Patent Grant
11254886
The invention is in the field of combination products derived from solid hydrocarbonaceous and/or solid carbonaceous material with liquid hydrocarbons, particularly the combination of coal with fuel oil, in order to create a combined product that may be used as a fuel. In particular, the invention is in the field of introduction of solid hydrocarbonaceous material, such as coal, into fuel oil in order to upgrade the solid hydrocarbonaceous material and replace a proportion of the fuel oil.
Coal fines and ultrafines, including microfines are small particles of coal generated from larger lumps of coal during the mining and preparation process. While coal fines retain the same energy potential of coal they are generally considered a waste product as the particulate nature of the product renders it difficult to market and transport. Coal fines are therefore generally discarded as spoil close to the colliery forming large waste heaps that require careful future management in order to avoid environmental contamination or even the threat to human life as demonstrated in the 1966 Aberfan disaster in South Wales, UK.
Nevertheless, coal fines do offer a cheap and plentiful supply of hydrocarbons particularly rich in carbon. It is known to add slurries of coal fines in water to fuel oils in order to upgrade the coal fine product and reduce the cost per unit volume of the blended fuel oil (see for example U.S. Pat. Nos. 5,096,461, 5,902,359 and 4,239,426). However, in its natural state, coal fines typically contain significant levels of ash-forming components that would render it unsuitable for blending directly with fuel oil. Furthermore, the amount of water present in coal fines (ca. 35% by mass or % m) is also undesirable for use in fuel oil. Selecting coal fines with low mineral matter content is one possibility for ameliorating these problems. Suitable coal fines can be manufactured by crushing and grinding seam coal with inherently low mineral matter content (e.g. <5% m), however, this limits quite substantially the types of coal that can be utilised. This approach can be expensive, and fails to address the issue of water content in the fines produced.
Water is present within seam coal in situ, held within an internal pore structure that ranges in diameter from less than two nanometres to tens of microns. The total porosity of coals varies considerably, based on the type of coal and the quantity of pore-held water. For example, water content increases from approximately 1-2% m for low-volatile and medium-volatile bituminous coals, to 3-10% m in high volatile bituminous coals, and 10-20% m in sub-bituminous coals; on to 20-50% m for brown coals (lignites). Although thermal drying can remove pore-held water, this is a temporary solution, as water is readily re-adsorbed to it natural level from the atmosphere.
Once the coal has been mined, it can be separated from extraneous mineral matter by various coal density and froth flotation techniques, which typically depend on excess water being added to the mined coal to produce a coal slurry. Furthermore, modern methods that grind minerals economically to microfine particle sizes<20 microns (20 μm), also require water to be added, resulting in a slurry. Such coal slurries typically contain 40-80% m of water, most of which is surface water attached to the outer surfaces of particles and water held loosely in the interstices between particles. The interstitial water can be removed by mechanical filter presses, or reduced by drainage during transportation or storage, prior to utilisation.
However, surface water continues to be attached to particles. As coal particles are reduced in size the area of external surfaces increases markedly, and the quantity of surface water increases similarly. After mechanical dewatering a microfine coal sample can look and feel dry to the touch, but still contain 25% m to 50% m water. Most of this water is surface water, the remainder being pore-held.
Thus, reducing water content in coals economically to levels of the order of 2% m is a significant and challenging target for microfine coal, especially from coals with high pore-held moistures.
There has been previous research into methods of converting coal into liquid hydrocarbon products: these mainly involve solvent extraction of coal at temperatures above 400° C. under pressure in the presence of hydrogen or a hydrogen donor solvent, e.g. tetralin (1,2,3,4-tetrahydronaphthalene). This has led to several pilot scale developments and at least one full-scale operating plant using the Shenhua process at Ejin Horo Banner, Ordos, Inner Mongolia, China. Exploitation of this process involves, however, a very large capital investment and high associated running costs.
Fuel oil is a higher distillate product derived from crude oil. The term “fuel oil” covers a range of petroleum grades having a boiling point higher than that of gasoline products. Typical fuel oils are residual fuel oils (RFOs) and marine fuel oils (MFOs).
Fuel oil is classed as a fossil fuel and is a non-renewable energy source. Furthermore, while crude oil prices are quite volatile the refined products that are obtained therefrom are always relatively expensive. A way in which fuel oil could be blended with a lower cost hydrocarbon source such as coal, to extend the finite reserves of crude oil, and the resultant refined distillate products, would be highly desirable.
These and other uses, features and advantages of the invention should be apparent to those skilled in the art from the teachings provided herein.
U.S. Pat. No. 2,590,733 and DE3130662 refer to use of RFO-coal dispersions for burners/boilers designed for the use of RFO. U.S. Pat. Nos. 4,265,637, 4,251,229, 4,511,364, JPS5636589, JPS6348396, DE3130662, U.S. Pat. Nos. 5,503,646, 4,900,429 and JPS2000290673, U.S. Pat. No. 2,590,733 and DE3130662 utilise coarse particle sizes in the pulverised coal range (<200 μm) or even larger which would not be suitable for passing through fuel filters.
U.S. Pat. Nos. 4,417,901 and 4,239,426 focus on high coal loadings: 30-70% m.
U.S. Pat. Nos. 5,096,461, 5,902,359, 4,511,364 and JPS2000290673 relate specifically to coal-oil-water dispersions.
U.S. Pat. Nos. 4,389,219, 4,396,397, 4,251,229, JPS54129008 and JPS5636589 include or specify stabilising additives which may move the properties of the resultant fuel oil-coal blend out of specification.
U.S. Pat. No. 4,090,853A and CA 1096620 A1, plus Clayfield, E. et al., Colloil manufacture and application (Fuel, 1981, 60, 865) relate specifically to coarser particles (<500 μm) suspended in fuel oil and water.
U.S. Pat. No. 8,177,867 B2 and Nunez, G. A. et al., Colloidal coal in water suspensions (Energy and Environmental Science, 2010 3(5), 629) relate specifically to colloidal coal-in-water slurries with 20-80% particles<1 μm size.
U.S. Pat. Nos. 4,319,980 and 4,425,135 describe respectively the manufacture and use in automotive fuels of a material prepared by amine extraction at elevated temperatures of an undefined coal. This amine extraction process splits coal into two materials with different molecular structure, i.e. coal extract chemically different from seam coal and undissolved organic material derived from coal.
U.S. Pat. No. 1,329,423 refers to the use of froth flotation to separate coal from mineral matter for particles ground to below 300 μm size. This patent does not extend the technique to particles below 20 μm in diameter.
US 2011/0239973 A1 refers to a fuel mixture comprising a suspension of a combustible solid powder in a liquid fuel, where the combustible solid is restricted to lignin or biomass nitrification products, which are not chemically quite different to coal and do not require similar preparation techniques.
The present invention addresses the problems that exist in the prior art, not least reducing reliance on fuel oil and upgrading coal fines that would otherwise be treated as a waste product, and provides environmental benefits accordingly.
Accordingly, in a first aspect the invention provides a fuel oil composition comprising:
(i) a particulate material, wherein at least about 90% by volume (% v) of the particles are no greater than about 20 μm (microns) in diameter; and
(ii) a liquid fuel oil,
wherein the particulate material is present in an amount of at most about 30% m (thirty percent by mass) of the total mass of the fuel oil composition; and
wherein the particulate material is selected from the group consisting of: hydrocarbonaceous material and carbonaceous material.
Typically the solid hydrocarbonaceous and/or solid carbonaceous material comprises coal the coal comprises sedimentary mineral-derived solid carbonaceous material selected from hard coal, anthracite, bituminous coal, sub-bituminous coal, brown coal, lignite, or combinations thereof. Optionally the coal is microfine coal.
In an embodiment of the first aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 20 μm in diameter.
In an further embodiment of the first aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 10 μm in diameter.
According to a specific embodiment of the invention the solid hydrocarbonaceous and/or solid carbonaceous material is dewatered prior to combination with the liquid fuel oil. Typically, the particulate material has a water content of less than about 15% m, 5% m or 2% m. The total water content of the fuel composition is typically less than 5% m, or 2% m.
In another embodiment of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material is subjected to at least one de-ashing step or de-mineralising step prior to combination with the liquid fuel oil.
In an alternative embodiment of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material comprises a dewatered ultrafine coal preparation that comprises a low inherent ash content.
Suitably the ash content of the particulate material is less than about 20% m of the coal preparation; optionally less than about 15% m, suitably less than about 10% m, or less than about 5% m, or less than about 2% m, or less than 1% m.
According to a specific embodiment of the invention, the liquid fuel oil is selected from one of the group consisting of: marine diesel, diesel and kerosene for stationary applications, marine bunker oil; residual fuel oil; and heavy fuel oil. Suitably the liquid fuel oil conforms to, or is defined by, the main specification parameter included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards. Alternatively, the liquid fuel oil conforms to the main specification parameters included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards. Suitably the liquid fuel oil conforms to the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards.
In embodiments of the invention, the term “main specification parameter” refers to a parameter selected from the group consisting of: viscosity at 100° C.; viscosity at 50° C.; viscosity at 40° C.; density at 15° C.; ash content; sulphur content; water content; flash point; and pour point.
In embodiments of the invention, the term “main specification parameters” refers to two or more parameters, suitably, 2, 3, 4, 5, 6, 7, 8, 9 or 10 parameters, selected from the group consisting of: viscosity at 100° C.; viscosity at 80° C.; viscosity at 50° C.; viscosity at 40° C.; density at 15° C.; ash content; sulphur content; water content; flash point; and pour point.
In an embodiment of the invention the fuel oil composition comprising both solid hydrocarbonaceous and/or solid carbonaceous material and liquid fuel oil conforms to the main specification parameter included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards. Alternatively, the fuel oil composition comprising both solid hydrocarbonaceous and/or solid carbonaceous material and liquid fuel oil conforms to the main specification parameters included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards. Suitably, the fuel oil composition comprising both solid hydrocarbonaceous and/or solid carbonaceous material and liquid fuel oil conforms the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards.
According to a specific embodiment of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material is present in an amount of at most about 20% m, suitably about 15% m, optionally about 10% m of the total mass of the fuel oil composition.
In one embodiment of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material is present in an amount of at least about 0.01% m, suitably at least about 0.10% m, optionally about 1% m of the total mass of the fuel oil composition.
In a particular embodiment of the invention, the fuel oil composition comprises the solid hydrocarbonaceous and/or solid carbonaceous material in the form of a suspension. Typically the suspension is stable for at least 1 hour, optionally at least 24 hours, suitably at least 72 hours. In one embodiment of the invention the suspension is stable for more than 72 hours. In an embodiment of the invention, the fuel composition comprises a dispersant additive.
A second aspect of the invention provides a process for the preparation of a fuel oil composition comprising combining a solid hydrocarbonaceous and/or solid carbonaceous material, wherein the material is in particulate form, and wherein at least about 90% v of the particles are no greater than about 20 μm in diameter; and a liquid fuel oil, wherein the solid hydrocarbonaceous and/or solid carbonaceous material is present in an amount of at most about 30% m (30% by mass) of the total mass of the fuel oil composition.
In an embodiment of the second aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 20 μm in diameter.
In an further embodiment of the second aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 10 μm in diameter.
In an embodiment of the second aspect of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material is dispersed in the liquid fuel oil. Suitably, the dispersion is achieved by a method selected from the group consisting of: high shear mixing; ultrasonic mixing, or a combination thereof.
In an embodiment of the second aspect of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material comprises coal.
In some embodiments of the second aspect of the invention, the solid hydrocarbonaceous and/or solid carbonaceous material is de-watered prior to combination with the liquid fuel oil. Optionally, the solid hydrocarbonaceous and/or solid carbonaceous material is subject to a de-mineralising/de-ashing step prior to combination with the liquid fuel oil. Suitably, the de-ashing or de-mineralisation is via froth flotation techniques.
In some embodiments of the process of the present invention, the solid hydrocarbonaceous and/or solid carbonaceous material is subjected to a particle size reduction step prior to combination with the liquid fuel oil. Particle size reduction may be achieved by any appropriate method. Suitably, the particle size reduction is achieved by a method selected from the group consisting of: milling, grinding, crushing, high shear grinding or a combination thereof.
In an embodiment of the invention, the liquid fuel oil is selected from one of the group consisting of: marine diesel, diesel and kerosene for stationary applications, marine bunker oil; residual fuel oil; and heavy fuel oil. Alternatively, or in addition, the liquid fuel oil conforms to, or is defined by, the main specification parameter included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards. Alternatively, the liquid fuel oil conforms to the main specification parameters included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards. Suitably, the liquid fuel oil conforms to the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards
A third aspect of the invention comprises a method for changing the grade of a liquid fuel oil comprising adding to the fuel oil a solid hydrocarbonaceous and/or solid carbonaceous material, wherein the material is in particulate form, and wherein at least about 90% v of the particles are no greater than about 20 μm in diameter.
In an embodiment of the third aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 20 μm in diameter.
In an further embodiment of the third aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 10 μm in diameter.
Suitably the grade of the liquid fuel oil is defined by the main specification parameter included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D975-14; ASTM D396; BS 2869:2010; GOST10585-99, GOST10585-75 and equivalent Chinese standards. Alternatively, the liquid fuel oil is defined by the main specification parameters included in one or more of the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D975-14; ASTM D396; BS 2869:2010; GOST10585-99, GOST10585-75 and equivalent Chinese standards. Suitably, the liquid fuel oil is defined by the fuel oil standards selected from the group consisting of: ISO 8217:2010; ISO 8217:2012; ASTM D396; ASTM D975-14, BS 2869:2010, GOST10585-99, GOST10585-75 and equivalent Chinese standards.
A fourth aspect of the invention comprises a method of adjusting the flash point of a liquid fuel oil, wherein the method comprises combining a liquid fuel oil with particulate material, wherein the fuel oil is selected from the group consisting of: marine diesel; diesel for stationary applications, kerosene for stationary applications, marine bunker oil; residual fuel oil; and heavy fuel oil. Suitably, the particulate material comprises coal.
In an embodiment of the fourth aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 20 μm in diameter.
In an further embodiment of the fourth aspect, at least 95% v of the particles forming the particulate material, optionally 98% v, suitably 99% v are no greater than about 10 μm in diameter.
It will be appreciated that the features of the invention may be subjected to further combinations not explicitly recited above.
The invention is further illustrated by reference to the accompanying drawings in which:
All references cited herein are incorporated by reference in their entirety. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
The invention relates, in a specific embodiment, to preparing and blending de-ashed or de-mineralised, de-watered/dehydrated coal powder, commonly termed in the industry “fines”, suitably selected from “microfines” (typical particle size<20 μm), with fuel oil to produce a combined blended product. The inventive concept further extends to the uses of the blended fuel oil product, including preparing fuels based on blended fuel oil products.
Prior to further setting forth the invention, a number of definitions are provided that will assist in the understanding of the invention.
As used herein, the term “comprising” means any of the recited elements are necessarily included and other elements may optionally be included as well. “Consisting essentially of” means any recited elements are necessarily included, elements that would materially affect the basic and novel characteristics of the listed elements are excluded, and other elements may optionally be included. “Consisting of” means that all elements other than those listed are excluded. Embodiments defined by each of these terms are within the scope of this invention.
The term “coal” is used herein to denote readily combustible sedimentary mineral-derived solid carbonaceous material including, but not limited to, hard coal, such as anthracite; bituminous coal; sub-bituminous coal; and brown coal including lignite (as defined in ISO 11760:2005 and in equivalent Chinese standards). The term “coal” does not extend to extracts, or products derived from coal, where the chemical composition of the hydrocarbonaceous content of the material has been altered.
The definition of a fuel oil varies geographically. As used herein, fuel oils may relate to:
As used herein, the term “ash” refers to the inorganic—e.g. non-hydrocarbon—component found within most types of fossil fuel, especially that found in coal. Ash is comprised within the solid residue that remains following combustion of coal, sometimes referred to as fly ash. As the source and type of coal is highly variable, so is the composition and chemistry of the ash. However, typical ash content includes several oxides, such as silicon dioxide, calcium oxide, iron (III) oxide and aluminium oxide. Depending on its source, coal may further include in trace amounts one or more substances that may be comprised within the subsequent ash, such as arsenic, beryllium, boron, cadmium, chromium, cobalt, lead, manganese, mercury, molybdenum, selenium, strontium, thallium, and vanadium.
As used herein the term “de-ashed coal” refers to coal that has a proportion of ash-forming components that is lower than that of its natural state. The related term “demineralised coal” is used herein to refer to coal that has a reduced proportion of inorganic minerals compared to its natural state. The terms “de-ashed coal” and “demineralised coal” may also be used to refer to coal that has a low naturally-occurring proportion of ash-forming components, or minerals respectively, as may the terms “low ash coal” or “low mineral content coal”.
As used herein, the term “coal fines” refers to coal in particulate form with a maximum particle size typically less than 1.0 mm. The term “coal ultrafines” or “ultrafine coal” or “ultrafines” refers to coal with a maximum particle size typically less than 0.5 mm. The term “coal microfines” or “microfine coal” or “microfines” refers to coal with a maximum particle size typically less than 20 μm.
The term “pulverised coal” as used herein refers to a coal that has been crushed to a fine dust. The particle size is generally large in the order of 200 μm with wide distribution that lacks uniformity.
The term “hydrocarbonaceous material” as used herein refers to fossilised organic matter containing hydrocarbons; hydrocarbons being an organic compound consisting substantially of the elements hydrogen and carbon.
The term “carbonaceous material” as used herein refers to materials containing predominantly carbon including coke, activated carbon and carbon black. Carbonaceous material may be derived by pyrolysis of organic matter.
The term “carbon black” as used herein refers to finely divided forms of substantially pure elemental carbon prepared by the incomplete combustion or thermal decomposition of gaseous or liquid hydrocarbons, especially petroleum products.
The term “activated carbon” as used herein refers to very porous carbon processed from materials like nutshells, wood, and coal by various combinations of pyrolysis and activation steps. Activation involves high temperature treatment of pyrolysed materials in the absence of air, either with steam, carbon dioxide, or oxygen, or following impregnation by certain specific acids, bases or salts.
The term “dispersant additive” as used herein refers to a substance added to a mixture to promote dispersion or to maintain dispersed particles in suspension.
As used herein, the term “water content” refers to the total amount of water within a sample, and is expressed as a concentration or as a mass percentage. When the term refers to the water content in a coal sample, it includes the inherent or residual water content of the coal, and any water or moisture that has been absorbed from the environment. When the term refers to the water content in the fuel composition, it includes the total water content of the composition introduced from all components, including the liquid fuel oil, the particulate material and any additives or other components.
As used herein the term “dewatered particulate material” refers to particulate material that has a proportion of water that is lower than that of its natural state. The term “dewatered particulate material” may also be used to refer to particulate material that has a low naturally-occurring proportion of water. The term “dewatered coal” has a corresponding meaning for when the particulate material is coal. In embodiments of the present invention the amount of water as a proportion of the total mass of the particulate material is substantially low enough that the material, when combined with a liquid fuel oil, remains capable of falling within the main specification parameters of that fuel oil.
Fuel oil is expensive and is a non-renewable source of energy. Coal-fines are generally regarded as a waste product and are available cheaply in plentiful supply. The problem addressed by the present invention is to provide a blended fuel oil that is cheaper than current alternatives, yet still meet required product and emission criteria to enable its use as a direct replacement in burners and boilers designed for fuel oil with minimal or no adaptation. Non-automotive use of fuel oil includes boilers and engines both for marine use and stationary applications, such as power stations and industrial, commercial and residential use. These fuels are now tightly specified to protect more sophisticated burner and boiler equipment controls are also needed to limit boiler emissions. Different specifications apply for the range of technologies and these may vary according to the region or country of use. The main parameters from some of some widely used specifications are shown below in Tables 1a, 1b and 1c. This includes details for international trading specifications for Heavy Fuel Oil used in China (S&P Global Platts Methodology and Specifications Guide: China Fuel Oil).
Mineral matter content is controlled in most fuel oil grades by specifying the ash content. The limits for ash content for these fuel oil grades vary from 0.01% m (marine distillate fuel oil) to 0.15% m (Marine RFO grade RMK and ASTM D396 Heavy fuel oil No. 5). The proportion of a microfine coal (e.g. one with 1% m ash content) that can be added to fuel oil and remain within specifications can vary considerably therefore from <1% m in marine distillate fuel oil (also known as marine diesel) to <15% m in ASTM D396 HFO No. 5, and is unconstrained in ASTM D396 HFO No. 6. For the purposes of these calculations, the ash content of the fuel oil is assumed to be close to zero. It is therefore important to demineralise (or de-ash) the microfine coal as effectively as possible.
In view of the above, there exists a technical prejudice in the mind of the skilled person against using coal in fuel oils due to the perceived abundance of mineral matter (or ash-forming components) in most coals.
2
890-920
3
254
65
1GOST standard 10585-75 is also still used in trading. This contains some added specification parameters shown in italics.
2 7 grades are specified based on sulphur content: I: <0.5% m, II: <1.0% m, III: <1.5% m, IV: <2.0% m, V: <2.5% m, VI: <3.0% m, VII: <3.5% m.
3 2 grades: low-ash: <0.05% m, more ash: <0.14% m
4Referred to as temperature of solidification
The limits for water content vary from 0.3% m (e.g. Marine RFO grade RMA) to 1% m (UK BS 2869 RFO burner fuel grades G and H). ASTM D396 specifies water plus sediment and the most viscous HFO grade No. 6 has a limit of 2% m for water plus sediment. The proportion of a microfine coal (e.g. one with 2% m water content) that can be added to fuel oil and remain within specifications can vary considerably therefore from <15% m in Marine RFO grade RMA to <50% m in UK BS 2869 RFO burner fuel grades G and H. It is therefore important to dewater the coal as effectively as possible. Table 2 illustrates the range of maximum limits allowable in various non-automotive fuels by ASTM specifications, and how low they must be. These are long-standing limits which have been required since the 1980s or earlier.
In view of the above, the skilled person would be dissuaded from considering inclusion of particulate material, in particular coal, in fuel oils due to the need to keep water content low (for example, <2% m), amongst other considerations.
The proportion of a microfine coal (e.g. one with 0.5% m sulphur content) that can be added to fuel oil is only constrained by those fuel oil specifications with sulphur content limits of below 0.5% m.
Most fuel oil specifications allow sulphur content at 1% m or higher; in these cases microfine coal addition is a benefit and will reduce fuel sulphur content and the associated sulphur oxides emitted from combustion devices using fuel oil containing microfine coal. Until recently, for the fuel oil specifications shown below, the level of microfine coal addition was only limited by sulphur content in Marine RFO supplied in Emission Control Areas, and in this case to <20% m.
However, on 27 Oct. 2016, the International Maritime Organisation voted to adopt a 0.50% m maximum sulphur global limit for ship bunker fuels from 2020. As such, the sulphur level in the global market for marine fuel will reduce from 3.50% m to 0.50% m. Meeting these new requirements will have a massive impact on refinery configuration and operations, and hence cost. There is also an alternative which permits the use of abatement measures on ships (e.g. exhaust flue gas scrubbing), or sulphur trading schemes, to give an equivalent environmental performance to burning lower sulphur fuels.
Upgrading coal fines by blending with fuel oil is known when the coal fines are in their natural state. However, in their natural state, coal fines typically contain levels of ash-forming components and sulphur that would render them unsuitable for blending with fuel oils which must meet set current fuel oil specifications and emissions limits to operate efficiently in burners and boilers designed for fuel oil. Furthermore, the amount of water present in coal fines (ca. 35% m) is also undesirable for use in fuel oils.
To date, it has not been possible to produce economically a coal-fuel oil blend which can meet fuel oil specifications requiring very low mineral matter content and particle sizes predominantly <10 μm (preferably mainly <2 μm) i.e. much smaller than the 500 micron upper limit associated with “ultrafine” coal.
Hitherto published information regarding dispersion of coal fines in fuel oil has not addressed fitness for use in fuel oil boilers, but has been concerned with reducing spontaneous combustion risks, especially for lignite, simplifying transportation via improved pumpability, and improving combustion in coal-fired boilers, often via the use of fuel-water emulsions containing coal and fuel oil.
Particulate material, in particular, coal fines or microfine coal fines for use in the present invention typically have a low water content (suitably <15% m, <10% m, <5% m, <3% m, <2% m, <1% m, <0.5% m, of the total mass of the fuel composition) and a low ash content (suitably <10% m, <5% m, <2% m, <1% m, <0.5% m, of the total mass of the fuel composition).
Demineralising (or de-ashing) and dewatering of particulate material, in particular coal fines, is typically achieved via a combination of froth flotation separation, specifically designed for ultrafines and microfine particles, plus mechanical and thermal dewatering techniques known in the art. De-watered particulate material or coal fines may also be provided as a cake comprising particles in a hydrocarbon solvent, water having been removed through the use of one or more hydrophilic solvents. Reduction of mineral ash content in coal fines is described, for example, in U.S. Pat. No. 4,537,599, US 20110174696 A1, US2016/082446 and Osborne D. et al., Two decades of Jameson Cell installations in coal, (17th International Coal Preparation Congress, Istanbul, 1-6 Oct. 2013).
Alternatively, certain coal seams produce coal that have a suitable ash, and potentially water content. Suitable treatment of this coal to produce coal fines of the required particle size would also be suitable for the invention.
It has surprisingly been found that dewatered, demineralised (or de-ashed) coal microfines product is particularly suitable for providing a blended fuel oil which can still meet the required specifications for use in stationary and marine boilers designed for fuel oil, by having an acceptable level of water, mineral matter, sulphur and particle size.
The present invention blends (i.e. suspends or disperses) the solid particulate matter, suitably demineralised (or de-ashed), de-watered/dehydrated microfine coal, in fuel oil. This not only upgrades the particulate material product and reduces the overall cost of the heavy fuel oil, but also maintains desirable emission characteristics (i.e. low ash, low sulphur emissions) and satisfactory boiler operability. The amount of particulate material, suitably microfine coal that may be blended with the fuel oil is typically determined by the content of ash-forming components, water and sulphur. The concept has been demonstrated with blends of 10% m coal microfines in residual fuel oils. The amount of blended particulate material may be well in excess of 10% m of the blend, for example up to 30% m, 40% m, 50% m, 60% m or more.
Due to the fine particulate nature of the particulate material, suitably microfine coal, it has been found that there is no significant settling of the solids on long-term storage, more than several months, at ambient temperatures. The particles may also pass through filters employed in systems that utilise fuel oils such as residual fuel oils, marine diesel, diesel heating fuel and kerosene heating fuel.
Any particle size of the particulate material, suitably coal fines, that is suitable for blending with fuel oil is considered to be encompassed by the invention. Suitably, the particle size of the particulate material is in the ultrafine range. Most suitably the particle size of the particulate material is in the microfine range. Specifically, the maximum average particle size may be at most about 50 μm. More suitably, the maximum average particle size may be at most around 40 μm, 30 μm, 20 μm, 10 μm, or 5 μm. The minimum average particle size may be 0.01 μm, 0.1 μm, 0.5 μm, 1 μm, 2 μm, or 5 μm.
An alternative measure of particle size is to quote a maximum particle size and a percentage value or “d” value for the proportion by volume of the sample that falls below that particle size. For the present invention any particle size of particulate material, suitably coal fines, that is suitable for blending with fuel oil is considered to be encompassed by the invention. Suitably, the particle size of the blending with fuel oil is in the ultrafine range. Most suitably the particle size of the particulate material is in the microfine range. Specifically, the maximum particle size may be at most around 50 μm. More suitably, the maximum particle size may be at most about 40 μm, 30 μm, 20 μm, 10 μm, or 5 μm. The minimum particle size may be 0.01 μm, 0.1 μm, 0.5 μm, 1 μm, 2 μm, or 5 μm. Any “d” value may be associated with these particle sizes. Suitably, the “d” value associated with any of the above maximum particle sizes may be d99, d98, d95, d90, d80, d70, d60, or d50.
Preparing dewatered, low ash coal particles having an average particle size of <5 μm ready for dispersion into fuels, requires the combination of froth flotation, crushing, grinding and blending steps. The procedure may differ depending on whether the source is a coal fines deposit or a production coal. For coal fines deposits, coarse grinding may precede froth flotation that, in turn, is followed by wet fine grinding of coal to sizes significantly below industry norms, prior to the dewatering steps. For low ash production wet coal, crushing and coarse grinding also need to be followed by wet grinding techniques not commonly used for coal, with final dewatering. For low-ash coal with a low, in situ moisture content, crushing and grinding can be carried out dry, followed by minimal or no water removal.
This technology upgrades the coal fines product. The overall cost of the fuel oil is reduced as is the amount of fuel oil per unit of the blended fuel composition.
The amount of particulate material, suitably coal or microfine coal, that may be blended with the fuel oil is at least 0.1 wt %, suitably at least 1 wt %, 5 wt %, typically around 10 wt % or 20 wt %, at most 70 wt %, suitably at most 60 wt %, optionally at most 50 wt %, 40 wt %, 30 wt %.
The invention is further illustrated by the following non-limiting examples.
The coal slurry is screened, collected in a tank and froth flotation agents are added using controlled dose rates. Micro particle separators filled with process water and filtered air from an enclosed air compressor are used to sort hydrophobic carbon materials from hydrophilic mineral materials. Froth containing carbon particles overflows the tank and this froth is collected in an open, top gutter. The mineral pulp is retained in the separation tank until discharged, whereas the demineralised coal slurry is de-aerated, before being pumped to the pelletisation step. Further coal particle size reduction may be achieved, if necessary, by various known milling techniques, including ones where a hydrocarbon oil is used as a milling aid.
Mechanical dewatering of the demineralised microfine coal slurry is carried out via a rotary vacuum drum filter or filter press. The resultant microfine coal wet-cake may be dried thermally or mechanically to a powder form or pelletized before drying. For pelletisation, a specific modifier is added to the filter cake in a mixer to optimize pelletisation and the modified cake is transported to an extruder where it is compressed into pellets. The demineralised coal pellets are then dried thermally by conveying them via an enclosed conveyor belt and a bucket elevator into a vertical pellet dryer where oxygen-deprived hot process air is blown directly through the microfine coal pellets.
In this way microfine coals 1, 3, 4b, 5, 7 and 8 have been prepared, see Table 3. Their particle size decreases in the order:
Coals D, F, 5, 6 and 8 are examples of coals with very low ash contents of 1.4% m, 1.5% m, 1.5% m, 1.8% m and 1.6% m respectively. Coal 7 has an exceptionally low ash content of just 0.8% m. Fuel oil ash content specifications vary from 0.01% m (marine distillate fuel oil) to 015% m (marine RFO grade RMK). Assuming the fuel oil ash content is close to zero, then the proportions of microfine coals D, F, 5, 6, 7 and 8 that can be added to RMK and remain within specifications are 10.7% m, 10.0% m, 10.0% m, 8.3% m 18.8% m and 9.4% m, respectively. Another froth flotation fraction, coal 7A, prepared alongside coal 7 had an even lower ash content of 0.5% m. Similarly, not only could coal 7A be added to RMK at a concentration up to 30% m, but coal 7A could be added to marine distillate fuel oil at a concentration up to 2% m.
These preparation techniques also result in producing microfine coal with a low sulphur content; coals 3 and 8, Table 3, are examples of coals with low sulphur contents of 1.0% m and 0.9% m respectively which can readily be used in most RFO grades with a sulphur limit of 3.5% m. The sulphur content of coal 7 of just 0.4% m is exceptionally low and would be compatible with future (post 2020) marine RFO grades requiring the lower sulphur limit of 0.5% m. Because of the large investment by refineries anticipated to meet such a low RFO sulphur specification, there is here a clear commercial opportunity for microfine coal.
The type of coal may be selected based on favourable properties of the coal such as low ash or water content or ease of grindability (e.g. high Hardgrove Grindability Index). Coal microfines were obtained by a variety of standard crushing and grinding size reduction techniques in wet media followed by dewatering
Coal microfines were obtained by standard crushing, grinding and pulverising size reduction techniques in a dry state.
In this way several different size fractions (coals 2A-2E) have been prepared from coal D which has a very low ash content of 1.4% m, see Tables 3 and 5. Their particle size decreases in the order:
Assuming the fuel oil ash content is close to zero, then the proportions of microfine coal D that can be added to RMK and remain within specifications is 10.7% m. Coal D is another example of a coal with a very low sulphur content of 0.6% m which could readily be used in most RFO grades.
Obtaining Microfine Coal-Fuel Oil Cake By Grinding Dry Coal with a Fuel Oil or Similar Oil Product
A cake of microfine coal in fuel oil was obtained by grinding dry coal (e.g. coal D, Table 3) in a Netzsch LME4 Horizontal media mill or Laboratory Agitator Bead Mill “LabStar” apparatus with fuel oil as they fluid medium at a 40-50% m solids concentration in the slurry.
In this way different size samples of microfine coal D have been prepared with d90 values as low as 10.7 μm and 2.2 μm respectively.
The resultant blends of diesel and coal D were well-dispersed when the grinding was completed. A dispersion test was carried out at ambient temperatures by storing the 40% m coal-diesel slurry in a 1 litre measuring cylinder at ambient temperatures. After 24 hours 50 ml samples of dispersed slurry were taken from the top, middle and bottom of the measuring cylinder and the coal concentration determined by filtration. Values for coal concentration of 34.7% m, 35.2% m and 40% m were obtained for the top, middle and bottom layers respectively. This showed that dispersions of microfine coal in diesel remain stable for at least 24 hours at ambient temperatures. The particle size distribution of the coal particles in the fuel oil cake was obtained by laser scattering using the dilution method described in Example 15.
Dried microfine coal powder (e.g. coal samples 1, 3, 4b, 8 and 5 in Table 3) a dried pellet of microfine coal, or microfine coal mixed with hydrocarbon oil in the form of a cake, is de-agglomerated and dispersed in fuel oil using a high-shear mixer in a vessel and blended with an additive to aid dispersancy, if required. Optionally, the vessel may be fitted with an ultrasonic capability to induce cavitation to enhance de-agglomeration. Shear mixing is carried out either at ambient temperatures or for more viscous fuel oils at elevated temperatures typically up to 50° C. Suitable shear mixers are manufactured by Charles Ross & Son Co. 710 Old Willets Path, Hauppauge, N.Y. 11788, USA, Silverson Machines Inc., 355 Chestnut St., East Longmeadow, Mass. 01028, USA, and Netzsch-Feinmahltechnik.
This process will typically take place at: a distillation plant, oil depot or bunkering facility, power plant, or industrial process site. The resultant fuel oil/microfine coal dispersion may be stored in tanks with agitation and heating equipment, stable for several months at ambient temperatures, or for short periods at elevated temperatures. The product can also be delivered immediately to end-user's combustion equipment.
Three fuel oils (two RFO samples and one marine distillate, i.e. marine diesel) have been blended with microfine coal samples with an additive to aid dispersancy and a set of analytical test results obtained for a range of specification parameters, see Table 4.
Four microfine coal samples derived from the same generic US low-volatile bituminous coal source were tested (samples 1, 3, 4b and 8), together with three samples of US high-volatile bituminous coals (samples 5, 6 and D), and one high-volatile bituminous coal from Colombia (sample F), and another from Australia (sample 7).
Characterisation tests of the coal samples are given in Table 3. The microfine coal samples differ primarily in terms of particle size and ash content:
Samples 1 and 3 were derived from the same low-volatile bituminous coal source, samples 5 and 6 from two different high-volatile bituminous coal sources, and the results of characterisation tests are given in Table 3. (n.a.=not yet available). All microfine coal samples, excepting D and F had >99% of particles below 20 μm in diameter. Sample 5 had the highest proportion (30% m) of microfine coal particles below 1 μm.
An increase, both in density and in viscosity is observed from addition of three microfine coal samples 3, 4b and 8, Table 4. Density increases more rapidly for sample 3>sample 4b>sample 8; which may be associated with changes in particle size. However, there is little difference in the rate of viscosity increase between samples 3 and 8, suggesting that reducing coal particle size from an average diameter of 6.2 μm to 1.8 μm has surprisingly little impact on viscosity. The viscosity increase for sample 4b is less than for the other two coals, and this may be attributable to the higher ash content of this coal.
A small increase in density is observed from addition of 10% m microfine coal sample 1 to the very heavy RFO-1 from 999.5 kg/cm3 to 1026.9 kg/cm3 at 15° C. (with analogous results obtained for density at 60° C.) and a corresponding small increase in viscosity from 881 to 1128 CSt @ 50° C.).
A very small, but detectable, increase in density is observed from addition of 1% m microfine coal sample 1 to marine diesel from 0.8762 g/cm3 to 0.8769 g/cm3 @ 15° C. (with analogous results obtained for density at 60° C.). A consistent corresponding increase in viscosity was not detectable.
The impact of the density and viscosity increases from microfine coal addition correspond approximately to the difference in density and viscosity between adjacent grades of fuel oil (Tables 1a to 1c). It has been surprisingly found that the addition of 10% m microfine coal only changes the fuel oil grade to the next heaviest fuel oil grade. Thus RFO-II, which is an RMK 380 grade, becomes RMK 700 on addition of 5% m microfine coal 3 or 5% m microfine coal 8. As density exceeds 1010 kg/m3 and viscosity exceeds 700 mm2/s, the application of RFO-microfine coals to marine and stationary equipment becomes more limited and the rate that at which particular microfine coals increase density and viscosity may become more important than ash content in determining the maximum amount of microfine coal that can be accommodated in practice.
Although addition of microfine coal to RFO increases viscosity, unexpectedly and a positive finding is that the Pour Point of RFO was relatively unaffected by the addition of microfine coal, Table 3. Note that the repeatability and reproducibility of RFO Pour Point determination are 2.6° C. and 6.6° C. respectively, so a value of 3° C. or 9° C. is not significantly different to 6° C. Hence, neither samples 3 nor 4b significantly affected Pour Point at a concentration of 10% m. However, addition of 10% m and 15% m of the lowest particle size coal sample 8 did produce a slightly higher Pour Point of 12° C. Similarly the Pour Point of marine diesel was unaffected by the addition of 1% m microfine coal.
The Flash Point of RFO and marine diesel is improved (i.e. higher value) by blending microfine coal with the base fuel oil, Example 7 and
The total acid number (TAN), a measurement of RFO acidity, can be improved by addition of microfine coal, Example 8, albeit consistent improvement is not observed from all the blends tested. In neither case did TAN deteriorate from microfine coal addition. On the one hand Coal 3 progressively reduced the RFO-II TAN value from 0.3 to 0.12 to 0.01 mg KOH/g fuel as concentration was increased from 0 to 5% m to 10% m. However a marked reduction in TAN by coal 8 at 5% m addition from 0.3 to 0.03 mg KOH/g fuel was followed by values of 0.5 and 0.26 mg KOH/g fuel at 10% m and 15% m respectively which are commensurate with that for the base fuel alone.
RFO-II has been blended with 5 microfine coal samples of different particle size derived from coal D (samples 2A-2E) and viscosity measured for concentrations up to 15% m, Table 5 and
The rate of viscosity increase is least for coal 2E which in turn is less than 2D<2C<2B and 2A. This order coincides with most measures of particle size increasing in the order 2E>2D>2C>2B>2A. Thus viscosity increase of RFO-microfine coal blends is inversely proportional to particle size. It is worth noting that the viscosity-particle size traces for 2A and 2B crossover: although 2A has a lower d50 and d90 than 2B, and contains 35% of sub-1 μm particles, it contains less particles <10 μm than 2B and its d95, d98 and d99 values are higher.
As the upper limit for RFO viscosity used in most ship is 700 cSt @ 50° C., and that for most stationary boilers is approximately 60 cSt @ 100° C. (e.g. RFO-1), viscosity increase will limit the highest coal concentration that can be used. Similarly as particle size in turn influence viscosity increase then particle size distribution becomes a critical factor for determining an acceptable concentration of microfine coal in RFO. Although sub-1 micron particles increase RFO viscosity more quickly when concentration is increased, a surprisingly high concentrations of sub-1 μm can be accommodated, e.g. with RFO-II a blend of approximately 8% m coal 2A, which contains as much as 35% sub-1 micron particles would be acceptable for marine use.
RFO-II has been blended with 3 microfine coal samples of different particle size derived from coal D (samples 2A-2E) and with coals 3, 4b, 7 and 8. Density was measured for concentrations up to 15% m, Table 6. As shown in
In contrast to viscosity changes, the differences in particle size have less impact on density than the increasing coal concentration. The rate of density increase is least for coal 2E, is approximately the same for 2D and 2C, with that for coals 3, 7 and 8 the highest. This order is approximately in line with increasing particle size. Thus density increase of RFO-microfine coal blends is inversely proportional to particle size.
The upper limit for RFO density used in most shipping is in practice 1250 kg/m3 @ 15° C., which is determined by the upper operating limit for the most commonly used type of centrifuge (Alcap type). Some older fuel oil centrifuges have an upper operating limit of 1010 kg/m3 @ 15° C. Stationary boiler fuel oil specifications do not usually include a maximum density requirement.
As density and viscosity increases, the application of RFO-microfine coals to marine and stationary equipment can become more limited and the rate that at which particular microfine coals increase both these parameters may become as important as ash content in determining the maximum amount of microfine coal that can be accommodated in practice.
Pour Point was measured for RFO-II blends with a similar set of coals as that used for Example 5. The results are shown in Table 7. Although addition of microfine coal to RFO increases viscosity, the unexpected positive finding is that the Pour Point of RFO only increases by a small amount when microfine coal is added.
The repeatability and reproducibility of RFO Pour Point determination is 2.6° C. and 6.6° C. respectively, so a value of 3° C. or 9° C. is not significantly different to 6° C. Hence, neither samples 3 nor 2C significantly affected Pour Point at concentrations up to 10% m and 15% m respectively. However, addition of 10% m and 15% m of the coal samples 2A, 8, 2B and & 8 did produce a slightly higher Pour Point of 12° C. The latter four coal samples have smaller particle sizes than coals 2C and 3 indicating the Pour Point increase for RFO blends is greater for coals with the lowest particle size, which is consistent with higher viscosity increases observed for lower coal particle sizes at the same coal concentration, Example 4.
In Example 3 it was discussed that the Flash Point of marine diesel and RFO could be improved (i.e. higher value) by a significant amount from blending microfine coal 1 with the base fuel, (Table 4). Flash Point was measured for RFO-II blends with a similar set of coals as that used for Example 6. The results are shown in Table 8 and
In 5 of the 6 coal samples tested, addition of just 5% m of microfine coal increased the Flash Point of the RFO blend from by over 10° C. from 108° C. in RFO-II alone to over 120° C. Further coal additions of 10% m and 15% m to RFO-II increased Flash Point further to values of around 125° C. and 130° C. respectively. In one case, coal 2C, Flash Point was elevated to 150° C. by 10% m and 15% m addition (
These are significant increases for a parameter that can be a limiting specification parameter in RFO refinery manufacturing. Being able to manipulate the flashpoint of the blended coal-fuel oil may be useful in bringing the blend back into specification when the non-blended fuel oil falls outside. To help with context, there are no fuel additives available commercially that can be used to adjust Flash Point in a predictable way.
The total acid number (TAN), a measurement of RFO acidity, can be improved by addition of microfine coal, Table 9, albeit that consistent improvement is not observed from all the blends tested. On the one hand Coal 3 progressively reduced the RFO-II TAN value from 0.3 to 0.12 to 0.01 mg KOH/g fuel as concentration was increased from 0 to 5% m to 10% m. However a marked reduction in TAN by coal 8 at 5% m addition from 0.3 to 0.03 mg KOH/g fuel was followed by values of 0.35 and 0.26 mg KOH/g fuel at 10% m and 15% m respectively which are commensurate with that for the base fuel alone.
A stainless steel rig was designed for testing the dispersion of microfine coal samples in RFO,
The results demonstrate that dispersions of 10% m microfine coal in RFO can be produced. These dispersions are stable up to 48 hours if prepared by shear mixing with a dispersant additive for 60 minutes (test 8). Shorter stability times of 24 hours were obtained if only 10 minutes mixing was carried out (tests 1-4).
A blend of 1% m microfine coal and marine diesel, plus a fuel oil dispersant additive, was shear mixed at 11,000 rpm in a 100 ml glass sample bottle for 20 minutes, then left to stand at ambient temperature for 1 hour and 24 hours (test 12 and 13). This was then repeated in an ultrasonic bath (tests 14 and 15). After settling for 1 hr, a 10 mL aliquot of the fuel-coal particle suspension was taken by Eppendorf pipette from the top (first) and from the bottom (second) of the sample. Each aliquot was vacuum filtered through pre-weighed 0.8 μm cellulose nitrate membrane filters using a sintered glass Buchner flask. The solid residue+filter were washed four times with n-heptane before reweighing, after a minimum of 24 hrs drying time, to determine mass of undissolved solids in each aliquot and hence, uniformity of dispersion.
The results show that dispersions of 1% m microfine coal in marine diesel can be produced that are stable for at least 1 hour. A more uniform dispersion is obtained if shear mixing occurs in an ultrasonic bath.
0.2
0.2
0.15
0.19
2.5
0.4
9.5
1.4
0.35
0.45
26.0
29.2
In Example 9 it was shown that dispersions of 10% m microfine coal in RFO can be produced, stable up to 48 hours at 80° C., if prepared by shear mixing with a dispersant additive for 60 minutes at 80° C. Further work using the same method as described in Example 9 has been carried out, Table, 11. Thus in Test No. 9, 10% m of coal 3 was dispersed and held at 80° C. for 2 days without dispersant additive. Test No. 8 was identical except for the presence of the dispersant additive. Both tests showed a stable dispersion with almost all (91-97% m) of the microfine coal suspended in the top, middle and bottom layers. However the dispersed coal concentrations (expressed as % of initial coal concentration) were slightly higher 95-97% m with dispersant present than without (91-94% m) showing that addition of this dispersant was improving dispersion stability.
The inclusion of a proprietary dispersant additive improves dispersion. Suitable fuel dispersant additives are manufactured by most petroleum fuel additive manufacturers, e.g. Innospec Ltd., Oil Sites Road, Ellesmere Port, Cheshire, CH65 4EY, UK; Baker Hughes, 2929 Allen Parkway, Suite 2100, Houston, Tex. 77019-2118, USA; BASF SE, 67056 Ludwigshafen, Germany.
The dispersion stability at 80° C. of 10% m microfine coal 3 in RFO-II after shear mixing for 60 minutes at 80° C. in the presence of a dispersant additive was tested for longer periods of 4 days and 7 days, see Test nos. 10 and 11, Table 11.
Excellent stability was obtained after 4 days with almost all (97-102% m) of the microfine coal suspended in the top, middle and bottom layers, Test 10. Note that because of experimental errors in the dispersion and the measurement of dispersed coal, values slightly above 100% m have been reported for several blends. Unless these values above 100% m appertain to the dead bottom layer where particles start to settle out when the dispersion breaks down, they should be treated as not significantly different in magnitude to 100% m.
In Test 11 the dispersion experiment was extended to 7 days at 80° C. In this case relatively good stability was still obtained with most (80-81% m) of the microfine coal suspended in the top, middle and bottom layers. These two tests show that these dispersions have excellent stability beyond 4 days with a small amount of settlement beginning to occur after 7 days.
Once these dispersions of coal in RFO-II have been prepared in the rig (
The dispersion stability at 80° C. of different concentrations of microfine coal 2B (10% m to 30% m) in RFO-III (for analytical details, see Table 5) has been measured after shear mixing for 60 minutes at 80° C. and storage at 80° C. for a period of 4 days, see Test nos. 16-19, Table 11. Excellent stability was obtained at 10% m, 15% m and 20% m where almost all (90->100% m, note comment in Example 10) of the microfine coal is suspended in the three main layers. The stability of a 30% m blend of coal 2B in RFO-III was also good (81-87% m 90->100% m of the microfine coal is suspended in the top, middle and bottom layers) with just a small amount of settlement occurring at the dead bottom.
The dispersion stability at 80° C. of 15% m of microfine coals 7 and 8 in RFO-III has been measured after shear mixing for 60 minutes at 80° C. and storage at 80° C. for a period of 4 days, see Test nos. 20-21, Table 11. Excellent stability was obtained for the blend of 15% m of coal 8, where almost all (95->100% m, note comment in Example 10) of the microfine coal is suspended in the three main layers. The stability of the 15% coal 7 blend is good, but there is evidence of small settlement in the dead bottom layer (129% m), compared with 70% m in the top layer, with 100% m in the middle and bottom layers. That the particle size of coal 8 (d50=1.8 μm) is lower than that of coal 2B (d50=2.7 μm) and of coal 7 (d50=3.2 μm) may provide an explanation for the better stability performance observed for coals 8 and 2B than coal 7.
The combustion properties of blends of RFO-III with different concentrations of coal 7 between 5% m and 15% m have been determined by the Standard Institute of Petroleum (London) Method IP541, Quantitative determination of ignition and combustion characteristics of residual fuels for use in compression ignition engines. In this method, a small sub-sample is injected into compressed air in a constant volume combustion chamber and the start of injection and pressure changes during each combustion cycle detected. This is repeated 25 times and ignition and combustion characteristics are calculated from the averaged pressure-time and rate of pressure change-time traces.
Table 12, shows the various ignition and combustion characteristics and the range applicable to conventional RFO for each of them. Blends from 5% m to 15% m of coal 7 in RFO-III are within these applicable will depend on the choice of base RFO, the coal type and the coal particle size, as well as the coal concentration. This pass data shows that such RFO-coal blends would perform well in normal large, low- and medium-speed, marine diesel engines.
Particle size distributions are typically determined by a laser scattering method which measures the particle volume of particles between a series of incremental size ranges.
Typically the particle distribution width is quantified by particle diameter values on the x-axis, d50, d90, d95, d98 and d99, as shown in
In view of the above, it has been surprisingly found that it is possible to engineer coal fines to obtain sufficiently low mineral matter content (or ash content), moisture content, sulphur content and particle size in order to meet those fuel oil specifications, and which also could be dispersed in fuel oil to provide a dispersion that is stable over at least 48 hours. Furthermore, preparation of a stable, if relatively short term, suspension of fine coal particles with a 1.0% m coal loading in Marine Fuel, which is much less viscous than RFO. The improvement in Flash Point of marine diesel as a result of blending in 1% m microfine coal was also unexpected.
Based on the above results, the present invention shows industrial application in:
Although particular embodiments of the invention have been disclosed herein in detail, this has been done by way of example and for the purposes of illustration only. The aforementioned embodiments are not intended to be limiting with respect to the scope of the invention. It is contemplated by the inventors that various substitutions, alterations, and modifications may be made to the invention without departing from the spirit and scope of the invention.
| Number | Date | Country | Kind |
|---|---|---|---|
| 1605768 | Apr 2016 | GB | national |
| 1607557 | Apr 2016 | GB | national |
| 201611044116.0 | Nov 2016 | CN | national |
| Number | Name | Date | Kind |
|---|---|---|---|
| 1329493 | Bacon | Feb 1920 | A |
| 2590733 | Stillman | Mar 1952 | A |
| 2754267 | Bondi | Jul 1956 | A |
| 3327402 | Lamb et al. | Jun 1967 | A |
| 4090853 | Clayfield et al. | May 1978 | A |
| 4239426 | Nakabayashi et al. | Dec 1980 | A |
| 4251229 | Naka et al. | Feb 1981 | A |
| 4255155 | Frankovich | Mar 1981 | A |
| 4265637 | Anderson | May 1981 | A |
| 4282004 | Masologites | Aug 1981 | A |
| 4306683 | Mallison | Dec 1981 | A |
| 4309269 | Denker et al. | Jan 1982 | A |
| 4319980 | Jenkins | Mar 1982 | A |
| 4330300 | Cairns | May 1982 | A |
| 4334976 | Yan | Jun 1982 | A |
| 4358293 | Mark | Nov 1982 | A |
| 4377392 | Massey et al. | Mar 1983 | A |
| 4382001 | Kulprathipanja et al. | May 1983 | A |
| 4389219 | Naka et al. | Jun 1983 | A |
| 4396397 | Kugel et al. | Aug 1983 | A |
| 4417901 | Ando et al. | Nov 1983 | A |
| 4420445 | Yamamoto et al. | Dec 1983 | A |
| 4425135 | Jenkins | Jan 1984 | A |
| 4459762 | Hardesty et al. | Jun 1984 | A |
| 4511364 | Mitsumor | Apr 1985 | A |
| 4537599 | Greenwald, Sr. | Aug 1985 | A |
| 4552725 | Audeh | Nov 1985 | A |
| 4671801 | Burgess et al. | Jun 1987 | A |
| 4780110 | Beshore | Oct 1988 | A |
| 4783198 | Hueschen | Nov 1988 | A |
| 4859209 | Szabo nee Mogyorossi et al. | Aug 1989 | A |
| 4900429 | Richardson | Feb 1990 | A |
| 5096461 | Frankiewicz et al. | Mar 1992 | A |
| 5242470 | Salter et al. | Sep 1993 | A |
| 5379902 | Wen et al. | Jan 1995 | A |
| 5503646 | McKenny et al. | Apr 1996 | A |
| 5902359 | Grosso et al. | May 1999 | A |
| 6083286 | Ono | Jul 2000 | A |
| 6767465 | Choung et al. | Jul 2004 | B1 |
| 6793079 | Khan et al. | Sep 2004 | B2 |
| 7431744 | Sugita et al. | Oct 2008 | B2 |
| 7537700 | Kanda et al. | May 2009 | B2 |
| 8177867 | Joseph et al. | May 2012 | B2 |
| 8591607 | Fleming et al. | Nov 2013 | B2 |
| 8610071 | Kamba et al. | Dec 2013 | B2 |
| 9328920 | Sirdeshpande et al. | May 2016 | B2 |
| 9777235 | Snaith | Oct 2017 | B2 |
| 20070228509 | Okada et al. | Oct 2007 | A1 |
| 20100287828 | Flemming et al. | Nov 2010 | A1 |
| 20110174696 | Young et al. | Jul 2011 | A1 |
| 20110239973 | Qin | Oct 2011 | A1 |
| 20120167457 | Harsh et al. | Jul 2012 | A1 |
| 20120177923 | Kumara | Jul 2012 | A1 |
| 20120317878 | Taulbee | Dec 2012 | A1 |
| 20130152453 | Baird et al. | Jun 2013 | A1 |
| 20150184099 | Swensen et al. | Jul 2015 | A1 |
| 20160082446 | Swensen et al. | Mar 2016 | A1 |
| 20160160141 | Sakaguchi et al. | Jun 2016 | A1 |
| 20180134977 | Swensen et al. | May 2018 | A1 |
| Number | Date | Country |
|---|---|---|
| 1096620 | Mar 1981 | CA |
| 1109820 | Sep 1981 | CA |
| 1354227 | Jun 2002 | CN |
| 101245918 | Aug 2008 | CN |
| 101397514 | Apr 2009 | CN |
| 101649220 | Feb 2010 | CN |
| 101735871 | Jun 2010 | CN |
| 102434343 | May 2012 | CN |
| 105567321 | May 2016 | CN |
| 108148610 | Jun 2018 | CN |
| 2849128 | May 1979 | DE |
| 2849124 | May 1980 | DE |
| 3130662 | Feb 1983 | DE |
| 3200240 | Jul 1983 | DE |
| 0012606 | Jun 1980 | EP |
| 0042727 | Dec 1981 | EP |
| 0062220 | Oct 1982 | EP |
| 0105236 | Apr 1984 | EP |
| 3438048 | Feb 2019 | EP |
| 2595711 | Nov 1982 | FR |
| 2164271 | Mar 1986 | GB |
| 53117002 | Oct 1978 | JP |
| S53117002 | Oct 1978 | JP |
| S5440808 | Mar 1979 | JP |
| S54129008 | Oct 1979 | JP |
| S5636589 | Apr 1981 | JP |
| S5798595 | Jun 1982 | JP |
| S62172093 | Jul 1987 | JP |
| S6348396 | Mar 1988 | JP |
| 2002290673 | Oct 2002 | JP |
| 5582192 | Sep 2014 | JP |
| 5730795 | Jun 2015 | JP |
| 5780484 | Sep 2015 | JP |
| 1838384 | Aug 1993 | RU |
| 2541322 | Feb 2015 | RU |
| 2010039315 | Apr 2010 | WO |
| 2011084730 | Jul 2011 | WO |
| 2015187450 | Dec 2015 | WO |
| 2017166920 | Oct 2017 | WO |
| 2017174973 | Oct 2017 | WO |
| Entry |
|---|
| China Office Action pertaining to CN2019107714058 dated Dec. 29, 2020. |
| Japan Office Action pertaining to JP2018-539146 dated Dec. 1, 2020. |
| Office Action pertaining to U.S. Appl. No. 15/981,372 dated Dec. 10, 2020. |
| Office Action pertaining to U.S. Appl. No. 16/082,678 dated Dec. 23, 2020. |
| Cui et al., “A Novel Process for Preparation of an Ultra-Clean Superfine Coal-Oil Summary”, Fuel, vol. 87, pp. 2296-2303, 2008. |
| Trass et al., “Coal Slurry Fuel Technology”, The Canadian Journal of Chemical Engineering, vol. 65, pp. 177-201, Apr. 1987. |
| Shaver, Robert G., “A Solvent-Refined Coal Process for Clean Utility Fuel”, Advances in Chemistry Series, 1974, 127, 89-90. |
| U.S. Non-Final Office Action issued in U.S. Appl. No. 15/981,362 dated Sep. 21, 2018. |
| U.S. Non-Final Office Action issued in U.S. Appl. No. 15/981,372 dated Sep. 6, 2018. |
| U.S. Non-Final Office Action issued in U.S. Appl. No. 15/981,372 dated Sep. 20, 2019, 15 pages. |
| Search Report pertaining to corresponding Great Britain Patent Application No. GB1815791.7, dated Mar. 1, 2019. |
| Examination Report pertaining to corresponding Russian Patent Application No. 2018123758/04(037656), dated Jan. 25, 2019. |
| Examination Report pertaining to corresponding Russian Patent Application No. 2018123748/04(037645), dated Jan. 25, 2019. |
| Wibberly et al., “Premium Coal Fuels with Advanced Coal Beneficiation”, 40th Interational Technical Conference Clean Coal & Fuel Systems, May 31-Jun. 4, 2015, Sheraton Sand Key, Clearwater, Florida, USA. |
| Grimanis et al., “Storage, transportation, and atomization of CWF for residential applications”, Final Report, Sep. 27, 1989-Nov. 15, 1991, pp. 1-153, retrieved from https://www.osti.gov/biblio/101128538-storage-transportation-atomization-cwf-residential-applications-final-report-september-november. |
| Baek Se Hyun et al., “The Effect of the Coal Blending Method in a Coal Fired Boiler on Carbon in Ash and N0x Emission”, Fuel, IPC Science and Technology Press Guildford, GB, vol. 128, Mar. 6, 2014, pp. 62-70. |
| International Search Report dated Feb. 6, 2020 for application No. PCT/GB2018/052738 filed Sep. 27, 2019. |
| Zhichao, et al., Ultra-clean coal's laboratory investigation for the coal preparation plant of Taqixi, pp. 1-10, retrieved from http://www.paper.edu.cn/releasepaper/content/201003-1050 (date unknown). |
| Examination Report pertaining to Indian Application No. 201817029523 dated Jun. 26, 2020. |
| Examination Report pertaining to Colombian Application No. 20189998147 dated Jun. 18, 2020. |
| Office Action pertaining to Chinese Application No. 20161104416.0 dated Jun. 19, 2020. |
| Office Action pertaining to Australia Application No. 2017246679 dated Jul. 31, 2020. |
| International Search Report and Written Opinion pertaining to PCT/GB2018/050939 dated Jul. 13, 2017. |
| Office Action pertaining to U.S. Appl. No. 16/082,678 dated Apr. 30, 2020. |
| Office Action pertaining to U.S. Appl. No. 16/082,678 dated Nov. 1, 2019. |
| Office Action pertaining to Japanese Application No. 2018-539158 dated Aug. 2, 2011. |
| Office Action pertaining to Indonesia Application No. PID201804912 dated Aug. 24, 2020. |
| Office Action pertaining to Japanese Application No. 2018-539146 dated Aug. 2, 2018. |
| Office Action pertaining to India Application No. 201817029522 dated Jul. 24, 2020. |
| India Office Action pertaining to Application No. 201918033361 dated Jan. 8, 2021. |
| China Office Action pertaining to Application No. 201780012719 dated Jan. 14, 2021. |
| Colombia Office Action pertaining to Application No. NC2018/0009147 dated Jan. 8, 2021. |
| Office Action pertaining to Columbia Application No. NC2018/0009148 dated Aug. 21, 2020. |
| Office Action pertaining to Korean Application No. 9-5-2020-065058002 dated Sep. 21, 2020. |
| Indonesia Office Action pertaining to Application No. HKI-3-HI.05.02.01.PID201804937-TA dated Oct. 21, 2020 with English Translation. |
| China Office Action pertaining to Application No. 2017800112831 dated Oct. 30, 2020 with English Translation. |
| Japan Office Action pertaining to Application No. 2018-539158 dated Nov. 17, 2020 with English Translation. |
| Jing et al., “Preparation of Slurry with Colloid Mill and the Effect of the Particle Size of Coal on Direct Liquefaction Properties of the Oil”, Coal Conversion, vol. 37, Issue 2, pp. 28-32, Apr. 2014. |
| Final Rejection pertaining to U.S. Appl. No. 15/981,372 dated Jun. 9, 2021. |
| China Office Action pertaining to Application No. 2017800112831 dated Aug. 10, 2021. |
| China Office Action pertaining to Application No. 2019107714058 dated Jul. 15, 2021. |
| Examination Report pertaining to Colombian Application No. 20180009148 dated Jun. 21, 2021. |
| China Office Action pertaining to Application No. 2017800112719 dated Jul. 15, 2021. |
| Brazil Office Action pertaining to Application No. BR112018068810-0 dated Jul. 21, 2021. |
| Brazil Office Action pertaining to Application No. BR112018068818-5 dated Jul. 21, 2021. |
| Colombia Office Action pertaining to Application No. NC2018/0009148 dated Feb. 8, 2021. |
| Korean Office Action pertaining to Application No. 10-2020-7017301 dated Apr. 15, 2021, 7 pages. |
| Office Action Chinese Application No. CN201780011283A dated Apr. 24, 2021, with English translation. |
| Office Action Saudi Application No. 518392003 dated Mar. 29, 2021, with English translation. |
| Office Action pertaining to European Patent Application No. 17722125.6 dated Jun. 21, 2021. |
| Chinese Office action pertaining to Application No. 201611044116.0 dated Aug. 12, 2021. |
| Korean Rejection pertaining to Application No. 52018044771 dated Oct. 20, 2021. |
| Colombia Office Action pertaining to Application No. NC2018/0009147 dated Sep. 15, 2021. |
| Notice of Allowance pertaining to U.S. Appl. No. 15/981,372 dated Oct. 14, 2021. |
| Notice of Allowance pertaining to U.S. Appl. No. 16/082,678 dated Nov. 17, 2021. |
| China Rejection pertaining to Application No. 20178001271.9 dated Nov. 3, 2021. |
| China Rejection pertaining to Application No. 201910771405.8 dated Nov. 4, 2021. |
| Saudi Arabia Office Action pertaining to Application No. 518392002 dated Nov. 16, 2021. |
| Number | Date | Country | |
|---|---|---|---|
| 20200377812 A1 | Dec 2020 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 16082678 | US | |
| Child | 16999530 | US | |
| Parent | 15284995 | Oct 2016 | US |
| Child | 16082678 | US |
