CN101760241A - Corrosion-resistant processing method of crude oil with high acid content - Google Patents

Corrosion-resistant processing method of crude oil with high acid content Download PDF

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CN101760241A
CN101760241A CN200910244465A CN200910244465A CN101760241A CN 101760241 A CN101760241 A CN 101760241A CN 200910244465 A CN200910244465 A CN 200910244465A CN 200910244465 A CN200910244465 A CN 200910244465A CN 101760241 A CN101760241 A CN 101760241A
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tower
millimeter
hydrocracking
distillate
oil
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CN101760241B (en
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吴青
郑明光
夏长平
孙亮
王旭
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China National Offshore Oil Corp CNOOC
CNOOC Research Institute of Refining and Petrochemicals Beijing Co Ltd
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Abstract

The invention provides a corrosion-resistant processing method of crude oil with high acid content, wherein the method comprises the following steps: (1) cutting the crude oil with high acid content to obtain oil of multiple distillates; (2) detecting the acid values of oil of each distillate; and (3) determining materials of equipment used in the processing process of the crude oil with high acid content according to the acid values. The corrosion-resistant processing method of the crude oil with high acid content provided by the invention fully considers the properties of the crude oil, reasonably cuts the crude oil, and adopts the reasonable secondary processing method on the oil of each distillate, so the whole process has low energy consumption and good economical efficiency. Particularly, through selecting materials with different corrosion-resistant effects for different positions (selecting materials with high corrosion-resistant performance for positions with high corrosion-resistant requirements, and selecting materials with low corrosion-resistant performance or conventional materials for positions with low corrosion-resistant requirements), the invention can reach the goals of meeting the requirements of the production process and the equipment service life and reducing the equipment cost.

Description

A kind of corrosion-resistant processing method of crude oil with high acid content
Technical field
The invention relates to a kind of corrosion-resistant processing method of crude oil with high acid content.
Background technology
Crude oil is a kind of very complicated mixture, and it is mainly formed is hydro carbons, also contains compound and trace metal organic compound such as sulphur, nitrogen, oxygen.The crude oil of different field produces is often formed and different in kind.Even same oil field, because producing horizon position difference, oil property difference also may be very big.With the Daqing oil field is representative, and most of oil field of exploitation all belongs to the low-sulfur waxy crude oil before China.Technology such as distillation, hot-work such as delayed coking, catalytic cracking, catalytic reforming, hydrofining and hydrocracking are generally adopted in the processing of crude oil.Crude oil is cut into various cuts such as gasoline, solvent oil, rocket engine fuel, solar oil, heavy gas oil and various decompression side line distillates by distillation.
Atmospheric and vacuum distillation is a method commonly used in the crude oil processing, first procedure in the crude oil processing normally, and it utilizes the distillatory principle that crude separation is become the cut of various different boiling, obtains the raw material of various oil products and downstream machining cell.The quality of device and atmospheric and vacuum distillation design and operation all has a significant impact to the quality product of refinery, yield and to effective utilization of crude oil.
Device and atmospheric and vacuum distillation generally comprise successively the electrical desalter that connects, flashing tower, atmospheric pressure kiln, atmospheric tower, atmospheric stripping tower, decompression process furnace, vacuum distillation tower, decompression stripping tower, with return tank of top of the tower and interchanger, air cooler and water cooler that atmospheric tower is connected with the vacuum distillation tower cat head, generally connect between these equipment by pipeline.
The oil hydrogen addition technology is the important means of refining of petroleum products, upgrading and heavy oil upgrading, mainly comprises hydrofining and hydrocracking.Hydrocracking equipment is the important secondary processing means of refinery, can obtain high-quality light-weight fuel oil, be characterized in strong to adaptability to raw material, can process straight run heavy gas oil, catalytic cracking turning oil, coker distillate, even can produce gasoline, boat coal and low freezing point diesel fuel, secondly with the diasphaltene heavy residual stocks, production decision is flexible, can change production decision according to different seasons, and good product quality, the product yield height.
Hydrocracking process can be divided into high-pressure hydrocracking and middle pressure hydrocracking according to reaction pressure, depends mainly on the quality, depth of conversion and the requirement of purpose quality product that are processed raw material.When processing is light, the less raw material of impurity, control depth of conversion simultaneously again when low, generally all adopt middle pressure hydrocracking technology.The raw material of middle pressure hydrocracking equipment is the normal pressure coal diesel oil of 170-365 ℃ of cut scope and the mixing raw material of catalytic diesel oil, and product comprises liquefied gas, petroleum naphtha, boat coal, diesel oil etc.The raw material of high-pressure hydrocracking equipment is generally the second line of distillation wax oil of atmospheric and vacuum distillation unit and subtracts three-way wax oil and coker wax oil, and product comprises hydrogenation tail oil, diesel oil, boat coal and weight petroleum naphtha.
Catalytic cracking generally is used to produce products such as stop bracket gasoline, diesel oil and liquefied gas, and its raw material sources are wider, can be used to process fresh distillate, also can be used to process recycle stock.Catalytic reforming is the main processes from oil production aromatic hydrocarbons and high octane gasoline component, and its stock oil is done and generally is no more than 180 ℃, is generally the crude oil virgin oil.
Delayed coking generally is used to process heavy oil residue, is mink cell focus or residual oil are converted into the course of processing of gas and lightweight oil, intermediate oil and coke through degree of depth thermally splitting, polymerization, and be the main means that refinery improves yield of light oil and produces refinery coke.
Delayed coking method comprises coking and decoking, and coking is operate continuously, and decoking is that two towers replace the discontinuous operation.The typical delays coking process comprises that stock oil is after the process furnace heating, make oil product short period of time in process furnace reach the needed temperature of pyrogenic reaction by high flow velocity (water filling in boiler tube) and high hot strength (500 ℃ of furnace outlet temperature), pass through separation column then rapidly, fractionate out gas, gasoline, behind diesel oil and the distilled oil, bottom product enters the convection zone of coking heater earlier through the overshoot inlet line, after the convection zone heating, enter the radiation section of process furnace, enter coke drum at the bottom of the tower of coke drum fast through outlet line again and carry out coking, reaction is not deferred at process furnace to be carried out in the coke drum, the coke that obtains is discharged at the bottom of tower, and light component is discharged from cat head and entered separation column.
Although the complete processing to the low-sulfur waxy crude oil is very ripe at present, yet along with the exhaustion of high-quality low-sulfur waxy crude oil, exploiting and utilizing acid-containing raw oil inferior has been trend of the times.Because acid-containing raw oil character is relatively poor, its working method is inevitable different with the low wax sulphur-bearing crude of high-quality, for example, the device and atmospheric and vacuum distillation of above-mentioned processing low-sulfur waxy crude oil and delayed coking unit generally adopt carbon steel to make, and the material of hydroeracking unit is generally the chromemolybdenum steel with TP347H overlay cladding.Aforesaid device generally can both meet the demands for the processing of the crude oil of conventional acidity, but, when using such apparatus processing crude oil with high acid content, for example during the high-acid crude oil of Peng Lai, can not satisfy erosion-resisting requirement, service life of equipment is low, and quality product is affected because of equipment corrosion, has increased the cost of subsequent disposal.Therefore how economical, reasonably to utilize acid-containing raw oil be the present technical issues that need to address.
Summary of the invention
The objective of the invention is for a kind of corrosion-resistant processing method that can process crude oil with high acid content economically and reasonably is provided.
The corrosion-resistant processing method of crude oil with high acid content provided by the invention may further comprise the steps: cut described crude oil with high acid content (1), obtains a plurality of distillates; (2) measure the acid number of each distillate; (3) determine the material of equipment used in the treating processes of described crude oil with high acid content according to above-mentioned acid number.
The corrosion-resistant processing method of crude oil with high acid content provided by the invention takes into full account its oil property, crude oil has been carried out rational cutting and each distillate has been adopted rational secondary processing method, thereby made that the energy consumption of whole technology is lower, better economy.The particularly preferred various device of the application of the invention and work-ing life of having improved a whole set of system of processing greatly, thus improve production efficiency and improved quality product.And by material (the high corrosion location selection high corrosion resistance material of selecting to have different erosion resistancies at different sites, low corrosion location is selected low corrosion resistant material or conventional material), the requirement of both having satisfied production technique and equipment life can be reached, the purpose of equipment cost can be reduced again.
Description of drawings
Fig. 1 is the process flow sheet of the corrosion-resistant processing method of Peng Lai crude oil.
Embodiment
For the purpose of simplifying the description, only unlike the prior art place is described below.For the content of part same as the prior art, the descriptions thereof are omitted or only it is simply described.
The described method that described crude oil with high acid content is cut can be the conventional various cutting methods of using in this area, for example method of atmospheric and vacuum distillation.Cut point can cut according to the requirement or the product requirement of following process, for example, and can be according to the method cutting that crude oil is cut into gasoline fraction, rocket engine fuel cut, diesel oil distillate, lubricating oil distillate, catalytically cracked material cut and residual oil.
Among the present invention, described crude oil with high acid content can be the higher crude oil of the acid number in various sources, and the acid number that for example can be various sources is the crude oil of 3-5mgKOH/g, for example can be Peng Lai, Bohai Sea crude oil.The API of this crude oil is 20-25, and sulphur content is 0.3-0.5 weight %, and acid number is 3-4mgKOH/g.Above-mentioned Peng Lai crude oil is a kind of crude oil with high acid content, belongs to low-sulfur cycloalkanes intermediate base crude oil, and the acid number height is therefore serious to the naphthenic acid corrosion that wherein used various device such as device and atmospheric and vacuum distillation cause.
Although all take rotproofing also can reach the rot-resistant effect to the equipment and the pipeline that relate in the whole complete processing,, obviously this can increase cost undoubtedly greatly for example increases equipment cost or reduces productivity.In order not only to reach the rot-resistant purpose but also equipment cost is increased too much, the present inventor creatively finds, distribute to determine in the whole complete processing of described crude oil with high acid content that thereby which step or equipment or its position needs take anti-acid corrosion targetedly technology or the more serious part of equipment corrosion to be taked rotproofing according to acid number, then adopt conventional treatment method to address the above problem other not serious parts of corrosion.
For this reason, the present inventor is an example with Peng Lai PL19-3 crude oil, a large amount of research has been carried out in the anticorrosion processing of crude oil with high acid content, thereby finished the present invention.
Above-mentioned Peng Lai crude oil is a kind of crude oil with high acid content, the API of this crude oil is 20-25, sulphur content is 0.3-0.5 weight %, acid number is 3-4mgKOH/g, have stronger high temperature corrosion, corrosion product is dissolved in oil, and it is bigger influenced by the velocity of medium fluidised form, etch state is and washes away type corrosion, and the corrosion failure that is caused has bigger danger.The representative data of the physico-chemical property of PL19-3 crude oil is listed in the table below 1.165-360 ℃ cut oil properties is listed in the table below 2.
Table 1
Project Analytical results Project Analytical results
Density (20 ℃)/gcm -3 ??0.9212 The crude oil boiling range
The API degree ??21.5 Initial boiling point/℃ ??123
Viscosity/mm 2·s -1 140 ℃ of quantity of distillate/volume % ??0.5
??50℃ ??72.44 160 ℃ of quantity of distillate/volume % ??2.1
??80℃ ??21.10 180 ℃ of quantity of distillate/volume % ??4.3
??100℃ ??12.71 200 ℃ of quantity of distillate/volume % ??5.9
Condensation point/℃ ??＜-35 220 ℃ of quantity of distillate/volume % ??7.5
Moisture/weight % ??0.25 240 ℃ of quantity of distillate/volume % ??10.7
Acid number/mgKOHg -1 ??3.20 260 ℃ of quantity of distillate/volume % ??13.9
Wax content/weight % ??4.75 280 ℃ of quantity of distillate/volume % ??17.1
Carbon residue/weight % ??5.62 300 ℃ of quantity of distillate/volume % ??21.9
Project Analytical results Project Analytical results
Ash content/weight % ??0.022 Metal analysis/μ gg -1
Sulphur/weight % ??0.31 Iron ??9.50
Nitrogen/weight % ??0.39 Nickel ??26.11
Throw out/weight % ??0 Copper ??0.69
Net thermal value/kJkg -1 ??41490 Vanadium ??2.25
Salt/gm -3 ??45.4 Plumbous ??＜0.01
Colloid/weight % ??16.98 Sodium ??1.87
Bituminous matter/weight % ??0.56 Calcium ??35.38
The crude oil classification Low-sulfur cycloalkanes intermediate base Magnesium ??14.96
Table 2
Boiling spread/℃ ??165～360
Yield, % ??24.52
Density (20 ℃)/gcm -3 ??0.8719
Kinematic viscosity (20 ℃)/mm 2·s -1 ??5.569
Condensation point/℃ ??＜-35
Acid number/mgKOH (100mL) -1 ??272.20
Sulphur content, % ??0.14
Flash-point (remaining silent)/℃ ??82
Copper corrosion/level ??2
Existent gum/mg (100mL) -1 ??65
Boiling spread/℃ ??165～360
Cetane value ??38.0
The cetane value index ??41.2
Boiling range/℃
Initial boiling point ??199.3
10 volume % ??226.1
30 volume % ??251.9
50 volume % ??274.7
70 volume % ??296.1
90 volume % ??318.8
95 volume % ??326.8
Final boiling point ??330.6
Yield, volume % ??97.5
The cut hydrocarbon composition, weight %
Paraffinic hydrocarbons ??20.1
One ring cycloalkanes ??11.7
Bicyclic ring alkane ??28.8
Tricyclic naphthenes ??9.4
Total cycloalkanes ??49.9
Total stable hydrocarbon ??70.0
Alkylbenzene ??7.3
Boiling spread/℃ ??165～360
Indane or tetrahydronaphthalene ??6.2
The indenes class ??3.8
Total mononuclear aromatics ??17.3
Naphthalene ??0.7
The naphthalene class ??6.4
The acenaphthene class ??2.4
The acenaphthylene class ??2.3
Total double ring arene ??11.8
Thrcylic aromatic hydrocarbon ??0.9
Total aromatic hydrocarbons ??30.0
Gross weight ??100.0
By further discovering, in the above-mentioned crude oil with high acid content,＜180 ℃ of acidity with＜200 ℃ of gasoline fractions are respectively 15.05mgKOH/100mL and 20.07mgKOH/100mL, and sulphur content is respectively 191.30 μ gg -1With 278.58 μ gg -1, nitrogen content is respectively 1.95 μ gg -1With 2.69 μ gg -1, copper corrosion is 1 grade;
The 130-240 ℃ of acidity with 180-280 ℃ of crude oil rocket engine fuel cut is respectively 61.46mgKOH/g and 112.90mgKOH/g, and sulphur content is respectively 502.41 μ gg -1With 3417.82 μ gg -1, nitrogen content is respectively 6.26 μ gg -1With 24.73 μ gg -1, copper corrosion is respectively 1 grade and 2 grades, and silver slice corrosion is 4 grades;
The 180-350 ℃ of acidity with 200-350 ℃ of diesel oil distillate is big, is respectively 272.20mgKOH/100mL, 203.21mgKOH/100mL, and sulphur content is respectively 0.14 weight %, 0.15 weight %, and copper corrosion is respectively 2 grades, 1 grade;
The acid number height of 350-400 ℃, 400-450 ℃ and 450-500 ℃ of lubricating oil distillate is respectively 4.28mgKOH/g, 3.48mgKOH/g, 3.48mgKOH/g;
The acid number height of 350-560 ℃ of catalytically cracked material is 3.48mgKOH/g, and sulphur content is 0.29 weight %, and nitrogen content is 0.23 weight %, and iron, nickel and content of vanadium are low, is respectively 0.54 μ g/g, 0.50 μ g/g and 0.03 μ g/g;
The sulphur content of＞350 ℃ of heavy oil is 0.36 weight %, and the nitrogen content height is 0.58 weight %, and heavy metal nickel, magnesium and calcium contents height are respectively 35.71 μ g/g, 20.64 μ g/g and 47.81 μ g/g;
The sulphur content of＞560 ℃ of residual oil is 0.49 weight %, and the nitrogen content height is 0.86 weight %, and metallic iron, nickel, magnesium and calcium contents height are respectively 38.92 μ g/g, 79.0 μ g/g, 43.61 μ g/g and 92.48 μ g/g.
Distribute according to above-mentioned acid number, the present inventor selects the material at each position of device and atmospheric and vacuum distillation, hydrocracking equipment and delayed coking equipment targetedly, provides a cover to be suitable for the crude oil with high acid content method for processing.
According to method provided by the invention, when the acid number of described crude oil with high acid content is 3-5mgKOH/g, the method of described cutting comprises carries out atmospheric and vacuum distillation with crude oil with high acid content, obtain the overhead gas component, boiling range be 30 ℃ to less than 165 ℃ first distillate, boiling range is 165-360 ℃ second distillate, boiling range is 360-450 ℃ the 3rd distillate, boiling range is 450-520 ℃ the 4th distillate, boiling range be 520-545 ℃ the 5th distillate and boiling range greater than 545 ℃ tower at the bottom of residual oil, the acid number of described first distillate is 10-20mgKOH/100mL, the acid number of described second distillate is 250-300mgKOH/100mL, boiling range is that the acid number of the distillate of 360-400 ℃ distillate and 400-450 ℃ is respectively 3.5-4.5mgKOH/g in described the 3rd distillate, 3-4mgKOH/g, described boiling range is that the acid number of the 4th distillate is 3-5mgKOH/g, the acid number of described the 5th distillate is 3-5mgKOH/g, the acid number of residual oil is 1-3mgKOH/g at the bottom of the described tower, described first distillate is carried out catalytic reforming under the catalytic reforming condition, distillate A or distillate B contacted with hydrocracking catalyst under hydrocracking condition carry out hydrocracking, described distillate A is described second distillate and the 3rd distillate, described distillate B is described second distillate and the 3rd distillate and to small part the 4th distillate, with described the 5th distillate or described the 5th distillate and at least remainder the 4th distillate under catalytic cracking condition, carry out catalytic cracking, residual oil at the bottom of the described tower is carried out delayed coking.
The device and atmospheric and vacuum distillation that wherein is used for atmospheric and vacuum distillation comprises atmospheric tower, atmospheric pressure kiln to the atmospheric tower heat supply, vacuum distillation tower and to the vacuum furnace of vacuum distillation tower heat supply, described atmospheric tower and vacuum distillation tower comprise tower body separately, tower tray and filler, the number of plies of the tower tray of described atmospheric tower is more than 40, described atmospheric pressure kiln and vacuum furnace comprise convection tubes and radiator tube separately, wherein, described atmospheric tower be Monel (Monel) alloy in the 40th layer of tower tray to the material of the tower body between the cat head, 0Cr13,316L, SAF2205, the metal composite of one or more among SAF2507 and the SAF2304 and carbon steel, the material of tower tray are 0Cr13,316L, SAF2205, among SAF2507 and the SAF2304 one or more; Material to the tower body between the 40th layer of tower tray at the bottom of the tower of described atmospheric tower is the metal composite of 316L and carbon steel, and the material of 28-39 layer tower tray is the 0Cr13 material, and the material of 1-28 layer tower tray is 316L; The material of the tower body of described vacuum distillation tower is the metal composite of 316L and carbon steel, and the material of the 2 layers of filler in top of described vacuum distillation tower is the 316L material, and the material of other filler is 317L; The material of the convection tubes of described atmospheric pressure kiln is the 316L material, and the material of radiator tube is the 316L material; The material of the convection tubes of described vacuum furnace is the 316L material, and the material of the radiator tube of described vacuum furnace is the 316L material.
According to device and atmospheric and vacuum distillation provided by the invention, described atmospheric tower comprises for example 40-60 layer tower tray.Among the present invention, unless stated otherwise, what layer tower tray be meant from the bottom of the tower to how many layers of the direction of cat head.For example, suppose that atmospheric tower has 44 layers of tower tray, then the first layer tower tray is near that one deck at the bottom of the tower, and the 44th layer is that one deck near cat head.
The method for preparing metal composite has a lot, the method of the method for Tu Fuing, casting for example, among the present invention, described metal composite is preferably the metallic substance by the method acquisition of explosive welding, wherein carbon steel such as 16MnR are substrate layer, another kind of material is called composite bed, is also referred to as anticorrosion layer.For example in the metal composite of 316L and carbon steel, 316L is a composite bed.Wherein, the intensity that provides equipment required is provided substrate layer, therefore, the thickness of substrate layer can be the thickness of the material when not considering protection against corrosion in the conventional device and atmospheric and vacuum distillation, and general different position or positions is because of the pressure difference of bearing, needed intensity difference, therefore thickness is generally also different, but all has been conventionally known to one of skill in the art, and the present invention does not repeat them here.The main effect of composite bed is anticorrosion, therefore its material and thickness all depend primarily on the required anticorrosion rank that reaches, generally use the good material of antiseptic property at the serious position of acid corrosion, under the situation of same material, it is big that the thickness of the composite bed at the position that acid corrosion is serious is wanted.
In the described metal composite, the thickness of described anticorrosion layer is not particularly limited, usually, the thickness of anticorrosion layer is big more, and the anti-corrosion capability of this material and the equipment that made by this material is strong more, but the cost of corresponding material itself is also just high more.The present inventor discovers, under the situation of crude oil with high acid value of the present invention, the thickness of anticorrosion layer is not less than 3 millimeters and can effectively realizes anticorrosionly, guarantees that the life-span of this material reaches 15 years to 20 years.Consider in comprehensive cost and work-ing life, the 40th layer of tower tray of the preferred described atmospheric tower of the present invention one or more total thickness to anticorrosion layer Monel metal, 0Cr13,316L, SAF2205, SAF2507 and the SAF2304 of the tower body between the cat head is preferably the 3-5 millimeter, the thickness of the 316L of the tower body of the 40th layer of tower tray of described atmospheric tower between at the bottom of the tower is preferably the 3-5 millimeter, and the thickness of the 316L of the tower body of described vacuum distillation tower is preferably the 3-5 millimeter.And the 40th layer of tower tray of described atmospheric tower to the 40th layer of tower tray of the more described atmospheric tower of thickness of the composite bed of the tower body between the cat head to tower at the bottom of between the thickness of 316L of tower body little, and be not less than the thickness of composite bed of the tower body of described vacuum distillation tower.
Described vacuum distillation tower is preferably the 5-10 layer, and other filler is meant that the 2nd layer at top is to the filler between the rest layers tower tray.At the bottom of the 2nd layer at described top is meant from cat head to tower the 1st and the 2nd layer of direction.Further under the preferable case, the material of internals such as described distribution pipe and supporting beam is 316L.
According to device and atmospheric and vacuum distillation of the present invention, for the lightweight oil that crude oil has been gasified in the heat exchange temperature-rise period in time steams, make it not enter atmospheric pressure kiln and fall, thereby save unitary energy consumption and process cost with the thermal load of reduction process furnace and the working pressure of heat exchanger network system; In addition, also in order to make the atmospheric tower operation more stable, described device and atmospheric and vacuum distillation provided by the invention also comprises flashing tower.Described flashing tower comprises tower body, is positioned at the intravital tower tray of tower, and the number of plies of the preferred described tower tray of the present invention amounts to the 4-8 layer.Also has certain acid number owing to enter the product of flashing tower, therefore, for the work-ing life of further improving the subsequent technique catalyzer and the work-ing life of a whole set of device and atmospheric and vacuum distillation, the material of the tower body of described flashing tower is preferably the metal composite of 304L and carbon steel, and the material of tower tray is preferably 304 and/or 321.
By selecting the flashing tower of above-mentioned materials for use, can further reduce the iron concentration in the atmospheric and vacuum distillation product, thereby further improve the work-ing life of the catalyzer of following process, and effectively prevent the perforation of flashing tower, thereby further improve the work-ing life of a whole set of device and atmospheric and vacuum distillation.
The above-mentioned metal composite that is used for flashing tower preferably also obtains by the explosive welding connection, and wherein the thickness of 304L is preferably the 3-5 millimeter.
According to device and atmospheric and vacuum distillation of the present invention, wherein, described device and atmospheric and vacuum distillation also comprises atmospheric stripping tower and/or decompression stripping tower.There is the acid corrosion problem equally owing to enter the product of atmospheric stripping tower and decompression stripping tower, therefore, in order to guarantee the operation more steady in a long-term of a whole set of device and atmospheric and vacuum distillation, the present inventor also furthers investigate the material of the tower body of described atmospheric stripping tower and decompression stripping tower.Find that the material of the tower body of described atmospheric stripping tower and decompression stripping tower preferably is the metal composite of 316L and carbon steel, when the material of tower tray preferably is 316L, both can guarantee further to reduce the work-ing life of subsequent technique catalyzer, can also guarantee atmospheric stripping tower and/or decompression stripping tower and aforementioned preferred atmospheric tower, vacuum distillation tower, atmospheric pressure kiln and suitable substantially life-span of vacuum furnace, under the situation of 1200 tons/year amount of finish, be 15-20.
According to device and atmospheric and vacuum distillation of the present invention, wherein, the described metal composite that is used for atmospheric stripping tower and decompression stripping tower preferably also obtains by the explosive welding connection, and wherein the thickness of 316L is preferably the 3-5 millimeter.
Described device and atmospheric and vacuum distillation also comprises the air cooler of the cat head that is positioned at atmospheric tower and/or vacuum distillation tower usually; the present inventor also finds; in the atmospheric and vacuum distillation course of processing of above-mentioned crude oil with high acid content; high acid value in the described crude oil mainly is comparatively serious to the tube bank corrosion of air cooler to the work-ing life of the air cooler that carbon steel is made certain influence being arranged also.For the life-span that makes air cooler consistent with the work-ing life at other position of device and atmospheric and vacuum distillation, the material of the bobbin carriage of the preferred described air cooler of the present invention is a carbon steel, the material of the tube bank of described air cooler is preferably titanium, SAF2507 or Monel metal.So both can guarantee the work-ing life of corresponding raising air cooler, and can also only use the position of the good material of antiseptic property to use corresponding stage method for distinguishing material targetedly, thereby reduce the production cost of equipment needs.
Generally speaking, described device and atmospheric and vacuum distillation also comprises the charging side line interchanger that is communicated with the charging side line of atmospheric tower and/or vacuum distillation tower, because also there is certain influence in the acid in the crude oil to this charging side line interchanger, so the present invention has also carried out research and corresponding the improvement to the material of charging side line interchanger.Under the preferable case, the material of the housing of this charging side line interchanger, bobbin carriage, tube sheet is the metal composite of 316L and carbon steel, and the material of described tube bank is 316L and/or 304L.The described metal composite that is used for this charging side line interchanger preferably also obtains by the explosive welding connection, and wherein the thickness of 316L is the 3-5 millimeter.
In addition, described device and atmospheric and vacuum distillation also comprises and is used to make that vacuum residuum and crude oil carries out heat exchange subtracts the slag crude heat exchanger, the described slag crude heat exchanger that subtracts can be the various interchanger that are used for vacuum residuum and crude oil heat exchange in the prior art, the preferred described slag crude heat exchanger that subtracts of the present invention is the shell side interchanger, for convenience of description, hereinafter referred to as subtracting slag crude oil shell side interchanger.This subtracts slag crude oil shell side interchanger and is divided into and subtracts skull journey and crude oil shell side, and each shell side comprises housing, bobbin carriage, tube sheet and tube bank separately.When the temperature that subtracts slag in subtracting the skull journey is lower than 220 ℃, describedly subtracts the skull journey influenced by acid corrosion in the crude oil with high acid content less, the material of housing, bobbin carriage, tube sheet and tube bank all can be carbon steel.When the temperature of crude oil in the described crude oil shell side was lower than 220 ℃, it is less that the housing of described crude oil shell side, bobbin carriage, tube sheet are influenced by the acid corrosion in the crude oil with high acid content, all can use carbon steel; But the size that tube bank is influenced by the acid corrosion in the crude oil with high acid content depends on and subtracts the slag temperature in the tube side, and when subtracting the slag temperature in the tube side and be lower than 220 ℃, described tube bank still can be made by carbon steel; When subtracting the slag temperature in the tube side and be higher than 288 ℃, when the material of described tube bank is 316L, could guarantee effectively that this life-span that subtracts slag crude oil shell side interchanger is 15-20 when reaching 1200 tons/year amount of finish; When subtracting the slag temperature in the tube side and be 220-288 ℃, when the material of described tube bank is 304L, can guarantee effectively that this life-span that subtracts slag crude oil shell side interchanger is 15-20 when reaching 1200 tons/year amount of finish.
But subtract when subtracting the slag temperature in the skull journey and being not less than 220 ℃ when described, use carbon steel then can not satisfy requirement for anticorrosion, at this moment, the material of the described housing that subtracts the skull journey, bobbin carriage, tube sheet is the metal composite of 316L and/or 304L and carbon steel, and the material of tube bank is 316L and/or 304L.Further, when subtracting the slag temperature and be not higher than 288 ℃, the material of described housing, bobbin carriage and tube sheet is the metal composite of 304L and carbon steel, and the material of tube bank is 304L; When the temperature that subtracts slag was higher than 288 ℃, the material of described housing, bobbin carriage and tube sheet all was preferably the metal composite of 316L and carbon steel, and the material of tube bank then is preferably 316L.
When the temperature of crude oil in the described crude oil shell side was not less than 220 ℃, the material of the housing of described crude oil shell side, bobbin carriage, tube sheet was the metal composite of 316L and/or 304L and carbon steel, and the material of tube bank is 316L and/or 304L.Further, when crude oil temperature was 220-288 ℃, the material of described housing, bobbin carriage and tube sheet was the metal composite of 304L and carbon steel, and the material of tube bank is 304L; When the temperature of crude oil was higher than 288 ℃, the material of described housing, bobbin carriage and tube sheet all was preferably the metal composite of 316L and carbon steel, and the material of tube bank then is preferably 316L.
Be used for this described metal composite that subtracts slag crude oil shell side interchanger and preferably also obtain, and wherein the thickness of composite bed is the 3-5 millimeter by the explosive welding connection.
According to device and atmospheric and vacuum distillation of the present invention, wherein, described device and atmospheric and vacuum distillation also comprises transfer line, between described atmospheric pressure kiln and the atmospheric tower, between atmospheric tower and the vacuum furnace and be communicated with by transfer line between vacuum distillation tower and the vacuum furnace.The material of the preferred described transfer line of the present invention is 316L.The material of described transfer line is applicable to low speed segment and high regime.
According to device and atmospheric and vacuum distillation of the present invention, wherein, Mo content is not less than 2.5 weight % among the described 316L, is preferably 2.5-3 weight %.Mo content can slow down naphthenic acid corrosion speed 50-80% in this scope by controlling wherein.
The preferred described carbon steel of the present invention is that carbon content is soft steel and/or the low alloy steel of≤0.20 weight %, can guarantee that so described device and atmospheric and vacuum distillation has enough intensity.The preferred austenitic stainless steel of described carbon steel.
The carbon steel that satisfies above-mentioned requirements for example can be among No. 10 steel, No. 20 steel, 20HP, 15MnHP, 20R, 20MnR and the 16MnR one or more.
Because thereby the present invention mainly improves the antiseptic property that improves device and atmospheric and vacuum distillation by the material that the acid number to crude oil with high acid content distributes targetedly to the device and atmospheric and vacuum distillation of routine, thereby make it can be used in the atmospheric and vacuum distillation of crude oil with high acid content, state in the use under the situation of material, the various structures and the annexation of existing device and atmospheric and vacuum distillation all can realize purpose of the present invention, so the present invention no longer gives unnecessary details in this structure and annexation to each position of device and atmospheric and vacuum distillation.
Because device and atmospheric and vacuum distillation of the present invention distributes according to the acid number of crude oil with high acid content and targetedly the required antiseptic property in each position of normal pressure regulating equipment has been carried out systematic research, and determined the material at each position according to this antiseptic property, thereby shoot the arrow at the target antiseptic property high quality material is preferably selected for use in the stronger position of corrosion, conventional material is then selected for use in the more weak position of corrosion, the device and atmospheric and vacuum distillation of Huo Deing like this, can effectively prevent on the one hand the etching problem that brings because of peracid and high metal content, the whole service life of effective raising equipment, save the maintenance and the cost of exchange device more, all use expensive impregnating material to compare and greatly reduce cost than whole plant on the other hand, thereby device and atmospheric and vacuum distillation provided by the invention has industrial application value preferably, is particularly suitable for the peracid heavy sweet crude oil of the similar Peng Lai of working properties crude oil.
Because mainly being the good device and atmospheric and vacuum distillation of antiseptic property that the application of the invention provides, atmospheric vacuum distillation method provided by the invention realizes the atmospheric and vacuum distillation of crude oil with high acid content, actual conditions and operation to atmospheric and vacuum distillation are not particularly limited, and adopt to well known to a person skilled in the art that actual conditions and operation get final product.For example, for example, the temperature of flashing tower generally can be 215-230 ℃, the stage number of atmospheric distillation tower can be the 40-60 piece, be preferably 44, tower top temperature can be 90-130 ℃, is preferably 110-125 ℃, and the trim the top of column temperature can be 30-60 ℃, be preferably 40-45 ℃, inlet temperature of stabilizer can be 350-370 ℃, is preferably 355-365 ℃, and the feed zone stage number can be 35-45, atmospheric tower can be established 3-4 bar side line, normal line extraction temperature can be 170-200 ℃ at the bottom of wherein from cat head to tower, and normal two wires is extracted temperature out can be 230-320 ℃, and atmosphere 3rd side cut is extracted temperature out can be 320-350 ℃.Described vacuum distillation tower adopts and divides the five-part form filler, underpressure distillation cat head residual voltage can be for being not more than 3kPa, be preferably 0.3-2.5kPa, tower top temperature can be for being not more than 75 ℃, be preferably 60-70 ℃, column bottom temperature can be 370-375 ℃, and the top pumparound temperature can be 35-40 ℃, and vacuum distillation tower is established 3-4 bar side line.
The device and atmospheric and vacuum distillation of crude oil with high acid content of the present invention, the material of atmospheric tower, atmospheric pressure kiln, vacuum distillation tower and vacuum furnace limits by making wherein targetedly, efficiently solve the equipment corrosion problem of crude oil with high acid content atmospheric and vacuum distillation, and owing to can use low erosion resistance or conventional material in the not too serious place of corrosion, greatly reduce the cost of equipment, thereby obtained favorable economic benefit.In addition, owing to solved the equipment corrosion problem of crude oil with high acid content atmospheric and vacuum distillation, make that the metal content in the distillage can not roll up extraly, thereby can not influence the work-ing life of catalyzer in the following process process.
According to above-mentioned cut oil properties, acid number, sulphur content and composition, the present inventor also selects the material of each parts of hydrocracking equipment targetedly, thereby determined that a kind of height that is applicable to contains the hydrocracking equipment of acid starting material oil, this equipment comprises hydrocracking reactor, high-pressure separator and light pressure separator, wherein, the material of the housing of described hydrocracking reactor is for containing chromemolybdenum steel, the metal composite of TP316L and TP309L, the material of the internals of described hydrocracking reactor is TP316L, the material of the housing of described high-pressure separator is for containing chromemolybdenum steel, the metal composite of TP309L and TP316L, the material of the internals of described high-pressure separator is TP316L, and the material of the housing of described light pressure separator is anti-hydrogen induced cracking (HIC) soft steel.
Can realize purpose of the present invention although satisfy above-mentioned condition, under the preferable case, described metal composite is by obtaining at chromemolybdenum steel surface overlaying TP309L and TP316L.In above-mentioned metal composite, TP309L is used to good sticking power is provided between chromemolybdenum steel and the TP316L between chromemolybdenum steel and TP316L, plays the main TP316L of preservative activity, so as long as the thickness of TP316L is can be anticorrosion.Chromemolybdenum steel mainly provides the intensity of container at the required pressure of hydrocracking reaction as base material.In the material as the housing of hydrocracking reactor, the total thickness of described TP316L overlay cladding and TP309L overlay cladding is preferably the 4-7 millimeter, and the thickness of chromemolybdenum steel is preferably the 205-280 millimeter, the thickness of TP309L and the TP316L 3-4 millimeter of respectively doing for oneself; In the material as the housing of described high-pressure separator, the thickness of chromemolybdenum steel is the 180-200 millimeter, and the thickness of described TP316L overlay cladding and TP309L overlay cladding is the 4-7 millimeter, and the thickness of TP316L is the 3-4 millimeter.Gauge control by making chromemolybdenum steel, TP316L overlay cladding and TP309L overlay cladding is in above-mentioned scope, can play preservative activity, can make that again the thickness increase of hydrocracking reactor is not too big, that is to say to make hydrocracking reaction obtain big as far as possible volume, and make that the cost of hydrocracking reactor is low as far as possible.And can guarantee under above-mentioned selection and the thickness condition that amount of finish is that work-ing life of hydrocracking reactor under 4,000,000 tons/year the situation is 15-20.
Above-mentioned metal composite can obtain by the whole bag of tricks, for example can be commercially available, and also can make by overlaying method well known in the art.Can effectively guarantee combining closely between chromemolybdenum steel and TP316L and the TP309L by built-up welding, and guarantee to obtain required thickness, thereby effectively play the rot-resistant effect.The concrete operations of described overlaying method and condition have been conventionally known to one of skill in the art, and the present invention is not giving unnecessary details at this.
According to the present invention, it is that 165-360 ℃ second distillate carries out hydrocracking under the middle pressure hydrocracking condition that the method that distillate A or distillate B are carried out hydrocracking comprises boiling range, is that the 4th distillate that 360-450 ℃ the 3rd distillate or boiling range the 3rd distillate that is 360-450 ℃ and part boiling range are 450-520 ℃ carries out hydrocracking under the high-pressure hydrocracking condition with boiling range.
The condition of described middle pressure hydrocracking comprises that temperature can be 250-450 ℃, is preferably 340-400 ℃, and pressure can be the 10-15 MPa, is preferably the 12-13 MPa, and liquid hourly space velocity can be 0.5-1.5 hour -1, be preferably 1.0-1.25 hour -1, hydrogen to oil volume ratio can be 100-1000, is preferably 500-600; The condition of described high-pressure hydrocracking comprises that temperature can be 250-450 ℃, is preferably 380-400 ℃, and pressure can be the 12-20 MPa, the 14-16 MPa, and liquid hourly space velocity can be 0.5-2 hour -1, 1.0-1.5 hour -1, hydrogen to oil volume ratio can be 100-1000, is preferably 760-800.Described hydrocracking catalyst can be the conventional various hydrocracking catalysts that use in this area, and is for example concrete, and preferred described hydrocracking refined section catalyzer can use the HC-K catalyst for refining, and cracking zone can use home-made 3824 catalyzer.
Described hydrocracking (comprising middle pressure hydrocracking and high-pressure hydrocracking) is carried out in hydrocracking equipment, and described hydrocracking equipment comprises hydrocracking reactor, high-pressure separator and light pressure separator.
The present inventor finds, because that light pressure separator is subjected to height to contain the influence of acid starting material oleic acid value is less, therefore the housing of described light pressure separator and the material of internals preferably are anti-hydrogen induced cracking (HIC) soft steel.Under these conditions, both can guarantee amount of finish be under 4,000,000 tons/year the situation work-ing life of light pressure separator be 15-20, and the whole cost of equipment is also lower.
The material of the housing of described hydrocracking reactor is the metal composite that contains chromemolybdenum steel, TP316L and TP309L, the material of the internals of described hydrocracking reactor is TP316L, the material of the housing of described high-pressure separator is the metal composite that contains chromemolybdenum steel, TP309L and TP316L, the material of the internals of described high-pressure separator is TP316L, and the material of the housing of described light pressure separator is anti-hydrogen induced cracking (HIC) soft steel.Described metal composite is by obtaining at chromemolybdenum steel surface overlaying TP309L and TP316L, in the material as the housing of hydrocracking reactor, the thickness of described TP316L overlay cladding and TP309L overlay cladding is the 4-7 millimeter, the thickness of chromemolybdenum steel is the 205-280 millimeter, and the thickness of TP309L is the 3-4 millimeter; In the material as the housing of described high-pressure separator, the thickness of chromemolybdenum steel is the 180-200 millimeter, and the thickness of described TP316L overlay cladding and 309L overlay cladding is the 4-7 millimeter, and the thickness of TP316L is the 3-4 millimeter.
Usually, described hydrocracking equipment also comprises hydrocracking reaction product air cooler, and described hydrocracking reaction product air cooler comprises bobbin carriage and tube bank, and the material of the bobbin carriage that wherein enters the mouth is INCOLOY825, the material of described tube bank is INCOLOY825, and described pipe end ingress is lined with titanium.The length of preferred liner titanium is 300-600mm, promptly is lined with titanium from the inside 300-600mm of pipe end ingress edge.By above-mentioned selection, can guarantee that reach 15-20 the work-ing life of hydrocracking reaction product air cooler, thereby guarantee that in whole hydrocracking scope equipment life, the iron level of hydrocracking products obtained therefrom all can satisfy the requirement of following process.
Described hydrocracking equipment of the present invention also comprises hydrocracking raw material oil line.The present inventor finds, it is different to the extent of corrosion of hydrocracking raw material oil line different sites that height contains the high acid value of acid starting material oil, and closely related with the temperature of hydrocracking raw material oil, and with whether to contact hydrogen irrelevant or relation is very little.For this reason, the present invention is divided into first feeding line, second feeding line and the 3rd feeding line with hydrocracking raw material oil line according to the temperature of the hydrocracking raw material oil of contact with it.What contact with the hydrocracking raw material oil that is lower than 220 ℃ is first feeding line, be that oily what contact is second feeding line, being higher than 288 ℃ hydrocracking raw material with temperature, oily what contact is the 3rd feeding line for 220-288 ℃ hydrocracking raw material with temperature, the material of described first feeding line is a carbon steel, the material of described second feeding line is 316L and/or 321, and the material of described the 3rd feeding line is 316L.By above-mentioned selection, thereby can make above-mentioned feeding line hydrocracking reaction equipment reach optimum balance aspect equipment cost and work-ing life.Described carbon steel can be the various carbon steels that have or do not have antiseptic property, for example can be in A105,20# steel and the WCB carbon steel one or more.
According to hydrocracking equipment of the present invention, wherein, described hydrocracking equipment also comprises the solvent regeneration tower air cooler, and described solvent regeneration tower air cooler comprises bobbin carriage and tube bank, the material of described bobbin carriage is anti-hydrogen induced cracking (HIC) austenitic stainless steel, and the material of described tube bank is 304L or TP321.By above-mentioned selection, can guarantee that reach 15-20 the work-ing life of solvent regeneration tower air cooler, thereby guarantee that in whole hydrocracking scope equipment life, the iron level of hydrocracking products obtained therefrom all can satisfy the requirement of following process.
Usually, described hydrocracking equipment also comprises depriving hydrogen sulphide stripping tower air cooler, and described depriving hydrogen sulphide stripping tower air cooler comprises bobbin carriage and tube bank, and the material of described bobbin carriage is anti-hydrogen induced cracking (HIC) soft steel, and the material of described tube bank is 304L.By above-mentioned selection, can guarantee that reach 15-20 the work-ing life of depriving hydrogen sulphide stripping tower air cooler, thereby guarantee that in whole hydrocracking scope equipment life, the iron level of hydrocracking products obtained therefrom all can satisfy the requirement of following process.
In order to improve the capacity usage ratio of a whole set of hydrocracking equipment, described hydrocracking equipment also comprises being used to make and carries out the interchanger of heat exchange between hydrogen and the isocrackate and be used to make the interchanger that carries out heat exchange between hydrocracking raw material oil and the isocrackate.The material of this interchanger is the metal composite that contains TP316L, TP309L and chromemolybdenum steel.Described metal composite is by obtaining at chromemolybdenum steel surface overlaying TP316L and TP309L, and wherein the thickness of chromemolybdenum steel is preferably the 200-280 millimeter, and the thickness of TP316L is preferably the 3-4 millimeter.
According to hydrocracking equipment provided by the invention, wherein, described heat exchange unit also comprises and is used to make the interchanger that carries out heat exchange between hydrocracking raw material oil and the overhead product, wherein the material of the housing of hydrocracking raw material oil side is the metal composite that contains TP316L, TP309L and chromemolybdenum steel, and the material of traverse baffle is TP316L; The material of the bobbin carriage of isocrackate side is the metal composite that contains chromemolybdenum steel and TP316L.Described metal composite is by obtaining at chromemolybdenum steel surface overlaying TP316L and TP309L, and wherein the thickness of chromemolybdenum steel is preferably the 200-280 millimeter, and the thickness of TP316L is preferably the 3-4 millimeter.
According to hydrocracking equipment of the present invention, described hydrocracking equipment also comprises hydrocracking raw material oil process furnace and stripping tower process furnace, the material of described hydrocracking raw material oil process furnace is TP321 and/or 347, and the material of described stripping tower process furnace is one or more among T9, T11, the 1Cr5Mo.
Among the present invention, described chromemolybdenum steel is chosen by the Nelson curve.Further under the preferable case, described chromemolybdenum steel is 2.25Cr-1Mo-V, and described 2.25Cr-1Mo-V satisfies the condition shown in following formula (1)-Shi (3):
J coefficient (W Si+ W Mn) * (W P+ W Sn) * 10000＜100% (1)
X coefficient (10W P+ 5W Sb+ 4W Sn+ W As) * 0.01＜15ppm (2)
VTr54+3.0ΔVTr54＜10℃?????????????????(3)
Among above-mentioned formula (1)-Shi (3), W Si, W Mn, W P, W Sn, W P, W Sb, W AsRepresent Si, Mn, P, Sn, Sb and the As quality percentage composition in 2.25Cr-1Mo respectively, preferred W SiAnd W MnBe respectively the lower value of standard range.By limiting W SiAnd W MnBe its lower value, can further improve the erosion resistance of 2.25Cr-1Mo-V.VTr54 represents that the ballistic work of the preceding v-notch sample of embrittlement is 54 joules of pairing temperature; Δ VTr54 represents to quicken that the ballistic work of v-notch sample is 54 joules of pairing temperature after the ladder refrigeration test of embrittlement.
Preferred described ladder process for cooling such as following table 3 can further obtain better hydrogen-induced cracking resistance energy like this, thus the work-ing life of further improving equipment.
Table 3
Temperature, ℃ Soaking time, h The heating speed of cooling, ℃/h
Room temperature ??50
??593 ??1 ??5.6
??537 ??15 ??5.6
??524 ??24 ??5.6
??496 ??60 ??2.8
??468 ??100 ??27.8
??315 Cool to room temperature in the immobilized air
Further preferable case, described 2.25Cr-1Mo-V is made by electrosmelting and vacuum deaeration method, can obtain the better effect of anti-hydrogen induced cracking (HIC) like this.
Further preferable case, described 2.25Cr-1Mo-V is made by electrosmelting and vacuum deaeration method, can obtain the better effect of anti-hydrogen induced cracking (HIC) like this.
Among the present invention, the Mo content of described TP316L is not less than 2.5 weight %, is preferably 2.5-3 weight %, more preferably 2.8-3 weight %.Mo content can slow down naphthenic acid corrosion speed 50-80% in this preferable range by controlling wherein.
Among the present invention, described anti-hydrogen induced cracking (HIC) soft steel can be the austenitic stainless steel that various hydrogen-induced cracking resistances can satisfy the requirement of NACE TM0284 " evaluation of pressurized vessel and the anti-hydrogen induced cracking (HIC) of pipe line steel " method, one or more that concrete for example is in 304,321,347.
Except above-mentioned parts or structure, hydrocracking equipment according to the present invention can also comprise one or a few person in desulfuration of liquefied gas extraction tower, debutanizing tower, depropanizing tower, deisobutanizer, the dry gas thionizer, their annexation and effect have been conventionally known to one of skill in the art, and the present invention does not repeat them here.Other structure, parts and the pipeline that does not specialize in the present invention can use the conventional various materials that use in this area, for example, can use carbon steel.Described carbon steel is preferably austenitic stainless steel, and its carbon content is preferably≤0.2 weight %.
According to hydrocracking equipment of the present invention, wherein, described hydrocracking equipment generally also comprises hydrogen gas lines and other pipeline,
When described hydrogen gas lines was used under being lower than 200 ℃, material was a carbon steel, and when using under being not less than 200 ℃, material is a chromemolybdenum steel;
When described other pipeline used under being lower than 240 ℃, material was a carbon steel, and when using under being not less than 240 ℃, material is 1Cr5Mo and/or 321.
In addition, the inventor also selects the material of each parts of delayed coking equipment targetedly, determined that a kind of height that is applicable to contains the delayed coking equipment of acid starting material oil, this delayed coking equipment comprises process furnace, separation column and the coke drum that is communicated with by pipeline each other, described process furnace comprises convection tubes, radiator tube, radiation section inlet line, radiation section egress line, wherein, the material of described radiator tube is T9 and/or 321H, the material of described radiation section inlet line is 1Cr5Mo and/or 321, and the material of described radiation section egress line is P9 and/or 316L.
Although other position uses anti-hydrogen-type corrosion performance better material also can realize anticorrosion and purpose prolongs life, but under these conditions, reach more than 15 years the work-ing life that can guarantee process furnace, and the whole service life of a whole set of delayed coking equipment was higher than more than 3 years, can also guarantee simultaneously in the delayed coking products obtained therefrom metal ion particularly the content of iron ion can not raise because of the material of delayed coking equipment too much, the cost that can also guarantee equipment in addition is low as far as possible, realizes the better balance between product iron ion content and the equipment cost.
Usually, the coke drum of described delayed coking equipment comprises the upper and lower, described top be the top of coke drum to 200 millimeters section below the foam layer, the residue section is the bottom.According to delayed coking equipment provided by the invention, the material on described top is 405 and/or the metal composite of 410S and 14Cr1MoR, and the material of bottom is 14Cr1MoR and/or 15Cr1MoR.
The present invention is preferably used as in the described metal composite of coke drum top material, 405 and the thickness of 410S be that (when described metal composite is 405 during with the metal composite of 14Cr1MoR, 405 thickness is the 3-5 millimeter to the 3-5 millimeter; When described metal composite was the metal composite of 410S and 14Cr1MoR, the thickness of 410S was the 3-5 millimeter; When described metal composite is 405 and during the metal composite of 410S and 14Cr1MoR, 405 and the total thickness of 410S be the 3-5 millimeter, following analogue is similarly).In above-mentioned preferable range, can make the work-ing life of coke drum identical, thereby particularly the content of iron is lower for the metal content that further guarantees coke chemicals in the whole work-ing life of described delayed coking equipment with the life-span of the process furnace of described delayed coking equipment.
The separation column of described delayed coking equipment generally all comprises tower body and tower tray, according to delayed coking equipment provided by the invention, wherein, described separation column generally is divided into three sections because of the temperature difference of raw material of contact is that the service temperature of tower is different, from top to bottom, service temperature raises gradually, and wherein the part that contacts with the raw material that is lower than 220 ℃ is called first section, the part that contacts with 220-288 ℃ raw material is called second section, and the part that contacts with the raw material that is higher than 288 ℃ is called the 3rd section.Among the present invention, the material of described first section tower body is preferably carbon steel, and the material of tower tray is preferably the metal composite that 0Cr13 is 410S; The material of described second section tower body is preferably the metal composite of carbon steel and 410S, and the material of tower tray is preferably 304; The material of described the 3rd section tower body is preferably the metal composite of carbon steel and 321, and the material of tower tray is preferably 321.In the described metal composite, the thickness of composite bed is preferably the 3-5 millimeter.In above-mentioned preferable range, can make the work-ing life of separation column identical, thereby particularly the content of iron is lower for the metal content that further guarantees coke chemicals in the whole work-ing life of described delayed coking equipment with the life-span of the process furnace of described delayed coking equipment.
According to delayed coking equipment provided by the invention, described separation column preferably also comprises the overhead oil gas tank that is used to separate fractionator overhead oil gas, and the material of described overhead oil gas tank is that sulphur content is no more than the anti-hydrogen induced cracking (HIC) carbon steel that 0.002 weight %, phosphorus content are no more than 0.008 weight %.Among the present invention, the hydrogen-induced cracking resistance of described anti-hydrogen induced cracking (HIC) carbon steel can satisfy NACE TM0284 " the anti-1Cr5Mo of pressurized vessel and pipe line steel.
Among the present invention, unless stated otherwise, the numbering of material therefor all adopts the conventional numbering of using in this area, generally all generally adopt GB9948 standard, U.S. ASME standard or U.S. Mechanic Engineer association criterion from GB4237-92, particularly tubing, for example, 0Cr13,00Cr17Ni14Mo2 and 00Cr19Ni3Mo2 are the numbering among the GB4237-92.316L, TP316L, TP317L, 304,304L, 321,347,321H, TP309L, 405,410S are the numbering in the U.S. ASME standard.SAF2205, SAF2507 and SAF2304 are the numbering in the U.S. Mechanic Engineer association criterion.Their concrete composition has been conventionally known to one of skill in the art.And, use the material of this numbering of above-mentioned various standards all can realize purpose of the present invention if the above-mentioned materials numbering all has in different standards to be related to.
Because the present invention relates generally to the design of operational path and the selection of equipment and materials, and the concrete operations of each step and the internal structure of each equipment and the annexation between annexation and the equipment components are not particularly limited, those skilled in the art can determine according to prior art.For example, the working pressure that the main operational condition of delayed coking generally comprises the coke cat head is 0.15-0.17MPa (gauge pressure), the furnace outlet temperature is 495-505 ℃, the coke tower top temperature is 420-440 ℃, fractionation tower temperature is 110-120 ℃, fractionator bottom temperature is 380-400 ℃, and the combined cycle ratio is generally 0.2-0.4.Described combined cycle is than being meant that a part is than the circulation oil mass of coker distillate weight and the ratio of raw material oil mass in the coking fractional distillation column.The condition of described catalytic cracking comprises that temperature of reaction is 450-600 ℃, is preferably 500-520 ℃, and the agent oil volume is than being 1-10, be preferably 5.8-6.0, the reaction times is 0.2-8 second, preferred 1.2-1.4 second, reaction pressure is 300-500 kPa, is preferably 210-350 kPa.The condition of described catalytic reforming comprises that weighted average bed temperature is 480-520 ℃, is preferably 470-500 ℃, and pressure is 0.2-0.5MPa, is preferably 0.22-0.26MPa, and volume space velocity is for being not more than 1.5h -1, be preferably 0.1-1.5h -1, the hydrogen oil molecule is than being 2-3.
According to preferred implementation of the present invention, in order further to improve the compactedness of technology, this method also comprise wax oil that delayed coking is obtained as the raw material of high-pressure hydrocracking carry out high-pressure hydrocracking and/evaluation of hydrogen induced cracking (HIC) " requirement of method.
Under the preferable case, delayed coking equipment of the present invention also comprises the absorption stabilizer tower, and described absorption stabilizer tower is communicated with separation column.Described absorption stabilizer tower comprises tower body, tower tray and return tank of top of the tower, the material of described tower body is a carbon steel, the material of described tower tray is 0Cr13, and the material of described return tank of top of the tower is that sulphur content is no more than the anti-hydrogen induced cracking (HIC) carbon steel that 0.002 weight %, phosphorus content are no more than 0.008 weight %.Select above-mentioned material for use by making above-mentioned overhead oil gas tank and absorbing stabilizer tower, can guarantee further that reach 15-20 the work-ing life of these equipment, thereby the life-span that helps a whole set of delayed coking equipment reaches 15-20.
According to delayed coking equipment of the present invention, wherein, described delayed coking equipment also comprises stripping tower, and described stripping tower is communicated with separation column, is used for the side line component of knockout tower is carried out stripping.The material of described stripping tower is preferably the metal composite of 0Cr13 and carbon steel, and described metal composite obtains by the explosive welding connection, and wherein the thickness of 0Cr13 is the 3-5 millimeter.By making above-mentioned stripping tower select above-mentioned material for use, can guarantee further that reach 20 years the work-ing life of this equipment, thereby the life-span that helps a whole set of delayed coking equipment reaches 15-20.
According to delayed coking equipment of the present invention, wherein, described delayed coking equipment also comprises air cooler and the water cooler that is communicated with fractionator overhead, and the material of the tube bank of described air cooler and water cooler is respectively done for oneself, and sulphur content is no more than 0.002 weight %, phosphorus content is no more than the anti-hydrogen induced cracking (HIC) carbon steel of 0.008 weight % or the low alloy steel of hydrogen sulfide corrosion-resistant.
Among the present invention, described sulphur content be no more than 0.002 weight %, phosphorus content be no more than 0.008 weight % anti-hydrogen induced cracking (HIC) carbon steel for example be 20R steel and/or 16MnR (HIC) steel, the low alloy steel of described hydrogen sulfide corrosion-resistant for example is the low alloy steel of 09Cr2AlMoRe material.Among the present invention, described carbon steel can be 16MnR, 20MnR, 10# steel, 20# steel.
According to delayed coking equipment provided by the invention, wherein, described delayed coking equipment also comprises fractionation Tata bottom line, and the material of described fractionation Tata bottom line is 1Cr5Mo.
According to delayed coking equipment provided by the invention, wherein, described delayed coking equipment also comprises stock oil line and wax oil line, and the material of described stock oil line is 1Cr5Mo, and the material of described wax oil line is or the high-pressure hydrocracking tail oil is carried out delayed coking as the delayed coking raw material.In addition, method provided by the invention is also preferably carried out catalytic reforming with the heavy naphtha in the isocrackate as catalytic reforming raw material.
According to preferred implementation of the present invention, this method also comprises fuel gas and LPG in isocrackate, coking product and the catalytic cracking production sent into carries out desulfurization in the desulfurizer, and the gasoline in the catalytic cracking production is sent into carry out mercaptan removal in the sweetening unit.
Among the present invention, gasoline refers to that boiling range is 40-205 ℃ a component, and light naphthar refers to that boiling range is 40-80 ℃ a component, and heavy naphtha refers to that boiling range is 80-165 ℃ a component, and the boat coal refers to that boiling range is 165-250 ℃ a component, and diesel oil refers to that boiling range is 250-350 ℃ a component.
The following examples will the present invention is further illustrated.In the above among embodiment of Miao Shuing and the following embodiment that will describe, the selection at other position that does not specify in each equipment is the conventional selection of conventional apparatus, be generally carbon steel, all use the 20# steel as the pipeline of atmospheric and vacuum distillation unit, container uses 16MnR.
Embodiment 1
This embodiment is used to illustrate the corrosion-resistant processing method of crude oil with high acid content provided by the invention.
Peng Lai PL19-3 crude oil after adopting technical process shown in Figure 1 to electric desalting carries out processing treatment.Wherein as above shown in the table 1, saltiness is less than 3 mg/litre (testing method GB6532-86) after the electric desalting for the character of PL19-3 crude oil, and water content contains the sodium amount less than 1 mg/litre (atomic absorption spectrometry) less than 0.1 weight % (testing method GB260-77).Amount of finish is 1,200 ten thousand tons/year.Atmospheric tower in the device and atmospheric and vacuum distillation is totally 44 layers of tower tray, the material of the tower body between 40 layers of tower tray of cat head to the is that thickness is the metal composite that the Monel metal of 22 millimeters 16MnR steel and 3 millimeters obtains by the explosive welding connection, the material of tower tray is SAF2205, the material of the 40th layer of tower tray tower body between at the bottom of the tower be thickness be 22 millimeters the 16MnR steel with and 3 millimeters 316L, the material of tower tray is 316L, the number of plies of vacuum distillation tower is 5 layers, the material of the filler that the top is 2 layers is 316L, the material that remains 3 layers filler is 317L, atmospheric tower, vacuum distillation tower, the material of atmospheric pressure kiln and vacuum furnace is as shown in table 4 below.Wherein the carbon content of austenitic stainless steel 16MnR is 0.01 weight %, and the Mo content among the 316L is 3 weight %.The temperature that crude oil after the electric desalting advances flashing tower is 224 ℃ (pure liquid phases), flashing tower has 4 layers of tower tray, and the temperature of advancing atmospheric tower is 350-365 ℃, and the temperature of advancing vacuum distillation tower is 390-400 ℃, decompression cat head residual voltage is 1.0-2.0kPa, and crude oil heat exchange temperature eventually is 280-300 ℃.The atmospheric and vacuum distillation product is pressed boiling range order from low to high and is distributed as follows: fuel gas (overhead gas component), 0.15 volume %;＜165 ℃ of cuts (first distillate), 4.46 volume %; 165-235 ℃ of cut (second distillate), 6.39 volume %; 235-360 ℃ of cut (the 3rd distillate), 19.25 volume %; 360-450 ℃ of cut (the 3rd distillate), 17.13 volume %; 450-520 ℃ of cut (the 4th distillate), 14.58 volume %; 520-545 ℃ of cut (the 5th distillate), 3.8 volume %; Greater than residual oil at the bottom of 545 ℃ the tower, 34.24 volume %.
Described first distillate and middle pressure hydrocracking heavy naphtha and high-pressure hydrocracking heavy naphtha are carried out catalytic reforming under the catalytic reforming condition, described second distillate is carried out hydrocracking under the middle pressure hydrocracking condition, be 360-450 ℃ the 3rd distillate with boiling range and be that 450-520 ℃ the 4th distillate carries out hydrocracking under the high-pressure hydrocracking condition to the small part boiling range, described the 5th distillate and remainder the 4th distillate are carried out catalytic cracking under catalytic cracking condition, residual oil at the bottom of the described tower and high-pressure hydrocracking tail oil are carried out delayed coking, and with isocrackate, fuel gas and LPG send into and carry out desulfurization in the desulfurizer in coking product and the catalytic cracking production, and the gasoline in the catalytic cracking production are sent into carry out mercaptan removal in the sweetening unit.The condition of described catalytic reforming comprises that weighted average bed temperature is 470-500 ℃, and pressure is 0.22-0.26MPa, and volume space velocity is 1-1.5h -1, hydrogen to oil volume ratio is 2-3, catalytic reforming catalyst is Uop Inc.'s development, the FR-234 catalytic reforming catalyst that Fushun Petrochemical Company north catalyst plant is produced.The catalytic reforming product be distributed as fuel gas, the 0.89 volume % of 0.18 volume % tops, (wherein the volumn concentration of hydrogen is 42% to the hydrogen-containing gas of 9.84 volume %, be 4.17 volume %), the pentane of the LPG of 1.87 volume %, 0.97 volume % and the reformed oil of 86.24 volume %.450-600 ℃, the agent oil volume is than being 1-205.8-6.0, and first reaction times was 1.2-1.40.2-8 second, about 330 kPas of reaction pressure.
The condition of described middle pressure hydrocracking comprises that temperature is 340-400 ℃, and pressure is the 12-13 MPa, and liquid hourly space velocity is 1-1.25 hour -1, hydrogen to oil volume ratio is 500-600.The middle pressure hydrocracking product is distributed as 0.19 volume % dry gas, 2.97 volume % fuel gas, 3.66 volume %LPG, 3.77 volume % light naphthars, 23.62 volume % heavy naphtha, 29.03 volume % boat coal, 41.43 volume % diesel oil.The condition of described high-pressure hydrocracking comprises that temperature is 380-400 ℃, and pressure is the 14-16 MPa, and liquid hourly space velocity is 1-1.5 hour -1, hydrogen to oil volume ratio is 760-800.The condition of described catalytic cracking comprises that temperature of reaction is 500-520 ℃, and the agent oil volume is than being 5.8-6.0, and the reaction times is 1.2-1.4 second, and reaction pressure is about 330 kPas.Entering hydroeracking unit is 1: 2 with the volume ratio that enters the 4th distillate of catalytic cracking unit, hydrocracking refined section catalyzer is the HC-K catalyst for refining, cracking zone is home-made 3824 catalyzer, the MIP catalytic cracking catalyst that described catalytic cracking catalyst provides for China Petroleum ﹠ Chemical Corporation Research Institute of Petroleum.The catalytic cracking products obtained therefrom is distributed as 0.15 volume % dry gas, 4.58 volume % fuel gas, 23.27 volume %LPG, 39.50 volume % gasoline, 23.00 volume % diesel oil, 2.50 volume % slurry oils and 7 volume % and burns.The material of each parts of hydrocracking equipment is as shown in table 5 below.In the table 5, chromemolybdenum steel is the 2.25Cr-1Mo-V steel, adopts ladder process for cooling shown in the table 3 by the acquisition of vacuum deaeration method, and manganese content is 3.0 weight % among the 316L, and the pipe end ingress of isocrackate air cooler is lined with 300 millimeters titanium.The high-pressure hydrocracking products obtained therefrom is distributed as the lighter-than-air gas component (hydrogen sulfide and ammonia) of 0.71 volume %, 1.78 the fuel gas of volume %, 5.91 the LPG of volume %, 4.17 the light naphthar of volume %, 18.96 the heavy naphtha of volume %, 30.31 the boat coal of volume %, the hydrocracking tail oil of the diesel oil of 26.85 volume % and 14.34 volume %.
Delayed coking employing Design and Machining amount is " two stoves, four towers " delayed coking equipment of 4,200,000 tons/year, wherein to link be a cover for a process furnace and two coke drums, a coke drum reacts and fills Jiao, another has filled burnt coke drum and has then carried out hydraulic decoking, two coke drums switch with four-way valve, by changing the mutual blocked operation of tower working order.The main operational condition of delayed coking comprises that the working pressure of coke cat head is 0.15-0.17MPa (gauge pressure), the furnace outlet temperature is 495-505 ℃, the coke tower top temperature is 420-440 ℃, fractionation tower temperature is 110-120 ℃, fractionator bottom temperature is 380-400 ℃, and the combined cycle ratio is 0.3.Process furnace adopts two-sided radiation ladder stove, and coke drum adopts
Figure G2009102444650D00281
The specification of 9800mm * 23900mm (cutting).The selection of the major parts of delayed coking equipment is as shown in table 6.The fuel gas of the dry gas that consists of 0.13 volume % of delayed coking products obtained therefrom (hydrogen sulfide and ammonia), 3.94 volume %, the LPG of 4.38 volume %,, the petroleum naphtha of 21.77 volume %, the diesel oil of 23.13 volume %, the wax oil of 17.47 volume %, the wax slop of 2.99 volume % and the coke of 26.19 volume %.
The product of whole technology is distributed as the diesel oil of the gasoline of about 10 weight %, the boat coal of about 20 weight %, about 30 weight %, the coke of about 10 weight %, and the energy consumption of whole technology is 70.4 kilograms of mark oil/ton stock oils.
Table 4
Figure G2009102444650D00282
Figure G2009102444650D00291
Table 5
Figure G2009102444650D00301
Table 6
Figure G2009102444650D00302
Figure G2009102444650D00311
Method measuring result according to embodiment 1 is found, behind the equipment continuous operation 1 year, the etching extent of the tower body between 40 layers of tower tray of the cat head to the of atmospheric tower is 001 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the 40th layer of tower tray tower body between at the bottom of the tower is 0.01 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the convection tubes of atmospheric pressure kiln is 0.01 millimeter, the etching extent of the radiator tube of atmospheric pressure kiln is 0.01 millimeter, the etching extent of vacuum distillation tower tower body is 0.01 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the 2nd layer of filler in top is 0.01 millimeter, the etching extent of 3 layers of filler of residue is 0.01 millimeter, the etching extent of the convection tubes of vacuum furnace is 0.01 millimeter, and the etching extent of the radiator tube of vacuum furnace is 0.01 millimeter, and the etching extent of flashing tower tower body is 0.01 millimeter, the etching extent of cat head end socket is 0.01 millimeter, and the etching extent of tower tray is 0.01 millimeter; The tower body of atmospheric stripping tower and the etching extent of tower tray are 0.01 millimeter, the etching extent of decompression return tank of top of the tower is 0.01 millimeter, the etching extent of decompression stripping tower is 0.3 millimeter, the etching extent of ordinary decompression column head space cooler tube bank is 0.01 millimeter, the etching extent of ordinary decompression column feeder side body is 0.01 millimeter, the etching extent of tube bank is 0.01 millimeter, subtract the etching extent that the slag crude heat exchanger subtracts slag side body and tube bank and be 0.01 millimeter, the etching extent of crude oil side body and tube bank is 0.01 millimeter, and the etching extent of normal pressure transfer line and pressure-reducing line for oil-transferring is 0.01 millimeter.
The etching extent of hydrocracking reactor housing is 0.03 millimeter, and the etching extent of internals is 0.04 millimeter; The etching extent of high-pressure separator housing is 0.01 millimeter, and the etching extent of internals is 0.01 millimeter; The etching extent of light pressure separator housing is 0.009 millimeter, and the etching extent of internals is 0.009 millimeter; The etching extent of hydrogen and isocrackate interchanger hydrogen gas side housing is 0.01 millimeter, the etching extent of isocrackate side is 0.01 millimeter, hydrocracking raw material oil is 0.01 millimeter with the etching extent of the oily feeding side housing of isocrackate interchanger, and the etching extent of isocrackate side is 0.01 millimeter; The etching extent of isocrackate air cooler pipe end ingress is 0.01 millimeter; The etching extent of solvent regeneration tower air cooler is 0.01 millimeter, the etching extent of depriving hydrogen sulphide stripping tower air cooler is 0.01 millimeter, the etching extent of hydrocracking raw material oil process furnace is 0.01 millimeter, the etching extent of stripping tower process furnace is 0.01 millimeter, and the etching extent of hydrocracking raw material oil line is 0.01 millimeter.
The etching extent of delayed coking equipment process furnace convection tubes is 0.01 millimeter, the etching extent of radiator tube is 0.01 millimeter, the etching extent of radiation section inlet line is 0.03 millimeter, the etching extent of radiation section egress line is that etching extent is 0.01 millimeter, the etching extent of separation column tower body is 0.01 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of cat head catch pot is 0.01 millimeter, the etching extent of fractionation cat head water cooler tube bank is 0.01 millimeter, the etching extent of air cooler tube bundle is 0.01 millimeter, the etching extent of separation column bottom line is 0.01 millimeter, the etching extent that absorbs the stabilizer tower bottom line is 0.01 millimeter, the etching extent of stripping tower is 0.01 millimeter, and the etching extent of coke drum upper and lower is respectively 0.01 millimeter and 0.01 millimeter, and the etching extent of hydrocracking raw material oil line and wax oil line is 0.02 millimeter.
Comparative Examples 1
Carry out processing treatment according to the method for embodiment 1 pair and embodiment 1 identical PL19-3 crude oil, different is, the material of device and atmospheric and vacuum distillation is austenitic stainless steel 16MnR, the convection tubes of delayed coking equipment process furnace, the material of radiation section inlet line are the 20# steel, and radiator tube and radiation section egress line are 1Cr5Mo.Found that, the equipment continuous operation is after 3 months, the etching extent of the tower body between 40 layers of tower tray of the cat head to the of atmospheric tower is 1 millimeter, the etching extent of tower tray is 1 millimeter, the etching extent that the perforation tower tray appears in the 40th layer of tower tray tower body between at the bottom of the tower is 1 millimeter, the etching extent of the convection tubes of atmospheric pressure kiln is 1 millimeter, the etching extent of the radiator tube of atmospheric pressure kiln is 1 millimeter, the etching extent of the tower body of vacuum distillation tower is 1 millimeter, the etching extent of tower tray is 1 millimeter, the etching extent of the filler that the top is 2 layers is 1 millimeter, and the etching extent of 3 layers of filler of residue is 1 millimeter, and the etching extent of the convection tubes of vacuum furnace is 1 millimeter, the etching extent of the radiator tube of vacuum furnace is 1 millimeter, the etching extent of flashing tower tower body is 0.1 millimeter, and the etching extent of cat head end socket is 0.1 millimeter, and the etching extent of tower tray is 0.1 millimeter; The tower body of atmospheric stripping tower and the etching extent of tower tray are 0.1 millimeter, the etching extent of decompression return tank of top of the tower is 0.1 millimeter, the etching extent of decompression stripping tower is 0.3 millimeter, the etching extent of ordinary decompression column head space cooler tube bank is 0.1 millimeter, the etching extent of ordinary decompression column feeder side body is 0.2 millimeter, the etching extent of tube bank is 0.1 millimeter, subtract the etching extent that the slag crude heat exchanger subtracts slag side body and tube bank and be 0.3 millimeter, the etching extent of crude oil side body and tube bank is 0.3 millimeter, and the etching extent of normal pressure transfer line and pressure-reducing line for oil-transferring is 0.2 millimeter.The etching extent of delayed coking equipment process furnace convection tubes is 2 millimeters, the etching extent of radiator tube is 1 millimeter, the etching extent of radiation section inlet line is 2.5 millimeters, the etching extent of radiation section egress line is that etching extent is 1 millimeter, the etching extent of separation column tower body is 0.02 millimeter, the etching extent of tower tray is 0.02 millimeter, the etching extent of cat head catch pot is 0.02 millimeter, the etching extent of fractionation cat head water cooler tube bank is 0.02 millimeter, the etching extent of air cooler tube bundle is 0.02 millimeter, the etching extent of separation column bottom line is 0.02 millimeter, the etching extent that absorbs the stabilizer tower bottom line is 0.02 millimeter, the etching extent of stripping tower is 0.02 millimeter, and the etching extent of coke drum upper and lower is respectively 0.01 millimeter and 0.01 millimeter, and the etching extent of stock oil line and wax oil line is 0.02 millimeter.
Embodiment 2
This embodiment is used to illustrate the corrosion-resistant processing method of crude oil with high acid content provided by the invention.
Method according to embodiment 1 is that the PL19-3 crude oil that 3.3 milligrams of KOH/ restrain carries out processing treatment to acid number content, different is, only the material of atmospheric tower, vacuum distillation tower, atmospheric pressure kiln and vacuum furnace is identical with embodiment 1 in the device and atmospheric and vacuum distillation, and the material at other parts shown in the table 2 or position is material 16MnR used in the conventional device and atmospheric and vacuum distillation.The material of the hydrocracking reactor in the hydrocracking equipment, high-pressure separator and light pressure separator is with embodiment 1, and the material at all the other positions is the conventional material Low Alloy Steel Plate that uses in this area.Delayed coking equipment is except that process furnace, and the material of other container is carbon steel 16MnR steel, and the material of pipeline is the 20# steel.
Found that the equipment continuous operation is after 1 year, the etching extent of the tower body between 40 layers of tower tray of the cat head to the of atmospheric tower is 0.01 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the 40th layer of tower tray tower body between at the bottom of the tower is 0.01 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the convection tubes of atmospheric pressure kiln is 0.01 millimeter, the etching extent of the radiator tube of atmospheric pressure kiln is 0.01 millimeter, the etching extent of vacuum distillation tower tower body is 0.01 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the 2nd layer of filler in top is 0.01 millimeter, and the etching extent of 3 layers of filler of residue is 0.01 millimeter, and the etching extent of the convection tubes of vacuum furnace is 0.01 millimeter, the etching extent of the radiator tube of vacuum furnace is 0.01 millimeter, the etching extent of flashing tower tower body is 0.2 millimeter, and the etching extent of cat head end socket is 0.2 millimeter, and the etching extent of tower tray is 0.3 millimeter; The tower body of atmospheric stripping tower and the etching extent of tower tray are 0.2 millimeter, the etching extent of decompression return tank of top of the tower is 0.2 millimeter, the etching extent of decompression stripping tower is 0.3 millimeter, the etching extent of ordinary decompression column head space cooler tube bank is 0.4 millimeter, the etching extent of ordinary decompression column feeder side body is 0.5 millimeter, the etching extent of tube bank is 0.5 millimeter, subtract the etching extent that the slag crude heat exchanger subtracts slag side body and tube bank and be 0.5 millimeter, the etching extent of crude oil side body and tube bank is 0.6 millimeter, and the etching extent of normal pressure transfer line and pressure-reducing line for oil-transferring is 0.6 millimeter.The etching extent of hydrocracking reactor housing is 0.03 millimeter, and the etching extent of internals is 0.04 millimeter; The etching extent of high-pressure separator housing is 0.01 millimeter, and the etching extent of internals is 0.01 millimeter; The etching extent of light pressure separator housing is 0.009 millimeter, and the etching extent of internals is 0.009 millimeter; The etching extent of hydrogen and isocrackate interchanger hydrogen gas side housing is 0.6 millimeter, the etching extent of isocrackate side is 0.6 millimeter, hydrocracking raw material oil is 0.8 millimeter with the etching extent of the oily feeding side housing of isocrackate interchanger, and the etching extent of isocrackate side is 0.6 millimeter; The etching extent of isocrackate air cooler pipe end ingress is 0.8 millimeter; The etching extent of solvent regeneration tower air cooler is 0.4 millimeter, the etching extent of depriving hydrogen sulphide stripping tower air cooler is 0.4 millimeter, the etching extent of hydrocracking raw material oil process furnace is 0.4 millimeter, and the etching extent of stripping tower process furnace is 0.4 millimeter, and the etching extent of hydrocracking raw material oil line is 0.8 millimeter.The etching extent of delayed coking equipment process furnace convection tubes is 0.01 millimeter, the etching extent of radiator tube is 0.01 millimeter, the etching extent of radiation section inlet line is 0.03 millimeter, the etching extent of radiation section egress line is that etching extent is 0.01 millimeter, the etching extent of separation column tower body is 1 millimeter, the etching extent of tower tray is 1 millimeter, the etching extent of cat head catch pot is 1 millimeter, the etching extent of fractionation cat head water cooler tube bank is 1 millimeter, the etching extent of air cooler tube bundle is 1 millimeter, the etching extent of separation column bottom line is 1 millimeter, the etching extent that absorbs the stabilizer tower bottom line is 1 millimeter, the etching extent of stripping tower is 1 millimeter, and the etching extent of coke drum upper and lower is respectively 1 millimeter and 1 millimeter, and the etching extent of stock oil line and wax oil line is 1.1 millimeters.
Embodiment 3
This embodiment is used to illustrate the corrosion-resistant processing method of crude oil with high acid content provided by the invention.
Method according to embodiment 1 is that the PL19-3 crude oil that 3.5 milligrams of KOH/ restrain carries out processing treatment to acid number content, different is, the material of device and atmospheric and vacuum distillation is as shown in table 7, the material of hydrocracking equipment is as shown in table 8, and the pipe end ingress of isocrackate air cooler does not serve as a contrast titanium, the convection tubes of delayed coking equipment and the material of radiator tube are 321H, and the material of radiation section inlet line is 321, and the material of radiation section egress line is 316L.
Table 7
Figure G2009102444650D00361
Table 8
Equipment Material
Hydrocracking reactor Housing: chromemolybdenum steel+TP309L overlay cladding+TP316L overlay cladding (total thickness of overlay cladding is 7 millimeters, and the thickness of TP316L is 3 millimeters) internals: TP316L
High-pressure separator Housing: chromemolybdenum steel+TP309L overlay cladding+TP316L overlay cladding (total thickness of overlay cladding is 7 millimeters, and the thickness of TP316L is 4 millimeters) internals: TP316L
Figure G2009102444650D00371
Found that, behind the equipment continuous operation 1 year, the etching extent of the tower body between 40 layers of tower tray of the cat head to the of atmospheric tower is 0.02 millimeter, the etching extent of tower tray is 0.01 millimeter, the etching extent of the 40th layer of tower tray tower body between at the bottom of the tower is 0.02 millimeter, the etching extent of tower tray is 0.02 millimeter, the etching extent of the convection tubes of atmospheric pressure kiln is 0.01 millimeter, the etching extent of the radiator tube of atmospheric pressure kiln is 0.01 millimeter, the etching extent of vacuum distillation tower tower body is 0.02 millimeter, and the etching extent of tower tray is 0.01 millimeter, and the etching extent of the 2nd layer of filler in top is 0.01 millimeter, the etching extent of 3 layers of filler of residue is 0.01 millimeter, the etching extent of the convection tubes of vacuum furnace is 0.02 millimeter, and the etching extent of the radiator tube of vacuum furnace is 0.01 millimeter, and the etching extent of flashing tower tower body is 0.01 millimeter, the etching extent of cat head end socket is 0.02 millimeter, and the etching extent of tower tray is 0.01 millimeter; The tower body of atmospheric stripping tower and the etching extent of tower tray are 0.01 millimeter, the etching extent of decompression return tank of top of the tower is 0.01 millimeter, the etching extent of decompression stripping tower is 0.3 millimeter, the etching extent of ordinary decompression column head space cooler tube bank is 0.01 millimeter, the etching extent of ordinary decompression column feeder side body is 0.01 millimeter, the etching extent of tube bank is 0.01 millimeter, subtract the etching extent that the slag crude heat exchanger subtracts slag side body and tube bank and be 0.01 millimeter, the etching extent of crude oil side body and tube bank is 0.01 millimeter, and the etching extent of normal pressure transfer line and pressure-reducing line for oil-transferring is 0.01 millimeter.The etching extent of hydrocracking reactor housing is 0.03 millimeter, and the etching extent of internals is 0.04 millimeter; The etching extent of high-pressure separator housing is 0.01 millimeter, and the etching extent of internals is 0.01 millimeter; The etching extent of light pressure separator housing is 0.009 millimeter, and the etching extent of internals is 0.009 millimeter; The etching extent of hydrogen and overhead product interchanger hydrogen gas side housing is 0.01 millimeter, the etching extent of reaction overhead product side is 0.01 millimeter, the etching extent of the oily feeding side housing of stock oil and overhead product interchanger is 0.01 millimeter, and the etching extent of reaction overhead product side is 0.01 millimeter; The etching extent of reaction overhead product air cooler pipe end ingress is 0.8 millimeter; The etching extent of solvent regeneration tower air cooler is 0.01 millimeter, the etching extent of depriving hydrogen sulphide stripping tower air cooler is 0.01 millimeter, the etching extent of stock oil process furnace is 0.01 millimeter, and the etching extent of stripping tower process furnace is 0.01 millimeter, and the etching extent of stock oil line is 0.01 millimeter.The etching extent of delayed coking equipment process furnace convection tubes is 0.02 millimeter, the etching extent of radiator tube is 0.02 millimeter, the etching extent of radiation section inlet line is 0.04 millimeter, the etching extent of radiation section egress line is that etching extent is 0.02 millimeter, the etching extent of separation column tower body is 0.02 millimeter, the etching extent of tower tray is 0.03 millimeter, the etching extent of cat head catch pot is 0.02 millimeter, the etching extent of fractionation cat head water cooler tube bank is 0.02 millimeter, the etching extent of air cooler tube bundle is 0.02 millimeter, the etching extent of separation column bottom line is 0.03 millimeter, the etching extent that absorbs the stabilizer tower bottom line is 0.02 millimeter, and the etching extent of stripping tower is 0.02 millimeter, and the etching extent of coke drum upper and lower is respectively 0.02 millimeter and 0.03 millimeter, the etching extent of stock oil line is 0.04 millimeter, and the etching extent of wax oil line is 0.04 millimeter.
Embodiment 4
This embodiment is used to illustrate the corrosion-resistant processing method of crude oil with high acid content provided by the invention.
Method according to embodiment 3 is that the PL19-3 crude oil that 3.5 milligrams of KOH/ restrain carries out processing treatment to acid number content, and different is that wherein the Mo content among the 316L of device and atmospheric and vacuum distillation is 2 weight %.Found that the equipment continuous operation is after 1 year, use the corrosion at position of this 316L obviously serious than embodiment 3, etching extent is all than embodiment 3 serious 50-80%.

Claims (31)

1. the corrosion-resistant processing method of a crude oil with high acid content is characterized in that, this method may further comprise the steps:
(1) described crude oil with high acid content is cut, obtain a plurality of distillates;
(2) measure the acid number of each distillate;
(3) determine the material of equipment used in the treating processes of described crude oil with high acid content according to above-mentioned acid number.
2. method according to claim 1, wherein, the acid number of described crude oil with high acid content is 3-5mgKOH/g, the method of described cutting comprises carries out atmospheric and vacuum distillation with crude oil with high acid content, obtain the overhead gas component, boiling range be 30 ℃ to less than 165 ℃ first distillate, boiling range is 165-360 ℃ second distillate, boiling range is 360-450 ℃ the 3rd distillate, boiling range is 450-520 ℃ the 4th distillate, boiling range be 520-545 ℃ the 5th distillate and boiling range greater than 545 ℃ tower at the bottom of residual oil, the acid number that records described first distillate is 10-20mgKOH/100mL, the acid number of described second distillate is 250-300mgKOH/100mL, boiling range is that the acid number of the distillate of 360-400 ℃ distillate and 400-450 ℃ is respectively 3.5-4.5mgKOH/g in described the 3rd distillate, 3-4mgKOH/g, described boiling range is that the acid number of the 4th distillate is 3-5mgKOH/g, the acid number of described the 5th distillate is 3-5mgKOH/g, the acid number of residual oil is 1-3mgKOH/g at the bottom of the described tower, described first distillate is carried out catalytic reforming under the catalytic reforming condition, distillate A or distillate B contacted with hydrocracking catalyst under hydrocracking condition carry out hydrocracking, described distillate A is described second distillate and the 3rd distillate, described distillate B is described second distillate and the 3rd distillate and to small part the 4th distillate, with described the 5th distillate or described the 5th distillate and at least remainder the 4th distillate under catalytic cracking condition, carry out catalytic cracking, residual oil at the bottom of the described tower is carried out delayed coking.
3. method according to claim 2, wherein, described atmospheric and vacuum distillation carries out in device and atmospheric and vacuum distillation, described device and atmospheric and vacuum distillation comprises atmospheric tower, atmospheric pressure kiln to the atmospheric tower heat supply, vacuum distillation tower and to the vacuum furnace of vacuum distillation tower heat supply, described atmospheric tower and vacuum distillation tower comprise tower body and tower tray separately, the number of plies of the tower tray of described atmospheric tower is more than 40, described atmospheric pressure kiln and vacuum furnace comprise convection tubes and radiator tube separately, described atmospheric tower be Monel metal in the 40th layer of tower tray to the material of the tower body between the cat head, 0Cr13,316L, SAF2205, the metal composite of one or more among SAF2507 and the SAF2304 and carbon steel, the material of tower tray are Monel metal, 0Cr13,316L, SAF2205, among SAF2507 and the SAF2304 one or more;
Material to the tower body between the 40th layer of tower tray at the bottom of the tower of described atmospheric tower is the metal composite of 316L and carbon steel, and the material of 28-39 layer tower tray is the 0Cr13 material, and the material of 1-28 layer tower tray is 316L;
The material of the tower body of described vacuum distillation tower is the metal composite of 316L and carbon steel, and the material of the 2 layers of filler in top of described vacuum distillation tower is the 316L material, and the material of other filler is 317L;
The material of the convection tubes of described atmospheric pressure kiln is one or more among Monel metal, 0Cr13,316L, SAF2205, SAF2507 and the SAF2304, and the material of radiator tube is one or more among Monel metal, 0Cr13,316L, SAF2205, SAF2507 and the SAF2304;
The material of the convection tubes of described vacuum furnace is one or more among Monel metal, 0Cr13,316L, SAF2205, SAF2507 and the SAF2304, and the material of radiator tube is one or more among Monel metal, 0Cr13,316L, SAF2205, SAF2507 and the SAF2304.
4. method according to claim 3, wherein, described metal composite obtains by the explosive welding connection, the 40th layer of tower tray that is used as described atmospheric tower is to the metal composite of the material of the tower body between the cat head, Monel metal, 0Cr13,316L, SAF2205, one or more total thickness is the 3-5 millimeter among SAF2507 and the SAF2304, as at the bottom of the tower of described atmospheric tower to the 316L and carbon steel metal composite of the material of the tower body between the 40th layer of tower tray, the thickness of 316L is the 3-5 millimeter, in the metal composite as the 316L of the material of the tower body of described vacuum distillation tower and carbon steel, the thickness of 316L is the 3-5 millimeter.
5. method according to claim 3, wherein, described device and atmospheric and vacuum distillation also comprises the air cooler of the cat head that is positioned at atmospheric tower and/or vacuum distillation tower, the material of the bobbin carriage of described air cooler is a carbon steel, and the material of the tube bank of described air cooler is one or more in titanium, 0Cr13,316L, SAF2205, SAF2507, SAF2304 and the Monel metal.
6. method according to claim 3, wherein, described device and atmospheric and vacuum distillation also comprises and is used to make that vacuum residuum and crude oil carries out heat exchange subtracts slag crude oil shell side interchanger, this subtracts housing, the bobbin carriage of slag crude oil shell side interchanger, the material of tube sheet is the metal composite of 316L and/or 304L and carbon steel, and the material of tube bank is 316L and/or 304L.
7. method according to claim 6, wherein, obtain by the explosive welding connection as the described 316L of the material of the described housing that subtracts slag crude oil shell side interchanger, bobbin carriage, tube sheet and/or the metal composite of 304L and carbon steel, and wherein the thickness of 316L and 304L is the 3-5 millimeter.
8. according to any described method among the claim 3-7, wherein, Mo content is not less than 2.5 weight % among the described 316L.
9. method according to claim 3, wherein, the stage number of described atmospheric tower is the 40-60 piece, tower top temperature is 110-125 ℃, and the trim the top of column temperature is 30-60 ℃, and inlet temperature of stabilizer is 350-370 ℃, the cat head residual voltage of described vacuum distillation tower is not more than 3kPa, tower top temperature is for being not more than 75 ℃, and column bottom temperature is 340-360 ℃, and the top pumparound temperature is 35-40 ℃.
10. method according to claim 1, wherein, it is that 165-360 ℃ second distillate carries out hydrocracking under the middle pressure hydrocracking condition that the method that distillate A or distillate B are carried out hydrocracking comprises boiling range, is that the 4th distillate that 360-450 ℃ the 3rd distillate and part boiling range are 450-520 ℃ carries out hydrocracking under the high-pressure hydrocracking condition with boiling range.
11. method according to claim 10, wherein, the condition of described middle pressure hydrocracking comprises that temperature is 250-450 ℃, and pressure is the 10-15 MPa, and liquid hourly space velocity is 0.5-1.5 hour -1, hydrogen to oil volume ratio is 100-1000; The condition of described high-pressure hydrocracking comprises that temperature is 250-450 ℃, and pressure is the 12-20 MPa, and liquid hourly space velocity is 0.5-1.5 hour -1, hydrogen to oil volume ratio is 100-1000.
12. according to claim 2,10 or 11 described methods, wherein, described hydrocracking is carried out in hydrocracking equipment, described hydrocracking equipment comprises hydrocracking reactor, high-pressure separator and light pressure separator, the material of the housing of described hydrocracking reactor is for containing chromemolybdenum steel, the metal composite of TP316L and TP309L, the material of the internals of described hydrocracking reactor is TP316L, the material of the housing of described high-pressure separator is for containing chromemolybdenum steel, the metal composite of TP309L and TP316L, the material of the internals of described high-pressure separator is TP316L, and the material of the housing of described light pressure separator is anti-hydrogen induced cracking (HIC) soft steel.
13. method according to claim 12, wherein, described metal composite is by obtaining at chromemolybdenum steel surface overlaying TP309L and TP316L, in the material as the housing of hydrocracking reactor, the thickness of described TP316L overlay cladding and TP309L overlay cladding is the 4-7 millimeter, the thickness of chromemolybdenum steel is the 205-280 millimeter, and the thickness of TP309L is the 3-4 millimeter; In the material as the housing of described high-pressure separator, the thickness of chromemolybdenum steel is the 180-200 millimeter, and the thickness of described TP316L overlay cladding and 309L overlay cladding is the 4-7 millimeter, and the thickness of TP316L is the 3-4 millimeter.
14. method according to claim 12, wherein, described hydrocracking equipment also comprises the isocrackate air cooler, described isocrackate air cooler comprises bobbin carriage and tube bank, the material INCOLOY825 of described bobbin carriage, the material of described tube bank is INCOLOY825, and described bobbin carriage ingress is lined with titanium.
15. method according to claim 14, wherein, the length of lining titanium is 300-600mm.
16. method according to claim 12, wherein, described hydrocracking equipment also comprises hydrocracking raw material oil line, described hydrocracking raw material oil line comprises with oily first feeding line that contacts of the hydrocracking raw material that is lower than 220 ℃, is 220-288 ℃ oily second feeding line that contacts of hydrocracking raw material, is higher than 288 ℃ oily the 3rd feeding line that contacts of hydrocracking raw material with temperature with temperature, the material of described first feeding line is a carbon steel, the material of described second feeding line is 316L and/or 321, and the material of described the 3rd feeding line is 316L.
17. method according to claim 12, wherein, described hydrocracking equipment comprises also and is used to make the interchanger that carries out heat exchange between hydrogen and the isocrackate that the material of this interchanger is the metal composite that contains TP316L, TP309L and chromemolybdenum steel.
18. method according to claim 12, wherein, as the described metal composite of the material of this interchanger by obtaining at chromemolybdenum steel surface overlaying TP316L and TP309L, wherein the thickness of chromemolybdenum steel is the 200-280 millimeter, the thickness of TP316L is the 3-4 millimeter, and the total thickness of TP316L and TP309L is the 4-7 millimeter.
19. method according to claim 12, wherein, described hydrocracking equipment also comprises and is used to make the interchanger that carries out heat exchange between hydrocracking raw material oil and the isocrackate, wherein the material of the housing of hydrocracking raw material oil side is the metal composite that contains TP316L, TP309L and chromemolybdenum steel, and the material of traverse baffle is TP316L; The material of the bobbin carriage of isocrackate side is the metal composite that contains TP316L, TP309L and chromemolybdenum steel.
20. method according to claim 19, wherein, as the described metal composite of the material of this interchanger by obtaining at chromemolybdenum steel surface overlaying TP316L and TP309L, wherein the thickness of chromemolybdenum steel is the 200-280 millimeter, the thickness of TP316L is the 3-4 millimeter, and the total thickness of TP316L and TP309L is the 4-7 millimeter.
21. method according to claim 12, wherein, described hydrocracking equipment also comprises hydrocracking raw material oil process furnace and stripping tower process furnace, the material of described hydrocracking raw material oil process furnace is TP321 and/or 347, and the material of described stripping tower process furnace is one or more among T9, T11, the Cr5Mo.
22. method according to claim 10, wherein, this method also comprises the heavy naphtha that heavy naphtha that middle pressure hydrocracking is obtained and high-pressure hydrocracking obtain and first distillate merges or nonjoinder after under the catalytic reforming condition, carry out catalytic reforming, the tail oil that high-pressure hydrocracking is obtained and described the 5th distillate or the 5th distillate and under catalytic cracking condition, carry out catalytic cracking after the merging of remainder the 4th distillate or the nonjoinder at least.
23. according to claim 2 or 22 described methods, wherein, the condition of described catalytic cracking comprises that temperature of reaction is 450-600 ℃, the agent oil volume is than being 1-10, and the reaction times is 0.2-8 second, and reaction pressure is 300-500 kPa.
24. according to claim 2 or 22 described methods, wherein, the condition of described catalytic reforming comprises that weighted average bed temperature is 480-520 ℃, pressure is 0.2-0.5MPa, and volume space velocity is 0.1-1.5h -1, the hydrogen oil molecule is than being 2-3.
25. method according to claim 10, wherein, this method comprises that also wax oil that delayed coking is obtained carries out high-pressure hydrocracking as the raw material of high-pressure hydrocracking.
26. according to claim 1 or 25 described methods, wherein, described delayed coking is carried out in delayed coking equipment, described delayed coking equipment comprises process furnace, separation column and coke drum, described process furnace comprises convection tubes, radiator tube, radiation section inlet line, radiation section egress line, and wherein, the material of described convection tubes and radiator tube is T9 and/or 321H, the material of described radiation section inlet line is 1CrMo5 and/or 321, and the material of described radiation section egress line is P9 and/or 316L.
27. method according to claim 26, wherein, the coke drum of described delayed coking equipment comprises the upper and lower, described top is that the top of coke drum is to 200 millimeters section below the foam layer, the residue section is the bottom, the material on described top is 405 and/or the metal composite of 410S and 14Cr1MoR, and the material of bottom is 14Cr1MoR and/or 15Cr1MoR.
28. method according to claim 27, wherein, described metal composite is obtained by the explosive welding connection, 405 and the thickness of 410S be the 3-5 millimeter.
29. method according to claim 28, wherein, the separation column of described delayed coking equipment comprises tower body and tower tray, and the temperature according to the contact raw material is divided into first section, second section and the 3rd section from top to bottom from low paramount described separation column, the material of described first section tower body is a carbon steel, and the material of tower tray is 410S; The material of described second section tower body is the metal composite of carbon steel and 410S, and the material of tower tray is 304; The material of described the 3rd section tower body is the metal composite of carbon steel and 321, and the material of tower tray is 321.
30. method according to claim 29, wherein, described metal composite is obtained by the explosive welding connection, in the metal composite of described carbon steel and 410S, the thickness of 410S is the 3-5 millimeter, and in described carbon steel and 321 the metal composite, 321 thickness is the 3-5 millimeter.
31. method according to claim 26, wherein, the condition of described delayed coking comprises that the working pressure of coke cat head is 0.15-0.17MPa, the furnace outlet temperature is 495-505 ℃, the coke tower top temperature is 420-440 ℃, fractionation tower temperature is 110-120 ℃, and fractionator bottom temperature is 380-400 ℃, and combined cycle is than being 0.2-0.4.
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103102983A (en) * 2011-11-10 2013-05-15 中国石油化工股份有限公司 Delayed coking-hydrorefining process for shale oil
CN103965958A (en) * 2013-01-30 2014-08-06 中国石油天然气股份有限公司 Method for processing acid-containing oil
CN109575982A (en) * 2018-10-12 2019-04-05 中国石油大学(华东) A kind of method of crude oil preparing low-carbon olefin by catalytically cracking and aromatic hydrocarbons

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103102983A (en) * 2011-11-10 2013-05-15 中国石油化工股份有限公司 Delayed coking-hydrorefining process for shale oil
CN103102983B (en) * 2011-11-10 2015-02-18 中国石油化工股份有限公司 Delayed coking-hydrorefining process for shale oil
CN103965958A (en) * 2013-01-30 2014-08-06 中国石油天然气股份有限公司 Method for processing acid-containing oil
CN103965958B (en) * 2013-01-30 2015-12-02 中国石油天然气股份有限公司 A kind of working method containing sour oil
CN109575982A (en) * 2018-10-12 2019-04-05 中国石油大学(华东) A kind of method of crude oil preparing low-carbon olefin by catalytically cracking and aromatic hydrocarbons

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