CN108910836A - A kind of technique and device of gypsum Sulphuric acid coproduction lime - Google Patents
A kind of technique and device of gypsum Sulphuric acid coproduction lime Download PDFInfo
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- CN108910836A CN108910836A CN201811119583.4A CN201811119583A CN108910836A CN 108910836 A CN108910836 A CN 108910836A CN 201811119583 A CN201811119583 A CN 201811119583A CN 108910836 A CN108910836 A CN 108910836A
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- lime
- gypsum
- sulphuric acid
- technique
- preheater
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- 239000010440 gypsum Substances 0.000 title claims abstract description 75
- 229910052602 gypsum Inorganic materials 0.000 title claims abstract description 75
- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 69
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 69
- 239000004571 lime Substances 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 68
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 235000011149 sulphuric acid Nutrition 0.000 title claims abstract description 56
- 239000001117 sulphuric acid Substances 0.000 title claims abstract description 56
- 238000001035 drying Methods 0.000 claims abstract description 78
- 239000002994 raw material Substances 0.000 claims abstract description 59
- 238000000227 grinding Methods 0.000 claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 18
- 239000000446 fuel Substances 0.000 claims abstract description 16
- 238000001354 calcination Methods 0.000 claims abstract description 13
- 238000002425 crystallisation Methods 0.000 claims abstract description 9
- 230000008025 crystallization Effects 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 53
- 239000000463 material Substances 0.000 claims description 25
- 239000000571 coke Substances 0.000 claims description 14
- 239000000428 dust Substances 0.000 claims description 14
- 239000002006 petroleum coke Substances 0.000 claims description 9
- 239000004575 stone Substances 0.000 claims description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 5
- 239000006071 cream Substances 0.000 claims description 4
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 claims description 3
- 239000003830 anthracite Substances 0.000 claims description 3
- 239000002817 coal dust Substances 0.000 claims description 3
- 239000000295 fuel oil Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000003345 natural gas Substances 0.000 claims description 3
- 229910052698 phosphorus Inorganic materials 0.000 claims description 3
- 239000011574 phosphorus Substances 0.000 claims description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical group [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 2
- 235000019504 cigarettes Nutrition 0.000 claims 1
- 229910052717 sulfur Inorganic materials 0.000 claims 1
- 239000011593 sulfur Substances 0.000 claims 1
- 238000010438 heat treatment Methods 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 239000003546 flue gas Substances 0.000 description 44
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 39
- 238000010304 firing Methods 0.000 description 10
- 239000000047 product Substances 0.000 description 10
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 8
- 238000001816 cooling Methods 0.000 description 7
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 239000005864 Sulphur Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 5
- 239000013589 supplement Substances 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000002349 favourable effect Effects 0.000 description 4
- 239000004615 ingredient Substances 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 210000000952 spleen Anatomy 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- -1 phosphorus compound Chemical class 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 230000036642 wellbeing Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/02—Oxides or hydroxides
- C01F11/04—Oxides or hydroxides by thermal decomposition
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention belongs to gypsum Sulphuric acid coproduction lime fields more particularly to a kind of technique and device of gypsum Sulphuric acid coproduction lime, the technique of the gypsum Sulphuric acid coproduction lime to include the following steps：Step 1：It will be dried containing the raw material after gypsum and reducing agent grinding, remove the mechanical water and the crystallization water in raw material；Step 2：After raw material after drying enter preheating, calcining and decomposing is carried out, generates lime.Gas caused by stoving process enters powder-grinding process in the step 1.Enter relieving haperacidity program after gas caused by pre-heating technique and natural air heat exchange in the step 2, the natural air after heat exchange enters hot-blast stove, and hot-blast stove exit gas enters stoving process.The present invention provides one kind and can reduce production lime fuel consumption and can improve SO2The technique and device of the gypsum Sulphuric acid coproduction lime of concentration.
Description
Technical field
The invention belongs to gypsum Sulphuric acid coproduction lime field more particularly to a kind of techniques of gypsum Sulphuric acid coproduction lime
And device.
Background technique
The prior art and defect：
Typical industry by-product gypsum includes ardealite, desulfurized gypsum, bunt gypsum, fluorgypsum etc..China's ardealite year arranges
High-volume more than 50,000,000 tons (add up heap high-volume more than 2.5 hundred million tons), desulfurized gypsum annual emissions are up to 43,000,000 tons, bunt gypsum
Annual emissions are more than 500 ten thousand tons, and these industry by-product gypsums will continue to increase with industrial expansions such as phosphorus compound fertilizers.Phosphorus
Gypsum typically contains harmful substance because of complicated component, and utilization rate is even more less than 20%, and long-term stack does not only take up a large amount of soil
Ground, and environmental pollution is easily caused, it comprehensively utilizes extremely urgent.
The general raw material of lime production is lime stone at present, and the technique generally produced is using rotary kiln, shaft kiln, Mai Er Hereby
Three kinds of methods of kiln, it is desirable that the grade of ore raw materials is higher, the more dependence to natural resources, if can be using industry such as ardealites
By-product gypsum substitutes lime stone and produces lime, and flue gas is used to Sulphuric acid, can integrate the pollution problem for solving ardealite, while real
Now certain economic well-being of workers and staff.Sulfuric acid is important basic chemical industry raw material, it is reported that, SO in flue gas2Concentration improve 1%, relieving haperacidity
System investments about reduce by 10%.
There is scholar to research and develop gypsum suspended state decomposer, but industrialized production is not implemented so far.Due under suspended state, with coke
Charcoal is that the solid-solid reaction of reducing agent is not susceptible to, and is easier to occur using CO as the gas-solid reaction of reducing agent, and temperature is more than
Fluidization equipment is not easy to control at 1200 DEG C, and material is tacky, and the running rate of system cannot be guaranteed.Also have individually using rotary kiln
The report of calcined phosphogypsum lime, disadvantage is first is that relieving haperacidity flue gas SO2Concentration is lower, second is that the unrecovered flue gas using system
Waste heat, system energy consumption are higher.
Solve the difficulty and meaning of above-mentioned technical problem：
Therefore, these problems are based on, providing one kind can reduce production lime fuel consumption and can improve SO2The stone of concentration
The technique and device of cream Sulphuric acid coproduction lime have important practical significance.
Summary of the invention
Present invention aims at provide one kind to solve technical problem present in well-known technique and can reduce production stone
Grey fuel consumption and SO can be improved2The technique of the gypsum Sulphuric acid coproduction lime of concentration.
Another object of the present invention is to provide one kind to solve technical problem present in well-known technique and can reduce life
It produces lime fuel consumption and SO can be improved2The device of the gypsum Sulphuric acid coproduction lime of concentration.
The present invention is adopted the technical scheme that solve technical problem present in well-known technique：
A kind of technique of gypsum Sulphuric acid coproduction lime, the technique of the gypsum Sulphuric acid coproduction lime includes following step
Suddenly：
Step 1：It will be dried containing the raw material after gypsum and reducing agent grinding, remove the mechanical water in raw material and crystallization
Water；
Step 2：After raw material after drying enter preheating, calcining and decomposing is carried out, generates lime.
The present invention separates the heat that gypsum dehydration consumes from the heat consumption of preheater, reduces and generates this partial heat
The exhausted air quantity that required fuel combustion generates in firing system, the vapor for being dehydrated formation are not mixed with the flue gas of Sulphuric acid,
Water vapour content in relieving haperacidity flue gas is reduced, and flue gas dew point temperature is improved, and can reduce the corrosion risk of equipment, entire technique
Low energy consumption, exhaust gas total amount few using fuel and then generating is few, and SO in flue gas can be improved2Concentration, be subsequent Sulphuric acid work
Sequence creates favorable conditions；Preheater makes full use of waste gas residual heat, rotary kiln controllable, production efficiency to the calcining of material
It is high.The present invention is with low energy consumption, high reliablity, SO2The high advantage of flue gas concentration can carry out scale disposition ardealite production stone
Ash.
The present invention can also use following technical scheme：
In the technique of above-mentioned gypsum Sulphuric acid coproduction lime, further, stoving process is produced in the step 1
Raw gas enters powder-grinding process.
The exhaust gas of drying unit of the present invention is isolated with the exhaust gas that preheater exports enters powder-grinding process, dries for raw material mill
Dry, since the hot air source of drying unit can also give raw material grinding system hot wind supply, the supplement as raw material grinding dries heat source, in this way
It is not necessarily raw material grinding system and individually sets hot-blast stove, system flow can be simplified.
In the technique of above-mentioned gypsum Sulphuric acid coproduction lime, further, pre-heating technique is produced in the step 2
Enter relieving haperacidity program after raw gas and natural air heat exchange, the natural air after heat exchange enters hot-blast stove, and hot-blast stove is worked off one's feeling vent one's spleen
Body enters stoving process.
The present invention goes out the preheated device of exhaust gas of rotary kiln and raw material exchange heat after cooling down and form relieving haperacidity flue gas (260~400 DEG C),
The gas of preheater outlet contains SO2It can be used for relieving haperacidity, relieving haperacidity flue gas enters towerman's sequence after over-heat-exchanger heats air, together
When, relieving haperacidity flue gas transfers heat to air by heat exchanger, and air enters hot-blast stove, the high-temperature gas that hot-blast stove generates into
Enter drying unit for drying and dewatering, recycles the heat of relieving haperacidity flue gas.Hot-blast stove provides the heat source of drying unit, reduces back
The firing rate of rotary kiln and resulting exhaust gas, improve the SO of relieving haperacidity flue gas2Concentration is to 11% or more.
In the technique of above-mentioned gypsum Sulphuric acid coproduction lime, further, pre-heating technique is produced in the step 2
Enter relieving haperacidity program after raw gas and natural air heat exchange, the natural air after heat exchange enters hot-blast stove, and hot-blast stove is worked off one's feeling vent one's spleen
Body enters powder-grinding process.
Hot wind outlet of still of the present invention can reserve the bypass of raw material mill, and hot-blast stove can also be directly to raw material grinding system heat supply
Wind, the supplement as raw material grinding dry heat source.
In the technique of above-mentioned gypsum Sulphuric acid coproduction lime, further, the gypsum is ardealite, desulfurization stone
At least one of cream, fluorgypsum and natural gypsum, the reducing agent be in coke, anthracite, petroleum coke and sulphur coal extremely
Few one kind, n (C)/n (SO of the reducing agent3) it is 0.5~0.8, the technique of the ardealite Sulphuric acid coproduction lime is used
Fuel be at least one of coal dust, natural gas and heavy oil.
A kind of device of gypsum Sulphuric acid coproduction lime, the device of the gypsum Sulphuric acid coproduction lime include being sequentially connected
Drying unit, preheater, rotary kiln and cooler.
In the device of above-mentioned gypsum Sulphuric acid coproduction lime, further, the ardealite Sulphuric acid coproduction lime
Device further include the heat exchanger and hot-blast stove communicated with preheater, the heat exchanger to gas caused by preheater with
Air exchanges heat, and the air after heat exchange enters the hot-blast stove by pipeline.
The relieving haperacidity flue gas of preheater of the present invention outlet connect by pipeline with heat exchanger, cold air pass through heat exchanger and
Enter hot-blast stove after flue gas indirect heat exchange as combustion air, hot-blast stove provides heat source, that is, hot wind and enters drying unit.
In the device of above-mentioned gypsum Sulphuric acid coproduction lime, further, the drying unit includes drying pipeline
The cyclone cylinder that gathers dust being connected with the drying pipeline, the cyclone cylinder that gathers dust are mounted below material distributing valve, the drying pipe
The import in road is equipped with material-strewing device.
The material that the cyclone cylinder that gathers dust of drying unit of the present invention takes down enters preheater, and outlet exhaust is sent into grinding work
Sequence, drying pipeline are equipped with the material-strewing device for feeding raw material, and the heat source of drying pipeline comes from hot-blast stove.
In the device of above-mentioned gypsum Sulphuric acid coproduction lime, further, the preheater be one cyclonic cylinder extremely
The series connection of Category Four cyclone cylinder, the feeder pipe of the cyclone cylinder that gathers dust of the drying unit pass through each rotation of material distributing valve and the preheater
The blast pipe of air duct is separately connected, and the exhaust gas of most upper level cyclone cylinder outlet is connected with the heat exchanger, most next stage whirlwind
Cylinder is connect with the rotary kiln.Material is from drying unit, and the gas of preheater is from rotary kiln.
Drying unit of the present invention needs the different situations run according to system, feeds the cyclone cylinder of its lower different location, with
Just material temperature of the relieving haperacidity flue-gas temperature and raw material of control preheater outlet in preheater, avoids reducing agent advanced combustion, dries
The material of device can enter preheater different parts by material distributing valve as needed.
In the device of above-mentioned gypsum Sulphuric acid coproduction lime, further, the rotary kiln revolving speed is 0~4rpm.
Rotary kiln of the present invention provides the reasonable residence time for gypsum decomposition, is easier to control calcining temperature than suspension calcining
It spends (1100~1300 DEG C), the preheater blocking for preventing previous patent fluidized calcination from generating.
In conclusion the present invention has the advantages that：
1, the drying and dewatering process of gypsum is moved to baking by previous by the present invention in pre-heating system or in rotary kiln
In equipment for drying, the heat for consuming gypsum dehydration is separated from the heat consumption of firing system, generates this part heat to reduce
The exhausted air quantity that is generated in firing system of fuel combustion needed for amount, and be dehydrated the vapor of formation not with the flue gas of Sulphuric acid
It is mutually mixed, SO in flue gas can be improved2Concentration, create favorable conditions for subsequent Sulphuric acid process.
2, the water vapour content in relieving haperacidity flue gas of the present invention is reduced, and flue gas dew point temperature is improved, and can reduce equipment
Corrosion risk.
3, the exhaust gas that the present invention goes out drying unit is dried for raw material mill, and the relieving haperacidity flue gas of preheater passes through heat exchanger out
Air is heated, and hot-air is led into hot-blast stove and is used, the waste heat of exhaust gas can be efficiently used, reduce system heat consumption.
4, the hot air source of drying unit of the present invention can also give raw material grinding system hot wind supply, and the supplement as raw material grinding is dried
Heat source, it is not necessary to individually set hot-blast stove for raw material grinding system, system flow can be simplified.
Detailed description of the invention
Technical solution of the present invention is described in further detail below with reference to drawings and examples, but should
Know, these attached drawings are designed for task of explanation, therefore not as the restriction of the scope of the invention.In addition, except non-specifically
It points out, these attached drawings are meant only to conceptually illustrate structure construction described herein, without to be drawn to scale.
Fig. 1 is process flow diagram of the invention；
Fig. 2 is structural schematic diagram of the invention.
In figure：
1, drying unit, 2, preheater, 3, rotary kiln, 4, cooler, 5, heat exchanger, 6, hot-blast stove；
1-1, material-strewing device, 1-2, drying pipeline, 1-3, gather dust cyclone cylinder, 1-4, material distributing valve；
2-1, one cyclonic cylinder, 2-2, second level cyclone cylinder, 2-3, three-level cyclone cylinder, 2-4, Category Four cyclone, 2-5, preheater
With rotary kiln connecting pipe；
3-1, smoke-box, 3-2, kiln hood burner.
Specific embodiment
Firstly, it is necessary to which explanation, illustrates gypsum Sulphuric acid coproduction stone of the invention for by way of example below
Technique and specific structure, the features and advantages of device etc. of ash, however what all descriptions were intended merely to be illustrated, without answering
It is understood as forming any restrictions to the present invention.In addition, what is be described by or imply in each embodiment mentioned by this paper appoints
It anticipates single technical characteristic, or shown or implicit any single technical characteristic in the drawings, it still can be in these technologies
Continue any combination between feature (or its equivalent) or delete, to obtain the sheet that may do not referred to directly herein
More other embodiments of invention.In addition, same or like technical characteristic is in the same figure for the sake of simplifying drawing
It may only be indicated at one.
It will be understood that when component ' attach ' to another component when it is said that, it can be directly connected to another component or
There may be intermediate members.On the contrary, when component " being directly connected to " being arrived another component when it is said that, then it represents that middle part is not present
Part.
Fig. 1 gives process flow diagram of the invention, and by Fig. 2 shows structural schematic diagram of the invention,
Just Fig. 1 to Fig. 2 is combined to illustrate the present invention below.
In order to further understand the content, features and effects of the present invention, the following examples are hereby given, and cooperate attached drawing
Detailed description are as follows：
A kind of technique of gypsum Sulphuric acid coproduction lime, the technique of the gypsum Sulphuric acid coproduction lime includes following step
Suddenly：
Step 1：It will be dried containing the raw material after gypsum and reducing agent grinding, remove the mechanical water in raw material and crystallization
Water；
Step 2：After raw material after drying enter preheating, calcining and decomposing is carried out, generates lime.
The present invention separates the heat that gypsum dehydration consumes from the heat consumption of preheater 2, reduces and generates this part heat
The exhausted air quantity that fuel combustion needed for amount generates in firing system, the vapor for being dehydrated formation is not mixed with the flue gas of Sulphuric acid
It closes, the water vapour content in relieving haperacidity flue gas is reduced, and flue gas dew point temperature is improved, and can reduce the corrosion risk of equipment, entirely
Process energy consumption is low, exhaust gas total amount few using fuel and then generating is few, and SO in flue gas can be improved2Concentration, be subsequent sulphur processed
Sour process creates favorable conditions；Preheater 2 makes full use of waste gas residual heat, and rotary kiln 3 is controllable to the calcining of material, raw
It produces high-efficient.The present invention is with low energy consumption, high reliablity, SO2The high advantage of flue gas concentration can carry out scale disposition ardealite
Produce lime.
Further for, can also consider in the present invention, in the step 1 gas caused by stoving process into
Enter powder-grinding process.
The exhaust gas of drying unit 1 of the present invention is isolated with the exhaust gas that preheater 2 exports enters powder-grinding process, dries for raw material mill
Dry, since the hot air source of drying unit 1 can also give raw material grinding system hot wind supply, the supplement as raw material grinding dries heat source, this
Sample is not necessarily raw material grinding system and individually sets hot-blast stove 6, can simplify system flow.
Further for, can also consider in the present invention, in the step 2 gas caused by pre-heating technique with
Enter relieving haperacidity program after natural air heat exchange, the natural air after heat exchange enters hot-blast stove 6, and 6 exit gas of hot-blast stove enters baking
Dry technique.
The preheated device 2 of exhaust gas and formation relieving haperacidity flue gas (260~400 after raw material heat exchange cooling that the present invention goes out rotary kiln 3
DEG C), the gas that preheater 2 exports contains SO2It can be used for relieving haperacidity, relieving haperacidity flue gas enters relieving haperacidity after over-heat-exchanger 5 heats air
Process, meanwhile, relieving haperacidity flue gas transfers heat to air by heat exchanger 5, and air enters hot-blast stove 6, what hot-blast stove 6 generated
High-temperature gas enters drying unit 1 for drying and dewatering, has recycled the heat of relieving haperacidity flue gas.Hot-blast stove 6 provides drying unit 1
Heat source reduces the firing rate and resulting exhaust gas of rotary kiln 3, improves the SO of relieving haperacidity flue gas2Concentration.
Relieving haperacidity flue gas (260~400 DEG C) are formed through heat after the preheated device 2 of the exhaust gas of rotary kiln 3 and raw material heat exchange cooling out
Exchanger 5 enters relieving haperacidity process, and the exhaust gas of drying unit 1 is isolated with the exhaust gas that preheater 2 exports enters powder-grinding process, preheater
The relieving haperacidity flue gas of 2 outlets recycles heat cold air through over-heat-exchanger 5 and enters hot-blast stove 6, and the heat source of drying unit 1 comes from
The firing rate and resulting exhaust gas of rotary kiln 3 are reduced in hot-blast stove 6, preheater 2, which has carried out recuperation of heat, to be reduced
Firing rate and resulting exhaust gas, this three kinds of approach improve the SO of relieving haperacidity flue gas2Concentration.
It should be pointed out that entering relieving haperacidity after gas caused by pre-heating technique and natural air heat exchange in the step 2
Program, the natural air after heat exchange enter hot-blast stove 6, and 6 exit gas of hot-blast stove enters powder-grinding process, cooling in the step 2
One branch of hot-air that machine 4 generates enters rotary kiln 3, and remaining part enters hot-blast stove 6.
Hot-blast stove 6 of the present invention exports, and can reserve the bypass of raw material mill, and hot-blast stove 6 can also be supplied directly to raw material grinding system
Hot wind, the supplement as raw material grinding dry heat source.
It should be pointed out that the gypsum is at least one of ardealite, desulfurized gypsum, fluorgypsum and natural gypsum,
The reducing agent is at least one of coke, anthracite, petroleum coke and sulphur coal, it is desirable that volatile matter is as low as possible (≤8%)；
The volatile matter of the reducing agent is as low as possible, and volatile matter is excessively high, more easy to discharge heat in advance, is easy to produce skinning, it is general I
Require 5%, n (C)/n (SO of the reducing agent3) it is 0.5~0.8, the technique institute of the ardealite Sulphuric acid coproduction lime
The fuel used is at least one of coal dust, natural gas and heavy oil.
Embodiment one：Using ardealite and coke burden, phosphogypsum quality accounting 90%-95%, coke quality accounting 10-
5%, when preheater 2 is using level Four preheater 2, heat consumption is 1150-1450kcal/kg lime product, and preheater 2 exports SO2It is dense
Degree >=11.6%.
Embodiment two：Using desulfurized gypsum and coke burden, phosphogypsum quality accounting 90%-95%, coke quality accounting
10-5%, when preheater 2 is using level Four preheater 2, heat consumption is 1150-1450kcal/kg lime product, and preheater 2 exports SO2
Concentration >=11.6%.
Embodiment three：Using fluorgypsum and coke burden, phosphogypsum quality accounting 90%-95%, coke quality accounting 10-
5%, when preheater 2 is using level Four preheater 2, heat consumption is 1150-1450kcal/kg lime product, and preheater 2 exports SO2It is dense
Degree >=11.6%.
Ardealite, fluorgypsum, desulfurized gypsum, property is all similar, and harmful components slightly have difference, can control the same
Energy consumption and SO2。
Example IV：Using the natural gypsum and coke burden, natural gypsum quality accounting 90%-95%, coke quality is accounted for
Than 10-5%, when preheater 2 is using level Four preheater 2, heat consumption is 1150-1450kcal/kg lime product；Preheater 2 exports
SO2Concentration >=12.3%.
Embodiment five：Using ardealite and coke burden, phosphogypsum quality accounting 90%-95%, coke quality accounting 10-
5%, when preheater 2 is using three-level preheater 2, heat consumption is 1250-1550kcal/kg lime product, and preheater 2 exports SO2It is dense
Degree >=10%.
Embodiment six：Using desulfurized gypsum and petroleum coke ingredient, phosphogypsum quality accounting 90%-95%, Petroleum Coke
Accounting 10-5%, when preheater 2 is using three-level preheater 2, heat consumption is 1300-1500kcal/kg lime product, and preheater 2 goes out
Mouth SO2Concentration >=10.0%.
Embodiment seven：Using desulfurized gypsum and sulphur coal ingredient, phosphogypsum quality accounting 90%-95%, Petroleum Coke
Accounting 10-5%, when preheater 2 is using three-level preheater 2, heat consumption is 1300-1500kcal/kg lime product, and preheater 2 goes out
Mouth SO2Concentration >=10.0%.
Embodiment eight：Using fluorgypsum and petroleum coke ingredient, phosphogypsum quality accounting 90%-95%, Petroleum Coke is accounted for
Than 10-5%, when preheater 2 is using three-level preheater 2, heat consumption is 1300-1500kcal/kg lime product, and preheater 2 exports
SO2Concentration >=10.0%.
Embodiment nine：Using fluorgypsum and sulphur coal ingredient, phosphogypsum quality accounting 90%-95%, Petroleum Coke is accounted for
Than 10-5%, when preheater 2 is using three-level preheater 2, heat consumption is 1300-1500kcal/kg lime product, and preheater 2 exports
SO2Concentration >=10.0%.
A kind of device of gypsum Sulphuric acid coproduction lime, the device of the gypsum Sulphuric acid coproduction lime include being sequentially connected
Drying unit 1, preheater 2, rotary kiln 3 and cooler 4.
For further, it can also consider in the present invention, the device of the ardealite Sulphuric acid coproduction lime also wraps
The heat exchanger 5 and hot-blast stove 6 communicated with preheater 2 is included, the heat exchanger 5 is to gas caused by preheater 2 and air
It exchanges heat, the air after heat exchange enters the hot-blast stove 6 by pipeline.The preheater 2 and rotary kiln 3 by preheater with
The 2-5 connection of rotary kiln connecting pipe.
The relieving haperacidity flue gas that preheater 2 of the present invention exports is connect by pipeline with heat exchanger 5, and cold air passes through heat exchanger
5 are used as combustion air with hot-blast stove 6 is entered after flue gas indirect heat exchange, and hot-blast stove 6 provides heat source, that is, hot wind and enters drying unit 1.
It should be pointed out that the drying unit 1 includes drying pipeline 1-2 and is connected with the drying pipeline 1-2
Gather dust cyclone cylinder 1-3, and the cyclone cylinder 1-3 that gathers dust is mounted below material distributing valve 1-4, and the import of the drying pipeline 1-2 is equipped with
Material-strewing device 1-1.
The material that cyclone cylinder 1-3 takes down that gathers dust of drying unit 1 of the present invention enters preheater 2, and outlet exhaust is sent into powder
Grinder sequence, drying pipeline 1-2 are equipped with the material-strewing device 1-1 for feeding raw material, and the heat source of drying pipeline 1-2 comes from hot-blast stove
6。
It should be pointed out that the preheater 2 is one cyclonic cylinder 2-1 to Category Four cyclone cylinder 2-4 series connection, the drying dress
The feeder pipe for setting the 1 cyclone cylinder 1-3 that gathers dust is distinguished by the blast pipe of material distributing valve 1-4 and each cyclone cylinder of the preheater 2
The exhaust gas of connection, the outlet of most upper level cyclone cylinder is connected with the heat exchanger 5, most next stage cyclone cylinder and the rotary kiln 3
Connection.Material is from drying unit 1, and the gas of preheater 2 is from rotary kiln 3.
The preheater 2 includes one cyclonic cylinder 2-1, second level cyclone cylinder 2-2, three-level cyclone cylinder 2-3 and Category Four cyclone cylinder
2-4.Meanwhile the number of cyclone cylinder is not limited only to four in the preheater 2.
Drying unit 1 of the present invention needs the different situations run according to system, feeds the cyclone cylinder of its lower different location, with
Just material temperature of the relieving haperacidity flue-gas temperature and raw material that control preheater 2 exports in preheater 2, avoids reducing agent advanced combustion, dries
The material of equipment for drying 1 can enter 2 different parts of preheater by material distributing valve 1-4 as needed.
It should be pointed out that 3 revolving speed of rotary kiln is 0~4rpm, the rotary kiln 3 is fired with smoke-box 3-1 and kiln hood
Temperature point is equipped in burner 3-2, the 3 smoke-box 3-1 of rotary kiln.
Rotary kiln 3 of the present invention provides the reasonable residence time for gypsum decomposition, is easier to control calcining than suspension calcining
Temperature (1100~1300 DEG C), the temperature of such smoke-box 3-1 is easily controllable, and (smoke-box 3-1 has temperature point, control range 550-
850 DEG C), the preheater 2 for preventing previous patent fluidized calcination from generating blocks.
The cooler 4 is grate cooler 4, rotary cooler 4 or third generation cooler 4, the cold sky of cooler 4
Gas is after the hot material heat exchange heating that rotary kiln 3 comes out, and into the combustion-supporting fuel of kiln, remaining part enters hot-blast stove 6.
As an example, in the present invention, following steps are taken：
Step 1：The physics in drying unit 1 completely removing raw material will be passed through containing the raw material after gypsum and reducing agent grinding
Water and the crystallization water；
Step 2：After raw material after drying enter the exhaust gas heat exchange come out in preheater 2 and rotary kiln 3, into rotary kiln 3
Calcining and decomposing generates lime；
Step 3：It is cooling into cooler 4, obtain final lime product.
The cooler 4 is grate cooler 4, rotary cooler 4 or third generation cooler 4, natural air conduct
Cooling wind is passed through naturally or enters cooler 4 by air blower.The cold air of cooler 4 passes through the hot material that rotary kiln 3 comes out
After heat exchange heating, into the combustion-supporting fuel of kiln, remaining part enters hot-blast stove 6.
The present invention individually carries out raw material dehydration from detaching in preheater 2 in drying unit 1.Utilize revolution
Kiln 3 calcines preheated raw meal.Kiln tail goes out 2 exhaust gas of preheater for heating air, and heat entrained by hot-air is for drying
Device 1 is dehydrated raw material.The feeder pipe of drying unit 1 can be with each cyclone cylinder of preheater 2 by material distributing valve 1-4
Blast pipe is attached, and realizes the switching between 2 cyclone cylinder difference series of preheater.
The course of work and principle of the invention：
Drying unit 1 will be fed containing the raw material of gypsum and reducing agent, raw material are carried out using the hot wind provided by hot air source
Drying and dehydration, to remove the crystallization water in a small amount of mechanical water and gypsum remained in raw material, by controlling drying and dewatering device
Outlet temperature, it is ensured that completely removing raw material in mechanical water and the crystallization water.Drying unit 1 includes drying pipeline 1-2 furnace
With the cyclone cylinder 1-3 that gathers dust, dusty gas gathered dust cyclone cylinder 1-3 realize Conveyance after, according to system run different situations,
The principle that raw material enters kiln temperature degree cannot be ignited and improved as far as possible in preheater 2 in line with reducing agent, by adjusting connection drying
The material distributing valve 1-4 of device 1 and 2 blanking of preheater, by the blast pipe of certain grade of cyclone cylinder of hot raw material feeding preheater 2, after progress
Continuous heat exchange, the hot raw material of most next stage cyclone cylinder 2-1 enter rotary kiln 3 and are decomposed and calcined out.The drying of drying unit 1 out
Exhaust gas leads to raw material mill as drying heat source；Heat exchanger 5 is set on the relieving haperacidity flue of preheater 2 out, utilizes heat exchange
The heat content that device 5 recycles heats air, and hot-air is led to hot-blast stove 6 and is used, and is used for after the purified processing of the flue gas after cooling
Sulphuric acid.
The drying unit 1 can be the structural shapes such as duct type or fluidized bed type, the air feed of air inlet and hot-blast stove 6
Pipeline is connected, and air outlet is also that discharge port is connected with preheater 2；Hot wind and raw material are carried out in drying unit 1 with suspended state
Heat exchange, can be arranged several neckings on duct type drying unit 1, to form effect of spurting, strengthen the heat exchange between gas, material；It fills
Dust-contained airflow temperature after dividing heat exchange is controlled at 150~300 DEG C, is guaranteeing to remove mechanical water and the crystallization water in raw material completely
In the case of, as far as possible the temperature of dust-contained airflow is controlled lower, to reduce drying heat consumption.The arrangement of drying unit 1 can be embedding
Enter in 2 pylon of preheater, so that the design of whole system is more compact.
The present invention can pass through control drying unit 1 outlet temperature, it is ensured that by raw material mechanical water and the crystallization water it is complete
Removing, the heat for consuming gypsum dehydration are separated from the heat consumption of firing system, generate this partial heat institute to reduce
The exhausted air quantity that is generated in firing system of fuel combustion needed, and be dehydrated the vapor of formation also not with the Gas phase Smoke of Sulphuric acid
It is mixed, to improve SO in flue gas2Concentration, create favorable conditions for subsequent Sulphuric acid process.Simultaneously as water steams in flue gas
Gas content is reduced, and flue gas dew point temperature is improved, and can reduce the corrosion risk of equipment.Hot raw material after drying are directly entered pre-
Hot device 2 reduces the intermediate storage link in previous technical process, is conducive to reduce and burn using the raw material heat content for going out drying system
At the heat consumption of system.The drying exhaust gas of drying unit 1 is for raw material mill drying out, and the relieving haperacidity flue gas of preheater 2 is handed over by heat out
Parallel operation 5 can heat air, and hot-air is led to hot-blast stove 6 and is used, and efficiently use the waste heat of exhaust gas.It is dried by effective use
The waste heat of exhaust gas and relieving haperacidity flue gas has achieved the purpose that energy saving of system, reduces system heat consumption.
In conclusion can reduce production lime fuel consumption the present invention can provide one kind and SO can be improved2The stone of concentration
The technique and device of cream Sulphuric acid coproduction lime.
Above embodiments describe the invention in detail, but content is only the preferred embodiment of the present invention, no
It can be believed to be used to limit the scope of the invention.Any changes and modifications in accordance with the scope of the present application,
It should still fall within the scope of the patent of the present invention.
Claims (10)
1. a kind of technique of gypsum Sulphuric acid coproduction lime, it is characterised in that：The technique packet of the gypsum Sulphuric acid coproduction lime
Include following steps：
Step 1：It will be dried containing the raw material after gypsum and reducing agent grinding, remove the mechanical water and the crystallization water in raw material；
Step 2：After raw material after drying enter preheating, calcining and decomposing is carried out, generates lime.
2. the technique of gypsum Sulphuric acid coproduction lime according to claim 1, it is characterised in that：It is dried in the step 1
Gas caused by technique enters powder-grinding process.
3. the technique of gypsum Sulphuric acid coproduction lime according to claim 1, it is characterised in that：It is preheated in the step 2
Enter relieving haperacidity program after gas caused by technique and natural air heat exchange, the natural air after heat exchange enters hot-blast stove, hot wind
Outlet of still gas enters stoving process.
4. the technique of gypsum Sulphuric acid coproduction lime according to claim 1, it is characterised in that：It is preheated in the step 2
Enter relieving haperacidity program after gas caused by technique and natural air heat exchange, the natural air after heat exchange enters hot-blast stove, hot wind
Outlet of still gas enters powder-grinding process.
5. the technique of gypsum Sulphuric acid coproduction lime according to claim 1, it is characterised in that：The gypsum is phosphorus stone
At least one of cream, desulfurized gypsum, fluorgypsum and natural gypsum, the reducing agent are coke, anthracite, petroleum coke and high-sulfur
At least one of coal, n (C)/n (SO of the reducing agent3) it is 0.5~0.8, the work of the ardealite Sulphuric acid coproduction lime
Fuel used in skill is at least one of coal dust, natural gas and heavy oil.
6. a kind of device of gypsum Sulphuric acid coproduction lime, it is characterised in that：The device packet of the gypsum Sulphuric acid coproduction lime
Include sequentially connected drying unit, preheater, rotary kiln and cooler.
7. the device of gypsum Sulphuric acid coproduction lime according to claim 6, it is characterised in that：The ardealite Sulphuric acid
The device of coproduction lime further includes the heat exchanger and hot-blast stove communicated with preheater, and the heat exchanger is to produced by preheater
Gas exchange heat with air, the air after heat exchange by pipeline enter the hot-blast stove.
8. the device of gypsum Sulphuric acid coproduction lime according to claim 6, it is characterised in that：The drying unit includes
Drying pipeline and the cyclone cylinder that gathers dust being connected with the drying pipeline, the cyclone cylinder that gathers dust are mounted below material distributing valve, institute
The import for stating drying pipeline is equipped with material-strewing device.
9. the device of gypsum Sulphuric acid coproduction lime according to claim 6, it is characterised in that：The preheater is level-one
Cyclone cylinder to Category Four cyclone cylinder is connected, and the feeder pipe of the cyclone cylinder that gathers dust of the drying unit passes through material distributing valve and the preheater
The blast pipe of each cyclone cylinder be separately connected, the exhaust gas of most upper level cyclone cylinder outlet is connected with the heat exchanger, most lower
One cyclonic cylinder is connect with the rotary kiln.
10. the device of gypsum Sulphuric acid coproduction lime according to claim 6, it is characterised in that：The rotary kiln revolving speed
For 0~4rpm, the rotary kiln has smoke-box and kiln hood burner, is equipped with temperature point, the cigarette in the rotary kiln smoke-box
Room temperature is 550~850 DEG C.
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| CN201811119583.4A CN108910836A (en) | 2018-09-25 | 2018-09-25 | A kind of technique and device of gypsum Sulphuric acid coproduction lime |
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| CN109916186A (en) * | 2019-01-04 | 2019-06-21 | 贵州芭田生态工程有限公司 | A kind of recovery method for calcining phosphorus ore thermal energy |
| CN114956009A (en) * | 2022-07-07 | 2022-08-30 | 山东鲁北企业集团总公司 | Production system and method for preparing sulfuric acid and co-producing cement clinker by using gypsum |
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