CN210464112U - Heat exchange plate for directly exchanging heat between gas and liquid - Google Patents
Heat exchange plate for directly exchanging heat between gas and liquid Download PDFInfo
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- CN210464112U CN210464112U CN201920967869.1U CN201920967869U CN210464112U CN 210464112 U CN210464112 U CN 210464112U CN 201920967869 U CN201920967869 U CN 201920967869U CN 210464112 U CN210464112 U CN 210464112U
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Abstract
The utility model provides a heat transfer board for gaseous and the direct heat transfer of liquid, the shape of heat transfer board is round platform shape, round platform shape heat transfer board have positive round platform shape heat transfer board (1) and radius platform shape heat transfer board (2). The right circular truncated cone-shaped heat exchange plate (1) and the reverse circular truncated cone-shaped heat exchange plate (2) are adjacently installed up and down in the tower. A heat exchange unit is formed by one regular circular truncated cone-shaped heat exchange plate (1) and an adjacent inverse circular truncated cone-shaped heat exchange plate (2), and the number of the heat exchange units and the specification and the size of the heat exchange plates are determined according to gas-liquid flow and heat exchange load. The liquid of the round platform-shaped heat exchange plate flows downwards along the circumference and is uniformly distributed; the gas flows from the center to the periphery or from the periphery to the center, and bias flow is not generated. The length of the gas-liquid contact surface of the truncated cone-shaped heat exchange plate is larger, and the contact heat exchange area of gas and liquid is increased. The round platform-shaped heat exchange plate can be rolled by steel plates, and has the advantages of convenient material taking, easy manufacture and installation and higher strength.
Description
Technical Field
The utility model relates to a heat transfer field of high temperature oil gas and oil in delayed coking device blowing empty tower or fractionating tower among the petrochemical trade mainly relates to a heat transfer board that is used for gaseous and the direct heat transfer of liquid.
Background
At present, the heat exchange equipment for high-temperature oil gas and oil products in a steam blowing emptying tower or a fractionating tower of a delayed coking device at home and abroad mainly comprises: the main shapes of the circle-lacking baffle, the herringbone baffle and the duck tongue baffle are shown in figures 1-3.
As shown in fig. 1, the circle-lacking baffle is a flat plate with a part cut off according to the process requirements, the circle-lacking plate is horizontally installed or has a certain inclination angle according to the liquid flow direction, the liquid of the upper layer plate automatically flows to the lower layer, and is contacted with high-temperature gas in a cross flow manner in the process that the liquid flows downwards, so that heat exchange is realized, the gas is cooled, and the liquid is heated. Generally, 10-14 layers of heat exchange plates are arranged in the emptying tower and used for direct heat exchange of steam-blowing emptying gas and tower top reflux liquid, and 6-8 layers of heat exchange plates are arranged in the fractionating tower and used for direct heat exchange of high-temperature oil gas and liquid oil. And determining the number of the heat exchange baffles according to the size of the tower diameter and the heat exchange load. The heat exchange area of the high-temperature oil gas and the low-temperature oil product of the circle-lacking baffle plate is mainly determined by the overflow length of the outlet side of the heat exchange plate and the plate interval. In order to increase the heat exchange area, the overflow length needs to be increased, but the overflow length is limited by the diameter of the tower, or the plate spacing is increased and the overflow length is influenced by the height of the tower. In addition, the liquid flow paths on the circle-lacking baffle plates are different in length, so that the integral overflow strength is easily uneven, and the heat exchange effect is influenced.
As shown in figure 2, the herringbone baffle plate is formed into a herringbone shape by two rectangular flat plates according to a certain angle, a plurality of herringbone baffle plates are horizontally arranged to form a layer of heat exchange unit, generally 10-14 layers of heat exchange units are arranged in the emptying tower, and 3-5 layers of heat exchange plates are arranged in the fractionating tower and used for direct heat exchange of oil gas and liquid oil products. And determining the size of the rectangular flat plate, the number of the herringbone baffles and the number of layers of the herringbone baffles according to the size of the tower diameter and the heat exchange load. Each layer of herringbone baffle plate is composed of single plates formed by a plurality of two rectangular flat plates, the manufacturing precision and the installation levelness of each herringbone baffle plate are difficult to be consistent, the uniformity of gas and liquid distribution can be influenced, and the contact heat exchange effect can be influenced if liquid or gas flows in a bias mode.
The duck tongue type baffle shown in figure 3 is an improvement on a herringbone baffle, an oil collecting tank is arranged at a liquid outlet of a plate for preventing liquid from flowing obliquely, an overflow weir is arranged at the outlet of the oil collecting tank, sieve holes are formed in the bottom of the oil collecting tank, one plate is usually used as a layer and is arranged in a vertically staggered mode, the design aim is to contact and exchange heat between the liquid sprayed by the sieve holes and gas of cross flow, and the oblique flow caused by uneven liquid distribution is avoided. The use effect shows that when the operation medium contains coke powder or catalyst particles, the coke powder or the catalyst particles deposited in the oil collecting tank block the sieve pores to influence heat transfer; the duck tongue type baffle has a larger liquid flowing area, and the area can not be in direct contact with gas, so that the heat exchange effect is influenced.
In summary, in the prior art, one of the common problems of the round-missing baffle, the herringbone baffle and the duck tongue type baffle for direct heat exchange of oil gas is that gas or liquid on the heat exchange baffle is not uniformly distributed, bias flow is easy to occur, the heat exchange effect is affected, and coking is easy to occur due to over-temperature when the liquid is heavy oil. This is mainly one of them: because the temperature of oil gas is high and the property of liquid-phase oil is poor, the liquid-phase oil usually undergoes a polymerization reaction to generate coke when directly contacting and exchanging heat; the second step is as follows: due to the structural defects of the heat exchange baffle, the fluid distribution and the heat distribution on the heat exchange baffle are not uniform, and local overheating is caused. The second common problem is that the heat exchange efficiency of the heat exchange baffle is low, and in order to meet the heat exchange requirement, more heat exchange plates must be adopted, thus increasing the engineering investment. The third common problem is that the installation strength of the heat exchange plate is low due to the structural problem of the heat exchange baffle, the heat exchange plate falls off when the gas load is increased,
SUMMERY OF THE UTILITY MODEL
The utility model discloses a solve the technical problem that exists among the above-mentioned prior art, provide a problem that exists based on above-mentioned prior art, develop a gas-liquid heat transfer area big, gas and liquid distribution are even, the fluctuation strong adaptability of heat transfer load, investment save long service life, simple to operate, heat transfer efficiency are high be used for the equipment of the direct heat transfer of gas and liquid. The utility model discloses a heat transfer board that is used for gaseous and liquid direct heat transfer has been researched and developed. The utility model discloses a high-efficient heat transfer board of round platform shape structure overcomes unreasonable or certain defect that exists of current heat transfer baffle structural style for the direct heat transfer of high temperature oil gas and liquid phase oil, under the same condition of gas flow, liquid flow and heat load, through the quantity that improves heat transfer efficiency in order to reduce the heat transfer board.
The utility model is realized by the following technical proposal,
the heat exchange plate for direct heat exchange between gas and liquid is in the shape of circular truncated cone, and has one heat exchange plate in the shape of circular truncated cone and one heat exchange plate in the shape of circular truncated cone. The heat exchange unit is formed by a right circular truncated cone-shaped heat exchange plate and an adjacent reverse circular truncated cone-shaped heat exchange plate, liquid flows downwards along the inclined surface of the right circular truncated cone-shaped heat exchange plate, and gas flows to a peripheral circular ring from the axis of the tower.
Preferably, the diameter phi of the upper circle of the right circular truncated cone-shaped heat exchange plate (1)1Is less than the diameter phi of the lower circle2The diameter phi of the upper circle of the heat exchange plate (2) with the shape of an inverted frustum3Is greater than the diameter phi of the lower circle4The upper and lower cone angles of the extension of the regular circular truncated cone-shaped heat exchange plate (1) and the extension of the inverted circular truncated cone-shaped heat exchange plate (2) are both 30-150 degrees.
Preferably, the diameter phi of the upper circle of the right circular truncated cone-shaped heat exchange plate (1)1As small as possible, diameter of lower circle phi2The method needs to be determined according to gas-liquid load in the tower and the diameter of the tower; the diameter phi of the upper circle of the inverted frustum-shaped heat exchange plate (2)3The diameter of the lower circle is equal to the diameter of the tower4The diameter phi of the lower circle of the heat exchange plate (1) in the shape of a right circular truncated cone2And (5) the consistency is achieved.
Preferably, when the right circular truncated cone-shaped heat exchange plate (1) is used as a liquid material feeding plate, the diameter phi of an upper circle1Suitably enlarged, and welded thereto.
Preferably, the feeding distributor welded on the right circular table-shaped heat exchange plate (1) consists of a feeding pipe connecting flange (3), a feeding pipe (4), a rectifying tank (5) and a discharging port (6). The feeding pipe connecting flange (3) of the feeding distributor is connected with the liquid phase feeding pipe flange, the discharging port (6) is a square or circular hole which is formed in the horizontal direction of the side face of the lower part of the feeding pipe (4), the total area of the holes is larger than the sectional area of the feeding pipe, and the circumferential edge of the upper outlet of the rectifying groove (5) must be horizontal.
Drawings
FIG. 1 is a schematic view of a prior art heat exchange baffle having a shape of a missing circle;
FIG. 2 is a schematic view of a chevron heat exchange baffle of the prior art;
FIG. 3 is a schematic view of a prior art duck-tongue heat exchange baffle;
fig. 4 is a schematic structural view of the heat exchange device of the present invention.
The contents of the above-described drawings are to be considered in connection with the background and the detailed description.
In fig. 1: a is a liquefied oil product; b is high-temperature oil gas; 101 is a baffle plate module unit with a shape of a broken circle; 102 is a column; 103 is a layer of baffle plate with a shape of missing a circle; 104 is an assembly of out-of-round baffles.
In fig. 2: a is a liquefied oil product; b is high-temperature oil gas; 201 is a herringbone baffle module unit; 202 is a column; 203 is a layer of herringbone baffle; 204 is a single herringbone baffle
In fig. 3: a is a liquefied oil product; b is high-temperature oil gas; 301 is a duck tongue shaped baffle plate module unit; 302 is a column; 303 is a layer of baffle shaped like a duck tongue; 304 is a single canard-shaped baffle;
in FIG. 4, A is the liquefied oil; b is high-temperature oil gas; 1 is a right circular truncated cone-shaped heat exchange plate; 2 is an inverted frustum-shaped heat exchange plate; 3 is a feeding connecting pipe flange; 4 is a feeding pipe; 5 is a rectifying tank; 6 is a discharge hole; 7 is a tower; phi 1 is the diameter of the upper circle of the right circular truncated cone-shaped heat exchange plate; phi 2 is the diameter of the lower circle of the right circular truncated cone-shaped heat exchange plate; phi 3 is the upper circle diameter of the inverted frustum-shaped heat exchange plate; phi 4 is the lower circle diameter of the inverted frustum-shaped heat exchange plate.
In the above drawings, 1#, 2#, etc. indicate the number of layers.
Detailed Description
As shown in fig. 4, the heat exchange plate for directly exchanging heat between gas and liquid is in the shape of a truncated cone, and the truncated cone-shaped heat exchange plate is provided with a right truncated cone-shaped heat exchange plate 1 and an inverted truncated cone-shaped heat exchange plate 2. The diameter phi of the upper circle of the right circular truncated cone-shaped heat exchange plate 11Is less than the diameter phi of the lower circle2Upper diameter phi of heat exchange plate with inverted circular truncated cone shape3Is greater than the diameter phi of the lower circle4The upper and lower cone angles of the regular circular truncated cone-shaped heat exchange plate and the inverted circular truncated cone-shaped heat exchange plate 2 are both 30-150 degrees.
Aiming at an emptying tower 7 with the diameter of 4 meters, the total number of the heat exchange plates is determined to be 4 layers according to the gas flow and the temperature as well as the liquid flow and the temperature, and the emptying tower is composed of two layers of heat exchange plates with the shape of a right circular truncated cone and two layers of heat exchange plates with the shape of an inverted circular truncated coneThe area of the lower circle of the right circular truncated cone-shaped heat exchange plate is about 1/2 of the cross section area of the tower, so that the diameter phi of the lower circle of the right circular truncated cone-shaped heat exchange plate is determined22.8 m, the diameter phi of the upper circle of the right circular truncated cone-shaped heat exchange plate based on manufacturing and installation factors1Determined to be 0.4 m; upper circle diameter phi of inverted frustum-shaped heat exchange plate3The diameter of the lower circle phi of the heat exchange plate is 4 m and is the same as the diameter of the tower4And phi2Equal to 2.8 meters, and the upper and lower cone angles of the regular circular truncated cone-shaped heat exchange plate and the inverted circular truncated cone-shaped heat exchange plate are both designed to be 135 degrees.
The top layer of the right circular table-shaped heat exchange plate is used as a liquid feeding plate, the specification of a feeding connecting pipe flange is DN100 according to the calculation of liquid flow, the specification of a feeding pipe is DN100, a discharging port is a hole which is provided with 100 mm height and 30 mm width in four directions at the lower part of the feeding pipe, a rectifying groove is cylindrical, the diameter of the cylinder is 0.4 meter, and the height of the cylinder is 0.6 meter.
Based on the round table-shaped heat exchange plates, the area of the outer surface of the round table of a single right round table-shaped heat exchange plate is 6.53 square meters, the area of the outer surface of the round table of a single reverse round table-shaped heat exchange plate is 5.445 square meters, and the difference between the area of the outer surface of the round table of the single reverse round table-shaped heat exchange plate and the area of the outer surface of the round table of the semi-circular heat exchange. The liquid of the round platform-shaped heat exchange plate flows downwards along the circumference and is uniformly distributed; the liquid overflow of the round table-shaped heat exchange plate is 8.79 meters along the circumference of the round table, which is doubled compared with the liquid overflow of the semicircular heat exchange plate along the length of 4 meters, namely the contact area of gas and liquid is doubled. The gas flows from the center of the tower to the surrounding circular ring and is distributed relatively uniformly. The utility model is used for delayed coking blows the oil gas of vapour evacuation tower and the heat transfer of liquid oil, can reduce 6 layers of round platform shape heat transfer boards by conventional 12 layers semi-circular heat transfer baffle, because gaseous and liquid distribution are even, can alleviate the coking and the scale deposit of heat transfer board simultaneously, extension device operation cycle, improvement device throughput.
The above technical solution and embodiments are only one embodiment of the present invention, and it is easy for those skilled in the art to make various modifications or variations based on the application method and principle of the present invention, rather than to limit the invention to the method described in the above embodiments of the present invention, so that the above described method is preferred and not restrictive.
Claims (4)
1. The utility model provides a heat transfer board for gaseous and liquid direct heat transfer which characterized in that, the shape of heat transfer board is round platform shape, round platform shape heat transfer board have positive round platform shape heat transfer board (1) and inverted circular platform shape heat transfer board (2), adjacent installation about in the tower, a heat transfer unit is constituteed with adjacent inverted circular platform shape heat transfer board (2) to a positive round platform shape heat transfer board (1), liquid flows downwards along positive round platform shape heat transfer board (1) inclined surface, and gas flow is that the tower axial is to ring flow all around.
2. A heat exchanger plate according to claim 1, characterized in that the diameter of the upper circle phi 1 of the right circular truncated cone shaped heat exchanger plate (1) is smaller than the diameter of the lower circle phi 2, the diameter of the upper circle phi 3 of the inverted truncated cone shaped heat exchanger plate (2) is larger than the diameter of the lower circle phi 4, and the upper and lower cone angles of the extension of the right circular truncated cone shaped heat exchanger plate (1) and the inverted truncated cone shaped heat exchanger plate (2) are both 30-150 °.
3. A heat exchanger plate according to claim 1 or 2, characterized in that the feed distributor is welded on when the right circular truncated cone shaped heat exchanger plate (1) is used as a liquid material feed plate.
4. A heat exchange plate according to claim 1 or 2, characterized in that the feeding distributor welded on the right circular truncated cone-shaped heat exchange plate (1) is composed of a feeding pipe flange (3), a feeding pipe (4), a rectifying groove (5) and a discharging port (6), the feeding pipe flange (3) of the feeding distributor is connected with the liquid phase feeding pipe flange, the discharging port (6) is a square or circular hole opened in the horizontal direction on the lower side of the feeding pipe (4), the total area of the holes is larger than the sectional area of the feeding pipe, and the circumference edge of the outlet on the rectifying groove (5) must be horizontal.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920967869.1U CN210464112U (en) | 2019-06-25 | 2019-06-25 | Heat exchange plate for directly exchanging heat between gas and liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920967869.1U CN210464112U (en) | 2019-06-25 | 2019-06-25 | Heat exchange plate for directly exchanging heat between gas and liquid |
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| Publication Number | Publication Date |
|---|---|
| CN210464112U true CN210464112U (en) | 2020-05-05 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920967869.1U Active CN210464112U (en) | 2019-06-25 | 2019-06-25 | Heat exchange plate for directly exchanging heat between gas and liquid |
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| Country | Link |
|---|---|
| CN (1) | CN210464112U (en) |
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- 2019-06-25 CN CN201920967869.1U patent/CN210464112U/en active Active
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