CN111088068A - Production method of low-sulfur marine fuel oil - Google Patents
Production method of low-sulfur marine fuel oil Download PDFInfo
- Publication number
- CN111088068A CN111088068A CN201811239893.XA CN201811239893A CN111088068A CN 111088068 A CN111088068 A CN 111088068A CN 201811239893 A CN201811239893 A CN 201811239893A CN 111088068 A CN111088068 A CN 111088068A
- Authority
- CN
- China
- Prior art keywords
- oil
- fuel oil
- slurry
- unit
- hydrogenation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000011593 sulfur Substances 0.000 title claims abstract description 80
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 80
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 54
- 239000010762 marine fuel oil Substances 0.000 title claims abstract description 35
- 239000003921 oil Substances 0.000 claims abstract description 242
- 239000002002 slurry Substances 0.000 claims abstract description 133
- 230000003197 catalytic effect Effects 0.000 claims abstract description 87
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 86
- 239000003054 catalyst Substances 0.000 claims abstract description 54
- 238000006243 chemical reaction Methods 0.000 claims abstract description 54
- 238000002156 mixing Methods 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 33
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 31
- 238000000034 method Methods 0.000 claims abstract description 25
- 239000001257 hydrogen Substances 0.000 claims abstract description 21
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 20
- 239000010747 number 6 fuel oil Substances 0.000 claims abstract description 19
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 239000000463 material Substances 0.000 claims abstract description 14
- 230000009471 action Effects 0.000 claims abstract description 6
- 238000004062 sedimentation Methods 0.000 claims abstract description 4
- 239000007791 liquid phase Substances 0.000 claims abstract description 3
- 239000000295 fuel oil Substances 0.000 claims description 28
- 239000011280 coal tar Substances 0.000 claims description 20
- 238000004523 catalytic cracking Methods 0.000 claims description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 14
- 238000005352 clarification Methods 0.000 claims description 11
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 claims description 8
- 239000002699 waste material Substances 0.000 claims description 8
- 238000009835 boiling Methods 0.000 claims description 7
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 6
- 230000008569 process Effects 0.000 claims description 6
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical compound C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 5
- 239000010779 crude oil Substances 0.000 claims description 4
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 claims description 4
- 230000009467 reduction Effects 0.000 claims description 4
- 239000010426 asphalt Substances 0.000 claims description 3
- 239000002893 slag Substances 0.000 claims description 3
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 claims description 2
- 239000003245 coal Substances 0.000 claims description 2
- 235000019253 formic acid Nutrition 0.000 claims description 2
- 239000003027 oil sand Substances 0.000 claims description 2
- 239000007787 solid Substances 0.000 abstract description 21
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 1
- 239000002245 particle Substances 0.000 description 25
- 238000001914 filtration Methods 0.000 description 21
- 239000012535 impurity Substances 0.000 description 16
- 239000000843 powder Substances 0.000 description 11
- 239000000654 additive Substances 0.000 description 9
- 230000000996 additive effect Effects 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 7
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 7
- 239000000571 coke Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 239000011331 needle coke Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 2
- 230000002776 aggregation Effects 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000010941 cobalt Substances 0.000 description 2
- 229910017052 cobalt Inorganic materials 0.000 description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012065 filter cake Substances 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 229920006395 saturated elastomer Chemical group 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 2
- 229910052721 tungsten Inorganic materials 0.000 description 2
- 239000010937 tungsten Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000010835 comparative analysis Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000003828 downregulation Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Inorganic materials O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 230000003245 working effect Effects 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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
-
- 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
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 discloses a production method of low-sulfur marine fuel oil, which comprises the steps of mixing catalytic slurry oil and a first auxiliary agent, performing sedimentation separation after mixing treatment, and obtaining a first material and residue after separation; the first material enters a hydrotreating unit, hydrogenation reaction is carried out under the action of a hydrotreating catalyst and hydrogen, liquid phase effluent obtained by the reaction enters a clarifying unit, clarified oil obtained after separation is further subjected to solid-liquid separation to obtain purified oil slurry, and the purified oil slurry is mixed with poor-quality raw material hydrogenation tail oil to obtain the low-sulfur marine fuel oil. The method of the invention can not only reduce the solid content and the sulfur content of the catalytic oil slurry and produce high-quality purified oil slurry, but also produce the scarce low-sulfur bunker fuel oil at present by blending with residual oil raw materials.
Description
Technical Field
The invention belongs to the field of oil refining chemical industry, and particularly relates to a process for producing low-sulfur marine fuel oil.
Background
The MAPPOL convention provides detailed regulations on the emission control region of fuel oil sulfur content used by a ship, the limit value and the implementation time of the fuel oil sulfur content, and the sulfur content of the fuel oil for the ship is not more than 0.5% when the ship sails in a general region on the sea after 1 month 1 day 2020; when sailing in the emission control area, the sulfur content of the fuel used on the ship should not exceed 0.1 percent. Research shows that the annual low-sulfur fuel oil demand is about 300 ten thousand tons if the MAPPO convention is strictly executed to meet the use requirement of the low-sulfur fuel oil, but from the current market situation, because the sulfur content of crude oil in most production places is higher, almost no refinery which can produce fuel oil with the sulfur content of 0.5 percent or even below 0.1 percent is available all over the world, the market gap of the low-sulfur fuel oil is large, and the production enterprises have urgent technical requirements on the production of the low-sulfur fuel oil.
At present, China has catalytic cracking processing capacity of more than 150Mt/a, the yield of catalytic cracking slurry oil generally accounts for 6-8% of catalytic cracking processing amount, the yield of catalytic slurry oil is very large, the catalytic slurry oil has the characteristics of high density, high sulfur content, high content of heavy components such as colloid and the like, and in addition, the catalytic slurry oil also contains a large amount of catalyst powder, so that the economic value of the catalytic slurry oil is low, and the catalytic slurry oil becomes a key problem to be solved by enterprises. If the catalytic cracking is used as a blending component of low-sulfur fuel oil, the catalytic slurry oil must be pretreated to reduce the density, sulfur content and solid content, especially to remove the solid content, so that the slurry oil de-solidification becomes a key step for realizing efficient utilization of the slurry oil, which is also an important problem in the industry at present.
The method for removing solid from catalytic slurry oil is mainly a filtering solid-removing method, and Huangfu et al, application of slurry oil filtering technology in heavy oil catalytic cracking unit, introduces a method for filtering solid from catalytic slurry oil. Wherein, the core element of the oil slurry filtering system is a porous metal powder sintered filter element. As the hot slurry passes through the filter element, the slurry liquid can pass through the filter element, clean slurry (filtrate) enters the downstream equipment, and solid catalyst particles are trapped on the inner surface of the filter element. The filtered solid catalyst filter cake is back flushed with dry gas and discharged
And a filter cake receiving tank. During the deslagging process, the rapid pressure release and the reverse flow of the filtrate can rapidly strip the solids off the inner surface of the filter element and allow all of the media inside the filter to flow out of the filter through the reject valve. The method needs to be provided with a pre-filtering device and a fine filtering device, and also needs to be provided with auxiliary equipment such as back flushing oil, so that the operation is complicated, the back flushing is frequent, and the actual operation has certain difficulty.
Patent CN 103789028A introduces a pretreatment method of raw material for producing needle coke, in which the raw material for producing needle coke is catalytic cracking slurry oil, in the patent technology, the catalytic cracking slurry oil is firstly filtered by adopting a filtering technology to remove catalyst powder in the slurry oil, then the solid removal slurry oil is hydrogenated by adopting a hydrogenation means to remove part of sulfur and saturated part of aromatic hydrocarbon, and then the ideal component is obtained by distillation and cutting to be used as the raw material for producing needle coke. In the technology, the filtering means is a relatively common oil slurry de-solidification means, but because the particle size of catalyst powder in the catalytic oil slurry is small, and the catalytic oil slurry contains certain viscosity, the catalyst powder is wrapped in the heavy component of the catalytic oil slurry and is difficult to remove through the filtering means, and meanwhile, the heavy component of the catalytic oil slurry is still easy to intercept on a filter screen in the filtering process, so that the filtering effect is poor, and meanwhile, the loss of the heavy component is also caused.
The patent CN 102888244A introduces a production method of low-sulfur marine fuel oil, and the invention relates to a production method of marine fuel oil, which comprises the following steps: heating catalytic slurry oil, filtering the catalytic slurry oil with a precise filtering device to remove tiny catalyst particles in the slurry oil, mixing the catalytic slurry oil with hydrogen, heating, contacting the mixture with a residual oil hydrofining catalyst, a distillate oil hydrofining catalyst and a distillate oil hydrocracking catalyst, reacting the hydrogenated catalytic mixture, separating and fractionating obtained reactants to obtain a tail oil fraction, and mixing the tail oil fraction with vacuum residual oil according to different proportions to obtain a finished product. The method of the invention adopts filtering equipment with larger investment and has larger liquid loss in the actual operation process.
Disclosure of Invention
The catalytic slurry oil obtained by catalytic cracking of heavy oil has the problems of high solid content and small particle size, and when the catalytic slurry oil is treated by means of conventional filtration and the like, the conditions of high liquid recovery loss, incomplete catalyst powder removal, easy blockage of a filter, frequent back washing and unstable operation of a filter device exist, so that most of the catalytic slurry oil can only be used as a coking device feed at present, a large amount of coke with low value is produced as a byproduct, and the value of the catalytic slurry oil cannot be fully exerted. Meanwhile, the residual oil is used as the heaviest component in the crude oil, and how to treat the residual oil and obtain a value-added product is also an urgent problem to be solved.
Aiming at the problems in the prior art, the invention provides a method for producing low-sulfur fuel oil, which starts from the existence state of catalyst powder in catalytic slurry oil and the property characteristics of residual oil, can reduce the solid content and the sulfur content of the catalytic slurry oil, produce high-quality purified slurry oil, and further blend with the residual oil raw material to produce the rare low-sulfur marine fuel oil.
The invention provides a production method of low-sulfur marine fuel oil, which comprises the following steps:
(1) mixing the catalytic slurry oil with a first auxiliary agent, performing sedimentation separation after mixing treatment, and obtaining a first material and residue after separation;
(2) the first material obtained by separation in the step (1) and hydrogen enter a hydrotreating unit and react under the action of a hydrotreating catalyst;
(3) the liquid phase effluent obtained in the step (2) enters a clarification unit, and clarified oil is obtained after separation;
(4) carrying out solid-liquid separation on the clarified oil obtained in the step (3), and obtaining purified oil slurry after separation;
(5) and (4) mixing the purified oil slurry obtained in the step (4) with hydrogenated tail oil to obtain the low-sulfur marine fuel oil.
In the production method of the low-sulfur marine fuel oil, the hydrogenated tail oil in the step (5) has the sulfur content of 0.1-1.0 wt% and the viscosity (50 ℃) of 300-450 mm2And s. The hydrogenated tail oil can be one or more of topping tail oil, hydrogenated normal residue and hydrogenated slag reduction obtained after hydrotreating inferior raw materials, and the inferior raw materials can be one or more of vacuum residue, atmospheric residue, extra heavy oil, oil sand asphalt, coal liquefaction oil and coal tar.
In the method for producing the low-sulfur marine fuel oil, the weight ratio of the purified oil slurry to the hydrogenated tail oil in the step (5) is 0.05-3: 1.
In the method for producing the low-sulfur marine fuel oil, a step (1.1) can be added between the step (1) and the step (2), wherein in the step (1.1), the first material obtained by separating in the step (1) and hydrogen firstly enter a hydrogenation pretreatment unit, hydrogenation reaction is carried out in the presence of a hydrogenation pretreatment catalyst, and the reaction effluent enters a hydrogenation treatment unit to carry out the step (2).
In the method for producing low-sulfur bunker fuel oil, the catalytic slurry oil referred to in step (1) is heavy oil from a catalytic cracking unit containing catalyst particles or catalyst powder, wherein the catalyst particles or catalyst powder are generated by collision and abrasion between the catalyst particles or between the catalyst particles and the reactor wall during the operation of the catalytic cracking unit. The catalytic slurry oil can be one or more of distillate oil catalytic cracking slurry oil, heavy oil catalytic cracking slurry oil, residual oil catalytic cracking slurry oil or distillate oil blending residual oil catalytic cracking slurry oil; the residual oil comprises one or more of atmospheric residual oil and vacuum residual oil, the heavy oil can be obtained by subjecting crude oil to topping treatment, and the distillate oil comprises one or more of Vacuum Gas Oil (VGO) and Atmospheric Gas Oil (AGO).
In the method for producing the low-sulfur marine fuel oil, the dry point temperature of the catalytic slurry oil in the step (1) is 300-580 ℃.
In the method for producing the low-sulfur marine fuel oil, the first auxiliary agent in the step (1) is coal tar and/or coal tar distillate oil, and specifically can be one or more of full-fraction medium-low temperature coal tar, full-fraction high-temperature coal tar, medium-low temperature coal tar distillate oil and high-temperature coal tar distillate oil.
In the production method of the low-sulfur marine fuel oil, the weight ratio of the first auxiliary agent to the catalytic slurry oil in the step (1) is 1: 10-1: 30, preferably 1: 15-1: 25; the mixing treatment temperature is 50-150 ℃, and the preferable mixing treatment temperature is 60-120 ℃; the mixing treatment time is 0.5-4 h, and preferably 1-2 h.
In the production method of the low-sulfur marine fuel oil, a second auxiliary agent can be added in the step (1), wherein the second auxiliary agent is one or more of tetrahydronaphthalene, decahydronaphthalene, formic acid, formaldehyde and methanol, and is preferably one or more of tetrahydronaphthalene and decahydronaphthalene; the weight ratio of the second auxiliary agent to the catalytic slurry oil is 1: 30-1: 100, and preferably 1: 50-1: 80.
In the method for producing the low-sulfur marine fuel oil, the hydrogenation pretreatment unit in the step (1.1) can adopt one or more of a fixed bed hydrogenation process, a boiling bed hydrogenation process, a suspended bed hydrogenation process and a moving bed hydrogenation process. The hydrogenation pretreatment unit is provided with more than 1 hydrogenation pretreatment reactor, and when more than 2 hydrogenation pretreatment reactors are arranged, more than 2 reactors can be connected in series and/or in parallel.
In the method for producing the low-sulfur marine fuel oil, the operation conditions of the hydrogenation pretreatment unit are as follows: the reaction temperature is 300-380 ℃, the reaction pressure is 4-9 Mpa, and the volume airspeed is 0.4-2.0 h-1The hydrogen-oil volume ratio is 400-1000, the preferable reaction temperature is 320-360 ℃, the reaction pressure is 6-8 Mpa, and the volume airspeed is 0.6-1.2 h-1The volume ratio of hydrogen to oil is 500-800.
In the method for producing the low-sulfur marine fuel oil, the hydrotreating unit in the step (2) can adopt one or more of a fixed bed hydrogenation process, a boiling bed hydrogenation process, a suspended bed hydrogenation process and a moving bed hydrogenation process, and preferably adopts the boiling bed hydrogenation process. The hydrotreating unit is provided with more than 1 hydrotreating reactor, and when more than 2 hydrotreating reactors are arranged, more than 2 hydrotreating reactors can be connected in series and/or in parallel.
In the method for producing the low-sulfur marine fuel oil, the operation conditions of the hydrogenation treatment unit in the step (2) are as follows: the reaction temperature is 360-420 ℃, the reaction pressure is 6.0-14.0 Mpa, and the volume airspeed is 0.5-2.5 h-1The hydrogen-oil volume ratio is 300-1000, preferably, the reaction temperature is 370-410 ℃, the reaction pressure is 7.0-11.0 Mpa, the volume space velocity is 0.8-1.5 h < -1 >, and the hydrogen-oil volume ratio is 500-800.
In the method for producing the low-sulfur marine fuel oil, the hydrogenation pretreatment unit and the hydrotreating unit can be arranged in one reactor or can be respectively provided with independent reactors.
In the method for producing low-sulfur marine fuel oil, the catalyst used in the hydrogenation pretreatment unit can be any one of the existing hydrogenation pretreatment catalysts, for example, commercially available hydrogenation pretreatment catalysts developed by the research institute of petrochemical industry can be used.
In the method for producing the low-sulfur marine fuel oil, when the hydrotreating unit adopts a boiling bed hydrogenation process, the waste catalyst discharged by the hydrotreating unit can be used as a hydrogenation pretreatment catalyst of a hydrogenation pretreatment unit.
In the method for producing the low-sulfur marine fuel oil, the catalyst used in the hydrotreating unit is a hydrotreating catalyst which is conventional in the art, wherein the active metal of the catalyst can be one or more of nickel, cobalt, molybdenum or tungsten. For example, the catalyst composition may comprise, in weight percent: 0.1-12% of nickel or cobalt (calculated according to the oxide thereof), 5-15% of molybdenum or tungsten (calculated according to the oxide thereof), and the carrier can be one or more of alumina, silica, alumina-silica or titanium oxide. The catalyst is in the shape of extrudate or sphere, and the bulk density is 0.4-0.9 g/cm3The particle diameter (spherical diameter or strip diameter) is 0.08-0.8 mm, and the specific surface area is 100-200 m2/g。
In the method for producing the low-sulfur marine fuel oil, the clarifying unit in the step (5) can be one or more of a standing clarifying unit and a forced clarifying unit by means of external force; the clarifying units are at least one, and can be operated in series or in parallel. The clarifying unit is mainly used for separating large-particle catalysts larger than 25 microns, and the separated large-particle catalysts can be treated with the waste catalysts of the catalytic cracking unit.
In the method for producing the low-sulfur marine fuel oil, the solid-liquid separation unit in the step (6) is mainly used for separating the small-particle catalyst which cannot be clarified in the step (5), the solid-liquid separation unit can adopt one of the existing methods in the field for realizing solid-liquid separation, preferably adopts an external force means of a high-speed centrifuge to forcibly realize solid-liquid separation, and the operation conditions of the centrifuge are as follows: the rotating speed is 1500-3000 r/min, the temperature is 60-80 ℃, and the operation conditions are preferably as follows: the rotating speed is 1900-2500 r/min, and the temperature is 65-75 ℃. The separated catalyst powder may be sent out for treatment together with the catalyst particles obtained in step (4).
Compared with the prior art, the method for producing the low-sulfur marine fuel oil has the following advantages:
1. the catalytic slurry oil is high in solid content and difficult to treat, and the conventional treatment means is to use the catalytic slurry oil and residual oil together as a coking device feeding material or compound the catalytic slurry oil and the residual oil with high-quality distillate oil to produce qualified fuel oil, so that the catalytic slurry oil and the residual oil cannot be fully utilized, and a large amount of high-quality distillate oil is consumed. The method not only realizes the purification treatment of the catalytic slurry oil to obtain high-quality purified slurry oil and improve the utilization value of the catalytic slurry oil, but also develops a production route of low-sulfur fuel oil, and the hydrogenated tail oil replaces high-quality distillate oil to produce the low-sulfur fuel oil, thereby greatly saving the production cost.
2. In the method for producing the low-sulfur marine fuel oil, the catalytic oil slurry is subjected to graded treatment by using the first auxiliary agent and the second auxiliary agent, and through hydrogenation pretreatment, hydrotreating, clarification treatment and solid-liquid separation, the graded removal of solid impurities with different sizes in the catalytic oil slurry is realized. Firstly, under the combined action of a first auxiliary agent and a second auxiliary agent, the aggregation, sedimentation and separation of large-particle catalyst particles in catalytic slurry oil are promoted; and then the catalytic slurry oil treated by the auxiliary agent is subjected to hydrogenation treatment through a hydrogenation pretreatment unit and a hydrogenation treatment unit, unsaturated hydrocarbons such as colloid and the like influencing the system viscosity and subsequent filtration are subjected to hydrogenation saturation, the reduction of the viscosity of heavy components is facilitated, and because the hydrogenation treatment unit uses a fluidized bed reactor, the bed layer can be prevented from being blocked by catalyst powder, and the device can be ensured to run for a long period.
3. In the method for producing the low-sulfur marine fuel oil, the second auxiliary agent can generate a synergistic effect with the first auxiliary agent to promote the settling separation of solid impurities in the catalytic slurry oil, and can release active hydrogen under the condition of hydrogenation pretreatment in the hydrogenation pretreatment unit to carry out hydrogenation saturation on the easily-coked precursor contained in the first auxiliary agent, and simultaneously carry out hydrogenation pretreatment on the catalytic slurry oil to promote the complex use of the hydrogenation treatment unit, alleviate the hydrogenation reaction of the second hydrogenation treatment unit and reduce the operation difficulty.
4. In the method for producing the low-sulfur marine fuel oil, the hydrotreating unit uses the fluidized bed reactor, the waste catalyst discharged by the fluidized bed reactor can be used as a hydrogenation pretreatment catalyst of the hydrogenation pretreatment unit, the waste catalyst discharged by the hydrotreating unit still has certain hydrogenation activity, and meanwhile, as the catalyst has passed through an initial activity period due to hydrogenation reaction, the possibility of coking and carbon deposition of aromatic hydrocarbons such as unsaturated hydrocarbons and the like on the surface of the waste catalyst is greatly reduced; on the other hand, the catalytic slurry oil has a high content of unsaturated hydrocarbons, and the structure and the content of the unsaturated hydrocarbons have a certain distribution rule, wherein the catalytic slurry oil contains a part of components which are easily condensed to form coke when heated, for example, if the catalytic slurry oil is completely and directly fed into a hydrotreating unit to carry out a hydrogenation reaction, on one hand, the hydrogenation reaction of the unsaturated hydrocarbons can release a large amount of heat, a large amount of cold hydrogen needs to be injected, the energy consumption is high, and on the other hand, the unsaturated hydrocarbons which are easily condensed to form coke when partially heated coke are coke. The waste catalyst discharged by the hydrotreating unit is adopted to carry out mild hydrotreating pretreatment on the catalytic slurry oil in advance, so that the problems can be effectively avoided, and the recycling of the waste catalyst is realized.
4. The method can obviously improve the utilization rate of the catalytic slurry oil, the traditional filtering method has low solid impurity removal efficiency, the yield of the catalytic slurry oil after filtering is damaged due to the interception and recombination of the filter screen, and meanwhile, the operation period of the filtering equipment is shortened due to the rapid increase of the pressure drop of the filter screen. The method combines the property characteristics of the catalytic slurry oil, and by adding a certain auxiliary agent, the viscosity of the catalytic slurry oil is reduced, meanwhile, the aggregation and precipitation of small particles in the catalytic slurry oil are realized, and the operation complexity is reduced; meanwhile, the heavy component wrapped with the small particle impurities is hydrogenated by adopting a hydrogenation means, so that the small particle impurities are resolved and precipitated from the heavy component, and finally the solid impurities are efficiently removed.
5. In the method for producing the low-sulfur marine fuel oil, the reaction pressure and the reaction temperature are adjusted to control the pre-hydrogenation reaction depth of the catalytic slurry oil, the catalytic slurry oil is firstly subjected to shallow hydrogenation to improve the thermal stability of the slurry oil, the hydrogenation depth is too deep, the reaction hydrogen consumption is high, and the cost is high; meanwhile, the softening point and the viscosity of the hydrogenated oil slurry are greatly reduced, and the blending proportion of high-grade road asphalt or low-sulfur fuel oil is influenced.
Detailed Description
The invention is further described below by means of specific embodiments without limiting the scope of protection of the invention.
The production method of the low-sulfur marine fuel oil comprises the following steps: the catalytic slurry oil is fully mixed with a first auxiliary agent according to a certain proportion, whether a second auxiliary agent is added or not can be determined according to needs, and the fully mixed raw materials are subjected to settling separation to obtain a first material and large-particle residues; the first material and hydrogen are mixed and firstly enter a hydrogenation pretreatment unit, the mixed material is subjected to shallow hydrogenation, components which are easy to generate coke in a hydrogenation saturated system are hydrogenated, the mixed material subjected to shallow hydrogenation continuously enters the hydrogenation treatment unit for deep hydrogenation to remove sulfur and nitrogen impurities and reduce the content of unsaturated hydrocarbons, the material obtained after hydrogenation treatment enters a clarification unit to remove part of large particles precipitated due to viscosity reduction, clarified oil after removal of a small amount of large particles enters a solid-liquid separation unit, the viscosity and solid content of the system are greatly reduced at the moment, small particles are thoroughly removed under the action of external force, and finally low-sulfur, low-aromatic hydrocarbon and solid-free purified oil slurry is obtained, and then the purified oil slurry and the hydrogenated tail oil are mixed in a certain proportion to obtain a low-sulfur fuel oil product.
The hydrogenation pretreatment catalyst used in the invention can be FF-36 catalyst developed by the comforting petrochemical research institute; the used hydrotreating catalyst is microspherical molybdenum-nickel catalyst with alumina as carrier, and the catalyst contains MoO313.8 wt% and NiO content 6.2 wt%. Packing of catalystThe degree is 0.78g/cm3Surface area 205m2The catalyst particles had an average diameter of 0.31 mm/g.
The properties of the catalytic slurry oil, the first auxiliary agent (including coal tar whole fraction and coal tar distillate oil) and the hydrogenated tail oil raw materials used in the examples and comparative examples of the present invention are shown in table 1.
The hydrogenated tail oil used in the examples and the comparative examples of the invention is derived from hydrogenated heavy oil (more than 350 ℃) produced by a fixed bed residual oil hydrogenation device, and the specific properties are shown in table 1, and can also be other heavy oil such as residue boiling bed hydrogenated tail oil (more than 500 ℃ or 540 ℃).
Example 1
Example 1 a catalytic slurry oil is used as a raw material, and by using the catalytic slurry oil treatment method of the present invention, the catalytic slurry oil is first mixed with a first auxiliary agent, namely, coal tar full fraction, at a ratio of 17:1, the mixing treatment temperature and mixing treatment time of the catalytic slurry oil and the first auxiliary agent are 72 ℃ and 1.2 hours, respectively, to remove a portion of large particulate matter, and then the catalytic slurry oil and hydrogen gas enter a hydrogenation pretreatment reactor together to perform a shallow hydrogenation reaction to remove easily condensed coke-forming substances, wherein the reaction conditions of the hydrogenation pretreatment reactor are as follows: the reaction temperature is 337 ℃, the reaction pressure is 6.5Mpa, and the volume space velocity is 0.7h-1Hydrogen to oil volume ratio 600; then the mixture enters a hydrotreating reactor for deep impurity removal reaction, wherein the reaction conditions of the hydrotreating reactor are as follows: the reaction temperature is 384 ℃, the reaction pressure is 8.4Mpa, and the volume space velocity is 1.0h-1Hydrogen to oil volume ratio of 600, wherein the hydrotreating reactor uses an ebullated bed reactor. The mixed system after the impurity removal reaction is respectively treated by a clarification unit and a forced solid-liquid separation unit to obtain purified oil slurry, and the operation conditions of the forced solid-liquid separation unit are as follows: the rotation speed is 2100r/min, and the temperature is 68 ℃. The blending ratio of the purified slurry oil to the hydrogenated tail oil is 1:1, and the reaction results are shown in tables 2-3.
Example 2
Example 2 using catalytic slurry oil as a raw material, according to the catalytic slurry oil treatment method of the present invention, the catalytic slurry oil is first mixed with a first additive, namely, a coal tar whole fraction, and a second additive, namely, tetrahydronaphthalene, in a ratio of 18:1 to 6 for the catalytic slurry oil, the first additive and the second additive, respectively1:1, the mixing treatment temperature and the mixing treatment time of the catalytic slurry oil, the first auxiliary agent and the second auxiliary agent are respectively 82 ℃ and 1.5h, part of large-particle substances are removed, and then the catalytic slurry oil and hydrogen enter a hydrotreating reactor together for deep impurity removal reaction, wherein the reaction conditions of the hydrotreating reactor are as follows: the reaction temperature is 389 ℃, the reaction pressure is 8.9Mpa, and the volume space velocity is 1.2h-1And a hydrogen to oil volume ratio of 650, wherein the hydroprocessing reactor uses an ebullated bed reactor. The mixed system after the impurity removal reaction is respectively treated by a clarification unit and a forced solid-liquid separation unit to obtain purified oil slurry, and the operation conditions of the forced solid-liquid separation unit are as follows: the rotation speed is 2200r/min, and the temperature is 70 ℃. The blending ratio of the purified slurry oil to the hydrogenated tail oil is 1:2, and the reaction results are shown in tables 2-3.
Example 3
Embodiment 3 takes catalytic slurry oil as a raw material, and by using the catalytic slurry oil treatment method of the present invention, the catalytic slurry oil is mixed with a first additive, namely coal tar full fraction, the ratio of the catalytic slurry oil to the first additive is 21:1, the mixing treatment temperature and the mixing treatment time of the catalytic slurry oil and the first additive are 87 ℃ and 1.6 hours, respectively, a part of large particulate matter is removed, and then the catalytic slurry oil and hydrogen enter a hydrotreating reactor together for deep impurity removal reaction, wherein the reaction conditions of the hydrotreating reactor are as follows: the reaction temperature is 394 ℃, the reaction pressure is 9.3Mpa, and the volume space velocity is 1.4h-1Hydrogen to oil volume ratio of 700, wherein the hydroprocessing reactor uses an ebullated bed reactor. The mixed system after the impurity removal reaction is respectively treated by a clarification unit and a forced solid-liquid separation unit to obtain purified oil slurry, and the operation conditions of the forced solid-liquid separation unit are as follows: the rotating speed is 2300r/min, and the temperature is 75 ℃. The blending ratio of the purified slurry oil to the hydrogenated tail oil is 1:2, and the reaction results are shown in tables 2-3.
Example 4
Example 4 using catalytic slurry oil as a raw material, according to the catalytic slurry oil treatment method of the present invention, the catalytic slurry oil is first mixed with a first additive, namely, a coal tar whole fraction, and a second additive, namely, tetrahydronaphthalene, at a ratio of 22:1 to 70:1, respectively, and at a mixing temperature and for a mixing time of 92 ℃ to 1.8 hours, respectively, the catalytic slurry oil is removedPart of large-particle substances enter a hydrogenation pretreatment reactor together with hydrogen to carry out a shallow hydrogenation reaction to remove easily condensed coke-forming substances, wherein the reaction conditions of the hydrogenation pretreatment reactor are as follows: the reaction temperature is 347 ℃, the reaction pressure is 7.7Mpa, and the volume space velocity is 0.8h-1Hydrogen to oil volume ratio 650; then the mixture enters a hydrotreating reactor for deep impurity removal reaction, wherein the reaction conditions of the hydrotreating reactor are as follows: the reaction temperature is 398 ℃, the reaction pressure is 9.8Mpa, and the volume space velocity is 1.4h-1Hydrogen to oil volume ratio 750, wherein the hydroprocessing reactor uses an ebullated bed reactor. The mixed system after the impurity removal reaction is respectively treated by a clarification unit and a forced solid-liquid separation unit to obtain purified oil slurry, and the operation conditions of the forced solid-liquid separation unit are as follows: the rotation speed is 2350r/min, and the temperature is 78 ℃. The blending ratio of the purified slurry oil to the hydrogenated tail oil is 1:1, and the reaction results are shown in tables 2-3.
Comparative example 1
The method is basically the same as the example 1, except that the catalytic slurry oil in the comparative example 1 is directly subjected to hydrotreating without any treatment in a hydrotreating pretreatment unit and a hydrotreating unit, the blending ratio of the purified slurry oil to the hydrogenated tail oil is 1:1, and the reaction results are shown in tables 2-3.
Comparative example 2
The method is basically the same as the example 1, except that in the comparative example 2, the catalytic slurry oil is firstly filtered by a conventional filtering method (the filtering diameter is 25 μm), and then enters a hydrogenation pretreatment unit and a hydrogenation treatment unit for hydrogenation reaction, the blending ratio of the purified slurry oil to the hydrogenated tail oil is 1:1, and the reaction results are shown in tables 2-3.
TABLE 1 Properties of the raw materials
TABLE 2 actual working effect of tar purification in different cases
TABLE 3 Down-Regulation and Low sulfur Fuel oil Property index for different cases
Through the above description and comparative analysis of the embodiment and the comparative example, it is found that, for the catalytic slurry oil which is an inferior raw material with high solid content and high aromatic hydrocarbon, the method of the invention adopts the combined action of the auxiliary agent solid removal and the hydrogenation solid removal to ensure the high-efficiency impurity removal and solid removal of the catalytic slurry oil and the long-term operation of the device, provides a good technical means for improving the value of the catalytic slurry oil, can produce qualified low-sulfur fuel oil by blending the purified slurry oil and the hydrogenation tail oil, and has the key link of well performing the solid removal of the catalytic slurry oil containing the solid and the long-term operation of the device.
Claims (18)
1. A method for producing low-sulfur marine fuel oil, comprising the following steps:
(1) mixing the catalytic slurry oil with a first auxiliary agent, performing sedimentation separation after mixing treatment, and obtaining a first material and residue after separation;
(2) the first material obtained by separation in the step (1) and hydrogen enter a hydrotreating unit and react under the action of a hydrotreating catalyst;
(3) the liquid phase effluent obtained in the step (2) enters a clarification unit, and clarified oil is obtained after separation;
(4) carrying out solid-liquid separation on the clarified oil obtained in the step (3), and obtaining purified oil slurry after separation;
(5) and (4) mixing the purified oil slurry obtained in the step (4) with hydrogenated tail oil to obtain the low-sulfur marine fuel oil.
2. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: in the step (5), the sulfur content of the hydrogenated tail oil is 0.1-1.0 wt%, and the viscosity at 50 ℃ is 300-450 mm2/s。
3. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: and (5) the hydrogenated tail oil is one or more of topped tail oil obtained after the poor-quality raw material is subjected to hydrotreating, hydrogenated normal slag and hydrogenated slag reduction.
4. A process for the production of low sulfur bunker fuel oil as claimed in claim 3, wherein: the inferior raw material is one or more of vacuum residue oil, atmospheric residue oil, extra heavy oil, oil sand asphalt, coal liquefaction oil and coal tar.
5. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: adding a step (1.1) between the step (1) and the step (2), wherein in the step (1.1), the first material obtained by separating in the step (1) and hydrogen firstly enter a hydrogenation pretreatment unit, hydrogenation reaction is carried out in the presence of a hydrogenation pretreatment catalyst, and the reaction effluent enters a hydrogenation treatment unit to carry out the step (2).
6. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the catalytic slurry oil in the step (1) is one or more of distillate oil catalytic cracking slurry oil, heavy oil catalytic cracking slurry oil, residual oil catalytic cracking slurry oil or distillate oil blending residual oil catalytic cracking slurry oil; the residual oil comprises one or more of atmospheric residual oil and vacuum residual oil, the heavy oil is obtained by performing topping treatment on crude oil, and the distillate oil comprises one or more of vacuum gas oil and atmospheric gas oil.
7. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the dry point temperature of the catalytic slurry oil in the step (1) is 300-580 ℃.
8. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the first auxiliary agent in the step (1) is coal tar and/or coal tar distillate oil.
9. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the first auxiliary agent in the step (1) is one or more of full-range medium-low temperature coal tar, full-range high-temperature coal tar, medium-low temperature coal tar distillate oil and high-temperature coal tar distillate oil.
10. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the weight ratio of the first auxiliary agent to the catalytic slurry oil in the step (1) is 1: 10-1: 30, and preferably 1: 15-1: 25.
11. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the mixing treatment temperature in the step (1) is 50-150 ℃, and preferably 60-120 ℃; the mixing treatment time is 0.5-4 h, preferably 1-2 h.
12. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: adding a second auxiliary agent in the step (1), wherein the second auxiliary agent is one or more of tetrahydronaphthalene, decahydronaphthalene, formic acid, formaldehyde and methanol, and preferably one or more of tetrahydronaphthalene and decahydronaphthalene.
13. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the weight ratio of the second auxiliary agent to the catalytic slurry oil is 1: 30-1: 100, and preferably 1: 50-1: 80.
14. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the operating conditions of the hydrogenation pretreatment unit are as follows: the reaction temperature is 300-380 ℃, the reaction pressure is 4-9 Mpa, and the volume airspeed is 0.4-2.0 h-1The hydrogen-oil volume ratio is 400-1000, the preferable reaction temperature is 320-360 ℃, the reaction pressure is 6-8 Mpa, and the volume airspeed is 0.6-1.2 h-1The volume ratio of hydrogen to oil is 500-800.
15. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: in the step (2), the hydrotreating unit adopts one or more of a fixed bed hydrogenation process, a boiling bed hydrogenation process, a suspended bed hydrogenation process and a moving bed hydrogenation process, and preferably adopts the boiling bed hydrogenation process.
16. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the operation conditions of the hydrogenation treatment unit in the step (2) are as follows: the reaction temperature is 360-420 ℃, the reaction pressure is 6.0-14.0 Mpa, and the volume airspeed is 0.5-2.5 h-1The hydrogen-oil volume ratio is 300-1000, preferably, the reaction temperature is 370-410 ℃, the reaction pressure is 7.0-11.0 Mpa, the volume space velocity is 0.8-1.5 h < -1 >, and the hydrogen-oil volume ratio is 500-800.
17. A process for the production of low sulfur bunker fuel oil as claimed in claim 15 wherein: when the hydrotreating unit adopts an ebullated bed hydrogenation process, the waste catalyst discharged from the hydrotreating unit is used as a hydrogenation pretreatment catalyst of a hydrogenation pretreatment unit.
18. The method for producing low sulfur bunker fuel oil according to claim 1, wherein: the clarification unit in the step (3) is one or more of a standing clarification unit and a forced clarification unit with the help of external force; at least one clarifying unit is arranged, and the clarifying units are operated in series or in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811239893.XA CN111088068A (en) | 2018-10-24 | 2018-10-24 | Production method of low-sulfur marine fuel oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811239893.XA CN111088068A (en) | 2018-10-24 | 2018-10-24 | Production method of low-sulfur marine fuel oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111088068A true CN111088068A (en) | 2020-05-01 |
Family
ID=70391993
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811239893.XA Pending CN111088068A (en) | 2018-10-24 | 2018-10-24 | Production method of low-sulfur marine fuel oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111088068A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112852484A (en) * | 2021-01-05 | 2021-05-28 | 陕西延长石油（集团）有限责任公司 | Production method of low-sulfur marine fuel oil blending component |
| CN114106877A (en) * | 2020-08-27 | 2022-03-01 | 中国石油化工股份有限公司 | System and method for producing low-sulfur marine fuel oil |
| CN114437797A (en) * | 2020-10-16 | 2022-05-06 | 中国石油化工股份有限公司 | Production method of marine fuel oil blending component |
| CN114806638A (en) * | 2021-01-19 | 2022-07-29 | 中国石油化工股份有限公司 | Production method of low-sulfur marine fuel oil |
| EP4227384A4 (en) * | 2020-10-19 | 2024-04-10 | China Petroleum & Chemical Corporation | Method and system for producing fuel oil and use thereof, and fuel oil and use thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5215649A (en) * | 1990-05-02 | 1993-06-01 | Exxon Chemical Patents Inc. | Method for upgrading steam cracker tars |
| CN1955261A (en) * | 2005-10-24 | 2007-05-02 | 中国石油化工股份有限公司 | Hydrocracking method of midbarrel oil circulation |
| CN103540353A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Combined hydrogenation process method for treating coal tar and residual oil |
| CN103642539A (en) * | 2013-12-25 | 2014-03-19 | 济南开发区星火科学技术研究院 | Regulating method of bunker fuel oil |
| CN104212489A (en) * | 2013-06-05 | 2014-12-17 | 中国石油天然气股份有限公司 | Processing method for high nitrogen content heavy oil |
| CN108102710A (en) * | 2016-11-25 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of method for preparing needle coke |
-
2018
- 2018-10-24 CN CN201811239893.XA patent/CN111088068A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5215649A (en) * | 1990-05-02 | 1993-06-01 | Exxon Chemical Patents Inc. | Method for upgrading steam cracker tars |
| CN1955261A (en) * | 2005-10-24 | 2007-05-02 | 中国石油化工股份有限公司 | Hydrocracking method of midbarrel oil circulation |
| CN103540353A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Combined hydrogenation process method for treating coal tar and residual oil |
| CN104212489A (en) * | 2013-06-05 | 2014-12-17 | 中国石油天然气股份有限公司 | Processing method for high nitrogen content heavy oil |
| CN103642539A (en) * | 2013-12-25 | 2014-03-19 | 济南开发区星火科学技术研究院 | Regulating method of bunker fuel oil |
| CN108102710A (en) * | 2016-11-25 | 2018-06-01 | 中国石油化工股份有限公司 | A kind of method for preparing needle coke |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114106877A (en) * | 2020-08-27 | 2022-03-01 | 中国石油化工股份有限公司 | System and method for producing low-sulfur marine fuel oil |
| CN114106877B (en) * | 2020-08-27 | 2023-06-09 | 中国石油化工股份有限公司 | System and method for producing low-sulfur marine fuel oil |
| CN114437797A (en) * | 2020-10-16 | 2022-05-06 | 中国石油化工股份有限公司 | Production method of marine fuel oil blending component |
| CN114437797B (en) * | 2020-10-16 | 2023-05-26 | 中国石油化工股份有限公司 | Production method of blending components of marine fuel oil |
| EP4227384A4 (en) * | 2020-10-19 | 2024-04-10 | China Petroleum & Chemical Corporation | Method and system for producing fuel oil and use thereof, and fuel oil and use thereof |
| CN112852484A (en) * | 2021-01-05 | 2021-05-28 | 陕西延长石油（集团）有限责任公司 | Production method of low-sulfur marine fuel oil blending component |
| CN112852484B (en) * | 2021-01-05 | 2023-03-31 | 陕西延长石油（集团）有限责任公司 | Production method of low-sulfur marine fuel oil blending component |
| CN114806638A (en) * | 2021-01-19 | 2022-07-29 | 中国石油化工股份有限公司 | Production method of low-sulfur marine fuel oil |
| CN114806638B (en) * | 2021-01-19 | 2023-02-03 | 中国石油化工股份有限公司 | Production method of low-sulfur marine fuel oil |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111088068A (en) | Production method of low-sulfur marine fuel oil | |
| CN101885982B (en) | Hydrogenation method for coal tar suspension bed of heterogeneous catalyst | |
| EP2818535A1 (en) | Process for producing mesophase pitch by hydrogenation of high-temperature coal tar | |
| CN109294622B (en) | Process and device for realizing heavy oil lightening by using suspension bed hydrogenation | |
| CN103265971A (en) | Heterogeneous coal tar suspension bed hydrogenation method | |
| CN111378490B (en) | Coal tar full-fraction fluidized bed-fixed bed combined treatment process | |
| CN107557064B (en) | Coal tar combined bed hydrogenation method and system for coal tar combined bed hydrogenation | |
| CN102041047B (en) | Heavy oil hydrogenation modifying method | |
| CN103059997B (en) | Combined technique of hydrotreating and delay coking of residual oil | |
| CN114045179A (en) | Multiphase flow residual oil hydro-upgrading and catalytic cracking combined process and system | |
| CN106635152A (en) | Method for processing full-range oil in coal tar | |
| CN103540359B (en) | A kind of inferior heavy oil catalytic conversion process improving low-carbon alkene and yield of gasoline | |
| CN106433779B (en) | A kind of coal tar maximizes the system and method for production light Fuel | |
| CN103540356B (en) | A kind of inferior heavy oil catalytic conversion process improving low-carbon alkene and diesel yield | |
| CN111378491B (en) | Inferior heavy oil hydrotreating process | |
| CN111088071A (en) | Catalytic slurry oil treatment method | |
| CN111088070A (en) | Inferior heavy oil treatment method | |
| CN114574239A (en) | Preparation method of marine fuel oil | |
| CN114437792A (en) | Method and apparatus for processing residual oil | |
| CN114574240A (en) | Method for preparing bunker fuel oil by hydrogenation | |
| CN108504378B (en) | Preparation method of coal hydropyrolysis hydrogen-donating solvent oil, hydrogen-donating solvent oil prepared by same and application thereof | |
| CN111088074A (en) | Coal tar and residual oil combined treatment process | |
| CN113862035B (en) | Method for producing high-end needle coke raw material from catalytic cracking slurry oil | |
| CN115011377B (en) | Method for separating solid matters from catalytic cracking slurry oil | |
| CN114806638B (en) | Production method of low-sulfur marine fuel oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20240320 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant after: CHINA PETROLEUM & CHEMICAL Corp. Country or region after: Zhong Guo Applicant after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Applicant before: CHINA PETROLEUM & CHEMICAL Corp. Country or region before: Zhong Guo Applicant before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |
|
| TA01 | Transfer of patent application right |