CN102311771B - Crude oil processing method - Google Patents
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Abstract
The invention discloses a crude oil processing method, which comprises normal-pressure distillation and reduced-pressure distillation, wherein the heavy oil at the bottom of a normal-pressure distillation tower, namely normal bottom oil, is mixed with part of circular reduced-pressure residual oil at the bottom of a reduced-pressure distillation tower, the mixture enters a flash tower, and a top gas phase, namely flash top gas, of the flash tower undergoes heat exchange and is condensed into a liquid phase to be discharged out of the device as a product; and bottom oil, namely flash bottom oil, of the flash tower, is heated in a reduced-pressure furnace to 390 to 420 DEG C, the heated bottom oil is intruded into a flash section of the reduced-pressure distillation tower from a reduced-pressure oil transfer line for reduced-pressure distillation, proper distillate product is drawn from a side line of the reduced-pressure distillation tower, part of reduced-pressure residual oil drawn out from the bottom of the reduced-pressure distillation tower is circulated, and another part of the reduced-pressure residual oil is discharged of the device. Compared with the prior art, the method can effectively improve the drawing rate of a reduced-pressure distillation process and can reduce the load of the reduced-pressure furnace and the reduced-pressure distillation tower at the same time.
Description
Technical field
The invention belongs to refining of petroleum field, relate in particular to a kind of crude oil processing method, more specifically say a kind of atmospheric vacuum distillation method that improves extracting rate.
Technical background
Crude oil atmospheric vacuum distillation technique is the first operation of refining of petroleum, is the component that by the method for distillation, crude oil is divided into different boiling range scopes, 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: after crude oil upgrading, enter primary tower (or flashing tower), then enter atmospheric distillation tower through atmospheric pressure kiln heating, at the bottom of atmospheric distillation tower, oil is delivered to vacuum still through vacuum furnace heating by pressure-reducing line for oil-transferring, complete air distillation and underpressure distillation to crude oil, obtain and meet the product of specification of quality and the raw material of downstream unit.Conventionally using 500 ℃ of cut content of < in device total extracting rate of benzoline and residual oil as the index of weighing device operation.
In recent years, 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 atmospheric and vacuum distillation unit energy consumption, improve 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, China's oil total quantity consumed will be broken 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, size investment optimizing, has very important status in the Sustainable development that realizes China's oil chemical industry.
Therefore, the depth of cut that newly-built CDU is had relatively high expectations, in vacuum residuum, 500 ℃ of following cut content are less than 5% (quality), even lower; Many old atmospheric and vacuum distillation unit, in 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 crude capacity.
For this reason, the decompression deep drawing of Chinese scholars to Atmospheric Vacuum Unit, energy-saving and cost-reducing, reduce investment and compare deep research, 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 tower total pressure drop, keep higher flash zone vacuum tightness; (3) improve transfer line design, reduce transfer line pressure drop and temperature drop; (4) optimize washing section design and operation, the fractionation concept of strengthening washing section; (5) the efficient gas of development of new and liquid distributor; (6) adopt strengthening crude distillation method 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 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 and in tower, 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 distillate quality.But plant investment and energy consumption are to a certain degree increased; Method two has been realized gently, last running sectional feeding, improve the operation of crude distillation separation column, be conducive to improve 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 and separates, and have a vacuum system interface to be connected with top vacuum system at the bottom of tower.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 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 complexity of this utility model simultaneously, 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 containing 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 furnace outlet temperature by maintaining the certain vaporization rate of crossing of charging, keep minimum furnace outlet temperature, thereby reduce energy consumption.The method can add to maximum amplitude hot feed under the prerequisite of avoiding oil product cracking, and reduces its dividing potential drop and improve 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 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 a 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 absorption oil that vacuum still subtracts three line dischargings and enter downward spray and the reverse mass-and heat-transfer of oil gas upwards 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 vacuum still stripping stage experience a steam stripped process of the degree of depth by setting up washing tank, is conducive to improve decompression extracting rate.But the method is just optimized improvement to vacuum still stripping stage, subtract preferably third fractional oil as washing oil by quality, in economic benefit, wait research.
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 enters 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 raising treatment capacity, improves extracting rate, reduces the object 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 stokehold flashing tower is relatively not high, the effect of flashing tower flash distillation gasification is limited, and 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.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of crude oil processing method, can obviously improve the extracting rate in vacuum distillation process, reduce plant energy consumption.Technology of the present invention is rationally advanced, and energy consumption level is low, and vacuum residuum yield is low, for the transformation of old device, have scrap build amount few, invest lowly, the transformation duration is short, device income is the advantage such as quick obviously; For the design and construction of new device, there is technique rationally advanced, the feature such as energy consumption level is low.
Crude oil processing method of the present invention comprises air distillation and underpressure distillation, to be normal end oil be mixed into flashing tower with vacuum residuum at the bottom of the vacuum still tower of part circulation with heavy oil at the bottom of atmospheric distillation tower tower (hereinafter referred to as oil of the normal end), flash distillation top gaseous phase (hereinafter referred to as dodging top gas) dodge top gas through heat exchange, be condensed into liquid phase as product discharger; Oil at the bottom of flashing tower (hereinafter referred to as dodging end oil) dodges end oil and is heated to 390 ℃～420 ℃ through vacuum furnace, introduce vacuum still flash zone by pressure-reducing line for oil-transferring and carry out underpressure distillation, from the product of the suitable cut of vacuum still lateral line withdrawal function, at the bottom of vacuum still tower, extract the circulation of vacuum residuum part out, part discharger.
In crude oil processing method of the present invention, kind and institute's depth of cut that requires etc. that crude oil was loaded, processed to the amount of the vacuum residuum of part circulation according to the processing of device are because usually determining, be generally 20%～70% of discharging weight at the bottom of vacuum still tower, preferably 40%～50%.
Flashing tower described in crude oil processing method of the present invention is vertical structure, is mainly used in the vacuum flashing of gas-liquid separation and lighting end, and 1～3 block of column plate can be set in flashing tower.Flash distillation tower top working pressure is by dodging the gaseous phase outlet control on point flow container after top gas condensation, and control pressure is than the high 2kPa～60kPa of vacuum still tower top pressure, preferred high 2kPa～15kPa.
In crude oil processing method of the present invention, be condensed into liquid phase caterpillar after dodging top gas and the heat exchange of device domestic demand heated stream, or with a certain of vacuum still or certain several fractions mixing caterpillar.
Described vacuum still can be fuel type vacuum still, can be also Lube Type vacuum still; Wet type operation be can adopt, micro-wet type or dry type operation also can be adopted; Sideline product number is not limit, and determines according to product needed and oil variety.
In crude oil processing method of the present invention, other technology contents, if atmospheric pressure kiln, atmospheric distillation tower, vacuum furnace, vacuum still are technology contents well known to those skilled in the art.
Vacuum still of the present invention and vacuum flasher can share a set of pumped vacuum systems, control device is set controls respectively the vacuum tightness of vacuum still and vacuum flasher; Two cover pumped vacuum systems also can be set, the vacuum pumping respectively of vacuum still and vacuum flasher.The vacuum degree control of vacuum flasher is arranged on dodges on top gas condenser knockout drum afterwards.In oil of the normal end, lighting end flashes off in vacuum flasher, reduced vacuum still and vacuumized load, although by two cover pumped vacuum systems or a set of pumped vacuum systems for two equipment, reality do not increase device total vacuumize load.The vacuum pumping of vacuum still and vacuum flasher can adopt the method and apparatus of this area routine.
Compared with prior art, the present invention has the following advantages:
1) vacuum residuum part circulation freshening, can significantly reduce vacuum residuum yield, improves the extracting rate of distillate, improves the economy of device.
2) before vacuum furnace, flashing tower is set, oil of the normal end and circulation residual oil are mixed into vacuum flasher, utilize high-temperature pressure-reduction residual oil to heat oil of the normal end, make wherein lighter cut flash off and no longer enter vacuum furnace and vacuum still through vacuum flasher, take full advantage of on the one hand the entrained heat of vacuum residuum; Be conducive on the other hand reduce the load of vacuum furnace, reduce plant energy consumption; In addition, vacuum still gas phase load reduces, and tower diameter can reduce, and is conducive to the capacity expansion revamping of old device.Meanwhile, the minimizing of lighting end is also conducive to reduce transfer line pressure drop.
3) before vacuum furnace, vacuum flasher keeps suitable vacuum tightness, makes vacuum furnace internal pressure lower, and oil of normal end gasification point in vacuum furnace in advance, under the prerequisite that requires identical heater outlet temperature, is conducive to reduce vacuum furnace load, reduces plant energy consumption.
4) utilize in sudden strain of a muscle top gas and device and need heated stream to carry out heat exchange, reduce plant energy consumption.
5) Technology of the present invention is rationally advanced, and energy consumption level is low, and facility investment is few, and vacuum residuum yield is low, for the transformation of old device, have scrap build amount few, invest lowly, the transformation duration is short, device income is the advantage such as quick obviously; For the design and construction of new device, there is technique rationally advanced, energy consumption level is low, and size investment is little, and equipment takes up an area the features such as few.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of a kind of crude oil processing method of the present invention.
Wherein 1 is crude oil after pre-treatment, and 2 is vacuum furnace, and 3 is vacuum still, and 4 is vacuum flasher, 5 is atmospheric distillation tower, and 6 is oil of the normal end, and 7 is stripped vapor, and 8 for dodging top product, 9 is pumped vacuum systems, and 10 is vacuum distillate, and 11 is normal top product, 12 is vacuum residuum, and 13 for dodging end oil, and 14 for dodging top gas interchanger, 15 for dodging top gas condenser, and 16 is atmospheric distillate, and 17 divide flow container for dodging top gas, 18 is circulation vacuum residuum, and 19 is atmospheric pressure kiln, and 20 for dodging top gas.
Embodiment
The inventive method arranges a vacuum flasher 4 between vacuum furnace 2 and atmospheric distillation tower 5.After pre-treatment, crude oil 1 is heated to 350 ℃～370 ℃ through atmospheric pressure kiln 19 and enters atmospheric distillation tower 5 and carry out air distillation.Tower top obtains normal top product 11, and lateral line withdrawal function atmospheric distillate 16 is extracted oil of the normal end 6 out at the bottom of tower.Oil of the normal end 6 enters vacuum flasher 4 together with circulation vacuum residuum 18.Dodge top gas 20 by tank deck cold logistics heat exchange in dodging top gas interchanger 14 and installing, after sudden strain of a muscle top gas condenser 15 is cooling, entering sudden strain of a muscle top gas again divides flow container 17 separatory, at the bottom of dividing flow container, liquid phase is as dodging top product 8 liquid phase dischargings, and point flow container gas phase connects a pumped vacuum systems 9 and controls vacuum flashing pressure tower at 5kPa～20kPa.Sudden strain of a muscle end oil 13 enters vacuum furnace 2 and heats to 390 ℃～420 ℃, enters vacuum still 3 flash zones through pressure-reducing line for oil-transferring.Under the effect of stripped vapor 7 and underpressure distillation tower top pumped vacuum systems 9, carry out underpressure distillation, obtain sideline product 10 dischargings in tower.Vacuum residuum pressurizes through pump, and a part is as vacuum residuum 12 dischargings; Another part returns to vacuum flasher 4 as circulation residual oil 18 and carries out freshening.
Vacuum residuum part of the present invention loops back crude oil processing method and the equipment of the front flashing tower of vacuum furnace, improve crude oil atmospheric vacuum distillation technique, made full use of the entrained heat of high temperature circulation vacuum residuum and in vacuum flasher, lighter cut in oil of the normal end is evaporated.Not only reduce the yield of vacuum residuum, and reduced the load of vacuum furnace.Confirm through analog calculation, process the residual oil yield few 5～8 percentage points (quality) of the more existing operational path of identical raw material processing method of the present invention, vacuum furnace load reduction 10%～15%.
The present invention, in the time of start up, can open large vacuum furnace load, and heating is fed to 390 ℃～400 ℃, guarantees underpressure distillation normal running.After going into operation normally, make full use of lighting end in high temperature circulation residual oil evaporation gasification oil of the normal end, reduce the load of vacuum furnace, implement device is energy-conservation.
Embodiment 1:
Method of the present invention is for the design of certain newly-built Atmospheric Vacuum Unit.
Pre-treatment is identical with conventional atmospheric and vacuum distillation unit with normal pressure part.The treatment capacity of relief portion separating device is 1,200,000 tons/year.Vacuum still is regular packed tower, adopts wet process operation, and tower bottom blowing vapour amount is 1% (quality) of tower charging, and tower top working pressure is 1.315kPa, and full tower pressure drop is 600Pa～750Pa.
Oil of the normal end is fed into decompression part with 150 tons/hour, enters vacuum flasher with together with the circulation residual oil of 370 ℃～390 ℃, and the control of flashing tower pressure on top surface is 5kPa～20kPa.After vacuum flasher adiabatic flash, dodge top gas and account for oil of the normal end 16%～20% (quality).Sudden strain of a muscle end oil heats to 392 ℃～420 ℃ through vacuum furnace and enters 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.A part goes out device, a part (account for underpressure distillation tower bottom flow go out thing weight 50%) loop back vacuum flasher.Tower top oil gas is cooling through condenser, 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 and a point flow container, vacuum still tower diameter 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, loads higher than option A with vacuumizing at overhead condensation, and there is no recovered energy aspect plant energy consumption; Result in option A aspect 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/ton of vacuum residuum and vacuum distillates calculates, and option A 1 year (counting 8000 hours) can increase by 1682.4 ten thousand yuan of economic benefits than option b.
Embodiment 2:
Method of the present invention is for the capacity expansion revamping of certain Atmospheric Vacuum Unit, and pre-treatment is identical with conventional atmospheric and vacuum distillation unit with normal pressure part, and decompression part mainly comprises vacuum flasher, vacuum furnace, vacuum still.
Filling structured packing in vacuum still, tower top working pressure is 1.315kPa, full tower pressure drop is 600Pa～750Pa.
Oil of the normal end is fed into decompression part with 150 tons/hour, enters vacuum flasher with together with the circulation residual oil of 370 ℃～390 ℃, and the control of flashing tower pressure on top surface is 5kPa～20kPa.After vacuum flasher adiabatic flash, dodge top gas and account for oil of the normal end 16%～20% (quality).Sudden strain of a muscle end oil heats to 392 ℃～420 ℃ through vacuum furnace and enters 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.A part goes out device, and a part loops back vacuum flasher.Tower top oil gas is cooling through condenser, 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 retained original vacuum furnace and vacuum still, and underpressure distillation column internals and filler are transformed.Newly-increased main equipment is vacuum flasher, sudden strain of a muscle top gas interchanger.After transformation, device decompression part working ability can improve 20%～50% (quality), and plant energy consumption reduces by 3%～5%, and 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 to 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, adopt option A to carry out capacity expansion revamping to old device more less than the newly-built equipment of option b, make especially main equipment few, engineering amount of reform is little, thereby construction investment is less, and the transformation duration is short; Also obviously better in device income.Option A has larger rectification advantage.
Claims (11)
1. a crude oil processing method, comprise air distillation and underpressure distillation, it is characterized in that: at the bottom of atmospheric distillation tower tower, to be normal end oil be mixed into flashing tower with vacuum residuum at the bottom of the vacuum still tower of part circulation with heavy oil, flash distillation top gaseous phase dodge top gas through heat exchange, be condensed into liquid phase as product discharger; At the bottom of flashing tower, oil dodge end oil and be heated to 390 ℃～420 ℃ through vacuum furnace, introduce vacuum still flash zone by pressure-reducing line for oil-transferring and carry out underpressure distillation, from the product of the suitable cut of vacuum still lateral line withdrawal function, at the bottom of vacuum still tower, extract the circulation of vacuum residuum part out, part discharger.
2. it is characterized in that in accordance with the method for claim 1: the amount of the vacuum residuum of part circulation be at the bottom of vacuum still tower discharging weight 20%～70%.
3. it is characterized in that in accordance with the method for claim 1: the amount of the vacuum residuum of part circulation be at the bottom of vacuum still tower discharging weight 40%～50%.
4. it is characterized in that in accordance with the method for claim 1: flashing tower is vertical structure.
5. according to the method described in claim 1 or 4, it is characterized in that: 1～3 block of column plate is set in flashing tower.
6. ask the method described in 1 or 4 according to right, it is characterized in that: flash distillation tower top working pressure divides the gaseous phase outlet control on flow container after dodging top gas condensation, and control pressure is than the high 2kPa～60kPa of vacuum still tower top pressure.
7. it is characterized in that in accordance with the method for claim 1: after dodging top gas and installing the heat exchange of domestic demand heated stream, be condensed into liquid phase caterpillar.
8. in accordance with the method for claim 1, it is characterized in that: vacuum still is fuel type vacuum still, or Lube Type vacuum still.
9. in accordance with the method for claim 1, it is characterized in that: vacuum distillation apparatus arranges a set of pumped vacuum systems, vacuum still and flashing tower share a set of pumped vacuum systems vacuum pumping.
10. in accordance with the method for claim 1, it is characterized in that: two cover pumped vacuum systems are set, the vacuum pumping respectively of vacuum still and flashing tower.
11. 1 kinds of crude oil processing methods, comprise air distillation and underpressure distillation, it is characterized in that: at the bottom of atmospheric distillation tower tower, to be normal end oil be mixed into flashing tower with vacuum residuum at the bottom of the vacuum still tower of part circulation with heavy oil, after flash distillation top gaseous phase dodges top gas and install the heat exchange of domestic demand heated stream, be condensed into after liquid phase and a certain of vacuum still or certain several fractions mixing caterpillar; At the bottom of flashing tower, oil dodge end oil and be heated to 390 ℃～420 ℃ through vacuum furnace, introduce vacuum still flash zone by pressure-reducing line for oil-transferring and carry out underpressure distillation, from the product of the suitable cut of vacuum still lateral line withdrawal function, at the bottom of vacuum still tower, extract the circulation of vacuum residuum part out, part discharger.
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| CN103242896B (en) * | 2012-02-06 | 2015-02-18 | 中国石油化工股份有限公司 | Reduced pressure distillation method with low energy consumption and deep total distillation rate |
| CN103540354B (en) * | 2012-07-09 | 2015-11-25 | 中国石油化工集团公司 | A kind of combination heavy oil treatment processes |
| CN103540357B (en) * | 2012-07-09 | 2015-04-08 | 中国石油化工集团公司 | Heavy oil treatment process |
| CN106085582B (en) * | 2016-08-15 | 2018-09-28 | 河南东和环保科技股份有限公司 | A kind of device using producing base oil by regenerating waste lubricating 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 |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1344780A (en) * | 2000-09-25 | 2002-04-17 | 王仲华 | Normal pressure pregasifying and several section amterial feeding process of crude oil distiller |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101624535A (en) * | 2009-08-03 | 2010-01-13 | 中海石油炼化有限责任公司 | Atmospheric and vacuum distillation device and atmospheric and vacuum distillation method of high acid-content crude oil |
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| JP3021373B2 (en) * | 1996-12-05 | 2000-03-15 | 三井造船株式会社 | Topping method |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1344780A (en) * | 2000-09-25 | 2002-04-17 | 王仲华 | Normal pressure pregasifying and several section amterial feeding process of crude oil distiller |
| CN101376068A (en) * | 2008-09-17 | 2009-03-04 | 天津大学 | Atmospheric vacuum distillation method and apparatus with vacuum flash vaporizer |
| CN101624535A (en) * | 2009-08-03 | 2010-01-13 | 中海石油炼化有限责任公司 | Atmospheric and vacuum distillation device and atmospheric and vacuum distillation method of high acid-content crude oil |
Non-Patent Citations (1)
| Title |
|---|
| JP特开平10-158664A 1998.06.16 |
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