CN105018143B - Method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil - Google Patents
Method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil Download PDFInfo
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Abstract
The invention discloses a method and system for producing naphtha and diesel oil, petroleum coke and high-grade lubricating oil base oil through poor-quality crude oil. The method organically combines poor-quality crude oil pretreatment, desulfuration and cracking, heavy raw material treatment, catalytic lightweight, isodewaxing reaction, finishing refining reaction, and gas purification and preparation, the poor-quality crude oil is converted into light oil, petroleum coke and the third kind of base oil urgently needed in China to the maximum extent, and the base oil is low in viscosity and low in pour point, and the viscosity index is larger than 120. Products are multiple in variety, development requirements of multiple fields can be met, the technological process can be simplified, and overall energy consumption is reduced.
Description
Technical field
The invention belongs to oil refining, petrochemical industry, coal chemical technology, it is related to a kind of method of crude oil with poor quality lighting, specifically
Say be crude oil with poor quality is pre-processed, heavy charge is processed, desulfurization and cracking, catalysis lighting, base oil preparation and gas purification
Lighting process with preparation technology organic assembling.
Background technology
Become weight, deteriorate with worldwide oil property, and the requirement of sustained economic development and environmental regulation
Increasingly stringent, people are increasing to the demand of light clean fuel, these require existing oil Refining Technologies are carried out perfect
And improvement, satisfactory product is produced with minimum cost processing crude oil with poor quality.
Because crude oil with poor quality viscosity is high, higher than great, heavy metal and sulfur content and colloid, asphalitine, using existing refining
Oil tech carries out crude oil with poor quality processing, there is gasoline and diesel yield is low, and heat energy loss is big, the unfavorable factor such as equipment investment height.
Petroleum coke is the material producing electrode, graphite, carbon, nuclear reactor deceleration rod etc., in industry, national defence, medical treatment, boat
The aspect such as it and atomic energy also has been widely used, and is a kind of material that national economy and scientific technological advance are had a major impact
Material.Produce petroleum coke using crude oil with poor quality to meeting China's economy and scientific technological advance important in inhibiting.
With developing by leaps and bounds of auto manufacturing of China, aerospace industries and high-speed railway, the consumption of China's lubricating oil
Total amount also presents and increases substantially.It is reported that, China's lubricating oil consumption figure in 2012 is more than 10,000,000 tons, and lubricating oil annual production is then
Ten thousand tons only more than 800, huge breach can only rely on import to make up, particularly top-grade lubricating oil, and 80% needs to rely on import.High
Shelves lubricating oil is a kind of very high product of technology content, and it is related to various important industries, such as: automobile, aviation, engine, machine
Tool manufacture, national defence etc., passive situation therefore under one's control should change as early as possible.
Lubricating oil is to be main body by base oil, adds a small amount of additive and be in harmonious proportion forming, the technical indicator of base oil and matter
Amount decides lubricants performance and technical indicator.The production of top-grade lubricating oil, basic oil quality is a highly important ring.At present
Internal lube oil base oil also need to be from a large amount of import in the ground such as Korea S, Singapore, this explanation, and China is in the producer of top-grade lubricating oil
Face does not change passive situation under one's control yet.
Produce top-grade lubricating oil base oil using crude oil with poor quality, raw material sources can be increased, reduce production cost, right
Meeting China's economic development has definite meaning.
Patent cn1746265a discloses a kind of processing technology of poor-quality oil catalytic cracking.Inferior oil material is through catalytic cracking
The light diesel fuel cut Returning catalyticing cracking device obtaining carries out freshening, and the heavy diesel fuel cut obtaining carries out solvent extraction, extracts
Heavy aromatics as product, Returning catalyticing cracking device freshening of raffinating oil.But, this process is to crude oil with poor quality lighting not
Enough abundant, catalytic cracked oil pulp is not made full use of.
Content of the invention
The purpose of the present invention is in prior art basis, provides a kind of crude oil with poor quality pretreatment, heavy charge to process, take off
Sulphur and the lighting process of cracking, catalysis lighting, base oil preparation and gas purification and preparation technology organic assembling,
Crude oil with poor quality is changed into the low-viscosity of light-end products, petroleum coke and China's urgent need, low pour point, Viscosity Index 120 by limits ground
Class base oil, simplification of flowsheet, reduce overall energy consumption.
The purpose of the present invention is accomplished by:
A kind of crude oil with poor quality produces gasoline, the method for diesel oil, petroleum coke and top-grade lubricating oil base oil, and the method includes bad
The pretreatment of matter crude oil, desulfurization are reacted with cracking, heavy charge process, catalysis lighting, isomerization dewaxing and post-refining reacts, gas
Body purifies and preparation process, specifically comprises the following steps that
A () crude oil with poor quality pre-processes: crude oil with poor quality is carried out washing, desalination, dehydration and de- solid, heat exchange to 200 DEG C～
250 DEG C (preferably heat exchange to 220 DEG C～230 DEG C), then be heated to 360 DEG C～390 DEG C by heating furnace and (be preferably heated to 380 DEG C
～390 DEG C), enter atmospheric fractional tower: isolate gas, gasoline, diesel oil, 330 DEG C～350 DEG C AGO (atmospheric gas oil)s and 350 DEG C of ＞
Residual oil；
(b) desulfurization and cracking: 330 DEG C～350 DEG C AGO (atmospheric gas oil)s that step (a) obtains (are hydrogenated with through hydrofinishing
Desulfurization and cracking) obtain gas, gasoline, diesel oil, fcc raw material and hydrogenation tail oil；(gasoline, diesel oil can be sold as product,
Gas proceeds gas purification and preparation, and fcc raw material proceeds to be catalyzed lighting process, and hydrogenation tail oil enters basis
Oily unit carries out isomerization dewaxing reaction and post-refining reaction.)
C () heavy charge is processed: 350 DEG C of residual oil of ＞ that step (a) is obtained are heated to 495 DEG C～500 DEG C and are cracked
And condensation reaction, generate coke and oil gas；(oil gas can send the fractionating column of crude oil with poor quality pretreatment unit back to, is flocked on coke drum
Interior coke can be cut burnt system through water conservancy and be sent by coke drum, as production marketing.)
D () is catalyzed lighting: the fcc raw material that step (b) is obtained occurs cracking reaction (big in the presence of catalyst
Molecule is cracked into small molecule, long-chain is fractured into short chain), obtain dry gas, liquefied gas, gasoline, diesel oil and catalytic slurry；Catalytic slurry
The heavy charge carrying out step (c) is processed；Liquefied gas, gasoline, diesel oil are sold as product；
The reaction of (e) isomerization dewaxing and post-refining reaction: the hydrogenation tail oil that step (b) obtains is sent out in the presence of catalyst
Raw isomerization dewaxing reaction (the high condensation point normal alkane isomerization by hydrogenation tail oil) and post-refining reaction, produce class basis
Oil；Such base oil have low-viscosity (class 4, No. 6 100 DEG C of kinematic viscosity range of class be respectively 3.50～
4.50mm2.s-1, 5.50～6.50mm2.s-1, be specifically shown in Table 6), low pour point (class 4, the pour point not higher than -18 of class 6
DEG C, specifically it is shown in Table 6), the feature of Viscosity Index ＞ 120.
(f) gas purification and preparation: the dry gas that the gas that isolate step (a) and step (b) and step (d) obtain
And the gas that step (e) obtains carries out desulfurization and absorption purification, 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 containing middle coalite tar
Crude oil with poor quality.Above-mentioned paraffinic base crude oil with poor quality be at a temperature of the original reservoir degassing oil viscosity be 10000～50000mpa.s, relatively
Density is more than the paraffinic base crude oil with poor quality that 0.93, sulfur content is more than 2.0%；The pyrolysis temperature of described middle coalite tar is respectively
For 700 DEG C～900 DEG C and 500 DEG C～700 DEG C.
In step (a), crude oil with poor quality is first dehydrated under the conditions of 80 DEG C～140 DEG C and carries out again washing after settling with solid, take off
Salt, dehydration and de- solid, are preferably carried out under the conditions of 90 DEG C.
, because of colloid, asphalitine height in crude oil with poor quality, light component is few, using pretreatment unit, and adopts for step (a) of the present invention
" stove one tower " flow process, this pretreatment unit is mainly by raw material oil tank, electrical desalter, heat exchanger, atmospheric pressure kiln and normal pressure
Fractionating column forms: crude oil with poor quality is heated to 80～140 DEG C in raw material oil tank, enters electrical desalter afterwards, in electro-desalting
In tank after washing, desalination, dehydration and de- solid after with product oil heat exchange to 200 DEG C～250 DEG C (1.2mpa～1.7mpa)
With being pumped to heating furnace, it is heated to 360 DEG C～390 DEG C entrance atmospheric fractional towers: the gas isolated enters gas purification and system
Standby unit, the gasoline isolated and diesel oil deliver to hydro-refining unit as outside product；Isolate 330 DEG C～350 DEG C normal pressures watt
This oil enters desulfurization and Cracking Unit, and the 350 DEG C of residual oil of ＞ isolated enter heavy charge processing unit.With conventional atmospheric distillation
Difference is to increased 330 DEG C～350 DEG C AGO (atmospheric gas oil)s and 350 DEG C of residual oil separation functions of ＞, and residual oil is divided into desulfurization
With Cracking Unit raw material and heavy charge processing unit feedstock oil.Drop on the basis of meeting desulfurization and Cracking Unit ingredient requirement
The treating capacity of low heavy charge processing unit, reaches the purpose saving operating cost and energy consumption.
Step (b) of the present invention carries out desulfurization and cracking, and feedstock oil and hydrogen mixed before entering heating furnace.Using desulfurization with
Cracking Unit, this unit arranges multiple reactors, to improve processing capacity；The type of hydrogenation reactor can be fixed bed, movement
Bed or ebullated bed.The catalyst that hydrofining reaction is used refers to functions such as hydrodesulfurization, hydrodenitrogeneration, HDMs
Simple function or several functions combination catalyst.Adoptable base metal active component, the preferably gold of b race and race
Belong to oxide and sulfide, wherein active best as w, mo, co, ni, noble metal has pt, pd etc.；For improving hydrogenation catalyst
Hydrodenitrogeneration and aromatic hydrocarbons saturation performance can add acid additive, acid additive can be 0.5%～4.0% f, p or b or
3%～10% amorphous silicic aluminium or molecular sieve；Selectable carrier has neutral carrier activated alumina, activated carbon, diatom
Soil etc., or acid carrier alumina silicate, magnesium silicate, atlapulgite, molecular sieve etc..Add the acid such as a small amount of p, f in the catalyst
Property component not only can help to improve the cracking activity of c-n key and arene saturating activity, and be favorably improved hydrogenation activity group
The decentralization dividing, increases the utilization rate of active metal.In desulfurization described in step (b) of the present invention and Cracking Unit, hydrofinishing
The condition of operation is: 350 DEG C～400 DEG C of temperature, hydrogen dividing potential drop 10mpa～25mpa, volume space velocity 0.5h-1～2.0h-1, preferably body
Long-pending air speed 0.8h-1～1.5h-1, hydrogen to oil volume ratio 500～1200nm3/m3, preferably hydrogen to oil volume ratio 800～1000nm3/m3.Former
Material oil removes sulphur, nitrogen, metal impurities in hydrogenation reactor, and carries out aromatic hydrocarbons saturated reaction.
Step (c) heavy charge of the present invention processes and uses heavy charge processing unit, and this unit is mainly by coking heater
With coke drum composition, do not set fractionating device.350 DEG C of residual oil of ＞ are pumped into Jiao by the atmospheric fractional tower bottom charging of pretreatment unit
Change heating furnace, be heated to the bottom of 495 DEG C～500 DEG C about entrance coke drums, carry out conventional cracking in coke drum and be condensed
Reaction, top of coke tower operating pressure is 0.15mpa～0.2mpa, and preferred operations pressure is 0.18mpa, generates coke and oil gas.
Oil gas delivers to the atmospheric fractional tower of pretreatment unit, and the coke being flocked in coke drum is cut burnt system through water conservancy and sent by coke drum
Go out, as production marketing.
Using catalysis lighting unit, this unit is mainly by reactor, catalyst again for step (d) catalysis lighting of the present invention
Raw device, after-fractionating tower forms.Fcc raw material enters reactor, and cracking reaction occurs in the presence of catalyst, and macromolecular is split
Chemical conversion small molecule, long-chain are fractured into short chain.Product enters after-fractionating tower, be fractionated into obtaining dry gas, liquefied gas, gasoline,
Diesel oil and catalytic slurry.Dry gas enters gas sweetening unit, and liquefied gas, gasoline, diesel oil are sold as product, and catalytic slurry enters
Heavy charge processing unit.Catalyst enters catalyst regenerator after participating in reaction, returns to reactor after coke burning regeneration
It is continuing with.
Catalyst employed in step (d) be selected from molecular sieve, heat-resistant inorganic oxide, molecular sieve and clay composition,
Heat-resistant inorganic oxide and one or more of clay composition, molecular sieve, heat-resistant inorganic oxide and clay composition；Excellent
Catalyst is selected to be one or more of molecular sieve.Molecular sieve be selected from y type zeolite with or without rare earth element, with or without
The super steady y type zeolite of rare earth element, the silica-rich zeolite with five-membered ring structure, β zeolite, one of modenite, omega zeolite
Or it is several.The silica-rich zeolite with five-membered ring structure can be zsm-5 zeolite or zrp zeolite.Heat-resistant inorganic oxide is selected from
One or more of aluminum oxide, silica, amorphous silicon aluminium, zirconium oxide, titanium oxide, boron oxide and alkaline earth oxide.
Clay be selected from kaolin, halloysite, montmorillonite, diatomite, galapectite, saponite, tired de- soil, sepiolite, attapulgite,
One or more of hydrotalcite and boron-moisten soil.The activity of wherein molecular sieve cracking catalyst is high, and green coke amount is few, gasoline yield
High, conversion ratio highest.
In catalysis lighting step described in step (d) of the present invention, the reaction condition of catalytic cracking is: reaction temperature 470
DEG C～550 DEG C, 480 DEG C～500 DEG C of preferable reaction temperature, 600 DEG C～800 DEG C of regeneration temperature, preferably 700 DEG C of regeneration temperature～
750 DEG C, the mass ratio 3～18 of catalyst and fcc raw material, preferred mass ratio 8～12, reaction time 0.5s～5s, preferably reacts
Time 2～4s, pressure 0.1mpa～0.5mpa.Feedstock oil catalysis lighting unit process separate after obtain dry gas, liquefied gas,
Gasoline, diesel oil and catalytic slurry (including catalytic cracking recycle oil and slurry oil), catalytic slurry delivers to heavy charge processing unit.
Step (e) isomerization dewaxing reaction of the present invention and post-refining reaction adopt base oil unit, and this unit includes isomery
Dewaxing reactor, post-refining reactor and separator.The catalyst of isomerization dewaxing reaction, can select commonly used in the art
Lube oil hydrogenation heterogeneous catalyst, it is possible to use commodity hydrogenation catalyst it is also possible to according to this area general knowledge preparation.Should
Catalyst includes carrier and active metal component, or also includes auxiliary agent.The carrier of hydroisomerization catalyst is generally lkz molecule
Sieve or zsm-22 molecular sieve etc., usual molecular sieve content in the catalyst is 30wt%～80wt%, preferably 40wt%～
70wt%.Metal component in catalyst is generally one or more of pt, pd, ru and rh, and active metal component is in catalysis
Content in agent is 0.1wt%～30.0wt%.Selectable adjuvant component is containing one of boron, fluorine, chlorine and P elements
Or multiple, auxiliary agent content in the catalyst is 0.1wt%～5.0wt%.The specific surface area of catalyst is 150m2/ g～
500m2/ g, pore volume is 0.15ml/g～0.60ml/g.Using front, reduction treatment is carried out to catalyst, so that hydrogenation active metals is existed
It is in reducing condition in course of reaction.Post-refining catalyst is conventional reduced form Hydrobon catalyst, and this catalyst can
Including carrier and active metal component, or also include auxiliary agent.Its active metal is one of pt, pd or two kinds or reduction-state
Raney nickel, active metal pt and/or pd weight content in the catalyst generally 0.05%～1%, reduction in catalyst
The active metal of state Raney nickel is calculated as 30wt%～80wt% with oxide weight, and carrier is generally al2o3Or al2o3-sio2,
Auxiliary agent contains the elements such as p, ti, b, zr.The reduction of routine can be carried out using procatalyst it is ensured that hydrogenation active metals were being reacted
It is in reduction-state in journey.
In step (e) of the present invention, 1. isomerization dewaxing reaction condition includes: temperature be 210 DEG C～400 DEG C, preferably 310 DEG C～
390 DEG C, hydrogen dividing potential drop is 10.0mpa～25.0mpa, preferred 15.0mpa～25.0mpa, and volume space velocity is 0.2h-1～2.0h-1、
Preferably 0.6h-1～2.0h-1, hydrogen to oil volume ratio is 100～2000nm3/m3, preferably 700～1000nm3/m3.2. post-refining is anti-
The condition is answered to be: temperature is 100 DEG C～290 DEG C, preferably 200 DEG C～290 DEG C, hydrogen dividing potential drop is 10.0mpa～25.0mpa, preferably
15.0mpa～25.0mpa, volume space velocity is 0.2h-1～2.0h-1, preferred 0.6h-1～2.0h-1, hydrogen to oil volume ratio be 100～
2000nm3/m3, preferably 700～1000nm3/m3.
Step (f) the gas purification adsorptive pressure used with absorption purification in preparation process is 1.2mpa～3.0mpa.
The crude oil with poor quality that the present invention realizes said method employing produces gasoline, diesel oil, petroleum coke and top-grade lubricating oil basis
The system of oil, including crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy charge processing unit, catalysis lighting list
Unit, base oil unit and gas purification and preparation unit；
Crude oil with poor quality pretreatment unit passes through pipeline and desulfurization and Cracking Unit, heavy charge processing unit, gas respectively
Purify and be connected with preparation unit；
Desulfurization and Cracking Unit pass through pipeline and catalysis lighting unit, base oil unit and gas purification and preparation respectively
Unit is connected；
Heavy charge processing unit is connected with catalysis lighting unit by pipeline；
Catalysis lighting unit is connected with preparation unit with gas purification by pipeline respectively；
Base oil unit is connected with preparation unit with gas purification by pipeline.
Crude oil with poor quality pretreatment unit includes raw material oil tank, electrical desalter, heat exchanger, atmospheric pressure kiln and normal pressure fractionation
Tower；Multiple outlets of the atmospheric fractional tower of crude oil with poor quality pretreatment unit connect desulfurization and Cracking Unit, weight by pipeline respectively
Matter material processing unit, gas purification and preparation unit and hydro-refining unit.
Desulfurization and Cracking Unit include the first hydrogenation reactor, the second hydrogenation reactor and the first fractionating column；
Heavy charge processing unit includes coking heater and coke drum；Catalysis lighting unit includes reactor, catalysis
Agent regenerator and after-fractionating tower；Base oil unit includes isomerization dewaxing reactor, post-refining reactor and separator；Gas
Body is purified and is made up of desulfurizing tower and psa purifying plant with preparation unit；Multiple outlets of crude oil with poor quality pretreatment unit fractionating column
Connect the first fractionating column, the coking heater of heavy charge processing unit and the coke of desulfurization and Cracking Unit respectively by pipeline
The desulfurizing tower of tower, gas purification and preparation unit；The entrance of the heat exchanger of crude oil with poor quality pretreatment unit connects catalysis lighting
The outlet of the after-fractionating tower of unit.
Desulfurization and the outlet of the first fractionating column of Cracking Unit are connected the desulfurizing tower of gas purification and preparation unit, base respectively
The isomerization dewaxing reactor of plinth oil unit, the reactor of catalysis lighting unit, desulfurization and the first fractionating column of Cracking Unit
Entrance connects the outlet of the second hydrogenation reactor.
The entrance of the coking heater in heavy charge processing unit passes through second point of pipeline and catalysis lighting unit
The outlet evaporating tower is connected, and meanwhile, coke drum, coking heater and atmospheric fractional tower connect into loop by pipeline.
The de- of pipeline and gas purification and preparation unit is passed through in the outlet of the after-fractionating tower of catalysis lighting unit respectively
Sulphur tower, and the heat exchanger of crude oil with poor quality pretreatment unit is connected, the entrance of the after-fractionating tower of catalysis lighting unit is even
Connect the outlet of reactor.
The isomerization dewaxing reactor of base oil unit passes through the psa purifying plant phase of pipeline and gas purification and preparation unit
Connect.
The separator of base oil unit is connected with the desulfurizing tower of preparation unit with gas purification by pipeline.
Described gas purification is connected the entrance of heating furnace, heating furnace with the psa purifying plant of preparation unit by pipeline
Outlet connect desulfurization and Cracking Unit the first hydrogenation reactor entrance.
Steam(-)coil is set in described raw material oil tank.
Pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body in the present invention
All send into gas purification and preparation unit.Gas purification supplies hydrodesulfurizationunit unit and base oil list with preparation unit institute hydrogen producing
Unit uses, and release gas is used as furnace fuel.
Gas purification of the present invention is made up of desulfurizing tower and psa purifying plant with preparation unit.Pretreatment unit, desulfurization and split
Change unit, catalysis lighting unit and base oil unit institute aerogenesis body and fully enter desulfurizing tower, deviate from h2Psa purification is entered after s
Device, psa purifying plant adopts 10-2-4 flow process (10 adsorbent beds, 2 air inlets are all pressed for 4 times)；By in dry gas in adsorbent bed
Co, co2Fall Deng Impurity Absorption, respectively obtain hydrogen and release gas.The hydrogen purity obtaining be more than 99.9%, for desulfurization with split
Change unit and base oil unit uses, release gas is used as furnace fuel.Psa device carries out adsorbing the selected adsorbent of purification
It is all the solid particle with large specific surface area, such as activated alumina, the molecular sieve of activated carbon, silica type and routine；Absorption
Pressure is 1.2mpa～3.0mpa, and preferably adsorptive pressure is 2mpa.
Crude oil with poor quality quality testing is according to (the mensure potentiometric titration of gb/t18609-2011 acid value for crude oil；sy/t7550-
The mensure of wax, colloid, asphalt content in 2012 crude oil；Gb/t17280-2009 crude distillation standard test method 15- is theoretical
Plate distillation column；Gb/t17280-2009 crude distillation standard test method 15- theoretical plate distillation column) carry out, the present invention is not detailed
Described equipment and method of operating all can be realized according to this area general knowledge.
Beneficial effects of the present invention compared with the prior art:
(1) crude oil with poor quality is pre-processed by the present invention, heavy charge is processed, desulfurization and cracking, catalysis lighting, base oil and
Gas purification is organically combined with preparation technology, to greatest extent by crude oil with poor quality change into light-end products, petroleum coke and
The low-viscosity of China's urgent need, low pour point, the class base oil of Viscosity Index 120；Product category is many, can meet multi-field development
Need, and can simplification of flowsheet, reduce overall energy consumption.
(2) pretreatment unit increased 330 DEG C～350 DEG C AGO (atmospheric gas oil)s and 350 DEG C of residual oil separation functions of ＞, by residual oil
It is divided into desulfurization and Cracking Unit raw material and heavy charge processing unit feedstock oil.Meeting desulfurization and Cracking Unit ingredient requirement
On the basis of reduce the treating capacity of heavy charge processing unit, reach the purpose saving operating cost and energy consumption.
(3) heavy charge processing unit does not set fractionating device, simplifies technological process, reduces equipment investment and operates into
This, decrease thermal loss simultaneously.
(4) pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body all enter
Enter desulfurizing tower, deviate from h2After s enter psa purifying plant, through psa purification, the hydrogen purity obtaining be more than 99.9%, for desulfurization with
Cracking Unit and base oil unit use；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 AGO (atmospheric gas oil)s and 350 DEG C of residual oil of ＞ by pretreatment unit.330 DEG C～
350 DEG C of AGO (atmospheric gas oil)s enter desulfurization and Cracking Unit, and 350 DEG C of residual oil of ＞ are used after heavy charge processing unit processes again
In desulfurization and Cracking Unit raw material, both improve the yield of gasoline, diesel oil, reduce technical difficulty and the hydrogen consumption of hydrotreating again,
Extend the operation cycle.
(6) crude oil with poor quality pretreatment, heavy charge process, desulfurization and cracking, catalysis lighting, base oil and gas purification
With preparation unit cooperation, both reduce investment, improve full factory heat utilization ratio again.
Brief description
Fig. 1 is that a kind of crude oil with poor quality of the present invention produces gasoline, diesel oil and petroleum coke and top-grade lubricating oil base oil
System schematic.
Wherein, 1, raw material oil tank, 2, electrical desalter, 3, heat exchanger, 4, atmospheric pressure kiln, 5, atmospheric fractional tower, 6, burnt
Change heating furnace, 7, coke drum, 8, reactor, 9, catalyst regenerator, 10, after-fractionating tower, the 11, first hydrogenation reactor, 12,
Second hydrogenation reactor, the 13, first fractionating column, 14, separator, 15, post-refining reactor, 16, isomerization dewaxing reactor,
17th, desulfurizing tower, 18, psa purifying plant, 19, hydro-refining unit, 20, heating furnace.
Specific embodiment
Below in conjunction with the accompanying drawings method provided by the present invention is further described.
As shown in figure 1, a kind of crude oil with poor quality produces gasoline, the system of diesel oil, petroleum coke and top-grade lubricating oil base oil, should
System includes crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy charge processing unit, catalysis lighting unit, base
Plinth oil unit and gas purification and preparation unit；
Crude oil with poor quality pretreatment unit includes raw material oil tank 1, electrical desalter 2, heat exchanger 3, atmospheric pressure kiln 4 and normal pressure
Fractionating column 5；Multiple outlets of the atmospheric fractional tower 5 of crude oil with poor quality pretreatment unit connect desulfurization and cracking list by pipeline respectively
Unit, heavy charge processing unit, gas purification and preparation unit and hydro-refining unit 19.
Desulfurization and Cracking Unit include the first hydrogenation reactor 11, the second hydrogenation reactor 12 and the first fractionating column 13；
Heavy charge processing unit includes coking heater 6 and coke drum 7；Catalysis lighting unit includes reactor 8, urges
Agent regenerator 9 and after-fractionating tower 10；Base oil unit includes isomerization dewaxing reactor 16, post-refining reactor 15 and divides
From device 14；Gas purification is made up of desulfurizing tower 17 and psa purifying plant 18 with preparation unit；Crude oil with poor quality pretreatment unit divides
The multiple outlets evaporating tower 5 connect the first fractionating column 13 of desulfurization and Cracking Unit, heavy charge processing unit respectively by pipeline
Coking heater 6 and coke drum 7, the desulfurizing tower 17 of gas purification and preparation unit；The heat exchange of crude oil with poor quality pretreatment unit
Device 3 connects the outlet of the after-fractionating tower 10 of catalysis lighting unit.
Desulfurization is connected the desulfurizing tower of gas purification and preparation unit respectively with the outlet of the first fractionating column 13 of Cracking Unit
17th, the isomerization dewaxing reactor 16 of base oil unit, the reactor 8 of catalysis lighting unit, desulfurization and the first of Cracking Unit
The entrance of fractionating column 13 connects the outlet of the second hydrogenation reactor 12.
The entrance of the coking heater 6 in heavy charge processing unit passes through second point of pipeline and catalysis lighting unit
The outlet evaporating tower 10 is connected, and meanwhile, coke drum 7, coking heater 6 and atmospheric fractional tower 5 connect into loop by pipeline.
Pipeline and gas purification and preparation unit are passed through in the outlet of the after-fractionating tower 10 of catalysis lighting unit respectively
Desulfurizing tower 17, and the heat exchanger 3 of crude oil with poor quality pretreatment unit is connected, the after-fractionating tower 10 of catalysis lighting unit
The outlet of entrance coupled reaction device 8.
The isomerization dewaxing reactor 16 of base oil unit passes through the psa purifying plant of pipeline and gas purification and preparation unit
18 are connected.
The separator 14 of base oil unit is connected with the desulfurizing tower 17 of preparation unit with gas purification by pipeline.
Described gas purification is connected the entrance of heating furnace 20 with the psa purifying plant 18 of preparation unit by pipeline, plus
The outlet of hot stove 20 connects the entrance of desulfurization and the first hydrogenation reactor 11 of Cracking Unit.
Steam(-)coil is set in described raw material oil tank 1.
Crude oil with poor quality produces gasoline, the method for diesel oil, petroleum coke and top-grade lubricating oil base oil, specifically includes following step
Rapid:
External crude oil with poor quality is sent into raw material oil tank and (is inside set steam(-)coil, be heated to coal tar using steam
90 DEG C carry out being dehydrated, solid sedimentation) storage.Crude oil with poor quality, is carried out washing with being pumped to electrical desalter by storage tank, desalination, dehydration
With after de- solid with product oil heat exchange to 220 DEG C (1.6mpa) with being pumped to atmospheric pressure kiln, be heated to 380 DEG C and enter normal pressures and divide
Evaporate tower, the gas isolated enters gas purification and preparation unit, the gasoline isolated and diesel oil are sent into hydro-refining unit, obtained
To treated gasoline product and diesel product；330 DEG C isolating～350 DEG C of AGO (atmospheric gas oil)s enter desulfurization and Cracking Unit, point
350 DEG C of residual oil of the ＞ separating out enter heavy charge processing unit.
The purifying hydrogen of hydrogen that 330 DEG C～350 DEG C AGO (atmospheric gas oil)s are produced with subsequent cell mix after through being pumped to heating furnace, plus
Heat sequentially enters the first hydrogenation reactor, the second hydrogenation reactor and fractionating column to after uniform temperature, through hydrodesulfurization with split
Change and obtain dry gas, gasoline products, diesel product, fcc raw material and hydrogenation tail oil.Dry gas enters gas purification and preparation unit, vapour
Oil, 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 of ＞ are pumped into coking heater by the Fractionator Bottom charging of pretreatment unit, be heated to 495 DEG C～
500 DEG C enter from the entrance of the bottom of coke drum, cracked and condensation reaction, generate coke and oil gas in coke drum.Oil gas
Deliver to the atmospheric fractional tower of pretreatment unit, the coke being flocked in coke drum is cut burnt system through water conservancy and sent by coke drum,
As production marketing.
The fcc raw material being obtained by desulfurization and Cracking Unit enters catalysis lighting unit, and catalysis lighting unit is by reacting
Device, catalyst regenerator, after-fractionating tower forms.Fcc raw material enters reactor, occurs cracking anti-in the presence of catalyst
Should, macromolecular is cracked into small molecule, long-chain is fractured into short chain.Product enters after-fractionating tower, is fractionated into obtaining dry air-liquid
Change gas, gasoline products, diesel product and catalytic slurry.Dry gas enters gas purification and preparation unit, liquefied gas, gasoline, diesel oil
Sell as product, catalytic slurry enters heavy charge processing unit.Catalyst enters catalyst regenerator, warp after participating in reaction
Return to reactor after crossing coke burning regeneration to be continuing with.
The purifying hydrogen of hydrogen that hydrogenation tail oil is produced with subsequent cell enters base oil unit after mixing, and base oil unit includes different
Structure dewaxing reactor, post-refining reactor and separator, reacted and separation obtains dry gas and low-viscosity, low pour point, sticks
The class base oil of degree index 120.Dry gas enters gas purification and preparation unit, and base oil is as production marketing.
The all gas that this device produces fully enter gas purification and preparation unit, and this unit is carried by desulfurizing tower and psa
Pure device composition.Gas fully enters desulfurizing tower, deviates from h2Enter psa purifying plant after s, obtain purifying hydrogen of hydrogen and release gas.
The hydrogen purity obtaining is more than 99.9%, uses with Cracking Unit and base oil unit for desulfurization, and release gas is used as heating furnace and fires
Material.
It is described further below by the method that specific embodiment provides to the present invention, but therefore do not limit this
Invention.
Embodiment 1
Full device total technological process adopts inferior raw material pretreatment-heavy oil feedstock process-desulfurization and cracking-catalysis lightweight
The lighting process that the production-gas purification of change-base oil is organically combined with preparation technology.
Feed material preparation units by crude cut be dry gas, gasoline, diesel oil, AGO (atmospheric gas oil) and residual oil.Dry gas enters gas
Body purifies and preparation unit, and gasoline and diesel oil deliver to hydro-refining unit as outside product, obtains refined petrol and diesel oil product, and 330
DEG C～350 DEG C of AGO (atmospheric gas oil)s enter desulfurization and Cracking Unit, the 350 DEG C of residual oil of ＞ isolated enter heavy charges process single
Unit.
330 DEG C～350 DEG C AGO (atmospheric gas oil)s enter desulfurization and Cracking Unit, through hydrodesulfurization and cracking obtain gas,
Gasoline, diesel oil, fcc raw material and hydrogenation tail oil.Gasoline, diesel oil is sold as product, and it is single with preparation that gas enters gas purification
Unit, fcc raw material enters catalysis lighting unit, and hydrogenation tail oil enters base oil unit.
350 DEG C of residual oil of ＞ enter heavy charge processing unit, and residual oil is by the Fractionator Bottom charging pumping of pretreatment unit
Enter heating furnace, be heated to the bottom of 495 DEG C～500 DEG C about entrance coke drums, cracked in coke drum and condensation reaction,
Generate coke and oil gas.High-temperature oil gas deliver to the fractionating column of pretreatment unit, and the coke being flocked in coke drum cuts Jiao through water conservancy
System is sent by coke drum, as production marketing.
Enter catalysis lighting unit from the fcc raw material of desulfurization and Cracking Unit, make in zsm-5 zeolite or zrp zeolite
For in the presence of catalyst occur cracking reaction, macromolecular is cracked into small molecule, long-chain is fractured into short chain, thus obtain dry gas,
Liquefied gas, gasoline, diesel oil and catalytic slurry.Dry gas enters gas purification and preparation unit unit, and liquefied gas, gasoline, diesel oil are made
Sell for product, catalytic slurry enters heavy charge processing unit.
Hydrogenation tail oil enters base oil unit, in the presence of lube oil hydrogenation heterogeneous catalyst, isomerization reaction occurs,
Post-refining catalyst is conventional reduced form Hydrobon catalyst: its active metal is nickel, is calculated as with oxide weight
50wt%～60wt%, carrier is al2o3.By the high condensation point normal alkane isomerization in feedstock oil, produce the low glutinous of China's urgent need
Degree, low pour point, the class base oil of Viscosity Index 120.
Pretreatment unit, desulfurization and Cracking Unit, catalysis lighting unit and base oil unit institute aerogenesis body in the present invention
All send into gas purification and preparation unit.Gas purification supplies hydrodesulfurizationunit unit and base oil list with preparation unit institute hydrogen producing
Unit uses, and release gas is used as furnace fuel.
The crude oil with poor quality feedstock property of embodiment and comparative example employing is shown in Table 1, and prevailing operating conditions are shown in Table 2, product slates
It is shown in Table 3, gasoline property is shown in Table 4, diesel oil property is shown in Table 5, and the criteria for classification of lube base oil is shown in Table 6, base oil technical requirements
It is shown in Table 7, basic oil nature is shown in Table 8, and petroleum coke property is shown in Table 9.
Embodiment 2
Using raw material, technological process same as Example 1, change the reaction condition of desulfurization and Cracking Unit, catalysis is light
The catalyst that matter unit uses is aluminum oxide, and other reaction conditions are constant, and as shown in table 2, product slates are shown in Table 3, product
Matter is shown in Table 4～9.
Embodiment 3
Using raw material, technological process same as Example 1, change the reaction condition of catalysis lighting unit, catalysis is light
The catalyst that matter unit uses is the y type zeolite containing rare earth element, and other reaction conditions are constant, as shown in table 2, product slates
It is shown in Table 3, product property is shown in Table 4～9.
Embodiment 4
Using raw material, technological process same as Example 1, change base oil unit reaction condition, be catalyzed lighting
The catalyst that unit uses is y type zeolite without rare earth element, silica and kaolin according to the mixture of 1:1:1, other
Reaction condition is constant, and as shown in table 2, product slates are shown in Table 3, and product property is shown in Table 4～9.
Comparative example
Using raw material same as Example 1, as different from Example 1, dry gas deviates from h through digester2After s without
Cross gas purification and preparation unit and use with Cracking Unit and base oil unit for desulfurization directly as recycle hydrogen；Operating condition
It is shown in Table 2, product slates are shown in Table 3, the product property obtaining is shown in Table 4, table 5, table 8.
Table 1 oil property
| 20 DEG C of density, g/cm3 | 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 |
| Asphalitine, m% | 0.1 |
| Boiling range | |
| 15～200 DEG C | 7.51 |
| 200～350 DEG C | 24.55 |
| 350～500 DEG C | 32.44 |
| >500℃ | 35.5 |
Table 2 prevailing operating conditions
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 |
| Inferior raw material pretreatment unit | ||||
| Feedstock oil storage tank heat temperature/DEG C | 90 | 90 | 90 | 90 |
| With temperature after product oil heat exchange/DEG C | 220 | 220 | 220 | 220 |
| With pressure/mpa after product oil heat exchange | 1.6 | 1.6 | 1.6 | 1.6 |
| Furnace outlet temperature/DEG C | 380 | 380 | 380 | 380 |
| Heavy charge processing unit | ||||
| Outlet Temperature in Delayed Coking Furnace/DEG C | 500 | 500 | 500 | 500 |
| Top of coke tower operating pressure/mpa | 0.18 | 0.18 | 0.18 | 0.18 |
| Desulfurization and Cracking Unit | ||||
| First hydrogenation reactor | ||||
| Reactor inlet hydrogen dividing potential drop/mpa | 25 | 15.3 | 25 | 25 |
| Hydrogen to oil volume ratio nm3/m3 | 1000 | 800 | 1000 | 1000 |
| At the beginning of operating/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 hydrogenation reactor | ||||
| Reactor inlet hydrogen dividing potential drop/mpa | 24.7 | 15 | 24.7 | 24.7 |
| Hydrogen to oil volume ratio nm3/m3 | 900 | 800 | 900 | 900 |
| At the beginning of operating/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 | ||||
| Reaction temperature/DEG C | 500 | 500 | 480 | 500 |
| Regeneration temperature/DEG C | 750 | 750 | 750 | 750 |
| Catalyst/fcc raw material/m% | 10 | 10 | 10 | 10 |
| Reaction time/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 nm3/m3 | 1000 | 1000 | 1000 | 800 |
| At the beginning of operating/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 nm3/m3 | 900 | 900 | 900 | 800 |
| At the beginning of operating/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 purification and preparation unit | ||||
| Psa purifies | ||||
| Adsorbent | 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 |
| Lube base oil (wt%) | 16.58 | 17.07 | 18.34 | 15.58 |
| Petroleum 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 lube base oil criteria for classification
Table 7 base oil technical requirements
Table 8 base oil property list
| Product | Embodiment 1 | Embodiment 2 | Embodiment 4 | Comparative example |
| Class 6 | ⅱ+Class 6 | Class 4 | ⅱ+Class 4 | |
| Density (20 DEG C)/kg.m-1 | 836.5 | 832.1 | 833.9 | 831.5 |
| Viscosity (100 DEG C)/mm2.s -1 | 6.242 | 6.108 | 3.925 | 4.237 |
| Viscosity index (VI) | 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 |
| Sulfur content/μ g.g-1 | 1.0 | ＜ 10.0 | ＜ 10.0 | ＜ 10.0 |
| Saturated hydrocarbons/% | ＞ 99.0 | ＞ 99.0 | ＞ 99.0 | ＞ 99.0 |
| Oxidation stability/min | ＞ 300 | ＞ 300 | ＞ 300 | ＞ 300 |
Table 9 petroleum coke property list
| Title | Petroleum coke |
| Real density, g/cm3 | 1.85 |
| Sulfur content, wt% | 2.53 |
| Ash content, wt% | 0.36 |
| Volatile matter, wt% | 15 |
| Moisture, wt% | 15.2 |
Claims (10)
1. a kind of crude oil with poor quality produces the method for gasoline, diesel oil, petroleum coke and top-grade lubricating oil base oil it is characterised in that being somebody's turn to do
Method is included crude oil with poor quality pretreatment, desulfurization and is reacted with cracking, heavy charge process, catalysis lighting, isomerization dewaxing and supplement
Refining reaction, gas purification and preparation process, specifically comprise the following steps that
A () crude oil with poor quality pre-processes: crude oil with poor quality is carried out washing, desalination, dehydration and de- solid, heat exchange to 200 DEG C ~ 250 DEG C,
Be heated to 360 DEG C ~ 390 DEG C by heating furnace again, enter atmospheric fractional tower, isolate gas, gasoline, diesel oil, 330 DEG C ~ 350 DEG C
AGO (atmospheric gas oil) and 350 DEG C of residual oil of ＞；
(b) desulfurization and cracking: 330 DEG C ~ 350 DEG C AGO (atmospheric gas oil)s that step (a) obtains obtain gas, vapour through hydrofinishing
Oil, diesel oil, fcc raw material and hydrogenation tail oil；
C () heavy charge is processed: 350 DEG C of residual oil of ＞ that step (a) is obtained are heated to 495 DEG C ~ 500 DEG C and are cracked and be condensed
Reaction, generates coke and oil gas；
D () is catalyzed lighting: the fcc raw material that step (b) is obtained occurs cracking reaction in the presence of catalyst, is done
Air-liquid gas, gasoline, diesel oil and catalytic slurry；The heavy charge that catalytic slurry carries out step (c) is processed；
The reaction of (e) isomerization dewaxing and post-refining reaction: the hydrogenation tail oil that step (b) obtains occurs different in the presence of catalyst
Structure dewaxing reaction and post-refining reaction, produce class base oil；
(f) gas purification and preparation: dry gas that the gas that isolate step (a) and step (b) and step (d) obtain and
The gas that step (e) obtains carries out desulfurization and absorption purification, obtains hydrogen and release gas.
2. crude oil with poor quality according to claim 1 produces gasoline, the side of diesel oil, petroleum coke and top-grade lubricating oil base oil
Method is it is characterised in that the reaction condition that in step (b), hydrofinishing is processed is: 350 DEG C ~ 400 DEG C of temperature, hydrogen dividing potential drop 10mpa ~
25mpa, volume space velocity 0.5h-1~2.0h-1, hydrogen to oil volume ratio 500 ~ 1200 nm3/m3.
3. crude oil with poor quality according to claim 1 produces gasoline, the side of diesel oil, petroleum coke and top-grade lubricating oil base oil
Method it is characterised in that in step (d) cracking reaction condition be: 470 DEG C ~ 550 DEG C of reaction temperature, regeneration temperature 600 DEG C ~ 800
DEG C, the mass ratio 3 ~ 18 of catalyst and fcc raw material, reaction time 0.5s ~ 5s, pressure 0.1 mpa ~ 0.5mpa.
4. crude oil with poor quality according to claim 1 produces gasoline, the side of diesel oil, petroleum coke and top-grade lubricating oil base oil
Method it is characterised in that in step (e) isomerization dewaxing reaction condition include: temperature be 210 DEG C ~ 400 DEG C, hydrogen dividing potential drop be 10.0mpa
~ 25.0mpa, volume space velocity is 0.2 h-1~2.0h-1, hydrogen to oil volume ratio is 100 ~ 2000 nm3/m3.
5. crude oil with poor quality according to claim 1 produces gasoline, the side of diesel oil, petroleum coke and top-grade lubricating oil base oil
Method it is characterised in that in step (e) post-refining reaction condition be: temperature be 100 DEG C ~ 290 DEG C, hydrogen dividing potential drop be 10.0mpa ~
25.0mpa, volume space velocity is 0.2 h-1~2.0h-1, hydrogen to oil volume ratio is 100 ~ 2000 nm3/m3.
6. a kind of crude oil with poor quality for described in claim 1 produces gasoline, diesel oil, petroleum coke and top-grade lubricating oil base oil side
The system of method is it is characterised in that this system includes crude oil with poor quality pretreatment unit, desulfurization and Cracking Unit, heavy charge processes list
Unit, catalysis lighting unit, base oil unit and gas purification and preparation unit；
Crude oil with poor quality pretreatment unit passes through pipeline and desulfurization and Cracking Unit, heavy charge processing unit, gas purification respectively
It is connected with preparation unit；Crude oil with poor quality pretreatment unit includes raw material oil tank (1), electrical desalter (2), heat exchanger (3), often
Pressure heating furnace (4) and atmospheric fractional tower (5)；
Desulfurization and Cracking Unit pass through pipeline and catalysis lighting unit, base oil unit and gas purification and preparation unit respectively
It is connected；
Heavy charge processing unit is connected with catalysis lighting unit by pipeline；
Catalysis lighting unit is connected with preparation unit with gas purification by pipeline；
Base oil unit is connected with preparation unit with gas purification by pipeline, and base oil unit includes isomerization dewaxing reactor
(16), post-refining reactor (15) and separator (14)；Gas purification is purified by desulfurizing tower (17) and psa with preparation unit
Device (18) forms.
7. system according to claim 6 is it is characterised in that the atmospheric fractional tower (5) of crude oil with poor quality pretreatment unit
Multiple outlets respectively by pipeline connect desulfurization and Cracking Unit, heavy charge processing unit, gas purification and preparation unit with
And hydro-refining unit (19).
8. system according to claim 6 it is characterised in that
Desulfurization and Cracking Unit include the first hydrogenation reactor (11), the second hydrogenation reactor (12) and the first fractionating column (13)；
Heavy charge processing unit includes coking heater (6) and coke drum (7)；
Catalysis lighting unit includes reactor (8), catalyst regenerator (9) and after-fractionating tower (10)；
Multiple outlets of crude oil with poor quality pretreatment unit fractionating column (5) connect the first of desulfurization and Cracking Unit respectively by pipeline
Fractionating column (13), the coking heater (6) of heavy charge processing unit and coke drum (7), gas purification is de- with preparation unit
Sulphur tower (17)；The heat exchanger (3) of crude oil with poor quality pretreatment unit connects going out of after-fractionating tower (10) of catalysis lighting unit
Mouthful.
9. system according to claim 8 it is characterised in that
Desulfurization is connected the desulfurizing tower of gas purification and preparation unit respectively with the outlet of first fractionating column (13) of Cracking Unit
(17), the isomerization dewaxing reactor (16) of base oil unit, reactor (8), desulfurization and the Cracking Unit of catalysis lighting unit
The first fractionating column (13) entrance connect the second hydrogenation reactor (12) outlet；
The entrance of the coking heater (6) in heavy charge processing unit passes through the after-fractionating of pipeline and catalysis lighting unit
The outlet of tower (10) is connected, and meanwhile, coke drum (7), coking heater (6) and atmospheric fractional tower (5) are connected into by pipeline
Loop；
The de- of pipeline and gas purification and preparation unit is passed through in the outlet of the after-fractionating tower (10) of catalysis lighting unit respectively
Sulphur tower (17), and the heat exchanger (3) of crude oil with poor quality pretreatment unit is connected, the after-fractionating tower of catalysis lighting unit
(10) outlet of entrance coupled reaction device (8)；
The isomerization dewaxing reactor (16) of base oil unit passes through the psa purifying plant of pipeline and gas purification and preparation unit
(18) it is connected.
10. system according to claim 8 it is characterised in that
The separator (14) of base oil unit is connected with the desulfurizing tower (17) of preparation unit with gas purification by pipeline；
Gas purification is connected the entrance of heating furnace (20), heating furnace with the psa purifying plant (18) of preparation unit by pipeline
(20) outlet connects the entrance of desulfurization and first hydrogenation reactor (11) of Cracking Unit.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5076910A (en) * | 1990-09-28 | 1991-12-31 | Phillips Petroleum Company | Removal of particulate solids from a hot hydrocarbon slurry oil |
| CN101987972A (en) * | 2009-08-06 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Method for processing inferior crude oil through combined processes |
| CN204097413U (en) * | 2014-04-27 | 2015-01-14 | 中石化南京工程有限公司 | Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil |
| CN103289738B (en) * | 2013-06-25 | 2015-10-28 | 中石化南京工程有限公司 | A kind of hydrocracking tail oil hydrogenation produces the combined method of top-grade lubricating oil base oil |
-
2014
- 2014-04-27 CN CN201410180507.XA patent/CN105018143B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5076910A (en) * | 1990-09-28 | 1991-12-31 | Phillips Petroleum Company | Removal of particulate solids from a hot hydrocarbon slurry oil |
| CN101987972A (en) * | 2009-08-06 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Method for processing inferior crude oil through combined processes |
| CN103289738B (en) * | 2013-06-25 | 2015-10-28 | 中石化南京工程有限公司 | A kind of hydrocracking tail oil hydrogenation produces the combined method of top-grade lubricating oil base oil |
| CN204097413U (en) * | 2014-04-27 | 2015-01-14 | 中石化南京工程有限公司 | Produce the system of petrol and diesel oil, refinery coke and top-grade lubricating oil base oil |
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Address after: No. 3 horses horses Science Park Avenue in Qixia District of Nanjing City, Jiangsu province 210049 Patentee after: SINOPEC NANJING ENGINEERING & CONSTRUCTION Inc. Patentee after: Sinopec Engineering (Group) Co.,Ltd. Address before: 211112 No. 1189, Jian Jian Road, Jiangning District, Jiangsu, Nanjing Patentee before: SINOPEC NANJING ENGINEERING & CONSTRUCTION Inc. Patentee before: Sinopec Engineering (Group) Co.,Ltd. |