CN1351643A - Process for treating crude oil - Google Patents
Process for treating crude oil Download PDFInfo
- Publication number
- CN1351643A CN1351643A CN 00807697 CN00807697A CN1351643A CN 1351643 A CN1351643 A CN 1351643A CN 00807697 CN00807697 CN 00807697 CN 00807697 A CN00807697 A CN 00807697A CN 1351643 A CN1351643 A CN 1351643A
- Authority
- CN
- China
- Prior art keywords
- oil
- distillation
- cracking
- thermo
- crude
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
Abstract
A process for treating a crude oil having a crude oil distillation and a separation step for distilling a crude oil to separate into a distillate oil and a residual oil, a thermal cracking step for subjecting to heat-decomposition the residual oil which is obtained substantially as a bottom fraction from the distillation and separation step, to thereby convert it to a light oil, and a thermally cracked product distillation and separation step for distilling and separating the thermally cracked product from the thermal cracking step, characterized in that the crude oil distillation and separation step and the thermally cracked product distillation and separation step are carried out at the same time in a distillation section comprising a reduced pressure distillation apparatus. The process makes a crude oil treating process more simple and more space-efficient and can reduce the cost for treating. Further, the process can be advantageously employed in a small scale oil refinery.
Description
Technical field
The present invention relates to the treatment process of crude oil, particularly relate in refining of petroleum, comprise heavy oil content contained in the crude oil is transformed into method that the mink cell focus lightweight oil content, so-called the upgrades crude Treatment method as major portion with crude production high additive value petroleum products.
Background technology
With reference to Fig. 3 the treating processes of the general crude oil that carries out is up to now described.
That refinery is received, finish the crude oil 2 of regulation pre-treatment, be distilled separation by atmospheric distillation plant 100, downward from cat head, distill out gas part 101, kerosene part 103, diesel oil part 105 etc. respectively, separated at tower bottom heavy oil content 107 as Residual oil.
From cat head expellant gas part 101,, for example can be divided into light gas part (H2, C1, C2) 111, LPG part (C3, C4) 113, C5～C6 part 115, petroleum naphtha part 117 in gas recovery district 110.Light gas part 111 and LPG part 113 and C5～C6 part 115 usually, adopts washing device to remove hydrogen sulfide respectively, and light gas part 111 is used to our factory's fuel, and LPG part 113 is made into the LPG product.C5～C6 part 115 is made into gasoline blender.
Petroleum naphtha 117 generally carries out desulfurization and denitrogenation processing with hydro-refining unit 120, carries out in reformer 125 then behind the catalytic reforming boosting of octane rating as gasoline blender.
Kerosene part 103, by hydro-refining unit 130 (having desulfurization cracking reactor R1 and the D1 of rectifying portion), it is refining to carry out hydrogenating desulfurization, removes desulfuration composition and nitrogen component etc., makes kerosene product or jet fuel usually.
Diesel oil part 105 is carried out hydrogenating desulfurization and is made with extra care too in hydro-refining unit 140 (having desulfurization cracking reactor R2 and the D2 of rectifying portion), remove desulfuration composition etc., makes solar oil.
The heavy oil content 107 of discharging from the tower bottom of atmospheric distillation plant 100 is admitted to the vacuum distillation apparatus 200, so that be transformed into the so-called processing of upgrading of light ends.At this, heavy oil content 107 is separated into decompression diesel oil 201 and becomes the decompression residual oil 205 of thermo-cracking raw material.Decompression diesel oil 201 is in hydrotreater 210 (having desulfurization cracking reactor R3 and the D3 of rectifying portion), carrying out the desulfurization crack refinement separates, isolated each cut (being separated into petroleum naphtha, kerosene, solar oil, decompression diesel oil) at the D3 of rectifying portion, usually be admitted to above-mentioned gas recovery district 110 as shown in the figure, produce product with the product line merging of kerosene and solar oil.
On the other hand, adopt vacuum distillation apparatus 200 isolating decompression residual oils 205 to supply with thermo-cracking district 220 (having reactor R4 and the D4 of rectifying portion).220 thermo-cracking raw materials are by thermo-cracking in the thermo-cracking district, generate cracked gas as the thermo-cracking resultant, cracked oil, as the pitch or the oil coke of residue.Thermal cracking oil is handled for 2 times through hydrofining, hydrocracking, catalytic pyrolysis, separation etc. and is become the finished product.When thermal cracking oil being carried out handle for 2 times, normally mix with isolating in advance kerosene part 103 in atmospheric distillation plant 100 and vacuum distillation apparatus 200, diesel oil part 105, decompression diesel oil distillate 201.Therefore, in order to meet these boiling spreads, thermal cracking oil also will be divided into a plurality of boiling spreads at rectifying portion (D4).
In the aforesaid method, especially the grade of the mink cell focus in the thermo-cracking district by in the past improves when receiving publicity, and for obtaining thermo-cracking raw material 205 (decompression residual oil 205), must carry out two sections distillation procedures of atmospheric distillation plant 100 and vacuum distillation apparatus 200.And then, reclaim for thermal cracking oil being carried out handle for 2 times, thermal cracking oil must be divided into the boiling spread identical distilled oil is mixed with the distilled oil (for example, 101,105,201) of atmospheric distillation plant 100 and vacuum distillation apparatus 200.Therefore, 220 must add distiller D4 in the thermo-cracking district, and 3 distillation towers 100,200, D4 must be arranged at least.
Therefore, the device formation of the usefulness of upgrading of the mink cell focus of employing thermo-cracking is extremely complicated and is expensive device.But also must guarantee the spacious space that is provided with.The cost of this class problem and each goods of purified improves directly related, so be extremely strict for the introducing of novel processing unit at present.
Just because of this, the grade of the relevant mink cell focus that is caused by thermo-cracking that should address the above problem improves, and wishing to propose a kind of technology of can simplifying again can cheap treatment process.
In addition, investigate based on above-mentioned Fig. 3 in the past whole technologies common often to technology be, at the crude oil 2 that imports after 2 distillation procedures are separated into each composition, for each separated component, (R1～R4) (D1～D4) combination of grade carries out same hydrogenating desulfurization purification operations respectively repeatedly with rectifying portion by the desulfurization cracking reactor.The cost that system for handling in the past like this can be described as direct and each product of purified improves associated, and is the same with the grade raising of the mink cell focus that is caused by above-mentioned thermo-cracking, and the hope proposition is a kind of can simplify the treatment process that whole technologies are again cheapnesss.
The present invention just is being based on the inventive arrangements that such present situation proposes, and its purpose is, improves complicated that device in the past constitutes, and provides a kind of and promptly can seek to simplify technology and save the space, can seek to reduce the crude Treatment method of processing cost again.In addition, also provide the treatment process that can be fit to the crude oil of small-scale refining of petroleum requirement.
Disclosure of an invention
For solving such problem, the present invention is the crude Treatment method with following operation: the crude distillation separation circuit that crude distillation is separated into distilled oil and heavy oil content, to separate the heavy oil content thermo-cracking that obtains from the bottom in fact and the thermo-cracking operation of carrying out lighting by this crude distillation separation circuit, with will carry out the thermo-cracking resultant fractionation by distillation operation of fractionation by distillation by the thermo-cracking resultant that this thermo-cracking operation lighting obtains, it is characterized in that this method is the constituted mode that carries out above-mentioned crude distillation separation circuit and thermo-cracking resultant fractionation by distillation operation in the distillation zone that is made of vacuum distillation apparatus simultaneously.
In addition, be that pre-separate device and main tripping device are contained in the distillation zone that above-mentioned crude distillation separation circuit and thermo-cracking resultant fractionation by distillation operation are carried out simultaneously as preferred version of the present invention.
In addition, the preferred embodiments of the invention are that with respect to distilled oil 100 weight parts of distillation zone, the heavy oil content of being discharged from the bottom by the cracking of above-mentioned distillation zone will reach 15～55 weight parts.
Also have, be, separating from the bottom discharge by above-mentioned crude distillation separation circuit and supplying to the heavy oil content of thermo-cracking operation, do not contain diesel oil part and decompression diesel oil part in fact as preferred version of the present invention.
Moreover, be not contain the heavy oil branch in the thermo-cracking Residual oil in above-mentioned thermo-cracking operation as preferred version of the present invention.
As another preferred version of the present invention be, crude distillation separation circuit that employing is carried out simultaneously in above-mentioned distillation zone and the isolating distilled oil of thermo-cracking resultant fractionation by distillation operation carry out together in same hydrotreatment district that desulfurization cracking hydrotreatment constitutes like that.
The simple declaration of accompanying drawing
Fig. 1 is the process flow sheet of expression the preferred embodiments of the invention;
Fig. 2 is the detailed process figure of the distillation zone 10 in the detailed presentation graphs 1;
Fig. 3 is a process flow sheet of representing general crude Treatment scheme in the past.
Be the preferred plan that carries out an invention
Explain the present invention based on technical process shown in Figure 1 below.
The crude oil that refinery is received usually, after leaving standstill in unrefined oil tank, removes with demineralizer (desalter) and to anhydrate and mud.Finishing the crude oil 2 of this pre-treatment, as preferred version of the present invention, is to be directed to contain with the distillation zone 10 of vacuum distillation apparatus as main device.Figure 2 illustrates the detailed artwork of distillation zone 10.
As shown in Figure 2, crude oil 2 is imported initial pre-separate device, for example, simple flash drum 3 is separated into gas part 3a and liquid distillate 3b.Liquid distillate 3b is imported vacuum distillation apparatus 10 ', be separated into the oily 11a of the extraction of extracting out and divide 15 decompression residual oil (crude distillation separation circuit) as the heavy oil that comes out from tower bottom from tower top.In addition, will further be separated into gas part 12 and liquid distillate 11b from the gas part 3a condensation of flash drum 3.Liquid distillate 11b with mix from the extraction of vacuum distillation apparatus 10 ' oil 11a, become the stock oil (distilled oil) 11 of hydrotreatment.Contain decompression diesel oil part, diesel oil part, kerosene part and petroleum naphtha part in the distilled oil 11, in gas part 12, contain LP gas part and light gas part etc.
Suitable operational condition as the distillation zone 10 of containing this vacuum distillation apparatus 10 ' is that pressure is that 1～10kPa, temperature are about 350～400 ℃.The ratio that separates of the distilled oil 11 in the distillation zone 10 and decompression residual oil (15), by weight, with respect to 100 parts of distilled oils 11, decompression residual oil (15) is 15～55 parts.This separates ratio, determines according to oily kind is different, and for example, the occasion at the arabian oil crude oil of heavy makes decompression residual oil (15) become 45～55 parts for good.Decompression residual oil (15) is during less than 45 parts, the metal ingredient that contains in the mink cell focus, residual carbon composition are sent to the hydrotreatment district 30 in downstream, the pore of the desulfurization catalyst for cracking in hydrotreatment district 30 because metal and oil coke result in blockage, its result has increased the weight of catalyst activity and has reduced the unfavorable problem that makes catalyst life shortening and so on.On the other hand, when decompression residual oil (15) surpasses 55 parts, because the heat scission reaction speed of decompression residual oil descends significantly, necessitate so the reaction time in thermo-cracking district is prolonged or make temperature of reaction exacting terms such as uprise, as a result, produce the undesirable situation of cracking and so on effectively that hinders.On the other hand, the occasion of the Arabic ultralight matter of light-weight petroleum crude oil is because reason same as described above makes decompression residual oil (15) become 15～30 parts for good.
In addition, supply with the crude oil of distillation zone 10, also can be the overweight matter crude oil such as Reno difficult to understand section tar of husky pitch of Canadian oil and Venezuela, in this occasion, can be with the separate raw material that than be adjusted to can be fit to supply with thermo-cracking district and hydrotreatment district of the oil 11 of the extraction in the distillation zone 10 with decompression residual oil (15).In addition, supplying with the crude oil of distillation zone 10, also can be the air distillation Residual oil, in this occasion, can separate ratio with above-mentioned similarly the adjusting.
In addition, in crude distillation separation circuit of the present invention, supplying to the heavy oil content 15 of thermo-cracking operation, coming down under the situation that does not contain diesel oil part, decompression diesel oil part, to operate from the tower bottom discharge.And diesel oil part, decompression diesel oil partly are that the mode of taking out on the production line of above-mentioned distilled oil 11 is carried out the operation of crude distillation separation circuit.
As shown in Figure 1, contain in the distillation zone 10 of vacuum distillation apparatus 10 ' by in fact directly crude oil 2 being imported, the purpose of adjustment of the mixing oil that can finish adjustment, constitute as petroleum naphtha, kerosene, diesel oil and the decompression diesel oil of hydrotreatment district stock oil together and so on as the decompression residual oil of the stock oil of pyrolysis zone, owing to do not need each cut of petroleum naphtha, kerosene, diesel oil and decompression diesel oil is carried out fractionation by distillation, so can save large-scale atmospheric distillation plant in the past.
Separate the heavy oil content 15 (decompression residual oil (15)) that 10 bottom obtains from the distillation zone in fact by the crude distillation separation circuit that uses such distillation zone 10 and import thermo-cracking district 20, here heavy oil content 15 is separated into the thermo-cracking resultant 21 and the thermo-cracking Residual oil 25 (thermo-cracking operation) of lighting by thermo-cracking.
The thermo-cracking resultant 21 of lighting turns back to above-mentioned distillation zone 10, carries out underpressure distillation here and reclaims low boiling point component (thermo-cracking resultant fractionation by distillation operation) effectively.That is, at first in the present invention, first is characterised in that above-mentioned crude distillation separation circuit and thermo-cracking resultant fractionation by distillation operation are to carry out simultaneously in same distillation zone 10, and proper raw material oil is offered thermo-cracking district and hydrotreatment district.That is, form about the separation of distillation zone 10, from the distilled oil (gassiness body portion) of crude oil with the mixture of thermal cracking oil (gassiness body portion) from the distillation zone 10 cat head or be divided into a plurality of boiling spreads taking-ups (symbol 11).On the other hand, the mixture from the part of the distillation Residual oil of crude oil and cracking mink cell focus takes out and is supplied to as thermo-cracking raw material (15) at the bottom of the tower of distillation zone 10.Because the 1st such feature can be sought the simplification of operation and the densification of device.
In addition, because the present invention is so that heavy oil product becomes zero as purpose, so thermo-cracking district 20 does not contain in the thermo-cracking Residual oil 25 in the thermo-cracking operation under the condition that heavy oil divides to operate.
Even, in above-mentioned thermo-cracking district 20, generally be to make the thermo-cracking raw material preheating with tubular oven, can also carry out pre-cracking according to occasion, again it is carried out thermo-cracking with grooved (eureka (EUREKA), delay coking device) or mobile stratotype (flexible coker, stream are stopped the bed coker) reactor, generate.Separation is as the splitting gas of thermo-cracking resultant, cracked oil or as the pitch or the oil coke of residue.
In the thermo-cracking operation in the present invention, it is possible using known in the past various thermo-crackings district, but wherein, uses the thermo-cracking district of said eureka (EUREKA), is particularly preferred from the bonded viewpoint with the hydrotreatment operation in downstream.
Eureka technology, normally the thermo-cracking decompression residual oil is produced splitting gas, cracked oil and bituminous technology, its details are at " special public clear 57-15795 communique ", " firepower nuclear power generation " Vol.36, No.2, P151-P166 (1985), " the 17th refining Team Conference minutes of institute of Petroleum " P93-P102 (1992), " catalyzer in refining of petroleum and petrochemical industry (Catalysts in Petroleum Refining andPetrochemical Inclustries) 1995 " P293-P301 (nineteen ninety-five), disclosed among " refining of petroleum method (petroleum refinement プ ロ セ ス) " P202-P203 (institute of Petroleum's distribution in 1998) etc.The reaction system of eureka method adopts the semi-batch mode of combination cast pyrolyzer and tank reactor, can seek to have both reaction time distribute the hot melt property PRODUCTION OF PITCH of narrow homogeneous and the economy of technology.Reactor constitutes by 21 group, alternatively switches material feeding by automatic transfer valve with about 90 minutes cycle.In temperature of reaction is that 400～450 ℃, pressure are roughly under the condition of non-pressurized 30～70kPa G and turn round.Also to be blown into about 600～700 ℃ superheated vapour to the bottom of reactor in addition, thus cracked oil promptly is discharged to outside the reaction system, thereby suppress over-drastic cracking polycondensation.Therefore cracked oil compares with other thermal cracker, has the few feature of polycondensation molecule.When this polycondensation molecule was present in the stock oil, the desulfurization cracking hydrogenation reaction in downstream required more exacting terms.With with the present invention who is combined as feature of this hydrotreatment operation in, it is desirable to the generation method still less of these polycondensation molecules in the thermo-cracking operation.
In the 10 isolating distilled oils 11 of distillation zone, contain decompression diesel oil branch, diesel oil branch, kerosene branch, petroleum naphtha branch as previously mentioned, these not in accordance with regulations boiling spread separate but import together in the same hydrotreatment district 30, carry out desulfurization cracking hydrogenation reaction here together and handle.Contain unsaturated hydrocarbons in the thermal cracking oil that in the thermo-cracking operation, generates, quality instability under its intact situation, thus saturated in addition with hydrogen, the hydrotreatment of the stabilization of making it must be arranged.Therefore, when adopting the Residual oil of thermo-cracking to upgrade scheme by in the past technology, thermal cracking oil is distillated and is separated into each cut, with after each distilled oil from the petroleum naphtha of crude oil, kerosene, diesel oil, decompression diesel oil etc. mixes, generally is that each cut is carried out hydrofining respectively.Therefore, when the pressure of each hydrofining reaction portion that is conceived to distilled oil, do not carry out the occasion of Residual oil thermo-cracking, this pressure normally uprises like that to heavy from lightweight by the raw material oil fraction and sets.But, be attended by the occasion of the Residual oil thermo-cracking that the present invention touches upon, even its pressure is also set higherly for lightweight oil, so the hydrofining pressure of each cut has the tendency of equalization the processing from lightweight to the heavy oil content.Specifically, hydrofining pressure, in the occasion of not carrying out the Residual oil thermo-cracking, petroleum naphtha is that 500～3000kPaG, kerosene are that 1000～4000kPaG, diesel oil are that 4000～7000kPaG, decompression diesel oil are the scopes of 5000～7000kPaG, is that 5000kPaG, decompression diesel oil are 6000kPaG but typical petroleum naphtha and kerosene are 2000～3000kPaG, diesel oil.In contrast, follow the occasion of Residual oil thermo-cracking, the hydrofining pressure of each cut of petroleum naphtha, kerosene, diesel oil, decompression diesel oil is typically set the 6000kPaG of same level for.Therefore, in the refining scheme that has made up the Residual oil thermo-cracking, the certainty of carrying out hydrorefined technology respectively is few, carries out the technological rationality height of hydrotreatment together.Hydrotreatment together in the present invention is different from the technical background difference of not following Residual oil cracked occasion (for example, the spy opens flat 7-82573 communique etc.), can be described as distinctive technology in the Residual oil thermo-cracking scheme.
In addition, when the viewpoint of economy was said, in not following the refining scheme of residual cracked, the occasion of carrying out the hydrotreatment together of distilled oil was necessary the light crude that meets the heavy oil product needs is prepared processing especially.This occasion, in the investment of reclaiming rightly for new installation, the income that obtains from crude oil and product price difference as its former fund must be sufficient.But, crude oil and product price by the decision of market principle now, the occasion that such light crude is handled, the price difference of crude oil and product is little, not follow Residual oil cracked novel appts to stop economically be extremely difficult so make.On the other hand, follow the economy of the occasion of Residual oil thermo-cracking, improve owing to become the low price and the price difference between lightweight and the heavy oil product of the heavy crude of raw material, so can guarantee the former fund that the novel appts investment is reclaimed.
Hydrotreatment together among the present invention, different with the general technology that will carry out hydrotreatment from the distilled oil of crude oil together, aspect the synthesization of afterheat cracked, can see its technology and economic meaning and feature place thereof.
Do not have special restriction for reaction formation, for example, can take various forms such as fixed bed, fluidized-bed, moving-bed.And in hydrotreatment district 30, the component that there is no need to handle is removed from the process object constituent together.
The treated oil 31 that carries out desulfurization cracking hydrotreatment by hydrotreatment district 30 together is low-sulfurs and is the synthetic crude that does not contain the high additive value of decompression residual oil cut, can adopt the refining scheme of conventional art to handle in the downstream.
Among the present invention, except the 1st above-mentioned feature, the distilled oil 11 that also contains the refining thing after thermo-cracking is handled is carried out desulfurization cracking hydrotreatment together, after managing herein simultaneously, by carrying out the fractionation by distillation operation uniformly, can further seek the simplification of whole technology and the reduction of processing cost.
And, the thermo-cracking resultant 21 of lighting, its part does not turn back to distillation zone 10 and might deliver to hydrotreatment district 30.
More than be based on Fig. 1 and Fig. 2 and understand technological process of the present invention in detail, but conduct as mentioned above, the suitable variation of part also can be to constitute the distillation zone 10 that imports crude oil 2 like that to contain pre-separate device and main tripping device.This occasion, as pre-separate device, specifiable have flash drum, a simple and easy distillation tower etc., as main tripping device is adducible vacuum distillation apparatus arranged.By default pre-separate device, part decompression diesel oil also can be separated, so can produce the advantage that reduces process furnace, vacuum still size and so on.
Flash drum is than the preferred mode of distillation tower in pre-separate device.Its reason is, the hydrotreatment district 30 in downstream takes to handle together, and the lock out operation that it is above not only can not satisfy technical requirement, and economically neither be best.
Specific embodiment is shown below, so that illustrate in greater detail the present invention.
Experimental example 1
Embodiment 1
Based on technological process of the present invention shown in Figure 1, carry out the refining of crude oil by following main points and handle experiment.The kind and the rerum natura of the crude oil that uses
The crude oil that uses: Arabic heavy crude (100Vol%)
Proportion: 0.896, the operating condition of sulphur concentration: 3.07wt% in steaming district 10
Pressure: 1～10kPa
Temperature: 350～400 ℃ of operating conditions at thermo-cracking district 20 (eureka)
Pressure: 30～60kPaG
425～440 ℃ of operating conditions of temperature in hydrotreatment district 30
Chemistry hydrogen consumption: 55～60Nm
3/ kl
Reaction tower temperature: 340～380 ℃
Hydrogen dividing potential drop: the operating condition in 6000kPa fractionation by distillation district 40
Pressure: 60～100kPaG
Temperature: 330～360 ℃
The yield of the product that obtains under such operating condition and the quality of product are shown in respectively in following table 1 and the table 2.
Table 1 product yield
Raw produce
Arabic heavy crude-
Petroleum naphtha (Vol%) 19 23
Kerosene (Vol%) 9 10
Diesel oil (Vol%) 21 26
Decompression diesel oil (Vol%) 26 36
Decompression residual oil (Vol%) 26-
Oil adds up to (Vol%) 100 96
Pitch (wt%)-8
Table 2 quality product
Raw produce
Arabic heavy crude-
Petroleum naphtha
Proportion (-) 0.722 0.726
Sulphur containing ratio (wt%) 0.02 0.001
Kerosene
Proportion (-) 0.800 0.796
Sulphur containing ratio (wt%) 0.30 0.01
Smoke point (mm) 26 22
Diesel oil
Proportion (-) 0.856 0.847
Sulphur containing ratio (wt%) 1.54 0.05
Cetane index (-) 51 54
Decompression diesel oil
Proportion (-) 0.941 0.925
Sulphur containing ratio (wt%) 3.40 0.63
Decompression residual oil
Proportion (-) 1.053-
Sulphur containing ratio (wt%) 6.00-
Metal alkane containing ratio (wtppm) 300-
Product yield shown in the above-mentioned table and quality confirmed with employing shown in Figure 3 in the past these indexs of the product cut (diesel oil sulphur containing ratio is that 500wtppm is following) that obtains of processing method are identical levels.In addition, the factory construction expense can be confirmed can reduce 15% than in the past technology.This shows, adopt processing method of the present invention under the situation that does not reduce product yield and quality product, can seek the simplification and the saving space of technological process, so can confirm to seek the reduction of processing cost.
Embodiment 2
In the foregoing description 1, except doing the following change at the operating condition in hydrotreatment district 30, the refining of other and the foregoing description 1 same operation carrying out crude oil of embodiment 2 is handled.The operating condition in hydrotreatment district 30
Chemistry hydrogen consumption: 60～70Nm
3/ kl
Reaction tower temperature: 340～380 ℃
Hydrogen dividing potential drop: 6000kPa
Reactor volume: make 2 times of volumetrical that become the foregoing description 1
The yield of the product that obtains under such operating condition and the weight of product are shown in respectively in following table 3 and the table 4.
Table 3 product yield
Raw produce
Arabic heavy crude-
Petroleum naphtha (Vol%) 19 23
Kerosene (Vol%) 9 10
Diesel oil (Vol%) 21 23
Decompression diesel oil (Vol%) 26 39
Decompression residual oil (Vol%) 26-
Oil adds up to (Vol%) 100 96
Pitch (wt%)-8
Table 4 product weight
Raw produce
Arabic heavy crude-petroleum naphtha
Proportion (-) 0.722 0.726
Sulphur containing ratio (wt%) 0.02 0.0005 kerosene
Proportion (-) 0.800 0.796
Sulphur containing ratio (wt%) 0.30 0.001
Smoke point (mm) 26 22 diesel oil
Proportion (-) 0.856 0.843
Sulphur containing ratio (wt%) 1.54 0.004
Cetane index (-) 51 56 decompression diesel oil
Proportion (-) 0.941 0.919
Sulphur containing ratio (wt%) 3.4 0.24 decompression residual oils
Proportion (-) 1.053-
Sulphur containing ratio (wt%) 6.00-
Metal alkane containing ratio (wtppm) 300-
These indexs that can confirm the product cut (diesel oil sulphur containing ratio is that 50wtppm is following) that the product yield shown in the above-mentioned table and quality and employing technical process in the past shown in Figure 3 obtains are identical levels.Can confirm that also the comparable technical process in the past of factory construction expense reduces by 15%.Therefore can confirm, can under the prerequisite that the weight that does not make product yield and product descends, seek the simplification of technical process and save the space with technology of the present invention, and can seek the reduction of processing cost.
From above result as seen, effect of the present invention is tangible.Promptly, the present invention has the crude distillation separation circuit that crude distillation is separated into distilled oil and heavy oil content, with will separate the thermo-cracking operation that the heavy oil content thermo-cracking that obtains from the bottom is in fact carried out lighting by this crude distillation separation circuit, treatment process with the crude oil of the thermo-cracking resultant fractionation by distillation operation that will carry out fractionation by distillation by the thermo-cracking resultant that this thermo-cracking operation lighting obtains, it is characterized in that, with aforementioned crude distillation separation circuit and thermo-cracking resultant fractionation by distillation operation, the mode of carrying out simultaneously in the distillation zone that is made of vacuum distillation apparatus constitutes, and, by crude distillation separation circuit and the isolating distilled oil of thermo-cracking resultant fractionation by distillation operation that carries out simultaneously in above-mentioned distillation zone, carry out desulfurization cracking hydrotreatment together in same hydrotreatment district, can produce low-sulfur and not contain the high synthetic crude of value added of decompression residual oil cut, then, the refining scheme of the conventional art that adopts in the downstream is processed, so can seek the simplification of technical process and save the space, and can seek the reduction of processing cost, in addition, can also adapt to requirement for small-sized petroleum refinement.
Industrial applicibility
Crude Treatment method of the present invention can be used as, and particularly, is using the crude oil production height In the petroleum refining of the oil product of surcharge, the heavy oil content that contains in the crude oil is changed into Light ends, the method that so-called mink cell focus is upgrade.
Claims (6)
1. the treatment process of a crude oil, this method is the treatment process with crude oil of following operation:
With crude distillation be separated into distilled oil and heavy oil content the crude distillation separation circuit and
Will by this crude distillation separation circuit separate that the heavy oil content that obtains from the bottom in fact carry out thermo-cracking and the thermo-cracking operation of lighting and
The thermo-cracking resultant fractionation by distillation operation of the thermo-cracking resultant fractionation by distillation that will obtain by this thermo-cracking operation lighting,
It is characterized in that, carry out above-mentioned crude distillation separation circuit and thermo-cracking resultant fractionation by distillation operation in the distillation zone that constitutes by vacuum distillation apparatus simultaneously.
2. according to the treatment process of the described crude oil of claim 1, it is characterized in that, carry out the distillation zone of above-mentioned crude distillation separation circuit and thermo-cracking resultant fractionation by distillation operation simultaneously, contain pre-separate device and main tripping device.
3. according to the treatment process of the described crude oil of claim 1, it is characterized in that, with respect to distilled oil 100 weight parts of distillation zone, make by above-mentioned distillation zone and separate the heavy oil content of discharging from the bottom, is 15～55 weight parts.
4. according to the treatment process of the described crude oil of claim 1, it is characterized in that, separate from the bottom by above-mentioned crude distillation separation circuit and discharge, and supply in the heavy oil content of thermo-cracking operation, do not contain diesel oil branch, decompression diesel oil branch in fact.
5. according to the treatment process of the described crude oil of claim 1, it is characterized in that, do not contain the heavy oil branch in the thermo-cracking Residual oil in the above-mentioned thermo-cracking operation.
6. according to the treatment process of the described crude oil of claim 1, it is characterized in that, crude distillation separation circuit and the isolating distilled oil of thermo-cracking resultant fractionation by distillation operation by carrying out simultaneously in above-mentioned distillation zone carry out desulfurization cracking hydrotreatment together in same hydrotreatment district.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13548199 | 1999-05-17 | ||
| JP135481/99 | 1999-05-17 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1351643A true CN1351643A (en) | 2002-05-29 |
| CN100419046C CN100419046C (en) | 2008-09-17 |
Family
ID=15152735
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB008076979A Expired - Fee Related CN100419046C (en) | 1999-05-17 | 2000-05-16 | Process for treating crude oil |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP1199347B1 (en) |
| JP (1) | JP4564176B2 (en) |
| CN (1) | CN100419046C (en) |
| DE (1) | DE60016755T2 (en) |
| WO (1) | WO2000069992A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100441666C (en) * | 2006-09-01 | 2008-12-10 | 周斌 | Method of obtaining high quality biologic diesel oil |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100933308B1 (en) * | 2009-03-17 | 2009-12-22 | 재원산업 주식회사 | Apparatus for refining of opportunity crude and method for refining |
| CN101962568A (en) * | 2010-10-19 | 2011-02-02 | 中海沥青股份有限公司 | Wax-reducing method for producing petroleum asphalt |
| RU2490307C1 (en) * | 2012-10-01 | 2013-08-20 | Андрей Владиславович Курочкин | Oil processing method |
| RU2495084C1 (en) * | 2012-11-27 | 2013-10-10 | Андрей Владиславович Курочкин | Oil refining method |
| RU2515938C1 (en) * | 2013-04-24 | 2014-05-20 | Андрей Владиславович Курочкин | Oil refining method |
| RU2707188C2 (en) * | 2016-03-17 | 2019-11-25 | Андрей Владиславович Курочкин | Run-down distillation plant |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB748427A (en) * | 1953-09-10 | 1956-05-02 | Exxon Research Engineering Co | A combination process for fractionating, cracking and coking petroleum hydrocarbons |
| US3487006A (en) * | 1968-03-21 | 1969-12-30 | Lummus Co | Direct pyrolysis of non-condensed gas oil fraction |
| EP0050030B1 (en) * | 1980-10-13 | 1985-01-09 | Peter Spencer | Reactor for the thermal cracking of heavy hydrocarbons and a process and apparatus for the distillation and thermal cracking of a crude oil feedstock using such a reactor |
| FR2504936B1 (en) * | 1981-04-29 | 1985-08-09 | Raffinage Cie Francaise | PROCESS FOR OBTAINING SYNTHETIC CRUDE OIL |
| GB2108997B (en) * | 1981-11-03 | 1985-08-07 | Peter Spencer | Process and apparatus for thermal cracking and fractionation of hydrocarbons |
| US4454023A (en) * | 1983-03-23 | 1984-06-12 | Alberta Oil Sands Technology & Research Authority | Process for upgrading a heavy viscous hydrocarbon |
| AU4944196A (en) * | 1995-03-02 | 1996-09-18 | Shell Internationale Research Maatschappij B.V. | Process for the conversion of a hydrocarbon oil |
-
2000
- 2000-05-16 EP EP00925681A patent/EP1199347B1/en not_active Expired - Lifetime
- 2000-05-16 WO PCT/JP2000/003125 patent/WO2000069992A1/en active IP Right Grant
- 2000-05-16 DE DE60016755T patent/DE60016755T2/en not_active Expired - Lifetime
- 2000-05-16 CN CNB008076979A patent/CN100419046C/en not_active Expired - Fee Related
- 2000-05-16 JP JP2000618400A patent/JP4564176B2/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100441666C (en) * | 2006-09-01 | 2008-12-10 | 周斌 | Method of obtaining high quality biologic diesel oil |
Also Published As
| Publication number | Publication date |
|---|---|
| JP4564176B2 (en) | 2010-10-20 |
| DE60016755D1 (en) | 2005-01-20 |
| CN100419046C (en) | 2008-09-17 |
| DE60016755T2 (en) | 2005-12-01 |
| EP1199347A1 (en) | 2002-04-24 |
| WO2000069992A1 (en) | 2000-11-23 |
| EP1199347A4 (en) | 2003-05-02 |
| EP1199347B1 (en) | 2004-12-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1037112C (en) | Method for producing feedstocks of high quality lube base oil from unconverted oil of fuels hydrocracker operating in recycle mode | |
| US6726832B1 (en) | Multiple stage catalyst bed hydrocracking with interstage feeds | |
| CN101068908A (en) | Process for the conversion of heavy charges such as heavy crude oils and distillation residues | |
| CN1398953A (en) | Converting process of heavy material, such as heavy raw oil and distilled residue | |
| CN1324116C (en) | Method for catalytic conversion of heavy oil and device thereof | |
| CN101054534A (en) | Process and installation for conversion of heavy petroleum fractions in a boiling bed with integrated production of middle distillates with a very low sulfur content | |
| CN1484684A (en) | Method for hydrotreatment of heavy hydrocarbon fraction with switchable reactors and reactors capable of being shorted out | |
| RU2495086C2 (en) | Selective recycling of heavy gasoil for purpose of optimal integration of heavy crude oil and vacuum gas oil refining | |
| CN1487989A (en) | Method of refining petroleum | |
| TW201516138A (en) | Process for producing marine fuels with low sulphur content from a hydrocarbon-containing cut originating from catalytic cracking of the HCO or slurry type, and employing a hydrotreating stage | |
| CN105567314A (en) | Process for converting petroleum feedstocks for producing fuel oil with low content of sediments | |
| CN1729275A (en) | Process for the conversion of heavy feedstocks such as heavy crude oils and distillation residues | |
| CN1212993A (en) | Petroleum processing method and apparatus | |
| CN1248610A (en) | Method for hydrotreating crude oil and crude oil reformed by the method | |
| CN107557064B (en) | Coal tar combined bed hydrogenation method and system for coal tar combined bed hydrogenation | |
| CN1351643A (en) | Process for treating crude oil | |
| CN104277879A (en) | Two-stage slurry bed hydrogenation process of medium and low temperature coal tar | |
| EP0067020A2 (en) | Hydrostripping process of crude oil | |
| CN1483069A (en) | Method of desulfurizing gas oil fraction, desulfurized gas oil, and desulfurizer for gas oil fraction | |
| CN1195829C (en) | Poor heavy and residual oil weight-lightening process | |
| CN1621495A (en) | Hydrogenation modification process for low grade gasoline | |
| CN1132912C (en) | Suspension bed hydrogenation process for refining heavy and residual oil mixed with waste oil | |
| CN1425053A (en) | Process for the desulfurization of petroleum feeds | |
| CN1649986A (en) | Improved hydrocracking process | |
| RU2671816C1 (en) | Installation for hydroprocessing of residual oil fractions |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080917 Termination date: 20160516 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |