CN101607797B - Method for producing low alkali cement by using high alkali raw materials - Google Patents
Method for producing low alkali cement by using high alkali raw materials Download PDFInfo
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- CN101607797B CN101607797B CN2009101574801A CN200910157480A CN101607797B CN 101607797 B CN101607797 B CN 101607797B CN 2009101574801 A CN2009101574801 A CN 2009101574801A CN 200910157480 A CN200910157480 A CN 200910157480A CN 101607797 B CN101607797 B CN 101607797B
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- 239000003513 alkali Substances 0.000 title claims abstract description 95
- 239000004568 cement Substances 0.000 title claims abstract description 94
- 239000002994 raw material Substances 0.000 title claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 29
- 239000000460 chlorine Substances 0.000 claims abstract description 67
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 49
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 24
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000000446 fuel Substances 0.000 claims abstract description 16
- 235000019738 Limestone Nutrition 0.000 claims abstract description 4
- 239000006028 limestone Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 47
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 42
- 239000003546 flue gas Substances 0.000 claims description 42
- 125000001309 chloro group Chemical group Cl* 0.000 claims description 25
- 150000001875 compounds Chemical class 0.000 claims description 25
- 239000003500 flue dust Substances 0.000 claims description 19
- 230000009897 systematic effect Effects 0.000 claims description 16
- 238000002156 mixing Methods 0.000 claims description 13
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 8
- 229910052700 potassium Inorganic materials 0.000 claims description 8
- 239000011591 potassium Substances 0.000 claims description 8
- BITYAPCSNKJESK-UHFFFAOYSA-N potassiosodium Chemical compound [Na].[K] BITYAPCSNKJESK-UHFFFAOYSA-N 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 4
- 238000007710 freezing Methods 0.000 claims description 3
- 230000008014 freezing Effects 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims 2
- 239000002699 waste material Substances 0.000 abstract description 13
- 239000000428 dust Substances 0.000 abstract description 10
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 7
- 239000000126 substance Substances 0.000 abstract description 7
- 229910001413 alkali metal ion Inorganic materials 0.000 abstract description 3
- 238000002844 melting Methods 0.000 abstract description 2
- 230000008018 melting Effects 0.000 abstract description 2
- 239000000779 smoke Substances 0.000 abstract 4
- 238000000354 decomposition reaction Methods 0.000 abstract 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 21
- 239000000470 constituent Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 8
- 229910004298 SiO 2 Inorganic materials 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 239000011734 sodium Substances 0.000 description 5
- 239000002918 waste heat Substances 0.000 description 4
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000002585 base Substances 0.000 description 2
- 229910052728 basic metal Inorganic materials 0.000 description 2
- 150000003818 basic metals Chemical class 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 229910021645 metal ion Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241000370738 Chlorion Species 0.000 description 1
- 208000006558 Dental Calculus Diseases 0.000 description 1
- 229910003251 Na K Inorganic materials 0.000 description 1
- 206010037660 Pyrexia Diseases 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002939 deleterious effect Effects 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000002688 persistence Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 229910001414 potassium ion Inorganic materials 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910021653 sulphate ion Inorganic materials 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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Classifications
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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
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
- Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods
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- Curing Cements, Concrete, And Artificial Stone (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a method for producing low alkali cement by using high alkali raw materials, which includes the steps of: putting the raw material limestone with an alkali equivalent about 0.80% into a dry cement rotary kiln through a normal channel for putting the raw material into the kiln; adding chlorine-containing substances into the rotary kiln at the locations of a kiln head, a kiln head fuel burner, a flue chamber at kiln tail end, a pre-decomposition kiln or a pre-burning furnace; opening holes at the bottom part of the pre-decomposition kiln and inducting the chlorine-containing smoke gas enriched in the position into a smoke dust collection system and collecting the smoke dust in the smoke gas. The method for producing low alkali cement by using high alkali raw materials uses the special property that alkali metal ions, chloride ions and sulfate ions mutually affect the melting point temperature under the high temperature coexistence condition, adds the chlorine-containing substances during the production process, and leads the chlorine in wastes to be reacted with the alkali in the raw materials by controlling the proportion between the alkali metal ions, chloride ions and sulfate ions entering the cement kiln, thereby achieving the double effects of reducing the alkali in the cement and processing high-chlorine wastes.
Description
Technical field
The present invention relates to a kind of method of producing cement and disposing waste, in particular, be that a kind of dry cement production line of band suspended preheater and predecomposition furnace and high alkalinity Wingdale of utilizing produced low alkali cement, and the method for high chlorine contents waste such as cooperative disposal PCB.
Background technology
In manufacture of cement, the alkali equivalent of raw material has direct influence to the quality of cement products.If (Na K), can improve the burn-ability of raw material, improves the early strength of raw material to contain micro-alkali in the raw material.If but the alkali equivalent in the raw material is too high, cause the alkali equivalent in the grog to surpass certain scope,, can make that the free ca in the grog improves for example greater than about 0.80% o'clock, cause strength of cement and folding strength to reduce, and influence the work-ing life of buildings.
According to statistics,, cause concrete generation alkali, can make the lost of life of buildings to 1/4th of normal buildings because the alkali equivalent is too high, in addition shorter.Therefore, using low alkali cement is an essential condition that guarantees the buildings life-span.
Produce low alkali cement,, certain requirement is arranged, generally need to use low alkali raw material produce low alkali cement as the alkali equivalent of clay and sandstone etc. just to Wingdale and other raw materials.But in China, a large amount of high-alkali normal limestone resources is arranged, these Wingdales are thrown aside because the alkali equivalent is too high, and this has not only wasted a large amount of resources, has also taken a large amount of soils.
At present, mostly concentrate on both at home and abroad and utilize on the low alkali raw material production low alkali cement, though high-alkali raw material production low alkali cement is had certain research, but research is not deeply, technology is still immature, and the process energy consumption of the high-alkali raw material production low alkali cement of existing use is very big, and technique controlling difficulty is also very big.When utilizing traditional technology, need carry out certain transformation to the production technique of cement clinker with high-alkali raw material production low alkali cement, will be to the deleterious element of cement clinker, as, excessive N a and K separate from kiln system, to reduce the alkali equivalent in the grog.But this need leak informaton from system in a large number, and the amount of leaking informaton can reach the 20-30% of systematic air flow usually, has increased the energy consumption of producing cement clinker greatly, has also increased the difficulty of technology controlling and process simultaneously.Nonetheless, make also to differ in this way and produce qualified low alkali cement surely.Therefore, this technology is not used on a large scale.
Need a large amount of low alkali cements on the market on the one hand, the deficiency of low alkali raw material makes the supply of low alkali cement can not satisfy the demand of low alkali cement far away on the other hand.So, press for a kind of method effective, energy-conservation, that can utilize high-alkali raw material production low alkali cement now.
Summary of the invention
The invention provides the method for the high-alkali raw material production low alkali cement of a kind of usefulness, comprising step:
(1) the alkali equivalent being gone into the kiln channel greater than about 0.80% raw material limestone by raw material drops in the dry method cement rotary kiln;
(2) at kiln hood, kiln hood fuel burner, kiln tail smoke-box, nsp kiln or pre-burner place chlorine-bearing compound is added in the dry method cement rotary kiln, so that the chlorine in the described chlorine-bearing compound consumes the potassium in the raw material;
(3) at the tip position opening of nsp kiln, the chloride flue gas of enrichment is herein introduced in the flue dust collecting system, collected flue dust wherein.
This method mainly utilizes KCl can be converted into solid-state this characteristic by gaseous state in 760 ℃, content by the suitable increase cement kiln Cl of system makes free K combine with Cl, for example, add the Cl that is enough in conjunction with alkali excessive in the high-alkali raw material (K), make it participate in reaction, solid-state KCl is drawn in suitable position in kiln system then, reaches the purpose of K content in the reduction system, thereby realizes utilizing high-alkali raw material production low alkali cement.So contain a large amount of KCl in the flue dust of collecting, recyclablely utilize again as chemical substance.
Preferred described flue dust collecting system comprises mixing section, at first directly enters mixing section after wherein the chloride flue gas of pyritous takes out from the nsp kiln top and freezing air mixes, and flue-gas temperature is descended fast.Therefore, a large amount of potassium ions in the flue gas and chlorion can be combined into Repone K and become solid-state separating out fast.
Preferred used chlorine-bearing compound is high chloride waste, for example is rich in the useless transformer insulated wet goods of polychlorobiphenyl PCB.Like this, the low alkali cement of not only having used high-alkali raw material production can also reach the technique effect of the high chlorine-containing waste of associated treatment.
The chlorinity of the chlorine-bearing compound that uses in preferred this method is greater than about 10%, to reduce to add the volume of material.More preferably, the amount of the chlorine-bearing compound that adjust to add, in mole, the amount of chlorine that makes adding is greater than (amount of potassium sodium amount sum-2 * sulfate radical in the system), and less than the amount of potassium in the system, described system comprises the chlorine-bearing compound of high-alkali raw material and adding.Do not contain potassium, sodium and sulfate ion in the preferred chlorine-bearing compound that adds.Because the molten boiling point of sodium sulfate and vitriolate of tartar is higher than Repone K, the gaseous bases metal ion preferentially combines with sulfate ion, so,, the molar weight of chlorine can be adjusted into poor greater than potassium sodium amount sum and twice sulphate amount in the system for the basic metal in the removal system more effectively.In above-mentioned scope, both the basic metal in the effectively removal system can not introduced excessive chlorine again, avoided causing secondary pollution and tail gas to exceed standard.The alkali equivalent of the low alkali cement of preferably, producing is lower than about 0.60%.
The chloride flue gas that takes out at the tip position of nsp kiln can account for about 1-10% of systematic air flow.Get the top of gas choice of location at nsp kiln, be because chloride flue gas, mainly be that wherein Repone K composition reaches enrichment herein, so only need take out a fraction of flue gas that accounts for systematic air flow, 1-10% for example, can reach the purpose that reduces alkali equivalent and cl content in the production system, and can not influence the operation of whole manufacture of cement, and energy consumption also reduces greatly.More preferably, only need to take out the flue gas that accounts for the about 1-4% of systematic air flow, can realize above-mentioned purpose, further reduced energy consumption at the tip position of nsp kiln.
The high-temperature flue gas that takes out after treatment, temperature is at approximately 300-450 ℃, these high temperature wind can be used to dry the crude fuel of producing cement or reclaim by special equipment, with the thermal source as other purposes.Especially when the flue gas that takes out accounts for about 4-10% of systematic air flow, the heat recuperation of flue gas can be used, for example be used for generating electricity, heat, dry crude fuel or other purposes, thereby can further save the energy.
Description of drawings
Fig. 1 is the schematic flow sheet of explanation an embodiment of the invention.
Embodiment
Below in conjunction with description of drawings the specific embodiment of the present invention; should understand; these embodiments all are exemplary; the present invention is not limited to embodiment disclosed herein, and those skilled in the art can suitably revise according to disclosing herein and not deviate from spirit of the present invention and protection domain.
As shown in Figure 1, as the raw material of producing cement, enter dry method cement rotary kiln by 1 feed system with high-alkali raw material, this dry method cement rotary kiln is a kind of dry method cement rotary kiln with suspended preheater and predecomposition furnace.The alkali equivalent is higher than 0.80% in the raw material in the adding kiln system, generally is not suitable for producing low alkali cement, and wherein the alkali equivalent is with Na
2O+0.658K
2The O meter.According to the alkali equivalent in the high-alkali raw material that adds, a place or many places in kiln hood, kiln hood fuel burner, kiln tail smoke-box, nsp kiln or pre-burner add an amount of chlorine-bearing compound in the kiln with 2 chlorine-bearing compound throwing devices (equipment feeds intake as spray gun or feeding pump etc.).The amount of the chlorine-bearing compound that is added should be enough to reduce alkali equivalent in the finished product cement to the level that allows, and for example less than about 0.6%, obtains the low alkali cement product.Simultaneously, because Na
2SO
4And K
2SO
4Molten boiling point be higher than KCl, the gaseous bases metal ion preferentially combines with sulfate ion, more up hill and dale alkalimetal ion is removed from kiln system for more effective, the amount of the chlorine-bearing compound that may command adds, make wherein the difference of amount that deducts the sulfate radical of twice in the amount of the chlorine of mole greater than the amount of sodium potassium in the kiln system that comprises high-alkali raw material and chlorine-bearing compound, that is the amount of chlorine＞(amount of the amount of sodium potassium-2 * sulfate radical).Make its amount (in mole) simultaneously, exceed standard with secondary pollution and the tail gas of avoiding excessive chlorine to cause less than potassium in the described system.Also should control the kind of the chlorine-bearing compound of adding, in system, not introduce sulfate ion and basic ion again, as far as possible as sodium and potassium.The preferably high chlorine-containing waste of chlorine-bearing compound, for example (PCB is one of 12 kinds of persistence organic pollutants paying close attention in the world at present to polychlorobiphenyl PCB, once be widely used in transformer and capacitor insulation oil, easer, dye dispersant and the agent of agricultural chemicals prolongation of effect etc.), or domestic garbage incineration flyash (flying dust is in the burning city domestic garbage process, residual substance in that flue gas purification system is collected wherein often contains a large amount of chlorine), pesticide D-D T and phenyl-hexachloride etc.When utilizing high-alkali raw material production low alkali cement, also dispose high chloride waste, further realized the technique effect of environmental protection of the present invention.
The high chlorine-bearing compound that adds in the kiln system can be liquid, also can be solid-state, and preferred cl content is more than 10%.The chlorine-bearing compound that adds and the reaction equation of the alkali in the high-alkali raw material are as follows:
When adding PCB:
mK
2O+(29-0.5m)O
2+2C
12H
10-mCl
m→2mKCl+24CO
2+(10-m)H
2O (1)
When adding other chlorinated organics:
zK
2O+(2x+0.5y-0.5z)O
2+2C
xH
yCl
z→2zKCl+2xCO
2+yH
2O (2)
zK
2O+(2x+0.5y-0.5z-r)O
2+2C
xH
yCl
zO
r→2zKCl+2xCO
2+yH
2O (3)
As described in above-mentioned chemical formula, the chlorine-bearing compound that adds enters in the kiln and the high-alkali raw material reaction that has participated in the manufacture of cement, K in the high-alkali raw material combines with Cl in the chlorine-bearing compound of adding, because temperature is higher in the kiln, KCl with gaseous form in the flue gas of cement system in the top of nsp kiln (the about 900-1000 of flue-gas temperature herein ℃) position enrichment.As shown in Figure 1, at 3 nsp kiln tip position openings, the chloride flue gas of enrichment is herein introduced in 4 mixing sections, in 4 mixing sections, flue gas is cooled to below 760 ℃, preferred below 700 ℃, utilize KCl in 760 ℃, can be converted into solid-state this characteristic by gaseous state, KCl is cooled to solid-state separating out, collection contains the ash of KCl, reclaims chemical substance wherein.
The flue dust collecting system can comprise cooling system and dust-removal system.Cooling system can comprise various devices that can fast cooling known in the art such as settling pocket, mixing section, and for example, the chloride flue gas of taking-up is introduced into and mixes with freezing air in the mixing section, and temperature descends fast, and KCl becomes solid-state separating out; The flue dust that settles down is delivered in the ash-storing bin by spiral conveyer.Dust-removal system can comprise the various devices that can be used for collecting flue dust known in the art such as cyclone, bag filter and dust precipitator.The flue dust of collecting can be by pipeline transportation to special storing device, and the potassium sodium content in the flue dust is higher, is used as the chemical industry raw material after can reclaiming and uses.
As shown in Figure 1, chloride flue gas is lowered the temperature in 4 mixing sections, and KCl is cooled to solid-state separating out, and the flue dust that settles down is delivered in 8 ash-storing bins by spiral conveyer.Simultaneously, the flue dust of collecting in 6 tornado dust collector and 7 sack cleaners is also delivered in 8 ash-storing bins by spiral conveyer.KCl in 8 ash-storing bins can reclaim and fully utilize.
The chloride flue gas that takes out can be with its heat recovery and utilization because temperature is higher.When the exhaust gas volumn of taking out is about 1-4% of systematic air flow, can and reclaim the oven dry that flue dust flue gas afterwards is used for the manufacture of cement crude fuel with the cooling dedusting, also can enter atmosphere by total blowdown system.For example, shown in Fig. 1, remaining hot blast is sent to the oven dry crude fuel after 6 tornado dust collector dedustings.When the amount of the flue gas that takes out is about 4-10% of systematic air flow, can use 5 interchanger when in 4 mixing sections, collecting the flue dust that contains KCl and/or after collecting flue dust, heat in the flue gas of drawing stored or be transferred in the other system and use by heating agent, for example afterheat generating system can also be used for waste heat heating.Flue gas after the dedusting can also be sent to and be used to dry crude fuel in the crude fuel preparation system.
The heat that interchanger obtains can further be delivered in the system that can utilize waste heat by medium such as water or thermal oil, for example heating installation or device for generating power by waste heat.In the cement kiln system, the temperature of gas reduces from front to back gradually in the kiln, and temperature of charge raises from front to back gradually.For example, the temperature at nsp kiln top is lower than the temperature of nsp kiln bottom.But from the inside flue gas chlorinity of cement kiln system, the place of enrichment is at the top of nsp kiln.So the present invention is from collecting the angle of Repone K, the place of taking out flue gas is chosen in the nsp kiln top to reach the purpose of the wherein unnecessary alkali of removal.Collect after the Repone K, residue has the words of heat to recycle.That is to say, be not main purpose of the present invention for the recovery of waste heat, and only be to attach a technique effect that obtains.And in the embodiment that reclaims surplus heat, mixing section should be installed in before the interchanger, that is to say, high-temperature flue gas after most of flue dust is removed in the mixing section cooling, enters interchanger earlier again, and surplus heat is reclaimed.This is because if be introduced into interchanger, though reclaimed heat more fully, the flue dust of a large amount of sedimentary KCl of containing is easy to stop up interchanger, causes the damage of equipment, increases production cost.
In addition, volatile matter circulation enrichments such as alkali, chlorine, sulphur in precalcining system, the skinning that causes easily decomposing pre-heating system cooling melting knot stops up, in technical scheme of the present invention, by leaking informaton, the KCl that not only can get rid of its middle and high concentration can also get rid of easy cooling and melt the objectionable impurities that knot causes skinning.
Generally speaking, the present invention has compared following advantage with the technology of traditional production low alkali cement:
1. can utilize high-alkali raw material production low alkali cement, solve a large amount of environmental problems of bringing such as occupation of land on the shelf of high-alkali raw material simultaneously;
2. energy consumption is low, and is less to the cement kiln influence.Because the hot blast rate that will take out from kiln system required for the present invention seldom, only accounts for the 1-10% of system's total blast volume, even still less, 1-4%, be significantly less than the 20-30% of the extraction air quantity that needs in the conventional art, reduced energy consumption, and the adding of chlorine makes the removal of excessive alkali more effective;
3. do not increase the technique controlling difficulty of cement kiln.The air quantity that takes out from cement kiln is more little, just more little to the influence of whole cement industry.Therefore, present method is compared with traditional method, and technique controlling difficulty reduces greatly;
4. the kind of all right cooperative disposal waste when utilizing high-alkali raw material production low alkali cement, and increase cement kiln disposal waste.Because Cl can produce adverse influence to the cement kiln system, as, cause system jams, influence product performance.Therefore, general cement kiln system can not dispose and contain the higher waste of Cl amount.And method provided by the present invention makes Cl play the effect of " catalyzer ", therefore neither can have a negative impact to cement kiln system and cement products itself, and the disposal for high chlorine-containing waste provides a new method again;
5. solve the problem of oven dry crude fuel shortage of heat.In the conventional art, after the cement kiln synergic processing waste, can cause the hot blast water content of oven dry crude fuel to raise, influence drying effect.In preferred implementation of the present invention, can utilize and extract the entrained heat oven dry raw materials and fuel of flue gas out, even the heat that reclaims can be used for generating, heating etc.;
6. reduced the formation of skinning to a certain extent, prolonged the duration of service of equipment, reduced production cost from another angle.
Be example with PCB and flying dust below, exemplary illustration the present invention.
Embodiment 1
3000 tons of certain cement mill production line daily output cement clinkers are (about 3000 tons in hectic fever raw material, about 4500 tons in raw material) (using the dry method cement rotary kiln of band suspended preheater and nsp kiln), in cement kiln extra add the Cl element before the constituent content of raw material and cement products see the following form 1 and table 2.
Table 1 is gone into each constituent content (%) in the hot raw material of kiln
| SiO 2 | Al 2O 3 | Fe 2O 3 | CaO | MgO | K 2O | Na 2O | P 2O 5 | Cl | SO 3 |
| 16.19 | 4.99 | 3.02 | 69.72 | 2.4 | 1.72 | 0.22 | 0.124 | 0.511 | 0.62 |
Each constituent content (%) in table 2 cement
| SiO 2 | Al 2O 3 | Fe 2O 3 | CaO | MgO | K 2O | Na 2O | SO 3 |
| 23.48 | 7.87 | 3.16 | 57.06 | 2.53 | 1.16 | 0.14 | 2.53 |
Under this condition, the alkali equivalent of cement products is 0.14%+0.658 * 1.16%=0.90328%, greater than 0.60%, does not meet the requirement of low alkali cement.
The amount that calculates the chlorine of adding should be greater than 14.7 tons, less than 38.97 tons, and formula (4) and (5) as follows.In kiln system, add PCB30 ton, Cl content 60% by kiln hood.2% of systematic air flow is extracted out from the nsp kiln tip position by the system of leaking informaton, and the flue gas of extracting out is handled, gather up KCl wherein.Add after the PCB, each constituent content of the cement products of producing sees Table 3.
3000 * [35.5 (1.72% ÷, 94 * 2+0.22% ÷, 62 * 2-2 * 0.62% ÷ 80)-0.511%]=14.7 tons (4)
3000 * 35.5 * 1.72% ÷, 94 * 2=38.97 ton (5)
Each constituent content (%) in the cement after the table 3 interpolation Cl
| SiO 2 | Al 2O 3 | Fe 2O 3 | CaO | MgO | K 2O | Na 2O | SO 3 |
| 24.67 | 8.26 | 3.21 | 57.46 | 2.45 | 0.63 | 0.13 | 2.73 |
The alkali equivalent that adds the cement products of producing behind the PCB is 0.13%+0.658 * 0.63%=0.54454%, less than 0.60%, meets the requirement of low alkali cement.
Embodiment 2
3000 tons of cement clinkers of certain cement mill production line daily output (dry method cement rotary kiln of band suspended preheater and nsp kiln), in the cement kiln extra add the Cl element before the constituent content of raw material and cement products shown in table 4, table 5.
Table 4 is gone into each constituent content (%) in the hot raw material of kiln
| SiO 2 | Al 2O 3 | Fe 2O 3 | CaO | MgO | K 2O | Na 2O | P 2O 5 | Cl | SO 3 |
| 16.29 | 5.29 | 3.12 | 68.91 | 2.35 | 1.82 | 0.27 | 0.12 | 0.471 | 0.65 |
Each constituent content (%) in table 5 cement
| SiO 2 | Al 2O 3 | Fe 2O 3 | CaO | MgO | K 2O | Na 2O | SO 3 |
| 23.38 | 7.88 | 3.19 | 57.06 | 2.63 | 1.26 | 0.16 | 2.73 |
The amount that calculates the chlorine of adding should be greater than 19.07 tons, less than 41.24 tons of formula (6) and (7) as follows.In kiln system, per hour add 7.5 tons of flying dusts, Cl content 12% by kiln hood.And by 10% extraction of device provided by the invention with systematic air flow, through entering interchanger after the mixing section cooling, with heat-conducting oil heating in the interchanger, thermal oil provides heat for other heat-needing facility to hot flue gas more earlier.Flue gas after coming out from interchanger is through the cyclone dedusting, and collects the dust that contains KCl.Part gas is used for oven dry preparation cement raw fuel, and other other enter qualified discharge after the sack cleaner purifying treatment.Add after the flying dust, each constituent content of the cement products of producing is as shown in table 6.
3000 * [35.5 (1.82% ÷, 94 * 2+0.27% ÷, 65 * 2-2 * 0.65% ÷ 80)-0.511%]=19.07 tons (6)
3000 * 35.5 * 1.82% ÷, 94 * 2=41.24 ton (7)
Each constituent content (%) in the cement after the table 6 interpolation Cl
| SiO 2 | Al 2O 3 | Fe 2O 3 | CaO | MgO | K 2O | Na 2O | SO 3 |
| 23.58 | 8.19 | 3.18 | 59.06 | 2.5 | 0.6 | 0.12 | 2.68 |
The alkali equivalent that adds the cement products of producing behind the flying dust is 0.12%+0.658 * 0.60%=0.5148%, less than 0.60%, meets the requirement of low alkali cement.
Though described the present invention in conjunction with specific embodiments at this; but be understood that the present invention is not limited to these disclosed embodiments; on the contrary, the present invention's scope required for protection contains various changes and the equivalent in the spirit and scope that are included in claims.
Claims (17)
1. method with high-alkali raw material production low alkali cement, comprising step:
(1) the alkali equivalent being gone into the kiln channel greater than 0.80% raw material limestone by raw material drops in the dry method cement rotary kiln;
(2) place or the many places in kiln hood, kiln hood fuel burner, kiln tail smoke-box, nsp kiln or pre-burner add chlorine-bearing compound in the dry method cement rotary kiln, so that the chlorine in the described chlorine-bearing compound consumes the potassium in the raw material;
(3) at the tip position opening of nsp kiln, the chloride flue gas of enrichment is herein introduced in the flue dust collecting system, collected flue dust wherein.
2. the method for claim 1, wherein said flue dust collecting system comprises mixing section, described chloride flue gas at first enters in the mixing section and mixes with freezing air, so that described chloride flue-gas temperature descends fast.
3. method as claimed in claim 1 or 2, the chlorinity of wherein said chlorine-bearing compound is greater than 10%.
4. method as claimed in claim 1 or 2, wherein, adjust the amount of the described chlorine-bearing compound that adds, in mole, the amount of chlorine that makes adding is greater than (amount of potassium sodium amount sum-2 * sulfate radical in the system), and less than the amount of potassium in the system, described system comprises the chlorine-bearing compound of described high-alkali raw material and adding.
5. method as claimed in claim 3 wherein, is adjusted the amount of the described chlorine-bearing compound that adds, in mole, the amount of chlorine that makes adding is greater than (amount of potassium sodium amount sum-2 * sulfate radical in the system), and less than the amount of potassium in the system, described system comprises the chlorine-bearing compound of described high-alkali raw material and adding.
6. as each described method in the claim 1,2 or 5, the alkali equivalent of wherein said low alkali cement is lower than 0.60%.
7. method as claimed in claim 3, the alkali equivalent of wherein said low alkali cement is lower than 0.60%.
8. method as claimed in claim 4, the alkali equivalent of wherein said low alkali cement is lower than 0.60%.
9. as each described method in the claim 1,2 or 5, wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 1-10% of systematic air flow.
10. method as claimed in claim 3, wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 1-10% of systematic air flow.
11. method as claimed in claim 4, wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 1-10% of systematic air flow.
12. method as claimed in claim 9, wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 1-4% of systematic air flow.
13. as claim 10 or 11 described methods, wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 1-4% of systematic air flow.
14. method as claimed in claim 9 when wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 4-10% of systematic air flow, comprises that further the heat in the chloride flue gas that will take out is recycled by interchanger.
15., when wherein the chloride flue gas that takes out at the tip position of nsp kiln accounts for the 4-10% of systematic air flow, comprise that further the heat in the chloride flue gas that will take out is recycled by interchanger as claim 10 or 11 described methods.
16. method as claimed in claim 14, wherein said recycling comprises: with the crude fuel of described heat generating, heating and oven dry preparation cement.
17. method as claimed in claim 15, wherein said recycling comprises: with the crude fuel of described heat generating, heating and oven dry preparation cement.
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| CN1603268A (en) * | 2004-09-27 | 2005-04-06 | 武汉理工大学 | Preparation method of phosphorus slag portland cement chamotte and preparation method thereof |
| CN101050070A (en) * | 2007-03-30 | 2007-10-10 | 山东金鲁城有限公司 | Method for producing Portland cement |
| WO2007128619A1 (en) * | 2006-05-10 | 2007-11-15 | F L Smidth A/S | Method and plant for manufacturing cement clinker |
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| CN1603268A (en) * | 2004-09-27 | 2005-04-06 | 武汉理工大学 | Preparation method of phosphorus slag portland cement chamotte and preparation method thereof |
| WO2007128619A1 (en) * | 2006-05-10 | 2007-11-15 | F L Smidth A/S | Method and plant for manufacturing cement clinker |
| CN101050070A (en) * | 2007-03-30 | 2007-10-10 | 山东金鲁城有限公司 | Method for producing Portland cement |
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