CN101838543A

CN101838543A - Apparatus for refining of opportunity crude and method for refining

Info

Publication number: CN101838543A
Application number: CN200910142956A
Authority: CN
Inventors: 沈成元
Original assignee: JAEWON IND CO Ltd
Current assignee: JAEWON IND CO Ltd
Priority date: 2009-03-17
Filing date: 2009-05-15
Publication date: 2010-09-22
Anticipated expiration: 2029-05-15
Also published as: JP2010215882A; SG165216A1; MY159050A; KR100933308B1; JP5014379B2; CN101838543B

Abstract

The present invention discloses an apparatus for refining of opportunity crude and a method for refining. The apparatus and method are used for producing low-cost fuel with opportunity crude thereby remarkably reducing the production cost. The apparatus for refining of opportunity crude comprises the following components: an opportunity crude storage tank; a vacuum distillation tower which is used for receiving the opportunity crude stored in the storage tank and eliminating the low-viscosity fraction in vacuum while the bunker C fuel which has a flash point higher than 70 DEG C and is used as kerosene is produced; and a storage part which is used for receiving the bunker C fuel which is produced from the vacuum distillation tower.

Description

The equipment and the method for refining thereof that are used for refining of opportunity crude

CROSS-REFERENCE TO RELATED APPLICATIONS

The application requires the right of priority of the 10-2009-0022541 korean patent application submitted on March 17th, 2009, and its full content is hereby expressly incorporated by reference.

Technical field

The present invention relates to a kind of crude refining equipment and method for refining thereof, more specifically, relate to a kind of equipment that is used for refining of opportunity crude and method for refining thereof with prevent during refining to the corrosion of equipment and will be at a low price optionally raw material make heavy fuel oil (heavy fuel oil).

Background technology

Opportunity crude (opportunity crude) is meant the oil that has with visibly different constituent of conventional crude and physical property, and opportunity crude is exploitation and production in a small amount normally.According to the production area, can refer to opportunity crude by different titles.For example, although the characteristic of the characteristic of Dar Blend crude oil and Doba Blend crude oil is basic identical, the opportunity crude of producing in the Sudan (Sudan) is called Dar Blend, and the opportunity crude of producing in Chad (Chad) is called Doba Blend.

As mentioned above, for the C level oil fuel peculiar to vessel (bunker fuel C-oil) that satisfies by producing from above-mentioned opportunity crude refining is higher than 70 ℃ flash-point, it is that 3% to 4% low viscous composition may be necessary that removal is present in concentration in the opportunity crude, and wherein this flash-point is the standard that is used to define C level oil fuel peculiar to vessel.

In order to remove such 3% to 4% the low viscosity composition that comprises in opportunity crude, most of oil refinery companies use corrosives to refine processing usually under condition of normal pressure, cause the heavy corrosion to refining equipment.

Corrosives may comprise the high salt concentration such as calcium chloride (calcium chloride), magnesium chloride (magnesium chloride) etc., these high salt concentrations at high temperature decompose generation hydrochloric acid (hydrochloric acid), cause the heavy corrosion to refining equipment.In addition, acid fraction (such as naphthenic acid (naphthenic acid) cut, its content uses TAN (total acid value) (total acid number) to represent usually) may cause the corrosion to the reboiler (reboiler) that is provided with in the distillation tower (distillation column).

If the content of acid fraction increases, crude oil may have very high viscosity.Than conventional crude, because opportunity crude has very high TAN value, so opportunity crude at room temperature is solid-state.

Opportunity crude has and is less than 0.1% sulphur content (sulfur content).Therefore, the etching problem that is caused by sulphur content is not so important for oil refiner (oil refiner).

Prepare the crude oil that uses by oil refiner by in conventional crude, adding a spot of opportunity crude, the amount of opportunity crude is corresponding to (correspond to) desalting plant (desalting device) (electric desalting apparatus normally, for example, the capacity demineralizer of making by the NATCO group (desalter)).Crude oil through desalting plant is heated to 360 ℃ to 380 ℃ in stove (furnace), under normal pressure, be injected into distillation tower to produce petroleum naphtha (naphtha), gasoline (gasoline), kerosene (kerosene), diesel oil (diesel) etc., and then further passing through handling under the vacuum in the treating processes in the generation high boiling substance, to reclaim (recover) diesel oil residue.

The content of the salt that has been comprised in will the crude oil through desalting plant controls to and is less than per thousand barrel of 1.5 part (1.5 parts per thousand barrels) (PTB).Yet, because advanced in recent years desalting technology, standard at the salts contg of the outlet of desalting plant is reduced to about 0.15PTB to prevent the corrosion to refining equipment, and the corrosion that the prevents refining equipment minimization device frequency of repairing (plant repair) and/or safeguarding conversely, thereby boost productivity.

Simultaneously, the temperature of the decomposition of magnesium chloride is approximately 200 ℃, and produces hydrogen chloride gas during decomposing.For the desalination operation, need some such as the chemical preparations that is used for pH control and the additive of emulsifying agent (emulsifying agents).In the process that refinery is handled, use various corrosion inhibitors such as phosphoric acid ester to prevent the corrosion that causes by acid fraction to reboiler.

As for using opportunity crude optional fuel is directly made C level oil fuel peculiar to vessel, opportunity crude has the TAN of high content of salt and increase, thereby the viscosity (at 60 ℃) that often shows about 170cP, this viscosity have surpassed desired viscosity (at the 60 ℃) 5cP that is used for the desalination operation.Therefore, opportunity crude may not be applied to desalting treatment.

Such desalting treatment is also being brought extra problem aspect operation and installation (installation) cost.Therefore, need be to for preventing to corrode the operational condition that improved and/or to the Research on development and the investigation of optional processing.In addition, based on such research and investigation, still exist being used for producing usually needs as the technology of the improvement C level peculiar to vessel oil fuel of fuel.Consider the problem aspect fuel reservoir and/or conveying,, also can in fuel, add extra flow point toughener to provide some user partials required low-viscosity fuel even when fuel has the flash-point of expectation.

Fig. 1 shows the schematic construction in order to traditional crude refining method of the method for explanation refining of opportunity crude.

As shown in fig. 1, traditional crude refining equipment comprises crude oil storage tank 10, demineralizer 20, stove 30, atmospheric distillation tower (atmospheric distillation column) 40 and vacuum tower 50.

Crude oil storage tank 10 comprises crude oil, and wherein, crude oil can comprise various dissolved solidss (dissolved solids), such as salt, ferric oxide, sand etc.

Demineralizer 20 receives the crude oil that stores from crude oil storage tank 10 and is included in salt cut the crude oil with removal, and this salt cut is preheated to 170 ℃ to 260 ℃.Here, demineralizer 20 can also comprise a spot of opportunity crude, such as other additives of chemical preparations that is used for pH control and/or emulsifying agent and/or such as the various corrosion inhibitors of phosphoric acid ester, corrosion inhibitor is used to prevent the corrosion to equipment that caused by acid fraction.

Stove 30 will extremely carry out 360 ℃ to 380 ℃ required temperature of air distillation to this mixture through the crude oil of demineralizer 20 and the mixture heating up of opportunity crude.Herein, temperature can change with the distillation of crude oil or the type of final product.

Based on the difference of boiling point, atmospheric distillation tower 40 is to be the equipment of LPG, petroleum naphtha, kerosene, diesel oil, C level fuel wet goods peculiar to vessel with crude separation.Constituent in the crude oil can separate based on these compositions have intrinsic (inherent) evaporation characteristic under different pressure and temperatures principle.Briefly, distillation tower 40 can be separated into separately composition with the blended distillment based on the internal temperature of tower and pressure, and internal temperature and pressure can be classified according to the height of tower.Because distillation tower is approaching to carry out work under the non-pressurized usual pressure, thereby distillation tower often is known as " atmospheric distillation tower ".

In atmospheric distillation tower 40, have about 30 to 40 tower trays (tray) usually, oily stream in tower can become to assign to separate with steam by the contact fluid composition, wherein, fluid composition is in upper strata tower tray condensation and flow downward, and the steam composition is in lower floor's tower tray evaporation and upwards flow.

Atmospheric distillation tower 40 can be removed the low viscosity cut that is included in about 3% to 4% in the opportunity crude.

Vacuum tower 50 is worked under vacuum, with when producing high boiling point oil, reclaims via the remaining diesel oil residue in the atmospheric distillation tower 40 isolating oil.

For the refining equipment of said structure, opportunity crude is added in the conventional oil with a small amount of of the capacity that satisfies demineralizer 20.Be injected in the atmospheric distillation tower 40 with preparation petroleum naphtha, gasoline, diesel oil, kerosene etc. via stove 30 through the oil of demineralizer 20, and vacuum tower 50 is worked under vacuum and can be produced high boiling substance.During such vacuum work, also can produce the C level oil fuel peculiar to vessel that acts as a fuel widely and use.

Yet, only use the oil Refining Technologies of opportunity crude still flourishing inadequately.

Especially, when using opportunity crude directly with optional feedstock production to be C level oil fuel peculiar to vessel, the opportunity crude with TAN of aforesaid high content of salt and increase can not be applied in the desalting treatment.Desalting treatment has run into such as operation and/or the high extra problem of installation costs.

The present invention is directed to the above-mentioned problem that solves about routine techniques, an object of the present invention is to provide a kind of equipment that is used for refining of opportunity crude, this equipment can detect the suitable operational condition that does not influence equipment corrosion, and can under the vacuum operating condition, not need desalting plant (preventing corrosion) and refining of opportunity crude to equipment, so that produce C level oil fuel peculiar to vessel, thereby produce low-cost fuel and help to reduce cost.

Another object of the present invention provides and a kind ofly is used to use above-mentioned refining equipment to come the method for refining of opportunity crude.

Summary of the invention

In order to realize such purpose and other advantage and, to provide a kind of equipment that is used for refining of opportunity crude, comprising: the opportunity crude storage tank according to purpose of the present invention; Vacuum tower is used for receiving the opportunity crude from storage tank stores, then, when production has the C level oil fuel peculiar to vessel as kerosene of the flash-point that is higher than 70 ℃, removes the low viscosity cut under vacuum; And reservoir, this reservoir is used for receiving and storing the C level oil fuel peculiar to vessel that produces from vacuum tower.

The present invention also provides a kind of method that is used for refining of opportunity crude, and this method comprises: receive opportunity crude from storage tank, and when production has the C level oil fuel peculiar to vessel of the flash-point that is higher than 70 ℃, remove the low viscosity cut under vacuum; Cooling low viscosity cut is to produce the low viscosity condensate oil; Storage has the C level oil fuel peculiar to vessel of the flash-point that is higher than 70 ℃; And the C level oil fuel peculiar to vessel and the flow point (condensation point, pour point) that will have the flash-point that is higher than 70 ℃ strengthen the oil mixing so that produce low viscosity C level peculiar to vessel oil fuel.

Be understandable that, above-mentioned describe, in general terms of the present invention and following specific descriptions all are exemplary with illustrative, be in order clearly to understand purpose of the present invention, feature and other advantage, and aim to provide desired further explanation of the present invention.

Description of drawings

In order to provide further understanding of the present invention, the application comprises accompanying drawing, and accompanying drawing is incorporated into the application and constitutes the application's a part.Accompanying drawing shows the specific embodiment of the present invention and is used to set forth principle of the present invention together with specification sheets.In the accompanying drawings:

Fig. 1 shows the schematic configuration diagram of the method for refining of opportunity crude in the oily refining equipment of routine.

Fig. 2 shows the schematic configuration diagram that is used for the equipment of refining of opportunity crude according to of the present invention.

Fig. 3 and Fig. 4 show the graphic representation of the corrosion detection of using TAN.Wherein, Fig. 4 comprises the typical burn into temperature comparison (with respect to the corrosion per-cent of low-sulfur Texas crude oil (sweet Texas crude)) of the crude oil of naphthenic acid.

Fig. 5 shows the schema that is used for the method for refining of opportunity crude according to of the present invention.

Embodiment

Hereinafter, other purposes of the present invention, feature and advantage will be by becoming more apparent in conjunction with exemplary embodiment and following embodiment in conjunction with the accompanying drawings.

Fig. 2 shows the schematic diagram that is used for the equipment of refining of opportunity crude according to of the present invention.

As shown in Figure 2, refining equipment of the present invention comprises opportunity crude storage tank 110, heat exchanger 120, vacuum tower 130, reboiler 140, water cooler 150 and reservoir 160.

Opportunity crude storage tank 110 stores opportunity crude, wherein, opportunity crude can comprise the removed various compositions of needs for the standard flash-point that satisfies the C level oil fuel peculiar to vessel that is higher than 70 ℃, for example, has low viscous 3% to 4% composition such as butane, pentane, pentamethylene, methylpentane (methylpentane), dimethylbutane, dimethylpentane, normal hexane etc. less than 70 ℃.

Opportunity crude can comprise the typical salt (for example, calcium chloride, magnesium chloride etc.) that at high temperature decomposes generation hydrochloric acid, causes the heavy corrosion to equipment.Opportunity crude can also have a large amount of acid fraction (representing by TAN usually) such as naphthenic acid, may cause the corrosion to the reboiler in the distillation tower.

The flow point of opportunity crude is about 38 ℃, and opportunity crude can be placed and be in about 50 ℃ storage tank, and in about 50 ℃ of temperature, opportunity crude has the viscosity of about 250cP.

Under the temperature more than the flow point, the viscosity of opportunity crude is lower than C level fuel oil viscosity peculiar to vessel.Yet at room temperature, because the content of acid fraction, opportunity crude may become hard solid, as chocolate.Therefore, be used for that opportunity crude can be had reboiler 140 from the pipeline that crude oil storage tank 110 is transported to (feeding) vacuum tower 130, to prevent that opportunity crude from hardening in pipeline, reboiler 140 is equipped with a steam sleeve (steam jacket) or steam tracing device (steam tracing device).

Briefly, heat exchanger 120 and reboiler 140 are installed between crude oil storage tank 110 and the vacuum tower 130, and heat exchanger 120 is used between product and raw material exchanging heat reclaiming (recover) heat, and reboiler 140 provides thermal source to distillation tower.

Following table 1 shows the composition that comprises in opportunity crude true boiling-point (true boiling point) (TBP) and the relation between the output (volume %), table 2 shows the representative physical properties of opportunity crude.

Table 1

Consider natural characteristics, than conventional crude, opportunity crude partly has very little distribution for gasoline and kerosene.Table 1 shows the result who uses the TBP test of 15 layers of tower tray glass mould (15-tray glass type) distillation tower enforcement with 5: 1 reflux ratio.

Table 2

Vacuum tower 130 receives from reboiler 140 inject and opportunity crudes that be heated to certain temperature, then, removes 3% to 4% low viscosity cut, and produces the C level oil fuel peculiar to vessel with the flash-point that is higher than 70 ℃.

Just, vacuum tower 130 is worked under vacuum and is not used demineralizer, so that oil refining prevents the corrosion to refining equipment simultaneously, thereby produces the C level oil fuel peculiar to vessel with the flash-point that is higher than 70 ℃.

Vacuum tower 130 is discharged boiling composition (boiling ingredients) at the top, and produces 96% to 97% product in its bottom.For save energy and minimum thermal decomposition, vacuum tower is being worked under via the optimum treatment condition of heat exchanger 120 in the heat exchange between product and the crude oil, wherein, the temperature of the product that obtains after heat exchange by heat exchanger 120 remains on 60 ℃ to 70 ℃ so that handle in the reservoir 160 product and like a cork product is loaded on ship or the tanker truck.

Table 3 illustrates for the compensation (satisfaction) of determining flash-point under vacuum (be used for pre-etch-proof be lower than under 150 ℃ the temperature work) result to overhead fraction (overhead cut) (O/H cut) (O/H cut) test of distillation tower.Use 15 layers of theoretical tower tray glass mould distillation tower, implement the batch processing mode test under non-backflow (non-reflux) condition, its result is shown in the table 3.Briefly, table 3 shows the relation between the O/H cut rate (cut rates) that is in 150 ℃ and flash-point.

Table 3

Table 4 illustrates for the compensation of the determining flash-point result to the O/H cut test of distillation tower under vacuum (be used for pre-etch-proof be lower than under 130 ℃ the temperature work).Use 15 layers of theoretical tower tray glass mould distillation tower, implement the batch processing mode test under non-reflux conditions, its result is shown in the table 4.Briefly, table 4 shows the relation between the O/H cut rate that is in 130 ℃ and flash-point.

Table 4

Water cooler 150 makes from vacuum tower 130 isolated low viscosity cut condensations, makes low viscosity cut liquefaction by the vacuum pump (not shown) then, so that the capacity of minimized vacuum pump and operation distillation is stably handled.

More specifically, if water cooler 150 be installed in vacuum pump before bring in liquefaction low viscosity cut, thereby reduce the capacity of vacuum pump significantly and operation distillation is stably handled.Therefore, use vacuum tower 130 can be eliminated the general issues for the low viscosity cut that satisfies the extensive vacuum pump removal 3% to 4% of the flash-point needs that are higher than 70 ℃.

Table 5 shows the result that theoretic 10 layers of tower tray guiding distillation towers (pilot distillation column) are worked under vacuum.The result of table 5 expression continuous mode work, and table 3 and table 4 show the result of batch processing mode work.Condenser comprises that the water cooler that uses dry ice is to come condensation low viscosity cut by non-reflux operation.

Table 5

Table 5 shows after having stablized working treatment with 3 hours interval 8 specimen sample is carried out the result of test, at the temperature condensation O/H low-viscosity substances (less than 5 ℃, 5 ℃ to 75 ℃) that is lower than 5 ℃, and collects the condensation material by dry ice.

Water cooler 150 uses dry ice to make from vacuum tower 140 isolated low viscosity cut condensations, and discharge has low viscous condensate oil.

Reservoir 160 receptions and storage by distilled C level oil fuel peculiar to vessel, strengthen oil from outside reception flow point from vacuum tower 130, and the oily C level oil fuel peculiar to vessel with storage of flow point enhancing is mixed to prepare low viscous C level oil fuel surrogate peculiar to vessel.

In this, because some users need at room temperature product to be carried out simple operation and/or processing,, flow point is added into C level oil fuel peculiar to vessel to satisfy the intrinsic flash-point of product so being strengthened oil.Therefore, strengthen oil as the flow point of oily synthetics (oil composite) and can be used for effectively producing and substitute oil, this oil synthetics has high boiling point and relative low viscosity.

Fig. 3 and Fig. 4 show the result's of the corrosion test that uses TAN graphic representation.

As shown in Fig. 3 and Fig. 4, according to SET laboratory (SET Laboratories) Inc. (12873 Capricorn Drive Stafford, Texas, USA) data that (380 pages) disclose in naphthenic acid (Naphthenic acid) corrosive comment are being lower than the corrosion that can not take place to be caused by TAN under 150 ℃ the temperature as can be seen.

Table 6 shows the result to the test of mixture, and this mixture obtains by flow point being strengthened the oily product that is added into by the opportunity crude refining.

Table 6

As shown in the table 6, the flow point of opportunity crude product is about 40 ℃, and this flow point is higher than the flow point of bunker B oil (B level peculiar to vessel (Bunker-B), 10 ℃ flow point) and the flow point of C bunker A oil (C level peculiar to vessel, 30 ℃ or higher flow point).In order at room temperature to give (impart) opportunity crude product flowability (this makes it use become simple again conversely), low viscosity oil synthetics (composite) is added into product and detects mixture.From the result of test as can be seen, the oily synthetics with 10% to 12% adds the oil mixt of industry Ji in next life in the product to.

As shown in Figure 5, opportunity crude method for refining of the present invention comprises opportunity crude is placed opportunity crude storage tank S100.

Herein, needs are removed some compositions for the standard flash-point that satisfies the C level oil fuel peculiar to vessel that is higher than 70 ℃, for example, some have the low viscous composition less than 70 ℃ such as butane, pentane, pentamethylene, methylpentane (methylpentane), dimethylbutane, normal hexane etc., these compositions with 3% to 4% amount be included in opportunity crude in.

In other words, opportunity crude can comprise typical salt (for example, calcium chloride, magnesium chloride etc.), and these salts at high temperature decompose generation hydrochloric acid, cause the heavy corrosion to equipment.Opportunity crude can also have a large amount of acid fraction (TAN), such as naphthenic acid, may cause the corrosion to the reboiler that is provided with in distillation tower.

The flow point of opportunity crude is about 38 ℃, and opportunity crude can be placed and be in about 50 ℃ storage tank, and at about 50 ℃, opportunity crude has the viscosity of about 250cP.

Under the temperature more than the flow point, the viscosity of opportunity crude is lower than C level fuel oil viscosity peculiar to vessel.Yet at room temperature, because the content of acid fraction, opportunity crude may become hard solid, as chocolate.

Be used for that opportunity crude can be had steam sleeve or the steam tracing device that is used for opportunity crude is heated to preferred temperature from the pipeline that storage tank is transported to vacuum tower, so that prevent the opportunity crude S120 that in pipeline, hardens.

Vacuum tower is discharged the boiling composition at the top, and produces 96% to 97% product in its bottom.For save energy and minimum thermal decomposition, vacuum tower is for the S130 that works under via the optimum treatment condition of heat exchanger in the heat exchange between product and the crude oil.

In this case, the temperature of the product that obtains after heat exchange by heat exchanger remains on 60 ℃ to 70 ℃, so that handle the product in the reservoir and like a cork product is loaded on ship or the tanker truck.

, under vacuum remove be included in the low viscosity cut of in opportunity crude about 3% to 4% in, produce heavy oil and/or C level oil fuel surrogate S140 peculiar to vessel by the opportunity crude that is stored in the storage tank thereafter.

Then, the low viscosity cut cools off under vacuum and uses the vacuum pump condensation with production low viscosity condensate oil S150.

Heavy oil that will obtain under vacuum and/or C level oil fuel surrogate peculiar to vessel store S160.

In addition, flow point is strengthened oil and be added into the heavy oil of production and/or C level oil fuel surrogate peculiar to vessel with final production low viscosity C level peculiar to vessel oil fuel surrogate S170.

Equipment and the method that is used for refining of opportunity crude according to the present invention has following functional effect:

At first, work for the distillation tower that is used for opportunity crude, neither need desalting plant also not need to be used to prevent the corrosive additive that causes by TAN, wherein, refining of opportunity crude and preventing is used for the corrosion of the equipment of refining of opportunity crude, so that produce the replaceable fuel of heavy oil (C level oil fuel peculiar to vessel), thereby embody economic method for refining with the flash-point that is higher than 70 ℃.

Secondly, the front end that water cooler is installed in vacuum pump is to liquefy 3% to 4% low viscosity cut, this low viscosity cut of 3% to 4% need remove so that meet the desired flash-point by vacuum operating, thereby the capacity of minimized vacuum pump, operation distillation is stably handled, and reclaims effective constituent to greatest extent from opportunity crude.

The 3rd, during refining oil, obtain 96% to 97% final product in the bottom of distillation tower.For save energy and minimum thermal decomposition, the temperature of crude oil and product heat exchange and the product that obtains after heat exchange remains on 60 ℃ to 70 ℃, so that the product in the processing storage tank and product is loaded on ship or the tanker truck like a cork, thereby save energy also reduces the size of thermal source (heat source) feeding mechanism significantly, and this reduces cost of investment conversely again.

The 4th, because some users need at room temperature product to be carried out simple operation and/or processing, can be added into product effectively so that satisfy the intrinsic flash-point of product and the flow point that improves product with strengthen oil as flow point with high boiling point and relative low viscous oily synthetics, thus the economic worth that improves the sales volume of the product (product sales) and guarantee product by the variation in the current market of product.

Technology of the present invention constitutes and other technical characterictic although described, for what those skilled in the art understood be, the present invention is not limited to exemplary embodiment described above and accompanying drawing, and the present invention can cover various displacements to embodiment, change and/or modification and the scope of the present invention that do not break away from claims and limited.

Claims

1. equipment that is used for refining of opportunity crude comprises:

The opportunity crude storage tank;

Vacuum tower receives the opportunity crude that stores from described storage tank, then, when production has the C level oil fuel peculiar to vessel as kerosene of the flash-point that is higher than 70 ℃, removes the low viscosity cut under vacuum; And

Reservoir, described reservoir are used for receiving the C level oil fuel of being produced peculiar to vessel from described vacuum tower.

2. equipment according to claim 1 wherein, is discharged described low viscosity cut at the top of described vacuum tower, and has the described C level oil fuel described peculiar to vessel that is higher than 70 ℃ flash-point from the bottom discharge of described vacuum tower.

3. equipment according to claim 1 further comprises reboiler, and the described opportunity crude that described reboiler is used for flowing to described vacuum tower from described storage tank is heated to certain temperature.

4. equipment according to claim 1 further comprises water cooler, and described water cooler is used for the described low viscosity cut that cooling is fast discharged from described vacuum tower, with production low viscosity condensate oil.

5. equipment according to claim 4 further comprises vacuum pump, and described vacuum pump is used for discharging the described low viscosity condensate oil that produces at described water cooler.

6. equipment according to claim 1 wherein, strengthens oil with flow point and is added into described reservoir with production low viscosity C level peculiar to vessel oil fuel.

7. equipment according to claim 1, wherein, described reservoir stores described C level oil fuel peculiar to vessel at 60 ℃ to 70 ℃.

8. equipment according to claim 1, wherein, described opportunity crude is handled in 110 ℃ to the 150 ℃ work under vacuum of described vacuum tower.

9. equipment according to claim 1, wherein, described vacuum tower is produced described C level oil fuel peculiar to vessel with batch processing mode or continuous mode work.

10. equipment according to claim 1 wherein, is used for described opportunity crude is equipped with steam sleeve or steam tracing device from the pipeline that described storage tank is transported to described vacuum tower, hardens in described pipeline to prevent described opportunity crude.

11. equipment according to claim 1 further comprises heat exchanger, described heat exchanger places between described opportunity crude storage tank and the described vacuum tower, thereby reclaims heat to carry out heat exchange between product and raw material.

12. a method that is used for refining of opportunity crude comprises:

Receive described opportunity crude from storage tank, and when production has the C level oil fuel peculiar to vessel of the flash-point that is higher than 70 ℃, under vacuum, remove the low viscosity cut;

Cool off described low viscosity cut with production low viscosity condensate oil;

Storage has the described C level oil fuel described peculiar to vessel that is higher than 70 ℃ flash-point; And

To have described C level oil fuel described peculiar to vessel and the flow point that is higher than 70 ℃ flash-point and strengthen the oil mixing, so that production low viscosity C level peculiar to vessel oil fuel.

13. method according to claim 12 wherein, when the described opportunity crude of heating arrives certain temperature, is supplied with described opportunity crude.

14. method according to claim 12 wherein, uses dry ice to carry out described cooling with the described low viscosity cut of condensation.

15. method according to claim 12, wherein, the amount with 10% to 12% strengthens oil with flow point and is added into described C level oil fuel peculiar to vessel.