CN103102979B - Method for producing light fuel oil from ethylene tar - Google Patents

Abstract

The invention discloses a method for producing light fuel oil from ethylene tar. The method is as below: fractionating ethylene tar into a light fraction and a heavy fraction; mixing the heavy fraction with a conventional coking raw material, and subjecting the mixture to delayed coking to obtain coker gasoline, coker diesel and coker gas oil; mixing the coker gasoline and the coker diesel with the light fraction of the ethylene tar, and subjecting the mixture to a hydrofining reaction; distilling the product to obtain a gasoline fraction I and a fraction heavier than the gasoline; subjecting the fraction heavier than the gasoline to a hydrogenation treatment to obtain light fuel oil, and distilling to obtain a gasoline fraction II and a diesel product; and mixing the gasoline fraction I and the gasoline fraction II to obtain a final gasoline product. The method provided by the invention utilizes the characteristics of high contents of ethylene tar aromatic hydrocarbons, colloid, carbon residue and glial and asphaltene of ethylene tar to fractionate the ethylene tar into the light fraction and the heavy fraction; different processing methods are employed to improve the added value of ethylene tar, increase yield of gasoline and diesel, improve product quality of light fuel oil and realize long-period stable operation of devices.

Description

A kind of ethylene bottom oil produces the method for light-weight fuel oil

Technical field

The present invention relates to a kind of method that ethylene bottom oil produces light-weight fuel oil, specifically a kind of delayed coking of blending ethylene tar and the combined technical method of hydrogenation.

Background technology

The scarcity day by day of world petroleum resource and the day by day raised of price thereof, make refinery reduce discharging synergy and necessitate, ethylene bottom oil is sold mainly as heavy fuel oil (HFO) or carbon black raw material at present, and added value is lower.

Ethylene bottom oil be ethylene cracking material at steam-cracking process Raw and product pyrocondensation product, its initial boiling point is at 170 ~ 260 DEG C, and final boiling point > 600 DEG C, is generally 600 ~ 700 DEG C, belongs to last running scope.The mixture of the ethylene bottom oil mainly above condensed-nuclei aromatics of dicyclo, aromaticity content reaches more than 90%, and density (20 DEG C) is greater than 1.0 g/cm ³, the foreign matter content such as sulphur and nitrogen is low, substantially not metal impurities.

In order to increase economic efficiency, multiple method of comprehensive utilization developed by each refinery, such as extracts naphthalene and series product thereof, light constituent (<300 DEG C) synthesizing petroleum resin, tar heavy oil produce carbon fibre asphalt and gac etc. is produced in carbon fiber, >540 DEG C last running.Still have some intermediate oils not to be fully used in aforesaid method, overall economic efficiency needs to be further improved.

Method disclosed in CN1970688A ethylene bottom oil is cut out the lighting end that boiling point is less than 260 ~ 280 DEG C, the unsaturated hydro carbons in this lighting end is removed again by hydrorefined method, and then therefrom extract naphthalene and methylnaphthalene product, a small amount of solvent oil product of by-product simultaneously.The method only make use of the lighting end that in ethylene bottom oil, proportion is little, still have an appointment more than 80% ethylene bottom oil cut be not effectively addressed; Simultaneously its Hydrofinishing conditions provided cannot process boiling point higher than the ethylene bottom oil cut of 280 DEG C.

The report carrying out delayed coking about vacuum residuum blending ethylene tar has: CN101608132A, " Responds Surface Methodology optimizes the delayed coking research of blending ethylene pyrolysis fuel oil " is (see " refining of petroleum and chemical industry " the 8th phase P5-P8 in 2009, " delayed coking unit mixes the research of refining grand celebration pyrolysis fuel oil " (see " refining of petroleum and chemical industry " the 12nd phase P20-P22 in 2007), " blending ethylene cracking masout is on the impact of delayed coking " (see " petrochemical technology and application " the 1st phase P44-P49 in 2010) and " Coking Test of Vacuum Residue with Ethylene Heavy Tar " are (see " Maoming College's journal " the 1st phase P7-P9 in 2008 etc., these researchs are all complete for ethylene bottom oil cut and vacuum residuum are mixed to refine as delayed coking raw material, the yield of liquid yield and light Fuel oil production can be made so lower, and its gained liquid product---coker gasoline, the quality of diesel oil and wax oil is still poor, also need further processing treatment.

Summary of the invention

In order to overcome deficiency of the prior art, the invention provides a kind of method that ethylene bottom oil utilization ratio is high, petrol and diesel oil fuel output is high, the measured ethylene bottom oil of matter produces light-weight fuel oil.

Ethylene bottom oil provided by the invention produces the method for light-weight fuel oil, comprise: ethylene bottom oil is fractionated into lighting end and last running, last running mixes with conventional coking raw material, delayed coking obtains coker gasoline and coker gas oil, coker gasoline and coker gas oil and ethylene bottom oil lighting end are mixed to get mixing raw material, through hydrofining reaction, the hydrofining of gained generates oil and is isolated to gasoline fraction I and overweights vapour oil fraction, overweight vapour oil fraction and carry out hydrotreatment, namely successively through hydrofining reaction district and hydrocracking reaction district, gained hydrocracking generates oil and is isolated to gasoline fraction II and diesel product, gasoline fraction II and gasoline fraction I is mixed to get gasoline products.

In the inventive method, the cut point of ethylene bottom oil lighting end and last running is 400 ~ 520 DEG C, is preferably 460 ~ 520 DEG C.

In the inventive method, the blending ratio of ethylene bottom oil last running and conventional coking raw material is 1:1 ~ 9.

Described conventional coking raw material can be weight, the residual oil raw material of initial boiling point >350 DEG C, generally can be selected from long residuum, vacuum residuum, visbroken resids, the heavy deasphalted oil of deasphalting unit, catalytically cracked oil, viscous crude and topped crude one or more, certainly also can be selected from other as: one or more in liquefied coal coil, shale wet goods, are preferably vacuum residuum.Described delayed coking can adopt conventional operational condition, and be generally: temperature of reaction 480 ~ 530 DEG C, reaction pressure 0.05MPa ~ 0.80MPa, preferably at 0.10MPa ~ 0.20MPa; Residence time 5min ~ 50min, best 10 min ~ 30min; Circulation weight ratio is 0.01 ~ 1.0, preferably 0.2 ~ 0.6.The coker gasoline of delayed coking gained and coker gas oil can not be isolated to the mixing oil of coker gasoline and coker gas oil, also can obtain coker gasoline and coker gas oil respectively, and then mix.

In the inventive method, after coker gasoline, coker gas oil and ethylene bottom oil lighting end mixing, first generate oily heat exchange with hydrofining, then reach hydrofining reactor inlet temperature requirements through the mode that process furnace heats up.Overweight vapour oil fraction and first generate oily heat exchange with hydrocracking, then reach the inlet temperature requirements in hydrofining reaction district through the mode that raw materials furnace and heating heats up.

In the inventive method; Hydrobon catalyst is loaded in mixing raw material hydrofining reactor; preferably load hydrogenation protecting agent in the upstream of Hydrobon catalyst, wherein hydrogenation protecting agent and Hydrobon catalyst are seated in same reactor, or load respectively in two reactors.Described hydrogenation protecting catalyst can adopt residual hydrogenation protective material or residuum hydrogenating and metal-eliminating catalyst, and hydrogenation protecting agent used accounts for 10% ~ 30% of Hydrobon catalyst volume.In the inventive method, hydrogenation protecting catalyst is with group vib and/or group VIII metal for active metal component, and with aluminum oxide or silicon-containing alumina for carrier, group vib metal is Mo and/or W, and group VIII metal is Co and/or Ni; With the weight of catalyzer for benchmark, active metallic content take oxide basis as 0.5wt% ~ 18wt%.Such as: FZC-103, FZC-200 catalyzer of Fushun Petrochemical Research Institute's research and development.In the inventive method, mixing raw material hydrofining reaction condition is: temperature of reaction 320 ~ 370 DEG C, hydrogen dividing potential drop 13.0 ~ 17.0MPa, hydrogen to oil volume ratio 1300:1 ~ 1500:1 and liquid time volume space velocity 0.3 ~ 0.7h ^-1.

In the inventive method, hydrofining reaction district and the hydrocracking reaction district of hydrotreatment adopt one-stage serial technique, two reaction zones in same reactor, or respectively in different reactors.The hydrofining reaction district filling Hydrobon catalyst of hydrotreatment; Hydrocracking catalyst is loaded in described hydrocracking reaction district, preferably at the loaded upstream removal of ccr by hydrotreating catalyzer of hydrocracking catalyst, the Hydrobon catalyst that wherein hydrotreatment is used accounts for 60% ~ 100% of hydrocracking catalyst admission space, and the admission space of removal of ccr by hydrotreating catalyzer accounts for 5% ~ 40% of hydrocracking catalyst admission space.In the inventive method, the hydrofining reaction district preferred operations condition of hydrotreatment is: temperature of reaction 360 ~ 390 DEG C, hydrogen dividing potential drop 13.0 ~ 17.0MPa, hydrogen to oil volume ratio 1300:1 ~ 1500:1 and liquid time volume space velocity 0.3 ~ 0.7h ^-1; Described hydrocracking reaction district preferred operations condition is: temperature of reaction 380 ~ 400 DEG C, hydrogen dividing potential drop 14.0 ~ 17.0MPa, hydrogen to oil volume ratio be 1300:1 ~ 1500:1 and liquid time volume space velocity 0.3 ~ 0.7h ^-1.

In the inventive method, the Hydrobon catalyst that the Hydrobon catalyst that the hydrofining reaction district of the Hydrobon catalyst that mixing raw material hydrofining reaction is used and hydrotreatment uses is routine or pretreating catalyst by hydrocracking, generally with group vib and/or group VIII metal for active ingredient, with the aluminum oxide of aluminum oxide, silicon-containing alumina or siliceous and phosphorus for carrier, group vib metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.With the weight of catalyzer for benchmark, group vib metal content take oxide basis as 10wt% ~ 35wt%, and group VIII metal content take oxide basis as 3wt% ~ 15wt%, and its character is as follows: specific surface area is 100 ~ 350m ²/ g, pore volume is 0.15 ~ 0.60ml/g.Main catalyzer have China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute to develop 3936,3996, FF-16, FF-26 etc.

In the inventive method, hydrocracking catalyst can adopt one or more conventional hydrocracking catalysts, generally with group vib and/or group VIII metal for active ingredient, group vib metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.The carrier of this catalyzer is two or more in aluminum oxide, silicon-containing alumina and molecular sieve, preferably adopts the hydrocracking catalyst containing molecular sieve and amorphous aluminum silicide.The present invention recommends (with the weight of catalyzer for benchmark) composed as follows: the content of Y molecular sieve or beta-molecular sieve is 10% ~ 40%, the content of amorphous aluminum silicide is 20% ~ 60%, group vib hydrogenation active metals with the content of oxide basis for 15% ~ 40%, group VIII hydrogenation active metals is with the content of oxide basis for 1% ~ 10%, and surplus is little porous aluminum oxide; The character of hydrocracking catalyst is as follows: specific surface area is 180 ~ 300m ²/ g, pore volume is 0.25 ~ 0.45ml/g.FC-14, ZHC-02 that such as Fushun Petrochemical Research Institute develops, the hydrocracking catalysts such as 3974.

Described removal of ccr by hydrotreating catalyzer is with group vib metal and group VIII metal for hydrogenation active component, as two or three in W, Mo, Ni and Co, is preferably W, Mo and Ni, and this catalyzer containing auxiliary agent Si and Ti, take preferably aluminum oxide as carrier.With the weight of catalyzer for benchmark, WO ₃content be 16% ~ 23%, MoO ₃content be the content of 6% ~ 13%, NiO be 3% ~ 8%, silicone content is with SiO ₂count 4% ~ 12%, be preferably 5% ~ 9%, titanium oxide content is 0.5% ~ 4%, and be preferably 1% ~ 2%, surplus is aluminum oxide.The character of this catalyzer is as follows: pore volume is 0.30 ~ 0.55cm ³/ g, specific surface area is 120 ~ 300m ²/ g, average pore diameter is 5 ~ 10nm, is preferably 5 ~ 8nm.

The inventive method tool has the following advantages:

1, ethylene bottom oil last running is mixed refining in conventional coking raw material as the raw material of delayed coking by the inventive method, such one side expands the raw material sources of delayed coking unit, ethylene bottom oil lighting end and coking vapour on the other hand, diesel oil mixes, first through hydrofining, overweight vapour oil fraction after separation and be converted into clean vapour completely through hydrotreatment again, diesel oil blending component, by refinery's by-product---be converted into ethylene bottom oil maximum the light-weight fuel oil of the huge market demand, vapour simultaneously, diesel product quality be improved significantly, these are all favourable to raising refinery economic benefit.

2, the coker gasoline of coking gained and coker gas oil mix with ethylene bottom oil lighting end by the inventive method, as hydrorefined raw material, can alleviate the difficult feed problem that ethylene bottom oil lighting end causes greatly because of viscosity so on the one hand, effectively reduce energy consumption; Also reduce the olefin(e) centent in coker gasoline and coker gas oil simultaneously, and make carbon residue and asphalt content also corresponding reduction in ethylene bottom oil lighting end, this two aspect is all conducive to device long-term operation.

3, the coker gasoline of coking gained and coker gas oil and ethylene bottom oil lighting end are mixed into hydrofining reactor by the inventive method, employing lesser temps first removes sulphur, nitrogen impurity in lighting end, gasoline fraction as product caterpillar is cleaned, so also can save the energy.

4, the product after hydrofining is separated by the inventive method after distillation, obtain the gasoline fraction I that sulphur content obviously reduces, this gasoline fraction I mixes with the gasoline fraction II of follow-up generation as final gasoline blending component product caterpillar, instead of proceed hydrotreatment reaction again, the yield of C1 ~ C4 component can be reduced like this, favourable to raising yield of light oil.

5, the inventive method hydrocracking catalyst upstream stage in hydrotreating reactor is equipped is filled with Hydrobon catalyst, make the aromatic hydrocarbons of more than the dicyclo that content in raw material is higher by ring filling, the aromatic hydrocarbons of these fractional saturations is again under hydrocracking catalyst effect, be converted into the more satisfactory component of clean vapour, diesel oil more---with the monocycle hydro carbons of side chain, and then effectively can improve yield of light oil, and improve quality product.

6, the inventive method grading loading removal of ccr by hydrotreating catalyzer, not only be conducive to the running period of extension fixture, and the increase of removal of ccr by hydrotreating catalyzer, also improve the saturation exponent of aromatic hydrocarbons, be conducive to next step hydrocracking reaction, improve the yield of light-weight fuel oil.In addition, raw material, successively through Hydrobon catalyst, removal of ccr by hydrotreating catalyzer and hydrocracking catalyst, can make exothermic heat of reaction even, avoid the temperature rise of hydrocracking bed too high, favourable to the safety and steady operation of device.

7, the present invention is that the ethylene bottom oil that added value is lower provides a kind of working method improving its economy; Under the present situation of crude supply growing tension, synergy is reduced discharging to refinery useful.

Accompanying drawing explanation

Fig. 1 is the block diagram of the inventive method.

Embodiment

The invention will be further described for composition graphs 1.Ethylene bottom oil 1 obtains lighting end 3 and last running 4 through separation column 2 fractionation, last running 4 and conventional coking raw material 5 mix, delayed coker 6 obtains coker gasoline 7, coker gas oil 8 and wax tailings 9, coker gasoline 7, after coker gas oil 8 and ethylene bottom oil lighting end 3 mix, obtain mixed hydrogenation process raw material 10, mixed hydrogenation process raw material 10 is after hydrofining reactor 11, gained hydrofining generates oil 12 and separates gasoline fraction I 14 through stripping tower and distillation tower 13 and overweight vapour oil fraction 15, overweight vapour oil fraction 15 to enter hydrotreating reactor 16 and carry out hydrotreatment reaction, gained generates oil 17, gasoline fraction II 19 and diesel product 20 is obtained through stripping tower and separation column 18, gasoline fraction II 19 and gasoline fraction I 14 are mixed to get final gasoline products.Wax tailings 9 is generally as the raw material caterpillar of catalytic cracking or hydrocracking.

Ethylene bottom oil described in the inventive method is ethylene cracker by-product---Pyrolysis fuel oil PFO.

The following examples will be further described present method, but be not limited in this.In the present invention, wt% is massfraction.

Embodiment of the present invention hydrocracking catalyst used is prepared as follows:

1, containing the preparation of the hydrocracking catalyst of amorphous aluminum silicide and Y zeolite: A1, A2

(1) hydrocracking catalyst A1:

By amorphous aluminum silicide (specific surface area 520m2/g, SiO ₂35wt%, pore volume 1.2ml/g) and Y molecular sieve (SiO ₂/ Al ₂o ₃mol ratio is 9, lattice constant 2.432, specific surface area 650m2/g, infrared acidity 0.45mmol/g), add after mixing (added by the little porous aluminum oxide of pore volume 0.42ml/g prepared by dust technology peptization) tackiness agent roll agglomerating after, after putting into banded extruder extruded moulding, 110 DEG C of dryings 10 hours, 500 DEG C of activation, 4 hours obtained carriers, then be total to impregnation fluid with Mo-Ni, then 110 DEG C of dryings 12 hours, and 500 DEG C activate 3 hours.Catalyzer finally consists of: amorphous aluminum silicide 48wt%, Y molecular sieve 15wt%, aluminum oxide 12wt%, nickel oxide 5wt%, molybdenum oxide 20wt%.Specific surface area of catalyst 220m ²/ g, pore volume 0.35ml/g.

(2) hydrocracking catalyst A2:

By amorphous aluminum silicide (specific surface area 490m2/g, SiO ₂45wt%, pore volume 1.0ml/g) and Y molecular sieve (SiO ₂/ Al ₂o ₃mol ratio is 12, lattice constant 2.436, specific surface area 680m2/g, infrared acidity 0.41mmol/g), the tackiness agent adding (preparation being added dust technology peptization by the little porous aluminum oxide of pore volume 0.42ml/g) after mixing roll agglomerating after, after putting into banded extruder extruded moulding, 110 DEG C of dryings 10 hours, after 500 DEG C of activation, 4 hours obtained carriers, again with W-Ni impregnation fluid altogether, then 110 DEG C of dryings 12 hours, and 500 DEG C activate 3 hours.Catalyzer finally consists of: amorphous aluminum silicide 45wt%, Y molecular sieve 13wt%, aluminum oxide 12wt%, nickel oxide 6.5wt%, Tungsten oxide 99.999 22.5wt%.Specific surface area of catalyst 210m ²/ g, pore volume 0.31ml/g.

2, containing the preparation of the hydrocracking catalyst B1 of amorphous aluminum silicide and beta-molecular sieve

Hydrocracking catalyst B1:

By beta-molecular sieve (SiO ₂/ Al ₂o ₃mol ratio is 40, specific surface area 580m2/g, infrared acidity 0.21mmol/g), amorphous aluminum silicide (specific surface area 450m2/g, SiO ₂55wt%, pore volume 0.9ml/g) mix, add by little porous aluminum oxide (the specific surface area 240m of the dilute nitric acid solution peptization of concentration 3.3wt% ²/ g, pore volume is 0.42ml/g) tackiness agent that obtains, continue kneading until become paste, extruded moulding, institute obtains the drying 12 hours at 110 DEG C of shaping bar, 500 DEG C activate 4 hours obtained activated carriers after.The carrier of above-mentioned preparation is flooded again with W-Ni co-impregnated solution, then 110 DEG C of dryings 8 hours, and 500 DEG C activate 3 hours.Catalyzer finally consists of: β zeolite 25wt%, amorphous aluminum silicide 25wt%, aluminum oxide 20wt%, nickel oxide 7.5wt%, Tungsten oxide 99.999 22.5wt%.Specific surface area of catalyst 235m ²/ g, pore volume 0.32ml/g.

Embodiment of the present invention removal of ccr by hydrotreating used catalyst preparing is as follows:

Take 298g Si-Al ₂o ₃(butt 67w%, dioxide-containing silica is 19w%) powder, sesbania powder 5g, is mixed, and adds by 188g water, 43.0g containing 17wt%TiCl ₃tiCl ₃the acidic solution that solution and 22g acetic acid mix, kneading 1.5 hours, gained plastic, extruded moulding, this strip at 108 DEG C dry 4 hours, roasting 4 hours at 550 DEG C.With the impregnated activated metal of ordinary method, molybdenum, tungsten and nickel, then at 120 DEG C dry 2 hours, at 550 DEG C, roasting 3 hours, namely made catalyzer HDC-1.The composition of this catalyzer and physico-chemical property see the following form 1.

The composition of table 1 removal of ccr by hydrotreating catalyzer and character

Catalyzer	HDC-1
		Composition, %(massfraction)
WO 3	22
		MoO 3	11
NiO	5
		SiO 2	9
TiO 2	2
		Al 2O 3	Surplus
Character
		Specific surface area, m 2/g	220
Average pore diameter, nm	6.8

Embodiment 1 ~ 3

Adopt Fig. 1 flow process.Ethylene bottom oil is divided into lighting end and last running through distillation, respectively with 420 DEG C and 480 DEG C for cut point, obtain respectively after distillation gently, last running, character lists in table 2, and Vacuum Residue Properties lists in table 3.The last running of gained ethylene bottom oil mixes with vacuum residuum, and the character of mixing raw material and delay coking process condition, gained gasoline and diesel oil distillate is in table 4.Coker gasoline, coker gas oil and ethylene bottom oil lighting end mixing; as the raw material of hydrofining reactor; this reactor loads hydrogenation protecting agent FZC-103, Hydrobon catalyst 3936 from top to bottom; the volume ratio of two kinds of catalyzer is 1:4, and hydrofining reaction processing condition and gained overweight vapour oil fraction character in table 5.In the present embodiment, to overweight vapour oil fraction for raw material, obtain light-weight fuel oil through hydrotreatment, hydroprocessing technique condition is in table 6.Hydrotreating reactor adopts two reactors in series modes, and one instead loads Hydrobon catalyst 3936, two anti-filling from top to bottom removal of ccr by hydrotreating catalyzer hDC-1and hydrocracking catalyst, in embodiment 1 and 3, the volume ratio of these three kinds of catalyzer is 40:15:45, in embodiment 2, the volume ratio of these three kinds of catalyzer is 45:10:45, product is separated through separation system, together with the gasoline fraction of gained after hydrofining, obtain quality be improved significantly clean vapour, diesel oil blending component product, reaction result is in table 7.In addition, this device has carried out the service test of 5000 hours, product slates and each narrow fraction product property is substantially constant or change is very little, illustrates that present method is improving vapour, while diesel product quality, also can solving device running period short problem.

Comparative example 1

Ethylene bottom oil is without distillation, and full cut mixes with mass ratio 1:1 with vacuum residuum, and this mixture carries out the processing condition of delayed coking and product property in table 4.The hydrofining reaction processing condition of coker gasoline and coker gas oil mixture and overweight gasoline fraction character in table 5; this hydrofining reactor loads hydrogenation protecting agent FZC-103 from top to bottom, the volume ratio of Hydrobon catalyst 3936, two kinds of catalyzer is 1:6.Overweight gasoline fraction and obtain light-weight fuel oil through hydrotreatment, hydroprocessing technique condition is in table 6.Hydrotreating reactor adopts two reactors in series modes, and one instead loads Hydrobon catalyst 3936, two anti-filling from top to bottom removal of ccr by hydrotreating catalyzer hDC-1and hydrocracking catalyst, the volume ratio of these three kinds of catalyzer is 55:10:35, and reaction result is in table 7.

Table 2 ethylene bottom oil adopts that different cut point gained is light, last running character

Cut point	420℃	420℃	480℃	480℃
					Crude title	Lighting end	Last running	Lighting end	Last running
Numbering	L1	H1	L2	H2
					S，μg/g	398	458	402	466
N，μg/g	48	196	56	218
					CCR，wt%	3.9	23.65	4.6	26.9
Aromatic hydrocarbons, wt %	50.1	38.1	46.6	33.2
					Colloid+bituminous matter, wt %	46.9	61.7	51.4	65.1
Metal content, μ g/g
					Ni	0.06	0.1	0.07	0.1
V	0.01	0.01	0.01	0.01

Table 3 Vacuum Residue Properties

Crude title	Vacuum residuum
		S，wt%	2.98
N，mg/kg	4913
		CCR，wt%	17.12
Aromatic hydrocarbons, wt %	47.7
		Colloid+bituminous matter, wt %	34.6
Metal content, μ g/g
		Ni	61.7
V	172.5

Table 4 delayed coking condition and product property

Scheme	Embodiment 1	Embodiment 2	Embodiment 3	Comparative example 1
					Processing condition
Temperature of reaction, DEG C	510	495	500	495
					Reaction pressure/MPa	0.10	0.17	0.15	0.17
Recycle ratio	0.4	0.5	0.4	0.5
					Ethylene bottom oil last running	H1	H1	H2	-
Ethylene bottom oil last running: vacuum residuum (mass ratio)	1：3	1：5	1：7	The full cut of 1:1(: subtract slag)
					Coker naphtha character	G1	G2	G3	G4
Boiling range, DEG C	55~181	50~176	52~180	49~179
					Yield, wt%(is to mixing raw material)	9.45	9.32	9.39	9.35
Sulphur content, μ g/g	2742	2613	2719	2701
					Research octane number (RON)	74	78	76	78
Fraction of coker gas oil character	D1	D2	D3	D4
					Boiling range, DEG C	173~458	174~463	178~461	179~452
Yield, wt%(is to mixing raw material)	56.75	51.47	50.50	52.10
					Density (20 DEG C), g/cm 3	0.9768	0.9840	0.9887	0.9850
Sulphur content, μ g/g	5956	6115	6221	6134
					Cetane value	＜-21.5	＜-21.5	＜-21.5	＜-21.5
Wax tailings cut character	W1	W2	W3	W4
					Boiling range, DEG C	458~528	463~524	461~521	450~526
Yield, wt%(is to mixing raw material)	15.52	15.41	15.16	16.10
					Sulphur content, μ g/g	17900	17400	16882	17607

Table 5 hydrofining technology condition and gained overweight the character of gasoline fraction

Scheme	Embodiment 1	Embodiment 2	Embodiment 3	Comparative example 1
					Raw material	G1+D1+L1	G2+D2+L1	G3+D3+L2	G4+D4
Processing condition
					Hydrogen dividing potential drop/MPa	16.0	15. 0	14. 0	12.0
Temperature of reaction/DEG C	330~335	340~345	350~355	340~345
					Volume space velocity/h during liquid -1	0.4	0.5	0.6	0.8
Hydrogen to oil volume ratio	1400	1300	1500	1300
					Overweight the character of gasoline fraction	HH1	HH2	HH3	HH4
Boiling range/DEG C
					IBP	172	170	168	174
EBP	458	451	486	453
					Density (20 DEG C), g/cm 3	0.9901	0.9882	0.9879	0.9896
S，μg/g	990	984	950	950
					N，μg/g	163	154	160	166
Four composition, wt%
					Aromatic hydrocarbons	68.5	70.28	69.54	68.90
Colloid	11.05	10.00	10.81	10.10
					Bituminous matter	0.65	0.57	0.62	0.56

Table 6 hydroprocessing technique condition

Scheme	Embodiment 1	Embodiment 2	Embodiment 3	Comparative example 1
					Raw material	HH1	HH2	HH3	HH4
Hydrobon catalyst	3936	3936	3936	3936
					Removal of ccr by hydrotreating catalyzer	HDC-1	HDC-1	HDC-1	HDC-1
Hydrocracking catalyst	A2	B2	A1	B2
					Processing condition
Hydrogen dividing potential drop/MPa	14.5	15.5	16.5	15.0
					One anti-temperature/DEG C	370~375	380~385	360~365	360~365
Two anti-temperature/DEG C	395~400	380~385	390~395	390~395
					One anti-/ bis-anti-air speed/h -1	0.5/0.5	0.4/0.4	0.6/0.6	1.0/1.0
Hydrogen to oil volume ratio	1500	1400	1300	1200

The character of table 7 embodiment and the final gained diesel oil distillate of comparative example and gasoline fraction

Scheme	Embodiment 1	Embodiment 2	Embodiment 3	Comparative example 1
					Diesel oil distillate character
Yield, wt%(is to ethylene bottom oil)	53.2	50.7	54.1	40.6
					Density (20 DEG C), g/cm 3	0.8678	0.8641	0.8720	0.8681
Sulphur content, μ g/g	9	8	8	9
					Nitrogen content, μ g/g	1	1	1	1
Condensation point/DEG C	-52	＜-53	＜-52	＜-53
					Cold filter clogging temperature/DEG C	-30	-28	-29	-30
Boiling range/DEG C
					50%	194	193	201	195
90%	270	270	278	278
					95%	304	301	308	305
Cetane value	36.5	37.0	36.7	34
					Gasoline fraction character
Yield, wt%(is to ethylene bottom oil)	25.9	26.0	25.9	20.7
					Research octane number (RON)	85	82	84	84
Sulphur content, μ g/g	7	6	4	6

Can be seen by table 7, complete for ethylene bottom oil cut is mixed delayed coking gained gasoline, diesel oil and wax oil with vacuum residuum, gasoline fraction and diesel oil distillate adopt the processing and treating method similar with present method, and gained yield of light oil is only 61.3%, and total liquid yield is 77.4%; Present method gained light-weight fuel oil yield is minimum is 76.7%, and total liquid yield is minimum is 85.9%, all higher than the former.In product property, present method is also better than the former.

Claims (12)

1. the method for an ethylene bottom oil production light-weight fuel oil, comprise: ethylene bottom oil is fractionated into lighting end and last running, last running mixes with conventional coking raw material, delayed coking obtains coker gasoline and coker gas oil, coker gasoline and coker gas oil and ethylene bottom oil lighting end are mixed to get mixing raw material, through hydrofining reaction, the hydrofining of gained generates oil and is isolated to gasoline fraction I and overweights vapour oil fraction, overweight vapour oil fraction and carry out hydrotreatment, namely successively through hydrofining reaction district and hydrocracking reaction district, gained hydrocracking generates oil and is isolated to gasoline fraction II and diesel product, gasoline fraction II and gasoline fraction I is mixed to get gasoline products, described ethylene bottom oil lighting end and the cut point of last running are 460 ~ 520 DEG C, described ethylene bottom oil last running and the mixing quality ratio of conventional coking raw material are 1:1 ~ 9, the operational condition of described delayed coking, for: temperature of reaction 480 ~ 530 DEG C, reaction pressure 0.05MPa ~ 0.80MPa, residence time 5min ~ 50min, circulation weight ratio is 0.01 ~ 1.0, the hydrofining reaction district operational condition of hydrotreatment is: temperature of reaction 360 ~ 390 DEG C, hydrogen dividing potential drop 13.0 ~ 17.0MPa, hydrogen to oil volume ratio 1300:1 ~ 1500:1 and liquid time volume space velocity 0.3 ~ 0.7h ^-1, described hydrocracking reaction district operational condition is: temperature of reaction 380 ~ 400 DEG C, hydrogen dividing potential drop 14.0 ~ 17.0MPa, hydrogen to oil volume ratio be 1300:1 ~ 1500:1 and liquid time volume space velocity 0.3 ~ 0.7h ^-1.

2. in accordance with the method for claim 1, it is characterized in that described conventional coking raw material is weight, the residual oil raw material of initial boiling point >350 DEG C, be selected from one or more in long residuum, vacuum residuum, visbroken resids, the heavy deasphalted oil of deasphalting unit, catalytically cracked oil, viscous crude, topped crude, liquefied coal coil, shale oil.

3. in accordance with the method for claim 1, it is characterized in that described conventional coking raw material is vacuum residuum.

4. in accordance with the method for claim 1, after it is characterized in that described coker gasoline, coker gas oil and ethylene bottom oil lighting end mixing, first generate oily heat exchange with hydrofining, then reach hydrofining reactor inlet temperature requirements through the mode that process furnace heats up.

5. in accordance with the method for claim 1, it is characterized in that, overweight vapour oil fraction and first generate oily heat exchange with hydrocracking, then reach the inlet temperature requirements in hydrofining reaction district through the mode that raw materials furnace and heating heats up.

6. in accordance with the method for claim 1; it is characterized in that; load Hydrobon catalyst in mixing raw material hydrofining reactor, in the loaded upstream hydrogenation protecting agent of Hydrobon catalyst, hydrogenation protecting agent used accounts for 10% ~ 30% of Hydrobon catalyst volume.

7. in accordance with the method for claim 1, it is characterized in that, mixing raw material hydrofining reaction condition is: temperature of reaction 320 ~ 370 DEG C, hydrogen dividing potential drop 13.0 ~ 17.0MPa, hydrogen to oil volume ratio 1300:1 ~ 1500:1 and liquid time volume space velocity 0.3 ~ 0.7h ^-1.

8. in accordance with the method for claim 1, it is characterized in that, the hydrofining reaction district filling Hydrobon catalyst of hydrotreatment; Hydrocracking catalyst is loaded in described hydrocracking reaction district, at the loaded upstream removal of ccr by hydrotreating catalyzer of hydrocracking catalyst, the Hydrobon catalyst that wherein hydrotreatment is used accounts for 60% ~ 100% of hydrocracking catalyst admission space, and the admission space of removal of ccr by hydrotreating catalyzer accounts for 5% ~ 40% of hydrocracking catalyst admission space.

9. in accordance with the method for claim 1, it is characterized in that the hydrocracking catalyst that described hydrocracking reaction district adopts is the hydrocracking catalyst containing molecular sieve and amorphous aluminum silicide.

10. according to the method described in claim 8 or 9, it is characterized in that described hydrocracking catalyst, with the weight of catalyzer for benchmark, the content of Y molecular sieve or beta-molecular sieve is 10% ~ 40%, the content of amorphous aluminum silicide is 20% ~ 60%, group vib hydrogenation active metals is with the content of oxide basis for 15% ~ 40%, and group VIII hydrogenation active metals is with the content of oxide basis for 1% ~ 10%, and surplus is little porous aluminum oxide; The character of hydrocracking catalyst is as follows: specific surface area is 180 ~ 300m ²/ g, pore volume is 0.25 ~ 0.45ml/g.

11. in accordance with the method for claim 8, it is characterized in that described removal of ccr by hydrotreating catalyzer, with the weight of catalyzer for benchmark, and WO ₃content be 16% ~ 23%, MoO ₃content be the content of 6% ~ 13%, NiO be 3% ~ 8%, silicone content is with SiO ₂count 4% ~ 12%, titanium oxide content is 0.5% ~ 4%, and surplus is aluminum oxide; The character of this catalyzer is as follows: pore volume is 0.30 ~ 0.55cm ³/ g, specific surface area is 120 ~ 300m ²/ g, average pore diameter is 5 ~ 10nm.

12. in accordance with the method for claim 8, it is characterized in that described removal of ccr by hydrotreating catalyzer, with the weight of catalyzer for benchmark, and WO ₃content be 16% ~ 23%, MoO ₃content be the content of 6% ~ 13%, NiO be 3% ~ 8%, silicone content is with SiO ₂count 5% ~ 9%, titanium oxide content is 1% ~ 2%, and surplus is aluminum oxide; The character of this catalyzer is as follows: pore volume is 0.30 ~ 0.55cm ³/ g, specific surface area is 120 ~ 300m ²/ g, average pore diameter is 5 ~ 10nm.