CN102453507B - Conversion method for hydrocarbon oil - Google Patents
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- CN102453507B CN102453507B CN201010519116.8A CN201010519116A CN102453507B CN 102453507 B CN102453507 B CN 102453507B CN 201010519116 A CN201010519116 A CN 201010519116A CN 102453507 B CN102453507 B CN 102453507B
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Abstract
The invention provides a conversion method for hydrocarbon oil. According to the method, the raw material of diesel oil and the raw material of gasoline are respectively introduced into an upper reaction zone and a lower reaction zone in a riser reactor and respectively contact and react with a high temperature catalyst; therefore, the yield of ethylene and propylene is improved, and the content of alkene and sulfur in reacted gasoline is substantially reduced, thereby improving the quality of the gasoline.
Description
Technical field
The present invention relates to a kind of method of hydrocarbon oil conversion, more particularly, relating to is that the productive rate of a kind of ethene and propylene is high and can effectively reduce sulphur content in gasoline and the conversion method for hydrocarbon oil of olefin(e) centent.
Background technology
The at present production of ethene and propylene mainly adopts take the steam cracking method that petroleum naphtha is raw material, and the temperature of reaction of steam cracking is high, high to requirement harshness and the energy consumption of conversion unit.In addition, along with the demand of ethene and propylene is increased day by day, faster to the demand growth of propylene especially.By improving steam cracking process condition, can improve the ratio of propylene/ethylene, but the productive rate of total olefin and the economy of reaction unit be affected, be therefore subject to certain restrictions.
Catalytic cracking is one of important means of oil secondary processing, for producing gasoline, diesel oil, liquefied gas etc. from heavy raw oil.
Catalytic cracking process adopts molecular sieve catalyst, the steam atomizing of stock oil water also sprays in riser reactor, high temperature catalyst (550-700 ℃) contact reacts in riser tube with from revivifier, makes progress along riser tube together, leaves subsequently riser reactor.Reaction product, through isolate catalyzer in settling vessel, goes separation column to carry out product separation afterwards.
The problem that above-mentioned conversion method for hydrocarbon oil exists is that the productive rate of ethene and propylene is lower, and after reaction, olefin(e) centent and the sulphur content in hydrocarbon ils is higher.Therefore, need urgently to develop the productive rate of a kind of ethene and propylene high and can effectively reduce sulphur content in hydrocarbon ils and the conversion method for hydrocarbon oil of olefin(e) centent.
Summary of the invention
The productive rate that the object of the invention is to overcome ethene that existing conversion method for hydrocarbon oil exists and propylene is low, and olefin(e) centent and the higher shortcoming of sulphur content in gasoline after reaction, provide the productive rate of a kind of ethene and propylene high and can effectively reduce the conversion method for hydrocarbon oil of sulfur content in gasoline and olefin(e) centent.
The invention provides a kind of conversion method for hydrocarbon oil, wherein, the method comprises:
(1) pre-lift medium, gasoline stocks and regenerated catalyst and/or half regenerated catalyst are sent into the lower reaction zone of riser reactor, at the temperature of 600-750 ℃, carry out contact reacts, the oil gas of generation and reacted catalyzer are upwards sent into the reaction zone, top of riser reactor;
(2) diesel raw material and regenerated catalyst are sent into the reaction zone, top of riser reactor, at the temperature of 500-650 ℃, made described diesel raw material, regenerated catalyst and carry out contact reacts from the oil gas of lower reaction zone together with catalyzer;
(3) mixture at the reacted oil gas in reaction zone, top and catalyzer is carried out to finish separated, the oil gas after finish separation is sent to subsequent separation system separating reaction product, and the catalyzer after gas-oil separation obtains reclaimable catalyst after stripping;
(4) described reclaimable catalyst is carried out to coke burning regeneration, obtain regenerated catalyst, or in the regenerating unit containing the first revivifier and Second reactivator, carry out coke burning regeneration, from the first revivifier and Second reactivator, obtain respectively half regenerated catalyst and regenerated catalyst;
(5) lower reaction zone of the regenerated catalyst obtaining and/or half regenerated catalyst being returned to riser reactor recycles, and/or the reaction zone, top that the regenerated catalyst obtaining returns to riser reactor is recycled.
Conversion method for hydrocarbon oil provided by the invention is by carrying out hydrocarbon oil conversion in the riser reactor comprising upper and lower two reaction zones, by introducing respectively diesel raw material and gasoline stocks in two reaction zones up and down at riser reactor, and by diesel raw material and gasoline stocks respectively with high temperature catalyst contact reacts, thereby improved significantly the productive rate of ethene and propylene, and the content of alkene and the content of sulphur in reacted hydrocarbon ils are reduced significantly, improved the quality of hydrocarbon ils.
Accompanying drawing explanation
Fig. 1 is the structural representation of the riser reactor that uses in embodiment of the present invention 1-2.
Embodiment
The invention provides a kind of conversion method for hydrocarbon oil, wherein, the method comprises:
(1) pre-lift medium, gasoline stocks and regenerated catalyst and/or half regenerated catalyst are sent into the lower reaction zone of riser reactor, at the temperature of 600-750 ℃, carry out contact reacts, the oil gas of generation and reacted catalyzer are upwards sent into the reaction zone, top of riser reactor;
(2) diesel raw material and regenerated catalyst are sent into the reaction zone, top of riser reactor, at the temperature of 500-650 ℃, made described diesel raw material, regenerated catalyst and carry out contact reacts from the oil gas of lower reaction zone together with catalyzer;
(3) mixture at the reacted oil gas in reaction zone, top and catalyzer is carried out to finish separated, the oil gas after finish separation is sent to subsequent separation system separating reaction product, and the catalyzer after gas-oil separation obtains reclaimable catalyst after stripping;
(4) described reclaimable catalyst is carried out to coke burning regeneration, obtain regenerated catalyst, or in the regenerating unit containing the first revivifier and Second reactivator, carry out coke burning regeneration, from the first revivifier and Second reactivator, obtain respectively half regenerated catalyst and regenerated catalyst;
(5) lower reaction zone of the regenerated catalyst obtaining and/or half regenerated catalyst being returned to riser reactor recycles, and/or the reaction zone, top that the regenerated catalyst obtaining returns to riser reactor is recycled.
In the present invention, the definition of term " gasoline stocks " and kind are conventionally known to one of skill in the art, can for boiling range, be petroleum hydrocarbon cut or the petroleum hydrocarbon cut of boiling range within the scope of 30-210 ℃ of 30-210 ℃, wherein preferred boiling range be the petroleum hydrocarbon cut of 30-180 ℃.The above-described petroleum hydrocarbon cut petroleum naphtha (fraction boiling range is 30-210 ℃) that can be crude oil produce through time processing, the gasoline fraction (fraction boiling range is 30-210 ℃) of producing through secondary processing, one or more the mixture in petroleum naphtha (fraction boiling range is 30-100 ℃) fraction, described time processing is crude oil atmospheric distillation, and described secondary processing comprises catalytic cracking, coking, hydrocracking, hydrotreatment, hydrofining etc.For example, described gasoline stocks can be one or more in coker gasoline, straight-run spirit, catalytic gasoline, pressure gasoline and reforming raffinate oil.
In addition, the definition of term " diesel raw material " and kind are conventionally known to one of skill in the art, can for boiling range, be petroleum hydrocarbon cut or the petroleum hydrocarbon cut of boiling range within the scope of 180-380 ℃ of 180-380 ℃, wherein preferred boiling range be the petroleum hydrocarbon cut of 180-330 ℃.The mixture of one or more in the above-described petroleum hydrocarbon cut straight-run diesel oil (fraction boiling range is 180-350 ℃) that can be crude oil produce through time processing, the fraction of diesel oil (fraction boiling range is 180-350 ℃) produced through secondary processing, described time processing is crude oil atmospheric distillation, and described secondary processing comprises catalytic cracking, coking, hydrocracking, hydrotreatment, hydrofining etc.For example, can be one or more in straight-run diesel oil, catalytic diesel oil, thermally splitting diesel oil, hydrotreatment diesel oil, hydrofining diesel oil, hydrocracking diesel oil.
In the present invention, in preferred situation, described gasoline stocks and regenerated catalyst and/or the catalytic temperature of half regenerated catalyst can be 600-750 ℃, and most preferably gasoline stocks contacts with regenerated catalyst, and catalytic temperature is 700-730 ℃.In the present invention, by the temperature of reaction of lower reaction zone is controlled in above-mentioned scope, gasoline stocks is contacted with the regenerated catalyst of high temperature, gasoline stocks carries out cracking, thereby has increased ethene and third rare yield; Or gasoline stocks and half regenerated catalyst contact reacts, sulphur content and the olefin(e) centent of reduction gasoline; In reaction zone, top, diesel raw material contacts with regenerated catalyst, and diesel raw material is carried out to cracking, increases the yield of gasoline, propylene etc.
According to the present invention, the contact pressure of described gasoline stocks and regenerated catalyst and/or half regenerated catalyst can be 100-450 kPa, is preferably 280-320 kPa; The time of contact can be 0.1-10 second, is preferably 2-5 second.The weight ratio of described regenerated catalyst and/or half regenerated catalyst and gasoline stocks can in very large range change, and is 2-30 under preferable case: 1, and 5-10 more preferably: 1.
According to the present invention, in preferred situation, the catalytic temperature 550-590 ℃ of described diesel raw material and regenerated catalyst.The contact pressure of described diesel raw material and regenerated catalyst can be 130-450 kPa, is preferably 220-280 kPa; The time of contact can be 0.1-10 second, is preferably 3-7 second.The weight ratio of described regenerated catalyst (regenerated catalyst newly adding) and diesel raw material can in very large range change, and under preferable case, the weight ratio of described regenerated catalyst and diesel raw material can be 2-25: 1, and 5-10 more preferably: 1.
In the present invention, in described riser reactor, lower reaction zone has no particular limits with the ratio of the volume of reaction zone, top, the diameter of each reaction zone of riser reactor can be identical, also can be different, when the diameter of each reaction zone of riser reactor is identical, the aspect ratio of reaction zone, top and reaction zone, top is volume ratio, therefore, by adjustment, rise the flow velocity of medium, can control the duration of contact of reaction raw materials and catalyzer in riser reactor, under preferable case, described lower reaction zone is 1 with the ratio of the volume of reaction zone, top: 0.2-10, more preferably 1: 6-10.
According to the present invention, described pre-lift medium can be various pre-lift medium well known to those skilled in the art, as one or more in water vapor, refinery dry gas, light paraffins, light olefin.The effect of pre-lift medium is to make catalyzer accelerate to rise, and forms the catalyst activity plug flow of even density in riser reactor bottom.The consumption of pre-lift medium is as well known to those skilled in the art, and preferably, the consumption of pre-lift medium accounts for the 1-30 % by weight of hydrocarbon ils total amount, preferably 2-15 % by weight.
According to the present invention, the ratio between described diesel raw material and gasoline stocks can in very large range change, and under preferable case, the weight ratio of diesel raw material and gasoline stocks can be 0.1-10: 1, and 0.2-5 more preferably: 1, most preferably be 0.5-1: 1.
In the present invention, described catalyzer is the cracking catalyst that contains molecular sieve, and consisting of of described cracking catalyst is conventionally known to one of skill in the art, for example, described cracking catalyst can contain one or more molecular sieves, heat-resistant inorganic oxide, and the clay that contains of selectivity; Wherein, the content of molecular sieve, heat-resistant inorganic oxide and clay is conventionally known to one of skill in the art.
The kind of described molecular sieve is conventionally known to one of skill in the art, for example, can be mesopore and/or the large pore molecular sieve as active component of cracking catalyst.Described large pore molecular sieve as containing or not phosphorus element-containing y-type zeolite, containing or not containing the ultrastable Y－type zeolite of rare earth element; Described mesoporous molecular sieve for containing or one or more in the supersiliceous zeolite with five-membered ring structure, β zeolite, mordenite, omega zeolite of phosphorus element-containing not, the supersiliceous zeolite with five-membered ring structure can be ZSM-5 zeolite and/or ZRP zeolite, preferably containing or the not ZSM-5 zeolite with five-membered ring structure and/or the ZRP zeolite of phosphorus element-containing.
Described heat-resistant inorganic oxide is conventionally known to one of skill in the art, as being selected from one or more in aluminum oxide, silicon oxide, amorphous silicon aluminium, zirconium white, titanium oxide, boron oxide, alkaline earth metal oxide.
Described clay is conventionally known to one of skill in the art, as being selected from one or more in kaolin, halloysite, polynite, diatomite, halloysite, saponite, tired de-soil, sepiolite, attapulgite, hydrotalcite, boron-moisten soil.
Referring to Fig. 1, describe reaction process of the present invention in detail.
Gasoline stocks after preheating enters the bottom of lower reaction zone 1 by the first atomizing nozzle 5 of riser reactor, regenerated catalyst and/or half regenerated catalyst enter the bottom of lower reaction zone 1 through the first catalyst inlet 3 of riser reactor simultaneously, under the castering action of pre-lift medium that enters riser reactor bottom through pipeline 7, described regenerated catalyst and/or half regenerated catalyst and gasoline stocks stream rise and contact reacts in lower reaction zone 1 along riser reactor, afterwards, the reactant flow of lower reaction zone 1 enters reaction zone, top 2.
Diesel raw material after preheating enters reaction zone, top 2 by the second atomizing nozzle 6 of riser reactor, simultaneously regenerated catalyst enters reaction zone, top 2 through the second catalyst inlet 4 of riser reactor, diesel raw material and regenerated catalyst, from reactant flow mixing and contacting reaction in reaction zone, top 2 of lower reaction zone 1; Afterwards, the reactant flow of reaction zone, top 2 enters settlement separator after continuing to rise to riser reactor outlet, separating catalyst and reaction product, catalyzer obtains reclaimable catalyst through stripper stripping, reclaimable catalyst enters revivifier and burns and obtain regenerated catalyst, or enter in the regenerating unit that comprises the first revivifier and Second reactivator and carry out coke burning regeneration, from the first revivifier and Second reactivator, obtain respectively half regenerated catalyst and regenerated catalyst.Regenerated catalyst and/or half regenerated catalyst recycle, and reaction product enters subsequent product separating device.
In aforesaid method of the present invention, in stripper, adopt water vapor to carry out stripping, its effect is that the oil gas that is full of between granules of catalyst and in particle hole is cemented out, and improves oil product productive rate.Amount for steam stripped water vapor is as well known to those skilled in the art.In general, for the consumption of steam stripped water vapor, account for the 0.1-0.8 % by weight of catalyst recirculation amount, preferably 0.2-0.4 % by weight.Term " internal circulating load " generally refers to the weight that unit time inner catalyst transmits between reaction-regeneration system, refers in particular in the unit time by the catalyst weight of stripper herein.Because catalyzer is after circulation after a while, have loss, therefore, need regularly or fresh makeup catalyst aperiodically, by live catalyst by small-sized charging system or alternate manner introducing revivifier, with the regenerated catalyst use that is mixed.
Mode below in conjunction with accompanying drawing with embodiment is further described in detail the present invention, but should not think the restriction of scope that the present invention is protected.
In following examples, account for approximately 0.4 % by weight of catalyst recirculation amount for the consumption of steam stripped water vapor, pre-lift medium adopts water vapor.
Embodiment 1
The present embodiment adopts middle scale riser reactor, this riser reactor is that total height is 10 meters, and diameter is the cylindrical structure of 25 centimetres, wherein, the aspect ratio of bottom, reaction zone, top is 1: 7.5, and the below that this riser tube foot is lower reaction zone is pre lift zone.
From lower reaction zone, introduce gasoline stocks and regenerated catalyst, wherein, gasoline stocks is catalytically cracked gasoline, introduces diesel raw material and regenerated catalyst from reaction zone, top, and wherein, diesel raw material is straight-run diesel oil.The weight ratio of the inlet amount of straight-run diesel oil and the inlet amount of catalytically cracked gasoline is 1: 2, and the character of raw material is listed in table 1.The catalyzer that the trade mark that the catalyzer using is produced for Sinopec group Shandong catalyst plant is CEP-1, its character is listed in table 2.
Concrete steps are, as shown in Figure 1, gasoline stocks after preheating enters lower reaction zone 1 by the first atomizing nozzle 5, regenerated catalyst from revivifier enters lower reaction zone 1 through the first catalyst inlet 3, gasoline stocks contacts with regenerated catalyst (CEP-1), under the effect of pre-lift medium that enters riser reactor bottom through pipeline 7, along riser reactor, rise, enter reaction zone, top 2.
Straight-run diesel oil after preheating enters reaction zone, top 2 by the second atomizing nozzle 6, regenerated catalyst from revivifier enters reaction zone, top 2 through the second catalyst inlet 4, straight-run diesel oil and regenerated catalyst (CEP-1) and from the logistics contact reacts of lower reaction zone; Reactant flow from bottom, reaction zone, top enters settlement separator after riser reactor rises to riser reactor outlet, separating catalyst and reaction product, catalyzer obtains reclaimable catalyst through stripper stripping, reclaimable catalyst enters revivifier and burns and obtain regenerated catalyst, regenerated catalyst is recycled, and reaction product enters subsequent product separating device.Concrete operational condition and product distribute and list in respectively table 3 and table 4.The gasoline products quality that reaction obtains is listed in table 5.
Table 1
| Catalytically cracked gasoline | Straight-run diesel oil | |
| Density (20 ℃)/gram centimeter -3 | 0.70 | 0.89 |
| Sulphur content/% by weight | 0.062 | 0.28 |
| Alkene/% by weight | 47.3 | |
| Alkane/% by weight | 23.7 | 86 |
| Aromatic hydrocarbons/% by weight | 23.4 | 14 |
| Boiling range | ||
| Initial boiling point/℃ | 34 | 189 |
| 10 volume % distillate a little/℃ | 57 | 205 |
| 30 volume % distillate a little/℃ | 70 | 226 |
| 50 volume % distillate a little/℃ | 91 | 231 |
| 70 volume % distillate a little/℃ | 123 | 253 |
| 90 volume % distillate a little/℃ | 159 | 279 |
Table 2
| Catalyzer trade names | CEP-1 |
| Molecular sieve active ingredient | ZSM-5 |
| Chemical constitution, wt% | |
| Aluminum oxide | 46.3 |
| Sodium oxide | 0.04 |
| Ferric oxide | 0.27 |
| Tap density, kg/m 3 | 860 |
| Pore volume, ml/g | 0.24 |
| Specific surface area, m 2/g | 153 |
| Abrasion index, wt%h ～1 | 1.0 |
| Size composition, wt% | |
| 0-40μm | 17.9 |
| 40-80μm | 41.4 |
| ＞80μm | 40.7 |
Embodiment 2
According to the method identical with embodiment 1, carry out hydrocarbon oil conversion, difference is that reaction conditions is different.Concrete operational condition and product distribute and list in respectively table 3 and table 4.The gasoline products quality that conversion reaction obtains is listed in table 5.
Comparative example 1
According to the method identical with embodiment 1, carry out hydrocarbon oil conversion, difference is that catalyzer is not introduced in reaction zone, top.Concrete operational condition and product distribute and list in respectively table 3 and table 4.The gasoline products quality that conversion reaction obtains is listed in table 5.
Comparative example 2
According to the method identical with embodiment 1, carry out hydrocarbon oil conversion, difference is that reaction conditions is different.Concrete operational condition and product distribute and list in respectively table 3 and table 4.The gasoline products quality that conversion reaction obtains is listed in table 5.
Table 3
Table 4
| Product distributes, % by weight | Embodiment 1 | Embodiment 2 | Comparative example 1 | Comparative example 2 |
| Dry gas | 10.89 | 9.72 | 6.37 | 4.37 |
| Ethene | 5.63 | 4.78 | 2.85 | 1.8 |
| Liquefied gas | 44.63 | 40.51 | 31.38 | 20.15 |
| Propylene | 21.56 | 18.76 | 15.34 | 9.12 |
| C5+ gasoline | 30.67 | 38.63 | 46.76 | 57.65 |
| Diesel oil | 11.57 | 8.51 | 13.34 | 15.68 |
| Heavy oil | 0.29 | 0.38 | 0.26 | 0.25 |
| Coke | 1.95 | 2.25 | 1.89 | 1.9 |
From the data of table 4, can find out, compare with 2 with comparative example 1, adopt in the embodiment 1-2 of method for transformation of the present invention, the productive rate of propylene and ethene significantly improves, wherein the productive rate of embodiment 1 ethene and propylene is respectively 5.63 % by weight and 21.56 % by weight, and the ethene of embodiment 2 and the productive rate of propylene are respectively 4.78 % by weight and 18.76 % by weight.
Table 5
| Embodiment 1 | Embodiment 2 | Comparative example 1 | Comparative example 2 | |
| Density (20 ℃)/gram centimeter ～1 | 0.706 | 0.711 | 0.713 | 0.712 |
| Alkene/volume % | 18.7 | 20.5 | 26.7 | 29.9 |
| Normal paraffin/volume % | 7.1 | 7.7 | 9.2 | 8.7 |
| Isoparaffin/weight volume % | 32.8 | 32.7 | 26.3 | 24.1 |
| Aromatic hydrocarbons/volume % | 41.4 | 39.1 | 37.8 | 37.3 |
| Sulphur content (% by weight) | 0.03 | 0.03 | 0.05 | 0.05 |
| Boiling range | ||||
| Initial boiling point/℃ | 33 | 34 | 34 | 34 |
| 10 volume % distillate a little/℃ | 56 | 56 | 57 | 58 |
| 30 volume % distillate a little/℃ | 70 | 72 | 69 | 70 |
| 50 volume % distillate a little/℃ | 90 | 94 | 91 | 92 |
| 70 volume % distillate a little/℃ | 121 | 122 | 122 | 120 |
| 90 volume % distillate a little/℃ | 163 | 162 | 162 | 163 |
From the data of table 5, can find out, compare with 2 with comparative example 1, adopt in the embodiment 1-2 of method for transformation of the present invention, in gasoline products, the content of alkene and the content of sulphur obviously decline, the content of aromatic hydrocarbons and isoparaffin significantly increases, this shows, the quality of the gasoline products obtaining is significantly improved.
In sum, conversion method for hydrocarbon oil provided by the invention not only can improve the productive rate of ethene and propylene significantly, can also make the content of alkene and the content of sulphur in reacted gasoline oil reduce significantly, has improved the quality of product gasoline.
Claims (11)
1. a conversion method for hydrocarbon oil, is characterized in that, the method comprises:
(1) pre-lift medium, gasoline stocks and regenerated catalyst and/or half regenerated catalyst are sent into the lower reaction zone of riser reactor, at the temperature of 600-750 ℃, carry out contact reacts, the oil gas of generation and reacted catalyzer are upwards sent into the reaction zone, top of riser reactor;
(2) diesel raw material and regenerated catalyst are sent into the reaction zone, top of riser reactor, at the temperature of 500-650 ℃, made described diesel raw material, regenerated catalyst and carry out contact reacts from the oil gas of lower reaction zone together with catalyzer;
(3) mixture at the reacted oil gas in reaction zone, top and catalyzer is carried out to finish separated, the oil gas after finish separation is sent to subsequent separation system separating reaction product, and the catalyzer after gas-oil separation obtains reclaimable catalyst after stripping;
(4) described reclaimable catalyst is carried out to coke burning regeneration, obtain regenerated catalyst, or in the regenerating unit containing the first revivifier and Second reactivator, carry out coke burning regeneration, from the first revivifier and Second reactivator, obtain respectively half regenerated catalyst and regenerated catalyst;
(5) lower reaction zone of the regenerated catalyst obtaining and/or half regenerated catalyst being returned to riser reactor recycles, and/or the reaction zone, top that the regenerated catalyst obtaining returns to riser reactor is recycled.
2. method according to claim 1, wherein, described gasoline stocks contacts with regenerated catalyst, and catalytic temperature is 700-730 ℃.
3. method according to claim 1 and 2, wherein, described gasoline stocks is 100-450 kPa with the pressure contacting of regenerated catalyst and/or half regenerated catalyst, the time of contact is 0.1-10 second.
4. method according to claim 1, wherein, the weight ratio of described regenerated catalyst and/or half regenerated catalyst and gasoline stocks is 2-30: 1.
5. method according to claim 1, wherein, described diesel raw material and the pressure contacting of regenerated catalyst are that 130-450 kPa, time of contact are 0.1-10 second.
6. method according to claim 1, wherein, the weight ratio of described regenerated catalyst and diesel raw material is 2-25: 1.
7. method according to claim 1, wherein, the weight ratio of described diesel raw material and gasoline stocks is 0.1-10: 1.
8. method according to claim 7, wherein, described diesel raw material and the weight ratio of gasoline stocks are 0.2-5: 1.
9. method according to claim 1, wherein, described gasoline stocks is one or more in coker gasoline, straight-run spirit, catalytic gasoline, pressure gasoline and reforming raffinate oil.
10. method according to claim 1, wherein, described diesel raw material is one or more in straight-run diesel oil, catalytic diesel oil, thermally splitting diesel oil, hydrotreatment diesel oil, hydrofining diesel oil, hydrocracking diesel oil.
11. methods according to claim 1, wherein, described catalyzer is the cracking catalyst that contains molecular sieve, described molecular sieve for containing or not phosphorus element-containing y-type zeolite, containing or not containing the ultrastable Y－type zeolite of rare earth element, containing or one or more in the supersiliceous zeolite with five-membered ring structure, β zeolite, mordenite, omega zeolite of phosphorus element-containing not.
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| CN101531558A (en) * | 2008-03-13 | 2009-09-16 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing propylene and aromatic hydrocarbons |
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