CN103059918B - Vacuum distillation method for gradual gasification segmented feed - Google Patents
Vacuum distillation method for gradual gasification segmented feed Download PDFInfo
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Abstract
The invention discloses a vacuum distillation method for gradual gasification segmented feed. The method includes: making atmospheric tower bottom oil enter a first stage gasification furnace, conducting heating to make the tower bottom oil enter a first stage flash tank to perform separation, leaving a gas phase to enter an upper fractionation segment of a vacuum tower, and leaving a liquid phase to enter a second stage gasification furnace; heating the liquid phase and making it enter a second stage flash tank, letting the generated gas phase enter a middle fractionation segment of the vacuum tower, and letting the generated liquid phase enter a third stage gasification furnace; heating the liquid phase and making it enter a third stage flash tank, letting the generated gas phase enter a lower fractionation segment of the vacuum tower, and letting the generated liquid phase enter a flash segment of the vacuum tower; and subjecting the feed of each segment to vacuum distillation in the vacuum tower, extracting a lateral line product from a vacuum tower lateral line, and extracting vacuum residue from the tower bottom. The method provided in the invention can substantially enhance the distillate yield of a crude oil vacuum distillation process, reduce equipment energy consumption, increase equipment economic benefits, and save equipment investment.
Description
Technical field
The invention belongs to refining of petroleum field, relate in particular to the sectional feeding of the gasification gradually vacuum distillation method improving decompression extracting rate in a kind of crude oil underpressure distillation.
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.
Along with the continuous growth that scientific and technical develop rapidly and social life are consumed, world petroleum demand amount increases year by year along with expanding economy, in crude resources supply, heavy oil and overweight oil supplying ratio progressively increase, and lightweight oil, middle matter oil supplying constant decline.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 sectional feeding of gasification gradually vacuum distillation method improving decompression extracting rate, the extracting rate in crude oil vacuum distillation process can be significantly improved, reduce crude oil vacuum distillation apparatus energy consumption, increase device economic benefit, economy system is invested.
Gradually gasification sectional feeding vacuum distillation method and device provided by the invention comprise following content: oil at the bottom of the atmospheric tower of crude oil after air distillation (hereinafter referred to as oil of the normal end) enters vacuum distillation apparatus, in vacuum distillation process, adopt gasification gradually and the technique that gradually reduces pressure, underpressure distillation out with making the lighting end maximum in oil of the normal end.Gradually gasification refers to and gradually heats oil of the normal end, 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.
The one provided by the invention sectional feeding vacuum distillation method that gradually gasifies is achieved in that
(1) oil at the bottom of the atmospheric tower come by air distillation (being called for short oil of the normal end) first enters one-level vapourizing furnace, and enter primary flash tank after being heated to 370 ~ 380 DEG C, primary flash gas phase enters vacuum still top distillation stage;
(2) the primary flash liquid phase come from (1) enters secondary vapourizing furnace, and enter two-stage flash tank after being heated to 390 ~ 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.
The present invention is gasified in sectional feeding vacuum distillation method gradually, and described primary flash tank is vertical structure, can be provided with the equipment being beneficial to gas-liquid separation and gasification in tank, and can be also slack tank, tank deck working pressure be controlled by gaseous phase outlet.Primary flash tank 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.
The present invention is gasified in sectional feeding vacuum distillation method gradually, described two-stage flash tank 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, and 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.
The present invention is gasified in sectional feeding vacuum distillation method gradually, three grades of described flash tanks 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, and 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.
The present invention is gasified sectional feeding vacuum distillation method gradually, eliminate the setting of conventional vacuum transfer line, gradually vapourizing furnace and gradually separating device are set between atmospheric tower and vacuum distillation tower, connect with pipeline between vapourizing furnace at different levels and separating device, can compactly arrange, without the need to considering that conventional vacuum transfer line is not less than the transfer line setting of 15 meters.
The present invention is gasified in sectional feeding vacuum distillation method gradually, and described vacuum still can be fuel type vacuum still, also can be Lube Type vacuum still.Vacuum still 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.
The present invention is gasified in sectional feeding vacuum distillation method gradually, and described vacuum still comprises the parts such as condensation segment, distillation stage, washing section, 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 the number of distillation stage 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 still most end lateral line discharging; Flash zone installs the less feed distributor of pressure drop.
The present invention gradually gasify sectional feeding vacuum distillation method and in, described underpressure distillation column overhead carries out vacuum pumping, and controlling vacuum distillation tower tower top pressure is 1 kPa ~ 10 kPa, is preferably 1kPa ~ 5 kPa.Vacuum pumping can adopt method and apparatus conventional in this area.
The present invention is gasified in sectional feeding vacuum distillation method gradually, 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.
The present invention is gasified in sectional feeding vacuum distillation method gradually, and described primary flash tank, two-stage flash tank, three grades of flash tanks can independently be arranged, also can arranged superposed, to reduce plant area.
The present invention is gasified in sectional feeding vacuum distillation method gradually, and 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.
The present invention is gasified in sectional feeding vacuum distillation method gradually, by the gasification gradually to decompression charging, gasifies, significantly reduce the non-reversibility of heating and cooling under charging being heated to the temperature close to condensation; By gradually reducing pressure, in time the lighting end of gasification being separated, reducing 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, make vapourizing furnace internal pressure at different levels lower, oil of the normal end and the gasification point of flash tank liquid phase at different levels in vapourizing furnace are in advance, outlet of still vaporization rate is high, ensure that higher total vaporization rate, thus be conducive to improving decompression extracting rate.
2, the 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, the 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, gradually vapourizing furnace and gradually separating device can adopt compact Layout.Eliminate 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, the present invention just utilizes simple heating and separating device, and device structure is simple, be convenient to design, and turndown ratio is good.
8, present invention process advanced technology is reasonable, and energy consumption level is low, and vacuum residuum yield is low, for the transformation of old device, has 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 the schematic diagram of gradually gasify sectional feeding vacuum distillation method and device of the present invention.
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 vacuum distillate discharging; 11 is stripped vapor; 12 is vacuum residuum.
Embodiment
The technique that the inventive method is taked the heavy oil after to air distillation gradually to gasify and gradually reduced pressure, gasification, vacuum flashing gas phase out enter the different distillation stages 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 eliminates 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.
Composition graphs 1 couple of the present invention sectional feeding vacuum distillation method that gradually gasifies is described:
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, tank deck connects the top distillation stage of vacuum still 8, vacuum flashing separation is carried out under making that there is in tank certain vacuum degree condition, gas phase is sent to the distillation stage on vacuum still top by tank deck, and liquid phase at the bottom of tank enters secondary vapourizing furnace 4.The mixture be heated to 390 DEG C ~ 400 DEG C in secondary vapourizing furnace 4 after with certain vaporization rate enters two-stage flash tank 5, and 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.In three grades of vapourizing furnaces 6, material enters three grades of flash tanks 7 after being again heated to 410 DEG C ~ 420 DEG C, and tank deck gas phase enters the distillation stage of vacuum still 8 bottom, and liquid phase at the bottom of tank enters vacuum still 8 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, from each condensation segment oil header of vacuum still, extract vacuum distillate discharging 10 carrying device out successively, vacuum residuum 12 is extracted out and is sent outside at the bottom of vacuum still 8 tower.
The present invention is gasified sectional feeding vacuum distillation method gradually, 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; In addition, in time the gas phase separation of gasification out, take the flash distillation gas phase of different fractions scope 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.Confirm through the analog calculation of Aspen process simulation software, process the few 2% ~ 5%(weight 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%.
Below by specific embodiment, the inventive method is described in detail.
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 same as shown in Figure 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, enters primary flash tank 3 after one-level vapourizing furnace 2 is heated to 370 DEG C, and 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 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, and enter three grades of flash tanks, 7, three grades of flash distillation gas phases after heating to 410 DEG C and enter vacuum still 8 bottom distillation stage, 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.
comparative example 1
Relate to the design of newly-built 1,000 ten thousand tons/year of crude oil atmospheric vacuum distillation devices in embodiment 1 equally.The treatment capacity of reliever is 5,000,000 tons/year.Adopt 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 | 410(disregards 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) | 37.50 | 40.85 |
| Decompressed wax oil cut point/DEG C | 605 | 565 |
| Dodge top gas amount/% | — | 1.45 |
| Primary flash tolerance/% | 16.2 | — |
| Two-stage flash tolerance/% | 28.85 | — |
| Three grades of flash distillation tolerance/% | 11.22 | — |
| Energy consumption | ||
| Vacuum furnace load/MW | — | 39.27 |
| One-level vapourizing furnace load/MW | 14.25 | — |
| Secondary vapourizing furnace load/MW | 14.19 | — |
| Three grades of vapourizing furnace load/MW | 9.305 | — |
| Total heating load/MW | 37.745 | 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/37.745 MW | 1/39.27 MW |
| Flash tank | 3 | 1 |
As seen from Table 1, 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 vacuum distillation tower tower diameter is less in embodiment 1, 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 scheme of embodiment 1 is obviously better than comparative example 1; In decompression extracting rate, the result of embodiment 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.
In embodiment 1, the yield of vacuum residuum to decompression charging is 37.50%(quality), the cut point of decompressed wax oil reaches 605 DEG C.Calculate by the method described in comparative example 1, 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 the underpressure distillation flow process of the embodiment of the present invention 1, 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 the flow process of embodiment 1, total heating load is 37.745 MW.As adopted the flow process of embodiment 1, vacuum furnace load is 39.27 MW, adopts the energy consumption of apparatus of the present invention to occur declining to a great extent.
Calculate by 1,000 ten thousand tons/year of atmospheric and vacuum distillation unit, relief portion divides charging to be about 550 tons/hour, embodiment 1 comparatively comparative example 1 reduces yield of residual oil 3.35%, and come in residual oil and mixed gatch price difference 250 yuan/ton, year amounts to Renminbi: 550 × 3.35% × 250 × 8400=3869.25 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, enters primary flash tank 3 after one-level vapourizing furnace 2 is heated to 370 DEG C, and 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 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, and enter three grades of flash tanks, 7, three grades of flash distillation gas phases after heating to 410 DEG C and enter vacuum still 8 bottom distillation stage, 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.
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 | 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/% (m) | 42.18 | 37.50 | 40.85 |
| Decompressed wax oil cut point/DEG C | 540 | 605 | 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 37.50%(quality), the cut point of decompressed wax oil reaches 605 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, embodiment 2 comparatively comparative example 2 reduces yield of residual oil 3.35%, and come in residual oil and mixed gatch price difference 250 yuan/ton, year amounts to Renminbi: 550 × 3.35% × 250 × 8400=3869.25 ten thousand yuan.Add the part that device reduces energy consumption, the device economic benefit highly significant obtained.
Claims (12)
1. gasify the vacuum distillation method of sectional feeding gradually, 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 ~ 380 DEG C, primary flash gas phase enters vacuum still top distillation stage;
(2) the primary flash liquid phase come from (1) enters secondary vapourizing furnace, and enter two-stage flash tank after being heated to 390 ~ 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.
2. in accordance with the method for claim 1, it is characterized in that, described primary flash tank 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.
3. in accordance with the method for claim 1, it is characterized in that, described primary flash tank is vertical structure, and primary 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 two-stage flash tank 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.
5. in accordance with the method for claim 1, it is characterized in that, described two-stage flash tank is vertical structure, the equipment that flash tank is slack tank or arranges in tank due to gas-liquid separation and the words said in a fit of rage.
6. in accordance with the method for claim 1, it is characterized in that, 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.
7. in accordance with the method for claim 1, it is characterized in that, 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.
8. in accordance with the method for claim 1, it is characterized in that, described vacuum still is fuel type vacuum still or Lube Type vacuum still, and vacuum still adopts wet type operation, micro-wet type or dry operational; Sideline product number is 3 ~ 4.
9. in accordance with the method for claim 1, it is characterized in that: described underpressure distillation column overhead carries out vacuum pumping, control tower pressure on top surface is 1 kPa ~ 10 kPa.
10. in accordance with the method for claim 1, it is characterized in that, described one-level vapourizing furnace, secondary vapourizing furnace and three grades of vapourizing furnaces are independently arranged 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. in accordance with the method for claim 1, it is characterized in that, described primary flash tank, two-stage flash tank and three grades of flash tanks are independently arranged, or arranged superposed.
12. in accordance with the method for claim 1, it is characterized in that, vapourizing furnace at different levels and flash tank at different levels inner and/or between pipeline take expanding process.
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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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| 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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