CN1108380A - An apparatus for precalcining raw cement with a fuel gasification device - Google Patents
An apparatus for precalcining raw cement with a fuel gasification device Download PDFInfo
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- CN1108380A CN1108380A CN 94105558 CN94105558A CN1108380A CN 1108380 A CN1108380 A CN 1108380A CN 94105558 CN94105558 CN 94105558 CN 94105558 A CN94105558 A CN 94105558A CN 1108380 A CN1108380 A CN 1108380A
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- 239000000446 fuel Substances 0.000 title claims abstract description 184
- 239000004568 cement Substances 0.000 title claims abstract description 15
- 238000002309 gasification Methods 0.000 title claims description 29
- 239000002994 raw material Substances 0.000 claims abstract description 88
- 238000002485 combustion reaction Methods 0.000 claims description 115
- 239000007789 gas Substances 0.000 claims description 35
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 23
- 238000001354 calcination Methods 0.000 claims description 23
- 239000001301 oxygen Substances 0.000 claims description 23
- 229910052760 oxygen Inorganic materials 0.000 claims description 23
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 15
- 239000012530 fluid Substances 0.000 claims description 7
- 239000002002 slurry Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 4
- 238000009434 installation Methods 0.000 abstract description 15
- 238000010438 heat treatment Methods 0.000 abstract description 8
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 230000008016 vaporization Effects 0.000 abstract 1
- 239000002245 particle Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 14
- 238000001816 cooling Methods 0.000 description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 12
- 230000008569 process Effects 0.000 description 10
- 238000010586 diagram Methods 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 230000008901 benefit Effects 0.000 description 7
- 238000000197 pyrolysis Methods 0.000 description 6
- 206010020843 Hyperthermia Diseases 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000008246 gaseous mixture Substances 0.000 description 4
- 230000036031 hyperthermia Effects 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 238000007634 remodeling Methods 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- 238000009826 distribution Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 238000005242 forging Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 239000008240 homogeneous mixture Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000003380 propellant Substances 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
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- Curing Cements, Concrete, And Artificial Stone (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention discloses a raw cement precalcination device which makes a precalcination furnace connect between a rotary kiln and a suspension-type raw material pre-heater and is equipped with an independent heating source. The precalcination device comprises an upper part and a lower part, and is provided with one set or a few sets of fuel vaporizing equipments, which deliver the fuel into the lower part. The upper part is provided with an outlet pipeline so as to discharge the calcined raw material into the lowest cyclone separator; the upper part is connected with the lower part, the upper part is arranged with a combustion-supporting air input duct, and the lower part is communicated with an exhaust duct returning the stack furnace. The adoption of the structure is capable of reducing size of the precalcination furnace, improving precalcination efficiency, decreasing installation costs of the precalcination furnace and the pre-heater and is capable of ensuring stable operation of the device.
Description
The present invention relates to the device of the cement slurry of a kind of pre-burning such as fine and so on, this device comprises that one is gone up separating part and a following separating part, comprises a fuel gasification equipment in addition.
Usually, the device of precalcining cement slurry comprises a precalcining stove, and the independent thermal source of heating raw material is housed in the stove, and this thermal source places between rotary furnace (or kiln) and the suspended preheater.Because fuel and air evenly mix and do not form flame, the time of fuel combustion is lacked (about 1/3 second) very much in the precalcining stove.
Above-mentioned fuel combustion process comprises the heating pellet, discharges volatile component, the combustion reaction of remaining carbon in the combustion reaction of above-mentioned volatile component and the pellet under burning condition.Specifically, said process carries out at folded mutually each other section in succession successively.
Principal element to the combustion process that influences fuel at each section is commented as follows: the bringing-up section of fuel particle is influenced by the main flow temperature of particle and the thermogravimetric amount of particle; Pyrolysis section is influenced by fuel type, particle temperature and particle heating process, and oxidation panel is subjected to the influence of the type (for example volatile matter or charcoal) of oxygen concentration around the fuel and propellant composition.
In above-mentioned fuel process, the burning time in each section in preheating and the volatilization process is longer, and the volatile component combustion process is very short, and the combustion process of residue carbon is also long.
Therefore, before fuel combustion, when fuel being carried out preheating, discharge volatile component and make carbon pyrolysis (hereinafter being referred to as " preliminary treatment of fuel ") in the particle make fuel that fuel gasification will gasify then spray in the combustion air, can realize completing combustion in a short period of time.Yet,, can not form the hot gas district because the caloric value of vaporising fuel reduces.
Therefore, make its gasification when the fuel that has gasified is burnt in the oxygen-enriched combustion-supporting air, require burning rapidly, and in calcining furnace, can obtain high temperature and do not have gas zone by pre-heating fuel in the precalcining stove.
For pre-heating fuel, need a large amount of heat energy.In order to make carbon pyrolysis in the fuel particle, adopt a kind of CO
2The dividing potential drop height and O
2The gas that forces down of branch be favourable.Combustion air through separating the combustion air input channel and flow into without rotary kiln in the situation of precalcining stove, flow into the delivery temperature height (for example 900～1100 ℃) of precalcining stove and its CO from rotary kiln
2Dividing potential drop very high (for example about 20%～30%).In addition, O in the exhaust
2Dividing potential drop very low (being lower than 5%).
The gas of discharging from rotary kiln has needed enough heat energy of preliminary treatment fuel and the needed gas componant of pyrolytic reaction.Therefore, use the gas preliminary treatment fuel of discharging, can obtain vaporising fuel effectively by the utmost point from rotary kiln.
When with the exhaust of rotary kiln fuel being carried out preliminary treatment, being used for the required capacity of preliminary treatment fuel should be minimum.In the pyrolytic reaction of the carbon in fuel particle, the CO in the exhaust of rotary kiln
2The dividing potential drop height is very favourable, but unfavorable to the burning of vaporising fuel.With the required minimum rotary kiln exhaust of preliminary treatment fuel fuel is being carried out the pretreated fuel gasification that makes simultaneously, the fuel that has gasified is burnt the oxygen-enriched combustion-supporting air that flows into from clinker cooler, thereby shortened burning time, so can obtain higher efficiency of combustion.
| Temperature ℃ | Gas component (%) | |||
| O 2 | CO 2 | N 2 | ||
| The rotary kiln exhaust | 900－1100 | ＜5 | 20－30 | 65－80 |
| Combustion air | 700－1100 | 21 | － | 79 |
Usually, in the device of preliminary treatment fuel, adopted following three process.The first procedure fixed bed, second road, 2 preface fluid beds, last, three process is with carrying suspension bed.
Above-mentioned first and second procedures are provided with an air distribution plate on the height that is lower than their beds separately, and three process is not provided with above-mentioned air distribution plate.The gas temperature of discharging from rotary kiln very high (about 900-1100 ℃) contains a large amount of dusts and coagulation in the exhaust.For above-mentioned reasons, what three process used is the suspension bed that carries of not adorning the air matching board, and this preliminary treatment for fuel is optimal.
In addition, even above-mentionedly carry the suspension bed flow process to also have an advantage be spray liquid composition owing to temperature raises when preliminary treatment fuel, in this flow process, fuel is carried out preliminary treatment and skin also can not occur expecting.
According to introducing the rotary kiln exhaust and from clinker cooler, introduce the method for combustion air and the combustion method of fuel, the traditional precalcining device that is used to produce cement can be divided into five classes.The structure and the characteristics of all kinds of precalcining stoves are as follows.In the following description, identical parts are represented with same label.
First kind precalcining stove shape is the simplest, and as shown in figure 10, it is used as the rotary kiln discharge duct 28 in traditional precalcining stove as a precalcining stove 23.
That is to say that the combustion air of supplying with precalcining stoves 23 from clinker cooler 22 flows through the rotary kiln 21 that not have to install the air input channel that separates from the top, mix with the rotary kiln exhaust again, afterwards, gaseous mixture is sent into by rotary kiln discharge duct 28.Fuel is sprayed into and makes it burning (U.S. Pat 3986818 and 4050883) in the gaseous mixture of rotary kiln exhaust and combustion air by burner 26.
Because this class precalcining stove, need not give calcining furnace and pays mounting cost in addition as a precalcining stove 23 with rotary kiln discharge duct 28 in order to install.But, introduce in the gaseous mixture add the low combustion air of rotary kiln exhaust and oxygen concentration and burn owing to will import fuel in the precalcining stove, make the efficiency of combustion reduction.
Therefore, in precalcining heater exhaust outlet conduit 29, have a large amount of unburned carbon, and unburned carbon contained combustion reaction is carried out in pre-heater.Consequently, owing to thermal loss is increased from the delivery temperature rising of pre-heater, and the installation and operation of air exhauster 32 is produced harmful effect, this is the shortcoming of this type of precalcining stove.
The second class precalcining furnace structure is simple, and the pressure loss is little, and easy and simple to handle, therefore, in traditional precalcining stove, common this class precalcining stove (as shown in figure 11) of selecting for use of people.The structure of this type of calcining furnace is to use rotary kiln discharge duct 28 to communicate with the bottom of calcining furnace 23, and temperature is that the rotary kiln exhaust of 900 ℃-1100 ℃ heat forms one deck jetted layers in the bottom of precalcining stove 23.The combustion air input channel 25 that transports from the combustion air of the oxygen-enriched combustion-supporting air of clinker cooler 22 links to each other with the sidewall of precalcining stove 23, combustion air from the center or tangential direction be admitted in the stove.Most of fuel is sprayed into and in the oxygen-enriched combustion-supporting air, burn by a burner 26a, make part of fuel spray into and in the rotary kiln exhaust, burn through a denitration burner 26b, in this burner, removed the nitrogen oxide (Japanese patent application publication No. 134028/1978 in the rotary kiln exhaust, 90228/1979, Japanese patent application publication No. 32176/1978 and South Korea patent publication No. 1568/1987).
For fuel is sprayed in the precalcining stove equably, a large amount of Cryogenic air that this class precalcining stove uses (send into the precalcining stove whole combustion airs 14～20%) be that 26b sends into from burner 26a.Therefore, can reduce the hot combustion-supporting air quantity of introducing from clinker cooler, and introduce Cryogenic air from burner, the consequence of thereupon bringing is that heat consumption increases.
In addition, the burning that sprays into through burner flows into the high flow rate of 10～40m/s together with mist, and when fuel flowed in the gaseous mixture of combustion air and rotary kiln exhaust, fuel burnt in the oxygen-enriched combustion-supporting air.Therefore, the shortcoming of this class calcining furnace is that the configuration of device is increased, and the precalcining stove increases, and causes the mounting cost costliness, and the calcining ability of unit volume reduces.
As shown in figure 12, the 3rd class calcining furnace can use low grade for fuel by means of the calcination efficiency that improves the second class calcining furnace.
Fuel is sent into through burner 26 together with low temperature combustion air (accounting for the 4-5% of total combustion air of input precalcining stove), the fuel that provides through burner 26 sprays into the center of swinging precalcining stove 23c together with hot-air (700-1100 ℃), so that combustion air input channel 25 is left in burning partly.Some remaining combustion airs tangentially flow from the sidewall of circulation precalcining stove 23c, and the raw material that flow out from raw material inlet duct 27 separate by wall surface.In the center of circulation precalcining stove 23c has the combustion air of low-density raw material, form thermal-flame, therefore can aggravate the burning of fuel.Raw material (US 3,834,860) around the photothermal heat that above-mentioned circulation precalcining stove produces thermal-flame is supplied with.
The advantage of this class precalcining stove is to shorten the burning time of material, and fuel burns in the precalcining stove when only forming flame by high-temperature oxygen-enriched combustion air, so can improve efficiency of combustion, also can use low grade for fuel.But, when input fuel,, heat consumption is increased owing to use Cryogenic air, this is the weak point of this class precalcining stove.In addition, because the discharge position of this class circulation precalcining stove 23c is located at the bottom, air-flow is circulation down, thereby the pressure loss is increased.
As shown in figure 13, in the 4th class precalcining stove, fuel only burns with the oxygen-enriched combustion-supporting air of the heat of sending into by combustion air input channel 25 from clinker cooler 22, and without the rotary kiln exhaust, therefore, this class precalcining stove and accessory has the pre-heater that separates separately that utilizes the precalcining heater exhaust.
The combustion air input channel 25 that hot oxygen-enriched combustion-supporting air flows through is communicated with the bottom of precalcining stove 23, and combustion air is sprayed by above-mentioned pipeline.Fuel is sprayed into (US-4,045,162) in the combustion air through burner 26 together with low temperature combustion air (accounting for the 4-5% of total combustion air of sending into the precalcining stove).
Because fuel burns in the oxygen-enriched combustion-supporting air of heat, so the advantage of this class precalcining stove is the efficiency of combustion height.But when input fuel, heat consumption increases.In addition, fuel is that the high flow rate gas of 10～40m/s sprays into together through burner with flow velocity, and in order to realize completing combustion, the height of precalcining stove need increase.Therefore, the mounting cost of precalcining stove increases, and the calcining ability of unit volume reduces.
When being a kind of fuel combustion, the 5th class precalcining stove makes fuel and the mixed uniformly device of raw material without burner with fluid bed 23d, as shown in figure 14, by the combustion air input channel 25 that communicates with fluid bed 23d top, burning is occurred in from the combustion air that clinker cooler 22 flows out.
The raw material fluidisation that provides by the fuel of burner 26 inputs and raw material inlet duct 30a is provided the Cryogenic air of sending from the blower fan that is used for fluidisation 33 that is in precalcining stove 23 bottoms when Cryogenic air flows through the fluidisation plate, forms homogeneous mixture then.Then, make fuel combustion (Japanese patent application publication No. 45020/1991) by means of hot oxygen-enriched combustion-supporting air from combustion air input channel 25 outputs of clinker cooler 22 through communicating with fluid bed 23d top.
The advantage of this class precalcining stove is: utilize fluid bed 23d that fuel and raw material are evenly mixed, therefore, being evenly distributed of temperature in the precalcining stove and raw material.
Consequently the precalcining stove is stable, can not form localized hyperthermia.
But, heat consumption is increased because this class precalcining stove forms fluid bed 23d with a large amount of cooling air (account for total combustion air of sending into this precalcining stove 10～15%).
In addition, (flow velocity is 4～20m/s) the mobile and burning of combustion air, and in order to realize completing combustion, the height of precalcining stove need increase because fuel is with flowing fast.Therefore, the mounting cost height of this class precalcining stove, the calcining ability of unit volume reduces.
As mentioned above, for efficiency of combustion and the calcination efficiency that improves the precalcining stove, developed traditional precalcining stove with various structures.But, when importing fuel and making fuel combustion, owing to all use the cooling air, the cooling air volume that the hot combustion-supporting air quantity of introducing from clinker cooler is reduced to and introduces as many, this point is all open questions of all rotary kiln, and heat consumption is increased.
In addition, because the fuel in the input precalcining stove is fully burnt in this stove, fuel should stay for some time in the precalcining stove, so that completing combustion.For this reason, should shorten burning time.And while the precalcining stove should be higher.In order to make fuel completing combustion in the precalcining stove, traditional precalcining stove is often all higher.The result makes the installation site of preheater become higher, and the size of precalcining stove also increases, thereby has increased mounting cost and the calcining ability of unit volume is reduced.
The present invention has carried out deep discussion to the problem of the above-mentioned shortcoming that how to overcome traditional precalcining stove, and the result has found following corrective measure.First, before spraying into fuel in the combustion air, fuel is carried out preheating, makes volatile component discharge and make carbon pyrolysis in the fuel particle to shorten in the precalcining stove fuel completing combustion required burning time by means of apparatus for gasifying fuel, the size of precalcining stove is reduced, like this, just can improve the calcining ability of unit volume.The second, in the time of will forging material input and burning, make the cooling air volume minimum of importing, like this, just can reduce heat consumption.
Below in conjunction with accompanying drawing some embodiments of the present invention are described, wherein:
Fig. 1 is the schematic diagram of first embodiment that the production cement equipment of apparatus for gasifying fuel of the present invention is housed;
Fig. 2 is the schematic diagram of second embodiment that the production cement equipment of apparatus for gasifying fuel of the present invention is housed;
Fig. 3 is the enlarged drawing of the precalcining device among Fig. 1;
Fig. 4 is the profile that I-the I line is cut open in Fig. 3 of some embodiments that show combustion air input channel and apparatus for gasifying fuel;
Fig. 5 is and the similar schematic diagram of Fig. 3 that it shows another embodiment of precalcining device;
Fig. 6 is the profile that II-the II line is cut open in Fig. 5 of some embodiments that show combustion air input channel and apparatus for gasifying fuel;
Fig. 7 is the schematic diagram of some embodiment of apparatus for gasifying fuel of the present invention;
Fig. 8 is the enlarged drawing of another embodiment of precalcining device shown in Figure 2;
Fig. 9 is the profile that III-the III line is cut open in Fig. 8 of some embodiments that show combustion air input channel, rotary type discharge duct and gasification fuel inlet pipeline;
Figure 10 to Figure 14 is the schematic diagram of the cement equipment of existing production.
According to the present invention, in the equipment of this class precalcining cement slurry, the precalcining stove is connected between the floated preheater of rotary kiln and preheated raw meal, an independently thermal source is housed in the calcining furnace, it is characterized in that above-mentioned precalcining stove comprises a top 3a and a bottom that links to each other with top who takes mouthful pipeline out of, above-mentioned top outlet conduit is used for the raw material after the calcining are entered minimum cyclone separator, and react so that finish precalcining with being used for the bottom that raw material are sent into fuel linked to each other on top; The bottom is provided with one or a few input channel, so as will from the combustion air of clinker cooler from then on the sidewall of bottom send into, this bottom communicates with the rotary kiln discharge duct, so that the thermal exhaust in the rotary kiln is imported; Above-mentioned air duct is provided with one or more raw material inlet duct; Described precombustion stove also has one or more apparatus for gasifying fuel, fuel is sent into precalcining stove bottom.
On the other hand, according to the present invention, in the equipment of this class precalcining cement slurry, the precalcining stove is contained between the floated preheater of rotary kiln and preheating particulate raw material, be provided with an independently thermal source in the precalcining stove, it is characterized in that above-mentioned precalcining stove comprises a top and a bottom, top is provided with an outlet conduit that the raw material after the precalcining is entered minimum cyclone separator, and top links to each other with the bottom, so that finish the precalcining reaction of raw material and fuel; The bottom links to each other with top, the bottom is provided with an input channel 5, be used for and import with tangential direction being lower than on the height of bottom from the combustion air of clinker cooler, also be provided with the inlet duct that the raw material of the preheating that an input channel that the thermal exhaust of part rotary kiln and the fuel that gasified are introduced and one or more will flow out from minimum cyclone separator are sent into, to finish the precalcining reaction of raw material.This precalcining stove also comprises an apparatus for gasifying fuel, and this device has a fuel to carry inlet duct in contiguous rotary kiln air exit cover part.
Describe the present invention in detail below in conjunction with accompanying drawing.
Referring to Fig. 1, there is shown first embodiment that produces the equipment of cement with apparatus for gasifying fuel of the present invention.
In Fig. 1, at first, the subparticle raw material of having pulverized with certain size are flowed through be positioned at a raw material inlet duct 11 on the floated preheater, and by the gas preheating of discharging from the cyclone separator C4 that is in above-mentioned inlet duct 11 tops.So, raw material in proper order the several cyclone separators by serial connection (as C5 → C4 → C3 → C2) be preheated.
The raw material that are collected among the cyclone separator C2 of the second level are infeeded in the precalcining stove 3 through raw material inlet duct 7, so that precalcining in this stove.Raw material after the precalcining are discharged through precalcining heater exhaust outlet conduit 9 together with gas.Will be in low cyclone separator C1 the raw material of opening separated from the gas (precalcining rate: 80-85%) send in the rotary kiln 1, so that in this kiln, finish the grog reaction by raw material inlet duct 10.
To send into for example a kind of chiasma type heat exchanger of known clinker cooler 2(from the hot grog that rotary kiln 1 is discharged), by the cooling air grog is cooled off rapidly, it is discharged, to realize the calcining of raw material from cooler 2.
Fuel is imported in the combustion air after one or more is arranged on apparatus for gasifying fuel preliminary treatment in the precalcining stove 3 and burns, and as the thermal source of precalcining stove 3.
Above-mentioned fuel gasification equipment has the rotary kiln exhaust input channel 8b that is separately positioned on its bottom and at the fuel inlet pipeline 15 of its sidewall.Therefore, do not cooling off under the conditions of air, being suspended in the temperature of being discharged by outlet 8b in the fuel pretreating zone 17 through the fuel of pipeline 15 input is that 900-1100 ℃ part is turned round in the 7 kiln thermal exhausts (be lower than the total exhaust of rotary kiln 40%), so that fuel is carried out preheating, discharges volatile component and makes the carbon in the fuel particle carry out pyrolytic reaction.
The fuel of gasification is sprayed into the oxygen-enriched combustion-supporting air of the combustion air input channel 5 that leads to precalcining stove 3 by gas vent pipeline 19 from gasification installation 14, make it burning in pipeline 5.Therefore, this device has efficiency of combustion that improves fuel and the advantage that precalcining stove size is dwindled.
In addition, during the fuel combustion of having gasified, owing to do not generate hot fuel, can not produce the impurity as material skin and so in the precalcining stove, therefore, this device can stable operation.
In order to form spouted bed in the bottom of precalcining stove 3, the bottom of the main flow part of rotary kiln exhaust (rotary kiln exhaust 60% or more) being introduced precalcining stove 3 by rotary kiln exhaust input channel 8a.Therefore, the time of staying of raw material is longer, thereby has quickened the precombustion of raw material.
Fig. 2 is the schematic diagram of second embodiment of being furnished with the cement manufacture plant of apparatus for gasifying fuel of the present invention.
As shown in Figure 2,, the main flow of rotary kiln exhaust is not partly sent in the precalcining stove because rotary kiln discharge duct 8a links to each other with minimum cyclone separator C1, and the temperature that will from clinker cooler 2, extract to be 700～1100 ℃ hot oxygen-enriched combustion-supporting air (for example contain O
221%) introduce in the precalcining stove 3 by combustion air input channel 5, so that the fuel combustion of being supplied with, and make the raw material precalcining.Therefore, this device is referred to as separate type equipment, be provided with in this equipment one with the separation of rotary kiln exhaust heating preheater independently.
At first, make subparticle raw material that having of having pulverized set size by laying respectively at two raw material inlet ducts 11 and 11 on two floated preheaters ' send into, then, by means of from the cyclone separator C4 that is installed in above-mentioned raw material inlet duct 11 and 11 ' lower position and C ' 4 with its preheating.Then, make the raw material of preheating flow through cyclone separator C5 and the C ' 5 that is arranged on inlet duct 11 and 11 ' upper position, therefore, raw material are spent each cyclone separator (as C5 → C4 → C3 → C2 and C ' 5 → C ' 4 → C ' 3 → C ' 2) time in sequential flow and are preheated.
Making the raw material that are collected at second level cyclone separator C2 and C ' 2 be introduced into rotary kiln exhaust input channel 8a by raw material inlet duct 7a and 7b, is that the thermal exhaust (rotary kiln exhaust 60% or more) of 900-1100 ℃ rotary kiln makes the precalcining of part raw material by means of temperature.Separate from the rotary kiln exhaust by the cyclone separator C1 that links to each other with the rotary kiln exhaust input channel 8a raw material after with precalcining.Then, above-mentioned raw material are sent in the precalcining stove 3 through raw material inlet duct 10a.
Enter that raw material in the precalcining stove 3 circulate and by precalcining, the exhaust with the precalcining stove is discharged among the cyclone separator C ' 1 through precalcining heater exhaust outlet conduit 9 together then in this stove.Cyclone separator C ' 1 separates the exhaust of above-mentioned raw material and precalcining stove, and the raw material after separating subsequently are admitted in the rotary kiln 1 through raw material inlet duct 10b.Next, in above-mentioned rotary kiln 1, finish the clinker maturing reaction of raw material.
The hot grog that flows out from rotary kiln 1 is by for example a kind of cross-flow heat exchanger of clinker cooler 2() in the cooling air cool off rapidly, be discharged from this clinker cooler 2 then, so that raw material are calcined.
The method that realizes heat supply in the precalcining stove that does not have setting apparatus for gasifying fuel 14 separately is as follows.
That is, making fuel send into and be suspended in temperature from rotary kiln 1 by the fuel inlet pipeline 15 that is equipped with rotary kiln discharge duct 8b under the situation of not cooling off air is (be lower than the total exhaust of rotary kiln 30%) in 900-1100 ℃ the hot rotary kiln exhaust.Then, make the fuel preheating, discharge volatile component and make carbon pyrolysis in the fuel particle, so that obtain vaporising fuel.Vaporized fuel is sprayed in the oxygen-enriched combustion-supporting air of precalcining stove 3, and it is burnt in combustion air.Do the efficiency of combustion that can improve fuel like this, and can reduce the size of precalcining stove 3.
In addition, owing to high temperature do not occur during the vaporising fuel burning, device can stable operation, and can not produce any material skin because of fuel combustion.Exhaust by means of rotary kiln can make the precalcining of part raw material, and then, the residue raw material by precalcining, therefore, can improve calcination efficiency in precalcining stove 3.
Fig. 3 is the enlarged drawing of the precalcining furnace apparatus 3 among Fig. 1.
According to the present invention, this calcining furnace 3 comprises a top 3a and a bottom, comprises a fuel gasification equipment 14 in addition.
Above-mentioned apparatus for gasifying fuel 14 has the rotary kiln discharge duct 8b that is separately positioned on its bottom and at the fuel inlet pipeline 15 of its sidewall.Therefore, being suspended in the temperature that is entered by pipeline 8b in the fuel preheating zone 17 through the fuel that pipeline 15 is sent under not cooling off conditions of air is in 900-1100 ℃ the part rotary kiln thermal exhaust (be lower than the total exhaust of rotary kiln 30%), so that fuel is carried out preheating, discharges volatile component and makes the carbon in the fuel particle carry out pyrolytic reaction.
In the fuel that gasification installation 14 has gasified is directly sprayed into oxygen-enriched combustion-supporting air among the bottom 3b that is in precalcining stove 3, or sprayed into by gas vent pipeline 19 and to be in, and by means of above-mentioned combustion air burning near in the oxygen-enriched combustion-supporting air in the combustion air input channel 5 of bottom 3b.
Therefore, the advantage of this class device is that efficiency of combustion is improved.Because the heat output of fuel that has gasified is low, can not form localized hyperthermia, so device can stable operation.
Precalcining stove bottom is the cyclonic separation type.The combustion air input channel 5 that links to each other with its sidewall is sent into this lower central with the oxygen-enriched combustion-supporting air with the flow velocity of 10-30m/s or is tangentially imported wherein.
Fuel is supplied with by the raw material inlet duct 7 that is loaded in the combustion air input channel 5 that links to each other with above-mentioned bottom 3b.
In order to quicken the precalcining reaction, utilize the coarse granule in the combustion-supporting air flow collection fuel, then, it is in 900-1100 ℃ the spouted bed of rotary furnace thermal exhaust that above-mentioned particle is sent into temperature, and above-mentioned thermal exhaust sprays into the rotary kiln exhaust input channel 8a that the flow velocity of 20-40m/s communicates from the bottom with precalcining stove bottom.Next make raw material after the precalcining be suspended in the top 3a of precalcining stove.
The raw material big particle that is difficult to precalcining can be by flowing through the part that formed by the rotary kiln exhaust manys once heating than subparticle, and therefore makes its precalcining rate can become even according to the grain diameter of raw material.Its result, the precalcining rate of whole raw material is improved.
Because the bottom width of top 3a is designed to littler than the width of bottom 3b, raw material mix in the bottom with the gas that rises from bottom 3b.Again the high flow rate of formed mixture with 10-30m/s sprayed among the 3a of top.By the way, because the top width broadening of top 3a, gas flow rate reduces, the gas in flowing through bottom 3b, and the gas flow rate that flows through top is 4-8m/s.Therefore, the circulation of raw material is reinforced, and helps the precalcining of raw material.
In addition, because that the core of top 3a is processed into is cylindrical, when being carried out precalcining, raw material can increase the time of staying of raw material.
As following described, in precalcining stove 3, undertaken among the minimum cyclone separator C1 by precalcining heater exhaust outlet conduit 9 together with the precalcining heater exhaust through the raw material (the precalcining rate is 85-95%) of precalcining.Then, in cyclone separator C1, raw material and above-mentioned gas are separated, so that raw material are infeeded in the rotary kiln 1 by raw material inlet duct 10.
Fig. 4 is the profile that I-the I line is cut open in Fig. 3 of some embodiments that show combustion air input channel and apparatus for gasifying fuel.
Referring to the structure shown in Fig. 4 (a),, sprayed into the combustion air input channel 5 of close bottom 3b by the fuel of gasification installation 14 gasifications because combustion air tangentially flows into bottom 3b.Therefore, the fuel that has gasified can be in the airborne burning of oxygen-enriched combustion-supporting, and burning is violent.
In Fig. 4 (b), the fuel that has gasified is sprayed in the circulation of the combustion air among the 3b of bottom.
In Fig. 4 (c), help air to flow into bottom 3b along center position, the fuel that has gasified is sprayed near in the combustion air input channel 5 of bottom 3b.
Fig. 5 is and the similar schematic diagram of Fig. 3 another embodiment of its reflection precalcining device.
According to structure shown in Figure 5, the precalcining stove comprises a top 3a and a bottom 3b, also comprises two gasification installation 14a and 14b.
Referring to structure shown in Figure 5, owing to combustion air can be imported bottom 3b symmetrically, flowing of combustion air is stable.The fuel that has gasified is directly sprayed in the oxygen-enriched combustion-supporting air of bottom 3b, or it is sprayed among the combustion air input channel 5a and 5b adjacent with bottom 3b.
Therefore, the fuel that has gasified and the mixing of combustion air can reach the best, thereby have quickened combustion reaction.
Fig. 6 is the profile that II-the II line is cut open in Fig. 5 of some embodiments that show combustion air input channel and apparatus for gasifying fuel.
Shown in Fig. 6 (a), make combustion air tangentially from two side inflow bottoms (3b) of bottom, will spray near the combustion air input channel 5a and 5b of bottom 3b from the vaporising fuel of two gasification installation 14a and 14b outflow.Therefore, the fuel that has gasified can burn in the oxygen-enriched combusting air, and burning is violent.
In Fig. 6 (b), the gasification, and combustion that will flow out from two gasification installation 14a and 14b sprays in the circulation of the combustion air among the 3b of bottom.
In Fig. 6 (c), make the two side inflow bottom 3bs of combustion air, and will spray near the air input channel 5a and 5b of bottom 3b from the fuel that has gasified of two gasification installation 14a and 14b outflow along center position from the bottom.
Fig. 7 is the schematic diagram of some embodiment of apparatus for gasifying fuel 14 of the present invention.
Shown in Fig. 7 (a), the bottom width of the equipment 14 that communicates with rotary kiln exhaust input channel 8b and 8c can be designed to narrow passage, so that the rotary kiln exhaust of high flow rate (for example about 20-40m/s) is sprayed into, thereby can prevent to be deposited in the bottom of device 14 not cooling off under the conditions of air fuel of supplying with said apparatus 14 by fuel inlet pipeline 15.
Owing to middle part (for example for cylindrical) width can be designed to the width greater than above-mentioned bottom, therefore, shorten the time of staying of fuel, and accelerated the pyrolytic reaction of fuel.
On the other hand, can be similar owing to be used for the width of the upper end that communicates with the gas discharge outlet pipeline of vaporising fuel to the bottom width, therefore can improve the flow velocity that is sprayed into the vaporising fuel in the combustion air, vaporising fuel and combustion air mix thereby can make.
Fig. 7 (b) shows the embodiment of a kind of remodeling of the present invention, and the width of gasification installation 14 is similar to the width of rotary kiln discharge gas pipeline 8b and 8c in this example.
Fig. 7 (c) shows the embodiment of another remodeling of the present invention, and in this example, in order to prolong the time of staying of fuel, the width of gasification installation is widened from the lower to the upper gradually.
Fig. 8 is the enlarged drawing of another embodiment of precalcining equipment shown in Figure 2.This precalcining stove has an independent preheater, and this stove comprises top 3a and bottom 3b, also comprises an apparatus for gasifying fuel 14.
By after the preheater preheating and be collected in raw material among second level cyclonic separation C2 and the C ' 2 by raw material inlet tube 7,7a and 7b are imported into rotary kiln exhaust input channel 8a, are that the thermal exhaust (rotary kiln exhaust 60% or more) of 900-1100 ℃ rotary kiln makes the precalcining of part raw material by temperature.
Simultaneously, the raw material that are collected among the minimum cyclone separator C1 that communicates with rotary kiln exhaust input channel 8b are passed through raw material inlet duct 10a, " a sends into bottom 3b to 10 ' a and 10.
At this moment, preferably make the raw material that are provided along the sidewall of bottom 3b towards dirty, preventing forming localized hyperthermia when the fuel combustion of having gasified, but also can reduce the radiation loss of precalcining furnace wall.The inclination angle of bottom 3b is preferably 45 °-75 °.
The raw material that are admitted to precalcining stove 3 form circulation below the 3b of bottom, be that the rising combustion air of 30-40m/s makes raw material evenly distribute with respect to the wall of bottom 3b by means of flow velocity.Simultaneously, utilize the combustion air of flow velocity, make raw material circulation and precalcining, gradually it is moved on to top 3a then for the rising of 10-20m/s.
Raw material evenly mix the interface channel 16 of reduced with the combustion air that rises from bottom 3b, and the two-forty with 30-40m/s sprays among the 3a of top then.Make of the speed recirculation of the raw material of top 3a, to finish the precalcining reaction with 5-10m/s.
Having finished the raw material (the precalcining rate is 85-95%) of precalcining reaction discharges through calcining air exit pipeline 9 together with the precalcining heater exhaust, be collected in then among the minimum cyclone separator C ' 1 that communicates with pipeline 9, so that infeeded in the rotary kiln 1 by raw material inlet duct 10b.
In apparatus for gasifying fuel 14, owing to the fuel sent into by fuel inlet pipeline 15 suspended and be that 900-1100 ℃ rotary kiln thermal exhaust is carried by the temperature that flows through rotary kiln exhaust input channel 8b, can carry out preheating to fuel, discharge the pyrolysis of the carbon in volatile component and the realization fuel particle.
The vaporising fuel that generated by gasification installation 14 is sprayed towards the centre from the bottom of bottom 3b with the flow velocity of 30-40m/s, flow out the combustion air that flows into by combustion air input channel 5 than clinker cooler 2 and surround the above-mentioned fuel that has gasified, so that form circulation.Therefore, can improve the efficiency of combustion of fuel.
Fig. 9 is the profile that III-the III line is cut open in Fig. 8 of some embodiments that show combustion air input channel, rotary kiln exhaust input channel and gasification fuel inlet pipe.
In Fig. 9 (a), make from the fuel that has gasified of gasification installation 14 flow velocity and spray towards the centre, and surrounded by the combustion air that is tangentially entered from clinker cooler 2 from the bottom of bottom 3b with 30-40m/s, like this, can improve efficiency of combustion.
Show the embodiment of of the present invention one our remodeling at Fig. 9 (b), in this example, the combustion air that tangentially flows into by means of the both sides from bottom 3b makes vaporising fuel burning.
As mentioned above, the precalcining stove that links to each other with gasification installation of the present invention can shorten burning time, and burning improves efficiency of combustion in the oxygen-enriched combustion-supporting air by fuel gasification is made it then, and in addition, the size of precalcining stove is also very little.
Preheater can be installed in lower position, and its advantage is to reduce the mounting cost of preheater and precalcining stove.
In addition, during burning, high temperature does not appear in the fuel that has gasified, in fuel combustion process, does not expect skin in the precalcining stove, so device can stably move.
Moreover in fuel supply process, owing to different cooling air use the fuel inlet pipeline to supply with fuel, cooling air volume can drop to minimum.Therefore, can be used to temperature from clinker cooler and be 700-1100 ℃ hot combustion air and replace the cooling air (4-20% of the total combustion air of precalcining stove) supplied with in traditional precalcining stove, the result can reduce heat consumption.
According to originally stating principle, use precalcining stove of the present invention to shorten burning time, improve efficiency of combustion, reduce the thermal source parts, eliminate the localized hyperthermia district, and directly obtain consistent calcining rate according to particle.Therefore, precalcining stove of the present invention can be designed to minimum, and can improve the calcining rate of unit volume, reduces the mounting cost of precalcining stove and preheater, moves highly stable.
Claims (19)
1, a kind of the precalcining stove is connected cement slurry precalcining device between a rotary kiln and the floated raw material preheater, it is equipped with independent thermal source, it is characterized in that described precalcining stove comprises a top (3a) and a bottom (3b), top (3a) is provided with the outlet conduit (9) that the raw material after the precalcining is entered minimum cyclone separator (C1), top links to each other with the bottom that is used for raw material are sent into fuel, so that finish the precalcining reaction; Bottom (3b) links to each other with top (3a), it be provided with one or a few input channel (5,5a, 5b), so that will send into from the sidewall of described bottom from the combustion air of clinker cooler (2), described bottom also communicates with rotary kiln discharge duct (8a), to be used for the thermal exhaust that input is flowed out from rotary kiln (1), described air duct (5,5a, 5b) be provided with one or a few raw material inlet duct (7,7a, 7b); In addition, this calcining furnace also have one or more apparatus for gasifying fuel (14,14a, 14b) so that fuel is sent into described bottom (3b).
2, device as claimed in claim 1, the lower end that it is characterized in that described top (3a) is by interface channel (16,16a) upper end with described bottom (3b) links to each other, interface channel (16, it is 10-30m/s that structure 16a) can make the gas flow rate that flows through in it, and it is 4-8m/s that the structure on while top (3a) can make the gas flow rate that flows through in it.
3, device as claimed in claim 1, it is characterized in that described combustion air input channel (5,5a, structure 5b) can make combustion air flow into described bottom (3b) along center position or tangential direction with the flow velocity of 10-30m/s.
4, device as claimed in claim 1, it is 20-40m/s that the structure that it is characterized in that being positioned at the interface channel between described bottom (3b) and the rotary kiln discharge duct (8a) can make the flow velocity of the gas that flows through this passage, and the volume of described bottom (3b) can guarantee that the gas flow rate that flows through in it is 4-8m/s.
5, device as claimed in claim 1, it is characterized in that described apparatus for gasifying fuel (14,14a, 14b) comprise be used for from rotary kiln (1) extract the part thermal exhaust input channel (8b, 8c); Be used for fuel sent into described bottom (3b) so as with the thermal exhaust of rotary kiln make fuel gasification inlet duct (15,15a, 15b); Be used for the thermal exhaust fluid fuel gasification of rotary kiln inlet duct (15,15a, 15b); Be used for making the pretreating zone (17) of fuel gasification with the thermal exhaust of rotary kiln; The fuel that is used for having gasified spray into the oxygen-enriched combustion-supporting air of leading into bottom (3b) in case by means of described air make the vaporising fuel burning inlet duct (19,19a, 19b).
6, device as claimed in claim 5 is characterized in that (8b, 8c) gas flow of Yin Ruing is lower than 30% of rotary kiln gross exhaust gas by described input channel.
7, device as claimed in claim 5, (19,19a is 19c) with (5,5a 5b) communicates near the combustion air pipeline of described bottom (3b) to it is characterized in that described outlet conduit.
8, device as claimed in claim 5 is characterized in that (19,19a 19c) is exactly described bottom (3b) to described outlet conduit.
9, device as claimed in claim 5, it is characterized in that above-mentioned fuel pretreating zone (17,17a, structure 17b) can make the gas flow rate in it be higher than by input channel (8b, 8c) introduce its interior gas flow rate, or be higher than by outlet conduit (19,19a, the flow velocity of the vaporising fuel that 19b) sprays into.
10, device as claimed in claim 5, it is characterized in that described fuel pretreating zone (17,17a, structure 17b) can make the gas flow rate in it equal by input channel (8b, 8c) introduce its interior described gas flow rate, or equal by outlet conduit (19,19a, 19b) spray into change the flow velocity of fuel.
11, device as claimed in claim 5, it is characterized in that described apparatus for gasifying fuel (14,14a, structure 14b) can make at described fuel pretreating zone (17,17a, (8b, 8c) flow velocity of the gas of Yin Ruing reduced gradually by input channel when 17b) gas in flowed up.
12, a kind of the precombustion stove is connected cement slurry precalcining device between a rotary kiln and the floated subparticle raw material preheater, it is equipped with independently thermal source, it is characterized in that described precalcining stove comprises a top and a bottom, top (3a) is provided with an outlet conduit (9) that the raw material after the precalcining is entered minimum cyclonic separation (C1), this top links to each other with top (3a) with bottom (3b), to finish the precalcining reaction of raw material and fuel; Bottom (3b) links to each other with top (3a), it is provided with one and is used for from the combustion air of clinker cooler (2) input channel (5) with the tangential direction input on the height that is lower than bottom (3b), also be provided with a input channel (8b) with the thermal exhaust of part rotary kiln and the fuel input of having gasified, and the inlet duct (10a that sends into of the raw material of one or more preheating that will flow out from minimum cyclone separator (C1), 10 ' a, 10 " a), to finish the precalcining reaction of raw material; This precalcining stove also comprises an apparatus for gasifying fuel (14), and this device is provided with a fuel inlet pipeline (15) at contiguous rotary kiln air exit cover (4).
13, device as claimed in claim 12, the structure that it is characterized in that described input channel (8b) can make the exhaust of part rotary kiln and vaporising fuel the bottom of (3b) flows into along center position with the flow velocity of 30-40m/s from the bottom.
14, device as claimed in claim 12 is characterized in that described input channel (8b) is positioned at the core of combustion air input channel (5), causes rotary kiln exhaust of the fashionable encirclement part of combustion-supporting air flow and vaporising fuel.
15, device as claimed in claim 14, the structure that it is characterized in that described combustion air input channel (5) can make the combustion air along continuous straight runs enter the inside that is distributed to described bottom (3b) behind the bottom of described bottom (3b) with the flow velocity of 30-40m/s up.
16, device as claimed in claim 12 is characterized in that the structure of described bottom (3b) can make gas flow through in it with the flow velocity of 10-20m/s.
17, device as claimed in claim 12 is characterized in that the bottom of described bottom (3b) has 45 ℃-75 ℃ inclination angle so that by inlet duct (raw material that 10a, 10a ', 10a ") flow into along the wall surface of bottom towards current downflow.
18, device as claimed in claim 12, it is 30-40m/s that the structure that it is characterized in that being positioned at the interface channel between described top (3a) and described bottom (3b) can make the gas flow rate that flows through it.
19, device as claimed in claim 12, it is 5-10m/s that the structure that it is characterized in that described top (3a) can make by the gas flow rate in it.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1019930006472A KR960001003B1 (en) | 1993-04-17 | 1993-04-17 | Device for calcining cement |
| KR6472/93 | 1993-04-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1108380A true CN1108380A (en) | 1995-09-13 |
Family
ID=19354107
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 94105558 Pending CN1108380A (en) | 1993-04-17 | 1994-04-15 | An apparatus for precalcining raw cement with a fuel gasification device |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JPH07109155A (en) |
| KR (1) | KR960001003B1 (en) |
| CN (1) | CN1108380A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100368750C (en) * | 2000-08-24 | 2008-02-13 | F·L·施米思公司 | Method and plant for mfg. cement clinker |
| CN114644469A (en) * | 2020-12-17 | 2022-06-21 | 中国科学院工程热物理研究所 | Cement material processing device and cement material processing method |
| CN114644468A (en) * | 2020-12-17 | 2022-06-21 | 中国科学院工程热物理研究所 | Cement material processing device and cement material processing method |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4777044B2 (en) * | 2005-11-04 | 2011-09-21 | 太平洋セメント株式会社 | Cement manufacturing apparatus and cement manufacturing method |
| WO2024047685A1 (en) * | 2022-08-29 | 2024-03-07 | 太平洋エンジニアリング株式会社 | Waste treatment apparatus and treatment method |
-
1993
- 1993-04-17 KR KR1019930006472A patent/KR960001003B1/en not_active IP Right Cessation
-
1994
- 1994-04-15 CN CN 94105558 patent/CN1108380A/en active Pending
- 1994-04-18 JP JP7851094A patent/JPH07109155A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100368750C (en) * | 2000-08-24 | 2008-02-13 | F·L·施米思公司 | Method and plant for mfg. cement clinker |
| CN114644469A (en) * | 2020-12-17 | 2022-06-21 | 中国科学院工程热物理研究所 | Cement material processing device and cement material processing method |
| CN114644468A (en) * | 2020-12-17 | 2022-06-21 | 中国科学院工程热物理研究所 | Cement material processing device and cement material processing method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH07109155A (en) | 1995-04-25 |
| KR960001003B1 (en) | 1996-01-17 |
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