CN1627035A - Gas and solid circular flow warmer - Google Patents
Gas and solid circular flow warmer Download PDFInfo
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- CN1627035A CN1627035A CN 200410033932 CN200410033932A CN1627035A CN 1627035 A CN1627035 A CN 1627035A CN 200410033932 CN200410033932 CN 200410033932 CN 200410033932 A CN200410033932 A CN 200410033932A CN 1627035 A CN1627035 A CN 1627035A
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- 239000007787 solid Substances 0.000 title claims abstract description 69
- 239000002245 particle Substances 0.000 claims description 41
- 239000011148 porous material Substances 0.000 claims description 8
- 238000005057 refrigeration Methods 0.000 claims description 6
- 238000005192 partition Methods 0.000 claims description 4
- 238000012546 transfer Methods 0.000 abstract description 44
- 230000000694 effects Effects 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 3
- 239000008187 granular material Substances 0.000 abstract 1
- 230000003134 recirculating effect Effects 0.000 abstract 1
- 239000012530 fluid Substances 0.000 description 11
- 238000000034 method Methods 0.000 description 10
- 239000000498 cooling water Substances 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 230000005484 gravity Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 230000001965 increasing effect Effects 0.000 description 4
- 238000005728 strengthening Methods 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 230000002411 adverse Effects 0.000 description 2
- 230000003416 augmentation Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 230000005514 two-phase flow Effects 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/10—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically
- F28D7/12—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged one within the other, e.g. concentrically the surrounding tube being closed at one end, e.g. return type
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
- F28D2021/0045—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for granular materials
Abstract
The invention relates to a gas-solid recirculating heating apparatus. It includes the following components: circular tank type vertical shell body, feeding pipe, gas outlet pipe, solid granules outlet pipe, draft tube, gas distributor and porous sieve plate, etc. Said invention also provides the concrete structure of the every component and their connection mode. Said invention is not only simple in structure, but also its heat transfer coefficient is high and its heat transfer effect is good.
Description
Technical field
The present invention relates to a kind of heat collector, especially a kind of gas-solid loop flow heat collector belongs to chemical process and apparatus field.
Background technology
Heat exchanger is the common apparatus of chemical industry, oil, power, food and other many industrial departments, occupies very consequence aborning.It can be divided into heater, heat collector (cooler), condenser, evaporimeter and reboiler etc. by purposes.Principle and mode by exchange heat can be divided into hybrid (direct contact type), heat accumulating type (back-heating type) and dividing wall type three classes.
The characteristics of dividing wall type heat exchanger are between hot and cold two kinds of fluids a solid wall surface to be arranged, and in two side flow of solid wall surface, two kinds of fluids directly do not contact two fluids respectively, and heat transmits by wall.Industrial most widely used heat exchanger promptly is a dividing wall type.According to the pattern of heat-transfer area, dividing wall type heat exchanger can be divided into the custom design heat exchanger of jacket type, tubular type, board-like and various special-shaped heat-transfer area composition.
The emphasis of design of heat exchanger is the reinforcement of heat transfer process, is exactly how to improve the rate of heat transfer between cold and hot fluid in the heat exchanger.By total rate of heat transfer equation Q=KA Δ Tm as can be seen, enhancing heat transfer K, heat transfer area A or mean temperature difference Δ Tm all can improve rate of heat transfer.
The method of expansion heat transfer area should be reasonably to improve the heat transfer area of FU volume, as adopt finned tube, bellows, screwed pipe to replace light pipe etc., from improving the angle increasing heat transfer area of heat-transfer area structure and layout, to reach efficient, the compact purpose of heat transmission equipment.
The size of mean temperature difference depends primarily on the temperature conditions of two fluids, but when two fluids in the heat exchanger all do not have phase transformation, adopts adverse current or can obtain bigger heat transfer temperature difference near the flow direction of adverse current from structure.
Enhancing heat transfer be in strengthening heat transfer, should consider emphatically aspect.Desire improves heat transfer coefficient, just must reduce convection heat transfer' heat-transfer by convection thermal resistance, dirtiness resistance and wall resistance.Because every thermal resistance portion difference, so should manage to reduce main thermal resistance in the diabatic process.In heat transmission equipment, the metal partition is relatively thinner and thermal conductivity factor is higher, generally can not become main thermal resistance.Cooling medium in the heat removing tube can adopt demineralized water, thereby can reduce even avoid the formation of inside pipe wall dirtiness resistance.Therefore, thermal-convection resistance becomes the key that improves heat transfer coefficient.Cooling medium water in the heat removing tube undergoes phase transition in heat transfer process, and heat transfer coefficient is very high.So improving the outer fluid convection heat transfer coefficient of heat removing tube is the key of augmentation of heat transfer.The method that the approach of strengthening fluid convection heat transfer' heat-transfer by convection strengthens convection heat transfer' heat-transfer by convection mainly contains: 1. the flow condition that changes fluid.2. change physical properties of fluids.3. change the heating surface situation.
The circulation chemical reactor is a kind of novel reactor that occurred in 20th century.It combines the advantage of bubble tower and mechanical stirring kettle, have gas holdup height, heat and mass speed fast, mix, good characteristic such as simple in structure.Research concentrates on solution-air and gas-liquid-solid three-phase system at first, extends to gas-solid system afterwards again.
Present catalytic cracking external warmer is not also used circulation type heat-obtaining mode, but adopts the way that increases heat-obtaining tube bank and fin to increase heat transfer area, has increased production cost; And the gas-solid two-phase is disposable by heat-obtaining tube bank heat exchange, and heat transfer coefficient is not high enough, and demands urgently further being improved.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of gas-solid loop flow heat collector, by changing the flow condition of fluid, the circulation that forms the gas-solid two-phase flows, improve the outer gas-solid two-phase convective heat-transfer coefficient of heat-obtaining tube bank, reduced thermal-convection resistance, realize strengthening the purpose of conducting heat, can reduce the quantity of heat-obtaining tube bank simultaneously, save cost.
Technical problem to be solved by this invention is achieved by the following technical solution:
A kind of gas-solid loop flow heat collector, it comprises the housing that the round can type is erect, and the top of described housing is provided with feed pipe, and the top is provided with gas outlet tube, and the bottom is a funnel-form, and in the perpendicular downwards solid particle outlet of establishing of end; Bottom in the described housing is provided with the guide shell with the coaxial upper and lower opening of housing, this guide shell comprises the heat removing tube that is circle-shaped setting arrangement, on the heat removing tube outer wall, be provided with fin vertically, fin is two or a multi-disc of symmetry, and the mutual overlap joint of the fin on the adjacent heat removing tube surrounds guide shell; The two ends mouth of pipe of described heat removing tube stretches out outside the housing respectively, and is connected with the external refrigeration circulation;
The fin of described heat removing tube is for axially to be welded on the outer wall of heat removing tube, and to extending all around, the layout of fin will be guaranteed the formation guide shell that can overlap mutually of the fin between the different heat removing tubes, and fin is two or a multi-disc of symmetry, and its concrete number is determined according to required heat transfer area;
Described guide shell is divided into inside and outside two parts with the lower space in the housing, and the guide shell inner space is the guide shell district, and the zone between guide shell and the housing is an annulus;
Described guide shell district and annulus below are respectively equipped with annular tube shaped guide shell district gas distributor and annulus gas distributor, and its tube wall has pore, and is provided with the air inlet pipe that connects the hull outside feeder in a side;
Top in the described housing is provided with funnel shaped porous sieve plate, and terminal the erecting downwards of porous sieve plate established the center tremie pipe, and the center tremie pipe extends downwardly into the guide shell district.
Described heat removing tube is a coaxial sleeve, pipe and outer tube in being divided into, and the outer tube endcapped also is connected with interior pipe in inner; Described heat removing tube top curves and stretches out outside the housing to hull outside, and is connected with the external refrigeration circulation respectively; Described fin can be divided into more than one section or one section in the axial direction; The hop count that described guide shell is divided in the axial direction according to fin on the heat removing tube forms single hop guide shell or two sections guide shells or multistage guide shell.
Described center tremie pipe extends downwardly into bottom, guide shell district, also can extend to the middle part or the top in guide shell district.
The pore of described gas distributor is offered downwards, can effectively avoid the obstruction of solid particle; Described air vent aperture is 3～20mm, and percent opening is 0.05～3%.
The angle angle of described porous sieve plate wooden partition is 45 °～120 °, and the aperture of perforate is 5～30mm, percent opening 3～20%.
The angle of described funnel shaped bottom outer wall angle is 45 °～90 °.
Gas enters guide shell district gas distributor and annulus gas distributor by the air inlet pipe of hull outside by gas distributor, and by the pore ejection, enters guide shell district and annulus respectively; (guide shell district linear gas velocity is controlled at 0.1～0.8m/s to gas output by regulating guide shell district's gas distributor and annulus gas distributor, the annulus linear gas velocity is controlled at 0～0.2m/s) makes the tolerance that enters the guide shell district much larger than the tolerance that enters annulus, therefore, the bed density of annulus is greater than the bed density in guide shell district, and the bed layer pressure of annulus bottom is greater than the bed layer pressure of bottom, guide shell district.
The solid particle for the treatment of heat-obtaining enters heat collector by feed pipe, enters bottom, guide shell district through funnel shaped porous sieve plate and center tremie pipe.
Cooling circulating water is entered by the interior pipe of heat removing tube; The solid particle quilt that arrives bottom, guide shell district is upwards flowed by the gas drive of guide shell district gas distributor ejection, passes through the outer wall and the fin of heat removing tube in flow process, with the cooling water heat exchange in the heat removing tube; When solid particle arrived the top in guide shell district, most of bubble broke and separates with solid particle, and isolated gas passes how empty sieve plate to be continued upwards, is discharged by the blast pipe at heat collector top; Solid particle after the separation is carried the gas separated that is not able to do in time on a small quantity secretly and is entered annulus, relies on gravity to flow downward, and once more with heat removing tube in the cooling water heat exchange; When solid particle arrived the annulus bottom, because the bed layer pressure of annulus bottom is higher than the bed layer pressure of bottom, guide shell district, most of solid particle flowed back to bottom, guide shell district, forms circulation; The fraction solid particle falls into the solid particle outlet of bottom because the gravity effect flows downward.Solid particle behind the heat-obtaining is emitted by heat collector bottom solid particle outlet, and gas is discharged by heat collector upper gas outlet, and the water vapour D that forms in the heat removing tube is discharged by outer tube.
Gas-solid loop flow heat collector of the present invention belongs to the dividing wall type heat collector, structurally constitutes guide shell, makes the gas-solid two-phase form circulation and flows, and improves the outer gas-solid two-phase convective heat-transfer coefficient of heat-obtaining tube bank, has reduced thermal-convection resistance, realizes strengthening the purpose of conducting heat.Adopted coaxial sleeve and fin to increase heat transfer area simultaneously, the quantity of heat-obtaining tube bank of having utilized the guide shell structure decrease provides cost savings.
Description of drawings
Fig. 1 is the heat collector structural representation of first embodiment of the present invention;
Fig. 2 is a guide shell horizontal section structure chart of the present invention;
Fig. 3 is a heat removing tube structural representation of the present invention;
Fig. 4 is the heat removing tube structural representation with two sections fins of the present invention;
Fig. 5 is an annular tube shaped gas distributor face upwarding assumption diagram of the present invention;
Fig. 6 looks squarely partial sectional view for annular tube shaped gas distributor of the present invention;
Fig. 7 is the heat collector structural representation of second embodiment of the present invention.
The specific embodiment
Below in conjunction with the drawings and specific embodiments technical scheme of the present invention is further specified:
First embodiment:
As shown in Figure 1, heat collector structural representation for first embodiment of the present invention, a kind of gas-solid loop flow heat collector, it comprises the housing 1 that the round can type is erect, the top of this housing 1 is provided with feed pipe 6, and the top is provided with gas outlet tube 7, and the bottom is a funnel-form, the angle beta of its outer wall angle is 45 °～90 °, and in the perpendicular downwards solid particle outlet 8 of establishing of end;
Bottom in the housing 1 is provided with the guide shell 2 with the coaxial upper and lower opening of housing 1, this guide shell 2 comprises the heat removing tube 20 that is circle-shaped setting arrangement, on heat removing tube 20 outer walls, be provided with fin 201 vertically, fin 201 is two or a multi-disc of symmetry, and the 201 mutual overlap joints of the fin on the adjacent heat removing tube 20 surround guide shell 2; The mouth of pipe of heat removing tube 20 stretches out outside the housing 1, and is connected with the external refrigeration circulation; The fin 201 of heat removing tube 20 is for axially to be welded on the outer wall of heat removing tube 20, and to extending all around, the layout of fin 201 will be guaranteed that the fin 201 between the adjacent heat removing tube 20 can overlap mutually and form guide shell 2, fin 201 is two or a multi-disc of symmetry, and its concrete number is determined according to required heat transfer area.
Top in housing 1 is provided with funnel shaped porous sieve plate 4, and the angle angle [alpha] of porous sieve plate 4 wooden partitions is 45 °～120 °, and the aperture of perforate is 5～30mm, percent opening 3～20%; Porous sieve plate 4 terminal erecting are downwards established center tremie pipe 5, and center tremie pipe 5 extends downwardly into 21 bottoms, guide shell district.
The structure of aforesaid guide shell 2, as shown in Figure 2, guide shell 2 is surrounded by fin 201 overlap joint of heat removing tube 20, and heat removing tube 20 is circumferential arrangement in housing 1, and its fin 201 overlaps mutually and forms the cylinder-like structure coaxial with housing 1.
The structure of aforesaid heat removing tube 20, as shown in Figure 3, heat removing tube 20 is a coaxial sleeve, being nested together by the different pipe of diameter forms, pipe 202 and outer tube 204 in being divided into, outer tube 204 endcappeds also are connected with interior pipe 202 in inner; Heat removing tube 20 tops curve and stretch out outside the housing 1 to housing 1 outside, and are connected with the external refrigeration circulation respectively; Cooling circulating water C is entered by interior pipe 202, and by outer tube wall 203 and the solid particle A heat exchange for the treatment of heat-obtaining, the steam D of formation is discharged by outer tube 204 at outer tube 204.For increasing heat exchange area, outer tube wall 203 axially is welded with the fin 201 that extends to all around, and fin 201 is at least two of symmetry, also can be multi-disc as required.Fin 201 also is the critical component that forms guide shell 2 (as shown in Figure 2) except increasing heat exchange area.Fin 201 can be divided in the axial direction more than one section or one section and (as shown in Figure 4, is the heat removing tube structural representation with two sections fins).
The structure of aforesaid guide shell district gas distributor 31 and annulus gas distributor 32, as Fig. 5 and shown in Figure 6, gas distributor 31 or 32 is annular tube shaped structure, and has pore 33 straight down, is provided with air inlet pipe 34 in a side.Pore 33 apertures are 3～20mm, and percent opening is 0.05～3%, and the obstruction of solid particle can be effectively avoided in perforate straight down.Gas B enters gas distributor 31 or 32 by air inlet pipe 34, again by pore 33 ejections.
The concrete steps of present embodiment are as follows:
As shown in Figure 1, the solid particle A that treats heat-obtaining enters by the feed pipe 6 on heat collector top, relies on gravity to fall on the funnel shaped porous sieve plate 4, enters 21 bottoms, guide shell district through center tremie pipe 5 then.
Gas B enters guide shell district 21 and annulus 22 respectively by guide shell district gas distributor 31 and annulus gas distributor 32 simultaneously, (guide shell district linear gas velocity is controlled at 0.1～0.8m/s to gas flow by regulating guide shell district 21 and annulus 22, the annulus linear gas velocity is controlled at 0～0.2m/s), make guide shell district 21 gas flows much larger than annulus 22 gas flows, then annulus 22 bed densities are greater than guide shell district 21 bed densities, and annulus 22 bottom bed stressor layers are greater than guide shell district 21 bottom bed stressor layers.
The solid particle A quilt that arrives 21 bottoms, guide shell district is upwards flowed by the gas B drive of guide shell district gas distributor 31 ejections, passes through the outer wall and the fin 201 of heat removing tube 20 in flow process, with the cooling water C heat exchange in the heat removing tube 20; When solid particle A arrived the top in guide shell district 21, most of bubble broke and separates with solid particle A, and isolated gas B passes how empty sieve plate 4 to be continued upwards, is discharged by the gas outlet tube 7 at heat collector top; Solid particle A after the separation carries the gas separated B that is not able to do in time on a small quantity secretly and enters annulus 22, relies on gravity to flow downward, and once more with heat removing tube 20 in cooling water C heat exchange; When solid particle A arrives 22 bottoms, belt district, because the bed layer pressure of annulus 22 bottoms is higher than the bed layer pressure of 21 bottoms, guide shell district, most of solid particle A flows back to 21 bottoms, guide shell district, form circulation, reach the heat transfer boundary layer of eliminating between heat removing tube 20 and the solid particle A, strengthen the convection heat transfer' heat-transfer by convection process, improve the purpose of heat-transfer effect; Fraction solid particle A falls into the solid particle outlet 8 of bottom because the gravity effect flows downward.
After solid particle A carries out repeatedly circulation heat-exchange around the guide shell 2 that is formed by heat removing tube 20, emitted by heat collector bottom solid particle outlet 8, gas B is discharged by heat collector upper gas outlet 7, and the water vapour D that forms in the heat removing tube 20 is discharged by outer tube.
Second embodiment:
As shown in Figure 7, be the structural representation of second embodiment of the present invention, the basic structure of its gas-solid loop flow heat collector is identical with first embodiment of the present invention; Different is with first embodiment of the present invention, and heat removing tube 20 has two sections fins 201 to be arranged by mode shown in Figure 4, and fin 201 overlaps mutually and forms two sections guide shell 2a and 2b.
The concrete steps of present embodiment are as follows:
As shown in Figure 7, the solid particle A that treats heat-obtaining is entered by the feed pipe 6 on heat collector top, enters one section guide shell 2a bottom through funnel shaped porous sieve plate 4 and center tremie pipe 5; Gas B enters guide shell district 21 and annulus 22 respectively by guide shell district gas distributor 31 and annulus gas distributor 32 simultaneously, (guide shell district linear gas velocity is controlled at 0.1～0.8m/s to gas flow by regulating guide shell district 21 and annulus 22, the annulus linear gas velocity is controlled at 0～0.2m/s), make the gas flow that enters guide shell district 21 much larger than the gas flow that enters annulus 22, then annulus 22 bed densities are greater than guide shell district 21 bed densities, and annulus 22 bottom bed stressor layers are greater than guide shell district 21 bottom bed stressor layers.
The solid particle A quilt that arrives 21 bottoms, guide shell district is upwards flowed by the gas B drive of guide shell district gas distributor 31 ejections, passes through the outer wall and the fin 201 of heat removing tube 20 in flow process, with the cooling water C heat exchange in the heat removing tube 20; When arriving two sections guide shell 2b tops, gas B separates with solid particle A, and gas B passes porous sieve plate 4 to be continued upwards, is discharged by the gas outlet tube 7 at heat collector top; Solid particle A after the separation carries the gas separated B that is not able to do in time on a small quantity secretly and enters annulus 22, dependence gravity flows downward, and once more with heat removing tube 20 in cooling water C heat exchange, when arriving the bottom of two sections guide shell 2b, part solid particle A returns guide shell district 21, diversed tube district air-flow drives again and upwards flows, and forms two sections circulation; Another part solid particle A continues to flow downward at annulus 22, and once more with heat removing tube 20 in cooling water C heat exchange, when arriving the bottom of one section guide shell 2a, because the bed layer pressure of annulus 22 bottoms is higher than the bed layer pressure of 21 bottoms, guide shell district, most of solid particle A flows back to 21 bottoms, guide shell district, form one section circulation, fraction solid particle A falls into the solid particle outlet 8 of bottom because the gravity effect flows downward;
Solid particle A between annulus 22 and guide shell district 21 through after the cooling water C heat exchange in repeatedly circulation and the heat removing tube 20, emit by heat collector bottom solid particle outlet 8, gas B is discharged by heat collector upper gas outlet 7, and the water vapour D that forms in the heat removing tube 20 is discharged by outer tube.
Implementation of the present invention can also further be divided into multistage with the fin on the heat removing tube on this basis, constitutes the multistage guide shell, makes solid particle form multistage circulation, thereby forms multistage circulation heat collector.
The present invention utilizes the good heat-transfer character of circulating device by the careful analysis to the augmentation of heat transfer means, designs a kind of gas-solid loop flow heat collector.It is good to have heat-transfer effect, and heat-transfer intensity is big, and equipment is simple, and advantages such as cost are saved in control easily.Can be widely used in the chemical process that relates to gas-solid two-phase heat-obtaining, as catalytic cracked regenerated catalyst outside heat removing process.
It should be noted last that, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although the present invention is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement technical scheme of the present invention, and not breaking away from the spirit and scope of technical solution of the present invention, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (7)
1, a kind of gas-solid loop flow heat collector, it comprises the housing that the round can type is erect, the top of described housing is provided with feed pipe, the top is provided with gas outlet tube, the bottom is a funnel-form, and in the perpendicular downwards solid particle outlet of establishing of end, it is characterized in that: the bottom in the described housing is provided with the guide shell with the coaxial upper and lower opening of housing, this guide shell comprises the heat removing tube that is circle-shaped setting arrangement, on the heat removing tube outer wall, be provided with fin vertically, fin is two or a multi-disc of symmetry, and the mutual overlap joint of the fin on the adjacent heat removing tube surrounds guide shell; The two ends mouth of pipe of described heat removing tube stretches out outside the housing respectively, and is connected with the external refrigeration circulation;
Described guide shell is divided into inside and outside two parts with the lower space in the housing, and the guide shell inner space is the guide shell district, and the zone between guide shell and the housing is an annulus;
Described guide shell district and annulus below are respectively equipped with annular tube shaped guide shell district gas distributor and annulus gas distributor, the tube wall of described guide shell district's gas distributor and annulus gas distributor has axial pore, and is provided with the air inlet pipe that connects the hull outside feeder in a side;
Top in the described housing is provided with funnel shaped porous sieve plate, and terminal the erecting downwards of porous sieve plate established the center tremie pipe, and the center tremie pipe extends downwardly into the guide shell district.
2, gas-solid loop flow heat collector according to claim 1 is characterized in that: described center tremie pipe extends downwardly into bottom, guide shell district.
3, gas-solid loop flow heat collector according to claim 1, it is characterized in that: described heat removing tube is a coaxial sleeve, pipe and outer tube in being divided into, the outer tube endcapped also is connected with interior pipe in inner, the heat removing tube top curves and stretches out outside the housing to hull outside, and is connected with the external refrigeration circulation respectively.
4, gas-solid loop flow heat collector according to claim 3 is characterized in that: described fin can be divided into more than one section or one section in the axial direction; The hop count that described guide shell is divided in the axial direction according to fin on the heat removing tube forms single hop guide shell or two sections guide shells or multistage guide shell.
5, according to claim 1 or 2 or 3 or 4 described gas-solid loop flow heat collectors, it is characterized in that: the pore of described gas distributor is offered downwards, and described air vent aperture is 3～20mm, and percent opening is 0.05～3%.
6, according to claim 1 or 2 or 3 or 4 described gas-solid loop flow heat collectors, it is characterized in that: the angle angle of described porous sieve plate wooden partition is 45 °～120 °, and the aperture of perforate is 5～30mm, percent opening 3～20%.
7, according to claim 1 or 2 or 3 or 4 described gas-solid loop flow heat collectors, it is characterized in that: the angle of described funnel shaped bottom outer wall angle is 45 °～90 °.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100339322A CN1313795C (en) | 2004-04-19 | 2004-04-19 | Gas and solid circular flow warmer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100339322A CN1313795C (en) | 2004-04-19 | 2004-04-19 | Gas and solid circular flow warmer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1627035A true CN1627035A (en) | 2005-06-15 |
| CN1313795C CN1313795C (en) | 2007-05-02 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100339322A Expired - Lifetime CN1313795C (en) | 2004-04-19 | 2004-04-19 | Gas and solid circular flow warmer |
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| Country | Link |
|---|---|
| CN (1) | CN1313795C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102080940A (en) * | 2010-12-30 | 2011-06-01 | 南京圣诺热管有限公司 | Process gas afterheat recovery device of coking carbonization chamber furnace top and heat-removing element |
| CN103743265A (en) * | 2014-01-22 | 2014-04-23 | 衢州昀睿工业设计有限公司 | Spray water-cooling condenser |
| CN109331746A (en) * | 2018-09-28 | 2019-02-15 | 大连理工大学 | A kind of novel solid particle thermal chemical reaction device and method |
| CN109780916A (en) * | 2019-01-17 | 2019-05-21 | 南京华电节能环保设备有限公司 | The device and method that suspension type flash cooler, blast furnace cinder recovery waste heat generate electricity |
| CN111076575A (en) * | 2019-12-13 | 2020-04-28 | 天津大学 | Spiral plate heat exchange device of gas-solid circulating fluidized bed and operation method thereof |
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| US4189299A (en) * | 1978-03-13 | 1980-02-19 | Calcimatic International, Limited | Direct cooler for calcining apparatus |
| CN2287519Y (en) * | 1997-01-03 | 1998-08-12 | 清华大学 | Gas-solid-solid external circulation fluidizing reactor for catalytic reaction system |
| US5906482A (en) * | 1997-07-01 | 1999-05-25 | Extru-Tech, Inc. | Double wall vertical cooler |
| CN1060404C (en) * | 1998-05-21 | 2001-01-10 | 石油大学(北京) | Gas-solid quickly separating method and apparatus for lift-leg outlet having close-phase circulation prestripping device |
| CN2455355Y (en) * | 2000-11-10 | 2001-10-24 | 石油大学(北京) | High performance reproduced catalyst stripping apparatus |
| CN2518585Y (en) * | 2001-12-20 | 2002-10-30 | 沈阳化工研究院 | Gas spouted outside circulation reaction device |
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2004
- 2004-04-19 CN CNB2004100339322A patent/CN1313795C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102080940A (en) * | 2010-12-30 | 2011-06-01 | 南京圣诺热管有限公司 | Process gas afterheat recovery device of coking carbonization chamber furnace top and heat-removing element |
| CN103743265A (en) * | 2014-01-22 | 2014-04-23 | 衢州昀睿工业设计有限公司 | Spray water-cooling condenser |
| CN103743265B (en) * | 2014-01-22 | 2015-05-20 | 衢州昀睿工业设计有限公司 | Spray water-cooling condenser |
| CN109331746A (en) * | 2018-09-28 | 2019-02-15 | 大连理工大学 | A kind of novel solid particle thermal chemical reaction device and method |
| CN109331746B (en) * | 2018-09-28 | 2021-11-19 | 大连理工大学 | Novel solid particle thermochemical reaction device and method |
| CN109780916A (en) * | 2019-01-17 | 2019-05-21 | 南京华电节能环保设备有限公司 | The device and method that suspension type flash cooler, blast furnace cinder recovery waste heat generate electricity |
| CN109780916B (en) * | 2019-01-17 | 2024-02-20 | 南京华电节能环保股份有限公司 | Suspension type rapid cooler, device and method for generating power by recycling waste heat of blast furnace slag |
| CN111076575A (en) * | 2019-12-13 | 2020-04-28 | 天津大学 | Spiral plate heat exchange device of gas-solid circulating fluidized bed and operation method thereof |
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