WO1980000450A1 - Procede de preparation d'un combustible pulverulent carbone - Google Patents

Procede de preparation d'un combustible pulverulent carbone Download PDF

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Publication number
WO1980000450A1
WO1980000450A1 PCT/US1979/000623 US7900623W WO8000450A1 WO 1980000450 A1 WO1980000450 A1 WO 1980000450A1 US 7900623 W US7900623 W US 7900623W WO 8000450 A1 WO8000450 A1 WO 8000450A1
Authority
WO
WIPO (PCT)
Prior art keywords
alcohol
fluid material
flashing
coal
separator
Prior art date
Application number
PCT/US1979/000623
Other languages
English (en)
Inventor
L Keller
Original Assignee
Keller Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from US05/935,351 external-priority patent/US4192651A/en
Application filed by Keller Corp filed Critical Keller Corp
Publication of WO1980000450A1 publication Critical patent/WO1980000450A1/fr

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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
    • C10L9/00—Treating solid fuels to improve their combustion

Definitions

  • This invention relates to a process of separating coal particles from alcohol by single stage flashing.
  • the flashing process consist of dropping the pressure of a heated liquid to a sufficiently low pressure so that a portion of the liquid spontaneously vaporizes, therefore effecting a drop in temperature which stabilizes the remaining liquid at its saturation pressure condition imposed by the process. Only a relatively small percentage of the liquid phase material may be converted to vapor in conventional flashing. Therefore, in order to convert most, or perhaps all, of a mass of liquid to vapor, several sequential cycles of liquid pressurizing, heating, then pressure reduction, followed by removal of the vaporized portion must be performed.
  • the coal that is empolyed in this invention may be any of the commercially available coals, ranging from the relatively pure and high carbon content anthracite coal through the bituminous coals to and including the less desirable soft coals, lignite and the like.
  • the coal is crushed, pulverized, and worked in the presence of alcohol to form the suspensoid of coal in alcohol as described in U.S. Patent application Serial No. 615,697 mentioned above, and in the newsletter, Energy Studies, also mentioned above.
  • the suspensoid may be described as a mechanically stabilized pseudo-thixotropic suspensoid of particulate carbon-hydrocarbon particles derived from coal or other carbonaceous materials suspended in alcohol as a base fluid or carrier and suspended in a ratio of solids to liquids that essentially precludes the possibility of settling.
  • Pipeline transportation of coal-alcohol as a suspensoid is economical, since it takes less energy per unit of fuel to pump the suspensoid and in addition two-thirds of the material by weight is carbon.
  • the alcohol employed for forming the suspensoid preferrably is a methyl fuel which is a mixture of crude alcohols predominantly methanol and which may include smaller amounts of ethanol, n-propanol or iso-butanol. These alcohols all include one to four carbon atoms. If the coal is to be used for chemical processes, gassification, or as a dried combustion fuel which is either burned by itself or mixed with other hydro-carbon fuels, the coal particles in alcohol will be of a size range predominantly from 10 to 100 microns.
  • Reference numeral 21 depicts a pipeline, in which the suspensoid of coal particles in alcohol is transported from a distant location, or a storage facility where the fluid suspensoid is stored after being transported from the distant location through a pipeline. From the facility 21, the suspensoid is pumped continuously by pumping means 23 to a heating means 25.
  • the pumping means provides high pressures and high volume capacity flow rates for the fluid. The pressures employed are sufficient to prevent vaporization during heating and may be from a few hundred pounds per square inch, to over 1000 pounds per square inch, depending on the nature of the volatilizable materials in the fluids.
  • the heated fluid is flowed to a controllable pressure reduction device 27 to maintain back-pressure on the heating means and to instantaneous drop the pressure exiting the device 27 to near-atmospheric pressure to allow flashing to vapor.
  • the output of the pressure-reduction device 27 comprises a mixture of saturated dry vapor and dry solids. This output mixture is flowed to a gas/solids separator device 29, heated to prevent condensation of vapors, to remove the particulate solids from the gas stream either as a single product or divided by settling velocity separation into various particle-size fractions which may be defined for example, as fine, medium and coarse.
  • the solids are collected in hoppers intergral with the separator and purged of alcohol vapors by hot inert gas, then removed to storage means 31 for storage under inert gas i.e. CO 2 or N 2 .
  • the separated vapors are applied to sequential condensers 33, 35, and 37 as will be described subsequently.
  • the heating means 25 the fluid suspensoid is heated to a temperature sufficient to allow single stage flashing to take place in the pressure-reduction device 27. For this to occur, the fluid suspensoid must be heated to a temperature of at least about 200° F above the original fluid temperature and which is approximately the minimum for complete vaporization of the alcohols.
  • the enthalpy that has been put into the carbon material by heating is sufficient, in addition to the heat energy that is in the alcohol, to effect total flashing to complete dry vapor of substantially 100% of the alcohol in single stage flashing.
  • the fluid suspensoid may be heated to temperatures above the minimum required for single stage flashing to occur, for example up to 600° F to 800°F above ambient or higher for the purpose of vaporizing and recovering valuable by-products or for the purpose of recovering organic compounds from th ⁇ coal.
  • the heating preferably is done in a mono-tube or parallel-tube heat exchanger in which sufficient fluid velocity is maintained to insure good heating transfer rates, and turbulence is introduced, or effected, to provide uniform heating of the fluid, both the liquid materials and the solid materials. Sufficient retention time is provided to allow heating throughout the individual particles of solid material. This is desired for providing the energy required for vaporizing, pressuring, and removing the volitizable materials from within the particles and for effecting increased porosity and permeability and also for effecting further comminution by fragmentation during the next phase of processing which is the pressure reduction.
  • the pressure reduction device 27 may be either an adjustable venturi restriction, or an expansion motor, or some other flow-restricting device to drop the pressure and intiate flashing and evaporation.
  • the separator 29 is a gas-solids separator such as a bag house, cyclonic separator, multiclone cyclonic separator, etc.
  • the product resulting from flashing will be a mixture of saturated dry vapor and dry solid.
  • the solids resulting from the flashing and which are separated by the separator are of a different nature than the crushed and pulverized carbon worked with the alcohol to form suspensoid.
  • the flashing affects the surface texture, the internal pore space, the internal surface area, and the permeability of the particles and this results in the production of dry, pulverulent, low-density, high porosity, high permeability, high-reactivity particles.
  • the resulting separated solids can be used as fuels, as feed stock for gassification, for chemical processes or for mixture with other hydrocarbon fuels such as diesel fuel. From the separator, the solids may be separated into different grades of sizes depending upon the usage desired.
  • the vapors from the separator are applied to the sequential condensers 33, 35.and 37 which are commercially available condensers which gradually drop the temperature for sequential condensation.
  • the first stage condenser removes water or if any is present, hydrocarbons and by-products chemicals which condense at the 180° F to 220° F range and most of the particulate carbon which is not removed by the separator 29.
  • the second stage, or intermediate, condenser 35 removes the alcohols and lower boiling-temperature, hydrocarbons, and also some by-product chemical compounds, depending on the nature of the coal or lignite source.
  • the last stage condenser 37 may strip any low-boiling hydrocarbons and traces of alcohol and may be operated lower than ambient temperature or at elevated pressure (both) if found feasible for some materials. From the condenser 37 the non- condensible gas is pumped out and exhausted to the atmosphere. These gases may be treated to remove contaminants if required or necessary. They may also be burned as an additive fuel, if high enough in fuel value.
  • the preferred embodiment has been described as a process for single stage flashing of a stable suspensoid of coal particles and alcohol, it is to be understood that the process could be employed for single stage flashing of a slurry comprising a mixture of coal particles and alcohol of the same type as mentiond above.
  • the temperature at which the slurry of coal and alcohol would be heated for single stage flashing may be slightly higher than that of the stable suspensoid of coal and alcohol because of the difference of specific heat in the carbon and alcohol.
  • the carbon has a specific heat of approximately .2 while that of alcohol is about .6.
  • the specific heat of the stable suspensoid of carbon and alcohol is about .33 since it is about two-thirds of carbon in weight.
  • a slurry cannot be effectively handled at a ratio of more than about 50% solids to liquid.
  • the specific heat for the coal-alcohol slurry would be slightly higher than that of the stable suspensoid of coal and alcohol and would require a somewhat higher temperature for flashing.
  • the slurry may be formed specifically for flashing in order to remove the undesirable by-products from the coal in order to produce a clear burning high quality fuel.
  • the stable suspensoid of coal and alcohol may be also formed specifically for flashing purposes in order to remove the undesirable by-products for the purpose of producing a clean burning high quality fuel.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

Production d'un combustible carbone sec, pulverulent, de basse densite a haute porosite, de haute permeabilite et hautement reactif a partir de coulis de charbon et d'alcool ou de suspensoides stabilises de charbon et d'alcool par distillation eclair en une etape. Les coulis ou suspensoides sont chauffes sous pression a une temperature suffisante pour effectuer la distillation eclair en une etape de sensiblement tout l'alcool. Le produit resultant de la distillation eclair est alors separe en vapeurs et materiaux carbones solides particulaires. Les vapeurs sont condensees en alcool et le materiau carbone particulaire est soumis a une operation supplementaire ou utilise selon demande.
PCT/US1979/000623 1978-08-01 1979-08-20 Procede de preparation d'un combustible pulverulent carbone WO1980000450A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US05/935,351 US4192651A (en) 1977-11-21 1978-08-21 Method of producing pulverulent carbonaceous fuel
US935351 1986-11-26

Publications (1)

Publication Number Publication Date
WO1980000450A1 true WO1980000450A1 (fr) 1980-03-20

Family

ID=25466959

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1979/000623 WO1980000450A1 (fr) 1978-08-01 1979-08-20 Procede de preparation d'un combustible pulverulent carbone

Country Status (2)

Country Link
EP (1) EP0019623A4 (fr)
WO (1) WO1980000450A1 (fr)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9937577B2 (en) 2006-12-20 2018-04-10 Lincoln Global, Inc. System for a welding sequencer
CN101936641A (zh) * 2010-09-21 2011-01-05 宋显华 一种用闪蒸法去除煤炭中水分的方法和装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2049013A (en) * 1931-08-07 1936-07-28 Universal Oil Prod Co Treatment of hydrocarbon oils
US3607667A (en) * 1966-12-30 1971-09-21 Edward M Knapp Desalination of water by heat exchange,microwave heating and flash distillation
US3729042A (en) * 1971-02-22 1973-04-24 Pollutant Separation Inc Apparatus for separating pollutants and obtaining separate liquids & solids
US4030893A (en) * 1976-05-20 1977-06-21 The Keller Corporation Method of preparing low-sulfur, low-ash fuel
US4070268A (en) * 1976-06-01 1978-01-24 Kerr-Mcgee Corporation Solvent recovery in a coal deashing process

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3867109A (en) * 1972-04-27 1975-02-18 Bechtel Int Corp Process for improving the bunkerability of coal
US4045092A (en) * 1975-09-22 1977-08-30 The Keller Corporation Fuel composition and method of manufacture
ZA774576B (en) * 1976-09-08 1978-06-28 Phillips Petroleum Co Processing of coal for fuel

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2049013A (en) * 1931-08-07 1936-07-28 Universal Oil Prod Co Treatment of hydrocarbon oils
US3607667A (en) * 1966-12-30 1971-09-21 Edward M Knapp Desalination of water by heat exchange,microwave heating and flash distillation
US3729042A (en) * 1971-02-22 1973-04-24 Pollutant Separation Inc Apparatus for separating pollutants and obtaining separate liquids & solids
US4030893A (en) * 1976-05-20 1977-06-21 The Keller Corporation Method of preparing low-sulfur, low-ash fuel
US4070268A (en) * 1976-06-01 1978-01-24 Kerr-Mcgee Corporation Solvent recovery in a coal deashing process

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP0019623A4 *

Also Published As

Publication number Publication date
EP0019623A1 (fr) 1980-12-10
EP0019623A4 (fr) 1980-12-12

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