CN103525458B - Catalytic conversion method - Google Patents

Abstract

The invention discloses a catalytic conversion method. The method comprises the following steps: carrying out aromatic saturation reaction by employing contact of a distillate raw material of which the distillation range is 160-400 DEG C with hydrogen and an aromatic hydrogenated saturated catalyst, and separating to obtain hydrogenated distillate; contacting the hydrogenated distillate with a catalytic cracking catalyst; carrying out catalytic cracking reaction under the conditions that the temperature is 400-750 DEG C, the weight hourly space velocity is 0.1-100 h<-1>, the reaction pressure is 0.10-1.0 MPa, the weight ratio of the catalyst to the raw material is 1-100, and the weight ratio of vapor to the raw material is 0.02-1.0; separating a reaction oil gas from a to-be-produced catalytic cracking catalyst; separating the reaction oil gas to obtain a gasoline product containing aromatic hydrocarbon, and recycling the to-be-produced catalytic cracking catalyst after gas stripping and regenerating. The gasoline fraction produced by the method can be used as a raw material for producing the aromatic hydrocarbon, and also can be used as a high-octane petrol blending component; no heavy oil or a little heavy oil is generated; the coke yield is low; the requirements of catalytic cracking thermal balance can be maintained.

Description

A kind of catalysis conversion method

Technical field

The invention belongs to the catalysis conversion method of petroleum hydrocarbon, more particularly, relate to the catalysis conversion method that the aromatic type gasoline being rich in benzene,toluene,xylene produced by distillate.

Background technology

Benzene in aromatic hydrocarbons, toluene and dimethylbenzene (being called for short BTX) are the basic materials of chemical technology, benzene can be used for the products such as synthesizing styrene, phenol and aniline, the fine solvent of organic synthesis is not only by toluene, and can synthesizing isocyanate and cresols product, in dimethylbenzene, paraxylene, ortho-xylene and meta-xylene are all good industrial chemicals.The main production of BTX aromatic hydrocarbons comprises naphtha catalytic reforming process, preparing ethylene by steam cracking by-product BTX, toluene disproportionation and transalkylation, light-hydrocarbon aromatized technology etc., because BTX demand is still vigorous, therefore how expanding BTX source is still one of target of technical development pursuit.

Along with the development of society, while providing diesel cetane-number, reduction derv fuel arene content and sulfur content have become the important indicator of environmental protect quality.Europe V derv fuel standard-required sulfur content not higher than 10 micrograms/gram, polycyclic aromatic hydrocarbon volume fraction is not higher than 11%, and Cetane number at least reaches 46.But the diesel oil that catalytic cracking is produced, especially diesel oil that inferior raw material is produced is rich in aromatic hydrocarbons, can up to 50%-75%, and mononuclear aromatics content is at 19-25%, and aromatic hydrocarbons Cetane number is very low, and the more Cetane number of aromatic ring are lower.Therefore, catalytic diesel oil often needs deep hydrogenation upgrading could dispatch from the factory as diesel oil blending component.In fact, for double ring arene naphthalene class, though dicyclo completely saturated be after decahydronaphthalene compounds, Cetane number still only can reach about 30.And deep hydrogenation upgrading is invested and operating cost is high, and yield is relatively low.Therefore the how cost-effective problem utilizing catalytic diesel oil Shi Ge research unit and enterprise's primary study always.

CN101559380A discloses a kind of catalyst and the preparation method that produce BTX aromatic hydrocarbons and clean gasoline for catalytic gasoline, the percentage by weight of this catalyst component is rare earth metal 0.05-3.0%, alkaline-earth metal 3-20%, IIB B metal 0.1-15%, molecular sieve 10-80%, Al ₂o ₃surplus.Used is the gasoline components such as catalytically cracked gasoline, direct steaming gasoline and coking naphtha originally.

CN101348405A discloses a kind of method utilizing hydrocarbon raw material to prepare light aromatics and light paraffins.The method be by adopt reformate, drippolene, containing C9+(carbon nine and more than) mixture of aromatic hydrocarbons, naphtha and their mixture be that raw material carries out hydrogenation lighting process, make heavy arene that de-alkyl and transalkylation reaction occur, and the reaction such as light aromatics generation isomerization is converted into the component being rich in BTX light aromatics, catalyst used contains the modenite, Β type zeolite, Y zeolite, at least one in ZSM-5 or ZSM-11 type zeolite that are selected from least one in Pt or Pd and are selected from binder free.

US4577050 discloses a kind of method of ZSM-5/ZSM-12 catalyst mixture cracking alkylbenzene.The raw materials used diisopropylbenzene (DIPB) comprising at least 50 heavy % of the method, the benzene,toluene,xylene of at least 5 heavy % and ethylo benzene hydrocarbon mixture, used catalyst is the ZSM-12 mixed molecular sieve catalyst of the heavy % of the heavy %-90 of ZSM-5 and 10 of the heavy % of 10 heavy %-90.

US5685972 discloses a kind of method producing BTX from cat cracked naphtha.The raw materials used cat cracked naphtha of the method and coking naphtha, the preferred ZSM-5 of used catalyst or with hydrogenating function component (as molybdenum etc.) catalyst.

CN101747928A discloses the catalysis conversion method of a kind of preparing low-carbon olefins and aromatic hydrocarbons, the method is that the differential responses district feedstock oil of different cracking performance being entered the first riser reactor contacts with catalytic cracking catalyst and carries out cracking reaction, be separated reclaimable catalyst and reaction oil gas, wherein reaction oil gas be isolated to comprise low-carbon alkene, gasoline, boiling range be the 180 DEG C ~ cut of 250 DEG C and the product of catalytic wax oil, wherein gasoline obtains light aromatic hydrocarbons through light Aromatics Extractive Project and gasoline is raffinated oil; Cracked stock is sent in the second riser reactor again, contacts with hot regenerated catalyst, carries out catalyzed conversion, and the reclaimable catalyst of two riser reactors returns two riser reactors respectively in same regenerator after coke burning regeneration.The method produces the low-carbon alkene such as propylene, ethene to greatest extent from heavy charge, and its productive rate can weigh % more than 40, simultaneously the aromatic hydrocarbons such as coproduction toluene and dimethylbenzene.

CN101362961A discloses the catalysis conversion method of a kind of preparing aromatic hydrocarbon and low-carbon alkene.The method is that the raw material of 160 DEG C-260 DEG C contacts with catalytic cracking catalyst, at temperature 450 DEG C-750 DEG C, weight (hourly) space velocity (WHSV) 0.1h by boiling range ^-1-800h ^-1, reaction pressure 0.10MPa-1.0MPa, catalytic cracking catalyst and raw material weight ratio 1-150, the weight ratio of water vapour and raw material is under 0.05-1.0 condition, cracking reaction is carried out in fluidized-bed reactor, be separated reclaimable catalyst and reaction oil gas, reclaimable catalyst is Returning reactor after regeneration, and separating reaction oil gas is isolated to object product low-carbon alkene and aromatic hydrocarbons.The method ethene, productivity of propylene and selectively significantly to increase, the yield of gasoline and the productive rate of Aromatic Hydrocarbon in Gasoline all very high, only have a small amount of heavy oil to generate, and coke yield is lower.

Although CN101747928A and CN101362961A to some extent solves a part of catalytic diesel oil and can produce aromatic hydrocarbons, heavy distillat sulfur content and the arene content of the production such as catalytic cracking unit are still very high, still need further process.In general, the order of aromatic hydrogenation saturated activity is followed successively by polycyclic aromatic hydrocarbon > double ring arene > mononuclear aromatics.For catalytic cracking, mononuclear aromatics and cycloalkane are extraordinary raw materials, have stronger catalyzed conversion active, and after reaction, gasoline products has the advantages that productive rate is high, octane number is high and be rich in BTX product.In addition, in catalytic cracking process and hydrogenation process, in diesel oil, sulphur can shift further as hydrogen sulfide gas.

Summary of the invention

The object of this invention is to provide and a kind ofly produce the catalysis conversion method being rich in BTX aromatic type gasoline from distillate.

Provided by the inventionly produce from distillate the catalysis conversion method being rich in BTX aromatic type gasoline and comprise the following steps:

(1) boiling range be 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably the distillate feedstock of 250 DEG C-350 DEG C contact with hydrogen, hydrocatalyst for saturating arylhydrocarbon, at reaction temperature 250 DEG C-500 DEG C, hydrogen dividing potential drop 3-15MPa, volume space velocity 0.1-10h ^-1, hydrogen to oil volume ratio 300-2000Nm ³/ m ³condition under carry out aromatic saturation reaction, be isolated to hydrogenation distillate;

(2) hydrogenation distillate contacts with catalytic cracking catalyst, at temperature 400 DEG C-750 DEG C, weight (hourly) space velocity (WHSV) 0.1-100h ^-1, reaction pressure 0.10MPa-1.0MPa, the weight ratio 1-100 of catalyst and raw material, water vapour and raw material weight ratio be carry out catalytic cracking reaction under 0.02-1.0 condition, reaction oil gas is separated with catalytic cracking catalyst to be generated, wherein reaction oil gas is isolated to the product comprising the gasoline being rich in BTX aromatic hydrocarbons, and catalytic cracking catalyst to be generated uses through stripping, regeneration Posterior circle.

Step (2) the gained reaction oil gas of the method can be isolated to conventional products as dry gas, liquefied gas, the gasoline being rich in BTX aromatic hydrocarbons, diesel oil, heavy oil etc., also can be separated as required and obtain dry gas, liquefied gas, the gasoline being rich in BTX aromatic hydrocarbons, boiling range are 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably products such as cut of 250 DEG C-350 DEG C, wherein boiling range be 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably the cut of 250 DEG C-350 DEG C return step (1) remove hydrogenation together with raw material.

The gasoline that step (2) gained of the method is rich in BTX aromatic hydrocarbons can obtain BTX aromatic hydrocarbon product through solvent extraction further.The solvent of extracting is selected from one or more the above mixtures in sulfolane, methyl-sulfoxide, N-formyl-morpholine, tetraethylene glycol, triethylene glycol and 1-METHYLPYRROLIDONE; the temperature of solvent extraction is 40-120 DEG C, and the volume ratio between solvent and solvent extraction raw material is 2-6.

Described distillate feedstock be selected from boiling range be 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably 250 DEG C-350 DEG C time processing oil, one or more in secondary operations oil, wherein time processing oil for boiling range be 160 DEG C 400 DEG C preferably 180 DEG C-350 DEG C more preferably atmospheric and vacuum distillation unit cuts of 250 DEG C-350 DEG C, secondary operations grease separation is 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably catalytic cracking product cuts of 250 DEG C-350 DEG C from boiling range, coke chemicals cut, residual hydrogenation equipment product cut, Wax Oil Hydrogenation Unit product cut, Diesel Oil Hydrofining Unit cut, hydrocracking unit cut, thermal cracking diesel oil, coal liquefaction diesel oil, coal liquefaction heavy distillat, shale oil cut, one or more in biodiesel cut.

This distillate feedstock has the advantages that to be rich in aromatic hydrocarbons, especially double ring arene is rich in 250 DEG C of-350 DEG C of distillates, this distillate can obtain the distillate being rich in mononuclear aromatics and/or being rich in cycloalkane after hydrogenation, and be extraordinary catalytically cracked material, reactivity worth is better than existing convenient source.

Described catalytic cracking catalyst comprises zeolite, inorganic oxide and optional clay, and each component accounts for total catalyst weight respectively: zeolite 1-50 heavy %, inorganic oxide 5-99 heavy %, surplus clay.

Its mesolite, as active component, is selected from large pore zeolite or/and mesopore zeolite.

The preferred ZSM series zeolite of mesopore zeolite and/or ZRP zeolite, also modification can be carried out to transition metals such as the nonmetalloids such as above-mentioned mesopore zeolite phosphorus and/or iron, cobalt, nickel, about the more detailed description of ZRP is see US5,232,675, ZSM series zeolite is selected from one or more the mixture among the zeolite of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and other similar structures, about the more detailed description of ZSM-5 is see US3,702,886.

The preferred free Rare Earth Y of large pore zeolite (REY), rare earth hydrogen Y(REHY), one or more mixture in this group zeolite of forming of the distinct methods super steady Y, the high silicon Y that obtain.

Inorganic oxide, as bonding agent, is selected from silica (SiO ₂) and/or alundum (Al2O3) (Al ₂o ₃).

Clay, as matrix (i.e. carrier), is selected from kaolin and/or halloysite.

Described hydrocatalyst for saturating arylhydrocarbon is selected from VI B race and/or group VIII metal for active component, with aluminium oxide or silicon-containing alumina for carrier.With the gross weight of hydrofinishing agent for benchmark, and with oxide basis, group vib metal is Mo and/or W, preferred content 10-50%; Group VIII metal be Ni or/and Co, preferred content 0.5-7%.Preferred Ni-Mo, Ni-W or Ni-W-Mo class hydrogenation catalyst.

Described catalyst cracker be selected from riser, etc. the fluid bed of linear speed, isodiametric fluid bed, upstriker pipeline, the combination of one or both serial or parallel connections of downstriker pipeline.Riser can be conventional isodiametric riser, also can be the riser of various forms reducing.Wherein the gas speed of fluid bed is 0.1-2 meter per second, and the gas speed of riser is 2 meter per second-30 meter per seconds (disregarding catalyst).

Described hydrogenation aromatic saturation condition is preferably: reaction temperature 300-450 DEG C, hydrogen dividing potential drop 6-10MPa, volume space velocity 0.2-5h ^-1, hydrogen to oil volume ratio 500-1000Nm ³/ m ³.

Described catalytic cracking reaction condition is preferably: temperature 500-700 DEG C, weight (hourly) space velocity (WHSV) 0.5-50h ^-1, reaction pressure 0.2-0.8MPa, catalyst and raw material weight ratio 4-15, the weight ratio of water vapour and raw material is 0.03-0.4.

Described gasoline light fraction is selected from the end point of distillation≤180 DEG C, the preferred end point of distillation≤160 DEG C.

The present invention compared with prior art has following unforeseeable technique effect:

1, the gasoline fraction produced is rich in BTX, can be used as the raw material producing BTX aromatic hydrocarbons, also can be used as high-knock rating gasoline blend component;

2, only have a small amount of heavy oil generate or do not produce heavy oil, and coke yield is lower, can maintain catalytic cracking thermal balance needs.

Accompanying drawing explanation

Fig. 1 provided by the inventionly produces the catalysis conversion method schematic flow sheet being rich in BTX aromatic type gasoline.

Fig. 2 is the catalysis conversion method schematic flow sheet producing BTX aromatic hydrocarbons provided by the invention.

Detailed description of the invention

Below in conjunction with accompanying drawing, preferred forms provided by the present invention is further described.

Fig. 1 is that the catalysis conversion method schematic flow sheet being rich in BTX aromatic type gasoline produced by distillate provided by the invention.

Technological process is as follows:

Boiling range be 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably the distillate of 250 DEG C-350 DEG C enter hydrogenation plant 10 through pipeline 11, obtain hydrogenation distillate and draw as catalytic cracking unit raw material through pipeline 12.

Pre-lift medium enters by bottom riser reactor 2 through pipeline 1, from the regenerated catalyst of regenerator sloped tube 9 under the castering action of pre-lift medium along riser upwards accelerated motion, hydrogenation distillate is through pipeline 3 injecting lift pipe 2 together with the atomizing steam from pipeline 4, mix with the existing logistics of riser reactor, cracking reaction is there is in raw material on the catalyst of heat, and upwards accelerated motion.The reaction oil gas generated and the reclaimable catalyst of inactivation enter the cyclone separator in settler 5, realize being separated of reclaimable catalyst and reaction oil gas, reaction oil gas enters subsequent separation system 13 through pipeline 6, separation obtains dry gas, liquefied gas is respectively through pipeline 14, 15 draw, the gasoline being rich in BTX aromatic hydrocarbons is drawn through pipeline 16, the products such as diesel oil are drawn through pipeline 17, heavy oil is drawn through pipeline 18, catalyst fines returns settler 5 stripping section by dipleg and carries out steam stripping, the oil gas that stripping goes out from reclaimable catalyst enters subsequent separation system after cyclone separator, reclaimable catalyst after stripping enters regenerator 8 through inclined tube 7 to be generated and to contact coke on burning-off reclaimable catalyst with the air from pipeline 19, the reclaimable catalyst of inactivation is regenerated, flue gas draws regenerator through pipeline 20, catalyst after regeneration enters riser reactor 2 through regenerator sloped tube 9 and recycles.

Fig. 2 is the catalysis conversion method schematic flow sheet that BTX aromatic hydrocarbons produced by distillate provided by the invention.

Technological process is as follows:

Boiling range be 160 DEG C-400 DEG C preferably 180 DEG C-350 DEG C more preferably the distillate of 250 DEG C-350 DEG C enter hydrogenation plant 10 ' through pipeline 11 ', obtain hydrogenation distillate and draw as catalytic cracking unit raw material through pipeline 12 '.

Pre-lift medium is entered by riser reactor 2 ' bottom through pipeline 1 ', from the regenerated catalyst of regenerator sloped tube 9 ' under the castering action of pre-lift medium along riser upwards accelerated motion, hydrogenation distillate is through pipeline 3 ' injecting lift pipe 2 ' together with the atomizing steam from pipeline 4 ', mix with the existing logistics of riser reactor, cracking reaction is there is in raw material on the catalyst of heat, and upwards accelerated motion.The reaction oil gas generated and the reclaimable catalyst of inactivation enter the cyclone separator in settler 5 ', realize reclaimable catalyst and generate being separated of oil gas, generation oil gas enters subsequent separation system 13 ' through pipeline 6 ' and obtains dry gas, liquefied gas, gasoline light fraction, gasoline heavy distillat, diesel oil, heavy oil is respectively through pipeline 20 ', 21 ', 15 ', 22 ', 23 ', 24 ' extraction (or by gasoline heavy distillat, diesel oil and heavy oil three kinds of cuts merge draws, hydrogenation plant 10 ' can be entered) through pipeline 25 ', wherein gasoline light fraction is sent into extraction device 14 ' and is obtained benzene, toluene and xylene product are respectively through pipeline 16 ', 17 ' and 18 ' draws, light fraction is raffinated oil and to be drawn through pipeline 19 '.

Catalyst fines returns settler 5 ' stripping section by dipleg and carries out steam stripping, the oil gas that stripping goes out from reclaimable catalyst enters subsequent separation system after cyclone separator, reclaimable catalyst after stripping enters regenerator 8 ' through inclined tube 7 ' to be generated and to contact coke on burning-off reclaimable catalyst with the air from pipeline 26 ', the reclaimable catalyst of inactivation is regenerated, flue gas draws regenerator through pipeline 27 ', and the catalyst after regeneration enters riser reactor through regenerator sloped tube 9 ' and recycles.

The following examples will be further described this method, but therefore not limit this method.

Feedstock property used in embodiment and comparative example is as shown in table 1,2.In embodiment and comparative example catalytic cracking catalyst trade names used be MLC-500 and, MMC-2 and CGP-1, hydrocatalyst for saturating arylhydrocarbon trade names are RIC-1, and by Sinopec catalyst, branch company produced.

Embodiment 1

The present embodiment illustrates and adopts method provided by the invention, and carry out at kitty cracker and medium-sized hydrogenation plant, flow process is with reference to figure 1.

First distillate (raw material A) is sent into medium-sized hydrogenation plant and carry out aromatic hydrogenation saturated reaction, obtain hydrogenating materials C, hydrogenating materials C feeding kitty cracker carries out system and is rich in the reaction of BTX aromatic type gasoline, catalytic cracking catalyst is MLC-500, operating condition and product slates list in table 3, and gasoline property lists in table 4.

Comparative example 1

Distillate (raw material A) elected as by catalytic cracking reaction feedstock oil compared with embodiment 1, and raw material A is sent into kitty cracker and reacted, and catalyst is MLC-500, and operating condition and product slates list in table 3, and gasoline property lists in table 4.

As can be seen from Table 3, compared with comparative example, embodiment 1 gasoline yield reaches 70.8 heavy %, and increase by 56.7 percentage points, increasing degree is up to 402.1%.As can be seen from Table 4, embodiment 1 is produced gasoline and is had the advantages that to be rich in BTX, and wherein the mass fraction of benzene is 1.0 heavy %, and the mass fraction of toluene is 12.6 heavy %, and the mass fraction of dimethylbenzene is 22.3 heavy %.

Embodiment 2

The present embodiment illustrates and adopts method provided by the invention, and carry out at kitty cracker and medium-sized hydrogenation plant, flow process is with reference to figure 1.

First distillate (raw material A) is sent into medium-sized hydrogenation plant and carry out aromatic hydrogenation saturated reaction, obtain hydrogenating materials B, hydrogenating materials B feeding kitty cracker carries out system and is rich in the reaction of BTX aromatic type gasoline, catalytic cracking catalyst is MMC-2, operating condition and product slates list in table 3, and gasoline property lists in table 4.

As can be seen from Table 3, gasoline yield is 34.1%.As can be seen from Table 4, produce gasoline and have the advantages that to be rich in BTX, wherein the mass fraction of benzene is 4.1 heavy %, and the mass fraction of toluene is 15.5 heavy %, and the mass fraction of dimethylbenzene is 18.3 heavy %.

Embodiment 3

The present embodiment illustrates and adopts method provided by the invention, and carry out at kitty cracker, medium-sized hydrogenation plant and medium-sized extraction device, flow process is with reference to figure 2.

First distillate (raw material D) is sent into medium-sized hydrogenation plant and carry out aromatic hydrogenation saturated reaction, obtain hydrogenating materials E, hydrogenating materials E sends into kitty cracker and carries out catalytic cracking reaction, catalytic cracking catalyst is CGP-1, extraction device is sent in the gasoline light fraction (end point of distillation 160 DEG C) produced, and operating condition and product slates list in table 5.

As can be seen from Table 5, the productive rate of benzene is 1.7 heavy %, and the productive rate of toluene is 11.5 heavy %, and the productive rate of dimethylbenzene is 17.2 gross production rates weighing %, BTX products is 30.4 heavy %.

Embodiment 4

The present embodiment illustrates and adopts method provided by the invention, and carry out at kitty cracker, medium-sized hydrogenation plant and medium-sized extraction device, flow process is with reference to figure 2.

First distillate (raw material D) is sent into medium-sized hydrogenation plant and carry out aromatic hydrogenation saturated reaction, obtain hydrogenating materials E, hydrogenating materials E sends into kitty cracker and carries out catalytic cracking reaction, catalytic cracking catalyst is CGP-1, extraction device is sent in the gasoline light fraction (end point of distillation 160 DEG C) produced, gasoline heavy distillat, diesel oil and heavy oil three kinds of cuts merging return hydrogenation plant, and operating condition and product slates list in table 5.

As can be seen from Table 5, the productive rate of benzene is 1.9 heavy %, and the productive rate of toluene is 13.0 heavy %, and the productive rate of dimethylbenzene is 19.7 gross production rates weighing %, BTX products is 34.6 heavy %.

Table 1

Feedstock oil character	Distillate	Hydrogenation distillate	Hydrogenation distillate
				Feedstock oil is numbered	A	B	C
Density (20 DEG C), g/cm 3	0.978	0.904	0.856
				Sulfur content, microgram/gram	2500	15	3
Mass spectrum forms, w%
				Alkane	7.5	12.4	13.3
Cycloalkane	2.6	29.9	69.7
				Total aromatic hydrocarbons	89.9	57.7	17.0
Mononuclear aromatics	11.7	50.3	15.1
				Boiling range, DEG C (ASTM D2887)
Initial boiling point	250	180	150
				5%	254	221	191
50%	300	272	250
				95%	332	300	283
The end point of distillation	345	330	321

Table 2

Feedstock oil character	Distillate	Hydrogenation distillate
			Feedstock oil is numbered	D	E
Density (20 DEG C), g/cm 3	0.945	0.898
			Sulfur content, microgram/gram	1700	10
Mass spectrum forms, w%
			Alkane	9.5	13.2
Cycloalkane	3.1	30.9
			Total aromatic hydrocarbons	87.4	55.9
Mononuclear aromatics	24.3	53.1
			Boiling range, DEG C (ASTM D2887)
Initial boiling point	180	152
			5%	199	168
50%	265	244
			95%	341	318
The end point of distillation	356	345

Table 3

	Embodiment 1	Comparative example 1	Embodiment 2
				Feedstock oil is numbered	C	A	B
Catalytic cracking unit
				Reaction temperature, DEG C	515	515	510
Reaction pressure, MPa	0.3	0.3	0.3
				Oil ratio, m/m	5.0	5.0	8.0
Water vapour/raw material weight ratio	0.05	0.05	0.05
				The catalyst trade mark	MLC-500	MLC-500	MMC-2
Micro-activity	66	66	60
				Aromatic hydrogenation saturation unit
Reaction temperature, DEG C	330	/	350
				Hydrogen dividing potential drop, MPa	9.0	/	10.0
Volume space velocity, h -1	1.5	/	1.0
				Hydrogen to oil volume ratio, Nm 3/m 3	500	/	500
Product slates, heavy %
				Dry gas	1.6	2.8	2.7
Liquefied gas	14.5	10.1	20.7
				Gasoline	70.8	14.1	34.1
Diesel oil	11.6	43.8	40.1
				Heavy oil	0.0	20.3	0.8
Coke	1.5	8.9	1.6
				Add up to	100.0	100.0	100.0

Table 4

Gasoline forms, heavy %	Embodiment 1	Comparative example 1	Embodiment 2
				N-alkane	2.7	2.4	2.8
Isoparaffin	19.8	9.6	15.1
				Alkene	7.0	9.6	11.2
Cycloalkane	17.6	8.3	7.9
				Aromatic hydrocarbons	52.9	70.1	63.0
Benzene	1.0	1.2	4.1
				Toluene	12.6	4.2	15.5
Dimethylbenzene	22.3	10.8	18.3
				Amount to	100.0	100.0	100.0

Table 5

	Embodiment 3	Embodiment 4
			Feedstock oil is numbered	E	E
Catalytic cracking unit
			Reaction temperature, DEG C	590	575
Reaction pressure, MPa	0.25	0.25
			Oil ratio, m/m	6.0	6.0
Water vapour/raw material weight ratio	0.04	0.05
			The catalyst trade mark	CGP-1	CGP-1
Micro-activity	67	67
			Aromatic hydrogenation saturation unit
Reaction temperature, DEG C	320	320
			Reaction pressure, MPa	10.0	10.0
Volume space velocity, h -1	1.6	1.8
			Hydrogen to oil volume ratio, Nm 3/m 3	500	500
BTX extracting rectification unit
			Extraction solvent	Sulfolane	Sulfolane
Extraction temperature, DEG C	70	70
			Oil ratio, m/m	4.5	4.5
Product slates, heavy %
			Dry gas	2.8	2.6
Liquefied gas	25.1	27.0
			Benzene	1.7	1.9
Toluene	11.5	13.0
			Dimethylbenzene	17.2	19.7
Gasoline	29.9*	33.8**
			Diesel oil	9.5	0.0
Heavy oil	0.2	0.0
			Coke	2.1	2.0
Add up to	100.0	100.0

* gasoline light fraction is raffinated oil+heavy petrol

The light fraction of * gasoline is raffinated oil.

Claims (9)

1. a catalysis conversion method, is characterized in that the method comprises the following steps:

(1) boiling range is that the distillate feedstock of 160 DEG C-400 DEG C contacts with hydrogen, hydrocatalyst for saturating arylhydrocarbon, at reaction temperature 250 DEG C-500 DEG C, hydrogen dividing potential drop 3-15MPa, volume space velocity 0.1-10h ^-1, hydrogen to oil volume ratio 300-2000Nm ³/ m ³condition under carry out aromatic saturation reaction, be isolated to hydrogenation distillate;

(2) hydrogenation distillate contacts with catalytic cracking catalyst, at temperature 400 DEG C-750 DEG C, weight (hourly) space velocity (WHSV) 0.1-100h ^-1, reaction pressure 0.10MPa-1.0MPa, the weight ratio 1-100 of catalyst and raw material, water vapour and raw material weight ratio be carry out catalytic cracking reaction under 0.02-1.0 condition, reaction oil gas is separated with catalytic cracking catalyst to be generated, wherein reaction oil gas is isolated to the product comprising the gasoline being rich in aromatic hydrocarbons, and catalytic cracking catalyst to be generated uses through stripping, regeneration Posterior circle.

2. method according to claim 1, is characterized in that step (2) gained reaction oil gas is isolated to dry gas, liquefied gas, the gasoline being rich in aromatic hydrocarbons, diesel oil, heavy oil.

3. method according to claim 1, it is characterized in that the cut that step (2) gained reaction oil gas is isolated to dry gas, liquefied gas, the gasoline being rich in aromatic hydrocarbons, boiling range are 160 DEG C-400 DEG C, wherein boiling range is that the cut of 160 DEG C-400 DEG C returns step (1) remove hydrogenation together with raw material.

4. method according to claim 1, it is characterized in that described distillate feedstock is selected from the time processing oil that boiling range is 160 DEG C-400 DEG C, one or more in secondary operations oil, wherein time processing oil for boiling range be the atmospheric and vacuum distillation unit cut of 160 DEG C-400 DEG C, secondary operations grease separation is the catalytic cracking product cut of 160 DEG C-400 DEG C from boiling range, coke chemicals cut, residual hydrogenation equipment product cut, Wax Oil Hydrogenation Unit product cut, Diesel Oil Hydrofining Unit cut, hydrocracking unit cut, thermal cracking diesel oil, coal liquefaction diesel oil, coal liquefaction heavy distillat, shale oil cut, one or more in biodiesel cut.

5. the method according to claim 1 or 4, is characterized in that the boiling range of described distillate feedstock is 180 DEG C-350 DEG C.

6. method according to claim 1; it is characterized in that the gasoline that step (2) gained is rich in BTX aromatic hydrocarbons obtains BTX aromatic hydrocarbon product through solvent extraction; the solvent of extracting is selected from one or more the above mixtures in sulfolane, methyl-sulfoxide, N-formyl-morpholine, tetraethylene glycol, triethylene glycol and 1-METHYLPYRROLIDONE; the temperature of solvent extraction is 40-120 DEG C, and the volume ratio between solvent and solvent extraction raw material is 2-6.

7. method according to claim 1, it is characterized in that described catalytic cracking catalyst comprises zeolite, inorganic oxide and optional clay, each component accounts for total catalyst weight respectively: zeolite 1-50 heavy %, inorganic oxide 5-99 heavy %, surplus clay.

8. method according to claim 1, is characterized in that catalytic cracking reaction condition is: temperature 500-700 DEG C, weight (hourly) space velocity (WHSV) 0.5-50h ^-1, reaction pressure 0.2-0.8MPa, catalyst and raw material weight ratio 4-15, the weight ratio of water vapour and raw material is 0.03-0.4.

9. method according to claim 1, is characterized in that described hydrogenation aromatic saturation condition is: reaction temperature 300-450 DEG C, hydrogen dividing potential drop 6.0-10MPa, volume space velocity 0.2-5h ^-1, hydrogen to oil volume ratio 500-10000Nm ³/ m ³.