CN204739934U - Shell and tube heat exchanger and ft synthesis thick liquid attitude bed reactor - Google Patents
Shell and tube heat exchanger and ft synthesis thick liquid attitude bed reactor Download PDFInfo
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- CN204739934U CN204739934U CN201520365706.8U CN201520365706U CN204739934U CN 204739934 U CN204739934 U CN 204739934U CN 201520365706 U CN201520365706 U CN 201520365706U CN 204739934 U CN204739934 U CN 204739934U
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Abstract
Shell and tube heat exchanger and ft synthesis thick liquid attitude bed reactor, shell and tube heat exchanger form by at least a set of heat transfer unit, the heat transfer unit include upper portion heat transfer tubulation (1), with heat transfer tubulation two piece communicating at least heat transfer branch pipe (2) and lower part through heat transfer tubulation (1) component that the heat transfer branch pipe assembled, the pipe diameter of heat transfer tubulation be not less than the pipe diameter of heat transfer branch pipe, the contained angle of heat transfer tubulation and heat transfer branch pipe be the obtuse angle. The utility model provides a shell and tube heat exchanger can effectively realize the evenly distributed of the interior temperature of ft synthesis thick liquid attitude bed reactor to guarantee the activity of catalyst, guarantee the security of reactor operation and yield and the selectivity that improves target product.
Description
Technical field
The utility model relates to a kind of tubular heat exchanger, more particularly, relates to a kind of tubular heat exchanger for F-T synthesis paste state bed reactor and F-T synthesis paste state bed reactor.
Background technology
Due to China's oil shortage of resources, in order to ensure national energy security, in conjunction with the feature of China's energy resource structure, to take coal as waste liquid fuel be alleviates the effective way of this problem, and wherein F-T synthesis is one of main method.F-T synthesis is with coal or natural gas for synthesis gas prepared by raw material, and synthesis gas, at the temperature of 400 ~ 500 DEG C, based under the catalyst effect of iron or cobalt etc., produces the method for hydro carbons or alcohol liquid fuel.Fischer-Tropsch synthesis is a strong exothermal reaction, and thermal discharge is large.When carrying out Fischer-Tropsch synthesis, normal generation catalyst hot-spot, and cause catalyst carbon deposition even to block bed, cause selectivity of product to reduce.Therefore, need effectively to remove the heat generated in reactor, ensure the security of reactor operation and improve the yield of object product.Simultaneously, the distribution of Fischer-Tropsch synthetic and the activity of catalyst very responsive to temperature, the temperature maintaining relative constancy in reactor to carrying out smoothly of reacting in paste state bed reactor and safety operation very important, therefore development of new effective heat exchanger form is very important, at present existing many multi-form heat exchangers.
CN101396647A discloses a kind of new type heat exchanger being applicable to paste state bed reactor, and its heat exchanger section can adopt one-part form main heat exchanger, also can adopt two sections of main heat exchangers.Owing to there is larger space between the component of Disengagement zone, according to need of production, can consider outside upper main heat exchanger, arrange Mini-type heat exchanger element group, play the effect of the temperature regulating liquid-solid separating region to take up space.Add mozzle in this heat exchanger, realize the thermal coupling of two sections heat exchanger, subtract two intersegmental thermic load differences, add operating flexibility, therefore heat-exchange temperature can ensure fully carrying out of the interior reaction of paste state bed reactor.The heat exchanger of this invention is in order to enhanced heat exchange effect and Separation of Solid and Liquid, just account for 70 ~ 90% of reactor cross-section at heat transfer zone, the top heat exchanging pipe sectional area of heat exchanger, the heat transfer requirements that near the air inlet being not suitable for paste state bed reactor bottom, reaction temperature is higher.
CN101480595A discloses a kind of pin fin-type heat exchanger, and the outer wall of heat exchanging pipe is provided with the needle type fin of level, and the pin wing number that every root heat exchanging pipe is installed is 80 ~ 800, and needle type fin diameter is 1 ~ 10mm, and length is in 10 ~ 125mm scope.Adopt needle type fin heat exchanger tube, can heat exchange area be increased, enhancing reactor exchange capability of heat on the one hand; The needle type fin of heat exchanging pipe outer wall can have inhibition to the flowing of liquid phase fluid in tower on the other hand, the precipitous effect of flowing that common heat exchanging pipe causes (namely " stack effect) can be contained; improve the velocity flow profile in slurry bed system, realize augmentation of heat transfer and improve the dual-use function of flowing.But this pin fin-type heat exchanger exists and manufactures complicated feature, and along with the increase of reactor size, the pin finned length that certainly will will increase on tubulation and number, both added manufacturing difficulty under guarantee heat transfer effect prerequisite.
US4187902 discloses a kind of heat exchanger utilizing high pressure cooling medium to carry out heat exchange, this heat exchanger main feature is that heat exchanging pipe is longer and in folding shape bending, the effect of thermal compensation is played in heat transfer process, when carrying out heat exchange, heat exchanging pipe can shake with gas-liquid movement, to with sedimentary liquid phase, utilize the shock effect of bending tubulation can reduce the deposition of sediment on tubulation, prevent fouling on tubulation, improve heat transfer effect.The size of heat exchanging pipe, not by the restriction of reactor size, according to the heat exchanging pipe installing any amount in need of production reactor, then can carry out reactor body size according to the size of heat exchanger.Because this heat exchanging pipe is the bending of larger angle, increase the flow resistance of heat transferring medium in tubulation, in order to ensure that heat transfer effect must increase the power consumption of heat transferring medium.
CN202339124U discloses a kind of screw twisted flat pipe heat exchanger, comprises housing, tube sheet, slideway and heat-exchanging tube bundle.Heat-exchanging tube bundle in the shape of a spiral, containing two spiral flat tubes, inside and outside flat tube, spin motion, enhances liquid phase less turbulence, improve the coefficient of heat transfer by medium.Rely on the spirality outer rim of flat tube to keep supporting mutually between tube bank, and tied together by strapping.Owing to not having deflection plate, there is not dead band, and have dividing plate to separate formation double-shell side in the middle of tube bank, shell side medium flow process increases, and heat exchange efficiency improves 20 ~ 30% compared with common shell side heat exchanger.The width of this heat exchanger middle slideway is the subject matter of this heat exchanger, if wide, increase, improve manufacture difficulty and cost to the requirement of strength of material; If narrow, heat transfer effect can not be improved preferably.
WO2009154333A1 discloses a kind of heat exchanger being applied to Fischer-Tropsch synthesis device, wherein each heat-exchanging tube bundle is made up of concentric inner and outer tubes, heat transferring medium (high-pressure cooling water) enters heat exchanger top, and then shunting enters and offers foraminate interior pipe by certain rule.Band cooling water pressure in interior pipe is with Sprayable spirt outer tube from aperture, and utilize the process implementation heat exchange object that the thermal transition of water smoke absorption reaction is steam, steam is finally pooled to heat exchanger top and discharges from interior pipe.The maximum feature of this heat exchanger is that heat exchanging pipe adopts inside and outside sleeve form, and will dig aperture on inner tube wall and realize heat exchange, just increases the manufacture difficulty of heat exchanger thus, increases production cost.
In prior art, there is scope of application limitation in such as above-mentioned similar tubular heat exchanger, it is excessive and manufacture the problems such as complicated to take reactor volume, especially heat exchange pointedly can not be carried out to zones of different in paste state bed reactor, after heat exchange, still there is the even phenomenon of temperature distributing disproportionation in paste state bed reactor, the F-T synthesis paste state bed reactor that inside exists strong exothermal reaction can not be applicable to better.For F-T synthesis paste state bed reactor, need the better tubular heat exchanger of design heat exchange efficiency, to improve heat exchange efficiency, realize homogeneous temperature distribution in bed, impel reaction efficiently to carry out.
Summary of the invention
One of the technical problems to be solved in the utility model is to provide a kind of for the tubular heat exchanger in paste state bed reactor.Two of the technical problem solved is to provide a kind of F-T synthesis paste state bed reactor, to realize the uniform heat exchange in F-T synthesis slurry bed system.
A kind of tubular heat exchanger, be made up of at least one group of heat exchange unit, the heat exchanging pipe that the heat exchanging pipe that one group of heat exchange unit comprises top, at least two heat exchange arms communicated with heat exchanging pipe and lower end are converged through heat exchange arm forms, the caliber of described heat exchanging pipe is not less than the caliber of heat exchange arm, and described heat exchanging pipe and the angle of heat exchange arm are obtuse angle.
In the tubular heat exchanger that the utility model provides, the angle between described heat exchanging pipe and heat exchange arm is preferably 120 ° ~ 150 °, is more preferably 130 ° ~ 140 °.
In the tubular heat exchanger that the utility model provides, in described heat exchange unit, described heat exchange arm is uniformly distributed ringwise centered by heat exchanging pipe, and the number of heat exchange arm is 2 ~ 12.
A kind of F-T synthesis paste state bed reactor, arrange above-mentioned tubular heat exchanger in paste state bed reactor, the synthesis gas import of described paste state bed reactor is positioned at the axial region of the heat exchange arm of described tubular heat exchanger.
Accompanying drawing explanation
Fig. 1 is the front view of the first embodiment two-pipe heat exchange unit;
Fig. 2 is the cross-sectional view of the first embodiment two-pipe heat exchange unit;
Fig. 3 is the front view of the second embodiment three-tube type heat exchange unit;
Fig. 4 is the cross-sectional view of the second embodiment three-tube type heat exchange unit;
Fig. 5 a, b are respectively the cross-sectional view of four tubular type tube banks and nine tubular types tube bank heat exchange unit;
Fig. 6 is the paste state bed reactor cross-sectional view with tubular heat exchanger;
The front view of the F-T synthesis paste state bed reactor that Fig. 7 a provides for the utility model, wherein section A-A and section B-B, represents the cross section of tubular heat exchanger top and bottom position respectively.
Fig. 7 b is the Plane Installation schematic diagram of thermocouple probe on each cross section.
Wherein: 1-heat exchanging pipe, 2-heat exchange arm, 3-heat transferring medium entrance, 4-heat transferring medium exports, 5-thermocouple insert port, 6-synthesis gas entrance, 7-feed(raw material)inlet, 8-product exit, 9-thermocouple probe.
Detailed description of the invention
The tubular heat exchanger that the utility model provides and F-T synthesis paste state bed reactor are so concrete enforcement, it should be noted that, the 50%-100% of the height from top to bottom that " top " mentioned in description refers to, described " bottom " refers to the 0-50% place of height from top to bottom.
A kind of tubular heat exchanger, be made up of at least one group of heat exchange unit, the heat exchanging pipe that the heat exchanging pipe that one group of heat exchange unit comprises top, at least two heat exchange arms communicated with heat exchanging pipe and lower end are converged through heat exchange arm forms, the caliber of described heat exchanging pipe is not less than the caliber of heat exchange arm, and described heat exchanging pipe and the angle of heat exchange arm are obtuse angle.
In the tubular heat exchanger that the utility model provides, the angle between described top heat exchanging pipe and heat exchange arm and the angle between bottom heat exchanging pipe and heat exchange straight tube can be the same or different.Preferably, the angle between described heat exchanging pipe and heat exchange arm is 120 ° ~ 150 °, is more preferably 130 ° ~ 140 °.
In one group of basic heat exchange unit of the tubular heat exchanger that the utility model provides, a heat exchanging pipe separates at least two heat exchange arms at paste state bed reactor lower area, and described heat exchange arm is uniformly distributed ringwise centered by heat exchanging pipe.This is because for F-T synthesis paste state bed reactor, large in the volume fraction of adjacent gas inlets gas, the abundant contact between gas-liquid, exothermic heat of reaction amount is comparatively large, and distribution heat exchange arm that must be intensive is to strengthen the heat transfer intensity in this region.The number of heat exchange arm and distribution radius are determined according to heat transfer requirements and reaction severe degree, and in the heat exchange unit in adjacent gas inlets region, because thermal discharge is large, a heat exchanging pipe needs the more heat exchange arms of arrangement.Preferably, the number of the heat exchange arm that every root heat exchanging pipe separates is 2 ~ 12, more preferably 2 ~ 6.
In the tubular heat exchanger that the utility model provides, the length of described top heat exchanging pipe, heat exchange arm and bottom heat exchanging pipe is determined according to the Temperature Distribution of paste state bed reactor axis and the height of paste state bed reactor, and top heat exchanging pipe is mainly distributed in the upper zone of paste state bed reactor.Preferably, in described heat exchange unit, the aspect ratio of the heat exchanging pipe of the heat exchanging pipe on top, heat exchange arm and bottom is 5-9:5-1:1.
In the tubular heat exchanger that the utility model provides, the caliber of described heat exchanging pipe is not less than the caliber of heat exchange arm, and preferably, described heat exchanging pipe is 1-12:1, more preferably 2-6:1 with the caliber ratio of heat exchange arm.According to the national standard size of heat exchanging pipe, the diameter of described heat exchanging pipe is 19 ~ 200mm, is preferably 38 ~ 100mm, and the caliber of described heat exchanging pipe arm is 10 ~ 200mm, is preferably 19 ~ 38mm.
The distribution radius of heat exchange arm is determined according to the tube pitch between the heat exchanging pipe of each heat exchange unit and concrete heat transfer requirements.Equal in order to ensure the heat exchange area of each heat exchange arm, preferably, the tube pitch between adjacent heat exchange arm is 2 ~ 10:1 with the ratio of the caliber of heat exchange arm, to realize being uniformly distributed of temperature in paste state bed reactor radial direction.Described tube pitch refers to the distance between heat exchanging pipe and heat exchange arm axle center.
A kind of F-T synthesis paste state bed reactor, any one tubular heat exchanger above-mentioned is set in paste state bed reactor, the synthesis gas import of described paste state bed reactor is positioned at the axial region of the heat exchanging pipe arm of described tubular heat exchanger, and described paste state bed reactor top arranges product exit.
The tubular heat exchanger structure that the utility model provides is simple, applied widely, has both been applicable to small-sized paste state bed reactor, is also applicable to the even industrialized large-scale paste state bed reactor of medium-sized paste state bed reactor.Owing to being positioned at the dense distribution of the heat exchange arm of paste state bed reactor bottom, can to a certain degree play the effect being similar to gas distributor, while enhanced heat exchange effect, make bubble distribution in paste state bed reactor evenly, be conducive to reaction and carry out.
The structure of tubular heat exchanger that the utility model provides and F-T synthesis paste state bed reactor is illustrated referring to accompanying drawing, and its application process.
Accompanying drawing 1, accompanying drawing 2 are front view and the cross-sectional view of the first embodiment two-pipe heat exchange unit.As shown in Figure 1 and Figure 2, in a basic heat exchange unit of tubular heat exchanger, top heat exchanging pipe separates two heat exchange arms 2, and the caliber of heat exchanging pipe 1 is not less than the caliber of heat exchange arm 2.Angle between heat exchanging pipe 1 and heat exchange arm 2 is obtuse angle.Fig. 3, Fig. 4 are front view and the cross-sectional view of the second embodiment three-tube type heat exchange unit, and as shown in Figure 3, Figure 4, top heat exchanging pipe separates three heat exchange arms 2, and the caliber of heat exchanging pipe 1 is not less than the caliber of heat exchange arm 2.
The heat exchange unit of many groups is comprised in the tubular heat exchanger that the utility model provides, each heat exchange unit is uniformly distributed on the cross section of paste state bed reactor, be four tube bank tubular heat exchanger cross-sectional views as shown in Figure 5 a, comprise 4 basic heat exchange units in described tubular heat exchanger, 1 heat exchanging pipe in a basic heat exchange unit separates 3 heat exchange arms.Accompanying drawing 5b is the cross-sectional view of 19 tube bank tubular heat exchangers, and comprise 19 basic heat exchange units in described tubular heat exchanger, 1 heat exchanging pipe in a basic heat exchange unit separates 3 heat exchange arms.
According to the size of paste state bed reactor, the tubular heat exchanger that one or more groups the utility model provides can be installed, Fig. 6 is the cross-sectional view of the paste state bed reactor of band tubular heat exchanger, as shown in Figure 6, be provided with in a paste state bed reactor 7 group 19 tube bank tubular heat exchanger, 6 group four restrain tubular heat exchanger and 6 groups of single tube bundle tubular heat exchangers.
The F-T synthesis paste state bed reactor that Fig. 7 a provides for the utility model, any one tubular heat exchanger above-mentioned is set in paste state bed reactor, described tubular heat exchanger comprises heat exchanging pipe and heat exchange arm, heat transferring medium enters shell and tube device by heat transferring medium entrance 3, export 4 by heat transferring medium and discharge tubular heat exchanger, in paste state bed reactor, thermocouple insert port 5 is set vertically, synthesis gas enters paste state bed reactor by synthesis gas entrance 6, react with the catalyst exposure entered by reaction mass entrance 7, the liquid product be obtained by reacting goes out reactor by product exit 8.For the reaction temperature in monitor and forecast paste state bed reactor, arrange organize thermocouple probe more in thermocouple insert port, the Plane Installation schematic diagram of the thermocouple probe vertically in each section A-A of paste state bed reactor, section B-B is shown in shown in Fig. 7 b.
Illustrate structure of the present utility model, using method and effect by the following examples, but therefore the utility model is not subject to any restriction.
Embodiment 1
Paste state bed reactor installs the tubular heat exchanger of 19 tube banks, and as shown in Figure 7, wherein section A-A and section B-B represent the cross section of heat exchanger top and bottom position to structure respectively.As shown in fig. 5b, the front of the heat exchange unit of shell and tube reactor and cross sectional representation are as shown in accompanying drawing 3,4 for paste state bed reactor cross-sectional view.Paste state bed reactor diameter is D=0.5m, and height is H=6m, and in reactor, liquid level height i.e. heat exchanger height are 4m.The length of tubular heat exchanger heat exchanging pipe is 2.8m, and caliber (external diameter) is 25mm, and heat exchange arm adopts equilateral triangle mode to arrange, and the tube pitch of heat exchange arm is 90mm; Point 3 heat exchange arms on every root heat exchanging pipe, in 135 ° of angles between heat exchanging pipe and heat exchange arm, it is 1.2m that length of tube is propped up in heat exchange, and external diameter is 14mm, and the tube pitch of heat exchange arm and heat exchanging pipe is 40mm.
Heat transferring medium enters heat exchanger by heat transferring medium entrance 3, through heat exchanging pipe, flow in each heat exchange arm, discharges tubular heat exchanger finally by heat transferring medium outlet 4.Slurry containing catalyst adds paste state bed reactor from paste state bed reactor bottoms material entrance 7, synthesis gas enters paste state bed reactor through reactor bottom synthesis gas entrance 6, after reaction, gas is from reactor head outflow reactor, and the liquid-phase product comprising catalyst flows out paste state bed reactor from product exit 8.
Axially thermocouple probe is installed at paste state bed reactor, measures the body temperature after heat exchange, thus whether realize uniform heat exchange according to Axial Temperature Distribution determination heat exchanger.Paste state bed reactor section A-A, section B-B are installed 3 thermocouple probes respectively, and on cross section, the arrangement of thermocouple probe as shown in Figure 7b, and the probe of probe is all in distance radial center 1/2 radius.By this 3 some temperature averages and temperature standard variance, check the temperature homogeneity in this cross section.The equidistant installation of axial direction between this two sections 3 thermocouple probes, each thermocouple probe axial spacing is 1m, temperature averages and temperature standard variance is put, the uniformity of inspection axial temperature by 5 on this axial height (including the average temperature value in above-mentioned two sections).When superficial gas velocity is 0.1884m/s, each temperature monitoring point temperature is as shown in table 1,2.
Comparative example 1
In order to the improvement effect of heat exchanger more of the present utility model and other heat exchangers, disclosed in CN101480595A, pin fin-type heat exchanger is applicable to bubbling bed reactor, bubbling bed interior temperature distribution is similar to slurry bed system with flow feature, therefore with heat exchanger of the present utility model there is good comparativity.Except the radius of arm, three parameters such as caliber and distribution radius, other data are all substantially identical with embodiment 1, shell side heat transferring medium gives every root heat exchanging pipe by bottom liquid distributor, overhead-liquid lump device is aggregated into after heat exchange, discharge from heat exchanger, shell-side fluid and tube side medium following current mode upwards flow, and reaction paste adds reactor from bottom, outflow reactor after reaction.In CN101480595A, heat exchanger pin wing damping area density is unit fluid volume, perpendicular to the cross-sectional area of flow direction pin fin, selects pin wing damping area density 4.26m in comparative example
2/ m
3.With similar in embodiment 1, along the equidistant installation in heat exchanger axial height direction 5 thermocouple probes, each thermocouple probe spacing is 1m, and when superficial gas velocity is 0.1884m/s, each temperature monitoring point temperature is as shown in table 1,2.
As shown in Table 1, in embodiment 1, the standard variance of upper and lower section temperature is little compared with the standard variance of section temperature upper and lower in comparative example 1, and the Temperature Distribution of the upper lower section in obvious embodiment one is more even, therefore better uniform heat exchange.As shown in Table 2, the axial temperature standard variance of embodiment 1 is little compared with the axial temperature standard variance of comparative example 1, and the temperature standard variance of visible embodiment 1 is less, and the heat exchanger in obvious embodiment 1 can the axial uniform heat exchange of more effective realization.For at reactor lower part, the distribution that heat exchange arm 2 is intensive, both improve heat transfer effect, can play again the effect of similar gas distributor, contributed to the abundant contact between gas-liquid two-phase.
Table 1 embodiment 1 compares with comparative example 1 radial section monitoring point temperature (DEG C)
Table 2 embodiment 1 and comparative example 1 axially the comparing of each monitoring point temperature (DEG C)
| T down,ave | T 1 | T 2 | T 3 | T up,ave | Standard variance | |
| Embodiment 1 | 220.20 | 220.35 | 221.56 | 220.76 | 220.39 | 0.55 |
| Comparative example 1 | 220.67 | 220.46 | 223.80 | 219.32 | 220.26 | 1.70 |
Embodiment 2
Tubular heat exchanger in medium-sized paste state bed reactor, tubular heat exchanger slurry bed system cross section distribution as shown in Figure 6.The front of shell and tube reactor heat exchange unit and cross sectional representation are as shown in accompanying drawing 3,4.Paste state bed reactor tower diameter is 1m, and tower height is 15m, and heat transferring medium is identical with embodiment 1 with the reaction mass fluid type of flow.Heat exchanging pipe length is 10m, and diameter is 38mm, and tube pitch is 158mm; Heat exchange arm is 3m around the axial vertical length of heat exchanging pipe, the diameter 19mm of heat exchange arm, and the tube pitch of heat exchange arm and heat exchanging pipe is 70mm.
Axially thermocouple probe is installed at paste state bed reactor, measures the body temperature after heat exchange, thus whether realize uniform heat exchange according to Axial Temperature Distribution determination heat exchanger.As shown in accompanying drawing 7a, heat exchanger section A-A, section B-B are installed 3 thermocouple probes respectively, the distribution mode of probe on cross section is as shown in accompanying drawing 7b, and the probe of probe is all in distance radial center 1/2 radius, by this 3 some temperature averages and temperature standard variance, check the temperature homogeneity in this cross section.The equidistant installation of axial direction between this two sections 3 thermocouple probes, each thermocouple probe axial spacing is 3m, by the some temperature averages of 5 on this axial height and temperature standard variance, the uniformity of inspection axial temperature.When superficial gas velocity is 0.25m/s, each temperature monitoring point temperature as shown in Table 3, 4.
Comparative example 2
Structure in comparative example 1 being scaled up into tower diameter is 1m, and tower height is the bubbling bed reactor of 15m, similar to Example 2, and the heat exchanging pipe 1 that same employing 163 heat exchanging pipe overall lengths are 10m, caliber is 38mm, tube pitch is 158mm.Shell-side fluid is identical with embodiment 1 with the tube side fluid type of flow.Identical with comparative example 1, the pin wing density on tubulation wall is also 4.26m
2/ m
3.Similar with embodiment two, along the equidistant installation in heat exchanger axial height direction 5 thermocouple probes, each thermocouple probe spacing is 3m, and when superficial gas velocity is 0.25m/s, each temperature monitoring point temperature as shown in Table 3, 4.
As table 3 is known, in embodiment 2, the standard variance of upper and lower section temperature is little compared with the standard variance of section temperature upper and lower in comparative example 2, the Temperature Distribution of the upper lower section in obvious embodiment 2 is more even, therefore in embodiment 2 two cross sections, place radial direction on the better uniform heat exchange of heat-energy transducer.As shown in Table 4, the axial temperature standard variance of embodiment 2 is little compared with the axial temperature standard variance of comparative example 2, and the temperature standard variance of visible embodiment 2 is less, and the heat exchanger in obvious embodiment 2 can the axial uniform heat exchange of more effective realization.For at reactor lower part, the distribution that arm 2 is intensive, both improve heat transfer effect, can play again the effect of similar gas distributor, contributed to the abundant contact between gas-liquid two-phase.
Table 3 embodiment 2 compares with lower section monitoring point temperature (DEG C) in comparative example 2
Table 4 embodiment 2 and comparative example 2 axially the comparing of each monitoring point temperature (DEG C)
| T down,ave | T 1 | T 2 | T 3 | T up,ave | Standard variance | |
| Embodiment two | 218.20 | 218.22 | 218.58 | 217.46 | 217.36 | 0.53 |
| Comparative example two | 219.28 | 219.56 | 221.23 | 217.67 | 220.19 | 1.31 |
From the comparative result of above-described embodiment and comparative example, the tubular heat exchanger that the utility model provides, effectively can realize the uniform heat exchange of F-T synthesis paste state bed reactor axial direction; And show in the Temperature Distribution of adjacent gas inlets place reactor cross-section, this regional temperature distribution uniform, can meet the heat transfer requirements of F-T synthesis paste state bed reactor preferably.
Claims (10)
1. a tubular heat exchanger, be made up of at least one group of heat exchange unit, it is characterized in that, heat exchange unit comprises the heat exchanging pipe (1) converged through heat exchange arm in top heat exchanging pipe (1), at least two heat exchange arms (2) communicated with heat exchanging pipe and bottom and forms, the caliber of described heat exchanging pipe is not less than the caliber of heat exchange arm, and described heat exchanging pipe and the angle of heat exchange arm are obtuse angle.
2. according to tubular heat exchanger according to claim 1, it is characterized in that, the angle between described heat exchanging pipe and heat exchanging pipe arm is 120 ° ~ 150 °.
3. according to tubular heat exchanger according to claim 2, it is characterized in that, the angle between described heat exchanging pipe and heat exchanging pipe arm is 130 °-140 °.
4. according to tubular heat exchanger according to claim 1, it is characterized in that, in described heat exchange unit, described heat exchange arm is uniformly distributed ringwise centered by heat exchanging pipe, and the number of heat exchange arm is 2 ~ 12.
5. according to tubular heat exchanger according to claim 1, it is characterized in that, in described heat exchange unit, the aspect ratio of the heat exchanging pipe of the heat exchanging pipe on top, the heat exchange arm at middle part and bottom is 5-9:5-1:1.
6. according to tubular heat exchanger according to claim 1, it is characterized in that, described heat exchanging pipe is 1 ~ 12:1 with the caliber ratio of heat exchange arm.
7. according to tubular heat exchanger according to claim 6, it is characterized in that, the diameter of described heat exchanging pipe is 19 ~ 200mm, and the caliber of described heat exchange arm is 10 ~ 200mm.
8. according to tubular heat exchanger according to claim 7, it is characterized in that, the diameter of described heat exchanging pipe is 38 ~ 100mm, and the caliber of described heat exchange arm is 19 ~ 38mm.
9. according to tubular heat exchanger according to claim 1, it is characterized in that, the tube pitch between adjacent described heat exchange arm is 2 ~ 10:1 with the caliber ratio of heat exchange arm.
10. a F-T synthesis paste state bed reactor, it is characterized in that, arrange according to the tubular heat exchanger in claim 1-9 described in any one in paste state bed reactor, the synthesis gas import of described paste state bed reactor is positioned at the axial region of the heat exchange arm of described tubular heat exchanger.
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| CN201520365706.8U CN204739934U (en) | 2015-05-29 | 2015-05-29 | Shell and tube heat exchanger and ft synthesis thick liquid attitude bed reactor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107952493A (en) * | 2016-10-14 | 2018-04-24 | 阿克森斯公司 | For the heat transfer solids cooling device of precise control of temperature, described device can be associated with neither endothermic nor exothermic process |
| CN109173942A (en) * | 2018-09-10 | 2019-01-11 | 李洁 | A kind of tubular heat exchanger and F- T synthesis paste state bed reactor |
| CN111351378A (en) * | 2018-12-21 | 2020-06-30 | 赛峰航空助推器股份有限公司 | Fuel oil heat exchanger |
-
2015
- 2015-05-29 CN CN201520365706.8U patent/CN204739934U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107952493A (en) * | 2016-10-14 | 2018-04-24 | 阿克森斯公司 | For the heat transfer solids cooling device of precise control of temperature, described device can be associated with neither endothermic nor exothermic process |
| CN109173942A (en) * | 2018-09-10 | 2019-01-11 | 李洁 | A kind of tubular heat exchanger and F- T synthesis paste state bed reactor |
| CN109173942B (en) * | 2018-09-10 | 2021-01-01 | 山东嘉隆新能源股份有限公司 | Fischer-Tropsch synthesis slurry bed reactor containing tube type heat exchanger |
| CN111351378A (en) * | 2018-12-21 | 2020-06-30 | 赛峰航空助推器股份有限公司 | Fuel oil heat exchanger |
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