CN115181584B - Production process and system of residue type low-sulfur marine fuel oil - Google Patents
Production process and system of residue type low-sulfur marine fuel oil Download PDFInfo
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- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 112
- 239000011593 sulfur Substances 0.000 title claims abstract description 112
- 239000010762 marine fuel oil Substances 0.000 title claims abstract description 90
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 53
- 239000003921 oil Substances 0.000 claims abstract description 191
- 238000002156 mixing Methods 0.000 claims abstract description 106
- 238000006243 chemical reaction Methods 0.000 claims abstract description 97
- 238000000034 method Methods 0.000 claims abstract description 62
- 230000008569 process Effects 0.000 claims abstract description 59
- 239000000203 mixture Substances 0.000 claims abstract description 50
- 238000007385 chemical modification Methods 0.000 claims abstract description 22
- 230000006641 stabilisation Effects 0.000 claims abstract description 14
- 238000011105 stabilization Methods 0.000 claims abstract description 14
- 238000000265 homogenisation Methods 0.000 claims abstract description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 78
- 239000000295 fuel oil Substances 0.000 claims description 55
- 238000003860 storage Methods 0.000 claims description 33
- 230000003197 catalytic effect Effects 0.000 claims description 30
- 238000002347 injection Methods 0.000 claims description 29
- 239000007924 injection Substances 0.000 claims description 29
- 230000000087 stabilizing effect Effects 0.000 claims description 28
- 239000002002 slurry Substances 0.000 claims description 23
- 238000004939 coking Methods 0.000 claims description 19
- 238000004227 thermal cracking Methods 0.000 claims description 15
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 11
- 239000005977 Ethylene Substances 0.000 claims description 11
- 230000003111 delayed effect Effects 0.000 claims description 10
- 239000012530 fluid Substances 0.000 claims description 10
- 239000010426 asphalt Substances 0.000 claims description 7
- 239000012752 auxiliary agent Substances 0.000 claims description 5
- 238000004231 fluid catalytic cracking Methods 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 3
- 238000007872 degassing Methods 0.000 claims description 2
- 238000005194 fractionation Methods 0.000 claims description 2
- 238000012546 transfer Methods 0.000 claims description 2
- 239000005864 Sulphur Substances 0.000 claims 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 99
- 239000002283 diesel fuel Substances 0.000 description 26
- 238000010791 quenching Methods 0.000 description 14
- 230000000171 quenching effect Effects 0.000 description 13
- 239000002994 raw material Substances 0.000 description 10
- 239000011269 tar Substances 0.000 description 8
- 238000011156 evaluation Methods 0.000 description 7
- 239000000446 fuel Substances 0.000 description 7
- 230000004048 modification Effects 0.000 description 7
- 238000012986 modification Methods 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000000084 colloidal system Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 5
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 239000010763 heavy fuel oil Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- 230000032798 delamination Effects 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 238000006011 modification reaction Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 239000010703 silicon Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 238000005299 abrasion Methods 0.000 description 2
- -1 amide compounds Chemical class 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 2
- VZSRBBMJRBPUNF-UHFFFAOYSA-N 2-(2,3-dihydro-1H-inden-2-ylamino)-N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]pyrimidine-5-carboxamide Chemical compound C1C(CC2=CC=CC=C12)NC1=NC=C(C=N1)C(=O)NCCC(N1CC2=C(CC1)NN=N2)=O VZSRBBMJRBPUNF-UHFFFAOYSA-N 0.000 description 1
- YLZOPXRUQYQQID-UHFFFAOYSA-N 3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]propan-1-one Chemical compound N1N=NC=2CN(CCC=21)CCC(=O)N1CCN(CC1)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F YLZOPXRUQYQQID-UHFFFAOYSA-N 0.000 description 1
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229920002367 Polyisobutene Polymers 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002641 tar oil Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a production process and a system of residue type low-sulfur marine fuel oil, wherein the production process of the residue type low-sulfur marine fuel oil comprises the following steps: the low-quality heavy component is subjected to chemical modification to generate high-temperature modified oil gas, the high-temperature modified oil gas and the blending component are subjected to contact mixing reaction under the high-temperature condition, and the obtained mixture is subjected to homogenization and stabilization, and the light component in the mixture is separated, so that the residue type low-sulfur marine fuel oil is obtained. The process provided by the invention has the advantages of simple flow and low energy consumption, and the uniformity and stability of the obtained low-sulfur marine fuel oil product are greatly improved.
Description
Technical Field
The invention relates to a production process and a production system of residue type low-sulfur marine fuel oil, and belongs to the technical field of petroleum refining.
Background
Marine fuel oil is a main power source of ocean vessels, and mainly comprises light diesel oil, heavy diesel oil, fuel oil and residual oil type fuel oil, and specifically comprises the following components: 0# diesel oil, -10# diesel oil, 20# heavy diesel oil, 4# fuel oil, 120# fuel oil, 180# fuel oil, 380# fuel oil, and the like. According to the tonnage of the ship, various ships need different brands of fuel. In recent years, due to the improvement of environmental protection requirements, the demand of road fuel is shrinking, the global fuel consumption is generally reduced, but the demand of marine fuel is vigorous under the drive of continuous increase of global maritime trade.
Marine fuel oils are classified into distillate type and residue type according to quality. After 2015, the sulfur content of the fraction type marine fuel oil is generally required to be not more than 0.1%, corresponding requirements can be met by hydrodesulfurizing the blending components, the technical route is mature, and therefore the requirements have little influence on the production of the future fraction type marine fuel oil. However, for the residue type marine fuel oil, a large adjustment of the production process is required to achieve the requirement that the sulfur content is not more than 0.5%. Even if the sulfur content of straight-run residuum of low sulfur crude oil is not more than 0.5%, it is necessary to carry out desulfurization treatment to produce satisfactory ship fuel oil, and the primary investment and processing cost of the conventional residuum hydrogenation apparatus are high, resulting in an increase in production cost.
In order to reduce the burden on the transportation industry, the fuel supply link has been dedicated to reducing the cost of marine fuel oil. Therefore, the production mode mainly comprises two routes of raw material preference, component modification and product blending. The main raw materials for production comprise low-value components such as vacuum residuum, catalytic slurry oil, coker wax oil, ethylene tar oil and the like, and high-value components such as catalytic diesel oil, coker diesel oil and the like with different blending proportions are also required to be added for adjusting indexes such as viscosity, pour point and the like. The global main petroleum enterprises are beginning to research the low-sulfur marine fuel oil production technology, and the partial hydro-conversion modification technology can realize the low-sulfur marine fuel oil (marine combustion) production. However, for economic reasons, multi-component blending is always the most important measure for producing low-sulfur marine fuel, the traditional production mode of marine fuel is tank type batch blending, cleanliness and compatibility of the marine fuel produced by blending are important considerations, blending component selection and matching are key for producing qualified fuel, and residue type marine fuel doped with non-petroleum-based raw materials can meet the requirements of national standard marine fuel in terms of indexes, but in actual use, problems such as blockage of a fuel supply system, abrasion of a high-pressure oil pump and a nozzle, poor combustion performance and the like can occur.
The common oil blending process is divided into batch blending of oil tanks and continuous blending of pipelines. The domestic marine fuel oil blending is mainly tank type batch blending, single quantitative production is carried out, and components to be blended are mixed according to a specified blending proportion by methods of pump circulation, electric stirring and the like, and intermittent operation is carried out. The method has the advantages of simple operation, no influence of fluctuation of component oil quality, but the defects of multiple component tanks, long blending period, easy oxidation, inaccurate proportion and the like, and the stability of the oil product needs to be improved. Another oil blending process is continuous blending in pipelines, and most of mixing elements for continuous blending in pipelines adopt static mixers, and the mixing is realized by changing the flowing direction of fluid through various elements in the pipelines. Chinese patent CN201969532U discloses a marine fuel oil blending device, which adopts the technical scheme that: the light and heavy blending components respectively enter a static mixer and a colloid mill in sequence through a valve, a pipeline and a flowmeter so as to realize component mixing and colloid refinement. However, for light and heavy components with large density and viscosity difference, uniform mixing is difficult to realize, oil products are easy to delaminate, colloid particles are difficult to uniformly mix although the particle size of the oil products is small after the oil products enter a colloid mill for refining, and the power of the used colloid mill is high and the energy consumption is high. Chinese patent CN206325416U discloses a residue type marine fuel oil blending device, and the technical scheme is: the heavy oil, the reflux blending oil and the light oil are connected through the component oil tank, the three groups of static mixers and the shearing mixing unit, so that the viscosity of the mixed oil is reduced step by step, and the problem of uneven local mixing caused by large viscosity and density difference of the mixed oil is avoided to a certain extent.
In addition to sulfur content limitations, marine fuel oils are specified for such metrics as kinematic viscosity, density, cetane index, carbon aromaticity index (CCAI), flash point, hydrogen sulfide, acid number, total deposit, oxidation stability, carbon residue, cold filter point, cloud point, pour point, appearance, moisture, ash, vanadium, sodium, aluminum + silicon, net heat value, lubricity, used lubricating oil, etc., and different grades of fuel oils have different requirements for each project.
The kinematic viscosity is a main basis for classifying the fuel oil grade, the density can be used as a basis for the fuel oil quality, and the marine fuel oil blending production process generally firstly considers three indexes of density, kinematic viscosity and sulfur content; flash point is an effective indicator for evaluating the risk of a fuel oil fire, and the flash point of a light fraction can directly affect the flash point of a blended fuel oil product; the existence of the moisture can reduce the heat value of the fuel oil and influence the mechanical combustion performance of the fuel; ash refers to inorganic matters obtained by carbonizing fuel oil and calcining the fuel oil under specified conditions, so that the heat transfer efficiency is affected, aluminum and silicon are mainly derived from catalyst powder remained in residual oil, abrasion can be generated on combustion equipment, and indexes such as ash, aluminum and silicon limit the use of low-value blending components such as catalytic slurry oil and the like; high sodium and vanadium contents can cause "hot corrosion" that damages the components of the oil extraction machine and aggravates the total ash, creating deposition problems.
Catalytic slurry oil and coked wax oil generally have the characteristics of low sulfur and low cost, but often contain solid matters, which affect the usability of the blended product. Chinese patent CN203007222U discloses a process and apparatus for producing marine fuel oil by using catalytic slurry oil, distilling the catalytic slurry oil at the bottom of a catalytic cracking fractionating tower by a vacuum fractionating tower, separating two parts of overhead slurry oil and bottom topped slurry oil, pumping the slurry oil into a dewatering storage tank by a pump, selling the slurry oil as marine residue fuel oil meeting national standards, or pumping the dewatered slurry oil out by a pump, mixing the slurry oil with blending components in a pipeline, entering a blending storage tank after passing through a venturi mixer, blending with diesel oil to produce distillate type marine fuel oil meeting national standard requirements, or blending with residual oil to produce residue type marine fuel oil meeting national standard requirements. Chinese patent CN106753611a discloses a marine fuel oil and its production process and apparatus, which adopts catalytic slurry oil, catalytic diesel oil, vacuum residue oil, shale oil, coal tar, methanol, ethanol and auxiliary agent to blend according to a certain proportion to produce 180# product meeting the requirements, adopts low-value raw materials to reduce production cost to the maximum extent, and adopts various blending components to flexibly switch to cope with price fluctuation of the raw materials. The device adopts an upper structure and a lower structure, the upper part is a blending kettle with a heating function, the lower part is connected with an electrostatic separation device, and a three-electrode electrostatic separation mode is adopted to purify raw materials so as to improve the addition amount of low-value catalytic slurry oil, reduce the production cost and improve the utilization rate of the internal space of the device.
The oil blending technology is mature in the field of finished oil, and because the source of the finished oil blending raw materials is stable, the optimal blending ratio can be solved according to the feasible region defined by the known index prediction model; for marine fuel oil, the related technology is still immature, the blending raw materials are numerous in variety, mainly low-value inferior oil products, the property and price fluctuation are large, the properties of the same oil products in different batches are also greatly different, and the difficulty of blending uniform and stable products is large. Heavy blending components such as vacuum residuum, asphalt and the like have large viscosity and high pour point, and the heavy blending components are reduced in viscosity and viscosity by modifying means, so that the compatibility of the blending components is optimized, the dosage of the light blending components is reduced, and a more economical production formula can be formed. Chinese patent CN202530048U discloses a device for hydrogen-supplied thermal cracking of inferior heavy oil, which realizes low-cost modification, reduces viscosity of extra heavy oil, and improves API. Chinese patent CN106883873a discloses a method for upgrading and reducing viscosity of inferior heavy oil, which can produce low-viscosity upgraded crude oil in maximum, meet the requirements of storage and transportation, and have low investment, and can ensure the stability of the upgraded oil.
Through prior art analysis, hydrocracking technology can directly produce acceptable low sulfur marine combustion products, but requires significant primary investment and higher operating costs. Other production technologies all need at least two links, namely heavy component modification is firstly carried out, tank or pipeline blending is adopted later, the production flow is longer, and the uniformity and stability of the blended product are poor.
Therefore, providing a novel production process and system of residue type low-sulfur marine fuel oil, which can reduce production cost and improve stability of the obtained product, has become a technical problem to be solved in the art.
Disclosure of Invention
In order to solve the above-mentioned disadvantages and shortcomings, an object of the present invention is to provide a process for producing residue type low sulfur marine fuel oil.
The invention also aims at providing a production system of the residue type low-sulfur marine fuel oil.
In order to achieve the above object, in one aspect, the present invention provides a process for producing a residue type low sulfur marine fuel oil, wherein the process for producing a residue type low sulfur marine fuel oil comprises:
the low-quality heavy component is subjected to chemical modification to generate high-temperature modified oil gas, the high-temperature modified oil gas and the blending component are subjected to contact mixing reaction under the high-temperature condition, and the obtained mixture is subjected to homogenization and stabilization, and the light component in the mixture is separated, so that the residue type low-sulfur marine fuel oil is obtained.
As a specific embodiment of the above process of the present invention, wherein the process further comprises continuing to add the blending component to the mixture after separation of the light components to increase the yield of the low sulfur marine fuel oil.
As a specific embodiment of the above process of the present invention, the process further comprises adding an auxiliary agent to the blending component to further improve the quality of the low sulfur marine fuel oil.
In the invention, the auxiliary agent comprises one or more of benzene, alcohol, amine, phenol, sulfonic acid, phenol, amide compounds and derivatives thereof which are substituted by alkyl.
As a specific embodiment of the above process of the present invention, the low-quality heavy component includes one or a mixture of several of oil refining chemical secondary processing products such as residual oil, catalytic slurry oil, coker gas oil, ethylene tar, deoiled asphalt, etc.
Wherein the residuum includes atmospheric residuum, vacuum residuum, mixtures thereof, and the like.
As a specific embodiment of the above process of the present invention, the chemical modification includes one or a combination of several of visbreaking, hydrogen-donating thermal cracking, hydro-thermal cracking, fluidized thermal conversion, delayed coking, and heavy oil hydro-conversion.
The visbreaking, hydrogen-supplying thermal cracking, hydrogen-critical thermal cracking, fluidization thermal conversion, delayed coking and heavy oil hydro-conversion processes used in the invention are all conventional processes, and the technical parameters used in the processes can be reasonably set by a person skilled in the art according to the actual operation needs on site, so long as the purpose of the invention can be realized.
As a specific embodiment of the above process of the present invention, the heavy oil hydroconversion comprises one or a combination of several of fixed bed, suspended bed, ebullated bed, moving bed heavy oil hydrogenation processes.
The fixed bed, the suspension bed, the ebullated bed and the moving bed heavy oil hydrogenation processes used in the invention are all conventional processes, and the technical parameters and the like used in the processes can be reasonably set by a person skilled in the art according to the actual operation needs on site, so long as the purpose of the invention can be realized.
As a specific embodiment of the above process of the present invention, wherein the fluidized thermal conversion comprises one or a combination of several of fluid coking, flexicoking, fluid catalytic cracking and circulating fluid bed processes.
The fluid coking, flexible coking, fluid catalytic cracking and circulating fluid bed processes used in the invention are all conventional processes, and the technical parameters and the like used in the processes can be reasonably set by a person skilled in the art according to the actual operation needs on site, so long as the purpose of the invention can be realized.
As a specific embodiment of the process of the present invention, the high temperature modified oil gas is a gas-liquid mixture, and the temperature is above 360 ℃.
In the invention, the high-temperature modified oil gas at the oil gas outlet of the chemical modification unit is a gas-liquid mixture with the temperature of more than 360 ℃. In the conventional process in the field, the oil gas enters a fractionation unit after heat exchange or cooling, and the separated partial fraction is conveyed to a tank area to be blended with other components in a product formula to produce a standard product.
As a specific embodiment of the process, the blending component comprises one or a mixture of a plurality of catalytic diesel oil, catalytic slurry oil, hydrogenated residual oil, coker diesel oil, coker wax oil, ethylene tar and straight-run diesel oil.
As a specific embodiment of the process, the blending component is used in an amount of 3-100% of the high-temperature modified oil-gas quality.
As a specific embodiment of the above process of the present invention, wherein the reaction temperature of the reaction is 80 ℃ or higher;
preferably, the reaction temperature of the reaction is 120 ℃ or higher.
As a specific embodiment of the process of the present invention, a blending component is injected into one or more of an oil gas outlet of a chemical modification unit for chemical modification, an inlet of a homogenizing and stabilizing unit for homogenizing and stabilizing, and an oil gas conveying pipeline connecting the oil gas outlet and the inlet of the homogenizing and stabilizing unit, and the high-temperature modified oil gas and the blending component are contacted and mixed under a high-temperature condition for reaction.
As a specific embodiment of the above process of the present invention, wherein the low sulfur marine fuel oil has a sulfur content of less than 0.5% and a kinematic viscosity at 50 ℃ of less than 500mm 2 And/s. Unless otherwise specified, the sulfur contents described in the present invention are all weight percentages, and the kinematic viscosity is that at 50 ℃.
In the invention, the low-quality heavy component is subjected to chemical modification to generate high-temperature modified oil gas, wherein the chemical modification comprises targeted modification of indexes such as sulfur content, acid value, viscosity, pour point and the like of the low-quality heavy component, so that the low-quality heavy component meets or approximates to the quality standard of a product.
As a specific embodiment of the above process of the present invention, the process further comprises an operation of pretreating the low-quality heavy component raw material, wherein the pretreatment comprises dehydration, solid removal and purification treatment, etc.
In the invention, the mixture obtained after the high-temperature contact mixing reaction of the high-temperature modified oil gas and the blending component contains the light component, and the light component can cause the safety problem in the storage, transportation and use processes of the obtained residue type low-sulfur marine fuel oil product, so that the light component is required to be separated from the mixture in a homogenizing and stabilizing unit, the flash point of the light component is ensured to exceed 60 ℃, and the low-sulfur marine fuel oil with qualified index and uniform and stable can be obtained.
On the other hand, the invention also provides a production system of the residue type low-sulfur marine fuel oil, wherein the production system of the residue type low-sulfur marine fuel oil comprises the following components:
the device comprises a chemical modification unit, a homogenizing and stabilizing unit and/or a product storage tank, wherein at least one injection opening is arranged between an oil gas outlet of the chemical modification unit and an inlet of the homogenizing and stabilizing unit, the injection opening is used for injecting a blending component, the blending component and high-temperature modified oil gas are subjected to contact mixing reaction, and a mixture obtained by the reaction is injected into the homogenizing and stabilizing unit or the product storage tank through an oil gas conveying pipeline;
and/or a mixing section is arranged on an oil gas conveying pipeline between an oil gas outlet of the chemical modification unit and an inlet of the homogenizing and stabilizing unit, blending components and high-temperature modified oil gas are mixed and contacted in the mixing section for reaction, and the obtained mixture is injected into the homogenizing and stabilizing unit or a product storage tank through the oil gas conveying pipeline;
when the system comprises a chemical modification unit, a homogenizing and stabilizing unit and a product storage tank, the outlet of the homogenizing and stabilizing unit is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
As a specific embodiment of the system according to the present invention, when the system includes a chemical modification unit, a homogenizing and stabilizing unit, and a product tank, at least one injection port is provided between an outlet of the homogenizing and stabilizing unit and an inlet of the product tank, the injection port being used for injecting a blending component;
and/or a mixing section is arranged on the oil gas conveying pipeline between the outlet of the homogenizing and stabilizing unit and the inlet of the product storage tank.
As a specific embodiment of the above system of the present invention, the homogenizing and stabilizing unit includes one or a combination of several of a fractionating tower, a flash tower and a degassing tank.
As a specific embodiment of the system of the present invention, the chemical modification unit includes one or a combination of several of a visbreaking reaction device, a hydrogen-supplying thermal cracking reaction device, a hydro-thermal cracking reaction device, a fluidized thermal conversion reaction device, a delayed coking reaction device and a heavy oil hydro-conversion reaction device.
The visbreaking reaction device, the hydrogen-supplying thermal cracking reaction device, the hydro-thermal cracking reaction device, the fluidized thermal conversion reaction device, the delayed coking reaction device and the heavy oil hydro-conversion reaction device used in the invention are all conventional devices, and any commercially available or self-built device can be reasonably selected by a person skilled in the art according to the field operation requirement, so long as the purpose of the invention can be realized.
As a specific embodiment of the system, the heavy oil hydro-conversion reaction device comprises one or a combination of a plurality of fixed bed heavy oil hydro-conversion reaction devices, suspension bed heavy oil hydro-conversion reaction devices, ebullated bed heavy oil hydro-conversion reaction devices and moving bed heavy oil hydro-conversion reaction devices.
The fixed bed heavy oil hydroconversion reaction device, the suspension bed heavy oil hydroconversion reaction device, the ebullated bed heavy oil hydroconversion reaction device and the moving bed heavy oil hydroconversion reaction device used in the invention are all conventional devices, and any commercially available or self-built devices can be reasonably selected by a person skilled in the art according to the field operation needs, so long as the purpose of the invention can be realized.
As a specific embodiment of the above system of the present invention, the fluidized thermal conversion reaction device comprises one or a combination of several of a fluidized coking reaction device, a flexible coking reaction device, a fluidized catalytic cracking reaction device and a circulating fluidized bed reaction device.
The fluid coking reaction device, the flexible coking reaction device, the fluid catalytic cracking reaction device and the circulating fluid bed reaction device used in the invention are all conventional devices, and any commercially available or self-built devices can be reasonably selected by a person skilled in the art according to the field operation requirement, so long as the purpose of the invention can be realized.
As a specific embodiment of the system of the present invention, the system further comprises a pretreatment unit for pretreating the low-quality inferior heavy component raw material, wherein the pretreatment unit comprises a dehydration unit, a solid removal purification treatment unit and the like.
The invention provides a process and a system for producing residue type low-sulfur marine fuel oil by heavy component modification coupling in-situ blending, wherein the process specifically comprises the following steps: the low-quality heavy component is subjected to chemical modification to generate high-temperature modified oil gas, the high-temperature modified oil gas and the preferable blending component are subjected to contact mixing reaction under the high-temperature condition, and the obtained mixture is subjected to homogenization and stabilization, and the light component in the mixture is separated, so that the residue type low-sulfur marine fuel oil is obtained. The process provided by the invention has the advantages of simple flow and low energy consumption, and the uniformity and stability of the obtained low-sulfur marine fuel oil product are greatly improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for the description of the embodiments will be briefly described, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to the drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic diagram of delamination of rmg380# low sulfur marine fuel oil provided in example 1 of the present invention after storage for 30 days.
FIG. 2 is a schematic diagram showing delamination of the RMG380# low sulfur marine fuel oil provided in comparative example 1 after storage for 21 days.
Detailed Description
In order to make the technical features, objects and advantageous effects of the present invention more clearly understood, the technical aspects of the present invention will now be described in detail with reference to the following specific examples, but should not be construed as limiting the scope of the present invention.
System embodiment
Example 1-1
The embodiment provides a production system of residue type low-sulfur marine fuel oil, wherein the system comprises a visbreaking reaction device, a fractionating tower and a product storage tank, an oil gas outlet of the visbreaking reaction device is provided with a quenching oil injection port, the quenching oil injection port is used for injecting a blending component, the blending component is contacted and mixed with high-temperature modified oil gas at the oil gas outlet of the visbreaking reaction device, and a mixture obtained by the reaction is injected into the fractionating tower through an oil gas conveying pipeline;
the outlet of the fractionating tower is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
Example 2-2
The embodiment provides a production system of residue type low-sulfur marine fuel oil, wherein the system comprises a hydro-thermal cracking reaction device, a fractionating tower and a product storage tank, an oil gas outlet of the hydro-thermal cracking reaction device is provided with a quenching oil injection port, the quenching oil injection port is used for injecting a blending component, the blending component and high-temperature modified oil gas at the oil gas outlet of the hydro-thermal cracking reaction device are subjected to contact mixing reaction, and a mixture obtained by the reaction is injected into the fractionating tower through an oil gas conveying pipeline;
the outlet of the fractionating tower is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
Examples 3 to 3
The embodiment provides a production system of residue type low-sulfur marine fuel oil, wherein the system comprises a circulating fluidized bed reaction device, a fractionating tower and a product storage tank, an oil gas outlet of the circulating fluidized bed reaction device is provided with a quenching oil injection port, the quenching oil injection port is used for injecting a blending component, the blending component is contacted and mixed with high-temperature modified oil gas at the oil gas outlet of the circulating fluidized bed reaction device, and a mixture obtained by the reaction is injected into the fractionating tower through an oil gas conveying pipeline;
the outlet of the fractionating tower is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
Examples 4 to 4
The embodiment provides a production system of residue type low-sulfur marine fuel oil, wherein the system comprises a delayed coking reaction device, a fractionating tower and a product storage tank, an oil gas outlet of the delayed coking reaction device is provided with a quenching oil injection port, the quenching oil injection port is used for injecting a blending component, the blending component is in contact and mixed reaction with high-temperature modified oil gas at the oil gas outlet of the delayed coking reaction device, and a mixture obtained by the reaction is injected into the fractionating tower through an oil gas conveying pipeline;
the outlet of the fractionating tower is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
Examples 5 to 5
The embodiment provides a production system of residue type low-sulfur marine fuel oil, wherein the system comprises a visbreaking reaction device, a heavy oil hydroconversion device, a fractionating tower and a product storage tank, wherein the visbreaking reaction device is connected with the heavy oil hydroconversion device through a pipeline, an oil gas outlet of the heavy oil hydroconversion device is provided with a quenching oil injection port, the quenching oil injection port is used for injecting blending components, the blending components and high-temperature modified oil gas at the oil gas outlet of the heavy oil hydroconversion device are subjected to contact mixing reaction, and a mixture obtained by the reaction is injected into the fractionating tower through an oil gas conveying pipeline;
the outlet of the fractionating tower is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
Examples 6 to 6
The embodiment provides a production system of residue type low-sulfur marine fuel oil, wherein the system comprises a fluidized thermal conversion reaction device, a fractionating tower and a product storage tank, a mixing section is arranged on an oil gas conveying pipeline between an oil gas outlet of the fluidized thermal conversion reaction device and the fractionating tower, blending components and high-temperature modified oil gas are in contact mixing reaction in the mixing section, and a mixture obtained by the reaction is injected into the fractionating tower through the oil gas conveying pipeline;
the outlet of the fractionating tower is connected with the inlet of the product storage tank through an oil gas conveying pipeline, and a mixing section is also arranged on the oil gas conveying pipeline between the outlet of the fractionating tower and the inlet of the product storage tank.
Process examples
Example 1
The present embodiment provides a production process of a residue type low sulfur marine fuel oil, wherein the process is implemented by using the production system of the residue type low sulfur marine fuel oil provided in embodiment 1-1, which comprises the following steps:
the sulfur content of a vacuum residue is 0.82%, and the kinematic viscosity is 68200mm 2 And/s, enabling the vacuum residuum to enter a visbreaking reaction device, reacting for 30min at 425 ℃ to generate high-temperature modified oil gas, wherein the temperature of the high-temperature modified oil gas is 416 ℃, and injecting catalytic diesel oil into a quenching oil injection port of an oil gas outlet at the top of the visbreaking reaction device, wherein the kinematic viscosity of the catalytic diesel oil is 5mm 2 The sulfur content is 0.10%, the injection amount is 12% of the quality of high temperature modified oil gas, the high temperature modified oil gas is contacted and mixed with catalytic diesel oil and is stabilized at 360 ℃, the mixture obtained after the reaction enters a fractionating tower for homogenizing and stabilizing, and after 1.5m% (m% represents the mass percentage content in the invention) of light components in the oil gas are separated from the top of the fractionating tower, the bottom of the fractionating tower directly obtains the light components with the quality reaching the standard (the kinematic viscosity at 50 ℃ is 355 mm) 2 RMG380# residue low sulfur marine fuel oil with sulfur content of 0.49%);
the performance of the RMG380# residue type low-sulfur marine fuel oil is evaluated according to ASTM-D2781/D4740, and the product stability is determined to be first-order after the evaluation; and the RMG380# residue type low sulfur marine fuel oil was left to stand for 30 days without delamination, as shown in fig. 1.
Example 2
The embodiment provides a production process of residue type low-sulfur marine fuel oil, wherein the process is realized by using the production system of the residue type low-sulfur marine fuel oil provided in the embodiment 2-2, and the production process comprises the following steps:
sulfur content of some heavy fuel oil is 1.65%, kinematic viscosity is 485mm 2 And/s, the heavy fuel oil enters a hydro thermal cracking reaction device, and high-temperature modified oil gas is generated after 25min desulfurization reaction under the conditions of 405 ℃ and 3.5MPa, wherein the temperature of the high-temperature modified oil gas is 390 DEG CInjecting catalytic slurry oil into a quenching oil injection port of an oil gas outlet of the hydro-thermal cracking reaction device, wherein the kinematic viscosity of the catalytic slurry oil is 185mm 2 The sulfur content is 0.25%, the injection amount is 25% of the quality of high-temperature modified oil gas, the high-temperature modified oil gas is contacted and mixed with catalytic slurry oil and is subjected to stabilization reaction at 350 ℃, the mixture obtained after the reaction enters a fractionating tower to be homogenized and stabilized, 1m% of light components in the oil gas are separated from the top of the fractionating tower, and the quality reaching the standard (the kinematic viscosity at 50 ℃ is 167 mm) is directly obtained at the bottom of the fractionating tower 2 RMG180# residue low sulfur marine fuel oil with sulfur content of 0.46% and flash point of 62 ℃;
the performance of the RMG180# residue type low sulfur marine fuel oil was evaluated according to ASTM-D2781/D4740, and the product stability was determined to be first order after the evaluation.
Example 3
The present embodiment provides a production process of a residue type low sulfur marine fuel oil, wherein the process is implemented by using the residue type low sulfur marine fuel oil system provided in embodiments 3-3, and the production process comprises the following steps:
the sulfur content of a certain atmospheric residuum is 1.05%, and the kinematic viscosity is 4395mm 2 And (3) per second, wherein the acid value is 4.4mg KOH/g, the atmospheric residuum enters a circulating fluidized bed reactor, FCC waste catalyst is adopted, high-temperature modified oil gas is generated after modification reaction under the reaction time condition of 485 ℃ and 5s, the temperature of the high-temperature modified oil gas is 480 ℃, a mixture of coker wax oil and coker diesel is introduced into a quench oil injection port of an oil gas outlet of the circulating fluidized bed reactor, and the kinematic viscosity of the mixture is 15mm 2 S, sulfur content is 0.15%, injection amount is 17% of high temperature modified oil gas mass, high temperature modified oil gas is contacted and mixed with coked wax oil and coked diesel oil mixture and is stabilized at 405 ℃, the mixture obtained after the reaction enters a fractionating tower for homogenizing and stabilizing, and after 8m% of gasoline fraction in the oil gas is separated from the top of the fractionating tower, the quality reaching the standard (the kinematic viscosity at 50 ℃ is 367 mm) is directly obtained at the bottom of the fractionating tower 2 Per s, sulfur content 0.48%) RMG380# residue low sulfur marine fuel oil;
the performance of the RMG380# residue type low sulfur marine fuel oil was evaluated according to ASTM-D2781/D4740, and the product stability was determined to be first order after the evaluation.
Example 4
The present embodiment provides a production process of a residue type low sulfur marine fuel oil, wherein the process is implemented by using the production system of the residue type low sulfur marine fuel oil provided in embodiments 4 to 4, and the production process comprises the following steps:
the sulfur content of some deoiled asphalt is 1.05%, and the kinematic viscosity is 664395mm 2 The acid value is 2.4mg KOH/g, the deoiled asphalt and the catalytic slurry oil are mixed and enter a delayed coking reaction device, high-temperature modified oil gas is generated after modification reaction under the reaction condition of 505 ℃ and 0.15Mpa and zero circulation ratio, the temperature of the high-temperature modified oil gas is 498 ℃, ethylene tar and catalytic diesel oil mixture is introduced into a quenching oil injection port of an oil gas outlet of the delayed coking reaction device, and the kinematic viscosity of the mixture is 15mm 2 S, sulfur content is 0.15%, injection amount is 30% of high temperature modified oil gas mass, high temperature modified oil gas is contacted and mixed with ethylene tar and catalytic diesel oil mixture, stabilization reaction is carried out at 395 ℃, the mixture obtained after the reaction enters a fractionating tower for homogenization and stabilization, 5m% of coked light gasoline in oil gas is separated from the top of the fractionating tower, and the quality reaching the standard (the kinematic viscosity at 50 ℃ is 357 mm) is directly obtained at the bottom of the fractionating tower 2 RMG380# residue low sulfur marine fuel oil with sulfur content of 0.49%);
the performance of the RMG380# residue type low sulfur marine fuel oil was evaluated according to ASTM-D2781/D4740, and the product stability was determined to be first order after the evaluation.
Example 5
The embodiment provides a production process of residue type low-sulfur marine fuel oil, wherein the process is realized by using the production system of the residue type low-sulfur marine fuel oil provided by the embodiments 5-5, and the production process comprises the following steps:
the sulfur content of some deoiled asphalt is 1.05%, and the kinematic viscosity is 664395mm 2 The acid value is 2.4mg KOH/g, the deoiled asphalt and the catalytic slurry oil are mixed and enter a visbreaking reaction device, and after being modified under the reaction condition of 408 ℃ and 0.6Mpa, the heavy oil is addedThe hydrogen conversion device generates high-temperature modified oil gas after desulfurization treatment under the conditions of 385 ℃ and 5.0Mpa, the temperature of the high-temperature modified oil gas is 381 ℃, ethylene tar and catalytic diesel oil mixture is injected into an injection port of an oil gas outlet of the heavy oil hydro-conversion unit, and the kinematic viscosity of the mixture is 15mm 2 And/s, sulfur content is 0.15%, injection amount is 60% of high-temperature modified oil gas mass), the high-temperature modified oil gas is contacted and mixed with ethylene tar and catalytic diesel oil mixture, and stabilization reaction is carried out at 345 ℃, the mixture obtained after the reaction enters a fractionating tower for homogenizing and stabilizing, 1.8m% of light components in the oil gas are separated from the top of the fractionating tower, and the quality reaching the standard (the kinematic viscosity at 50 ℃ is 346 mm) is directly obtained from the bottom of the fractionating tower 2 RMG380# residue low sulfur marine fuel oil with sulfur content of 0.49%);
the performance of the RMG380# residue type low sulfur marine fuel oil was evaluated according to ASTM-D2781/D4740, and the product stability was determined to be first order after the evaluation.
Example 6
The present embodiment provides a production process of a residue type low sulfur marine fuel oil, wherein the process is implemented by using the production system of the residue type low sulfur marine fuel oil provided in embodiments 6 to 6, which comprises the following steps:
the sulfur content of a certain atmospheric residuum is 1.05%, and the kinematic viscosity is 4395mm 2 And (3) per second, wherein the acid value is 4.4mg KOH/g, the atmospheric residuum enters a fluidized thermal conversion reaction device, high-temperature modified oil gas is generated after modification reaction under the reaction condition of 425 ℃ and 15min, the temperature of the high-temperature modified oil gas is 410 ℃, a mixture of coker diesel oil and ethylene tar dissolved with polyisobutene succinimidyl phenylboronic acid stabilizing additive is injected into a mixing section arranged on an oil gas outlet pipeline of the fluidized thermal conversion reaction device, and the kinematic viscosity of the mixture is 15mm 2 S, sulfur content is 0.15%, injection amount is 18% of high temperature modified oil gas mass, high temperature modified oil gas is contacted and mixed with mixture of coking diesel oil and ethylene tar dissolved with stabilizing auxiliary agent, and stabilization reaction is carried out at 397 ℃, the mixture obtained after reaction enters a fractionating tower to be homogenized and stabilized, and after 2m% of light component in oil gas is separated from tower top, the tower bottom directly obtains the product with quality reaching the standard(kinematic viscosity at 50 ℃ C. Is 367 mm) 2 Per s, sulfur content 0.48%) RMG380# residue low sulfur marine fuel oil;
the performance of the RMG380# residue type low-sulfur marine fuel oil is evaluated according to ASTM-D2781/D4740, and the product stability is determined to be first-order after the evaluation;
adding coked diesel oil into a part of RMG380# residue type low-sulfur marine fuel oil in a mixing section arranged on an oil gas conveying pipeline between an outlet of the fractionating tower and an inlet of a product storage tank, wherein the dosage of the coked diesel oil is 5% of the mass of the part of RMG380# residue type low-sulfur marine fuel oil, and the quality reaches the standard (the kinematic viscosity at 50 ℃ is 163 mm) 2 RMG180# low sulfur marine fuel oil with sulfur content of 0.45% and flash point of 62 ℃).
Comparative example 1
The present comparative example provides a process for producing low sulfur marine fuel oil, wherein the process comprises the steps of:
the sulfur content of a vacuum residue is 0.82%, and the kinematic viscosity is 68200mm 2 And/s, the vacuum residuum enters a visbreaking reaction device, high-temperature modified oil gas is generated after reaction for 30min at 425 ℃, the oil gas enters a fractionating tower after heat exchange and temperature reduction, light components are separated from the top of the fractionating tower, the obtained visbreaking heavy oil enters a storage tank, and is blended with catalytic diesel oil after standing for three days, wherein the kinematic viscosity of the catalytic diesel oil is 5mm 2 S, the sulfur content is 0.10%, the addition amount is 12% of the mass of the viscosity-reduced heavy oil, and the kinematic viscosity is 375mm after blending 2 Per s, rmg380# low sulfur marine fuel oil with sulfur content of 0.49%;
the performance of the RMG380# low sulfur marine fuel oil was evaluated according to ASTM-D2781/D4740, and after the evaluation, the product stability was determined to be secondary, and the RMG380# low sulfur marine fuel oil was layered after standing for 21 days, as shown in fig. 2;
and evaluating the performance of the RMG380# low sulfur marine fuel oil after standing and storing for 21 days according to ASTM-D2781/D4740, and determining that the stability of the product is reduced to three levels after evaluating.
Comparative example 2
The present comparative example provides a process for producing low sulfur marine fuel oil, wherein the process comprises the steps of:
sulfur content of some heavy fuel oil is 1.65%, kinematic viscosity is 485mm 2 And/s, the heavy fuel oil enters a hydro-upgrading device, and is subjected to desulfurization reaction for 25min at 405 ℃ and 3.5MPa to generate high-temperature upgraded oil gas, wherein the temperature of the high-temperature upgraded oil gas is 390 ℃, so that the high-temperature upgraded oil gas and catalytic slurry oil (the kinematic viscosity is 185 mm) 2 And/s, the sulfur content is 0.25%, the dosage is 25% of the high-temperature modified oil gas quality) is directly mixed to obtain an oil product, and the kinematic viscosity of the obtained oil product at 50 ℃ is 143mm 2 S, sulfur content 0.44%; but the flash point is 57 ℃, and the index requirement of the flash point higher than 60 ℃ in the standard of the RMG180# low-sulfur marine fuel oil product is not met.
The foregoing description of the embodiments of the invention is not intended to limit the scope of the invention, so that the substitution of equivalent elements or equivalent variations and modifications within the scope of the invention shall fall within the scope of the patent. In addition, the technical features and the technical features, the technical features and the technical invention can be freely combined for use.
Claims (13)
1. A production process of residue type low sulfur marine fuel oil, wherein the production process of residue type low sulfur marine fuel oil comprises:
the low-quality heavy component is subjected to chemical modification to generate high-temperature modified oil gas, the high-temperature modified oil gas and the blending component are subjected to contact mixing reaction under the high-temperature condition, and the obtained mixture is homogenized and stabilized, and the light component in the mixture is separated to obtain the residue type low-sulfur marine fuel oil;
wherein the chemical modification comprises one or a combination of several modes of visbreaking, hydrogen-supplying thermal cracking, fluidized thermal conversion, delayed coking and heavy oil hydro-conversion;
wherein the high-temperature modified oil gas is a gas-liquid mixture, and the temperature of the gas-liquid mixture is more than 360 ℃;
the reaction temperature of the reaction is above 345 ℃.
2. The process of claim 1, further comprising continuing to add the blending component to the mixture after separating the light components.
3. The process of claim 1 further comprising adding an auxiliary agent to the blending component to further improve the quality of the low sulfur marine fuel oil.
4. A process according to any one of claims 1 to 3, wherein the low quality heavy fraction comprises one or a mixture of several of residuum, catalytic slurry, coker gas oil, ethylene tar, deoiled asphalt.
5. The process of claim 1 wherein the heavy oil hydroconversion comprises one or a combination of fixed bed, suspended bed, ebullated bed, moving bed heavy oil hydroconversion processes.
6. The process of claim 1, wherein the fluid thermal conversion comprises one or a combination of several of fluid coking, flexicoking, fluid catalytic cracking, and circulating fluid bed processes.
7. A process according to any one of claims 1 to 3 wherein the blending component comprises one or a mixture of several of catalytic diesel, catalytic slurry, hydrogenated residuum, coker diesel, coker wax oil, ethylene tar, straight run diesel.
8. A process as claimed in any one of claims 1 to 3 wherein the blending component is present in an amount of 3 to 100% of the high temperature upgraded oil and gas mass.
9. A process according to any one of claims 1 to 3 wherein blending components are injected into one or more of the oil gas outlet of the chemical upgrading unit for chemical upgrading, the inlet of the homogenizing stabilization unit for homogenizing stabilization and the oil gas transfer line connecting the oil gas outlet and the inlet of the homogenizing stabilization unit and the high temperature upgraded oil gas is brought into contact with the blending components under high temperature conditions for mixing.
10. A process according to any one of claims 1 to 3, wherein the residual low sulphur marine fuel oil has a sulphur content of less than 0.5wt%, a kinematic viscosity at 50 ℃ of less than 500mm 2 /s。
11. A production system of a residue type low sulfur marine fuel oil for realizing the production process of a residue type low sulfur marine fuel oil according to any one of claims 1 to 10, wherein the production system of a residue type low sulfur marine fuel oil comprises: the device comprises a chemical modification unit, a homogenizing and stabilizing unit and/or a product storage tank, wherein at least one injection opening is arranged between an oil gas outlet of the chemical modification unit and an inlet of the homogenizing and stabilizing unit, the injection opening is used for injecting a blending component, the blending component and high-temperature modified oil gas are subjected to contact mixing reaction, and a mixture obtained by the reaction is injected into the homogenizing and stabilizing unit or the product storage tank through an oil gas conveying pipeline;
and/or a mixing section is arranged on an oil gas conveying pipeline between an oil gas outlet of the chemical modification unit and an inlet of the homogenizing and stabilizing unit, blending components and high-temperature modified oil gas are mixed and contacted in the mixing section for reaction, and the obtained mixture is injected into the homogenizing and stabilizing unit or a product storage tank through the oil gas conveying pipeline;
when the system comprises a chemical modification unit, a homogenizing and stabilizing unit and a product storage tank, the outlet of the homogenizing and stabilizing unit is connected with the inlet of the product storage tank through an oil gas conveying pipeline.
12. The system of claim 11, wherein when the system comprises a chemical modification unit, a homogenization stabilization unit, and a product tank, at least one injection port is disposed between an outlet of the homogenization stabilization unit and an inlet of the product tank, the injection port for injecting a blending component;
and/or a mixing section is arranged on the oil gas conveying pipeline between the outlet of the homogenizing and stabilizing unit and the inlet of the product storage tank.
13. The system of claim 11 or 12, wherein the homogeneous stabilization unit comprises one or a combination of several of a fractionation column, a flash column, a degassing tank.
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