CN109705912B - Production method of high-octane gasoline - Google Patents
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Abstract
The invention relates to a production method of high-octane gasoline, which comprises the following steps: spraying a heavy raw material into the riser reactor from a first nozzle, contacting with a first catalytic cracking catalyst from the bottom of the riser reactor and a second catalytic cracking catalyst from the middle of the riser reactor, and carrying out catalytic cracking reaction to obtain a reaction product and a spent catalyst; separating the obtained reaction products to at least obtain catalytic cracking gasoline and catalytic cracking light cycle oil; feeding the catalytic cracking light cycle oil into a hydrogenation reactor to contact with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil; and (3) sending the hydrogenated light cycle oil into the riser reactor from a second nozzle to perform the catalytic cracking reaction. The method of the invention feeds the hydrogenated light cycle oil and the heavy raw material from different positions, and can supplement the catalyst and produce the gasoline with high octane number to the maximum extent.
Description
Technical Field
The invention relates to a production method of high-octane gasoline.
Background
With the development of crude oil heaviness and the rapid increase of the market demand for light oil products, the catalytic cracking technology for heavy oil heaviness is rapidly developed in China. However, one must face the fact that catalytically cracked diesel (or light cycle oil) has been relatively poor in quality, high in density, high in aromatics content, low in cetane number, and even by diesel hydro-upgrading technology, it has been difficult to meet increasingly stringent diesel specifications. How to solve the problem of catalytic cracking of light cycle oil is a serious problem. Meanwhile, another problem exists in that domestic finished gasoline is in short supply for a long time, and catalytic cracking gasoline accounts for 80 percent of the finished gasoline. Therefore, how to achieve maximum production of high octane gasoline from heavy feedstock without producing light cycle oil by catalytic cracking process may be a new way to solve the above problems.
US patent US4585545 discloses a catalytic conversion method for producing gasoline rich in monocyclic aromatic hydrocarbons by hydrotreating a whole fraction of catalytically cracked light cycle oil to obtain hydrogenated diesel oil and then catalytically cracking the hydrogenated diesel oil.
Chinese patent CN14232327A discloses a method for modifying catalytic cracking cycle oil, which is to deeply hydrogenate light cycle oil produced by a first catalytic cracking unit using heavy oil as a raw material, and then to subject the obtained hydrogenated cycle oil to a second catalytic cracking unit. On the basis of this process, chinese patent CN423689A emphasizes that the catalyst in the second catalytic cracking unit requires 50-95% shape selective zeolite and 5-50% large pore zeolite with a pore size greater than or equal to about 0.7nm to selectively increase the light olefin yield.
Chinese patent CN1466619A discloses a conversion method of catalytic cracking light cycle oil, which is to divide a catalytic cracking riser reactor into an upstream reaction zone and a downstream reaction zone, wherein heavy oil is injected into the downstream reaction zone, and hydrogenated cycle oil obtained by hydrotreating the catalytic cracking product light cycle oil is injected into the upstream reaction zone. On the basis of the method, the feed of the downstream zone in the method of the Chinese patent CN1425054A is added with naphtha besides the hydrogenated cycle oil. However, in the method, not only is the hydrogen consumption high, but also the hydrogenation cycle oil reacts in an upstream area to seriously affect the conversion of heavy oil in the downstream area.
From the above published literature, it can be found that one of the important routes for processing catalytically cracked light cycle oil is to subject it to hydrotreating followed by catalytic cracking. It must be noted that the light cycle oil, whether hydrogenated or not, has a small molecular size and a large bond energy compared to the large molecules of the heavy oil, and therefore how to control the operating parameters of catalytic cracking is one of the keys in the light cycle oil processing. Meanwhile, if the light cycle oil is hydrogenated, the operation control of the hydrogenation process is also one of the keys of the light cycle oil processing. In addition, maximizing the production of high octane gasoline without producing light cycle oil during the catalytic cracking of heavy feedstocks, consideration must be given to achieving selective catalytic cracking of heavy feedstocks and light cycle oil.
Disclosure of Invention
The invention aims to provide a method for producing high-octane gasoline, which feeds hydrogenated light cycle oil and heavy raw materials from different positions, can supplement catalysts and furthest produce the high-octane gasoline.
In order to achieve the above object, the present invention provides a method for producing a high octane gasoline, comprising: spraying a heavy raw material into the riser reactor from a first nozzle, contacting with a first catalytic cracking catalyst from the bottom of the riser reactor and a second catalytic cracking catalyst from the middle of the riser reactor, and carrying out catalytic cracking reaction to obtain a reaction product and a spent catalyst; separating the obtained reaction products to at least obtain catalytic cracking gasoline and catalytic cracking light cycle oil; feeding the obtained spent catalyst into a regenerator for scorching regeneration to obtain a regenerated catalyst; feeding regenerated catalyst as the first catalytic cracking catalyst and the second catalytic cracking catalyst into the riser reactor; feeding the catalytic cracking light cycle oil into a hydrogenation reactor to contact with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil; and (3) sending the hydrogenated light cycle oil into the riser reactor from a second nozzle to perform the catalytic cracking reaction, wherein the second nozzle and the first nozzle are arranged at intervals in the height direction.
Optionally, the second nozzle is disposed above the first nozzle along the height direction, and the second catalytic cracking catalyst is fed into the riser reactor from a position above the second nozzle or between the first nozzle and the second nozzle.
Optionally, in the riser reactor between the first nozzle and the second nozzle, the residence time of the reaction oil gas is 0.05-2 seconds.
Optionally, the heavy feedstock is at least one selected from straight-run wax oil, coker wax oil, deasphalted oil, hydrofined oil, hydrocracked tail oil, vacuum residue and atmospheric residue.
Optionally, the conditions of the catalytic cracking reaction of the heavy feedstock include: the reaction temperature is 520-650 ℃, the absolute pressure is 0.15-0.4 MPa, the weight ratio of the total weight of the first catalytic cracking catalyst and the second catalytic cracking catalyst to the heavy raw material is 1-50, the oil gas retention time is 1-10 seconds, the weight ratio of the water vapor to the heavy raw material is 0.01-0.5, the micro-reaction activity of the regenerated catalyst is not lower than 60, and the micro-reaction activity is determined by a micro-reaction activity test method of an RIPP 92-90 catalytic cracking industrial equilibrium catalyst.
Optionally, the regenerated catalyst comprises 10-50 wt% zeolite, at least one selected from rare earth-containing or non-rare earth-containing Y, HY, USY and Beta zeolites, 5-90 wt% inorganic oxide and 0-70 wt% clay.
Optionally, the riser reactor is an equal-diameter riser reactor or a reducing riser reactor.
Optionally, the hydrotreating catalyst includes an active metal component and a carrier, the active metal component is a group VIB metal and/or a group VIII non-noble metal, and the carrier is at least one selected from alumina, silica, and amorphous silica-alumina.
Optionally, the active metal component is nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum.
Optionally, the hydrotreating conditions are: hydrogen partial pressure of 5.0-22.0 MPa, reaction temperature of 330-450 deg.c and volume space velocity of 0.1-10.0 hr-1Hydrogen to oil volume ratio of 100-2000Nm3/m3。
Optionally, the content of bicyclic aromatic hydrocarbons in the hydrogenated light cycle oil is not more than 20 wt%.
Optionally, the catalytic cracking reaction conditions of the hydrogenated light cycle oil include: the reaction temperature is 520-650 ℃, the absolute pressure is 0.15-0.4 MPa, the weight ratio of the total weight of the first catalytic cracking catalyst and the second catalytic cracking catalyst to the hydrogenated light cycle oil is 5-100, the oil gas residence time is 1-15 seconds, and the weight ratio of the water vapor to the hydrogenated light cycle oil is 0.01-0.3.
Optionally, in unit time, the circulating weight ratio of the first catalytic cracking catalyst to the second catalytic cracking catalyst is 1: (0.02-1).
The invention has the advantages that:
1. the catalytic cracking of heavy raw materials can be completely realized without producing light cycle oil.
2. The heavy raw material and the hydrogenated light cycle oil are respectively processed by adopting two layers of feeding at different positions of a riser reactor and supplementing regenerated catalysts, so that the operation conditions of the two raw materials are respectively optimized, the maximum conversion of the two raw materials is realized, and the catalytic cracking gasoline with high octane number is produced to the maximum extent.
3. The hydrogenated light cycle oil is injected at the downstream of the heavy raw material, so that the reaction time can be effectively shortened, and the yield of the high-octane gasoline is improved.
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 line 2 line 3 hydrogenation reactor
4 line 5 line 6 second nozzle
7 first nozzle 8 regeneration inclined tube 9 regeneration slide valve
10 regeneration inclined tube 11 regeneration slide valve 12 settler
13 regenerator 14 line 15 line
16 line 17 line 18 fractionation column
19 riser reactor I heavy feed reaction zone II hydrogenation light cycle oil reaction zone
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 production method of high-octane gasoline, which comprises the following steps: spraying a heavy raw material into the riser reactor from a first nozzle, contacting with a first catalytic cracking catalyst from the bottom of the riser reactor and a second catalytic cracking catalyst from the middle of the riser reactor, and carrying out catalytic cracking reaction to obtain a reaction product and a spent catalyst; separating the obtained reaction products to at least obtain catalytic cracking gasoline and catalytic cracking light cycle oil; feeding the obtained spent catalyst into a regenerator for scorching regeneration to obtain a regenerated catalyst; feeding regenerated catalyst as the first catalytic cracking catalyst and the second catalytic cracking catalyst into the riser reactor; feeding the catalytic cracking light cycle oil into a hydrogenation reactor to contact with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil; and (3) sending the hydrogenated light cycle oil into the riser reactor from a second nozzle to perform the catalytic cracking reaction, wherein the second nozzle and the first nozzle are arranged at intervals in the height direction.
According to the present invention, the relative positions of the first nozzle and the second nozzle are not particularly required, and the first nozzle may be disposed above or below the second nozzle, preferably, the second nozzle is disposed above the first nozzle in the height direction, and the second catalytic cracking catalyst is fed into the riser reactor from a position above the second nozzle or between the first nozzle and the second nozzle. The stratified entering of the hydrogenated light cycle oil and the heavy raw material has the advantages that the reaction conditions of different fractions of catalytic cracking can be optimized, so that the maximum conversion is realized, particularly, the regenerated catalyst is further supplemented before/after the mixture of the reaction oil gas and the catalyst is contacted with the hydrogenated light cycle oil, and the conversion of the hydrogenated light cycle oil is favorably strengthened. The residence time of the reaction oil gas in the riser reactor between the first nozzle and the second nozzle can be 0.05-2 seconds, preferably 0.1-1 second.
Heavy feedstocks are well known to those skilled in the art in accordance with the present invention, and for example, the heavy feedstock may be at least one selected from the group consisting of straight run waxy oil, coker waxy oil, deasphalted oil, hydrofinished oil, hydrocracked tail oil, vacuum residue, and atmospheric residue, although other heavy feedstocks may be employed by those skilled in the art.
Catalytic cracking reactions according to the present invention are well known to those skilled in the art, for example, the conditions for catalytic cracking reactions of heavy feedstocks may include: the reaction temperature (at the riser outlet) may be 520-650 ℃, preferably 550-590 ℃, the absolute pressure may be 0.15-0.4 mpa, the weight ratio of the total weight of the first catalytic cracking catalyst and the second catalytic cracking catalyst to the heavy feedstock is 1-50, preferably 3-30, the oil gas residence time (from the first nozzle to the riser reactor outlet) is 1-10 seconds, preferably 2-8 seconds, and the (mixed) weight ratio of steam to heavy feedstock is 0.01-0.5, preferably 0.02-0.2. The catalytic cracking reaction conditions of the hydrogenated light cycle oil may include: the reaction temperature (at the outlet of the riser) can be 520-650 ℃, preferably 550-590 ℃, the absolute pressure can be 0.15-0.4 MPa, the weight ratio of the total weight of the first catalytic cracking catalyst and the second catalytic cracking catalyst to the hydrogenated light cycle oil is 5-100, preferably 8-50, the oil gas residence time (from the second nozzle to the outlet of the riser reactor) is 1-10 seconds, preferably 2-8 seconds, the (mixed) weight ratio of the steam and the hydrogenated light cycle oil is 0.01-0.3, preferably 0.02-0.1, the micro-reaction activity of the regenerated catalyst is not less than 60, preferably not less than 62, and the micro-reaction activity is determined by the micro-reaction activity test method of the RIPP 92-90 catalytic cracking industrial equilibrium catalyst (the petrochemical analysis method (RIPP test method), the edition of Yankee et al, 1990 edition). The circulating weight ratio of the first catalytic cracking catalyst to the second catalytic cracking catalyst per unit time may be 1: (0.02-1), preferably 1: (0.03-0.5). The riser reactor can be an equal-diameter riser reactor or a reducing riser reactor.
In one embodiment, a first catalytic cracking catalyst is fed into the riser reactor from a conventional catalyst inlet of the riser reactor, and a second catalytic cracking catalyst is fed from a make-up agent inlet in the middle of the riser reactor to enhance the conversion of the hydrogenated light cycle oil.
Catalytic cracking catalysts are well known to those skilled in the art in accordance with the present invention, for example, the regenerated catalyst may comprise 10 to 50 wt% zeolite, which is at least one selected from the group consisting of rare earth-containing or non-rare earth-containing Y, HY, USY and Beta zeolites, 5 to 90 wt% inorganic oxide and 0 to 70 wt% clay, although other catalysts may be employed by those skilled in the art.
Hydrotreating is well known to those skilled in the art in accordance with the present invention, for example, the hydrotreating catalyst may include an active metal component which is a group VIB metal and/or a group VIII non-noble metal, and a support which may be at least one selected from alumina, silica, and amorphous silica-alumina, and the active metal component may be nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum, or cobalt-molybdenum. The hydrotreating conditions may be: hydrogen partial pressure of 5.0-22.0 MPa, preferably 8.0-15.0 MPa, reaction temperature of 330-450 deg.C, preferably 340-380 deg.C, and volume space velocity of 0.1-10.0 hr-1Hydrogen to oil volume ratio of 100-2000Nm3/m3. Hydrotreating the obtained product, separating to obtain initial boiling point>250 ℃ and preferably>The fraction at 260 ℃ is called hydrogenated diesel oil or hydrogenated light cycle oil, and the content of bicyclic aromatics in the hydrogenated light cycle oil is generally not more than 20 wt%, preferably not more than 10 wt%.
The following further describes embodiments of the method of the present invention in conjunction with the drawings, but the invention is not limited thereto.
As shown in fig. 1, heavy feedstock also enters the riser reactor 19 through the first nozzle 7 via line 5, light cycle oil enters the hydrogenation reactor 3 via line 1, and hydrogen is simultaneously introduced into the hydrogenation reactor 3 via line 2. The hydrogenated product, hydrogenated light cycle oil, enters the catalytic cracking riser reactor 19 through a second nozzle 6 via a line 4. The regenerated catalyst from the regenerator 13 as a first catalytic cracking catalyst enters the bottom of the riser reactor through a regeneration inclined tube 10 under the control of a regeneration slide valve 11, moves upwards under the action of a pre-lifting medium, enters a heavy raw material reaction zone I, and contacts, reacts and moves upwards with the heavy raw material entering through a first nozzle 7 in the reaction zone; and then the mixture of the reaction oil gas and the catalyst enters a hydrogenation light cycle oil reaction area II, contacts, reacts and ascends with hydrogenation light cycle oil entering through a second nozzle 6 in the reaction area, and simultaneously, a part of regenerated catalyst from a regenerator 13 is used as a second catalytic cracking catalyst and also supplementarily enters the hydrogenation light cycle oil reaction area II through a regeneration inclined pipe 8 and a regeneration slide valve 9 to strengthen the cracking reaction of the hydrogenation light cycle oil. The reaction product and the spent catalyst after the reaction enter a settler 12 for separation of the reaction product and the catalyst, and the separated catalyst enters a regenerator 13 for regeneration and circulation. The reaction product enters a fractionating tower 18 through a pipeline 14, and oil slurry from the fractionating tower 18 is discharged out of the device as a product through a pipeline 17; the oil gas from the fractionating tower 18 enters a subsequent absorption stabilizing system through a pipeline 15 to obtain dry gas, liquefied gas and high-octane gasoline; and the light cycle oil introduced by the fractionating tower 18 enters the hydrogenation reactor 3 for circulation through a pipeline 16 and a pipeline 1.
The following examples further illustrate the invention but are not intended to limit the invention thereto. In the embodiment, the hydrotreating catalyst filled in the hydrogenation reactor has a commercial brand of RN-32V, the protective agent has a commercial brand of RG-1, and the filling volume ratio of the hydrotreating catalyst to the protective agent is 95:5, which are 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, and the commercial designation thereof is HAC, manufactured by China petrochemical catalyst division.
The heavy feedstock used in the examples and comparative examples was a mixed feedstock of 90 wt% straight run wax oil and 10 wt% vacuum residue, the properties of which are shown in table 2.
The light cycle oil circulation weight ratio is the weight of the light cycle oil hydrogenated and recycled/the weight of the heavy raw material;
the gasoline octane number determination method (RON) is carried out by the GB/T5487-2015 method, and the gasoline octane number determination method (motor method, MON) is carried out by the GB/T503-2016 method.
Example 1
This example illustrates the method of the present invention as shown in fig. 1, and the specific flow is as described in the previous embodiments. The main operating parameters of the catalytic cracker are shown in table 3.
The light cycle oil enters a medium-sized hydrogenation reactor, and the test conditions of the hydrogenation treatment are as follows: hydrogen partial pressure 8.0 MPa, average bed reaction temperature 360 deg.c and volume space velocity 0.5 hr-1Hydrogen to oil volume ratio 1100Nm3/m3。
The residence time of the reaction oil gas is 0.2 seconds within the distance between the positions where the hydrogenation light cycle oil and the heavy raw material enter the lifting pipe. The distribution of the reaction products, the hydrogen consumption and the gasoline octane number are shown in Table 4.
Example 2
In example 2, the hydrogenated light cycle oil enters from the position of the first nozzle in fig. 1, and the heavy oil feedstock enters from the second nozzle, and the catalytic cracking unit and the catalytic cracking catalyst in example 2 are exactly the same as those in example 1. The operating conditions of the catalytic cracking unit in example 2 are shown in table 3. The distribution of the reaction products, the hydrogen consumption and the gasoline octane number are shown in Table 4.
Comparative example 1
The hydrogenated light cycle oil and the heavy oil feedstock in comparative example 1 were mixed and introduced into the riser reactor through the first nozzle 7. The catalytic cracking apparatus and the catalytic cracking catalyst in comparative example 1 were exactly the same as those in the examples. The agent-to-oil ratio in comparative example 1 is for the total mixed feed, i.e., including the heavy oil feedstock and the hydrogenated light cycle oil. The operating conditions of the catalytic cracking unit are shown in Table 3, and the distribution of the reaction products, the hydrogen consumption and the gasoline octane number are shown in Table 4.
Comparative example 2
Comparative example 2 was operated substantially the same as example 1 except that the middle of the riser reactor was not replenished with catalyst and the regenerated catalyst was all introduced from the bottom of the riser reactor. The operating conditions of the catalytic cracking unit are shown in Table 3, and the distribution of the reaction products, the hydrogen consumption and the gasoline octane number are shown in Table 4.
From the analysis in table 4, it can be seen that the gasoline yield in example 1 is 63.5 wt% compared to example 2, and 6.4 percentage points greater than example 2, due to the shortened residence time of the hydrogenated light cycle oil in the riser. Meanwhile, compared with the comparative example 1, the stratified feeding is increased and the regenerant is supplemented in the example 1, but the regenerant is not supplemented in the comparative examples 1-2 for circulation, so that the heavy oil conversion rate is obviously reduced, and the gasoline yield is greatly reduced compared with the example. In addition, the octane number of the gasoline is obviously reduced compared with the example.
TABLE 1
TABLE 2
| Raw oil name | Mixing the raw materials |
| Density (20 ℃) kg/m3 | 916.8 |
| Freezing point, DEG C | 32 |
| Refractive index (70 ℃ C.) | 1.4968 |
| Carbon residue, by weight% | 2.67 |
| Average molecular weight | 404 |
| Distillation range, deg.C | |
| Initial boiling point | 294 |
| 5% by weight | 361 |
| 10% by weight | 381 |
| 30% by weight | 422 |
| 50% by weight | 451 |
| 70% by weight | 497 |
| Sulfur content, wt.% | 1.1 |
| Nitrogen content, wt.% | 0.24 |
| Hydrogen content, wt.% | 12.6 |
| Metal content, mg/kg | |
| Ni | 6.6 |
| V | 1.2 |
TABLE 3
TABLE 4
| Item | Example 1 | Example 2 | Comparative example 1 | Comparative example 2 |
| Hydrogen consumption, wt.% | 1.43 | 1.43 | 2.6 | 2.6 |
| Distribution of the product, weight% | ||||
| Dry gas | 3.8 | 4.5 | 3.6 | 4.6 |
| Liquefied gas | 18.3 | 19.5 | 17.5 | 18.3 |
| Gasoline (gasoline) | 63.5 | 57.1 | 53.4 | 53.4 |
| Light cycle oil | 0.0 | 0.0 | 0.0 | 0.0 |
| Heavy oil | 4.2 | 8.4 | 14.7 | 13.0 |
| Coke | 10.2 | 10.5 | 10.8 | 10.7 |
| Total up to | 100.0 | 100.0 | 100.0 | 100.0 |
| Octane number of gasoline | ||||
| RON | 95.0 | 93.5 | 91.5 | 91.6 |
| MON | 84.6 | 82.6 | 80.4 | 80.3 |
Claims (12)
1. A process for producing a high octane gasoline, the process comprising:
spraying a heavy raw material into the riser reactor from a first nozzle, contacting with a first catalytic cracking catalyst from the bottom of the riser reactor and a second catalytic cracking catalyst from the middle of the riser reactor, and carrying out catalytic cracking reaction to obtain a reaction product and a spent catalyst;
separating the obtained reaction products to at least obtain catalytic cracking gasoline and catalytic cracking light cycle oil;
feeding the obtained spent catalyst into a regenerator for scorching regeneration to obtain a regenerated catalyst;
feeding regenerated catalyst as the first catalytic cracking catalyst and the second catalytic cracking catalyst into the riser reactor;
feeding the catalytic cracking light cycle oil into a hydrogenation reactor to contact with a hydrotreating catalyst and carrying out hydrotreating to obtain hydrogenated light cycle oil;
sending hydrogenated light cycle oil into the riser reactor from a second nozzle to perform the catalytic cracking reaction, wherein the second nozzle and the first nozzle are arranged at intervals in the height direction; the second nozzle is arranged above the first nozzle along the height direction, and the second catalytic cracking catalyst is fed into the riser reactor from a position above the second nozzle or between the first nozzle and the second nozzle.
2. The production method according to claim 1, wherein the residence time of the reaction oil gas in the riser reactor between the first nozzle and the second nozzle is 0.05-2 seconds.
3. The production process according to claim 1, wherein the heavy feedstock is at least one selected from the group consisting of straight-run wax oil, coker wax oil, deasphalted oil, hydrorefined oil, hydrocracked tail oil, vacuum residue, and atmospheric residue.
4. The production process according to claim 1, wherein the conditions of the catalytic cracking reaction of the heavy feedstock comprise: the reaction temperature is 520-650 ℃, the absolute pressure is 0.15-0.4 MPa, the weight ratio of the total weight of the first catalytic cracking catalyst and the second catalytic cracking catalyst to the heavy raw material is 1-50, the oil gas retention time is 1-10 seconds, the weight ratio of the water vapor to the heavy raw material is 0.01-0.5, the micro-reaction activity of the regenerated catalyst is not lower than 60, and the micro-reaction activity is determined by a micro-reaction activity test method of an RIPP 92-90 catalytic cracking industrial equilibrium catalyst.
5. The production process according to claim 1, wherein the regenerated catalyst comprises 10 to 50% by weight of zeolite which is at least one selected from the group consisting of Y, HY, USY and Beta zeolites with or without rare earth, 5 to 90% by weight of inorganic oxide and 0 to 70% by weight of clay.
6. The production method according to claim 1, wherein the riser reactor is a constant-diameter riser reactor or a variable-diameter riser reactor.
7. The production method according to claim 1, wherein the hydrotreating catalyst comprises an active metal component which is a group VIB metal and/or a non-noble group VIII metal, and a support which is at least one selected from alumina, silica and amorphous silica-alumina.
8. The production method according to claim 7, wherein the active metal component is nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum, or cobalt-molybdenum.
9. The production process according to claim 1, wherein the conditions of the hydrotreatment are: hydrogen partial pressure of 5.0-22.0 MPa, reaction temperature of 330-450 deg.c and volume space velocity of 0.1-10.0 hr-1Hydrogen to oil volume ratio of 100-2000Nm3/m3。
10. The production process according to claim 1, wherein the content of bicyclic aromatics in the hydrogenated light cycle oil is not more than 20 wt%.
11. The production method according to claim 1, wherein the catalytic cracking reaction conditions of the hydrogenated light cycle oil comprise: the reaction temperature is 520-650 ℃, the absolute pressure is 0.15-0.4 MPa, the weight ratio of the total weight of the first catalytic cracking catalyst and the second catalytic cracking catalyst to the hydrogenated light cycle oil is 5-100, the oil gas residence time is 1-10 seconds, and the weight ratio of the water vapor to the hydrogenated light cycle oil is 0.01-0.3.
12. The production process according to claim 1, wherein the circulating weight ratio of the first catalytic cracking catalyst to the second catalytic cracking catalyst per unit time is 1: (0.02-1).
Priority Applications (8)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711010110.6A CN109705912B (en) | 2017-10-25 | 2017-10-25 | Production method of high-octane gasoline |
| TW107137639A TWI810212B (en) | 2017-10-25 | 2018-10-24 | Method for producing high-octane catalytic cracking gasoline |
| BR102018071838-0A BR102018071838B1 (en) | 2017-10-25 | 2018-10-24 | PROCESS FOR PRODUCING HIGH OCTANAGE CATALYTIC CRACKING GASOLINE AND CATALYTIC CRACKING SYSTEM FOR CARRYING OUT THE SAID PROCESS |
| US16/169,424 US10961471B2 (en) | 2017-10-25 | 2018-10-24 | Process for producing catalytic cracking gasoline with a high octane number |
| SG10201809462WA SG10201809462WA (en) | 2017-10-25 | 2018-10-25 | Process for producing catalytic cracking gasoline with a high octane number |
| KR1020180128305A KR102573786B1 (en) | 2017-10-25 | 2018-10-25 | Process for producing catalytic cracking gasoline with a high octane number |
| EP18202626.0A EP3476919B1 (en) | 2017-10-25 | 2018-10-25 | Process for producing catalytic cracking gasoline with a high octane number |
| JP2018200709A JP7187263B2 (en) | 2017-10-25 | 2018-10-25 | Method for producing high octane catalytic cracking gasoline |
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| CN1466619A (en) * | 2000-04-17 | 2004-01-07 | ����ɭ�о����̹�˾ | Cycle oil conversion process |
| CN1912068A (en) * | 2005-08-08 | 2007-02-14 | 洛阳石化设备研究所 | Method and device of heavy oil two stage catalytic cracking reforming and gasoline upgrade coupling |
| CN101058744A (en) * | 2006-04-21 | 2007-10-24 | 中国石油天然气股份有限公司 | Lift leg catalytic conversion process and apparatus |
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