil ratio is 64.4, the retention time is 0.2s, the weight ratio of the 500 ten thousand normal three-way diesel oil to 300 ten thousand catalyst is 0.1:1, the reaction pressure is 130 kilopascals, and the temperature of the regenerated catalyst is 670 ℃; 300 million catalysts with mass flow rate of 1500g/h are sprayed out from 4 heavy hydrocarbon outer spray holes 33 on a heavy hydrocarbon outer spray head 18 of an integrated nozzle 12, a regenerated catalyst conveyed from a heavy hydrocarbon reaction zone and a second regenerant conveying pipe 9 and a carbon-deposited catalyst which moves upwards from a diameter-expanded light hydrocarbon reaction zone I are contacted and reacted together, the reacted products and the catalysts continue to move upwards under the conditions of the heavy hydrocarbon oil contact temperature 530 ℃, the reactor outlet temperature 505 ℃, the agent-oil ratio 8, the reaction time of 1.9s and the reaction pressure of 145 kilopascals, the products and the catalysts enter a stripper 5 for stripping after passing through a light hydrocarbon reaction zone II, the stripped catalysts to be generated enter a regenerator 7 for burning through a catalyst conveying pipe 6, and the burnt catalysts enter a riser reactor 4 through the first regenerant conveying pipe 8 and the second regenerant conveying pipe 9. Oil gas generated by the reaction of the riser reactor 4 and the stripper 5 enters a fractionating tower 11 through an oil-gas pipeline 10 and is separated into dry gas, liquefied gas, gasoline, diesel oil and oil slurry. The specific reaction conditions and reaction results are shown in Table 4.
Comparative example 1
Comparative example 1 was conducted using a catalytic cracking atomized feed nozzle as described in patent CN201120267386.4, using the apparatus shown in fig. 3.
The mixed raw material of 300 ten thousand normal third-line diesel oil and 500 ten thousand normal third-line diesel oil with the mass flow rate of 1650g/h (the mass ratio of 500 ten thousand normal third-line diesel oil to 300 ten thousand normal third-line diesel oil is 0.1:1) is sprayed out from a conventional nozzle 31 to be in contact reaction with the catalyst, the product after the reaction and the catalyst continue to move upwards under the conditions of 530 ℃ of contact temperature of oil, 505 ℃ of outlet temperature of a reactor, 8 ℃ of catalyst-oil ratio, 2.1s of reaction time and 145 kilopascals of reaction pressure, the catalyst after the steam stripping enters a stripper 25 to be stripped, the catalyst after the steam stripping enters a regenerator 27 to be burnt through a spent agent conveying pipe 26, and the catalyst after the burning enters a riser reactor 24 through a regenera. Oil gas generated by the reaction of the riser reactor 24 and the stripper 25 enters a fractionating tower 30 through an oil-gas pipeline 29 and is separated into dry gas, liquefied gas, gasoline, diesel oil and slurry oil. The specific reaction conditions and reaction results are shown in Table 4.
Table 4 reaction conditions and reaction results of example 1 and comparative example 1
Example 2
Tests were carried out using the apparatus shown in figure 1 and the integrated nozzle shown in figure 2.
The heights of the expanded light hydrocarbon reaction zone I, the heavy hydrocarbon reaction zone and the light hydrocarbon reaction zone II respectively account for 5 percent, 35 percent and 55 percent of the total height of the riser reactor. The ratio of the inner diameter of the riser reactor of the expanded light hydrocarbon reaction zone I to the inner diameter of the riser reactor of the heavy hydrocarbon reaction zone is 1.5: 1. The ratio of the outer diameter of the light hydrocarbon sleeve 20 of the integrated nozzle 12 to the outer diameter of the heavy hydrocarbon outer sleeve 19 is 2.20:1, and the ratio of the aperture of a single light hydrocarbon spray hole on the light hydrocarbon spray head 16 to the aperture of a single heavy hydrocarbon spray hole on the heavy hydrocarbon outer spray head 18 is 1.429: 1. The pre-lift medium is nitrogen.
The 500 ten thousand normal three-way diesel oil with the mass flow rate of 150g/h is sprayed out from 4 light hydrocarbon spray holes 32 on a light hydrocarbon spray head 16 of an integrated nozzle 12, an expanded light hydrocarbon reaction area I in a riser reactor 4 is in contact reaction with a regenerated catalyst conveyed by a first regenerant conveying pipe 8, the catalyst after the reaction continues to move upwards under the conditions of the contact temperature of light hydrocarbon oil, 590 ℃, the agent-oil ratio of 64.4, the residence time of 0.2s, the weight ratio of the 500 ten thousand normal three-way diesel oil to 300 ten thousand catalyst, the mass ratio of 0.1:1, the reaction pressure of 125 kPa and the temperature of the regenerated catalyst of 630 ℃, the 300 ten thousand catalyst with the mass flow rate of 1500g/h is sprayed out from 4 heavy hydrocarbon outer spray holes 33 on an integrated nozzle 12 heavy hydrocarbon outer spray head 18, the regenerated catalyst conveyed by a second regenerant conveying pipe 9 in a heavy hydrocarbon reaction area and the carbon accumulated catalyst which moves upwards from the expanded light hydrocarbon reaction area I are in contact and react together, under the conditions that the contact temperature of a heavy hydrocarbon oil agent is 515 ℃, the outlet temperature of a reactor is 500 ℃, the agent-oil ratio is 8, the reaction time is 1.9s and the reaction pressure is 140 kPa, a product after reaction and a catalyst continue to move upwards, the product and the catalyst enter a stripper 5 for stripping after passing through a light hydrocarbon reaction zone II, the catalyst to be generated after stripping enters a regenerator 7 for burning through a catalyst to be generated conveying pipe 6, and the catalyst after burning enters a riser reactor 4 through a first regenerant conveying pipe 8 and a second regenerant conveying pipe 9. Oil gas generated by the reaction of the riser reactor 4 and the stripper 5 enters a fractionating tower 11 through an oil-gas pipeline 10 and is separated into dry gas, liquefied gas, gasoline, diesel oil and oil slurry. Specific reaction conditions and reaction results are shown in Table 5.
Comparative example 2
Comparative example 2 was conducted using a catalytic cracking atomized feed nozzle as described in patent CN201120267386.4, using the apparatus shown in fig. 3.
The mixed raw material of 300 ten thousand normal third-line diesel oil and 500 ten thousand normal third-line diesel oil with the mass flow rate of 1650g/h (the mass ratio of 500 ten thousand normal third-line diesel oil to 300 ten thousand normal third-line diesel oil is 0.1:1) is sprayed out from a conventional nozzle 31 to be in contact reaction with the catalyst, the product after the reaction and the catalyst continue to move upwards under the conditions of the contact temperature of oil, the outlet temperature of a reactor of 500 ℃, the catalyst-oil ratio of 8, the reaction time of 2.1s and the reaction pressure of 140 kilopascals, the catalyst enters a stripper 25 to be stripped to enter a regenerator 27 to be coked through a spent catalyst conveying pipe 26, and the coked catalyst enters a riser reactor 24 through a regenerant conveying pipe 28. Oil gas generated by the reaction of the riser reactor 24 and the stripper 25 enters a fractionating tower 30 through an oil-gas pipeline 29 and is separated into dry gas, liquefied gas, gasoline, diesel oil and slurry oil. Specific reaction conditions and reaction results are shown in Table 5.
Table 5 reaction conditions and reaction results of example 2 and comparative example 2
Example 3
Tests were carried out using the apparatus shown in figure 1 and the integrated nozzle shown in figure 2.
The heights of the expanded light hydrocarbon reaction zone I, the heavy hydrocarbon reaction zone and the light hydrocarbon reaction zone II respectively account for 5 percent, 35 percent and 55 percent of the total height of the riser reactor. The ratio of the inner diameter of the riser reactor of the expanded light hydrocarbon reaction zone I to the inner diameter of the riser reactor of the heavy hydrocarbon reaction zone is 1.5: 1. The ratio of the outer diameter of the light hydrocarbon sleeve 20 of the integrated nozzle 12 to the outer diameter of the heavy hydrocarbon outer sleeve 19 is 2.20:1, and the ratio of the aperture of a single light hydrocarbon spray hole on the light hydrocarbon spray head 16 to the aperture of a single heavy hydrocarbon spray hole on the heavy hydrocarbon outer spray head 18 is 1.429: 1. The pre-lift medium is nitrogen.
The 500 ten thousand normal three-way diesel oil with the mass flow rate of 150g/h is sprayed out from 4 light hydrocarbon spray holes 32 on a light hydrocarbon spray head 16 of an integrated nozzle 12, an expanded light hydrocarbon reaction area I in a riser reactor 4 is in contact reaction with a regenerated catalyst conveyed by a first regenerant conveying pipe 8, the catalyst after the reaction continues to move upwards under the conditions that the contact temperature of light hydrocarbon oil is 650 ℃, the agent-oil ratio is 64.4, the residence time is 0.2s, the weight ratio and the mass ratio of the 500 ten thousand normal three-way diesel oil to 300 ten thousand catalyst are 0.1:1, the reaction pressure is 135 kilopascal and the temperature of the regenerated catalyst is 710 ℃, the 300 ten thousand catalyst with the mass flow rate of 1500g/h is sprayed out from 4 heavy hydrocarbon outer spray holes 33 on a heavy hydrocarbon outer spray head 18 of the integrated nozzle 12, the heavy hydrocarbon reaction area is in contact with the regenerated catalyst conveyed by a second regenerant conveying pipe 9 and the carbon deposition catalyst which moves upwards from the expanded light hydrocarbon reaction area I, under the conditions that the contact temperature of a heavy hydrocarbon oil agent is 540 ℃, the outlet temperature of a reactor is 510 ℃, the agent-oil ratio is 8, the reaction time is 1.9s and the reaction pressure is 145 kilopascals, a product after reaction and a catalyst continue to move upwards, the product and the catalyst enter a stripper 5 for stripping after passing through a light hydrocarbon reaction zone II, the catalyst to be generated after stripping enters a regenerator 7 for burning through a catalyst to be generated conveying pipe 6, and the catalyst after burning enters a riser reactor 4 through a first regenerant conveying pipe 8 and a second regenerant conveying pipe 9. Oil gas generated by the reaction of the riser reactor 4 and the stripper 5 enters a fractionating tower 11 through an oil-gas pipeline 10 and is separated into dry gas, liquefied gas, gasoline, diesel oil and oil slurry. The specific reaction conditions and the reaction results are shown in Table 6.
Comparative example 3
Comparative example 3 a conventional nozzle was used which was a catalytic cracking atomized feed nozzle as described in patent CN201120267386.4 and was tested using the apparatus shown in figure 3.
The mixed raw material of 300 ten thousand normal third-line diesel oil and 500 ten thousand normal third-line diesel oil with the mass flow rate of 1650g/h (the mass ratio of 500 ten thousand normal third-line diesel oil to 300 ten thousand normal third-line diesel oil is 0.1:1) is sprayed out from a conventional nozzle 31 to be in contact reaction with the catalyst, the product after the reaction and the catalyst continue to move upwards under the conditions of the contact temperature of the oil agent of 540 ℃, the outlet temperature of the reactor of 510 ℃, the agent-oil ratio of 8, the reaction time of 2.1s and the reaction pressure of 145 kilopascals, the catalyst after the steam stripping enters a stripper 25 to be stripped and enters a regenerator 27 to be burnt through a spent agent conveying pipe 26, and the catalyst after the burning enters a riser reactor 24 through a regenerant conveying. Oil gas generated by the reaction of the riser reactor 24 and the stripper 25 enters a fractionating tower 30 through an oil-gas pipeline 29 and is separated into dry gas, liquefied gas, gasoline, diesel oil and slurry oil. The specific reaction conditions and the reaction results are shown in Table 6.
Table 6 reaction conditions and reaction results of example 3 and comparative example 3
Compared with the comparative example 1, the yield of gasoline after reaction is improved by 5.13 percent, the total liquid yield is improved by 2.61 percent, the conversion rate is improved by 12.09 percent, the yield of diesel oil is reduced by 7.91 percent, the yield of heavy oil is reduced by 4.18 percent, the yield of propylene is improved by 1.99 percent, and the yield of butylene is improved by 2.45 percent under the reaction conditions of completely same feeding quality and different feeding nozzles and feeding methods.
Compared with the comparative example 2, in the reaction conditions of completely same feeding quality and different feeding nozzles and feeding methods, the yield of gasoline after reaction is improved by 4.99 percent, the total liquid yield is improved by 2.27 percent, the conversion rate is improved by 11.39 percent, the yield of diesel oil is reduced by 7.62 percent, the yield of heavy oil is reduced by 3.77 percent, the yield of propylene is improved by 1.70 percent, and the yield of butylene is improved by 2.13 percent.
Compared with the comparative example 3, in the reaction conditions of completely same feeding quality and different feeding nozzles and feeding methods, the gasoline yield is improved by 4.66 percent after the reaction, the total liquid yield is improved by 2.09 percent, the conversion rate is improved by 12.93 percent, the diesel oil yield is reduced by 8.92 percent, the heavy oil yield is reduced by 4.01 percent, the propylene yield is improved by 2.35 percent, and the butylene yield is improved by 2.94 percent.
The data of the examples and the comparative examples show that the invention has the characteristic of increasing the yield of gasoline and low-carbon olefin.
The present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof, and it is therefore intended that all such changes and modifications as fall within the true spirit and scope of the invention be considered as within the following claims.
Claims (12)
1. A catalytic conversion method for increasing yields of gasoline and low-carbon olefins is characterized by comprising the following steps: the reaction zone is a light hydrocarbon reaction zone I, a heavy hydrocarbon reaction zone and a light hydrocarbon reaction zone II which are expanded from bottom to top along the vertical direction of the riser reactor; introducing two regenerant conveying pipes from a regenerator to respectively convey the regenerated catalyst to a light hydrocarbon reaction zone I and a heavy hydrocarbon reaction zone with expanded diameters, simultaneously and respectively spraying preheated light hydrocarbon and heavy hydrocarbon into the light hydrocarbon reaction zone I and the heavy hydrocarbon reaction zone from an integrated nozzle, and contacting the preheated light hydrocarbon and heavy hydrocarbon with the catalyst from the regenerator to perform catalytic cracking reaction; the light hydrocarbon is petroleum hydrocarbon fraction with the distillation range of 140-320 ℃, the heavy hydrocarbon is petroleum hydrocarbon fraction with the initial boiling point of more than or equal to 245 ℃ and/or animal and vegetable oil and/or coal liquefaction products containing hydrocarbon, and the mass ratio of the light hydrocarbon to the heavy hydrocarbon is 0.001: 1-0.55: 1; the catalyst is a catalytic cracking catalyst, and the method comprises the following steps:
(1) the pre-lifting medium is sprayed upwards from the bottom of the riser reactor, light hydrocarbon is sprayed out from a light hydrocarbon spray head in the integrated spray nozzle, and is contacted and reacted with the high-temperature regenerated catalyst from the regenerator in the expanded light hydrocarbon reaction zone I, and the generated reaction product and the reacted carbon-deposited catalyst move upwards and enter the heavy hydrocarbon reaction zone;
(2) the heavy hydrocarbon is sprayed out of a heavy hydrocarbon outer spray head in the integrated nozzle, enters the reactor from the bottom of the heavy hydrocarbon reaction zone, is contacted and reacted with the high-temperature regenerated catalyst from the regenerator and the carbon deposit catalyst moving upwards from the expanded light hydrocarbon reaction zone I, and the generated reaction product and the reacted catalyst move upwards and enter a light hydrocarbon reaction zone II;
(3) the generated reaction product and the catalyst enter a cyclone separation system after leaving the light hydrocarbon reaction zone II;
(4) after the reaction products are separated, the catalyst to be generated enters a stripper for steam stripping, the catalyst after steam stripping enters a regenerator, and the catalyst after steam stripping enters a light hydrocarbon reaction zone I with the diameter expanded by a riser or a heavy hydrocarbon reaction zone for recycling after being burnt by the regenerator; and the reaction product enters a fractionating tower through an oil-gas pipeline to be fractionated to obtain a corresponding product.
2. The method of claim 1, wherein the integrated nozzle comprises a light hydrocarbon nozzle, a light hydrocarbon casing, a heavy hydrocarbon nozzle and a heavy hydrocarbon casing, wherein the light hydrocarbon nozzle is provided with a light hydrocarbon spray head, the heavy hydrocarbon nozzle is provided with a heavy hydrocarbon outer spray head, and the light hydrocarbon spray head and the heavy hydrocarbon outer spray head can simultaneously and respectively spray light hydrocarbon and heavy hydrocarbon; the light hydrocarbon sleeve in the integrated nozzle is coaxial with the heavy hydrocarbon outer sleeve, and the outer pipe wall of the heavy hydrocarbon outer sleeve and the inner pipe wall of the light hydrocarbon sleeve form a light hydrocarbon annular atomizing chamber; 1-5 heavy hydrocarbon outer spray holes are uniformly formed in the heavy hydrocarbon outer spray head, 4-10 light hydrocarbon spray holes are uniformly formed in the light hydrocarbon spray head, the ratio of the outer diameter of the light hydrocarbon sleeve to the outer diameter of the heavy hydrocarbon outer sleeve is 2.20: 1-2.28: 1, and the ratio of the aperture of a single light hydrocarbon spray hole in the light hydrocarbon spray head to the aperture of a single heavy hydrocarbon outer spray hole in the heavy hydrocarbon outer spray head is 0.1: 1-2.0: 1.
3. The method of claim 1, wherein the ratio of the inner diameter of the riser reactor of the expanded diameter light hydrocarbon reaction zone I to the inner diameter of the riser reactor of the heavy hydrocarbon reaction zone is 1.1:1 to 3: 1.
4. The method of claim 1, wherein the expanded light hydrocarbon reaction zone I, the heavy hydrocarbon reaction zone and the light hydrocarbon reaction zone II respectively have heights which account for 1-15%, 1-40% and 1-60% of the total height of the riser reactor.
5. The method according to claim 1, wherein the pre-lifting medium is selected from one or a mixture of two or more of nitrogen, helium, catalytic cracking dry gas and steam.
6. The method of claim 1, wherein the light hydrocarbon in the expanded diameter light hydrocarbon reaction zone I is a distillate oil having a boiling point range of 140 to 320 ℃, a sulfur content of 0.03 to 0.27 wt%, and a cetane number of 55 to 65.
7. The method of claim 1 or 6, wherein the light hydrocarbon is selected from one or more of normal vacuum equipment straight-run diesel oil, vacuum diesel oil, hydrogenated diesel oil, residual hydrogenated diesel oil, coked diesel oil, catalytic diesel oil and catalytic cracking equipment light/heavy cycle oil.
8. The process of claim 1, wherein the heavy hydrocarbons of the heavy hydrocarbon reaction zone are at least one selected from the group consisting of atmospheric gas oil, vacuum residue, atmospheric residue, low grade diesel, coal tar, residue hydrogenation tail oil, solvent deasphalted oil, raffinate oil, coker wax oil, shale oil, oil sand bitumen, and heavy crude oil.
9. The method of claim 1, wherein the oil solution contact temperature of the expanded light hydrocarbon reaction zone I is 450 to 710 ℃; the reaction pressure is normal pressure to 320 kilopascal; the retention time is 0.05-3 s; the catalyst-light hydrocarbon solvent-oil ratio is 5: 1-160: 1; the mass ratio of the light hydrocarbon to the heavy hydrocarbon is 0.001: 1-0.55: 1; the temperature of the regenerated catalyst is 570-755 ℃.
10. The method of claim 9, wherein the oil solution contact temperature of the expanded light hydrocarbon reaction zone I is 590-650 ℃; the reaction pressure is 100-270 kPa; the retention time is 0.1-0.7 s; the catalyst-light hydrocarbon solvent-oil ratio is 15: 1-130: 1; the mass ratio of the light hydrocarbon to the heavy hydrocarbon is 0.05: 1-0.15: 1; the temperature of the regenerated catalyst is 630-720 ℃.
11. The method of claim 1, wherein the oil solution contact temperature in the heavy hydrocarbon reaction zone is 450-640 ℃; the catalyst and the raw material in the reaction zone have a catalyst-to-oil ratio of 5: 1-25: 1; the residence time of oil gas molecules is 0.05-2.5 s; the reaction pressure is from normal pressure to 320 kPa.
12. The method of claim 11, wherein the oil solution contact temperature in the heavy hydrocarbon reaction zone is 500-600 ℃; the catalyst-to-oil ratio of the catalyst to the raw materials in the reaction zone is 6: 1-18: 1; the residence time of oil gas molecules is 0.5-1.5 s; the reaction pressure is 100-270 kPa.
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| CN205532544U (en) * | 2016-02-04 | 2016-08-31 | 陕西贝克工贸有限公司 | Oil gas well integral type nozzle |
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| CN103897723A (en) * | 2004-12-23 | 2014-07-02 | Abb拉默斯环球有限公司 | Processing of different feeds in a fluid catalytic cracking unit |
| CN102746880A (en) * | 2011-04-20 | 2012-10-24 | 中国石油化工股份有限公司 | Method for preparing gasoline, diesel oil, ethylene and propylene through coupled catalytic cracking of light hydrocarbons and heavy oil |
| US9353316B2 (en) * | 2011-06-15 | 2016-05-31 | Baozhen Shi | Method and device for catalytic cracking |
| CN205532544U (en) * | 2016-02-04 | 2016-08-31 | 陕西贝克工贸有限公司 | Oil gas well integral type nozzle |
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