CN104197752B - A kind of have the waste heat utilization heat exchanger that multiple directions blow ash - Google Patents
A kind of have the waste heat utilization heat exchanger that multiple directions blow ash Download PDFInfo
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- CN104197752B CN104197752B CN201410412142.9A CN201410412142A CN104197752B CN 104197752 B CN104197752 B CN 104197752B CN 201410412142 A CN201410412142 A CN 201410412142A CN 104197752 B CN104197752 B CN 104197752B
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Abstract
The invention discloses a kind of have multiple directions blow ash waste heat utilization heat exchanger, comprise heat-exchanging tube bundle, inlet exhaust gas, offgas outlet and housing, heat-exchanging tube bundle is arranged in the housing, described heat-exchanging tube bundle assumes diamond in shape structural arrangement, housing has the diamond structure matched with heat-exchanging tube bundle, heat exchanger arranges multiple ash blowing mouth, heat-exchanging tube bundle assumes diamond in shape structural arrangement, housing has the diamond structure matched with heat-exchanging tube bundle, inlet exhaust gas is arranged on the first angular position place of the diamond structure of shell, offgas outlet is arranged on the second angular position place of the diamond structure of shell, the present invention is by the different setting of the distance between heat-exchanging tube bundle heat-exchanging tube bundle in the two directions, heat-exchanging tube bundle is made to be in-line arrangement crossflow regenerator, having good effect of heat exchange, be easy to the advantages such as cleaning, is a kind of heat exchange equipment being applicable to reclaim cement rotary kiln exhaust gas heat.
Description
The application is the application number of application on December 9th, 2013 is the divisional application of " waste heat utilization heat exchanger that a kind of output fluid temperature is constant " of 2013106640399.
Technical field
The present invention relates to a kind of have multiple directions blow ash waste heat utilization heat exchanger, belong to technical field of heat exchangers.
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 a highly energy-consuming, the industry of high pollution.In the tail gas that cement rotary kiln produces, dust content is high, poor quality.Cement rotary kiln afterheat generating system can carry out recycling to using waste heat from tail gas, realizes the object of energy-saving and emission-reduction.But in relevant boiler of power generation by waste heat, the fouling phenomenon of heat transmission equipment is serious, heat-transfer capability is poor, deashing difficulty, these problems demand solve.
In existing heat reclaim unit, the arrangement of heat-exchanging tube bundle has two kinds usually, and in-line arrangement and fork row, see Fig. 1 and Fig. 2.Flow field when fluid scouring in-line arrangement and staggered tubes bundle is different.Flow in the bending channel of fluid alternating contractions and expansion between pipe during fork row, than during in-line arrangement between pipe the flow disturbance of corridor violent, therefore the exchange capability of heat of the row of pitching is stronger than in-line arrangement.Meanwhile, the drag losses of staggered tubes bundle is greater than in-line arrangement, and for the tube bank needing flush clean, in-line arrangement has easy cleaned advantage.
In the waste heat utilization heat exchanger of prior art, different according to the temperature of the tail gas of UTILIZATION OF VESIDUAL HEAT IN, or because of the difference of the heat transfer effect that dust stratification causes, cause the difference of the temperature of the heat exchanging fluid exported, be therefore badly in need of realizing a kind of heat exchanger keeping output fluid temperature constant.
Summary of the invention
The present invention is directed to the problem that the temperature of output heat exchanging fluid that existing waste heat utilization heat exchanger exists is different, propose and a kind of there is the waste heat utilization heat exchanger that multiple directions blow ash.
Of the present invention a kind of have multiple directions blow ash waste heat utilization heat exchanger, by the following technical solutions:
This waste heat utilization heat exchanger, comprise heat-exchanging tube bundle, housing, import header and outlet header, heat-exchanging tube bundle is arranged in the housing, the two ends of heat-exchanging tube bundle are connected with import header and outlet header respectively, import header is provided with inlet tube, for to delivery heat transfer fluid in heat-exchanging tube bundle, outlet header is provided with outlet, for the heat exchanging fluid after heat exchange is discharged from heat-exchanging tube bundle, inlet exhaust gas and offgas outlet are separately positioned on the upper and lower of housing, are respectively used to input and output tail gas in housing; Inlet tube is provided with valve, for controlling the flow of the heat exchanging fluid entering heat exchanger bundle, in inlet tube, be provided with inlet temperature sensor, for measuring the temperature of heat exchanging fluid in inlet tube, outlet temperature sensor is provided with, for measuring the temperature of heat exchanging fluid in outlet in outlet; Temperature sensor and valve all with central controller communication link, central controller carrys out the aperture of by-pass valve control according to the temperature of heat exchanging fluid in the outlet of temperature sensor measurement, if the temperature of heat exchanging fluid is higher than setting value in outlet, central controller controls valve strengthens aperture, improve the flow of the heat exchanging fluid entered, if the temperature of heat exchanging fluid is lower than setting value in outlet, central controller controls valve reduces aperture, reduces the flow of the heat exchanging fluid entered.
Described heat-exchanging tube bundle assumes diamond in shape arrangement, housing is in the diamond structure matched with heat-exchanging tube bundle diamond array, be called rhombus housing, inlet exhaust gas is arranged on the first angular position place of rhombus housing, offgas outlet is arranged on the second angular position place of rhombus housing, rhombus housing the first angle and the second angle be diagonal angle, the bottom that heat-exchanging tube bundle on first angle summit of heat-exchanging tube bundle diamond array is arranged on inlet exhaust gas is put and relative with inlet exhaust gas, heat-exchanging tube bundle on second angle summit of heat-exchanging tube bundle diamond array is arranged on the top of offgas outlet and relative with offgas outlet, first angle of heat-exchanging tube bundle diamond array and the second angle of heat-exchanging tube bundle diamond array are diagonal angles, tail gas is entered by inlet exhaust gas, heat-exchanging tube bundle first on the first angle summit of heat-exchanging tube bundle diamond array, then transversal flow heat-exchanging tube bundle, heat-exchanging tube bundle again on the second angle summit of heat-exchanging tube bundle diamond array, finally discharge from offgas outlet.
First angle of heat-exchanging tube bundle diamond array is made up of the first limit of heat-exchanging tube bundle diamond array and the Second Edge of heat-exchanging tube bundle diamond array, heat exchanger tube spacing on the first edge direction (distance between the central axis referring to adjacent heat exchange tubes) is L1, heat exchanger tube spacing on Second Edge direction is that L2, L1 and L2 are unequal.Preferably, L1 is 1.3 times of L2.
Heat exchanger tube spacing L in first included angle A of heat-exchanging tube bundle diamond array, heat-exchanging tube bundle and the relation of heat exchanger tube outer diameter D meet following formula:
3.7 × D>L>2.4 × D, wherein 20mm<D<50mm;
Sin (A/2)=b × (L/D)
c, wherein b, c are parameter, and b is 1.65-1.8, c is-0.8 to-0.9.
Two limits of the first angle of described rhombus housing arrange 1# ash blowing mouth and 2# ash blowing mouth respectively, two limits of the second angle of rhombus housing arrange 3# ash blowing mouth and 4# ash blowing mouth respectively, wherein 1# ash blowing mouth and the limit of the rhombus housing at 3# ash blowing mouth place are two relative limits, and 2# ash blowing mouth and the limit of the rhombus housing at 4# ash blowing mouth place are two relative limits; Wherein 1# ash blowing mouth is positioned at the bottom on limit, place, 2# ash blowing mouth is positioned at the top on limit, place, 3# ash blowing mouth is positioned at the top on limit, place, 4# ash blowing mouth is positioned at the bottom on limit, place, thus making the distance of 1# ash blowing mouth distance inlet exhaust gas be greater than 2# ash blowing mouth distance inlet exhaust gas distance, the distance of 3# ash blowing mouth distance offgas outlet is greater than 4# ash blowing mouth distance offgas outlet distance.
Described rhombus housing is also provided with 5# ash blowing mouth, 6# ash blowing mouth, 7# ash blowing mouth, 8# ash blowing mouth, wherein 5# ash blowing mouth and No. 1 ash blowing mouth are positioned at same, and are positioned at the top on limit, place; 6# ash blowing mouth and 2# ash blowing mouth are positioned at on one side, and are positioned at the bottom on limit, place; 7# ash blowing mouth and 3# ash blowing mouth are positioned at on one side, and are positioned at the bottom on limit, place; 8# ash blowing mouth and 4# ash blowing mouth are positioned at on one side, and are positioned at the top on limit, place; Thus making the distance of 5# ash blowing mouth distance inlet exhaust gas be less than 6# ash blowing mouth distance inlet exhaust gas distance, the distance of 7# ash blowing mouth distance offgas outlet is less than 8# ash blowing mouth distance offgas outlet distance.
Heat-exchanging tube bundle in the present invention assumes diamond in shape arrangement, is a kind of high-efficiency cleaning formula heat reclaim unit, have heat-transfer capability strong, etc. feature.Compared with prior art, the present invention has following advantage:
1) by controlling flow, the temperature remained constant of output fluid is made.
2) the present invention to be assumed diamond in shape arrangement by heat-exchanging tube bundle, make heat exchanger have flow resistance little, be convenient to blow ash, long service life.
3) by setting that the distance between heat-exchanging tube bundle heat-exchanging tube bundle is in the two directions different, heat-exchanging tube bundle is made to be in-line arrangement crossflow regenerator, having good effect of heat exchange, be easy to the advantages such as cleaning, is a kind of heat exchange equipment being applicable to reclaim cement rotary kiln exhaust gas heat.
4) housing and heat-exchanging tube bundle have the diamond structure matched, and can reduce the dead band of heat exchange area, make the flow velocity of the tail gas in heat transfer process keep relatively consistent simultaneously.
5) draw the best relation formula of heat-exchanging tube bundle spacing and caliber, meet the demand of heat exchange and minimizing dust stratification.
Accompanying drawing explanation
Fig. 1 is the schematic diagram that heat-exchanging tube bundle in-line arrangement of the prior art is arranged;
Fig. 2 is the schematic diagram that the arrangement of heat-exchanging tube bundle of the prior art fork is put;
Fig. 3 is the schematic diagram of heat-exchanging tube bundle rhombus of the present invention distribution;
Fig. 4 is the schematic diagram of the partial enlargement in Fig. 3;
Fig. 5 is the profile along two angles up and down of diamond structure in Fig. 3;
Fig. 6 is the insert row of heat-exchanging tube bundle diamond array of the present invention and prior art, the coefficient of heat transfer effectiveness comparison figure of in-line arrangement;
Fig. 7 is blower fan FREQUENCY CONTROL flow chart;
Fig. 8 is the whirlpool schematic diagram blowing ash formation;
Fig. 9 is another embodiment blowing ash.
In figure: 1, inlet exhaust gas, 2, offgas outlet, 3, 1# ash blowing mouth, 4, 2# ash blowing mouth, 5, 3# ash blowing mouth, 6, 4# ash blowing mouth, 7, heat-exchanging tube bundle, 8, housing, 9, outlet header, 10, import header, 11, dividing plate, 12, inlet tube, 13, outlet, 14, inlet temperature sensor, 15, outlet temperature sensor, 16, valve, 17, first angle summit heat exchanger tube, 18, second angle summit heat exchanger tube, 19, first limit of heat-exchanging tube bundle diamond array, 20, the Second Edge of heat-exchanging tube bundle diamond array, 21, rhombus housing first straight flange, 22, rhombus housing second straight flange, 23, rhombus housing the 3rd straight flange, 24, rhombus housing the 4th straight flange, 25, 3rd angle summit heat exchanger tube, 26, the 4th angle summit heat exchanger tube, 27,5# ash blowing mouth, 28,6# ash blowing mouth, 29,7# ash blowing mouth, 30,8# blows grey interface.
Detailed description of the invention
The diamond structure of the heat-exchanging tube bundle diamond array (heat-exchanging tube bundle is made up of some heat exchanger tubes) described in following content and housing is the shape of the tangent plane from the central axis perpendicular to heat-exchanging tube bundle; Heat exchanger tube spacing refers to the distance between the central axis of adjacent heat exchange tubes.
As shown in Figure 3, heat exchanger of the present invention comprises heat-exchanging tube bundle 7, inlet exhaust gas 1, offgas outlet 2 and housing 8.Heat-exchanging tube bundle 7 is arranged in housing 8, heat-exchanging tube bundle assumes diamond in shape arrangement, first limit 19 of this heat-exchanging tube bundle diamond array is adjacent with the Second Edge 20 of heat-exchanging tube bundle diamond array, as shown in Figure 4, first limit 19 is that the heat exchanger tube arranged by outermost two is formed with Second Edge 20, the angle of the cross section circle center line connecting formation of the heat exchanger tube on these two limits is first included angle A (i.e. the angles of outermost two row's heat exchanger tubes formation of Fig. 3 middle and upper part) of heat-exchanging tube bundle diamond array, second angle of heat-exchanging tube bundle diamond array that relative with the first angle is, two other angle is respectively the 3rd angle of heat-exchanging tube bundle diamond array and the 4th angle of heat-exchanging tube bundle diamond array, four angle summits place is respectively the first angle summit heat exchanger tube 17, second angle summit heat exchanger tube 18, 3rd angle summit heat exchanger tube 25 and the 4th angle summit heat exchanger tube 26.Housing 8 has and arranges with heat-exchanging tube bundle 7 diamond structure matched, be called rhombus housing, comprise rhombus housing first straight flange 21, rhombus housing second straight flange 22, rhombus housing the 3rd straight flange 23 and rhombus housing the 4th straight flange 24, the angle that rhombus housing first straight flange 21 and rhombus housing second straight flange 22 extension line are formed is rhombus housing first angle, and the angle that rhombus housing the 3rd straight flange 23 and rhombus housing the 4th straight flange 24 extension line are formed is rhombus housing second angle.Inlet exhaust gas 1 is arranged on the rhombus housing first angular position place on housing 8, and offgas outlet 2 is arranged on the rhombus housing second angular position place on housing 8, and rhombus housing first angle and rhombus housing second angle are diagonal angle.First angle summit heat exchanger tube 17 is arranged on the position of inlet exhaust gas 1, and the second angle summit heat exchanger tube 18 is arranged on offgas outlet 2 position.Cement rotary kiln tail gas enters from inlet exhaust gas 1, first through the first angle summit heat exchanger tube 17, then the heat exchanger tube of transversal flow between the first angle summit heat exchanger tube 17 and the second angle summit heat exchanger tube 18, then through the second angle summit heat exchanger tube 18, finally discharge from offgas outlet 2.
Because be diamond structure, therefore the first angle of heat-exchanging tube bundle diamond array is identical with the second angle, and in like manner, the first angle of rhombus housing is identical with the second angle.
Preferably, first angle of rhombus housing is greater than the first angle of heat-exchanging tube bundle diamond array, arranging like this can make the flow area of tail gas in housing be that first to increase the amplitude reduced afterwards larger, can ensure constantly to increase in the tail gas speed of bottom, take away more dust stratification, reduce as far as possible and cause dust stratification because of the minimizing of flow velocity.
Above-mentioned waste heat utilization heat exchanger can be applied to cement rotary kiln tail gas field of waste heat utilization, certainly for a person skilled in the art, be not limited to cement rotary kiln tail gas field of waste heat utilization, can also be comprised other and utilize flue gas to carry out the field of UTILIZATION OF VESIDUAL HEAT IN, such as, in boiler exhaust gas.
The heat-exchanging tube bundle of the above-mentioned waste heat utilization heat exchanger of the present invention assume diamond in shape heat-exchanging tube bundle in heat-exchanging tube bundle in-line arrangement is arranged and Fig. 2 provides in the prior art of arranging and providing with Fig. 1 prior art pitch the contrast of the coefficient of heat transfer put of arranging can see Fig. 6.As can be seen from Figure 6, three kinds of tube banks arrange that the shell-side average surface heat transfer coefficient produced all increases with the increase of flow velocity, and the average surface heat transfer coefficient that diamond structure is arranged is maximum, far away higher than the heat exchanger of other two kinds of structures, be about 2-3 times of other two kinds of structures.
Adopt heat-exchanging tube bundle to assume diamond in shape the heat exchanger of structural configuration, because be applied to the field of waste heat utilization of tail gas, therefore easily produce fouling phenomenon.Therefore in order to reduce the generation of dust stratification, the size of the first included angle A of reasonably combined heat exchanger tube spacing (distance between the central axis of adjacent heat exchange tubes) and diamond array is needed.When heat exchanger tube diameter is certain, reduce heat exchanger tube spacing, more heat exchanger tube can be distributed in the volume of unit, this can increase heat exchange area, strengthen the utilization of waste heat, but while heat exchanger tube spacing reduces, because the reduction in exhaust gas flow space, easily cause dust stratification, time serious, even block the heat exchanger channels of shell side.For the size of the first included angle A of heat-exchanging tube bundle diamond array, be also needs rational scopes.If the first included angle A is too little, then be equivalent to more and more level off to a line along the distribution of exhaust gas flow direction heat exchanger tube, make heat exchange route long, easily cause dust stratification, simultaneously because the heat exchanger tube quantity of unit volume distribution obviously reduces, also the decline of heat transfer effect is caused, in like manner, if the first included angle A is too large, the distribution being then equivalent to vertical exhaust gas flow direction heat exchanger tube more and more levels off to a line, tail gas is made to need circulation path in the horizontal long, and the camber that needs turn is excessive, easily cause dust stratification, simultaneously because the heat exchanger tube quantity of unit volume distribution obviously reduces, also the decline of heat transfer effect is caused, therefore need there is a rational scope to the first included angle A.
By test of many times, meeting the mediation in heat exchange and resistance two kinds of situations, the outer diameter D of the rational heat exchanger tube obtained and the relational expression of heat exchanger tube spacing L are:
3.7 × D>L>2.4 × D, wherein 20mm<D<50mm;
Preferably, the relation of L and D meets as follows: L=a × D, a are parameters, wherein a=3.2.
The relation of first included angle A and L and D of changing heat-exchanging tube bundle diamond array meets following formula:
Sin (A/2)=b × (L/D)
c, wherein b, c are parameter, and b is 1.65-1.8, c is-0.8 to-0.9.Preferably, b is 1.72, c is-0.815.
First included angle A of heat-exchanging tube bundle diamond array is 70-110 °, most preferably 87 °.
As a preferred embodiment, the four edges forming the rhombus of heat-exchanging tube bundle is parallel to each other with the four edges of the rhombus forming housing.
As shown in Figure 3 and Figure 4, direction along the first limit 19 of heat-exchanging tube bundle diamond array has arranges heat exchanger tube more, direction along the Second Edge 20 of heat-exchanging tube bundle diamond array has arranges heat exchanger tube more, heat exchanger tube spacing on the first direction, limit 19 is L1, and the heat exchanger tube spacing on Second Edge 20 direction is L2, as a preferred embodiment, L1 and L2 is unequal, because if L1 and L2 is unequal, then the arrangement mode of heat-exchanging tube bundle is exactly stagger mutually, like this can augmentation of heat transfer further.As a preferred embodiment, L1 is 1.3 times of L2.Under this kind of multiple, can distribute more heat exchanger tube, makes whole heat exchanger have the very high coefficient of heat transfer, and resistance increases not quite substantially simultaneously.Certainly, as a preferred embodiment, L1 and L2 also can be identical.
If the heat exchanger tube (the first limit 19 in such as Fig. 3 and the heat exchanger tube of Second Edge 20) in heat-exchanging tube bundle on most limit is if the distance of distance housing 8 straight flange is too near, tail gas convection space can be caused too little, easy dust stratification, if but it is too far away, then easily cause a large amount of tail gas not through heat-exchanging tube bundle, cause the expansion in heat exchange dead band, worsen heat exchange.Therefore for the heat exchanger tube on the first limit 19 and the minimum distance condition that also demand fulfillment is certain of housing 8 straight flange.Draw the distance S demand fulfillment 3.8D>S>4.6D of central axis distance housing 8 straight flange of the heat exchanger tube on most limit by experiment, wherein 20mm<D<50mm, can meet heat exchange simultaneously and avoid the demand of dust stratification.
The preferred Ingredient percent of material for heat exchanger tube is as follows:
Ni 30%; Cr 20%; Al 6%; C 0.03%; B 0.016%; Co 2%; Ti 3%; Nb 0.1%; La 0.2%; Ce0.2%; Surplus is Fe.
The manufacture method of alloy is: become ingot by the composition smelting and pouring according to alloy in vaccum sensitive stove, then at 1200 DEG C-900 DEG C, alloy pig forge hot is become bar, be rolled into dish material at 1200 DEG C-900 DEG C, then become different silk materials in room temperature by external diameter specification requirement cold-drawn.
After tested, above-mentioned alloy has very high thermal conductivity, has higher heat resistance simultaneously, meets the multiple requirements in cement rotary kiln tail gas waste heat utilization heat exchanger.
As a preferred embodiment, along the direction of exhaust gas flow, heat exchanger tube spacing first reduces rear increase.Main cause is because of the flowing along with tail gas, simultaneously along with the circulation area of tail gas first becomes greatly to diminish, thus cause the speed of tail gas to be first diminish to become large afterwards, cause the easy dust stratification of part that middle tail gas speed diminishes, therefore can be arranged so that the speed of tail gas remains unchanged substantially by heat exchanger tube spacing, can reduce along with the reduction of the speed of tail gas as far as possible and cause the dust stratification in the middle part of heat exchanger, thus ensure the minimizing of dust stratification.
Because the place that to be tail gas circulation area maximum, the position of pipe row (a row heat exchanger tube) at the place of the line between two other angle of heat-exchanging tube bundle diamond array (trigonometric sum the 4th jiao), therefore being ever-reduced by the heat exchanger tube spacing inlet exhaust gas to trigonometric sum the 4th jiao of line, is constantly become large from the heat exchanger tube spacing be wired between offgas outlet of trigonometric sum the 4th jiao.Along the upper and lower of the line symmetry between trigonometric sum the 4th jiao, the heat exchanger tube spacing of bottom is less than the heat exchanger tube spacing on top.
Certainly, along with the flow process of tail gas, because wash away heat-exchanging tube bundle, its kinetic energy is constantly reduced, thus cause in upper and lower, the i.e. top of trigonometric sum the 4th jiao of line, there is the position of same circulation area, if the distribution of heat exchanger tube spacing is identical, then the tail gas speed on top significantly will be greater than the tail gas speed of bottom, therefore, in identical circulation area situation, the heat exchanger tube spacing of bottom is less than the heat exchanger tube spacing on top, thus makes the tail gas speed of bottom keep substantially identical in the position of identical circulation area with top.
Preferably, same circulation area, the heat exchanger tube spacing on top is 1.05-1.1 times of the heat exchanger tube spacing of bottom.
As a preferred embodiment, on the direction of exhaust gas flow, the maximum spacing of heat exchanger tube is 1.3-1.5 times of minimum spacing.
Even if but heat exchanger tube spacing constantly increases, the relation between heat exchanger tube spacing and heat exchanger tube external diameter also meets formula above.
As a preferred embodiment, the outer wall of heat exchanger tube arranges projection, along with the increase of the distance of distance inlet exhaust gas 1, the height of heat exchanger tube projection is more and more higher.Main cause is along with along on the flow direction of tail gas, exhaust temperature is in continuous decline, the caloric receptivity of the fluid in heat-exchanging tube bundle is caused also constantly to decline, thus cause the increase of the distance along with distance inlet exhaust gas 1, in heat exchanger tube, the temperature increase speed of fluid is also come slower, therefore by the increase of the distance along with distance inlet exhaust gas, the height of heat exchanger tube projection is more and more higher, the caloric receptivity of heat exchanger tube can be strengthened, ensure that the fluid well-distributing in each heat exchanger tube is heated, the uniformity ensureing the temperature of the fluid of heating and the uniformity of being heated, also avoid part heat exchanger tube overheated or excessively cold.
As a preferred embodiment, the maximum height of projection on heat exchanger tube outer wall be the 1.5-1.6 of minimum height of projection doubly.
As preferably, the height of projection on same heat exchanger tube is different along with the difference of the distance of distance inlet exhaust gas, can ensure so same heat exchanger tube evenly absorbs heat.
As preferably, the height of projection on same heat exchanger tube can be identical, but the height of projection on various heat exchange pipe can be different.
As the embodiment that can substitute, along with the increase of the distance of distance inlet exhaust gas 1, the distribution density of heat exchanger tube projection is increasing.By the increase of distribution density, can make expand heat exchange area along with distance inlet exhaust gas distance increasing, ensure that the fluid well-distributing in each heat exchanger tube is heated, the uniformity ensureing the temperature of the fluid of heating and the uniformity of being heated, also avoid part heat exchanger tube overheated or excessively cold.
The housing 8 of heat exchanger of the present invention also comprises ash blowing mouth.As shown in Figure 3, rhombus housing first straight flange 21 be connected with inlet exhaust gas 1 and rhombus housing second straight flange 22 arrange 1# ash blowing mouth 3 and 2# ash blowing mouth 4 respectively, rhombus housing the 3rd straight flange 23 be connected with offgas outlet 2 and rhombus housing the 4th straight flange 24 arrange 3# ash blowing mouth 5 and 4# ash blowing mouth 6 respectively; Wherein 1# ash blowing mouth 3 is positioned at the bottom of place rhombus housing first straight flange 21,2# ash blowing mouth 4 is positioned at the top of place rhombus housing second straight flange 22,3# ash blowing mouth 5 is positioned at the top of place rhombus housing the 3rd straight flange 23,4# ash blowing mouth 6 is positioned at the bottom of place rhombus housing the 4th straight flange 24, thus making 1# ash blowing mouth 3 be greater than the distance of 2# ash blowing mouth 4 apart from inlet exhaust gas 1 apart from the distance of inlet exhaust gas 1,3# ash blowing mouth 5 is greater than the distance of 4# ash blowing mouth 6 apart from offgas outlet 1 apart from the distance of offgas outlet 1.
Above-mentioned ash blowing mouth can open 2-4, by the setting of the position of above-mentioned ash blowing mouth, the wind blowing ash can be made in heat exchanger shell to form whirlpool, as shown in Figure 8.Each ash blowing mouth is connected with blower fan.
If open 2 ash blowing mouthes, then need two the relative ash blowing mouthes opening opposite side, such as 1# ash blowing mouth 3 and 3# ash blowing mouth 5, or 2# ash blowing mouth 4 and 4# ash blowing mouth 6.
By multiple ash blowing mouthes of above-mentioned setting, can make when one or 2 ash blowing mouthes can not work, other ash blowing mouth still can keep normal work.
The embodiment of ash is preferably blown as another, as shown in Figure 9, four straight flanges of housing 8 all arrange two ash blowing mouthes, wherein 5# ash blowing mouth 27 and No. 1 ash blowing mouth 3 are located on the first straight flange 21, but on the top of the first straight flange 21,6# ash blowing mouth 28 and 2# ash blowing mouth 4 are located on the second straight flange 22, but in the bottom of the second straight flange 22,7# ash blowing mouth 29 and 3# ash blowing mouth 5 are located on the 3rd straight flange 23, but in the bottom of the 3rd straight flange 23,8# ash blowing mouth 30 and 4# ash blowing mouth 6 are located on the 4th straight flange 24, but on the top of the 4th straight flange 24.Thus making 5# ash blowing mouth 27 be less than 6# ash blowing mouth 28 apart from inlet exhaust gas distance apart from the distance of inlet exhaust gas 1,7# ash blowing mouth 29 is less than the distance of 8# ash blowing mouth 30 apart from offgas outlet apart from the distance of offgas outlet.
By above-mentioned setting, can make to blow in grey process, air, along at clockwise and counterclockwise movement, increases the dynamics of blowing ash.Fig. 7 gives blower fan FREQUENCY CONTROL flow process.
Cement rotary kiln tail gas waste heat utilization heat exchanger specifically to blow grey process as follows:
1) 1# ash blowing mouth 3,2# ash blowing mouth 4,3# ash blowing mouth 5 and 4# ash blowing mouth 6 is closed, open 5# ash blowing mouth 27,6# ash blowing mouth 28,7# ash blowing mouth 29 and 8# ash blowing mouth 30, make air along counterclockwise running, realize counterclockwise blowing ash, remove the anticlockwise dust stratification of heat-exchanging tube bundle outer surface;
2) 5# ash blowing mouth 27,6# ash blowing mouth 28,7# ash blowing mouth 29 and 8# ash blowing mouth 30 is closed, open 1# ash blowing mouth 3,2# ash blowing mouth 4,3# ash blowing mouth 5 and 4# ash blowing mouth 6, air is run clockwise, realize blowing ash clockwise, remove the clockwise dust stratification of heat-exchanging tube bundle outer surface.
Blow grey cyclic process through multiple, can comprehensive, high-efficient cleaning except the dust stratification on heat-exchanging tube bundle 7 surface.Ash blowing mouth place flange is for connecting blowing pipe road, and described blowing pipe connecting fan, the adjustment of blowing ash wind and air quantity is realized by blower fan.The ash bucket that the dust stratification blown off enters below offgas outlet 2 stores.
As preferential choosing, the blower fan that each ash blowing mouth connects and central controller communication link, central controller regulates the frequency of blower fan automatically according to dust stratification situation.
Central controller controls the frequency of blower fan according to the size of thermal conduction resistance.If thermal conduction resistance is excessive, then show that dust stratification is serious, then need the air quantity strengthening blower fan, otherwise, then need to adopt the blower fan frequency used lower, economize energy.
In the central controller, first prestore a part of data, these data comprise the heat exchanging tube bank internal face convective heat-transfer coefficient of fluid at friction speed, temperature in heat-exchanging tube bundle, the convective heat-transfer coefficient of the heat exchanging tube bank outer surface of tail gas under friction speed and different temperatures.Consider that the influence factor of temperature effects on surface heat transfer coefficient becomes large, then also only can consider the convection transfer rate situation under a storage speed change.
For obtaining of the above-mentioned coefficient of heat transfer, by test or can obtain by inquiring about existing convection transfer rate table.
As shown in Figure 5, same one end of all heat-exchanging tube bundles is all connected with import header 10, the other end is connected with outlet header 9, import header 10 is provided with inlet tube 12, for to replace tubes heat intrafascicular delivery heat transfer fluid, outlet header 9 is provided with outlet 13, for being discharged from heat-exchanging tube bundle by the heat exchanging fluid after heat exchange.Inlet tube 12 is provided with valve 16, for controlling the flow of the heat exchanging fluid entering heat exchanger bundle.Inlet temperature sensor 14 is provided with, for measuring the temperature of heat exchanging fluid in inlet tube 12 in inlet tube 12.Outlet temperature sensor 15 is provided with, for measuring the temperature of heat exchanging fluid in outlet 13 in outlet 13.Valve 16 adopts electrically operated valve, valve 16, inlet temperature sensor 14 and outlet temperature sensor 15 all with central controller (not shown in FIG.) communication link, in the outlet 13 that central controller is measured according to outlet temperature sensor 15, the temperature of fluid carrys out the aperture of by-pass valve control 16, if fluid temperature (F.T.) is higher than setting value in outlet 13, the aperture of central controller controls valve, improving the fluid flow entered in import header 10, reducing the lifting of fluid temperature (F.T.) by increasing flow; If the fluid temperature (F.T.) of outlet 13 is lower than setting value, central controller controls valve reduces aperture, reduces the fluid flow entered in import header 10, makes the higher of the lifting of fluid temperature (F.T.) by reducing flow.
As preferably, as shown in Figure 5, by arranging dividing plate 11 in import header 10 and outlet header 9, whole heat exchanger can be set to multiple tube side.
At inlet exhaust gas 1, place is provided with inlet exhaust gas temperature sensor, and at offgas outlet 2, place is provided with outlet exhaust gas temperature sensor, detects the exhaust temperature T at inlet exhaust gas 1 place respectively
w1with the exhaust temperature T at offgas outlet 2 place
w2.Inlet temperature sensor 14 and outlet temperature sensor 15 detect heat-exchanging tube bundle inlet fluid temperature T respectively
l1with heat-exchanging tube bundle exit fluid temperature T
l2.Multiple positions in inlet exhaust gas 1, offgas outlet 2 and housing 8 between inlet exhaust gas 1 and offgas outlet 2 are provided with the first current meter measuring tail gas flow velocity, are provided with the second current meter measuring heat exchanging fluid flow velocity in heat exchanger tube import department.Go out to enter fluid volume flow V in heat-exchanging tube bundle by measuring numerical computations
l, the mean value of the numerical value simultaneously recorded by the current meter of multiple measurement tail gas flow velocity obtains the mean flow rate of tail gas; The caloric receptivity that the temperature difference of the fluid of heat-exchanging tube bundle and flow can obtain fluid is flowed through, namely total heat exchange amount Q, Q=ρ V by calculating
l* C
p* (T
l2-T
l1), wherein, ρ is the density of fluid in heat-exchanging tube bundle, C
pfor the specific heat at constant pressure of fluid in heat-exchanging tube bundle; Then according to total heat exchange amount Q=K*A* △ T
m, wherein △ T
mthe logarithmic mean temperature difference (LMTD) of heat transfer process, △ T
m=((T
w1-T
l2)-(T
w2-T
l1))/ln ((T
w1-T
l2)/(T
w2-T
l1)), K is the total heat transfer coefficient of heat exchanger, and A is heat exchange area, takes heat pipe external diameter to calculate, and draws total coefficient of heat transfer K.From the data prestored, the surface coefficient of heat transfer h of heat exchanger tube outer wall and inwall is drawn according to the flow velocity of the mean flow rate of tail gas and heat exchanger tube inner fluid, temperature
wand h
l.Central controller is according to the K calculated, h
wand h
l,the dust stratification thermal conduction resistance R outside heat exchanger tube is gone out according to heat transfer formulae discovery
do.
In above-mentioned formula, K is total heat transfer coefficient; h
wfor the surface coefficient of heat transfer that heat exchanger tube outer wall tail gas is right; h
lfor the surface coefficient of heat transfer of heat exchanger tube inner fluid; d
ofor heat exchanger tube overall diameter; d
ifor heat exchanger tube interior diameter; d
mfor heat exchanger tube average diameter, equal (d
o+ d
i)/2; δ is the wall thickness of heat exchanger tube, equals (d
o-d
i)/2; λ is the thermal conductivity factor of heat exchanger tube; R
dofor the dust stratification thermal conduction resistance of heat exchanger tube.
When blowing ash, central controller can transfer the last ruuning situation, draws the dust stratification thermal conduction resistance of current heat exchanger tube, automatically chooses suitable blower fan frequency according to the size of dust stratification thermal conduction resistance.
Present invention also offers a kind of another kind of method measuring dust stratification thermal conduction resistance.The method is as follows:
1) inlet exhaust gas temperature T is detected respectively
w1, offgas outlet exhaust temperature T
w2, heat-exchanging tube bundle inlet fluid temperature T
l1with heat-exchanging tube bundle exit fluid temperature T
l2; Being arranged on the second current meter of rate of flow of fluid in the measurement heat-exchanging tube bundle of heat-exchanging tube bundle import, going out fluid volume flow V in heat-exchanging tube bundle by measuring numerical computations
l;
2) temperature difference and flow by calculating the fluid of heat-exchanging tube bundle can obtain the caloric receptivity of fluid, namely total heat exchange amount Q, Q=ρ V
l* C
p* (T
l2-T
l1), wherein, ρ is the density of fluid in heat-exchanging tube bundle, C
pfor the specific heat at constant pressure of fluid in heat-exchanging tube bundle;
3) then according to total heat exchange amount Q=K*A* △ T
m, wherein △ T
mthe logarithmic mean temperature difference (LMTD) of heat transfer process, △ T
m=((T
w1-T
l2)-(T
w2-T
l1))/ln ((T
w1-T
l2)/(T
w2-T
l1)), K is the total heat transfer coefficient of heat exchanger, and A is heat exchange area, takes heat pipe external diameter to calculate, and draws total coefficient of heat transfer K;
4) by heat convection formula, Q=h
w* A
w* (T
w1-T
w2)=h
l* A
l* (T
l2-T
l1) calculate the surface coefficient of heat transfer h of heat exchanger tube outer wall and inwall
wand h
l, wherein A
w, A
lthe area of heat exchanger tube outer wall and inwall respectively;
5) central controller is according to the K calculated, h
wand h
l,the dust stratification thermal conduction resistance R outside pipe is gone out according to heat transfer formulae discovery
do.。
In above-mentioned formula, K is total heat transfer coefficient; h
wfor managing the right surface coefficient of heat transfer of outer tail gas; h
lfor the surface coefficient of heat transfer of heat exchanger tube inner fluid; d
ofor heat exchanger tube overall diameter; d
ifor heat exchanger tube interior diameter; d
mfor heat exchanger tube average diameter, equal (d
o+ d
i)/2; δ is the wall thickness of heat exchanger tube, equals (d
o-d
i)/2; λ is the thermal conductivity factor of heat exchanger tube; R
dofor the dust stratification thermal conduction resistance of heat exchanger tube.
When blowing ash, central controller can transfer the last ruuning situation, draws the dust stratification thermal conduction resistance of current heat-exchanging tube bundle, automatically chooses suitable blower fan frequency according to the size of dust stratification thermal conduction resistance.
Fluid in described heat-exchanging tube bundle is preferably water.
Preferably, when dust stratification thermal conduction resistance is greater than predetermined value, during lower than the first numerical value, blower fan runs with first frequency, when dust stratification thermal conduction resistance is greater than the first numerical value lower than second value, blower fan runs with the second frequency being greater than first frequency, when dust stratification thermal conduction resistance is greater than second value lower than third value, blower fan runs with the 3rd frequency being greater than second frequency, when dust stratification thermal conduction resistance is greater than third value lower than the 4th numerical value, blower fan runs with the 4th frequency being greater than the 3rd frequency, when dust stratification thermal conduction resistance is greater than the 5th numerical value, blower fan runs with the 5th frequency being greater than the 4th frequency.
Preferably, can arrange an information, when the dust stratification thermal conduction resistance of heat exchanger tube is greater than certain numerical value, give a warning information automatically, reminds and need to carry out scale removal.
Certainly because the composition of tail gas and speed relatively stable, simultaneously the flow velocity of heat exchanging fluid is relative with inlet temperature also stablizes, and relatively simple mode now can be taked to detect.Which is exactly determine whether heat exchange worsens by the temperature of the heat exchanging fluid of detection outlet.
If exit fluid temperature is lower than the first temperature, then can judge that heat exchange worsens, now need to carry out deashing, now blower fan runs according to the first power; If exit fluid temperature is lower than second temperature lower than the first temperature, then blower fan runs according to the second power being greater than the first power; If exit fluid temperature is lower than three temperature lower than the second temperature, then blower fan runs according to the 3rd power being greater than the second power; If exit fluid temperature is lower than four temperature lower than the 3rd temperature, then blower fan runs according to the 4th power being greater than the 3rd power.
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 (6)
1. one kind has the waste heat utilization heat exchanger that multiple directions blow ash, described heat exchanger comprises heat-exchanging tube bundle, inlet exhaust gas, offgas outlet and housing, described heat-exchanging tube bundle is arranged in the housing, it is characterized in that: described heat-exchanging tube bundle assumes diamond in shape structural arrangement, housing has the diamond structure matched with heat-exchanging tube bundle, inlet exhaust gas is arranged on the first angular position place of the diamond structure of housing, and offgas outlet is arranged on the second angular position place of the diamond structure of housing; Two limits of the diamond structure of the housing be connected with inlet exhaust gas are arranged respectively the blue interface of 1# ash blowing method and the blue interface of 2# ash blowing method, two limits of the diamond structure of the housing be connected with offgas outlet are arranged respectively the blue interface of 3# ash blowing method and the blue interface of 4# ash blowing method, wherein the blue interface of 1# ash blowing method is two relative limits with the limit of the housing diamond structure at the blue interface place of 3# ash blowing method, and the blue interface of 2# ash blowing method is two relative limits with the limit of the housing diamond structure at the blue interface place of 4# ash blowing method; Wherein the blue interface of 1# ash blowing method is positioned at the bottom on limit, place, the blue interface of 2# ash blowing method is positioned at the top on limit, place, the blue interface of 3# ash blowing method is positioned at the top on limit, place, the blue interface of 4# ash blowing method is positioned at the bottom on limit, place, thus making the distance of the blue interface distance inlet exhaust gas of 1# ash blowing method be greater than 2# ash blowing method blue interface distance inlet exhaust gas distance, the distance of the blue interface distance offgas outlet of 3# ash blowing method is greater than 4# ash blowing method blue interface distance offgas outlet distance;
Described heat exchanger also comprises the blue interface of 5# ash blowing method, the blue interface of 6# ash blowing method, the blue interface of 7# ash blowing method, the blue interface of 8# ash blowing method, wherein the blue interface of 5# ash blowing method and the blue interface of 1# ash blowing method are positioned at one side and are positioned at the top on limit, place, the blue interface of 6# ash blowing method and the blue interface of 2# ash blowing method are positioned at one side and the bottom on limit, place, the blue interface of 7# ash blowing method and the blue interface of 3# ash blowing method are positioned at one side and are positioned at the bottom on limit, place, the blue interface of 8# ash blowing method and the blue interface of 4# ash blowing method are positioned at one side and are positioned at the top on limit, place, thus make the distance of the blue interface distance inlet exhaust gas of 5# ash blowing method be less than 6# ash blowing method blue interface distance inlet exhaust gas distance, the distance of the blue interface distance offgas outlet of 7# ash blowing method is less than 8# ash blowing method blue interface distance offgas outlet distance.
2. heat exchanger as claimed in claim 1, it is characterized in that: the tube bank on the summit of the first angle of heat-exchanging tube bundle diamond structure is arranged on the position of the bottom of inlet exhaust gas and relative with inlet exhaust gas, the tube bank on the summit of the second angle of heat-exchanging tube bundle diamond structure is arranged on the top of offgas outlet and relative with offgas outlet, first angle of wherein said heat-exchanging tube bundle diamond structure and the second angle are the diagonal angles of rhombus, cement rotary kiln tail gas enters from inlet exhaust gas, first through the tube bank on the summit at the first angle place of heat-exchanging tube bundle diamond structure, then transversal flow heat-exchanging tube bundle, again through the tube bank on the summit at the second angle place of heat-exchanging tube bundle diamond structure, finally discharge from offgas outlet.
3. heat exchanger as claimed in claim 1, it is characterized in that: the distance between described heat-exchanging tube bundle is L, the external diameter of heat-exchanging tube bundle is D, and the first angle of heat-exchanging tube bundle diamond structure is A, and the relation of described L and D meets formula:
3.7 × D>L>2.4 × D, wherein 20mm<D<50mm;
The relation of A and L, D meets following formula:
Sin(A/2)＝b×(L/D)
c，70°>A>110°，
Wherein b, c are parameter, and b is between 1.65-1.8, and c is between-0.8 to-0.9.
4. heat exchanger as claimed in claim 1, is characterized in that: the height of projection on same heat-exchanging tube bundle is different along with the difference of the distance of distance inlet exhaust gas, to ensure same heat-exchanging tube bundle evenly absorbs heat.
5. heat exchanger as claimed in claim 1, is characterized in that: the outer wall of heat-exchanging tube bundle arranges projection, and along with the increase of the distance of distance inlet exhaust gas, the height of heat-exchanging tube bundle projection is more and more higher.
6. heat exchanger as claimed in claim 5, is characterized in that: the maximum height of projection on heat-exchanging tube bundle outer wall be the 1.5-1.6 of minimum height of projection doubly.
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|---|---|---|---|
| CN201410412142.9A CN104197752B (en) | 2013-12-09 | 2013-12-09 | A kind of have the waste heat utilization heat exchanger that multiple directions blow ash |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310664039.9A CN103615919B (en) | 2013-12-09 | 2013-12-09 | Waste-heat utilization heat exchanger with constant output fluid temperature |
| CN201410412142.9A CN104197752B (en) | 2013-12-09 | 2013-12-09 | A kind of have the waste heat utilization heat exchanger that multiple directions blow ash |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310664039.9A Division CN103615919B (en) | 2013-12-09 | 2013-12-09 | Waste-heat utilization heat exchanger with constant output fluid temperature |
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| Publication Number | Publication Date |
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| CN104197752A CN104197752A (en) | 2014-12-10 |
| CN104197752B true CN104197752B (en) | 2015-08-19 |
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| CN201410412142.9A Expired - Fee Related CN104197752B (en) | 2013-12-09 | 2013-12-09 | A kind of have the waste heat utilization heat exchanger that multiple directions blow ash |
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| CN105546817A (en) * | 2014-10-31 | 2016-05-04 | 青岛经济技术开发区海尔热水器有限公司 | Heat exchanger and water heater |
| CN105222617B (en) * | 2015-09-28 | 2017-09-22 | 清华大学 | A kind of low flow resistance heat exchanger for natural cycle system |
| CN112406450A (en) * | 2019-08-23 | 2021-02-26 | 上海汽车集团股份有限公司 | Heat recovery system of new energy vehicle and control method thereof |
| CN111336844B (en) * | 2019-12-25 | 2021-01-29 | 山东大学 | Circular structure plate heat exchanger with adjacent temperature comparison control flow |
| CN111895817B (en) * | 2020-07-21 | 2021-08-31 | 包头轻工职业技术学院 | Horizontal heat exchanger |
| CN113390284B (en) * | 2021-05-10 | 2023-04-18 | 西安交通大学 | Household fuel cell waste heat utilization system and method |
| CN116046659B (en) * | 2023-01-28 | 2024-10-22 | 山东蓝想环境科技股份有限公司 | Intelligent monitoring heat exchanger and state monitoring method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100487351C (en) * | 2001-09-28 | 2009-05-13 | 株式会社日本触媒 | Shell-and-tube heat exchanger and method for producing acrylic acid using the same |
| CN102226653A (en) * | 2011-04-19 | 2011-10-26 | 山东理工大学 | Solid thermal carrier heat exchanger |
| CN203116325U (en) * | 2013-03-06 | 2013-08-07 | 南阳师范学院 | Intelligent control solar water heater based on multiple sensors |
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2013
- 2013-12-09 CN CN201310664039.9A patent/CN103615919B/en not_active Expired - Fee Related
- 2013-12-09 CN CN201410412142.9A patent/CN104197752B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100487351C (en) * | 2001-09-28 | 2009-05-13 | 株式会社日本触媒 | Shell-and-tube heat exchanger and method for producing acrylic acid using the same |
| CN102226653A (en) * | 2011-04-19 | 2011-10-26 | 山东理工大学 | Solid thermal carrier heat exchanger |
| CN203116325U (en) * | 2013-03-06 | 2013-08-07 | 南阳师范学院 | Intelligent control solar water heater based on multiple sensors |
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|---|---|
| CN104197752A (en) | 2014-12-10 |
| CN103615919B (en) | 2014-09-10 |
| CN103615919A (en) | 2014-03-05 |
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