CN103242896B - Reduced pressure distillation method with low energy consumption and deep total distillation rate - Google Patents
Reduced pressure distillation method with low energy consumption and deep total distillation rate Download PDFInfo
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Abstract
The invention discloses a reduced pressure distillation method with low energy consumption and deep total distillation rate. By arranging a reduced pressure flashing tower behind a reduced pressure heating furnace, light fractions vaporized by heat are separated out, load of a reduced pressure distillation tower is reduced and energy consumption of an apparatus is reduced; by arranging a reduced pressure flashing tank behind the reduced pressure distillation tower, relatively light fractions in reduced pressure residues can be further flashed under a vacuum degree higher than that of the bottom of a reduced pressure distillation tower, yield of reduced pressure distillate oil is increased, and thus a reduced pressure distillation operation with low energy consumption and deep total drawing rate can be realized. With the reduced pressure distillation method, the content of fractions with a temperature lower than 500 DEG C in the reduced pressure residues can be reduced to the minimum, so that the distillation rate of the reduced pressure distillation is increased and economic benefits of the apparatus can be increased.
Description
Technical field
The invention belongs to refining of petroleum field, relate to the vacuum distillation method that a kind of less energy-consumption is deeply always pulled out.Relate in particular in a kind of crude oil vacuum distillation process the vacuum distillation method improving extracting rate, reduce energy consumption.
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.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.Usually using < 500 DEG C of ends content in the energy consumption of total extracting rate of device benzoline, device and vacuum residuum as the index weighing plant running.The height of its benzoline yield and the size of energy consumption directly affect the economic benefit of refining of petroleum.The flow process of the conventional many employings of crude oil reduced pressure distillation process " stove one tower ": crude oil completes after air distillation through atmospheric tower, oil at the bottom of atmospheric tower delivers to vacuum distillation tower through vacuum furnace heating by pressure-reducing line for oil-transferring, obtains meet the product of specification of quality and the vacuum distillate of downstream unit from vacuum distillation tower side line.
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 deep vacuum distillation technology, 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 US7172686 has delivered a kind of method improving crude distillation distillate yield, and method one extracts gaseous stream out from tower inside cord, and carry out separation and obtain product, a part of gas phase returns in tower; Method two is incoming mixture by boiling point height heating and separating is lighting end, middle runnings, last running, then enters in tower at different feed entrance points respectively and carries out fractionation, extract out successively gently from side line, last running.Method one is equivalent to side line and has added a stripping tower, improves distillate quality.But to a certain degree add plant investment and energy consumption; Method two achieves gently, last running sectional feeding, improve the operation of crude distillation separation column, be conducive to improving distillate yield, but the lighting end of having separated from parallel feeding is sent in tower again carry out fractionation, repetitive operation increases plant energy consumption and does not reduce the load of tower.
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 discloses 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 the vacuum distillation method that a kind of less energy-consumption is deeply always pulled out, the extracting rate in vacuum distillation process can be significantly improved, reduce plant energy consumption, increase the economic benefit of crude oil reduced pressure distillation process.
The vacuum distillation method that a kind of less energy-consumption of the present invention is deeply always pulled out comprises following content: cancel pressure-reducing line for oil-transferring, between vacuum furnace and vacuum still, arrange vacuum flasher; After vacuum still, reduced-pressure flash tank is set.
The vacuum distillation method that a kind of less energy-consumption provided by the invention is deeply always pulled out 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 heating under reduced pressure stove after heat exchange heats up, and is heated to 390 ~ 420 DEG C;
(2) the gas-liquid mixed vacuum furnace discharging come from step (1) enters vacuum flasher, flashing tower gas phase (dodging gas hereinafter referred to as one) enters knockout drum after tower after heat exchange, condensing cooling, separating tank top connects pumped vacuum systems, discharges vacuum distillate bottom separating tank;
(3) the flashing tower liquid phase come from step (2) enters vacuum still feed zone and carries out underpressure distillation, and underpressure distillation column overhead connects pumped vacuum systems, from vacuum still lateral line withdrawal function decompression benzoline, extracts depressed heavy oil out at the bottom of vacuum still tower;
(4) depressed heavy oil come from step (3) enters reduced-pressure flash tank, and flash tank gas phase (dodging gas hereinafter referred to as two) enters knockout drum after tank after heat exchange, condensing cooling, and separating tank top connects pumped vacuum systems, discharges vacuum distillate bottom separating tank;
(5) the flash tank liquid phase vacuum residuum come from step (4) is extracted out by pump.
In vacuum distillation method of the present invention, described vacuum flasher can arrange 2 ~ 10 blocks of column plates or filler, also can be void tower, tower top working pressure is controlled by knockout drum gaseous phase outlet after tower, controlling flashing tower pressure by the control valve on gaseous phase outlet is 10 kPa ~ 80 kPa, is preferably 20 kPa ~ 50 kPa.
In vacuum distillation method of the present invention, described one dodge gas and enter vacuum furnace before the heat exchange of underpressure distillation raw material after be condensed into liquid phase caterpillar, or with a certain of vacuum still or certain several fractions mixing caterpillar.Underpressure distillation raw material is generally oil at the bottom of atmospheric distillation tower tower (hereinafter referred to as oil of the normal end).
In vacuum distillation method of the present invention, eliminate the setting of pressure-reducing line for oil-transferring in conventional vacuum distillation, vertical flashing tower being set between vacuum furnace and vacuum distillation tower, can compactly arranging between flashing tower and vacuum furnace, vacuum still, arranging without the need to considering to arrange the transfer line being not less than 15 meters.
In vacuum distillation method of the present invention, the reduced-pressure flash tank described in step (4) is horizontal tank, to realize the larger flash distillation face of reduced-pressure flash tank.
In vacuum distillation method of the present invention, pressure comparatively low 2 kPa ~ 5 kPa of vacuum still tower bottom pressure of described reduced-pressure flash tank, the depressed heavy oil that vacuum distillation tower is discharged flows into reduced-pressure flash tank by self-pressure.Tank deck working pressure is controlled by knockout drum gaseous phase outlet after tank.
In vacuum distillation method of the present invention, the depressed heavy oil of discharging at the bottom of vacuum still tower introduces reduced-pressure flash tank by expanding pipeline step by step, makes the lighting end in vacuum residuum divide pressure to be evaporated at the oil gas reduced step by step, finally in the complete flash distillation of reduced-pressure flash tank.
In vacuum distillation method of the present invention, the position of reduced-pressure flash tank height is in vacuum still, and reduced-pressure flash tank opening for feed is positioned at 30% ~ 70% place of liquid level at the bottom of vacuum still tower, and preferably 45% ~ 55%.Ensure that vacuum still can not be evacuated, and prevents liquid phase residual overlong time at the bottom of vacuum still tower from causing coking on the other hand on the one hand.
In vacuum distillation method of the present invention, vacuum flashing head space gas phase and the normal end oil or device in need heat logistics heat exchange, reduce plant energy consumption.
In vacuum distillation method of the present invention, extracted out the vacuum residuum of degree of depth flash distillation at the bottom of reduced-pressure flash tank tank by pump, liquid automatic control pump discharge flow at the bottom of tank.
In vacuum distillation method of the present invention, a set of pumped vacuum systems can be set, vacuum still, vacuum flasher and reduced-pressure flash tank share a set of pumped vacuum systems vacuum pumping, can arrange control device, control the vacuum tightness of vacuum still, vacuum flasher and reduced-pressure flash tank respectively; Also can arrange two covers or three cover pumped vacuum systems, vacuum still, vacuum flasher and reduced-pressure flash tank are combined or vacuum pumping respectively between two.Vacuum pumping can adopt the method and apparatus of this area routine.
In vacuum distillation method of the present invention, other technology contents such as vacuum furnace, underpressure distillation Deethanizer design and operation are technology contents well known to those skilled in the art.
The vacuum distillation method that a kind of less energy-consumption of the present invention is deeply always pulled out, by arranging vacuum flasher after vacuum furnace, separates the lighting end of heating and gasifying in time, reduces vacuum still load, reduces the energy consumption of device; By arranging reduced-pressure flash tank after vacuum still, making cut relatively light in vacuum residuum obtain flash distillation further, improving vacuum distillate yield, thus realize the underpressure distillation operation that less energy-consumption deeply always pulls out.Compared with prior art, the present invention has the following advantages:
1) vacuum furnace outlet is directly communicated with vacuum flasher, and vacuum distillation tower is introduced in the discharging of flashing tower bottom liquid phases.Shorten reduced pressure distillation process flow process, greatly reduce process pressure drop and the calorific loss of pressure-reducing line for oil-transferring in prior art, make vacuum furnace internal pressure lower, outlet of still vaporization rate is higher.
2) 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.Through adjusting, the cost of flashing tower is starkly lower than the cost of extra heavy pipe footpath, large pipe range transfer line.
3) dodge end oil and enter vacuum still separately, significantly reduce the processing load of vacuum still, decrease the theoretical stage needed for vacuum distillation tower, can suitably reduce tower height and tower diameter, economy system is invested; Eliminate " bottleneck " of vacuum distillation tower treatment capacity, be conducive to the capacity expansion revamping of old device; Avoid the Vapor Entrainment that gas-liquid mixed charging causes, ensure that decompression side line quality product; Reduce full tower pressure drop, be conducive to improving decompression extracting rate, reduce Top of Vacuum Tower condensation and vacuumize load.Achieve underpressure distillation less energy-consumption, high vacuum, the operation of high extracting rate.
4) a sudden strain of a muscle gas and oil of the normal end carry out heat exchange, reduce vacuum furnace load, reduce plant energy consumption.
5) reduced-pressure flash tank degree of depth flash distillation, improves the vacuum distillate yield of this device on the one hand, and the cut of < 500 DEG C and < 538 DEG C in vacuum residuum is reduced greatly.; Reduce the load of the process such as downstream coking or visbreaking vacuum residuum device on the other hand, reduce the cracking loss of benzoline.
6) reduced-pressure flash tank can be used as the surge tank of discharging pump at the bottom of tower, prevents discharging pump at the bottom of tower from finding time.
7) heat exchange is carried out in two logistics of dodging gas and oil of the normal end or the heat supply of device domestic demand, reduces plant energy consumption.
8) present invention process advanced technology is reasonable, and energy consumption level is low, and vacuum residuum yield is low, and for the design and construction of new device, have rational technology advanced person, energy consumption level is low, the features such as vacuum distillate yield is high, less investment; For the transformation of old device, have scrap build amount few, invest low, the transformation duration is short, and device income is the advantage such as quick obviously.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the vacuum distillation method that a kind of less energy-consumption of the present invention is deeply always pulled out.
Wherein 1 is oil of the normal end (i.e. oil at the bottom of atmospheric tower); 2 is vacuum furnace; 3 is a sudden strain of a muscle gas; 4 is vacuum flasher; 5 is vacuum still; 6 is depressed heavy oil; 7 is stripped vapor; 8 for dodging end oil; 9 is pumped vacuum systems; 10 is vacuum distillate; 11 is vacuum residuum; 12 is reduced-pressure flash tank; 13 is knockout drum after tower; 14 is knockout drum after tank.
Embodiment
The inventive method is directly communicated with a flashing tower in vacuum furnace outlet, and vacuum distillation tower is introduced in the discharging of flashing tower bottom liquid phases.The gas-liquid mixed charging that vacuum furnace heat air rate is very high carries out gas-liquid flash separation under the condition of flashing tower condition of high vacuum degree.One dodge gas by tank deck through and vacuum furnace charging heat exchange, then enter knockout drum after tower after water cooler cooling, liquid phase vacuum distillate is as product discharge.Dodge end oil and directly enter vacuum still feed zone, at the bottom of with tower stripped vapor vacuum still in carry out fractionation further, from vacuum still lateral line withdrawal function vacuum distillate, depressed heavy oil directly enters reduced-pressure flash tank by extracting out at the bottom of tower, makes depressed heavy oil carry out vacuum flashing under the condition of reduced-pressure flash tank condition of high vacuum degree.Two dodge gas by tank deck through with heat exchange, cool after enter knockout drum after tank.Gas-liquid separation tank top connects pumped vacuum systems, maintains the vacuum tightness that reduced-pressure flash tank is relatively high; Bottom extracts vacuum distillate out as product.Vacuum residuum is extracted out at the bottom of reduced-pressure flash tank tank.
The vacuum distillation method that composition graphs 1 pair of less energy-consumption of the present invention is deeply always pulled out is described:
As shown in Figure 1: oil of the normal end 1 first enters vacuum furnace 2 after heat exchange raised temperature, and in vacuum furnace, heating temperatures directly enters vacuum flasher 4 after 400 DEG C ~ 420 DEG C.Gas-liquid separation and flash distillation is carried out in vacuum flasher, gas phase is discharged one through Froth demist net by tank deck and is dodged gas, cool through condenser again after lower the temperature with normal end oil and enter gas-liquid separator 13 after tower, connection pumped vacuum systems 9 in gas-liquid separator top after tower, the vacuum tightness that maintenance vacuum flasher is certain.Vacuum distillate 10 is discharged in bottom.Vacuum flasher liquid phase is dodged end oil and 8 is directly entered vacuum still 5 feed zone, carries out underpressure distillation, obtain sideline product vacuum distillate 10 in tower under the effect of stripped vapor 7 and underpressure distillation tower top pumped vacuum systems 9.Depressed heavy oil 6 is by VACUUM TOWER BOTTOM discharging.Introduce reduced-pressure flash tank 12 through expanding pipeline step by step, under the condition of reduced-pressure flash tank high vacuum, the depressed heavy oil of high temperature obtains further flash distillation.Two dodge gas enters knockout drum 14 after tank after heat exchange cooling, and separating tank top connects pumped vacuum systems 9, maintains the vacuum tightness that reduced-pressure flash tank 12 is higher, extracts vacuum distillate 10 out as product discharge bottom separating tank.Reduced-pressure flash tank liquid phase is extracted out by the bottom of tank, as vacuum residuum 6 discharging.
Vacuum flasher, vacuum still and reduced-pressure flash tank have Level Detection to show respectively.
Vacuum still described in the present invention can be fuel type vacuum still, also can be Lube Type vacuum still; Can be wet distiller, also can decline wet distiller; Sideline product discharging number is specifically arranged as required.
After vacuum furnace of the present invention with after flashing tower, vacuum distillation tower with the vacuum distillation method of flash tank and equipment, improve crude oil reduced pressure distillation process, parallel feeding lower pressure heat air rate in vacuum furnace being reached 50% ~ 60% carries out gas-liquid separation in vacuum flasher, long pressure-reducing line for oil-transferring low speed segment need not be set again to carry out gas-liquid separation (prior art requires that transfer line low speed segment length is as 15m), avoid the horizontal thermal walking of transfer line that extra heavy pipe footpath, greatly pipe range low speed segment cause.Flash distillation top gaseous phase and vacuum furnace charging are direct as product after carrying out heat exchange, condensation, and liquid phase enters vacuum still separately.Thus decrease the processing load of vacuum still, decrease the theoretical stage needed for vacuum still to a certain extent, can suitably reduce tower height and tower diameter, significantly reduce the condensation of underpressure distillation tower top simultaneously and vacuumize load; And the Vapor Entrainment that gas-liquid mixed charging can be avoided to cause, ensure that decompression side line quality product.The reduced-pressure flash tank that the depressed heavy oil of VACUUM TOWER BOTTOM enters condition of high vacuum degree again carries out further flash distillation, cut relatively light in depressed heavy oil is flashed off completely, ensure that in vacuum residuum, the cut of < 500 DEG C and the ends content of < 538 DEG C are reduced to minimum, thus improve the extracting rate of underpressure distillation, increase the economic benefit of device.Confirm through the analog calculation of Aspen Hysys process simulation software, process the yield of residual oil few 2% ~ 5% of the identical more existing operational path of raw material present invention process method, and the sensible heat that contains of the vacuum flashing tower top oil gas that accounts for charging 50% ~ 60% and latent heat to be enough to the oil heat exchange of the normal end, to 390 DEG C ~ 400 DEG C, greatly reduce the load of vacuum furnace.
The present invention, when device goes into operation, can open large vacuum furnace load, and heating is fed to 390 DEG C ~ 400 DEG C, ensures underpressure distillation operation.Go into operation after stablizing, the sensible heat and the latent heat that make full use of high temperature sudden strain of a muscle top gas heat to oil of the normal end, and can reduce the load of vacuum furnace, implement device is energy-conservation.
Below by specific embodiment, method of the present invention is described in detail.In embodiment and comparative example, data are that the analog calculation of Aspen process simulation software obtains.
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 5,500,000 tons/year, and decompression flow process comprises vacuum furnace, vacuum flasher, vacuum still and reduced-pressure flash tank.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 650 tons/hour, enters vacuum flasher 4 after vacuum furnace 2 is heated to 400 DEG C, and controlling flashing tower pressure is 10 kPa.Sudden strain of a muscle end oil enters vacuum distillation tower and carries out underpressure distillation, and after distillation, depressed heavy oil enters reduced-pressure flash tank, and flash tank pressure is 1.2 kPa.At the bottom of reduced-pressure flash tank, oil is as vacuum residuum discharging.
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 5,500,000 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) | 650 | 650 |
| Charging kind | Iran crude > 350 DEG C of parts | Iran crude > 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 | 400 | 400 |
| Tower flash zone feeding temperature/DEG C | 400(disregards heat radiation) | 394(disregards heat radiation) |
| Flashing tower pressure/kPa | 10 | — |
| Flash tank pressure/kPa | 1.2 | 20 |
| Yield(to decompression charging) | ||
| Vacuum residuum yield/% (m) | 35.14 | 38.42 |
| Decompressed wax oil cut point/DEG C | 618 | 565 |
| Energy consumption | ||
| Vacuum furnace load/MW | 31.45 | 38.54 |
| 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 5200 | 1/φ 8400 |
| Vacuum pump | 1 | 1 |
| Process furnace | 1/31.45 MW | 1/38.54 MW |
| Flash tank | 1 | 1 |
| Flashing tower | 1/φ 4600 | — |
As seen from Table 1, in facility investment, although utilize the multiplex flashing tower of the embodiment of the present invention 1, vacuum distillation tower tower diameter is less, and investment reduces, and corresponding column internals and filler investment also will reduce, and total plant investment can't increase; 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 35.14%(quality), the cut point of decompressed wax oil reaches 618 DEG C.Calculate by the method described in comparative example 1, vacuum residuum is 38.42% 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 5200mm, and as adopted the flow process of comparative example 1, then the maximum tower diameter of vacuum distillation tower is φ 8400mm, and the facility investment of device can significantly reduce.
Adopt the flow process of embodiment 1, total heating load is 31.45MW.As adopted the flow process of embodiment 1, vacuum furnace load is 38.54MW, adopts the energy consumption of apparatus of the present invention to decline about 20%.
Calculate by 1,000 ten thousand tons/year of atmospheric and vacuum distillation unit, relief portion divides charging to be about 650 tons/hour, embodiment 1 comparatively comparative example 1 reduces yield of residual oil 3.28%, and come in residual oil and mixed gatch price difference 300 yuan/ton, year amounts to Renminbi: 650 × 3.28% × 300 × 8400=5372.64 ten thousand yuan.Add the part that device reduces energy consumption, the device economic benefit highly significant obtained.
embodiment 2
The expansion that method of the present invention is used for certain 8,000,000 tons/year of Atmospheric Vacuum Unit can be 1,000 ten thousand tons/year of transformations.The transformation of normal pressure part is identical with conventional atmospheric and vacuum distillation unit, and the treatment capacity of reliever can be 5,500,000 tons/year by original 4,500,000 tons/year of expansions.
Decompression flow process comprises vacuum furnace, vacuum flasher, vacuum still and reduced-pressure flash tank.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 650 tons/hour, enters vacuum flasher 4 after vacuum furnace 2 is heated to 400 DEG C, and controlling flashing tower pressure is 10 kPa.Sudden strain of a muscle end oil enters vacuum distillation tower and carries out underpressure distillation, and after distillation, depressed heavy oil enters reduced-pressure flash tank, and flash tank pressure is 1.2 kPa.At the bottom of reduced-pressure flash tank, oil is as vacuum residuum discharging.
This device capacity expansion revamping relief portion is divided and is retained original vacuum furnace and vacuum distillation tower, transforms, carry out capacity expansion revamping to vacuum furnace to vacuum distillation tower internals and filler.Newly-increased main equipment is vacuum flasher, reduced-pressure flash tank.
Vacuum flasher is regular packed tower, in-built single hop high-throughput, low pressure drop structured packing.
After transformation, device decompression part working ability can improve 30% ~ 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 | 650 | 650 |
| Charging kind | Iran crude > 350 DEG C of parts | Iran crude > 350 DEG C of parts | Iran crude > 350 DEG C of parts |
| Vacuum residuum yield/% (m) | 39.79 | 35.14 | 38.42 |
| Decompressed wax oil cut point/DEG C | 540 | 618 | 565 |
| Main equipment transformation situation | |||
| Vacuum distillation tower | φ6500 | 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, | Transformation, expands load |
| Flash tank | Nothing | Newly-built 1 φ 3000 | Newly-built 1 φ 4200 |
| Flashing tower | Nothing | Newly-built 1 φ 4600 | Nothing |
| Investment | |||
| Construction investment | — | Moderate | Bigger |
After carrying out capacity expansion revamping according to embodiment 2, the yield of vacuum residuum to decompression charging is 35.14%(quality), the cut point of decompressed wax oil reaches 618 DEG C.And the method for pressing described in comparative example 2, vacuum residuum is 38.42% 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.And transform rear plant energy consumption decline about 10% by embodiment 2.
Calculate by 1,000 ten thousand tons/year of atmospheric and vacuum distillation unit, relief portion divides charging to be about 650 tons/hour, embodiment 1 comparatively comparative example 1 reduces yield of residual oil 3.28%, and come in residual oil and mixed gatch price difference 300 yuan/ton, year amounts to Renminbi: 650 × 3.28% × 300 × 8400=5372.64 ten thousand yuan.Add the part that device reduces energy consumption, the device economic benefit highly significant obtained.
Claims (9)
1. the vacuum distillation method that deeply always pulls out of less energy-consumption, comprises following content:
(1) at the bottom of the atmospheric tower come by air distillation, first oil enter heating under reduced pressure stove after heat exchange heats up, and is heated to 390 ~ 420 DEG C;
(2) the gas-liquid mixed vacuum furnace discharging come from step (1) enters vacuum flasher, and flashing tower gas phase enters knockout drum after tower after heat exchange, condensing cooling, and separating tank top connects pumped vacuum systems, discharges vacuum distillate bottom separating tank;
(3) the flashing tower liquid phase come from step (2) enters vacuum still feed zone and carries out underpressure distillation, and underpressure distillation column overhead connects pumped vacuum systems, from vacuum still lateral line withdrawal function decompression benzoline, extracts depressed heavy oil out at the bottom of vacuum still tower;
(4) depressed heavy oil come from step (3) enters reduced-pressure flash tank, and flash tank gas phase enters knockout drum after tank after heat exchange, condensing cooling, and separating tank top connects pumped vacuum systems, discharges vacuum distillate bottom separating tank; Described reduced-pressure flash tank is horizontal tank;
(5) the flash tank liquid phase vacuum residuum come from step (4) is extracted out by pump.
2. in accordance with the method for claim 1, it is characterized in that, described vacuum flasher arranges 2 ~ 10 blocks of column plates or filler or is void tower.
3. in accordance with the method for claim 1, it is characterized in that, described vacuum flashing column overhead working pressure is controlled to be 10 kPa ~ 80 kPa by knockout drum gaseous phase outlet after tower.
4. in accordance with the method for claim 1, it is characterized in that, described flashing tower gas phase with enter vacuum furnace before the heat exchange of underpressure distillation raw material after be condensed into liquid phase caterpillar, or with the one of vacuum still or certain several fractions mixing caterpillar.
5. in accordance with the method for claim 1, it is characterized in that, pressure comparatively low 2 kPa ~ 5 kPa of vacuum still tower bottom pressure of described reduced-pressure flash tank.
6. in accordance with the method for claim 1, it is characterized in that, the depressed heavy oil of discharging at the bottom of described vacuum still tower introduces reduced-pressure flash tank by expanding pipeline step by step, makes the lighting end in vacuum residuum divide pressure to be evaporated at the oil gas reduced step by step, finally in the complete flash distillation of reduced-pressure flash tank.
7. in accordance with the method for claim 1, it is characterized in that, the position height of described reduced-pressure flash tank is in vacuum still, and the opening for feed of reduced-pressure flash tank is positioned at 30% ~ 70% place of liquid level at the bottom of vacuum still tower.
8. in accordance with the method for claim 1, it is characterized in that, a set of pumped vacuum systems is set, vacuum still, vacuum flasher and reduced-pressure flash tank share a set of pumped vacuum systems vacuum pumping, control device is set, controls the vacuum tightness of vacuum still, vacuum flasher and reduced-pressure flash tank respectively.
9. in accordance with the method for claim 1, it is characterized in that, arrange two covers or three cover pumped vacuum systems, vacuum still, vacuum flasher and reduced-pressure flash tank are combined or vacuum pumping respectively between two.
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| CN107057747B (en) * | 2016-11-07 | 2020-04-28 | 中国石油大学(华东) | Atmospheric-vacuum energy-saving deep drawing process based on clear cutting |
| CN107022375B (en) * | 2017-04-17 | 2018-12-14 | 山东京博石油化工有限公司 | A kind of Etherification of Light FCC Gasoline system and Etherification of Light FCC Gasoline technique |
| CN107699273B (en) * | 2017-11-15 | 2019-09-06 | 中国石油大学(北京) | A kind of anhydrous atmospheric and vacuum distillation technique and device |
| CN112717444A (en) * | 2020-12-23 | 2021-04-30 | 九三粮油工业集团有限公司 | Mixed oil negative pressure evaporation equipment |
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| Publication number | Priority date | Publication date | Assignee | Title |
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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 |
| CN102309863A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Reduced pressure distillation method and device |
| CN102311771A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Crude oil processing method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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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 |
| CN102309863A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Reduced pressure distillation method and device |
| CN102311771A (en) * | 2010-07-07 | 2012-01-11 | 中国石油化工股份有限公司 | Crude oil processing method |
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