CN103242896A - 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 the 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 to the vacuum distillation method that improves extracting rate, cuts down the consumption of energy in a kind of crude oil vacuum distillation process.
Technical background
Refinery crude oil atmospheric vacuum distillation technology is first procedure of refining of petroleum, is that the method by distillation is divided into the component of different boiling range scopes with crude oil, to adapt to product and downstream unit to the processing requirement of raw material.Reduced pressure distillation process utilizes the underpressure distillation principle exactly, reduce by vacuumizing the pressure that makes fluid surface, thereby the boiling point that reduces liquid makes component vaporization lighter relatively in the liquid mixture, reaches the purpose of fractionation.Reduced pressure distillation process requires to extract as much as possible vacuum distillate under the condition of as far as possible avoiding oil plant generation cracking.In the energy consumption and vacuum residuum of common total extracting rate with the device benzoline, device＜500 ℃ of indexs that the cut content move as the measurement device.The size of the height of its benzoline yield and energy consumption directly influences the economic benefit of refining of petroleum.Conventional crude oil reduced pressure distillation process adopts the flow process of " stove one tower " more: after crude oil is finished air distillation through atmospheric tower, oil is delivered to vacuum distillation tower through the vacuum furnace heating by pressure-reducing line for oil-transferring at the bottom of the atmospheric tower, obtains to satisfy the product of specification of quality and the vacuum distillate of downstream unit from the vacuum distillation tower side line.
Continuous growth along with scientific and technical develop rapidly and social life consumption, the world oil demand is along with expanding economy increases year by year, heavy oil and overweight oil supplying ratio progressively increase in the crude resources supply, and lightweight oil, middle matter oil supplying ratio continue to descend.Improve the extracting rate in the crude oil atmospheric vacuum distillation, obtain more light oil distillate oil, reduce the atmospheric and vacuum distillation unit energy consumption, improve the device economic benefit and become the common problem of paying close attention to of global refinery industry.And along with the fast development of Chinese national economy, the China's oil total quantity consumed is estimated to break through 6.5 hundred million tons at the year two thousand twenty, and the external interdependency of crude oil will reach 50%～60%.Rationally utilize crude resources, optimizing complete processing has been the imperative act of China's oil chemical industry.In device maximization and the integrated novel refinery design of refinery, crude oil atmospheric vacuum distillation device as " tap " rationalizes at utilization of resources maximization, energy utilization economized, running cost, the size investment optimizing, has critical role in the Sustainable development of realization China's oil chemical industry.Therefore, newly-built crude unit requires higher depth of cut, and cut content below 500 ℃ is less than the 5%(quality in the vacuum residuum), in addition lower; Many old atmospheric and vacuum distillation unit face process scale and can not satisfy the situation that treatment capacity requires and oil variety constantly changes when requiring higher cut point, need carry out capacity expansion revamping to device, eliminate " bottleneck ", improve the crude distillation ability.
For this reason, Chinese scholars compares deep research to decompression deep drawing technology, for improving the extracting rate of vacuum fractionation tower, has drawn a series of experience, and can be summed up as: (1) adopts advanced vacuum system, improves the vacuum tightness of vacuum fractionation cat head; (2) adopt novel, high efficiency packing, reduce the tower internal drop, make that flash zone keeps higher vacuum at the bottom of the tower; (3) improve the transfer line design, reduction transfer line pressure falls with temperature and falls; (4) optimize washing section design and operation, strengthen the fractionation concept of washing section; (5) adopt new and effective gas and liquid distributor etc.
Patent US7172686 has delivered a kind of method that improves crude distillation distillate yield, and method one is to extract gaseous stream out from the tower inside cord, separates obtaining product, and a part of gas phase is returned in the tower; Method two is incoming mixture by boiling point height heating and separating is lighting end, middle runnings, last running, enter at different feed entrance points respectively then and carry out fractionation in the tower, from side line extract out successively gently, last running.Method one is equivalent to side line and has added a stripping tower, has improved the distillate quality.But plant investment and energy consumption have to a certain degree been increased; Method two has been realized gently, the last running sectional feeding, improved the operation of crude distillation separation column, be conducive to improve the distillate yield, carry out fractionation in the tower but the lighting end of having separated sent into again from parallel feeding, 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 at the bottom of the tower and separates, and have a vacuum system interface to link to each other with the top vacuum system.This utility model separates the rectifying section of vacuum distillation tower and the deep drawing section of bottom by liquid seal device, oil quality and extracting rate can be paid attention to respectively, can relatively improve the decompression extracting rate, but the oil quality of deep drawing is difficult to satisfy downstream unit to the processing requirement of raw material, the tower structure complexity of this utility model simultaneously, top vacuum system loading height, plant energy consumption relatively can be high.
Patent CN1287872A discloses a kind of crude oil atmospheric vacuum distillation method that has degree of depth stripping process, be at vacuum distillation tower side washing tank in parallel, 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 after cooling off, enter downward spray and the reverse mass-and heat-transfer of oil gas that makes progress by washing tank top, the top of vacuum distillation tower is returned in the tank deck oil gas discharging of washing tank, and a jar end discharging is returned vacuum distillation tower as washing oil.This technology makes the vacuum distillation tower stripping stage experience a steam stripped process of the degree of depth by setting up washing tank, is conducive to improve the decompression extracting rate.But this method has just carried out optimizing improvement to the vacuum distillation tower stripping stage, subtracts third fractional oil preferably as washing oil with quality, waits research in economic benefit.
Patent CN1884441A discloses the method that improves light oil yield of atmospheric and vacuum distillation of petroleum oil, and the additive that will contain rosin is added in the crude oil of atmospheric and vacuum distillation of petroleum tower, by changing the light oil yield that the intermolecular reactive force of crude oil improves atmospheric and vacuum distillation.But this method does not fundamentally change distillation technique in Technology, and will consume a large amount of additives, the operation easier that has increased device running cost and added chemical reagent.
Patent CN101376068A discloses a kind of atmospheric vacuum distillation method and equipment that has vacuum flasher, is that a vacuum flasher is set before long residuum is gone into vacuum furnace.The oil process furnace that advances to reduce pressure at the bottom of the flashing tower, flash distillation overhead gas enter that certain sideline product close with flash distillation overhead gas cut extract out mouthful above or below.This method reaches the raising treatment capacity by increasing the flow process that vacuum flasher improves atmospheric and vacuum distillation unit, improves extracting rate, the purpose that cuts down the consumption of energy.But oil is gone into flashing tower at the bottom of the atmospheric tower, because the temperature of oil is relatively low at the bottom of the atmospheric tower, the vacuum tightness of adding the stokehold flashing tower is not high relatively, the effect of flashing tower flash distillation gasification is limited, and flash distillation cat head gas phase is gone into vacuum distillation tower, be equivalent to vacuum distillation tower sectional feeding after the flash distillation, not in the fractionation that fundamentally changes vacuum distillation tower.
Pressure-reducing line for oil-transferring is the connection line between vacuum furnace and the vacuum distillation tower, and tube fluid belongs to the moving process of alternating temperature stream-liquid two-phase flow.Under high temperature, high vacuum operational condition, the temperature of pressure-reducing line for oil-transferring inner fluid, pressure and flow velocity are along the variation in the transfer line cross section equilibrium evaporation rate important influence to the transfer line inner fluid, and then directly influence the vaporescence of vacuum distillation tower flash zone, the decompression extracting rate is played crucial effects.In the last few years, replaced high speed transfer line in the past gradually with major diameter (general diameter can reach more than the 2m) low speed pressure-reducing line for oil-transferring technology in the vacuum distillation apparatus, its objective is under the condition that guarantees vacuum distillation tower feed zone vaporization branch rate, reduce the 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, divide rate to improve product.For reaching this purpose, have only and reduce boiler tube and transfer line pressure drop as far as possible, make the oil product evaporating point in advance.Because transfer line must adopt 15m above (to guarantee that gas-liquid has certain separation time mutually, be conducive to improve the quality of products and the 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, factors such as calorific loss and pressure drop increase all are unfavorable for the operation of vacuum still simultaneously, and the thermal stresses, the thermal walking that form cause certain degree of difficulty to design and installation in security.
Summary of the invention
At 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, can obviously improve the extracting rate in the vacuum distillation process, 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: the cancellation pressure-reducing line for oil-transferring arranges vacuum flasher between vacuum furnace and vacuum still; The vacuum flashing jar is set behind vacuum still.
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 (being called for short oil of the normal end) at first enters the decompression process furnace at the bottom of the atmospheric tower by air distillation after heat exchange heats up, and is heated to 390～420 ℃;
(2) the gas-liquid mixed vacuum furnace discharging that comes from step (1) enters vacuum flasher, flashing tower gas phase (dodging gas to call one in the following text) knockout drum after entering tower after heat exchange, the condensation cooling, the separating tank top connects pumped vacuum systems, and vacuum distillate is discharged in the separating tank bottom;
(3) enter the vacuum still feed zone from the next flashing tower liquid phase of step (2) and carry out underpressure distillation, the underpressure distillation column overhead connects pumped vacuum systems, extracts the decompression benzoline out from the vacuum still side line, extracts depressed heavy oil at the bottom of the underpressure distillation Tata out;
(4) depressed heavy oil that comes from step (3) enters the vacuum flashing jar, and flash tank gas phase (dodging gas to call two in the following text) enters a jar back knockout drum after heat exchange, condensation cooling, and the separating tank top connects pumped vacuum systems, and vacuum distillate is discharged in the separating tank bottom;
(5) the flash tank liquid phase vacuum residuum that comes from step (4) is extracted out by pump.
In the 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, the cat head working pressure is by knockout drum gaseous phase outlet control behind the tower, controlling flashing tower pressure by the control valve on the gaseous phase outlet is 10 kPa～80 kPa, is preferably 20 kPa～50 kPa.
In the vacuum distillation method of the present invention, described one is condensed into the liquid phase caterpillar after dodging gas and the underpressure distillation raw material heat exchange that enters before the vacuum furnace, perhaps with a certain of vacuum still or certain several cut mixing caterpillar.The underpressure distillation raw material is generally oil (to call oil of the normal end in the following text) at the bottom of the air distillation Tata.
In the vacuum distillation method of the present invention, cancelled the setting of pressure-reducing line for oil-transferring in the conventional underpressure distillation, vertical flashing tower is set between vacuum furnace and vacuum distillation tower, can compactly arranges between flashing tower and vacuum furnace, the vacuum still, need not to consider to arrange the transfer line setting that is not less than 15 meters.
In the vacuum distillation method of the present invention, the described vacuum flashing jar of step (4) is horizontal tank, to realize the bigger flash distillation face of vacuum flashing jar.
In the vacuum distillation method of the present invention, the pressure of described vacuum flashing jar is than low 2 kPa of vacuum still tower bottom pressure～5 kPa, and the depressed heavy oil that vacuum distillation tower is discharged is by going into the vacuum flashing jar from baric flow.The tank deck working pressure is by a jar back knockout drum gaseous phase outlet control.
In the vacuum distillation method of the present invention, the depressed heavy oil of discharging at the bottom of the underpressure distillation Tata is introduced the vacuum flashing jar by hole enlargement pipeline step by step, lighting end in the vacuum residuum is depressed at the oil gas branch that reduces step by step be evaporated, finally in the complete flash distillation of vacuum flashing jar.
In the vacuum distillation method of the present invention, the position height of vacuum flashing jar is in vacuum still, and vacuum flashing jar opening for feed is positioned at 30%～70% place of liquid level at the bottom of the underpressure distillation Tata, preferred 45%～55%.On the one hand guarantee that vacuum still can not be evacuated, prevent the underpressure distillation Tata on the other hand at the bottom of the liquid phase residual overlong time cause coking.
In the vacuum distillation method of the present invention, need the logistics heat exchange of heating in vacuum flashing tank deck gas phase and oil of the normal end or the device, reduce plant energy consumption.
In the vacuum distillation method of the present invention, extracted out the vacuum residuum of degree of depth flash distillation at the bottom of the vacuum flashing jar jar by pump, jar end liquid automatic control pump discharge flow.
In the vacuum distillation method of the present invention, one cover pumped vacuum systems can be set, vacuum still, vacuum flasher and vacuum flashing jar share a cover pumped vacuum systems vacuum pumping, and control device can be set, and control the vacuum tightness of vacuum still, vacuum flasher and vacuum flashing jar respectively; Two covers or three cover pumped vacuum systems also can be set, and vacuum still, vacuum flasher and vacuum flashing jar are united or vacuum pumping respectively in twos.Vacuum pumping can be adopted the method and apparatus of this area routine.
In the vacuum distillation method of the present invention, other technology contents such as vacuum furnace, vacuum still 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 vacuum flasher is set behind vacuum furnace, is in time separated the lighting end of heating and gasifying, reduces the vacuum still load, has reduced the energy consumption of device; By the vacuum flashing jar is set behind vacuum still, make in the vacuum residuum relatively that lighter cut further obtains flash distillation, improve the vacuum distillate yield, thereby realize the underpressure distillation operation that less energy-consumption is deeply always pulled out.Compared with prior art, the present invention has the following advantages:
1) the vacuum furnace outlet directly is communicated with vacuum flasher, and vacuum distillation tower is introduced in the discharging of flashing tower bottom liquid phases.Shorten the reduced pressure distillation process flow process, greatly reduce process pressure drop and the calorific loss of pressure-reducing line for oil-transferring in the prior art, make the vacuum furnace internal pressure lower, the outlet of still vaporization rate is higher.
2) cancellation pressure-reducing line for oil-transferring, the reduced pressure distillation process design has been optimized in the transfer line thermal walking of having avoided extra heavy pipe footpath, big pipe range transfer line low speed segment to cause.Through adjusting, the cost of flashing tower is starkly lower than the cost of extra heavy pipe footpath, big pipe range transfer line.
3) dodge end oil and enter vacuum still separately, significantly reduce the processing load of vacuum still, reduced the required theoretical stage of vacuum distillation tower, can suitably reduce tower height and tower diameter, the economy system investment; Eliminated " bottleneck " of vacuum distillation tower treatment capacity, be conducive to the capacity expansion revamping of old device; The gas phase of having avoided the gas-liquid mixed charging to cause is carried secretly, has guaranteed depressurised side line products quality; Reduce full tower pressure drop, be conducive to improve the decompression extracting rate, reduced the decompression overhead condensation and vacuumized load.Underpressure distillation less energy-consumption, high vacuum, the operation of high extracting rate have been realized.
4) a sudden strain of a muscle gas and oil of the normal end carry out heat exchange, have reduced the vacuum furnace load, reduce plant energy consumption.
5) vacuum flashing jar degree of depth flash distillation improves on the one hand the vacuum distillate yield of this device, make in the vacuum residuum＜cuts of 500 ℃ and＜538 ℃ reduce greatly.Reduce downstream coking or visbreaking etc. on the other hand and handle the load of vacuum residuum device, reduce the cracking loss of benzoline.
6) the vacuum flashing jar can be used as the surge tank of discharging pump at the bottom of the tower, prevent tower at the bottom of discharging pump find 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) Technology of the present invention is rationally advanced, and energy consumption level is low, and the vacuum residuum yield is low, and for the design and construction of new device, it is rationally advanced to have technology, and energy consumption level is low, characteristics such as vacuum distillate yield height, less investment; For the transformation of old device, have that the scrap build amount is few, investment is low, it is short to transform the duration, and the device income is advantage such as quick obviously.
Description of drawings
The process flow diagram of the vacuum distillation method that Fig. 1 deeply always pulls out for a kind of less energy-consumption of the present invention.
Wherein 1 is oil of the normal end (be atmospheric tower at the bottom of oil); 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 are the vacuum flashing jar; 13 is knockout drum behind the tower; 14 is a jar back knockout drum.
Embodiment
The inventive method directly is communicated with a flashing tower in the vacuum furnace outlet, and vacuum distillation tower is introduced in the discharging of flashing tower bottom liquid phases.The gas-liquid flash separation is carried out in the gas-liquid mixed charging that vacuum furnace heating and gasifying rate is very high under the condition of flashing tower condition of high vacuum degree.One dodge gas by tank deck through and vacuum furnace charging heat exchange, knockout drum after entering tower after the water cooler cooling again, the liquid phase vacuum distillate is as the product discharging.Dodge end oil and directly enter the vacuum still feed zone, at the bottom of having tower, further carry out fractionation in the vacuum still of stripped vapor, extract vacuum distillate out from the vacuum still side line, depressed heavy oil is extracted out at the bottom of by tower and is directly entered the vacuum flashing jar, makes depressed heavy oil carry out vacuum flashing under the condition of vacuum flashing jar condition of high vacuum degree.Two dodge gas by tank deck through entering a jar back knockout drum with heat exchange, after cooling off.The gas-liquid separation tank top connects pumped vacuum systems, keeps the higher relatively vacuum tightness of vacuum flashing jar; The bottom is extracted vacuum distillate out as product.Vacuum residuum is extracted out at the bottom of vacuum flashing jar jar.
The vacuum distillation method that deeply always pulls out in conjunction with the less energy-consumption of the present invention of Fig. 1 is described:
As shown in Figure 1: oil of the normal end 1 enters vacuum furnace 2 earlier after heat exchange rising temperature, temperature directly enters vacuum flasher 4 after being heated to 400 ℃～420 ℃ in vacuum furnace.In vacuum flasher, carry out gas-liquid separation and flash distillation, gas phase is discharged one through broken foam demist net by tank deck and is dodged gas, with gas-liquid separator 13 after the condenser cooling enters tower again after the oil cooling of the normal end, the gas-liquid separator top connects pumped vacuum systems 9 behind the tower, keeps the certain vacuum tightness of vacuum flasher.Vacuum distillate 10 is discharged in the bottom.The vacuum flasher liquid phase is dodged end oil 8 and is directly entered vacuum still 5 feed zones, carries out underpressure distillation under the effect of stripped vapor 7 and underpressure distillation cat head pumped vacuum systems 9, obtains sideline product vacuum distillate 10 in the tower.Depressed heavy oil 6 is by the VACUUM TOWER BOTTOM discharging.Introduce vacuum flashing jar 12 through hole enlargement pipeline step by step, under the condition of vacuum flashing jar high vacuum, the depressed heavy oil of high temperature obtains further flash distillation.Two dodge gas enters a jar back knockout drum 14 after the heat exchange cooling, the separating tank top connects pumped vacuum systems 9, keeps the higher vacuum tightness of vacuum flashing jar 12, and extraction vacuum distillate 10 is as the product discharging bottom the separating tank.Vacuum flashing jar liquid phase is extracted out at the bottom of by jar, as vacuum residuum 6 dischargings.
Vacuum flasher, vacuum still and vacuum flashing jar have Level Detection to show respectively.
Vacuum still described in the present invention can be the fuel type vacuum still, also can be lubricated oil type vacuum still; Can be wet distiller, wet distiller also can decline; Sideline product discharging number specifically arranges as required.
Have the vacuum distillation method and the equipment that have flash tank behind flashing tower, the vacuum distillation tower behind the vacuum furnace of the present invention, improved the crude oil reduced pressure distillation process, lower pressure heating and gasifying rate in vacuum furnace reached 50%～60% parallel feeding and in vacuum flasher, carry out gas-liquid separation, need not establish long pressure-reducing line for oil-transferring low speed segment again and carry out gas-liquid separation (it is 15m that prior art requires transfer line low speed segment length), the horizontal thermal walking of transfer line of having avoided extra heavy pipe footpath, big pipe range low speed segment to cause.Flash distillation cat head gas phase and vacuum furnace charging are carried out after heat exchange, the condensation directly as product, and liquid phase enters vacuum still separately.Thereby reduced the processing load of vacuum still, reduced the required theoretical stage of vacuum still to a certain extent, can suitably reduce tower height and tower diameter, significantly reduced the condensation of underpressure distillation cat head and vacuumized load simultaneously; And the gas phase that can avoid the gas-liquid mixed charging to cause carries secretly, guaranteed depressurised side line products quality.The vacuum flashing jar that the depressed heavy oil of VACUUM TOWER BOTTOM enters condition of high vacuum degree again carries out further flash distillation, make in the depressed heavy oil that the lighter complete flash distillation of cut is come out relatively, in the assurance vacuum residuum＜500 ℃ cut is reduced to minimum with＜538 ℃ cut content, thereby improve the extracting rate of underpressure distillation, increase the economic benefit of device.Calculate confirmation through Aspen Hysys flowsheeting software simulation, handle the residual oil yield few 2%～5% of the existing operational path of identical raw material processing method of the present invention, and the vacuum flashing cat head accounts for sensible heat that the oil gas of charging 50%～60% contains and latent heat and is enough to oil heat exchange to 390 of the normal end ℃～400 ℃ is reduced the load of vacuum furnace greatly.
When the present invention goes into operation at device, can open big vacuum furnace load, heating is fed to 390 ℃～400 ℃, guarantees the underpressure distillation operation.Go into operation stable after, take full advantage of sensible heat and the latent heat that high temperature dodges top gas and give the oil heating of the normal end, can reduce the load of vacuum furnace, implement device is energy-conservation.
Below by specific embodiment method of the present invention is elaborated.Data are that Aspen flowsheeting software simulation calculates acquisition in embodiment and the comparative example.
Embodiment 1
Method of the present invention is used for certain newly-built 1,000 ten thousand tons of/year crude oil atmospheric vacuum distillation Design of 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 the decompression flow process comprises vacuum furnace, vacuum flasher, vacuum still and vacuum flashing jar.Vacuum still is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging, and the cat head working pressure is 1.315 kPa, and full tower pressure drop is 685Pa.
Oil 1 of the normal end is fed into vacuum distillation apparatus with 650 tons/hour, enters vacuum flasher 4 after vacuum furnace 2 is heated to 400 ℃, and control flashing tower pressure is 10 kPa.Sudden strain of a muscle end oil enters vacuum distillation tower and carries out underpressure distillation, and distillation back depressed heavy oil enters the vacuum flashing jar, and flash tank pressure is 1.2 kPa.Oil is as the vacuum residuum discharging at the bottom of the vacuum flashing jar.
Comparative example 1
Relate to newly-built 1,000 ten thousand tons of/year crude oil atmospheric vacuum distillation Design of device among the embodiment 1 equally.The treatment capacity of reliever is 5,500,000 tons/year.Adopt the disclosed atmospheric vacuum distillation method that has vacuum flasher among the CN101376068A.
Under same feedstock, processing condition, listed the employing embodiment of the invention 1 and comparative example 1 in the table 1 at aspects such as decompression extracting rate, plant energy consumption, investments, use the data contrast that Aspen flowsheeting software carries out modeling effort.
Table 1
| Project | Embodiment 1 | Comparative example 1 |
| Operational condition | ? | ? |
| The nominal treatment capacity/(ton/hour) | 650 | 650 |
| The charging kind | Iran crude＞350 ℃ part | Iran crude＞350 ℃ part |
| Vacuum distillation tower tower top pressure/kPa | 1.315 | 1.315 |
| Tower pressure drop/kPa | 0.685 | 0.685 |
| The vacuum furnace temperature out/℃ | 400 | 400 |
| Tower flash zone feeding temperature/℃ | 400(disregards heat radiation) | 394(disregards heat radiation) |
| Flashing tower pressure/kPa | 10 | — |
| Flash tank pressure/kPa | 1.2 | 20 |
| Yield(to the decompression charging) | ? | ? |
| Vacuum residuum yield/% (m) | 35.14 | 38.42 |
| The decompressed wax oil cut point/℃ | 618 | 565 |
| Energy consumption | ? | ? |
| Vacuum furnace load/MW | 31.45 | 38.54 |
| Consumption 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, aspect facility investment, though utilize the embodiment of the invention 1 to use a flashing tower, the vacuum distillation tower tower diameter is less more from table 1, and investment reduces, and corresponding column internals and filler investment also will reduce, and total plant investment can't increase; Aspect plant energy consumption, the scheme of embodiment 1 obviously is better than comparative example 1; Aspect the decompression extracting rate, the result of embodiment 1 is better than comparative example 1 far away, and the degree of deep drawing is also higher relatively, and declining to a great extent appears in the vacuum residuum yield.
Among the embodiment 1, vacuum residuum is the 35.14%(quality to the yield of decompression charging), the cut point of decompressed wax oil reaches 618 ℃.Press comparative example 1 described method and calculate, vacuum residuum is 38.42% to the yield of combined feed total feed, and the decompressed wax oil cut point is 565 ℃, and the deep drawing degree is not as good as the present invention.
Adopt the underpressure distillation flow process of the embodiment of the invention 1, the maximum tower diameter of vacuum distillation tower is φ 5200mm, and as adopting 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 adopting the flow process of embodiment 1, the vacuum furnace load is 38.54MW, adopts the energy consumption of apparatus of the present invention to descend about 20%.
Calculate by 1,000 ten thousand tons of/year atmospheric and vacuum distillation unit, the charging of decompression part is about 650 tons/hour, embodiment 1 reduces residual oil yield 3.28% than comparative example 1, comes for 300 yuan/ton in residual oil and mixed gatch price difference, and year is amounted to Renminbi: 650 * 3.28% * 300 * 8400=5372.64 ten thousand yuan.Add the part that device cuts down the consumption of energy, the device economic benefit highly significant of obtaining.
Embodiment 2
The expansion that method of the present invention is used for certain 8,000,000 tons of/year crude oil atmospheric and vacuum distillation unit can be 1,000 ten thousand tons of/year transformations.It is identical with conventional atmospheric and vacuum distillation unit that normal pressure is partly transformed, and the treatment capacity of reliever can be 5,500,000 tons/year by 4,500,000 tons of/year original expansions.
The decompression flow process comprises vacuum furnace, vacuum flasher, vacuum still and vacuum flashing jar.Vacuum still is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% of tower charging, and the cat head working pressure is 1.315 kPa, and full tower pressure drop is 685Pa.
Oil 1 of the normal end is fed into vacuum distillation apparatus with 650 tons/hour, enters vacuum flasher 4 after vacuum furnace 2 is heated to 400 ℃, and control flashing tower pressure is 10 kPa.Sudden strain of a muscle end oil enters vacuum distillation tower and carries out underpressure distillation, and distillation back depressed heavy oil enters the vacuum flashing jar, and flash tank pressure is 1.2 kPa.Oil is as the vacuum residuum discharging at the bottom of the vacuum flashing jar.
This device capacity expansion revamping relief portion is divided and is kept original vacuum furnace and vacuum distillation tower, and vacuum distillation tower internals and filler are transformed, and vacuum furnace is carried out capacity expansion revamping.Newly-increased main equipment is vacuum flasher, vacuum flashing jar.
Vacuum flasher is regular packed tower, interior dress single hop high-throughput, low pressure drop structured packing.
Transform back device decompression part working ability and can improve 30%～50%, plant energy consumption reduces by 10%～15%, and the vacuum residuum yield reduces by 2%～5%.
Comparative example 2
At the same set of crude oil atmospheric vacuum distillation device that relates among the embodiment 2, the disclosed atmospheric vacuum distillation method that has vacuum flasher carries out capacity expansion revamping among the employing CN101376068A.
Under same feedstock, processing condition, listed the employing embodiment of the invention 2 and comparative example 2 in the table 2 at same set of atmospheric and vacuum distillation unit decompression part transformation situation, use the data contrast that Aspen flowsheeting software carries out modeling effort.
Table 2
| Project | Before the transformation | Embodiment 2 | Comparative example 2 |
| The nominal treatment capacity/(t/h) | 450 | 650 | 650 |
| The charging kind | Iran crude＞350 ℃ part | Iran crude＞350 ℃ part | Iran crude＞350 ℃ part |
| Vacuum residuum yield/% (m) | 39.79 | 35.14 | 38.42 |
| The decompressed wax oil cut point/℃ | 540 | 618 | 565 |
| Main equipment is transformed 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 | Transform, | Transform, enlarge load |
| Flash tank | Do not have | Newly-built 1 φ 3000 | Newly-built 1 φ 4200 |
| Flashing tower | Do not have | Newly-built 1 φ 4600 | Do not have |
| Investment | ? | ? | ? |
| Construction investment | — | Moderate | Bigger |
After carrying out capacity expansion revamping according to embodiment 2, vacuum residuum is the 35.14%(quality to the yield of decompression charging), the cut point of decompressed wax oil reaches 618 ℃.And press comparative example 2 described methods, vacuum residuum is 38.42% to the yield of combined feed total feed, the decompressed wax oil cut point is 565 ℃, though carrying out certain expansion, 2 pairs of original devices of comparative example can upgrade, the decompressed wax oil cut point has the raising of certain amplitude, but the investment of transforming is slightly larger than embodiment 2, and the vacuum residuum yield is higher than embodiment 2, and the deep drawing degree is also not as good as the embodiment of the invention 2.And transform the back plant energy consumptions by embodiment 2 and descend about 10%.
Calculate by 1,000 ten thousand tons of/year atmospheric and vacuum distillation unit, the charging of decompression part is about 650 tons/hour, embodiment 1 reduces residual oil yield 3.28% than comparative example 1, comes for 300 yuan/ton in residual oil and mixed gatch price difference, and year is amounted to Renminbi: 650 * 3.28% * 300 * 8400=5372.64 ten thousand yuan.Add the part that device cuts down the consumption of energy, the device economic benefit highly significant of obtaining.
Claims (10)
1. vacuum distillation method that less energy-consumption is deeply always pulled out comprises following content:
(1) oil at first enters the decompression process furnace at the bottom of the atmospheric tower by air distillation after heat exchange heats up, and is heated to 390～420 ℃;
(2) the gas-liquid mixed vacuum furnace discharging that comes from step (1) enters vacuum flasher, and the flashing tower gas phase is knockout drum after entering tower after heat exchange, the condensation cooling, and the separating tank top connects pumped vacuum systems, and vacuum distillate is discharged in the separating tank bottom;
(3) enter the vacuum still feed zone from the next flashing tower liquid phase of step (2) and carry out underpressure distillation, the underpressure distillation column overhead connects pumped vacuum systems, extracts the decompression benzoline out from the vacuum still side line, extracts depressed heavy oil at the bottom of the underpressure distillation Tata out;
(4) depressed heavy oil that comes from step (3) enters the vacuum flashing jar, and the flash tank gas phase enters a jar back knockout drum after heat exchange, condensation cooling, and the separating tank top connects pumped vacuum systems, and vacuum distillate is discharged in the separating tank bottom;
(5) the flash tank liquid phase vacuum residuum that comes 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 by tower after the knockout drum gaseous phase outlet be controlled to be 10 kPa～80 kPa.
4. in accordance with the method for claim 1, it is characterized in that, be condensed into the liquid phase caterpillar after described flashing tower gas phase and the underpressure distillation raw material heat exchange that enters before the vacuum furnace, perhaps with a kind of of vacuum still or certain several cut mixing caterpillar.
5. in accordance with the method for claim 1, it is characterized in that the described vacuum flashing jar of step (4) is horizontal tank.
6. in accordance with the method for claim 1, it is characterized in that the pressure of described vacuum flashing jar is than low 2 kPa of vacuum still tower bottom pressure～5 kPa.
7. in accordance with the method for claim 1, it is characterized in that, the depressed heavy oil of discharging at the bottom of the described underpressure distillation Tata is introduced the vacuum flashing jar by hole enlargement pipeline step by step, lighting end in the vacuum residuum is depressed at the oil gas branch that reduces step by step be evaporated, finally in the complete flash distillation of vacuum flashing jar.
8. in accordance with the method for claim 1, it is characterized in that the position height of described vacuum flashing jar is in vacuum still, the opening for feed of vacuum flashing jar is positioned at 30%～70% place of liquid level at the bottom of the underpressure distillation Tata.
9. in accordance with the method for claim 1, it is characterized in that, one cover pumped vacuum systems is set, vacuum still, vacuum flasher and vacuum flashing jar share a cover pumped vacuum systems vacuum pumping, control device is set, controls the vacuum tightness of vacuum still, vacuum flasher and vacuum flashing jar respectively.
10. in accordance with the method for claim 1, it is characterized in that two covers or three cover pumped vacuum systems are set, and vacuum still, vacuum flasher and vacuum flashing jar are united or vacuum pumping respectively in twos.
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| CN107057747A (en) * | 2016-11-07 | 2017-08-18 | 中国石油大学(华东) | It is a kind of based on the energy-efficient deep drawing technique of Atmospheric vacuum clearly cut |
| CN107699273A (en) * | 2017-11-15 | 2018-02-16 | 中国石油大学(北京) | A kind of anhydrous atmospheric and vacuum distillation technique and device |
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| 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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| 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 |
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| CN107057747A (en) * | 2016-11-07 | 2017-08-18 | 中国石油大学(华东) | It is a kind of based on the energy-efficient deep drawing technique of Atmospheric vacuum clearly cut |
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