CN102288044A - Pipeless heat exchanger and residual-heat recovery system - Google Patents
Pipeless heat exchanger and residual-heat recovery system Download PDFInfo
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- CN102288044A CN102288044A CN2011102066353A CN201110206635A CN102288044A CN 102288044 A CN102288044 A CN 102288044A CN 2011102066353 A CN2011102066353 A CN 2011102066353A CN 201110206635 A CN201110206635 A CN 201110206635A CN 102288044 A CN102288044 A CN 102288044A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C3/00—Other direct-contact heat-exchange apparatus
- F28C3/10—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material
- F28C3/12—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid
- F28C3/14—Other direct-contact heat-exchange apparatus one heat-exchange medium at least being a fluent solid, e.g. a particulate material the heat-exchange medium being a particulate material and a gas, vapour, or liquid the particulate material moving by gravity, e.g. down a tube
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Abstract
The invention discloses a pipeless heat exchanger and a residual-heat recovery system. The pipeless heat exchanger is formed by connecting at least one granule-curtain heat-exchanging unit, the granule-curtain heat-exchanging unit is provided with a horizontal straight-pipe-shaped gas passage, a granule inlet and a granule outlet are arranged on the gas passage, a granule curtain is formed by granules as heat-exchanging media from the granule inlet to the granule outlet, and the granules are inert solid granules. The residual-heat recovery system comprises a pipeless heat exchanger called as a smoke-gas pipeless heat exchanger, a pipeless heat exchanger called as an air pipeless heat exchanger and a granule-conveying device, wherein smoke is introduced into the smoke-gas pipeless heat exchanger, air is introduced into the air pipeless heat exchanger, and the smoke-gas pipeless heat exchanger, the air pipeless heat exchanger and the granule-conveying device are connected through granule pipelines. The pipeless heat exchanger and the residual-heat recovery system disclosed by the invention have the advantages of high heat-exchanging efficiency, low equipment-material consumption, low operating and maintenance cost, good sealing property and low energy consumption and are applicable to various kinds of industrial equipment and reactors with higher gas-discharging temperature and residual-heat utilizing value.
Description
Technical field
The present invention relates generally to high efficient heat exchanging and heat recovery technical field, be specially adapted to have the various industrial equipments and the reactor of higher exhaust gas temperature and UTILIZATION OF VESIDUAL HEAT IN value, comprise Industrial Boiler, station boiler, various stove, smelting furnace, sintering furnace, heating furnace and waste calcining facility etc.
Technical background
There are the surprising various Industrial Boilers of number, station boiler, metallurgical furnace and various heating stove in China, and the primary energy that these boiler and stoves consumed accounts for three/the last two of China's fossil fuel.Because the reason of the fuel characteristic, operating condition and the equipment deficiency that use in the design defect of these boilers and stove and running aspects such as (descending) as heat transfer efficiency, make the delivery temperature of most of boilers and stove be higher than design load (40～150 ℃), thereby caused great energy waste.
Existing Industrial Boiler, station boiler and industrial heating furnace adopt shell-and-tube or regenerative air preheater based on metal or glass material to reclaim the air that its using waste heat from tail gas is used with preheated burning mostly, and then improve catching fire and burning of fuel.Owing to be subjected to the restriction of air preheater structure and heat-transfer mechanism aspect, shell that these are traditional and heat accumulating type do not have heat exchange of heat pipe and exist following problem also not to be resolved for a long time all the time: (1) heat exchange efficiency is not high, the metal of no heat exchange of heat pipe or glass consumption are huge, the equipment heaviness, manufacturing, operation and maintenance cost height; (2) inleakage big (8%～30%) makes and send the air-introduced machine power consumption to increase more than 15～30%, and has a strong impact on unit operation and exert oneself; (3) very easily cause fouling of heating surface, obstruction, cold end corrosion, increase flowing resistance (up to 2500Pa) greatly, thereby increase the operation expense that send air-introduced machine power consumption and equipment greatly; (4) be difficult to further improve the temperature (mostly about 400 ℃) of preheated air, thereby be difficult to reach various low-quality solid fuel stability and high efficiencies burnings and low-quality gas, the aphlogistic high temperature requirement of liquid fuel; (5) when boiler or stove existed design and equipment deficiency, fuel quality and operating mode to change, the preheater of existing structure did not have real-time regulating measure etc.
Summary of the invention
The object of the present invention is to provide a kind of heat exchange efficiency height, the equipment consumptive material is low, operation and maintenance cost is low, good airproof performance, no heat exchange of heat pipe and residual neat recovering system that energy consumption is low.
This no heat exchange of heat pipe provided by the invention is linked to be by a particle curtain heat exchange unit at least, described particle curtain heat exchange unit has the tubular gas passage of straight horizontal, this gas passage is provided with a particle import and a particle outlet, particle forms the particle curtain as heat transferring medium from the particle import to particle outlet, described particle is an inert solid particle.
Described inert solid particle adopts the mixing of a kind of in silica sand and the aluminium oxide or two kinds, and particle diameter is below 250 microns.
In order to make no heat exchange of heat pipe that the multi-stage heat exchanger effect be arranged, no heat exchange of heat pipe is vertically arranged series connection up and down by bend pipe with the particle curtain that plural at least particle curtain heat exchange unit is linked to be snakelike and each particle curtain heat exchange unit, and perhaps this no heat exchange of heat pipe is linked to be the tubular and particle curtain each particle curtain heat exchange unit of straight horizontal by straight tube with plural at least particle curtain heat exchange unit and vertically arranges.
In order to regulate grain flux and to make uniform particles enter the particle import, described particle import department is provided with grain flux regulating part, particle current-sharing part.
In order effectively to shorten the length of particle curtain, described particle import department is provided with the guide into the particle guiding.
In order to make between gas and the particle curtain heat exchange abundant, the gas passage front end of this no heat exchange of heat pipe is connected with gas current-sharing member, gas enters gas passage through this current-sharing member, described gas current-sharing member comprises the big orifice plate of current-sharing bare cloth, current-sharing flute plate, big orifice plate gathers, to form the current-sharing of 3-5 level, described flute plate is arranged side by side by many straight tubes and is formed.
The residual neat recovering system that the present invention makes with above-mentioned no heat exchange of heat pipe, comprise that no heat exchange of heat pipe that a no heat exchange of heat pipe that feeds flue gas is referred to as flue gas and does not have heat exchange of heat pipe, a bubbling air is referred to as air and does not have heat exchange of heat pipe, particle transport device, by the particle pipeline connect described flue gas and do not have heat exchange of heat pipe, air does not have heat exchange of heat pipe and particle transport device.
As preferential embodiment, flue gas does not have heat exchange of heat pipe and air and does not have heat exchange of heat pipe and all adopt snakelikely, and flue gas does not have heat exchange of heat pipe and is arranged in air and do not have the heat exchange of heat pipe top, does not have heat exchange of heat pipe with air and connects.Perhaps flue gas does not have heat exchange of heat pipe and air does not have heat exchange of heat pipe and all adopts snakelikely, and flue gas does not have heat exchange of heat pipe and air, and not have heat exchange of heat pipe in parallel.Perhaps flue gas does not have heat exchange of heat pipe and air does not have heat exchange of heat pipe and all adopts straight horizontal tubular, flue gas does not have the particle curtain of each particle curtain heat exchange unit of heat exchange of heat pipe and connects one to one with the particle curtain that air does not have each particle curtain heat exchange unit of heat exchange of heat pipe, form corresponding closed circuit, parallel between each loop.Perhaps flue gas does not have heat exchange of heat pipe and air does not have heat exchange of heat pipe and all adopts straight horizontal tubular, and flue gas does not have the particle curtain of each particle curtain heat exchange unit of heat exchange of heat pipe and connects with the particle curtain that air does not have each particle curtain heat exchange unit of heat exchange of heat pipe.
The present invention do not have heat exchange of heat pipe with the particle curtain as heat transferring medium, this heat exchange mode can make gas and particle reach thermal balance fast, thereby significantly improve heat exchange efficiency, the present invention does not have residual neat recovering system that heat exchange of heat pipe forms and does not have the heat exchange of heat pipe technology with traditional shell-and-tube and compare with equipment, there is not the shell-and-tube heating surface in the conventional tube shell heat exchanger, but utilize the fine particle and the direct contact heat-exchanging of air-flow of the very big and good fluidity of specific area, thereby this heat transfer technology is a kind of brand-new heat exchange and heat recovery technology.Compare with system with various industrial heat exchange that adopt in the present industrial circle and heat recovery technology device, this heat transfer technology based on particle curtain in the no heat exchange of heat pipe has very remarkable technical performance:
(1) air leakage coefficient of heat transmission equipment can be reduced to minimum, can reduce to 0 in theory, and the flow resistance of flue gas and air is very little, has only 1/5～1/3 of existing heat transmission equipment and system;
(2) heat exchange efficiency is than high more than 3～5 times based on traditional heat transmission equipment of shell-and-tube heat exchanger, thereby the volume of heat-exchanger rig and steel consumption amount will significantly reduce, and equipment manufacturing cost reduces greatly;
(3) ceiling temperature that can break through existing heat transmission equipment limits, the temperature of combustion air can be heated to higher temperature levels (more than 800 ℃), thereby the stable and efficient burning that can be various low-rank fuels creates very advantageous conditions, also will bring major transformation for the design of combustion apparatus such as boiler;
(4) can be coupled thermal current/cold particle, cold airflow/two heat transfer process of hot particle and heat transfer process is carried out continuously, thereby can effectively overcome many technological deficiencies in the heat accumulating type high-temperature preheater system, for the high-temperature air burning or the MILD burning of the low-quality gaseous fuel of metallurgy industry provides the brand-new technology support;
(5) the correlation technique parameter (particle enters angle, grain flux, flowing velocity, particle curtain thickness and particle grain size etc.) that participates in the particle of heat exchange can be controlled in running in real time, thereby when the operating condition of equipment such as boiler and industrial furnace changes, can realize that by the relevant technologies parameter of regulating heat exchange particle curtain this will bring major transformation for the design and the economical operation of various boilers and stove equipment to the smoke discharging accuracy control over temperature;
(6) when materials such as heat exchange particle employing silica sands, its wide material sources, has good high temperature resistant, wear-resistant, corrosion-resistant and thermal shock resistance, can effectively overcome the conventional tube shell-type and not have the problems such as cold end corrosion, wearing and tearing, tired broken ring and passage obstruction that exist in the heat exchange of heat pipe, its equipment dependability and service life, operation and maintenance cost was far below existing heat transmission equipment far above existing heat transmission equipment.
The present invention does not have heat exchange of heat pipe and residual neat recovering system is important breakthrough theoretical to existing traditional heat exchangers and technology, have unrivaled technology and economic advantages, and will bring great technological change to design, manufacturing and the operation of Industrial Boiler, station boiler, heating stove etc., having broad application prospects in fields such as the recycling of industrial equipment using waste heat from tail gas, combustion air preheating and combustion technologies, is the important technology support that improves efficiency of energy utilization and implement energy-saving and emission-reduction.
Description of drawings
Fig. 1 the present invention does not have particle curtain heat exchange unit schematic diagram in the heat exchange of heat pipe.
Fig. 2 the present invention does not have the snakelike no heat exchange of heat pipe schematic diagram of a kind of three grades of heat exchange in the heat exchange of heat pipe.
Fig. 3 the present invention does not have the tubular no heat exchange of heat pipe schematic diagram of a kind of three grades of straight horizontal in the heat exchange of heat pipe.
Fig. 4 the present invention does not have the heat exchange of heat pipe structural representation.
Fig. 5 reflects that the present invention does not have another kind of conducting element structural representation for the particle guiding in the heat exchange of heat pipe.
Fig. 6 residual neat recovering system schematic diagram of the present invention.
Fig. 7 snake bend formula tertiary granule curtain tandem is arranged residual neat recovering system (transmission of particle concentrated phase strength) in the same way.
Fig. 8 snake bend formula tertiary granule curtain tandem reversed arrangement residual neat recovering system (transmission of particle concentrated phase strength).
The parallel residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission) of arranging of Fig. 9 snake bend formula tertiary granule curtain.
Figure 10 snake bend formula tertiary granule curtain tandem is arranged residual neat recovering system (transmission of particle dilute phase strength) in the same way.
Figure 11 snake bend formula tertiary granule curtain tandem reversed arrangement residual neat recovering system (transmission of particle dilute phase strength).
The parallel residual neat recovering system (transmission of particle dilute phase strength) of arranging of Figure 12 snake bend formula tertiary granule curtain
The vertical tandem of Figure 13 snake bend formula level Four particle curtain is arranged residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission) in the same way.
The vertical tandem reversed arrangement of Figure 14 snake bend formula level Four particle curtain residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission).
The parallel residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission) of arranging of accompanying drawing 15 snake bend formula level Four particle curtains.
The vertical tandem of accompanying drawing 16 snake bend formula level Four particle curtains is arranged residual neat recovering system (transmission of particle dilute phase strength).
The vertical tandem reversed arrangement of Figure 17 snake bend formula level Four particle curtain residual neat recovering system (transmission of particle dilute phase strength).
The parallel residual neat recovering system (transmission of particle dilute phase strength) of arranging of accompanying drawing 18 snake bend formula level Four particle curtains.
The parallel residual neat recovering system (particle concentrated phase strength is carried or machinery is carried) of arranging of accompanying drawing 19 straight horizontal tubular type tertiary granule curtains.
Accompanying drawing 20 straight horizontal tubular type tertiary granule curtains adverse current tandem are in the same way arranged residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission).
Accompanying drawing 21 straight horizontal tubular type tertiary granule curtain reverse counterflow tandems are arranged residual neat recovering system (particle concentrated phase strength is carried or machinery is carried).
The parallel residual neat recovering system (conveying of particle dilute phase strength) of arranging of accompanying drawing 22 straight horizontal tubular type tertiary granule curtains.
Accompanying drawing 23 horizontal straight tubes/tertiary granule curtain adverse current tandem is in the same way arranged residual neat recovering system (particle dilute phase+concentrated phase strength transmits).
Accompanying drawing 24 straight horizontal tubular type tertiary granule curtain reverse counterflow tandems are arranged residual neat recovering system (particle dilute phase+concentrated phase strength is carried).
Accompanying drawing 25 horizontal straight tubes/level Four particle curtain adverse current tandem is in the same way arranged residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission).
Accompanying drawing 26 horizontal straight tubes/level Four particle curtain reverse counterflow tandem is arranged residual neat recovering system (particle concentrated phase strength transmits or mechanical transmission).
Accompanying drawing 27 horizontal straight tubes/level Four particle curtain adverse current tandem is in the same way arranged residual neat recovering system (particle dilute phase+concentrated phase strength transmits).
Accompanying drawing 28 horizontal straight tubes/level Four particle curtain reverse counterflow tandem is arranged residual neat recovering system (particle dilute phase+concentrated phase strength transmits).
The specific embodiment
Fig. 1 shows the basic structure that the present invention does not have heat exchange of heat pipe, as can be seen from the figure this no heat exchange of heat pipe has a particle curtain heat exchange unit 1, this particle curtain heat exchange unit has the tubular gas passage of straight horizontal 11, this gas passage is provided with a particle import 12 and a particle outlet 13, and particle forms particle curtain 14 as heat transferring medium from the particle import to particle outlet.Gas (such as high-temperature flue gas) enters horizontal gas passage from the left side, solid particle falls to entering grain flow (hereinafter to be referred as the particle curtain) that horizontal gas tunnel-shaped becomes a curtain shape and meet with high temperature (heat) gas of bottom horizontal flow sheet to come in contact and convection current and radiation heat transfer take place from the particle import.Calculate with experiment test and show, when the diameter of solid particle less than 250 microns and particle gap 0.98 when above, hot gas and solid particle just can reach balance within 0.1 to 0.01 second, thereby made gas temperature decline, the rising of solid particle temperature.Obviously, the amounts of particles that enters in the unit interval in the flue is many more, and total caloric receptivity of particle is many more, and the thermal discharge of gas is also big more, and the temperature of exit gas is also low more.If there is not gas to flow through in the horizontal flue, promptly gas flow rates is 0 o'clock, and solid particle will form the particle curtain of a vertical drop; And flow through as gas; be gas flow rates greater than 0 o'clock, then under the effect of gas viscosity power, particle can produce skew from left to right; make its drop point depart from center line one segment distance of import hopper, thereby form arc particle curtain as shown in Figure 1 in the flue bottom.Studies show that a particle curtain approximately can be finished the heat exchange of two theoretical particle curtain heat exchange units.Give an example, if require gas temperature to drop to 150 ℃ from 800 ℃, the heat that utilizes gas is heated to 700 ℃ with particle from 100 ℃, and so theoretical particle curtain heat exchange unit number is (800 – 150)/(800 – 700)=6.5.
On the basis of above-mentioned no heat exchange of heat pipe basic structure, can design the no heat exchange of heat pipe of multi-form various heat exchange progression, be a kind of snakelike no heat exchange of heat pipe of three grades of heat exchange as shown in Figure 2, contain three particle curtain heat exchange units in this no heat exchange of heat pipe, can certainly be two, four, five and above particle curtain heat exchange unit, each particle curtain heat exchange unit is connected to become snakelike by bend pipe, the particle curtain of each particle curtain heat exchange unit is vertically arranged and series connection up and down.Fig. 3 is that a kind of straight horizontal tubular type does not have heat exchange of heat pipe, contains three particle curtain heat exchange units in this no heat exchange of heat pipe of this no heat exchange of heat pipe, and it is tubular to be linked to be straight horizontal between them, and the particle curtain of each particle curtain heat exchange unit is vertically arranged.Particle curtain heat exchange unit in this obviously no heat exchange of heat pipe also can be an any number.No heat exchange of heat pipe more than this two-stage can directly be held two or more particle imports 12 and particle outlet 13 in the above with coiled pipe or horizontal straight tube, to arrange two or more particle curtains as required when reality is made.
As no heat exchange of heat pipe, also should consider selecting for use and the adjusting of particle curtain and how to make the particle curtain and the problem of the abundant heat exchange of gas and do not have the problem of heat exchange of heat pipe compact conformation of particle, it can also be seen that from Fig. 1 and Fig. 4, be provided with particle dispensing Control Component 2 at particle import 12 places, and be connected with gas current-sharing member 3 at gas passage 11 front ends.
Selecting for use and the adjusting of particle curtain of particle:
Solid particle employing silica sand and diameter used in the particle curtain heat exchange unit should be less than 250 microns, and the particle voids degree should help reaching between gas and particle the Rapid Thermal balance like this greater than 0.98 in the particle curtain.
The particle curtain is short more good more, helps the residual neat recovering system compact conformation.Shorten particle curtain length two kinds of methods are arranged.First method is to make particle enter gas passage with certain initial velocity, and the particle inlet velocity is high more, and the length of particle curtain can be short more.The fluid bed dispenser that the bottom has osculum can change the initial velocity that particle enters gas passage.1 meter dark bed can provide about 20
0.5The particle speed of m/s, the bed that 2m is dark can provide about 40
0.5The particle speed of m/s.Actual speed that it should be noted that particle is relevant with fluid bed bottom opening width.Second kind can make the method for particle curtain contraction in length is to make particle enter gas passage against air-flow at a certain angle.
Particle dispensing Control Component is referring to Figure 4 and 5.
In order to make the normal continuously operation of particle curtain in the particle curtain heat exchange unit, and realize efficient heat exchange, it can also be seen that in particle import 12 the present invention from Fig. 1 and Fig. 4 and to have designed particle dispensing Control Component 2, this assembly from top to bottom mainly is made up of particle hopper 21, circular material blanking tube 22, transition conduit 23, rectangle material blanking tube 24, electric butterfly valve 25, porous plate 26, mesh screen 27 and conducting element 28 etc.Wherein, the pore size of porous plate and layout density have determined the maximum through-current capacity of particle; The big I of the unlatching of electric butterfly valve and aperture thereof is controlled the particle curtain thickness of whereabouts in real time; Mesh screen 27 adopts the multi-deck screen host will play the current-sharing effect, even particle evenly distributes on the material blanking tube cross section, finally guarantees the uniformity of distribution of particles on the particle curtain cross section; The main effect of conducting element is that the control grain flow enters angle and the particle curtain thickness in the gas passage, when grain flow enters angle in the airflow line when suitable, can be with the particle curtain finally fall point control near particle import center line, like this, desired length of straight pipe is less when arranging multistage particle curtain on the straight horizontal pipeline section, in other words, on the straight length of certain-length, can arrange more particle curtain.
Conducting element 28 can adopt fixing tilting platy structure also can adopt the rotatable platy structure of regulating as shown in Figure 4.Conducting element 28 can also adopt the inclination bend pipe structure, as shown in Figure 5.If adopt adjustable setting, being in operation to enter angle in the gas pipeline by the angle control grain flow of regulating conducting element.In addition, this adjustable conducting element matches with the particle material blanking tube, in real time the thickness of control particle curtain.
Gas current-sharing member is referring to Fig. 4.
In order to make the particle in the particle curtain evenly fully contact, reach fast thermal balance, thereby improve heat exchange efficiency between gas and solid particle curtain, require the Velocity Profiles on the particle curtain admission section even with gas medium.Consider flue gas, air hose in the engineering practical application say (connecing) mouthful incompatible with the air/flue cross sectional shape and the physical dimension of particle curtain particle curtain heat exchange unit, therefore, necessarily require a transition tube coupling section that the flue gas in the engineering reality/air outlet slit pipe is not had heat exchange of heat pipe and link up, and flue gas or air draught are evenly distributed on the gas passage section of no heat exchange of heat pipe.Designed gas current-sharing member 3, its structure composition and operation principle are as shown in Figure 4 for this reason.
Consider that the present invention does not have the application of heat exchange of heat pipe, such as relevant flue gas/air duct two kinds of typical cross sectional shapes---circle and rectangular duct are arranged at boiler and heating stove, for this reason, the present invention proposes the gas current-sharing member 3 that connects circular pipe and rectangular duct, to be connected by a transitional pipe segment 4, connecting flange 5 and gas current-sharing member 3 in turn between flue gas or air duct and the no heat exchange of heat pipe, gas current-sharing member 3 can adopt three to the Pyatyi current-sharing, as shown in Figure 4.Wherein, first order current-sharing part is for adopting the big orifice plate 31 of the sparse layout of triangle battle array, the about 10mm in aperture, and current-sharing part in the second level is a flute pipeline section 32, and this flute pipeline section is arranged in side by side in the outer straight tube by many little pipes and forms.Third level current-sharing part is the fine and close aperture plate of arranging 33.
The present invention does not have the UTILIZATION OF VESIDUAL HEAT IN that heat exchange of heat pipe can be widely used in some courses of reaction, such as the boiler air preheat, can also be used for catalytic reaction and gas absorption.
It is to utilize high-temperature flue gas by particle curtain heat exchange unit heat transfer process combustion air to be carried out preheating that the present invention does not have one of important use of heat exchange of heat pipe.Reach the purpose that makes air preheat with high-temperature flue gas by following two steps:
The first step: the flue gas heated particle makes flue-gas temperature drop to the scope of requirement simultaneously.The present invention adopts cryogenic particles to contact with low-temperature flue gas, and the process that high-temperature particle contacts with high-temperature flue gas its objective is that particle temperature is raised to is the highest, and it is minimum that flue-gas temperature is dropped to.Studies show that, with 3～5 particle curtains particle is heated to more than 700 ℃ from about 100 ℃ usually, flue-gas temperature is dropped to below 150 ℃ from about 800 ℃.
Second step: the particle after the intensification heats air.Similar with the first step, just change flue gas into air, promptly allow cryogenic particles contact Cryogenic air, high-temperature particle contact high temperature air.Can make air heat to maximum temperature like this, it is minimum that particle temperature is dropped to.Studies show that, with 3 to 5 particle curtains air is heated to more than 600 ℃ from about 30 ℃ usually, particle temperature is dropped to below 120 ℃ from about 700 ℃.
When the present invention did not have heat exchange of heat pipe and is used for the boiler air preheat, the first step and second step can couple together, and have just constituted a basic residual neat recovering system, as shown in Figure 6.Its groundwork process is: cryogenic particles (for example 100 ℃) falls into exhaust gases passes from no heat exchange of heat pipe top, and in exhaust gases passes, form the particle curtain of high diffusion, particle one-level one-level is heated by flue gas, and flue-gas temperature one-level one-level reduces simultaneously, and last low-temperature flue gas is discharged after dedusting; Particle one-level one-level after the intensification is with air heat, particle temperature one-level one-level reduces simultaneously, air after the intensification is introduced burner and is used for burning, and last cryogenic particles is delivered to the particle porch, top of smoke inlet section by the particle transport device from no heat exchange of heat pipe bottom.Like this, the whole particle flow process forms a closed circuit continuous cyclic process.
Be noted that it is to finish the heat transmission of high-temperature flue gas to air by solid particle (for example fine sand) as heat transfer medium that the present invention does not have heat exchange of heat pipe essence.Do not have heat exchange of heat pipe with the present invention and will omit tube plate structure in the traditional heat exchangers, compare following advantage with conventional air preheater: (1) is in operation can be according to the variation of boiler and stove fuel characteristic and load condition, flow by regulating the heat exchange particle, particle curtain thickness etc. are the control exhaust gas temperature in real time, this is an important breakthrough of boiler and stove technology, will bring great technological change for the design and the operation of boiler and stove equipment; (2) the final exhaust gas temperature of boiler and various stoves is reduced greatly (for example being reduced to about 70 ℃), thereby the thermal efficiency is significantly improved, this means that under given energy output condition present technique can make boiler and stove equipment emission amount of carbon dioxide reduce greatly; (3) in heat exchange, can in circulating granular, add desulfurizing agent (for example limestone particle), thereby reach the purpose of effective control sulfur dioxide (SO2) emissions; (4) can effectively solve burn into wearing and tearing, stifled ash that the air preheater of traditional structure run in design and running, many technical barriers such as leak out; (5) cost of the pre-device of air is reduced greatly; (6) flowing resistance of air preheater is reduced greatly, its main cause is that pressure main in the heat transfer process falls from gas being quickened and to the lifting effect (this effect makes the particle sinking speed step-down) of particle.
There is not heat exchange of heat pipe based on the present invention, according to different heat recovery objects, tail gas character, tail gas parameter (flow and temperature) and on-the-spot equipment and pipe arrangement, can construct flexile particle curtain residual neat recovering system, this system comprises that no heat exchange of heat pipe that a no heat exchange of heat pipe that feeds flue gas is referred to as flue gas and does not have heat exchange of heat pipe A, a bubbling air is referred to as air and does not have heat exchange of heat pipe B, particle transport device 5, is connected by particle pipeline 6 that flue gases do not have heat exchange of heat pipe A, air does not have heat exchange of heat pipe B and particle transport device 5.
Below several exemplary particles curtain residual neat recovering systems are described.
Embodiment one: be three grades of residual neat recovering systems of snake bend formula, referring to Fig. 7-Figure 12.
When the exhaust emissions pipeline of boiler or other reactors and preheated air pipeline can adopt a kind of among Fig. 7 and Figure 12 when short transverse has enough arrangement space, the no heat exchange of heat pipe of using in these several systems is snakelike no heat exchange of heat pipe, and wherein Fig. 7 illustrates air does not have heat exchange of heat pipe B and vertically be arranged in flue gas and do not have below the heat exchange of heat pipe A and do not have heat exchange of heat pipe A with flue gas and vertically connect.High-temperature flue gas does not have heat exchange of heat pipe A bottom from flue gas and enters and discharge from the top, particle relies on gravity to fall to forming the tertiary granule curtain naturally from the top hopper, and dropping process successively with the hot flue gas generation heat exchange of rising, after three grades of heat exchange are finished, low-temperature flue gas is discharged from top, and high-temperature particle enters the hopper that the bottom air does not have heat exchange of heat pipe B, make it fall to forming the tertiary granule curtain naturally, and carry out heat exchange with the low temperature that enters from the bottom (cold) air, after three grades of heat exchanges are finished, high temperature air is discharged from the top and cryogenic particles enters the hopper of bottom, cryogenic particles is delivered to flue gas and is not had the heat exchange of carrying out next circulation in the hopper of heat exchange of heat pipe A by particle transport device 5 again, constitutes a complete snake bend formula tertiary granule curtain serial residual neat recovering system thus.Particle transport device 5 can adopt mechanical transmission device, carries as belt than using; Also can adopt pneumatic conveying, make particle upwards mobile precalculated position that reaches under the effect of high pressure gas such as in particle pipeline 6, feeding gases at high pressure.This residual neat recovering system only needs once to transmit, because of hot particle and air very low through multistage heat exchange its temperature when exporting hopper, adopt the mechanical type conveyer simpler this moment, directly the hopper transmission of particle toward top particle import department got final product, and do not need to take to be incubated especially measure by belt.This residual neat recovering system also can adopt high pressure gas to transmit particle.The main feature of this system is: (1) only needs the primary granule conveyer, thereby system is simple relatively; (2) all particle curtains have been formed organic series connection residual neat recovering system in vertical direction, and each the grade particles curtain in the system all can influence the work of its next stage particle curtain, and certain primary granule curtain can not overhaul separately when breaking down.Therefore, the status of equipment of every grade particles curtain all can normally move the generation considerable influence to whole residual neat recovering system in the system, thereby reliability of system operation is relatively low.
Residual neat recovering system and Fig. 7 shown in Figure 8 are closely similar, the layout that the flue gas of system shown in Figure 7 that different is does not have heat exchange of heat pipe A and air and do not have heat exchange of heat pipe B is in the same way, and the layout that its flue gas of system shown in Figure 8 does not have heat exchange of heat pipe A and air does not have a heat exchange of heat pipe B is reverse.Flue gas does not have heat exchange of heat pipe A and air does not in actual applications have heat exchange of heat pipe B and comes to determine the installation site as required.
Fig. 9 illustrates flue gas, and not have that heat exchange of heat pipe A do not have between the heat exchange of heat pipe B with air be relation in parallel, cryogenic particles makes the particle heating with hot flue gas generation heat exchange earlier, afterwards again by the particle conveyer with the particle hopper of particle transport to air particles curtain top, in air duct, form the tertiary granule curtain then with air heat, constitute a heat exchange circulation like this.After considering operation a period of time, the fine grained in the participation heat transfer process can be taken away by flue gas and produce loss, is provided with particle supplementary device 7 in system for this reason.
Residual neat recovering system shown in Figure 10, its flue gas does not have that heat exchange of heat pipe A and air do not have the structure of heat exchange of heat pipe B and annexation thereof and system shown in Figure 5 is just the same, different is that system shown in Figure 7 has been set up a cyclone separator 8 before particle hopper, and the air after separated is introduced into preheated air passage.Obviously, this system has increased the complexity of system, has only and can consider to adopt when particle transport air large usage quantity, thereby only be applicable to the residual neat recovering system that adopts particle dilute phase conveying device.
In like manner we can also be according to Fig. 8, corresponding image pattern 11, the such residual neat recovering system of Figure 12 of obtaining of system shown in Figure 9.
Embodiment two: be snake bend formula level Four residual neat recovering system, referring to Figure 13-Figure 18
When the exhaust emissions pipeline of boiler or other reactors and preheated air pipeline have enough arrangement space and exhaust temperature when higher in short transverse, can adopt snake bend formula level Four or Pyatyi residual neat recovering system, as Figure 13-shown in Figure 180, compare to three grades of residual neat recovering systems of snake bend formula shown in Figure 12 with Fig. 7, what the no heat exchange of heat pipe of present embodiment adopted as can be seen is that the snake bend formula with four particle curtain heat exchange units does not have heat exchange of heat pipe, heat exchange progression has increased, other building block, particle conveyer 5(strength or mechanical transmission) and all similar to the reliability of system and maintenance and the flexibility that moves etc. to aforementioned snake bend tertiary granule curtain residual neat recovering system.Do not give unnecessary details at this.
Embodiment three: be three grades of residual neat recovering systems of straight horizontal tubular type, referring to Figure 19-Figure 24.
When the exhaust emissions temperature road of boiler or other reactors not really high and and air duct in same vertical plane, when horizontally disposed up and down, can adopt as Figure 19-three grades of residual neat recovering systems shown in Figure 24.Compare with three grades of waste heat residual neat recovering systems of snake bend formula, the transmission more complicated of particle between each grade particles curtain heat exchange unit in three grades of residual neat recovering systems of straight horizontal tubular type, required particle conveyer quantity is more.
As can be seen from Figure 19, this is three grades of parallel systems, the native system flue gas does not have heat exchange of heat pipe A and air and does not have heat exchange of heat pipe B and all adopt straight horizontal tubular, flue gas does not have the particle curtain of each particle curtain heat exchange unit of heat exchange of heat pipe and connects one to one with the particle curtain that air does not have each particle curtain heat exchange unit of heat exchange of heat pipe, form corresponding closed circuit, in parallel between each loop.After considering operation a period of time, the fine grained in the participation heat transfer process can be taken away by flue gas and produce loss, is provided with particle supplementary device 7 for this reason in each closed circuit, and is provided with particle conveyer 5.The particle conveyer adopts pneumatic type, and high pressure positive blower is carried high-pressure blasts by high-pressure air hose 9 to each particle conveyer 5, and particle conveyer 5 does not have cold particle that heat exchange of heat pipe B comes out with air and delivers to flue gas and do not have in the hopper of heat exchange of heat pipe A and carry out cycle heat exchange.In this residual neat recovering system, because the parallel relatively independent operation of each grade particles curtain between each loop, its status of equipment does not influence the operation of other each grade particles curtains, can overhaul separately in each grade particles curtain when breaking down, thereby reliability of system operation is higher; It is less when in addition, certain primary granule curtain breaks down to the equipment and the whole production technogenic influence of particle curtain residual neat recovering system upstream.
Particle after three grades of heat transfer process are finished transmits and can all adopt the concentrated phase strength to carry or the mechanical transmission mode, also can partly adopt the concentrated phase strength to carry (for high-temperature particle) and machinery to carry (for cryogenic particles).
System shown in Figure 20 is three grades of tandem systems of a horizontal straight tube, and the main difference of this system and three grades of tandem systems of snake bend formula shown in Figure 7 is: (1) particle conveyer quantity more (many 2～3); (2) the flue gas tertiary granule curtain that do not have heat exchange of heat pipe A and air and do not have a heat exchange of heat pipe B has been formed a big train, and each the grade particles curtain in the system all can influence the work of its next stage particle curtain, and certain primary granule curtain can not overhaul separately when breaking down.Therefore, the situation of every grade particles curtain all can normally be moved the generation considerable influence to whole residual neat recovering system in the residual neat recovering system, thereby the residual neat recovering system reliability of operation is relatively low.Its particle conveyer can all adopt the concentrated phase strength to carry or machinery is carried, and also can partly adopt the concentrated phase strength to carry with machinery and carry, and also can partly adopt the dilute phase strength to carry.
When we system shown in Figure 20 in flue gas heat exchange device A and air heat exchanger B reversed arrangement, can obtain system as shown in figure 21, also be three grades of tandem systems of a horizontal straight tube.
For the air of avoiding particle transport fully enters exhaust gases passes, " leaking out " amount that makes is zero, then can adopt as Figure 22-residual neat recovering system shown in Figure 24, the main distinction of itself and Figure 19-residual neat recovering system shown in Figure 21 is to have set up a cyclone separator 8 before flue gas heat exchange device particle hopper 21, and the air after separated is introduced into preheated air passage.Obviously, this system has increased the complexity of system, has only and can consider to adopt when particle transport air large usage quantity, thereby only be applicable to the residual neat recovering system that adopts particle dilute phase conveying device.
Embodiment four: be straight horizontal tubular type level Four serial residual neat recovering system, referring to Figure 25-Figure 28.When the exhaust emissions temperature road of boiler or other reactors very high and and air duct in same vertical plane, adopt Figure 25-residual neat recovering system shown in Figure 28 when horizontally disposed up and down, present embodiment has very similar place to Figure 20 in the embodiment three with Figure 21, Figure 23 and Figure 24 as can be seen from these figure, unique different particle curtain heat exchange unit that is flue gas does not have heat exchange of heat pipe and air and do not have in the heat exchange of heat pipe in the present embodiment respectively has four, can certainly be 5 even more, form level Four or Pyatyi residual neat recovering system.
For the respective embodiments described above, its particle conveyer 5 can select concentrated phase pneumatic or dilute phase is pneumatic or machine driving as required, form and putting position that flue gas does not have heat exchange of heat pipe A and air and do not have heat exchange of heat pipe B can design as required, and flue gas does not have heat exchange of heat pipe A and air and do not have among the heat exchange of heat pipe B connection between each particle curtain and can adopt polyphone as required and connect even mixed connection.Therefore the form of residual neat recovering system of the present invention is not limited among the figure listed.
Claims (11)
1. no heat exchange of heat pipe, it is characterized in that this no heat exchange of heat pipe is linked to be by a particle curtain heat exchange unit (1) at least, described particle curtain heat exchange unit has the tubular gas passage of straight horizontal (11), this gas passage is provided with a particle import (12) and a particle outlet (13), particle forms particle curtain (14) as heat transferring medium from the particle import to particle outlet, described particle is an inert solid particle.
2. no heat exchange of heat pipe according to claim 1 is characterized in that inert solid particle adopts the mixing of a kind of in silica sand and the aluminium oxide or two kinds, and particle diameter is below 250 microns.
3. no heat exchange of heat pipe according to claim 1 and 2, it is characterized in that this no heat exchange of heat pipe vertically arranges series connection up and down by bend pipe with the particle curtain (14) that plural at least particle curtain heat exchange unit (1) is linked to be snakelike and each particle curtain heat exchange unit, perhaps this no heat exchange of heat pipe is linked to be the tubular and vertical layout of particle curtain (14) each particle curtain heat exchange unit of straight horizontal by straight tube with plural at least particle curtain heat exchange unit (1).
4. no heat exchange of heat pipe according to claim 3 is characterized in that described particle import (12) locates to be provided with particle dispensing Control Component 2, and this assembly comprises electric butterfly valve (25) and screen cloth (27).
5. no heat exchange of heat pipe according to claim 3 is characterized in that described particle import (12) locates to be provided with the conducting element (28) into the particle guiding.
6. no heat exchange of heat pipe according to claim 3, the gas passage front end that it is characterized in that this no heat exchange of heat pipe is connected with gas current-sharing member (3), gas enters gas passage through this current-sharing member, described gas current-sharing member comprises the big orifice plate of current-sharing bare cloth (31), flute pipeline section (32), big orifice plate (33) gathers, to form the current-sharing of 3-5 level, described flute pipeline section is arranged in side by side in the outer straight tube by many little pipes and forms.
7. residual neat recovering system made from the described particle curtain of one of claim 1-6 heat exchange unit, it is characterized in that no heat exchange of heat pipe that this system comprises that a no heat exchange of heat pipe that feeds flue gas is referred to as flue gas and does not have heat exchange of heat pipe (A), a bubbling air is referred to as air and does not have heat exchange of heat pipe (B), particle transport device (5), connect by particle pipeline (6) that described flue gas does not have heat exchange of heat pipe (A), air does not have heat exchange of heat pipe (B) and particle transport device (5).
8. residual neat recovering system according to claim 7, it is characterized in that flue gas does not have heat exchange of heat pipe (A) and air and do not have heat exchange of heat pipe (B) and all adopt snakelike, flue gas does not have heat exchange of heat pipe (A) and is arranged in air and does not have heat exchange of heat pipe (B) top, does not have heat exchange of heat pipe (B) with air and connects.
9. residual neat recovering system according to claim 7 is characterized in that flue gas does not have heat exchange of heat pipe (A) and air and do not have heat exchange of heat pipe (B) and all adopt snakelikely, and flue gas does not have heat exchange of heat pipe (A) and air, and not have heat exchange of heat pipe (B) in parallel.
10. residual neat recovering system according to claim 7, it is characterized in that flue gas does not have heat exchange of heat pipe (A) and air and do not have heat exchange of heat pipe (B) and all adopt straight horizontal tubular, flue gas does not have the particle curtain (14) of each particle curtain heat exchange unit (1) of heat exchange of heat pipe (A) and connects one to one with the particle curtain that air does not have each particle curtain heat exchange unit of heat exchange of heat pipe (B), form corresponding closed circuit, parallel between each loop.
11. residual neat recovering system according to claim 7, it is characterized in that flue gas does not have heat exchange of heat pipe (A) and air and do not have heat exchange of heat pipe (B) and all adopt straight horizontal tubular, flue gas does not have the particle curtain of each particle curtain heat exchange unit of heat exchange of heat pipe (A) and connects with the particle curtain that air does not have each particle curtain heat exchange unit of heat exchange of heat pipe (B).
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| CN2011102066353A CN102288044A (en) | 2011-07-22 | 2011-07-22 | Pipeless heat exchanger and residual-heat recovery system |
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Cited By (7)
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| CN102607297A (en) * | 2011-12-21 | 2012-07-25 | 卓卫民 | Device for carrying out heat exchange between gas and solid particulate matters |
| CN105169857A (en) * | 2015-10-13 | 2015-12-23 | 马军 | Heat recovery device |
| CN105169938A (en) * | 2015-09-30 | 2015-12-23 | 马军 | Flowing particle heat exchange type organic waste gas oxidation equipment |
| CN107014234A (en) * | 2017-04-12 | 2017-08-04 | 东南大学 | A kind of device and method of granules in pipe fluid interchange |
| CN110806131A (en) * | 2019-10-18 | 2020-02-18 | 中国科学院广州能源研究所 | High-efficient compact high pressure heat accumulation device |
| CN111701543A (en) * | 2019-03-18 | 2020-09-25 | 四川大学 | Continuous freezing and gas purifying method for cold-hot particle circulating moving bed |
| CN113528194A (en) * | 2020-04-16 | 2021-10-22 | 国家能源投资集团有限责任公司 | Method and equipment for treating high-temperature coal gas |
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| CN111701543A (en) * | 2019-03-18 | 2020-09-25 | 四川大学 | Continuous freezing and gas purifying method for cold-hot particle circulating moving bed |
| CN111701543B (en) * | 2019-03-18 | 2021-07-23 | 四川大学 | Continuous freezing and gas purifying method for cold-hot particle circulating moving bed |
| CN110806131A (en) * | 2019-10-18 | 2020-02-18 | 中国科学院广州能源研究所 | High-efficient compact high pressure heat accumulation device |
| CN113528194A (en) * | 2020-04-16 | 2021-10-22 | 国家能源投资集团有限责任公司 | Method and equipment for treating high-temperature coal gas |
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Application publication date: 20111221 |