CN103940276B - Exhaust gas inlet device and regenerative heat exchanger containing same - Google Patents
Exhaust gas inlet device and regenerative heat exchanger containing same Download PDFInfo
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- CN103940276B CN103940276B CN201410184980.5A CN201410184980A CN103940276B CN 103940276 B CN103940276 B CN 103940276B CN 201410184980 A CN201410184980 A CN 201410184980A CN 103940276 B CN103940276 B CN 103940276B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/14—Thermal energy storage
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Abstract
The invention provides a smoke inlet device, including an adjustable smoke baffle, a smoke dusting baffle, a shell, a dusting pipeline, and a smoke inlet pipeline, wherein the smoke inlet pipeline is arranged at a lower end, a smoke outlet end is arranged at an upper end, the dusting pipeline is arranged in the shell for housing and collecting the dust in the smoke, a regular dusting mechanism is connected to the inferior of the dusting pipeline; the shell is composed of a first vertical segment at the lower end, an outward incline segment connected to the first vertical segment, a second vertical segment connected to the incline segment and a horizontal segment arranged at top and connected to the second vertical segment, the adjustable smoke baffle is connected to the other end portion of the horizontal segment and adjusts the angle around the other end portion of the horizontal segment; the first vertical segment forms a smoke inlet, the dusting pipeline goes deep into the shell from the smoke inlet, the smoke dusting baffle is connected to the upper end portion of the dusting pipeline arranged in the shell; in the vertical direction, and the upper end and the lower end of the smoke dusting baffle are arranged between the upper end and the lower end of the second vertical segment. The repeatedly efficient dust removal of smoke can be realized, the dust stratification problem of devices in the flue is reduced to a large extent, and the heat exchange efficiency after the smoke enters a heat exchanger is improved.
Description
Technical field
The present invention relates to a kind of heat regenerator of high-efficiency cement production process UTILIZATION OF VESIDUAL HEAT IN, belong to the field of heat exchangers of F28d.
Background technology
Along with China's rapid economic development, energy resource consumption increases day by day, and the problem that urban air quality goes from bad to worse is also outstanding all the more, and the problem of economize energy and the discharge of minimizing environment harmful is extremely urgent.In common field of heat energy power, high, the with serious pollution one of the main reasons of energy consumption is that the exhaust gas temperature of flue gas is too high, namely wastes mass energy, causes environmental pollution again.Cement industry is the industry of a highly energy-consuming, high pollution.Cement industry afterheat generating system can carry out recycling to using waste heat from tail gas, realizes the object of energy-saving and emission-reduction.But relevant waste heat has intermittence, the features such as poor quality, makes the efficiency of electricity generation system low, and these problems demand solve.
Application heat-storing material can make discontinuous steam in industry-by-industry production process become continuous steam, is conducive to the efficiency improving afterheat generating system.Such as, at home in existing copper smelting process, melting converter produces a large amount of rich steam, but because load fluctuation is large, large portion directly to sky discharge, causes mass energy to waste, by setting up storage heater, it can be made to become steam turbine and to stablize filling source, take full advantage of Copper making process waste, achieve the cascade utilization of the energy.Storage heater in existing UTILIZATION OF VESIDUAL HEAT IN industry, mainly comprises various types of shell-and-tube heat exchanger, and such as, fountain, light pipe, Needle fin tube, gilled tube, heat pipe etc., also can utilize plate type heat exchanger to realize accumulation of heat and exothermic process.But Problems existing is, accumulation of heat and thermal desorption system complex structure, accumulation of heat and heat release are large with heat exchanger volume, and high in cost of production, the improvement therefore for heat-accumulating process heat transmission equipment is necessary.
Summary of the invention
The present invention is directed to Problems existing in the thermal storage equipment of existing cement industry UTILIZATION OF VESIDUAL HEAT IN, propose a kind of novel heat regenerator.
To achieve these goals, technical scheme of the present invention is as follows: a kind of heat regenerator of cement production process UTILIZATION OF VESIDUAL HEAT IN, described heat exchanger comprises the first tube bank and the second tube bank, high-temperature flue gas import, high-temperature flue gas exports, cryogenic fluid entrance, cryogenic fluid outlet and housing, polylith heat-storing material is set in described heat exchanger shell, described polylith heat-storing material is stacked, first pore and the second pore are set in every block heat-storing material, first pore and the second pore arranged in a crossed manner, described first tube bank and the second tube bank are each passed through the first pore and the second pore, the external diameter of the first tube bank and the second tube bank equals the diameter of the first pore and the second pore respectively, described first restrains the flue gas produced for the cement production process that circulates, and the second tube bank is for the cryogenic fluid that circulates, described flue gas enters from high-temperature flue gas entry, and through the first tube bank, then discharge from high-temperature flue gas outlet, cryogenic fluid enters from cryogenic fluid entrance, through the second tube bank, then discharges from cryogenic fluid outlet, multiple dividing plate is set on the flow direction of flue gas, the first hole is divided into multiple independently passage, alignment housing both sides in vertical along housing, the distance between dividing plate is more and more less.
A kind of heat regenerator of cement production process UTILIZATION OF VESIDUAL HEAT IN, described heat exchanger comprises the first tube bank and the second tube bank, high-temperature flue gas import, high-temperature flue gas exports, cryogenic fluid entrance, cryogenic fluid outlet and housing, polylith heat-storing material is set in described heat exchanger shell, described polylith heat-storing material is stacked, first pore and the second pore are set in every block heat-storing material, first pore and the second pore arranged in a crossed manner, described first tube bank and the second tube bank are each passed through the first pore and the second pore, the external diameter of the first tube bank and the second tube bank equals the diameter of the first pore and the second pore respectively, described first restrains the flue gas produced for the cement production process that circulates, and the second tube bank is for the cryogenic fluid that circulates, described flue gas enters from high-temperature flue gas entry, and through the first tube bank, then discharge from high-temperature flue gas outlet, cryogenic fluid enters from cryogenic fluid entrance, through the second tube bank, then discharges from cryogenic fluid outlet, cryogenic fluid tube bank is perpendicular to the flow direction of flue gas being parallel-connection structure, and along on the direction of flow of flue gas, the caliber of cryogenic fluid tube bank constantly reduces.
A kind of heat regenerator of cement production process UTILIZATION OF VESIDUAL HEAT IN, described heat exchanger comprises the first tube bank and the second tube bank, high-temperature flue gas import, high-temperature flue gas exports, cryogenic fluid entrance, cryogenic fluid outlet and housing, polylith heat-storing material is set in described heat exchanger shell, described polylith heat-storing material is stacked, first pore and the second pore are set in every block heat-storing material, first pore and the second pore arranged in a crossed manner, described first tube bank and the second tube bank are each passed through the first pore and the second pore, the external diameter of the first tube bank and the second tube bank equals the diameter of the first pore and the second pore respectively, described first restrains the flue gas produced for the cement production process that circulates, and the second tube bank is for the cryogenic fluid that circulates, described flue gas enters from high-temperature flue gas entry, and through the first tube bank, then discharge from high-temperature flue gas outlet, cryogenic fluid enters from cryogenic fluid entrance, through the second tube bank, then discharges from cryogenic fluid outlet, each block heat-storing material described is rectangular configuration, in every block heat-storing material, arrange two ranked first hole and and ranked second hole, second hole is positioned at the centre that two ranked first hole, two to ranked first the center line in hole identical with the distance of the center line in middle second hole, between first hole and the second hole, structure is set to 90 degrees, distance between the center of circle in same adjacent two holes that ranked first in hole is L3, and the relation between described L3 and the first bore dia D1 meets: 1.5<L3/D1<2.7.
A kind of smoke inlet device, comprise adjustable gas baffle, flue gas dusting baffle plate, housing, ash removal pipe, smoke inlet pipeline, smoke inlet pipeline is positioned at lower end, smoke outlet is positioned at upper end, ash removal pipe is built in housing, for the dust in sedimentation and collection flue gas, below it, connect regular ash exhauster; Described housing is made up of the first vertical section of lower end, the outside tilting section be connected with the first vertical section, the second vertical section be connected with tilting section and the horizontal segment be connected with the second vertical section that is positioned at top, described adjustable gas baffle is connected with the other end of horizontal segment, round the other end adjustment angle of horizontal segment; Described first vertical section constitutes the entrance of flue gas, and described ash removal pipe is deep in housing from smoke inlet, and flue gas dusting baffle plate is connected with the upper end being positioned at housing of ash removal pipe; In the vertical direction, the top and bottom of described flue gas dusting baffle plate are between the top and bottom of the second vertical section.
Align with the end in the vertical direction be connected with adjustable gas baffle 15 of horizontal segment in the end of described flue gas dusting baffle plate 16, described flue gas dusting baffle plate 16 is 15-40 ° with the angle of horizontal direction, described tilting section and the angle of horizontal direction are 20-45 °, in the vertical direction, the height of the second vertical section is 2.5-5.6 times of tilting section height, aligns with first vertical section of in the vertical direction in the end be connected with adjustable gas baffle 15 of horizontal segment.
A kind of method of cement production process UTILIZATION OF VESIDUAL HEAT IN, described method comprises heat regenerator, described heat exchanger comprises the first tube bank and the second tube bank, high-temperature flue gas import, high-temperature flue gas exports, cryogenic fluid entrance, cryogenic fluid outlet and housing, polylith heat-storing material is set in described heat exchanger shell, described polylith heat-storing material is stacked, first pore and the second pore are set in every block heat-storing material, first pore and the second pore arranged in a crossed manner, described first tube bank and the second tube bank are each passed through the first pore and the second pore, the external diameter of the first tube bank and the second tube bank equals the diameter of the first pore and the second pore respectively, described first restrains the flue gas produced for the cement production process that circulates, and the second tube bank is for the cryogenic fluid that circulates, described flue gas enters from high-temperature flue gas entry, and through the first tube bank, then discharge from high-temperature flue gas outlet, cryogenic fluid enters from cryogenic fluid entrance, through the second tube bank, then discharges from cryogenic fluid outlet,
In endothermic process, high-temperature flue gas heat release in the first hole, heat-storing material storing heat; When high-temperature flue gas intermittence stops, by cryogenic fluid in cryogenic fluid tube bank, the heat-storing material of storing heat carries out heat release to the cryogenic fluid in the second tube bank, realizes storage and the utilization of cement production process waste heat.
Compared with existing, heat regenerator of the present invention has following advantage:
1) provide a kind of split type regenerative heat exchanger newly, maintain easily, save cost.
2) the present invention has possessed the function of hot tank in conventional hold over system and cold tank, can realize the heat absorption and release function of heat-storing material simultaneously, optimize the structure of hold over system, decrease initial investment and operating cost.
3) the present invention is simple by heat regenerator structure, is easy to manufacture, and cost reduces.
4) heat release while accumulation of heat can also be realized, greatly optimize the utilization of preheating.
5) by test of many times, optimize the optimum structure of heat exchanger, realize the needs that heat exchanger meets heat storage capacity and cost simultaneously.
6) by arranging dividing plate, making overall accumulation of heat even, strengthening convection current simultaneously.
7) by automatically controlling, avoiding cold end corrosion, reaching maximum exhaust heat utilization effect simultaneously.
8) being arranged by the thickness of heat-storing material or the change of heat storage capacity, providing cost savings when meeting accumulation of heat demand.
9) provide a kind of new heat-storing material, meet the demand of the UTILIZATION OF VESIDUAL HEAT IN in manufacture of cement.
10) a kind of flue gas separation unit is provided.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of heat-absorbing structure in heat regenerator of the present invention;
Fig. 2 is the schematic diagram of heat radiation structure in heat regenerator of the present invention;
Fig. 3 is the schematic top plan view of heat regenerator of the present invention;
Fig. 4 is the upper left corner partial enlarged drawing of the heat regenerator of Fig. 3;
Fig. 5 is the schematic diagram of a detailed description of the invention of heat-storing material of the present invention;
Fig. 6 is the schematic diagram of another detailed description of the invention of heat-storing material of the present invention;
Fig. 7 is another embodiment of heat radiation structure in heat regenerator of the present invention;
Fig. 8 is the detailed description of the invention of smoke inlet device;
Fig. 9 is another detailed description of the invention of smoke inlet device;
Figure 10 be Fig. 8 smoke inlet device from the schematic diagram viewed from bottom.
reference numeral
1, high-temperature flue gas outlet, the 2, heat exchanger shell, 3, first tube bank, 4, vertical baffle, 5, high-temperature flue gas import, 6, vertical baffle, 7, vertical baffle, the 8, sender property outlet, 9, second tube bank, 10, working medium entrance, 11, inlet tube, 12, inlet header, 13, control valve, 14 heat-storing materials, 15 adjustable gas baffles, 16 flue gas dusting baffle plates, 17 housings, 18 ash removal pipes, 19 smoke inlet pipelines.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.
As shown in Figure 1, a kind of heat regenerator of cement production process UTILIZATION OF VESIDUAL HEAT IN, described heat exchanger comprises the first tube bank 3 and the second tube bank 4, high-temperature flue gas import 5, high-temperature flue gas outlet 1, cryogenic fluid entrance 10, cryogenic fluid outlet 8 and housing 2, described first tube bank 3 and the second tube bank 4 are arranged in housing 2, the flue gas that described first tube bank 3 produces for the cement production process that circulates, second tube bank 4 for the cryogenic fluid that circulates, the first tube bank 3 and the second tube bank 9 arranged in a crossed manner; Described flue gas enters from high-temperature flue gas entry 5, and through the first tube bank 3, then discharge from high-temperature flue gas outlet 1, cryogenic fluid enters from cryogenic fluid entrance 8, through the second tube bank 9, then discharges from cryogenic fluid outlet 10.
As seen in figures 3-6, polylith heat-storing material 14 is set in described heat exchanger shell, described polylith heat-storing material 14 is stacked, first pore and the second pore are set in every block heat-storing material 14, first pore and the second pore arranged in a crossed manner, described first tube bank and the second tube bank are each passed through the first pore and the second pore, are to heat-storing material heat release and heat absorption respectively.The external diameter of the first tube bank and the second tube bank equals the diameter of the first pore and the second pore respectively, to reduce thermal contact resistance.
Heat-storing material is divided into polylith, can conveniently carry, and safeguards, such as, when certain block heat-storing material loses heat storage capacity, is convenient for changing.
Flue gas is through the first tube bank time, and heat-storing material absorbs the heat in flue gas, and then the heat of absorption is passed to the cryogenic fluid of the second tube bank by heat storage medium, thus completes heat transfer process.
Flue gas and cryogenic fluid can flow simultaneously, and heat-storing material, while absorption flue gas heat, transfers heat to cryogenic fluid.Certainly alternatively, flue gas and cryogenic fluid can not simultaneously between section carry out heat exchange with heat storage medium respectively.In endothermic process, high-temperature flue gas heat release in pipe, heat-storing material storing heat; When needing to utilize the heat stored, by cryogenic fluid in the second tube bank, absorb the heat of heat storage medium.Such as when high-temperature flue gas intermittence stop time, heat-storing material and second restrain in cryogenic fluid carry out exothermic reaction, realize storage and the utilization of cement production process waste heat, improve the utilization rate of the energy.
As one preferably, each block heat-storing material 14 described is cube structure, in every block heat-storing material 14, arrange two ranked first pore and and ranked second pore, second pore is positioned at the centre that two ranked first pore, two to ranked first the center line of pore identical with the distance of the center line of middle second pore, the plane that often ranked first pore center line place is parallel with cubical outer surface, and the plane that often ranked second pore center line place is parallel with cubical outer surface; Between first pore and the second pore, structure is set to 90 degrees.As Figure 4-Figure 6, distance wherein between the first tube bank 3 and the second tube bank 9 center lines can not be excessive, if excessive, then can there is no enough heats because of flue gas, cause heat-storing material cannot store full heat, cause the waste of heat-storing material, the temperature of outlet 5 flue gas also can be caused too low simultaneously, cause cold end corrosion; If apart from too small, then cause heat-storing material cannot store satisfied enough heats, cause the demand that cannot meet heat exchange, cause the waste of the energy, in like manner, for the result that the first pore is best with the same demand fulfillment of nearest distance one on heat-storing material border.Therefore, the present invention is the size relationship of the heat exchanger of the best summed up by the test data of the heat exchanger of multiple different tube diameters.
As shown in Figure 4, wherein the external diameter of the first pore is D1, the external diameter of the second pore is D2, distance between the center line of the center line of the first pore and the second tube bank is L2, the distance in the face of the heat-storing material that the plan range at the center line place of the first pore is nearest is L1, then D1, D2 and L1, L2 meet following formula:
L1/L2=a*ln(D2/D1)+b，
D2>D1,L2>L1,
Wherein ln is logarithmic function, and a, b are parameter, wherein 1.28<=a<=1.45,0.37<=b<=0.43;
25mm<=D1<=60mm, 25mm<=D2<=60mm,
The unit of L, D1, D2 is mm.
Distance between the center of circle of same adjacent two pipes that ranked first in tube bank is L3, the distance of L3 can not be excessive, cause heat cannot store completely if cross conference, cause the waste of heat-storing material, if too small, the heat storage capacity of heat-storing material can be caused too low, accumulation of heat demand cannot be met, the loss of waste heat can be caused.By test of many times, the relation that the described L3 and first determined restrains between outer diameter D 1 meets: 1.5<L3/D1<2.7, preferably, and 1.9<L3/D1<2.1.
In like manner, the Distance geometry second between the second tube bank restrains the proportion of external diameter preferably between 1.5-2.7, most preferably is between 1.9-2.1.
As preferably, as Figure 1-3, described heat exchanger is vertical structure, first tube bank 3 is vertical direction setting, second tube bank 9 is horizontal direction setting, and in the vertical direction arranges multiple dividing plate 4,6,7, holding multiple pieces heat-storing material between dividing plate and between outermost layer dividing plate and the sidewall of housing, be divided into many groups by heat-storing material, by multiple dividing plate, the first tube bank be divided into multiple independently passage.By dividing plate, be conducive to the convection heat transfer' heat-transfer by convection performance improving flue gas further.Vertical baffle 4, vertical baffle 6 and vertical baffle 7 are also the gripper shoes of working medium heat-exchanging tube bundle 9 simultaneously.
As one preferably, alignment housing both sides in vertical along housing, the distance between dividing plate is more and more less.The distance of the intermediate space that such as described dividing plate is formed is greater than the distance being positioned at housing both sides.As shown in Figure 2, the space that its median septum 4,6 is formed and 6 and 7 spaces formed are greater than the space that dividing plate 4 is formed with left side housing, are greater than the space that dividing plate 7 is formed with right side housing simultaneously.Main cause is because the speed of flue gas of housing both sides is less than middle speed, can be that speed air flow in whole housing is consistent substantially, thus heat-storing material is evenly absorbed heat on the whole by arranging of dividing plate.
As preferably, as shown in Figure 2, in the vertical direction between described the second adjacent tube bank 9, bend pipe structure is set, thus makes the second tube bank form coiled pipe structure in the vertical direction.
As one preferably, along the direction of flow of flue gas, the heat storage capacity of described heat-storing material reduces gradually.Main cause is the flow direction along flue gas, and the temperature of flue gas is more and more lower, and the emission capacity of flue gas reduces gradually, does not therefore need the material of high accumulation of heat energy, can save the cost of heat-storing material like this.
In Fig. 2, the second tube bank is the coiled pipe arranging many parallel connections parallel to each other in vertical direction, and cryogenic fluid vertically flows, but the arrangement mode of the second tube bank is not limited to the form shown in Fig. 2.As another kind of set-up mode, second tube bank is the pipe of in the horizontal direction many parallel connection parallel to each other, and described pipe can be coiled pipe, and the pipe namely on same plane is linked together by bend pipe in end, being cascaded structure at same plane, is parallel-connection structure at the pipe of Different Plane.Certainly, described pipe also can not arrange bend pipe, is namely all parallel-connection structure with all pipes in vertical direction in the plane, as shown in Figure 7, arranges the collector of the second tube bank in the left and right sides.The collector of the both sides of certain Fig. 7 can be arranged on outside housing, is not limited to the set-up mode of Fig. 7.
For the form shown in Fig. 6,7, as one preferably, along on the direction of flow of flue gas, the caliber of the second tube bank constantly reduces.Main cause is because of the direction along flow of flue gas, the temperature of flue gas constantly declines, heat-storing material institute storing heat is also fewer and feweri, therefore by reducing caliber, reduce the flow of the cryogenic fluid flowing through heat-storing material, thus make along on the flow direction of delaying, the temperature rising difference of the entirety of cryogenic fluid is little, cryogenic fluid temperature before combination after heating is consistent substantially, avoid the uneven of the temperature of heating, also the second tube bank can be avoided to be heated uneven and to cause local temperature too high simultaneously, affect its service life.
Illustrate a row four pieces of heat-storing materials in Fig. 6, but be not limited to the quantity shown in Fig. 6.
As one preferably, along the direction of flow of flue gas, the distance between the center line of the first described tube bank 3 and the center line of the second tube bank 9 is that L reduces gradually.Main cause is the flow direction along flue gas, and the temperature of flue gas is more and more lower, and the emission capacity of flue gas reduces gradually, and therefore required heat-storing material is also just fewer and feweri, can save the cost of heat-storing material like this.
For above-mentioned situation, but L numerical value now also meets above-mentioned formula.The numerical value that L constantly changes can be adjusted by the size adjusting a, b two parameters.
As one preferably, the entrance of the second tube bank 9 arranges control valve 13, for regulating the flow of the medium entering the second tube bank 9, simultaneously, set temperature sensor (not shown) on 1 position is exported, for measuring the temperature of the flue gas of heat exchanger exit at high-temperature flue gas; Control valve 13, temperature sensor and central controller (not shown) carry out data cube computation, and center-control, according to the size of the temperature of temperature sensor measurement, regulates the flow entering the medium of the second tube bank 9 automatically.
If the temperature measured is lower than the first temperature, then central controller reduces the aperture of control valve automatically, if the temperature measured is higher than the second temperature, then central controller increases the aperture of control valve automatically, and wherein the second temperature is greater than the first temperature.
Why take above-mentioned measure, main purpose is to prevent cold end corrosion.Because if flue gas exit temperature is too low, flue-gas temperature can be caused lower than dew-point temperature, the cold end corrosion to smoke discharging pipe and heat exchanger can be caused, by reducing the flow of the cryogenic fluid participating in heat exchange, reduce heat exchange amount, improve outlet temperature, the generation of cold end corrosion can be avoided the control of temperature; In like manner, if the temperature measured is higher than uniform temperature, then shows that exhaust gas temperature is too high, can waste be caused, therefore, need the flow increasing fluid, absorb more heat.
Preferably, described heat-storing material comprises seal casinghousing and heat storage medium, and heat storage medium is sealed in seal casinghousing, and heat storage medium is middle thermohaline based phase-change material, and described middle thermohaline sill consists of the following composition: KNO
3, NaNO
3, NaNO
2, CaNO
3, KNO
2, the mass percent of each composition is respectively: 33-35%KNO
3, 19-21%NaNO
3, 32-33%NaNO
2, 7.14%CaNO
3, all the other are KNO
2.
Preferably, 33.34%KNO
3, 20.21%NaNO
3, 32.35%NaNO
2, 7.14%CaNO
3, all the other are KNO
2.
Above-mentioned heat-storing material is the result obtained by test of many times, and fusing point, more than 200 DEG C, meets the absorbing waste heat in cement production process completely.
Certainly, as one preferably, heat-storing material can be pottery or other solid heat storage media, does not so just need shell.
Present invention also offers a kind of smoke inlet device, as shown in Figure 8.Described smoke inlet device is arranged on the position entering mouth 5 of afterheat heat exchanger, to avoid more solid combustion particle to enter afterheat heat exchanger, avoids dust stratification.
As shown in Figure 8, smoke inlet device, comprises adjustable gas baffle 15, flue gas dusting baffle plate 16, housing 17, ash removal pipe 18, smoke inlet pipeline 19.Smoke inlet pipeline 19 is positioned at lower end, is the entrance point of flue gas, rounded.Flue gas from cement production process is entered by inlet duct 19 from bottom to top, is flowed out after sedimentation ash disposal by the exit position of housing 17 crown center.Smoke outlet is square, as shown in Figure 9.Ash removal pipe 18 is built in housing 17, for the dust in sedimentation and collection flue gas, connects regular ash exhauster below it.Flue gas dusting baffle plate 16 and ash removal pipe 18 top are interconnected, in Y-type layout, to increase the area gathered dust.Adjustable baffle plate 15 is arranged on the top of housing 17, is flexibly connected with housing 17.The flow velocity of smoke outlet can be adjusted, to obtain good dust removing effects by the angle changing adjustable baffle plate 17.
As shown in Figure 8, described housing 17 is made up of the first vertical section of lower end, the outside tilting section be connected with the first vertical section, the second vertical section be connected with tilting section and the horizontal segment be connected with the second vertical section that is positioned at top, described adjustable gas baffle 15 is connected with the other end of horizontal segment, round the other end adjustment angle of horizontal segment; Described first vertical section constitutes the entrance of flue gas, and described ash removal pipe 18 is deep in housing 17 from smoke inlet, and flue gas dusting baffle plate 16 is connected with the upper end being positioned at housing 17 of ash removal pipe 18; In the vertical direction, the top and bottom of described flue gas dusting baffle plate 16 are between the top and bottom of the second vertical section; Described tilting section is outward-dipping, the circulation area of flue gas is increased, reduces the flow velocity of flue gas, and then by the second vertical section, the circulation area of flue gas remains unchanged substantially, last because the existence of the second vertical section, makes flue gas change flow direction.
First vertical section can be pipe as shown in Figure 10, also can be square tube or other structures.
In implementation process, flue gas enters smoke inlet device via smoke inlet pipeline 19, and by the space formed by smoke inlet pipeline 19 and ash removal pipe 18, now the circulation area of flue gas is less, and corresponding flow velocity is larger.In flue gas uphill process, the circulation area of flue gas increases gradually, and flow velocity reduces gradually, and contained dust is separated gradually with flue gas, and this thing there occurs first time separation.When air-flow continues to rise, owing to being subject to the obstruction of flue gas dusting baffle plate 17, flue gas deflects, and the dust in flue gas is subject to the effect of gravity and inertia force, and dust and flue gas carry out second time and be separated.Continue at flue gas in the process risen, because the reason of horizontal segment, flue gas turns round, and in turning process, dust and flue gas have carried out being separated for the third time; Along with the continuation of flue gas is flowed, a passage contrary with flow of flue gas direction is formed between adjustable gas baffle 15 with flue gas dusting baffle plate 16, flue gas flow through herein passage time flowing in be subject to comparatively large disturbances, due to inertia, gravity and adjustable baffle plate 15 and the inhibition of flue gas dusting baffle plate 16, flue gas is separated for the 4th time with dust.This region is the region that flue gas is efficiently separated with dust.Isolated dust falls into ash removal pipe 18 and builds up, and when dust stratification reaches certain degree, the ash-removing mouth opened bottom ash removal pipe 18 implements ash discharge.By the angle of adjustment adjustable baffle plate 15, specific flue gas flexure type runner can either be formed, the velocity of liquid assets of flue gas can be regulated again.Therefore, the structure of adjustable gas baffle 15 and flue gas dusting baffle plate 16 can realize the repeatedly high-effective dust-removing of flue gas, decreases equipment dust stratification problem in flue significantly, turn improve flue gas enter heat exchanger after heat exchange efficiency.
Be separated for above-mentioned four times, be wherein most importantly separated for the 4th time, the dust be now separated is maximum, and for the dust of first three separation, relative is less, so there is no the device arranging separately ash disposal.
As one preferably, described flue gas enters in housing by independent flue 19, as shown in Figure 9, in such cases, the dust of first three separation can fall into the first vertical space between section and flue 19, then at the first vertical spatial placement ash handling equipment between section and flue 19, intermittent dust removal.
Preferably, the height in the housing that stretches into of flue 19 is higher than the height of the first vertical section.
For above-mentioned two kinds of embodiments, as one preferably, align with the end in the vertical direction be connected with adjustable gas baffle 15 of horizontal segment in the end of described flue gas dusting baffle plate 16, described flue gas dusting baffle plate 16 is 15-40 ° with the angle of horizontal direction, described tilting section and the angle of horizontal direction are 20-45 °, in the vertical direction, the height of the second vertical section is 2.5-5.6 times of tilting section height.
Preferably, align with first vertical section of in the vertical direction in the end be connected with adjustable gas baffle 15 of horizontal segment.
Although the present invention discloses as above with preferred embodiment, the present invention is not defined in this.Any those skilled in the art, without departing from the spirit and scope of the present invention, all can make various changes or modifications, and therefore protection scope of the present invention should be as the criterion with claim limited range.
Claims (2)
1. a smoke inlet device, comprise adjustable gas baffle, flue gas dusting baffle plate, housing, ash removal pipe, smoke inlet pipeline, smoke inlet pipeline is positioned at lower end, smoke outlet is positioned at upper end, ash removal pipe is built in housing, for the dust in sedimentation and collection flue gas, below ash removal pipe, connect regular ash exhauster; Described housing is made up of the first vertical section of lower end, the outside tilting section be connected with the first vertical section, the second vertical section be connected with tilting section and the horizontal segment be connected with the second vertical section that is positioned at top, described adjustable gas baffle is connected with the other end of horizontal segment, round the other end adjustment angle of horizontal segment; Described first vertical section constitutes the entrance of flue gas, and described ash removal pipe is deep in housing from smoke inlet, and flue gas dusting baffle plate is connected with the upper end being positioned at housing of ash removal pipe; In the vertical direction, the top and bottom of described flue gas dusting baffle plate are between the top and bottom of the second vertical section;
Align with the end in the vertical direction be connected with adjustable gas baffle of horizontal segment in the end of described flue gas dusting baffle plate, described flue gas dusting baffle plate and the angle of horizontal direction are 15-40 °, described tilting section and the angle of horizontal direction are 20-45 °, in the vertical direction, the height of the second vertical section is 2.5-5.6 times of tilting section height, aligns with first vertical section of in the vertical direction in the end be connected with adjustable gas baffle of horizontal segment.
2. the heat regenerator of a cement production process UTILIZATION OF VESIDUAL HEAT IN, described heat exchanger comprises the first tube bank and the second tube bank, be positioned at the high-temperature flue gas import of lower end, be positioned at the high-temperature flue gas outlet of upper end, cryogenic fluid entrance, cryogenic fluid outlet and housing, polylith heat-storing material is set in described heat exchanger shell, described polylith heat-storing material is stacked, first pore and the second pore are set in every block heat-storing material, first pore and the second pore arranged in a crossed manner, described first tube bank and the second tube bank are each passed through the first pore and the second pore, the external diameter of the first tube bank and the second tube bank equals the diameter of the first pore and the second pore respectively, described first restrains the flue gas produced for the cement production process that circulates, and the second tube bank is for the cryogenic fluid that circulates, described flue gas enters from high-temperature flue gas entry, and through the first tube bank, then discharge from high-temperature flue gas outlet, cryogenic fluid enters from cryogenic fluid entrance, through the second tube bank, then discharges from cryogenic fluid outlet, described heat exchanger is vertical structure, and the first pore is vertical direction, and the second pore is horizontal direction, on the flow direction of flue gas, arrange multiple dividing plate, is divided into by the first pore and organizes independently passage more, alignment housing both sides in vertical along housing, the distance between dividing plate is more and more less, it is characterized in that, high-temperature flue gas import arranges smoke inlet device, and described smoke inlet device is smoke inlet device according to claim 1.
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| CN201410184980.5A CN103940276B (en) | 2014-05-05 | 2014-05-05 | Exhaust gas inlet device and regenerative heat exchanger containing same |
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| CN201410184980.5A CN103940276B (en) | 2014-05-05 | 2014-05-05 | Exhaust gas inlet device and regenerative heat exchanger containing same |
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| CN103940276A CN103940276A (en) | 2014-07-23 |
| CN103940276B true CN103940276B (en) | 2015-03-04 |
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| CN111174618B (en) * | 2019-12-23 | 2021-02-02 | 青岛建设集团有限公司 | Heat storage heat exchanger and fresh air system |
| CN111076594A (en) * | 2019-12-26 | 2020-04-28 | 思安新能源股份有限公司 | Vertical heat storage tower |
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| CN2769822Y (en) * | 2004-11-09 | 2006-04-05 | 陈应忠 | Long-service life combined fireproof heat accumulator |
| CN201057506Y (en) * | 2007-05-22 | 2008-05-07 | 俞琦 | High-temperature energy accumulation device of central air conditioner |
| CN202013127U (en) * | 2011-04-02 | 2011-10-19 | 刘阳 | Solid heat accumulation structure |
| CN102589328A (en) * | 2012-02-10 | 2012-07-18 | 刘小江 | Pure-countercurrent cellular plate-pin heat exchanger and combination thereof |
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- 2014-05-05 CN CN201410184980.5A patent/CN103940276B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2769822Y (en) * | 2004-11-09 | 2006-04-05 | 陈应忠 | Long-service life combined fireproof heat accumulator |
| CN201057506Y (en) * | 2007-05-22 | 2008-05-07 | 俞琦 | High-temperature energy accumulation device of central air conditioner |
| CN202013127U (en) * | 2011-04-02 | 2011-10-19 | 刘阳 | Solid heat accumulation structure |
| CN102589328A (en) * | 2012-02-10 | 2012-07-18 | 刘小江 | Pure-countercurrent cellular plate-pin heat exchanger and combination thereof |
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Effective date of registration: 20220210 Address after: No.18, Lashan Road, Shizhong District, Jinan City, Shandong Province Patentee after: Shandong Zhonghe Thermal Technology Co.,Ltd. Address before: 250013 Room 101, Qilu Software Park, Jinan City, Shandong Province Patentee before: SHANDONG Research Institute OF ENERGY & ENVIRONMENT |