CN102008832B - Device for directly exchanging heat of oil and gas - Google Patents
Device for directly exchanging heat of oil and gas Download PDFInfo
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- CN102008832B CN102008832B CN 200910170139 CN200910170139A CN102008832B CN 102008832 B CN102008832 B CN 102008832B CN 200910170139 CN200910170139 CN 200910170139 CN 200910170139 A CN200910170139 A CN 200910170139A CN 102008832 B CN102008832 B CN 102008832B
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Abstract
The invention belongs to equipment for directly exchanging the heat of oil and gas in the petrochemical industry, in particular to an anti-coking high-efficiency heat-exchanging plate for directly exchanging the heat of high-temperature oil and gas with liquid oil and having the mass transfer function. The device comprises a heat-exchanging plate (1) with a cambered longitudinal cross section, and a group of holes is formed on the oil-gas exchanging surface of the heat-exchanging plate (1). In the invention, holes are respectively made at the top and both sides of the cambered heat-exchanging plate, the positions, the angles, the shapes, the sizes and the number of the holes on the cambered heat-exchanging plate are determined according to the flow and the property of a heat-exchanging medium with the consideration of the heat transfer efficiency and the mass transfer efficiency as well as the flushing action on coke powder. The cambered heat-exchanging plate is processed and manufactured by adopting a circular steel tube, uses material easily obtained, is easy to manufacture and mount and has higher strength.
Description
Technical field
The invention belongs to the equipment that is used for the oil gas direct heat transfer in the petroleum chemical industry, relate in particular to a kind of anti-coking high efficient heat exchanging plate that is used for high-temperature oil gas and liquid oil direct heat transfer and possesses mass transfer function.
Background technology
The equipment of high-temperature oil gas and liquid oil direct heat transfer mainly contains both at home and abroad at present: chevron shaped baffle plate, duck tongue type baffle plate, tray deck, structured packing and random packing, its main shape is seen Fig. 1-4.
As shown in Figure 1, chevron shaped baffle plate is made up of chevron shaped according to certain angle two rectangular flats, and several chevron shaped baffle plate horizontal arrangement are formed one deck heat exchange unit, generally is installed in by 3～8 layers of heat exchange unit to be used for oil gas and liquid oil direct heat transfer in the tower.According to the size of tower diameter and size, the quantity of chevron shaped baffle plate and the number of plies of chevron shaped baffle plate of the definite rectangular flat of heat exchange load.Chevron shaped baffle plate is higher to the levelness and the liquid distribution uniformity requirement of installing, and the heat transfer of chevron shaped baffle plate and mass-transfer efficiency are all very low, is prone to cause liquid bias current and hot-spot to produce coking.
Duck tongue type baffle plate shown in Figure 2 is the improvement on chevron shaped baffle plate basis; For preventing that the liquid bias current is provided with oil sump tank at the liquid outlet of plate, downflow weir is established in the oil sump tank outlet, and the oil sump tank bottom has sieve aperture; A common plate is as one deck; Interlaced arrangement up and down, purpose of design are liquid and the gas contact heat-exchangings of cross-flow under the sieve aperture spray, the bias current of having avoided the liquid distribution inequality to cause.Result of use shows that when operation medium contains coke powder or catalyst granules oil sump tank deposition coke powder or catalyst granules stop up the sieve aperture influence and conduct heat; This duck tongue type baffle plate does not have mass transfer effect basically in addition, and the part distillate product in the gas phase can be absorbed and the entering liquid phase by the liquid phase oil product of heavy, causes part light distillate circulation, the waste energy; Duck tongue type baffle plate has bigger liquid flow zone, and this zone can not directly contact with gas, influences the heat exchange effect.
As shown in Figure 3; Tray deck is the square type or lacks the equipment that has fixing or float trap on the round plate, in order to adapt to the different operation operating mode, is main purpose to improve mass-transfer efficiency; The size of perforate and float trap and shape vary on the column plate; Its principal character is that plate is a square type or scarce round, and level is installed, and gas and liquid is the transmission of heat by contact mass transfer on column plate.Because the use of tray deck is with strong points, complex structure, characteristics that installation requirement is high; Fluctuation adaptability to gas on the plate and liquid load is relatively poor; Gas or liquid load are excessive or too smallly all can not normally use; Therefore and stop up because of gathering coke powder easily, seldom be used for the direct heat transfer of high-temperature oil gas and liquid oil at the bottom of the fractionating column.
As shown in Figure 4; Filler is the variform mass-and heat-transfer element that is formed by thin steel plate or steel band compacting, is divided into structured packing and random packing, is installed in the tower according to certain height and arrangement mode; Filler is had relatively high expectations to gas and distribution of liquid, and charging will be provided with distributor usually.Be generally used for oil product fractionation, absorption and extraction operating mode, mass-and heat-transfer efficient is higher, owing to must use by the configuration distributor, equipment manufacturing cost is higher, and stops up because of gathering coke powder easily, and is relatively poor to the adaptability for working condition that gas or liquid impurity content are more.Also seldom be used at present the direct heat transfer of high-temperature oil gas and liquid oil at the bottom of the fractionating column.
To sum up; In the prior art; Being used for one of common problem of chevron shaped baffle plate and the duck tongue type baffle plate of oil gas direct heat transfer is to be easy to take place coking on the heat exchange baffle plate; This mainly is an one of which: because the oil gas temperature is higher, and the character of liquid phase oil product is relatively poor, and directly the liquid phase oil product is understood polymerization reaction take place usually and generated coke during contact heat-exchanging; Its two: because the fault of construction of heat exchange baffle plate, fluid on the heat exchange baffle plate is distributed and heat distribution inhomogeneous, cause hot-spot.Its three: because the heat exchange baffle plate do not have the self-cleaning function, the coke powder that carries in the high-temperature oil gas can gather on the heat exchange baffle plate.Two of common problem is that the heat exchange baffle plate does not have mass transfer function basically; When high-temperature oil gas and liquid oil heat exchange; Part distillate product in the gas phase can be absorbed and the entering liquid phase by the liquid phase oil product of heavy, causes the circulation of part distillate, not only wastes fuel consumption and power consumption; And have influence on the yield of the liquid of gaseous products after fractionation, cause the certain economic loss.Three of common problem is that heat exchange baffle design, manufacturing and installation are complicated, and service life is shorter.
And in the prior art, what be used for the oil gas direct heat transfer also has the square type or lacks tray deck, structured packing and the random packing that has fixing or float trap on the round plate.The design main purpose of tray deck, structured packing and random packing is to be used for separating of oil product; Mass-transfer efficiency is higher; Being used for one of common problem of oil gas direct heat transfer is that tray deck is that level is installed, and gathers coke powder on the plate easily, and the perforate on the blocking plate influences normal running; The passage of structured packing and random packing is less, also stops up because of gathering coke powder than being easier to, and is relatively poor to the adaptability for working condition that gas or liquid impurity content are more.Two of common problem is that tray deck, structured packing and random packing are relatively poor to the fluctuation adaptability of gas on the plate and liquid load, and gas or liquid load are excessive or too smallly all can not normally use.Three of common problem is that the manufacturing of tray deck, structured packing and random packing requires height, installation more complicated, service life is short, cost is higher.
Summary of the invention
The present invention is in order to solve the technical problem that exists in the above-mentioned prior art; A kind of problem that exists based on above-mentioned prior art is provided, develop a kind of operating flexibility big, strong to the fluctuation adaptability of gas and liquid load, prevent coking and gather coke powder, investment saving long service life, easy for installation, heat transfer efficiency is high and the equipment that is used for the oil gas direct heat transfer of certain mass-transfer performance is arranged.The inventor has researched and developed a kind of device that is used for the oil gas direct heat transfer.The present invention has designed and has had heat transfer, mass transfer on a kind of arc of arcuate structure and from the anti-coking high efficient heat exchanging plate of flushing hole; Overcome the unreasonable of existing heat exchange baffle arrangement form or have certain defective; Be used for high-temperature oil gas and the direct heat transfer of liquid phase oil product, can alleviate the coking and the heat and mass efficient that increases the heat exchange baffle plate of heat exchange baffle plate.
The present invention realizes through following technical scheme,
A kind of device that is used for the oil gas direct heat transfer, said device includes heat exchanger plates 1, and said heat exchanger plates 1 curve form is a spherical crown; The oil gas exchange face of said heat exchanger plates 1 is provided with one group of perforate.
The arc radius of said circular arc heat exchanger plates 1 is 10 millimeters～500 millimeters, and the corresponding central angle of arc length is 30～180 °.
Said one group of perforate comprises the top drilling group, and promptly top drilling 2 is arranged on circular arc heat exchanger plates 1 top, and top drilling 2 is shaped as a kind of in circle, triangle, square, rectangle, the polygon; The top drilling area accounts for 0.3～8% of circular arc heat exchanger plates surface area.
In order more to help conducting heat and mass transfer, said one group of perforate also comprises the side groups of openings, i.e. side perforate 2 ' is arranged on around the side of heat exchanger plates 1 circular arc oil gas exchange face; And side perforate 2 ' is shaped as a kind of in circle, square, triangle rectangle and the polygon, and the side perforated area accounts for 0.5～10% of circular arc heat exchanger plates surface area.The shape of perforate, direction, size and quantity more help heat transfer, mass transfer and the flushing certainly of heat exchanger plates, improve heat and mass efficient, prevent the heat exchanger plates coking.
Select polylith circular arc heat exchanger plates horizontal arrangement to form one deck heat exchange flaggy according to different gas-liquid loads and specification of equipment. be several piece circular arc heat exchanger plates horizontal arrangement; Form one deck heat exchange flaggy; Every circular arc heat exchanger plates two is fixed on Ta Bishang through the circular arc fixture; Promptly on the tower wall, weld the circular arc fixture, the fixture overlap joint on circular arc heat exchanger plates two ends and the tower wall is also used bolt.Multilayer circular arc heat exchange flaggy vertical direction is put heat and mass unit of composition by certain distance and is installed in the fractionating column.Every heat exchange flaggy is fixing respectively separately, does not have connector between the multilayer heat exchange flaggy.
Described polylith circular arc heat exchanger plates horizontal arrangement is formed one deck heat exchange flaggy, and the distance at adjacent heat exchanger plates edge is 0～2 times of the profound length of circular arc, and every layer mass-transfer efficiency reaches 10～20%.Described multilayer circular arc heat exchange flaggy vertical direction arranges that by certain distance forming a heat and mass unit is that a heat and mass unit is made up of 2～10 layers of heat exchanger plates, and the distance minimum between every layer is the distance on two circular arc limit tangent line joinings and circular arc summit.
The present invention has the hole at circular arc heat exchanger plates top and both sides; The position of perforate, angle, shape, size and quantity on the circular arc heat exchanger plates; Flow and character according to heat transferring medium are confirmed, should consider to conduct heat and mass-transfer efficiency, consider the flushing action to coke powder again.The circular arc heat exchanger plates adopts the round steel pipe processing and manufacturing, draws materials conveniently, makes and installs easily, and intensity is higher, and service life is longer; Above-mentionedly drawing materials easily manufacturedly, is to adopt common steel alloy or carbon steel piping cutting just can make; Above-mentioned installation is fixing the getting final product in this camber plate two in tower easily; Above-mentioned intensity higher service life, length was that the wall thickness of alloy pipe is generally big than general steel plate.The use of this heat exchanger plates is formed one deck by polylith arc anti-coking high efficient heat exchanging plate, forms a heat and mass unit by several layers.
A kind of oil gas direct heat transfer device that is used for of the present invention has following effect:
The one, circular arc heat exchanger plates top and both sides have the hole, have both improved heat transfer and mass-transfer efficiency, and the coke powder of exchanging again on the hot plate has flushing action, prevent the heat exchanger plates coking, and are favourable to the extension fixture on-stream time.
The 2nd, this heat exchanger plates adopts common steel alloy or carbon steel piping cutting just can make, and is convenient at the oil plant material source, can gather materials on the spot and the field machining manufacturing.
The 3rd, the circular arc heat exchanger plates is higher than dull and stereotyped intensity, and is easy for installation, and prolong service life, reduces the operating cost because of the high temperature corrosion frequent change.
Description of drawings
Fig. 1 is a herringbone heat exchange baffle plate sketch map in the prior art;
Fig. 2 is a duck ligulate heat exchange baffle plate sketch map in the prior art;
Fig. 3 is a tray deck sketch map in the prior art;
Fig. 4 is whole filler and a random packing sketch map in the prior art;
Fig. 5 is a heat-exchanger rig structural representation of the present invention.
The content of above-mentioned each width of cloth accompanying drawing will combine the background technology and the specific embodiment to explain.
Among Fig. 1: A is the liquefaction oil product; B is a high-temperature oil gas; 101 is herringbone damper modules unit; 102 is fractionating column; 103 is one deck chev(e)ron baffle; 104 is the monolithic chev(e)ron baffle
Among Fig. 2: A is the liquefaction oil product; B is a high-temperature oil gas; 201 is duck tongue font damper modules unit; 202 is fractionating column; 203 is one deck duck tongue font baffle plate; 204 is monolithic duck tongue font baffle plate;
Among Fig. 3, A is the liquefaction oil product; B is a high-temperature oil gas; 301 is fractionating column; 302 is tray deck; 303 is seal pot; 304 is downspout;
Among Fig. 4, A is the liquefaction oil product; B is a high-temperature oil gas; 401 is liquid distribution trough; 402 is regular mellapak packing; 403 is fractionating column; 404 are random packing; 405 is single random packing;
Among Fig. 5, A is the liquefaction oil product; B is a high-temperature oil gas; 1 is the circular arc heat exchanger plates, and 2 is top drilling, and 2 ' is the side perforate; 3 are the heat exchange flaggy; 4 is fractionating column.
1# in above-mentioned each width of cloth accompanying drawing, which number of plies 2# etc. represent.
The specific embodiment
As shown in Figure 5, a kind of oil gas direct heat transfer device that is used for comprises the circular arc that is shaped as of heat exchanger plates 1, and the perforate 2 that makes progress of the top of described circular arc heat exchanger plates 1, side perforate 2 '.Described heat exchanger plates 1 selects polylith circular arc heat exchanger plates level to put composition one deck heat exchange flaggy 3 according to gas-liquid load and specification of equipment.Described heat exchange flaggy 3 selects multilayer circular arc heat exchanger plates vertical direction to put heat and mass unit 4 of composition according to gas-liquid load and specification of equipment.
Described circular arc heat exchanger plates 1, arc radius are 10 millimeters～500 millimeters, and the corresponding central angle of arc length is 30～180 °.Being shaped as of the perforate 2 that said circular arc heat exchanger plates top makes progress is circular, square, a kind of in the rectangle, triangle, polygon, and perforated area accounts for 0.3～8% of circular arc heat exchanger plates surface area.Being shaped as of said circular arc heat exchanger plates side perforate 2 ' is circular, square, a kind of in the rectangle, triangle, polygon, perforated area accounts for 0.5～10% of circular arc heat exchanger plates surface area.Arc anti-coking high efficient heat exchanging plate of the present invention has the heat exchanger plates of raising and conducts heat and mass-transfer efficiency, prevents the characteristics of heat exchanger plates coking extension fixture on-stream time.
Embodiment:
Shown in accompanying drawing 5, the described heat exchanger plates 1 that is shaped as circular arc adopts 426 millimeters of overall diameters, the pipe manufacturing that wall thickness is 8 millimeters, and the circular arc interior diameter is 410 millimeters, the corresponding central angle of arc length is 120 °, 429 millimeters of arc length, 355 millimeters of the profound length of arc; Hole is upwards opened at described circular arc heat exchanger plates top, and for the circular port of 10 millimeters of diameters, to the fractionating column of 4.2 rice diameters, 200 of number of aperture are evenly arranged at the longest heat exchanger plates top, centre, and perforated area accounts for 0.91% of circular arc heat exchanger plates surface area; Described circular arc heat exchanger plates side perforate; For respectively opening a round in both sides, angle is 60 ° in the center of circle, horizontal opened round hole; 8 millimeters in aperture; To the fractionating column of 4.2 rice diameters, the longest heat exchanger plates both sides number of aperture in centre amounts to 400 and even layout, and perforated area accounts for 1.82% of circular arc heat exchanger plates surface area; Described polylith circular arc heat exchanger plates level is put and is formed one deck heat exchange flaggy 3; Fractionating column to 4.2 rice diameters; The distance at adjacent heat exchanger plates edge is designed to nearly a times 350 millimeters of profound length; Arrange 6 heat exchanger plates .6 piece circular arc heat exchanger plates horizontal arrangement for every layer, form one deck heat exchange flaggy, every circular arc heat exchanger plates two is fixed on Ta Bishang through the circular arc fixture; Promptly on the tower wall, weld the circular arc fixture, the fixture overlap joint on circular arc heat exchanger plates two ends and the tower wall is also used bolt.Described every distance minimum between two-layer is the distance on two circular arc limit tangent line joinings and circular arc summit, and the distance on these routine two circular arc limit tangent line joinings and circular arc summit is 450 millimeters, and this example designs according to 700 millimeters, forms a heat exchange unit by 5 layers.Every heat exchange flaggy is fixing respectively separately, does not have connector between each layer heat exchange flaggy.The present invention is used for the desuperheating of evaporator section high-temperature oil gas at the bottom of the delayed coker fractionator, can alleviate the coking and the heat and mass efficient that increases the heat exchange baffle plate of heat exchange baffle plate, the extension fixture operation cycle, improves the apparatus processes ability.
Technique scheme and embodiment are one embodiment of the present invention; For those skilled in the art; On the basis that the invention discloses application process and principle, be easy to make various types of improvement or distortion, and be not limited only to the described method of the above-mentioned specific embodiment of the present invention; Therefore the mode of front description is preferably, and does not have restrictive meaning.
Claims (3)
1. device that is used for the oil gas direct heat transfer; It is characterized in that; Said device comprises a mass-and heat-transfer unit, and said mass-and heat-transfer unit comprises one group of heat exchange flaggy (3) at least, and said each heat exchange flaggy (3) comprises a described heat exchanger plates (1) at least; And said heat exchanger plates (1) curve form is a spherical crown, and the oil gas exchange face of said heat exchanger plates (1) is provided with one group of perforate;
The arc radius of said heat exchanger plates (1) is 10 millimeters～500 millimeters, and the corresponding central angle of arc length is 30 °～180 °;
Said one group of perforate comprises the top drilling group, and promptly top drilling (2) is arranged on heat exchanger plates (1) top; And said top drilling (2) is shaped as a kind of in circle or the polygon; The top drilling area accounts for 0.3～8% of circular arc heat exchanger plates surface area;
Said one group of perforate also comprises the side groups of openings, i.e. side perforate (2 ') is arranged on around the side of heat exchanger plates (1) circular arc oil gas exchange face; Said side perforate (2 ') is shaped as a kind of in circle or the polygon, and the side perforated area accounts for 0.5～10% of circular arc heat exchanger plates surface area.
2. a kind of device that is used for the oil gas direct heat transfer according to claim 1 is characterized in that,
Said each heat exchange flaggy (3) is that one group of said heat exchanger plates (1) horizontal arrangement is formed; And the distance at adjacent heat exchanger plates (1) edge is 0～2 times of the profound length of said heat exchanger plates circular arc.
3. a kind of device that is used for the oil gas direct heat transfer according to claim 1 is characterized in that,
Said mass-and heat-transfer unit comprises 2～10 groups of heat exchange flaggies (3), and respectively organizes heat exchange flaggy (3) parallel arrangement, and the distance between every group of heat exchange flaggy (3) is more than or equal to the distance on two heat exchanger plates circular arc limit tangent line joinings and heat exchanger plates circular arc summit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910170139 CN102008832B (en) | 2009-09-04 | 2009-09-04 | Device for directly exchanging heat of oil and gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200910170139 CN102008832B (en) | 2009-09-04 | 2009-09-04 | Device for directly exchanging heat of oil and gas |
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| Publication Number | Publication Date |
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| CN102008832A CN102008832A (en) | 2011-04-13 |
| CN102008832B true CN102008832B (en) | 2012-12-26 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 200910170139 Active CN102008832B (en) | 2009-09-04 | 2009-09-04 | Device for directly exchanging heat of oil and gas |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104556279B (en) * | 2014-12-26 | 2018-07-17 | 巴布科克环境工程江苏有限公司 | A kind of board-like seawater desalination system liquid distributor |
| CN111396739A (en) * | 2020-04-20 | 2020-07-10 | 贵州电网有限责任公司 | Novel gas storage device and method in constant pressure ratio operation mode |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85106705A (en) * | 1985-08-31 | 1986-07-09 | 西安交通大学 | Low-temperature fractionating tower |
| CN1276253A (en) * | 1999-06-03 | 2000-12-13 | 株式会社日本触媒 | Purification tower and purification method for organic compound containing easily-clogged substance |
| CN1559903A (en) * | 2004-02-20 | 2005-01-05 | 自贡鸿鹤化工股份有限公司 | Carbonators with sieve-plate and hat shape mixture structure for preparing alkali by combined alkali process |
| CN101284191A (en) * | 2008-06-04 | 2008-10-15 | 天津市职业大学 | Electric heating membrane insulated glass compose distillation tower |
| CN201154242Y (en) * | 2007-10-18 | 2008-11-26 | 上海同特化工科技有限公司 | Vaporizing plate for updating liquid surface |
-
2009
- 2009-09-04 CN CN 200910170139 patent/CN102008832B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85106705A (en) * | 1985-08-31 | 1986-07-09 | 西安交通大学 | Low-temperature fractionating tower |
| CN1276253A (en) * | 1999-06-03 | 2000-12-13 | 株式会社日本触媒 | Purification tower and purification method for organic compound containing easily-clogged substance |
| CN1559903A (en) * | 2004-02-20 | 2005-01-05 | 自贡鸿鹤化工股份有限公司 | Carbonators with sieve-plate and hat shape mixture structure for preparing alkali by combined alkali process |
| CN201154242Y (en) * | 2007-10-18 | 2008-11-26 | 上海同特化工科技有限公司 | Vaporizing plate for updating liquid surface |
| CN101284191A (en) * | 2008-06-04 | 2008-10-15 | 天津市职业大学 | Electric heating membrane insulated glass compose distillation tower |
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| CN102008832A (en) | 2011-04-13 |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Sinopec Engineering Incorporation Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Engrg Construction Co., SINOPEC |
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Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: SINOPEC Group Patentee after: Sinopec Engineering Construction Co., Ltd Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: Sinopec Engineering Construction Co., Ltd |
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