CN104610999A - Underpressure distillation tower and underpressure distillation method - Google Patents
Underpressure distillation tower and underpressure distillation method Download PDFInfo
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- CN104610999A CN104610999A CN201310544719.7A CN201310544719A CN104610999A CN 104610999 A CN104610999 A CN 104610999A CN 201310544719 A CN201310544719 A CN 201310544719A CN 104610999 A CN104610999 A CN 104610999A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/06—Vacuum distillation
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Abstract
The invention discloses an underpressure distillation tower and an underpressure distillation method, which belong to the petroleum refining industry, so that problems of high height of the tower due to much filling material, large material consumption and high pressure drop of whole tower of the current underpressure distillation towers can be solved. The underpressure distillation tower comprises a cylindrical shell (10) and a tower inner member, a charging part, a washing part and a fractionation part from up to down. A gas distributor (1) is arranged in the charging part. Several fractionation segments are arranged at the fractionation part, each fractionation segment is composed of a spray-type liquid distributor (3) and an oil collection tank (6); a unidirectional nozzle (8) is arranged on the spray-type liquid distributor, and the oil collection tank is positioned below the spray-type liquid distributor. The underpressure distillation method is carried out by employing the underpressure distillation tower. The underpressure distillation method is mainly used for petroleum refining industry, height, material consumption and pressure drop of the whole drop of the underpressure distillation tower can be reduced, pull-out rate is increased, and product quality is improved.
Description
Technical field
The present invention relates to refining of petroleum industry a kind of vacuum still used and vacuum distillation method.
Background technology
The vacuum still that current refining of petroleum industry uses in operation, filler upper surface is evenly distributed to through tank type liquid distributor or spray-type liquid distributor after liquid return enters tower, descending along filler space again, fully contact with by oil gas up bottom filler, while heat transfer, carry out mass transfer; Light constituent rises, in the descending oil header fallen immediately below filler of heavy constituent.The sideline product oil pump formed is extracted out from oil header, and a part enters product tank, and a part passes back into tower and forms circulation.
Chinese patent CN2423942Y discloses a kind of separation column, comprises structured packing, tower body, liquid receiver and liquid dispenser.Liquid dispenser comprises level liquid distribution trough and secondary liquid distribution trough, and liquid receiver comprises brine collecting ring and liquid collecting tile.The shortcoming of this patent is that the complex structure of liquid dispenser and liquid receiver, manufacture difficulty are large, and the requirement for horizontality installed liquid dispenser is high.CN201737918U discloses a kind of vacuum distillation tower, forms by the bottom of tower top, tower body and tower.Described tower top is connected with vacuum extractor and tower top cold reflux device, and described tower body is connected with 4 side take-off devices and 3 stage casing refluxes.Have the four line segment column internalss comprising column plate and filler formation in this tower body, the 4th line segment column internals being positioned at tower body bottom is also provided with scum dredger.Be provided with opening for feed in the bottom of described column internals, bottom at the bottom of described tower, be provided with residual oil outlet at the bottom of tower.Described scum dredger is arranged on the superiors of the 4th line segment column internals in tower body, is connected with thermal backflow flushing arrangement in the below of this scum dredger, and the filler being arranged on the 4th line segment column internals is random packing.CN102441287A discloses a kind of Novel pressure-reducing distillation tower, comprises at the bottom of tower top, tower body and tower.Tower top is connected with pumped vacuum systems, and there is the liquid distributor of liquid-phase reflux tower top inside.Tower body comprises condensation segment, distillation stage and washing section, and tower body arranges 2 ~ 5 liquid-phase product extraction side lines, has opening for feed in washing section bottom.At the bottom of tower, inside is the stripping stage of column plate or filler, has stripped vapor opening below orlop column plate and filler, and residual oil outlet is drawn in bottom; On the top, condensation segment gas phase zone of at least one liquid-phase product extraction side line, gas phase extraction side line is set.The common issue that above-mentioned patent exists is: the filler used in tower is on the high side, makes the height of tower higher; More filler and higher tower body cause the high material consumption of vacuum still, it is bigger than normal to invest, and also makes the full tower pressure drop of vacuum still higher.In addition, the installation of filler needs piecemeal to assemble, and strut member, press strip and bolt be used fixing, more complicated.
Summary of the invention
The object of this invention is to provide a kind of vacuum still and vacuum distillation method, making the problems such as the height of tower is higher, high material consumption, full tower pressure drop are higher to solve existing vacuum still because using more filler.
For solving the problem, the technical solution used in the present invention is: a kind of vacuum still, comprise cylindrical shell and column internals, be divided into feeding part, washing part, fractionating section from bottom to top, feeding part is provided with gas distributor, and fractionating section is provided with multiple distillation stage, it is characterized in that: each distillation stage is made up of a spray-type liquid distributor and an oil header, spray-type liquid distributor is provided with one-way sprayer, and oil header is positioned at the below of spray-type liquid distributor.
Above-mentioned vacuum still is adopted to carry out the method for underpressure distillation, it is characterized in that: the oil gas containing solid particulate enters gas distributor, rise after gas distributor is uniformly distributed, enter washing part to wash, oil gas through washing continues up, the liquid countercurrent sprayed out downwards with the one-way sprayer on spray-type liquid distributor in each distillation stage of fractionating section contacts and carries out gas-liquid heat-transfer and mass transfer, extract pipe as sideline product out from the sideline product of vacuum still after the product liquid obtained falls into oil header to extract out, in the sideline product extracted out, a part enters spray-type liquid distributor set by distillation stage as ejecting liquid, gas products is extracted out from the top of vacuum still.
Compared with prior art, the present invention is adopted to have following beneficial effect: each distillation stage of fractionating section is only made up of a spray-type liquid distributor and an oil header, does not use filler, make the height of tower lower in vacuum still.And the materials consumption of vacuum still is less, investment is lower; Full tower pressure drop is also lower, be conducive to reducing energy consumption, reduce the content of light constituent (as be less than 500 DEG C of cuts or be less than 538 DEG C of cuts) in vacuum residuum at the bottom of the vacuum still tower specified in oil refining industry simultaneously, improve extracting rate, realize the greatest benefit of oil product combination.In addition, vacuum still of the present invention does not have filler to install Problems existing.
When processing Processing High-sulfur High-Acidity Crude Oils, require very harsh to the Corrosion Protection of vacuum still cylindrical shell and column internals material, material price is expensive.Adopt the solution of the present invention, due to the materials consumption of vacuum still can be reduced, so investment significantly can be reduced, effectively reduce costs.
The column internals of vacuum still of the present invention is less, and this is conducive to the long-term operation of vacuum still, reduces maintenance number of times, saves the cost of overhaul.
The present invention is mainly used in the vacuum distillation process of refining of petroleum industry.
Below in conjunction with accompanying drawing, embodiment and embodiment, the present invention is further detailed explanation.Accompanying drawing, embodiment and embodiment do not limit the scope of protection of present invention.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of vacuum still of the present invention.
Fig. 2 is the structural representation of another kind of vacuum still of the present invention.
Fig. 3 is the vertical view of a kind of spray-type liquid distributor that the present invention uses.
Fig. 4 is provided at the structural representation of a kind of one-way sprayer on spray-type liquid distributor.
Fig. 5 is provided at the structural representation of a kind of Bidirectional spray head on spray-type liquid distributor.
Fig. 6 is the enlarged detail of oil header in Fig. 1 and Fig. 2.
In Fig. 1 to Fig. 6, same reference numerals represents identical technical characteristic.
Embodiment
See Fig. 1, a kind of vacuum still of the present invention, comprises cylindrical shell 10 and column internals, is divided into feeding part, washing part, fractionating section from bottom to top.Feeding part is provided with gas distributor 1, and gas distributor 1 uses conventional gas distributor, as biserial vane-type, tangential etc.Fractionating section is provided with multiple distillation stage, and each distillation stage is made up of a spray-type liquid distributor 3 and an oil header 6; Spray-type liquid distributor 3 is provided with one-way sprayer 8, and oil header 6 is positioned at the below of spray-type liquid distributor 3.The top of vacuum still is provided with gas outlet tube 5, and bottom is provided with tower prime cement liquid and extracts pipe 4 out.Vacuum still is also provided with tower top vacuum extractor, instrumentation tap etc., and figure slightly.The column internals of vacuum still, refers to gas distributor 1, spray-type liquid distributor 3 and oil header 6 etc.
Fractionating section is generally provided with 3 ~ 4 distillation stages, and shown in Fig. 1 is be provided with 3 distillation stages.
Spray-type liquid distributor 3 set by distillation stage preferably uses the liquid spray distributing device described in CN201454359U.See Fig. 3 (view that the vertical view dextrorotation that Fig. 3 is equivalent to spray-type liquid distributor 3 set by distillation stage shown in Fig. 1 and Fig. 2 turn 90 degrees and obtains), it comprises charging supervisor 31, distribution arms 32 and fluid jetting head.Distribution arms 32 and charging are responsible for 31 and are connected, and fluid jetting head is responsible for 31 with distribution arms 32 and charging and is connected.Set fluid jetting head is one-way sprayer 8.See Fig. 4, this one-way sprayer 8 is provided with shower nozzle plug 84, shower nozzle cavity 82, charging straight tube 81 and squit hole 83.Shower nozzle cavity 82 is linear, the cylindrical or back taper of double-paraboloid, and squit hole 83 is in loudspeaker wide-angle shape.Described double-paraboloid line head cavity 82 (as shown in Figure 4), refer to shower nozzle cavity 82 for para-curve with the axial line of shower nozzle cavity 82 for turning axle rotates the para-curve rotator shaped surrounded, the shape of its sidewall on the vertical plane by shower nozzle cavity 82 axial line is two para-curves.Described back taper shower nozzle cavity 82, refers to that shower nozzle cavity 82 is for inverted conical butt.For the shower nozzle cavity 82 of non-cylindrical, its diameter refers to the diameter at minimum place.See Fig. 4, charging straight tube 81 is positioned at shower nozzle cavity 82 side and is communicated with shower nozzle cavity 82, the axes normal of its axis and shower nozzle cavity 82.Arrangement mode between one-way sprayer 8 is rounded projections arranged or diamond array.The spray area of described one-way sprayer 8 large (1.5 ~ 2 square metres can be reached), uniform effective; Also can use with other unidirectional fluid jetting head of its similar nature.The explanation of aforesaid liquid spray distribution apparatus (comprising one-way sprayer 8) structure and operating process, refers to CN201454359U.Spray-type liquid distributor 3 set by each distillation stage can according to the cross-sectional area of the flow of ejecting liquid 33 and vacuum still cylindrical shell 10, quantity, the size of adjustment one-way sprayer 8, the horizontal section of the vacuum still cylindrical shell 10 of corresponding spray-type liquid distributor 3 present position covers by the liquid that spray is gone out.
Oil header 6 set by distillation stage can use existing oil header (such as drum type brake oil header), preferably uses the liquid-collecting box described in CN202642532U.See Fig. 6, oil header 6 is mainly provided with upper part and props up intercepting basin 61, central branch intercepting basin 62 and bottom and gather intercepting basin 63.Bifurcation Set liquid bath is layered arrangement, and upper part is propped up intercepting basin 61 and arranged as one deck, central branch intercepting basin 62 are arranged as one deck.Leave gap between Bifurcation Set liquid bath in every layer, upper part props up intercepting basin 61 and central branch intercepting basin 62 interlayer leaves gap.Upper part is propped up intercepting basin 61 and is connected by strut member with central branch intercepting basin 62, and each Bifurcation Set liquid bath is connected with cylindrical shell 10 near one end of vacuum still cylindrical shell 10, and one end and the bottom of central branch intercepting basin 62 are gathered intercepting basin 63 and be connected.Bottom is gathered intercepting basin 63 and is connected with extraction pipe 7.In Fig. 6 of the present invention, each oil header 6 arranges one and extracts pipe 7 out, is connected to the bottom that intercepting basin 63 is gathered in bottom.In Fig. 1 and Fig. 2 of CN202642532U, each liquid-collecting box arranges two and extracts pipe out, is connected to the two ends (oil header 6 of the present invention also can use this structure) that intercepting basin is gathered in bottom.Extract out pipe 7 be used as in vacuum still of the present invention sideline product extract out pipe, each oil header 6 can according to sideline product number arrange one or more extract out pipe 7.Relative to existing drum type brake oil header, it is more even that the liquid-collecting box described in CN202642532U can make the gas distribution flow through obtain, thus ensure fully effectively to contact between gas-liquid, strengthens gas-liquid mass transfer effect.
Existing vacuum still, washing part typically uses tank type liquid distributor, arranges one section of filler (being generally corrugated plate packing) in the below of tank type liquid distributor.The requirement for horizontality of tank type liquid distributor is high, installation is complicated, spatial altitude that is that take is high and high material consumption.For overcoming this shortcoming, the present invention uses spray-type liquid distributor 3 in washing part, and does not use filler.Vacuum still shown in Fig. 1, the spray-type liquid distributor 3 (be provided with one-way sprayer 8) of washing set by part is identical with the spray-type liquid distributor 3 (comprising one-way sprayer 8) set by distillation stage.Spray-type liquid distributor 3 does not have tank type liquid distributor Problems existing.
The another kind of vacuum still of the present invention shown in Fig. 2 with the difference of vacuum still shown in Fig. 1 is, on the spray-type liquid distributor 3 set by washing part, setting is Bidirectional spray head 9 described in CN201702049U.See Fig. 5, Bidirectional spray head 9 is provided with feed-pipe 93, housing 95, is provided with cylindrical cavity 92 in housing 95.Be provided with connecting passage 94 between feed-pipe 93 and cylindrical cavity 92, the two ends of cylindrical cavity 92 are provided with wide-angle flaring exit 91.The spray area of described Bidirectional spray head 9 large (4 ~ 6 square metres can be reached), uniform effective; Also can use with other two-way fluid jetting head of its similar nature.The above-mentioned structure of Bidirectional spray head 9 and the explanation of operating process, refer to CN201702049U.Bidirectional spray head 9 can be connected to distribution arms described in CN201454359U by the mode identical with one-way sprayer 8 and charging is responsible for, and composition is provided with the spray-type liquid distributor 3 (changing the one-way sprayer 8 in Fig. 3 of the present invention into Bidirectional spray head 9) of Bidirectional spray head; Detail drawing omits.
The washing part of vacuum still of the present invention can arrange 1 spray-type liquid distributor 3 (as shown in Figure 1 and Figure 2), also can the spray-type liquid distributor (figure slightly) of more than 2 setting up and down.The spray-type liquid distributor 3 of washing set by part can according to the cross-sectional area of the flow of ejecting liquid 33 and vacuum still cylindrical shell 10, quantity, the size of adjustment one-way sprayer 8 or Bidirectional spray head 9, the horizontal section of the vacuum still cylindrical shell 10 of described spray-type liquid distributor 3 present position covers by the liquid that spray is gone out (forming upper and lower two-layer liquid to cover when using Bidirectional spray head 9).
Spray-type liquid distributor 3 of the present invention uses one-way sprayer described in CN201454359U or CN201702049U or Bidirectional spray head, be because its spatial altitude that is relatively simple for structure, that be easy to manufacture, take is low, be conducive to reducing the height of vacuum still and full tower pressure drop.One-way sprayer 8 and Bidirectional spray head 9 are all not easily blocked by solid particulate, can extension device work-ing life and turnaround.The liquid distribution sprayed out due to each one-way sprayer 8 and Bidirectional spray head 9 is even, in fine droplet, so can increase gas-to-liquid contact chance, strengthen gas-liquid mass transfer effect or strengthen the cleaning performance to solid particulate contained by oil gas.Spray-type liquid distributor 3 set by washing part uses Bidirectional spray head 9, can for reducing heavy metal and carbon residue content in sideline product, improve quality product more reliable and effective guarantee be provided.
For the vacuum still shown in Fig. 1, vacuum distillation method of the present invention is described below.Oil gas 20 containing solid particulate [heavy metal (as Ni, V) and char particle etc.] enters gas distributor 1 by the entrance 2 of gas distributor 1, rises, enter washing part and wash after gas distributor 1 is uniformly distributed.Ejecting liquid 33 enters the spray-type liquid distributor 3 set by washing part from the entrance 30 of spray-type liquid distributor 3, through charging supervisor 31, distribution arms 32, by one-way sprayer 8 evenly ejection downwards.During the liquid that the oil gas upruss containing solid particulate is sprayed out downwards by one-way sprayer 8, its solid particulate carried is washed down.In washing process, the oil gas containing solid particulate of the liquid that one-way sprayer 8 sprays out downwards and rising also carries out gas-liquid heat-transfer and mass transfer simultaneously.Liquid is become after the heavy constituent cooling that in rising oil gas, volatility is low, cooling, carry together with the ejecting liquid removing the high light constituent of volatility through gas-liquid heat-transfer after mass transfer and drop at the bottom of tower by the solid particulate that washes down is descending, become tower prime cement liquid 40 (tower prime cement liquid 40 i.e. vacuum residuum; Tower prime cement liquid 40 is finally extracted pipe 4 out by tower prime cement liquid and is discharged); Become vapor phase stream after the light constituent that in ejecting liquid, volatility is high is heated, rise together with remove the rising oil gas of the low heavy constituent of volatility after mass transfer through gas-liquid heat-transfer.Above-mentioned washing process, can prevent oil gas from carry on most of solid particulate and escape, thus reduces heavy metal and the carbon residue content of sideline product, promotes the quality of sideline product.
Oil gas (light constituent that in containing washing part ejecting liquid, volatility is high) through washing continues up, from bottom to top through each distillation stage of fractionating section.In each distillation stage, oil gas is first upwards uniformly distributed by the gap (as shown in the curve arrow in Fig. 6) between each Bifurcation Set liquid bath of oil header 6.Ejecting liquid 33 enters each spray-type liquid distributor 3 set by each distillation stage from the entrance 30 of spray-type liquid distributor 3, through charging supervisor 31, distribution arms 32, by one-way sprayer 8 evenly ejection downwards.The oil gas risen contacts with the liquid countercurrent that the one-way sprayer 8 of the spray-type liquid distributor 3 set by each distillation stage sprays out downwards and carries out gas-liquid heat-transfer and mass transfer.Become liquid after the cooling of heavy constituent that in rising oil gas, volatility is low, cooling, seamless unoccupied place falls into upper part and props up intercepting basin 61, central branch intercepting basin 62 and bottom and gather intercepting basin 63 together with the ejecting liquid removing the high light constituent of volatility through gas-liquid heat-transfer after mass transfer; Then the liquid that upper part is propped up in intercepting basin 61, central branch intercepting basin 62 constantly confluxes, and finally confluxes bottom accumulating to and gathers in intercepting basin 63.Aforesaid liquid product is extracted the pipe extraction pipe 7 of oil header 6 (each distillation stage) as sideline product out from the sideline product of vacuum still and is extracted out.In above-mentioned gas-liquid heat-transfer and mass transfer process, vapor phase stream is become after the light constituent that in ejecting liquid, volatility is high is heated, rise together with remove the rising oil gas of the low heavy constituent of volatility after mass transfer through gas-liquid heat-transfer, finally extract out as the gas outlet tube 5 of gas products from underpressure distillation top of tower.
Vacuum still of the present invention, when fractionating section is provided with 3 ~ 4 distillation stages, extracts the sideline product of 3 ~ 4 kinds of different boiling ranges out the most at last.Vacuum still shown in Fig. 1 and Fig. 2, fractionating section is equipped with 3 distillation stages, all extracts the sideline product of 3 kinds of different boiling ranges out.The sideline product wherein extracted out from a uppermost distillation stage is decompression one line.Entering the ejecting liquid 33 in each spray-type liquid distributor 3 set by each distillation stage, is a part (the stage casing backflow as returning vacuum still) of extracting out in the sideline product from each corresponding distillation stage; Entering the ejecting liquid 33 in the set spray-type liquid distributor 3 of washing part, is a part (washing oil as returning vacuum still) of extracting out in addition in the sideline product from a bottom distillation stage.
In the gas-liquid heat-transfer and mass transfer process of above-mentioned each distillation stage, while the oil gas risen contacts with the liquid countercurrent that the one-way sprayer 8 of the spray-type liquid distributor 3 set by distillation stage sprays out downwards and carries out gas-liquid heat-transfer and mass transfer, a small amount of solid particulate that described oil gas carries can be cleaned again by described ejecting liquid, and the solid content that oil gas is carried constantly reduces.
Shown in the operating process of the another kind of vacuum still of the present invention shown in Fig. 2 and Fig. 1, the difference of vacuum still operating process is that the Bidirectional spray head 9 on the spray-type liquid distributor 3 set by washing part sprays out two-layer liquid with below simultaneously upward; Oil gas 20 containing solid particulate rises after gas distributor 1 is uniformly distributed, and is undertaken washing and carry out gas-liquid heat-transfer and mass transfer, better effects if in washing part by this two-layer liquid.
Vacuum still of the present invention adopts preferred implementation (the spray-type liquid distributor 3 set by distillation stage uses the one-way sprayer described in CN201454359U, spray-type liquid distributor 3 set by washing part uses the one-way sprayer described in CN201454359U or the Bidirectional spray head described in CN201702049U, oil header 6 set by distillation stage use liquid-collecting box described in CN202642532U), under equal conditions compared with the vacuum still of existing use filler, the height of tower generally can reduce by more than 35%, and full tower pressure drop generally can reduce more than 5%.Except described full tower pressure drop, other prevailing operating conditions of vacuum still of the present invention is substantially identical with the conventional vacuum distillation tower of existing use filler, and explanation is omitted.
Embodiment
The vacuum still of the original Φ 6400mm of certain company, the long residuum that processing atmospheric distillation tower produces, designing treatment amount is 2,480,000 tons/year.The height of this vacuum still is 50m (rice), is provided with feeding part, washing part, fractionating section from bottom to top.Feeding part is provided with a two inlets streamline gas distributor.Washing part is provided with a tank type liquid distributor, is provided with the Mellapak structured packing that one section of 2.2m is high in the below of tank type liquid distributor.Fractionating section is provided with 3 distillation stages, has 3 extraction side lines, 3 stage casing backflows.Each distillation stage is provided with a tank type liquid distributor, and the below of tank type liquid distributor is provided with the high Mellapak structured packing of one section of 2.4m, and the below of filler is provided with a drum type brake oil header.During the operation of this tower, full tower pressure drop is 15mmHg post.Operating result shows, the cut being less than 500 DEG C in its vacuum residuum is higher, the line that reduces pressure, decompression two wires, reduce pressure carbon residue in three lines and heavy metal (Ni/V) content higher.
Because original vacuum still has employed 30 years nearly, equipment is outmoded seriously aging.In order to verify result of use of the present invention, the Φ 6400mm vacuum still that the said firm is newly-built implements reduced pressure distillation technique of the present invention.As shown in Fig. 2 of the present invention, (fractionating section is provided with 3 distillation stages to the structure of newly-built vacuum still, have 3 spray-type liquid distributors, 3 oil headers, 3 extraction side lines, 3 stage casing backflows), use the spray-type liquid distributor of Fig. 3, Fig. 4, Fig. 5, Fig. 6 shown type of the present invention, one-way sprayer, Bidirectional spray head and oil header; Feeding part is provided with a biserial vane-type gas distributor.The crude oil comprising the atmospheric and vacuum distillation unit processing of newly-built vacuum still is the commingled crude (identical commingled crude processed by original atmospheric and vacuum distillation unit) that the outstanding promise crude oil of triumph Gudao crude and import mixes by the weight ratio of 1:4.The height of newly-built vacuum still is 31m, the long residuum that processing atmospheric distillation tower produces; Designing treatment amount is 2,800,000 tons/year, and turndown ratio is 60% ~ 110%, and full tower pressure drop is not more than 10mmHg post, and vacuum tightness is not more than 98.6kPa.The main structure parameters of newly-built vacuum still is in table 1 (it is unlisted that appended with drawings and word have shown), and prevailing operating conditions is in table 2.
The newly-built vacuum still of the technology of the present invention is used to demarcate after 10 months in operation.Compared with original vacuum still, concrete outcome is as follows: the content being less than 500 DEG C of cuts in the line that reduces pressure is little.The cut being less than 500 DEG C in decompression two wires, three lines that reduce pressure brings up to 72.2w%, 53.45w% by 68w%, 24w% respectively, and the cut being less than 500 DEG C in vacuum residuum is reduced to 2.36w% by 3.65w%, makes vacuum residuum be able to further deep drawing.Reduce pressure a line, decompression two wires, reduce pressure in three lines, carbon residue (Conradson carbon residue) is reduced to 0.09w%, 0.56w%, 0.93w% by 0.1w%, 3.2w%, 9.8w% respectively; Ni/V heavy metal content (by weight) also significantly reduces, and is reduced to 0.2/0.05,0.9/0.1,1.4/0.1ppm respectively by 2.8/2.75,4.82/6.21,14.91/24.96ppm.The quality of each sideline product is greatly improved, and can be the raw material that downstream unit provides more high-quality.
Above data show, use the newly-built vacuum still of the technology of the present invention compared with original vacuum still, when the height of tower significantly reduces 38%, the quality of each sideline product still promotes to some extent.In addition, full tower pressure drop have dropped 5mmHg post.
Table 1
Table 2
| Project | Numerical value |
| Feeding temperature (namely the oil gas temperature of solid particulate is contained in gas distributor ingress)/DEG C | 395 |
| Vacuum still tower top pressure (absolute pressure)/mmHg | 20 |
| The full tower pressure drop/mmHg of vacuum still | 10 |
| Vacuum still vacuum tightness/kPa | 98.3 |
| Underpressure distillation column overhead temperatures/DEG C | 75 |
| Reduce pressure one line extract out temperature/DEG C | 140 |
| Reduce pressure one line stage casing backflow return tower temperature/DEG C | 50 |
| Decompression two wires extraction temperature/DEG C | 246 |
| Decompression stage casing, two wires backflow return tower temperature/DEG C | 151 |
| Reduce pressure three lines extract out temperature/DEG C | 292 |
| Reduce pressure three line stage casings backflow return tower temperature/DEG C | 219 |
| Washing oil return tower temperature/DEG C | 292 |
| Vacuum still column bottom temperature/DEG C | 367 |
| Vacuum still inlet amount (inlet amount of the oil gas namely containing solid particulate)/kg/hr | 294926 |
| Reduce pressure a line stage casing backflow quantity of reflux/kg/hr | 24811 |
| Decompression stage casing, two wires backflow quantity of reflux/kg/hr | 53656 |
| Reduce pressure three line stage casing backflow quantity of reflux/kg/hr | 85628 |
| Washing oil mass/kg/hr | 39038 |
Claims (6)
1. a vacuum still, comprise cylindrical shell (10) and column internals, be divided into feeding part, washing part, fractionating section from bottom to top, feeding part is provided with gas distributor (1), fractionating section is provided with multiple distillation stage, it is characterized in that: each distillation stage is made up of a spray-type liquid distributor (3) and an oil header (6), spray-type liquid distributor (3) is provided with one-way sprayer (8), and oil header (6) is positioned at the below of spray-type liquid distributor (3).
2. vacuum still according to claim 1, is characterized in that: fractionating section is provided with 3 ~ 4 distillation stages.
3. vacuum still according to claim 1, it is characterized in that: the one-way sprayer (8) on the spray-type liquid distributor (3) set by distillation stage is provided with shower nozzle plug (84), shower nozzle cavity (82), charging straight tube (81) and squit hole (83), squit hole (83) is in loudspeaker wide-angle shape, charging straight tube (81) is positioned at shower nozzle cavity (82) side and is communicated with shower nozzle cavity (82), the axes normal of its axis and shower nozzle cavity (82), oil header (6) set by distillation stage is provided with upper part and props up intercepting basin (61), intercepting basin (63) is gathered in central branch intercepting basin (62) and bottom, Bifurcation Set liquid bath is layered arrangement, upper part props up intercepting basin (61) row for one deck, central branch intercepting basin (62) row is one deck, gap is left between Bifurcation Set liquid bath in every layer, upper part props up intercepting basin (61) and central branch intercepting basin (62) interlayer leaves gap, upper part is propped up intercepting basin (61) and is connected by strut member with central branch intercepting basin (62), one end and the bottom of central branch intercepting basin (62) are gathered intercepting basin (63) and are connected, bottom is gathered intercepting basin (63) and is connected with extraction pipe (7).
4. the vacuum still according to claim 1 or 2 or 3, is characterized in that: washing part is provided with spray-type liquid distributor (3), which is provided with the one-way sprayer (8) identical with one-way sprayer described in claim 3.
5. the vacuum still according to claim 1 or 2 or 3, it is characterized in that: washing part is provided with spray-type liquid distributor (3), which is provided with Bidirectional spray head (9), Bidirectional spray head (9) is provided with feed-pipe (93), housing (95), cylindrical cavity (92) is provided with in housing (95), be provided with connecting passage (94) between feed-pipe (93) and cylindrical cavity (92), the two ends of cylindrical cavity (92) are provided with wide-angle flaring exit (91).
6. the method adopting vacuum still according to claim 1 to carry out underpressure distillation, it is characterized in that: the oil gas (20) containing solid particulate enters gas distributor (1), rising after gas distributor (1) is uniformly distributed, enter washing part to wash, oil gas through washing continues up, the liquid countercurrent sprayed out downwards with the one-way sprayer (8) on spray-type liquid distributor (3) in each distillation stage of fractionating section contacts and carries out gas-liquid heat-transfer and mass transfer, extract pipe as sideline product out from the sideline product of vacuum still after the product liquid obtained falls into oil header (6) to extract out.In the sideline product extracted out, a part enters spray-type liquid distributor (3) set by distillation stage as ejecting liquid (33), and gas products is extracted out from the top of vacuum still.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310544719.7A CN104610999B (en) | 2013-11-04 | 2013-11-04 | Underpressure distillation tower and underpressure distillation method |
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| CN106267864A (en) * | 2016-11-11 | 2017-01-04 | 中国天辰工程有限公司 | A kind of high-efficiency evaporator refined for adiponitrile and adiponitrile process for refining |
| CN106730970A (en) * | 2017-03-22 | 2017-05-31 | 中国石油大学(华东) | A kind of dual-flow tray takes the decompression tower internals of thermal coupling with spray |
| CN108211406A (en) * | 2018-03-20 | 2018-06-29 | 刘彦昌 | A kind of vacuum distillation equipment for waste lubricating oil pretreatment |
| CN108251152A (en) * | 2018-03-20 | 2018-07-06 | 刘彦昌 | A kind of vacuum tower of waste lubricating oil pretreatment |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106267864A (en) * | 2016-11-11 | 2017-01-04 | 中国天辰工程有限公司 | A kind of high-efficiency evaporator refined for adiponitrile and adiponitrile process for refining |
| CN106730970A (en) * | 2017-03-22 | 2017-05-31 | 中国石油大学(华东) | A kind of dual-flow tray takes the decompression tower internals of thermal coupling with spray |
| CN106730970B (en) * | 2017-03-22 | 2023-11-21 | 中国石油大学(华东) | Vacuum tower internal part of heat-taking coupling through-flow column plate and spraying |
| CN108211406A (en) * | 2018-03-20 | 2018-06-29 | 刘彦昌 | A kind of vacuum distillation equipment for waste lubricating oil pretreatment |
| CN108251152A (en) * | 2018-03-20 | 2018-07-06 | 刘彦昌 | A kind of vacuum tower of waste lubricating oil pretreatment |
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