CN102260527A - New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil - Google Patents
New catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil Download PDFInfo
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Abstract
The invention relates to a novel catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil. In the process, a tail oil circulating method in which heavy oil catalytic hydroprocessing thermal cracking, distillate hydrotreatment and liquid cyolonic separation treatment of vacuum tail oil are combined is adopted. The novel catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil has the characteristics of simple complexing agent dispersion, high distillate yield, good product property and less tailings throwing amount, and can be used for treating high-sulfur high-acid high-metal, high-carbon-residue high-asphaltene inferior heavy oil which is difficultly treated by using the existing processes such as fixed bed hydrocarcking, catalytic cracking and the like; and the yield of the distillate is up to 85%-90%, and the property of the product is good, thus the novel catalytic hydroprocessing thermal cracking-hydrotreating process of high-sulfur high-acid inferior heavy oil has great popularization and application prospects.
Description
Technical field
The invention belongs to the heavy oil lighting technological process in the refining of petroleum technology, specifically, relate to a kind of catalytic hydroprocessing thermo-cracking of high-sulfur, peracid inferior heavy oil and novel process that hydrotreatment is coupled handled.
Background technology
At present, the poor quality oil output of China constantly increases, and high-sulfur, the shared ratio of high-acid crude oil also are the trend of growth in the while imported crude oil.These crude oil with poor quality have high metal, high carbon residue, high-sulfur, high nitrogen, high acid value, high viscosity and light oil and contain the low characteristics of rate, are difficult to by existing processing technology it be carried out cost-effective processing.
Very active to the research of inferior heavy oil hydrocracking or hydrogenation modifying process both at home and abroad, but major part is in pilot scale and commerical test degree, only individual processes possesses industrialized condition, and, all there is weak point separately in these technologies, the EST technology of for example 1. Italian ENI company, the decompression tail oil of this technology adopts C3 or C4 to carry out solvent deasphalting, de-oiled asphalt (mainly being bituminous matter and catalyzer) circulating reaction, though this technology has possessed industrialized condition, the reaction severity is low, and the de-oiled asphalt internal circulating load is big, the fresh feed air speed is little, and economy is not good.The HDHPLUS-SHP technology of 2. French Axens/IFP and Venezuela Intevep/PDVSA cooperative development, this technology is the one-pass scheme of fresh feed, use water-soluble catalyst, 2 reactors in series, mode by the decompression deep drawing is handled the decompression tail oil, and this technology has been finished industrial test at present, is just carrying out basic design, but exist facility investment big, the high deficiency of running energy consumption.3. the VRSH technology of Chevron company, 3 reactors in series of this process using, a spot of catalyzer separates continuously, returns use behind the reactivate by side line, rely on the combination of polystep reaction/separating step, make weight components different in the stock oil realize transforming step by step, this technology is in the industrial test stage at present, but operation is comparatively complicated, quality product is good inadequately, and the separation of catalyzer, the activation also existing problems.4. the UniflexTM technology of Uop Inc., this technology are used iron-based nano-dispersed type catalyzer, and add-on is big, and wax slop circulation cracked mode makes decompression tail oil content height in the finished product, and economy is not strong.5. the heavy oil floating bed hydrocracking technology of the common exploitation of PetroChina Company Ltd. and Petroleum Univ. (East China), this technology has been finished industrial test, but owing to use water-soluble catalyst and wax oil recycle scheme, make catalyzer disperse the energy consumption height, decompression tail oil content is big in the finished product, and the economy return rate is not high.6. in addition, the similar technology that also has other at present both at home and abroad, for example: the VCC floating bed hydrocracking technology that KBR company and the cooperation of BP company are released and (HCAT/HC) 3 technologies of Headwater company etc., these technologies all are in lab scale and pilot scale stage mostly, exist problem at aspects such as catalyzer, product property or the processing of decompression tail oil, and the raw materials that above-mentioned technology great majority are handled are not inferior heavy oil, but the long residuum of low-sulfur or sulphur-bearing crude.
Summary of the invention
The objective of the invention is to avoid above-mentioned the deficiencies in the prior art, and proposed the novel process that a kind of high-sulfur, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking and hydrotreatment of using oil soluble recombiner and tail oil recycle scheme is coupled.This technology be with handle high-sulfur, the peracid inferior heavy oil is a purpose, adopt the heavy oil lighting technology that heavy oil catalytic hydroprocessing thermo-cracking, distillate hydrogenation are handled and spinning liquid separating treatment decompression tail oil combines, have recombiner and disperse simple, distillate yield height, product property is good, the tailings amount of getting rid of is little characteristics.
Technical solution of the present invention is as follows:
A kind of high-sulfur, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment novel process, this process using the tail oil circulation means that heavy oil catalytic hydroprocessing thermo-cracking, distillate hydrogenation are handled and spinning liquid separating treatment decompression tail oil combines, its concrete technology is:
(1) adopted a kind of oil soluble recombiner in the catalytic hydroprocessing pyrolysis reactor, described catalytic hydroprocessing pyrolysis reactor operational condition is: reaction pressure 10～20MPa, 425～455 ℃ of temperature of reaction, combined feed total feed volume space velocity 0.5～1.5h
-1Hydrogen/oil volume ratio is 600～1200, the mass ratio 0.2～0.7 of circulation tail oil/fresh feed, the recombiner consumption is 0.1%～0.4% of a fresh feed, described catalytic hydroprocessing pyrolysis reactor top material enters the first hot high score, the first hot high score bottom material and catalytic hydroprocessing pyrolysis reactor bottom material enter the low branch of first heat in the lump, the low branch top of first heat noncondensable gas removes pipe network, the low bottom material that divides of first heat enters the vacuum fractionation tower, vacuum fractionation tower side stream oil, the cold oil at the first hot high score top material and the low branch top of first heat enters online fixed bed hydrogenation treatment reactor in the lump;
(2) contain the conventional hydrotreating catalysts such as hydrofining and hydrocracking that provide in the online fixed bed hydrogenation treatment reactor, reaction pressure is than the low 1～2MPa of the pressure in the catalytic hydroprocessing pyrolysis reactor, temperature of reaction is 320～420 ℃, and volume space velocity is 0.6～2.0h
-1Hydrogen/oil volume ratio is 500～1000, the product of described online fixed bed hydrogenation treatment reactor enters the second hot high score, the second hot high score top material enters cold high score, cold high score top gas desulfurization processing is after circulating hydrogen compressor enters the recycle hydrogen system, cold high score bottom material enters cold low branch, top gas was removed pipe network in cold low minute, cold low branch bottom material enters stripping tower, the stripping tower top material is gas and liquid hydrocarbon product, the second hot high score bottom material enters the low branch of second heat, the low branch top gas of second heat is removed pipe network, and low bottom material and the stripping tower bottom material of dividing of second heat enters atmospheric fractional tower in the lump, and the atmospheric fractional tower top material is a naphtha product, the side line material is a diesel product, and the bottom material is that vacuum distillate is the wax oil product;
(3) wet cyclone is used to handle the effusive decompression tail oil of vacuum fractionation tower bottom, the decompression tail oil mixed by mass ratio with solvent in 1: 1～1: 4, enter wet cyclone, 80～150 ℃ of temperature, carrying out spinning liquid under pressure 0.5～2.0MPa condition separates, the spinning liquid top flows to into top stream solvent recovery tower, the spinning liquid underflow enters the underflow solvent recovery tower, top stream solvent recovery tower and underflow solvent recovery tower service temperature are 200～250 ℃, working pressure is a normal pressure, top stream solvent recovery tower and underflow solvent recovery tower top material are as circulating solvent, mix with the decompression tail oil in the lump with fresh solvent, top stream solvent recuperation tower bottom material is as the circulation tail oil, with fresh feed, recombiner, hydrogen mixes, and underflow solvent recuperation tower bottom material goes out device as effluxing tailings.
Further preferred, the oil soluble recombiner described in the step (1) mainly comprises the auxiliary agent of two components or three component oil solube metallic catalyzer, vulcanizing agent and inhibition coking.Described two components or three component oil solube metallic catalyzer are oil-soluble molybdenum-nickel salt, oil soluble cobalt-nickel salt, oil-soluble molybdenum-Ni-Fe salt, oil soluble Co-Ni-Fe salt; Described vulcanizing agent is sulphur powder or dithiocarbonic anhydride; The auxiliary agent of described inhibition coking is a kind of or several mixture of cationic surfactant, anion surfactant, lipid acid and aliphatic amide.
High-sulfur of the present invention, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment novel process, catalytic hydroprocessing pyrolysis reactor described in the step (1) are to have the reactor of discharge function up and down.
High-sulfur of the present invention, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment new technological flow are: install external stock oil certainly and come from recombiner that the recombiner pump extracts out after multistage static mixer and multi-buffer jar mix, with the incoming stock in the lump oily surge tank of the turning oil in the circulation oil tank, surge tank adopts mechanical stirring or pump round-robin mode, makes recombiner, stock oil and turning oil thorough mixing even.Mixed raw material with the high pressure charging pump extract out through after the heat exchange with from the external fresh hydrogen of device and come from the incoming stock in the lump oily process furnace of recycle hydrogen of circulating hydrogen compressor, enter the catalytic hydroprocessing pyrolysis reactor again after being heated to 425～455 ℃ of predetermined temperature of reaction.In the catalytic hydroprocessing pyrolysis reactor, mix hydrogen and stock oil the catalytic hydroprocessing heat scission reaction takes place under the effect of high temperature, high pressure and catalyzer.Reach 420～440 ℃ from the effusive reaction product temperature in catalytic hydroprocessing pyrolysis reactor top, in order to prevent coking in in-line and the high pressure hot separator, inject at the reactor head pipeline and to enter the first hot high score after light cycle oil is chilled to 400 ℃, the vacuum distillate of the gas that flashes off from the first hot high score top and cold oil that comes from the low branch top of first heat and vacuum fractionation tower side line enters online fixed bed hydrogenation treatment reactor in the lump and carries out hydrotreatment.After being chilled to 400 ℃, enter the low branch of first heat in the lump from the effusive reaction product in catalytic hydroprocessing pyrolysis reactor bottom with the first hot high score bottom material, the gas that flashes off from the low branch top of first heat enters online fixed bed hydrogenation treatment reactor in the lump through the side stream oil of cooled cold oil and vacuum fractionation tower, non-condensable gas enters pipe network, and the low generation oil of bottom that divides of first heat enters the decompression process furnace.Online fixed bed hydrogenation treatment reactor bottoms enters the second hot high score, the gas that the second hot high score top flashes off enters cold high score, cold high score top gas desulfurization processing is after circulating hydrogen compressor enters the recycle hydrogen system, cold high score bottom cold oil enters cold low branch, top gas entered pipe network in cold low minute, and cold low branch bottom cold oil enters fractionating system; The second hot high score bottom material enters the low branch of second heat, and the low branch top gas of second heat enters pipe network, and the low branch of second heat bottom material enters fractionating system.
The generation oil of the low branch of first heat bottom enters the decompression process furnace and enter the vacuum fractionation tower after heating, the cold oil at gas that the tower side line vacuum distillate and the first hot high score top flash off and the low branch top of first heat enters online fixed bed hydrogenation treatment reactor in the lump after heat exchange, vacuum residuum enters decompression tail oil solvent treatment system at the bottom of the tower.Cold low branch bottom cold oil enters stripping tower, the cat head effluent is gas and liquid hydrocarbon product, bottoms material and the low branch of second heat bottom material enter atmospheric pressure kiln in the lump and enter atmospheric fractional tower after heating, often after the fractionation of pressure fractionating tower, cat head is that naphtha fraction is as cracking of ethylene raw material or catalytic reforming raw material, the tower side line flows out diesel oil distillate directly as diesel product, and it is the stock oil of wax oil as catalytic cracking unit that tower bottom flow goes out vacuum distillate.
It is behind 1: 1～1: 4 the solvent, to enter wet cyclone that vacuum residuum at the bottom of the vacuum fractionation Tata mixes its mass ratio, revolves the branch top and flows to into top stream solvent recovery tower, revolves the branch underflow and enters the underflow solvent recovery tower.The recovery solvent that top stream solvent recovery tower and underflow solvent recuperation column overhead obtain is in the lump as circulating solvent, circulating solvent is with after fresh solvent mixes, with vacuum residuum by certain mass than mixing, top stream solvent recuperation tower bottom material as the circulation tail oil with enter the stock oil surge tank after fresh feed, recombiner mix, the conduct of underflow solvent recuperation tower bottom material effluxes the tailings product.
High-sulfur of the present invention, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking one hydrotreatment novel process are with the difference of existing all kinds of hydrogenation techniques:
(1) process object of this technology is high-sulfur, peracid, high metal, high carbon residue, high bitum inferior heavy oil.
(2) the catalytic hydroprocessing pyrolysis reactor of this technology uses a kind of oil soluble recombiner, this oil soluble recombiner mainly comprises the auxiliary agent of two components or three component oil solube metallic catalyzer, vulcanizing agent and inhibition coking, and described two components or three component oil solube metallic catalyzer are oil-soluble molybdenum-nickel salt, oil soluble cobalt-nickel salt, oil-soluble molybdenum-Ni-Fe salt, oil soluble Co-Ni-Fe salt; Described vulcanizing agent is sulphur powder or dithiocarbonic anhydride; The auxiliary agent of described inhibition coking is a kind of or several mixture of cationic surfactant, anion surfactant, lipid acid and aliphatic amide.The dispersing technology simple possible of this recombiner in stock oil, energy consumption is low.
(3) this process using tail oil recycle scheme, main products are petroleum naphtha, diesel oil, vacuum distillate and a spot of tailings that effluxes.
(4) mode that combines of this process using catalytic hydroprocessing pyrolysis reactor and online fixed bed hydrogenation treatment reactor has not only made full use of existing temperature of reaction and pressure, and has made product property good.
(5) this process using the isolating mode of spinning liquid handle tail oil, make that the loop tail oil nature is better, be difficult for green coke, reduced the outer discharge capacity of tailings simultaneously.
Compared with prior art, beneficial effect of the present invention is:
(1) dispersing technology of oil soluble recombiner is simple, and energy consumption is little, and the recombiner consumption is little, and cost is low, processes the employed recombiner cost of fresh feed per ton less than 100 yuans.
(2) catalytic hydroprocessing heat scission reaction temperature height is 425～455 ℃, and distillate yield height is 85%～90%, and the system green coke lacks it less than 1%.
(3) handle through online fixed bed hydrogenation less than 480 ℃ of cuts, product characteristics is good, naphtha fraction can be used as catalytic reforming or cracking of ethylene raw material, and diesel oil distillate can be directly as high-quality clean diesel product, and vacuum distillate can be used as the raw material of catalytic cracking unit.
The present invention can handle the reluctant high-sulfur of technology, peracid, high metal, high carbon residue, high bitum inferior heavy oil such as existing fixed bed hydrogenation cracking, catalytic cracking, its distillate yield is up to 85%～90%, product property is good, therefore has great popularizing application prospect.
Description of drawings
Fig. 1 is the schema of high-sulfur of the present invention, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment novel process.
Embodiment
Below in conjunction with the drawings and specific embodiments novel process of the present invention is described in further detail.In actual design and in service, planner of the present invention adopts technical process as shown in drawings, fresh feed, circulation tail oil and oil soluble recombiner mix through multi-buffer jar and multistage static mixer, and this hybrid mode can guarantee that a spot of recombiner is evenly dispersed in a large amount of raw materials.Compound is mixed into process furnace with fresh hydrogen and recycle hydrogen again, after being heated to 425～455 ℃, process furnace enters the catalytic hydroprocessing pyrolysis reactor from the bottom, at reaction pressure 10～20MPa, carry out the catalytic hydroprocessing heat scission reaction under 425～455 ℃ of conditions of temperature of reaction, higher temperature of reaction can guarantee higher transformation efficiency, the existence of recombiner can reduce green coke and the coking in the reactor, guarantees the long-term operation of technology.
Reach 420～440 ℃ from the effusive reaction product temperature in catalytic hydroprocessing pyrolysis reactor top, in order to prevent coking in in-line and the high pressure hot separator, inject at the reactor head pipeline and to enter the first hot high score after light cycle oil is chilled to 400 ℃, the vacuum distillate of the gas that flashes off from the first hot high score top and cold oil that comes from the low branch top of first heat and vacuum fractionation tower side line enters online fixed bed hydrogenation treatment reactor in the lump and carries out hydrotreatment.After being chilled to 400 ℃, enter the low branch of first heat in the lump from the effusive reaction product in catalytic hydroprocessing pyrolysis reactor bottom with the first hot high score bottom material, the gas that flashes off from the low branch top of first heat enters online fixed bed hydrogenation treatment reactor in the lump through the side stream oil of cooled cold oil and vacuum fractionation tower, non-condensable gas enters pipe network, and the low generation oil of bottom that divides of first heat enters the decompression process furnace.Online fixed bed hydrogenation treatment reactor bottoms enters the second hot high score, the gas that the second hot high score top flashes off enters cold high score, cold high score top gas desulfurization processing is after circulating hydrogen compressor enters the recycle hydrogen system, cold high score bottom cold oil enters cold low branch, top gas entered pipe network in cold low minute, and cold low branch bottom cold oil enters fractionating system; The second hot high score bottom material enters the low branch of second heat, and the low branch top gas of second heat enters pipe network, and the low branch of second heat bottom material enters fractionating system.This technology mode can guarantee that petroleum naphtha, diesel oil and the reduced pressure distillate oil production behind the catalytic hydroprocessing heat scission reaction all can obtain hydrotreatment, improves product property.
The generation oil of the low branch of first heat bottom enters the decompression process furnace and enter the vacuum fractionation tower after heating, the cold oil at gas that the tower side line vacuum distillate and the first hot high score top flash off and the low branch top of first heat enters online fixed bed hydrogenation treatment reactor in the lump after heat exchange, vacuum residuum enters decompression tail oil solvent treatment system at the bottom of the tower.Cold low branch bottom cold oil enters stripping tower, the cat head effluent is gas and liquid hydrocarbon product, bottoms material and the low branch of second heat bottom material enter atmospheric pressure kiln in the lump and enter atmospheric fractional tower after heating, often after the fractionation of pressure fractionating tower, cat head is that naphtha fraction is as cracking of ethylene raw material or catalytic reforming raw material, the tower side line flows out diesel oil distillate directly as diesel product, and tower bottom flow goes out the stock oil of vacuum distillate (wax oil) as catalytic cracking unit.
It is behind 1: 1～1: 4 the solvent, to enter wet cyclone that vacuum residuum at the bottom of the vacuum fractionation Tata mixes its mass ratio, revolves the branch top and flows to into top stream solvent recovery tower, revolves the branch underflow and enters the underflow solvent recovery tower.The recovery solvent that top stream solvent recovery tower and underflow solvent recuperation column overhead obtain is in the lump as circulating solvent, circulating solvent is with after fresh solvent mixes, with vacuum residuum by certain mass than mixing, top stream solvent recuperation tower bottom material as the circulation tail oil with enter the stock oil surge tank after fresh feed, recombiner mix, the conduct of underflow solvent recuperation tower bottom material effluxes the tailings product.This decompression tail oil processing mode can guarantee to circulate and contain less easy green coke component in the tail oil, and reduces the outer discharge capacity of tailings.
Be the example that Venezuela's oil fuel is carried out pilot scale by technical process of the present invention below:
The reaction conditions of Venezuela's oil fuel on 30 tons of/year catalytic hydroprocessing thermo-crackings and hydrotreatment pilot plant is: 440 ℃ of catalytic hydroprocessing thermo-cracking temperature, and reaction pressure 12.0MPa, hydrogen/oil volume is than 800: 1, combined feed total feed air speed 1.0h
-1, fresh feed air speed 0.74h
-1Fixed bed hydrogenation is handled 365 ℃ of average reaction temperature, reactor outlet stagnation pressure 11.0MPa, and hydrogen/oil volume is than 800: 1, charging air speed 0.8h
-1Account for about 90% of fresh feed less than 480 ℃ of products in the product, concrete data are as follows:
(1) Venezuela's oil fuel reaction after product distributes
| Products distribution, w% | Numerical value |
| Dry gas | 2.31 |
| Liquefied gas | 3.75 |
| Petroleum naphtha (IBP～180 ℃) | 9.75 |
| Diesel oil distillate (180～350 ℃) | 40.26 |
| Vacuum distillate (350～480 ℃) | 33.75 |
| Efflux tailings | 10.18 |
| Add up to | 100 |
| The hydrogen consumption | 2.30 |
(2) naphtha fraction (IBP～180 ℃) is formed and character
| Project | Numerical value |
| Fractions consisting, ℃ | IBP～180 |
| Hydrocarbon system forms, w% | ? |
| Normal paraffin | 17.02 |
| Isoparaffin | 37.15 |
| Alkene | 0.00 |
| Naphthenic hydrocarbon | 26.01 |
| Aromatic hydrocarbon | 19.82 |
| Density (20 ℃), gcm -3 | 0.7723 |
| Acidity, mgKOH/100ml | 0.21 |
| S，μg·ml -1 | 38.22 |
| N，μg·ml -1 | 14.21 |
| Basic nitrogen, μ gg -1 | 5.03 |
| Octane value (organon) | 78 |
(3) diesel oil distillate (180～350 ℃) is formed and character
| Project | Numerical value |
| Fractions consisting, ℃ | 180～350 |
| Density (20 ℃), gcm -3 | 0.8568 |
| Viscosity (50 ℃), mm 2·s -1 | 3.31 |
| Condensation point, ℃ | -24.0 |
| Acidity, mgKOH/100ml | 0.50 |
| S，μg·g -1 | 39.71 |
| N，μg·g -1 | 19.54 |
| Basic nitrogen, μ gg -1 | 7.42 |
| Colourity, number | 0.5 |
| Flash-point, ℃ | 87.0 |
| Cetane value | 50 |
(4) reduced pressure distillate oil distillate (350～480 ℃) is formed and character
| Project | Numerical value |
| Fractions consisting, ℃ | 350～480 |
| Density (20 ℃), gcm -3 | 0.8912 |
| Viscosity (50 ℃), mm 2·s -1 | 32.42 |
| Viscosity (80 ℃), mm 2·s -1 | 8.76 |
| Condensation point, ℃ | 26 |
| Acid number, mgKOH/g | 0.06 |
| Carbon residue, w% | 0.12 |
| C，w％ | 86.61 |
| H，w％ | 13.10 |
| S，μg·g -1 | 237.61 |
| N，μg·g -1 | 54.83 |
Claims (3)
1. a high-sulfur, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment novel process, it is characterized in that, this process using the tail oil circulation means that heavy oil catalytic hydroprocessing thermo-cracking, distillate hydrogenation are handled and spinning liquid separating treatment decompression tail oil combines, its concrete technology is:
(1) adopted a kind of oil soluble recombiner in the catalytic hydroprocessing pyrolysis reactor, described catalytic hydroprocessing pyrolysis reactor operational condition is: reaction pressure 10～20MPa, 425～455 ℃ of temperature of reaction, combined feed total feed volume space velocity 0.5～1.5h
-1Hydrogen/oil volume ratio is 600～1200, the mass ratio 0.2～0.7 of circulation tail oil/fresh feed, the recombiner consumption is 0.1%～0.4% of a fresh feed, described catalytic hydroprocessing pyrolysis reactor top material enters the first hot high score, the first hot high score bottom material and catalytic hydroprocessing pyrolysis reactor bottom material enter the low branch of first heat in the lump, the low branch top of first heat noncondensable gas removes pipe network, the low bottom material that divides of first heat enters the vacuum fractionation tower, vacuum fractionation tower side stream oil, the cold oil at the first hot high score top material and the low branch top of first heat enters online fixed bed hydrogenation treatment reactor in the lump;
(2) contain the conventional hydrotreating catalysts such as hydrofining and hydrocracking that provide in the online fixed bed hydrogenation treatment reactor, reaction pressure is than the low 1～2MPa of the pressure in the catalytic hydroprocessing pyrolysis reactor, temperature of reaction is 320～420 ℃, and volume space velocity is 0.6～2.0h
-1Hydrogen/oil volume ratio is 500～1000, the product of described online fixed bed hydrogenation treatment reactor enters the second hot high score, the second hot high score top material enters cold high score, cold high score top gas desulfurization processing is after circulating hydrogen compressor enters the recycle hydrogen system, cold high score bottom material enters cold low branch, top gas was removed pipe network in cold low minute, cold low branch bottom material enters stripping tower, the stripping tower top material is gas and liquid hydrocarbon product, the second hot high score bottom material enters the low branch of second heat, the low branch top gas of second heat is removed pipe network, and low bottom material and the stripping tower bottom material of dividing of second heat enters atmospheric fractional tower in the lump, and the atmospheric fractional tower top material is a naphtha product, the side line material is a diesel product, and the bottom material is that vacuum distillate is the wax oil product;
(3) wet cyclone is used to handle the effusive decompression tail oil of vacuum fractionation tower bottom, the decompression tail oil mixed by mass ratio with solvent in 1: 1～1: 4, enter wet cyclone, 80～150 ℃ of temperature, carrying out spinning liquid under pressure 0.5～2.0MPa condition separates, the spinning liquid top flows to into top stream solvent recovery tower, the spinning liquid underflow enters the underflow solvent recovery tower, top stream solvent recovery tower and underflow solvent recovery tower service temperature are 200～250 ℃, working pressure is a normal pressure, top stream solvent recovery tower and underflow solvent recovery tower top material are as circulating solvent, mix with the decompression tail oil in the lump with fresh solvent, top stream solvent recuperation tower bottom material is as the circulation tail oil, with fresh feed, recombiner, hydrogen mixes, and underflow solvent recuperation tower bottom material goes out device as effluxing tailings.
2. high-sulfur according to claim 1, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment novel process, it is characterized in that the oil soluble catalytic hydroprocessing thermo-cracking recombiner described in the step (1) mainly comprises the auxiliary agent of two components or three component oil solube metallic catalyzer, vulcanizing agent and inhibition coking.Described two components or three component oil solube metallic catalyzer are oil-soluble molybdenum-nickel salt, oil soluble cobalt-nickel salt, oil-soluble molybdenum-Ni-Fe salt, oil soluble Co-Ni-Fe salt; Described vulcanizing agent is sulphur powder or dithiocarbonic anhydride; The auxiliary agent of described inhibition coking is a kind of or several mixture of cationic surfactant, anion surfactant, lipid acid and aliphatic amide.
3. high-sulfur according to claim 1, peracid inferior heavy oil catalytic hydroprocessing thermo-cracking-hydrotreatment novel process is characterized in that, catalytic hydroprocessing pyrolysis reactor described in the step (1) is to have the reactor of discharge function up and down.
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| CN104164255A (en) * | 2013-05-20 | 2014-11-26 | 中国石油大学(华东) | Inferior heavy oil hydro-thermal cracking and tail oil decarbonization composite process and device |
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| CN108587668A (en) * | 2018-03-29 | 2018-09-28 | 南京大学连云港高新技术研究院 | A kind of method of inferior heavy oil cracking waste plastics desulfurization visbreaking production light petroleum gas |
| CN112500916A (en) * | 2020-11-12 | 2021-03-16 | 中国石油大学(华东) | Method for purifying waste lubricating oil by hydrogen pretreatment |
| CN112500917A (en) * | 2020-11-12 | 2021-03-16 | 中国石油大学(华东) | Waste lubricating oil hydrogenation recycling method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104164255A (en) * | 2013-05-20 | 2014-11-26 | 中国石油大学(华东) | Inferior heavy oil hydro-thermal cracking and tail oil decarbonization composite process and device |
| WO2016176983A1 (en) * | 2015-05-07 | 2016-11-10 | 北京中科诚毅科技发展有限公司 | Hydrogenation process temperature control method, and design method therefor and use thereof |
| CN108587668A (en) * | 2018-03-29 | 2018-09-28 | 南京大学连云港高新技术研究院 | A kind of method of inferior heavy oil cracking waste plastics desulfurization visbreaking production light petroleum gas |
| CN112500916A (en) * | 2020-11-12 | 2021-03-16 | 中国石油大学(华东) | Method for purifying waste lubricating oil by hydrogen pretreatment |
| CN112500917A (en) * | 2020-11-12 | 2021-03-16 | 中国石油大学(华东) | Waste lubricating oil hydrogenation recycling method |
| CN112500917B (en) * | 2020-11-12 | 2022-04-26 | 青岛翌星环保技术有限公司 | Waste lubricating oil hydrogenation recycling method |
| WO2022100763A1 (en) * | 2020-11-12 | 2022-05-19 | 中国石油大学(华东) | Hydrogenating cyclic utilization method for waste lubricating oil |
| CN113088330A (en) * | 2021-03-15 | 2021-07-09 | 西安近代化学研究所 | Thermal cracking coupling mild hydrogenation method for heavy oil |
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| CN102260527B (en) | 2014-05-28 |
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