CN102443406B - Crude oil distillation method - Google Patents
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Abstract
The invention discloses a crude oil distillation method. A primary flash distillation tower is arranged between a normal pressure distillation tower and a pressure reduction furnace, a pressure reduction oil line from an outlet of the pressure reduction furnace to a pressure reduction distillation tower is omitted, a secondary flash distillation tower is arranged between the pressure reduction furnace and the pressure reduction distillation tower, tower bottom heavy oil of the normal pressure distillation tower, i.e. normal bottom oil enters the primary flash distillation tower after being mixed with cyclic pressure reduction slag oil, the tower top gas phase of the primary flash distillation tower is converted into a liquid phase to be used as products through heat exchange and condensing, bottom oil of the primary flash distillation tower enters the secondary flash distillation tower through being heated by the pressure reduction furnace, the tower top gas phase of the secondary flash distillation tower is converted into a liquid phase to be used as products through heat exchange and condensing, and bottom oil of the secondary flash distillation tower is introduced into a flash distillation section of the pressure reduction distillation tower for pressure reduction distillation. Compared with the prior art, the method has the advantages that on one hand, the yield of the pressure reduction slag oil is reduced, and the economic benefits of devices are improved; and on the other hand, the load of the pressure reduction furnace and the pressure reduction distillation tower is reduced, the device investment is saved, and the energy consumption of the devices is reduced.
Description
Technical field
The invention belongs to the refining of petroleum field, relate in particular to a kind of crude oil distillation method, more specifically say a kind of crude oil distillation method that improves extracting rate.
Technical background
Crude oil atmospheric vacuum distillation technique is the first operation of refining of petroleum, is crude oil to be divided into the component of different boiling range scopes by the method for distilling, to adapt to product and the downstream unit processing requirement to raw material.Conventional crude oil atmospheric vacuum distillation technique adopts the flow process of " two stove three towers " more: enter primary tower (or flashing tower) after crude oil upgrading, then enter atmospheric distillation tower through the atmospheric pressure kiln heating, at the bottom of atmospheric distillation tower, oil is delivered to vacuum still through the vacuum furnace heating by pressure-reducing line for oil-transferring, complete air distillation and underpressure distillation to crude oil, obtain to meet the product of specification of quality and the raw material of downstream unit.Usually use in total extracting rate and residual oil of device benzoline＜500 ℃ of cut content are as the indexs of weighing the device operation.
In recent years, the world petroleum demand amount increases year by year with the development of world economy.In world's crude resources supply, heavy oil and overweight oil supplying ratio progressively increase, lightweight oil, middle matter oil supplying ratio continuous decrease.Therefore, improve the light oil extracting rate in crude oil atmospheric vacuum distillation, 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, as the crude oil atmospheric vacuum distillation device of " tap " rationalize at utilization of resources maximization, energy utilization economized, running cost, the size investment optimizing, realize having very important status in the Sustainable development of China's oil chemical industry.
Therefore, the depth of cut that newly-built crude unit is had relatively high expectations, in vacuum residuum, cut content below 500 ℃ is less than 5% (quality), and is even lower; Many old atmospheric and vacuum distillation unit when requiring higher cut point, face process scale and can not meet the situation that treatment capacity requires and oil variety constantly changes, and 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 the decompression deep drawing of Atmospheric Vacuum Unit, energy-saving and cost-reducing, reduce cost, has made significant headway.Developing direction mainly concentrates on the following aspects: (1) optimizes vacuum system, improves the vacuum tightness of vacuum fractionation tower top; (2) adopt novel, high efficiency packing and direct contact type heat transfer type, reduce the tower total pressure drop, keep higher flash zone vacuum tightness; (3) improve the transfer line design, reduce transfer line pressure drop and temperature drop; (4) optimize washing section design and operation, strengthen the fractionation concept of washing section; (5) the efficient gas of development of new and liquid distributor; (6) adopt the crude distillation method etc. of strengthening.
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 and obtains product, and a part of gas phase is returned in tower; Method two is incoming mixture is lighting end, middle runnings, last running by boiling point height heating and separating, then enter in tower and carry out fractionation at different feed entrance points respectively, 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, but the lighting end of having separated from parallel feeding is again sent in tower and carried 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 still, is provided with a liquid seal device and top at the bottom of tower and separates, and have a vacuum system interface to be connected with the top vacuum system.This utility model separates the deep drawing section of the rectifying section of vacuum still and 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 meet the processing requirement of downstream unit to 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 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 US4717468 has delivered a kind of distil process that utilizes minimum energy consumption to obtain maximum recovery, by sneak into rare gas element in charging, thereby maximum amplitude ground reduces the residence time and the dividing potential drop of charging in process furnace, optimize the furnace outlet temperature by keeping the certain vaporization rate of crossing of charging, keep minimum furnace outlet temperature, thereby reduce energy consumption.The method can avoid maximum amplitude ground under the prerequisite of oil product cracking to add hot feed, and reduces its dividing potential drop and improve the feeding gas rate, is conducive to improve extracting rate.But injecting inert gas has increased load and the device running cost of overhead condensation and pumped vacuum systems, offsets it and reduces the process furnace energy expenditure, and the energy consumption level of its device still requires study.
Patent CN1287872A has delivered a kind of crude oil atmospheric vacuum distillation method with degree of depth stripping process, at vacuum still side washing tank in parallel, the feed zone of vacuum still 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 still subtracts three line dischargings and enter downward spray and the reverse mass-and heat-transfer of oil gas that makes progress by washing tank top after cooling, the top of vacuum still is returned in the tank deck oil gas discharging of washing tank, and at the bottom of tank, discharging is returned to vacuum still as washing oil.This technique makes the vacuum still 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 still stripping stage, with quality, subtracts preferably third fractional oil as washing oil, waits research on economic benefit.
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 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 at the bottom of atmospheric distillation tower, oil enters flashing tower, because the temperature of oil at the bottom of atmospheric distillation tower is relatively low, 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 still, be equivalent to vacuum still sectional feeding after flash distillation, not in the fractionation that fundamentally changes vacuum still.
In the last few years, replaced gradually high speed transfer line in the past with major diameter (more than generally diameter can reach 2m) low speed pressure-reducing line for oil-transferring technology in vacuum distillation apparatus, its objective is under the condition that guarantees vacuum still 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.(to guarantee liquid phase, certain separation time is arranged due to transfer line more than 15m must be adopted, be conducive to improve the quality of products and the vacuum still 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 crude oil distillation method, can obviously improve the extracting rate in vacuum distillation process, reduce plant energy consumption, and reduce plant investment.Technology of the present invention is rationally advanced, and energy consumption level is low, and facility investment is few, and the vacuum residuum yield is low, is used for the transformation of old device, has that the scrap build amount is few, investment is low, and the transformation duration is short, and the device income is the advantage such as quick obviously; The design and construction that is used for new device, have technique rationally advanced, and energy consumption level is low, and size investment is little, and equipment takes up an area the characteristics such as few.
Crude oil distillation method of the present invention comprises air distillation and underpressure distillation, the one-level flashing tower is set between atmospheric distillation tower and vacuum furnace, the cancellation vacuum furnace is exported to the pressure-reducing line for oil-transferring between vacuum still, the two-stage flash tower is set between vacuum furnace and vacuum still, heavy oil at the bottom of the atmospheric distillation tower tower (hereinafter referred to as normal end oil) is oil of the normal end and enter the one-level flashing tower after circulation vacuum residuum mixes, one-level flash distillation top gaseous phase (hereinafter referred to as a sudden strain of a muscle gas) namely a sudden strain of a muscle gas through heat exchange, be condensed into liquid phase as product; Oil at the bottom of the one-level flashing tower (hereinafter referred to as one, dodging oil) namely one dodges oil and is heated to 390 ℃～420 ℃ through vacuum furnace and enters the two-stage flash tower, two-stage flash top gaseous phase (hereinafter referred to as two, dodging gas) namely two sudden strain of a muscle gas through heat exchange, be condensed into liquid phase as product; The oily vacuum still flash zone of introducing of oil at the bottom of the two-stage flash tower (hereinafter referred to as two, dodging oil) i.e. two sudden strains of a muscle carries out underpressure distillation, product from the suitable cut of vacuum still lateral line withdrawal function, extract vacuum residuum part carrying device at the bottom of the vacuum still tower out, the part circulation is mixed into the one-level flashing tower with oil of the normal end.
In crude oil distillation method of the present invention, the amount that is mixed into the circulation vacuum residuum of one-level flashing tower with oil of the normal end determines according to factors such as the kind of the processing load of device, processing crude oil and institute's depths of cut that requires, is generally 20%～70% of discharging weight at the bottom of the vacuum still tower.
One-level flashing tower described in crude oil distillation method of the present invention is vertical structure, and 1～3 block of column plate can be set in tower.Oil of the normal end and circulation vacuum residuum are mixed into the one-level flashing tower, utilize oil of the normal end of high temperature circulation vacuum residuum heating, make wherein lighter cut flash off and no longer enter vacuum furnace and vacuum still at the one-level flashing tower.The tower top working pressure divides the gaseous phase outlet on flow container to control after dodging gas heat exchange condensation by one, and control pressure is 5kPa～60kPa, is preferably 5kPa～20kPa.
Second depressurized flashing tower described in crude oil distillation method of the present invention is vertical structure, is mainly used in vacuum furnace the work off one's feeling vent one's spleen gas-liquid separation of the very high logistics of rate and the vacuum flashing of lighting end, and 1～3 block of column plate can be set in tower.The tower top working pressure divides the gaseous phase outlet on flow container to control after dodging gas heat exchange condensation by two, and control pressure is 3kPa～10kPa.
In crude oil distillation method of the present invention, be condensed into the liquid phase caterpillar after a sudden strain of a muscle gas and the heat exchange of device domestic demand heated stream, perhaps with a certain of vacuum still or certain several cut mixing caterpillar.
In crude oil distillation method of the present invention, two dodge gas with enter vacuum furnace one dodge oily heat exchange or with device in be condensed into the liquid phase caterpillar after other logistics heat exchange, perhaps with a certain of vacuum still or certain several cut mixing caterpillar.
In crude oil distillation method of the present invention, the normal pressure part is identical with conventional atmospheric and vacuum distillation unit, the one-level flashing tower is set between atmospheric distillation tower before vacuum furnace and vacuum furnace, cancel vacuum furnace outlet pressure-reducing line for oil-transferring, the two-stage flash tower is set between vacuum furnace and vacuum still, two flashing towers are connected with vacuum furnace, vacuum still by pipeline.One-level flashing tower and two-stage flash tower have respectively Level Detection to control.
Described vacuum still can be the fuel type vacuum still, can be also the Lube Type vacuum still; The wet type operation be can adopt, little wet type or dry type operation also can be adopted; The sideline product number is not limit, and according to product needed and oil variety, determines.
In crude oil distillation method of the present invention, other technology contents, be technology contents well known to those skilled in the art as atmospheric pressure kiln, atmospheric distillation tower, vacuum furnace, vacuum still.
Vacuum still of the present invention, one-level flashing tower and two-stage flash tower can share a cover pumped vacuum systems, control device is set controls respectively vacuum tightness separately; Pumped vacuum systems vacuum pumping respectively separately also can be set; Also can pumped vacuum systems be set separately the one-level flashing tower, two-stage flash tower and vacuum still share a cover pumped vacuum systems.
Oil of the normal end flashes off lighting end in the one-level flashing tower, carry out further vacuum flashing at the two-stage flash tower again after the vacuum furnace heating and gasifying, greatly reduce vacuum still gas phase load, thereby reduced vacuum still and vacuumized load, although use separately pumped vacuum systems or share a cover pumped vacuum systems, actual do not increase device total vacuumize load.The vacuum pumping of vacuum still and vacuum flasher can be adopted the method and apparatus of this area routine.
Compared with prior art, the present invention has the following advantages:
1) the vacuum residuum freshening that partly circulates, significantly reduced the vacuum residuum yield, improved the yield of distillate.
2) often end oil and circulation vacuum residuum carry out flash distillation at the one-level flashing tower, wherein lighter cut is flashed off no longer enter vacuum furnace and vacuum still, take full advantage of on the one hand the entrained heat of vacuum residuum; Be conducive on the other hand reduce gas speed in the vacuum furnace boiler tube, reduce the load of vacuum furnace, reduce plant energy consumption; In addition, also reduce vacuum still gas phase load, be conducive to the capacity expansion revamping of old device.
3) the one-level flashing tower keeps higher vacuum tightness, makes the vacuum furnace internal pressure lower, and oil of normal end gasification point in vacuum furnace in advance, under the prerequisite that requires identical outlet of still vaporization rate, is conducive to reduce the vacuum furnace load, reduces plant energy consumption.
4) cancel pressure-reducing line for oil-transferring, the transfer line thermal walking of having avoided extra heavy pipe footpath, large pipe range transfer line low speed segment to cause, optimized the 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.
5) flow process of vacuum furnace-two-stage flash tower-vacuum still, shortened the technical process that oil of the normal end heats-enter vacuum still, greatly reduce process pressure drop and the calorific loss of pressure-reducing line for oil-transferring in prior art, make the vacuum furnace internal pressure lower, oil of normal end gasification point in vacuum furnace shifts to an earlier date, and the outlet of still vaporization rate is higher.
6) two sudden strain of a muscle oil enter separately vacuum still, and two dodge gas does not enter vacuum still, significantly reduces the processing load of vacuum still, has eliminated " bottleneck " of vacuum still treatment capacity, is conducive to the capacity expansion revamping of old device.Two dodge oil enters separately vacuum still, has reduced to a certain extent the required theoretical stage of vacuum still, can suitably reduce tower height and tower diameter, the economy system investment.Two dodge oil enters separately vacuum still, and two dodge gas does not enter vacuum still, has reduced the gas phase load of vacuum still, and full tower pressure drop is reduced, and is conducive to improve the decompression extracting rate, and has significantly reduced the condensation of underpressure distillation tower top and vacuumized load.Underpressure distillation less energy-consumption, high vacuum, the operation of high extracting rate have been realized.Effectively reduce the yield that is worth low vacuum residuum.
7) two sudden strain of a muscle oil enter separately vacuum still, and the Vapor Entrainment of having avoided the gas-liquid mixed charging to cause, guaranteed depressurised side line products quality.
8) utilize and dodge logistics in a large amount of sensible heat of top gas (dodges gas and two dodges gas) and Topography device, reduce plant energy consumption.
9) Technology of the present invention is rationally advanced, and energy consumption level is low, and facility investment is few, and the vacuum residuum yield is low,, for the transformation of old device, has that the scrap build amount is few, investment is low, and the transformation duration is short, and the device income is the advantage such as quick obviously; For the design and construction of new device, have technique rationally advanced, energy consumption level is low, and size investment is little, and equipment takes up an area the characteristics such as few.
Description of drawings
Fig. 1 is the schematic flow sheet of a kind of crude oil distillation method of the present invention.
Wherein 1 is atmospheric pressure kiln, and 2 is vacuum furnace, and 3 is atmospheric distillation tower, and 4 is vacuum still, 5 is the one-level flashing tower, and 6 is the two-stage flash tower, and 7 are crude oil after pre-treatment, and 8 is oil of the normal end, 9 is normal top product, and 10 is atmospheric distillate, and 11 is a sudden strain of a muscle oil, 12 is a sudden strain of a muscle gas, and 13 is two sudden strain of a muscle oil, and 14 is two sudden strain of a muscle gas, 15 is pumped vacuum systems, and 16 for dodging the top product, and 17 is vacuum distillate, 18 for effluxing vacuum residuum, and 19 are circulation vacuum residuum, and 20 is stripped vapor.
Embodiment
The present invention arranges one-level flashing tower 5 between vacuum furnace 2 and atmospheric distillation tower 3; Cancel pressure-reducing line for oil-transferring, two-stage flash tower 6 is set after vacuum furnace.
After pre-treatment, crude oil 7 is heated to 350 ℃～370 ℃ through atmospheric pressure kiln 1 and enters atmospheric distillation tower 3 and carry out air distillation.Tower top obtains normal top product 9, and lateral line withdrawal function atmospheric distillate 10 is extracted oil of the normal end 8 out at the bottom of tower.Oil 8 of the normal end and circulation vacuum residuum 19 enter one-level flashing tower 5 together.One dodges gas 12 by tower top cold logistics heat exchange in interchanger and device, enter again the sudden strain of a muscle top gas and divide the flow container separatory after condenser is cooling, at the bottom of dividing flow container, liquid phase is as dodging top product 16 liquid phase dischargings, and minute flow container gas phase connects pumped vacuum systems 15 control tower pressure on top surfaces at 5kPa～20kPa.One dodges oil 11 enters vacuum furnace 2 and heats to 390 ℃～420 ℃ and enter two-stage flash tower 6.Two dodge gas 14 by tower top cold logistics heat exchange in interchanger and device, enter again the sudden strain of a muscle top gas and divide the flow container separatory after condenser is cooling, at the bottom of dividing flow container, liquid phase is as dodging top product 16 liquid phase dischargings, and minute flow container gas phase connects pumped vacuum systems 15 control tower pressure on top surfaces at 3kPa～10kPa.Two dodge oil enters vacuum still 4 flash zones.Carry out underpressure distillation under the effect of stripped vapor 20 and underpressure distillation tower top pumped vacuum systems 15, obtain sideline product 17 dischargings in tower.Vacuum residuum pressurizes through pump, and a part is as effluxing vacuum residuum 18 dischargings; Another part returns to one-level flashing tower 5 as circulation vacuum residuum 19 and carries out freshening.
Vacuum residuum of the present invention partly loops back after vacuum furnace previous stage flashing tower and vacuum furnace crude oil distillation method and the equipment with the two-stage flash tower, improve crude oil atmospheric vacuum distillation technique, not only utilized the entrained heat of high temperature circulation vacuum residuum in vacuum flasher, lighter cut in oil of the normal end to be evaporated; And after utilizing vacuum furnace, the second depressurized flash distillation has improved the yield of benzoline, has reduced on the one hand the yield of vacuum residuum, improves the device economic benefit; Reduce on the other hand the load of vacuum furnace and vacuum still, saved facility investment, reduced plant energy consumption.Confirm through analog calculation, process the residual oil yield few 5～9 percentage points (quality) of the existing operational path of identical raw material processing method of the present invention, vacuum furnace load reduction 10%～15%.
The present invention in design or transformation, can consider one-level flashing tower and two-stage flash tower vertical pile, and the vacuum furnace position is high to be arranged between two towers, at the bottom of two-stage flash tower tower discharging as far as possible with horizontal pipe near the vacuum still flash zone.Thereby reduce the e-quipment and pipe pressure drop, save and take up an area.
The present invention is when start up, and normal pressure part atmospheric and vacuum distillation unit routinely goes into operation and carries out, and the decompression part first can be opened large vacuum furnace load, and heating is fed to 390 ℃～400 ℃, guarantees the underpressure distillation normal running.After going into operation normally, adjust gradually circulation vacuum residuum amount, adjust vacuum furnace simultaneously and vacuum still vacuumizes load, guarantee that the vacuum still operation is normal, after the reduced pressure distillate oil quality met the demands, depth of cut as requested added systemic circulation vacuum residuum amount, adjust simultaneously vacuum furnace and vacuum still operation, until stable equipment operation, operation are normal, qualified product, depth of cut meets the requirements.
Embodiment 1:
Method of the present invention is used for the design of certain newly-built Atmospheric Vacuum Unit.
Pre-treatment is identical with conventional atmospheric and vacuum distillation unit with the normal pressure part.The treatment capacity of relief portion separating device is 1,200,000 ton/years, and the decompression flow process comprises one-level flashing tower, vacuum furnace, two-stage flash tower, vacuum still.Vacuum still is regular packed tower, adopts the wet process operation, and tower bottom blowing vapour amount is 1% (quality) of tower charging, and the tower top working pressure is 1.315kPa, and full tower pressure drop is 600Pa～750Pa.
Oil of the normal end is fed into the decompression part with 150 tons/hour, enters the one-level flashing tower together with the circulation vacuum residuum of 370 ℃～390 ℃, and one-level flashing tower pressure on top surface is controlled to be 5kPa～20kPa.A sudden strain of a muscle gas accounts for oil of the normal end 16%～20% (quality) after one-level flashing tower adiabatic flash.One sudden strain of a muscle oil heats to 390 ℃～420 ℃ through vacuum furnace and enters the two-stage flash tower, and the two-stage flash tower top pressure is controlled to be 3kPa～10kPa.Two dodge oil introduces the vacuum still flash zone, from vacuum still lateral line withdrawal function product.Vacuum residuum from the bottom of tower through the pump discharging of pressurizeing, half goes out device, half loops back the one-level flashing tower.
One dodges gas and two dodges gas respectively through tower top heat exchange condensation separatory, and liquid phase is as product, and non-condensable gas is extracted out by vacuum pumping pump, keeps vacuum tightness in tower.
Following table has been listed employing the present invention (option A) and has been adopted the Data Comparison that carries out modeling effort at aspects such as decompression extracting rate, plant energy consumption, investments with the atmospheric vacuum distillation method of vacuum flasher and the patent CN101376068A of equipment (option b).
Option A and option b contrast situation
As seen from the table, although aspect facility investment the multiplex interchanger of option A, a flashing tower and two minutes flow containers, the tower diameter of vacuum still is less, investment reduces, corresponding column internals and filler investment also will reduce; Although the lower slightly and option A of option b vacuum furnace load, do not have recovered energy aspect plant energy consumption; Result in option A aspect the decompression extracting rate is better than option b far away, and the degree of deep drawing is also relatively high.The price difference of pressing 200 yuan/tons of vacuum residuum and vacuum distillates calculates, and option A 1 year (count 8000 hours) can be than scheme B increase economic benefit: 150 tons/hour * 8000 hours * (37.64-29.82) % * 200 yuan/ton=1876.8 ten thousand yuan.
Embodiment 2:
Method of the present invention is used for the capacity expansion revamping of certain Atmospheric Vacuum Unit, and pre-treatment is identical with conventional atmospheric and vacuum distillation unit with the normal pressure part, and the decompression part mainly comprises one-level flashing tower, vacuum furnace, two-stage flash tower, vacuum still.Vacuum still is regular packed tower, and the tower top working pressure is 1.315kPa, and full tower pressure drop is 600Pa～750Pa.
The oil of the normal end of 350 ℃ is fed into the decompression part with 150 tons/hour, enters the one-level flashing tower together with the circulation vacuum residuum of 380 ℃～390 ℃, and one-level flashing tower pressure on top surface is controlled to be 5kPa～20kPa.A sudden strain of a muscle gas accounts for oil of the normal end 16%～20% (quality) after one-level flashing tower adiabatic flash.One sudden strain of a muscle oil heats to 390 ℃～420 ℃ through vacuum furnace and enters the two-stage flash tower, and the two-stage flash tower top pressure is controlled to be 3kPa～10kPa.Two dodge oil introduces the vacuum still flash zone, from vacuum still lateral line withdrawal function product.Vacuum residuum from the bottom of tower through the pump discharging of pressurizeing, half goes out device, half loops back the one-level flashing tower.
One dodges gas and two dodges gas respectively through tower top heat exchange condensation separatory, and liquid phase is as product, and non-condensable gas is extracted out by vacuum pumping pump, keeps vacuum tightness in tower.
This device capacity expansion revamping relief portion is divided and is kept original vacuum furnace and vacuum still, and underpressure distillation column internals and filler are transformed.Newly-increased main equipment is each of one-level flashing tower, two-stage flash tower, each two, tower top interchanger, condenser, minute flow container.After transformation, device decompression part working ability can improve 20%～70%, and plant energy consumption reduces by 3%～5%, and the vacuum residuum yield reduces by 5～8 percentage points (quality).
Following table has been listed employing the present invention (option A) and has been adopted the Data Comparison that certain atmospheric and vacuum distillation unit decompression part transformation situation is carried out modeling effort with the atmospheric vacuum distillation method of vacuum flasher and the patent CN101376068A of equipment (option b).
Option A and option b comparable situation
As can be seen from the table, although it is more more than the newly-built equipment of scheme B to adopt option A to carry out capacity expansion revamping to old device, main equipment is few, and engineering amount of reform is little, thereby construction investment is less, and the transformation duration is short; Also obviously better on the device income.Option A has larger rectification advantage.
Claims (11)
1. crude oil distillation method, comprise air distillation and underpressure distillation, it is characterized in that: the one-level flashing tower is set between atmospheric distillation tower and vacuum furnace, the two-stage flash tower is set between vacuum furnace and vacuum still, at the bottom of the atmospheric distillation tower tower, heavy oil is normal end oil and enter the one-level flashing tower after circulation vacuum residuum mixes, one-level flash distillation top gaseous phase be a sudden strain of a muscle gas through heat exchange, be condensed into liquid phase as product; At the bottom of the one-level flashing tower, oil namely one dodges oil and is heated to 390 ℃～420 ℃ through vacuum furnace and enters the two-stage flash tower, the two-stage flash top gaseous phase namely two dodge gas through heat exchange, be condensed into liquid phase as product; At the bottom of the two-stage flash tower, the oily vacuum still flash zones of introducing of i.e. two sudden strains of a muscle of oil carry out underpressure distillation, product from the suitable cut of vacuum still lateral line withdrawal function, extract vacuum residuum part carrying device at the bottom of the vacuum still tower out, the part circulation is mixed into the one-level flashing tower with oil of the normal end.
2. it is characterized in that in accordance with the method for claim 1: the amount that is mixed into the circulation vacuum residuum of one-level flashing tower with oil of the normal end be at the bottom of the vacuum still tower discharging weight 20%～70%.
3. it is characterized in that in accordance with the method for claim 1: the pressure of one-level flashing tower is 5kPa～60kPa.
4. it is characterized in that in accordance with the method for claim 1: the pressure of two-stage flash tower is 3kPa～10kPa.
5. it is characterized in that in accordance with the method for claim 1: one-level flashing tower and two-stage flash tower are vertical structure.
6. it is characterized in that in accordance with the method for claim 5: one-level flashing tower and two-stage flash tower arrange 1～3 block of column plate.
7. in accordance with the method for claim 1, it is characterized in that: vacuum still is the fuel type vacuum still, or the Lube Type vacuum still.
8. in accordance with the method for claim 1, it is characterized in that: vacuum still, one-level flashing tower and two-stage flash tower share a cover pumped vacuum systems, control device is set controls respectively vacuum tightness separately.
9. it is characterized in that in accordance with the method for claim 1: the vacuum pumping respectively of vacuum still, one-level flashing tower and the setting of two-stage flash tower pumped vacuum systems separately.
10. in accordance with the method for claim 1, it is characterized in that: the one-level flashing tower arranges separately pumped vacuum systems, and two-stage flash tower and vacuum still share a cover pumped vacuum systems.
11. it is characterized in that in accordance with the method for claim 3: the pressure of one-level flashing tower is 5kPa～20kPa.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2010105093254A CN102443406B (en) | 2010-10-13 | 2010-10-13 | Crude oil distillation method |
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| CN2010105093254A CN102443406B (en) | 2010-10-13 | 2010-10-13 | Crude oil distillation method |
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| CN102443406A CN102443406A (en) | 2012-05-09 |
| CN102443406B true CN102443406B (en) | 2013-11-20 |
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| CN105950227A (en) * | 2016-07-01 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Treatment system and method for pyrolyzed oil gas |
| CN109613133B (en) * | 2018-12-19 | 2022-04-29 | 东营联合石化有限责任公司 | Method for measuring extractable rate of each fraction of residual oil in crude oil |
| CN113063695B (en) * | 2021-03-24 | 2023-02-28 | 中国石油化工股份有限公司 | Method and device for measuring gasification rate of heavy oil |
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