CN102730731B - Lime powder production equipment taking bagasse as fuel - Google Patents
Lime powder production equipment taking bagasse as fuel Download PDFInfo
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- CN102730731B CN102730731B CN201210257676.XA CN201210257676A CN102730731B CN 102730731 B CN102730731 B CN 102730731B CN 201210257676 A CN201210257676 A CN 201210257676A CN 102730731 B CN102730731 B CN 102730731B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/20—Waste processing or separation
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Abstract
The invention discloses lime powder production equipment taking bagasse as a fuel. The set of lime powder production equipment mainly comprises a bagasse combustion furnace, a parallel flow decomposition furnace, a lime powder cooling machine and a raw material preheater. The lime powder production equipment takes bagasse which is the waste of a cane sugar factory as the fuel, and calcium carbonate with appropriate particle size of 80-120 microns as a raw material. The lime powder production equipment is very short in time and high in efficiency in firing lime powder, and recovers the waste heat in kiln gas of the decomposition furnace, thus saving energy.
Description
Invention field
The present invention relates to a kind of lime production device, particularly relating to a kind of bagasse is the lime powder production equipment of fuel.
Background technology
Lime is multiduty material, at building, sugaring and steel industry, all widely applies.The vertical furnaces that use in small-scale production, energy consumption is high more.More than cement industry 100t/d, in large-scale manufacture of cement, adopt precalcining device, Pyatyi eddy flow preheater and rotary kiln supporting more.In its precalcining device, calcium carbonate and high-temperature flue gas adverse current rotatablely move, and calcium carbonate powder resolves into lime under suspended state, required time only approximately 10 seconds.In this device because industrial scale is large, require efficient and simple for structure, adopted material and hot gas countercurrent movement lime decomposing furnace, adverse current decomposing furnace to operation control require very high, Controlling System that need supporting precision.When small scale is produced, the poor stability of adverse current decomposing furnace work.Sugar enterprise generally needs amount of lime below 300t/d, require to produce lime process stabilization, control simple, reduced investment.Directly adopt the adverse current decomposing furnace that manufacture of cement is used to be not suitable for for sugar refinery production lime.Sugar refinery will produce lime rapidly, still needs to study the decomposing furnace of new texture and principle.
Number of patent application 101010264386.9 adopts known manufacture of cement to support the use adverse current decomposing furnace and Pyatyi eddy flow preheater, uses gas production lime, lacks novelty.And sugar refinery is without coal gas, this technology is not suitable for sugar refinery yet.
Another deficiency of number of patent application 101010264386.9 is to need supporting grate cooler cooling for lime.Grate cooler is located in high temperature cylinder, and movable fire grate is worked in cylinder, and easy break-down is safeguarded also inconvenient.
Summary of the invention
The object of the invention is for sugar enterprise utilizes own bagasse is fuel, and a kind of lime powder production method and device of reliable, energy-conservation, reduced investment is provided.
The technical scheme that the present invention solves the problems of the technologies described above is as follows.
1. the lime powder production equipment that bagasse is fuel, is mainly comprised of bagasse roasting kiln Traffic Decomposition stove, lime powder cooler and feed preheater.
1) described bagasse roasting kiln is mainly comprised of bagasse burner, internal combustion cylinder, outer combustion barrel, high-temperature flue gas Guan He ash discharge mechanism; Wherein: internal combustion cylinder and outer combustion barrel coaxial line, bagasse burner is connected in internal combustion cylinder top, and the bottom of internal combustion cylinder is communicated with outer combustion barrel, and outer combustion barrel bottom picks out grey mechanism, the top of outer combustion barrel connects high-temperature flue gas pipe, and high-temperature flue gas pipe connects and Traffic Decomposition stove.
During production, the high-temperature flue gas that bagasse enters internal combustion cylinder burning Bing Sui generation by bagasse burner drops to internal combustion cylinder bottom, bagasse ashes enter ash discharge mechanism, high-temperature flue gas enters outer combustion barrel rising separated with flue dust, to outer combustion barrel top, by high-temperature flue gas pipe, discharge, complete the process of bagasse roasting kiln burning bagasse preparing high-temp flue gas.
2) described and Traffic Decomposition stove is mainly decomposed section, gas solid separation section, lime powder bin and central row smoke pipe and is formed by mixing tube, eddy flow.Wherein: mixing tube is Y-tube, one end of Y-tube level is connected with the high-temperature flue gas pipe of bagasse roasting kiln, the other end of Y-tube level tangentially stretches into and the eddy flow of Traffic Decomposition stove decomposes section, and Y-tube vertical end is connected with the Paris white outlet of feed preheater; Eddy flow decomposes pars infrasegmentalis and is connected with gas solid separation section, termination lime powder bin under gas solid separation section;
During production, high-temperature flue gas and raw material Paris white are mixed into the also eddy flow of Traffic Decomposition stove at mixing tube and decompose section, at eddy flow, decompose section raw material Paris white is resolved into lime powder, declining, it is separated with flue gas to enter gas solid separation section lime powder, flue gas is discharged by central row smoke pipe, lime powder enters lime powder bin, completes the whole process that Paris white reaction generates lime powder.
3) described lime powder cooler import connects the also lime powder outlet of the lime powder bin of Traffic Decomposition stove; Lime powder cooler can be any powder material cooler, preferably turns round cooler.
During production, the high temperature lime powder in lime powder bin enters lime powder cooler, in lime powder cooler, is cooled to normal temperature, completes the cooling process of lime powder.
4) described feed preheater, import connect respectively Paris white handling equipment and and the central row smoke pipe of Traffic Decomposition stove, Paris white after preheating connects mixing tube through the outlet lock air lock of feed preheater, and the flue gas after heat exchange connects off gas treatment through the outlet of feed preheater.Feed preheater can be any powder material preheater, preferred multistage feed preheater, and multistage feed preheater is connected in series by single feed preheater.
During production, jointly enter low temperature feedstock Paris white and the high-temperature flue gas of multistage feed preheater, gas solid separation after thermal exchange in multistage feed preheater, raw material Paris white obtains preheating, and flue gas is lowered the temperature, and completes the whole process of raw material Paris white preheating.
High-temperature flue-gas prepared by above-mentioned bagasse roasting kiln is 880 ℃～960 ℃, more preferably 940 ℃～950 ℃.
The height of the internal combustion cylinder of above-mentioned bagasse roasting kiln should be greater than 6m by bagasse burner inlet to the distance of bottom ash discharge mechanism; The thermal capacitance load of internal combustion cylinder should be got 350～550kw/m
3, preferred 450kw/m
3.
The section gas flow rate that eddy flow above-mentioned and Traffic Decomposition stove decomposes in section is preferably 3m/s～6m/s, and high-temperature flue gas is preferably 5S～8S with the time that calcium carbonate stream contact, and enters the also granularity of Traffic Decomposition stove raw material Paris white and is preferably 80 μ m～120 μ m.
To decompose section diameter identical in order to fall cone, upper end and eddy flow for the gas solid separation section of above-mentioned and Traffic Decomposition stove, is highly 2 times of eddy flow decomposition section diameters, and the bottom of falling cone is established lime powder and exported.
Gas solid separation section above-mentioned and Traffic Decomposition stove is upper end and to decompose section diameter identical for eddy flow, and lower end diameter is expanded as diffusion type cylindrical shell, the height of cylindrical shell is upper end diameter 2～3 times, the angle of cylindrical shell inclined-plane and vertical axis is 6 degree.Between gas solid separation section and lime powder bin, establishing cone angle is 45～60 ° of taper radiation shields, gap between taper radiation shield periphery and gas solid separation section lower shell is the passage that lime powder enters lime powder bin, and it is the breather hole of 0.04～0.05 times that eddy flow decomposes section diameter that a diameter is stayed on taper radiation shield top.
In above-mentioned multistage feed preheater, the structure of every grade of feed preheater is identical with general tornado dust collector.The connection of every grade of feed preheater is: the gas after next stage feed preheater gas solid separation, the gas feed of the feed preheater of access upper level; The solid outlet of upper level feed preheater, connects the solids inlet of next stage feed preheater through lock air lock.Gas after feed preheater separation at the highest level is discharged after feed preheater, connects induced draft fan to entering flare system.The feed preheater gas feed of subordinate, connects and the central row smoke pipe of Traffic Decomposition stove.The calcium carbonate powder that Cong subordinate feed preheater lower part outlet is discharged, connects the also Y-tube vertical end calcium carbonate powder import of the mixing tube of Traffic Decomposition stove.
Wherein: feed preheater inlet pipe and gas exhausting tube rate of flow of fluid are 16m/s～22m/s, section gas speed is 3m/s～6m/s; The progression of feed preheater is 2 grades～6 grades, preferably 3 grades～5 grades.
Beneficial effect of the present invention:
1, can utilize the waste material bagasse in sugar refinery to produce lime powder;
2, method production lime powder energy consumption of the present invention is low;
3, lime powder production equipment of the present invention is simple, and production stability is good, reduced investment;
Accompanying drawing explanation
The lime powder production scheme that bagasse is fuel is take in Fig. 1 the present invention;
Fig. 2 bagasse roasting kiln 1 structural representation;
Fig. 3 Traffic Decomposition stove 2 structure 1 schematic diagram.
Fig. 4 Traffic Decomposition stove 2 structure 2 schematic diagram.
Wherein: bagasse roasting kiln 1, and Traffic Decomposition stove 2, lime cooler 3, raw material preheating 4, bagasse burner 5, internal combustion cylinder 6, outer combustion barrel 7, high-temperature flue gas pipe 8 and ash discharge mechanism 9, mixing tube 10, eddy flow decompose section 11, gas solid separation section 12, lime powder bin 13 and central row smoke pipe 14, taper radiation shield 15, bagasse feeding machine 16, raw material Paris white handling equipment 17, lock air lock 18, induced draft fan 19, flare system 20, breather hole 21.
Embodiment
Below in conjunction with accompanying drawing, the present invention is further illustrated.
Bagasse of the present invention be the lime powder production method of fuel and apparatus structure as shown in Figure 1, Figure 2 and Figure 3, the lime powder production equipment that a kind of bagasse is fuel, is comprised of bagasse roasting kiln 1 Traffic Decomposition stove 2, lime powder cooler 3 and feed preheater 4.
1) described bagasse roasting kiln 1 is comprised of bagasse burner 5, internal combustion cylinder 6, outer combustion barrel 7, high-temperature flue gas pipe 8 and ash discharge mechanism 9.
Wherein: internal combustion cylinder 6 and outer combustion barrel 7 coaxial lines, bagasse burner 5 is connected in internal combustion cylinder 6 tops, and the bottom of internal combustion cylinder 6 is communicated with outer combustion barrel 7, and outer combustion barrel 7 bottoms pick out grey mechanism 9, the top of outer combustion barrel 7 connects high-temperature flue gas pipe 8, and high-temperature flue gas pipe 8 connects and Traffic Decomposition stove 2;
The high-temperature flue gas that bagasse enters the 6 burning Bing Sui generations of internal combustion cylinder by bagasse feeding machine 16 input bagasse burners 5 declines, to internal combustion cylinder 6 bottoms, ashes enter ash discharge mechanism 9, high-temperature flue gas enters outer combustion barrel 7 risings separated with flue dust, to outer combustion barrel top, by high-temperature flue gas pipe 8, discharge for 7, complete the process of bagasse roasting kiln burning bagasse preparing high-temp flue gas.
2) described and Traffic Decomposition stove 2 is decomposed section 11, gas solid separation section 12, lime powder bin 13 and central row smoke pipe 14 and is formed by mixing tube 10, eddy flow;
Wherein: mixing tube 10 one end connect the high-temperature flue gas pipe 8 of bagasse roasting kiln 1, one end connects the raw material Paris white outlet of feed preheater 4, and the tangential Shen of the other end enters and the eddy flow of Traffic Decomposition stove 2 decomposes section 11; Eddy flow decomposes section 11 bottoms and connects gas solid separation section 12,12 times termination lime powder bins 13 of gas solid separation section, high-temperature flue gas and Paris white are mixed into the also eddy flow of Traffic Decomposition stove 2 at mixing tube 10 and decompose section 11, at eddy flow, decompose section 11 and resolve into lime powder, declining, it is separated with flue gas to enter gas solid separation section 12 lime powders, flue gas is discharged by central row smoke pipe 12, and lime powder enters lime powder bin 13, completes the whole process that Paris white reaction generates lime powder;
3) described lime powder cooler 3 connects lime powder bin 13 lime powder outlets.Lime powder cooler 3 can be any powder material cooler, preferably turns round cooler;
High temperature lime powder in lime powder bin 13 enters lime powder cooler 3, in lime powder cooler 3, is cooled to normal temperature, completes the cooling process of lime powder;
4) described feed preheater 4, import connect low temperature Paris white handling equipment 17 and high temperature smoke pipe (as and the central row smoke pipe 14 of Traffic Decomposition stove 2), Paris white outlet through preheating connects the also mixing tube 10 of Traffic Decomposition stove, and after heat exchange, the outlet of low-temperature flue gas connects off gas treatment.Feed preheater 4 can be any powder material preheater, preferred multistage feed preheater;
Low temperature feedstock Paris white and the high-temperature flue gas of common incoming stock preheater 4, gas solid separation after thermal exchange in feed preheater 4, raw material Paris white obtains preheating, and flue gas is lowered the temperature, and completes the whole process of raw material Paris white preheating.Multistage feed preheater is a plurality of feed preheater 4 series windings.
The high-temperature flue-gas of above-mentioned bagasse roasting kiln 1 preparation is 880 ℃～960 ℃, more preferably 940 ℃～950 ℃;
Height-bagasse burner 5 entrances of above-mentioned internal combustion cylinder 6 to the distance of bottom ash discharge mechanism 9 should be greater than 6m; Internal combustion cylinder 6 thermal capacitance loads should be got 350～550kw/m
3, preferred 450kw/m
3;
The section gas flow rate that above-mentioned eddy flow decomposes in section 11 is preferably 3m/s～6m/s, and high-temperature flue gas is preferably 5S～8S with the time that calcium carbonate stream contact; Enter the also raw material Paris white granularity of Traffic Decomposition stove 2 and be preferably 80 μ m～120 μ m;
Above-mentioned gas solid separation section 12 is that upper end is identical with eddy flow decomposition section 11 diameters, highly for eddy flow, decomposes the cone of 2 times of section 11 diameters.Lime powder outlet is established at cone top;
Above-mentioned gas solid separation section 12 is that upper end is identical with eddy flow decomposition section diameter, the diffusion type cylindrical shell that lower end diameter expands.The height of diffusion type cylindrical shell is 2～3 times of inlet diameter, and spread angle (angle of inclined-plane and vertical axis) is 6 degree.It is 45～60 ° of taper radiation shields 15 that 13 of gas solid separation section 12 and lime powder bins are established cone angle, gap between taper radiation shield 15 peripheries and gas solid separation section 12 lower shells is the passage that lime powder enters lime powder bin 13, and it is the breather hole 21 of 0.04～0.05 times that eddy flow decomposes section 11 diameters that a diameter is stayed on taper radiation shield 15 tops;
In above-mentioned multistage feed preheater, the structure of every grade of feed preheater 4 is identical with general tornado dust collector.The connection of every grade of feed preheater 4 is: the gas after next stage feed preheater 4 gas solid separation, the gas feed of the feed preheater 4 of access upper level; The solid outlet of upper level feed preheater 4, connects the gas feed of next stage feed preheater 4 through lock air lock 18.Gas after feed preheater 4 separation at the highest level is discharged after feed preheater 4, connects induced draft fan 19 to entering flare system 20.Feed preheater 4 gas feeds of subordinate connect and the central row smoke pipe 14 of Traffic Decomposition stove 2.The Paris white that Cong subordinate feed preheater 4 lower part outlets are discharged connects the also Y-tube vertical end Paris white import of the mixing tube 10 of Traffic Decomposition stove 2.
Wherein: the inlet pipe of feed preheater 4 and gas exhausting tube rate of flow of fluid are 16m/s～22m/s, section gas speed is 3m/s～6m/s; The progression of feed preheater 4 is 2 grades～6 grades, preferably 3 grades～5 grades.
Embodiment
The method that bagasse is fuel production lime powder is take in the present invention, and concrete steps are as follows:
1) calcium carbonate is processed into the Paris white of fineness 80 μ m～120 μ m.
2) bagasse is sent into bagasse burner by feeding machine, with the air mixed that blower fan sprays into, spray into bagasse roasting kiln, adjust air capacity and pressure into stove, use bagasse fully to burn, control outlet of still flue-gas temperature in 880 ℃～950 ℃.
3) by the flue gas of 880 ℃～950 ℃, after mixing, mixing tube enters and the rotating decomposition section of Traffic Decomposition stove with sending into through the raw material Paris white of approximately 350 ℃ of feed preheater preheatings, in rotating decomposition section, also stream rotation declines, and through 5～8s, Paris white resolves into lime.Lime powder is with flue gas after segregation section is separated, and lime powder drains into lime powder bin, and temperature is reduced to the flue gas of approximately 500 ℃ and is expelled to feed preheater from the top of decomposing furnace.
4), from the lime powder that also Traffic Decomposition stove lime powder bin is discharged, enter after lime powder cooler is cooled to normal temperature and obtain product lime powder.
5) from and Traffic Decomposition stove top discharge the flue gas of approximately 500 ℃, with the cold Paris white from the input of raw material Paris white handling equipment, in feed preheater and flow rotating contact heat exchange, by the preheating of raw material Paris white.After gas solid separation, the top that gas rises to multistage feed preheater becomes the gas of approximately 100 ℃, discharge or recovery after purifying.Raw material Paris white through preheating enters step 3.
Embodiment 2
The device of producing 65t/d lime of take is example, and the Paris white amount that needs granularity 80～120 μ is 120t/d.
1, bagasse roasting kiln
Decomposing 1kg calcium carbonate needs the heat of 1777 kilojoules, in the thermo-efficiency 50% of decomposing furnace, needs to consume the about 55t/d of bagasse that calorific value is 7961KJ/kg.Thermal capacitance load is pressed 450kw/m
3, calculate and need the about 11.26m of internal combustion cylinder volume
3.The height of bagasse roasting kiln is got 6～8m, calculates internal combustion cylinder diameter and is about 1.34～1.54m.
2 and Traffic Decomposition stove
By burning bagasse 2291kgh, the flue gas 4048Hm that generation gas concentration lwevel is 10.77%
3/ h.The volume of 1000 ℃ of high temperature (ignoring pressure) is: 18872m
3/ h, enters and the flow velocity of Traffic Decomposition stove is got 12m/s, and calculating mixing tube internal diameter is 750mm.
And Traffic Decomposition stove decomposition 5000kg/h calcium carbonate, discharge carbonic acid gas 1120Hm
3/ d.Go out and Traffic Decomposition stove Decomposition of Calcium Carbonate after furnace gas cumulative volume be 5068Hm
3/ h, temperature is reduced to 500 ℃, and actual volume is 14350m
3/ h.Getting central row smoke pipe internal diameter is 750mm, and central row smoke pipe gas speed is 9m/s.
Getting central row smoke pipe external diameter is 1050mm, and eddy flow decomposes the gas speed 5m/s of section, counts to such an extent that the eddy flow internal diameter that decomposes section is 3.85m, the mid-diameter of flow rotation circle is 2.45m, the about 1.5s of time often turning around, rotates 5 circles and decomposes 7.5s, and eddy flow decomposes section and highly gets 3.75m.
3, revolution cooler
Employing internal diameter is 800mm, length 5m cylindrical shell.10 degree are got at the inclination angle of machine, and filling ratio gets 17%, and the rotating speed of machine is got 0.43～0.46r/min.In machine, residence time of material is approximately 79 minutes.
Claims (7)
1. the lime powder production equipment that bagasse is fuel, is mainly comprised of bagasse roasting kiln Traffic Decomposition stove, lime powder cooler and feed preheater;
1) described bagasse roasting kiln is mainly comprised of bagasse burner, internal combustion cylinder, outer combustion barrel, high-temperature flue gas Guan He ash discharge mechanism; Wherein: internal combustion cylinder and outer combustion barrel coaxial line, bagasse burner is connected in internal combustion cylinder top, and the bottom of internal combustion cylinder is communicated with outer combustion barrel, and outer combustion barrel bottom picks out grey mechanism, the top of outer combustion barrel connects high-temperature flue gas pipe, and high-temperature flue gas pipe connects and Traffic Decomposition stove;
During production, the high-temperature flue gas that bagasse enters internal combustion cylinder burning Bing Sui generation by bagasse burner drops to internal combustion cylinder bottom, bagasse ashes enter ash discharge mechanism, high-temperature flue gas enters outer combustion barrel rising separated with flue dust, to outer combustion barrel top, by high-temperature flue gas pipe, discharge, complete the process of bagasse roasting kiln burning bagasse preparing high-temp flue gas;
2) described and Traffic Decomposition stove is mainly decomposed section, gas solid separation section, lime powder bin and central row smoke pipe and is formed by mixing tube, eddy flow; Wherein: mixing tube is Y-tube, one end of Y-tube level is connected with the high-temperature flue gas pipe of bagasse roasting kiln, the other end of Y-tube level tangentially stretches into and the eddy flow of Traffic Decomposition stove decomposes section, and Y-tube vertical end is connected with the Paris white outlet of feed preheater; Eddy flow decomposes pars infrasegmentalis and is connected with gas solid separation section, termination lime powder bin under gas solid separation section;
During production, high-temperature flue gas and raw material Paris white are mixed into the also eddy flow of Traffic Decomposition stove at mixing tube and decompose section, at eddy flow, decompose section raw material Paris white is resolved into lime powder, declining, it is separated with flue gas to enter gas solid separation section lime powder, flue gas is discharged by central row smoke pipe, lime powder enters lime powder bin, completes the whole process that Paris white reaction generates lime powder;
3) described lime powder cooler import connects the also lime powder outlet of the lime powder bin of Traffic Decomposition stove; Lime powder cooler is any powder material cooler;
During production, the high temperature lime powder in lime powder bin enters lime powder cooler, in lime powder cooler, is cooled to normal temperature, completes the cooling process of lime powder;
4) described feed preheater, import connect respectively Paris white handling equipment and and the central row smoke pipe of Traffic Decomposition stove, Paris white after preheating connects mixing tube through the outlet lock air lock of feed preheater, and the flue gas after heat exchange connects flare system through the outlet of feed preheater; Feed preheater is multistage feed preheater, and multistage feed preheater is connected in series by single feed preheater;
During production, jointly enter low temperature feedstock Paris white and the high-temperature flue gas of multistage feed preheater, gas solid separation after thermal exchange in multistage feed preheater, raw material Paris white obtains preheating, and flue gas is lowered the temperature, and completes the whole process of raw material Paris white preheating.
2. the lime powder production equipment that bagasse claimed in claim 1 is fuel, is characterized in that, high-temperature flue-gas prepared by above-mentioned bagasse roasting kiln is 880 ℃～960 ℃.
3. the lime powder production equipment that bagasse claimed in claim 1 is fuel, is characterized in that, the height of the internal combustion cylinder of above-mentioned bagasse roasting kiln is greater than 6m by bagasse burner inlet to the distance of bottom ash discharge mechanism; The thermal capacitance load of internal combustion cylinder is got 350～550kW/m
3.
4. the lime powder production equipment that bagasse claimed in claim 1 is fuel, it is characterized in that, the section gas flow rate that eddy flow above-mentioned and Traffic Decomposition stove decomposes in section is 3m/s～6m/s, high-temperature flue gas is 5s～8s with the time that calcium carbonate stream contact, and entering the also granularity of Traffic Decomposition stove raw material Paris white is 80 μ m～120 μ m.
5. the lime powder production equipment that bagasse claimed in claim 1 is fuel, it is characterized in that, gas solid separation section above-mentioned and Traffic Decomposition stove is that inverted cone, upper end are identical with eddy flow decomposition section diameter, is highly that eddy flow decomposes 2 times of section diameters, and inverted cone bottom is established lime powder and exported.
6. the lime powder production equipment that bagasse claimed in claim 1 is fuel, it is characterized in that, gas solid separation section above-mentioned and Traffic Decomposition stove is that upper end is identical with eddy flow decomposition section diameter, lower end diameter is expanded as diffusion type cylindrical shell, the height of cylindrical shell is 2～3 times of upper end diameter, and the angle of cylindrical shell inclined-plane and vertical axis is 6 degree; Between gas solid separation section and lime powder bin, establishing cone angle is 45～60 ° of taper radiation shields, gap between taper radiation shield periphery and gas solid separation section lower shell is the passage that lime powder enters lime powder bin, and it is the breather hole of 0.04～0.05 times that eddy flow decomposes section diameter that a diameter is stayed on taper radiation shield top.
7. the lime powder production equipment that bagasse claimed in claim 1 is fuel, it is characterized in that, in above-mentioned multistage feed preheater, the structure of every grade of feed preheater is identical with general tornado dust collector, the connection of every grade of feed preheater is: the gas after next stage feed preheater gas solid separation, the gas feed of the feed preheater of access upper level; The solid outlet of upper level feed preheater, connects the solids inlet of next stage feed preheater through lock air lock, and the gas after feed preheater separation at the highest level is discharged after feed preheater, connects induced draft fan to entering flare system; The Paris white that the feed preheater gas feed of subordinate connects and the central row smoke pipe ，Cong subordinate feed preheater lower part outlet of Traffic Decomposition stove is discharged connects and the Y-tube vertical end Paris white import of the mixing tube of Traffic Decomposition stove;
Wherein: feed preheater inlet pipe and gas exhausting tube rate of flow of fluid are 16m/s～22m/s, section gas speed is 3m/s～6m/s; The progression of feed preheater is 2 grades～6 grades.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210257676.XA CN102730731B (en) | 2012-07-24 | 2012-07-24 | Lime powder production equipment taking bagasse as fuel |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210257676.XA CN102730731B (en) | 2012-07-24 | 2012-07-24 | Lime powder production equipment taking bagasse as fuel |
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| CN102730731A CN102730731A (en) | 2012-10-17 |
| CN102730731B true CN102730731B (en) | 2014-02-05 |
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| CN103524057A (en) * | 2013-10-22 | 2014-01-22 | 瓮福（集团）有限责任公司 | Method for preparing lime by using byproduct calcium carbonate obtained from preparation of ammonium sulfate by phosphogypsum as raw material |
| CN113446607A (en) * | 2019-12-12 | 2021-09-28 | 黄颖媛 | Heat storage baffling grading pretreatment module for hazardous waste treatment of electronic products |
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| GB1476963A (en) * | 1974-05-31 | 1977-06-16 | Schoppe F | Production of calcined lime |
| JP5088919B2 (en) * | 2005-05-13 | 2012-12-05 | 太平洋セメント株式会社 | Cement baking apparatus and waste treatment method |
| CN101570406A (en) * | 2009-06-11 | 2009-11-04 | 北京市琉璃河水泥有限公司 | Calcination process of active lime |
| CN101987783B (en) * | 2010-08-27 | 2012-08-22 | 山东钢铁股份有限公司 | Method for producing active pulverized lime by utilizing coal gas to calcine limestone through suspended state pre-heating decomposing furnace |
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