CN104232190A - Direct pulping process for floatation concentrate - Google Patents
Direct pulping process for floatation concentrate Download PDFInfo
- Publication number
- CN104232190A CN104232190A CN201410410945.0A CN201410410945A CN104232190A CN 104232190 A CN104232190 A CN 104232190A CN 201410410945 A CN201410410945 A CN 201410410945A CN 104232190 A CN104232190 A CN 104232190A
- Authority
- CN
- China
- Prior art keywords
- floating
- essence
- pulping process
- floating essence
- additive
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Paper (AREA)
Abstract
The invention discloses a direct pulping process for flotation concentrate. The direct pulping process for flotation concentrate, which is disclosed by the invention, is simple in process, high in production efficiency and low in production cost, the average pulping rate is over 95%, and in addition, 5% of products are large particles and can be recycled.
Description
Technical field
The present invention relates to coal water slurry preparing technical field, particularly relate to a kind of floating essence directly pulping process.
Background technology
Coal water slurry, it is a kind of fuel slurry, can pumping as oil, atomization, storage and stable burning, its calorific value is equivalent to the half of oil fuel, oil fuel can be replaced to be used for boiler, power station, industrial furnace and kiln, for replacing coal to use, having that combustion benefits is high, load adjustment is convenient, reducing environmental pollution, improving working conditions and the advantage such as saving coal.Coal water slurry is the best achievement of coal liquefaction, is also the practical technique that coal-cleaning utilization is the most cheap.
How to adopt simplify most operation, enhance productivity, reduce cost of labor, reduce equipment loss, on the whole reduce production cost be the problem to be solved in the present invention.
Summary of the invention
Object of the present invention is exactly defect for above-mentioned existence and provides a kind of floating essence directly pulping process.The present invention's floating essence directly slurrying, technique is simple, and production efficiency is high, and production cost is low, and pulping rate is on average more than 95%, and in addition, 5% is macrobead recoverable.
" floating essence " i.e. of the present invention floating cleaned coal is alternatively the cleaned coal selected by the method for flotation.
The floating essence of one of the present invention directly pulping process technical scheme is comprise the following steps:
(1) agitated pool operation:
Dig agitated pool at subsurface, while floating essence is injected agitated pool, water, additive are injected agitated pool simultaneously, stir, get final product pulping;
(2) filter pulp tank operation:
Pulping goes out pond, enters filter pulp tank operation, and by filter pulp tank, qualified finished pulp injects slurry can, waits to deliver; And in floating essence granularity more greatly, do not melt the particle of slurry, screenedly out reclaim, macrobead is accumulated to some amount, broken by ball mill link, slurrying again.
In step (1), described floating smart mean particle size is at below 0.5mm.
In step (1), floating essence, water, additive are by weight: 60-70:30-39:0.3-1.
Preferably, in step (1), floating essence, water, additive are by weight: 66:33:1.
In step (1), after floating essence, water, additive inject agitated pool, main liquid level reaches 2/3 At The Height of agitated pool.
In step (1), additive comprises sodium metnylene bis-naphthalene sulfonate, potassium primary phosphate, Sodium phosphate dibasic, wilkinite, ammoniacal liquor.
In step (1), additive comprises sodium metnylene bis-naphthalene sulfonate 15-25 part by weight, potassium primary phosphate 5-15 part, Sodium phosphate dibasic 5-15 part, wilkinite 5-10 part, ammoniacal liquor 15-35 part.
Preferably, in step (1), additive comprises sodium metnylene bis-naphthalene sulfonate 18 parts, potassium primary phosphate 12 parts, Sodium phosphate dibasic 8 parts, wilkinite 9 parts, ammoniacal liquor 25 parts by weight.
Beneficial effect of the present invention is: the present invention's pulping rate of the direct slurrying of floating essence, through many experiments, pulping rate is on average more than 95%, and in addition, 5% is macrobead recoverable.The present invention specifically has following advantage:
1. present invention process eliminates tradition and prepares lift, conveyer, ball mill operation in coal water slurry process, and operation simplifies, and saves the pulping time, improves production efficiency;
2. operation simplifies, and unit finished pulp cost lands vertically 43.9 yuan (the artificial expense of saving does not count);
The existing ball mill rated output of company is 630 kilowatt-hours, and power consumption per hour is 630 degree of electricity, by often spending the 0.9 yuan of calculating of level average price, the electricity charge per hour 567 yuan;
Conveyer rated output is 150 kilowatt-hours, and power consumption per hour is 150 degree of electricity, by often spending the 0.9 yuan of calculating of level average price, the electricity charge per hour 135 yuan;
Other utility appliance rated output of traditional technology amount to 50 kilowatt-hours, power consumption per hour 50 degree, by often spending the 0.9 yuan of calculating of level average price, the electricity charge per hour 45 yuan;
By the Production rate of present 17 tphs, present invention process is compared with traditional technology, and finished pulp cost per ton can directly reduce by 43.9 yuan.
(567 yuan+135 yuan+45 yuan) ÷ 17 tons=43.9 yuan/ton
Above data calculate according to the rated output saving equipment, are gross data, and in actual production, equipment runs and do not reach at full capacity, and power will be slightly less than rated output, and corresponding energy-conservation expense is slightly less than above data possibly.
(3) operation simplifies, and manually reduces, decreases the equipment loss of ball mill simultaneously.
embodiment:
In order to understand the present invention better, describe technical scheme of the present invention in detail with specific examples below, but the present invention is not limited thereto.
Embodiment 1
(1) agitated pool operation:
The agitated pool of 6.6 meters * 3 meters * 2.8 meters is dug, while floating essence (mean particle size is at below 0.5mm) is injected agitated pool successively, according to the proportional amount of water, medicament at subsurface, inject agitated pool, main liquid level stirs, gets final product pulping till reaching 2/3 At The Height of agitated pool.Floating essence, water, additive are by weight: 66:33:1.Additive comprises sodium metnylene bis-naphthalene sulfonate 18 parts, potassium primary phosphate 12 parts, Sodium phosphate dibasic 8 parts, wilkinite 9 parts, ammoniacal liquor 25 parts by weight.
(2) filter pulp tank operation:
Pulping goes out pond, enters filter pulp tank operation, and by filter pulp tank, qualified finished pulp injects slurry can, waits to deliver; And in floating essence granularity more greatly, do not melt the particle of slurry, screenedly out reclaim, macrobead is accumulated to some amount, broken by ball mill link, slurrying again.
Coal water slurry prepared by present invention process, concentration >67%, viscosity <1195(slurry temperature 20 DEG C, shearing rate 100s
-1time) mPa.s, thermal value >20.1MJ/kg, ash content <5.80%, sulfur <0.34%, coal ash melting property softening temperature >1250 DEG C.
According to regulation in the People's Republic of China's national standard " COAL-WATER SLURRY TECHNOLOGY condition " (GB/T18855-2002), be better than I grade standard.
This technique pulping rate of the direct slurrying of floating essence, through many experiments, pulping rate is on average more than 95%, and in addition, 5% is macrobead recoverable.Specifically there is following advantage:
1. present invention process eliminates tradition and prepares lift, conveyer, ball mill operation in coal water slurry process, and operation simplifies, and saves the pulping time, improves production efficiency;
2. operation simplifies, and unit finished pulp cost lands vertically 43.9 yuan (the artificial expense of saving does not count);
The existing ball mill rated output of company is 630 kilowatt-hours, and power consumption per hour is 630 degree of electricity, by often spending the 0.9 yuan of calculating of level average price, the electricity charge per hour 567 yuan;
Conveyer rated output is 150 kilowatt-hours, and power consumption per hour is 150 degree of electricity, by often spending the 0.9 yuan of calculating of level average price, the electricity charge per hour 135 yuan;
Other utility appliance rated output of traditional technology amount to 50 kilowatt-hours, power consumption per hour 50 degree, by often spending the 0.9 yuan of calculating of level average price, the electricity charge per hour 45 yuan;
By the Production rate of present 17 tphs, present invention process is compared with traditional technology, and finished pulp cost per ton can directly reduce by 43.9 yuan.
(567 yuan+135 yuan+45 yuan) ÷ 17 tons=43.9 yuan/ton
Above data calculate according to the rated output saving equipment, are gross data, and in actual production, equipment runs and do not reach at full capacity, and power will be slightly less than rated output, and corresponding energy-conservation expense is slightly less than above data possibly.
(3) operation simplifies, and manually reduces, decreases the equipment loss of ball mill simultaneously.
Claims (8)
1. a floating essence directly pulping process, is characterized in that, comprise the following steps:
(1) agitated pool operation:
Dig agitated pool at subsurface, while floating essence is injected agitated pool, water, additive are injected agitated pool simultaneously, stir, get final product pulping;
(2) filter pulp tank operation:
Pulping goes out pond, enters filter pulp tank operation, and by filter pulp tank, qualified finished pulp injects slurry can, waits to deliver; And in floating essence granularity more greatly, do not melt the particle of slurry, screenedly out reclaim, macrobead is accumulated to some amount, broken by ball mill link, slurrying again.
2. the floating essence of one according to claim 1 directly pulping process, it is characterized in that, in step (1), described floating smart mean particle size is at below 0.5mm.
3. the floating essence of one according to claim 1 directly pulping process, is characterized in that, in step (1), floating essence, water, additive are by weight: 60-70:30-39:0.3-1.
4. according to the floating essence of one according to claim 3 directly pulping process, it is characterized in that, in step (1), floating essence, water, additive are by weight: 66:33:1.
5. the floating essence of one according to claim 1 directly pulping process, is characterized in that, in step (1), after floating essence, water, additive inject agitated pool, main liquid level reaches 2/3 At The Height of agitated pool.
6. the floating essence of one according to claim 1 directly pulping process, it is characterized in that, in step (1), additive comprises sodium metnylene bis-naphthalene sulfonate, potassium primary phosphate, Sodium phosphate dibasic, wilkinite, ammoniacal liquor.
7. the floating essence of one according to claim 6 directly pulping process, it is characterized in that, in step (1), additive comprises sodium metnylene bis-naphthalene sulfonate 15-25 part by weight, potassium primary phosphate 5-15 part, Sodium phosphate dibasic 5-15 part, wilkinite 5-10 part, ammoniacal liquor 15-35 part.
8. the floating essence of one according to claim 7 directly pulping process, it is characterized in that, in step (1), additive comprises sodium metnylene bis-naphthalene sulfonate 18 parts, potassium primary phosphate 12 parts, Sodium phosphate dibasic 8 parts, wilkinite 9 parts, ammoniacal liquor 25 parts by weight.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410410945.0A CN104232190B (en) | 2014-08-20 | 2014-08-20 | A kind of floating essence directly pulping process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410410945.0A CN104232190B (en) | 2014-08-20 | 2014-08-20 | A kind of floating essence directly pulping process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104232190A true CN104232190A (en) | 2014-12-24 |
| CN104232190B CN104232190B (en) | 2016-01-20 |
Family
ID=52221102
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410410945.0A Expired - Fee Related CN104232190B (en) | 2014-08-20 | 2014-08-20 | A kind of floating essence directly pulping process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104232190B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242918A (en) * | 2013-05-16 | 2013-08-14 | 江苏神瑞新能源有限公司 | Method for preparing high-concentration water-coal slurry by using flotation clean coals |
| WO2013165217A1 (en) * | 2012-05-04 | 2013-11-07 | 한국생명공학연구원 | Method for producing biodiesel using microorganisms without drying process |
| CN103865598A (en) * | 2012-12-13 | 2014-06-18 | 大唐国际化工技术研究院有限公司 | Method using brown coal for preparation of high density coal water slurry |
-
2014
- 2014-08-20 CN CN201410410945.0A patent/CN104232190B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013165217A1 (en) * | 2012-05-04 | 2013-11-07 | 한국생명공학연구원 | Method for producing biodiesel using microorganisms without drying process |
| CN103865598A (en) * | 2012-12-13 | 2014-06-18 | 大唐国际化工技术研究院有限公司 | Method using brown coal for preparation of high density coal water slurry |
| CN103242918A (en) * | 2013-05-16 | 2013-08-14 | 江苏神瑞新能源有限公司 | Method for preparing high-concentration water-coal slurry by using flotation clean coals |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104232190B (en) | 2016-01-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106244266A (en) | Fractal grating technology is utilized to prepare the method for water-coal-slurry and the water-coal-slurry of preparation | |
| CN102992285A (en) | Method and equipment for producing yellow phosphorus by utilizing closed annular heating furnace | |
| CN102766494B (en) | Brewing wastewater is prepared the technique of water-coal-slurry | |
| CN103923715B (en) | With blue charcoal end for the method for water charcoal slurry prepared by raw material | |
| CN104293401A (en) | Coal-water slurry blended fuel and preparation method thereof | |
| CN104449775B (en) | Method for directly using red coke obtained by high-temperature pyrolysis of pulverized coal | |
| CN104232190B (en) | A kind of floating essence directly pulping process | |
| CN102977953B (en) | Anthracite coal water slurry for coal gasification and preparation method thereof | |
| CN102399606A (en) | Combustible slurry and preparation method thereof | |
| CN204550467U (en) | A kind of biomass charcoal heating manufacturing installation | |
| CN201165515Y (en) | Coke tar waste slag reclaiming apparatus | |
| CN105647602A (en) | Novel composite coal water slurry and a preparing method thereof | |
| CN208883516U (en) | A kind of boiler dusting water circulation use and sediment processing unit | |
| CN204325284U (en) | A kind of vapourizing furnace special alloy overflow type slag bath | |
| CN106479585B (en) | A kind of method that high concentration PVA waste water prepares water-coal-slurry | |
| Yongwei et al. | Analysis of the energy efficiency in the large enterprises from an industrial ecology perspective: Case study from BaoGang group | |
| CN203112135U (en) | Coal slime conveying pipeline | |
| CN202730071U (en) | Modified asphalt cosolvent melting tank | |
| CN202898050U (en) | System for producing liquid form high-modulus water glass by combination of dry and wet | |
| CN205137478U (en) | Special circulation bed of molasses alcohol waste liquid burns burning furnace | |
| CN115368943A (en) | Coal water slurry gasification coal blending method | |
| CN1986464A (en) | Glass smelting process | |
| CN115772432B (en) | Low-rank coal modification method, injection coal and coal blending system | |
| CN204369801U (en) | A kind of coke tar refuse system of processing | |
| CN214422582U (en) | Composite slurry fuel preparation system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160120 Termination date: 20170820 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |