CN1262327C - Spiral fractionation tower - Google Patents
Spiral fractionation tower Download PDFInfo
- Publication number
- CN1262327C CN1262327C CN 03132999 CN03132999A CN1262327C CN 1262327 C CN1262327 C CN 1262327C CN 03132999 CN03132999 CN 03132999 CN 03132999 A CN03132999 A CN 03132999A CN 1262327 C CN1262327 C CN 1262327C
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- float valve
- tray
- tower
- tongue type
- spiral
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Abstract
The present invention relates to a spiral fractionation tower which belongs to the field of an oil product separation plant in oil refining industry and comprises a tower body (8). The present invention is characterized in that the interior of the tower body (8) is divided into three sections, the lower part is a tongue-shaped section, the middle part is a filler material section, and the upper part is a floating valve section. Compared with the prior art, the present invention has the advantages of integration of component separation, decolorization and deodorization, simple structure, convenient manufacture and repair, low investment, low operating expense, high product quality, etc. The present invention has great popularization value in the oil refining industries using waste oil plastic rubber.
Description
Technical field
Spiral fractionation tower of the present invention belongs to petroleum refining industry oil product separation equipment field.
Background technology
Conventional fractionating column mainly comprises plate column and packed tower two big classes, and its effect only is to realize the component separation.Product trace impurity (making product tape abnormal color and smell) must be removed by special decolouring and deodorizing technology and equipment.Especially present people are taken in plastics, the oil refining of expense rubber in utilization, make the equipment complexity, investment is big, cost is high, and does not also have the qualified oil product of real output at present in this field.
Summary of the invention
The technical problem to be solved in the present invention is: overcome the deficiencies in the prior art, provide a kind of component that can realize to separate, can realize removing of trace impurity in the product again, simple in structure, manufacturing is easy to maintenance, product quality is high, at the Spiral fractionation tower that utilizes expense plastics, expense rubber oil refining industry to have promotional value.
The technical solution adopted for the present invention to solve the technical problems is: this Spiral fractionation tower, comprise: tower body 8, it is characterized in that: three sections of branches are set in the tower body 8, the bottom is a tongue type section, the middle part is a packing section, top is the float valve section, the tongue type section that the bottom is provided with is a tongue type tower tray 3, the middle part packing section is that packing layer 15 reaches, each one deck float valve tray 6 of below, the float valve section that top is provided with is a float valve tray 6, tongue type tower tray 3 is tabular, last interval is provided with a plurality of tongue type wings 31, one end of tongue type wing 31 is fixed, other end perk, form 20-60 ° of angle with tongue type tower tray 3, tongue type tower tray 3 is provided with multilayer, every installation one deck is with respect to following 20-60 ° of angle of the parallel rotation of one deck, the angular range 0-360 of rotation °.
The preferred 22.5-36 of angle ° of forming of above-mentioned tongue type wing 31 and tongue type tower tray 3, every layer is progressively strengthened, but single-candidate or non-single-candidate progressively strengthen, every layer of single-candidate of the present invention strengthens 36 °, five layers to 180 ° of 1-5.The angle of perk can be decided according to designing requirement, 0 °-360 ° of scopes.Tongue type tower tray 3 can be provided with multilayer according to designing requirement, five layers of the preferred 1-5 of the present invention, tongue type tower tray 3 when mounted, every installation one deck rotates to an angle with respect to down one deck is parallel, general 20-60 °, the preferred 22.5-36 of the present invention °, the angle of rotation scope 0-360 °, can be changeed clockwise or counterclockwise according to designing requirement, for making adsorption effect better, one deck coke adsorption layer also can be laid in tongue type tower tray 3 tops.
The float valve section is that float valve tray 6 comprises: tower tray outer wall, spherical float valve 27, downflow weir 11, downflow weir 11 is arranged on the two ends of float valve tray 6, whole float valve tray 6 is divided into four zones, the middle part is the float valve district, one side is that liquid receiving area 28, opposite side are for falling liquid zone 30, bubbling area 29 is arranged on the two ends in float valve district, spherical float valve 27 triangular in shape being distributed in the float valve district.Float valve tray 6 is arranged on the upper and lower of packing layer 15, and multilayer is set, and preferred 9 layers, eight layers of packing layer 15 tops, below one deck.
Packing section is each one deck float valve tray 6 of packing layer 15 and its upper and lower, and packing layer 15 is a kind of in metal Bao earrings or woven wire or metal mesh opening ripple type or the structured packing of metal acanthopore ripple type.
Compared with prior art, the effect of having a mind to of Spiral fractionation tower of the present invention is: the bottom is provided with tongue type section, the tongue type wing 31 of the tongue type tower tray 3 of this tongue type section is since 0 °, the angle of every layer of rotation of making progress progressively strengthens, general 20-60 °, tongue type tower tray 3 is provided with multilayer, every installation one deck rotates to an angle with respect to one deck is parallel down, be generally 20-60 °, to 180 ° or 360 ° of ends, form helical duct, air-flow is along 180 or 360 ° of commentaries on classics of helical duct rising, prolong running time and the distance of gas in tower body 8, advantages of good adsorption effect; The middle part is provided with packing section, the packing layer 15 of this packing section, impurity in the gas is further filtered, top is provided with the float valve section, and the float valve 27 of the float valve tray 6 of float valve section adopts rounded projections arranged, to gas, liquid distribution is even, the gas-liquid contact area is big, fractionating effect is good, and air-flow comes out from tongue type section, through one deck float valve layer, entering into packing section filters, enter into the fractionation of float valve section again, continue to rise to cat head, the top is provided with quencher 21, make and return cat head and rise to tower body 8 upper gas convection current, improve the quality of products, increase yield, the purified product quality reduces useless heavy oil and takes place; Have that gas phase media forms spiral in tower body 8, the time of staying is long, distilling effect good, integrate component separation, decolouring, deodorization, simple in structure, make easy to maintenance, reduced investment, operating cost is low, the product quality advantages of higher, is utilizing the old plastic, rubber oil refining industry of expense to have promotional value.
Description of drawings
Fig. 1 is that Spiral fractionation tower master of the present invention looks to cut open and shows structural representation;
Fig. 2 is that float valve tray 6A-A cuts open and shows schematic diagram among Fig. 1;
Fig. 3 is a float valve tray float valve rounded projections arranged schematic diagram among Fig. 2;
Fig. 4 is that tongue type tower tray 3B-B cuts open and shows schematic diagram among Fig. 1;
Fig. 5 is tongue type wing 31 schematic diagrames among Fig. 4;
Fig. 6 is that Fig. 5 tongue type wing C-C cuts open and shows schematic diagram;
Fig. 7 is Fig. 1 top withdrawing fluid dispensing arrangement schematic diagram;
Fig. 8 is that Fig. 7 top withdrawing fluid distributor sprays the corner structure schematic diagram.
Fig. 1-the 8th, the most preferred embodiment of Spiral fractionation tower of the present invention, wherein: 1 (a) cracking still is gone into tower mouth 2 (b
1), 4 (b
2), 5 (b
3), 7 (b
4), 16 (b
5) hand hole 3 tongue type tower trays 6 float valve trays 8 tower body 9 (c) gaseous phase outlet 10 (d) top withdrawing fluid distributor 11 downflow weirs 12 (e
1), 13 (e
2) kerosene outlet 14 (f
1), 17 (f
2) diesel oil exports 15 metal Bao earrings packing layer 18 (g) heavy oil and export 19 cooling tubes, 20,22 flanges, 21 quenchers, 23 valves, 24 outlet pipes, 25 water inlet pipes, 26 petroleum benzin flowlines, 27 float valves, 28 liquid receiving areas, 29 bubbling areas 30 and fall liquid zone 31 tongue type wings, 32 spray holes.
The specific embodiment
Below in conjunction with accompanying drawing Spiral fractionation tower of the present invention is described in further details: shown in Fig. 1-8, be provided with in this Spiral fractionation tower tower body 8 and be divided into three sections, it is tongue type tower tray 3 that the bottom is provided with tongue type section, be totally five layers of tabular 1-5, last interval is provided with a plurality of tongue type wings 31, and an end of tongue type wing 31 is fixed, other end perk, form certain angle with tongue type tower tray 3, general 20-60 °, preferred 36 ° of the present invention, tongue type tower tray 3 can be provided with multilayer, preferred 5 layers, every layer rotates to an angle with respect to down one deck is parallel during installation, and general 20-60 °, preferred 36 ° of the present invention, 1-5 layer to 180 ° formation helical duct, air-flow is along 180 ° of commentaries on classics of helical duct rising.Also can increase the number of plies or reduce 360 ° of commentaries on classics of angle of every layer of rotation.Resistance is little, the time of staying is long, and tray spacing is dwindled, and the height of tower body reduces greatly, reduces investment.The angle of tongue type tower tray 3 every layer of perk is better with the consistent effect of the angle of every layer of parallel rotation, and is better for making adsorption effect, and one deck coke adsorption layer also can be laid in tongue type tower tray 3 tops, and the present invention preferably adopts the thick coke adsorption layer of 100mm.Tower body 8 bottoms are provided with tongue type tower tray 3, it mainly has been the adsorption filtration effect, promptly heavy ends are adsorbed on the tongue type wing 31, along with temperature constantly increases, the very long whereabouts of heavy ends, engler distillation not in tower again, the gas that the produces formation spiral that makes progress away, rotation rises to last layer adsorbs once more, prolongs gas running time and distance, advantages of good adsorption effect.
The middle part is provided with packing section, and packing section is packing layer 15 and each one deck float valve tray 6 of upper and lower, and packing layer 15 also can adopt woven wire or metal mesh opening ripple type or the structured packing of metal acanthopore ripple type for metal Bao earrings.The present invention preferably adopts 25 * 25mm metal Bao earrings.The middle part is provided with packing layer 15 main filtrations, filters out the impurity in the gas.
Top is provided with the float valve section, the float valve section is that float valve tray 6 comprises: tower tray outer wall, spherical float valve 27, downflow weir 11, downflow weir 11 is arranged on the two ends of float valve tray 6, whole float valve tray 6 is divided into four zones, the middle part is the float valve district, one side be liquid receiving area 28, opposite side for falling liquid zone 30, bubbling area 29 is arranged on the two ends in float valve district, spherical float valve 27 triangular in shape being distributed in the float valve district.Float valve tray 6 is arranged on the upper and lower of packing layer 15, multilayer is set, preferred 9 layers of the present invention, packing layer 15 upper and lower one decks, and totally seven layers of the 6-12 of packing layer 15 tops, liquid enters liquid receiving area 28 from last layer, enters downflow weir after the float valve district is full, enter and fall the liquid zone, enter the next stage liquid receiving area again.Top is provided with float valve tray 6, plays fractionation, and float valve 27 adopts rounded projections arranged, and even to gas, liquid distribution, the gas-liquid contact area is big, and fractionating effect is good.Gas continues to make progress away after tongue type tower tray 3, packing layer 15 adsorption filtrations, and through float valve tray 6 fractionation, fractionating effect is good.
The quencher 21 that the top is provided with is a jar shape, comprise inlet tube and outlet tube 25,24, two valves 23 and middle cooling tube 19, quencher 21 tops and be higher than that the bottom sets out oil pipe 26, the bottom is provided with and link to each other with the interior top withdrawing fluid distributor 10 (d) of tower body 8 " U " shape return duct.Withdrawing fluid distributor 10 leading sections are tubulose, and the bottom is provided with a plurality of spray holes 32, and this spray hole 32 is arranged, and are uniform three spray holes 32 in 60 ° in the circular section, and spray hole 32 is gone up at withdrawing fluid distributor 10 (d) and laterally formed three rows.Tower body 8 one sides are established cracking still inlet 1 (a), hand hole 2 (b
1), 4 (b
2), 5 (b
3), 7 (b
4), 16 (b
5), opposite side is provided with kerosene efferent duct 12 (e
1), 13 (e
2), diesel oil efferent duct 14 (f
1), 17 (f
2), the top is provided with gaseous phase outlet 9 (c), and the bottom is provided with heavy oil outlet 18 (g) and links to each other with the sediment jar by flange, and the sediment outlet is returned cracking still by pipeline, valve.The top is provided with quencher 21, makes to return cat head and top uprising gas convection current, improves the quality of products, and reduces useless heavy oil and takes place, and improves yield, energy savings.The bottom is provided with the sediment jar, sediment is reclaimed be transported to cracking still again.
In order further to improve the quality of products and yield, tower body 8 sidepieces also can be provided with one or two and quencher 21 identical quenchers, and promptly stage casing quencher, hypomere quencher can be separately positioned on tower body 8 both sides.Tower body 8 outsides also can be provided with pre-thermal jacket.Heating thermal source to tower body 8 can adopt modes such as solar energy or plain cylindrical furnace.
Operation principle and process are as follows: the gas that comes out from cracking still enters tank body 8 by valve 1 (a) bottom → elder generation through 3 → every layer 36 ° of tongue type tower trays through five courses flow form spiral vapour → 180 ° rotation → packing layer 15 filtrations → float valve trays 6 → minute seven courses mobile → by cat head gaseous phase outlet 9 (c) → quencher 21 → substandard product → return tower body 8 through withdrawing fluid distributor 10, exchange the light component petroleum benzin flowline 26 output → heavy ends that make progress through gas-liquid and enter kerosene 12 (e from quencher 21 bottoms
1), 13 (e
2), diesel oil 14 (f
1), 17 (f
2) output → sediment enters the sediment jar through heavy oil outlet 18 (g), returns cracking still by pipeline, valve, forms a working cycles process.
Compared with prior art, have that gas phase media forms spiral in tower body, the time of staying is long, distilling effect good, the collection group Divide separation, decolouring, deodorization, simple in structure, make easy to maintenance, reduced investment, low, the product quality of operating cost Advantages of higher is utilizing expense plastics, expense rubber oil refining industry to have promotional value.
Claims (9)
1, Spiral fractionation tower, comprise: tower body (8), it is characterized in that: three sections of branches are set in the tower body (8), the bottom is a tongue type section, the middle part is a packing section, top is the float valve section, the tongue type section that the bottom is provided with is a tongue type tower tray (3), the middle part packing section is on packing layer (15) reaches, each one deck float valve tray (6) of below, the float valve section that top is provided with is float valve tray (6), tongue type tower tray (3) is tabular, the last a plurality of tongue type wings (31) that are provided with at interval, one end of tongue type wing (31) is fixed, other end perk, form 20-60 ° of degree angle with tongue type tower tray (3), tongue type tower tray (3) is provided with multilayer, every installation one deck is with respect to 20-60 ° of degree of the following parallel rotation of one deck angle, the angular range O-360 of rotation °.
2, Spiral fractionation tower according to claim 1 is characterized in that: the number of plies that tongue type tower tray (3) is provided with is 5 layers.
3, Spiral fractionation tower according to claim 1 and 2, it is characterized in that: angle 22.5-36 ° of tongue type wing (31) perk, angle 22.5-36 ° of the parallel rotation of the every rising one deck of tongue type tower tray (3), to 180 °, one deck coke adsorption layer is laid in tongue type tower tray (3) top.
4, Spiral fractionation tower according to claim 1, it is characterized in that: float valve tray (6) comprising: tower tray outer wall, spherical float valve (27), downflow weir (11), downflow weir (11) is arranged on the two ends of float valve tray (6), whole float valve tray (6) is divided into four zones, the middle part is the float valve district, one side be liquid receiving area (28), opposite side for falling liquid zone (30), bubbling area (29) is arranged on the two ends in float valve district, spherical float valve (27) is triangular in shape to be distributed in the float valve district.
5, according to claim 1 or 4 described Spiral fractionation towers, it is characterized in that: float valve tray (6) is arranged on the upper and lower of packing layer (15), and multilayer is set.
6, Spiral fractionation tower according to claim 5 is characterized in that: the number of plies of the float valve tray of setting (6) is 9 layers, eight layers of packing layer (15) tops, below one deck.
7, Spiral fractionation tower according to claim 1 is characterized in that: a kind of in metal Bao earrings or woven wire or metal mesh opening ripple type or the structured packing of metal acanthopore ripple type of packing layer (15).
8, Spiral fractionation tower according to claim 1, it is characterized in that: quencher (21) is a jar shape, comprise inlet tube and outlet tube (25), (24), two valves (23) and middle cooling tube (19), quencher (21) top and be higher than that the bottom sets out oil pipe (26), the bottom is provided with and link to each other with the interior top withdrawing fluid distributor (10) of tower body 8 " U " shape return duct.
9, according to claim 1 or 8 described Spiral fractionation towers, it is characterized in that: tower body (8) one sides are provided with cracking still inlet (1), opposite side is provided with kerosene efferent duct (12), (13), diesel oil efferent duct (14), (17), bottom and links to each other with the sediment jar by flange, and the sediment outlet is returned cracking still by pipeline, valve.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03132999 CN1262327C (en) | 2003-04-25 | 2003-07-26 | Spiral fractionation tower |
| JP2006521371A JP2007500072A (en) | 2003-07-26 | 2004-06-22 | Spiral rectification tower |
| KR1020067001896A KR100745090B1 (en) | 2003-07-26 | 2004-06-22 | A Helical fractionating column |
| PCT/CN2004/000662 WO2005009583A1 (en) | 2003-07-26 | 2004-06-22 | A helical fractionating column |
| EP04738260A EP1666113A4 (en) | 2003-07-26 | 2004-06-22 | A helical fractionating column |
| US11/341,700 US7695593B2 (en) | 2003-07-26 | 2006-01-28 | Helical fractionating column |
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2003112348.1 | 2003-04-25 | ||
| CN03112348.1 | 2003-04-25 | ||
| CN03112348 | 2003-04-25 | ||
| CN 03132999 CN1262327C (en) | 2003-04-25 | 2003-07-26 | Spiral fractionation tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1483499A CN1483499A (en) | 2004-03-24 |
| CN1262327C true CN1262327C (en) | 2006-07-05 |
Family
ID=34195540
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 03132999 Expired - Fee Related CN1262327C (en) | 2003-04-25 | 2003-07-26 | Spiral fractionation tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1262327C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103820422B (en) * | 2014-02-26 | 2016-02-03 | 中南林业科技大学 | A kind of method improving mould cellulase-producing |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100355475C (en) * | 2005-09-22 | 2007-12-19 | 上海天之冠可再生能源有限公司 | Highly efficient distilling filled tower |
| CN102391887B (en) * | 2011-09-29 | 2014-02-19 | 牛晓璐 | Dust cleaning mechanism and pyrolysis apparatus with same |
| CN110434240B (en) * | 2019-08-06 | 2024-02-23 | 嘉兴学院 | Automatic installing machine for toothed edge floating valve of chemical tower tray |
-
2003
- 2003-07-26 CN CN 03132999 patent/CN1262327C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103820422B (en) * | 2014-02-26 | 2016-02-03 | 中南林业科技大学 | A kind of method improving mould cellulase-producing |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1483499A (en) | 2004-03-24 |
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| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20060705 |
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| CF01 | Termination of patent right due to non-payment of annual fee |