CN103059918A - 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 the refining of petroleum field, relate in particular to the gradually gasification sectional feeding vacuum distillation method that improves the 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 that crude oil is divided into different boiling range scopes by the method for distillation, to adapt to product and downstream unit to the processing requirement of raw material.The size of the height of its light oil yield and energy consumption directly affects the economic benefit of refining of petroleum.Reduced pressure distillation process utilizes the underpressure distillation principle exactly, and by vacuumizing the pressure decreased that makes fluid surface, thereby the boiling point that reduces liquid makes component vaporization relatively light 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.
Continuous growth along with scientific and technical develop rapidly and social life consumption, the world petroleum demand amount is along with expanding economy increases year by year, heavy oil and overweight oil supplying ratio progressively increase in the crude resources supply, lightweight oil, middle matter oil supplying ratio continuous decrease.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 Refining Chemical 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, optimization processing technology has been the imperative act of China's oil chemical industry.In device maximization and Integrated Refinery And Petrochemical novel refinery design, crude oil atmospheric vacuum distillation device as " tap " rationalizes at utilization of resources maximization, energy utilization economized, running cost, the size investment optimizing, has very important status 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 to carry out capacity expansion revamping to device, eliminate " bottleneck ", improve the 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, has drawn a series of experience, 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, so that flash zone keeps higher vacuum at the bottom of the tower; (3) improve the transfer line design, reduce transfer line Pressure Drop and temperature and fall; (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 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 of this utility model is complicated simultaneously, the 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, at vacuum distillation tower side washing tank in parallel, the feed zone of vacuum distillation tower and stripping stage are separated by fluid-tight isolation sparger, 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, 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 discharging is returned vacuum distillation tower as washing oil at the bottom of the tank.This technique 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 the method just is optimized improvement to the vacuum distillation tower stripping stage, subtracts preferably third fractional oil 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, improves the light oil yield of atmospheric and vacuum distillation by changing the intermolecular reactive force of crude oil.But the 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 with vacuum flasher and equipment, is a vacuum flasher is set before long residuum enters vacuum furnace.The oil process furnace that advances to reduce pressure at the bottom of the flashing tower, flashing tower top gas enter that certain sideline product close with flashing tower top gas cut extract out mouthful above or below.The method is improved the flow process of atmospheric and vacuum distillation unit by increasing vacuum flasher, reach the raising treatment capacity, improves extracting rate, reduces the purpose of energy consumption.But oil enters 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 relatively not high, the effect of flashing tower flash distillation gasification is limited, and the flash distillation top gaseous phase enters 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 have important impact along the variation in transfer line cross section to the equilibrium evaporation rate of transfer line inner fluid, and then directly affect the vaporescence of vacuum distillation tower flash zone, the decompression extracting rate is played vital effect.In the last few years, replaced gradually high speed transfer line in the past 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 minute rate, reduce as far as possible the vacuum furnace temperature out, to prevent tube coking.In other words, be under the heater outlet temperature of regulation, improve as far as possible tower feed zone vaporization rate, divide rate to improve product.For reaching this purpose, only have and reduce as far as possible boiler tube and transfer line pressure drop, make the oil product evaporating point in advance.15m is above (to have certain separation time to guarantee liquid phase because transfer line must adopt, 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, the 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 difficulty to design and installation in security.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of gradually gasification sectional feeding vacuum distillation method that improves the decompression extracting rate, can obviously improve the extracting rate in the crude oil vacuum distillation process, reduce crude oil vacuum distillation apparatus energy consumption, increase the device economic benefit, the economy system investment.
Gradually sectional feeding vacuum distillation method and the device of gasifying provided by the invention comprises following content: crude oil oil (hereinafter referred to as oil of the normal end) at the bottom of the atmospheric tower after the normal pressure distillation enters vacuum distillation apparatus, in vacuum distillation process, adopt gradually gasification and the technique that gradually reduces pressure, make in the oil of the normal end the ground underpressure distillation of lighting end maximum out.Gradually gasification refers to oil of the normal end is heated gradually, and utilizes the feed separation after separating device in time will gasify to go out; Gradually decompression refers to the material gradually step-down in separating device to entering separating device after gradually gasifying, and realizes gasification under lower pressure.
A kind of sectional feeding vacuum distillation method that gradually gasifies provided by the invention is achieved in that
(1) oil (being called for short oil of the normal end) at first enters the one-level vapourizing furnace at the bottom of the atmospheric tower that is come by air distillation, enters the one-level flash tank after being heated to 370～380 ℃, and one-level flash distillation gas phase enters vacuum still top distillation stage;
(2) one-level flash distillation liquid phase of coming from (1) enters the secondary vapourizing furnace, enters the two-stage flash tank after being heated to 390～400 ℃, and the two-stage flash gas phase enters vacuum still middle part distillation stage;
(3) the two-stage flash liquid phase of coming from step (2) enters three grades of vapourizing furnaces, enters three grades of flash tanks after being heated to 410～420 ℃, and three grades of flash distillation gas phases enter vacuum still bottom distillation stage;
(4) three grades of flash distillation liquid phases coming from step (3) enter the vacuum still flash zone;
(5) each section feeding carries out underpressure distillation in vacuum still, and the underpressure distillation column overhead connects pumped vacuum systems, from each lateral line withdrawal function product of tower, extracts vacuum residuum at the bottom of the tower out.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, and described one-level flash tank is vertical structure, can be provided with the equipment that is beneficial to gas-liquid separation and gasification in the tank, also can be slack tank, and the tank deck working pressure is controlled by gaseous phase outlet.One-level flash tank gaseous phase outlet connects vacuum still top distillation stage, is 8 kPa～40 kPa by the control of the control valve on gaseous phase outlet one-level flash tank pressure, is preferably 10 kPa～20 kPa.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, described two-stage flash tank is vertical structure, can be provided with the equipment that is beneficial to gas-liquid separation and gasification in the tank, also can be slack tank, the tank deck working pressure is controlled by gaseous phase outlet, gaseous phase outlet connects vacuum still middle part distillation stage, is 5 kPa～30 kPa by the control of the control valve on gaseous phase outlet two-stage flash pressure tank, is preferably 6 kPa～15 kPa.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, described three grades of flash tanks are vertical structure, can be provided with the equipment that is beneficial to gas-liquid separation and gasification in the tank, also can be slack tank, the tank deck working pressure is controlled by gaseous phase outlet, gaseous phase outlet connects vacuum still bottom distillation stage, is 2 kPa～20 kPa by three grades of flash tank pressure of the control of the control valve on the gaseous phase outlet, is preferably 3 kPa～10 kPa.
The present invention's sectional feeding vacuum distillation method that gradually gasifies, cancelled the setting of conventional pressure-reducing line for oil-transferring, gradually vapourizing furnace and gradually separating device are set between atmospheric tower and vacuum distillation tower, connect with pipeline between vapourizing furnaces at different levels and the separating device, can compactly arrange, need not to consider that conventional pressure-reducing line for oil-transferring is not less than 15 meters transfer line setting.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, and described vacuum still can be the fuel type vacuum still, also can be the Lube Type vacuum still.Vacuum still can adopt the wet type operation, also can adopt the operation of little wet type or dry type; The sideline product number is generally 3～5, determines according to product needed and oil variety.
The present invention is gasified in the 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 the void tower arranged in form; Distillation stage arranges filler or the column plate of high-throughput, low pressure drop, and the number of distillation stage is generally 3～5, determines according to product needed and oil variety.The not susceptible to plugging filler of washing section setting or column plate are got to the washing section filler or washing is carried out in the column plate top with the bottom side line discharging of vacuum still; Flash zone is installed the less feed distributor of pressure drop.
The present invention gradually gasify the sectional feeding vacuum distillation method and in, described underpressure distillation column overhead is carried out vacuum pumping, control vacuum distillation tower tower top pressure is 1 kPa～10 kPa, is preferably 1kPa～5 kPa.Vacuum pumping can be adopted method and apparatus conventional in this area.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, described one-level vapourizing furnace, secondary vapourizing furnace, three grades of vapourizing furnaces can be can be three-in-one process furnace separately independently, also, and three grades of chargings are separately positioned on radiation sections different in the three-in-one process furnace.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, and described one-level flash tank, two-stage flash tank, three grades of flash tanks can independently arrange, also can arranged superposed, and to reduce plant area.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, and is excessive for fear of pressure drop, gradually gasification and gradually between pressure regulating equipment or the pipeline in the equipment can take hole enlargement to process.
The present invention is gasified in the sectional feeding vacuum distillation method gradually, by the gradually gasification to the decompression charging, charging is heated under the temperature near condensation gasifies, and significantly reduces the non-reversibility of heating and cooling; By gradually decompression, in time the lighting end of gasification is separated, reduce the load of vapourizing furnaces at different levels, thereby reduced the energy consumption of device.Compared with prior art, the present invention has the following advantages:
1, vapourizing furnace outlets at different levels directly are communicated with reduced-pressure flash tank, the flash drum overhead gas phase is introduced vacuum still, make vapourizing furnace internal pressures at different levels lower, oil of the normal end and the gasification point of flash tank liquid phases at different levels in vapourizing furnace are in advance, the outlet of still vaporization rate is high, guarantee higher total vaporization rate, thereby be conducive to improve the decompression extracting rate.
2, the lighting end that in time will gradually gasify by separation at different levels is separated, and vapourizing furnace only heats the liquid fraction of phase counterweight, and full cut all is heated to the underpressure distillation critical temperature in the more conventional reduced pressure distillation process, significantly reduces plant energy consumption.
3, liquid phase enters separately vacuum still after the flash distillation, and the Vapor Entrainment of having avoided the gas-liquid mixed charging to cause has guaranteed depressurised side line products quality.
4, the gas phase after the separation at different levels enters the vacuum still middle and upper part, reduces the full tower pressure drop of vacuum still, has reduced vacuumizing load, thereby reduces plant energy consumption.
5, the gas phase segmentation after the separation at different levels enters the different positions of vacuum still, avoided gas phase load skewness in the vacuum still, relatively light cut enters the vacuum still middle and upper part simultaneously, after the vacuum fractionation condensation in time from each lateral line withdrawal function, reduce the load of vacuum still, the expansion that is conducive to vacuum distillation apparatus can be upgraded.
6, gradually vapourizing furnace and gradually separating device can adopt compact Layout.Cancelled 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, large pipe range transfer line low speed segment to cause.
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, Technology of the present invention is rationally advanced, and energy consumption level is low, and the vacuum residuum yield is low, for the transformation of old device, has that the scrap build amount is few, original equipment utilization rate is high, the investment is low, an obvious advantage such as quick of short construction period, device income; For the design and construction of new device, have technique rationally advanced, energy consumption level is low, the vacuum distillate yield is high, and under the prerequisite of same size, can reduce the main equipment scale, the characteristics such as economy system investment.
Description of drawings
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 the one-level vapourizing furnace; 3 is the one-level flash tank; 4 is the secondary vapourizing furnace; 5 is the two-stage flash tank; 6 is three grades of vapourizing furnaces; 7 is three grades of flash tanks; 8 is vacuum still; 9 is pumped vacuum systems; 10 is the vacuum distillate discharging; 11 is stripped vapor; 12 is vacuum residuum.
Embodiment
The inventive method is taked the heavy oil after the air distillation is gasified and the technique that gradually reduces pressure gradually, the different distillation stages that gasification, vacuum flashing gas phase out enter respectively vacuum still, 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 has been cancelled the pressure-reducing line for oil-transferring in the conventional reduced pressure distillation process, adopts the method gradually heat and the increase separating device oil of the normal end that gasifies, and the feed separation after in time will gasify goes out, and thermo-cracking is crossed in the minimizing lighting end, has reduced the non-reversibility that heats; Adopt simultaneously gradually decompression technology, progressively lighting end is separated, to a certain degree reduced the oil gas dividing potential drop of material, make remaining material can under lower pressure, realize gasification, thereby gradually reduced the heating load of material, under the critical Heating temperature of oil product, can make more component gasify out, thereby greatly improve the decompression extracting rate.Present method is to the capacity expansion revamping of old device, in the situation that main equipment reuses, can greatly improve the utilization ratio of equipment, reduces plant energy consumption, improves unit capacity; To new device, optimized the reduced pressure distillation process design, economy system investment, the oily profit of ton of increase device.
In conjunction with Fig. 1 the present invention's sectional feeding vacuum distillation method that gradually gasifies is described:
Oil of the normal end 1 enters one-level vapourizing furnace 2, the mixture that is heated to the certain vaporization rate after 370 ℃～380 ℃ enters one-level flash tank 3, tank deck connects the top distillation stage of vacuum still 8, make to have in the tank and carry out the vacuum flashing separation under certain vacuum degree condition, gas phase is sent to the distillation stage on vacuum still top by tank deck, liquid phase enters secondary vapourizing furnace 4 at the bottom of the tank.Be heated to the mixture that has certain vaporization rate after 390 ℃～400 ℃ and enter two-stage flash tank 5 in secondary vapourizing furnace 4, the two-stage flash gas phase is sent to vacuum still 8 middle part distillation stages by tank deck, and liquid phase enters three grades of vapourizing furnaces 6 at the bottom of tank.Enter three grades of flash tanks 7 after three grades of vapourizing furnaces, 6 interior materials are heated to 410 ℃～420 ℃ again, the tank deck gas phase enters the distillation stage of vacuum still 8 bottoms, and liquid phase enters vacuum still 8 flash zones at the bottom of the tank.Each section feeding is in vacuum still 8, under the effect of stripped vapor 11 at the bottom of cat head pumped vacuum systems 9 and the tower, carry out underpressure distillation, extract successively vacuum distillate discharging 10 carrying devices from each condensation segment oil header of vacuum still out, vacuum residuum 12 is extracted out at the bottom of vacuum still 8 towers and is sent outside.
The present invention's sectional feeding vacuum distillation method that gradually gasifies, improved the crude oil reduced pressure distillation process, the processing method of taking gradually to heat and gradually reducing pressure, make the decompression charging under the Heating temperature of lower pressure and Geng Gao, gasify, flash distillation, guaranteed the higher vaporization rate of decompression charging, thereby 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 reduced the heating load of decompression charging, and reduced vacuum still and vacuumized load, significantly reduce the vacuum distillation apparatus energy consumption.Calculate confirmation through Aspen flowsheeting software simulation, process the few 2%～5%(weight of vacuum residuum yield of the existing operational path of identical raw material processing method of the present invention), 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 ton/years 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 ton/years, and the decompression flow process comprises one-level vapourizing furnace, one-level flash tank, secondary vapourizing furnace, two-stage flash tank, three grades of vapourizing furnaces, three grades of flash tanks, vacuum still.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 550 tons/hour, enters one-level flash tank 3 after one-level vapourizing furnace 2 is heated to 370 ℃, and the tank deck gas phase enters vacuum still 8 top distillation stages, and control tank deck gas phase guarantees that the one-level flash tank pressure is 10 kPa; Liquid phase enters secondary vapourizing furnace 4 at the bottom of the tank, enters two-stage flash tank 5 after heating to 390 ℃, and the two-stage flash gas phase enters vacuum still 8 middle part distillation stages, and control tank deck pressure is 6 kPa; The two-stage flash liquid phase enters three grades of vapourizing furnaces 6, enters 7, three grades of flash distillation gas phases of three grades of flash tanks after heating to 410 ℃ to enter vacuum still 8 bottom distillation stages, and controlling three grades of flashing pressures is 3 kPa, and three grades of flash distillation liquid phases enter vacuum still 8 flash zones.Each section feeding carries out underpressure distillation in vacuum still 8, from lateral line withdrawal function decompression product 10, vacuum residuum 12 is extracted out at the bottom of tower.
Comparative example 1
Relate to equally the design of newly-built 1,000 ten thousand ton/years of crude oil atmospheric vacuum distillation devices among the embodiment 1.The treatment capacity of reliever is 5,000,000 ton/years.Adopt disclosed atmospheric vacuum distillation method with 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 Comparison that Aspen flowsheeting software carries out modeling effort.
Table 1
| Project | Embodiment 1 | Comparative example 1 |
| Operational condition | ? | ? |
| The nominal treatment capacity/(ton/hour) | 550 | 550 |
| The charging kind | Kuwait Crude Oil＞350 ℃ part | Kuwait Crude Oil＞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/℃ | — | 410 |
| One-level vapourizing furnace temperature out/℃ | 370 | — |
| Secondary vapourizing furnace temperature out/℃ | 390 | — |
| Three grades of vapourizing furnace temperature outs/℃ | 410 | — |
| Tower flash zone feeding temperature/℃ | 410(disregards heat radiation) | 394(disregards heat radiation) |
| Total vaporization rate % (m) | 48.93 | 41.89 |
| Flash tank pressure/kPa | — | 20 |
| One-level flash tank pressure/kPa | 10 | — |
| Two-stage flash pressure tank/kPa | 6 | — |
| Three grades of flash tank pressure/kPa | 3 | — |
| Yield(to the decompression charging) | ? | ? |
| Vacuum residuum yield/% (m) | 37.50 | 40.85 |
| The decompressed wax oil cut point/℃ | 605 | 565 |
| Dodge top gas amount/% | — | 1.45 |
| One-level flash distillation 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 |
| 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 4800 | 1/φ 7916 |
| Vacuum pump | 1 | 1 |
| Process furnace | Three-in-one stove/37.745 MW | 1/39.27 MW |
| Flash tank | 3 | 1 |
As seen, aspect facility investment, although utilize the embodiment of the invention 1 multiplex two flash tanks, because the tank charging reduces gradually, the tank diameter of two-stage flash and three grades of flash tanks all can significantly dwindle, and can't increase plant investment from table 1; And the vacuum distillation tower tower diameter is less among the embodiment 1, and investment reduces, and corresponding column internals and filler investment also will reduce; And vacuum pump power is well below comparative example 1; 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 relatively high, and declining to a great extent appears in the vacuum residuum yield.
Among the embodiment 1, vacuum residuum is the 37.50%(quality to the yield of decompression charging), the cut point of decompressed wax oil reaches 605 ℃.Press comparative example 1 described method and calculate, vacuum residuum is 40.85% 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 4800mm, and as adopting 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 adopting the flow process of embodiment 1, the 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 ton/years of atmospheric and vacuum distillation unit, relief portion divides charging to be about 550 tons/hour, embodiment 1 reduces residual oil yield 3.35% than comparative example 1, comes in 250 yuan/tons of residual oil and mixed gatch price differences, year amounts to Renminbi: 550 * 3.35% * 250 * 8400=3869.25 ten thousand yuan.Add the part of device reduction energy consumption, the device economic benefit highly significant of obtaining.
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 the decompression part mainly comprises a grade vapourizing furnace, one-level flash tank, secondary vapourizing furnace, two-stage flash tank, three grades of vapourizing furnaces, three grades of flash tanks, vacuum still.
Vacuum distillation tower is regular packed tower, and the cat head 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 one-level flash tank 3 after one-level vapourizing furnace 2 is heated to 370 ℃, and the tank deck gas phase enters vacuum still 8 top distillation stages, and control tank deck gas phase guarantees that the one-level flash tank pressure is 10 kPa; Liquid phase enters secondary vapourizing furnace 4 at the bottom of the tank, enters two-stage flash tank 5 after heating to 390 ℃, and the two-stage flash gas phase enters vacuum still 8 middle part distillation stages, and control tank deck pressure is 6 kPa; The two-stage flash liquid phase enters three grades of vapourizing furnaces 6, enters 7, three grades of flash distillation gas phases of three grades of flash tanks after heating to 410 ℃ to enter vacuum still 8 bottom distillation stages, and controlling three grades of flashing pressures is 3 kPa, and three grades of flash distillation liquid phases enter vacuum still 8 flash zones.Each section feeding carries out underpressure distillation in vacuum still 8, 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 kept original vacuum furnace and vacuum distillation tower, and vacuum distillation tower internals and filler are transformed.Vacuum furnace is carried out capacity expansion revamping, and boiler tube and radiation chamber are transformed, and are transformed into three-in-one process furnace.Remove the transfer line low speed segment, newly-increased main equipment is one-level flash tank, two-stage flash tank, three grades of flash tanks.
Device decompression part working ability can improve 20%～50% after transforming, and plant energy consumption reduces by 10%～15%, and the vacuum residuum yield reduces by 2%～5%.
Comparative example 2
For the same set of crude oil atmospheric vacuum distillation device that relates among the embodiment 2, disclosed atmospheric vacuum distillation method with 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 for same set of atmospheric and vacuum distillation unit decompression part transformation situation, use the Data Comparison 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 | 550 | 550 |
| The charging kind | Kuwait Crude Oil＞350 ℃ part | Kuwait Crude Oil＞350 ℃ part | Kuwait Crude Oil＞350 ℃ part |
| Vacuum residuum yield/% (m) | 42.18 | 37.50 | 40.85 |
| The decompressed wax oil cut point/℃ | 540 | 605 | 565 |
| Main equipment is transformed 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 | Transform, enlarge load | Transform, enlarge load |
| Flash tank | Nothing | Newly-built 1 φ, 4800/ newly-built 2 φ 2200 | 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, vacuum residuum is the 37.50%(quality to the yield of decompression charging), the cut point of decompressed wax oil reaches 605 ℃.And press comparative example 2 described methods, vacuum residuum is 40.85% to the yield of combined feed total feed, the decompressed wax oil cut point is 565 ℃, although 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.
Calculate by 1000 ton/years of atmospheric and vacuum distillation unit, relief portion divides charging to be about 550 tons/hour, embodiment 2 reduces residual oil yields 3.35% than comparative example 2, comes in 250 yuan/tons of residual oil and mixed gatch price differences, year amounts to Renminbi: 550 * 3.35% * 250 * 8400=3869.25 ten thousand yuan.Add the part of device reduction energy consumption, the device economic benefit highly significant of obtaining.
Claims (12)
1. vacuum distillation method of sectional feeding that gradually gasifies comprises following content:
(1) oil at first enters the one-level vapourizing furnace at the bottom of the atmospheric tower that is come by air distillation, enters the one-level flash tank after being heated to 370～380 ℃, and one-level flash distillation gas phase enters vacuum still top distillation stage;
(2) one-level flash distillation liquid phase of coming from (1) enters the secondary vapourizing furnace, enters the two-stage flash tank after being heated to 390～400 ℃, and the two-stage flash gas phase enters vacuum still middle part distillation stage;
(3) the two-stage flash liquid phase of coming from step (2) enters three grades of vapourizing furnaces, enters three grades of flash tanks after being heated to 410～420 ℃, and three grades of flash distillation gas phases enter vacuum still bottom distillation stage;
(4) three grades of flash distillation liquid phases coming from step (3) enter the vacuum still flash zone;
(5) each section feeding carries out underpressure distillation in vacuum still, and the underpressure distillation column overhead connects pumped vacuum systems, from each lateral line withdrawal function product of tower, extracts vacuum residuum at the bottom of the tower out.
2. in accordance with the method for claim 1, it is characterized in that, described one-level flash tank gaseous phase outlet connects vacuum still top distillation stage, is 8 kPa～40 kPa by the control of the control valve on gaseous phase outlet one-level flash tank pressure.
3. in accordance with the method for claim 1, it is characterized in that, described one-level flash tank is vertical structure, and the one-level flash tank is slack tank or is provided with the equipment that is beneficial to gas-liquid separation and gasification in tank.
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 vacuum still middle part distillation stage, is 5 kPa～30 kPa by the control of the control valve on gaseous phase outlet two-stage flash pressure tank.
5. in accordance with the method for claim 1, it is characterized in that, described two-stage flash tank is vertical structure, and flash tank is slack tank or arranges in tank because the equipment of 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, is 2 kPa～20 kPa by three grades of flash tank pressure of the control of the control valve on the gaseous phase outlet.
7. in accordance with the method for claim 1, it is characterized in that, described three grades of flash tanks are vertical structure, and flash tank is slack tank or is provided with the equipment that is beneficial to gas-liquid separation and gasification in tank.
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 the wet type operation, little wet type or dry type operation; The 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 is carried out vacuum pumping, and the 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 independently arrange separately, and three-in-one process furnace perhaps is set, and three grades of chargings are separately positioned on radiation sections different in the three-in-one process furnace.
11. in accordance with the method for claim 1, it is characterized in that, described one-level flash tank, two-stage flash tank and three grades of flash tanks are independently arranged respectively, or arranged superposed.
12. in accordance with the method for claim 1, it is characterized in that, vapourizing furnaces at different levels and flash tank at different levels inner and/or between pipeline take hole enlargement to process.
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| CN107541245A (en) * | 2016-06-27 | 2018-01-05 | 中国石化工程建设有限公司 | A kind of hydrocracked product fractionating system and fractional method |
| EP3227407A4 (en) * | 2014-12-04 | 2018-07-18 | Uop Llc | Process for improved vacuum separations with high vaporization |
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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 |
| US20090261016A1 (en) * | 2006-07-31 | 2009-10-22 | Eni S.P.A. | Process for the total conversion of heavy feedstocks to distillates |
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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 |
| US20090261016A1 (en) * | 2006-07-31 | 2009-10-22 | Eni S.P.A. | Process for the total conversion of heavy feedstocks to distillates |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| EP3227407A4 (en) * | 2014-12-04 | 2018-07-18 | Uop Llc | Process for improved vacuum separations with high vaporization |
| CN107541245A (en) * | 2016-06-27 | 2018-01-05 | 中国石化工程建设有限公司 | A kind of hydrocracked product fractionating system and fractional method |
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