CN110551526A - Processing method of catalytic cracking light cycle oil - Google Patents
Processing method of catalytic cracking light cycle oil Download PDFInfo
- Publication number
- CN110551526A CN110551526A CN201810541365.3A CN201810541365A CN110551526A CN 110551526 A CN110551526 A CN 110551526A CN 201810541365 A CN201810541365 A CN 201810541365A CN 110551526 A CN110551526 A CN 110551526A
- Authority
- CN
- China
- Prior art keywords
- catalytic cracking
- light cycle
- cycle oil
- hydrogen
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
-
- 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
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 processing method of catalytic cracking light cycle oil, which comprises the following steps: (1) contacting the catalytic cracking light cycle oil with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil; (2) feeding the obtained hydrogenated light cycle oil and hydrogen-containing gas into a catalytic cracking reactor to contact with a catalytic cracking catalyst and perform catalytic cracking reaction to obtain a reaction product and a spent catalyst; (3) feeding the obtained spent catalyst into a regenerator for regeneration, and feeding the obtained regenerated catalyst serving as the catalytic cracking catalyst into a catalytic cracking reactor; (4) and separating the obtained reaction product to obtain a dry gas product, a liquefied gas product, a gasoline product, a light cycle oil product and a heavy oil product. The processing method of the invention has the advantages of high yield of the gasoline rich in aromatic hydrocarbon, low raw coke and good utilization rate of raw materials.
Description
Technical Field
The invention relates to a processing method of catalytic cracking light cycle oil.
Background
With the adjustment of economic structure of China, the diesel-gasoline ratio of market consumption is reduced year by year, and the increase of diesel consumption speed lower than that of gasoline consumption speed becomes a normal state. The catalytic cracking diesel oil (also called light cycle oil) is an important byproduct of a catalytic cracking device, is large in quantity, is rich in aromatic hydrocarbon, particularly polycyclic aromatic hydrocarbon, and belongs to poor diesel oil fraction. While the quality standard of the national automotive fuel oil is continuously improved, the national V diesel oil quality standard implemented in 1 month in 2017 requires that the polycyclic aromatic hydrocarbon content in the automotive diesel oil is not more than 11%, so that the catalytic cracking light cycle oil is difficult to meet the increasingly strict diesel oil specification even after being subjected to hydrofining or hydro-upgrading. On the other hand, aromatic hydrocarbons, especially light aromatic hydrocarbons including benzene, toluene, xylene and ethylbenzene, are important petrochemical raw materials, the added value of products is high, but the domestic aromatic production raw materials are in short supply for a long time. Therefore, the catalytic conversion of the poor-quality catalytic cracking light cycle oil to produce the gasoline rich in aromatic hydrocarbon has good market application prospect.
US patent US4585545 discloses a catalytic conversion method for producing gasoline rich in monocyclic aromatic hydrocarbons by carrying out hydrotreating on a catalytic cracking light cycle oil whole fraction to obtain hydrogenated diesel oil and then carrying out catalytic cracking.
Chinese patent CN1466619A discloses a conversion method of catalytic cracking light cycle oil, which is to divide a catalytic cracking riser reactor into an upper reaction zone and a lower reaction zone, inject heavy oil into the lower reaction zone, inject hydrogenated cycle oil obtained by hydrotreating the catalytic cracking product light cycle oil into the upper reaction zone, and then crack the hydrogenated cycle oil to generate light olefins and naphtha.
Chinese patent CN104560185A discloses a catalytic conversion method for producing gasoline rich in aromatic compounds, wherein catalytic cracking light cycle oil is first cut to obtain light fraction and heavy fraction, wherein the heavy fraction is hydrotreated to obtain hydrogenated heavy fraction, and the light fraction and the hydrogenated heavy fraction are separately layered through different nozzles and enter a catalytic cracking device to produce catalytic gasoline rich in benzene, toluene and xylene.
Chinese patent CN104560187A discloses a catalytic conversion method for producing gasoline rich in aromatic hydrocarbons, wherein catalytic cracking light cycle oil is first cut to obtain light fraction and heavy fraction, wherein the heavy fraction is hydrogenated to obtain hydrogenated heavy fraction, and the light fraction and the hydrogenated heavy fraction are separately and respectively fed into different riser reactors of a catalytic cracking device, thereby producing catalytic gasoline rich in benzene, toluene and xylene.
From the above published literature, it can be found that the prior art is to hydrotreat the catalytic cracked light cycle oil whole fraction or heavy fraction and then catalytically crack the whole fraction or heavy fraction to produce gasoline rich in aromatic hydrocarbons.
Disclosure of Invention
The invention aims to provide a processing method of catalytic cracking light cycle oil, which has the advantages of high yield of gasoline rich in aromatic hydrocarbon, low green coke and good utilization rate of raw materials.
in order to achieve the above object, the present invention provides a method for processing a catalytically cracked light cycle oil, comprising:
(1) Contacting the catalytic cracking light cycle oil with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil;
(2) Feeding the obtained hydrogenated light cycle oil and hydrogen-containing gas into a catalytic cracking reactor to contact with a catalytic cracking catalyst and perform catalytic cracking reaction to obtain a reaction product and a spent catalyst;
(3) Feeding the obtained spent catalyst into a regenerator for regeneration, and feeding the obtained regenerated catalyst serving as the catalytic cracking catalyst into a catalytic cracking reactor;
(4) And separating the obtained reaction product to obtain a dry gas product, a liquefied gas product, a gasoline product, a light cycle oil product and a heavy oil product.
Optionally, the aromatic content of the catalytic cracking light cycle oil is not less than 30 wt%.
optionally, the aromatic content of the catalytic cracking light cycle oil is not less than 50 wt%.
Optionally, the hydrotreating conditions include hydrogen partial pressure of 5.0-10.0 MPa, reaction temperature of 300-450 deg.c, volume space velocity of 1.0-10.0 hr -1, and hydrogen-oil volume ratio of 400-1600 standard cubic meter/cubic meter.
Optionally, the hydrotreating catalyst includes a carrier and an active metal component loaded on the carrier, where the carrier is at least one selected from amorphous silicon-aluminum, aluminum oxide and silicon dioxide, the active metal component is a group VIB metal and/or a group VIII non-noble metal, the group VIB metal is molybdenum and/or tungsten, and the group VIII non-noble metal is nickel and/or cobalt.
Optionally, the initial boiling point of the hydrogenated light cycle oil is greater than 150 ℃.
Optionally, the initial boiling point of the hydrogenated light cycle oil is greater than 200 ℃.
Optionally, the hydrogen-containing gas is at least one selected from hydrogen, catalytic cracking dry gas, hydrogenation low-molecular gas, hydrogenation dry gas and reforming hydrogen.
Optionally, the hydrogen content of the hydrogen-containing gas is greater than 10% by volume.
Optionally, the hydrogen content of the hydrogen-containing gas is greater than 20% by volume.
Optionally, the method further includes: at least part of the light cycle oil product obtained in the step (4) is used as the catalytic cracking light cycle oil to be subjected to the hydrotreatment in the step (1); and/or
Returning at least part of the dry gas product obtained in the step (4) as the hydrogen-containing gas to the step (2) for catalytic cracking reaction.
Optionally, according to the flow direction of the reaction material, the hydrogen-containing gas and the hydrogenated light cycle oil are injected into the catalytic cracking reactor together or the hydrogen-containing gas is injected into the catalytic cracking reactor at the downstream of the hydrogenated light cycle oil.
Optionally, the weight ratio of hydrogen in the hydrogen-containing gas to the hydrogenated light cycle oil is 0.01 to 15 wt% based on the weight of the hydrogenated light cycle oil.
Optionally, the weight ratio of hydrogen in the hydrogen-containing gas to the hydrogenated light cycle oil is 0.1 to 5 wt% based on the weight of the hydrogenated light cycle oil.
Optionally, the catalytic cracking reactor is at least one selected from a riser reactor, a fluidized bed reactor and a moving bed reactor.
Optionally, the conditions of the catalytic cracking reaction include: the reaction temperature is 500-680 ℃, the weight ratio of the catalytic cracking catalyst to the hydrogenated light cycle oil is 2-100, the oil gas retention time is 0.2-20 seconds, and the weight ratio of the water vapor to the hydrogenated light cycle oil is 0.01-0.6.
Optionally, the conditions of the catalytic cracking reaction include: the reaction temperature is 540-650 ℃, the weight ratio of the catalytic cracking catalyst to the hydrogenated light cycle oil is 5-50, the oil gas retention time is 0.5-10 seconds, and the weight ratio of the water vapor to the hydrogenated light cycle oil is 0.05-0.3.
optionally, the catalytic cracking catalyst comprises 1-50 wt% of zeolite, 5-99 wt% of inorganic oxide and 0-70 wt% of clay based on the dry weight of the catalytic cracking catalyst, wherein the zeolite is at least one selected from the group consisting of rare earth-containing or non-containing Y zeolite, rare earth-containing or non-containing HY zeolite, rare earth-containing or non-containing USY zeolite, rare earth-containing or non-containing ZSM-5 zeolite, rare earth-containing or non-containing ZRP zeolite and rare earth-containing or non-containing Beta zeolite.
The invention has the advantages that:
1. The yield of the catalytic gasoline rich in benzene, toluene and xylene can be obviously improved by means of injecting hydrogen-containing gas into the reactor.
2. The method of the invention can reduce coke formation and improve product distribution, thereby being beneficial to improving the utilization rate of raw materials.
3. The method can be implemented by slightly modifying the prior device, and the yield of the benzene, the toluene and the xylene with high added values can be obviously improved in a cheap mode.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:
FIG. 1 is a schematic flow diagram of one embodiment of the process of the present invention.
Description of the reference numerals
1 pipeline 2 pipeline 3 hydrotreater
4 line 5 feed nozzle 6 line
7 catalytic cracker 8 line 9 line
10 line 11 line
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
the invention provides a processing method of catalytic cracking light cycle oil, which comprises the following steps: (1) contacting the catalytic cracking light cycle oil with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil; (2) feeding the obtained hydrogenated light cycle oil and hydrogen-containing gas into a catalytic cracking reactor to contact with a catalytic cracking catalyst and perform catalytic cracking reaction to obtain a reaction product and a spent catalyst; (3) feeding the obtained spent catalyst into a regenerator for regeneration, and feeding the obtained regenerated catalyst serving as the catalytic cracking catalyst into a catalytic cracking reactor; (4) and separating the obtained reaction product to obtain a dry gas product, a liquefied gas product, a gasoline product, a light cycle oil product and a heavy oil product. The inventor finds out through experimental research that the hydrogenation light cycle oil catalytic cracking reaction can obtain higher yields of benzene, toluene and xylene and lower yield of coke under a hydrogen atmosphere. The method can obviously improve the yield of the gasoline rich in aromatic hydrocarbon by injecting the hydrogen-containing gas into the catalytic cracking reactor, and can also reduce coke formation, obviously improve the product distribution and improve the utilization rate of the raw materials.
according to the present invention, the catalytically cracked light cycle oil is one of the catalytically cracked products, and has a relatively high aromatic content, for example, the aromatic content of the catalytically cracked light cycle oil is not less than 30% by weight, preferably not less than 50% by weight.
-1In order to increase the aromatic content of the gasoline product, the hydrotreating preferably controls the polycyclic aromatic saturation in the catalytically cracked light cycle oil and avoids monocyclic aromatic saturation as much as possible, and the hydrotreating conditions may include hydrogen partial pressure of 5.0-10.0 MPa, reaction temperature of 300-.
According to the invention, the initial boiling point of the hydrogenated light cycle oil may be greater than 150 ℃, preferably greater than 200 ℃.
According to the present invention, the hydrogen-containing gas refers to a hydrogen-containing gas, which may have various sources, for example, the hydrogen-containing gas may be at least one selected from hydrogen, catalytic cracking dry gas, hydrogenation low-molecular gas, hydrogenation dry gas and reforming hydrogen, and the content of hydrogen in the hydrogen-containing gas may be more than 10% by volume, preferably more than 20% by volume. The hydrogen-rich gas may be used in a single pass or may be partially or fully recycled after separation from the reaction product.
According to the invention, the catalytic cracking light cycle oil and the hydrogen-containing gas can be produced by the method, and can also be produced by light cycle oil produced by an external catalytic cracking unit or hydrogen-containing gas produced by other units, and preferably, the method further comprises the following steps: at least part of the light cycle oil product obtained in the step (3) is used as catalytic cracking light cycle oil to be subjected to the hydrotreatment in the step (1); and/or returning at least part of the dry gas product obtained in the step (4) as hydrogen-containing gas to the step (2) for catalytic cracking reaction.
According to the present invention, the hydrogenated light cycle oil and the hydrogen-containing gas may be introduced into the catalytic cracking reactor in various manners and in various proportions, for example, the hydrogen-containing gas is injected into the catalytic cracking reactor together with the hydrogenated light cycle oil or the hydrogen-containing gas is injected into the catalytic cracking reactor downstream of the hydrogenated light cycle oil, in terms of the flow direction of the reaction material. The weight ratio of hydrogen to the hydrogenated light cycle oil in the hydrogen-containing gas is 0.01 to 15 wt%, preferably 0.1 to 5 wt%, and more preferably 0.2 to 2 wt%, based on the weight of the hydrogenated light cycle oil.
According to the present invention, the catalytic cracking reactor is well known to those skilled in the art, and for example, the catalytic cracking reactor may be at least one selected from a riser reactor, a fluidized bed reactor, and a moving bed reactor.
Catalytic cracking reactions according to the present invention are well known to those skilled in the art, for example, the conditions of the catalytic cracking reaction may include: the reaction temperature is 500-680 ℃, preferably 540-650 ℃, the weight ratio of the catalytic cracking catalyst to the hydrogenated light cycle oil is 2-100, preferably 5-50, the oil gas residence time is 0.2-20 seconds, preferably 0.5-10, and the weight ratio of the steam to the hydrogenated light cycle oil is 0.01-0.6, preferably 0.05-0.3.
The catalytic cracking catalyst according to the present invention is well known to those skilled in the art, and for example, may comprise, as an active component, 1 to 50% by weight of zeolite, which may be at least one selected from the group consisting of rare earth-containing or non-containing Y zeolite, rare earth-containing or non-containing HY zeolite, rare earth-containing or non-containing USY zeolite, rare earth-containing or non-containing ZSM-5 zeolite, rare earth-containing or non-containing ZRP zeolite, and rare earth-containing or non-containing Beta zeolite, 5 to 99% by weight of an inorganic oxide, and 0 to 70% by weight of clay, based on the dry weight of the catalytic cracking catalyst.
The best mode for carrying out the invention will be further described with reference to the accompanying drawings.
The catalytic cracking light cycle oil enters a hydrotreater 3 through a pipeline 1, and hydrogen is simultaneously introduced into the hydrotreater 3 through a pipeline 2. The hydrogenated product enters a catalytic cracking device 7 through a pipeline 4 and a feed nozzle 5, hydrogen-containing gas is injected into the catalytic cracking device 7 through a pipeline 6, catalytic cracking reaction is carried out in the presence of a catalytic cracking catalyst, the catalytic gasoline rich in aromatic hydrocarbon obtained by separating reaction products is led out through a pipeline 8, and light cycle oil which is the other catalytic cracking reaction product is led out through a pipeline 9 and enters a hydrotreating device 3 for circulation through a pipeline 10, a pipeline 11 and a pipeline 1. For simplicity, the outlet lines for other catalytic cracking reaction products, such as dry gas, liquefied gas, oil slurry, etc., are not shown in the figure.
The following examples further illustrate the process but are not intended to limit it.
In the examples and comparative examples, the hydrotreating reactor was a medium-sized fixed bed reactor, in which a hydrotreating catalyst having a commercial designation of RN-32V and a protectant having a commercial designation of RG-1 were loaded, and the loading volume ratio of the hydrotreating catalyst to the protectant was 95:5, which were all produced by China petrochemical catalyst division.
the physicochemical properties of the catalysts used in the catalytic cracking units of the examples and comparative examples are shown in Table 1, which is commercially available under the designation MLC-500, manufactured by China petrochemical catalyst division.
The properties of the feedstock (catalytic cracking light cycle oil) used in the examples and comparative examples are shown in table 2.
Example 1
This example illustrates the use of the method provided by the present invention.
The catalytic cracking light cycle oil enters a hydrotreating reactor for hydrotreating, wherein the hydrotreating conditions are that the hydrogen partial pressure is 8.0 MPa, the average bed reaction temperature is 350 ℃, the volume space velocity is 1.0 hour -1, the hydrogen-oil volume ratio is 800 standard cubic meters per cubic meter, and the hydrogenation light cycle oil with the initial boiling point of 155 ℃ is obtained by separating reaction oil gas.
The hydrogenated light cycle oil and the hydrogen-rich hydrogenated dry gas (the hydrogen content is 58.62 percent by volume) are heated to about 350 ℃ by a preheating furnace, and then enter a riser reactor of the medium-sized catalytic cracking unit from the bottom through a feed nozzle to contact with a hot regenerated catalyst for catalytic cracking reaction, and the main operating conditions and the product distribution of the medium-sized catalytic cracking unit are respectively listed in tables 3 and 4.
Comparative example
The same as example 1 except that: and no dry hydrogen gas is injected into the reactor during the reaction process. The main operating conditions and the product distribution after reaction of the catalytic cracking mesoscale unit are shown in tables 3 and 4, respectively.
Example 2
The same as example 1 except that: hydrogen with a purity of 99.99 percent by volume is used to replace hydrogenated dry gas and is injected into the reactor. The main operating conditions and the product distribution after reaction of the catalytic cracking mesoscale unit are shown in tables 3 and 4, respectively.
As can be seen from the comparative examples 1-2 and comparative example in Table 4, on the basis of the existing technology of producing the gasoline rich in aromatic hydrocarbon by catalytic cracking of hydrogenated light cycle oil, the method provided by the invention can obviously improve the yield and the product distribution of the gasoline rich in aromatic hydrocarbon; compared with the comparative example which does not inject hydrogen-rich gas under the same reaction conditions, the gasoline yield of the example 1 is increased by 6.6 percentage points, the weight fractions of benzene, toluene and xylene in the gasoline are also obviously increased, and the weight yield of benzene, toluene and xylene is increased from 14.32 percent to 24.83 percent and is increased by 10.51 percentage points. Compared with the comparative example which does not inject hydrogen-rich gas under the same reaction conditions, the gasoline yield of the example 2 is increased by 10.9 percentage points, the weight fractions of benzene, toluene and xylene in the gasoline are also obviously increased, and the weight yield of benzene, toluene and xylene is increased from 14.32 percent to 29.38 percent and is increased by 15.06 percentage points.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the content of the present invention as long as it does not depart from the gist of the present invention.
TABLE 1
| Catalyst numbering | MLC-500 |
| Chemical composition, weight% | |
| Al2O3 | 56.3 |
| SiO2 | 37.5 |
| RE2O3 | 3.5 |
| P2O5 | 0.36 |
| Specific surface area, rice2Per gram | 147 |
| Pore volume, ml/g | 0.195 |
| Particle size distribution,% (volume/volume) | |
| 0-40 micron | 20.1 |
| 0-40 micron | 63.9 |
| 0-40 micron | 95.9 |
| Average particle diameter, micron | 67.4 |
| Micro-inverse activity, weight% | 68 |
TABLE 2
| Raw oil name | Catalytic cracking light cycle oil |
| Density (20 deg.C), kg/m3 | 948.8 |
| 10% of carbon residue, by weight% | 0.37 |
| Freezing point, DEG C | -24 |
| Aniline point, deg.C | <30 |
| Average molecular weight | 187 |
| Distillation range, deg.C | |
| Initial boiling point | 190 |
| 10% by volume | 213 |
| 30% by volume | 222 |
| 50% by volume | 247 |
| 70% by volume | 272 |
| 90% by volume | 348 |
| 95% by volume | 363 |
| End point of distillation | 369 |
| Mass Spectrometry composition by weight% | |
| Alkane hydrocarbons | 10.7 |
| Total cycloalkanes | 4.6 |
| Total aromatic hydrocarbons | 84.7 |
| Monocyclic aromatic hydrocarbon | 31.7 |
| Bicyclic aromatic hydrocarbons | 45.0 |
| Total weight of | 100.0 |
TABLE 3
| Example 1 | Example 2 | Comparative example | |
| Operating parameters | |||
| Reaction temperature of | 580 | 580 | 580 |
| Balancing catalyst activity | 68 | 68 | 68 |
| Weight ratio of solvent to oil | 10 | 10 | 10 |
| Oil gas retention time in seconds | 2.5 | 2.5 | 2.5 |
| Weight ratio of water vapor to hydrogenated light cycle oil | 0.10 | 0.10 | 0.10 |
| The proportion of hydrogen to the hydrogenated light cycle oil is weight percent | 0.5 | 1.0 | - |
TABLE 4
| Example 1 | Example 2 | Comparative example | |
| Product distribution, weight% | |||
| Dry gas | 2.6 | 2.4 | 2.8 |
| Liquefied gas | 14.7 | 13.6 | 14.9 |
| Gasoline (gasoline) | 50.9 | 55.2 | 44.3 |
| Benzene + toluene + xylene | 24.83 | 29.38 | 14.32 |
| Light cycle oil | 26.8 | 24.8 | 31.2 |
| Heavy oil | 1.9 | 1.8 | 2.3 |
| Coke | 3.1 | 2.2 | 4.5 |
| Total up to | 100 | 100 | 100 |
| The aromatic hydrocarbon composition in the gasoline is weight percent | |||
| Benzene and its derivatives | 3.67 | 4.1 | 2.74 |
| Toluene | 18.79 | 20.09 | 12.75 |
| Xylene | 26.33 | 29.04 | 16.83 |
Claims (18)
1. A process for processing a catalytically cracked light cycle oil, the process comprising:
(1) Contacting the catalytic cracking light cycle oil with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil;
(2) Feeding the obtained hydrogenated light cycle oil and hydrogen-containing gas into a catalytic cracking reactor to contact with a catalytic cracking catalyst and perform catalytic cracking reaction to obtain a reaction product and a spent catalyst;
(3) Feeding the obtained spent catalyst into a regenerator for regeneration, and feeding the obtained regenerated catalyst serving as the catalytic cracking catalyst into a catalytic cracking reactor;
(4) And separating the obtained reaction product to obtain a dry gas product, a liquefied gas product, a gasoline product, a light cycle oil product and a heavy oil product.
2. The process of claim 1, wherein the catalytically cracked light cycle oil has an aromatics content of not less than 30 wt.%.
3. The process of claim 1, wherein the catalytically cracked light cycle oil has an aromatics content of not less than 50 wt.%.
4. The method as claimed in claim 1, wherein the hydrotreating conditions include a hydrogen partial pressure of 5.0-10.0 MPa, a reaction temperature of 300-450 ℃, a volume space velocity of 1.0-10.0 hours -1, and a hydrogen-oil volume ratio of 400-1600 normal cubic meters/cubic meter.
5. The process of claim 1, wherein the hydrotreating catalyst comprises a support and an active metal component supported on the support, the support being at least one selected from amorphous silica-alumina, alumina and silica, the active metal component being a group VIB metal and/or a group VIII non-noble metal, the group VIB metal being molybdenum and/or tungsten, the group VIII non-noble metal being nickel and/or cobalt.
6. The process of claim 1, wherein the hydrogenated light cycle oil has a first boiling point greater than 150 ℃.
7. The process of claim 1, wherein the hydrogenated light cycle oil has a first boiling point greater than 200 ℃.
8. The method according to claim 1, wherein the hydrogen-containing gas is at least one selected from the group consisting of hydrogen, catalytic cracking dry gas, hydrogenation low-molecular gas, hydrogenation dry gas, and reforming hydrogen.
9. The method of claim 1, wherein the hydrogen-containing gas has a hydrogen content greater than 10% by volume.
10. The method of claim 1, wherein the hydrogen-containing gas has a hydrogen content greater than 20% by volume.
11. The method of claim 1, further comprising: at least part of the light cycle oil product obtained in the step (4) is used as the catalytic cracking light cycle oil to be subjected to the hydrotreatment in the step (1); and/or
Returning at least part of the dry gas product obtained in the step (4) as the hydrogen-containing gas to the step (2) for catalytic cracking reaction.
12. The method of claim 1, wherein the hydrogen-containing gas is injected into the catalytic cracking reactor with or downstream of the hydrogenated light cycle oil, in terms of the flow direction of the reaction mass.
13. The process of claim 1, wherein the weight ratio of hydrogen to hydrogenated light cycle oil in the hydrogen-containing gas is from 0.01 to 15 wt%, based on the weight of the hydrogenated light cycle oil.
14. The process of claim 1, wherein the weight ratio of hydrogen to hydrogenated light cycle oil in the hydrogen-containing gas is from 0.1 to 5 wt%, based on the weight of the hydrogenated light cycle oil.
15. The process of claim 1, wherein the catalytic cracking reactor is at least one selected from the group consisting of a riser reactor, a fluidized bed reactor, and a moving bed reactor.
16. The process of claim 1, wherein the conditions of the catalytic cracking reaction comprise: the reaction temperature is 500-680 ℃, the weight ratio of the catalytic cracking catalyst to the hydrogenated light cycle oil is 2-100, the oil gas retention time is 0.2-20 seconds, and the weight ratio of the water vapor to the hydrogenated light cycle oil is 0.01-0.6.
17. The process of claim 1, wherein the conditions of the catalytic cracking reaction comprise: the reaction temperature is 540-650 ℃, the weight ratio of the catalytic cracking catalyst to the hydrogenated light cycle oil is 5-50, the oil gas retention time is 0.5-10 seconds, and the weight ratio of the water vapor to the hydrogenated light cycle oil is 0.05-0.3.
18. The process of claim 1 wherein the catalytic cracking catalyst comprises from 1 to 50 wt% of a zeolite, at least one selected from the group consisting of rare earth-containing or non-containing Y zeolite, rare earth-containing or non-containing HY zeolite, rare earth-containing or non-containing USY zeolite, rare earth-containing or non-containing ZSM-5 zeolite, rare earth-containing or non-containing ZRP zeolite, and rare earth-containing or non-containing Beta zeolite, from 5 to 99 wt% of an inorganic oxide, and from 0 to 70 wt% of a clay, based on the dry weight of the catalytic cracking catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810541365.3A CN110551526B (en) | 2018-05-30 | 2018-05-30 | Processing method of catalytic cracking light cycle oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810541365.3A CN110551526B (en) | 2018-05-30 | 2018-05-30 | Processing method of catalytic cracking light cycle oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110551526A true CN110551526A (en) | 2019-12-10 |
| CN110551526B CN110551526B (en) | 2021-08-06 |
Family
ID=68734152
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810541365.3A Active CN110551526B (en) | 2018-05-30 | 2018-05-30 | Processing method of catalytic cracking light cycle oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110551526B (en) |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962570A (en) * | 2010-10-22 | 2011-02-02 | 孙雪 | Method for producing high-octane gasoline by hydrocracking distillate oil of low-grade petroleum |
| CN101987971A (en) * | 2009-08-06 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Method for producing high-octane petrol by inferior diesel |
| CN102311795A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Hydrogenation method for producing high-octane gasoline components by diesel oil raw material |
| CN103184073A (en) * | 2011-12-31 | 2013-07-03 | 中国石油化工股份有限公司 | Hydrocracking method for producing gasoline blending component with high octane value |
| CN104560166A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method utilizing petroleum hydrocarbon to produce high-octane gasoline |
| CN104560184A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method of maximizing gasoline |
| CN104560167A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method of hydrocarbon oil |
| CN104560185A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method for producing gasoline containing rich aromatic compounds |
| CN104560186A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method capable of realizing maximum gasoline production |
-
2018
- 2018-05-30 CN CN201810541365.3A patent/CN110551526B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101987971A (en) * | 2009-08-06 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Method for producing high-octane petrol by inferior diesel |
| CN102311795A (en) * | 2010-06-29 | 2012-01-11 | 中国石油化工股份有限公司 | Hydrogenation method for producing high-octane gasoline components by diesel oil raw material |
| CN101962570A (en) * | 2010-10-22 | 2011-02-02 | 孙雪 | Method for producing high-octane gasoline by hydrocracking distillate oil of low-grade petroleum |
| CN103184073A (en) * | 2011-12-31 | 2013-07-03 | 中国石油化工股份有限公司 | Hydrocracking method for producing gasoline blending component with high octane value |
| CN104560166A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method utilizing petroleum hydrocarbon to produce high-octane gasoline |
| CN104560184A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method of maximizing gasoline |
| CN104560167A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method of hydrocarbon oil |
| CN104560185A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method for producing gasoline containing rich aromatic compounds |
| CN104560186A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Catalytic conversion method capable of realizing maximum gasoline production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110551526B (en) | 2021-08-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101519603B (en) | Method for hydrotreating high-sulfur and high-metal residual oil | |
| EP3460027B1 (en) | Catalytic cracking process with increased production of a gasoline having a low olefin content and a high octane number | |
| TWI810212B (en) | Method for producing high-octane catalytic cracking gasoline | |
| CN109554193B (en) | Catalytic cracking method for increasing production of low-olefin and high-octane gasoline | |
| CN103059998B (en) | Combined process for treating residual oil | |
| CN111718754A (en) | Method and system for producing gasoline and propylene | |
| CN101942339B (en) | Boiling-bed residual-oil hydrocracking and catalytic-cracking combined process method | |
| CN102041093B (en) | Catalytic conversion method for improving cetane number and yield of diesel | |
| CN110551526B (en) | Processing method of catalytic cracking light cycle oil | |
| CN110551527B (en) | Method for producing gasoline rich in aromatic hydrocarbon | |
| CN109554195B (en) | Catalytic cracking method for reducing diesel-steam ratio | |
| CN109705914B (en) | Method and system for catalytic cracking by adopting double lifting pipes | |
| CN109694741B (en) | Method for producing clean gasoline from Fischer-Tropsch synthetic wax | |
| CN102373085B (en) | Catalytic conversion method for maximum production of high-cetane diesel oil | |
| CN116622406B (en) | Process for producing olefin and aromatic hydrocarbon by catalytic cracking gasoline | |
| CN103059993A (en) | Catalytic conversion method of petroleum hydrocarbon | |
| CN114686252B (en) | Method for preparing chemicals from crude oil | |
| CN113355132B (en) | Method for catalytic cracking of hydrogenated oil | |
| CN113817502B (en) | Integrated process for maximizing production of chemicals | |
| CN115261068B (en) | Fixed bed residuum hydrogenation method | |
| CN109694743B (en) | Method for producing clean gasoline by taking Fischer-Tropsch synthetic wax as raw material | |
| CN111100710B (en) | Catalytic cracking method and system | |
| CN117903846A (en) | Coking gasoline and diesel oil hydrogenation method | |
| CN102041094B (en) | Prolific catalytic converting method for high-cetane diesel oil | |
| CN107557069B (en) | Method and system for hydro-conversion of coal tar raw material |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |