WO2013005222A2 - A system and a process to produce low ash clean coal from high ash coal - Google Patents
A system and a process to produce low ash clean coal from high ash coal Download PDFInfo
- Publication number
- WO2013005222A2 WO2013005222A2 PCT/IN2011/000593 IN2011000593W WO2013005222A2 WO 2013005222 A2 WO2013005222 A2 WO 2013005222A2 IN 2011000593 W IN2011000593 W IN 2011000593W WO 2013005222 A2 WO2013005222 A2 WO 2013005222A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- coal
- ash content
- storage tank
- slurry
- thermic fluid
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
- C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/32—Liquid carbonaceous fuels consisting of coal-oil suspensions or aqueous emulsions or oil emulsions
- C10L1/326—Coal-water suspensions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/10—Treating solid fuels to improve their combustion by using additives
Definitions
- the present invention generally relates to cleaning of coal with mineral matter finely disseminated in the organic-mass. More particularly, the invention relates to a system and a process to produce low ash clean coal from high ash coal.
- Main advantages of this process are i) ease of recovery of solvent in the main process stream, ii) solvolytic efficiency of recovered solvents as that of fresh solvent, iii) 95-98% recovery of the solvent, iv) improved coking properties of clean coal, and v) availability of industrial organic solvents.
- the operating cost of this process is high because of high cost of solvents and energy requirement in the process.
- the inventors made an effort to make this process techno-economic initially through lab-scale process by improving the yield upto 50-60% with less than 8% ash content, including reduction in the cost of solvent recovery.
- coal, solvent N-Methyl-2- Pyrrolidone, NMP
- co-solvent Ethylenediamine, EDA
- the coal slurry is extracted in a known manner which includes coal-solvent mixture.
- the mixture is separated in a separation unit to produce a coarser fraction and a finer fraction.
- the finer fraction is fed to an evaporator unit to allow 70 to 80% off solvent recovery.
- coal-solvent mixture is then flushed in a precipitation tank to precipitate the coal.
- water as an anti-solvent is used.
- Water separates the solvent from coal and a water- solvent mixture is obtained, which is fed to a distillation unit to separate solvent and anti- solvent.
- the precipitated coal is separated in a filter.
- coal, solvent and co- solvent are taken in a pre defined ratio.
- Coal to solvent ratio is varied from 1:6 to 1:17 (wt/vol, g mL, coal to solvent ratios being wtvol, and solvent to co-solvent ratio are vol/vol).
- Coal to co-solvent as well as co-solvent ratio is maintained as 1 :1 (g/mL).
- Another object of this invention is to propose a single reactor-based system to produce low ash clean coal from high ash coal.
- a further object of this invention is to propose a validation process to establish the efficiency of the inventive system and process to produce low ash clean coal from high ash coal, as compared to the output from the laboratory scale unit.
- a process flow diagram for an industrial plant with a single reactor is proposed.
- the important equipments constituting the inventive system are a thermic fluid heater, a reactor, a heat exchanger, a thermic fluid pump, and an inert gas (N 2 ) cylinder.
- Some of the associated equipments or vessels comprise a water storage tank, a diesel storage tank, a thermic fluid storage tank, and an expansion tank.
- a reflux condenser (12) is used to maintain pressure at a specified condition.
- the system also consists of about eighteen gate and ball valves, two pressure gauges, at least one temperature gauge, and four temperature transmitters,
- Solvents and coal are loaded into the reactor (10) with the help of opening on the reactor top.
- Sampling system has been provided at the bottom of the reactor (10) to draw the sample as and when required.
- an industrial process for treating coal to lower ash content in a system comprising a first water storage tank, a second water storage tank, a diesel storage thank, a thermic fluid heater, a thermic fluid storage tank, a thermic fluid pump, a heat exchanger, a thermic fluid expansion tank, a N 2 gas cylinder, a reactor, a water pump, and a reflux condenser, the method comprising (i) forming a slurry of coal fines in a N-Methyl-2-pyrrolidone (NMP) with Ethylenediamine (EDA), the NMP and EDA ratio varying between 5:1 to 25:1 solution, said slurry containing about 6 to 18 ml of solution per g of coal, (ii) maintaining said slurry in the reactor at a temperature range of 150°C to 220°C and at a pressure range of 1 to 4 gauge (kg/cm 2 ) for a period of about
- NMP N-Methyl
- Figure 1 - shows a block diagram of a system to produce low-ash clean coal from high- ash coal.
- the inventive system comprises a first water storage tank (1), a second water storage tank (2), a diesel storage tank (3), a thermic fluid heater (4), a thermic fluid storage tank (5), a thermic fluid pump (6), a heat exchanger (7), a toxic fluid expansion tank (8)m a N 2 gas cylinder (9), a reactor (10), a water pump (11), and a reflux condenser (12).
- Coal and solvent in a predetermined ratio are loaded into the reactor (10).
- Nitrogen gas is supplied through the N 2 cylinder (9) for maintaining inert environment.
- Diesel is supplied to a burner from the diesel storage tank (3).
- Thermic fluid is supplied into the system from the thermic fluid storage tank (5).
- Thermic fluid is heated in the thermic fluid heater (4). On heating, the volume of the thermic fluid increases.
- the expansion tank (8) is used to store extra thermic fluid.
- the reactor (10) is heated by the hot thermic fluid, which is pumped by the thermic fluid pump (6).
- a sample is withdrawn through a sample port with the help of valves (V9, V10).
- the burner is switched off.
- thermic fluid is passed through the heat exchanger (7).
- Water is pumped in the heat exchanger (7) through the water pump (11) from one of the first and second water storage tank (1 or 2).
- the reflux condenser (12) maintains pressure and temperature at a desired level.
- the reactor (10) is configured with desired dimension and capacity for example, diameter-630mm, height-850mm, conical height-175, capacity about 425 lit.
- Coal and solvents are loaded into the reactor (10) through valve V7 in a predetermined ratio.
- Coal to total solvent ratio is varied from 1:6 to 1:18 (wt/vol, g/mL, coal to solvent ratios are wt/vol and solvent: co-solvent ratios are vol/vol wherever mentioned).
- Co-solvent to solvent ratio is varied from 1:25 to 1:5.
- Nitrogen gas is purged into the system for maintaining inert environment.
- Thermic fluid is pumped into the system from the thermic fluid storage tank (5).
- Thermic fluid is heated in the thermic fluid heater (4) by the diesel fired burner.
- the reactor (10) is heated by hot thermic fluid through limpet coils.
- Reactor pressure is being varied from 1 to 4 gauge (kg/cm 2 ).
- Reactor temperature is varied from 150°C to 220°C. Extraction is being done for 1 to 3 hr in the reactor.
- the sample is withdrawn from the reactor (10) through the sample port at predetermined time intervals. This sample is filtered through a mesh. Filtration step separates the refluxed mix in two parts (i) residue and (ii) filtrate (extracted
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Geochemistry & Mineralogy (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US14/130,818 US20140245659A1 (en) | 2011-07-05 | 2011-09-01 | System and a Process to Produce Low Ash Clean Coal from High Ash Coal |
CN201180072802.8A CN103797099B (en) | 2011-07-05 | 2011-09-01 | The system and method for low ash coal is produced by ash coal |
NZ620692A NZ620692A (en) | 2011-07-05 | 2011-09-01 | A system and a process to produce low ash clean coal from high ash coal |
AU2011372675A AU2011372675B2 (en) | 2011-07-05 | 2011-09-01 | A system and a process to produce low ash clean coal from high ash coal |
JP2014518068A JP5840292B2 (en) | 2011-07-05 | 2011-09-01 | System and method for producing low ash refined coal from high ash coal |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
IN901/KOL/2011 | 2011-07-05 | ||
IN901KO2011 | 2011-07-05 |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2013005222A2 true WO2013005222A2 (en) | 2013-01-10 |
WO2013005222A3 WO2013005222A3 (en) | 2013-02-28 |
Family
ID=54192851
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/IN2011/000593 WO2013005222A2 (en) | 2011-07-05 | 2011-09-01 | A system and a process to produce low ash clean coal from high ash coal |
Country Status (6)
Country | Link |
---|---|
US (1) | US20140245659A1 (en) |
JP (1) | JP5840292B2 (en) |
CN (1) | CN103797099B (en) |
AU (1) | AU2011372675B2 (en) |
NZ (1) | NZ620692A (en) |
WO (1) | WO2013005222A2 (en) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN111040819B (en) * | 2018-10-12 | 2021-08-20 | 国家能源投资集团有限责任公司 | Ash removal method for solid carbonaceous material |
CN111068899A (en) * | 2019-12-17 | 2020-04-28 | 兖矿水煤浆气化及煤化工国家工程研究中心有限公司 | System and method for chemically washing clean and wet pulverized coal |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4325707A (en) * | 1980-05-12 | 1982-04-20 | California Institute Of Technology | Coal desulfurization by aqueous chlorination |
US5380342A (en) * | 1990-11-01 | 1995-01-10 | Pennsylvania Electric Company | Method for continuously co-firing pulverized coal and a coal-water slurry |
CN101070495B (en) * | 2007-04-30 | 2011-03-30 | 中国矿业大学 | Mild coal-family component separation method based on extraction and back extraction |
CN101177640B (en) * | 2007-11-30 | 2010-05-19 | 华南理工大学 | Stable ash-free method for preparing nano coal slurry |
CN101235328B (en) * | 2008-01-01 | 2011-03-09 | 中国矿业大学 | Mild technique for separating coal whole components |
WO2010020994A1 (en) * | 2008-08-19 | 2010-02-25 | Tata Steel Limited | Blended frother for producing low ash content clean coal through flotation |
WO2010029563A1 (en) * | 2008-09-12 | 2010-03-18 | Tata Steel Limited | Development of a techno-economic process for organo refining of coal |
-
2011
- 2011-09-01 NZ NZ620692A patent/NZ620692A/en not_active IP Right Cessation
- 2011-09-01 CN CN201180072802.8A patent/CN103797099B/en not_active Expired - Fee Related
- 2011-09-01 JP JP2014518068A patent/JP5840292B2/en not_active Expired - Fee Related
- 2011-09-01 AU AU2011372675A patent/AU2011372675B2/en not_active Ceased
- 2011-09-01 US US14/130,818 patent/US20140245659A1/en not_active Abandoned
- 2011-09-01 WO PCT/IN2011/000593 patent/WO2013005222A2/en active Application Filing
Non-Patent Citations (1)
Title |
---|
TATA STEEL LIMITED. ORGANOREFINING PROCESS TO PRODUCE LOW ASH CLEAN COAL WITH MAXIMUM POSSIBLE YIELD INDIAN PATENT APPLICATION IN 2006KO01292 vol. 149, 03 July 2008, COLOMBUS OHIO USA, * |
Also Published As
Publication number | Publication date |
---|---|
NZ620692A (en) | 2015-09-25 |
US20140245659A1 (en) | 2014-09-04 |
AU2011372675B2 (en) | 2017-05-25 |
WO2013005222A3 (en) | 2013-02-28 |
CN103797099A (en) | 2014-05-14 |
JP5840292B2 (en) | 2016-01-06 |
JP2014522890A (en) | 2014-09-08 |
AU2011372675A1 (en) | 2014-02-27 |
CN103797099B (en) | 2016-01-13 |
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