CN101480595A - Slurry bubble column reactor with needle type fin column tube bundle - Google Patents
Slurry bubble column reactor with needle type fin column tube bundle Download PDFInfo
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- CN101480595A CN101480595A CNA2009100952884A CN200910095288A CN101480595A CN 101480595 A CN101480595 A CN 101480595A CN A2009100952884 A CNA2009100952884 A CN A2009100952884A CN 200910095288 A CN200910095288 A CN 200910095288A CN 101480595 A CN101480595 A CN 101480595A
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Abstract
The invention discloses a slurry state bubble tower reactor with a needle type fin tube bundle. A plurality of vertical heat exchange tubes are arranged in the cylindrical reactor; the upper ends of the vertical heat exchange tubes are connected with a liquid distributor fixed below a container, while the upper ends are connected with a liquid collector fixed above the container; the outer walls of the heat exchange tubes are provided with horizontal needle type fins; the number of the needle fins arranged on the heat exchange tubes is 80-800 every meter, the diameter of the needle type fins is -10 mm, and the length of the needle type fins is 10 125 mm. The heat exchange tubes with the needle type fins are adopted to increase the heat exchange area and strength the heat exchange capability of the reactor on one hand, and on the other hand, the needle type fins distributed on the outer walls of the heat exchange tubes can obstruct the flowing of sizing agents and bubbles in the tower, can suppress the flow steeping effect caused by the vertical heat exchange tubes, improve the flow rate distribution of a slurry bed and achieve double functions of reinforcing heat transfer and improving the flow.
Description
Technical field
The present invention relates to a kind of slurry attitude bubbling column reactor that has needle type fin tubulation bundle, be applicable to the solid heterogeneous strong exothermic/endothermic course of reaction of gas-liquid/gas-liquid of chemical process.
Background technology
Gas-liquid bubble tower or gas-liquid-solid three-phase bubbling reactor (also claiming paste state bed reactor) are a kind of in the very wide reaction unit of many fields application such as chemical industry, the energy, environment, biochemistry, processes such as for example Fischer-Tropsch is synthetic, hydrogenation liquefaction, carbonylation, oxidation, halogenation, fermentation, GAS ABSORPTION.The design of paste state bed reactor and amplification mainly contain two aspect problems, and the one, move heat, the 2nd, back-mixing.The heat problem that moves for reactor, the industry paste state bed reactor adopts the method that vertical tube is installed in reactor to strengthen heat exchange more, but, document [1,2] after finding in that the vertical row tube bank adds, velocity flow profile in the slurry attitude bed and gas holdup distribute and will become more precipitous, cause an inner fluid back-mixing aggravation, and reactor performance reduces.For this reason, proposed the notion of " damping internal construction member " in patent [3,4] and the document [5,6], proposed to be provided with the horizontal silk screen of certain density, suppressed the too high fluid velocity in tower center, reduced back-mixing in the higher zone of flow velocity, tower center.Though above-mentioned measure can improve the VELOCITY DISTRIBUTION in the slurry attitude bed of being with tubulation, but the heat exchange efficiency of tubulation bundle is descended, and present way is that screen cloth damping member and tubulation heat exchange element are carried out simple combination, damping function is born respectively by different members with heat exchange function, lack collaborative humidification between two kinds of members of screen cloth and tubulation, therefore be difficult to the function of taking into account enhanced heat exchange and regulating and control to flow two aspects.
On the other hand, in recent years in the research of pipe-shell heat exchanger in order to strengthen the heat exchange property of tubulation bundle, a kind of needle type fin heat exchanging pipe technology has been proposed, at the heat exchanger tube outer wall intensive needle type fin is installed, to improve heat exchange area and to strengthen exchange capability of heat.In document [7～10] and patent [11～13], all describe the applicable cases of this type of technology in detail at aspects such as shell-and-tube heat exchanger, boiler, air-conditioning and refrigeration plants, and relevant Needle fin tube method for designing.But this so far technology only limits to use in the tubular heat exchanger of monophasic fluid, does not see that it is applied to paste state bed reactor.The situation of paste state bed reactor and common tubular heat exchanger is very different, mobile in the common heat exchanger is that pressure-actuated monophasic fluid flows, the increase of the outer fin of heat exchanger tube generally all makes coefficient of heat transfer folk prescription to increase, can not make flow velocity and distribute and take place significantly to change, except increasing certain flow resistance and manufacturing cost, can not bring other side effect.And mobile in the bubble tower heterogeneous the flowing that to be air bubble buoyancy drive, the tower central area upwards, near wall region is downward, the pin wing is installed on heat exchanging pipe will be brought effect conflicting aspect two: increased the tubulation heat exchange area on the one hand, help improving heat exchange efficiency, can reduce the flow velocity in the tower on the one hand again, reduce the tubulation coefficient of heat transfer.Therefore, as a kind of novel reactor, in slurry attitude bed, adopt the heat exchange of needle type fin tubulation to take into account to flow regulation and control and heat exchange to strengthen effect aspect two, try to achieve best general effect, and also do not have the research and technology of this respect to report in document and the patent at present.
List of references and patent
[1]Bernemann K.，Zur Fluiddynamik und zum Vermischungsverhalten derFluessigen Phase in Blasensaeulen mit Laengsangestroemten Rohrbuendeln.1989，Dissertation，University Dortmund.
[2]Larachi F，Desvigne D，Donnat L，Schweich D，Simulating the effects of liquidcirculation in bubble columns with internals，Chemical Engineering Science，2006，61：4195—4206.
[3] Li Xi, Chen Bin, Wang Liya, Wang Lijun becomes promising, has the bubbling column reactor of damping internal construction member, patent of invention CN200510061602.9.
[4] the slurry attitude bubbling column reactor of band heat exchanging pipe and grid type damping internal construction member, application number 200810162467
[5] Chen Bin, Wang Liya, Li Xi.The research (I) of band damping internal construction member bubble tower: inner member is to the influence of velocity flow profile.Chemical Reaction Engineering and technology, 2006,22 (4): 317-323.
[6] Wang Lijun, Wang Liya, Zhang Yu, all blue or green sodium, Li Xi, the research (II) of band damping internal construction member bubble tower: inner member is to the influence of gas-liquid mass transfer speed, Chemical Reaction Engineering and technology, 2007,23 (4): 109～113
[7] money panegyric, Cen Hanzhao, Jiang Nan, horse Xiao Ming, Fang Jiangmin, heat exchanger tube hydrodynamics and heat transfer, Sinopec publishing house,, Beijing in 2002.
[8] Zhu Dongsheng, the money panegyric, augmentation of heat transfer technology and technology thereof are used, chemical equipment technology, 2000,21 (6): 1-9.
[9] Fang Jiangmin, horse Xiao Ming, Li Hua, money panegyric, the optimization of Sunrod Needle fin tube and augmentation of heat transfer performance study, petrochemical equipment, 2002,31 (4): 10-13.
[10]A.Aziz，Kraus，D.Allan，Extended surface heat transfer，John Wiley，2001，NewYork.
[11] Wang Liduan, Gao Liping, money panegyric, Cen Hanzhao etc., a kind of Needle fin tube, utility model CN2253460Y
[12]Balint，Endre Water tube boiler PN WO92/18806
[13]Andersson，Erik A heat exchanger tube with surface enlarging elements PNWO90/02916
Summary of the invention
The purpose of this invention is to provide a kind of slurry attitude bubbling column reactor that has the band needle type fin tubulation bundle of the heat exchange reinforcement and the adjusting function that flows simultaneously, to realize the dual raising of paste state bed reactor heat exchange and back-mixing performance.
The slurry attitude bubbling column reactor of band needle type fin tubulation bundle of the present invention, comprise a cylindrical pressure vessel, many vertical heat exchanging pipes are installed in the container, the lower end of vertical heat exchanging pipe is connected with the liquid distributor that is fixed on the container below, the upper end is connected with the liquid trap that is fixed on the container top, below liquid distributor, be provided with gas distributor, container is provided with material turnover pipe, medium turnover pipe and gas turnover pipe, it is characterized in that the outer wall at heat exchanging pipe is equipped with the needle type fin of level, the pin wing number of installing on every meter heat exchanging pipe length is 80～800, and the diameter of needle type fin is 1～10mm, and length is 10～125mm.
The present invention adopts the heat exchanger tube that has needle type fin to replace the smooth heat exchanger tube of common employing in present bubble tower or the paste state bed reactor.On the one hand, the pin wing that is fixed on the tubulation can increase heat exchange area, the enhanced reactor exchange capability of heat; On the other hand, it is a kind of horizontal damping member that the pin fin also can be, and slurry in the reactor and bubble mobile had inhibition, can contain the mobile precipitousization effect that vertical heat exchanging pipe causes, and improves the velocity flow profile in the slurry attitude bed.Therefore, the tubulation of band pin wing is a kind of difunctional inner member, has augmentation of heat transfer concurrently, improves the dual-use function that flows.The present invention is applicable to the bubble tower structure of various tower diameters, ratio of height to diameter and band expanding reach and other inner member.
Description of drawings
Fig. 1 is the slurry attitude bubbling column reactor schematic diagram of band needle type fin tubulation bundle;
Fig. 2 is circular radiation profiles needle type fin schematic diagram, and 3 is heat exchanging pipe among the figure, and 2 is needle type fin;
Fig. 3 is the schematic diagram of rectangular radiation distribution needle type fin, and 3 is heat exchanging pipe among the figure, and 2 is needle type fin;
Fig. 4 is the radial pattern needle type fin schematic diagram that installs annular damped ring additional, and 3 is heat exchanging pipe among the figure, and 2 is needle type fin, and 14 is annular retainer plate;
Fig. 5 is the pin wing length that calculates and the density influence relation to the slurry attitude bed central liquid speed of band heat exchanging pipe; Abscissa is the length of needle type fin and the ratio of diameter, the long influence of expression pin wing; Pin wing density among the figure is the needle type fin number of installing on the every meter every heat exchanger tube, and ordinate is the liquid velocity on the bubble tower central axis.
Fig. 6 is the influence relation that model calculates the pin wing length provide and density exchange heat pipe heat transfer coefficient, and ordinate is the ratio of the Needle fin tube coefficient of heat transfer and the plain tube coefficient of heat transfer, and expression adds the multiple of pin wing coefficient of heat transfer increase later on; Abscissa is the length of needle type fin and the ratio of diameter, the long influence of expression pin wing; Pin wing density among the figure is the needle type fin number of installing on the every meter every heat exchanger tube.
Fig. 7 is a center arrangement pin wing heat exchanger tube, and annular space is arranged the schematic diagram of smooth heat exchanger tube, and 1 is the bubble tower wall, 2 heat exchanger tubes for band pin wing, and 3 is smooth heat exchanger tube;
Fig. 8 is the radial distribution figure of the liquid axial velocity of mensuration, measures the plane and is positioned at 2250mm place, gas distributor top, and abscissa r/R is the dimensionless radial position, and r is a radial coordinate, and R is the bubble tower radius, and r/R=0 is the center, and r/R=1 is the wall position; The axial velocity of ordinate for measuring, speed are upwards to flow on the occasion of expression, and negative value is represented to flow downward.
The specific embodiment
With reference to Fig. 1, the slurry attitude bubbling column reactor of band needle type fin tubulation bundle of the present invention, comprise reactor, reactor is the container 1 of a cylinder type, inside is equipped with many vertical heat exchanging pipes 3 and is fixed on the needle type fin 2 that tubulation outer wall along continuous straight runs extends, and gas distributor 4 and input and output material pipeline.The lower end of heat exchanging pipe bundle 3 is connected with the liquid distributor 11 that is fixed on the tower body below, and the upper end is connected with the liquid trap 12 that is fixed on the tower body top.Needle type fin as principal character of the present invention is the thin bar of a kind of diameter metal more much smaller than heat exchanging pipe, vertically is installed on the heat exchanging pipe outer wall, and the root of pin wing is fixed on the outer surface of heat exchanger tube, and many pin wings evenly distribute radially at outer surface.In working order down, inside reactor is equipped with gas-liquid two-phase or gas-liquid-solid phase reaction slurry, the operation liquid level is shown in 5 places, and needle type fin 2 and heat exchanger tube 3 and gas distributor 4 all are immersed in the reaction paste, and pin wing bar 2 and heat exchanging pipe 3 are positioned at gas distributor 4 tops.Gas feeds in the tower by gas distributor 4 bubblings of gas inlet pipe 6 at the bottom of the tower, and leaves liquid level 5 after reaction paste contact, exports outside the towers from offgas duct 7.The liquid and solid phase reaction slurry adds in the tower by feed pipe 8, contact concurrent biochemical reaction with gas reactant, product is by discharge nozzle 9 outputs, cooling water or heat medium enter heat exchanger tube 3 by heat transferring medium inlet tube 10 and liquid distributor 11, by exporting outside the towers by liquid trap 12 to heat transferring medium outlet 13 after the slurry heat exchange in tube wall and needle type fin 2 and the bed again.Gas-liquid-solid phase reaction thing in the tower is in turbulence bubble flow state under the stirring of bubble, solid suspends and the liquid good mixing, and temperature and CONCENTRATION DISTRIBUTION are even.
Be connected details further by Fig. 2～4 explanations between needle type fin 2 and the heat exchanging pipe 3.The root of pin wing is fixed on the heat exchanging pipe outer wall, and pin wing and heat exchanger tube are all made by metal material, has heat conductivility preferably.Down, heat exchanger tube 3 not only can carry out heat exchange by hydraulically smooth surface and slurry, can also carry out heat exchange by pin wing 2 in working order, and this has just increased the heat exchange area between heat transferring medium and the reaction paste widely, has improved the exchange capability of heat of reactor.On the other hand, the pin wing is again a kind of horizontal inner member, has to hinder the function that flows, and can be used for regulating and control velocity flow profile, prevents that central area gas is short-circuited, and improves gas-liquid phase back-mixing.The heat exchanging pipe design parameter of band pin wing comprises: shape, length, diameter and the packing density etc. of the caliber of heat exchanger tube and tube pitch, pin wing.The caliber of suitable heat exchanger tube is 20mm～80mm, tube pitch 60mm～250mm.The shape of cross section of pin wing generally is circular, also can be random geometries such as ellipse, rectangle, rhombus.The diameter of pin wing bar should be fully carefully so that enough big heat exchange area to be provided, but consider the requirement of mechanical strength and length aspect again.The diameter of the suitable needle type fin that the present invention provides is 1～10mm, and the diameter of optimization is 4～10mm.Consider from the angle of the regulation and control of flowing, the length of pin wing is relevant with the heat exchanger tube spacing, with the gap between the abundant filling heat exchanger tube is principle, the too short meeting of length stays excessive tubulation gap, be unfavorable for the formation of flowing is hindered and regulating and controlling effect, and the long overlapped collision of pin wing that can make on the various heat exchange pipe of length is unfavorable for installing and maintenance.Suitable pin wing length is about half of tubulation spacing (outer wall spacing), and for general industrial gas-liquid bubble tower or gas-liquid stereoplasm attitude bed, pin fin length is in the scope of 10～125mm, and the length of optimization is 20～80mm.In addition, different towards the pin wing also may have different length, relevant with the arrangement form of heat-exchanging tube bundle.When distributing for equilateral triangle between the tubulation, the pin wing can adopt isometric circular radiation pattern as shown in Figure 2 to arrange; When being distributed rectangular between tubulation, then can adopt rectangular radiation as shown in Figure 3 to distribute, make the pin wing can cover all spaces between the tubulation.Big and the peripheral area density of pin wing center area density that radial pattern distributes is little, is tending towards average for the area density that makes the pin wing distributes, and can install annular retainer plate 14 as shown in Figure 4 on the pin wing of every layer of radiation profiles additional.
The design of needle type fin length and number density is also noted that the double influence of its heat exchanging except considering the fluid resistance effect.Acting in the bubbling column reactor with different at general pipe-shell heat exchanger of needle type fin: the liquid of bubbling column reactor center is to the upper reaches, limit wall liquid is to dirty, horizontal needle type fin not only provides heat exchange area, the damping action that hinders fluid motion also is provided simultaneously, when in bubbling column reactor needle type fin being installed, flow velocity and distribution thereof can change, and central liquid speed can reduce with fluctuation velocity, cause total fluid motion speed to reduce, the heat exchanger tube heat transfer coefficient descends.Therefore, there are two kinds of conflicting effects in the diabatic process for band fin heat exchange pipe in the bubble tower: the adding of needle type fin increases heat transfer area on the one hand, and heat exchange efficiency improves; Fin causes flow velocity to descend again to the inhibition that flows on the other hand, and heat exchange efficiency reduces.Related experiment of the present invention shows, the range of decrease of reactor center district average speed is directly proportional with 2/3 power of pin wing damping area density (promptly hanging down as for the cross-sectional area/fluid volume of flow direction), and the range of decrease of fluctuation velocity is directly proportional with 1/4 power of damping area.Like this, after pin wing length and number density increased, the increase of tubulation heat exchange area formed opposite effect with the decline of fluid velocity, made the coefficient of heat transfer that calculates with smooth tubulation surface area present a maximum.Suitable pin wing design parameter is: the pin wing number of installing on every meter tubulation length is 80～800, and the diameter of needle type fin is 1～10mm, and length is 10～125mm.
Fig. 5 and Fig. 6 have provided under the differing needles wing number of densities condition, change the influence of the pin wing length convection cell central speed and the coefficient of heat transfer.Calculated examples system at
Bubble tower in the situation of 30 4 meters long band pin wing heat exchanging pipe is installed, the ordinate among Fig. 6 is the ratio of the Needle fin tube coefficient of heat transfer and the plain tube coefficient of heat transfer, expression adds the multiple that the coefficient of heat transfer increases after the pin wing; Abscissa is the length of needle type fin and the ratio of diameter, the long influence of expression pin wing; Pin wing density among the figure is the needle type fin number of installing on the every meter every heat exchanger tube.See that by Fig. 5 along with the increase of pin wing length and pin wing density, the fluid central speed is dull to descend, and this means that the flowing velocity in the full tower also can descend thereupon, causes the heat exchanger tube coefficient of heat transfer to reduce.Can see that by Fig. 6 under different pin wing number density conditions, the tubulation coefficient of heat transfer of band pin wing a maximum all can occur with the increase of pin wing length.More in short-term, the increase of its length or heat exchange area is remarkable to the facilitation of conducting heat at the pin wing, has surpassed fluid velocity and has reduced the heat transfer that causes and slow down effect, makes the coefficient of heat transfer increase with pin wing length.After pin wing length increased to a certain degree, it tended towards stability to the facilitation of conducting heat, and the damping action that flows then is tending towards significantly, made the coefficient of heat transfer descend with pin wing length increase (causing flow velocity to reduce).Can also see that from Fig. 6 pin wing number is many more, the coefficient of heat transfer will be big more, and is simultaneously also big more with the amplitude of pin wing length variations.Therefore, consider, should select higher pin wing density and short pin wing length to obtain the maximum coefficient of heat transfer from the angle of heat exchange.But, consider the requirement of the regulation and control of flowing, the length of pin wing also will be subjected to the constraint of tubulation spacing, adjusting leeway is little, therefore the selection of pin wing density just must be determined suitable scope according to its length, should weigh area increases the restrictive function that reduces by two kinds of effects with flow velocity, satisfying under certain mobile regulation and control require, obtains the higher coefficient of heat transfer.The size of pin wing density represents that by the wing degree wing degree is defined as the surface area of the needle type fin external surface area/smooth tubulation on the heat exchanger tube.
The design of needle type fin also will take into account the damping requirement of the regulation and control of flowing in the bubble tower except the factor of considering heat exchange reinforcement aspect.The inhibition of pin wing convection cell represents by the damping area density, is defined as on the heat exchanging pipe all needle type fins slurry volume of the total cross-sectional area/encirclement heat exchanging pipe of (promptly perpendicular to flow direction) in the horizontal direction.The size of damping area density will satisfy the flow principle of " resistance and do not keep off " of slurry, should apply certain resistance velocity flow profile is tending towards evenly, can not hinder again excessively so that formation local flow defective region.Suitable damping area density value is 1.0～10m
2/ m
3The distribution of pin wing density on the tower cross section can be uniformly, also can be uneven.Requirement for the regulation and control aspect that flows, the distribution form of optimizing is the distribution intensive in the tower center, that outer peripheral areas is sparse, as shown in Figure 7, this is because tower central area speed is higher, pin wing centralized arrangement can be brought into play its damping action in the central area the biglyyest, adopt less pin wing can reach the regulating effect that flows preferably.
(=volumetric flow of gas/(tower cross-sectional area-smooth heat exchanger tube total sectional area) scope of entering in the tower is 0.08m/s～1.0m/s to the superficial gas velocity that the present invention is applicable to, reactor is in turbulence bubbling state under this gas speed range of condition.The configuration of pin wing density is relevant with heat exchanger tube density with superficial gas velocity, and the tubulation bundle is intensive more, and gas speed is high more, and the effect of the damping of pin wing is obvious more, and it is few more to reach the identical required pin wing of damping damping area.
Embodiment
Starch attitude bubbling column reactor device as shown in Figure 1, diameter is 500mm, the high 4000mm of liquid level, and the porous plate gas distributor is installed in the bottom.Evenly arrange 30 heat exchange pipes that long 4000mm, diameter are the band needle type fin of 25mm in the tower, tube pitch is 70mm.The pin wing is the thin bar of round metal, the layout on heat exchanger tube as shown in Figure 2, the structural parameters of needle type fin are listed in table 1.The bubble tower central liquid speed of measuring and the coefficient of heat transfer that calculates are listed in table 2.
The heat exchange tube structure parameter of table 1 band pin wing
| Pin wing density (/ rice) | Pin wing diameter (mm) | Pin wing length (mm) | Pin wing damping area density (m 2/m 3) |
| 500 | 4 | 17 | 6.37 |
| 500 | 4 | 13 | 4.85 |
| 571 | 4 | 10 | 4.26 |
| 571 | 4 | 10 | 4.26 |
The pin wing tubulation coefficient of heat transfer and tower central liquid speed in the table 2 band pin wing heat exchanger tube bubble tower
| Superficial gas velocity (m/s) | The Needle fin tube coefficient of heat transfer, (kW/ ℃ of m 2) | Tower central liquid speed, (m/s) |
| 0.12 | 8.57 | 0.45 |
| 0.19 | 8.75 | 0.53 |
| 0.31 | 9.30 | 0.61 |
| 0.62 | 10.45 | 0.84 |
Comparative Examples
For the heat exchanger tube of band pin wing in the bubble tower relatively and plain tube in distribute difference aspect two of exchange capability of heat and liquid speed, this Comparative Examples adopts the pin wing heat exchanger tube among the smooth heat exchanger tube replacement embodiment, experimental provision and experimental technique and embodiment are basic identical.Provide the central liquid speed and the coefficient of heat transfer that same 30 pin wing heat exchanger tubes and smooth heat exchanger tube are housed in the table 3, further provided the liquid velocity radial distribution of measuring in the bubble tower under void tower, smooth heat exchanger tube, three kinds of situations of pin wing heat exchanger tube among Fig. 8.
Bubble tower relevant parameter with the smooth heat exchanger tube of embodiment similar number is housed in table 3 bubble tower
| Superficial gas velocity (m/s) | The plain tube coefficient of heat transfer (kW/ ℃ of m 2) | The Needle fin tube coefficient of heat transfer, (kW/ ℃ of m 2) | Plain tube tower central liquid speed (m/s) | Needle fin tube tower central liquid speed (m/s) |
| 0.12 | 6.68 | 8.51 | 1.03 | 0.45 |
| 0.19 | 6.94 | 8.75 | 1.15 | 0.53 |
| 0.31 | 7.34 | 9.30 | 1.30 | 0.61 |
| 0.62 | 8.30 | 10.45 | 1.79 | 0.84 |
Comparing embodiment and Comparative Examples be as can be seen:
1. the tubulation coefficient of heat transfer ratio that has the pin wing has not improved about 27% with the plain tube coefficient of heat transfer of pin wing, this means that the exchange capability of heat that installs the later heat exchanger tube of pin wing additional has improved more than 1/4, under same heat exchange load, can replace more smooth heat exchanger tube with less pin wing heat exchanging pipe, for example, can replace 38 plain tubes with 30 pin wing heat exchanger tubes for this example.
2. the central liquid speed under the pairing bubble tower central liquid of the pin wing heat exchanger tube speed ratio plain tube situation has descended 53～56%, and this will improve the VELOCITY DISTRIBUTION in the tower significantly, reduces gas-liquid phase back-mixing, improves reactor efficiency.Fig. 8 has provided the VELOCITY DISTRIBUTION of measuring in the tower, therefrom can see, in the void tower of no any heat exchanging pipe, VELOCITY DISTRIBUTION is comparatively smooth; After adding smooth heat exchanging pipe, it is precipitous that VELOCITY DISTRIBUTION is tending towards; After installing the pin wing on the tubulation additional, it is smooth that VELOCITY DISTRIBUTION is tending towards, more even velocity distribution when having obtained than void tower.
The presentation of results of the foregoing description and Comparative Examples, the heat exchanger tube of band needle type fin can significantly improve exchange capability of heat on the one hand in the bubble tower, can suppress the non-uniform Distribution of flow velocity in the tower on the one hand again, has enhanced heat exchange and improves the dual-use function that flows.
Claims (4)
1. slurry attitude bubbling column reactor with needle type fin tubulation bundle, comprise a cylindrical pressure vessel (1), many vertical heat exchanging pipes (3) are installed in the container, the lower end of vertical heat exchanging pipe is connected with the liquid distributor (11) that is fixed on the container below, the upper end is connected with the liquid trap (12) that is fixed on the container top, be provided with gas distributor (4) in the below of liquid distributor (11), container is provided with material turnover pipe, medium turnover pipe and gas turnover pipe, it is characterized in that the outer wall at heat exchanging pipe (3) is equipped with the needle type fin of level, the pin wing number of installing on every meter heat exchanging pipe length is 80～800, the diameter of needle type fin is 1～10mm, and length is 10～125mm.
2. the slurry attitude bubbling column reactor of band needle type fin tubulation bundle according to claim 1, the diameter that it is characterized in that heat exchanging pipe (3) is 20mm～80mm, tube pitch is 60mm～250mm.
3. the slurry attitude bubbling column reactor of band needle type fin tubulation bundle according to claim 1, the shape of cross section that it is characterized in that needle type fin is a random geometry.
4. the slurry attitude bubbling column reactor of band needle type fin tubulation bundle according to claim 1 is characterized in that needle type fin distributes in rounded radiation of heat exchanging pipe outer wall or rectangular radiation, perhaps is provided with annular damped ring (14) on every layer of needle type fin.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009100952884A CN101480595B (en) | 2009-01-08 | 2009-01-08 | Slurry bubble column reactor with needle type fin column tube bundle |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2009100952884A CN101480595B (en) | 2009-01-08 | 2009-01-08 | Slurry bubble column reactor with needle type fin column tube bundle |
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| CN101480595A true CN101480595A (en) | 2009-07-15 |
| CN101480595B CN101480595B (en) | 2011-05-04 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2009100952884A Expired - Fee Related CN101480595B (en) | 2009-01-08 | 2009-01-08 | Slurry bubble column reactor with needle type fin column tube bundle |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101844965A (en) * | 2010-04-30 | 2010-09-29 | 中国石油化工集团公司 | Heat exchange device for methanol synthesis reactor |
| CN102212080A (en) * | 2010-04-12 | 2011-10-12 | 中国科学院过程工程研究所 | Reaction device for preparing methyl chlorosilane and reaction system comprising same |
| CN104587943A (en) * | 2014-09-25 | 2015-05-06 | 德艾柯工程技术（上海）有限公司 | Inner heat exchange-type bubble column reactor |
| CN104826558A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation |
| CN106610239A (en) * | 2015-10-22 | 2017-05-03 | 天津新华能源设备科技有限公司 | Heat pipe with needle-shaped fins |
| CN108731021A (en) * | 2018-06-25 | 2018-11-02 | 西安交通大学 | A kind of various dimensions composite moduleization casting condensation enhanced heat exchange device |
| CN112090388A (en) * | 2020-09-07 | 2020-12-18 | 浙江大学 | Continuous flow reactor and application thereof in chemical reaction and synthesis |
| CN115611832A (en) * | 2022-10-17 | 2023-01-17 | 中国五环工程有限公司 | Process for preparing succinic anhydride by maleic anhydride hydrogenation |
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2009
- 2009-01-08 CN CN2009100952884A patent/CN101480595B/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102212080A (en) * | 2010-04-12 | 2011-10-12 | 中国科学院过程工程研究所 | Reaction device for preparing methyl chlorosilane and reaction system comprising same |
| CN101844965A (en) * | 2010-04-30 | 2010-09-29 | 中国石油化工集团公司 | Heat exchange device for methanol synthesis reactor |
| CN101844965B (en) * | 2010-04-30 | 2013-05-08 | 中国石油化工集团公司 | Heat exchange device for methanol synthesis reactor |
| CN104587943A (en) * | 2014-09-25 | 2015-05-06 | 德艾柯工程技术（上海）有限公司 | Inner heat exchange-type bubble column reactor |
| CN104826558A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation |
| CN106610239A (en) * | 2015-10-22 | 2017-05-03 | 天津新华能源设备科技有限公司 | Heat pipe with needle-shaped fins |
| CN108731021A (en) * | 2018-06-25 | 2018-11-02 | 西安交通大学 | A kind of various dimensions composite moduleization casting condensation enhanced heat exchange device |
| CN108731021B (en) * | 2018-06-25 | 2024-03-12 | 西安交通大学 | Multidimensional combined modularized casting condensation reinforced heat exchanger |
| CN112090388A (en) * | 2020-09-07 | 2020-12-18 | 浙江大学 | Continuous flow reactor and application thereof in chemical reaction and synthesis |
| CN115611832A (en) * | 2022-10-17 | 2023-01-17 | 中国五环工程有限公司 | Process for preparing succinic anhydride by maleic anhydride hydrogenation |
| CN115611832B (en) * | 2022-10-17 | 2024-04-05 | 中国五环工程有限公司 | Process for preparing succinic anhydride by maleic anhydride hydrogenation |
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| CN101480595B (en) | 2011-05-04 |
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