CN105001907B - A kind of method and system of paraffinic base crude oil with poor quality Poly-generation - Google Patents
A kind of method and system of paraffinic base crude oil with poor quality Poly-generation Download PDFInfo
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Abstract
The invention discloses a kind of method of paraffinic base crude oil with poor quality Poly-generation and its system, crude oil with poor quality pretreatment, heavy oil residue are processed, are catalyzed lighting, reformation lighting, diesel oil dewaxing and gas desulfurized step organic assembling by the method, to greatest extent crude oil with poor quality is changed into diesel oil, high-knock rating gasoline and aromatic hydrocarbons (PX raw material) and liquid paraffin, meet multi-field development need, and can simplification of flowsheet, reduce overall energy consumption.
Description
Technical field
The invention belongs to oil refining, petrochemical industry, coal chemical technology, it is related to a kind of side of paraffinic base crude oil with poor quality lighting
Method, specifically will be gentle to crude oil with poor quality pretreatment, heavy oil residue process, catalysis lighting, reformation lighting, diesel oil dewaxing
The lighting process of body sulfur removal 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.
According to the feature of crude oil with poor quality, explore new technique, crude oil with poor quality is changed into light-end products to greatest extent, and Simplified flowsheet stream
Journey, overall energy consumption is low, and China's sustained economic development is of great importance.
With developing by leaps and bounds of China's economy, the species of oil product demand and total quantity consumed present and increase substantially.Using
Crude oil with poor quality produces multiple product and has great significance to meeting China's economic development.
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 oil residue to process, urge
Change lighting, the lighting process of reformation lighting, diesel oil dewaxing and process of desulfurizing gases organic assembling.To greatest extent
Paraffinic base crude oil with poor quality is changed into the product of China's economic development needs, simplification of flowsheet, reduce overall energy consumption.
The purpose of the present invention is achieved in the following ways：
A kind of method of paraffinic base crude oil with poor quality Poly-generation, the method includes crude oil with poor quality pretreatment, heavy oil residue is processed,
Catalysis lighting, reformation lighting, diesel oil dewaxing and gas sweetening process, comprise the following steps that：
The pretreatment of (a) crude oil with poor quality：Crude oil with poor quality is carried out washing, desalination, dehydration and de- solid, heat exchange to 200 DEG C～
250 DEG C, then be heated to 360 DEG C～390 DEG C by heating furnace, enter atmospheric fractional tower, isolate gas, Petroleum, diesel oil,
330 DEG C～350 DEG C AGO (atmospheric gas oil)s and 350 DEG C of residual oil of ＞；
B () heavy oil residue is processed：350 DEG C of residual oil of ＞ that step (a) is obtained through solvent extraction obtain fcc raw material with
And asphalt for high grade road；
C () is catalyzed lighting：330 DEG C～350 DEG C normal pressures that the fcc raw material that obtain step (b) and step (a) obtain
There is cracking reaction in gas oil in the presence of catalyst, thus obtaining dry gas, liquefied gas, Petroleum, diesel oil and catalytic slurry；
The heavy oil residue that catalytic slurry carries out step (b) is processed；
(d) reformation lighting：The Petroleum that step (a) and step (c) are obtained enters reforming reactor, in catalyst
(cracking reaction occurring, dehydrogenation reaction, alkane isomerization, aromatic hydrocarbons take off alkyl, hydro carbons hydrogenolysis) is reacted, obtain is anti-under effect
Product is answered to be fractionated into obtaining hydrogen-rich gas and light naphthar；Light naphthar obtains high-knock rating gasoline and virtue through Aromatics Extractive Project
Hydrocarbon；Aromatic hydrocarbons can be used as PX raw material.
The dewaxing of (e) diesel oil and gas sweetening：The diesel oil that obtain step (a) and step (c) and isopropanol, aqueous solution of urea
Complex reactor is entered, product obtains liquid paraffin and low-coagulation diesel oil through separating with rectification after mixing；Step (a) separates
Dry gas that the gas going out and step (c) obtain and the hydrogen-rich gas that step (d) obtains carry out desulfurization respectively.
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 the step (b) of method of above-mentioned paraffinic base crude oil with poor quality Poly-generation, solvent extraction can be done using conventional mixing C4
Solvent, extraction temperature be 90 DEG C～140 DEG C, preferably extraction temperature be 100 DEG C～120 DEG C, extraction pressure be 2.8MPa～
4.2MPa, preferably extraction pressure are 3.0MPa～3.5MPa, and solvent ratio is for 4:1～7:1, preferred solvent is than for 5:1～6:1.Step
Suddenly first crude oil with poor quality can be heated to 80 DEG C～140 DEG C in (a) carry out being dehydrated, carry out water again in electrical desalter after solid sedimentation
Wash, desalination, dehydration and de- solid.
Catalyst employed in step (c) 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.The molecular sieve being adopted be selected from y-type zeolite with or without rare earth element,
The silica-rich zeolite that with or without the ultrastable of rare earth element, there is five-membered ring structure, β zeolite, modenite, omega zeolite
One or more of, the silica-rich zeolite preferably with five-membered ring structure is ZSM-5 zeolite or ZRP zeolite；Heat resistant inorganic aoxidizes
One of the optional self-alumina of thing, silicon oxide, amorphous silicon aluminium, zirconium oxide, titanium oxide, boron oxide and alkaline earth oxide
Or it is several；Clay is selected from Kaolin, halloysite, montmorillonite, kieselguhr, galapectite, saponite, tired de- soil, meerschaum, recessed
One or more of convex rod stone, brucite and boron-moisten soil.Wherein most preferably molecular sieve catalyst, its activity is high, and green coke amount is few,
Gasoline yield is high, conversion ratio highest.
In step (c), catalytic cracking reaction condition is preferably：470 DEG C～550 DEG C of reaction temperature, preferable reaction temperature 480
DEG C～500 DEG C, 600 DEG C～800 DEG C of regeneration temperature, preferably 700 DEG C～750 DEG C of regeneration temperature, the matter of catalyst and fcc raw material
Amount ratio 3～18, preferred mass ratio 8～12, response time 0.5s～5s, pressure 0.1MPa～0.5MPa.
The present invention realizes the system of the paraffinic base crude oil with poor quality Poly-generation method of said method employing, and to include crude oil with poor quality pre-
Processing unit, gas sweetening unit, heavy oil residue processing unit, catalysis lighting unit, reformation lighting unit and diesel oil take off
Wax unit；
Crude oil with poor quality pretreatment unit passes through pipeline and heavy oil residue processing unit, catalysis lighting unit, reformation respectively
Lighting unit, gas sweetening unit and diesel oil dewaxing unit are connected；
Heavy oil residue processing unit is connected with catalysis lighting unit by pipeline；
Catalysis lighting unit passes through pipeline and reformation lighting unit, diesel oil dewaxing unit and gas desulfurization unit respectively
It is connected；
Reformation lighting unit is connected with gas sweetening unit by pipeline.
Wherein, crude oil with poor quality pretreatment unit includes raw material oil tank, electrical desalter, heat exchanger, heating furnace and normal pressure and divides
Evaporate tower；Multiple outlets of crude oil with poor quality pretreatment unit fractionating column connect gas sweetening unit, reformation lightweight by pipeline respectively
Change unit, catalysis lighting unit, diesel oil dewaxing unit and heavy oil residue processing unit；
Heavy oil residue processing unit includes solvent column and mixing asphalt device；
Catalysis lighting unit includes reactor, catalyst regenerator and fractionating column；
Reformation lighting unit includes reforming reactor, stablizes fractionating column and Aromatics Extractive Project tower；
Diesel oil dewaxing unit includes complex reactor and separative element；
Multiple outlets of the atmospheric fractional tower of crude oil with poor quality pretreatment unit connect gas sweetening unit by pipeline respectively
Gas desulphurisation plant, the complex reactor in diesel oil dewaxing unit, catalysis lighting unit reactor, heavy oil residue process
The solvent column of unit；The heat exchanger of crude oil with poor quality pretreatment unit connects going out of the Aromatics Extractive Project tower of reformation lighting unit
Mouthful.
The reactor of pipeline and catalysis lighting unit is passed through in the outlet of the solvent column in heavy oil residue processing unit
Entrance be connected.The fractionating column of catalysis lighting unit pass through respectively pipeline and reformation lighting unit reforming reactor,
The complex reactor of diesel oil dewaxing unit is connected with the gas desulphurisation plant of gas desulfurization unit.Reformation lighting unit steady
Determine fractionating column outlet to be connected with the entrance of the gas sweetening unit of gas sweetening unit by pipeline.Described raw oil
Steam(-)coil is set in storage tank.
, because of colloid, asphalitine height in crude oil with poor quality, light component is few, and described pretreatment unit adopts for step (a) of the present invention
" stove one tower " flow process, is made up of electrical desalter, heat exchanger, heating furnace and atmospheric fractional tower equipment：Crude oil with poor quality process washing,
With product oil heat exchange to 200 DEG C～250 DEG C (1.2MPa～1.7MPa) with being pumped to heating furnace after desalination, dehydration and de- solid,
It is heated to 360 DEG C～390 DEG C entrance atmospheric fractional towers：The gas isolated enters gas sweetening unit, the Petroleum isolated
Enter reformation lighting unit, diesel oil enters diesel oil dewaxing unit；Isolate 330 DEG C～350 DEG C AGO (atmospheric gas oil)s and enter catalysis
Lighting unit, the 350 DEG C of residual oil of ＞ isolated enter heavy oil residue processing unit.It is with conventional atmospheric distillation difference
Increased 330 DEG C～350 DEG C AGO (atmospheric gas oil)s and 350 DEG C of residual oil separation functions of ＞, residual oil is divided into fcc raw material and heavy slag
Oil.Reduce the treating capacity of heavy oil residue processing unit on the basis of meeting catalysis lighting ingredient requirement, reach saving operation
Expense and the purpose of energy consumption.
Heavy oil residue processing unit described in step (b) of the present invention is made up of solvent extraction and mixing asphalt device, ＞ 350
DEG C residual oil, through solvent extraction, colloid, asphalitine abjection obtains fcc raw material and de-oiled asphalt.Fcc raw material sends into catalysis
Lighting unit, de-oiled asphalt enters mixing asphalt device, makees Colophonium mediation raw material with catalytic slurry, produces wide market
Asphalt for high grade road.
The solvent extraction apparatus in heavy charge processing unit described in step (b) of the present invention adopt relatively low operation pressure
Power, equipment is easily fabricated, and investment is low；Solvent is done using mixing C4, extraction temperature is 90 DEG C～140 DEG C, extraction pressure is
2.8MPa～4.2MPa, solvent is than for 4:1～7:1, deasphalted oil yield reaches 70%～85%, and carbon residue as little as 1.8%～
2.5%, and Ni, V content are low；Solvent recovery adopts supercritical process, and recycling design temperature is high, and plant energy consumption is low.If Colophonium
Attemperation apparatus, make Colophonium mediation raw material with catalytic slurry, it is possible to increase the quality of Colophonium, produce the high-grade of wide market
Road asphalt, during 25 DEG C of this asphalt for high grade road, needle penetration is 40～140 (0.1mm), and softening point is 40 DEG C～55 DEG C, 15 DEG C
Shi Yandu ＞ 150cm.
Catalysis lighting unit described in step (c) of the present invention is mainly by reactor, catalyst regenerator, fractionating tower equipment
Composition.Fcc raw material from crude oil with poor quality pretreatment unit and heavy oil residue processing unit enters reactor, in catalyst
Effect is lower to there is cracking reaction, and macromole is cracked into small molecule, long-chain is fractured into short chain.Product enters fractionating column, through dividing
Evaporate and obtain dry gas, liquefied gas, gasoline, diesel oil and catalytic slurry.Dry gas enters gas sweetening unit, and liquefied gas goes out as product
Sell, Petroleum enters reformation lighting unit, diesel oil enters diesel oil dewaxing unit, and catalytic slurry enters heavy oil residue and processes list
Unit, a part is as Colophonium mediation raw material；Another part is as the raw material of heavy oil residue processing unit.After reaction participated in by catalyst
Enter catalyst regenerator, return to reactor after coke burning regeneration and be continuing with.Raw oil is anti-in catalysis lighting unit
Dry gas, liquefied gas, Petroleum, diesel oil and catalytic slurry (including catalytic cracking recycle oil and slurry oil) should be obtained after separating, urge
Heavy oil residue processing unit delivered to by carburetion slurry.
Reformation lighting unit described in step (d) of the present invention mainly by reforming reactor, stablize fractionating column and aromatic hydrocarbons is taken out
Stripper equipment forms.Petroleum from crude oil with poor quality pretreatment unit and catalysis lighting unit enters reformation lighting unit
Reforming reactor, 480 DEG C～550 DEG C of reaction temperature, preferably 500 DEG C～520 DEG C；Reaction pressure 1MPa～3MPa, preferably
1MPa～1.5MPa；Volume space velocity is 1～2.5h-1, preferably 1～2h-1；Hydrogen to oil volume ratio 800～1500Nm3/m3, preferably 1100
～1300Nm3/m3.There is cracking reaction in the presence of conventional catalyst, dehydrogenation reaction, alkane isomerization, aromatic hydrocarbons take off alkane
Base, hydro carbons hydrogenolysis etc. are reacted.Product enters stablizes fractionating column, is fractionated into obtaining hydrogen-rich gas and light naphthar.Hydrogen rich gas
Body enters gas sweetening unit, and light naphthar enters Aromatics Extractive Project tower, obtains high-knock rating gasoline and aromatic hydrocarbons through Aromatics Extractive Project,
Aromatic hydrocarbons can be used as PX raw material.
Diesel oil dewaxing unit described in step (e) of the present invention adopts isopropanol water solution urea dewaxing process, for producing
Liquid paraffin and low-coagulation diesel oil.This unit is mainly made up of complex reactor and separative element, and separative element includes complex
Stirring and segregation, washing refine and reclaim distillation etc., and complex reaction temperature is 25 DEG C～35 DEG C, preferably 25 DEG C～28 DEG C；During reaction
Between be 1～3h, the mass percent of carbamide/isopropanol/water is 40:42:18；Light from crude oil with poor quality pretreatment unit and catalysis
The diesel oil of matter unit enters complex reactor after mixing with the aqueous solution of urea of isopropanol, normal concentration, and product enters
Separative element is separated and rectification obtains liquid paraffin and low-coagulation diesel oil.
Crude oil with poor quality pretreatment of the present invention, catalysis lighting, reformation lighting unit institute aerogenesis body fully enter
Desulfurizing tower, deviates from H2It is used as furnace fuel after S.Crude oil with poor quality quality testing is according to (GB/T18609-2011 acid value for crude oil
Measure potentiometric titration；The mensure of wax, colloid, asphalt content in SY/T7550-2012 crude oil；GB/T17280-2009 crude oil
Distillation standard test method 15- theoretical plate distillation column；GB/T17280-2009 crude distillation standard test method 15- theoretical plate steams
Fractional distillation column) carry out, the equipment that the present invention is not described in detail and operational approach 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 pretreatment, heavy oil residue are processed, are catalyzed lighting, reformation lighting, diesel oil dewaxing by the present invention
It is organically combined with process of desulfurizing gases, to greatest extent crude oil with poor quality is changed into diesel oil, high-knock rating gasoline and can
Aromatic hydrocarbons as PX raw material and liquid paraffin；Product category is many, can meet multi-field development need, and simplifies technique stream
Journey, reduces overall energy consumption.
(2) crude oil with poor quality pretreatment unit increased 330 DEG C～350 DEG C AGO (atmospheric gas oil)s and 350 DEG C of residual oil works of separation of ＞
Can, residual oil is divided into fcc raw material and heavy oil residue.Reduce heavy oil residue on the basis of meeting catalysis lighting ingredient requirement
The treating capacity of processing unit, reaches the purpose saving operating cost and energy consumption.
(3) crude oil with poor quality pretreatment, heavy charge process, catalysis lighting, reformation lighting unit institute aerogenesis body are whole
Enter desulfurizing tower, deviate from H2It is used as furnace fuel after S, at utmost make use of system internal product.
(4) 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 crude oil with poor quality pretreatment unit.
330 DEG C～350 DEG C AGO (atmospheric gas oil)s enter catalysis lighting unit, should not be used as 350 DEG C of residual oil of ＞ of fcc raw material through overweight
It is used further to after matter residual oil processing unit processes be catalyzed lighting unit raw material, both improved the yield of Petroleum, diesel oil, and reduced again
The technical difficulty of catalysis lighting and the operation cycle extending catalysis lighting unit.
(5) catalytic slurry of catalysis lighting unit is delivered to heavy oil residue processing unit to be incorporated in charging, treated
Deviate from the condensed ring containing and polycyclic aromatic hydrocarbon, that is, increased the raw material of catalysis lighting unit, meanwhile, be catalyzed urging of lighting unit
The condensed ring that carburetion slurry contains and polycyclic aromatic hydrocarbon enter in Colophonium, improve the quality of Colophonium.
(6) heavy oil residue processing unit sets mixing asphalt device, makees Colophonium mediation raw material with catalytic slurry, improves Colophonium
Quality, produces the asphalt for high grade road of wide market, increased product category.
(7) crude oil with poor quality pretreatment, heavy charge process, are catalyzed lighting, reformation lighting and gas desulfurization unit connection
Close and run, both reduced investment, and improve full factory heat utilization ratio again.
Brief description
Fig. 1 is the system schematic of paraffinic base crude oil with poor quality Poly-generation of the present invention.
Wherein, 1, raw material oil tank, 2, electrical desalter, 3, heat exchanger, 4, heating furnace, 5, atmospheric fractional tower, 6, solvent takes out
Stripper, 7, mixing asphalt device, 8, reactor, 9, catalyst regenerator, 10, fractionating column, 11, reforming reactor, 12, stable point
Evaporate tower, 13, Aromatics Extractive Project tower, 14, complex reactor, 15, separative element, 16, gas sweetening unit, 17, crude oil with poor quality
Pretreatment unit, 18, heavy oil residue processing unit, 19, catalysis lighting unit, 20, reformation lighting unit, 21, gas takes off
Sulfur unit, 22, diesel oil dewaxing unit.
Specific embodiment
Below in conjunction with the accompanying drawings method provided by the present invention is further described.
As shown in figure 1, the system of paraffinic base crude oil with poor quality Poly-generation method of the present invention includes crude oil with poor quality pretreatment unit
17, gas sweetening unit 21, heavy oil residue processing unit 18, it is catalyzed lighting unit 19, reformation lighting unit 20, diesel oil takes off
Wax unit 22；
Crude oil with poor quality pretreatment unit includes raw material oil tank 1, electrical desalter 2, heat exchanger 3, heating furnace 4 and normal pressure fractional distillation
Tower 5；Multiple outlets of the atmospheric fractional tower 5 of crude oil with poor quality pretreatment unit connect gas sweetening unit, weight by pipeline respectively
Whole lighting unit, catalysis lighting unit, diesel oil dewaxing unit and heavy oil residue processing unit；
Heavy oil residue processing unit includes solvent column 6 and mixing asphalt device 7；
Catalysis lighting unit includes reactor 8, catalyst regenerator 9 and fractionating column 10；
Reformation lighting unit includes reforming reactor 11, stablizes fractionating column 12 and Aromatics Extractive Project tower 13；
Diesel oil dewaxing unit includes complex reactor 14 and separative element 15；
Multiple outlets of the atmospheric fractional tower 5 of crude oil with poor quality pretreatment unit connect gas sweetening unit by pipeline respectively
Gas desulphurisation plant 16, the complex reactor 14 in diesel oil dewaxing unit, catalysis lighting unit reactor 8, heavy slag
The solvent column 6 of oil processing unit；The aromatic hydrocarbons that the heat exchanger 3 of crude oil with poor quality pretreatment unit connects reformation lighting unit is taken out
The outlet of stripper 13.
The reactor of pipeline and catalysis lighting unit is passed through in the outlet of the solvent column 6 in heavy oil residue processing unit
8 entrance is connected.The fractionating column 10 of catalysis lighting unit passes through the reforming reaction of pipeline and reformation lighting unit respectively
Device 11, the complex reactor 14 of diesel oil dewaxing unit are connected with the gas desulphurisation plant 16 of gas desulfurization unit.Reformation lightweight
Stable fractionating column 12 outlet changing unit is connected with the entrance of the gas desulphurisation plant 16 of gas sweetening unit by pipeline.Former
Steam(-)coil is set in material oil tank 1.
The method of above-mentioned paraffinic base crude oil with poor quality Poly-generation, specifically includes following steps：
External crude oil with poor quality is sent into raw material oil tank and (is inside set steam(-)coil, using steam by heating crude oil to 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 and
With product oil heat exchange to 220 DEG C (1.6MPa) with being pumped to atmospheric pressure kiln after de- solid, it is heated to 380 DEG C of entrance normal pressure fractional distillation
Tower：The gas isolated enters gas sweetening unit, and the Petroleum isolated enters reformation lighting unit, and diesel oil enters diesel oil
Dewaxing unit, the AGO (atmospheric gas oil) isolated enters catalysis lighting unit, and the 350 DEG C of residual oil of ＞ isolated enter heavy oil residue
Processing unit.
350 DEG C of residual oil of ＞ enter heavy oil residue processing unit, and heavy oil residue processing unit is adjusted by solvent column and Colophonium
Attach together and put 14 compositions, obtain deasphalted oil and de-oiled asphalt through solvent extraction, de-oiled asphalt enters Colophonium attemperation apparatus, use
Catalytic slurry 23 makees Colophonium mediation raw material, produces the asphalt for high grade road of wide market.
AGO (atmospheric gas oil) and deasphalted oil enter catalysis lighting unit, and catalysis lighting unit is by reactor, catalyst
Regenerator, the capital equipment such as fractionating column forms.Fcc raw material and deasphalted oil enter reactor, occur in the presence of catalyst
Cracking reaction, macromole is cracked into small molecule, long-chain is fractured into short chain.Product enters fractionating column, be fractionated into obtaining dry gas,
Liquefied gas, Petroleum, diesel oil and catalytic slurry.Dry gas enters gas sweetening unit, and Petroleum enters reformation lighting unit, liquid
Activating QI is sold as product, and diesel oil enters diesel oil dewaxing unit.Catalytic slurry enters heavy charge processing unit.Catalyst is participated in
Enter catalyst regenerator after reaction, return to reactor after coke burning regeneration and be continuing with.
Enter the weight of reformation lighting unit from the Petroleum of crude oil with poor quality pretreatment unit and catalysis lighting unit
, there is cracking reaction in the presence of catalyst, dehydrogenation reaction, alkane isomerization, aromatic hydrocarbons take off alkyl, hydro carbons hydrogenolysis in whole reactor
Deng reaction.Product enters stablizes fractionating column, is fractionated into obtaining hydrogen-rich gas and light naphthar.Light naphthar enters aromatic hydrocarbons and takes out
Stripper, obtains high-knock rating gasoline and aromatic hydrocarbons (PX raw material) through Aromatics Extractive Project.Hydrogen-rich gas enters gas sweetening unit, desulfurization
The processed gas that unit produces is used as furnace fuel.
From pretreatment unit and catalysis lighting unit diesel oil mix with isopropanol, aqueous solution of urea after entrance diesel oil
Dewaxing unit, diesel oil dewaxing unit is made up of complex reactor and separative element, and separative element includes complex stirring and segregation, washes
Wash refined and reclaim distillation etc.；Product obtains liquid paraffin and low-coagulation diesel oil through separating with rectification.
It is described further below by the method that specific embodiment provides to the present invention, but therefore do not limit this
Invention.
Embodiment
Full device total technological process processes-is catalyzed lighting-reformation lightweight using inferior raw material pretreatment-heavy oil residue
Change-diesel oil dewaxing-process of desulfurizing gases technology path.
Crude oil with poor quality pretreatment by crude cut be dry gas, Petroleum, diesel oil, AGO (atmospheric gas oil) and residual oil.Dry gas enters
Gas sweetening unit, Petroleum enters reformation lighting unit, and diesel oil enters diesel oil dewaxing unit, and AGO (atmospheric gas oil) enters catalysis
Lighting unit, residual oil enters heavy charge processing unit.
The partially catalyzed slurry oil mixing of residual oil and the generation of subsequent catalyst lighting unit, through solvent extraction, by colloid, Colophonium
Matter is deviate from, and obtains fcc raw material and de-oiled asphalt.Fcc raw material sends into catalysis lighting unit, and de-oiled asphalt enters mixing asphalt
Device, makees Colophonium mediation raw material with catalytic slurry, produces the asphalt for high grade road of wide market.
Enter catalysis lighting unit from the fcc raw material of crude oil with poor quality pretreatment unit and heavy oil residue processing unit,
There is cracking reaction in the presence of ZSM-5 zeolite or ZRP zeolite are as catalyst, be fractionated into obtaining dry gas, liquefied gas, vapour
Oil, diesel oil and catalytic slurry.Dry gas enters gas sweetening unit, and Petroleum enters reformation lighting unit, and diesel oil enters diesel oil
Dewaxing unit, liquefied gas is sold as product.Catalytic slurry enters heavy oil residue processing unit, and a part is in harmonious proportion former as Colophonium
Material, another part is as the raw material of heavy oil residue processing unit.Catalyst enters catalyst regenerator, through burning after participating in reaction
Return to reactor after burnt regeneration to be continuing with.
Enter the weight of reformation lighting unit from the Petroleum of crude oil with poor quality pretreatment unit and catalysis lighting unit
Whole reactor, product enters stablizes fractionating column, is fractionated into obtaining hydrogen-rich gas and light naphthar.Light naphthar enters aromatic hydrocarbons
Extraction tower, obtains high-knock rating gasoline and aromatic hydrocarbons (PX raw material) through Aromatics Extractive Project.Hydrogen-rich gas enters gas sweetening unit.
Diesel oil dewaxing unit adopts isopropanol water solution urea dewaxing process, for producing liquid paraffin and low-coagulation diesel oil.
From pretreatment unit and catalysis lighting unit diesel oil mix with isopropanol, aqueous solution of urea after entrance complex reactor,
Product obtains liquid paraffin and low-coagulation diesel oil through separating with rectification.
The crude oil with poor quality pretreatment of the present invention, heavy charge are processed, catalysis lighting unit, reformation lighting unit are produced
Gas all sends into gas sweetening unit, and the produced processed gas of gas sweetening unit is used as furnace fuel.
The feedstock property that embodiment adopts is shown in Table 1, crude oil with poor quality pretreatment, heavy charge processing unit, catalysis lighting
The material balance table of unit and reformation lighting unit is shown in Table 2～5 respectively.Prevailing operating conditions are shown in Table 6, and Reformed Gasoline property is shown in
The property of table 7, hydrofining diesel oil and catalytic diesel oil is shown in Table 8, and road asphalt property is shown in Table 9.
Comparative example 1
Full device total technological process adopt inferior raw material pretreatment-black oil oil processing-catalysis lighting-diesel oil dewax-
Process of desulfurizing gases technology path.Using with embodiment identical raw material, from unlike embodiment to feed material preparation units
And the Petroleum that catalysis lighting unit produces does not carry out reformation lighting, the anti-knock properties of direct steaming gasoline are poor, sensitivity
Smaller, catalytically cracked gasoline has preferable anti-knock properties.The property of direct steaming gasoline and catalytically cracked gasoline is shown in Table 7.
Comparative example 2
Full device total technological process adopts inferior raw material pretreatment-black oil oil processing-catalysis lighting-reformation lightweight
Change-process of desulfurizing gases technology path.Using with embodiment identical raw material, from feed material preparation units unlike embodiment
The straight-run diesel oil obtaining and the catalytic diesel oil of catalysis lighting unit generation be not through diesel oil dewaxing unit.Catalytic cracking diesel oil
Middle arene content is high, condensation point is higher, stability and Cetane lndex are all not as straight-run diesel oil.Catalytic cracking diesel oil and straight-run diesel oil
Property be shown in 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 crude oil with poor quality pretreatment distillation partial material balance
| Sequence number | Name of material | Flow rate |
| ×104t/a | kg/h | ||
| One | Raw material | ||
| 1 | Crude oil with poor quality | 250 | 297619 |
| Two | Product | ||
| 1 | Gas | 0.5 | 600 |
| 2 | Direct steaming gasoline | 22.38 | 26640 |
| 3 | Straight-run diesel oil | 43.76 | 52100 |
| 4 | AGO (atmospheric gas oil) | 86.77 | 103300 |
| 5 | >=350 residual oil | 96.58 | 114980 |
| Total | 250 | 297619 |
Table 3 heavy charge processing unit material balance
| Sequence number | Fraction title | Flow rate × 104t/a |
| Raw material | ||
| 1 | Decompression residuum | 96.58 |
| 2 | Catalytic slurry | 5.83 |
| Total | 102.41 | |
| Product | ||
| 1 | Deasphalted oil | 87.05 |
| 2 | Mediation Colophonium | 15.01 |
| 3 | Loss | 0.35 |
| Total | 99.49 |
Table 4 catalysis lighting supplies of unit balance
| Sequence number | Fraction title | Flow rate × 104t/a |
| Raw material | ||
| 1 | AGO (atmospheric gas oil) | 86.77 |
| 2 | Deasphalted oil | 87.05 |
| Total | 173.82 |
| Product | ||
| 1 | Catalysis drying gas | 5.77 |
| 2 | Catalytic liquid activating QI | 26.94 |
| 3 | Catalytic gasoline | 81.97 |
| 5 | Catalytic diesel oil | 44.31 |
| 6 | Catalytic slurry | 5.83 |
| 7 | Catalysis is burnt | 10.26 |
| 8 | Loss | 0.74 |
| Total： | 173.82 |
Table 5 reformation lighting supplies of unit balances
| Sequence number | Fraction title | Flow rate × 104t/a |
| Raw material | ||
| 1 | Direct steaming gasoline | 22.38 |
| 2 | Catalytic gasoline | 81.97 |
| Total | 104.35 | |
| Product | ||
| 1 | Dry gas | 4.47 |
| 2 | Reformed Gasoline | 97.57 |
| 3 | Aromatic hydrocarbons | 2.31 |
| Total | 104.35 |
Table 6 prevailing operating conditions
| Crude oil with poor quality pretreatment unit | |
| Raw oil storage tank heat temperature/DEG C | 90 |
| With temperature after product oil heat exchange/DEG C | 220 |
| With pressure/MPa after product oil heat exchange | 1.6 |
| Furnace outlet temperature/DEG C | 380 |
| Heavy oil residue processing unit | |
| Extraction temperature, DEG C | 120 |
| Extraction pressure, MPa | 3.2 |
| Solvent ratio | 6:1 |
| Catalysis lighting unit | |
| Reaction temperature, DEG C | 500 |
| Regeneration temperature, DEG C | 750 |
| Catalyst/fcc raw material, m% | 10 |
| Response time, s | 2 |
| Pressure, MPa | 0.2 |
| Reformation lighting unit | |
| Reaction temperature, DEG C | 505 |
| Reaction pressure, MPa | 1.2 |
| Volume space velocity, h-1 | 1.5 |
| Hydrogen to oil volume ratio, Nm3/m3 | 1200 |
| Diesel oil dewaxing unit | |
| Complex reaction temperature, DEG C | 28 |
| Response time, h | 2 |
| Urine/alcohol/water, % | 40:42:18 |
| Urine oil ratio, m% | 11 |
| Washing hop count, n | 4 |
| Washing oil ratio, m% | 2 |
Table 7 gasoline products property list
Table 8 diesel product property list
Table 9 asphaltic nature table
Claims (10)
1. a kind of method of paraffinic base crude oil with poor quality Poly-generation is it is characterised in that the method includes crude oil with poor quality pretreatment, heavy
Residual oil processes, is catalyzed lighting, reformation lighting, diesel oil dewaxing and gas sweetening process, comprises the following steps that：
The pretreatment of (a) crude oil with poor quality：Crude oil with poor quality is carried out washing, desalination, dehydration and de- solid, heat exchange to 200 DEG C～250
DEG C, then it is heated to 360 DEG C～390 DEG C by heating furnace, enter atmospheric fractional tower：Isolate gas, Petroleum, diesel oil, 330 DEG C
～350 DEG C of AGO (atmospheric gas oil)s and 350 DEG C of residual oil of ＞；
B () heavy oil residue is processed：350 DEG C of residual oil of ＞ that step (a) is obtained obtain fcc raw material and height through solvent extraction
Grade road asphalt；
C () is catalyzed lighting：330 DEG C～350 DEG C normal pressure gas that the fcc raw material that obtain step (b) and step (a) obtain
There is cracking reaction in oil in the presence of catalyst, thus obtaining dry gas, liquefied gas, Petroleum, diesel oil and catalytic slurry；Catalysis
The heavy oil residue that slurry oil carries out step (b) is processed；
(d) reformation lighting：The Petroleum that step (a) and step (c) are obtained enters reforming reactor, in the effect of catalyst
Under reacted, the product obtaining is fractionated into obtaining hydrogen-rich gas and light naphthar；Light naphthar obtains through Aromatics Extractive Project
To high-knock rating gasoline and aromatic hydrocarbons；
The dewaxing of (e) diesel oil and gas sweetening：The diesel oil that step (a) and step (c) are obtained is mixed with isopropanol, aqueous solution of urea
Enter complex reactor afterwards, product obtains liquid paraffin and low-coagulation diesel oil through separating with rectification；Step (a) is isolated
Dry gas that gas and step (c) obtain and the hydrogen-rich gas that step (d) obtains carry out desulfurization respectively.
2. a kind of method of paraffinic base crude oil with poor quality Poly-generation according to claim 1 is it is characterised in that in step (b)
The extraction temperature that solvent extraction adopts is 90 DEG C～140 DEG C, and extraction pressure is 2.8MPa～4.2MPa, and solvent ratio is for 4:1～7:
1.
3. a kind of method of paraffinic base crude oil with poor quality Poly-generation according to claim 1 is it is characterised in that in step (c)
Cracking reaction condition is：The matter of 470 DEG C～550 DEG C of reaction temperature, 600 DEG C～800 DEG C of regeneration temperature, catalyst and fcc raw material
Amount ratio 3～18, response time 0.5s～5s, pressure 0.1MPa～0.5MPa.
4. the method for paraffinic base crude oil with poor quality Poly-generation according to claim 1 is it is characterised in that reform in step (d)
480～550 DEG C of the reaction temperature adopting in reactor, reaction pressure 1MPa～3MPa, volume space velocity 1～2.5h-1, hydrogen oil volume
Than 800～1500Nm3/m3.
5. a kind of system for the paraffinic base crude oil with poor quality Poly-generation method described in claim 1 is it is characterised in that this system
Including crude oil with poor quality pretreatment unit, gas sweetening unit, heavy oil residue processing unit, catalysis lighting unit, reformation lightweight
Change unit and diesel oil dewaxing unit；
Crude oil with poor quality pretreatment unit passes through pipeline and heavy oil residue processing unit, catalysis lighting unit, reformation lightweight respectively
Change unit, gas sweetening unit and diesel oil dewaxing unit to be connected；
Heavy oil residue processing unit is connected with catalysis lighting unit by pipeline；
Catalysis lighting unit is connected with reformation lighting unit, diesel oil dewaxing unit and gas desulfurization unit by pipeline respectively
Connect；
Reformation lighting unit is connected with gas sweetening unit by pipeline.
6. system according to claim 5 it is characterised in that crude oil with poor quality pretreatment unit include raw material oil tank (1),
Electrical desalter (2), heat exchanger (3), heating furnace (4) and atmospheric fractional tower (5)；The atmospheric fractional tower of crude oil with poor quality pretreatment unit
(5) multiple outlets connect gas sweetening unit, reformation lighting unit, catalysis lighting unit, diesel oil by pipeline respectively
Dewaxing unit and heavy oil residue processing unit.
7. system according to claim 5 it is characterised in that heavy oil residue processing unit include solvent column (6) and
Mixing asphalt device (7)；Catalysis lighting unit includes reactor (8), catalyst regenerator (9) and fractionating column (10)；Reform
Lighting unit includes reforming reactor (11), stablizes fractionating column (12) and Aromatics Extractive Project tower (13)；Diesel oil dewaxing unit includes
Complex reactor (14) and separative element (15)；Multiple outlets of the atmospheric fractional tower (5) of crude oil with poor quality pretreatment unit divide
By the gas desulphurisation plant (16) of pipeline connection gas sweetening unit, the complex reactor (14) in diesel oil dewaxing unit,
The reactor (8) of catalysis lighting unit, the solvent column (6) of heavy oil residue processing unit；Crude oil with poor quality pretreatment unit
Heat exchanger (3) connect reformation lighting unit Aromatics Extractive Project tower (13) outlet.
8. system according to claim 7 is it is characterised in that solvent column (6) in heavy oil residue processing unit
Outlet is connected with the entrance of the reactor (8) of catalysis lighting unit by pipeline.
9. system according to claim 8 is it is characterised in that the fractionating column (10) of catalysis lighting unit passes through pipe respectively
The reforming reactor (11) of road and reformation lighting unit, the complex reactor (14) of diesel oil dewaxing unit and gas desulfurization unit
Gas desulphurisation plant (16) be connected.
10. system according to claim 7 is it is characterised in that the stable fractionating column (12) of reformation lighting unit exports
It is connected with the entrance of the gas desulphurisation plant (16) of gas sweetening unit by pipeline.
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Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6342152B1 (en) * | 1998-08-25 | 2002-01-29 | Idemitsu Kosan Co., Ltd. | Hydrogenation treatment process for crude oil and crude oil reformed thereby |
| CN1766055A (en) * | 2004-10-29 | 2006-05-03 | 中国石油化工股份有限公司 | One-stage tandem combined process for hydrocracking- aryl removal |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6342152B1 (en) * | 1998-08-25 | 2002-01-29 | Idemitsu Kosan Co., Ltd. | Hydrogenation treatment process for crude oil and crude oil reformed thereby |
| CN1766055A (en) * | 2004-10-29 | 2006-05-03 | 中国石油化工股份有限公司 | One-stage tandem combined process for hydrocracking- aryl removal |
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