CN204097413U - Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil - Google Patents
Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil Download PDFInfo
- Publication number
- CN204097413U CN204097413U CN201420221682.4U CN201420221682U CN204097413U CN 204097413 U CN204097413 U CN 204097413U CN 201420221682 U CN201420221682 U CN 201420221682U CN 204097413 U CN204097413 U CN 204097413U
- Authority
- CN
- China
- Prior art keywords
- unit
- oil
- desulfurization
- pipeline
- gas sweetening
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a kind of production petrol and diesel oil, the system of refinery coke and top-grade lubricating oil base oil, this system is by crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy feed stock processing unit, catalysis lighting unit, isomerization dewaxing reaction member and post-refining reaction member, gas sweetening with prepare unit and organically combine, to greatest extent crude oil with poor quality is changed into light-end products, the low-viscosity that refinery coke and China are badly in need of, low pour point, the III class base oil of viscosity index ﹥ 120, product category is many, multi-field development need can be met, and can simplification of flowsheet, reduce overall energy consumption.
Description
Technical field
The utility model belongs to oil refining, petrochemical complex, coal chemical technology, relating to a kind of system of crude oil with poor quality lighting, is by crude oil with poor quality pretreatment unit, heavy feed stock processing unit, desulfurization and Cracking Unit, catalysis lighting unit, base oil unit and gas sweetening and the lighting system preparing unit organic assembling specifically.
Background technology
Along with worldwide oil property becomes heavy, becomes bad, and the requirement of sustained economic development and the increasingly stringent of environmental regulation, the demand of people to light clean fuel is increasing, these all require to improve existing oil Refining Technologies, produce satisfactory product with minimum cost processing crude oil with poor quality.
Because crude oil with poor quality viscosity is high, higher than great, heavy metal and sulphur content and colloid, bituminous matter, utilize existing oil Refining Technologies to carry out crude oil with poor quality processing, the unfavorable factor such as there is gasoline and diesel yield is low, and heat energy loss is large, and facility investment is high.
Refinery coke is the material producing electrode, graphite, carbon element, nuclear reactor deceleration rod etc., and also having been widely used in industry, national defence, medical treatment, space flight and nuclear power etc., is a kind of material national economy and scientific technological advance being had to material impact.Crude oil with poor quality is utilized to produce refinery coke to meeting China's economy and scientific technological advance important in inhibiting.
Along with automobile industry of China, the developing by leaps and bounds of aerospace industries and high-speed railway, the total quantity consumed of China's lubricating oil also presents and increases substantially.It is reported, within 2012, China's lubricating oil consumption is more than 1,000 ten thousand tons, and lubricating oil annual production then only has more than 800 ten thousand tons, and huge breach can only rely on import to make up, particularly top-grade lubricating oil, and 80% needs to rely on import.Top-grade lubricating oil is the product that a kind of technology content is very high, and it is related to various important industry, as: automobile, aviation, engine, machinofacture, national defence etc., passive situation therefore under one's control should change as early as possible.
Lubricating oil is main body by base oil, and add a small amount of additive and be in harmonious proportion and form, the technical indicator of base oil and quality decide lubricants performance and technical indicator.The production of top-grade lubricating oil, base oil quality is a very important ring.Current internal lube oil base oil also need from a large amount of import in the ground such as Korea S, Singapore, and this illustrates, China does not change passive situation under one's control yet in the production of top-grade lubricating oil.
Utilize crude oil with poor quality to produce top-grade lubricating oil base oil, can raw material sources be increased, reducing production cost, having definite meaning to meeting China's Economic development.
Existing system is abundant not to crude oil with poor quality lighting, does not make full use of catalytically cracked oil.
Summary of the invention
The purpose of this utility model is on prior art basis, a kind of crude oil with poor quality pre-treatment, heavy feed stock process, desulfurization and cracking, catalysis lighting, base oil and gas sweetening are provided and prepare the lighting system of unit organic assembling, to greatest extent crude oil with poor quality is changed into the III class base oil of the low-viscosity of light-end products, refinery coke and China's urgent need, low pour point, viscosity index ﹥ 120, simplification of flowsheet, reduces overall energy consumption.
The purpose of this utility model realizes in the following manner:
Crude oil with poor quality produces a system for gasoline, diesel oil, refinery coke and top-grade lubricating oil base oil, and this system comprises crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy feed stock processing unit, catalysis lighting unit, base oil unit and gas sweetening and prepares unit;
Crude oil with poor quality pretreatment unit is respectively by pipeline and desulfurization and Cracking Unit, heavy feed stock processing unit, gas sweetening and prepare unit and be connected;
Desulfurization and Cracking Unit respectively by pipeline and catalysis lighting unit, base oil unit and gas sweetening with prepare unit and be connected;
Heavy feed stock processing unit is connected with catalysis lighting unit by pipeline;
Catalysis lighting unit respectively by pipeline and gas sweetening with prepare unit and be connected;
Base oil unit by pipeline and gas sweetening with prepare unit and be connected.
Crude oil with poor quality pretreatment unit is respectively by pipeline and desulfurization and Cracking Unit, heavy feed stock processing unit, gas sweetening and prepare unit and be connected;
Desulfurization and Cracking Unit respectively by pipeline and catalysis lighting unit, base oil unit and gas sweetening with prepare unit and be connected;
Heavy feed stock processing unit is connected with catalysis lighting unit by pipeline;
Catalysis lighting unit respectively by pipeline and gas sweetening with prepare unit and be connected;
Base oil unit by pipeline and gas sweetening with prepare unit and be connected.
Crude oil with poor quality pretreatment unit comprises stock oil storage tank, electrical desalter, interchanger, atmospheric pressure kiln and atmospheric fractional tower; Multiple outlets of the atmospheric fractional tower of crude oil with poor quality pretreatment unit connect desulfurization and Cracking Unit, heavy feed stock processing unit, gas sweetening respectively by pipeline and prepare unit and hydro-refining unit.
Desulfurization and Cracking Unit comprise the first hydrogenator, the second hydrogenator and the first separation column;
Heavy feed stock processing unit comprises coking heater and coke drum; Catalysis lighting unit comprises reactor, catalyst regenerator and after-fractionating tower; Base oil unit comprises isomerization dewaxing reactor, post-refining reactor and tripping device; Gas sweetening with prepare unit and be made up of thionizer and PSA purifying plant; Multiple outlets of crude oil with poor quality pretreatment unit separation column connect the first separation column of desulfurization and Cracking Unit, the coking heater of heavy feed stock processing unit and coke drum respectively by pipeline, gas sweetening and the thionizer preparing unit; The entrance of the interchanger of crude oil with poor quality pretreatment unit connects the outlet of the after-fractionating tower of catalysis lighting unit.
Desulfurization and the outlet of the first separation column of Cracking Unit are connected gas sweetening and thionizer, the isomerization dewaxing reactor of base oil unit, the reactor of catalysis lighting unit of preparing unit respectively, and desulfurization is connected the outlet of the second hydrogenator with the entrance of the first separation column of Cracking Unit.
The entrance of the coking heater in heavy feed stock processing unit is connected by the outlet of pipeline with the after-fractionating tower of catalysis lighting unit, and meanwhile, coke drum, coking heater and atmospheric fractional tower connect into loop by pipeline.
The outlet of the after-fractionating tower of catalysis lighting unit is respectively by pipeline and gas sweetening and the thionizer preparing unit, and the interchanger of crude oil with poor quality pretreatment unit is connected, the outlet of the entrance ligation device of the after-fractionating tower of catalysis lighting unit.
The isomerization dewaxing reactor of base oil unit is connected with the PSA purifying plant preparing unit with gas sweetening by pipeline.
The tripping device of base oil unit is connected with the thionizer preparing unit with gas sweetening by pipeline.
Described gas sweetening and the PSA purifying plant preparing unit are connected the entrance of process furnace by pipeline, the outlet of process furnace connects the entrance of the first hydrogenator of desulfurization and Cracking Unit.
Steam heating coil is established in described stock oil storage tank.
Application said system realizes the method that crude oil with poor quality produces gasoline, diesel oil, refinery coke and top-grade lubricating oil base oil, the method comprises crude oil with poor quality pre-treatment, desulfurization and cracking, heavy feed stock process, catalysis lighting, isomerization dewaxing and to react and post-refining reacts, gas sweetening and preparation process, and concrete steps are as follows:
The pre-treatment of (a) crude oil with poor quality: crude oil with poor quality is carried out wash, desalination, dehydration and de-solid, heat exchange is to 200 DEG C ~ 250 DEG C (preferred heat exchange is to 220 DEG C ~ 230 DEG C), be heated to 360 DEG C ~ 390 DEG C (being preferably heated to 380 DEG C ~ 390 DEG C) by process furnace again, enter atmospheric fractional tower: isolate gas, gasoline, diesel oil, 330 DEG C ~ 350 DEG C atmospheric gas oils and > 350 DEG C of residual oil;
(b) desulfurization and cracking: 330 DEG C ~ 350 DEG C atmospheric gas oils that step (a) obtains obtain gas, gasoline, diesel oil, fcc raw material and hydrogenation tail oil through hydrofining (i.e. hydrogenating desulfurization and cracking); (gasoline, diesel oil can be used as product sell, gas proceeds gas sweetening and preparation, and fcc raw material proceeds catalysis lighting process, and hydrogenation tail oil enter base oil unit carry out isomerization dewaxing reaction and post-refining react.)
C () heavy feed stock process: > step (a) obtained 350 DEG C of residual oil are heated to 495 DEG C ~ 500 DEG C and carry out cracking and condensation reaction, generates coke and oil gas; (oil gas can send the separation column of crude oil with poor quality pretreatment unit back to, and the coke be flocked in coke drum can be cut burnt system through water conservancy and send by coke drum, as production marketing.)
(d) catalysis lighting: cracking reaction (macromole is cracked into small molecules, long-chain is fractured into short chain) occurs fcc raw material step (b) obtained under the effect of catalyzer, obtains dry gas, liquefied gas, gasoline, diesel oil and catalytic slurry; Catalytic slurry carries out the heavy feed stock process of step (c); Liquefied gas, gasoline, diesel oil are sold as product;
The reaction of (e) isomerization dewaxing and post-refining reaction: isomerization dewaxing reaction (the high condensation point normal alkane isomerization by hydrogenation tail oil) and post-refining reaction occur the hydrogenation tail oil that step (b) obtains under the effect of catalyzer, produce III class base oil; This III class base oil has low-viscosity, and (III No. 4, class, III class No. 6 100 DEG C of kinematic viscosity range are respectively 3.50-4.50mm
2.s
-1, 5.50-6.50mm
2.s
-1, specifically in table 6), low pour point (pour point of III No. 4, class, No. 6, III class not higher than-18 DEG C, specifically in table 6), the feature of viscosity index > 120.
F () gas sweetening and preparation: the gas that the dry gas obtain step (a) and the isolated gas of step (b) and step (d) and step (e) obtain carries out desulfurization and adsorb purifying, obtain hydrogen and release gas.
Above-mentioned crude oil with poor quality is paraffinic base crude oil with poor quality or middle coalite tar or the paraffinic base crude oil with poor quality containing middle coalite tar.Above-mentioned paraffinic base crude oil with poor quality is the paraffinic base crude oil with poor quality that at the original reservoir temperature, degas oil viscosity is 10000 ~ 50000mPa.s, relative density is greater than 0.93, sulphur content is greater than 2.0%; The pyrolysis temperature of described middle coalite tar is respectively 700 DEG C ~ 900 DEG C and 500 DEG C ~ 700 DEG C.
The adsorptive pressure used in step (f) is 1.2MPa ~ 3.0MPa.
First crude oil with poor quality can first be carried out washing after dehydration and solid settlement under 80 DEG C ~ 140 DEG C conditions again in step (a), desalination, dehydration and de-solid, preferably carry out under 90 DEG C of conditions.
In step (a), because of colloid in crude oil with poor quality, bituminous matter is high, light constituent is few, described pretreatment unit adopts " stove one tower " flow process, this pretreatment unit is primarily of stock oil storage tank, electrical desalter, interchanger, atmospheric pressure kiln and atmospheric fractional tower composition: crude oil with poor quality is through washing, desalination, dehydration and de-solid after with processed oil heat exchange to 200 DEG C ~ 250 DEG C (1.2MPa ~ 1.7MPa) with being pumped to process furnace, be heated to 360 DEG C ~ 390 DEG C and enter atmospheric fractional tower: isolated gas enters gas sweetening and prepares unit, isolated gasoline and diesel oil deliver to hydro-refining unit as outside product, isolate 330 DEG C ~ 350 DEG C atmospheric gas oils and enter desulfurization and Cracking Unit, isolated > 350 DEG C of residual oil enter heavy feed stock processing unit.Distill difference with conventional atmospheric to be to add 330 DEG C ~ 350 DEG C atmospheric gas oils and > 350 DEG C of residual oil separation functions, residual oil is divided into desulfurization and Cracking Unit raw material and heavy feed stock processing unit stock oil.The basis meeting desulfurization and Cracking Unit ingredient requirement reduces the treatment capacity of heavy feed stock processing unit, reaches the object of saving process cost and energy consumption.
Step (b) uses desulfurization and Cracking Unit, and stock oil and hydrogen are entering the forward slip value of process furnace.This unit arranges multiple reactor, to improve amount of finish; The type of hydrogenator can be fixed bed, moving-bed or ebullated bed.The catalyzer of hydrogenation reaction refers to the single or combination catalyst with functions such as hydrogenating desulfurization, hydrodenitrification, hydrodemetallation (HDM).The base metal active ingredient of general employing, the preferably metal oxide of VI B race and VIII race and sulfide, as W, Mo, Co, Ni, precious metal has Pt, Pd etc.; The acid additive added can be F, P or B of 0.5% ~ 4.0% or the amorphous silicic aluminium of 3% ~ 10% or molecular sieve; Selectable carrier has neutral carrier activated alumina, gac, diatomite etc., or acid carrier pure aluminium silicate, Magnesium Silicate q-agent, atlapulgite, molecular sieve etc.At present in fixed bed hydrogenation technology, be often that multiple catalysts supports the use, stock oil contacts with protective material, hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrogenation catalyst successively, or is loaded in mixture by this several catalyzer.In desulfurization described in step (b) and Cracking Unit, the reaction conditions of hydrotreatment is: temperature 350 DEG C ~ 400 DEG C, hydrogen dividing potential drop 10MPa ~ 25MPa, volume space velocity 0.5h
-1~ 2.0h
-1, hydrogen to oil volume ratio 500 ~ 1200.Stock oil removes sulphur, nitrogen, metal impurities in hydrogenator, and carries out aromatic saturation reaction.
The process of step (c) heavy feed stock uses heavy feed stock processing unit, and this unit, primarily of coking heater and coke drum composition, does not establish fractionation plant.> 350 DEG C of residual oil send into coking heater by the bottom of the atmospheric fractional tower of pretreatment unit with fresh feed pump, be heated to the bottom that 495 DEG C ~ about 500 DEG C enter coke drum, conventional cracking and condensation reaction is carried out in coke drum, top of coke tower working pressure is 0.15-0.2MPa, preferred operations pressure is 0.18MPa, generates coke and oil gas.High-temperature oil gas delivers to the atmospheric fractional tower of pretreatment unit, and the coke be flocked in coke drum is cut burnt system through water conservancy and sent by coke drum, as production marketing.
Step (d) catalysis lighting uses catalysis lighting unit, and primarily of reactor, catalyst regenerator, after-fractionating tower forms.Fcc raw material enters reactor, under the effect of catalyzer, cracking reaction occurs, and macromole is cracked into small molecules, long-chain is fractured into short chain.Reaction product enters after-fractionating tower, obtains dry gas, liquefied gas, gasoline, diesel oil and catalytic slurry through fractionation.Dry gas enters gas sweetening unit, and liquefied gas, gasoline, diesel oil are sold as product, and catalytic slurry enters heavy feed stock processing unit.Catalyzer enters catalyst regenerator after participating in reaction, turns back to reactor and continue to use after coke burning regeneration.
The catalyzer adopted in step (d) be selected from molecular sieve, heat-resistant inorganic oxide, molecular sieve and clay composition, heat-resistant inorganic oxide and clay composition, molecular sieve, heat-resistant inorganic oxide and clay composition one or more; Preferred catalyst is one or more in molecular sieve.Molecular sieve is self-contained or do not contain the y-type zeolite of rare earth element, contain or do not contain ultrastable Y－type zeolite, the supersiliceous zeolite with five-membered ring structure, the β zeolite of rare earth element, one or more in mordenite, omega zeolite, the supersiliceous zeolite with five-membered ring structure can be ZSM-5 zeolite or ZRP zeolite.One or more in the optional self-alumina of heat-resistant inorganic oxide, silicon oxide, amorphous silicon aluminium, zirconium white, titanium oxide, boron oxide and alkaline earth metal oxide.Clay can be selected from one or more in kaolin, halloysite, polynite, diatomite, halloysite, saponite, tired de-soil, sepiolite, attapulgite, hydrotalcite and boron-moisten soil.Wherein the activity of molecular sieve cracking catalyst is high, and green coke amount is few, and gasoline yield is high, transformation efficiency is the highest.
Catalysis lighting unit described in step (d), the reaction conditions of catalytic cracking is: temperature of reaction 470 DEG C ~ 550 DEG C, preferable reaction temperature 480 DEG C ~ 500 DEG C, regeneration temperature 600 DEG C ~ 800 DEG C, preferred regeneration temperature 700 DEG C ~ 750 DEG C, the mass ratio 3 ~ 18 of catalyzer and fcc raw material, preferred mass is than 8 ~ 12, reaction times 0.5s ~ 5s, preferred reaction time 2-4s, pressure 0.1MPa ~ 0.5MPa.Stock oil obtains dry gas, liquefied gas, gasoline, diesel oil and catalytic slurry (comprising catalytic cracking recycle oil and slurry oil) after catalysis lighting unit process is separated, and catalytic slurry delivers to heavy feed stock processing unit.
The reaction of step (e) isomerization dewaxing and the base oil unit described in post-refining reaction comprise isomerization dewaxing reactor, post-refining reactor and tripping device.The catalyzer of isomerization dewaxing reaction, can to select in this area conventional lube oil hydrogenation heterogeneous catalyst, can commodity in use hydrogenation catalyst, also can prepare according to this area general knowledge.This catalyzer comprises carrier and active metal component, or also comprises auxiliary agent.The carrier of hydroisomerization catalyst is generally LKZ molecular sieve or ZSM-22 molecular sieve etc., and usual molecular sieve content is in the catalyst 30wt% ~ 80wt%, is preferably 40wt% ~ 70wt%.Metal component in catalyzer be generally in Pt, Pd, Ru and Rh one or more, active metal component content is in the catalyst 0.1wt% ~ 30.0wt%.Selectable adjuvant component is containing one or more in boron, fluorine, chlorine and phosphoric, and auxiliary agent content is in the catalyst 0.1wt% ~ 5.0wt%.The specific surface area of catalyzer is 150m
2/ g ~ 500m
2/ g, pore volume is 0.15ml/g ~ 0.60ml/g.Before using, reduction treatment is carried out to catalyzer, make hydrogenation active metals be in reduced state in reaction process.Post-refining catalyzer is conventional reduced form Hydrobon catalyst, and this catalyzer can comprise carrier and active metal component, or also comprises auxiliary agent.Its active metal is one or both or reduced state nickel catalyzer in Pt, Pd, in catalyzer, active metal Pt and/or Pd weight content is in the catalyst generally 0.05% ~ 1%, the active metal of reduced state nickel catalyzer counts 30wt% ~ 80wt% with oxide weight, and carrier is generally Al
2o
3or Al
2o
3-SiO
2, auxiliary agent contains the elements such as P, Ti, B, Zr.Use procatalyst can carry out conventional reduction, ensure that hydrogenation active metals is in reduction-state in reaction process.
In step (e), 1. isomerization dewaxing reaction conditions comprises: temperature is 210 DEG C ~ and 400 DEG C, preferably 310 DEG C ~ 390 DEG C, hydrogen dividing potential drop is 10.0MPa ~ 25.0MPa, preferably 15.0MPa ~ 25.0MPa, and volume space velocity is 0.2h
-1~ 2.0h
-1, preferred 0.6h
-1~ 2.0h
-1, hydrogen to oil volume ratio is 100 ~ 2000Nm
3/ m
3, preferred 700 ~ 1000Nm
3/ m
3.2. post-refining reaction conditions is: temperature is 100 DEG C ~ and 290 DEG C, preferably 200 DEG C ~ 290 DEG C, hydrogen dividing potential drop is 10.0MPa ~ 25.0MPa, preferably 15.0MPa ~ 25.0MPa, and volume space velocity is 0.2h
-1~ 2.0h
-1, preferred 0.6h
-1~ 2.0h
-1, hydrogen to oil volume ratio is 100 ~ 2000Nm
3/ m
3, preferred 700 ~ 1000Nm
3/ m
3.
In the utility model, pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body are all sent into gas sweetening and prepare unit.Gas sweetening with prepare unit institute hydrogen producing for hydrogenating desulfurization unit and base oil unit, discharge gas as furnace fuel.
Gas sweetening described in the utility model with prepare unit and be made up of thionizer and PSA purifying plant.Pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body all enter thionizer, deviate from H
2enter PSA purifying plant after S, PSA purifying plant adopts 10-2-4 flow process (10 adsorption beds, 2 air inlets are all pressed for 4 times); By CO, the CO in dry gas in adsorption bed
2fall Deng Impurity Absorption, obtain hydrogen and release gas respectively.The hydrogen purity obtained is greater than 99.9%, and for desulfurization and Cracking Unit and base oil unit, release gas is used as furnace fuel.It is all have the solid particulate compared with bigger serface that PSA device carries out adsorbing the sorbent material selected by purifying, and mainly contains the molecular sieve of activated alumina class, gac class, silica type and routine; Adsorptive pressure is 1.2MPa ~ 3.0MPa.
Crude oil with poor quality quality examination is according to (the mensuration potentiometric titration of GB/T18609-2011 acid value for crude oil; The mensuration of wax, colloid, asphalt content in SY/T7550-2012 crude oil; GB/T17280-2009 crude distillation standard test methods 15-theoretical stage distillation column; GB/T17280-2009 crude distillation standard test methods 15-theoretical stage distillation column) to carry out, the equipment that the utility model is not described in detail and working method all can realize according to this area general knowledge.
The beneficial effects of the utility model compared with the prior art:
(1) the utility model is by crude oil with poor quality pre-treatment, heavy feed stock process, desulfurization and cracking, catalysis lighting, base oil and gas sweetening and prepare unit and be organically combined, and to greatest extent crude oil with poor quality is changed into the III class base oil of low-viscosity that light-end products, refinery coke and China is badly in need of, low pour point, viscosity index ﹥ 120; Product category is many, can meet multi-field development need, and can simplification of flowsheet, reduces overall energy consumption.
(2) pretreatment unit adds 330 DEG C ~ 350 DEG C atmospheric gas oils and > 350 DEG C of residual oil separation functions, residual oil is divided into desulfurization and Cracking Unit raw material and heavy feed stock processing unit stock oil.The basis meeting desulfurization and Cracking Unit ingredient requirement reduces the treatment capacity of heavy feed stock processing unit, reaches the object of saving process cost and energy consumption.This is the core of this patent.
(3) heavy feed stock processing unit does not establish fractionation plant, simplifies technical process, reduces facility investment and running cost, decreases calorific loss simultaneously.
(4) pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body all enter thionizer, deviate from H
2enter PSA purifying plant after S, purify through PSA, the hydrogen purity obtained is greater than 99.9%, for desulfurization and Cracking Unit and base oil unit; Release gas is used as furnace fuel, at utmost make use of system internal product, reduces energy consumption.
(5) residual oil is fractionated into 330 DEG C ~ 350 DEG C atmospheric gas oils and > 350 DEG C of residual oil by pretreatment unit.330 DEG C ~ 350 DEG C atmospheric gas oils enter desulfurization and Cracking Unit, > 350 DEG C of residual oil are used further to desulfurization and Cracking Unit raw material after heavy feed stock processing unit processes, both the yield of gasoline, diesel oil had been improved, again reduce technical difficulty and the hydrogen consumption of hydrotreatment, prolong operation cycle.
(6) crude oil with poor quality pre-treatment, heavy feed stock process, desulfurization and cracking, catalysis lighting, base oil and gas sweetening and preparation unit associations are run, and both reduce investment, turn improve full factory heat utilization ratio.
Accompanying drawing explanation
Fig. 1 is the system schematic that the utility model crude oil with poor quality produces gasoline, diesel oil and refinery coke and top-grade lubricating oil base oil.
Wherein, 1, stock oil storage tank, 2, electrical desalter, 3, interchanger, 4, atmospheric pressure kiln, 5, atmospheric fractional tower, 6, coking heater, 7, coke drum, 8, reactor, 9, catalyst regenerator, 10, after-fractionating tower, the 11, first hydrogenator, 12, the second hydrogenator, the 13, first separation column, 14, tripping device, 15, post-refining reactor, 16, isomerization dewaxing reactor, 17, thionizer, 18, PSA purifying plant, 19, hydro-refining unit, 20, process furnace.
Embodiment
Below in conjunction with accompanying drawing, the utility model is further described.
As shown in Figure 1, crude oil with poor quality produces a system for gasoline, diesel oil, refinery coke and top-grade lubricating oil base oil, and this system comprises crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy feed stock processing unit, catalysis lighting unit, base oil unit and gas sweetening and prepares unit;
Crude oil with poor quality pretreatment unit comprises stock oil storage tank 1, electrical desalter 2, interchanger 3, atmospheric pressure kiln 4 and atmospheric fractional tower 5; Multiple outlets of the atmospheric fractional tower 5 of crude oil with poor quality pretreatment unit connect desulfurization and Cracking Unit, heavy feed stock processing unit, gas sweetening respectively by pipeline and prepare unit and hydro-refining unit 19.
Desulfurization and Cracking Unit comprise the first hydrogenator 11, second hydrogenator 12 and the first separation column 13;
Heavy feed stock processing unit comprises coking heater 6 and coke drum 7; Catalysis lighting unit comprises reactor 8, catalyst regenerator 9 and after-fractionating tower 10; Base oil unit comprises isomerization dewaxing reactor 16, post-refining reactor 15 and tripping device 14; Gas sweetening with prepare unit and be made up of thionizer 17 and PSA purifying plant 18; Multiple outlets of crude oil with poor quality pretreatment unit separation column 5 connect the first separation column 13 of desulfurization and Cracking Unit, the coking heater 6 of heavy feed stock processing unit and coke drum 7 respectively by pipeline, gas sweetening and the thionizer 17 preparing unit; The interchanger 3 of crude oil with poor quality pretreatment unit connects the outlet of the after-fractionating tower 10 of catalysis lighting unit.
Desulfurization and the outlet of the first separation column 13 of Cracking Unit are connected gas sweetening and thionizer 17, the isomerization dewaxing reactor 16 of base oil unit, the reactor 8 of catalysis lighting unit of preparing unit respectively, and desulfurization is connected the outlet of the second hydrogenator 12 with the entrance of the first separation column 13 of Cracking Unit.
The entrance of the coking heater 6 in heavy feed stock processing unit is connected by the outlet of pipeline with the after-fractionating tower 10 of catalysis lighting unit, and meanwhile, coke drum 7, coking heater 6 and atmospheric fractional tower 5 connect into loop by pipeline.
The outlet of the after-fractionating tower 10 of catalysis lighting unit is respectively by pipeline and gas sweetening and the thionizer 17 preparing unit, and the interchanger 3 of crude oil with poor quality pretreatment unit is connected, the outlet of the entrance ligation device 8 of the after-fractionating tower 10 of catalysis lighting unit.
The isomerization dewaxing reactor 16 of base oil unit is connected with the PSA purifying plant 18 preparing unit with gas sweetening by pipeline.
The tripping device 14 of base oil unit is connected with the thionizer 17 preparing unit with gas sweetening by pipeline.
Described gas sweetening and the PSA purifying plant 18 preparing unit are connected the entrance of process furnace 20 by pipeline, the outlet of process furnace 20 connects the entrance of the first hydrogenator 11 of desulfurization and Cracking Unit.
Steam heating coil is established in described stock oil storage tank 1.
Crude oil with poor quality produces the method for gasoline, diesel oil, refinery coke and top-grade lubricating oil base oil, specifically comprises the steps:
External crude oil with poor quality send into stock oil storage tank (inside establish steam heating coil, use steam coal tar is heated to 90 DEG C carry out dewatering, solid settlement) store.Crude oil with poor quality by storage tank with being pumped to electrical desalter, carry out washing, desalination, after dehydration and de-solid with processed oil heat exchange to 220 DEG C (1.6MPa) with being pumped to atmospheric pressure kiln, be heated to 380 DEG C and enter atmospheric fractional tower, isolated gas enters gas sweetening and prepares unit, hydro-refining unit sent into by isolated gasoline and diesel oil, obtains treated gasoline product and diesel product; Isolated 330 DEG C ~ 350 DEG C atmospheric gas oils enter desulfurization and Cracking Unit, and isolated > 350 DEG C of residual oil enter heavy feed stock processing unit.
Through being pumped to process furnace after 330 DEG C ~ 350 DEG C atmospheric gas oils mix with the purifying hydrogen of hydrogen that subsequent cell produces, enter the first hydrogenator, the second hydrogenator and separation column after being heated to certain temperature successively, obtain dry gas, gasoline products, diesel product, fcc raw material and hydrogenation tail oil through hydrogenating desulfurization and cracking.Dry gas enters gas sweetening and prepares unit, and gasoline, diesel oil are sold as product, and fcc raw material enters catalysis lighting unit, and hydrogenation tail oil enters base oil unit.
> 350 DEG C of residual oil send into coking heater by the Fractionator Bottom fresh feed pump of pretreatment unit, are heated to 495 DEG C ~ 500 DEG C and enter and enter from the bottom of coke drum, in coke drum, carry out cracking and condensation reaction, generate coke and oil gas.Oil gas delivers to the atmospheric fractional tower of pretreatment unit, and the coke be flocked in coke drum is cut burnt system through water conservancy and sent by coke drum, as production marketing.
The fcc raw material obtained by desulfurization and Cracking Unit enters catalysis lighting unit, and catalysis lighting unit is by reactor, catalyst regenerator, and after-fractionating tower forms.Fcc raw material enters reactor, under the effect of catalyzer, cracking reaction occurs, and macromole is cracked into small molecules, long-chain is fractured into short chain.Reaction product enters after-fractionating tower, obtains dry gas, liquefied gas, gasoline products, diesel product and catalytic slurry through fractionation.Dry gas enters gas sweetening and prepares unit, and liquefied gas, gasoline, diesel oil are sold as product, and catalytic slurry enters heavy feed stock processing unit.Catalyzer enters catalyst regenerator after participating in reaction, turns back to reactor and continue to use after coke burning regeneration.
Base oil unit is entered after the purifying hydrogen of hydrogen that hydrogenation tail oil and subsequent cell produce mixes, base oil unit comprises isomerization dewaxing reactor, post-refining reactor and tripping device, obtains the III class base oil of dry gas and low-viscosity, low pour point, viscosity index ﹥ 120 through reaction and separation processes.Dry gas enters gas sweetening and prepares unit, and base oil is as production marketing.
The all gas that this device produces all enters gas sweetening and prepares unit, and this unit is made up of thionizer and PSA purifying plant.Gas all enters thionizer, deviates from H
2enter PSA purifying plant after S, obtain purifying hydrogen of hydrogen and release gas.The hydrogen purity obtained is greater than 99.9%, and for desulfurization and Cracking Unit and base oil unit, release gas is used as furnace fuel.
Below by specific embodiment, the method that the utility model provides is described further, but does not therefore limit the utility model.
Embodiment 1
Full device total technological process adopts inferior raw material pre-treatment-heavy oil feedstock process-desulfurization and cracking-catalysis lighting-base oil to produce the-lighting processing method that organically combines of gas sweetening and preparation technology.
Crude cut is dry gas, gasoline, diesel oil, atmospheric gas oil and residual oil by feed material preparation units.Dry gas enters gas sweetening and prepares unit, gasoline and diesel oil deliver to hydro-refining unit as outside product, obtain refining petrol and diesel oil product, 330 DEG C ~ 350 DEG C atmospheric gas oils enter desulfurization and Cracking Unit, and isolated > 350 DEG C of residual oil enter heavy feed stock processing unit.
330 DEG C ~ 350 DEG C atmospheric gas oils enter desulfurization and Cracking Unit, obtain gas, gasoline, diesel oil, fcc raw material and hydrogenation tail oil through hydrogenating desulfurization and cracking.Gasoline, diesel oil is sold as product, and gas enters gas sweetening and prepares unit, and fcc raw material enters catalysis lighting unit, and hydrogenation tail oil enters base oil unit.
> 350 DEG C of residual oil enter heavy feed stock processing unit, residual oil sends into process furnace by the Fractionator Bottom fresh feed pump of pretreatment unit, be heated to the bottom that 495 DEG C ~ about 500 DEG C enter coke drum, in coke drum, carry out cracking and condensation reaction, generate coke and oil gas.High-temperature oil gas delivers to the separation column of pretreatment unit, and the coke be flocked in coke drum is cut burnt system through water conservancy and sent by coke drum, as production marketing.
Fcc raw material from desulfurization and Cracking Unit enters catalysis lighting unit, cracking reaction is there is under ZSM-5 zeolite or ZRP zeolite are as the effect of catalyzer, macromole is cracked into small molecules, long-chain is fractured into short chain, thus obtains dry gas, liquefied gas, gasoline, diesel oil and catalytic slurry.Dry gas enters gas sweetening and prepares unit unit, and liquefied gas, gasoline, diesel oil are sold as product, and catalytic slurry enters heavy feed stock processing unit.
Hydrogenation tail oil enters base oil unit, isomerization reaction is there is under the effect of lube oil hydrogenation heterogeneous catalyst, post-refining catalyzer is conventional reduced form Hydrobon catalyst: its active metal is nickel, counts 50wt% ~ 60wt% with oxide weight, and carrier is Al
2o
3.By the high condensation point normal alkane isomerization in stock oil, produce the III class base oil of the low-viscosity of China's urgent need, low pour point, viscosity index ﹥ 120.
In the present invention, pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body are all sent into gas sweetening and prepare unit.Gas sweetening with prepare unit institute hydrogen producing for hydrogenating desulfurization unit and base oil unit, discharge gas as furnace fuel.
The crude oil with poor quality feedstock property that embodiment and comparative example adopt is in table 1, prevailing operating conditions is in table 2, product slates is in table 3, gasoline property is in table 4, diesel oil character is in table 5, and the criteria for classification of lubricant base is in table 6, and base oil technical requirements is in table 7, base oil character is in table 8, and refinery coke character is in table 9.
Embodiment 2
Raw material, the technical process of employing are identical with embodiment 1, change the reaction conditions of desulfurization and Cracking Unit, and the catalyzer that catalysis lighting unit uses is aluminum oxide, and other reaction conditionss are constant, as shown in table 2, and product slates is in table 3, and product property is in table 4 ~ 9.
Embodiment 3
Raw material, the technical process of employing are identical with embodiment 1, change the reaction conditions of catalysis lighting unit, and the catalyzer that catalysis lighting unit uses is the y-type zeolite containing rare earth element, other reaction conditionss are constant, as shown in table 2, product slates is in table 3, and product property is in table 4 ~ 9.
Embodiment 4
Raw material, the technical process of employing are identical with embodiment 1, change the reaction conditions of base oil unit, the catalyzer that catalysis lighting unit uses is not containing the y-type zeolite of rare earth element, silicon oxide and kaolin are according to the mixture of 1:1:1, other reaction conditionss are constant, as shown in table 2, product slates is in table 3, and product property is in table 4 ~ 9.
Comparative example
Adopt the raw material identical with embodiment 1, as different from Example 1, dry gas deviates from H through digester
2after S without gas sweetening with prepare unit and directly as recycle hydrogen for desulfurization and Cracking Unit and base oil unit; Operational condition is in table 2, and product slates is in table 3, and the product property obtained is in table 4, table 5, table 8.
Table 1 oil property
| Density 20 DEG C, g/cm 3 | 0.9334 |
| C content, m% | 87.11 |
| H content, m% | 12.3 |
| S content, m% | 2.4 |
| N content, m% | 0.3 |
| Characterization factor, K | 13.5 |
| Carbon residue, m% | 6.2 |
| Metal (Ni+V), μ g/g | 30.4 |
| Colloid, m% | 16.0 |
| Bituminous matter, m% | 0.1 |
| Boiling range | ? |
| 15～200℃ | 7.51 |
| 200～350℃ | 24.55 |
| 350～500℃ | 32.44 |
| >500℃ | 35.5 |
Table 2 prevailing operating conditions
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 |
| Inferior raw material pretreatment unit | ? | ? | ? | ? |
| Stock oil storage tank heat temperature/DEG C | 90 | 90 | 90 | 90 |
| With temperature after processed oil heat exchange/DEG C | 220 | 220 | 220 | 220 |
| With pressure/MPa after processed oil heat exchange | 1.6 | 1.6 | 1.6 | 1.6 |
| Furnace outlet temperature/DEG C | 380 | 380 | 380 | 380 |
| Heavy feed stock processing unit | ? | ? | ? | ? |
| Outlet Temperature in Delayed Coking Furnace/DEG C | 500 | 500 | 500 | 500 |
| Top of coke tower working pressure/MPa | 0.18 | 0.18 | 0.18 | 0.18 |
| Desulfurization and Cracking Unit | ? | ? | ? | ? |
| First hydrogenator | ? | ? | ? | ? |
| Reactor inlet hydrogen dividing potential drop/MPa | 25 | 15.3 | 25 | 25 |
| Hydrogen to oil volume ratio Nm 3/m 3 | 1000 | 800 | 1000 | 1000 |
| Running just/latter stage average reaction temperature/DEG C | 360/395 | 355/390 | 360/395 | 360/395 |
| Volume space velocity/h -1 | 1.2 | 0.8 | 1.2 | 1.2 |
| Second hydrogenator | ? | ? | ? | ? |
| Reactor inlet hydrogen dividing potential drop/MPa | 24.7 | 15 | 24.7 | 24.7 |
| Hydrogen to oil volume ratio Nm 3/m 3 | 900 | 800 | 900 | 900 |
| Running just/latter stage average reaction temperature/DEG C | 350/385 | 345/380 | 350/385 | 350/385 |
| Volume space velocity/h -1 | 1.5 | 1 | 1.5 | 1.5 |
| Catalysis lighting unit | ? | ? | ? | ? |
| Temperature of reaction/DEG C | 500 | 500 | 480 | 500 |
| Regeneration temperature/DEG C | 750 | 750 | 750 | 750 |
| Catalyzer/fcc raw material/m% | 10 | 10 | 10 | 10 |
| Reaction times/s | 2 | 2 | 4 | 2 |
| Pressure/MPa | 0.2 | 0.2 | 0.28 | 0.2 |
| Base oil unit | ? | ? | ? | ? |
| Isomerization dewaxing segment process condition | ? | ? | ? | ? |
| Reactor inlet hydrogen dividing potential drop/MPa | 25 | 25 | 25 | 15.3 |
| Hydrogen to oil volume ratio Nm 3/m 3 | 1000 | 1000 | 1000 | 800 |
| Running just/latter stage average reaction temperature/DEG C | 340/380 | 340/380 | 340/380 | 320/380 |
| Volume space velocity/h -1 | 2.0 | 2.0 | 2.0 | 1.2 |
| Post-refining process condition | ? | ? | ? | ? |
| Reactor inlet hydrogen dividing potential drop/MPa | 24.7 | 24.7 | 24.7 | 15 |
| Hydrogen to oil volume ratio Nm 3/m 3 | 900 | 900 | 900 | 800 |
| Running just/latter stage average reaction temperature/DEG C | 220/270 | 220/270 | 220/270 | 220/285 |
| Volume space velocity/h -1 | 2.0 | 2.0 | 2.0 | 1.2 |
| Gas sweetening with prepare unit | ? | ? | ? | ? |
| PSA purifies | ? | ? | ? | ? |
| Sorbent material | Molecular sieve | Molecular sieve | Molecular sieve | Molecular sieve |
| Adsorptive pressure/MPa | 2.0 | 2.0 | 2.0 | 2.0 |
Table 3 product slates table
| ? | Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example |
| Gas (wt%) | 5.13 | 6.12 | 5.02 | 7.78 |
| Liquefied gas (wt%) | 4.88 | 6.38 | 4.75 | 6.88 |
| Gasoline (wt%) | 25.64 | 24.40 | 23.45 | 20.35 |
| Diesel oil (wt%) | 32.71 | 28.73 | 31.62 | 29.98 |
| Lubricant base (wt%) | 16.58 | 17.07 | 18.34 | 15.58 |
| Refinery coke (wt%) | 15.05 | 17.28 | 16.81 | 19.42 |
| Loss (wt%) | 0.01 | 0.02 | 0.01 | 0.01 |
Table 4 gasoline products property list
Table 5 diesel product property list
Table 6API lubricant base criteria for classification
The technical requirements of table 7 base oil
Table 8 base oil property list
| Product | Embodiment 1 | Embodiment 2 | Embodiment 4 | Comparative example |
| ? | III No. 6, class | Ⅱ +No. 6, class | III No. 4, class | Ⅱ +No. 4, class |
| Density (20 DEG C)/kg.m -1 | 836.5 | 832.1 | 833.9 | 831.5 |
| Viscosity (100 DEG C)/mm 2.s -1 | 6.242 | 6.108 | 3.925 | 4.237 |
| Viscosity index | 124 | 118 | 125 | 115 |
| Pour point/DEG C | -20 | -30 | -20 | -25 |
| Sai Shi color/number | +30 | +30 | +30 | +30 |
| Flash-point (opening)/DEG C | 215 | 210 | 190 | 186 |
| Sulphur content/μ g.g -1 | 1.0 | ＜10.0 | ＜10.0 | ＜10.0 |
| Stable hydrocarbon/% | ＞99.0 | ＞99.0 | ＞99.0 | ＞99.0 |
| Oxidation stability/min | ＞300 | ＞300 | ＞300 | ＞300 |
Table 9 refinery coke property list
| Title | Refinery coke |
| True density, g/cm 3 | 1.85 |
| Sulphur content, wt% | 2.53 |
| Ash content, wt% | 0.36 |
| Volatile matter, wt% | 15 |
| Moisture, wt% | 15.2 |
Claims (10)
1. produce a system for petrol and diesel oil, refinery coke and top-grade lubricating oil base oil, it is characterized in that this system comprises crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy feed stock processing unit, catalysis lighting unit, base oil unit and gas sweetening and prepares unit;
Crude oil with poor quality pretreatment unit is respectively by pipeline and desulfurization and Cracking Unit, heavy feed stock processing unit, gas sweetening and prepare unit and be connected;
Desulfurization and Cracking Unit respectively by pipeline and catalysis lighting unit, base oil unit and gas sweetening with prepare unit and be connected;
Heavy feed stock processing unit is connected with catalysis lighting unit by pipeline;
Catalysis lighting unit by pipeline and gas sweetening with prepare unit and be connected;
Base oil unit by pipeline and gas sweetening with prepare unit and be connected.
2. system according to claim 1, is characterized in that, crude oil with poor quality pretreatment unit comprises stock oil storage tank (1), electrical desalter (2), interchanger (3), atmospheric pressure kiln (4) and atmospheric fractional tower (5); Multiple outlets of the atmospheric fractional tower (5) of crude oil with poor quality pretreatment unit connect desulfurization and Cracking Unit, heavy feed stock processing unit, gas sweetening respectively by pipeline and prepare unit and hydro-refining unit (19).
3. system according to claim 1, is characterized in that, desulfurization and Cracking Unit comprise the first hydrogenator (11), the second hydrogenator (12) and the first separation column (13);
Heavy feed stock processing unit comprises coking heater (6) and coke drum (7);
Catalysis lighting unit comprises reactor (8), catalyst regenerator (9) and after-fractionating tower (10);
Base oil unit comprises isomerization dewaxing reactor (16), post-refining reactor (15) and tripping device (14);
Gas sweetening with prepare unit and be made up of thionizer (17) and PSA purifying plant (18);
Multiple outlets of crude oil with poor quality pretreatment unit separation column (5) connect first separation column (13) of desulfurization and Cracking Unit respectively by pipeline, the coking heater (6) of heavy feed stock processing unit and coke drum (7), gas sweetening and the thionizer (17) preparing unit; The interchanger (3) of crude oil with poor quality pretreatment unit connects the outlet of the after-fractionating tower (10) of catalysis lighting unit.
4. system according to claim 3, it is characterized in that, desulfurization and the outlet of first separation column (13) of Cracking Unit are connected gas sweetening and thionizer (17), the isomerization dewaxing reactor (16) of base oil unit, the reactor (8) of catalysis lighting unit of preparing unit respectively, and desulfurization is connected the outlet of the second hydrogenator (12) with the entrance of first separation column (13) of Cracking Unit.
5. system according to claim 3, it is characterized in that, the entrance of the coking heater (6) in heavy feed stock processing unit is connected by the outlet of pipeline with the after-fractionating tower (10) of catalysis lighting unit, meanwhile, coke drum (7), coking heater (6) and atmospheric fractional tower (5) connect into loop by pipeline.
6. system according to claim 3, it is characterized in that, the outlet of the after-fractionating tower (10) of catalysis lighting unit is respectively by pipeline and gas sweetening and the thionizer (17) preparing unit, and the interchanger of crude oil with poor quality pretreatment unit (3) is connected, the outlet of the entrance ligation device (8) of the after-fractionating tower (10) of catalysis lighting unit.
7. system according to claim 3, is characterized in that, the isomerization dewaxing reactor (16) of base oil unit is connected with the PSA purifying plant (18) preparing unit with gas sweetening by pipeline.
8. system according to claim 3, is characterized in that, the tripping device (14) of base oil unit is connected with the thionizer (17) preparing unit with gas sweetening by pipeline.
9. system according to claim 3, it is characterized in that described gas sweetening and the PSA purifying plant (18) preparing unit are connected the entrance of process furnace (20) by pipeline, the outlet of process furnace (20) connects the entrance of first hydrogenator (11) of desulfurization and Cracking Unit.
10. system according to claim 1, is characterized in that establishing steam heating coil in described stock oil storage tank (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420221682.4U CN204097413U (en) | 2014-04-27 | 2014-04-27 | Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420221682.4U CN204097413U (en) | 2014-04-27 | 2014-04-27 | Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204097413U true CN204097413U (en) | 2015-01-14 |
Family
ID=52265858
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420221682.4U Expired - Fee Related CN204097413U (en) | 2014-04-27 | 2014-04-27 | Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204097413U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018143A (en) * | 2014-04-27 | 2015-11-04 | 中石化南京工程有限公司 | Method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil |
| CN108138591A (en) * | 2015-08-24 | 2018-06-08 | 沙特阿拉伯石油公司 | The recycling and reuse of discarded energy in industrial equipment |
-
2014
- 2014-04-27 CN CN201420221682.4U patent/CN204097413U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105018143A (en) * | 2014-04-27 | 2015-11-04 | 中石化南京工程有限公司 | Method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil |
| CN105018143B (en) * | 2014-04-27 | 2017-01-25 | 中石化南京工程有限公司 | Method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil |
| CN108138591A (en) * | 2015-08-24 | 2018-06-08 | 沙特阿拉伯石油公司 | The recycling and reuse of discarded energy in industrial equipment |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103305271B (en) | The combined technical method of a kind of residual oil/middle coalite tar lighting | |
| CN102041029B (en) | Comprehensive utilization method of hydrocracking tail oil | |
| CN101191080A (en) | Catalyst continuous reproducible low octane rating gasoline modifying method | |
| CN105001908B (en) | The method and system of crude oil with poor quality production aromatic hydrocarbons, petroleum coke and high-knock rating gasoline | |
| CN104593068A (en) | A method of producing gasoline with a high octane number from residual oil | |
| CN102041047B (en) | Heavy oil hydrogenation modifying method | |
| CN106147852B (en) | A kind of method by producing diesel by utilizing coal tar component | |
| CN204097413U (en) | Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil | |
| CN112322343B (en) | Method and device for producing high-aromatic-content gasoline by MTP byproduct mixed aromatic hydrocarbon modification, high-aromatic-content gasoline and application thereof | |
| CN101724463A (en) | Combined process method for performing hydro-cracking and catalytic cracking on suspension bed residual oil | |
| CN103289741B (en) | A combined method of hydrotreating-catalytic cracking-PSA purification for heavy oil | |
| CN101942339B (en) | Boiling-bed residual-oil hydrocracking and catalytic-cracking combined process method | |
| CN105018138B (en) | Method and system for producing aromatic hydrocarbon, asphalt and high-octane gasoline through inferior crude oil | |
| CN100510022C (en) | Low-hydrogenloss hydrogenation of high-output qulified diesel oil | |
| CN109777481B (en) | Combined processing method for refinery gas | |
| CN203845992U (en) | Paraffin base inferior crude oil poly-generation system | |
| CN105001907B (en) | A kind of method and system of paraffinic base crude oil with poor quality Poly-generation | |
| CN104277878B (en) | A kind of two-stage slurry state bed hydroprocessing technique of high temperature coal-tar | |
| CN104611049A (en) | Catalytic diesel fuel reaction distillation method | |
| CN104593061B (en) | A kind of residual hydrocracking and catalytic cracking combined processing method | |
| CN105018143B (en) | Method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil | |
| CN109777488B (en) | Refinery gas combined processing technology | |
| CN103059951B (en) | Catalytic cracking and catalytic gasoline hydrogenation combined technological method | |
| CN204185436U (en) | Produce the system of gasoline, diesel oil, pitch and top-grade lubricating oil base oil | |
| CN105018142B (en) | Produce gasoline, the method and system of diesel oil, Colophonium and top-grade lubricating oil base oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150114 Termination date: 20210427 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |