CN103059920B - Method and device for crude oil deep vacuum distillation - Google Patents
Method and device for crude oil deep vacuum distillation Download PDFInfo
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Abstract
The invention discloses a method and a device for crude oil deep vacuum distillation. The method disclosed in the invention includes: introducing atmospheric tower bottom oil into a primary gasification furnace, conducting heating and leaving the oil to enter a primary flash tank to undergo separation, making the obtained gas phase enter a vacuum tower upper fractionation section, and letting the liquid phase enter a second stage gasification furnace; heating the liquid phase and making it enter a second-stage flash tank, leaving the obtained gas phase to enter a vacuum tower middle fractionation section, and making the obtained liquid phase enter a third-stage gasification furnace; heating the liquid phase and making it enter a third-stage flash tank, letting the obtained gas phase enter a vacuum tower lower fractionation section, and leaving the obtained liquid phase to enter a vacuum tower flash section; subjecting the feed of each section to vacuum distillation is the vacuum, extracting a lateral line product from a vacuum tower lateral line, and extracting vacuum residual oil from the tower bottom; and introducing part of the vacuum residual oil into the flash tanks of different stages respectively. The method provided in the invention can significantly improve the distillate yield of the crude oil in the distillation process, reduce device energy consumption, increase device economic benefits, and save device investment.
Description
Technical field
The invention belongs to refining of petroleum field, relate in particular to a kind of crude oil deep vacuum distillation method and device.
Technical background
Refinery crude oil atmospheric vacuum distillation technique is the first operation of refining of petroleum, is the component by the method for distillation crude oil being divided into different boiling range scope, to adapt to product and downstream unit to the processing requirement of raw material.The height of its light oil yield and the size of energy consumption directly affect the economic benefit of refining of petroleum.Reduced pressure distillation process utilizes underpressure distillation principle exactly, reduces by vacuumizing the pressure making fluid surface, thus the boiling point reducing liquid makes component vaporization relatively light in liquid mixture, reaches the object of fractionation.Reduced pressure distillation process requires to extract vacuum distillate as much as possible under the condition as far as possible avoiding oil plant generation cracking, makes the cut point of vacuum distillate reach 560 DEG C even higher.
Along with the fast development of global economy and the continuous growth of social life consumption, world petroleum demand amount increases year by year along with the development of world economy, in crude resources supply, heavy oil and overweight oil supplying ratio progressively increase, lightweight oil, middle matter oil supplying constant decline, and crude oil cost accounts for more than 80% of petroleum refining industry's total cost.Therefore, improve the extracting rate in crude oil atmospheric vacuum distillation, obtain more light oil distillate oil, reduce atmospheric and vacuum distillation unit energy consumption, raising device economic benefit becomes the problem that global Refining Chemical Industry is paid close attention to jointly.And along with the fast development of Chinese national economy, China's oil total quantity consumed is estimated breakthrough 6.5 hundred million tons at the year two thousand twenty, and the external dependence degree of crude oil will reach 50% ~ 60%.Appropriate application crude resources, optimization processing technology has been the imperative act of China's oil chemical industry.In larger-scale unit and Integrated Refinery And Petrochemical novel refinery design, as " tap " crude oil atmospheric vacuum distillation device maximum resource utilization, energy utilization economized, running cost rationalize, size investment optimizing, realize, in the Sustainable development of China's oil chemical industry, there is very important status.Therefore, newly-built crude unit requires higher depth of cut, and in vacuum residuum, less than 500 DEG C ends content are less than 5%(quality), even lower; Many old atmospheric and vacuum distillation unit, while requiring higher cut point, face process scale and can not meet the situation that treatment capacity requires and oil variety constantly changes, need to carry out capacity expansion revamping to device, eliminate " bottleneck ", improve crude distillation ability.
For this reason, Chinese scholars compares deep research to reduced pressure distillation technique, for improving the extracting rate of vacuum fractionation tower, having drawn a series of experience, can be summed up as: (1) adopts advanced vacuum system, improved the vacuum tightness of vacuum fractionation tower top; (2) adopt novel, high efficiency packing, reduce tower internal drop, make flash zone at the bottom of tower keep higher vacuum; (3) improve transfer line design, reduction transfer line Pressure Drop and temperature are fallen; (4) washing section design and operation is optimized, the fractionation concept of strengthening washing section; (5) new and effective gas and liquid distributor etc. are adopted.
Patent CN2242892Y discloses a kind of composite crude oil distillation vacuum distillation tower, is provided with a liquid seal device and top separates, and has a vacuum system interface to be connected with top vacuum system at the bottom of tower.This utility model is separated by the deep drawing section of liquid seal device by the rectifying section of vacuum distillation tower and bottom, oil quality and extracting rate can be paid attention to respectively, can relatively improve decompression extracting rate, but the oil quality of deep drawing is difficult to meet the processing requirement of downstream unit to raw material, the tower structure of this utility model is complicated simultaneously, top vacuum system loading is high, and plant energy consumption relatively can be high.
Patent CN1287872A has delivered a kind of crude oil atmospheric vacuum distillation method with degree of depth stripping process, it is a washing tank in parallel in vacuum distillation tower side, the feed zone of vacuum distillation tower and stripping stage are isolated sparger by fluid-tight and are separated, the oil gas of stripping stage is by entering the bottom of washing tank communicating pipe, take from the absorption oil that vacuum distillation tower subtracts three line dischargings and enter downwards spray and the reverse mass-and heat-transfer of oil gas upwards by washing tank top after cooling, the tank deck oil gas discharging of washing tank returns to the top of vacuum distillation tower, and discharging at the bottom of tank returns vacuum distillation tower as washing oil.This technique makes vacuum distillation tower stripping stage experienced by a steam stripped process of the degree of depth by setting up washing tank, is conducive to improving decompression extracting rate.But the method is just optimized improvement to vacuum distillation tower stripping stage, subtracts third fractional oil preferably as washing oil by quality, economic benefit waits research.
Patent CN1884441A discloses the method improving light oil yield of atmospheric and vacuum distillation of petroleum oil, is added in the crude oil of atmospheric and vacuum distillation of petroleum tower by the additive containing rosin, improves the light oil yield of atmospheric and vacuum distillation by changing the intermolecular reactive force of crude oil.But the method fundamentally changes distillation technique in Technology, and will consume a large amount of additives, add the operation easier of plant running cost and interpolation chemical reagent.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method with vacuum flasher and equipment, is before long residuum enters vacuum furnace, arrange a vacuum flasher.Oil at the bottom of flashing tower enters heating under reduced pressure stove, and flashing tower top gas enters above or below certain sideline product outlet port close with flashing tower top gas cut.The method improves the flow process of atmospheric and vacuum distillation unit by increasing vacuum flasher, reach raising treatment capacity, improves extracting rate, reduces the object of energy consumption.But oil enters flashing tower at the bottom of atmospheric tower, because at the bottom of atmospheric tower, the temperature of oil is relatively low, the vacuum tightness of adding stokehold flashing tower is relatively not high, the limited use that flashing tower is flash vaporized, and flash distillation top gaseous phase enters vacuum distillation tower, be equivalent to vacuum distillation tower sectional feeding after flash distillation, not in the fractionation fundamentally changing vacuum distillation tower.
Pressure-reducing line for oil-transferring is the connection line between vacuum furnace and vacuum distillation tower, and tube fluid belongs to alternating temperature Gas-liquid two-phase flow process.Under high temperature, high vacuum operational condition, the temperature of pressure-reducing line for oil-transferring inner fluid, pressure and flow velocity have important impact along the equilibrium evaporation rate of change on transfer line inner fluid in transfer line cross section, and then directly affect the vaporescence of vacuum distillation tower flash zone, vital effect is played to decompression extracting rate.In the last few years, high speed transfer line is in the past instead of gradually with major diameter (general diameter can reach more than 2m) low speed pressure-reducing line for oil-transferring technology in vacuum distillation apparatus, its objective is under the condition ensureing vacuum distillation tower feed zone vaporization ratio, reduce vacuum furnace temperature out as far as possible, to prevent tube coking.In other words, be under the heater outlet temperature of regulation, improve tower feed zone vaporization rate as far as possible, to improve product point rate.For reaching this purpose, only having and reducing boiler tube and transfer line pressure drop as far as possible, make oil product evaporating point in advance.Because transfer line must adopt more than 15m (to ensure that liquid phase has certain separation time, be conducive to improving the quality of products and vacuum distillation tower extracting rate), therefore the transfer line of the long distance of major diameter accounts for the larger proportion of vacuum distillation apparatus investment, simultaneously the factor such as calorific loss and pressure drop increase is all unfavorable for the operation of vacuum still, and the thermal stresses formed, thermal walking cause certain difficulty to design and installation in security.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of crude oil deep vacuum distillation method and device, the extracting rate in crude oil vacuum distillation process can be significantly improved, improve the cut point of vacuum distillate, realize the deep drawing operation of crude oil, and reduce plant energy consumption.
A kind of crude oil deep vacuum distillation of the present invention method comprises following content: cancel conventional pressure-reducing line for oil-transferring; Arrange gradually vapourizing furnace and gradually decompression separation tank oil at the bottom of atmospheric tower tower (hereinafter referred to as normal end oil) is gasified and the technique that gradually reduces pressure gradually; Extract vacuum residuum component loops at the bottom of vacuum still tower out and turn back to decompression separation tank at different levels.
A kind of crude oil of the present invention deep vacuum distillation method is by following process implementation:
(1) at the bottom of the atmospheric tower come by air distillation, first oil enter one-level vapourizing furnace, and enter primary flash tank after being heated to 370 DEG C ~ 380 DEG C, primary flash gas phase enters vacuum still top distillation stage;
(2) the primary flash liquid phase come from step (1) enters secondary vapourizing furnace, and DEG C enter two-stage flash tank after being heated to 390 DEG C ~ 400 DEG C, two-stage flash gas phase enters distillation stage in the middle part of vacuum still;
(3) the two-stage flash liquid phase come from step (2) enters three grades of vapourizing furnaces, and enter three grades of flash tanks after being heated to 410 ~ 420 DEG C, three grades of flash distillation gas phases enter vacuum still bottom distillation stage;
(4) the three grades of flash distillation liquid phases come from step (3) enter vacuum still flash zone;
(5) each section feeding carries out underpressure distillation in vacuum still, and underpressure distillation column overhead connects pumped vacuum systems, from each lateral line withdrawal function product of tower, extracts vacuum residuum out at the bottom of tower;
(6) the part reduced pressure residual oil come from step (5) divides three tunnels to introduce primary flash tank, two-stage flash tank and three grades of flash tanks said process respectively.
In a kind of crude oil deep vacuum distillation of the present invention method, primary flash tank described in step (1) is vertical structure, the equipment being beneficial to gas-liquid separation and gasification can be provided with in tank, also can be slack tank, tank deck working pressure is controlled by gaseous phase outlet, gaseous phase outlet connects vacuum still top distillation stage, and controlling primary flash pressure tank by the control valve on gaseous phase outlet is 8 kPa ~ 40 kPa, is preferably 10 kPa ~ 20 kPa.
Two-stage flash tank described in step (2) is vertical structure, the equipment being beneficial to gas-liquid separation and gasification can be provided with in tank, also can be slack tank, tank deck working pressure is controlled by gaseous phase outlet, gaseous phase outlet connects distillation stage in the middle part of vacuum still, controlling two-stage flash pressure tank by the control valve on gaseous phase outlet is 5 kPa ~ 30 kPa, is preferably 6 kPa ~ 15 kPa.
Three grades of flash tanks described in step (3) are vertical structure, the equipment being beneficial to gas-liquid separation and gasification can be provided with in tank, also can be slack tank, tank deck working pressure is controlled by gaseous phase outlet, gaseous phase outlet connects vacuum still bottom distillation stage, controlling three grades of flash tank pressure by the control valve on gaseous phase outlet is 2 kPa ~ 20 kPa, is preferably 3 kPa ~ 10 kPa.
In step (6), the part reduced pressure residual oil circulation of step (5) gained returns reduced-pressure flash tank at different levels, and vacuum residuum enters from the top of flash tank at different levels, and vapourizing furnace outlet streams at different levels enters in the middle part of separating tank.The ratio that the described quantity looping back the vacuum residuum of reduced-pressure flash tank at different levels accounts for whole vacuum residuum is the 5 heavy % in heavy % ~ 50, and the ratio wherein entering the vacuum residuum of one-level, secondary and three grades of flash tanks is generally 1.5 ~ 3:1 ~ 1.5:1.
In crude oil deep vacuum distillation method of the present invention, described underpressure distillation column overhead carries out vacuum pumping, and control tower pressure on top surface is 1 kPa ~ 10kPa, is preferably 1kPa ~ 5 kPa.Vacuum pumping can adopt the method and apparatus of this area routine.
Another technical problem that the present invention will solve is to provide a kind of crude oil deep vacuum distillation device improving extracting rate, described device comprises vacuum still (hereinafter referred to as vacuum distillation tower), tower top pumped vacuum systems, it is characterized in that, some vapourizing furnaces and some flash tanks are set between atmospheric tower and vacuum distillation tower, wherein oil pipeline at the bottom of atmospheric tower tower is connected with one-level vapourizing furnace entrance, the outlet of one-level vapourizing furnace is connected with one-level flash tank entrance, the liquid-phase outlet of primary flash tank is connected with secondary vapourizing furnace entrance, the outlet of secondary vapourizing furnace is connected with two-stage flash tank entrance, the liquid-phase outlet of two-stage flash tank is connected with the entrance of three grades of vapourizing furnaces, the outlet of three grades of vapourizing furnaces is connected with the entrance of three grades of flash tanks, the liquid-phase outlet of three grades of flash tanks is connected with vacuum distillation tower flash zone, wherein primary flash tank, the gaseous phase outlet of two-stage flash tank and three grades of flash tanks is respectively with the top distillation stage of vacuum distillation tower, middle part distillation stage is connected with bottom distillation stage, VACUUM TOWER BOTTOM oil outlet respectively by pipeline with one-level flash tank, two-stage flash tank is connected with three grades of flash tanks.
In crude oil deep vacuum distillation device of the present invention, eliminate the setting of conventional vacuum transfer line, gradually vapourizing furnace and gradually separating tank are set between atmospheric tower and vacuum distillation tower, connect with pipeline between vapourizing furnace at different levels and separating tank, can compactly arrange, without the need to considering that conventional vacuum transfer line is not less than the transfer line setting of 15 meters.
In crude oil deep vacuum distillation device of the present invention, described vacuum distillation tower can be fuel type vacuum still, also can be Lube Type vacuum still; Vacuum distillation tower can adopt wet type to operate, and also can adopt micro-wet type or dry operational; Sideline product number is generally 3 ~ 5, determines according to product needed and oil variety.
In crude oil deep vacuum distillation device of the present invention, described vacuum distillation tower generally includes the parts such as condensation segment, distillation stage, washing section and flash zone.Condensation segment can arrange column plate or filler, also can not establish column plate or filler, with void tower arranged in form; Distillation stage arranges high-throughput, the filler of low pressure drop or column plate, and number is generally 3 ~ 5, determines according to product needed and oil variety.Washing section arranges not susceptible to plugging filler or column plate, gets to above washing section filler or column plate carry out washing with vacuum distillation tower most end lateral line discharging; Flash zone installs the less feed distributor of pressure drop.
In crude oil deep vacuum distillation device of the present invention, described one-level vapourizing furnace, secondary vapourizing furnace, three grades of vapourizing furnaces can be can be independently, also three-in-one process furnace separately, and three grades of chargings are separately positioned on radiation sections different in three-in-one process furnace.
In a kind of crude oil deep vacuum distillation of the present invention device, described primary flash tank, two-stage flash tank, three grades of flash tanks can independently be arranged, also according to pressure height arranged superposed successively from top to bottom, can reduce plant area.
In a kind of crude oil deep vacuum distillation of the present invention device, in order to avoid pressure drop is excessive, gasification and the pipeline gradually between pressure regulating equipment or in equipment can take expanding process gradually.
A kind of crude oil deep vacuum distillation of the present invention method, by adopting gasification gradually and the technique that gradually reduces pressure in vacuum distillation process, gasification refers to and gradually heats oil of the normal end gradually, and utilizes separating device the feed separation after gasification to be gone out in time; Gradually decompression refers to and enters material step-down gradually in separating device of separating device to after gasification gradually, realizes gasification at much lower pressure.Thus significantly reducing the non-reversibility of heating and cooling, underpressure distillation is out with making the lighting end maximum in oil of the normal end, contributes to the extracting rate improving underpressure distillation; And in time the lighting end of gasification is separated, reduce the load of vapourizing furnace at different levels, thus reduce the energy consumption of device.
Compared with prior art, the present invention has the following advantages:
1) vapourizing furnace outlet at different levels is directly communicated with reduced-pressure flash tank, flash drum overhead gas phase introduces vacuum still, makes vapourizing furnace internal pressure at different levels lower, and oil of the normal end and flash tank liquid phase at different levels gasification point in vapourizing furnace shift to an earlier date, outlet of still vaporization rate is high, ensures higher total vaporization rate.Thus be conducive to improving decompression extracting rate.
2) lighting end of gradually gasifying separated in time by separation at different levels, vapourizing furnace only heats the liquid fraction of phase counterweight, and comparatively in conventional vacuum distil process, full cut is all heated to underpressure distillation critical temperature, significantly reduces plant energy consumption.
3) after flash distillation, liquid phase enters vacuum still separately, avoids the Vapor Entrainment that gas-liquid mixed charging causes, and ensure that decompression side line quality product.
4) gas phase after separation at different levels enters vacuum still middle and upper part, reduces the full tower pressure drop of vacuum still, reduces and vacuumize load, thus reduces plant energy consumption.
5) the gas phase segmentation after separation at different levels enters the different positions of vacuum still, avoid gas phase power load distributing in vacuum still uneven, relatively light cut enters vacuum still middle and upper part simultaneously, in time from each lateral line withdrawal function after vacuum fractionation condensation, reduce the load of vacuum still, the expansion being conducive to vacuum distillation apparatus can be upgraded.
6) vapourizing furnace and gradually separating device compact Layout gradually.Cancel pressure-reducing line for oil-transferring, avoid the transfer line thermal walking that extra heavy pipe footpath, greatly pipe range transfer line low speed segment cause, optimize reduced pressure distillation process design.
7) vacuum residuum component loops freshening, entered by the top of reduced-pressure flash tank at different levels, utilize the high temperature logistics of the certain vaporization rate of vapourizing furnace discharging to carry out steam stripping at reduced pressure to vacuum residuum, make < 500 DEG C of cuts in vacuum residuum carry out with ascending vapor as far as possible on the one hand; Reduce the entrainment of gas phase in the logistics of vapourizing furnace gas-liquid mixed on the other hand, thus significantly reduce vacuum residuum yield, improve the yield of distillate, ensure the quality of vacuum distillate.
8) present invention process advanced technology is reasonable, and energy consumption level is low, and vacuum residuum yield is low, and device composition is simple, be convenient to design, and turndown ratio is good.For the transformation of old device, have that scrap build amount is few, original equipment utilization rate is high, it is low to invest, short construction period, a device income obviously advantage such as quick; For the design and construction of new device, there is rational technology advanced person, energy consumption level is low, vacuum distillate yield is high, and under the prerequisite of same size, main equipment scale can be reduced, the features such as economy system investment.
Accompanying drawing explanation
Fig. 1 is a kind of crude oil deep vacuum distillation method and device technique schematic flow sheet.
Wherein 1 is oil of the normal end; 2 is one-level vapourizing furnace; 3 is primary flash tank; 4 is secondary vapourizing furnace; 5 is two-stage flash tank; 6 is three grades of vapourizing furnaces; 7 is three grades of flash tanks; 8 is vacuum still; 9 is pumped vacuum systems; 10 is the discharging of vacuum distillation tower sideline product vacuum distillate; 11 is stripped vapor; 12 go out device for vacuum residuum; 13 for returning primary flash tank vacuum residuum; 14 for returning two-stage flash tank vacuum residuum; 15 for returning three grades of flash tank vacuum residuum.
Embodiment
The inventive method is taked the heavy oil after to air distillation gradually to gasify and is gradually reduced pressure, the technique that vacuum residuum component loops returns, gasification, vacuum flashing gas phase is out made to enter the different distillation stage of vacuum still respectively, the flash zone that remaining liquid phase enters vacuum still carries out underpressure distillation, from the sideline product of vacuum still lateral line withdrawal function different fractions, vacuum residuum is extracted out at the bottom of tower.The method cancels the pressure-reducing line for oil-transferring in conventional vacuum distil process, adopts the method gasification normal end oil gradually heating and increase separating device, and the feed separation after gasification is gone out in time, reduce lighting end and cross thermo-cracking, reduce the non-reversibility of heating; Adopt decompression technology gradually simultaneously, progressively lighting end is separated, to a certain degree reduce the oil gas dividing potential drop of material, make remaining material can realize gasification at much lower pressure, thus gradually reduced the heating load of material, more component can be made to gasify out under the critical Heating temperature of oil product, thus greatly improve decompression extracting rate.Present method, to the capacity expansion revamping of old device, when main equipment reuses, can improve the utilization ratio of equipment greatly, reduces plant energy consumption, improves unit capacity; To new device, optimize reduced pressure distillation process design, economy system is invested, and increases the ton oil profit of device.
1 pair of a kind of crude oil deep vacuum distillation method of the present invention and device are described by reference to the accompanying drawings:
Oil of the normal end 1 enters one-level vapourizing furnace 2, the mixture being heated to the certain vaporization rate after 370 DEG C ~ 380 DEG C enters primary flash tank 3 together with the vacuum residuum 13 returned at the bottom of by vacuum still 8 tower, vacuum flashing separation is carried out under tank deck connection vacuum still 8 top distillation stage makes to have certain vacuum degree condition in tank, gas phase is sent to vacuum still top distillation stage by tank deck, and liquid phase at the bottom of tank enters secondary vapourizing furnace 4.In secondary vapourizing furnace 4, material has the mixture of certain vaporization rate and enters two-stage flash tank 5 by the vacuum residuum 14 returned at the bottom of vacuum still 8 tower after being heated to 390 DEG C ~ 400 DEG C, two-stage flash gas phase is sent to distillation stage in the middle part of vacuum still 8 by tank deck, and liquid phase enters three grades of vapourizing furnaces 6 at the bottom of tank.Three grades of flash tanks 7 are entered together with the vacuum residuum 15 returned at the bottom of by vacuum still 8 tower after material in three grades of vapourizing furnaces 6 is heated to 410 DEG C ~ 420 DEG C again, tank deck gas phase enters the distillation stage of vacuum still 8 bottom, and liquid phase at the bottom of tank enters vacuum still flash zone.Each section feeding is in vacuum still 8, at the bottom of tower top pumped vacuum systems 9 and tower stripped vapor 11 effect under carry out underpressure distillation, vacuum distillate 10 carrying device is extracted out successively from each condensation segment oil header of tower, vacuum residuum is extracted out at the bottom of vacuum still 8 tower, the outer carrying device 12 of part vacuum residuum, another part divides three tunnel circulations to return reduced-pressure flash tank gradually at different levels.
A kind of crude oil deep vacuum distillation method of the present invention and device, improve crude oil reduced pressure distillation process, the processing method taked gradually to heat and gradually reduce pressure, make decompression charging in the Heating temperature gasified of lower pressure and Geng Gao, flash distillation, ensure that the vaporization rate that decompression charging is higher, thus improve the extracting rate of underpressure distillation, increase the economic benefit of device, and in time the gas phase separation of gasification out, the flash distillation gas phase of different fractions scope is taked to carry out the different position of vacuum still, not only reduce the heating load of decompression charging, and reduce vacuum still and vacuumize load, significantly reduce vacuum distillation apparatus energy consumption, in addition, vacuum residuum circulation is adopted to return reduced-pressure flash tank gradually, utilize the high temperature logistics of the certain vaporization rate of vapourizing furnace discharging to carry out steam stripping at reduced pressure to vacuum residuum, significantly reduce < 500 DEG C of ends content in vacuum residuum, improve vacuum distillate yield to a certain extent.Confirm through the analog calculation of Aspen process simulation software, process the few 2% ~ 5%(weight percent of vacuum residuum yield of the identical more existing operational path of raw material present invention process method), plant energy consumption reduces by 10% ~ 30%.
embodiment 1:
Method of the present invention is used for the design of certain newly-built 1,000 ten thousand tons/year of crude oil atmospheric vacuum distillation device, and relief portion division technique flow process is identical with shown in accompanying drawing 1.
The treatment capacity of reliever is 5,000,000 tons/year, and decompression flow process comprises one-level vapourizing furnace, primary flash tank, secondary vapourizing furnace, two-stage flash tank, three grades of vapourizing furnaces, three grades of flash tanks, vacuum stills.Vacuum still is regular packed tower, and adopt wet process operation, tower bottom blowing vapour amount is 1% of tower charging, and tower top working pressure is 1.315 kPa, and full tower pressure drop is 685Pa.
Oil of the normal end 1 is fed into vacuum distillation apparatus with 550 tons/hour, primary flash tank 3 is entered after one-level vapourizing furnace 2 is heated to 370 DEG C, the vacuum residuum 13 returned at the bottom of vacuum still 8 tower enters primary flash tank top, and two bursts of chargings carry out vacuum flashing and gas-liquid separation in reduced-pressure flash tank.Tank deck gas phase enters vacuum still 8 top distillation stage, controls tank deck gas phase and ensures that primary flash pressure tank is 10 kPa; Liquid phase at the bottom of tank enters secondary vapourizing furnace 4, enters two-stage flash tank 5 after heating to 390 DEG C, and the vacuum residuum 14 returned at the bottom of vacuum still 8 tower enters two-stage flash tank top, and two bursts of chargings carry out vacuum flashing and gas-liquid separation in reduced-pressure flash tank.Two-stage flash gas phase enters distillation stage in the middle part of vacuum still 8, and controlling tank deck pressure is 6 kPa; Two-stage flash liquid phase enters three grades of vapourizing furnaces 6, enters three grades of flash tanks 7 after heating to 410 DEG C, and the vacuum residuum 15 returned at the bottom of vacuum still 8 tower enters three grades of flash tank tops, and two bursts of chargings carry out vacuum flashing and gas-liquid separation in reduced-pressure flash tank.Three grades of flash distillation gas phases enter vacuum still 8 bottom distillation stage, and controlling three grades of flashing pressures is 3 kPa, and three grades of flash distillation liquid phases enter vacuum still 8 flash zone.Each section feeding carries out underpressure distillation in vacuum still 8, and from lateral line withdrawal function decompression product 10, vacuum residuum 12 is extracted out at the bottom of tower.
It is 15% that the vacuum residuum that circulation returns flash tank at different levels accounts for the ratio that VACUUM TOWER BOTTOM all subtracts slag, return one-level, secondary, three grades of flash tanks the ratio of vacuum residuum be 5: 3: 2.
Comparative example 1:
Relate to the design of a set of newly-built 1,000 ten thousand tons/year of crude oil atmospheric vacuum distillation devices in embodiment 1.The treatment capacity of reliever is 5,000,000 tons/year, adopts the atmospheric vacuum distillation method with vacuum flasher disclosed in CN101376068A.
Under same feedstock, processing condition, list and adopt the embodiment of the present invention 1 and comparative example 1 in reduce pressure extracting rate, plant energy consumption, investment etc. in table 1, application Aspen process simulation software carries out the Data Comparison of modeling effort.
Table 1
| Project | Embodiment 1 | Comparative example 1 |
| Operational condition | ||
| Nominal treatment capacity/(ton/hour) | 550 | 550 |
| Charging kind | Kuwait Crude Oil > 350 DEG C of parts | Kuwait Crude Oil > 350 DEG C of parts |
| Vacuum distillation tower tower top pressure/kPa | 1.315 | 1.315 |
| Tower pressure drop/kPa | 0.685 | 0.685 |
| Vacuum furnace temperature out/DEG C | — | 410 |
| One-level vapourizing furnace temperature out/DEG C | 370 | — |
| Secondary vapourizing furnace temperature out/DEG C | 390 | — |
| Three grades of vapourizing furnace temperature outs/DEG C | 410 | — |
| Tower flash zone feeding temperature/DEG C | 409.4(disregard heat radiation) | 394(disregards heat radiation) |
| Total vaporization rate % (m) | 48.93 | 41.89 |
| Flash tank pressure/kPa | — | 20 |
| Primary flash pressure tank/kPa | 10 | — |
| Two-stage flash pressure tank/kPa | 6 | — |
| Three grades of flash tank pressure/kPa | 3 | — |
| Yield(to decompression charging) | ||
| Vacuum residuum yield/% (m) | 37.30 | 40.85 |
| Decompressed wax oil cut point/DEG C | 609 | 565 |
| Dodge top gas amount/% | — | 1.45 |
| Primary flash tolerance/% | 16.8 | — |
| Two-stage flash tolerance/% | 29.74 | — |
| Three grades of flash distillation tolerance/% | 13.96 | — |
| Energy consumption | ||
| Vacuum furnace load/MW | — | 39.27 |
| One-level vapourizing furnace load/MW | 14.96 | — |
| Secondary vapourizing furnace load/MW | 15.87 | — |
| Three grades of vapourizing furnace load/MW | 10.05 | — |
| Total heating load/MW | 40.88 | 39.27 |
| Consume steam/(kg/h) | 5500 | 5500 |
| Overhead condensation load/MW | 55.99 | 66.21 |
| Top vacuum pump load/MW | 1.08 | 1.27 |
| Facility investment | ||
| Vacuum distillation tower | 1/φ 4800 | 1/φ 7916 |
| Vacuum pump | 1 | 1 |
| Process furnace | Three-in-one furnace/40.88 MW | 1/39.27 MW |
| Flash tank | 3 | 1 |
As seen from the table, in facility investment, although utilize multiplex two flash tanks of the embodiment of the present invention 1, because tank charging reduces gradually, the tank diameter of two-stage flash and three grades of flash tanks all can significantly reduce, and can't increase plant investment; And the embodiment of the present invention 1 vacuum distillation tower tower diameter is less, investment reduces, and corresponding column internals and filler investment also will reduce; And vacuum pump power is well below comparative example 1; In plant energy consumption, the embodiment of the present invention 1 is obviously better than comparative example 1; In decompression extracting rate, the result of the embodiment of the present invention 1 is better than comparative example 1 far away, and the degree of deep drawing is also relatively high, and declining to a great extent appears in vacuum residuum yield.
The yield of vacuum residuum to decompression charging is 37.30%(quality), the cut point of decompressed wax oil reaches 609 DEG C.Same feedstock, processing condition calculate with the method described in comparative example 1, and vacuum residuum is 40.85% to the yield of combined feed total feed, and decompressed wax oil cut point is 565 DEG C, and deep drawing degree is not as good as the present invention.
Adopt flow process of the present invention, the maximum tower diameter of vacuum distillation tower is φ 4800mm, and as adopted the flow process of comparative example 1, then the maximum tower diameter of vacuum distillation tower is φ 7916mm, and the facility investment of device can significantly reduce.
Adopt flow process of the present invention, total heating load is 40.88 MW.As adopted the flow process of comparative example 1, vacuum furnace load is 39.27 MW, and furnace energy consumption is about the same.
Calculate by 1,000 ten thousand tons/year of atmospheric and vacuum distillation unit, relief portion divides charging to be about 550 tons/hour, and reduce yield of residual oil 3.55%, come in residual oil and mixed gatch price difference 250 yuan/ton, year amounts to Renminbi: 550 × 3.55% × 250 × 8400=4100.25 ten thousand yuan.Add the part that device reduces energy consumption, the device economic benefit highly significant obtained.
embodiment 2:
Method of the present invention is used for the capacity expansion revamping of certain Atmospheric Vacuum Unit, normal pressure part is identical with conventional atmospheric and vacuum distillation unit, and decompression part mainly comprises a grade vapourizing furnace, primary flash tank, secondary vapourizing furnace, two-stage flash tank, three grades of vapourizing furnaces, three grades of flash tanks, vacuum stills.
Vacuum distillation tower is regular packed tower, and tower top working pressure is 1.315 kPa, and full tower pressure drop is 685 Pa.
Oil of the normal end 1 is fed into vacuum distillation apparatus with 550 tons/hour, primary flash tank 3 is entered after one-level vapourizing furnace 2 is heated to 370 DEG C, the vacuum residuum 13 returned at the bottom of vacuum still 8 tower enters primary flash tank top, and two bursts of chargings carry out vacuum flashing and gas-liquid separation in reduced-pressure flash tank.Tank deck gas phase enters vacuum still 8 top distillation stage, controls tank deck gas phase and ensures that primary flash pressure tank is 10 kPa; Liquid phase at the bottom of tank enters secondary vapourizing furnace 4, enters two-stage flash tank 5 after heating to 390 DEG C, and the vacuum residuum 14 returned at the bottom of vacuum still 8 tower enters two-stage flash tank top, and two bursts of chargings carry out vacuum flashing and gas-liquid separation in reduced-pressure flash tank.Two-stage flash gas phase enters distillation stage in the middle part of vacuum still 8, and controlling tank deck pressure is 6 kPa; Two-stage flash liquid phase enters three grades of vapourizing furnaces 6, enters three grades of flash tanks 7 after heating to 410 DEG C, and the vacuum residuum 15 returned at the bottom of vacuum still 8 tower enters three grades of flash tank tops, and two bursts of chargings carry out vacuum flashing and gas-liquid separation in reduced-pressure flash tank.Three grades of flash distillation gas phases enter vacuum still 8 bottom distillation stage, and controlling three grades of flashing pressures is 3 kPa, and three grades of flash distillation liquid phases enter vacuum still 8 flash zone.Each section feeding carries out underpressure distillation in vacuum still 8, and from lateral line withdrawal function decompression product 10, vacuum residuum 12 is extracted out at the bottom of tower.
This device capacity expansion revamping relief portion is divided and is retained original vacuum furnace and vacuum distillation tower, transforms vacuum distillation tower internals and filler.Carry out capacity expansion revamping to vacuum furnace, boiler tube and radiation chamber are transformed, and are transformed into three-in-one process furnace.Remove transfer line low speed segment, newly-increased main equipment is primary flash tank, two-stage flash tank, three grades of flash tanks.It is 15% that the vacuum residuum that circulation returns flash tank at different levels accounts for the ratio that VACUUM TOWER BOTTOM all subtracts slag, return one-level, secondary, three grades of flash tanks the ratio of vacuum residuum be 5: 3: 2.
After transformation, device decompression part working ability can improve 20% ~ 50%, and plant energy consumption reduces by 10% ~ 15%, and vacuum residuum yield reduces by 2% ~ 5%.
Comparative example 2
For the same set of crude oil atmospheric vacuum distillation device related in embodiment 2, the atmospheric vacuum distillation method with vacuum flasher disclosed in CN101376068A is adopted to carry out capacity expansion revamping.
Under same feedstock, processing condition, list in table 2 and adopt the embodiment of the present invention 2 and comparative example 2 reduce pressure part transformation situation for same set of atmospheric and vacuum distillation unit, apply the Data Comparison that Aspen process simulation software carries out modeling effort.
Table 2
| Project | Situation before transformation | Embodiment 2 | Comparative example 2 |
| Nominal treatment capacity/(t/h) | 450 | 550 | 550 |
| Charging kind | Kuwait Crude Oil > 350 DEG C of parts | Kuwait Crude Oil > 350 DEG C of parts | Kuwait Crude Oil > 350 DEG C of parts |
| Vacuum residuum yield/% | 42.18 | 37.30 | 40.85 |
| Decompressed wax oil cut point/DEG C | 540 | 609 | 565 |
| Main equipment transformation situation | |||
| Vacuum distillation tower | φ4600 | Reuse, change internals and filler | Newly-built |
| Vacuum pump/kW | 195 | Reuse | Newly-built |
| Overhead condenser/MW | 58 | Reuse | Newly-built |
| Vacuum furnace/MW | 34.89 | Transformation, expands load | Transformation, expands load |
| Flash tank | Nothing | Newly-built 2 φ 2200 of newly-built 1 φ 4800/ | Newly-built 1 φ 4800 |
| Investment and benefit | |||
| Construction investment | — | Moderate | Bigger |
| Annual increase income/ten thousand yuan | — | 2310 | 1800 |
After carrying out capacity expansion revamping according to embodiment 2, the yield of vacuum residuum to decompression charging is 37.30%(quality), the cut point of decompressed wax oil reaches 609 DEG C.And the method for pressing described in comparative example 2, vacuum residuum is 40.85% to the yield of combined feed total feed, decompressed wax oil cut point is 565 DEG C, can upgrade although comparative example 2 pairs of original devices carry out certain expansion, decompressed wax oil cut point has the raising of certain amplitude, but the investment of transformation is slightly larger than embodiment 2, and vacuum residuum yield is higher than embodiment 2, and deep drawing degree is also not as good as the embodiment of the present invention 2.
Calculate by 1000 tons/year of atmospheric and vacuum distillation unit, relief portion divides charging to be about 550 tons/hour, reduce yield of residual oil compared with comparative example 2 many 3.55%, come in residual oil and mixed gatch price difference 250 yuan/ton, year amounts to Renminbi: 550 × 3.55% × 250 × 8400=4100.25 ten thousand yuan.Add the part that device reduces energy consumption, the device economic benefit highly significant obtained.
Claims (12)
1. a crude oil deep vacuum distillation method, comprises following content:
(1) at the bottom of the atmospheric tower come by air distillation, first oil enter one-level vapourizing furnace, and enter primary flash tank after being heated to 370 DEG C ~ 380 DEG C, primary flash gas phase enters vacuum still top distillation stage;
(2) the primary flash liquid phase come from step (1) enters secondary vapourizing furnace, and DEG C enter two-stage flash tank after being heated to 390 DEG C ~ 400 DEG C, two-stage flash gas phase enters distillation stage in the middle part of vacuum still;
(3) the two-stage flash liquid phase come from step (2) enters three grades of vapourizing furnaces, and enter three grades of flash tanks after being heated to 410 ~ 420 DEG C, three grades of flash distillation gas phases enter vacuum still bottom distillation stage;
(4) the three grades of flash distillation liquid phases come from step (3) enter vacuum still flash zone;
(5) each section feeding carries out underpressure distillation in vacuum still, and underpressure distillation column overhead connects pumped vacuum systems, from each lateral line withdrawal function product of tower, extracts vacuum residuum out at the bottom of tower;
(6) the part reduced pressure residual oil come from step (5) divides three tunnels to introduce primary flash tank, two-stage flash tank and three grades of flash tanks said process respectively.
2. in accordance with the method for claim 1, it is characterized in that: the ratio accounting for whole vacuum residuum looping back the vacuum residuum of reduced-pressure flash tank at different levels described in step (6) is the 5 heavy % in heavy % ~ 50, and the ratio wherein entering the vacuum residuum of one-level, secondary and three grades of flash tanks is generally 1.5 ~ 3:1 ~ 1.5:1.
3. in accordance with the method for claim 1, it is characterized in that: described primary flash tank is vertical structure, flash tank is slack tank or in tank, is provided with the equipment being beneficial to gas-liquid separation and gasification; Described two-stage flash tank is vertical structure, and flash tank is slack tank or in tank, is provided with the equipment being beneficial to gas-liquid separation and gasification; Three grades of described flash tanks are vertical structure, and flash tank is slack tank or in tank, is provided with the equipment being beneficial to gas-liquid separation and gasification.
4. in accordance with the method for claim 1, it is characterized in that, the gaseous phase outlet of described primary flash tank connects vacuum still top distillation stage, and controlling primary flash pressure tank by the control valve on gaseous phase outlet is 8 kPa ~ 40 kPa; The gaseous phase outlet that described two-stage flash tank is connects distillation stage in the middle part of vacuum still, and controlling two-stage flash pressure tank by the control valve on gaseous phase outlet is 5 kPa ~ 30 kPa; The gaseous phase outlet of described three grades of flash tanks connects vacuum still bottom distillation stage, and controlling three grades of flash tank pressure by the control valve on gaseous phase outlet is 2 kPa ~ 20 kPa.
5. in accordance with the method for claim 1, it is characterized in that, in step (6), the part reduced pressure residual oil circulation of step (5) gained returns reduced-pressure flash tank at different levels, vacuum residuum enters from the top of flash tank at different levels, and vapourizing furnace outlet streams at different levels enters in the middle part of separating tank.
6. in accordance with the method for claim 1, it is characterized in that, described underpressure distillation column overhead carries out vacuum pumping, and control tower pressure on top surface is 1 kPa ~ 10kPa.
7. one kind is improved the crude oil deep vacuum distillation device of extracting rate, described device comprises vacuum still, tower top pumped vacuum systems, it is characterized in that, some vapourizing furnaces and some flash tanks are set between atmospheric tower and vacuum distillation tower, wherein oil pipeline at the bottom of atmospheric tower tower is connected with one-level vapourizing furnace entrance, the outlet of one-level vapourizing furnace is connected with one-level flash tank entrance, the liquid-phase outlet of primary flash tank is connected with secondary vapourizing furnace entrance, the outlet of secondary vapourizing furnace is connected with two-stage flash tank entrance, the liquid-phase outlet of two-stage flash tank is connected with the entrance of three grades of vapourizing furnaces, the outlet of three grades of vapourizing furnaces is connected with the entrance of three grades of flash tanks, the liquid-phase outlet of three grades of flash tanks is connected with vacuum distillation tower flash zone, wherein primary flash tank, the gaseous phase outlet of two-stage flash tank and three grades of flash tanks is respectively with the top distillation stage of vacuum distillation tower, middle part distillation stage is connected with bottom distillation stage, VACUUM TOWER BOTTOM oil outlet respectively by pipeline with one-level flash tank, two-stage flash tank is connected with three grades of flash tanks.
8. according to device according to claim 7, it is characterized in that, described device eliminates the setting of conventional vacuum transfer line.
9. according to device according to claim 7, it is characterized in that, described vacuum distillation tower comprises condensation segment, distillation stage, washing section and flash zone, and the number of distillation stage is 3 ~ 5.
10. according to device according to claim 7, it is characterized in that, described one-level vapourizing furnace, secondary vapourizing furnace, three grades of vapourizing furnaces independently arrange separately, or arrange three-in-one process furnace, and three grades of chargings are separately positioned on radiation sections different in three-in-one process furnace.
11., according to device according to claim 7, is characterized in that, described primary flash tank, two-stage flash tank and three grades of flash tanks are independently arranged, or according to pressure height arranged superposed successively from top to bottom.
12., according to device according to claim 7, is characterized in that, expanding process taked by the pipeline between described vapourizing furnace and described flash tank or in equipment.
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| CN1454965A (en) * | 2003-05-08 | 2003-11-12 | 中国石化集团洛阳石油化工工程公司 | Petroleum atmospheric vacuum distillation process and unit |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
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