CN103756720A - Production method of high-cetane-number anthracene oil hydrogenated diesel oil - Google Patents
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Abstract
The invention discloses a production method of high-cetane-number anthracene oil hydrogenated diesel oil. The production method comprises the following steps: mixing anthracene oil with biodiesel oil according to a mass ratio to form a mixed raw material, performing hydro-refining, hydro-cracking and hydro-upgrading on the mixed raw material together with hydrogen in sequence, and performing oil-gas separation on effluent materials to obtain the high-cetane-number diesel oil. The production method has the advantages as follows: the biodiesel oil is mixed with the anthracene oil to form the mixed raw material, and compared with the anthracene oil, the mixed raw material has the characteristics that the viscosity and the contents of colloids, asphaltenes and carbon residues are all reduced, the hydrogen accessibility is enhanced, the desulfuration and denitrification effects are improved, and the catalyst activity time is prolonged; the requirement of the mixed raw material on the reaction conditions is lowered, the investment and operation expenses of a device are saved, and the economy of the production process is improved; the quality of diesel oil components is remarkably improved, the diesel oil components have the characteristics of ultralow sulfur content, high cetane number and low condensation point, and the requirements of national automotive diesel oil standards IV or V can be met; the yield of the diesel oil components is increased, the anthracene oil is completely converted into clean fuel for transportation, and the source of raw materials for producing the clean fuel is expanded.
Description
Technical field
The present invention relates to a kind of production method of diesel oil, particularly a kind of method of producing high-quality clean diesel by reconstructed coal tar anthracene oil product.
Background technology
Diesel oil is very important motor spirit, substantially by refining of petroleum, produces now.Along with the development of world economy, the continuous increase of population, the demand of diesel oil can be more and more large, and the raising of day by day exhausted and people's environmental consciousness of petroleum resources has promoted again countries in the world to accelerate the exploitation paces that engine substitutes oil product greatly.China attaches great importance to the development of alternative fuel, has just determined the developing direction of alternative fuel as far back as the Eleventh Five-Year Plan period, and the advantage energy (coal) substitutes the rare energy (oil), and renewable energy source substitutes fossil energy.Therefore high-quality clean diesel is produced in the deep processing of Development of Coal tar products, is to meet national industrial development direction of encouraging.
Carbolineum is the middle runnings of coal tar fractional distillation, and initial boiling point is generally 220～260 ℃, and final boiling point is generally 500 ℃ of left and right, and high can arrive 550 ℃, general final boiling point at more than 500 ℃ carbolineum also referred to as deep drawing anthracene oil.The mixture that the chemical constitution of carbolineum is comprised of anthracene, phenanthrene, fluorenes, acenaphthene, carbazole etc., constitutional features is containing three rings, Fourth Ring and above aromatic hydrocarbons thereof, density (20 ℃) generally surpasses 1.0g/m
3, and nitrogen content is high, what have surpasses 1wt%.At present, domestic carbolineum is mainly as the raw materials for production oil of carbon black or as mixing asphalt oil or for thick products such as wood preserving oil or separation and Extraction naphthalene, anthracene, acenaphthene, phenanthrene, carbazoles, but these purposes added values are little, separated product purity is low, energy consumption is high, price is low, deficiency in economic performance, do not make rational use of resources, process easily causes serious secondary pollution to environment simultaneously.
At present, producing light fuel oil by hydrogenating anthracene oil generally all adopts hydrofining and the hydrocracking process of multi-stage series, obtains petrol and diesel oil.Carbolineum method for hydrogen cracking (country origin: a China, publication number: 101024780, publication date: 2007-08-29) disclose and take carbolineum as raw material, adopted hydrofining-hydrocracking one-stage serial flow process, obtained vapour, diesel component product.But the ammonia and the water that generate in the method unifining process are not separated, follow-up hydrogenation catalyst activity stability is produced to adverse influence.A kind of method of hydrogenation conversion for anthracene oil (country origin: China, publication number: 101033409, publication date: 2007-09-12) disclosed method has overcome above-mentioned shortcoming, it adopts two-stage hydrogenation technique, after carbolineum hydrofining, Separation of Water and ammonia, simultaneously by refined products fractionation, what obtain is greater than 200 ℃ of cuts as hydrocracking raw material.But when above-mentioned two kinds of methods all exist refinement treatment, denitrogenation is clean, catalyst deactivation fast, affect the problem of the continuous cycle of operation of device, and the requirement that do not reach derv fuel oil standard of the diesel cetane-number of production.
The method of producing diesel by hydrogenating anthrancene oil (country origin: China, publication number: 101993740A, publication date: 2011-03-30) disclose employing carbolineum and mixed as raw material with washing oil, through hydrofining, separation, hydrocracking and hydro-upgrading.But the diesel oil obtaining also needs to add cetane number improver, could meet GB requirement.
Summary of the invention
Goal of the invention: for the problems referred to above, the object of this invention is to provide a kind of with coal tar carbolineum by the method for hydrogenation production super low sulfur, high hexadecane value, low freezing point diesel oil, extension fixture production run cycle.
Technical scheme: a kind of production method that improves carbolineum hydrogenated diesel oil cetane value, comprises the following steps:
Step (1): carbolineum and biofuel are formed to mixing raw material for 90: 10 in mass ratio～10: 90 and send in hydrofining reactor together with hydrogen, carry out denitrogenation, desulfurization and deoxygenation with Hydrobon catalyst, temperature of reaction is 260～420 ℃, reaction pressure is 6～18MPa, hydrogen to oil volume ratio is 800: 1～1800: 1, and volume space velocity is 0.2～5h-
1; After material outflow reactor, hydrogen, hydrogen sulfide, ammonia, water and oil are carried out separated, isolated oil content is heated up in a steamer, by 360 ℃ of 180 ℃ of <, 180～360 ℃, >, carry out cut and cut apart;
Step (2): the cut that the > that will obtain through step (1) is 360 ℃ mixes with hydrogen, send in hydrocracking reactor, react with hydrocracking catalyst, temperature of reaction is 320～400 ℃, reaction pressure is 10～16MPa, hydrogen to oil volume ratio is 600: 1～1800: 1, and volume space velocity is 0.1～2h
-1; After material outflow reactor, hydrogen, dry G&O are carried out to separation, isolated oil content is heated up in a steamer, by 360 ℃ of 180 ℃ of <, 180～360 ℃, >, carry out cut and cut apart;
Step (3): the cut of 180～360 ℃ that will obtain through step (1), step (2) mixes with hydrogen, send in hydro-upgrading reactor, react with catalyst for hydro-upgrading, temperature of reaction is 320～400 ℃, reaction pressure is 5～10MPa, hydrogen to oil volume ratio is 500: 1～1200: 1, and volume space velocity is 0.3～2h
-1; After material outflow reactor, carry out gas-oil separation, the oil obtaining is high hexadecane value diesel oil.
Described Hydrobon catalyst comprises carrier and active ingredient, described carrier is aluminum oxide, amorphous silicon aluminium, silicon-dioxide or titanium oxide etc., the base metal of described active ingredient Wei VIII family and/or group VIB, take catalyst weight as benchmark, tungsten and/or molybdenum are counted 15wt%～35wt% with oxide compound, and nickel and/or cobalt are counted 1wt%～10wt% with oxide compound; Best, tungsten and/or molybdenum are counted 20wt%～30wt% with oxide compound, and nickel and/or cobalt are counted 2wt%～8wt% with oxide compound.
Described hydrocracking catalyst is the dual-function catalyst simultaneously with cracking and hydrogenation: the activeconstituents of cracking function derives from H type molecular sieve, comprises ZSM series, Y or beta-molecular sieve, and its content accounts for 10%～40% of catalyst weight; The active ingredient Wei VIII family of hydrogenating function and/or the metal of group VIB, take catalyst weight as benchmark, and tungsten and/or molybdenum are counted 10wt%～40wt% with oxide compound, and nickel and/or cobalt are counted 1wt%～15wt% with oxide compound; Best, the activeconstituents of described cracking function derives from H type Y or beta-molecular sieve, its content accounts for 20%～30% of catalyst weight, the active ingredient of hydrogenating function be take catalyst weight as benchmark, tungsten and/or molybdenum are counted 15wt%～35wt% with oxide compound, and nickel and/or cobalt are counted 3wt%～10wt% with oxide compound.
Described catalyst for hydro-upgrading comprises carrier and active ingredient, and described active ingredient is supported on ZSM type molecular sieve and γ-Al with oxide form
2o
3or contain a small amount of SiO
2γ-Al
2o
3on carrier Deng solid acid, the metal in described active ingredient Wei VIII family, take catalyst weight as benchmark, and nickel and/or cobalt are counted 5wt%～25wt% with oxide compound; Best, nickel and/or cobalt are counted 10wt%～20wt% with oxide compound.
Described carbolineum is the product that high temperature, middle temperature, low temperature and middle coalite tar obtain through distillation, 220～560 ℃ of boiling ranges; Described biofuel is the fatty acid methyl ester being generated by animal-plant oil and methyl alcohol, wherein: described animal-plant oil is genetically engineered soybean oil, rapeseed oil, sunflower seed oil, palm wet goods vegetables oil, the animal tallows such as pig, ox, sheep, chicken, food and drink give up sewer oil, acidifying wet goods waste grease.
Best, in step (1), temperature of reaction is 320～380 ℃, and reaction pressure is 8～15MPa, and hydrogen to oil volume ratio is 1000: 1～1600: 1, and volume space velocity is 0.5～3h
-1; In step (2), temperature of reaction is 350～380 ℃, and reaction pressure is 12～15MPa, and hydrogen to oil volume ratio is 900: 1～1500: 1, and volume space velocity is 0.3～1.5h
-1; In step (3), temperature of reaction is 340～380 ℃, and reaction pressure is 6～8MPa, and hydrogen to oil volume ratio is 600: 1～1000: 1, and volume space velocity is 0.5～1.5h
-1.
In step (1), to hydrogen, hydrogen sulfide, ammonia, water and separating of oil after, recycle after hydrogen upgrading, hydrogen sulfide, ammonia, moisture class are processed, the cut that < that oil content heats up in a steamer is 180 ℃ is sold as petroleum naphtha or gasoline blending component; In step (2), to hydrogen, dry gas and separating of oil after, recycle after hydrogen upgrading, dry gas focuses on, the cut that < that oil content heats up in a steamer is 180 ℃ is sold as petroleum naphtha or gasoline blending component, and the cut that > is 360 ℃ is as the raw material of step (2); In step (3), after gas-oil separation, hydrogen recycle utilization.
Principle of the present invention is: the definition of (1) cetane value be exactly n-hexadecane be 100, the main chemical compositions of biofuel is positive 16 carbon fatty acid methyl esters and positive 18 carbon fatty acid methyl esters, after hydrogenation, being converted into Pentadecane, n-hexadecane, n-heptadecane and Octadecane, is all high hexadecane value component; (2) sulphur content of biofuel own is generally lower than 10ppm, and the finished product sulphur content after hydrogenation is lower, and state V diesel oil is to sulphur content, requirement is to be not more than 10ppm; (3) biofuel hydrogenation is low to operational condition requirement, after mixing, because biofuel has the effect of dissolving and diluting carbolineum, has reduced the hydrogenation difficulty of carbolineum with carbolineum; (4) blending ratio of biofuel and carbolineum is higher, and diesel yield is higher, biofuel and carbolineum mixing post-treatment, owing to having reduced reaction conditions, cracking reaction is reduced, the more diesel component generating of carbolineum, rather than generation cracking reaction is converted into gasoline or reacted gas component.
Beneficial effect: compared with prior art, advantage of the present invention is:
1, in carbolineum, call in biofuel and form mixing raw material, with carbolineum, compare, the content of viscosity and colloid, bituminous matter and carbon residue all reduces, and has increased the accessibility of hydrogen, has improved desulfurization and denitrification effect, also makes catalyst activity be extended;
2, mixing raw material reduces the requirement of reaction conditions, has saved plant investment expense and process cost, has improved the economy of production process;
3, the quality of diesel component is obviously improved, and super low sulfur, high hexadecane value, low condensation point can meet the requirement of derv fuel oil GuoIVHuo state V standard;
4, the yield of diesel component improves, and makes carbolineum be converted into clean transport fuel completely, has widened the raw material sources of producing clean fuel.
Embodiment
Below in conjunction with specific embodiment, further illustrate the present invention, should understand these embodiment is only not used in and limits the scope of the invention for the present invention is described, after having read the present invention, those skilled in the art all fall within the application's claims limited range to the modification of the various equivalent form of values of the present invention.
Embodiment 1: the biofuel of using carbolineum and waste grease to produce is raw material.The boiling range of carbolineum is 220～535 ℃, and quality index is: density 1.15g/cm
3, total sulfur content 5350 μ g/g, total nitrogen content 1110 μ g/g, aromaticity content 91.1wt%, colloid 8.9wt%.The quality index of biofuel is: density 0.87g/cm
3, sulphur content 5 μ g/g, metal content 2.3 μ g/g, fatty acid methyl ester 97.8wt%, moisture 0.025wt%.
Carbolineum is mixed in mass ratio with biofuel at 50: 50, and then increasing temperature and pressure is fully mixed with high pressure hydrogen, sends in hydrofining reactor and reacts, catalyzer and operational condition that hydrofining is used: catalyzer is that mass content is 8%CoO-35%MoO
3/ Al
2o
3, temperature of reaction is 380 ℃, and reaction pressure is 15MPa, and hydrogen to oil volume ratio is 1600: 1, and volume space velocity is 0.5h-
1.Material flows out the oil obtaining after hydrofining reactor, sulphur content is reduced to 53 μ g/g, nitrogen content is reduced to 135 μ g/g, this oil content is heated up in a steamer, carrying out rectifying cuts apart, the cut of 360 ℃ of > is mixed with hydrogen, send in hydrocracking reactor and react, catalyzer and operational condition that hydrocracking is used: catalyzer is that active ingredient is 10%NiO/30%WO
3/ 25%Y molecular sieve, temperature of reaction is 380 ℃, and reaction pressure is 14MPa, and hydrogen to oil volume ratio is 1500: 1, and volume space velocity is 1h
-1.Material flows out the oil obtaining after hydrocracking reactor, fractionation is carried out rectifying and is cut apart, the cut of 180～360 ℃ in hydrofining and hydrocracking is mixed with hydrogen, send in hydro-upgrading reactor and react, catalyzer and operational condition that hydro-upgrading is used: catalyzer is that mass content is 18%NiO/ γ-Al
2o
3, temperature of reaction is 350 ℃, and reaction pressure is 8MPa, and hydrogen to oil volume ratio is 800: 1, and volume space velocity is 1h
-1.Material flows out the separated diesel component obtaining after hydro-upgrading reactor, i.e. high hexadecane value diesel oil of the present invention, and yield is 91.3%, its quality character is: cetane value 57.5, density 0.865g/cm
3, sulphur content 27 μ g/g, 10% steams excess carbon residue 0.22%, condensation point-22 ℃, 58 ℃ of flash-points.
Embodiment 2: the biofuel of using carbolineum and rapeseed oil to produce is raw material.The boiling range of carbolineum is 220～510 ℃, and quality index is: density 1.09g/cm
3, total sulfur content 4670 μ g/g, total nitrogen content 970 μ g/g, aromaticity content 93.3wt%, colloid 6.7wt%.The quality index of biofuel is: density 0.87g/cm
3, sulphur content 1 μ g/g, metal content 1.1 μ g/g, fatty acid methyl ester 98.1wt%.
Carbolineum is mixed in mass ratio with biofuel at 70: 30, and then increasing temperature and pressure is fully mixed with high pressure hydrogen, sends in hydrofining reactor and reacts, catalyzer and operational condition that hydrofining is used: catalyzer is that mass content is 5%CoO-28%WO
3/ Al
2o
3, temperature of reaction is 370 ℃, and reaction pressure is 12MPa, and hydrogen to oil volume ratio is 1800: 1, and volume space velocity is 0.5h
-1.Material flows out the oil obtaining after hydrofining reactor, sulphur content is reduced to 47 μ g/g, nitrogen content is reduced to 99 μ g/g, this oil content is heated up in a steamer, carrying out rectifying cuts apart, the cut of 360 ℃ of > is mixed with hydrogen, send in hydrocracking reactor and react, catalyzer and operational condition that hydrocracking is used: catalyzer is that active ingredient is 8%CoO/30%MoO
3/ 25%Y molecular sieve, temperature of reaction is 370 ℃, and reaction pressure is 15MPa, and hydrogen to oil volume ratio is 1200: 1, and volume space velocity is 0.5h
-1.Material flows out the oil obtaining after hydrocracking reactor, fractionation is carried out rectifying and is cut apart, the cut of 180～360 ℃ in hydrofining and hydrocracking is mixed with hydrogen, send in hydro-upgrading reactor and react, catalyzer and operational condition that hydro-upgrading is used: catalyzer is that mass content is 15%CoO/ γ-Al
2o
3, temperature of reaction is 330 ℃, and reaction pressure is 7MPa, and hydrogen to oil volume ratio is 800: 1, and volume space velocity is 0.5h
-1.Material flows out the separated diesel component obtaining after hydro-upgrading reactor, i.e. high hexadecane value diesel oil of the present invention, and yield is 89.7%, its quality character is: cetane value 49.6, density 0.858g/cm
3, sulphur content 31 μ g/g, 10% steams excess carbon residue 0.26%, condensation point-11 ℃, 57 ℃ of flash-points.
Embodiment 3: the biofuel of using carbolineum and waste grease to produce is raw material.The boiling range of carbolineum is 220～450 ℃, and quality index is: density 1.07g/cm
3, total sulfur content 3670 μ g/g, total nitrogen content 890 μ g/g, aromaticity content 95.2wt%, colloid 4.8wt%.The quality index of biofuel is: density 0.87g/cm
3, sulphur content 5 μ g/g, metal content 2.3 μ g/g, fatty acid methyl ester 97.8wt%, moisture 0.025wt%.
Carbolineum is mixed in mass ratio with biofuel at 80: 20, and then increasing temperature and pressure is fully mixed with high pressure hydrogen, sends in hydrofining reactor and reacts, catalyzer and operational condition that hydrofining is used: catalyzer is that mass content is 3%CoO-35%WO
3/ Al
2o
3, temperature of reaction is 340 ℃, and reaction pressure is 10MPa, and hydrogen to oil volume ratio is 1200: 1, and volume space velocity is 2h
-1.Material flows out the oil obtaining after hydrofining reactor, sulphur content is reduced to 51 μ g/g, nitrogen content is reduced to 76 μ g/g, this oil content is heated up in a steamer, carrying out rectifying cuts apart, the cut of 360 ℃ of > is mixed with hydrogen, send in hydrocracking reactor and react, catalyzer and operational condition that hydrocracking is used: catalyzer is that active ingredient is 5%CoO/25%MoO
3/ 25% beta-molecular sieve, temperature of reaction is 350 ℃, and reaction pressure is 12MPa, and hydrogen to oil volume ratio is 900: 1, and volume space velocity is 1h
-1.Material flows out the oil obtaining after hydrocracking reactor, fractionation is carried out rectifying and is cut apart, the cut of 180～360 ℃ in hydrofining and hydrocracking is mixed with hydrogen, send in hydro-upgrading reactor and react, catalyzer and operational condition that hydro-upgrading is used: catalyzer is that mass content is 10%NiO/ γ-Al
2o
3, temperature of reaction is 360 ℃, and reaction pressure is 8MPa, and hydrogen to oil volume ratio is 600: 1, and volume space velocity is 1h
-1.Material flows out the separated diesel component obtaining after hydro-upgrading reactor, i.e. high hexadecane value diesel oil of the present invention, and yield is 93.8%, its quality character is: cetane value 46.1, density 0.861g/cm
3, sulphur content 22 μ g/g, 10% steams excess carbon residue 0.18%, condensation point-21 ℃, 58 ℃ of flash-points.
Claims (10)
1. improve a production method for carbolineum hydrogenated diesel oil cetane value, it is characterized in that comprising the following steps:
Step (1): carbolineum and biofuel are formed to mixing raw material for 90: 10 in mass ratio～10: 90 and send in hydrofining reactor together with hydrogen, carry out denitrogenation, desulfurization and deoxygenation with Hydrobon catalyst, temperature of reaction is 260～420 ℃, reaction pressure is 6～18MPa, hydrogen to oil volume ratio is 800: 1～1800: 1, and volume space velocity is 0.2～5h
-1; After material outflow reactor, hydrogen, hydrogen sulfide, ammonia, water and oil are carried out separated, isolated oil content is heated up in a steamer, by 360 ℃ of 180 ℃ of <, 180～360 ℃, >, carry out cut and cut apart;
Step (2): the cut that the > that will obtain through step (1) is 360 ℃ mixes with hydrogen, send in hydrocracking reactor, react with hydrocracking catalyst, temperature of reaction is 320～400 ℃, reaction pressure is 10～16MPa, hydrogen to oil volume ratio is 600: 1～1800: 1, and volume space velocity is 0.1～2h
-1; After material outflow reactor, hydrogen, dry G&O are carried out to separation, isolated oil content is heated up in a steamer, by 360 ℃ of 180 ℃ of <, 180～360 ℃, >, carry out cut and cut apart;
Step (3): the cut of 180～360 ℃ that will obtain through step (1), step (2) mixes with hydrogen, send in hydro-upgrading reactor, react with catalyst for hydro-upgrading, temperature of reaction is 320～400 ℃, reaction pressure is 5～10MPa, hydrogen to oil volume ratio is 500: 1～1200: 1, and volume space velocity is 0.3～2h-
1; After material outflow reactor, carry out gas-oil separation, the oil obtaining is high hexadecane value diesel oil.
2. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 1, it is characterized in that: described Hydrobon catalyst comprises carrier and active ingredient, described carrier is aluminum oxide, amorphous silicon aluminium, silicon-dioxide or titanium oxide etc., the base metal of described active ingredient Wei VIII family and/or group VIB, take catalyst weight as benchmark, tungsten and/or molybdenum are counted 15wt%～35wt% with oxide compound, and nickel and/or cobalt are counted 1wt%～10wt% with oxide compound.
3. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 2, is characterized in that: take catalyst weight as benchmark, tungsten and/or molybdenum are counted 20wt%～30wt% with oxide compound, and nickel and/or cobalt are counted 2wt%～8wt% with oxide compound.
4. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 1, it is characterized in that: described hydrocracking catalyst is the dual-function catalyst simultaneously with cracking and hydrogenation: the activeconstituents of cracking function derives from H type molecular sieve, comprise ZSM series, Y or beta-molecular sieve, its content accounts for 10%～40% of catalyst weight; The active ingredient Wei VIII family of hydrogenating function and/or the metal of group VIB, take catalyst weight as benchmark, and tungsten and/or molybdenum are counted 10wt%～40wt% with oxide compound, and nickel and/or cobalt are counted 1wt%～15wt% with oxide compound.
5. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 4, is characterized in that: the activeconstituents of described cracking function derives from H type Y or beta-molecular sieve, and its content accounts for 20%～30% of catalyst weight; The active ingredient of hydrogenating function be take catalyst weight as benchmark, and tungsten and/or molybdenum are counted 15wt%～35wt% with oxide compound, and nickel and/or cobalt are counted 3wt%～10wt% with oxide compound.
6. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 1, is characterized in that: described catalyst for hydro-upgrading comprises carrier and active ingredient, and described active ingredient is supported on ZSM type molecular sieve and γ-Al with oxide form
2o
3or contain a small amount of SiO
2's
γ-Al
2o
3on carrier Deng solid acid, the metal in described active ingredient Wei VIII family, take catalyst weight as benchmark, and nickel and/or cobalt are counted 5wt%～25wt% with oxide compound.
7. a kind of production method that improves carbolineum and washing oil hydrogenated diesel oil cetane value according to claim 6, is characterized in that: take catalyst weight as benchmark, nickel and/or cobalt are counted 10wt%～20wt% with oxide compound.
8. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 1, is characterized in that: described carbolineum is the product that high temperature, middle temperature, low temperature and middle coalite tar obtain through distillation, 220～560 ℃ of boiling ranges; Described biofuel is the fatty acid methyl ester being generated by animal-plant oil and methyl alcohol, wherein: described animal-plant oil is genetically engineered soybean oil, rapeseed oil, sunflower seed oil, palm wet goods vegetables oil, the animal tallows such as pig, ox, sheep, chicken, food and drink give up sewer oil, acidifying wet goods waste grease.
9. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 1, it is characterized in that: in step (1), temperature of reaction is 320～380 ℃, and reaction pressure is 8～15MPa, hydrogen to oil volume ratio is 1000: 1～1600: 1, and volume space velocity is 0.5～3h
-1; In step (2), temperature of reaction is 350～380 ℃, and reaction pressure is 12～15MPa, and hydrogen to oil volume ratio is 900: 1～1500: 1, and volume space velocity is 0.3～1.5h
-1; In step (3), temperature of reaction is 340～380 ℃, and reaction pressure is 6～8MPa, and hydrogen to oil volume ratio is 600: 1～1000: 1, and volume space velocity is 0.5～1.5h
-1.
10. a kind of production method that improves carbolineum hydrogenated diesel oil cetane value according to claim 1, it is characterized in that: in step (1), to hydrogen, hydrogen sulfide, ammonia, water and separating of oil after, recycle after hydrogen upgrading, hydrogen sulfide, ammonia, moisture class are processed, and the cut that < that oil content heats up in a steamer is 180 ℃ is sold as petroleum naphtha or gasoline blending component; In step (2), to hydrogen, dry gas and separating of oil after, recycle after hydrogen upgrading, dry gas focuses on, the cut that < that oil content heats up in a steamer is 180 ℃ is sold as petroleum naphtha or gasoline blending component, and the cut that > is 360 ℃ is as the raw material of step (2); In step (3), after gas-oil separation, hydrogen recycle utilization.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1741767A1 (en) * | 2005-07-04 | 2007-01-10 | Neste Oil OYJ | Process for the manufacture of diesel range hydrocarbons |
| CN102464998A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Method by catalyzing and hydrogenating animal and vegetable oil to produce high-quality diesel |
| CN102585898A (en) * | 2011-12-15 | 2012-07-18 | 何巨堂 | High-nitrogen high-aromatic-oil two-stage method hydrocarbon hydrogenation method |
-
2014
- 2014-01-26 CN CN201410038006.8A patent/CN103756720A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1741767A1 (en) * | 2005-07-04 | 2007-01-10 | Neste Oil OYJ | Process for the manufacture of diesel range hydrocarbons |
| CN102464998A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Method by catalyzing and hydrogenating animal and vegetable oil to produce high-quality diesel |
| CN102585898A (en) * | 2011-12-15 | 2012-07-18 | 何巨堂 | High-nitrogen high-aromatic-oil two-stage method hydrocarbon hydrogenation method |
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Application publication date: 20140430 |