CN201896071U - Improved producing device for making sulphuric acid and cement with gypsum - Google Patents
Improved producing device for making sulphuric acid and cement with gypsum Download PDFInfo
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- CN201896071U CN201896071U CN2010205980357U CN201020598035U CN201896071U CN 201896071 U CN201896071 U CN 201896071U CN 2010205980357 U CN2010205980357 U CN 2010205980357U CN 201020598035 U CN201020598035 U CN 201020598035U CN 201896071 U CN201896071 U CN 201896071U
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Abstract
The utility model relates to an improved producing device for making sulphuric acid and cement with gypsum. Crude materials comprise dihydrate gypsum, clay and reducing agent. Sulphuric acid and cement products are made through the processes of raw material drying, independent grinding, mechanical stirring and homogenizing, raw material decomposing and calcining in a preheating kiln, acid cleaning and purification of kiln gases, SO2 drying, double absorption techniques and cement grinding. The improved producing device is characterized in that by adopting dihydrate gypsum technology, the raw materials are dried by 70 DEG C to 85 DEG C bone dry tail gas from a sulphuric acid absorption tower, so as to obtain the dihydrate gypsum, the free water content of which is less than 5% wt, and then the dihydrate gypsum is directly homogenized with the clay and the reducing agent to be raw materials under the existence of CaC12 or Na2SO4. By adopting the dihydrate gypsum technology, the heat consumption is lowered by 30%, the power consumption is reduced by 20%, the investment is reduced by 20% to 40 %, and the cost is lowered by 25% to 30 %. The improved producing device overcomes the defects of high power consumption, high heat consumption, high investment and low operation rate and the like in conventional means, and 0.4 to 0.5 ton of side product vapor is produced per ton of sulphuric acid, so that the economic benefit is obvious.
Description
Technical field
The utility model relates to the technology that gypsum is produced sulfuric acid and cement, belongs to production technology and the comprehensive utilization of industry by-product gypsum residue resource and the enviromental protection and improvement field of sulfuric acid, cement industry.
Background technology
The research of gypsum system sulfuric acid and cement technology started from for 20 beginnings of the century.1916, the Miu Le of Germany and wealthy receiving (Muller Kuhne) exploitation plaster of paris system sulfuric acid and cement technology were obtained success, and have set up pilot plant; Thereafter, it is raw material production sulfuric acid and cement plant that Britain, Germany, Poland, Austria, South Africa etc. have been built up with the plaster of paris, anhydrite and phosphogypsum in succession, and puts into production, and its average productive capacity is for producing each 160 tons of sulfuric acid and cement daily.Because investment is big, hear rate is high, operation factor is low, deficiency in economic performance, external production equipment successively stopped production in the seventies in last century.
The present industrial gypsum annual emissions of China surpasses 7,000 ten thousand tons, and increases year by year.Owing to contain objectionable impurities in the industry by-product gypsum, discharging can cause serious environmental to pollute arbitrarily; The stockyard is set, and not only occupation of land is many, investment is big, slag expense height, and the geologic condition in stockyard is required height, and accumulation for a long time can cause surface water and phreatic pollution.
China is on the basis of summing up domestic and international technology, obtain the success that utilizes salt gypsum, phosphogypsum, the plaster of paris, desulfurated plaster system sulfuric acid and cement, and build 8 in last century Mo and overlap production equipments, the maximum scale that reaches 300,000 tons of cement of annual output 200000 tons of producing sulfuric acid and jointlies of phosphogypsum system becomes advanced, the largest device of world's gypsum relieving haperacidity technology.Investment is high, hear rate is big, power consumption is big, the shortcoming of deficiency in economic performance, so the stopping production that has but each device all exists.For example application number is 200810139276.2, name is called a kind of gypsum and produces in the patent application of improvement production technique of sulfuric acid and cement and use the semi-hydrated gypsum production technique, because raw material is that the hyperthermia drying that dihydrate gypsum need be heated to more than 160 ℃ just can obtain semi-hydrated gypsum, the complexity that hear rate is very big, device also compares, and rotary kiln ring formation very easily when adopting this technology, operation factor is low, investment is high, hear rate is big, and power consumption is big, deficiency in economic performance.
Summary of the invention
Technical problem to be solved in the utility model is to overcome that the hear rate that above-mentioned technology exists is big, the defective of deficiency in economic performance, a kind of gypsum system sulfuric acid and cement industry are provided, have raw material and draw materials extensively, energy consumption is low, less investment, high efficiency, the advantage of no waste water, waste sludge discharge.
The technical solution of the utility model is: the improvement production equipment of a kind of gypsum system sulfuric acid and cement, comprise the raw material stoving device, the auxiliary material drying unit, independent grinding device, mechanical stirring homogenizing storehouse, the raw material primary heater unit, rotary kiln, the purge drying device, conversion system, the sulfuric acid absorption device, cement grinds device, the raw material stoving device is connected with corresponding independent grinding device respectively with the auxiliary material drying unit, independent grinding device is connected with mechanical stirring homogenizing storehouse, mechanical stirring homogenizing storehouse is connected with the raw material primary heater unit, the raw material primary heater unit is connected with the sulfuric acid absorption device, it is characterized in that, described mechanical stirring homogenizing storehouse is that bottom mechanical stirs discharging steel cylinder homogenizing storehouse, and the thermal source import of described raw material stoving device is connected with the over dry tail gas outlet of sulfuric acid absorption device by pipeline.
The raw material primary heater unit is 2～5 grades of compound or cyclone preheaters.
The raw material stoving device is the pneumatic floating dryer.
Described sulfuric acid absorption device is divided into three parts by ball collar up and down, and middle part and bottom are 200～240 ℃ high temperature absorber portions, and top is 85～110 ℃ low temperature absorption section, is provided with SO in the bottom
3Import and the outlet of high temperature sulfuric acid, place at the middle part near the low temperature absorption section is provided with the import of high temperature sulfuric acid, be provided with the import of low temperature sulfuric acid at the top of low temperature absorption section, be provided with the outlet of low temperature sulfuric acid in the bottom of low temperature absorption section and be provided with scum dredger at the top of sulfuric acid absorption device, on scum dredger, be provided with the tail gas outlet, be filled with acid resistance filler in low temperature absorption section and high temperature absorber portion, the shell of described sulfuric acid absorption device is a round shape, the liner acid proof lining.
Described high temperature sulfuric acid exit is provided with vapour generator.
Beneficial effect:
1, two water conservancy project process flows are adopted in the gypsum oven dry, and drying plant adopts the pneumatic floating dryer, and 70～85 ℃ the over dry tail gas that thermal source adopts the sulfuric acid absorption device to come out can remove the free-water in the dihydrate gypsum.More traditional half water conservancy project process flow equipment volume is little, reduce investment outlay, throughput is big, saves the power consumption of 30% overall heat consumption and 20%.The employing dihydrate gypsum is a raw material, and the good stability of dihydrate gypsum does not lump, as long as free-water contained in the raw material is dried＜5%, need not be heated to high temperature more than 160 ℃ as half water conservancy project skill.Because sulfuric acid per ton is discharged 3.2～3.6 tons 70～85 ℃ over dry tail gas, consume 1.5 tons of dihydrate gypsums, amount to and contain 1.8 tons in free-water 20% gypsum, should remove 0.22 ton of moisture content as oven dry when containing free-water 5%.It is feasible removing 0.22 ton of free-water with 3.2～3.6 tons 70～85 ℃ over dry tail gas in the airflow dryer baking.
2. the raw material preparation adopts bottom mechanical to stir discharging steel cylinder homogenizing storehouse, and gypsum need not grinding can all change into qualified raw material with auxiliary material, has reduced by 30% power consumption and investment.
3. adopt 2～5 grades of compound primary heater units to decompose gypsum raw material new technology, compare with traditional kiln, system's hear rate reduces by 30%, increases throughput, economy system investment, uses the dihydrate gypsum raw material.
4. general semi-hydrated gypsum technology raw material decomposition temperature reaches 800～1200 ℃, enters clinkering zone at the branch gypsum that decomposes fully that ungirds not, branchs is ungirded and clinkering zone overlaps, and easily causes rotary kiln at the clinkering zone ring formation because of the gypsum fusing point hangs down, and operation factor is low.Raw material add the CaCl of 0.5-3%
2Or Na
2SO
4Reduce by 100～150 ℃ of gypsum decomposition temperatures, raising decomposition rate 20～30% ungirds branch and clinkering zone separates, and ungirding at branch enters clinkering zone after gypsum decomposes fully, prevents ring formation of rotary kiln, improves running period.
5. sulfuric acid is done and is inhaled operation employing low temperature recovery technology, the sulfuric acid absorption device divides two sections absorptions, go out tower acid temperature bottom and be 200～230 ℃ high temperature absorber portion, top is 80～110 ℃ low temperature absorption section, vapour generator is established in high temperature sulfuric acid outlet at the high temperature absorber portion, but compare 0.4～0.5 ton of common sulfuric acid absorption tower sulfuric acid producing steam per ton, outwards provide heat energy also can generate electricity, increase economic efficiency.
6. utilize the utility model to reduce by 25～40% with adopt the traditional method investment with scale producer; Hear rate reduces by 30%; Power consumption reduces by 20%.Cost reduces by 25～30%.
Description of drawings
Fig. 1 is each equipment connection diagram of the present utility model.
Wherein, 1 is the auxiliary material drying unit, and 2 is material separator, and 3 is blower fan, and 4 is the raw material stoving device, 5 is the raw material primary heater unit, and 6 is the purge drying device, and 7 is conversion system, and 8 is the sulfuric acid absorption device, 9 is rotary kiln, and 10 for cement grinds device, and 11 is mechanical stirring homogenizing storehouse, 12 auxiliary material separators.
Fig. 2 is a sulfuric acid absorption apparatus structure synoptic diagram.
Wherein, 8-1 is SO
3Import, 8-2 is the outlet of high temperature sulfuric acid, and 8-3 is the import of high temperature sulfuric acid, and 8-4 is the outlet of low temperature sulfuric acid, and 8-5 is the import of low temperature sulfuric acid, and 8-6 is the tail gas outlet, and 8-7 is a scum dredger, and 8-8 is a filler, 8-9 is an acid proof lining.
Embodiment
As shown in Figure 1, by low temperature over dry tail gas the free-water in the dihydrate gypsum is dried in the common incoming stock drying unit 4 of 70～85 ℃ the low temperature over dry tail gas that contains the industrial by-product dihydrate gypsum of free-water and come out by sulfuric acid absorption device 8, the dihydrate gypsum that obtains free-water＜5%wt uses as raw material, must grinding, as free-water is little then directly dries to free-water＜5% and grinding powdering with the oven dry mill because of containing with the plaster of paris.Raw material stoving device 4 can be selected the pneumatic floating dryer.Dried dihydrate gypsum is separated in the mechanical stirring homogenizing storehouse 11 through material separator 2, and waste gas is through blower fan 3 emptyings.Clay and reductive agent join in the auxiliary material drying unit 1, and thermal source adopts burn till waste heat or the contact of hot flue gas of coming out of rotary kiln 9 to carry out surface radiating and dry to moisture content≤10%wt.Perhaps adopt fluidizing furnace to provide thermal source also passable, fluidizing furnace is fuel with the coal, and the lime-ash of discharge can be as the additive of cement.Clay, reductive agent are dried grinding after 12 separation of auxiliary material separator also enter in the mechanical stirring homogenizing storehouse 11.Mechanical stirring homogenizing storehouse 11 preferably adopts bottom mechanical to stir the homogenizing form.Waste gas is through blower fan 3 emptyings.Dihydrate gypsum with oven dry is that main raw material, clay, reductive agent are auxiliary material, CaCl
2Or Na
2SO
4For stirring in the homogenizing storehouse 11 in bottom mechanical, additive is mixed with raw material.The raw material that mechanical stirring homogenizing storehouse 11 prepares enter decomposing and calcining in the rotary kiln 9 after joining the high-temperature tail gas preheating that raw material primary heater unit 5 and rotary kiln 9 come out and sloughing crystal water, burn the grog that and blended material and enter cement together and grind in the device 10 and manufacture cement products.Raw material primary heater unit 5 can adopt the multistage composite preheater kiln to carry out preheating.The crystal water of gypsum and the free-water that contains remove in preheater and heat in the raw material, enter rotary kiln 9 decomposing and calcining, and under the effect of additive, raw material decomposite SO fully at 700～1050 ℃
2, solid phase becomes cement clinker 1200～1450 ℃ of calcinings, grinds into cement.Contain 10～14.5%SO
2Gas phase adopt acid-scrubbing cleaning, double conversion and double absorption, low level waste heat recovery to make sulfuric acid.That decomposes contains SO
2Gas enters in the purge drying device 6 after raw material primary heater unit 5 and raw material heat exchange are lowered the temperature and enters in the conversion system 7 SO after the cooling dedusting
2Change into SO
3Enter then in the sulfuric acid absorption device 8 with purge drying device 6 in the diluted acid that produces manufacture sulfuric acid product, the reaction liberated heat is a byproduct steam, the byproduct steam power generation and heat supply.
This invention is saved hear rate 30% than other method, saves power consumption 20%, saves investment 25～40%, and cost reduces by 25～30%, prevents ring formation of rotary kiln, improves operation factor, no waste water, waste sludge discharge, remarkable in economical benefits.This wherein main improvement is exactly that raw material has adopted dihydrate gypsum directly to be mixed with raw material, and required bake out temperature just can be finished by 70～85 ℃ the over dry tail gas that sulfuric acid absorption device 8 comes out, and other processes are conventional production process.
Describe more specifically below:
1, raw material
(1) gypsum
With CaSO
4Be the natural or industry by-product gypsum of main component, comprise salt gypsum, phosphogypsum, the plaster of paris, desulfurated plaster, titanium gypsum, fluorgypsum, lemon gypsum etc., all can be used as the main raw material of producing sulfuric acid and cement clinker.Require SO
3〉=32%wt, CaO 〉=29%wt, SiO
2≤ 8.0%wt, P
2O
5＜2%wt, F＜0.35%wt.
(2) reductive agent
In decomposition course, be CaSO
4The reductive agent that decomposes.With coke, refinery coke, hard coal etc. all can, require C 〉=60%wt, volatile component Vad＜6%wt.Also tail gas SO can be substituted with industrial sulphur
2Concentration also can improve.
(3) clay
Be used for replenishing SiO
2Form required composition in grog, require SiO
2〉=60%wt.
2, raw material stoving
Determining of (1) two water conservancy project process flow
Conventional production methods all adopts half water conservancy project skill, and the utility model adopts two water conservancy projects skill, dihydrate gypsum good stability, do not lump, the oven dry hear rate is low, and the use thermal source is a system vitriolic over dry tail gas, save the hear rate that is heated to the hyperthermia drying more than 160 ℃, and reduce investment.Therefore the utility model determines to adopt two water conservancy project process flows.
(2) oven dry process description
The gypsum oven dry is carried out in raw material stoving device 4, can select to adopt the pneumatic floating dryer to dry.Gypsum contacts with 70～85 ℃ over dry tail gas from sulfuric acid absorption device 8 in dryer, makes free water evaporates, obtains containing the dihydrate gypsum of free-water＜5%wt.
Subsidiary material such as reductive agent, clay advance in the auxiliary material drying unit 1, contact and dry to moisture≤10%wt with burn till waste heat or the hot flue gas that rotary kiln 9 comes out.The auxiliary material drying unit also can adopt fluidizing furnace that thermal source is provided, and fluidizing furnace is fuel with the coal, and the lime-ash of discharge is as the additive of cement.
3, raw material preparation
Microcomputerized dosing, on-line analysis are adopted in the raw material preparation.Subsidiary material such as reductive agent after metering, clay are after grinding tails over below the 10%wt to fineness requirement 0.08mm square hole sieve together, in the dihydrate gypsum through metering enters the mechanical stirring homogenizing storehouse 11 of steel cylinder system that bottom band stirs discharging, become after the homogenizing and be used for the raw material of decomposing and calcining, add 0.5～3% CaCl simultaneously preparing burden
2Or Na
2SO
4Industry by-product gypsum reaches requirement without grinding fineness, and is little then with oven dry abrasive dust mill because of free water content when using the plaster of paris.
Raw material require:
(1) lime saturation factor
KH＝(CaO-1.18P
2O
5-0.35Fe
2O
3-1.65Al
2O
3)/2.8SiO
2＝1.0±0.1
(2) silica modulus
n＝SiO
2/(Al
2O
3+Fe
2O
3)＝3.7±0.5
(3) iron rate (or aluminium rate)
P＝Al
2O
3/Fe
2O
3＝2.5±0.3
(4) C/SO
3(mol ratio)=0.70～0.80
(5) mean particle size＜60 μ m.
4, preheating, decomposition, calcining
The key equipment of gypsum system producing sulfuric acid and jointly cement is preheating, decomposition, roasting assembly.The mutual combination of novel process such as raw material primary heater unit 5 can adopt that the compound or cyclone preheater of 2-5 level is generally preferable with 3 grades of preheaters, three or four air channel coal rifles and electrostatic precipitator and equipment combines with rotary kiln again; more help the calcining of gypsum dehydration, raw material, can guarantee SO in the kiln gas that rotary kiln 9 produced
2Concentration is 10～14.5%.As burn till with coal and adopt high sulphur coal, not only can reduce cost, also help and improve kiln gas SO
2Concentration.
Raw material after the homogenizing are gone in the inlet pipe of first step cyclone preheater of primary heater unit 5 after metering, after the spreading plate disperses, be carried to and carry out gas solid separation in the first step preheater by hot gas flow, gas is discharged, enters sulfate system after the dust precipitator dedusting through induced draft fan by air outlet tube, solid then enters in the inlet pipe of second stage preheater, is carried in the preheater of the second stage by hot gas flow after the spreading plate disperses.Like this, material passes through preheaters at different levels successively, after after the final stage preheater is preheating to 550～750 ℃, enter in the rotary kiln 9 decompose, calcining.
The decomposition reaction formula is:
2CaSO
4+ C---→ 2CaO+2SO
2↑+CO
2↑ (at CaCl
2Or Na
2SO
4Act on following minute and ungird and finish)
CaO that generates and the SiO in the material
2, Al
2O
3, Fe
2O
3Deng entering clinkering zone, the mineralising reaction takes place, form cement clinker, the calcination reaction formula is:
12CaO+2SiO
2+2Al
2O
3+Fe
2O
3→3CaO·SiO
2+2CaO·SiO
2+3CaO·Al
2O
3+4CaO·Al
2O
3·Fe
2O
3
Cement clinker send cement clinker library after cooler cooling, generation contain SO
2Be that 10～14.5% kiln gas enters the final stage preheater from kiln tail (700～900 ℃), behind the intermediary preheater, arrive the raw material counter current contact of first step cyclone preheater and adding successively, after carrying out heat exchange, discharge (220～280 ℃) from first step cyclone preheater, send into sulfate system through dust precipitator by hot induced draft fan.
Each oxide compound is not to exist with independent state in the cement clinker, but exists with the synthetic compound (common name mineral) of two or more oxide junction.Therefore, the ratio in cement production process between each oxide compound of control, more even more important than the content of controlled oxidation thing, the performance that more can express cement reaches incinerating is influenced.The cement clinker controlling index requires as follows:
1. lime saturation factor
KH＝(CaO-0.35Fe
2O
3-1.65Al
2O
3-0.70SO3-0.78CaS-fCaO-1.18P
2O
5)/2.8SiO
2
＝0.84±0.5
2. silica modulus
n＝SiO
2/(Al
2O
3+Fe
2O
3)＝3.4±0.4
3. iron rate (or aluminium rate)
P＝Al
2O
3/Fe
2O
3＝2.0±0.3
④CaS＜2％、SO
3＜2％、fCaO＜2％、MgO＜2％。
SO
2Gas and cement clinker all generate in rotary kiln 9.Should make SO
2The kiln gas that content is high makes the grog that meets the cement requirement again.Except the proportioning of strictness control raw material, also must strict control kiln atmosphere.When being reducing atmosphere in kiln, easily form elemental sulfur and CaS, elemental sulfur can stop up sulphuric acid device.When being oxidizing atmosphere, CaSO
4Decompose not exclusively, eutectic occurs, rotary kiln is prone to the ring formation phenomenon.So the long-pending content of the general oxysome of kiln atmosphere is controlled at 0.4～1.5%, CO≤0.5%.
5, sulfuric acid is produced
Main processes that sulfuric acid is produced and application number are 200810139276.2, and name is called a kind of gypsum, and to produce the method that is adopted in the patent application of improvement production technique of sulfuric acid and cement consistent.
In this operation, the utility model is 200810139276.2 for application number mainly, and name is called the sulfuric acid absorption operation that a kind of gypsum produces in the patent application of improvement production technique of sulfuric acid and cement and improves.By the SO that contains that transforms workshop section
3The reforming gas first time enter in the sulfuric acid absorption device 8 that to divide two sections absorptions, bottom be that high temperature absorbs, top is low temperature absorption, all use the sulfuric acid circulated sprinkling absorption of 98%wt concentration, makes sulfuric acid.By shown in Figure 3, described sulfuric acid absorption device 8 is divided into three parts by ball collar up and down, and middle part and bottom are 200～240 ℃ high temperature absorber portions, and top is 85～110 ℃ low temperature absorption section, is provided with SO in the bottom
3Import 8-1 and high temperature sulfuric acid outlet 8-2, place at the middle part near the low temperature absorption section is provided with high temperature sulfuric acid import 8-3, be provided with low temperature sulfuric acid import 8-5 at the top of low temperature absorption section, be provided with low temperature sulfuric acid outlet 8-4 in the bottom of low temperature absorption section and be provided with scum dredger 8-7 at the top of sulfuric acid absorption device, on scum dredger, be provided with tail gas outlet 8-6, be filled with acid resistance filler 8-8 in low temperature absorption section and high temperature absorber portion, the shell of described sulfuric acid absorption device 8 is a round shape, liner acid proof lining 8-9.Described high temperature sulfuric acid outlet 8-2 place is provided with vapour generator.
Contain SO
3Gas is through SO
3Import 8-1 enters sulfuric acid absorption device 8 and contacts the higher sulfuric acid of the generation denseer temperature of concentration with the sulfuric acid that enters from high temperature sulfuric acid import 8-3, sulfuric acid enters vapour generator generation byproduct steam from high temperature sulfuric acid outlet 8-2 and lowers the temperature simultaneously after pump is squeezed into high temperature sulfuric acid import 8-3, gas after the absorption enters the top of sulfuric acid absorption device 8, contacts and absorbs into sulfuric acid again with low temperature sulfuric acid import 8-5, low temperature sulfuric acid outlet 8-4.Contain SO
3Gas absorbs SO through two sections
3After removing the disacidify foam, scum dredger 8-7 discharges from tail gas outlet 8-6.Place two-layer acid resistance filler 8-8 in the sulfuric acid absorption device 8 and supported by ball collar, shell rolls with steel plate, liner acid proof lining 8-9.
Come further instruction below in conjunction with specific embodiment.In following examples, 70～85 ℃ the over dry tail gas that the sulfuric acid absorption tower that two used water base gypsum all are to use comes out is dried, and obtains the dihydrate gypsum of free water content＜5%wt, then with clay and reductive agent and CaCl
2Or Na
2SO
4Being mixed together homogenizing is raw material.
Embodiment 1 (doing raw material) with phosphogypsum:
1, the composition of main raw material phosphogypsum, clay, coke, coal is as follows:
(1) phosphogypsum (two is water base) main chemical compositions
| Phosphogypsum | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | MgO | SO 3 | P 2O 5 | F | ∑ |
| Wt，％ | 19.03 | 4.41 | 0.31 | 0.26 | 30.23 | 0.34 | 43.20 | 0.62 | 0.17 | 98.57 |
(2) clay main chemical compositions
| Clay | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | MgO | ∑ |
| Wt，％ | 9.09 | 63.18 | 4.05 | 12.38 | 6.49 | 2.07 | 97.26 |
(3) hard coal technical analysis, ash content analysis
Technical analysis % ash content analysis %
Coke
Wf Vf Af Cf SiO
2Fe
2O
3Al
2O
3CaO MgO adds up to
Wt，％ 1.11 4.14 15.95 77.80 47.88 6.84 31.66 8.72 1.50 96.05
(4) burn till with proximate analysis of coal, ash content analysis
Technical analysis % ash content analysis %
Qdw
Coal
Wf Vf Af Cf SiO
2Fe
2O
3Al
2O
3CaO MgO adds up to
(KJ/Kg)
Wt，％ 1.82 30.86 14.75 53.56 26864 55.10 8.05 21.18 6.84 2.10 93.44
2, the proportioning of raw material, main component and rate value
(1) proportioning of raw material is controlled to be: phosphogypsum 87.5%; Clay 7.0%; Hard coal 5.5%.
(2) the raw material main chemical compositions of Sheng Chenging
| Raw material | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | C | SO 3 | P 2O 5 | F | ∑ |
| Wt，％ | 17.28 | 8.68 | 0.60 | 1.50 | 26.84 | 4.27 | 37.58 | 0.56 | 0.15 | 97.75 |
(3) the rate value of raw material is: KH (lime saturation factor)=1.00; N (silica modulus)=4.13; P (iron rate)=2.50.
(4) fixed carbon C is 4.27%; C/SO
3(mol ratio) is 0.75.
3, the main operation index of cement rotary kiln
4, the main component of grog, rate value, mineral composition
(1) main chemical compositions of the grog of Sheng Chenging
| Grog | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | SO 3 | P 2O 5 | F | ∑ |
| Wt，％ | -0.40 | 21.82 | 1.96 | 3.95 | 65.48 | 0.81 | 1.81 | 0.28 | 95.71 |
(2) the rate value of grog is: KH (lime saturation factor)=0.86; N (silica modulus)=3.69; P (iron rate)=2.0.
(3) mineral composition of grog: CaS is 1.08%; FCaO is 0.92%; C
3S is 45.64%; C
2S is 29.06%; C
3A is 7.81%; C
4AF is 6.01%.
5, the main operation index of sulfuric acid apparatus
6, cement grinds the proportioning of blended material and gypsum: the blended material addition content is 15%; Gypsum (two is water base) addition content is 3%.
7, quality product
(1) sulfuric acid quality: concentration 92.62; Ignition residue 0.049%.(2) cement reaches GB ordinary Portland cement standard.
8, main consumption indicators
Embodiment 2 (doing raw material) with desulfurated plaster:
1, the composition of main raw material desulfurated plaster, clay, coke, coal is as follows:
(1) desulfurated plaster (two is water base) main chemical compositions
| Phosphogypsum | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | MgO | SO 3 | ∑ |
| Wt，％ | 18.22 | 0.85 | 0.23 | 0.29 | 32.02 | 1.15 | 45.36 | 98.12 |
(2) clay main chemical compositions
| Clay | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | MgO | ∑ |
| Wt，％ | 7.00 | 71.11 | 3.10 | 10.06 | 5.38 | 1.55 | 98.20 |
(3) proximate analysis of coke, ash content analysis
Technical analysis % ash content analysis %
Coke Wf Vf Af Cf SiO
2Fe
2O
3Al
2O
3CaO MgO adds up to
Wt，％ 0.87 3.91 21.01 74.54 52.43 6.77 31.89 3.61 0.89 95.59
(4) burn till with proximate analysis of coal, ash content analysis
Technical analysis % ash content analysis %
Qdw
Coal Wf Vf Af Cf (KJ/Kg) SiO
2Fe
2O
3Al
2O
3CaO MgO adds up to
Wt，％ 2.10 31.02 11.98 54.28 26427 49.41 6.37 22.10 11.92 1.54 91.20
2, the proportioning of raw material, main component and rate value
(1) proportioning of raw material is controlled to be: desulfurated plaster 84%; Clay 10.%; Coke 6.0%.
(2) the raw material main chemical compositions of Sheng Chenging
(3) the rate value of raw material is: KH (lime saturation factor)=1.01; N (silica modulus)=3.20; P (iron rate)=2.56.
(4) fixed carbon C is 4.47%; C/SO
3(mol ratio) is 0.78.
3, the main operation index of cement rotary kiln
4, the main component of grog, rate value, mineral composition
(1) main chemical compositions of the grog of Sheng Chenging
| Grog | LOSS | SiO 2 | Fe 2O 3 | Al 2O 3 | CaO | MgO | SO 3 | ∑ |
| Wt，％ | -0.69 | 22.11 | 1.97 | 4.18 | 65.78 | 2.23 | 1.27 | 96.74 |
(2) the rate value of grog is: KH (lime saturation factor)=0.86; N (silica modulus)=3.59; P (iron rate)=2.12.
(3) mineral composition of grog: CaS is 1.86%; FCaO is 1.60%; C
3S is 45.76%; C
2S is 28.03%; C
3A is 7.49%; C
4AF is 6.19%.
5, the main operation index of sulfuric acid apparatus
6, cement grinds the proportioning of blended material and gypsum: the blended material addition content is 15%; Gypsum (two is water base) addition content is 3%.
7, quality product
(1) sulfuric acid quality: concentration 92.68; Ignition residue 0.048%.
(2) go out to grind cement quality and meet GB ordinary Portland cement standard.
8, main consumption indicators
Claims (5)
1. the improvement production equipment of gypsum system sulfuric acid and cement, comprise raw material stoving device (4), auxiliary material drying unit (1), independent grinding device, mechanical stirring homogenizing storehouse (11), raw material primary heater unit (5), rotary kiln (9), purge drying device (6), conversion system (7), sulfuric acid absorption device (8), cement grinds device (9), raw material stoving device (4) is connected with corresponding independent grinding device respectively with auxiliary material drying unit (1), independent grinding device is connected with mechanical stirring homogenizing storehouse, mechanical stirring homogenizing storehouse is connected with the raw material primary heater unit, the raw material primary heater unit is connected with the sulfuric acid absorption device, it is characterized in that, described mechanical stirring homogenizing storehouse is that bottom mechanical stirs discharging steel cylinder homogenizing storehouse, and the thermal source import of described raw material stoving device is connected with the over dry tail gas outlet of sulfuric acid absorption device by pipeline.
2. the improvement production equipment of gypsum system sulfuric acid and cement according to claim 1 is characterized in that the raw material primary heater unit is 2～5 grades of compound or cyclone preheaters.
3. the improvement production equipment of gypsum system sulfuric acid and cement according to claim 1 is characterized in that the raw material stoving device is the pneumatic floating dryer.
4. the improvement production equipment of gypsum system sulfuric acid and cement according to claim 1, it is characterized in that described sulfuric acid absorption device (8) is divided into three parts by ball collar up and down, middle part and bottom are 200～240 ℃ high temperature absorber portions, top is 85～110 ℃ low temperature absorption section, is provided with SO in the bottom
3Import (8-1) and high temperature sulfuric acid outlet (8-2), place at the middle part near the low temperature absorption section is provided with high temperature sulfuric acid import (8-3), be provided with low temperature sulfuric acid import (8-5) at the top of low temperature absorption section, be provided with low temperature sulfuric acid outlet (8-4) in the bottom of low temperature absorption section and be provided with scum dredger (8-7) at the top of sulfuric acid absorption device, on scum dredger, be provided with tail gas outlet (8-6), be filled with acid resistance filler (8-8) in low temperature absorption section and high temperature absorber portion, the shell of described sulfuric acid absorption device (8) is a round shape, liner acid proof lining (8-9).
5. as the improvement production equipment of gypsum system sulfuric acid as described in the claim 4 and cement, it is characterized in that described high temperature sulfuric acid outlet (8-2) locates to be provided with vapour generator.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102863061A (en) * | 2012-09-24 | 2013-01-09 | 长沙理工大学 | Device and method for dry and energy-saving production of polyaluminum chloride water purifying agent |
| CN104944384A (en) * | 2014-03-25 | 2015-09-30 | 山东鲁北企业集团总公司 | Combined process and combined device for comprehensive utilization for chemical decomposition waste sulphuric acid and gypsum |
-
2010
- 2010-11-08 CN CN2010205980357U patent/CN201896071U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102863061A (en) * | 2012-09-24 | 2013-01-09 | 长沙理工大学 | Device and method for dry and energy-saving production of polyaluminum chloride water purifying agent |
| CN102863061B (en) * | 2012-09-24 | 2013-10-23 | 长沙理工大学 | Device and method for dry and energy-saving production of polyaluminum chloride water purifying agent |
| CN104944384A (en) * | 2014-03-25 | 2015-09-30 | 山东鲁北企业集团总公司 | Combined process and combined device for comprehensive utilization for chemical decomposition waste sulphuric acid and gypsum |
| CN104944384B (en) * | 2014-03-25 | 2018-06-19 | 山东鲁北企业集团总公司 | A kind of chemical breakdown Waste Sulfuric Acid and the process integration and device of gypsum comprehensive utilization |
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