CN115537231B - Method for realizing oil reduction and oil increase by changing material flow direction - Google Patents
Method for realizing oil reduction and oil increase by changing material flow direction Download PDFInfo
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- CN115537231B CN115537231B CN202211273205.8A CN202211273205A CN115537231B CN 115537231 B CN115537231 B CN 115537231B CN 202211273205 A CN202211273205 A CN 202211273205A CN 115537231 B CN115537231 B CN 115537231B
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- 238000000034 method Methods 0.000 title claims abstract description 25
- 230000009467 reduction Effects 0.000 title claims description 7
- 239000002994 raw material Substances 0.000 claims abstract description 61
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 37
- 238000002156 mixing Methods 0.000 claims abstract description 33
- 238000005336 cracking Methods 0.000 claims abstract description 21
- 239000002283 diesel fuel Substances 0.000 claims abstract description 19
- 239000003350 kerosene Substances 0.000 claims abstract description 15
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000005977 Ethylene Substances 0.000 claims abstract description 8
- 238000012545 processing Methods 0.000 claims abstract description 4
- 238000006243 chemical reaction Methods 0.000 claims description 61
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 36
- 239000007789 gas Substances 0.000 claims description 36
- 238000007670 refining Methods 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 21
- 229910052757 nitrogen Inorganic materials 0.000 claims description 18
- 238000007599 discharging Methods 0.000 claims description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims description 13
- 239000001257 hydrogen Substances 0.000 claims description 12
- 239000012071 phase Substances 0.000 claims description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 9
- 230000008569 process Effects 0.000 claims description 9
- 238000010992 reflux Methods 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 8
- 238000011084 recovery Methods 0.000 claims description 8
- 239000004215 Carbon black (E152) Substances 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000011001 backwashing Methods 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 3
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000003921 oil Substances 0.000 claims description 3
- 238000005191 phase separation Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 9
- 238000004523 catalytic cracking Methods 0.000 abstract description 6
- 238000013461 design Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 230000003197 catalytic effect Effects 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract description 2
- 238000012824 chemical production Methods 0.000 abstract description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 13
- 239000000047 product Substances 0.000 description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 10
- 239000011593 sulfur Substances 0.000 description 10
- 229910052717 sulfur Inorganic materials 0.000 description 10
- 238000004821 distillation Methods 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 7
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 5
- 239000003546 flue gas Substances 0.000 description 5
- 238000005194 fractionation Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
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- 208000012839 conversion disease Diseases 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
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- 238000010586 diagram Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
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- -1 ethylene, propylene, butadiene Chemical class 0.000 description 2
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- 238000004064 recycling Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
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- 208000027697 autoimmune lymphoproliferative syndrome due to CTLA4 haploinsuffiency Diseases 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
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- 238000007405 data analysis Methods 0.000 description 1
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- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000004767 nitrides Chemical class 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
Abstract
The invention discloses a device and a method for reducing and increasing oil by changing the flow direction of a material, comprising a wax oil hydrotreating system and a wax oil hydrocracking system, wherein straight-run heavy wax oil of an atmospheric and vacuum device is converted into hydrogenated wax oil to be used as a raw material of the wax oil hydrocracking system, the hydrogenated wax oil produced by the wax oil hydrotreating system is sent to the wax oil catalytic cracking system for processing according to the design, mainly produces stable gasoline, participates in gasoline blending, and produces by-product catalytic diesel oil and liquefied gas, if the hydrogenated wax oil is sent to the wax oil hydrocracking system, the heavy naphtha is mainly produced, aviation kerosene, diesel oil and hydrogenated tail oil are produced, the benefit is better than that of gasoline production, and the heavy naphtha and the hydrogenated tail oil are raw materials urgently needed by a chemical production device, so that the yield of finished oil is greatly reduced, the yield of aromatic hydrocarbon and ethylene cracking raw materials is increased, and the economic benefit of the material is forcefully improved.
Description
Technical Field
The invention relates to a method for realizing oil reduction and increase, in particular to a method for realizing oil reduction and increase by changing material flow direction, belonging to the field of petrochemical industry.
Background
As shown in fig. 1, in the prior art, the heavy wax oil produced by the atmospheric and vacuum device is sent to the wax oil hydrotreatment, the straight-run heavy wax oil is subjected to catalytic hydrogenation reaction by a hydrogenation reactor by utilizing the fixed bed wax oil hydrodesulfurization process technology, sulfur, nitrogen, metal and other impurities are removed, the produced hydrogenated wax oil is supplied to a wax oil catalytic cracking device, and the wax oil catalytic cracking device consists of parts such as reaction, regeneration, fractionation, stable absorption, a rich gas compressor unit, a flue gas energy recovery unit, a standby main fan unit, a flue gas waste heat boiler, flue gas desulfurization and denitrification and the like.
Description of the flow:
1) Wax oil hydroprocessing (system): the method comprises the steps of removing suspended particles from straight-run heavy wax oil of an atmospheric and vacuum device through an automatic backwashing system after heat exchange and temperature rising, boosting the raw material leaving a hot raw material buffer tank (raw material tank) to the pressure required by reaction through a high-pressure pump, exchanging heat with a reactor product, providing the rest required heat by a reaction feeding heating furnace, feeding the raw material into a hydrogenation reactor after passing through the heating furnace, controlling the outlet temperature of the heating furnace to reach the required temperature requirement of the reactor, introducing cold circulation quenching hydrogen between bed layers of the hydrogenation reactor to control the reaction temperature rising, and generating in the reactor: hydrodesulfurization reaction, hydrodemetallization reaction, hydrodenitrogenation reaction, aromatic hydrocarbon saturation reaction, olefin saturation reaction and hydrocracking reaction, wherein the reaction product of the reactor exchanges heat with raw materials and stripping tower bottom oil and then is sent to a dehydrosulfuration stripping tower, tower bottom materials for removing hydrogen sulfide gas enter a fractionating tower, and finally hydrogenated wax oil generated at the tower bottom of the fractionating tower is sent to a downstream device to be used as raw materials;
2) Wax oil catalytic cracking (system): the hydrogenated wax oil is pumped by an oil pump and sent to a raw material tank, is heated to a preset temperature by a raw material preheating furnace, enters a lifting pipe, contacts with a high-temperature catalyst which is from a regeneration inclined pipe and is lifted by pre-lifting steam to perform catalytic cracking reaction upwards, and reaction oil and gas are separated in a reaction settler. The oil gas enters a reaction oil gas pipeline of the recovery metering system through the gas collecting pipe. The coked spent catalyst flows into a stripping section, is stripped by stripping steam, flows down to a regenerator through a spent riser and a spent plug valve, and is in reverse contact with air entering from an air distribution pipe in the regenerator to burn off the coke on the catalyst to restore the activity of the catalyst. The flue gas generated by the burning enters a regenerated flue gas pipeline of the recovery metering system through the filter. The regenerated catalyst enters the bottom of the lifting pipe through the regeneration inclined pipe and is in contact with the raw material for recycling. The oil gas entering the reaction oil gas path enters the lower part of the fractionating tower, and the oil gas at the top of the fractionating tower enters the oil-gas separator at the top of the fractionating tower for gas, liquid and water separation after air cooling and water cooling. The separated liquid (crude gasoline) is sent into an absorption tower after being pressurized, dry gas is discharged from the top of the absorption tower, condensed oil at the bottom of the tower enters a stabilizing tower through a buffer tank, liquefied gas is resolved at the top of the tower, and the crude gasoline produced at the bottom of the tower is sent out of a device to participate in gasoline blending.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides the method for reducing and increasing the oil by changing the material flow direction, which has the technical characteristics of reducing the yield of the finished oil, optimizing the flow direction of wax oil components, increasing the yield of aromatic hydrocarbon and ethylene raw materials, having good economic benefit and the like.
In order to achieve the above purpose, the present invention is realized by the following technical scheme:
the invention discloses a device for reducing and increasing oil by changing the flow direction of a material, which comprises a wax oil hydrotreating system and a wax oil hydrocracking system connected with the wax oil hydrotreating system, wherein the wax oil hydrotreating system converts straight-run heavy wax oil of an atmospheric and vacuum device into hydrogenated wax oil to be used as a raw material of the wax oil hydrocracking system;
the wax oil hydrocracking system comprises a raw material tank, wherein the raw material tank is connected with a reaction feed heating furnace through a pipeline, the reaction feed heating furnace is connected with the upper end of a refining reactor through a pipeline, the lower end of the refining reactor is connected with the upper end of a cracking reactor through a pipeline, the lower end of the cracking reactor is connected with a stripping tower through a pipeline, the lower end of the stripping tower is sequentially connected with a wax feed tank, a fractionating tower heating furnace and a fractionating tower through pipelines, the upper end of the stripping tower is connected with a stripping tower discharge pipeline, and a plurality of material discharge pipelines are respectively arranged on the fractionating tower; the device also comprises a new hydrogen machine, wherein three pipelines are respectively arranged at the outlet end of the new hydrogen machine and are respectively connected to the upper end part of the refining reactor, the upper end part of the cracking reactor and the pipeline between the reaction feeding heating furnace and the refining reactor.
Preferably, the material discharge pipeline comprises a first discharge pipeline, a second discharge pipeline, a third discharge pipeline and a fourth discharge pipeline, the upper end and the lower end of the fractionating tower are respectively connected with the first discharge pipeline and the second discharge pipeline, and the middle part of the fractionating tower is independently connected with the third discharge pipeline for discharging aviation kerosene and the fourth discharge pipeline for discharging diesel oil.
Preferably, the stripper discharge line is provided with a fifth discharge line for discharging acid gas and a sixth discharge line for discharging heavy stones, and the first discharge line is connected with the sixth discharge line.
The invention discloses a method for realizing oil reduction and oil increase by changing the flow direction of materials, which comprises the following steps:
1) The method comprises the steps of mixing and feeding hydrogenated wax oil produced by a wax oil hydrotreating system with straight-run light wax oil produced by an atmospheric and vacuum device, exchanging heat with diesel oil, then automatically backwashing a filter through the raw oil to remove solid particles larger than 25 mu m, and then entering a raw material tank (raw oil buffer tank);
2) The mixture in the raw material tank is boosted by a reaction feed pump and then enters a reaction feed heating furnace, the reaction temperature is raised to be preferably 363 ℃, then the mixture sequentially enters a refining reactor (a hydrogenation reactor) and a cracking reactor for respectively carrying out hydrofining and hydrocracking reactions, and the reaction effluent, raw material oil and recycle hydrogen exchange heat to be preferably 282 ℃ and enter a thermal high-pressure separator;
3) The reaction effluent in the hot high-pressure separator is further sent to a stripping tower, the bottom of the stripping tower is fed with steam for stripping, the upper end of the stripping tower is stripped by acid gas and oil phase, wherein the acid gas and light hydrocarbon removing recovery device is used for further recovering liquefied gas, the oil phase at the top of the stripping tower is sent to a naphtha hydrofining device, the lower end of the stripping tower is used for obtaining stripping bottom oil, and the stripping bottom oil enters a wax feeding tank to be used as a fractionating tower for feeding;
4) The stripping tower bottom oil is subjected to heat exchange with a process material flow, is heated by a fractionating tower feeding heating furnace and then enters a fractionating tower;
5) The gas phase at the top of the fractionating tower enters a reflux tank after being condensed and cooled, the liquid phase of the fractionating tower is boosted by a reflux pump at the top of the fractionating tower and then goes to a light hydrocarbon recovery device, the fractionating tower is provided with independent side-stream extraction aviation kerosene and diesel oil which respectively enter a product tank, and the hydrogenated tail oil is discharged from the bottom of the fractionating tower and is sent to a cracking furnace as an ethylene raw material after heat exchange and cooling.
Preferably, the gas phase at the top of the stripping tower is cooled by an air cooler and a aftercooler and then enters a reflux tank at the top of the stripping tower to carry out oil, gas and water three-phase separation.
The beneficial effects are that: the invention makes full use of the load allowance of the existing wax oil hydrocracking device, changes the heavy wax oil component after hydrogenation from the catalytic device to the wax oil hydrocracking device, greatly reduces the yield of finished oil, increases the yield of cracking raw materials of aromatic hydrocarbon and ethylene, and strongly improves the economic benefit of the materials. Can be spread in the field of complex petrochemical industry in the same kind and has wide application prospect.
Drawings
FIG. 1 is a process flow diagram of the catalytic gasoline produced by heavy wax oil produced by an atmospheric and vacuum device in the prior art.
Fig. 2 is a process flow diagram of the present invention.
FIG. 3 is a graph showing the comparison of carbon residue in the feedstock of the present invention.
FIG. 4 is a graph showing the comparison of sulfur content in the feedstock of the present invention.
FIG. 5 is a plot of initial boiling point comparisons of the feedstock of the present invention.
FIG. 6 is a plot of 98% point-to-point comparison of the feedstock of the present invention.
FIG. 7 is a graph of the density of the feedstock of the present invention.
FIG. 8 is a graph comparing nitrogen content of the feedstock of the present invention.
FIG. 9 is a graph comparing the yields of heavy naphtha and aviation kerosene before and after blending in accordance with the present invention.
FIG. 10 is a graph comparing the 98% fractionation point and BMCI values of tail oil before and after blending in accordance with the present invention.
FIG. 11 is a graph showing the temperature change of the reaction before and after blending according to the present invention.
Description of the embodiments
The present invention will be further described with reference to the accompanying drawings, but the present invention is not limited to the following examples.
The hydrogenated wax oil produced by the wax oil hydrotreating system (device) is sent to the wax oil catalytic cracking system for processing according to the design, and stable gasoline is mainly produced to participate in gasoline blending; the byproduct part catalyzes diesel oil and liquefied gas. If the hydrogenated wax oil is sent to a wax oil hydrocracking system (device), heavy naphtha is mainly produced, aviation kerosene, diesel oil and hydrogenated tail oil are produced, the benefits of the four products are better than those of gasoline production, and the heavy naphtha and the hydrogenated tail oil are raw materials needed by chemical production devices.
At present, the finished oil has an excessive phenomenon, and new large-scale integrated refineries are put into production in the future, and the popularization of new energy automobiles is added, so that the market of the finished oil is limited; the basic organic chemical raw materials such as ethylene, propylene, butadiene, benzene, toluene and xylene are also insufficient in structural supply, and the development of the chemical products has a certain space from the current development trend. In order to achieve the aim of maximizing benefit, a method is developed, according to the physical and chemical properties of materials, after full evaluation, the hydrogenated wax oil produced by a wax oil hydrotreater is changed into a wax oil hydrocracking device, a single-stage series once-through process flow is adopted, and the hydrogenation wax oil is subjected to a reaction part (comprising a new hydrogen compressor part, a high-pressure separation part and a circulating hydrogen desulfurization part), a fractionation part (comprising H) 2 The stripper part, the fractionating tower part, the heavy naphtha side stripper part, the aviation kerosene side stripper part, the diesel side stripper part and the debutanizer part), the public engineering part and the like, and the hydrogenated wax oil is fractionated into heavy naphtha, aviation kerosene and diesel schemes. Wherein the heavy naphtha accounts for 37 percent and is used for producing an efficient product PX; the high-efficiency product aviation kerosene accounts for 27%; the total yield of liquefied gas, light naphtha, diesel oil and hydrogenated tail oil serving as ethylene cracking raw materials is 34%; the flow is adjusted and subtractedThe yield of gasoline is reduced, the yield of chemicals is increased, and the economic benefit of hydrogenated wax oil is greatly improved.
FIG. 2 shows a specific embodiment of an apparatus for reducing and increasing oil by changing the flow direction of a material, which includes a wax oil hydrotreating system (same as the prior art) and a wax oil hydrocracking system connected to the wax oil hydrotreating system, wherein the wax oil hydrotreating system converts straight-run heavy wax oil of an atmospheric and vacuum device into hydrogenated wax oil as a raw material of the wax oil hydrocracking system; the wax oil hydrocracking system comprises a raw material tank, wherein the raw material tank is connected with a reaction feed heating furnace through a pipeline, the reaction feed heating furnace is connected with the upper end of a refining reactor through a pipeline, the lower end of the refining reactor is connected with the upper end of a cracking reactor through a pipeline, the lower end of the cracking reactor is connected with a stripping tower through a pipeline, the lower end of the stripping tower is sequentially connected with a wax feed tank, a fractionating tower heating furnace and a fractionating tower through pipelines, the upper end of the stripping tower is connected with a stripping tower discharge pipeline, and a plurality of material discharge pipelines are respectively arranged on the fractionating tower; the device also comprises a new hydrogen machine, wherein three pipelines are respectively arranged at the outlet end of the new hydrogen machine and are respectively connected to the upper end part of the refining reactor, the upper end part of the cracking reactor and the pipeline between the reaction feeding heating furnace and the refining reactor.
In a preferred embodiment, the material discharge pipeline comprises a first discharge pipeline, a second discharge pipeline, a third discharge pipeline and a fourth discharge pipeline, the upper end and the lower end of the fractionating tower are respectively connected with the first discharge pipeline and the second discharge pipeline, and the middle part of the fractionating tower is independently connected with the third discharge pipeline for discharging aviation kerosene and the fourth discharge pipeline for discharging diesel oil.
In a preferred embodiment, the stripper discharge line is divided into a fifth discharge line for discharging acid gases and a sixth discharge line for discharging heavy stones, the first discharge line being connected to the sixth discharge line.
As shown in fig. 2, the method for changing the flow direction of the material to realize oil reduction and increase comprises the following steps:
1) The method comprises the steps of mixing and feeding hydrogenated wax oil produced by a wax oil hydrotreating system with straight-run light wax oil produced by an atmospheric and vacuum device, exchanging heat with diesel oil, then automatically backwashing a filter through the raw oil to remove solid particles larger than 25 mu m, and then entering a raw material tank (raw oil buffer tank);
2) The mixture in the raw material tank is boosted by a reaction feed pump and then enters a reaction feed heating furnace, the mixture is sequentially enters a refining reactor (a hydrogenation reactor) and a cracking reactor to carry out hydrofining and hydrocracking reactions respectively after being boosted to the reaction temperature, and the reaction effluent, raw material oil and circulating hydrogen exchange heat to a proper temperature and enter a thermal high-pressure separator;
3) The reaction effluent in the hot high-pressure separator is further sent to a stripping tower, the bottom of the stripping tower is filled with steam for stripping, and the upper end of the stripping tower is used for removing acid gas and oil phase, wherein the acid gas (H) 2 S) the light hydrocarbon removing and recycling device further recycles liquefied gas, the oil phase at the top of the tower is sent to a naphtha hydrofining device, the lower end of the stripping tower obtains stripping tower bottom oil, and the stripping tower bottom oil enters a wax feeding tank to be used as a fractionating tower for feeding; the gas phase at the top of the stripping tower is cooled by an air cooler and a aftercooler and then enters a reflux tank at the top of the stripping tower to carry out oil, gas and water three-phase separation;
4) The stripping tower bottom oil is subjected to heat exchange with a process material flow, is heated by a fractionating tower feeding heating furnace and then enters a fractionating tower;
5) The gas phase at the top of the fractionating tower enters a reflux tank after being condensed and cooled, the liquid phase of the fractionating tower is boosted by a reflux pump at the top of the fractionating tower and then goes to a light hydrocarbon recovery device, the fractionating tower is provided with independent side-stream extraction aviation kerosene and diesel oil which respectively enter a product tank, and the hydrogenated tail oil is discharged from the bottom of the fractionating tower and is sent to a cracking furnace as an ethylene raw material after heat exchange and cooling.
The wax oil hydrocracking device of the invention mixes the maximum proportion of the hydrogenated wax oil:
because the wax oil hydrogenation device (system) blends part of slurry state bed wax oil, the slurry state bed wax oil contains more polycyclic aromatic hydrocarbon, and the polycyclic aromatic hydrocarbon needs to undergo the process of ring-by-ring saturation-ring opening, and the conversion difficulty in the hydrocracking section is higher. Therefore, the blending proportion of the hydrogenated wax oil in the raw material of the wax oil hydrocracking device is not more than 10 percent, namely the processing amount of the hydrogenated wax oil is not more than 47.6t/h under the full load condition. The quantity and the quality of the product distribution of the wax oil hydrocracking device after blending in the invention are changed: after blending 10% refined wax oil, under the same heavy naphtha yield condition, the hydrogenated tail oil yield is expected to be slightly increased by 1-2 percent (the increase of aromatic hydrocarbon content in the tail oil fraction leads to the increase of BMCI value, but long-chain hydrocarbon has lower BMCI value), the aviation kerosene and diesel oil yield are correspondingly reduced (the fraction influence is smaller), the sulfur and nitrogen content of the heavy naphtha fraction still can meet the requirements of a reformer less than 0.5 mug/g, and the aromatic hydrocarbon potential content is slightly increased by the notice of improvement in the production operation of the invention: because refined wax oil is subjected to one-time hydrofining in a wax oil hydrogenation device, easily saturated hydrocarbons are reacted, and therefore, after entering a hydrocracking refining section, the difficult-to-react aromatic hydrocarbon and nitride in the refined wax oil need to be further saturated and deeply denitrified. After blending refined wax oil, hydrofining Duan Wensheng is reduced, but the reaction temperature needs to be further increased. As the molecular weight of refined wax oil becomes larger, polycyclic aromatic hydrocarbon increases, so that the diffusion rate of the hydrocracking section is reduced, the conversion difficulty is increased, and the hydrocracking section also needs higher reaction temperature under the condition of obtaining the same heavy naphtha yield. For wax oil hydrocracking units (systems), the average hydrofinishing and hydrocracking reactor temperatures are expected to increase by 3-5 ℃. In order to keep the device running stably and protect the hydrocracking catalyst, it is recommended to analyze the hydrogenated refined oil of the wax oil hydrocracking device in time when the blending proportion of the refined wax oil or the slurry bed wax oil proportion of the wax oil hydrocracking device is obviously changed, so as to ensure that the nitrogen mass fraction of the refined oil is not more than 10 mug/g. Data analysis of the specific implementation process of the invention: analysis of mixed raw materials
Carbon residue: the carbon residue value of the mixed raw material after the hydrogenated wax oil is blended is not greatly changed and is within the design range (< 0.2% mass fraction), and the hydrogenated wax oil is subjected to hydrogenation carbon residue removal treatment (see the carbon residue comparison in the materials shown in figure 3) mainly.
Sulfur content: the sulfur content of the mixed raw material after the hydrogenated wax oil is blended is reduced by 0.27 percent compared with that before the hydrogenated wax oil is blended, and the hydrogenated wax oil is subjected to hydrodesulfurization treatment (see the sulfur content in the raw material in the comparison of FIG. 4) for the main reasons that the sulfur content is reduced by less than 2.6 percent in the design range.
Initial point of distillation: the initial boiling point of the mixed raw material after blending the hydrogenated wax oil is basically stable compared with that before blending, and the control range is 160-168 ℃ (see the initial boiling point comparison of the raw material in figure 5).
98% fraction: the 98% point of the mixed raw material rises by 15 ℃ and 21 ℃ at most compared with the point before blending, the raw material becomes heavy, the hydrogenated wax oil is heavy in distillation range compared with light wax oil mainly due to the fact that the hydrogenated wax oil is heavy in distillation range, and the blending amount of the catalyst Jiao Chai is reduced while the hydrogenated wax oil is blended, so that the 98% of the mixed raw material rises (see 98% point comparison of the raw material in FIG. 6).
Density: the density of the mixed raw materials after blending the hydrogenated wax oil is basically stable and slightly reduced compared with that before blending, and is more than 910kg/m (see the raw material density vs g/cm in FIG. 7) 3 ）。
Nitrogen content: the average value 774mg/kg of the nitrogen content of the hydrogenated wax oil is within the designed raw material index, the control index is not more than 2000ppm, but the residual nitrogen is not easy to remove because the hydrogenated wax oil is subjected to hydrofining denitrification, and the refining temperature is required to be higher, so that the refining temperature is improved to be removed (see the raw material nitrogen content is compared with mg/kg in FIG. 8).
The structural analysis of the product of the invention:
the heavy naphtha oil yield is reduced by 2.3% compared with the heavy naphtha oil before blending, the aviation kerosene yield is basically stable, the change of the diesel oil and tail oil yield is relatively large after the blending amount reaches 110t/h compared with the heavy naphtha oil before blending, the diesel oil yield is limited by the final distillation point and is reduced by 5.8%, the tail oil yield is increased by 7.2% compared with the initial blending stage, the tail oil flow is obviously heavier, the BMCI value is increased by 50 ℃ at 98% compared with the initial blending stage, and the BMCI value is 10.5 at most mainly because the raw material quality is heavier, jiao Chai is stopped, the reaction depth is relatively low, the distillate oil at the upper part of a fractionating tower is reduced, and the tail oil component is increased. As shown in fig. 9, the yields of heavy naphtha and aviation kerosene before and after blending are compared, and the 98% fractionation point of tail oil before and after blending is compared with BMCI value in fig. 10.
As the blended hydrogenated wax oil passes through the hydrofining reactor, the device after blending has little heat release in the refining reaction, the reaction temperature slowly drops, the temperature of the refining bed layer drops more, and the total temperature drops 27-30 ℃. To ensure adequate conversion and product yield, the cracking reaction temperature was increased gradually by 7℃to 377.8 ℃as compared to before blending (FIG. 11 variation of reaction temperature before and after blending)
Summary of the specific embodiments of the invention:
after the device blends hydrogenated wax oil to 110t/h, the following problems occur:
the wax oil cracking operation is obviously changed after 8 months and 16 days (the date is shown by combining with the attached drawing 10), the total refining temperature rise is controlled to be more than 50 ℃, the refining reaction temperature is gradually increased by device technicians, the nitrogen content is controlled to be no more than 10ppm, the nitrogen content of refined oil is analyzed to reach 17ppm by assay, the refining reaction temperature of the device is increased by 11 ℃ to 374 ℃ before blending, the total temperature rise is 52 ℃, the cracking reaction temperature is increased by 7 ℃ to 377.8 ℃ before blending, the refined oil nitrogen content is further monitored by sample addition, and the reaction temperature is further adjusted according to the analysis result.
As the weight of the raw materials is increased, the distillation range of the product drawn from each side line becomes heavy, the diesel oil yield is reduced due to the limitation of the final distillation point index (not more than 365 ℃), and the phenomenon of exceeding the final distillation point of the diesel oil occurs in the period. The tail oil component is increased more, the reaction conversion rate is lower, the tail oil yield is increased more, and the device gradually improves the reaction conversion rate according to the raw material property and the product yield.
The wax oil treatment of the upstream device is recommended to improve the reaction temperature, further improve the denitrification efficiency and control the nitrogen content of the hydrogenated wax oil to be below 600ppm as much as possible.
The invention is particularly applied to influence evaluation:
the density and nitrogen content of the refined wax oil are equivalent to those of the mixed raw materials of the wax oil hydrocracking device, but the distillation range is obviously heavier, and the 90% point and the final distillation point are about 50 ℃. The refined wax oil with 1360-4500 mug/g sulfur and 710-920 mug/g nitrogen can be obtained from the wax oil raw material under different refining depths, the sulfur and nitrogen content of the wax oil raw material is greatly reduced after the wax oil raw material passes through a wax oil hydrogenation device, but the total aromatic hydrocarbon content is less changed, and simultaneously, the aromatic hydrocarbon with more than three rings still remains in a quite proportion. This indicates that the aromatic hydrocarbon saturation is lower and the polycyclic aromatic hydrocarbon remains largely unreacted under the wax oil hydrogenation operating conditions. Under the hydrocracking condition, the nitrogen content of the refined oil in the hydrofining section is generally less than 20 mug/g, the aromatic saturation rate can reach about 50%, and most of polycyclic aromatic hydrocarbon is removed, which is also a necessary condition that the refined oil can be fully converted in the hydrocracking section. Therefore, although the refined wax oil of the wax oil hydrogenation device has low sulfur and nitrogen content, the refined wax oil has the characteristics of high proportion of compounds difficult to denitrify, large molecular size, high aromatic hydrocarbon content and high polycyclic aromatic hydrocarbon content, and after entering the hydrocracking device, the reaction severity is required to be increased to maintain a comparable conversion rate, and meanwhile, the polycyclic aromatic hydrocarbon in the refined wax oil also has a certain influence on the product quality. Comparison of the prior art (original scheme) with the benefits of the present invention: aiming at a large-scale smelting integrated device with 4000 ten thousand tons/year, the invention has obvious effect and the monthly synergy is about 1.38 hundred million yuan.
The invention realizes the following steps: reduces the yield of the finished oil, smoothes the back way of wax oil components and creates conditions for the load of an upstream device. Increases the yield of aromatic hydrocarbon and ethylene raw materials and brings great benefit. The flow direction of wax oil components is optimized, and the wax oil components can be used for reference of similar enterprises.
Finally, it should be noted that the invention is not limited to the above embodiments, but that many variants are possible. All modifications directly derived or suggested to one skilled in the art from the present disclosure should be considered as being within the scope of the present invention.
Claims (2)
1. The method for realizing oil reduction and increase by changing the material flow direction is characterized by comprising the following steps:
1) The method comprises the steps of mixing and feeding hydrogenated wax oil produced by a wax oil hydrotreating system with straight-run light wax oil produced by an atmospheric and vacuum device, exchanging heat with diesel oil, removing solid particles larger than 25 mu m through a raw oil automatic backwashing filter, and entering a raw material tank;
2) The mixture in the raw material tank is boosted by a reaction feed pump and then enters a reaction feed heating furnace, the mixture is sequentially enters a refining reactor and a cracking reactor to carry out hydrofining and hydrocracking reactions after being boosted to the reaction temperature, and the reaction effluent, raw oil and recycle hydrogen exchange heat to a proper temperature and enter a thermal high-pressure separator;
3) The reaction effluent in the hot high-pressure separator is further sent to a stripping tower, the bottom of the stripping tower is fed with steam for stripping, the upper end of the stripping tower is stripped by acid gas and oil phase, wherein the acid gas and light hydrocarbon removing recovery device is used for further recovering liquefied gas, the oil phase at the top of the stripping tower is sent to a naphtha hydrofining device, the lower end of the stripping tower is used for obtaining stripping bottom oil, and the stripping bottom oil enters a wax feeding tank to be used as a fractionating tower for feeding;
4) The stripping tower bottom oil is subjected to heat exchange with a process material flow, is heated by a fractionating tower feeding heating furnace and then enters a fractionating tower;
5) Condensing and cooling the gas phase at the top of the fractionating tower, then entering a reflux tank, boosting the liquid phase of the fractionating tower by a tower top reflux pump, then removing the light hydrocarbon recovery device, arranging independent side-stream collected aviation kerosene and diesel oil in the fractionating tower, respectively entering a product tank, discharging hydrogenated tail oil at the bottom of the fractionating tower, exchanging heat, cooling and then sending the hydrogenated tail oil to a cracking furnace as an ethylene raw material;
the mixing proportion of hydrogenated wax oil in the raw materials of the oil hydrocracking device is not more than 10%, the processing amount of the hydrogenated wax oil is not more than 47.6t/h under the full load condition, and the mass fraction of refined oil nitrogen is not more than 10 mug/g;
the method is operated under a device which comprises a wax oil hydrotreating system and a wax oil hydrocracking system connected with the wax oil hydrotreating system, wherein the wax oil hydrotreating system converts straight-run heavy wax oil of an atmospheric and vacuum device into hydrogenated wax oil to be used as a raw material of the wax oil hydrocracking system;
the wax oil hydrocracking system comprises a raw material tank, wherein the raw material tank is connected with a reaction feed heating furnace through a pipeline, the reaction feed heating furnace is connected with the upper end of a refining reactor through a pipeline, the lower end of the refining reactor is connected with the upper end of a cracking reactor through a pipeline, the lower end of the cracking reactor is connected with a stripping tower through a pipeline, the lower end of the stripping tower is sequentially connected with a wax feed tank, a fractionating tower heating furnace and a fractionating tower through pipelines, the upper end of the stripping tower is connected with a stripping tower discharge pipeline, and a plurality of material discharge pipelines are respectively arranged on the fractionating tower; the device also comprises a new hydrogen machine, wherein the outlet end of the new hydrogen machine is provided with three pipelines which are respectively connected with the upper end part of the refining reactor, the upper end part of the cracking reactor and the pipeline between the reaction feeding heating furnace and the refining reactor;
the material discharge pipeline comprises a first discharge pipeline, a second discharge pipeline, a third discharge pipeline and a fourth discharge pipeline, the upper end and the lower end of the fractionating tower are respectively connected with the first discharge pipeline and the second discharge pipeline, and the middle part of the fractionating tower is independently connected with the third discharge pipeline for discharging aviation kerosene and the fourth discharge pipeline for discharging diesel oil;
the stripper discharge line is divided into a fifth discharge line for discharging acid gas and a sixth discharge line for discharging heavy naphtha, and the first discharge line is connected with the sixth discharge line.
2. A method for reducing oil and increasing oil by changing material flow direction according to claim 1, wherein: the gas phase at the top of the stripping tower is cooled by an air cooler and a aftercooler and then enters a reflux tank at the top of the stripping tower to carry out oil, gas and water three-phase separation.
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| CN101684417A (en) * | 2008-09-27 | 2010-03-31 | 中国石油化工股份有限公司 | Optimized hydrogenation-catalytic cracking combination process |
| CN102453535A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrocracking method for reforming material yield increase |
| CN103059985A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Middle-pressure hydrocracking method for producing aviation kerosene and low-freezing point diesel |
| CN109988635A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of hydrotreating and hydrocracking combined process |
| CN112410068A (en) * | 2020-11-27 | 2021-02-26 | 浙江石油化工有限公司 | Wax oil hydrocracking device and method for producing 5# industrial white oil by using same |
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| US10041008B2 (en) * | 2014-02-26 | 2018-08-07 | Uop Llc | Process and apparatus for hydroprocessing with two product fractionators |
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| CN101684417A (en) * | 2008-09-27 | 2010-03-31 | 中国石油化工股份有限公司 | Optimized hydrogenation-catalytic cracking combination process |
| CN102453535A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Hydrocracking method for reforming material yield increase |
| CN103059985A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Middle-pressure hydrocracking method for producing aviation kerosene and low-freezing point diesel |
| CN109988635A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of hydrotreating and hydrocracking combined process |
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