CN114644468A - Cement material processing device and cement material processing method - Google Patents
Cement material processing device and cement material processing method Download PDFInfo
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- CN114644468A CN114644468A CN202011497084.6A CN202011497084A CN114644468A CN 114644468 A CN114644468 A CN 114644468A CN 202011497084 A CN202011497084 A CN 202011497084A CN 114644468 A CN114644468 A CN 114644468A
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/38—Preparing or treating the raw materials individually or as batches, e.g. mixing with fuel
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/44—Burning; Melting
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/47—Cooling ; Waste heat management
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/48—Clinker treatment
Abstract
The invention relates to a cement material processing device and a method, wherein the device comprises: a pre-decomposition section; a pre-firing section; a firing section; the material inlet of the first separator is communicated with the material outlet of the pre-sintering part, and the material outlet of the first separator is communicated with the material inlet of the sintering part; and a material inlet of the second separator is communicated with a smoke outlet of the first separator through a first conveying channel, and a material outlet of the second separator is communicated with a material inlet of the pre-decomposition part. The device comprises a circulation loop, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, cement materials from a material outlet of the pre-decomposition part enter the pre-sintering part, a part of the cement materials from the material outlet of the pre-sintering part enter a material inlet of the second separator through a smoke outlet of the first separator, and the cement materials from a material outlet of the second separator enter the pre-decomposition part.
Description
Technical Field
The embodiment of the invention relates to the field of cement production, in particular to a cement material processing device and a cement material processing method.
Background
The cement clinker calcination mainly comprises the following processes: 1) preheating of raw meal and CaCO3Decomposing (800-900 ℃); 2)2CaO SiO2(C2S) generating (900-1200 ℃); 3)3CaO SiO2(C3S) generating>1300℃)。
At present, a traditional production system with higher efficiency in cement clinker calcination is mainly a novel dry predecomposition kiln, and the system has the advantages of low heat consumption, large production capacity of a single kiln, easy operation of an automatic process and the like, and is a mature technology at present. In a novel dry predecomposition kiln, preheating and decomposing the raw meal<900 ℃ is mainly carried out in cyclone and decomposing furnace equipment at all stages, and C2S (dicalcium silicate) and C3The S (tricalcium silicate) is sintered mainly in a rotary kiln (1000-1800 ℃).
However, the rotary kiln is huge in equipment, materials in the kiln are in a stacking state, the gas, liquid and solid heat exchange efficiency is low, the heat transfer speed in the kiln is low, and the temperature is not uniform. At present, indexes such as heat consumption, cost and the like of the rotary kiln cannot be further reduced, the maximum heat efficiency can only reach about 60 percent, and the process bottleneck cannot be broken through all the time.
In addition, the temperatures of the kiln head of the rotary kiln of the cement kiln up to 1800 ℃ make the rotary kiln contribute 80% of thermal type and 40% of fuel type NOx, which is one of the reasons why the cement kiln is an important source of fossil energy consumption and environmental pollution.
The fluidized cement calcining technology is expected to overcome the technical defects of the rotary kiln, and becomes a new generation cement clinker calcining technology. Chinese patent CN1073054C and japanese patent JP01148737A disclose a method and apparatus for firing cement clinker by granulating and firing (>1450 ℃) raw cement powder decomposed (900 to 1100 ℃) in a four-stage cyclone preheating and decomposing furnace in a fluidized bed, and then feeding the fired clinker into a cooler.
The US patent US4402754A discloses a device for burning cement clinker by using a circulating fluidized bed, cement raw material powder which is preheated by cyclone is subjected to clinker burning (1400 ℃) and sintering (950-1150 ℃) in a two-stage serial circulating fluidized bed device, and then the cement raw material powder is cooled and discharged.
Chinese patent CN1171066C discloses a device for calcining large granular fluidized cement clinker, which comprises a preheating chamber, a fluidized pre-calcining chamber, a fluidized calcining chamber and a cooling chamber, and combines moving bed technology and fluidization technology together, thereby improving the problem of poor quality of cement clinker in a moving bed vertical kiln.
The novel dry cement production process adopts a rotary kiln for firing, the equipment has large volume and large heat consumption, C2S and C3S is all burnt in the rotary kiln, and the kiln head of the rotary kiln has overhigh temperature (1800 ℃) and uneven burning temperature, thus causing high NOx emission, serious environmental pollution and low energy utilization rate.
The existing cement clinker fluidized firing method keeps the predecomposition equipment of a dry predecomposition kiln, simply replaces a rotary kiln with a bubbling fluidized bed, and has huge and complicated whole firing equipment and limited reduction of heat consumption; the whole reaction is still divided into raw material decomposition and clinker calcination, and C is not added2The S-firing process is separated from the clinker firing process.
In addition, the temperature distribution in the sintering/granulating furnace is uneven, the temperature is higher, the materials and high-temperature flue gas flow reversely, the flue gas amount in a clinker sintering area is large, the NOx emission level is high and unstable, and the equipment is difficult to enlarge.
Moreover, materials in each system of cement fluidized firing react step by step, and a material circulation process does not exist among the systems, so that the firing quality of fine material particles cannot be ensured.
Disclosure of Invention
The present invention has been made to mitigate or solve at least one aspect or at least one point of the above-mentioned problems.
According to an aspect of an embodiment of the present invention, there is provided a cement material processing apparatus including:
a pre-decomposition section adapted to perform a pre-decomposition treatment on the cement raw material;
the pre-burning part is suitable for pre-burning the cement materials, and the pre-decomposed cement materials enter the pre-burning part;
a burning part adapted to burn the cement material from the pre-burning part;
the material inlet of the first separator is communicated with the material outlet of the pre-sintering part, and the material outlet of the first separator is communicated with the material inlet of the sintering part;
a material inlet of the second separator is communicated with the smoke outlet of the first separator through a first conveying channel, a material outlet of the second separator is communicated with a material inlet of the pre-decomposition part,
wherein:
the device comprises a circulation loop, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, cement materials from a material outlet of the pre-decomposition part enter the pre-sintering part, a part of the cement materials from the material outlet of the pre-sintering part enter a material inlet of the second separator through a smoke outlet of the first separator, the cement materials from a material outlet of the second separator enter the pre-decomposition part, and the smoke outlet of the first separator is communicated with the material inlet of the second separator through a first conveying channel.
According to another aspect of an embodiment of the present invention, there is provided a method of treating a cement material, comprising the steps of:
providing a circulation loop and a sintering part, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, a flue gas outlet of the first separator is communicated with a material inlet of the second separator through a first conveying channel, and a material outlet of the first separator is communicated with a material inlet of the sintering part; and
such that: the cement material from the material outlet of the pre-decomposition part enters the pre-burning part, a part of the cement material from the material outlet of the pre-burning part enters the material inlet of the second separator through the smoke outlet of the first separator, and the cement material from the material outlet of the second separator enters the pre-decomposition part.
Drawings
FIG. 1 is a flow diagram of a cement material process according to an exemplary embodiment of the present invention;
FIG. 2 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, corresponding to the flow diagram shown in FIG. 1;
FIG. 3 is a schematic view of a cementitious material processing apparatus in accordance with another exemplary embodiment of the present invention, corresponding to the flow diagram shown in FIG. 1;
FIG. 4 is a flow diagram of a cement material process according to yet another exemplary embodiment of the present invention;
FIG. 5 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, corresponding to the flow chart shown in FIG. 4;
FIG. 6 is a flow chart of a cement material process according to yet another exemplary embodiment of the present invention;
FIG. 7 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, corresponding to the flow chart shown in FIG. 6;
FIG. 8 is a flow diagram of a cement material process according to yet another exemplary embodiment of the present invention;
FIG. 9 is a schematic view of a cementitious material handling apparatus in accordance with an exemplary embodiment of the present invention, which corresponds to the flow diagram shown in FIG. 8;
FIG. 10 is a flow chart of a cement material process according to yet another exemplary embodiment of the present invention;
fig. 11 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, which corresponds to the flowchart shown in fig. 10.
The reference signs are exemplary:
a pre-decomposition unit 10, a second separator 11, a decomposition furnace 12 and a first material returning device 13;
a pre-firing unit 20, a pre-firing furnace 21, a first separator 22;
a granulation/firing unit 30, a second material returning device 31, a main firing furnace 32;
a clinker cooling unit 40 and a clinker cooling furnace 41.
Detailed Description
The following description of the embodiments of the present invention with reference to the accompanying drawings is intended to explain the general inventive concept of the present invention and should not be construed as limiting the invention.
FIG. 1 is a flow diagram of a cement material process according to an exemplary embodiment of the present invention. As shown in fig. 1, the cement material treatment shown in fig. 1 includes four units, namely, a pre-decomposition unit 10, a pre-firing unit 20, a granulation/firing unit 30, and a clinker cooling unit 40.
As shown in FIG. 1, cement raw meal enters a pre-decomposition unit 10, and exchanges heat with high-temperature flue gas and fine particles (for example, the temperature of the flue gas is 1000-1200 ℃) from a pre-burning formation unit 20 in the pre-decomposition unit 10, so that the cement raw meal is preheated and CaCO is obtained3Decomposing to realize the recovery of the heat of the flue gas, and discharging the preheated flue gas (in one embodiment of the invention, the temperature can be less than 800 ℃). In one embodiment of the present invention, the pre-decomposition unit 10 operates at a temperature of 800-900 ℃.
Next, as shown in FIG. 1, preheating and CaCO are completed3The decomposed raw material (for example, 800 to 900 ℃) enters a pre-sintering unit 20 (for example, 1000 to 1200 ℃), the pre-sintering unit 20 is fed with fuel and air, and receives high-temperature flue gas and fine particles (as mentioned later, after cooling by chilled air, the temperature of the flue gas and the fine particles is, for example, 1000 to 1100 ℃) from a granulation/sintering unit 30, and the pre-sintering of the raw material C is completed in the pre-sintering unit 202The firing reaction of S (for example, the operating temperature of the pre-firing unit 20 is 1000 to 1200 ℃), and the fuel is firedThe heat required for the reaction is supplied to the pre-firing reaction by firing and high-temperature flue gas from the firing unit 30. The high-temperature flue gas and fine particles (the temperature of the high-temperature flue gas and the fine particles is 1000-1200 ℃) formed by the pre-sintering unit 20 enter the pre-decomposition unit 10 to participate in raw meal preheating and CaCO3And (5) decomposing.
Referring to fig. 1, the pre-fired material is introduced into a granulation/firing unit 30, where granulation and C of cement raw meal are performed3And S, sintering to form high-temperature clinker. The granulation/sintering unit 30 is provided with exciting cold air, and primarily cools the high-temperature clinker to below 1100 ℃, and the high-temperature flue gas and the unfired fine particles enter the pre-sintering unit 20 after being cooled to 1000-1100 ℃ to provide heat for the pre-sintering reaction with the raw materials. In one embodiment of the present invention, the pelletizing/firing unit 30 operates at a temperature between 1300 ℃ and 1450 ℃.
Referring to fig. 1, the fired high temperature clinker enters a clinker cooling unit 40 (e.g. clinker temperature <900 ℃ after cooling via the cooling unit), after cooling the clinker temperature is reduced to e.g. below 500 ℃. As shown in fig. 1, in the embodiment shown in fig. 1, air is used as cooling air to recover heat of clinker, and hot air (>500 ℃) after waste heat recovery enters the granulating/burning unit 30 or the pre-burning unit 20 to participate in fuel combustion as air distribution.
In the invention, the main reaction of the cement clinker sintering process is controlled by regions, and the temperature of each region is controlled to realize more accurate reaction control, which specifically comprises the following steps: CaCO3The pre-heating decomposition is carried out in a pre-decomposition unit 10 (e.g., 800-900 ℃), C2S firing is completed in a pre-firing unit 20 (e.g., 1000 to 1200 ℃), granulation, and C3S firing is completed in a granulation/firing unit 30 (e.g., 1300 to 1450 ℃), and a clinker cooling unit 40 (e.g.<The cooling and the utilization of sensible heat of the clinker are finished within 500 ℃. Because the optimal reaction temperatures of different reactions are different in the cement clinker sintering process, the temperature (heat) and the chemical reaction process can be matched by controlling the different reactions in different regions in the cement clinker sintering process, thereby greatly reducing the heat load of the clinker sintering region, and avoiding or reducing the reaction temperature of C2S firing, granulation and C3The S sintering is completed in the same sintering area, and the heat loss and the low chemical reaction rate caused by temperature mismatching are solved.
In addition, in the embodiment shown in fig. 1, for example, a circulation loop is constructed between the units, so that the system operation is safer and more stable, multiple cycles of fine material particles can be realized through control, sufficient sintering/granulating time of the fine material particles is fully ensured, and the sintering quality of clinker is effectively ensured.
Fig. 2 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, which corresponds to the flowchart shown in fig. 1.
In the embodiment shown in fig. 2, the pre-decomposition unit 10 comprises a second separator 11, a decomposing furnace 12 and a first return feeder 13, in which the cement raw meal is preheated and decomposed (e.g. 800-900 c).
Optionally, the pre-decomposition unit is provided with a fuel and an air distribution port for providing heat for the decomposition reaction of the decomposing furnace through combustion of the fuel.
The pre-firing unit 20 includes a pre-firing furnace 21 and a first separator 22, and the pre-firing furnace 21 is provided with a first circulation outlet a1, a circulation inlet B1, and a material inlet B2.
The first circulation outlet A1 of the pre-firing furnace 21 communicates with the material inlet of the first separator 22 through the first transfer passage C1. An outlet (a flue gas outlet) of the first separator 22 is connected with an inlet (a material inlet) of the second separator 11 of the pre-decomposition unit 10 through a third conveying channel C3 for conveying high-temperature flue gas (for example, 1000-1100 ℃) and fine material particles separated by the first separator 22 to the pre-decomposition unit 20, an inlet (a material inlet B2) of the pre-burning furnace 21 is connected with an outlet of the first material returning device 13, and the decomposed material is subjected to clinker production in the pre-burning furnace 21 of the pre-burning unit 20 to obtain an intermediate product mainly comprising C2The firing process of S (e.g., 1000 to 1200 ℃) is completed in the first separator 22.
The granulating/firing unit 30 comprises a secondary return feeder 31 and a main firing furnace 32, the firing furnace 32 being provided with a second circulation outlet a 2. Second circulation outlet A2 of main firing furnace 32The top of the dense phase zone (generally the zone below the fluidized pre-firing furnace transport separation height TDH, which can be looked up and calculated according to the relevant technical manual) of the pre-firing furnace 21 of the pre-firing unit 20 is in communication with the circulation inlet B1 via a second transport channel C2 for the incomplete granulation and C in the main firing furnace 323The S-sintered fine particle material is conveyed to the pre-sintering furnace 21 through a second circulation outlet A2 to continue the pre-sintering (for example, 1000-1200 ℃) and the granulating/sintering process (for example, 1300-1450 ℃).
As can be appreciated by those skilled in the art, the location of the circulation inlet B1 is not limited to the top of the dense phase zone so long as it can establish circulation between the pre-firing furnace and the firing furnace.
As shown in figure 2 and also shown in figure 1, the burnt high-temperature flue gas is cooled to 1000-1100 ℃ by chilling wind and then enters a pre-burning furnace 21 to be C2S sintering provides heat.
The outlet of the second material returning device 31 is communicated with the material inlet of the main burning furnace 32, and is used for conveying the coarse material particles separated by the first separator 22 into the main burning furnace 32, completing granulation and C of the cement raw material in the main burning furnace 323And (3) a sintering process of S.
As shown in fig. 2, the clinker cooling unit 40 includes a clinker cooling section 41 for introducing cooling air to cool the clinker. The cooled clinker is discharged from the clinker cooling section 41. Preheated hot air (e.g. air)>900 ℃) enters the pre-firing furnace 21 through a second circulation outlet A2 to be C2S sintering provides heat.
In the embodiment shown in fig. 2, the clinker cooling section 41 is in direct communication with the main firing furnace 32, and the cooling air provided at the bottom or lower part of the clinker cooling section 41 in the clinker cooling unit 40 (see fig. 2) provides an air separation function for the incompletely fired materials in the main firing furnace 32 to return to the pre-firing furnace 21, in addition to the function of cooling the cement clinker.
The embodiment shown in fig. 2 comprises two circulation loops, respectively: a circulation loop consisting of a pre-sintering furnace 21, a first separator 22, a second separator 11, a decomposing furnace 12 and a first material returning device 13; and a circulation loop consisting of a pre-sintering furnace 21, a first separator 22, a second material returning device 31 and a main sintering furnace 32.
The following exemplifies a specific process flow of the embodiment shown in fig. 2.
The cement raw meal enters from the outlet section of the first separator 22 (corresponding to the third conveying channel C3 communicated with the flue gas outlet of the first separator 22), and the cement raw meal enters into the second separator 11 and the decomposing furnace 12 after being preheated by high-temperature flue gas (1000-1100 ℃) from the first separator 22 to finish CaCO3The temperature of the decomposition process is controlled to be 800-1000 ℃. In the embodiment shown in fig. 2, fuel and air distribution inlets are also provided in the third transfer channel C3 to provide further heat for the pre-heating decomposition of cement raw meal. As can be understood by those skilled in the art, in the case where the fuel and the air distribution are added to the pre-burning and calcining kiln 21 enough to satisfy the heat requirement in the pre-decomposing kiln 12, the fuel and air distribution inlet may not be provided in the third transfer passage C3; or only a fuel inlet or a ventilation inlet may be provided.
Returning the decomposed materials to the pre-sintering furnace 21 through the first material returning device 13 for fluidization, and finishing the step C in the pre-sintering furnace 212S firing and granulation of part of the pellets, fuel and air being fed from the bottom of the pre-firing furnace 21 to supply C2And (3) controlling the temperature in the pre-sintering and forming furnace 21 to be 1000-1200 ℃ by using the heat required by S sintering and partial granulation.
The particles from the pre-firing furnace 21 enter the first separator 22 through the first conveying passage C1 to complete the separation process of coarse and fine particles. Separated coarse particles enter a main firing furnace 32 from a first separator 22 through a second return feeder 31 for granulation and clinker firing, unseparated fine particles enter a second separator 11 along with high-temperature flue gas (1000-1100 ℃) discharged from a flue gas outlet of a pre-firing furnace 21, the fine particles enter a decomposing furnace 12 after being trapped by the second separator 11, sensible heat of the fine particles can be used for providing reaction heat for the decomposing furnace 12, and then the fine particles return to the pre-firing furnace 21 through the first return feeder 13 and a material inlet B2 of the pre-firing furnace 21.
In the embodiment shown in fig. 2, because the flue gas in the pre-burning furnace 21 does not enter the main burning furnace 32, but is discharged after the raw meal preheating process is completed by the second separator 11, the flue gas amount entering the main burning furnace 32 is greatly reduced, and the technical defect of the prior fluidized cement burning technology that the flue gas amount in the main burning furnace is too high is avoided.
The main burning furnace 32 is used for granulating and burning clinker, the required heat is provided by burning fuel, and the temperature is controlled to be 1300-1450 ℃. In the embodiment shown in fig. 2, the fuel and air enters the main furnace 32 at the top or upper portion of the furnace 32, as shown in fig. 2.
The granulated and fired large particle cement clinker in the main firing furnace 32 is rapidly cooled by a chilling wind to, for example, 1100 ℃.
As shown in FIG. 2, the lower part of the main burning furnace 32 is communicated with a cooling section 41 of a clinker cooling unit, cooling air is introduced into the bottom of the cooling section 41, the cooling section 41 forms a fluidized bed, and air separation is completed on large-particle cement clinker and finer particles of incompletely-burned clinker entering the cooling section 41. Specifically, the incompletely burned fine particles are separated by air and then leave the main burning furnace 32 along with the high-temperature flue gas generated by the main burning furnace 32 and the hot air preheated by the clinker in the cooling section through the second circulation outlet a2 to return to the pre-burning furnace 21 for continuous reaction, and the large particle cement clinker after being burned enters the cooling section 41. High-temperature flue gas (1000-1100 ℃) generated by the main burning furnace and hot air (900 ℃) preheated by the clinker in the cooling section return to the pre-burning furnace 21 through a second circulation outlet A2, so that certain heat is provided for the pre-burning reaction in the pre-burning furnace 21.
In the cooling stage 41, the large particles of clinker are discharged through the bottom of the cooling stage 41 after being cooled to, for example, about 500 ℃.
Fig. 3 is a schematic view of a cement material processing apparatus according to another exemplary embodiment of the present invention, which corresponds to the flowchart shown in fig. 1.
As shown in fig. 3, the granulating/firing unit 30 includes a secondary return feeder 31 and a main firing furnace 32, wherein the difference from the embodiment shown in fig. 2 is that: in fig. 3, a second material returning device 31 is connected to the lower middle portion of the main burning furnace 32 for feeding the coarse material particles separated by the first separator 22 into the main burning furnace 32, and cement raw materials are fluidized in the main burning furnace 32 to produce cement raw materialsGranules and C3S sintering process; the main burning furnace 32 is communicated with a circulation inlet B1 provided at the middle upper portion of the pre-burning furnace 21 of the pre-burning unit 20, and is used for conveying the fine particles which are not completely burned into clinker in the main burning furnace 32 back to the pre-burning furnace 21 to continue the pre-burning process. As in the example shown in fig. 2, the granulated and fired large particle clinker and the unfinished granulated and fired fine particle material are subjected to an air separation process in the main firing furnace.
Alternatively, as shown in FIG. 3, the second circulation outlet A2 is provided at the upper portion or top of the main firing furnace 32.
The embodiment of fig. 3 also differs from the embodiment of fig. 2 in that: the clinker cooling unit 40 is arranged relatively independently of the main firing unit, i.e. no clinker can enter the main firing unit from the clinker cooling zone unit, and specifically the clinker cooling unit 40 comprises a separate clinker cooling furnace 41, the top of which clinker cooling furnace 41 is connected to the lower part of the main firing furnace 32 by a clinker passage or a fourth conveying passage C4. The incompletely burned finer particles leave the granulating/burning unit 30 from the upper part of the main burning furnace by air separation, and the burned clinker leaves from the lower outlet of the main burning furnace and enters a clinker cooling furnace 41, and the clinker cooling furnace 41 is used for introducing cooling air to cool the clinker. The cooled clinker is discharged from the clinker cooling furnace 41. The cooling air recovers the sensible heat of the clinker and enters the main burning furnace through a clinker channel or can be used in other places in the device where air distribution is needed.
The specific flow of the processing method corresponding to the embodiment shown in fig. 3 is different from the corresponding processing method of the embodiment shown in fig. 2 in that:
in the flow corresponding to the apparatus shown in fig. 3, the lower part of the main firing furnace 32 is communicated with the cooling furnace 41 of the clinker cooling unit through the clinker passage or the fourth conveyance passage C4, and cooling air is introduced into the bottom of the cooling furnace 41. And cooling large particles of clinker to about 500 ℃, and discharging from the bottom of the cooling furnace.
The granulated and fired large particle clinker and the unfinished granulated and fired finer particle material are subjected to a winnowing process in the main firing furnace 32. After the fine particles which do not complete the granulation and sintering processes are subjected to air separation, the fine particles leave the main sintering furnace along with high-temperature flue gas generated by the main sintering furnace 32 through a material return opening or a second circulating outlet A2 at the top or the upper part of the main sintering furnace 32, and enter the pre-sintering furnace 21 to continue the sintering cycle.
FIG. 4 is a flow diagram of a cement material process according to yet another exemplary embodiment of the present invention; fig. 5 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, which corresponds to the flow chart shown in fig. 4.
The embodiment shown in fig. 4-5 differs from the embodiment shown in fig. 1-3 in that in the embodiment shown in fig. 4-5, the clinker cooling unit 40 is moved from the lower end of the granulating/firing unit 30 to the bottom of the pre-firing unit 20, and the cooling air acts as both clinker cooling and fluidizing air for the pre-firing unit. Accordingly, in fig. 5, the second circulation outlet a2 of the granulating/calcining unit 30 is provided at the bottom of the granulating/calcining unit 30. Unlike the embodiment shown in fig. 2, in fig. 4-5, the air separation process is completed in the pre-firing kiln 21 for the granulated and fired large particle clinker and the unfinished granulated and fired fine particle material.
In the embodiment shown in fig. 4-5, the second recycling outlet a2 of the main firing furnace 32 also constitutes the material outlet of the main firing furnace 32.
Fig. 6 is a flowchart of a cement material processing according to still another exemplary embodiment of the present invention, and fig. 7 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, which corresponds to the flowchart shown in fig. 6.
The embodiment shown in fig. 6 to 7 is different from the embodiment shown in fig. 1 to 5 in that, in the embodiment shown in fig. 6 to 7, the pre-firing furnace 21 is not provided with the circulation inlet B1, so that there is no second circulation outlet a2 which is the same as the circulation inlet B1, in other words, there is no direct circulation between the main firing furnace 32 and the pre-firing furnace 21; secondly, in the embodiment shown in fig. 6-7, the third recycling outlet a3 of the main firing furnace 32 is directly connected to the third conveying channel C3 via a fifth conveying channel C5 in common with the flue gas outlet of the first separator 22.
In the embodiment shown in fig. 6 to 7, the high temperature flue gas and the unfired fine particles generated from the granulating/calcining unit 30 do not enter the pre-calcining unit 20, but enter the inlet section of the pre-heating decomposition unit 10, so that the fine particle cycle time is longer.
As shown in FIG. 7, a chilling wind inlet is provided above the third circulation outlet A3 of the main burning furnace 32, so that the temperature of the material flowing out of the main burning furnace 32 through the third circulation outlet A3 is in the range of 1000 ℃ to 1100 ℃ in one embodiment of the present invention.
Fig. 8 is a flowchart of a cement material processing according to still another exemplary embodiment of the present invention, and fig. 9 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, which corresponds to the flowchart shown in fig. 8.
The embodiment shown in fig. 8 to 9 is different from the embodiment shown in fig. 1 to 5 in that, in the embodiment shown in fig. 8 to 9, although the pre-firing furnace 21 is provided with the circulation inlet B1 and the main firing furnace 32 is provided with the second circulation outlet a2, the second circulation path C2 between the circulation inlet B1 and the second circulation outlet a2 is provided with the return device 33; secondly, in the embodiment shown in fig. 8-9, the third recycling outlet a3 of the main firing furnace 32 is directly connected to the third conveying channel C3 via a fifth conveying channel C5 together with the flue gas outlet of the first separator 22.
The embodiment shown in fig. 8-9 is similar to the embodiment shown in fig. 4-5 in that the clinker cooling unit 40 is moved from the lower end of the granulating/calcining unit 30 to the bottom of the pre-calcining unit 20, and the cooling air acts as both clinker cooling and fluidizing air for the pre-calcining unit. In fig. 8-9, the granulated and fired large particle clinker and the unfinished granulated and fired fine particle material are subjected to an air classification process in a pre-firing kiln 21.
In addition, as described above, in fig. 8 to 9, the material returning device 33 is added to the second conveying path C2 between the granulating/calcining furnace unit 30 and the pre-calcining furnace unit 20, the granulating/calcining furnace 32 is changed into a bubbling bed type, and large particles of calcined clinker are returned to the bottom of the pre-calcining furnace 21 through the material returning device 33, cooled, air-separated and cooled, and then discharged.
It should be noted that in the embodiment shown in fig. 8-9, the material returning device 33 may not be provided.
Fig. 10 is a flowchart of a cement material processing according to still another exemplary embodiment of the present invention, and fig. 11 is a schematic view of a cement material processing apparatus according to an exemplary embodiment of the present invention, which corresponds to the flowchart shown in fig. 10.
The embodiment shown in fig. 10 to 11 is different from the embodiment shown in fig. 1 to 5 in that, in the embodiment shown in fig. 10 to 11, the circulating inlet B1 is not provided in the pre-firing furnace 21, and the second circulating outlet a2 is not provided in the main firing furnace 32, so that there is no communication from the second circulating outlet a2 of the main firing furnace 32 to the circulating inlet B1 of the pre-firing furnace 21, in other words, there is no direct circulation between the main firing furnace 32 and the pre-firing furnace 21; secondly, in the embodiment shown in fig. 10-11, the third recycling outlet a3 of the main firing furnace 32 is directly connected to the third conveying channel C3 via a fifth conveying channel C5 in common with the flue gas outlet of the first separator 22.
The embodiment shown in fig. 10-11 is similar to the embodiment shown in fig. 3 in that the clinker cooling unit 40 is arranged independently of the main firing unit, and specifically the clinker cooling unit 40 comprises a separate clinker cooling furnace 41, and the top of the clinker cooling furnace 41 is connected to the lower part of the main firing furnace 32 by a clinker passage or a fourth conveying passage C4. The incompletely burned finer particles leave the granulating/burning unit 30 from a third circulation outlet A3 at the upper part of the main burning furnace under the action of air separation, and the burned clinker leaves from the lower outlet of the main burning furnace and enters a clinker cooling furnace 41, and the clinker cooling furnace 41 is used for introducing cooling air to cool the clinker. The cooled clinker is discharged from the clinker cooling furnace 41. The cooling air recovers the sensible heat of the clinker and can enter the main burning furnace through a clinker channel or a fourth conveying channel C4 or can be used in other places in the device where air distribution is needed.
The embodiment shown in fig. 1-11 includes the following circulation loops:
one is a circulation loop formed between the pre-firing unit 10 and the pre-decomposition unit 20 (fig. 1 to 11). The circulation loop comprises a pre-decomposition furnace 12, a pre-sintering furnace 21, a first separator 22 and a second separator 11 which are sequentially arranged, cement materials from a material outlet of the pre-sintering furnace 21 enter the pre-decomposition furnace 12, and cement materials from a material outlet of the pre-sintering furnace 21 enterThe material enters the second separator 11 via the first separator 22, and the cement material from the material outlet of the second separator 11 enters the pre-firing furnace 21. The high-temperature flue gas generated by the pre-sintering unit enters the pre-decomposition unit for preheating and decomposing raw materials, but does not enter a clinker burning area, so that the flue gas entering the clinker burning area can be greatly reduced, and the thermal NO of the system can be greatly reducedxThe amount of production of (c).
The second is a circulation loop formed between the granulating/calcining unit 30 and the pre-calcining unit 20 (fig. 1 to 5, fig. 9). The circulation circuit comprises a pre-firing furnace 21, a first separator 22 and a main firing furnace 32 arranged in sequence, cement material from a material outlet of the pre-firing furnace 21 enters the firing furnace 32 via the first separator 22, and a part of the cement material from the firing furnace 32 is adapted to return into the pre-firing furnace 21 via a circulation outlet and a circulation inlet. Based on the circulation loop, the fine material particles can be circulated for many times, sufficient sintering/granulating time of the fine material particles is fully ensured, and the sintering quality of clinker is effectively ensured.
The cement raw meal can realize the following processes in the cement clinker firing method of the invention: preheating (<800 ℃ decomposition (800-900 ℃) → C2S firing (1000-1200 ℃) → pelleting \ C3S baking (1300-1450 ℃) → cooling<500 deg.c) → clinker discharge process.
In the embodiment shown in fig. 1-5:
1) the high-temperature flue gas provides heat for preheating and decomposing raw materials;
2) decomposing the preheated raw materials in a decomposing furnace;
3) key intermediate product C of decomposed raw material in pre-burning furnace2S generation reaction and partial particle granulation;
4) separating coarse and fine particles of the material, wherein the fine particles can continuously participate in the processes 1) to 3) to form a first cycle, and the coarse particles enter a main firing furnace for granulation and C3S, firing;
5) the granules are granulated in a main firing furnace, C3S, a firing process, namely discharging the large-grained cement clinker after cooling and temperature reductionAnd returning the fine particles which are not sintered to the pre-sintering furnace to continue the processes from 3) to 5) to form a second cycle.
6) The flow direction of high-temperature flue gas of each part in the whole system is controlled, so that the high-temperature flue gas provides heat for the reaction of each part, and the matching of temperature (heat) and reaction in the whole reaction process is realized.
In the embodiment shown in fig. 6-11:
1) the high-temperature flue gas provides heat for preheating and decomposing raw materials;
2) decomposing the preheated raw materials in a decomposing furnace;
3) key intermediate product C of decomposed raw material in pre-burning furnace2S generation reaction and partial granulation;
4) separating coarse and fine particles of the material, wherein the fine particles can continuously participate in the processes 1) to 3) to form a first cycle, and the coarse particles enter a main firing furnace for granulation and C3S, firing;
5) the granules are granulated in a main firing furnace, and C3S, a sintering process, namely cooling and cooling the sintered large-particle cement clinker, then discharging the large-particle cement clinker, and returning the unfinished fine particles to the pre-decomposition furnace to continue the processes 1) to 3).
6) The flow direction of high-temperature flue gas of each part in the whole system is controlled, so that the high-temperature flue gas provides heat for the reaction of each part, and the matching of temperature (heat) and reaction in the whole reaction process is realized.
7) The high-temperature flue gas and unfired fine particles generated by the granulating/sintering unit 30 do not enter the pre-sintering unit 20, but enter the inlet section of the preheating decomposition unit 10, so that the fine particle cycle time is longer.
In the present invention, the preburning pair corresponds to the intermediate product C being mainly included2S is generated by a process comprising mainly granulation and C3S, sintering.
In the present invention, a pre-firing means (i.e., a pre-firing section) is provided to perform pre-firing treatment on a cement material, a granulation/firing means (i.e., a firing section) is provided to perform firing treatment on the cement material from the pre-firing means, and the granulation/firing means is provided to perform firing treatment on the cement material by being provided in the firing sectionThe first separator between the unit and the pre-firing unit separates and connects the processes of the firing unit and the pre-firing unit, thereby comparing the prior art with C2The S-firing process is separated from the clinker firing process.
In the invention, the first separator is arranged between the pre-sintering unit (namely the pre-sintering part) and the granulating/sintering unit (namely the sintering part), so that the flue gas from the pre-sintering part can be separated, and the direct entering of the flue gas into the sintering part is avoided or reduced, which is favorable for overcoming the problems of large flue gas amount, high NOx emission level and instability in a clinker sintering area in the prior art.
It is further noted that in the present invention, although the flue gas outlet of the first separator communicates with the feed inlet of the second separator, the present invention is not limited thereto. The flue gas outlet of the first separator may also not lead to the second separator or to the pre-decomposition unit. At this time, the second separator 11 may not be provided.
In the present invention, the return feeder 31 and/or the return feeder 13 may not be provided, in case it is possible to remove the return feeder 31 or 13 or other designs may be used instead.
It is to be noted that, in the present invention, unless otherwise explicitly indicated, all numerical ranges may include endpoints, and also include medians of all numerical ranges, which are within the scope of the present invention.
Based on the above, the invention provides the following technical scheme:
1. a cement material handling device comprising:
a pre-decomposition section adapted to perform a pre-decomposition treatment on the cement raw material;
the pre-burning part is suitable for pre-burning the cement materials, and the pre-decomposed cement materials enter the pre-burning part;
a burning part adapted to burn the cement material from the pre-burning part;
the material inlet of the first separator is communicated with the material outlet of the pre-sintering part, and the material outlet of the first separator is communicated with the material inlet of the sintering part;
a material inlet of the second separator is communicated with the smoke outlet of the first separator through a first conveying channel, a material outlet of the second separator is communicated with a material inlet of the pre-decomposition part,
wherein:
the device comprises a circulation loop, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, cement materials from a material outlet of the pre-decomposition part enter the pre-sintering part, a part of the cement materials from the material outlet of the pre-sintering part enter a material inlet of the second separator through a smoke outlet of the first separator, the cement materials from a material outlet of the second separator enter the pre-decomposition part, and the smoke outlet of the first separator is communicated with the material inlet of the second separator through a first conveying channel.
2. The apparatus of 1, wherein:
the sintering part is provided with a circulating outlet, and the circulating outlet and the smoke outlet of the first separator are converged to a first conveying channel.
3. The apparatus of claim 2, wherein:
the material inlet of the burning part is arranged at the top or the upper part of the burning part, and the circulating outlet is arranged at the lower part of the burning part.
4. The apparatus of claim 2, wherein:
the material inlet of the burning part is arranged at the lower part of the burning part, and the circulating outlet is arranged at the upper part or the top of the burning part.
5. The apparatus of claim 5, wherein:
the firing section includes a firing furnace in the form of a fluidized bed.
6. The apparatus of claim 2, wherein:
the material inlet of the sintering part is arranged at the top or the upper part of the sintering part, and the circulating outlet is arranged at the upper part of the sintering part;
the sintering part comprises a bubbling bed type sintering furnace, a return outlet is arranged at the lower part of the sintering furnace, a return inlet is arranged at the pre-sintering part, and a return unit is arranged in a channel between the return outlet and the return inlet;
the device also comprises a cooling part, a pre-sintering part and a cooling part, wherein the cooling part is suitable for cooling cement materials from the pre-sintering part, cooled cement clinker is suitable for being discharged from the cooling part, the cooling part and the pre-sintering part are vertically and integrally formed, and the cooling part is positioned below the pre-sintering part;
the fuel inlet of the pre-sintering part is arranged at the lower part of the pre-sintering part, and the bottom or the lower part of the cooling part is provided with the fuel air distribution inlet of the pre-sintering part.
7. The apparatus of any of claims 2-6, further comprising:
a cooling section adapted to cool the cement material from the firing section, the cooled cement clinker being adapted to be discharged from the cooling section.
8. The apparatus of claim 8, wherein:
the device is provided with a separation air inlet below the circulating outlet, and separation air is suitable for being introduced into the burning part through the separation air inlet.
9. The apparatus of claim 9, wherein:
the fuel inlet and the fuel air distribution inlet of the burning part are arranged at the top or the upper part of the burning part, and the circulating outlet of the burning part is arranged at the bottom or the lower part of the burning part;
the cooling part and the sintering part are integrally formed in the vertical direction, and the cooling part is positioned below the sintering part;
and a separation air inlet is formed in the bottom or the lower part of the cooling part, and separation air is suitable for upwards entering the sintering part through the separation air inlet.
10. The apparatus of claim 9, wherein:
the cooling part is arranged independently of the sintering part, at least one part of the cooling part is positioned below the sintering part, and the cooling part is communicated with the sintering part through a second conveying pipeline;
the fuel air distribution inlet of the burning part is arranged at the bottom or the lower part of the burning part, the fuel air distribution of the burning part forms the separation air, and the fuel air distribution inlet of the burning part forms the separation air inlet.
11. The apparatus of 1, wherein:
the first conveying channel is provided with a cement raw material inlet, a first fuel inlet and a first fuel air distribution inlet.
12. The apparatus of 1, further comprising:
and the first material returning device is arranged between the material outlet of the first separator and the material inlet of the sintering part.
13. The apparatus of 1, further comprising:
and the second material returning device is arranged between the material outlet of the pre-decomposition part and the material inlet of the pre-burning formation part, and the circulating loop comprises the second material returning device.
14. A method of treating a cementitious material comprising the steps of:
providing a circulation loop and a sintering part, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, a flue gas outlet of the first separator is communicated with a material inlet of the second separator through a first conveying channel, and a material outlet of the first separator is communicated with a material inlet of the sintering part; and
such that: the cement material from the material outlet of the pre-decomposition part enters the pre-burning part, a part of the cement material from the material outlet of the pre-burning part enters the material inlet of the second separator through the smoke outlet of the first separator, and the cement material from the material outlet of the second separator enters the pre-decomposition part.
15. The method of claim 15, wherein:
the sintering part is provided with a circulating outlet;
the method comprises the following steps: so that the recycling outlet and the flue gas outlet of the first separator are summed to said first conveying channel.
16. The method of claim 15 or 16, further comprising the step of:
the flue gases from the flue gas outlet of the first separator are used to heat the cement raw meal that is to be fed into the second separator.
17. The method of claim 17, wherein:
the temperature of the pre-decomposition treatment is controlled between 800 ℃ and 900 ℃; and/or
The temperature of the pre-sintering treatment is controlled between 1000 ℃ and 1200 ℃; and/or
The temperature of the sintering treatment is controlled between 1300 ℃ and 1450 ℃.
18. The method of 18, further comprising the steps of:
and introducing cooling air to cool the cement material from the sintering part.
19. The method of claim 16, further comprising the steps of:
a sorting air inlet is arranged below the circulating outlet;
and introducing separation air into the burning part through the separation air inlet.
20. The method of 20, wherein:
the sorting air inlet is a cooling air inlet of cement clinker; or
The separation air inlet is a fuel air distribution inlet of the burning part.
21. The method of claim 16, wherein:
the material inlet of the sintering part is arranged at the top or the upper part of the sintering part, the circulating outlet is arranged at the upper part of the sintering part, the sintering part comprises a sintering furnace in a bubbling bed mode, the lower part of the sintering furnace is provided with a return outlet, the pre-sintering part is provided with a return inlet, and a channel between the return outlet and the return inlet is provided with a return unit;
a cooling part suitable for cooling the cement materials from the burning part is vertically and integrally formed with the pre-burning part, the cooling part is positioned below the pre-burning part, and the cooled cement clinker is suitable for being discharged from the cooling part;
the fuel inlet of the pre-sintering part is arranged at the lower part of the pre-sintering part, the bottom or the lower part of the cooling part is provided with the fuel air distribution inlet of the pre-sintering part,
the method comprises the following steps: cooling air is introduced from the bottom of the cooling part.
22. The method of 20, wherein:
a chilling air inlet is arranged above the circulating outlet of the sintering part;
the method comprises the following steps: so that the temperature of the material flowing out of the burning part through the circulating outlet is in the range of 1000-1100 ℃.
Based on the scheme, the invention can obtain at least one of the following technical effects:
1. temperature matching, energy consumption reduction, raw material decomposition reaction and dicalcium silicate (C) in the process of cement clinker sintering2S) firing reaction and tricalcium silicate (C)3S, clinker) sintering reaction is controlled in different areas, and the matching of temperature (heat) and a chemical reaction process is realized, so that the energy consumption of a clinker sintering area is greatly reduced;
2. the temperature is uniform and mild, the pollution is reduced, the main reaction in the cement clinker sintering process is carried out in different areas, the temperature of the cement high-temperature sintering area is further reduced, and the NO of the cement high-temperature sintering is reducedxThe amount of production.
3. Fluidization reaction and good heat transfer effect.
4. The equipment adopts a fluidization structure, and the floor area is reduced.
5. Greatly reduces the smoke amount entering the clinker burning area, and further greatly reduces the thermal NO in the clinker burning areaxThe generated amount avoids the large smoke amount and the thermal NO in the main burning area in the prior fluidized burning technologyxThe technical disadvantage of large production amount.
6. Using a circulating hearth furnace type with dicalcium silicate (C)2S) Pre-burning Forming furnace, raw meal decomposing furnace, dicalcium silicate (C)2S) pre-sintering furnace and tricalcium silicate (C)3S, clinker) sintering furnaces, realizing different circulation paths of large particles and powder, realizing multiple circulation of fine particles of the material, further prolonging the circulating sintering time of unfired fine particles, and improving the sintering quality of cement clinker.
Although embodiments of the present invention have been shown and described, it would be appreciated by those skilled in the art that changes may be made in these embodiments and combinations of elements without departing from the principles and spirit of the invention, the scope of which is defined in the claims and their equivalents.
Claims (22)
1. A cement material handling device comprising:
a pre-decomposition section adapted to perform a pre-decomposition treatment on the cement raw material;
the pre-burning part is suitable for pre-burning the cement materials, and the pre-decomposed cement materials enter the pre-burning part;
a burning part adapted to burn the cement material from the pre-burning part;
the material inlet of the first separator is communicated with the material outlet of the pre-sintering part, and the material outlet of the first separator is communicated with the material inlet of the sintering part;
a material inlet of the second separator is communicated with the smoke outlet of the first separator through a first conveying channel, a material outlet of the second separator is communicated with a material inlet of the pre-decomposition part,
wherein:
the device comprises a circulation loop, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, cement materials from a material outlet of the pre-decomposition part enter the pre-sintering part, a part of the cement materials from the material outlet of the pre-sintering part enter a material inlet of the second separator through a smoke outlet of the first separator, the cement materials from a material outlet of the second separator enter the pre-decomposition part, and the smoke outlet of the first separator is communicated with the material inlet of the second separator through a first conveying channel.
2. The apparatus of claim 1, wherein:
the sintering part is provided with a circulating outlet, and the circulating outlet and the smoke outlet of the first separator are converged to a first conveying channel.
3. The apparatus of claim 2, wherein:
the material inlet of the burning part is arranged at the top or the upper part of the burning part, and the circulating outlet is arranged at the lower part of the burning part.
4. The apparatus of claim 2, wherein:
the material inlet of the burning part is arranged at the lower part of the burning part, and the circulating outlet is arranged at the upper part or the top of the burning part.
5. The apparatus of claim 5, wherein:
the firing section includes a firing furnace in the form of a fluidized bed.
6. The apparatus of claim 2, wherein:
the material inlet of the sintering part is arranged at the top or the upper part of the sintering part, and the circulating outlet is arranged at the upper part of the sintering part;
the sintering part comprises a bubbling bed type sintering furnace, a return outlet is arranged at the lower part of the sintering furnace, a return inlet is arranged at the pre-sintering part, and a return unit is arranged in a channel between the return outlet and the return inlet;
the device also comprises a cooling part, a pre-sintering part and a cooling part, wherein the cooling part is suitable for cooling cement materials from the pre-sintering part, cooled cement clinker is suitable for being discharged from the cooling part, the cooling part and the pre-sintering part are vertically and integrally formed, and the cooling part is positioned below the pre-sintering part;
the fuel inlet of the pre-sintering part is arranged at the lower part of the pre-sintering part, and the bottom or the lower part of the cooling part is provided with the fuel air distribution inlet of the pre-sintering part.
7. The apparatus of any of claims 2-6, further comprising:
a cooling section adapted to cool the cement material from the firing section, the cooled cement clinker being adapted to be discharged from the cooling section.
8. The apparatus of claim 8, wherein:
the device is provided with a separation air inlet below the circulating outlet, and separation air is suitable for being introduced into the burning part through the separation air inlet.
9. The apparatus of claim 9, wherein:
the fuel inlet and the fuel air distribution inlet of the burning part are arranged at the top or the upper part of the burning part, and the circulating outlet of the burning part is arranged at the bottom or the lower part of the burning part;
the cooling part and the sintering part are integrally formed in the vertical direction, and the cooling part is positioned below the sintering part;
and a separation air inlet is formed at the bottom or the lower part of the cooling part, and separation air is suitable for entering the sintering part upwards through the separation air inlet.
10. The apparatus of claim 9, wherein:
the cooling part is arranged independently of the sintering part, at least one part of the cooling part is positioned below the sintering part, and the cooling part is communicated with the sintering part through a second conveying pipeline;
the fuel air distribution inlet of the burning part is arranged at the bottom or the lower part of the burning part, the fuel air distribution of the burning part forms the separation air, and the fuel air distribution inlet of the burning part forms the separation air inlet.
11. The apparatus of claim 1, wherein:
the first conveying channel is provided with a cement raw material inlet, a first fuel inlet and a first fuel air distribution inlet.
12. The apparatus of claim 1, further comprising:
the first material returning device is arranged between the material outlet of the first separator and the material inlet of the sintering part.
13. The apparatus of claim 1, further comprising:
and the second material returning device is arranged between the material outlet of the pre-decomposition part and the material inlet of the pre-burning formation part, and the circulating loop comprises the second material returning device.
14. A method of treating a cementitious material comprising the steps of:
providing a circulation loop and a sintering part, wherein the circulation loop comprises a pre-decomposition part, a pre-sintering part, a first separator and a second separator which are sequentially arranged, a flue gas outlet of the first separator is communicated with a material inlet of the second separator through a first conveying channel, and a material outlet of the first separator is communicated with a material inlet of the sintering part; and
such that: the cement material from the material outlet of the pre-decomposition part enters the pre-burning part, a part of the cement material from the material outlet of the pre-burning part enters the material inlet of the second separator through the smoke outlet of the first separator, and the cement material from the material outlet of the second separator enters the pre-decomposition part.
15. The method of claim 15, wherein:
the sintering part is provided with a circulating outlet;
the method comprises the following steps: so that the recycling outlet and the flue gas outlet of the first separator are summed to said first conveying channel.
16. The method according to claim 15 or 16, further comprising the step of:
the flue gases from the flue gas outlet of the first separator are used to heat the cement raw meal that is to be fed into the second separator.
17. The method of claim 17, wherein:
the temperature of the pre-decomposition treatment is controlled between 800 ℃ and 900 ℃; and/or
The temperature of the pre-sintering treatment is controlled between 1000 ℃ and 1200 ℃; and/or
The temperature of the sintering treatment is controlled between 1300 ℃ and 1450 ℃.
18. The method of claim 18, further comprising the step of:
and introducing cooling air to cool the cement material from the sintering part.
19. The method of claim 16, further comprising the step of:
a sorting air inlet is arranged below the circulating outlet;
and introducing separation air into the burning part through the separation air inlet.
20. The method of claim 20, wherein:
the sorting air inlet is a cooling air inlet of cement clinker; or
The separation air inlet is a fuel air distribution inlet of the burning part.
21. The method of claim 16, wherein:
the material inlet of the sintering part is arranged at the top or the upper part of the sintering part, the circulating outlet is arranged at the upper part of the sintering part, the sintering part comprises a sintering furnace in a bubbling bed mode, the lower part of the sintering furnace is provided with a return outlet, the pre-sintering part is provided with a return inlet, and a channel between the return outlet and the return inlet is provided with a return unit;
a cooling part suitable for cooling the cement materials from the burning part is vertically and integrally formed with the pre-burning part, the cooling part is positioned below the pre-burning part, and the cooled cement clinker is suitable for being discharged from the cooling part;
the fuel inlet of the pre-sintering part is arranged at the lower part of the pre-sintering part, the bottom or the lower part of the cooling part is provided with the fuel air distribution inlet of the pre-sintering part,
the method comprises the following steps: cooling air is introduced from the bottom of the cooling part.
22. The method of claim 20, wherein:
a chilling air inlet is arranged above the circulating outlet of the sintering part;
the method comprises the following steps: so that the temperature of the material flowing out of the burning part through the circulating outlet is in the range of 1000-1100 ℃.
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