CN104492106B - A kind of coking desulfurization sulfur foam and the drying means of desulfurization waste liquor - Google Patents
A kind of coking desulfurization sulfur foam and the drying means of desulfurization waste liquor Download PDFInfo
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- CN104492106B CN104492106B CN201410820970.6A CN201410820970A CN104492106B CN 104492106 B CN104492106 B CN 104492106B CN 201410820970 A CN201410820970 A CN 201410820970A CN 104492106 B CN104492106 B CN 104492106B
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- desulfurization
- sulfur
- waste liquor
- desulfurization waste
- coking
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 132
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 123
- 230000023556 desulfurization Effects 0.000 title claims abstract description 123
- 238000001035 drying Methods 0.000 title claims abstract description 113
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 106
- 239000011593 sulfur Substances 0.000 title claims abstract description 106
- 239000006260 foam Substances 0.000 title claims abstract description 76
- 239000002699 waste material Substances 0.000 title claims abstract description 73
- 238000004939 coking Methods 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 claims abstract description 50
- 230000008569 process Effects 0.000 claims abstract description 20
- 239000000428 dust Substances 0.000 claims abstract description 10
- 238000005406 washing Methods 0.000 claims abstract description 10
- 239000007921 spray Substances 0.000 claims abstract description 7
- 238000001816 cooling Methods 0.000 claims abstract description 6
- 239000002002 slurry Substances 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 10
- 239000006071 cream Substances 0.000 claims description 6
- 239000012141 concentrate Substances 0.000 claims description 3
- 230000003009 desulfurizing effect Effects 0.000 claims description 3
- 238000010790 dilution Methods 0.000 claims description 3
- 239000012895 dilution Substances 0.000 claims description 3
- 239000008187 granular material Substances 0.000 abstract description 4
- 238000003860 storage Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 17
- 239000000571 coke Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 239000000843 powder Substances 0.000 description 6
- 150000003839 salts Chemical group 0.000 description 6
- 239000005864 Sulphur Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000006199 nebulizer Substances 0.000 description 3
- 230000008719 thickening Effects 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- XAQHXGSHRMHVMU-UHFFFAOYSA-N [S].[S] Chemical compound [S].[S] XAQHXGSHRMHVMU-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 238000005276 aerator Methods 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000005119 centrifugation Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 2
- 239000002341 toxic gas Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical class [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 1
- NIPNSKYNPDTRPC-UHFFFAOYSA-N N-[2-oxo-2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)ethyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 NIPNSKYNPDTRPC-UHFFFAOYSA-N 0.000 description 1
- CYTYCFOTNPOANT-UHFFFAOYSA-N Perchloroethylene Chemical group ClC(Cl)=C(Cl)Cl CYTYCFOTNPOANT-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 229940069428 antacid Drugs 0.000 description 1
- 239000003159 antacid agent Substances 0.000 description 1
- 230000001458 anti-acid effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000007500 overflow downdraw method Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 150000003463 sulfur Chemical class 0.000 description 1
- DHCDFWKWKRSZHF-UHFFFAOYSA-N sulfurothioic S-acid Chemical compound OS(O)(=O)=S DHCDFWKWKRSZHF-UHFFFAOYSA-N 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 230000026676 system process Effects 0.000 description 1
- 229950011008 tetrachloroethylene Drugs 0.000 description 1
- 239000010891 toxic waste Substances 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, it comprises the steps, it comprises the steps, coking desulfurization sulfur foam and desulfurization waste liquor are delivered to drying tower by conveying equipment and are dried by a；Sulfur foam and desulfurization waste liquor in step a described in b obtain thick sulfur powder from drying tower bottom collection in drying tower after drying；In step a described in c, the entrance of the tail gas in drying tower cyclone separator carries out dust removal process；In step c described in d, the tail gas entrance spray column through dust removal process carries out cooling washing.The method of the present invention makes coking desulfurization sulfur foam and desulfurization waste liquor be dried to obtain saliferous thick sulfur powder simultaneously, new way is provided for process and the utilization of desulfurization waste liquor in coking system, do not result in secondary pollution, and enable desulfurization waste liquor to be processed timely and effectively, the saliferous thick sulfur powder that the drying means of the present invention obtains does not lumps and does not draw tide, granule is uniform, easy storage and transport.
Description
Technical field
The present invention relates to the drying means of a kind of coking desulfurization, particularly relate to a kind of coking desulfurization sulfur foam and
The drying means of desulfurization waste liquor.
Background technology
Coke gas desulfurization by-product sulfur foam-drying belongs to the category preparing sulfur, but the impurity in sulfur foam is relatively
Many, typically need purified process.The method that at present sulfur purifies has a several types: 1. fusion method, the method
There is the problems such as Recovered sulphur purity is the highest, sulfur productivity is low, energy consumption is too high, production cost is high；2. extract
Method, utilizes extractant dissolve the sulfur in material and use the method for solid-liquid separation to be separated by sulfur.Often
Extractant have Carbon bisulfide, tetrachloroethylene, carbon tetrachloride etc.；3. sublimed method, will sulfur heating
After boiling point, the principle of evaporation purifies.It is the most melted that above several method is applied in the industrial production
Method, its technique have also been obtained the biggest improvement along with the development of technology.Such as first requirement in acid production with sulphur technique
Filtering after sulfur melting, its condition is that this sulfur purity wants height, and contained impurity is mainly nothing
Machine impurity；Extraction is relatively big due to the extractant toxicity of exploitation at present, and complex process, returning of extractant
Receiving and the process of residue, safety and environmental protection have certain difficulty, large-scale application exists the most in the industry
Technical bottleneck；Sublimed method develops into also create in current technique multiple method, such as vacuum distillation method, i.e. profit
The boiling point of sulfur is reduced by fine vacuum.Vacuum distillation method is currently mainly applied to the refinement of some rare metals,
Also someone applies it to the purification of sulfur, but vacuum distillation method needs decompressor, and process also needs material
Heat, be the most only in development.
In coke-oven plant's wet desulphurization by-product sulfur foam, impurity content is high at present, recycle difficulty, is generally made
For Solid Waste Treatment.Due to the above-mentioned way of distillation, extraction, sulfur melting method Recovered sulphur production cost height,
Existing sulfur foam recovery processes more employing filter press technique, and what filter press technique produced crosses cleaner liquid containing suspension sulfur content about
0.5%, greatly reduce suspension sulfur blocking tower body and the probability of equipment, improve doctor solution gas-liquid mass transfer efficiency,
Desulfurized effect；The energy-saving effect of filter press technique is obvious, is the developing direction of coking sulfur foam process technique, but this work
Secondary salt problem in skill untreated sulfur foam, makes desulphurization system produce substantial amounts of toxic waste liquid in running,
Environment is had a negative impact.
Wet method coke oven gas desulfurization is the most a lot of coal gas or the prevailing technology of coal chemical enterprise.But its desulfurization is given up
Liquid is not because containing substantial amounts of rhodanate, thiosulfate and sulfate etc., using at the methods such as biochemistry
Reason.The most mostly using two kinds of processing methods, one is to be discharged to coal works by directly outer for desulfurization waste liquor, enters coke oven
Burning disposal, but this method can bring environmental pollution to Coal Blending System, causes secondary pollution, and increases coking
Energy consumption, severe corrosion equipment, and also desulfurization waste liquor enters the sulfur content that can increase coke in coke, causes coke
Quality Down；Two is to arrange salt extraction device after sulfur removal technology, is extracted by the salt in desulfurization waste liquor, enters
Row recycles, but generally salt extraction installation cost is higher, and investment is reclaimed slow, and the purity salt extracted is relatively low,
Economy return is the highest.Therefore desulfurization waste liquor is the most intractable waste water in coke-oven plant.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of coking desulfurization sulfur foam and the dry side of desulfurization waste liquor
Method, the method can not be lumpd and not drawn saliferous damp, evengranular thick sulfur powder, easily preserve and
Transport, and the process and utilization for desulfurization waste liquor provides a kind of brand-new processing method, does not the most exist useless
The process problem of liquid, successfully solves the environmental pollution of existing technique and the problem that operating cost is high.
For solving above-mentioned technical problem, the invention provides being dried of a kind of coking desulfurization sulfur foam and desulfurization waste liquor
Method, it comprises the steps,
Coking desulfurization sulfur foam and desulfurization waste liquor are delivered to drying tower by conveying equipment and are dried by a；
Sulfur foam and desulfurization waste liquor in step a described in b obtain from drying tower bottom collection in drying tower after drying
To thick sulfur powder；
In step a described in c, the entrance of the tail gas in drying tower cyclone separator carries out dust removal process；
In step c described in d, the tail gas entrance spray column through dust removal process carries out cooling washing.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, in described step a, by coking
Desulfurization sulfur foam and desulfurization waste liquor are delivered to concentrator by conveying equipment and concentrate, concentrated after obtain
Sulfur foam and desulfurization waste liquor slurry enter drying tower be dried.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, described concentrator is centrifugal mist
Change device.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, the desulfurization sulfur bubble after described concentration
The solid-to-liquid ratio (weight) of foam and desulfurization waste liquor slurry is 20%-50%.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, in described step a, described
The top of drying tower arranges hot-air distributor, and this hot-air distributor connects with burner, so that burner produces
Hot blast by hot-air distributor even in described drying tower.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, in described entrance hot-air distributor
Hot blast temperature be 150-250 DEG C.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, through concentrating in described step a
The desulfurization sulfur foam of rear entrance drying tower and desulfurization waste liquor slurry and the heat being entered drying tower by hot-air distributor
The volume flow ratio of wind is 1:10 × 103-40×103。
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, in described step a in drying tower
The exhaust temperature of offgas outlet be 50-105 DEG C.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, drying tower in described step a
Top, middle part, bottom are respectively provided with pneumatic hammer.
Above-mentioned coking desulfurization sulfur foam and the drying means of desulfurization waste liquor, wherein, the coking in described step a takes off
Sulfur sulfur foam is the sulfur-bearing foam produced in wet desulfurizing process, or the sulfur of this treated generation of sulfur-bearing foam
Mud, sulfur cream, or sulfur mud, the sulfur cream sulfur-bearing slurry of gained after dilution.
Use coking desulfurization sulfur foam and the drying means of desulfurization waste liquor of the present invention, by coking desulfurization sulfur foam
And desulfurization waste liquor carries out thickening filtration jointly, being sent in drying tower by drying tower top afterwards, hot blast passes through
The hot-air distributor that drying tower top is arranged enters in drying tower, the sulfur foam carried from drying tower top
And desulfurization waste liquor enter into drying tower after under equally distributed hot wind action, be dried to the thick Cosan of saliferous
End.The tail gas that sulfur foam and desulfurization waste liquor are discharged in drying tower after drying is mainly steam and ammonia,
Tail gas after cyclone separator dedusting carries out cooling washing finally by spray column, after tail gas is purified
Can directly discharge, cleaning mixture can return desulphurization system.
The coking desulfurization sulfur foam of the present invention and the drying means of desulfurization waste liquor, have the advantages that
1, coking desulfurization sulfur foam and desulfurization waste liquor are sent in drying tower by the drying means of the present invention jointly
Row is dried, and obtains the thick sulfur powder of saliferous, and dried saliferous thick sulfur powder can be sent in incinerator
Carry out burning prepared sulfur dioxide, send into acid making system afterwards and prepare sulphuric acid.The method of the present invention makes coking take off
Sulfur sulfur foam and desulfurization waste liquor are dried simultaneously and obtain saliferous thick sulfur powder, for desulfurization waste liquor in coking system
Process and utilization provide new way, do not result in secondary pollution, enable desulfurization waste liquor to obtain in time
Effective process；
2, the exhaust temperature controlling drying tower in the drying means of the present invention is 50-105 DEG C, and be dried to obtain contains
Salt thick sulfur powder does not lump and does not draw tide, and easy storage and transport, granule is uniform；
3, the drying means of the present invention, it is possible to the effective sulphur-containing substance reclaimed in sulfur foam and desulfurization waste liquor,
The response rate can reach more than 98%；
4, in the drying means of the present invention dry run to coking desulfurization sulfur foam and desulfurization waste liquor, do not deposit
In the process of waste liquid, successfully solve the environmental pollution of existing technique and the problem that operating cost is high；
5, the tail gas after removing dust is washed in the drying means of the present invention can directly discharge, and washings can
Directly to return desulphurization system, meet environmental requirement.
Accompanying drawing explanation
Fig. 1 is the flow chart of the drying means of coking desulfurization sulfur foam of the present invention and desulfurization waste liquor；
Fig. 2 be in Fig. 1 A-A to sectional view.
Detailed description of the invention
The present invention is described in detail below in conjunction with the accompanying drawings with embodiment.
Embodiment 1
As depicted in figs. 1 and 2, coking desulfurization sulfur foam and desulfurization waste liquor are sent into screw pump 1 and pump into centrifugal
Thickening filtration is carried out in nebulizer 2.Through mist after sulfur foam and desulfurization waste liquor nebulizer 2 thickening filtration by centrifugation
Change nozzle and enter drying tower 3 top.After coking desulfurization sulfur foam and desulfurization waste liquor nebulizer 2 by centrifugation concentrates
Obtaining sulfur foam and desulfurization waste liquor slurry, the solid-to-liquid ratio (weight) of slurry is 30%, enters the sulfur of drying tower 3
The volume flow of foam and desulfurization waste liquor slurry is 2 cubes ms/h.
Air enters burner 5 by aerator 4, and the fuel of air and entrance burner 5 is in burner 5
Producing hot blast, hot blast temperature is 200 DEG C, and hot blast enters into the hot blast at drying tower 3 top by hot air duct
In allotter 6, hot blast enters in drying tower 3 afterwards, and the volume flow of the hot blast entering drying tower is 40 ×
103Cube m/h.Hot blast can also use the coke oven flue steam in coke-oven plant.As in figure 2 it is shown, it is hot
The hot-air distributor 6 that wind is arranged by drying tower 3 top enters in drying tower 3, sulfur foam after concentration and
Desulfurization waste liquor slurry enters in drying tower by the nozzle of the centrifugal atomizer 2 at drying tower 3 top, sulfur foam
And desulfurization waste liquor slurry enter into drying tower 3 after to be dried to saliferous under equally distributed hot wind action thick
Sulfur powder, sulfur foam after concentration and desulfurization waste liquor slurry and hot blast enter the volume flow ratio of drying tower 3
For 1:20 × 103。
Sulfur foam and desulfurization waste liquor slurry drying tower 3 are dried, are received by the valve 7 of drying tower 3 bottom
Collection obtains the thick sulfur powder of saliferous, and the temperature of drying tower 3 tail gas is 70 DEG C, and the tail gas of discharge is mainly water
Steam and ammonia.
The upper, middle and lower of drying tower 3 is respectively provided with three aerofluxus hammers 12, and compressed air enters three aerofluxuss
Hammer 12, drives upper, middle and lower three aerofluxus hammer 12, beats drying tower 3, make the sulfur-bearing powder being bonded on drying tower 3
Come off, improve the response rate.
Tail gas in drying tower 3 carries out dedusting by the cyclone separator 8 of two series connection, by controlling whirlwind
Valve 7 bottom separator 8 can be collected further and obtain dried thick sulfur powder.After dedusting
Tail gas enter spray column 10 via aerator 9, by spray column 10 carry out cooling washing, spray column 10
Using circulating pump 11 to carry cleaning mixture and carry out cooling washing, tail gas can directly discharge after being purified,
Cleaning mixture can return coking desulfurization system.
In the drying means of the present invention, coking desulfurization sulfur foam is the sulfur-bearing foam produced in wet desulfurizing process,
Or the sulfur mud of this treated generation of sulfur-bearing foam, sulfur cream, or sulfur mud, sulfur cream the containing of gained after dilution
Sulfur slurry.
The moisture content of the saliferous thick sulfur powder obtained in the present embodiment is 4.65%, does not lump and does not draw tide, granule
Uniformly, yield is up to 98.1%.
The drying means of embodiment 2-embodiment 5 and comparative example 1-3 is same as in Example 1, design parameter
It is shown in Table 1.
Table 1
Note: 1, solid content refer to concentrated after sulfur foam and the solid content (weight) of desulfurization waste liquor slurry；
2, hot blast temperature fingering enters the temperature of hot blast of drying tower；
3, volume flow ratio refer to concentrated after sulfur foam and desulfurization waste liquor slurry and hot blast enter the volume flow ratio of drying tower；
4, exhaust temperature refers to the offgas outlet temperature of drying tower；
5, moisture content refers to the moisture content (weight) of saliferous thick sulfur powder that drying tower obtains after drying；
6, yield refers to the yield of saliferous thick sulfur powder that drying tower obtains after drying, collects including after cyclone separator dedusting
The powder arrived；
7, powder outward appearance refers to the outward appearance of saliferous thick sulfur powder that drying tower obtains after drying；
8, exhaust gas component refers to the exhaust gas component of offgas outlet of drying tower.
As it can be seen from table 1 the offgas outlet temperature of drying tower is controlled at 50-105 DEG C by the present invention,
To the moisture content of saliferous thick sulfur powder substantially can control below 5%, granule is uniform, does not lump and does not draws
Tide, and the tail gas of the offgas outlet of drying tower is mainly steam and ammonia, straight after can washing with removing dust
Run in and put.In comparative example 1, the offgas outlet temperature of drying tower is too high, causes the saliferous material in powder to occur
Decompose, create toxic gas, environment is had a negative impact, it is impossible to directly discharge after removing dust washing,
And yield is decreased obviously.In comparative example 2, the offgas outlet temperature of drying tower is relatively low, the saliferous being dried to obtain
Thick sulfur powder moisture content is higher, the saliferous thick sulfur powder generation caking phenomenon obtained after drying, uneven,
Such powder is sent into when carrying out burning sulfur dioxide processed in follow-up incinerator, is easily caused equipment blocking.
In comparative example 3, hot blast temperature is the highest, causes offgas outlet temperature too high, causes the saliferous material in powder to be sent out
Solution estranged, creates toxic gas, has a negative impact environment, it is impossible to directly discharge after removing dust washing.
Coking desulfurization sulfur foam and two kinds of industrial wastes of desulfurization waste liquor are sent into by the drying means of the present invention jointly
Being dried in drying tower, process and utilization for desulfurization waste liquor provide new way.And, the present invention's
Drying means has obtained the thick Cosan of evengranular saliferous by the outlet temperature effectively controlling drying tower tail gas
End, water content may remain in less than 5%, does not lump and does not draws tide, easy storage and transport, and yield can
Reach more than 98%.The saliferous thick sulfur powder that the drying means of the present invention obtains can be sent directly into follow-up burning
Stove burns and prepares sulfur dioxide, send into acid making system antacid afterwards.
Claims (10)
1. coking desulfurization sulfur foam and a drying means for desulfurization waste liquor, it comprises the steps,
Coking desulfurization sulfur foam and desulfurization waste liquor are delivered to drying tower by conveying equipment and are dried by a；
Sulfur foam and desulfurization waste liquor in step a described in b obtain from drying tower bottom collection in drying tower after drying
To thick sulfur powder；
In step a described in c, the entrance of the tail gas in drying tower cyclone separator carries out dust removal process；
In step c described in d, the tail gas entrance spray column through dust removal process carries out cooling washing.
2. coking desulfurization sulfur foam as claimed in claim 1 and the drying means of desulfurization waste liquor, wherein, institute
State in step a, coking desulfurization sulfur foam and desulfurization waste liquor are delivered to concentrator by conveying equipment and carry out
Concentrate, concentrated after the sulfur foam that obtains and desulfurization waste liquor slurry enter drying tower and be dried.
3. coking desulfurization sulfur foam as claimed in claim 2 and the drying means of desulfurization waste liquor, wherein, institute
Stating concentrator is centrifugal atomizer.
4. coking desulfurization sulfur foam as claimed in claim 2 or claim 3 and the drying means of desulfurization waste liquor, wherein,
Desulfurization sulfur foam and the solid-to-liquid ratio (weight) of desulfurization waste liquor slurry after described concentration are 20%-50%.
5. coking desulfurization sulfur foam as claimed in claim 4 and the drying means of desulfurization waste liquor, wherein, institute
Stating in step a, arrange hot-air distributor at the top of described drying tower, this hot-air distributor is with burner even
Connect, so that the hot blast that burner produces passes through hot-air distributor even in described drying tower.
6. coking desulfurization sulfur foam as claimed in claim 5 and the drying means of desulfurization waste liquor, wherein, institute
State the hot blast temperature entered in hot-air distributor and be 150-250 DEG C.
7. coking desulfurization sulfur foam as claimed in claim 6 and the drying means of desulfurization waste liquor, wherein, institute
State and step a enters the desulfurization sulfur foam of drying tower after concentrating and desulfurization waste liquor slurry divides with by hot blast
The volume flow ratio of the hot blast that orchestration enters drying tower is 1:10 × 103-40×103。
8. coking desulfurization sulfur foam as claimed in claim 1 or 2 and the drying means of desulfurization waste liquor, wherein,
In described step a, the exhaust temperature of the offgas outlet in drying tower is 50-105 DEG C.
9. coking desulfurization sulfur foam as claimed in claim 1 or 2 and the drying means of desulfurization waste liquor, wherein,
In described step a, the top of drying tower, middle part, bottom are respectively provided with pneumatic hammer.
10. coking desulfurization sulfur foam as claimed in claim 1 or 2 and the drying means of desulfurization waste liquor, wherein,
Coking desulfurization sulfur foam in described step a is the sulfur-bearing foam produced in wet desulfurizing process, or this contains
The sulfur mud of the treated generation of sulfur foam, sulfur cream, or sulfur mud, the sulfur cream sulfur-bearing slurry of gained after dilution.
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| CN201410820970.6A CN104492106B (en) | 2014-10-17 | 2014-12-24 | A kind of coking desulfurization sulfur foam and the drying means of desulfurization waste liquor |
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| CN2014105537357 | 2014-10-17 | ||
| CN201410553735 | 2014-10-17 | ||
| CN201410820970.6A CN104492106B (en) | 2014-10-17 | 2014-12-24 | A kind of coking desulfurization sulfur foam and the drying means of desulfurization waste liquor |
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| Publication Number | Publication Date |
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| CN104492106B true CN104492106B (en) | 2016-08-24 |
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| CN110078028B (en) * | 2018-04-27 | 2022-09-13 | 李金山 | Drying method of sulfur salt mixture |
| CN109052330A (en) * | 2018-09-12 | 2018-12-21 | 昌吉学院 | A method of sulphur simple substance is prepared using coking of coal desulfurization waste liquor |
| CN109534299B (en) * | 2018-12-27 | 2023-11-28 | 中冶焦耐(大连)工程技术有限公司 | Process and device for preparing sulfur slurry by vacuum evaporation treatment of coked sulfur foam |
| CN113086951A (en) * | 2021-03-24 | 2021-07-09 | 武汉科技大学 | Process for preparing high-purity sulfur by hot blowing desorption method |
| CN114590946B (en) * | 2022-03-24 | 2023-03-17 | 安徽益硫环境科技有限公司 | Drying method of sulfur foam and desulfurization waste liquid |
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| CN101804970A (en) * | 2010-03-25 | 2010-08-18 | 安徽临泉化工股份有限公司 | Exchangeable process for recovering and separating regenerated sulfur by condensation and curing |
| CN102381687A (en) * | 2011-02-12 | 2012-03-21 | 李金山 | Method for preparing acid by using sulfur containing waste material and wet method desulphurization process containing method thereof |
| CN203855411U (en) * | 2014-01-23 | 2014-10-01 | 北京华泰焦化工程技术有限公司 | Device for producing liquid sulfur dioxide from sulfur foam or sulfur-containing impurities |
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| CN101804970A (en) * | 2010-03-25 | 2010-08-18 | 安徽临泉化工股份有限公司 | Exchangeable process for recovering and separating regenerated sulfur by condensation and curing |
| CN102381687A (en) * | 2011-02-12 | 2012-03-21 | 李金山 | Method for preparing acid by using sulfur containing waste material and wet method desulphurization process containing method thereof |
| CN203855411U (en) * | 2014-01-23 | 2014-10-01 | 北京华泰焦化工程技术有限公司 | Device for producing liquid sulfur dioxide from sulfur foam or sulfur-containing impurities |
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