JP2014055304A - Polydispersed mixed emulsion - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a fuel emulsion having desired fuel characteristics and calorific value, and excellent in combustion in any furnace or combustion arrangement.SOLUTION: A emulsified hydrocarbon fuel contains a composite emulsion formed from a plurality of in-water hydrocarbon emulsion and an emulsion stabilizer, the composite emulsion has single peaked hydrocarbon particle distribution, the hydrocarbon exits with 64 to 90 vol.%, the fuel contains at least two kinds of different precursor emulsions and the precursor emulsions have respective different hydrocarbon particle diameters. Each precursor emulsions has distinctive viscosity and the viscosity of the emulsified composite emulsion fuel is lower than the distinctive viscosity of the precursor emulsions.

Description

The present invention relates to an emulsion formed from a precursor emulsion having an arbitrary particle modal distribution, resulting in a unimodal emulsion with maximized desired chemical and physical properties. About that.

Simple two-phase emulsions are generally classified by the concentration of the dispersed phase, the size distribution of the dispersed droplets and the rheological properties of the emulsion. Emulsions with a dispersed phase of 0 to 30% by volume are low internal phase ratio (LIPR) emulsions, and emulsions with a dispersed phase of 30 to 70% by volume are medium internal phase ratio emulsions (medium internal phase
se: MIPR) and 70-100% by volume of dispersed phase emulsion is high internal phase emulsion (high
This is known as internal phase (HIPR). The rheological behavior of the emulsion can be Newtonian or non-Newtonian. The extent of its behavior will depend on the properties and concentration of the two liquids used to make the emulsion. Oil-i
For emulsions consisting of n-water (O / W), LIPR emulsions usually exhibit Newtonian behavior. As the dispersed oil phase concentration increases, the behavior becomes increasingly non-Newtonian.

R. Pal et al. [Emulsions in the Petroleum Industry Journal, Chapter 4, Rheology of
Emulsions] (Non-Patent Document 1) showed that O / W emulsions can be considered Newtonian up to a dispersed phase volume of 0.4 (ie 40% dispersed phase). This can be achieved at various dispersed phase concentrations.
/ W emulsions were prepared and obtained by measuring shear stress (τ) at various shear rates (γ). All emulsions contained droplets of the same average diameter and were performed at a constant temperature.

  The viscosity (η) of the emulsion is the shear stress (τ) vs. shear rate:

Defined as the ratio of This is the equation:

Given by.

The viscosity of a particular emulsion is R.I. Pal et al. [Emulsions in the Petroleum Indust
Relies on several factors according to ry Journal, Chapter 4, Rheology of emulsions].

1. The viscosity of the continuous phase.
2. Volume fraction of dispersed phase.
3. Dispersion phase viscosity.

4). Average particle size and distribution.
5. Shear rate.
6). The nature and concentration of the emulsifier.

7). temperature.
The viscosity of the dispersed phase may be involved in determining the emulsion viscosity. This is especially true when internal circulation of droplets occurs, reducing flow field distortion and lowering the viscosity of the emulsion. In such a system, when the viscosity of the dispersed phase increases, the internal circulation decreases,
The actual emulsion viscosity increases. In the presence of the emulsifier, the internal circulation is greatly hindered and the dispersed phase droplets are R.D. According to Pal et al. [Emulsions in the Petroleum Industry Journal, Chapter 4, Rheology of emulsions] (Non-Patent Document 1), it behaves more like a solid particle.
For this reason, such systems behave very much the same, and some of the experiments discussed in this document contain solid particles in suspension rather than fluid droplets.

All of the above factors are involved in determining the emulsion viscosity, but the most important is the volume fraction of the dispersed phase. Einstein was the first to show that the viscosity of the system increased as the volume fraction of dispersed particles increased. Einstein
The relative viscosity of the suspension is:

{Where η _r is the relative viscosity of the emulsion and φ is the volume fraction of the dispersed phase}. Although this equation was accurate, its applicability is very limited. Since the suspension must be very dilute (solids are less than 1% total volume), the particles are so far away that they are acting on fluid forces (eg caused by van der Waals attraction and Brownian motion) There are no particles and the particles are hard spheres. In such systems, particle size will not affect viscosity as long as the total volume is less than 1%.

Several empirical equations have been proposed to predict the relationship between viscosity and dispersed phase concentration. The most widely known and used is Krieger-Doug
herty) equation:

{Where φ _max is the maximum packing concentration of the dispersed phase and [η] is the intrinsic viscosity, which is a measure of the ability of the particles to affect viscosity (2.5 for hard spheres)}.

  Another equation used to predict dispersion viscosity is Mooney's equation:

{Where K is a constant reflecting droplet packing}.

The models commonly used to represent droplet filling in a monodisperse emulsion assume that all are non-deformable spherical droplets. The maximum packing fraction (φ _max ) of such a system is 0.74. This maximum is brought about when uniform spherical droplets are packed hexagonally into the continuous phase. This model of maximum filling concentration is applied when assuming that the dispersed phase is composed of non-deformed spheres. It may not be. In this case, the above model is Pal et al. [Colloids and Surfaces A: Physi
ochem. Eng. Aspects, 137, (1998), 275-286, A novel method to correlate
According to emulsion viscosity data] (Non-Patent Document 2), it is not accurate.

The Krieger-Doatty equation is the critical deformation volume
It seems to fit well with most of the collected data for emulsions with a total volume fraction below (fraction) (φ _d ). This is the point where high levels of droplet deformation can occur under shear stress. This critical deformation volume fraction is deformable for various emulsions and depends on both the disperse phase used and the properties of the emulsifier. As the total volume increases, the rheology of the emulsion becomes non-Newtonian. Equations that predict viscosity, such as the Krieger-Doatty equation and Mooney equation, are not accurate, but are based on experimental data and various assumptions. These show accuracy at low volume fractions, but there is a limit at high volume fractions where deviations occur in experimental data.

In recent years, rheological properties that are characteristic of various bimodal systems have attracted attention. These effects to be discussed are emulsions (ranging from LIPR to HIPR) and suspensions in the presence of any colloidal force.
(Diluted to concentrated) is also known.

The following properties are known in composite emulsions and suspensions:
High maximum packing fraction;
Reduced viscosity;
Reduced shear-thinning effect (usually an emulsion) at a given filling fraction;
Reduced shear-thickening effect at a given filling fraction (
Normal suspension);
Reduced storage / loss modulus.

In 1971, Chong et al. [Journal of Applied Polymer Science, 15 (8), 2007; 1971, Rhe
ology of concentrated suspensions] (Non-Patent Document 3), by mixing two different types of suspensions, each of different sized particles, the rheological properties of the mixed suspensions can be reduced to a specific volume fraction mixture. It was found that it was significantly modified. This experiment measures the relative viscosity of monodisperse and bidisperse suspensions, and for a specific volume percent combination, a bi-disperse suspension is a two-component monodisperse suspension. (two compo
The viscosity was considerably lower than that of nent mono-disperse suspension). This was evident at solid loading concentrations between 0.55 and 0.65 to varying degrees.

The minimum viscosity appeared to occur with about 40% globules in all solids in each case. Chong et al [
Journal of Applied Polymer Science, 15 (8), 2007; 1971, Rheology of concent
It was also noted that the viscosity could be further reduced in this respect by increasing the size difference between small and large spheres according to [rated suspensions].

There are three main variables that can be found even in this very early study to maximize the viscosity drop in a bimodal system:
Total volume fraction of the dispersed phase;
Fine droplet / particle ratio;
Fine and coarse droplet / particle diameter ratio.

Various theories have been proposed as to why such a viscosity drop occurs when adding fine particles or fine droplets to larger particles or larger droplets. One common way to consider this problem is with respect to the maximum fill fraction. It can be seen from the Krieger-Doatty equation that the maximum fill fraction directly dominates the viscosity of the suspension or emulsion. If particulates are added to the lattice of large particles, they can occupy that position in the space between the large particles and there is more space available, so the maximum filling fraction is not high. Larger space available means less viscosity because it means greater fluidity in the system.

Greenwood et al. [Colloids and Surfaces A: Physiochem. Eng. Aspects, 144 (1998) 1
39-147, Minimising the viscosity of concentrated dispersions by using bi
[modal particle size distributions] (Non-Patent Document 4) designed a detailed experiment to find out the effect of composition (of small particles compared to large particles) on the rheological properties of bimodal suspensions. The diameter ratio of small particles to large particles used in the experiment was 4.76. They report that this is the minimum ratio they have found in viscosity. Their work required measuring the viscosity of various bimodal suspensions containing 10-30% by volume of small particles. Viscosity measurements were performed on these suspensions with a total volume fraction between 0.45 and 0.65.

These results indicate that minimum viscosity occurs at a composition of 0.2 volume of small particles for each of the various total volume fractions. It is also clear that the viscosity drop became more pronounced as the total volume fraction increased.

Another way to investigate this situation relates to flocculation / aggregation in the system. Various unstable mechanisms that can behave differently in emulsions, ie solidification
(coagulation) / coalescence, creaming / sedimentation, Ostwald ripening and flocculation / aggregation
on). High flocculation in the emulsion resulting from high droplet-droplet interaction has the effect of increasing its viscosity. However, replacing coarse droplets with some fine droplets is thought to have the effect of breaking the flocculation interaction between larger particles. This increases the mobility of the droplets in the emulsion, resulting in a decrease in viscosity. As the disperse phase volume fraction increases, the flocculation becomes stronger (as the disperse phase droplets are closer), and when adding fine droplets, R.P. Pal [Chemical Eng Journal, 67 (1997) 37-44, Viscosity and storage / lo
As explained by ss moduli for mixtures of fine and course emulsions] (Non-Patent Document 5), there is a greater reduction in viscosity.

Both the theories described in this section describe the mechanism by which viscosity reduction occurs. The reality of this situation seems to be a combination of the two, both of which seem to contribute in many ways.

As already described, when modeling a monodisperse suspension of non-deformable sphere droplets, an optimal packing structure (hexagonal grid formation) will be obtained with a maximum packing concentration of 0.74. For bidisperse suspensions, however, the maximum loading concentration and, inevitably, the viscosity will depend on the relative contribution (volume) of the various sized particles mixed together. It will also depend on the shape of the particles and their size distribution.

If agglomeration occurs in the system, this can trap fluid between the solid particles, thus reducing the maximum packing concentration.
In 1968, Farris [Trans. Soc. Rheol. -12.281] (Non-Patent Document 6), in a bimodal suspension where there is a significant size difference between the small particles and the large particles, the small particle suspension is the suspension medium of the large particles. It was proposed to act as. Such a system proposes that a larger maximum packing concentration is possible because small particles can be packed tightly between large particles. Farris proposes numbers for the optimal composition of small and large particles at various loading concentrations between 70% and 86% as shown in Table 1.

From Table 1 it can be seen that the optimum proportion of small particles decreases with increasing packing concentration. Chong et al. [Journal of Applied Polymer Science, 15 (8), 2007; 1971, Rhe
From the results obtained by "ology of concentrated suspensions" (Non-Patent Document 3), it was found that the minimum viscosity generated at a filling concentration of about 40% was 0.55 to 0.65. These findings appear to be consistent with the cited data.

By this system, Tsehnoglou and Yang [Polymer Engineering and Science, Mid-Nov
1990, Volume 30, No. 21, Fluidity and optimum packing in suspensions of mi
xed dissimilar particles] (Non-Patent Document 7), the packing efficiency is greatly improved and the fluidity of the system is increased. This industrial relevance would create a bimodal suspension (or emulsion) containing a high dispersion volume fraction with the same viscosity as a unimodal system. Alternatively, this technology
It could be used to create a bimodal system with the same distributed sediment fraction but with a significantly lower viscosity compared to a unimodal system.

In bimodal suspensions, when shear thickening increases [Wagstaff and Chaffey, Journal-J C
olloid Interface Sci. 59 (1977) 53] (Non-patent Document 8) It was also found that the volume fraction of particles increased. R.Pal (Non-Patent Document 5) shows that when a fine emulsion is added, the shear-thinning action of the coarse emulsion is reduced, which is the two peaks in controlling rheological properties other than viscosity. It shows that the type system is important.

The overwhelming number of experiments associated with bimodal suspensions have shown that colloidal forc
It was related to a system with sufficiently large particles such as e) only. This may be because researchers have tried to simplify the system, or because more industrial use has involved large particles. However, D'Haene and Mewis [Rheological Acta, No. 33
Volume 3, Issue (1994), Rheological characterization of bimodal colloidal dispersi
ons] (Non-Patent Document 9) studied the rheological effects of particle size distribution in colloidal suspensions where more forces are involved. They used particles with a diameter of 129 nm to 823 nm (ie a diameter ratio of 6.38). It has been found that the viscosity is minimized in the same way as suspensions with negligible colloidal forces. As in other studies, this minimum is achieved with 25% by volume of small particles. It has also been found that when the composition of the small particles exceeds 50%, the viscosity is almost independent of the composition.

The minimum viscosity achieved was measured to be almost 200 times smaller than the pure fine fraction.
One thing to note about this particular system is that the layer of dispersant surrounding the particles is more important when the particles are small. In this case, the minimum viscosity is 25
Although appearing in volume%, the effective volume fraction is calculated to be 31.6% when the dispersant layer is taken into account.

Solid spheres can be filled in various ways, but usually simple cubes (φ
_max = 0.524), face centered cube (φ _max = 0.740) and hexagonal close packed (φ _max = 0.740).
A mixture known as random close packing has a maximum packing fraction of 0.639 (average from several publications). This is just a simplified model, but seems to be well related to experimental findings. However, taking into account emulsions, various other factors of droplet deformability and various instability mechanisms (eg, flocculation and aggregation) also become important.

Taking into account the possible close packing of solid spheres, and thus the smallest possible pore size, for example as shown in FIG. 2, the pore size relative to the sphere diameter (D _s ) using a relatively simple shape (pore diameter: D _p ) can be calculated. In this situation, the following equation is obtained to relate the hole diameter to the sphere diameter:

As a result, the critical diameter ratio of a small sphere that exactly fits a small hole made by a large sphere would be 6.49.

In 1997, Greenwood et al. [J. Colloid Interface Sci, 191, 11-21 (1997), The effec
t diameter ratio and volume ratio on the viscosity of bimodal suspens
ions of polymer lattices] (Non-Patent Document 10) focused on determining both the optimal diameter ratio and the optimal ratio of small spheres in a bimodal suspension. Monodispersed suspensions were made with fine and coarse particles and 25, 50 and 75 small particle volume percent bidisperse suspensions. The viscosity of these suspensions was measured at particle size ratios of 1.08, 2.81, 4.03, 5.67, 6.37, 7.83 and 11.15.

After first finding that the minimum relative viscosity usually appears at 25% by volume of small particles (in agreement with most studies to date), these researchers obtained the lowest viscosity at a diameter ratio of 7.83. I found out. The proportions of 4.03, 6.37 and 11.15 also showed a lower viscosity than that of the large particle monodisperse suspension. FIG. 2 shows the viscosity at 25% by volume of small particles [Greenwood et al. Collo
id Interface Sci, 191, 11-21 (1997), The effect diameter ratio and volume
ratio on the viscosity of bimodal suspensions of polymer lattices] (Non-Patent Document 10).

And the focus shifted to each of the effects of individual diameter ratio and small particle contribution on viscosity.
FIG. 3 shows the results at a diameter ratio of 6.37, where the viscosity minimum can be observed with 25% small particles as expected. Neither FIG. 4 (diameter ratio 2.81) nor FIG. 5 (diameter ratio 1.08) show a low viscosity at 25% small particles at any concentration. Perhaps this small particle may not be small enough to fit the gap created by the large particle.

However, a diameter ratio of 1.08 indicates a minimum viscosity with 75% small particles lower than that of large particles alone. There is only a slight decrease, but it occurs at all concentrations tested. Although the original paper does not seem to give a detailed explanation of these results, it may be a notable area in the future as it has been observed at many concentrations.

Although less research was done on bimodal emulsions than on suspensions, Pal performed experiments on such systems [Chemical Eng Journal, 67 (1997) 37-44, Viscosity.
and storage / loss moduli for mixtures of fine and course emulsions] (Non-Patent Document 5). Pal designed an experiment to observe the effect of bimodal emulsions in both O / W and W / O HIPR systems. Pal is from Greenwood et al. [Colloids and Surfaces A: Physioche
m. Eng. Aspects, 144 (1998) 139-147, Minimising the viscosity of concentrate
d dispersions by using bimodal particle size distributions] (Non-Patent Document 4)
Produced a fine (6.5 μm) and coarse (32 μm) O / W emulsion (size ratio 4.92) very similar to
These were mixed at various ratios of total oil volume fractions of 41, 0.63 and 0.78. Emulsions were produced using different speed homogenizers, keeping the shear rate low to produce a coarse emulsion and increasing the shear rate to produce a fine emulsion.

For various proportions of the fine emulsion, the viscosity was measured at each total oil volume fraction. The obtained results are shown in FIG. Pal [Chemical Eng Journal, 67 (1997) 37-44, Viscosi
ty and storage / loss moduli for mixtures of fine and course emulsions]]
(Non-patent document 5).

This result shows that the minimum viscosity appears in 28% by volume fine droplets, and at higher total oil volume fraction this viscosity drop is greater than the lower volume fraction. This result is consistent with previous experimental data for solid particles in a bidisperse suspension. Pal is also aware of the minimum storage / loss modulus for the same composition of fine particles.

Intevep has conducted extensive research on the application of bimodal emulsions in the process of viscous hydrocarbon removal [see, for example, US Pat. No. 5,503,722, “Bimodal emulsion and
its method of preparation ”[02/04/1996]; US Pat. No. 5419852,“ B
imodal emulsion and its method of preparation ”[30/05/1995] (Patent Document 2);
US Patent No. 5603684, “Method for the preparation of viscous hydrocarbon”
in aqueous buffer solution emulsions ”[18/02/1997]; US Pat. No. 69
03138, “Manufacture of stable bimodal emulsions using dynamic mixing”
[07/06/2005] (Patent Document 4); US Pat. No. 5,622,920, “Emulsion of viscous hydrocar
bon in aqueous buffer solution and method for preparing same ”[22/04/19
97] (Patent Document 5); US Pat. No. 5,555,574, “Emulsion of viscous hydrocarbon in
aqueous buffer solution and method for preparing same ”[17/09/1996]; and US Pat. No. 5480583,“ Emulsion of viscous hydrocarbon in aque ”
ous buffer solution and method for preparing same ”[02/01/1996]] (Patent Document 7). The use of conventional emulsions is limited to some extent by the volume of hydrocarbons that can be dispersed in the emulsion and the resulting viscosity. It was possible to increase the total volume to 85% and achieve a viscosity of 1500 cps at 30 ° C.

The long-term stability of emulsions with respect to dehydration and desalting has also been considered. This is because it is an important property when considering the transport of the emulsion. These patents claim that the initial control factor of viscosity is the ratio of small to large droplets.

A crude emulsion was prepared using an ethoxylated alkylphenol emulsifier at a concentration of 3000 mg / l oil, and a fine emulsion was prepared using a concentration of 5000 mg / l oil. Experiments with diameter ratios of 14, 7 and 6 showed that all the viscosities obtained were well below the two component emulsions. The lowest viscosity was obtained with a diameter ratio exceeding 10. This figure is larger than the pre-calculated value of 6.49 for hard spheres and may be due to the high level of droplet deformation that appears at a total volume of 80%. In their experiments, the coarse droplet diameter was 15-30 microns. Emulsions were made by dynamic mixing at 60 ° C., and the mixing speed and duration were varied to form various droplet sizes.

The viscosity of the dispersion is affected by several factors, and the volume fraction of the dispersed phase and the average particle size and dispersion are particularly important. It is known that the viscosity increases as the volume fraction of the dispersed phase increases and as the average particle / droplet size decreases. When trying to disperse a high volume fraction of a very viscous liquid or solid, the industry can be very limited. For the purpose of transport and handling, it is necessary to reduce the viscosity to a level where it can be handled.

It has been discovered that by mixing two separate dispersions having different average particle sizes, a lower viscosity than either component dispersion can be obtained. Hybrid dispersion
dispersion) also allows for very high maximum fill fractions, low shear-thinning or shear-thickening behavior and low storage / loss modulus.

Three main variables have been found to reduce viscosity with hybrid dispersions. Adding fine particles to a larger particle dispersion increases the volume fraction of the dispersed phase by filling the gap created by the larger particles, increasing the maximum filling fraction and increasing fluidity. Viscosity decreases. The mixing ratio of these fine particles to coarse particles is important, and the maximum fluidi
ty) was found to be achieved with 20-30% by volume of small particles. It is also important that the particle size ratio is accurate to increase the fluidity of the dispersion. By studying the particle packing arrangement, assuming that all particles are solid spheres, the diameter of the fine particles can be adjusted to fit any of the gaps created by the lattice of large particles. It was found that it must be one sixth of the diameter. In fact, it is very unlikely that all particles are hard spheres, but experimental evidence suggests that a reduction in maximum viscosity is likely to be achieved with a diameter ratio exceeding 6.49. Emulsion droplets, for example, deform at high dispersed phase concentrations, so the gaps between the droplets are smaller than the model used, and high diameter ratios are required to fill these gaps with fine particles It seems.

Knowledge of hybrid dispersions has already been greatly applied in various industries. Obtaining the advantageous rheological properties of bimodal dispersions of polymers such as latex can be found in paints, adhesives, rubbers,
It has become important in the manufacture of products such as inks, coatings, encapsulants and many others. Two or more mean polymer lengths according to the principles already described
A low viscosity is obtained by dispersing. The coal industry has spent time developing systems to disperse coal particles of various sizes in water in order to form a slurry that can be easily transported as an alternative energy to oil and burned directly. The recovery of various hydrocarbons has been facilitated by dispersing them as a very low viscosity bimodal oil-in-water emulsion to facilitate transport and excellent storage stability.

Other applications include cosmetics such as sunscreens in which the bimodal suspension improves the sun protection factor due to its high film-forming ability. This knowledge is used in many ways in the food industry and has significant utility in many areas of drugs such as drug delivery systems.

The first emulsion, emulsified hydrocarbon fuel, has become very important as a useful fuel for generating steam at power plants and other steam generating facilities to replace coal and petroleum coke However, there are environmental disadvantages and natural gas is relatively expensive. The soaring natural gas is particularly relevant to the oil processing industry, particularly the production of heavy oil and natural bitumen, particularly with the steam assisted gravity drainage technique (SAGD).
Adversely affected. As is well known, SAGD and congener techniques must use a steam generator to inject steam into the underground to move very viscous hydrocarbon material. Traditionally, natural gas has been used to ignite steam generators, which is not economically attractive and has other inherent disadvantages. With the advent of emulsified hydrocarbons, especially those derived from domestic hydrocarbon production and their products, it has been found that this heat content is suitable for combustion in a steam generating environment.

One of the pioneering fuels in this field was Orimulsion, manufactured in Venezuela by Bitor and transported worldwide to supply power plants. Based on success at Olimar John, other emulsified fuels, for example made by Quadrise Ltd., now Quadrise Canada
MSAR ™ (Multi-Phase Superfine Atom, further developed by Fuel Systems, Inc.
ized Residue) has been developed. MSAR ™ is an oil-in-water emulsion, where oil is a hydrocarbon with an API specific gravity of 15 to -10. Typical oil-water ratios range from 65% to 74%. Because of the presence of oil droplets in the water, MSAR ™ is essentially a pre-atomized fuel. This means that, as in conventional fuel oil combustion, the burner atomizer does not perform any mechanical operation to produce oil droplets, but this is an emulsion production device that produces oil droplets. Since pre-atomization literally means “before the atomizer”, the MSAR ™ manufacturing equipment is essentially an atomizer for this process. MSAR (
The typical average droplet size characteristic of TM is about 5 microns, while typical average droplet size characteristics generated during fuel oil atomization in a burner atomizer are 150-200 microns.
Thus, compared to conventional burner atomizers, the huge increase in surface area obtained, for example, by producing much smaller droplets in the MSAR (TM) manufacturing process, despite the presence of significant amounts of water , Much faster and complete combustion. In addition, 150-200 containing 5 micron oil droplets to burn when MSAR ™ passes through a conventional atomizer
Micron water droplets are formed. Thus, water enters the interstitial region between each collection of oil droplets. This interstitial water between the oil droplets will spontaneously evaporate, further disrupting already small (5 micron) droplets. This process is known as secondary atomization. Due to this secondary atomization and the previously described pre-atomization, MSAR ™ has proven to be a particularly efficient fuel, with a carbon burnout rate of 99.9%. Carbon complete combustion is clearly an important aspect of all combustion processes, and because MSAR ™ carbon complete combustion is very high, the amount of ash covered with carbon that accumulates in the combustion section and / or the furnace is substantial. Decrease. As is known, when carbon complete combustion is low, carbon will adhere to the boiler surface with the ash, effectively producing coke; this makes the entire process inefficient and / or inoperable. By providing 99% carbon full burn rate, these problems are successfully avoided.

The very small droplet size used in MSAR (TM) has clear advantages over the combustion process, but the smaller the droplet, the more viscous the MSAR (TM) will be, so for handling and pumping processes It is inconvenient. Therefore, to further promote emulsion fuel technology,
Current research conducted by other companies has developed means that can hold very small droplet sizes while at the same time generally reducing viscosity and providing improvements in storage, handling and transportation. As a result, research has progressed in the direction of bimodal emulsions, that is, emulsions that have two distinct droplet size peaks in their droplet size profile.

Examples of this include, among others, US Pat. No. 5,419,852 issued on May 30, 1995 to Rivas et al. And US Pat. No. 5,503,772 issued on Apr. 2, 1996 to US Pat. No. 5,503,772. There is. In these references, specific blends of emulsions that are produced independently and have different distinct characteristics are used to describe the invention. We conclude that this bimodal emulsion can be made to reduce viscosity and that the final emulsion is characteristically bimodal in its physical properties.

While it is desirable to obtain a bimodal emulsion, this method is not limited. It is known that the larger the average particle size, the lower the viscosity of the mixture. Unfortunately, the larger the particles in the emulsified fuel, the longer the furnace will be required because the oil droplets will burn and the longer it will take to descend the furnace. This also limits the amount of water that can be taken up between the grids. This advantage has already been described herein in the prior and related literature analyses. With respect to the furnace, if it is not long enough for the chosen furnace, the non-burned hydrocarbon material and / or smoke will give adverse results. In this way, current technology is limited by equipment used that can increase cost, complexity and other problems associated with contamination in the overall process.

Given the state of the art, it has been believed that the viscosity directs the entire system to larger oil droplets in the furnace while combustion leads the system to smaller droplets. Therefore, it is desirable to have a formulation that reduces the viscosity but changes the particle size distribution of the fuel emulsion to promote combustion. These latter two characteristics are most desirable to provide a highly efficient high enthalpy emulsified fuel. New approaches have been taken to form emulsions with the above properties as objectives and to give these properties to the emulsion.

Considering the packing of particles in the conventional method, it was found that it is very effective to adopt this method. It has the most desirable properties, ie a broad particle distribution composed of n-peak distributions, but where practically possible, the n-peak distribution as a single peak; For the purpose of producing emulsions, it has not previously been applied to the emulsion field.

A typical example of particle packing literature is the Journal of Computational Physics, 202 (2005), 7
Collected from pages 37 to 764 (Non-Patent Document 11), especially “Neighbor list collision-driven m”
olecular dynamics simulation for non-spherical hard particles. I. Algorith
mic details. A general algorithm for a system of particles having rela
There is a paper titled “tively small aspect ratios with small variations in size.” This paper was approved by Donve et al., “Neighbor list col by the same author.
lision-driven molecular dynamics simulation for non-spherical hard partic
les. II. Applications to ellipses and ellipsoids ”, Journal of Computation
al Physics, 202 (2005), 765-793 (Non-Patent Document 12) was also reviewed. Other common references for particle packing methods include: “Modeling the packing of gr
anular media by dissipative particle dynamics on an SGI Origin 2000, u
sing DL-POLY with MPI ”, Elliott et al. (13);“ Packing and Viscosity
of Concentrated polydisperse Coal-Water Slurries ”, Veytsman et al., Energy an
d Fuels, 1998, 12: 1031-1039 (Non-Patent Document 14); “Is Random Close Packing o
f Spheres Well Defined? ”, Physical Review Letters, March 6, 2000, Torquat
o et al. (Non-Patent Document 15) and “The random packing of heterogeneous propellants”
KNOTT et al. (Non-Patent Document 16).

US Pat. No. 4,725,287 (Patent Document 10), Canadian Occidental Petroleum, Ltd., 19
Published February 16, 1988, the general equation:

{Wherein μ = oil-in-water emulsion viscosity (cs);
μ _o = water continuous phase viscosity (cs);
φ = volume fraction of dispersed oil phase;
φ _p = maximum filling fraction for oil droplet size distribution of emulsion}
Is shown, which relates the viscosity to the maximum packing of a specific particle size distribution.

This equation shows the maximum packing fraction with a larger oil droplet size distribution (maximum packing fractio
In the case of n), it is explained that the viscosity of the oil-in-water emulsion decreases. This reduction can be achieved by forming an oil-in-water emulsion to obtain a wide range of oil droplet sizes or by forming a bimodal oil droplet size distribution. For illustration only, φ
When compared to a monodisperse oil-in-water emulsion with a = 0.5 oil droplet, a bimodal oil-in-water emulsion with an oil droplet size ratio of 5 to 1 is theoretically about 10 minutes, assuming oil particles that are spherical and do not interact Having a viscosity of 1. The greater this maximum fill factor, the lower the viscosity. In general, it is said that a single emulsion having a wide particle size distribution has a low viscosity. Furthermore, it is known that bimodal emulsions have a low viscosity and that not all emulsion mixtures are reduced in viscosity. Despite being a generally useful teaching, this document does not explicitly describe how to exclude “guess” from the selection of which particle size is maximal polydispersity in a unimodal emulsion.

US Pat. No. 5,283,001 (Patent Document 11) (Canadian Occidental Petroleum, Ltd.), 19
Published February 1, 1994, gives a general overview of mixing emulsions. It is shown as follows:
... Bimodal or multimodal (one or more) water-phase oil-in-water emulsions (one or more) in any suitable dynamic shearer and mixer (such as a rotor-stator mixer) ) Varying the residence time and / or shear rate of the mixture of the emulsified composition and the resulting crude hydrocarbon at various residence times and / or shear rates in any suitable tank or vessel, such as the emulsion tank 122 It can be formed using the emulsifier (s) of the present invention by collecting the spilling oil-in-water emulsion (s) resulting from the dynamic shear and mixer. The recovered effluent oil-in-water emulsion (s) produced at various residence times and / or shear rates in any suitable dynamic shearer and mixer is mixed in emulsion tank 122, From one dynamic shearer and mixer with fixed shear rate and / or residence time of the crude hydrocarbon and emulsifier (s) produced in the dynamic shearer and mixer; or one flow (and Bimodal or multimodal oil-in-water type with low viscosity of oil-in-water emulsion (s) produced from static shear and mixing device 108 with (shear) rate Form an emulsion. Thus, by way of example only, a mixture of the emulsified composition (s) and the resulting crude hydrocarbon is placed in a dynamic shearer and mixer with a shear field strength of 500 / sec for 4 seconds. The resulting mixture (one or more) of the water phase oil-in-water emulsion was blended in the same dynamic shearer and mixer having a shear field strength of 6,000 / sec and placed in the same mixture for 4 seconds (single or multiple). The viscosity of the bimodal water-in-oil emulsion (one or more) obtained by mixing with the oil-in-water emulsion in (5) was produced at a strength of 500 / sec or 6,000 / sec (single or It will be lower than the viscosity of each of the water phase oil-in-water emulsions. Similar results can be obtained by varying the residence time while the shear field strength is usually constant or fixed. (End of quotation)
It is recognized that the viscosity decreases when mixing (two or more) emulsions. The final emulsion can be multimodal or bimodal.

This technique is useful as a guide in considering generally bimodal or multimodal emulsions, but is not related to unimodal emulsions. This patent gives an example at column 88, line 48 (see below):
Example XIX:
This example is provided to demonstrate that the bimodal oil-in-water emulsion (s) has improved viscosity. The crude material was Manatokan. The aqueous phase was water. Surfactants are 714.3ppm NP40 (NP40 is 714.3ppm of Manatokan) and 714.3ppm NP100 (NP100
Was a mixture with Manatokan 714.3ppm). The emulsified composition was produced by mixing water and a surfactant. Two types of oil-in-water emulsions were prepared by mixing a known amount (one or more) of an emulsified composition with a known amount of Manatokan and stirring for 40 seconds in a rotor-stator mixer with a mixer energy of 3000 rpm. . The first (single or plural) oil-in-water emulsion had an average oil droplet size (μ) of 69.9, a dispersibility of 3.27, and a viscosity (cp) of 221. The second emulsion, a small amount of Manatokan, had an average oil droplet size of 54.9, a dispersibility of about 3.56, and a viscosity (cp) of about 198. When mixed with 1 liter of the first emulsion and 1 liter of the second emulsion, the average oil droplet size is about 61
A third oil-in-water emulsion of .7, dispersibility of about 3.88 and viscosity (cp) of about 140 was obtained. Thus, a bimodal emulsion has a lower viscosity than any of its emulsion components. (
(End of quotation)
An example is given of mixing two types of emulsions in a 50/50 ratio. This result explains that the final emulsion has a lower viscosity than the two types of precursor emulsions. However, different ratios would have resulted in significantly different viscosities higher than one of the two precursor emulsions. In addition, from column 110, line 29, it is shown that:
Emulsion viscosity
All asphalt emulsions made with 30 percent water are usually 13 at 120 ° F.
It falls within a relatively narrow range of 0 to 150 cp. The change with temperature was much less sensitive than the oil or heavy coarse emulsion as shown in FIG. Like other WCEs,
When the water content was reduced, the viscosity increased. For example, an experiment with 25% water BEPU-21 had a viscosity of 309 cp. (End of quotation)
The fact that the emulsion viscosity increases with hydrocarbon content is shown as an example; however, it does not suggest any hybrid emulsions with low viscosity.

In view of conventional techniques in the emulsion industry, there is still a need for an emulsion that facilitates changing the particle size distribution of the fuel emulsion to reduce viscosity, but that burns well and does not degrade carbon complete combustion. . The techniques herein provide for emulsion combustion optimization.

It has been found that by applying a filling model from a solid fuel to the present technology, the viscosity of the emulsion decreases as the particle size distribution becomes wider.
The present invention is that the final emulsion is a substantially hybrid emulsion of at least two precursor emulsions, which is in contrast to a unimodal distribution, i.e. a bimodal distribution as exemplified in the prior art. The most desirable properties of fuel emulsions that give a single peak emulsion have been summarized. As used herein, unimodal refers to the majority peak with a shoulder potentially associated but no separation peak. It can also be defined as having a single volumetric mode in which the volumetric probability of the particle monotonically decreases on both sides of the mode and no other local maximum exists. it can.

The present invention provides a particularly efficient hybrid fuel emulsion and methodology for synthesizing fuels, regardless of the properties of the precursor emulsion, while successfully integrating unrelated technologies and well controlling polydispersity. Obtained.

US Pat. No. 5,503,722, “Bimodal emulsion and its method of preparation” [02/04/1996] US Pat. No. 5419852, “Bimodal emulsion and its method of preparation” [30/05/1995] US Patent No. 5603684, “Method for the preparation of viscous hydrocarbon in aqueous buffer solution emulsions” [18/02/1997] US Patent No. 6903138, “Manufacture of stable bimodal emulsions using dynamic mixing” [07/06/2005] US Pat. No. 5622920, “Emulsion of viscous hydrocarbon in aqueous buffer solution and method for preparing same” [22/04/1997] US Pat. No. 5,555,574, “Emulsion of viscous hydrocarbon in aqueous buffer solution and method for preparing same” [17/09/1996] US Pat. No. 5480583, “Emulsion of viscous hydrocarbon in aqueous buffer solution and method for preparing same” [02/01/1996] Rivas et al., US Pat. No. 5,419,852, issued May 30, 1995 Rivas et al., US Pat. No. 5,503,772, issued April 2, 1996 US Pat. No. 4,725,287, Canadian Occidental Petroleum, Ltd., issued February 16, 1998 US Patent 5,283,001 (Canadian Occidental Petroleum, Ltd.), issued February 1, 1994

R. Pal et al. [Emulsions in the Petroleum Industry Journal, Chapter 4, Rheology of emulsions] R. Pal et al. [Colloids and Surfaces A: Physiochem. Eng. Aspects, 137, (1998), 275-286, A novel method to correlate emulsion viscosity data] Chong et al. [Journal of Applied Polymer Science, 15 (8), 2007; 1971, Rheology of concentrated suspensions] Greenwood et al. [Colloids and Surfaces A: Physiochem. Eng. Aspects, 144 (1998) 139-147, Minimising the viscosity of concentrated dispersions by using bimodal particle size distributions] R. Pal [Chemical Eng Journal, 67 (1997) 37-44, Viscosity and storage / loss moduli for combination of fine and course emulsions] Farris [Trans. Soc. Rheol. -12.281, 1968] Tsehnoglou and Yang [Polymer Engineering and Science, Mid-Nov 1990, Vol. 30, No. 21, Fluidity and optimum packing in suspensions of mixed dissimilar particles] Wagstaff and Chaffey [Journal-J Colloid Interface Sci, 59 (1977) 53] D’ Haene and Mewis [Rheological Acta, Vol.33, No.3 (1994), Rheological characterization of bimodal colloidal dispersions] Greenwood et al. [J. Colloid Interface Sci, 191, 11-21 (1997), The effect diameter ratio and volume ratio on the viscosity of bimodal suspensions of polymer lattices] the Journal of Computational Physics, 202 (2005), 737-764 Donev et al., Journal of Computational Physics, 202 (2005), 765-793, “Neighbor list collision-driven molecular dynamics simulation for non-spherical hard particles. II. Applications to ellipses and ellipsoids” Elliott et al., “Modeling the packing of granular media by dissipative particle dynamics on an SGI Origin, using DL-POLY with MPI” Veytsman et al., “Packing and Viscosity of Concentrated polydisperse Coal-Water Slurries” Energy and Fuels, 1998, Vol. 12, 1031-1039. Torquato et al., “Is Random Close Packing of Spheres Well Defined?”, Physical Review Letters, March 6, 2000. KNOTT et al. “The random packing of heterogeneous propellants”

  The technology of the present invention has industrial applicability in the field of emulsion synthesis.

One aspect of the present invention is to provide a substantially improved atomized fuel emulsion, which has highly desirable combustion characteristics, calorific value, and conventional methods. The fuel emulsion is provided that can be custom designed for combustion in any furnace or combustion arrangement that is significantly different from.

In accordance with a further aspect of one embodiment of the present invention, a blend of multiple hydrocarbon emulsions in water.
The composite emulsion has a unimodal hydrocarbon particle distribution, and the hydrocarbon is present in an amount of 64% to 90% by volume.

As already described with respect to the prior art in this specification, the high oil content in oil-in-water emulsions is already that the emulsions formed by conventional methods are not unimodal; multiple maxima exist on both sides of the mode That was recognized. By using this technique, not only can the hydrocarbon content be very high, but the overall system viscosity can be reduced relative to the individual viscosity of the precursor emulsion forming the hybrid, The complete burn rate is particularly attractive beyond 99.99% effectiveness.

A review of US Pat. No. 5,419,852 (Invetep, SA), issued May 30, 1995, discusses a stable, low-viscosity bimodal viscous hydrocarbon emulsion in water. This text indicates that the emulsion has a low viscosity and has excellent aging properties. He also teaches how to synthesize this emulsion. The invention further describes a process for making such bimodal viscous hydrocarbon emulsions in water. The patent addresses a bimodal emulsion and a specific mixing ratio of specific proportions and average particle sizes of the two precursor emulsions.

This disclosure does not provide details on the following:
i) Unimodal hybrid emulsion;
ii) using various hydrocarbons for the precursor emulsion;
iii) lack of specific requirements for specific average particle size ratios;
iv) lack of specific requirements for specific mixing ratios; and
v) A methodology for finding the optimal mixing ratio and optimal average particle size ratio using a predictive model.

An important advance in the technology of the present invention is the construction of a method for forming a hybrid emulsion where the polydispersity can be controlled much better than when we look at a single precursor emulsion. There are too many ways to produce polydisperse emulsions that are ineffective or very difficult to control. The method of the present invention teaches how to make a hybrid emulsion using any precursor emulsion. This is in stark contrast to the above reference which teaches how to make a hybrid emulsion from two very specific precursor emulsions.

Further, US patent application Ser. No. 10 / 162,042 (Gurfinkel Castillo, Mariano E. et al.) Describes another type of emulsion formation method. In the text of this application:
[0043] The second portion 62 is mixed with the hydrocarbon 70 in the mixer of the module 54 to form a second emulsion 72 having a small average droplet size. Then emulsion 6
8 and 72 are mixed in module 56 to form the desired final emulsion. In this regard, an additional amount of water 74 is conveniently added to the system, for example, by adding it to a small droplet size emulsion 72, resulting in a final bimodal having a desired amount of moisture, eg, about 29% or more. Mold emulsion can be provided and / or further water can be added downstream of the emulsion mixing process ...
[0052] Returning to FIG. 11, a bimodal emulsion can be conveniently formed by first producing a plurality of unimodal emulsions and then mixing the emulsions according to the process described above. FIG. 11 shows two different unimodal emulsions with respect to droplet size distribution and also shows the droplet size distribution of a bimodal or final emulsion product made from two unimodal emulsions. This final product is stable and has the desired properties. (End of quotation)
While the above paragraph describes the advantages of mixing multiple precursor emulsions,
There is no explanation on how to get it. This requires readers to infer or experiment with mixing ratios, emulsion types, etc. Furthermore, no mention is made of the advantages of mixing emulsions.

The precursor emulsion can include the same hydrocarbon material or different hydrocarbon materials, depending on the specific application of the emulsion. Furthermore, the particle size distribution and the droplet size may be the same or different. If the size distribution is the same, the hydrocarbon material may be different for each emulsion. As another possibility, the hybrid emulsion may be a hybrid emulsion in which a hydrocarbon is mixed in a water emulsion. As above, the hydrocarbon and hybrid emulsion in water may have the same or different hydrocarbon material, the same or different droplet size and / or the same or different particle size distribution.

In accordance with a further aspect of one embodiment of the present invention, there is provided a process for making a hybrid emulsion made from a variety of hydrocarbon materials having very different viscosities and thus very different emulsion making temperatures. Thus, when mixed with a precursor emulsion produced at a higher temperature, a precursor emulsion produced at a lower temperature can be used as a coolant. This eliminates or reduces the need to use heat exchange to reduce the temperature of emulsions produced above 100 ° C. to below 100 ° C. prior to storage.

In accordance with a further aspect of one embodiment of the present invention, a method of blending a hybrid emulsion having a low viscosity unimodal particle distribution relative to a precursor emulsion used to form the hybrid emulsion, comprising:
Prepare a system with n-peak particle distribution;
Forming a precursor emulsion of each n-peak distribution present in the system, wherein each said precursor emulsion has a characteristic viscosity; and a unimodal size distribution and each said precursor emulsion The method is provided comprising the steps of mixing a precursor emulsion to form the hybrid emulsion having a low viscosity relative to:

As already briefly discussed, it has been discovered that by using a hybrid emulsion, the hybrid emulsion has a viscosity that is easy to transport despite the high content of hydrocarbon material present in the emulsion. It was. This essentially provides a wider range of particle sizes,
This is probably due to the single particle size distribution. This in turn provides an advantage for the viscosity of the mixture.

In yet another aspect of one embodiment of the present invention, a source of hydrocarbon material is provided; producing a plurality of emulsions of said hydrocarbon material, each emulsion having a characteristic viscosity, each emulsion having a different particle size Having a diameter distribution; mixing the emulsions in a predetermined ratio to form a hybrid emulsion having a low viscosity relative to the emulsions; and mobilizing the hybrid emulsion, each step comprising a viscous A method for transporting various hydrocarbon materials is provided.

In yet another aspect of one embodiment of the present invention, a hydrocarbon emulsion is provided having a sufficiently high internal phase volume so that the droplets in the emulsion are non-spherical; Convert to a ridge emulsion system; form at least two precursor emulsions from this system; mix precursor emulsions at a predetermined rate to reduce viscosity; and synthesize hybrid emulsions with low viscosity from precursor emulsions A method for maximizing the viscous hydrocarbon content of an aqueous system for storage or transport, including each stage.

A further aspect of one embodiment of the present invention provides a system having an n-peak particle size distribution; forms a precursor emulsion for each unimodal distribution present in the system; each precursor emulsion Has a characteristic viscosity; for each precursor emulsion forms a plurality of mixed emulsions each having a low viscosity and a unimodal size distribution; and the mixed emulsion is mixed to a viscosity of the mixed emulsion A method for producing a hybrid emulsion with a unimodal particle distribution with low viscosity relative to the precursor emulsion, including each step, forming an amalgamated mixed emulsion with a low viscosity and a unimodal particle distribution It is.

In accordance with another beneficial aspect of one embodiment of the present invention, it has been found that HIPR (High Internal Phase Ratio) emulsions with very high hydrocarbon content can be efficiently transported. By using high internal phase ratio emulsions, these emulsions are at least bimodal or depending on the number of particle size distributions in the HIPR emulsion according to the method described above.
It has been found that an n-peak emulsion system can be converted and these individual bimodal emulsions can be formed into precursor emulsions and mixed to form a hybrid emulsion. In this case, the non-spherical or substantially non-spherical particles in water are reconstituted or converted into discrete types for individual emulsion synthesis, and subsequently for the synthesis of hybrid emulsions that can be transported more conveniently. Can be mixed. Particularly useful in that high hydrocarbon content materials can be moved without operating on conventional expensive equipment resulting from conventional processes such as preheating, addition of diluents or other viscosity reducing agents. is there. This material can be easily converted to a hybrid emulsion, and once converted essentially has the advantageous transport properties of a hybrid emulsion as previously described herein.

A method of modifying at least one of the combustion, storage and transport properties of an emulsion during pre-formation, during and after formation, comprising preparing the emulsion; Treating each step with an apparatus selected from the group consisting of additive addition, mechanical treatment, chemical treatment, physical treatment and combinations thereof; and modifying at least one characteristic of the emulsion by treatment; Including methods.

While the limitations in the emulsion formation industry have been discussed, the present invention, in many aspects, makes very complex conditions very simple with the current technology and allows an infinite range of designs. The particle size varies greatly for each polydisperse system. These particle sizes could theoretically be mixed in any proportions to give a myriad of hybrid emulsions, each with various polydispersities, droplet sizes and dynamic stability. In the present specification, it has already been stated that the conventional method has tried to teach a specific method for producing an emulsion. Given that any number of emulsions can be made with any number of precursor emulsions as described above, the challenge of pre-determining the final result of a hybrid emulsion is that it requires a great deal of experimental time and associated cost. It's a ridiculous job that not only costs money, but is essentially unrealistic for design chemists.

The method disclosed herein can improve the dynamic stability of any emulsion, ie, the dynamic stability of an existing hybrid emulsion. In addition, the process can reconstruct existing hybrid emulsions to improve or change physical and chemical characteristics.
This is very convenient. This is because potentially ineffective emulsions can be made essentially effective for subsequent use. As will be appreciated, this is very advantageous for in situ or on-site fuel modification, and a power generation station to utilize many different types of fuel. ) And so on.
Once a given set of fuel parameters can be achieved, this parameter can be modified to suit the combustion conditions in various environments.

In addition, off-specific materials such as fuel and precursor materials for pharmaceutical and food production
on materials) can be modified to be acceptable herein for subsequent use. This presents significant cost savings for materials that may be discarded due to their lack of utility.

Having generally described the invention, reference can be made to the accompanying drawings which illustrate preferred embodiments.
Note that like features are identified by like reference numerals throughout the accompanying drawings.

FIG. 1 shows the results obtained by Greenwood et al., Which is a plot of viscosity measurements in various small particle volumes and total volumes (from Greenwood et al.) [Colloids and Surfaces A: Physiochem. Eng. Aspects, 144 (1998) 139-147, Minimising the viscosity of concentrated dispersions by using bimodal particle size distributions]. FIG. 2 is a plot of the effect of diameter ratio on suspension viscosity (Greenwood et al. [J. Colloid Interface Sci, 191, 11-21 (1997), The effect diameter ratio and volume ratio on the viscosity of bimodal suspensions of polymer lattices]). FIG. 3 shows the effect of concentration and mixing ratio on suspension viscosity at a diameter ratio of 6.37. FIG. 4 shows the effect of concentration and mixing ratio on suspension viscosity at a diameter ratio of 2.81. FIG. 5 shows the effect of concentration and mixing ratio on suspension viscosity at a diameter ratio of 1.08. FIG. 6 plots the composition (small particle volume) in relative viscosity of a bimodal suspension at a diameter ratio of 6.37. The total volume fraction is shown as 0.40, 0.45, 0.50, 0.55 and 0.60. FIG. 7 plots the effect of composition (small particle volume) on the relative viscosity of a bimodal suspension at a diameter ratio of 2.81. The total volume fractions shown are 0.40, 0.45, 0.50, 0.55 and 0.60. FIG. 8 plots the composition of the relative viscosity composition (small particle volume) of the bimodal suspension at a diameter ratio of 1.08. The total volume fractions shown are 0.40, 0.45, 0.50, 0.55 and 0.60. FIG. 9 plots viscosity as a function of total oil volume fraction. FIG. 10 is a schematic diagram of the total synthesis mechanism of the present technique. FIG. 10A is a schematic representation of a variation of the total synthesis mechanism of the present technology. FIG. 6 is a diagram of particle size as a function of shear. 12A and 12B are diagrams of viscosity as a function of droplet size ratio. FIG. 13 is a diagram of the proportion of oil in the emulsion as a function of the furnace length. FIG. 14 is a diagram of a mixed emulsion of suspension and two precursors in 70% NE Alberta bitumen with median particle size of 5 μm and 24 μm. FIG. 15 is a diagram of mixed emulsion viscosity for various proportions of the same median particle size. FIG. 15A is a diagram of mixed emulsion viscosity for various proportions of the same median particle size. FIG. 15B is a diagram of hybrid emulsion viscosity for various proportions of the same median particle size. FIG. 15C is a diagram of mixed emulsion viscosity for various proportions of the same median particle size. FIG. 15D is a diagram of hybrid emulsion viscosity for various proportions of the same median particle size. FIG. 16 is a diagram of two type distributions of North Eastern Alberta bitumen particles of two particle sizes (5 microns and 10 microns). FIG. 17 is a plot of viscosity as a function of 5 micron MSAR ™ used in the precursor emulsion and the percentage of 10 micron MSAR ™ used in the second precursor emulsion. Figures 18A through 18C show the particle sizes of the hybrid emulsions formed from the respective emulsions of 5 microns and 10 microns for the proportions of 5 microns and 10 microns of 20% and 80%, 50% and 50%, 80% and 20%, respectively. Show the distribution. FIG. 19 shows the respective distributions of 6 micron and 12 micron modes, all of which precursor emulsions are formed using a 70% refined residue content and surfactant. FIG. 20 shows the viscosity as a function of the MSAR ™ mixture composed of 5 microns in the first emulsion and 12 microns in the second emulsion. FIGS. 20A-20C show the particle distribution results in 6 micron and 12 micron mixed emulsions with the following proportions of 20% and 80%, 50% and 50%, 80% and 20%, respectively. FIG. 21 is a graph of a precursor where emulsion number 1 includes a median particle size distribution of 6 microns and the emulsion has a median particle size distribution of 16 microns. FIG. 22 is a graphical representation of the viscosity of an MSAR ™ mixture composed of 6 micron and 16 micron 80/100 asphalt MSAR ™. 22A-22C show various proportions of 6 micron and 16 micron particles, ie 20% and 80%, 80% and 20%, 50% and 50%, respectively. FIG. 23 is a front view of the burner of the figure where North Eastern Alberta Bitumen MSAR ™ fuel number 1 is burning. FIG. 24 is a side view of the flame shown in FIG. FIG. 25 shows coke deposits on the nozzle after combustion of the fuel burning in FIGS. FIG. 26 is a view similar to FIG. 28 after the second combustion experiment of MSAR ™ fuel 1. FIG. 27 is a diagram of combustion from a burner of North Eastern Alberta Bitumen MSAR ™ Fuel 2. FIG. 28 is a photograph of the nozzle after fuel of MSAR ™ fuel 2 showing coke deposits. FIG. 29 shows a flame resulting from combustion of Northeastern Alberta Bitumen NSAR ™ hybrid fuel between MSAR ™ fuel 1 and MSAR ™ fuel 2. FIG. 30 is a side view of the flame of FIG. FIG. 31 is an illustration of a burner nozzle showing minimal coke deposition on the nozzle.

Referring to FIG. 10, a total synthesis mechanism, indicated generally by the numeral 10, is shown. This synthesis mechanism involves two major steps, indicated by numerals 12 and 14. In stage 12, the hydrocarbon material 16 is mixed with water 20 containing a surfactant 18 and the material is mixed in a mixing device 22 as a mixture.

The hydrocarbon material can include fuels of any hydrocarbon material, non-limiting examples of which include natural gas, bitumen, fuel oil, heavy oil, residue, emulsified fuel, multiphase ultrafine (superfi
ne) atomized residues (MSAR ™), asphaltenes, petroleum coke, coal and combinations thereof. It is desirable to use a hydrocarbon material of less than 18 API. Using an emulsion stabilizer (a chemical composition that prevents premature phase separation of the emulsion)
Stabilize phase separation. Surfactants are useful for this as well as other components of the stabilizer type.

In the term surfactant, it is known in the art that the surfactant may be nonionic, zwitterionic, cationic or anionic or a mixture thereof. Further, it may be in a liquid, solid or gas state. It is within the scope of the present invention to use a combination of materials to achieve a properly dispersed system that usually results from an emulsion.

The mixer can include any suitable mixer known to those skilled in the art. A suitable amount of emulsion stabilizer or surfactant comprises 0.01% to 5.0% by weight of the emulsion,
The hydrocarbon comprises any amount up to 90% by weight. In an embodiment, a colloid mill
al mill). When the material is subjected to a colloid mill, a first precursor emulsion 24 is formed. A similar step yields a second precursor emulsion 24 ', and common steps with the production of emulsion 1 are represented by numbers similar to the main symbols.

Once the precursor emulsion 24 and the second precursor emulsion 24 'have been formed, the two emulsions are introduced into the mixing device 26, which can be a colloid mill or a further selected device such as an inline static mixer. Similar shearing devices can be included.

In individual emulsions 24 and 24 ', one of the emulsions has a smaller average particle size compared to the second emulsion. These are then mixed together in a predetermined ratio to form a hybrid emulsion 28, which is a polydisperse fuel emulsion. This predetermined ratio is determined using a particle packing algorithm as described in the prior art discussion. The desired final properties in the hybrid determine the initial mix-in ratio. Thus, a precursor emulsion of any composition can be used to formulate or design any emulsion. This gives a very big achievement. As already mentioned, previous attempts in the art have failed to provide a “designer approach” for emulsion formulation. As already described, considerable experimentation and speculation was required when certain parameters and properties were desired in the final hybrid emulsion. This obviously requires a significant amount of time with potentially undesirable results. This result is easily achieved by the technology of the present invention. The final parameters of the hybrid are determined and entered into the algorithm,
The best possible results are then analyzed in terms of polydispersity, viscosity and maximum fill fraction relative to the ideal result of the final blend. It is clear that this can be used ubiquitously in all fields. One of the more preferred application areas is, as already mentioned, the boiler (steam generator)
It is a high-temperature furnace for use in, etc. Depending on the plant configuration, different sized furnaces may be required within the same plant. For this reason, many different furnaces are required to optimize combustion, depending on the length of the furnace, among other characteristics, which presents a great number of challenges for engineers. There is no doubt that several different fuels must be stored or retained when modifying one formulation in the field.

Returning to the algorithm, this computer model has already been applied to solid-based rocket fuels, and it is well known that using this algorithm in the synthesis of hybrid emulsions has been very successful. One particularly attractive achievement is that this hybrid emulsion is less than the viscosity of the precursor emulsion and is 3-5 times lower than the viscosity of the precursor emulsion containing small droplets. A further advantage arising from the integration of irrelevant technologies is that lower preheating temperatures are required for hybrid emulsions as opposed to the preheating temperatures required for previous or precursor emulsions.

Conveniently, the hybrid emulsion has very good dynamic and static stability and handling (all in-between manufacture and burner tips, eg storage, valves, pipes, tanks, etc.) It has also been found to have properties, initial storage and transportability. In combustion experiments, hybrid emulsions have a carbon burnout greater than 99.9%, even though this emulsion contained a high proportion of hydrocarbons in water.
).

Returning to FIG. 10A, a variation of the overall arrangement shown in FIG. 10 is shown. In this aspect, the process can be modified in various stages to carry out the transport, storage and / or combustion of the individual components of the emulsion or hybrid emulsion itself. In this way, FIG. 10A is modified at the pre-synthetic mixing point before the surfactant and water enter the mill 22 as shown by the numeral 30 or before being introduced into the mill as another option. Provides at least one variation of the above embodiment. This stage is indicated by numeral 32. As another possibility, the emulsion can be modified at the time of manufacture indicated by numeral 34 or 36 after formation. For numbers similar to the initial display, these steps apply to emulsion number 2, indicated by the number 24 '. As a further possibility,
Once the first emulsion 24 and the second emulsion 24 'are introduced, these are the numbers 3
8 can be modified or subsequently modified once the hybrid emulsion 28 is formed. This stage is indicated by the numeral 40.

Due to variations in this process as illustrated by FIG. 10A, the emulsion can be modified with respect to combustion, storage and / or transport properties during at least one of pre-formation, formation and post-formation, wherein Modification is at least additive addition, mechanical treatment,
Includes operations selected from chemical and physical processes, and combinations thereof. The addition of the additive will be described later.

Referring to FIG. 11, the particle size is illustrated as a function of shear. This allows the selection of various particle size distributions of the emulsion by changing the amount of shear used to produce the particles of the emulsion. As shown in FIG. 11, the amount of shear is related to the particle size and distribution width. The minimum droplet size is related to the parameters used to produce the emulsion. The amount of shear is increased by increasing the residence time in the mixing device or by increasing the speed at which the rotatable mixing device rotates.

For stabilization purposes, it has been found that it is advantageous to maintain the surfactant concentration relative to oil content substantially similar to the precursor emulsion. This is merely exemplary, and variations in surfactant concentration can vary depending on the desired final properties of the composite emulsion. In situations where different surfactants are used in different complex emulsions, of course, the surfactants are compatible. This example has already been discussed and other examples will be apparent to those skilled in the art.

Referring to FIGS. 12A and 12B, a graphical representation of viscosity as a function of the ratio of small to large droplets, with large droplets represented on the left side of the graph.
Referring now to FIG. 13, the oil content in the emulsion as a function of furnace length required to completely burn the fuel.

Referring to FIG. 14, a bimodal premixed particle distribution is shown, where the number 1 is 7
An emulsion containing surfactant with 0% North Eastern Alberta bitumen is shown, with the balance containing water. The first distribution was formulated using a high shear mixer at a high rotational speed. The median particle size for this distribution was 5 microns, whereas for distribution 2, the median particle size was 24 microns. In the premix, it is clear that each emulsion has a distinct mean and median droplet size.

FIG. 15 plots the composition (small particles, volume) in relative viscosity of a bimodal suspension at a diameter ratio of 6.37. The overall integration rates shown are 0.40, 045, 0.50, 0.55 and 0.60.
FIG. 15 shows the 5 micron MSAR ™ emulsion used in the mixture and 24 micron MS.
A graphical representation of the viscosity as a function of the proportion of AR ™. Inset 15A is shown in FIG.
FIG. 15B is a distribution representation of a 20% 5 micron and 80% 24 micron mixture with the characteristic viscosity indicated by the arrows in the graph of FIG. FIG. 15 is an inset containing a 24 micron particle size, with the arrows in FIG. 15 pointing to the characteristic viscosity. The final inset 15C shows a 50/50 blend of 24 micron and 5 micron particles, the viscosity characteristics being represented by arrows. Reviewing FIGS. 15A-15C,
It is clear that the particle distribution representation is effectively unimodal, despite including two separate emulsions with distinctly different mean and median droplet sizes independently.

Referring to FIG. 15D, a triangular diagram of three fractionation systems of 1 micron particle, 5 micron particle and 10 micron particle is shown. As is generally known, these plots are effective in showing the fill fraction. This data can be interpreted to determine which combination of particles can produce the most possible packing fraction. The triangle shown is 67
This is a representative example of mixing different types of particles. Various shadings indicate various filling fractions ranging from 0.62 to 0.76. As is apparent from the figure, in order to determine the best possible filling fraction,
Using the algorithm in this scenario is the best packing fraction
Is important to avoid the guesswork involved in determining. It will be apparent to those skilled in the art that it is almost impossible to attempt to predict what is shown in FIG. 6D. Even with the packing fraction shown, there is considerable variation in the particle fraction ratio, for example between 0.74 and 0.76. Thus, using the algorithm not only quickly processes the composition details of the best fill fraction, but also allows the designer to use various combinations within the region of the diagram that is common to a particular fill fraction.

As a further representative example, FIG. 16 provides the North Eastern Alberta bitumen particle distribution, where there is considerable overlap between the two modes of distribution in terms of median particle size. In this figure, using the same material as in the previous discussion, the 5 micron median particle distribution is represented by the number 1 generated at a relatively high speed, and the peak 2 is the slower produced 10 micron medial particle distribution. including. This is an example and was selected based on final requirements
Can be carried out in a low speed or high intensity mixer at rpm.

FIG. 17 shows the viscosity as a function of the 5 micron MSAR ™ ratio used in the precursor emulsion and the 10 micron MSAR ™ ratio used in the second precursor emulsion. Insets 18A, 18B, and 18C show 20% and 8% for 5 and 10 microns, respectively.
The particle distribution of a hybrid emulsion formed from 0%, 50% and 50%, 80% and 20% individual emulsions is shown. The respective arrows in the insets 18A-18C indicate the insets 18A, 18B and 18C.
Is a representation of the viscosity of each individual final hybrid mixture.

In FIG. 19, additional hydrocarbon material was used in the synthesis of the hybrid emulsion. FIG.
9 shows the respective distribution for the 6 micron and 12 micron modes, where both precursor emulsions were formed using a suitable surfactant, a 70% content refining tank 9 and the balance water. . About 10% of the refinery tank residue is light oil and 90% is a viscous hydrocarbon material. The 6 micron distribution was generated at a relatively high speed, while 12 microns was generated at a low speed.

FIG. 20 shows the viscosity as a function of a MSAR ™ mixture composed of 5 microns of the first emulsion and 12 microns of the second emulsion. FIGS. 20A-20C show the particle distribution results of the hybrid emulsion for 6 micron and 12 micron particles at the following proportions: 20% and 80%, 50% and 50%, 80% and 20%, respectively.

As is apparent from the inset, each has the characteristic viscosity shown in the graphical representation of FIG. Further, similar to the examples described above, in all cases the hybrid emulsion is virtually unimodal, thus providing a broad particle size distribution.

FIG. 21 lists the characteristics of the precursor emulsion, where emulsion number 1 contains a median particle size distribution of 6 microns and emulsion 2 contains a median particle size distribution of 16 microns. In this example, the surfactant was used as a surfactant with a hydrocarbon material containing 70% 80/100 asphalt, with the balance being water. This 6 micron distribution was compounded using a mill at a relatively high speed, and the 16 micron distribution was synthesized at a low speed.

Data similar to the example already shown is shown in FIG. 22, where the viscosity is shown.
Insets 22A-22C show specific hybrid emulsion formulations with 6 micron and 16 micron distributions in the following amounts: 20% and 80%, 80% and 20%, 50% and 50%, respectively.

Again, the hybrid emulsion has a characteristic viscosity in each of the insets 22A-22C.
A unimodal particle distribution is shown.
From this result, it is clear that the method of the present invention can conveniently formulate a unimodal hybrid fuel emulsion from individual precursor emulsions. It is known that the oil content or hydrocarbon content in conventional oil-in-water emulsions is usually limited to about 70%. Because,
This is because when the content increases beyond this point, the viscosity of the emulsion increases exponentially. This is clearly contrary to the desired properties achieved with the method of the present invention. By using the protocol described herein, the oil content is compared to conventional or HIPR emulsification,
The oil content can be increased up to 90% while maintaining a relatively low viscosity. The multiple polydispersed fuel emuls already described herein
The filling of the droplets during sion) is considered to be considerably better than a normal emulsion that does not exhibit a unimodal dispersion.

Many very useful features resulting from the use of this method not only produce excellent emulsified fuels with higher carbon burn rates than the respective emulsions in the hybrid, but also require a moisture requirement for transport ( The water requirement can be lowered.

Although briefly mentioned, one of the main advantages of the method of the present invention is that HIPR emulsions that are characteristically composed of aspherical particles, usually polyhedral, are converted into their respective emulsions, followed by mixing To form a hybrid emulsion with the advantages produced by the process of the present invention. In this regard, the HIPR emulsion can be converted to provide the desired properties of a hybrid emulsion in that it has a low viscosity, improved flammability, and a broader particle distribution. It is known that HIPR emulsions have very high viscosity and are very shear-thinning. It has not previously been proposed to convert HIPR emulsions into a combination of individual emulsions as disclosed herein to provide low viscosity with excellent flammability. The use of HIPR emulsions that can have a carbon complete burn rate of 99.9% has not previously been recognized.

For convenience of use, the emulsion technology described herein allows the emulsion to be individually tailored to the furnace and combustion arrangement as opposed to having to specifically design the furnace to burn the emulsion. Can be designed. The cost savings in this respect are substantial and it is clear that emulsion modification is much easier than designing and building new expensive equipment.

Furthermore, depending on the economy and requirements of the hybrid emulsion, the number of precursor emulsions is not limited and is within the scope of the present technology to provide an n-peak type system. Each emulsion must be blended and then mixed together to form a hybrid emulsion as a feature associated with this aspect of the invention, but each group of emulsions is mixed to form a hybrid emulsion. The hybrid emulsion thus formed can be further mixed to form an amalgamated emulsion of the individual hybrid emulsions. For bimodal or multimodal distributions used to form a hybrid emulsion, the hybrid can be reintroduced into a shear or mixing device to form a treated hybrid emulsion.

  Having described the details of the invention, reference is made to the following examples.

Experiments with three fuel types:
1) North Eastern Alberta Bitumen MSAR ™
Fuel 2, particle size 5.5 μm;
2) Northeastern Alberta Bitumen MSAR ™ Fuel 1, particle size 22μm; and 3) Northeastern Alberta Bitumen MSAR ™ Fuel 1 and MSAR ™ Fuel 2
50/50 mixture, particle size 5-22 μm.

Experiments were performed with a fuel with larger droplets (MSAR ™ Fuel 2).
A fuel firing rate of 30 kg / hour, lower than the normal 36 kg / hour, was used to avoid possible fuel clogging. This is because the fuel contained large sized droplets.
The same fuel burn rate was used for other fuel types to maintain consistency of conditions.

The initial temperature of MSAR ™ Fuel 1 was a fuel temperature of 85 ° C. and was slowly raised to 100 ° C. based on the observed flame characteristics.
Other parameters according to the protocol were as follows:
Atomizing air temperature 108 ° C;
78-79 ° C, burner;
Combustion air temperature 108 ° C;
O _2, 6.7,6.2.

The parameters observed for the MSAR fuel 2 fuel type were as follows:
Atomized air temperature 84 ℃;
Combustion air temperature 84 ° C;
Fuel temperature 65 ° C; and
O _2, 5.2,5.3.

For the data of this method, the terms used in the table have the following meaning / description:
Fuel: is the input to the furnace (mass velocity, temperature and pressure are the same for each of the three cases, ie 22 microns, 5 microns and hybrid).

Atomized air: is the air used for the initial atomization of the droplets. Usually, initial atomization typically produces 50-200 micron droplets.
Combustion air: is the main source of oxygen for combustion.

Flue gas: Emissions are normalized to a 3.5% oxygen content in the flue gas. For this reason, two columns are used; one for fuel and one for standardization.
Carbon monoxide emissions: The amount of carbon monoxide is a measure of incomplete combustion.

Particulate: The amount of carbon on the particulate material is a measure of incomplete combustion. The more carbon on the particulate matter, the greater the degree of incomplete combustion.
Heat transfer rate: This is a measure of the main transfer rate measured radially to the flame. All emulsions have a higher radial heat transfer coefficient (radia) than natural gas.
l heat transfer rate). The heat transfer coefficient of all three emulsions is about the same in each case.

Review of the data presented in the table and with reference to Table 4, the MSAR ™ blend or hybrid emulsion is above the value of 5 μm MSAR ™ and close to 22 μm MSAR ™ Provides thermal efficiency.

To enhance the perceived advantages of the hybrid emulsion, Table 3 provides flue gas emission data. Again, this provides evidence that NO _x and SO ₂ emissions are very attractive from the environmental aspect of the blend. It is particularly noteworthy that MSAR ™ blend hybrids have lower particulate matter carbon content and lower flue gas CO concentration than precursor emulsions, which makes the mixed emulsions much more It shows good carbon complete combustion rate.

Perhaps the most attractive part of this data is provided in Table 4 where heat transfer data is shown. The thermal fuel input ratio extracted in this example clearly shows that the hybrid provides a more favorable energy than the natural gas energy.

The data shown herein is further confirmed by FIGS.
Referring to FIG. 23, there is shown a photograph of a burner in which North Eastern Alberta bitumen MSAR ™ fuel 1 is burning. The shape of the flame is shown in the figure.

24 is a view showing a side surface of the flame from the burner of the fuel burning in FIG.
FIGS. 25 and 26 show the coke deposits on the burner nozzle after the first combustion experiment, and FIG. 26 shows the coke deposits on the burner nozzle after the second burn experiment. The difference is quite large.

FIG. 27 is a diagram of a burner during combustion of North Eastern Alberta bitumen MSAR ™ fuel 2.
FIG. 28 shows coke deposits on the burner nozzle after combustion of MSAR ™ fuel 2.

  In FIG. 29, the combustion of the hybrid emulsion is shown in the photograph. It is interesting that the flame shape is much more aggregated when burned than the flame shape of the respective precursor emulsion. This is further supported by FIG. 30, which shows a fairly long flame length and strength when the side view of the burner is taken. As already mentioned herein with respect to the combustion characteristics and other characteristics of the hybrid emulsion, FIG. 31 shows the cleanliness of the flame. Comparing the representation of coke deposits in FIG. 26 associated with MSAR ™ fuel 1, there is substantially no coke deposits on the nozzle after combustion.

CONCLUSION In view of the photographic and physical data presented during the hybrid emulsion experiment, the hybrid emulsion has significant advantages over the combustion of the precursor emulsion and in many cases the benefits of natural gas combustion. It is clear that it approximates this feature. Clearly, the combustion of this hybrid emulsion provides a more desirable energy output due to low monoxide emissions, burner nozzle low coke deposits, and low sulfur dioxide emissions, among other very useful features. As is evident from the drawings, the flame characteristics of this hybrid emulsion provide a lighter and more stable flame with a lighter brown coloration and lower carbon monoxide emissions, among other characteristics.
The present invention includes the following aspects.
[1] An emulsion containing a mixture of a plurality of hydrocarbons and an emulsion stabilizer in a water emulsion, wherein the mixture is a single mode absent loca
l maxima) and the oil is present in 64 to 90% by volume.
[2] The emulsified hydrocarbon fuel according to [1], wherein the fuel includes at least two different precursor emulsions.
[3] The emulsified hydrocarbon fuel according to [2], wherein the precursor emulsions have different hydrocarbon particle sizes.
[4] The emulsified hydrocarbon fuel according to [3], wherein the precursor emulsion contains the same hydrocarbon material.
[5] The emulsified hydrocarbon fuel according to [3], wherein the precursor emulsion contains different hydrocarbon materials.
[6] The emulsified hydrocarbon fuel according to [3], wherein each precursor emulsion has a different burning rate.
[7] The emulsified hydrocarbon fuel according to [5], wherein the emulsified hydrocarbon fuel is a hybrid emulsion containing at least two different emulsions at a predetermined ratio.
[8] The particle size of one emulsion is larger than the particle size of the second emulsion, [3
] The emulsified hydrocarbon fuel of description.
[9] The emulsified hydrocarbon fuel according to [7], wherein each precursor emulsion has a characteristic viscosity, and the viscosity of the hybrid emulsion fuel is lower than the characteristic viscosity of each precursor emulsion.
[10] The hybrid emulsion is 300 times the viscosity of the emulsion containing smaller particles.
The emulsified hydrocarbon fuel as set forth in [9], which has a viscosity of from% to 500% lower.
[11] The hybrid emulsion has a carbon burnout of at least 99.9%.
The emulsified hydrocarbon fuel according to [1], which has a rate).
[12] The emulsified hydrocarbon fuel according to [1], wherein the hybrid has a unimodal particle size distribution formed by mixing bimodal distributions of at least two precursor emulsions.
[13] The hybrid is a multiple emultion polydisperse fuel, [1]
The emulsified hydrocarbon fuel described in 1.
[14] The emulsified hydrocarbon fuel according to [1], wherein the fuel is a liquid fuel emulsified in an aqueous matrix hydrocarbon.
[15] The emulsified hydrocarbon fuel according to [1], wherein the hydrocarbon material contains less than 18 API.
[16] The emulsion stabilizer is present in an amount of 0.01 to 5.0% by weight of the emulsion. [1]
The emulsified hydrocarbon fuel described in 1.
[17] The emulsified hydrocarbon fuel according to [16], wherein the emulsion stabilizer is a surfactant.
[18] A method for blending a mixed emulsion having a low viscosity unimodal particle distribution with respect to a precursor emulsion used to form a mixed emulsion,
Prepare a system with n-peak particle distribution;
Forming a precursor emulsion for each n-peak distribution present in the system, wherein each said precursor emulsion has a characteristic viscosity; and said unimodal size distribution, each said precursor emulsion Mixing the precursor emulsion in a predetermined ratio determined by the desired characteristics of the hybrid emulsion to form the hybrid emulsion having a low viscosity with respect to the predetermined characteristics, wherein the unimodal partial distribution is a plurality of The method comprising each step of a single type where there is no local maximum.
[19] The method of [18], wherein the mixing comprises a shear mixing device.
[20] The method according to [15], wherein the system is a hybrid emulsion formed from at least two precursor emulsions.
[21] The method of [18], further comprising selecting a precursor emulsion having a sufficiently different particle size distribution to provide a hybrid emulsion having a substantially unimodal particle distribution.
[22] The method of [18], further comprising selecting a precursor emulsion for synthesizing the hybrid emulsion, wherein a median particle size differential exists between the selected emulsions. .
[23] The method of [18], wherein each precursor emulsion has a different burning rate.
[24] The method of [23], wherein the high burning rate precursor emulsion stabilizes the flame to more efficiently promote combustion of the low burning rate precursor emulsion.
[25] The method of [18], wherein each of the precursor emulsions contains the same hydrocarbon material.
[26] The method of [25], wherein the hydrocarbon material is less than 18 API.
[27] The method according to [18], wherein the precursor emulsion contains different hydrocarbon materials.
[28] The method of [27], wherein the hydrocarbon material is less than 18 API.
[29] The method according to [18], wherein the at least one precursor emulsion is produced at a lower temperature than the other precursor emulsion, and the at least one precursor emulsion functions as a coolant for the other precursor emulsion. .
[30] The method according to [25], wherein the same hydrocarbon materials have different particle size distributions.
[31] Each of the different hydrocarbon materials has a similar size distribution, [2
7].
[32] The method of [27], wherein each different hydrocarbon material has a different size distribution.
[33] The method of [18], further comprising subjecting the hybrid emulsion to a shearing operation.
[34] The viscosity of the hybrid emulsion is 300 less than the viscosity of the precursor emulsion.
The method according to [18], wherein the method is% to 500% lower.
[35] The method according to [18], wherein each of the precursor emulsions is mixed at a ratio that affects the low viscosity of the hybrid emulsion.
[36] Determine a predetermined ratio by providing a filling algorithm; prepare size distribution parameters for each precursor emulsion to be used; generate hybrid viscosity data; and analyze the minimum viscosity of the hybrid emulsion viscosity Further including each stage [34]
The method described in 1.
[37] The method according to [18], wherein the hybrid emulsion has an oil content of 64-90% by volume.
[38] The method of [37], wherein the emulsion stabilizer is present in an amount of 0.01 to 5.0% by weight of the emulsion.
[39] The method according to [18], wherein the mixed emulsion provides a wide temperature gradient when burned.
[40] The method according to [18], wherein the hybrid emulsion has a high burning rate relative to the burning rate of the precursor emulsion.
[41] A hydrocarbon in at least one precursor emulsion of the emulsion having a faster burning rate than a hydrocarbon material in the second emulsion of the emulsion to facilitate use of a hydrocarbon material having a low relative burning rate. Further comprising selecting a material [27].
The method described in 1.
[42] A method for transporting a viscous hydrocarbon material, comprising:
Providing a source of hydrocarbon material;
Producing a plurality of emulsions of said hydrocarbon material, each emulsion having a characteristic viscosity, each emulsion having a different particle size distribution;
In order to form a hybrid emulsion having a low viscosity for the plurality of emulsions,
Selecting the mixing ratio of the emulsion, the ratio being determined by a filling factor algorithm;
And moving the hybrid emulsion,
Said method comprising each step.
[43] The method according to [42], wherein the hydrocarbon content in the hybrid emulsion is 64 to 90% by volume.
[44] The method of [42], wherein the predetermined ratio is determined by analyzing a packing arrangement of particles in the plurality of emulsions.
[45] The method according to [44], further comprising lowering the freezing point of the hybrid emulsion.
[46] The method of [45], further comprising the step of adding ingredients in the hybrid emulsion to perform freezing point depression.
[47] The method of [46], wherein the material comprises at least one surfactant and alcohol.
[48] The method according to [44], further comprising increasing the calorific value of the hybrid emulsion by introducing at least one biofuel that is water dispersible or soluble in water.
[49] The method according to [48], wherein the biofuel comprises at least one of solid water-dispersible biomass, bioalcohol, and solid hydrocarbon.
[50] A method for maximizing viscous hydrocarbon content in an aqueous system for storage or transportation comprising
Providing a hydrocarbon emulsion having a sufficiently high hydrocarbon internal phase volume so that the droplets in the hydrocarbon emulsion are non-spherical;
Converting the emulsion to at least a bimodal emulsion system;
Forming at least two precursor emulsions from the system;
Selecting a mixing ratio of the precursor emulsion to reduce the viscosity, the ratio is determined by a filling factor algorithm; and synthesizing a hybrid emulsion from the precursor emulsion having the low viscosity;
Said method comprising each step.
[51] The method of [50], wherein the emulsion having non-spherical particles comprises polyhedral particles.
[52] The method according to [51], wherein the emulsion having non-spherical particles comprises a HIPR (high internal phase ratio) emulsion.
[53] The method of [50], wherein the viscosity of the emulsion is maximum when the non-spherical particles are included and is minimum when hybridized.
[54] A method of blending a hybrid emulsion having a unimodal particle size distribution with a low viscosity relative to a precursor emulsion,
Prepare a system with n-peak particle size distribution;
Forming a precursor emulsion for each peak distribution present in the system; each of the precursor emulsions has a characteristic viscosity;
Forming a plurality of hybrid emulsions having a low viscosity and a unimodal size distribution for each of the precursor emulsions; and a unimodal particle distribution and an amalgamated hybrid having a low viscosity relative to the viscosity of the hybrid emulsion Mixing the hybrid emulsion to form an emulsion, the distribution having a single type without a plurality of local maxima,
Said method comprising each step.
[55] The method of [54], wherein each hybrid emulsion of the hybrid emulsion has a different particle size distribution with respect to another hybrid emulsion.
[56] The method of [54], wherein at least the precursor emulsion comprises a HIPR emulsion.
[57] The method according to [54], wherein each hybrid emulsion is another hybrid emulsion in which there is no particle size distribution overlapping with another hybrid emulsion.
[58] A method of modifying at least one of the combustion, storage and transport properties of an emulsion before production, during production and after production,
Preparing an emulsion;
Subjecting the emulsion to unit operations selected from the group consisting of additive addition, mechanical processing, chemical treatment, physical treatment and combinations thereof; and modifying at least one characteristic of the emulsion by the treatment;
Denaturation method including each step.
[59] by introducing at least one of a water dispersible or water soluble biofuel,
The method according to [58], further comprising increasing the calorific value of the hybrid emulsion.
[60] The method according to [59], wherein the biofuel includes at least one of solid water-dispersible biomass, bioalcohol, and solid hydrocarbon.
[61] A method of converting a destabilized emulsion or an off-specification emulsion to a stabilized emulsion or a standard emulsion,
Providing a destabilized or substandard emulsion as the first precursor emulsion;
Chemically / physically characterize the characteristics of a stabilized or standard emulsion;
Input feature information into the filling factor algorithm;
Determining a predetermined mixing ratio of the first precursor emulsion and a second similar precursor emulsion based on stabilization specification characteristics; and mixing to form the stabilization or specification emulsion;
Said method comprising each step.

Claims (15)

An emulsified hydrocarbon fuel comprising a composite emulsion formed from a plurality of hydrocarbon-in-water emulsions and an emulsion stabilizer, wherein the composite emulsion has a unimodal hydrocarbon particle distribution and the hydrocarbon is 64 to 90 volumes The emulsified hydrocarbon fuel, wherein the fuel comprises at least two different precursor emulsions, each having a different hydrocarbon particle size. The emulsified hydrocarbon fuel of claim 1, wherein the precursor emulsion comprises the same hydrocarbon material. The emulsified hydrocarbon fuel according to claim 1, wherein the precursor emulsion comprises different hydrocarbon materials. The emulsified hydrocarbon fuel according to claim 1, wherein each precursor emulsion has a different burning rate. The emulsified hydrocarbon fuel according to claim 3, wherein the emulsified hydrocarbon fuel is a composite emulsion fuel containing at least two different emulsions at a predetermined ratio. The emulsified hydrocarbon fuel according to claim 1, wherein the particle size of one emulsion is larger than the particle size of the second emulsion. The emulsified hydrocarbon fuel according to claim 5, wherein each precursor emulsion has a characteristic viscosity, and the viscosity of the composite emulsion fuel is lower than the characteristic viscosity of each precursor emulsion. The composite emulsion is 300% to 500% than the viscosity of the emulsion containing smaller particles
Emulsified hydrocarbon fuel according to claim 7, having a low viscosity. The emulsified hydrocarbon fuel of claim 1, wherein the composite emulsion has a carbon full burn rate of at least 99.9%. The emulsified hydrocarbon fuel according to claim 1, wherein the composite has the unimodal particle size distribution formed by mixing bimodal distributions of at least two precursor emulsions. The emulsified hydrocarbon fuel according to claim 1, wherein the composite is a multi-emulsion polydisperse fuel. The emulsified hydrocarbon fuel according to claim 1, wherein the fuel is a liquid fuel emulsified in an aqueous matrix hydrocarbon. The emulsified hydrocarbon fuel of claim 1, wherein the hydrocarbon material comprises less than 18 API. The emulsified hydrocarbon fuel according to claim 1, wherein the emulsion stabilizer is present in an amount of 0.01 to 5.0% by weight of the composite emulsion. The emulsified hydrocarbon fuel according to claim 14, wherein the emulsion stabilizer is a surfactant.