WO2019056802A1 - Procédé d'accroissement de la densité énergétique d'un carburant liquide ou d'un carburant gazeux - Google Patents

Procédé d'accroissement de la densité énergétique d'un carburant liquide ou d'un carburant gazeux Download PDF

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WO2019056802A1
WO2019056802A1 PCT/CN2018/089956 CN2018089956W WO2019056802A1 WO 2019056802 A1 WO2019056802 A1 WO 2019056802A1 CN 2018089956 W CN2018089956 W CN 2018089956W WO 2019056802 A1 WO2019056802 A1 WO 2019056802A1
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Prior art keywords
particles
low
carbonaceous material
fuel
preferably less
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PCT/CN2018/089956
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English (en)
Chinese (zh)
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刘科
吴昌宁
翁力
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深圳瑞科天启科技有限公司
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Publication of WO2019056802A1 publication Critical patent/WO2019056802A1/fr

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    • 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
    • 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
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • 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
    • C10L10/00—Use of additives to fuels or fires for particular purposes
    • C10L10/18—Use of additives to fuels or fires for particular purposes use of detergents or dispersants for purposes not provided for in groups C10L10/02 - C10L10/16
    • 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
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/003—Additives for gaseous fuels
    • 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
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas

Definitions

  • the invention belongs to the field of fuel additives, and in particular relates to a method for increasing the energy density of a liquid fuel or a gas fuel.
  • Liquid fuels and gaseous fuels are the main fuel sources for various boilers (including various industrial boilers for thermal power plants, chemical plants, heating companies), internal combustion engines (including automotive internal combustion engines, marine internal combustion engines, and aerospace propulsion). It is desirable to increase the fuel density of these fuels in order to increase heat or work efficiency, increase the mileage of the unit fuel tank of the vehicle, and reduce fuel transportation costs per unit of heat.
  • a method for increasing the density of a liquid fuel or a gaseous fuel is to add a high-energy solid material such as ultrafine aluminum powder thereto, but the ultrafine aluminum powder is expensive and easily pyrophoric or explosive, and is not safe, so it is only suitable for cost. Insensitive military fields or aerospace fuels are not suitable for the wider civil industry.
  • the present invention is directed to solving the above problems.
  • the present invention provides a method for increasing the energy density of a liquid fuel or a gaseous fuel, the method comprising incorporating an ash content of ⁇ 3 wt% and a total sulfur content ⁇ 0.6 wt% and an average particle diameter ⁇ 500 micron low sulfur low ash ultrafine solid carbonaceous material particles.
  • the mass ratio of the low sulfur low ash ultrafine solid carbonaceous material particles to the liquid fuel is controlled to be 1:99 to 40:60, preferably 20:80 to 30:70, and the specific mass The ratio depends on the dispersion suspension performance of the former in the latter, the type and amount of dispersant used, and the required energy density target value, etc., so that the low sulfur low ash ultrafine solid carbonaceous material particles can be stably suspended in the liquid.
  • the fuel is correct.
  • the particle size of the low sulfur low ash ultrafine solid carbonaceous material particles is preferably less than 400 microns, more preferably less than 300 microns, still more preferably less than 200 microns, further preferably less than 100 microns, Still more preferably less than 50 microns, most preferably less than 5 microns.
  • the specific particle size will depend on the flow rate of the gaseous fuel in the delivery line. The larger the flow rate, the larger the particle size of the low-sulfur, low-ash, ultra-fine solid carbonaceous material particles that can be incorporated or the more the amount that can be incorporated.
  • the low sulfur low ash ultrafine solid carbonaceous material particles can be stably suspended in the gaseous fuel and are subject to the gaseous fuel delivery.
  • a dispersant is also added to the liquid fuel, the dispersant being a surface active molecule having a hydrophilic group and a hydrophobic group, preferably a pine oil, a camphor oil, a phenolic acid mixed fatty alcohol And an isomeric hexanol, octanol, ether alcohol or ester substance; the dispersant is added in an amount of 0.1 to 5% by weight of the low sulfur low ash ultrafine solid carbonaceous material particles.
  • the role of the dispersant is to improve the suspension stability of the former in the latter by improving the surface properties of the low sulfur low ash ultrafine solid carbonaceous material particles and the liquid fuel.
  • the liquid fuel is selected from the group consisting of a hydrocarbon fuel, an alcohol fuel, an ether fuel, a terpenoid fuel or a coal water slurry, and any other liquid fuel.
  • the hydrocarbon fuel includes conventional petroleum-based fuels such as gasoline, diesel oil, kerosene, heavy oil, and residual oil, and also includes high-density jet fuels such as various double-rings, spiral rings, and the like, and hydrocarbon fuels having intramolecular tension.
  • the alcohol fuel includes methanol, ethanol, and the like.
  • the ether fuel includes an ether fuel such as methyl ether, diethyl ether or ethylene glycol monomethyl ether.
  • the terpenoid fuel includes a fuel such as helium or dimethylhydrazine.
  • the diesel oil is preferably marine diesel oil, and the heavy oil and residual oil are low-end fuel oils produced in the petroleum refining industry, and are generally used as fuels in conventional boilers.
  • the gaseous fuel is selected from the group consisting of natural gas, coal-based gas, coalbed methane, biogas, oil field associated gas or oil gas.
  • the low sulfur low ash ultrafine solid carbonaceous material particles used in the present invention are obtained by a process comprising the following steps:
  • the carbonaceous material source comprising non-combustible minerals and carbon-hydrogen-containing combustible materials is wet-milled in water until the average particle size of the particulate matter is less than 500 micrometers, and additives are added in the coal water slurry during the continuous wet grinding process. It is thoroughly mixed and dispersed uniformly to obtain a micro-nano coal water slurry containing an additive;
  • the carbon-hydrogen-containing combustible particles obtained in step B are directly separated and used as the low-sulfur low-ash ultrafine solid carbonaceous material particles;
  • the floating stream containing the carbon-hydrogen-containing combustible particles is concentrated, followed by wet desulfurization, and then subjected to solid-liquid separation, and the carbon-hydrogen-containing combustible after desulfurization is performed.
  • the wet desulfurization comprises one of the following methods: A. adding a desulfurizing agent to desulfurize, adding a desulfurizing agent to the upward floating stream under the conditions of a temperature of 150-400 ° C and a pressure of 0.5-25 MPa, and the desulfurizing agent is selected. From hydrogen peroxide, sodium hypochlorite, oxygen, tetrachloroethylene, sodium carbonate or calcium oxide; B, high pressure boiled desulfurization; C, oxidative desulfurization; D, microbial desulfurization.
  • the carbonaceous material source is selected from the group consisting of coal gangue, lignite, sub-bituminous coal, bituminous coal, petroleum coke, oil shale or coal liquefaction residue.
  • the mixture of these carbonaceous materials in step A after grinding and water is collectively referred to as "coal slurry.”
  • the step A and the step are B is collectively referred to as "micro-mineral separation technology.”
  • the additive in step A is a hydrophilic nanoparticle, a collector or a surfactant, wherein the hydrophilic nanoparticle is an aluminosilicate nanoparticle, preferably separated by step B.
  • the mineral particles are further ground to a nanometer scale range; wherein the collector is an organic thio compound.
  • the surface active molecules of the group and the hydrophobic group are preferably pine oil, camphor oil, phenolic acid mixed fatty alcohol, isomeric hexanol, octanol, ether alcohol, esters. The action of these surfactants is to direct adsorption to the water-air interface, reduce the surface tension of the aqueous solution, and make the air filled in the water easily diffuse into bubbles and stabilize bubbles.
  • the additive in step A further comprises:
  • pH adjusting agents such as lime, sodium carbonate, sodium hydroxide and sulfuric acid
  • Flocculants such as polyacrylamide and starch.
  • the carbonaceous material source is comminuted in step A to an average particle size of less than 500 microns, preferably less than 400 microns, preferably less than 300 microns, preferably less than 200 microns, preferably less than 100 microns, preferably less than 50 microns, preferably less than Particles of 20 microns, preferably less than 10 microns, preferably less than 5 microns.
  • the diameter of the microbubbles in the step B is several micrometers to 200 micrometers, preferably several micrometers to several tens of micrometers, and more preferably the diameter of the microbubbles is in the range of 50% to 200% of the average particle diameter of the carbonaceous material source particles. .
  • the additive in the step A may further include: a pH adjuster and a flocculant.
  • the pH adjusting agent such as lime, sodium carbonate, sodium hydroxide and sulfuric acid serves to adjust the pH of the micro-nano coal slurry to control the surface characteristics of the mineral, the chemical composition of the slurry and the action conditions of various other agents, thereby Improving the flotation effect;
  • the flocculating agent such as polyacrylamide and starch acts to aggregate mineral fine particles into large particles to accelerate the sedimentation speed in water; flocculation-de-sludge and flocculation by selective flocculation Flotation.
  • the coal or coal gangue is comminuted in step A to an average particle size of less than 500 microns, preferably less than 400 microns, preferably less than 300 microns, preferably less than 200 microns, preferably less than 100 microns, preferably less than 50 microns, preferably less than Particles of 20 microns, preferably less than 10 microns, preferably less than 5 microns.
  • microbubbles are produced in step B by a microbubble generator having a diameter of from several micrometers to 200 micrometers, preferably from several micrometers to several tens of micrometers, more preferably the diameter of the microbubbles is average particles of coal or coal gangue particles. 50% to 200% of the diameter.
  • the present inventors have also found that using the above-mentioned micro-mineral separation technology, whether it is high-quality coal or inferior coal or coal gangue, usually the particle size of the crushed particles below 500 ⁇ m can make the carbon-hydrogen-containing combustible particles and The non-combustible mineral particles are significantly separated during the subsequent microbubble flotation process, the finer the particle size, and the smaller the diameter of the microbubbles and the diameter of the particles (for example, the diameter of the microbubbles is the average particle size of the coal or coal gangue particles) The range of 50% to 200%) is better in the subsequent microbubble flotation process.
  • inferior coal or coal gangue it is generally preferred to pulverize to below 500 microns, preferably below 400 microns, preferably below 300 microns, preferably below 200 microns, more preferably below 100 microns, such as around 80 microns, preferably around 30 microns. More preferably, it is about 10 micrometers, and most preferably 5 micrometers or less, so that the carbon-hydrogen-containing combustible particles and the incombustible mineral particles can be sufficiently separated in the subsequent bubble flotation process.
  • the above micro-mineral separation technology is particularly suitable for producing low-ash ultra-fine carbonaceous material particles by using inferior coal or coal gangue as raw materials.
  • the invention firstly adds low sulfur low ash ultrafine solid carbonaceous material particles to a liquid fuel or a gaseous fuel to increase energy density.
  • the total energy density of the blended fuel can be up to 1.4 times that of the individual liquid fuel or alone when the particles of low-sulfur, low-ash, ultra-fine solid carbonaceous material that are incorporated are stably suspended in the liquid fuel and gaseous fuel. 4 times the energy density of gaseous fuels.
  • the cost per unit volume or unit of calorific value liquid fuel is greatly reduced after blending.
  • the low-sulfur, low-ash, ultra-fine carbonaceous material particles in the present invention are stable in nature, do not spontaneously ignite or explode, and are very safe.
  • the low-sulfur, low-ash ultra-fine carbonaceous material particles in the invention can be industrially prepared at low cost by using energy-saving and environmentally-friendly micro-mineral separation technology and mature desulfurization technology, which makes the cost thereof greatly reduced, and is very suitable. It is used on a large scale in industry.
  • the raw materials may be low-grade raw materials such as coal gangue, inferior coal, petroleum coke, coal liquefaction residue or industrial waste, and also find good high-end industrial uses for these low-grade raw materials or industrial wastes, and maximize the resources of various raw materials. Utilization and recycling of waste.
  • the invention has wide application: for industrial boilers and marine internal combustion engines, due to the large volume of the internal combustion engine, it is found that when the particle size of the low-sulfur, low-ash, ultra-fine carbonaceous material particles is less than 200 ⁇ m, when it is added to the marine fuel, it is not It will affect its various flow properties and can be directly applied without any structural modification of existing marine engines.
  • the marine fuel allows a higher sulfur content, the upper limit of the sulfur content in the present invention can meet the requirements of marine fuel.
  • FIG. 1 is a schematic view showing the structure of a nano-micro separation apparatus used in the micro-mineral separation technique described in the present invention.
  • FIG. 2 is an exemplary process flow diagram for doping a liquid fuel with a low ash ultrafine carbonaceous material particle after desulfurization.
  • FIG. 3 is an exemplary process flow diagram for doping a gaseous fuel with a low ash ultrafine carbonaceous material particle after desulfurization.
  • This example illustrates the preparation of low sulfur low ash ultrafine carbonaceous material particles.
  • the carbonaceous material source used is peat with a mineral content of 30% by weight, which is transported to a crusher for preliminary crushing, and then introduced into a wet mill to be ground to a particle size of less than 50 ⁇ m, and water and additives are added for wet grinding. Mixing.
  • the prepared coal water slurry is stored in a coal water slurry storage tank, and the amount of the coal water slurry is controlled by a coal water slurry weighing instrument.
  • the coal water slurry is conveyed to the micro/nano separation device through a coal water slurry feed pump and a coal water slurry transfer line at a pumping pressure of 0.3 MPa.
  • the separation principle of micro-nano separation equipment is based on the difference of particle surface properties and the interference settlement principle of particles in fluidized fluid.
  • the composite force field is used to separate the separation of hydrocarbon combustible material particles and mineral impurity particles.
  • the structure is shown in Fig. 1.
  • the coal water slurry 1 after the addition of the micro-nano additive is fed from the upper part of the equipment to the ore distributor 2, and uniformly sent to the micro-nano separation column 3, according to the micro-nano separation column 3
  • the section moves slowly downwards.
  • the high-pressure gas 7 is pressed into the oil-containing bubble generator 5 by an air compressor; at the same time, the hydrophobic auxiliary agent 6 is injected into the oil-containing bubble generator 5, and micro-nano bubbles containing the hydrophobic auxiliary agent 6 are formed inside the oil-containing bubble generator 5.
  • the generated bubbles having a diameter of less than 100 ⁇ m are fed from the microbubble distributor 4 at the bottom of the micro-nano separation column 3, and the rising bubbles collide with the descending particles and uniformly spread over the surface of the hydrocarbon combustible material particles, thereby Make it a mineralized bubble.
  • a dynamic collision and separation environment of bubbles and particles is constructed inside the micro-nano separation column 3.
  • the hydrophobic ore particles are attached to the bubbles and rise to the foam layer along with the bubbles, and are discharged through the collecting device 8 to obtain clean micro-nano hydrocarbon solid fuel particles 9; and the mineral particles are hydrophilic ore particles under gravity
  • the bottom stream 10 is discharged as tailings to achieve effective separation.
  • the micro-nano separation column 3 is generally divided into two zones: a capture zone between the foam-slurry interface and the bubble generator, and a selection zone between the foam-slurry interface and the overflow. In the capture zone, mainly the bubble mineralization process, while the selection zone is the secondary enrichment of the mineralized foam, and the addition of the rinse water 11 further eliminates the mechanical impurities entrained in the foam.
  • the carbon-hydrogen-containing combustible particles obtained by the micro-mineral separation technique may already be referred to as low-ash ultrafine carbonaceous material particles, for example, the ash content thereof has been as low as ⁇ 3 wt%, preferably less than 2 wt%, more preferably ⁇ 1 wt.
  • the specific ash content and average particle size can be specifically adjusted according to the combination of various process parameters of the micro-mineral separation technique.
  • the floating stream containing the carbon-hydrogen-containing combustible particles is concentrated to a solid content of 40-60% by weight, and then subjected to wet desulfurization to sodium hypochlorite or hydrogen peroxide, and then subjected to solid-liquid separation, and after desulfurization
  • the carbon-hydrogen-containing combustible particles are separated to obtain the low-sulfur low-ash ultrafine solid carbonaceous material particles; or, the upper floating stream containing the carbon-hydrogen-containing combustible particles is concentrated at 300 Spray drying and inert desulfurization under inert gas or oxygen-poor gas at -700 ° C to obtain the low-sulfur low-ash ultrafine solid carbonaceous material particles; or, containing the carbon-hydrogen-containing combustible
  • the floating stream of the particles is dehydrated and then shaped and granulated, and then the shaped particles are subjected to pyrolysis desulfurization at 300-700 ° C and pulverized again to
  • the sulfur content of the low-ash ultrafine carbonaceous material particles is reduced by applying various existing desulfurization techniques to the above-mentioned low-ash ultrafine carbonaceous material particles to remove inorganic sulfur and/or organic sulfur.
  • the low sulfur low ash ultrafine solid carbonaceous material particles are obtained by 0.3 wt%, preferably ⁇ 0.2 wt%, further preferably ⁇ 0.1 wt%.
  • This embodiment exemplifies the mixing of the low-sulfur low-ash ultrafine solid carbonaceous material particles M obtained in Example 1 into various liquid fuels and gaseous fuels F (the blending ratio is calculated according to the M/F mass ratio).
  • the dispersant used is a terpineol oil in an amount of 2.5% by weight based on the weight of the low sulfur low ash ultrafine solid carbonaceous material particles.
  • the indicators before and after blending are determined. The specific data is shown in Table 1.
  • the M/F value of coal water slurry refers to the mass ratio of particle M to conventional coal powder for pulping.
  • the M/F value of coal water slurry refers to the mass ratio of particle M to conventional coal powder for pulping.
  • the advantage of coal water slurry after blending particles M is mainly reflected in the improvement of combustion efficiency by 5 to 8 percentage points and the ash content of single-ton coal water slurry by 2 to 3 percentage points.
  • This embodiment exemplifies the application effect of mixing the low-sulfur low-ash ultrafine solid carbonaceous material particles M obtained in Example 1 into liquid fuel F (a DMB marine fuel oil) (the blending ratio is 30%, according to M/F mass ratio calculation).
  • the pellet M was not subjected to wet or pyrolysis desulfurization, and the sulfur content was 0.2%.
  • the dispersant used was a terpineol oil in an amount of 3% by weight based on the weight of the low sulfur low ash ultrafine solid carbonaceous material particles.
  • the energy density changed from 33558 kJ/L before blending to 35417 kJ/L after blending; the viscosity of the liquid fuel increased slightly from 7.0 mm 2 /s before blending to 7.8 mm 2 /s after blending.
  • the unit calorific value liquid fuel cost is about 24% lower than that before blending.
  • the DME marine fuel oil has a sulfur content of 0.5%. After mixing the particles M, the liquid fuel sulfur content decreases by 0.41%, and the decrease rate is 18%, which can meet the requirements of the DMB marine fuel oil for the sulfur content of Grade I and II. Since the process of preparing the particle M does not require a desulfurization process, the cost advantage is more obvious.
  • Adding an exhaust gas caustic washing device to the ship for dust removal, desulfurization and denitrification can reduce the pollutant discharge of the marine fuel oil combustion process, so as to cope with the increasingly strict fuel oil discharge standards.
  • a coal water slurry or a coal coal slurry (such as methanol coal slurry) of pure particle M or partially mixed particles M can be prepared and used to replace the existing one. All kinds of marine diesel engines and their boiler fuel oil have the comprehensive advantages of cleanliness and supply cost.
  • This embodiment exemplifies the application effect of mixing the low-sulfur low-ash ultrafine solid carbonaceous material particles M obtained in Example 1 into liquid fuel F (a fuel oil of a F-D2 furnace) (the blending ratio is 30) %, calculated by M/F mass ratio).
  • the pellet M was not subjected to wet or pyrolysis desulfurization, and the sulfur content was 0.2%.
  • the dispersant used was a pine oil in an amount of 2.5 wt% based on the weight of the low sulfur low ash ultrafine solid carbonaceous material particles.
  • the fuel oil of the F-D2 furnace has a sulfur content of 0.4%, and the sulfur content of the liquid fuel decreases by 0.34% after mixing the particles M, and the decrease rate is 15%, which can meet the requirements of the sulfur content of the F-D2 furnace fuel oil. . Since the process of preparing the particle M does not require a desulfurization process, the cost advantage is more obvious.
  • Adding an exhaust gas caustic washing device to the boiler for dust removal, desulfurization and denitrification can reduce the pollutant discharge of the combustion process of the fuel oil for the furnace, so as to cope with the increasingly strict fuel oil discharge standard.
  • a coal water slurry or a coal coal slurry (such as methanol coal slurry) of pure particle M or partially mixed particles M can be prepared and used to replace the existing one.
  • Boiler fuel has the combined advantages of cleanliness and supply cost.

Abstract

La présente invention concerne un procédé d'accroissement de la densité énergétique d'un carburant liquide ou d'un carburant gazeux comprenant l'incorporation de particules de matériau carboné à faible teneur en soufre, à faible teneur en cendres, et solides ultrafines ayant une teneur en cendres < 3 % en pds, une teneur totale en soufre < 0,6 % en pds, et une taille moyenne de particule < 500 µm. Les particules de matériau carboné solides à faible teneur en soufre, à faible teneur en cendres, et ultrafines sont obtenues en séparant des particules de matériau carboné solides ultrafines à faible teneur en cendres d'une source de matériau carboné utilisant la technologie de séparation de minéraux sous forme de traces, et en utilisant la technologie de désulfurisation pour effectuer la désulfurisation ultérieure selon les besoins. Le procédé accroît la densité d'énergie par volume unitaire d'un carburant liquide de 1,4 fois, et accroît la valeur calorifique par volume unitaire des carburants gazeux de quatre fois.
PCT/CN2018/089956 2017-09-20 2018-06-05 Procédé d'accroissement de la densité énergétique d'un carburant liquide ou d'un carburant gazeux WO2019056802A1 (fr)

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CN107446632B (zh) * 2017-09-20 2019-05-17 深圳瑞科天启科技有限公司 一种提高液体燃料或气体燃料能量密度的方法
CN110437894A (zh) * 2019-07-30 2019-11-12 深圳瑞科天启科技有限公司 一种多元混合的类液体燃料及其制备方法
CN114456859B (zh) * 2022-01-17 2023-07-25 神华准格尔能源有限责任公司 富含高铝灰的原料水煤浆制备方法及高铝灰制取方法

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