# Patent

## Title
Method of manufacturing a cordierite structure

## Abstract

A diesel particulate filter comprising a plugged, wall-flow honeycomb filter body composed of cordierite and having a plurality of parallel end-plugged cell channels traversing the body from a frontal inlet end to an outlet end thereof, wherein the filter exhibits a CTE (25-800° C.) of less than 13×10−7/° C., a bulk filter density of less than 0.60 g/cm3, a median pore diameter, d50, of less than 25 micrometers, a porosity and pore size distribution that satisfy the relationship Pm≦3.75, wherein Pm is equal to 10.2474{1/[(d50)2(%porosity/100)]}+0.0366183(d90)−0.00040119(d90)2+0.468815(100/%porosity)2+0.0297715(d50)+1.61639(d50−d10)/d50, wherein d10, and d90 are pore diameters at 10% and 90% of the pore size distribution on a volumetric basis, and d10<d50<d90. A method of making the same is also provided.

## Background
The present invention is a divisional application of U.S. patent application Ser. No. 10/607,249 to Gregory A. Merkel et al., filed Jun. 25, 2003 and entitled “Cordierite Filters with Reduced Pressure Drop”, issued as U.S. Pat. No. 7,179,316.


BACKGROUND OF THE INVENTION
The present invention relates to diesel particulate filters, and in particular to cordierite wall-flow diesel particulate filters having high filtration efficiency, high strength and low pressure drops for catalyzed and uncatalyzed applications.
Porous, wall-flow ceramic filters have been utilized for the removal of carbonaceous soot particles from the exhaust stream of diesel engines since the early 1980s. A porous ceramic diesel particulate filter (DPF) ideally combines low CTE (for thermal shock resistance), low pressure drop (for engine efficiency and fuel economy), high filtration efficiency (for removal of most particles from the exhaust stream), high strength (to survive handling, canning, and vibration in use), and low cost. Cordierite has satisfied these requirements; however, benefit would be gained by further reducing the pressure drop of commercially available cordierite DPFs.
During use, the pressure drop of a ceramic filter increases as diesel particulate material or carbon soot is deposited within the filter. Typically, during the deposition of the first 0.5 to 1.0 gram/liter of soot, the increase in pressure drop is especially rapid. This has been attributed to the penetration of soot into the surface and near-surface pores of the filter walls. The presence of soot within the filter walls lowers the overall permeability of the wall, thereby increasing the resistance of gas flow through the wall and increasing the pressure drop across the filter. Once the surface and near-surface pores are filled with the porous soot deposit, additional soot accumulates on the outer surface of the walls of the inlet channels as a discrete porous soot layer, or “soot cake.” Although the permeability of this soot layer is very low, the rate of increase in pressure drop per unit mass of deposited soot is actually lower during the soot layer formation stage than during the initial stage in which soot penetrates the filter wall. Periodically, the soot must be burned out of the filter, in situ, in order to prevent clogging of the filter and to restore the filter to a low pressure drop state. This process is known as “regeneration” of the filter.
A recent trend in pollution control for diesel engines has been the application of a catalyst system to the DPF in order to promote the conversion of carbon monoxide and unburned hydrocarbons in the exhaust stream to carbon dioxide and water. These catalyst systems are generally comprised of a mixture of a highly dispersed noble metal catalyst supported on a high surface area metal oxide. The catalyst system may be present as a “washcoat” on the outer surfaces of the filter wall, but more typically resides primarily within the pores of the filter walls, where the oxides+metals form a thin coating that lines the surfaces of the pore walls.
In addition to catalyzing gas reactions, the catalysts can serve to lower the temperature at which the accumulated soot undergoes combustion during regeneration or can otherwise facilitate the regeneration of the filter. Regeneration of the filter requires that the temperature of the exhaust stream entering the filter be raised to the point at which the soot begins to burn. Various strategies have been adopted to provide this energy, all of which reduce the fuel efficiency of the vehicle. Thus, by reducing the energy that must be supplied in order to light-off of the soot, the catalyst can provide benefits in fuel efficiency and cost savings over the life of the vehicle.
It has been observed, however, that the application of a catalyst system to a DPF causes an increase in the pressure drop across the clean and soot-loaded filter. This is due to a reduction in the porosity and a change in the pore size distribution and pore connectivity of the filter with the application of the catalyst system. This change in pore microstructure reduces the permeability of the clean wall prior to soot loading, and also reduces the permeability of the soot-containing wall for any given mass of soot. In attempting to offset an increase in pressure drop observed in catalyzed filters it has been suggested to increase the porosity and median pore size. However, this combination of high porosity and large pore size causes lower filtration efficiency and lower mechanical strength, and does not yield an optimized filter. Furthermore, non-uniform distribution of the catalyst can result from broad pore size distributions.
A high-porosity cordierite DPF that provides a lower pressure drop in both the catalyzed and uncatalyzed state relative to filters that have been previously demonstrated, while maintaining high filtration efficiency and sufficient mechanical strength, would be an advancement in the art. The present invention provides such a cordierite DPF and a method of making the same.
SUMMARY OF THE INVENTION
In one aspect of the invention there is provided a diesel particulate filter comprising a plugged, wall-flow honeycomb filter body composed of cordierite and having a plurality of parallel end-plugged cell channels traversing the body from a frontal inlet end to an outlet end thereof, wherein the filter exhibits: (a) a CTE (25-800° C.) of less than 13×10−7/° C., preferably less than 10×10−7/° C., more preferably less than 7×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 13×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 10×10−7/° C., and even more preferably greater than 4×10−7/° C. and less than 7×10−7/° C.; (b) a bulk filter density of less than 0.60 g/cm3; (c) a median pore diameter, d50, of less than 25 micrometers, and a porosity and pore size distribution that satisfy the relationship Pm≦3.75, preferably Pm≦3.50, preferably Pm≦3.30, wherein Pm is equal to 10.2474{1/[(d50)2(%porosity/100)]}+0.0366183(d90)−0.00040119(d90)2+0.468815(100/%porosity)2+0.0297715(d50)+1.61639(d50−d10)/d50, wherein d10, and d90 are pore diameters in micrometers at 10% and 90% of the pore size distribution based upon volume, and d10<d50<d90. The inventive diesel particulate filter is suitable for both catalyzed and uncatalyzed applications. Preferred embodiments of the inventive diesel particulate filter are further described below.
In another aspect of the invention there is provided a method of making a cordierite structure for use in a diesel particulate filter, the method comprising: forming a mixture of cordierite-forming raw materials, a pore former and organic components, the cordierite-forming raw materials including talc, silica, an alumina-forming source, and optionally kaolin, each defining a median particle size, wherein the talc median particle size, the alumina-forming source median particle size, the pore former, and a pore former median particle size satisfy the relationship Rm≦−2.64, where Rm is equal to [−0.102(talc median particle diameter)+0.001466(talc median particle diameter)2−0.0491((weight percent super-addition of pore forming agent)/(density of pore forming agent))−0.00762(median particle diameter of pore forming agent)+0.0000760(median particle diameter of pore forming agent)2−0.0562(median particle diameter of the alumina-forming source)]; shaping the mixture into a green structure; and, firing the green structure at a temperature and for a time to produce a fired structure. Median particle diameters are in micrometers and density is in grams per cubic centimeter. Preferred embodiments of the inventive forming method are further described below.



BRIEF DESCRIPTION OF THE DRAWINGS
A complete understanding of the present invention may be obtained by reference to the accompanying drawings, when considered in conjunction with the subsequent detailed description, in which:
FIG. 1 is a graphical representation of the pressure drop value between the inlet and outlet ends of comparative filters (open circles) and inventive filters (filled circles), measured at a flow rate of 11.25 scfm of air at 25° C., as a function of the amount of dry, artificial carbon soot that was previously loaded into the filter at a flow rate of 15 scfm; all filters have approximately the same external dimensions (2 inches diameter, 6 inches long) and about the same cell densities (165-215 cells/in2);
FIG. 2 is a graphical representation of the pressure drop value between the inlet and outlet ends of comparative filters (open circles) and inventive filters (filled circles), measured at a flow rate of 11.25 scfm of air at 25° C. on 2 inch diameter by 6 inch long filters (165-215 cpsi) and at 5 grams/liter dry artificial carbon soot loading (deposited at a flow rate of 15 scfm), versus the pore microstructure parameter Pm;
FIG. 3 is a graphical representation of the pressure drop value between the inlet and outlet ends of comparative filters (open circles) and inventive filters (filled circles), measured at a flow rate of 11.25 scfm of air at 25° C. on 2 inch diameter by 6 inch long filters (165-215 cpsi) and at 5 grams/liter dry artificial carbon soot loading (deposited at a flow rate of 15 scfm), versus the percent of the total porosity that lies between 10 and 50 μm; and,
FIG. 4 is a graphical representation of the relationship between the pressure drop value between the inlet and outlet ends of comparative filters (open circles) and inventive filters (filled circles), measured at a flow rate of 11.25 scfm of air at 25° C. on 2 inch diameter by 6 inch long filters (165-215 cpsi) and at 5 grams/liter dry artificial carbon soot loading (deposited at a flow rate of 15 scfm), versus the raw material parameter Rm.



DETAILED DESCRIPTION OF THE INVENTION
Cordierite diesel particulate filters according to the present invention have an enhanced pore microstructure that is optimized for pore connectivity and uniform pore size distribution that results in significant reduction in pressure drop while maintaining mechanical strength and high filtration efficiency. Accordingly, the porosity and pore size distribution satisfy the relationship Pm≦3.75, in which Pm is computed as 10.2474{1/[(d50)2 (%Porosity/100)]}+0.0366183(d90)−0.00040119(d90)2+0.468815(100/%Porosity)2+0.0297715(d50)+1.61639(d50−d10)/d50. The values of d10, d50 and d90 are in units of micrometers, %porosity is dimensionless, where pore sizes and porosity are measured by mercury porosimetry. The values of d10, d50, and d90 are the pore diameters at 10%, 50%, and 90% of the total pore size distribution on a volumetric basis. Specifically, d10 is the pore diameter at 90% cumulative mercury intrusion volume, d50 is the pore diameter at 50% cumulative mercury intrusion volume, and, d90 is the pore diameter at 10% cumulative mercury intrusion volume. Thus, 10% of the pores are smaller than d10, 50% of the pores are smaller than d50, and 90% of the pores are smaller than d90, on a volumetric basis. The value of d50 is less than 25 μm.
In order to achieve lowest soot-loaded pressure drops, the value of Pm is preferably not greater than 3.50, and more preferably not greater than 3.30. To achieve the excellent pore connectivity that is associated with low soot-loaded pressure drop and low values of Pm, the %porosity is preferably not less than 53%, more preferably not less than 56%, and most preferably not less than 59%. Likewise, the value of (d50−d10)/d50 is preferably not greater than 0.60, more preferably not greater than 0.50, and most preferably not greater than 0.45. For high filtration efficiencies and high strength, the value of d50 is preferably less than 20 μm, more preferably less than 15 μm, and most preferably less than 12 μm. For similar reasons, the value of d90 is preferably less than 40 μm, more preferably less than 30 μm, and most preferably less than 20 μm.
The inventive filters further exhibit a CTE (25-800° C.) of less than 13×10−7/° C., preferably less than 10×10−7/° C., more preferably less than 7×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 13×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 10×10−7/° C., and even more preferably greater than 4×10−7/° C. and less than 7×10−7/° C., and a bulk filter density of less than 0.60 g/cm3. A high a modulus of rupture, as measured by the four-point method on a cellular bar cut parallel to the direction of the channels, is also provided of preferably at least 200 psi, more preferably at least 250 psi, and most preferably at least 300 psi.
In an embodiment, the inventive cordierite diesel particulate filter exhibits a CTE (25-800° C.) of less than 13×10−7/° C., a bulk filter density of less than 0.60 g/cm3, and a pressure drop in kPa across the filter, as measured at 25° C. and a flow rate of 11.25 scfm on a 2 inch diameter, 6 inch long filter having about 200 cpsi and a 0.012 inch wall thickness, of not more than 2.2 kPa when the filter contains 5 grams/liter of dry artificial carbon soot that was previously loaded onto the filter at a flow rate of about 15 scfm. The pressure drop as measured under these conditions is preferably not greater than 1.8 kPa, more preferably not greater than 1.5 kPa, and most preferably not greater than 1.3 kPa. The CTE (25-800° C.) is preferably less than 10×10−7/° C., more preferably less than 7×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 13×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 10×10−7/° C., and even more preferably greater than 4×10−7/° C. and less than 7×10−7/° C. In regards to the artificial carbon soot, the term “dry” signifies that the soot does not contain substantial amounts of adsorbed volatile organic compounds.
In another embodiment, the inventive cordierite diesel particulate filter exhibits a CTE (25-800° C.) of less than 13×10−7/° C., a bulk filter density of less than 0.60 g/cm3, and a pressure drop in kPa across the filter, as measured at 25° C. and a higher flow rate of 26.25 scfm on a 2 inch diameter, 6 inch long filter having about 200 cpsi and a 0.012 inch wall thickness, of not more than 5.8 kPa when the filter contains 5 grams/liter of dry artificial carbon soot that was previously loaded onto the filter at a flow rate of about 15 scfm. The pressure drop as measured under these conditions is preferably not greater than 5.0 kPa, more preferably not greater than 4.5 kPa, and most preferably not greater than 4.0 kPa. The CTE (25-800° C.) is preferably less than 13×10−7/° C., more preferably less than 7×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 13×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 10×10−7/° C., and even more preferably greater than 4×10−7/° C. and less than 7×10−7/° C.
The present invention also includes a wall-flow filter comprising a cordierite body having a CTE (25-800° C.) of less than 13×10−7/° C., a bulk filter density of less than 0.60 g/cm3, and a pressure drop at 1.0 gram/liter of soot loading that is not more than 0.75 kPa greater than the pressure drop of the clean (soot-free) filter when the pressure drop is measured at about 25° C. at a flow rate of 11.25 scfm across a 2-inch diameter by 6-inch long portion of a filter having about 200 cells/inch2 and a wall thickness of about 0.012 inches, and the soot is an a dry artificial soot that was previously loaded onto the filter at a flow rate of 15 scfm. The pressure drop difference as measured under these conditions is preferably less than 0.6 kPa, more preferably less than 0.5 kPa, and most preferably less than 0.4 kPa. The CTE (25-800° C.) is preferably less than 10×10−7/° C., more preferably less than 7×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 13×10−7/° C., even more preferably greater than 4×10−7/° C. and less than 10×10−7/° C., and even more preferably greater than 4×10−7/° C. and less than 7×10−7/° C.
There is also provided a method for fabricating the inventive cordierite structure or body by forming a mixture from certain inorganic raw materials having specific particle size restrictions. The inorganic raw materials include talc, silica, and an alumina-forming source. Optionally, the raw material mixture may also contain kaolin. Raw materials are blended together with a pore forming agent, and organic constituents that may include plasticizers, lubricants, and binders. Water is generally added as the solvent. The mixture is shaped into a green body, optionally dried, and then fired to form the product structure.
Regarding the inorganic raw materials, the talc, preferably platy (i.e., having a platelet particle morphology), has a median particle size of between 5 and 35 μm, the silica has a median particle size of between 1 and 35 μm, and the alumina source has a median particle size of between 1 and 18 μm. The alumina source is any material that, when heated, is convertible to Al2O3, such as but not limited to corundum, aluminum hydroxide, aluminum oxide hydroxide (such as boehmite), and so-called transition aluminas such as gamma-alumina and rho-alumina. If more than one alumina source is used the median particle size is computed as [w1(d50)1+w2(d50)2+ . . . +wn(d50)n]/[w1+w2+ . . . +wn] where wi represents the weight percentage of each alumina source and (d50)i is the median particle diameter of the respective alumina source. If kaolin is added it is preferred that the raw material mixture contain not more than about 10 weight percent kaolin, and especially not more than about 5 weight percent kaolin. All particle sizes are measured by a laser diffraction technique.
The pore former may be any natural or synthetic material capable of forming relic pores by evaporation or combustion during firing, such as carbon, coke, graphite, starch, flour, cellulose, or a synthetic organic polymer such as a polyacrylate, polyethylene, or polystyrene. The morphology of the pore forming agent may be platey, fibrous, spheroidal, or other shape. The median particle diameter of the pore forming agent is between 5 μm and 90 μm, preferably between 7 μm and 60 μm, and more preferably between 20 and 50 μm. The pore former is added as a super-addition such that the weight percent super-addition of pore forming agent is computed as 100(mass of pore forming agent)/(mass of cordierite-forming raw materials). All particle sizes are measured by a laser diffraction technique.
According to the present invention, the talc particle size, the median particle size of the combined alumina sources, the amount of pore former, and the median particle size of the pore former satisfy the relation Rm≦−2.64, where Rm is the raw material parameter defined as being equal to [−0.102(talc median particle diameter)+0.001466(talc median particle diameter)2−0.0491((weight percent super-addition of pore forming agent)/(density of pore forming agent))−0.00762(median particle diameter of pore forming agent)+0.0000760(median particle diameter of pore forming agent)2−0.0562(median particle diameter of the alumina sources)]. In the definition of Rm, particle diameters are in units of microns as measured by a laser diffraction technique, and density is in units of grams per cubic centimeter.
The inorganic raw materials and pore former are intimately blended with a solvent, and forming aids which impart plastic formability and green strength to the raw materials when they are shaped into a body. Forming may be done by, for example, molding or extrusion. When forming is done by extrusion, most typically methyl cellulose serves as a binder, and sodium stearate serves as a lubricant. The relative amounts of forming aids can vary depending on factors such as the nature and amounts of raw materials used, etc. For example, the typical amounts of forming aids are 2% to 10% by weight of methyl cellulose, preferably 3% to 6% by weight, and 0.5% to 2% by weight sodium stearate, preferably 0.6% to 1% by weight. The inorganic raw materials, pore former and the forming aids are mixed together in dry form and then mixed with water as the solvent. The amount of water can vary from one batch of materials to another and therefore is determined by pre-testing the particular batch for extrudability.
The resulting plastic mixture is then shaped into a green body, preferably a honeycomb structure. The honeycomb structure has an inlet and outlet end or face, and a multiplicity of cells extending from the inlet end to the outlet end, the cells having porous walls. The inventive filters have cellular densities from 70 cells/in2 (10.9 cells/cm2) to 400 cells/in2 (62 cells/cm2). Extrusion techniques are well known in the art. The green bodies are dried and then fired at a sufficient temperature and for a sufficient time to form the final product structure. The firing is preferably done by heating to a maximum temperature of 1390° to 1440° C. for 4 to 25 hours. The compositions of the present invention result in formation of a ceramic structure which is predominately of a phase approximating the stoichiometry Mg2Al4Si5O18.
Alternate channels of the honeycomb body are plugged at one end, either as part of the honeycomb-forming process, or after drying the unfired body, or after firing the body to form cordierite. A first portion of the cells at the inlet end or face are plugged at the ends, and a second portion of cells at the outlet end or face different from the inlet end cells are additionally plugged so that each cell of the structure is plugged only at one end. The preferred arrangement is to have every other cell on a given face plugged in a checkered pattern.
To more fully illustrate the invention, the following non-limiting examples are presented below. All parts, portions and percentages are on a weight basis unless otherwise stated.
EXAMPLES
Inventive and comparative examples are prepared by mixing together selected raw materials from Table 1 in the proportions listed for the examples in Tables 2 to 8. 100 parts by weight of the dry ingredients (oxides plus pore formers) are mixed with about 4 to 6 parts by weight methyl cellulose and 0.5 to 1 part by weight sodium stearate. The contents are then plasticized with about 25 to 40 parts by weight deionized water, and are extruded into honeycomb having a nominal cell density of 200 cells/inch2 and a wall thickness of 0.012 inches to 0.020 inches. The honeycombs are dried and subsequently fired to a temperature of 1405° C. to 1415° C., held at that temperature for 11 to 25 hours, and then cooled to room temperature.
Properties of comparative (non-inventive) examples are provided in Tables 2 and 3, and properties of inventive examples are given in Tables 4 to 8. Pore volume, %porosity, and pore size distribution are measured by mercury porosimetry. Coefficient of thermal expansion along the axial direction (parallel to the length of the channels) is measured by dilatometry. Modulus of rupture is measured by the four-point method on honeycomb bars cut parallel to axial direction of the filter. The filter bulk density is estimated from the cell density, wall thickness, and porosity of the materials, assuming a plug depth of 5 mm.
Some parts that are approximately 5 cm diameter by approximately 15 cm are plugged at the ends of alternate channels on the opposite faces in a checkered pattern such that a channel that is plugged at one end is open at the other end, thereby forming a wall-flow filter. Pressure drop across the length of the filter is measured at ambient temperature at air flow rates of 11.25 and 26.25 standard cubic feet per minute (scfm). These flow rates are equivalent to 0.319 and 0.743 normal cubic meters per minute, Nm3/min, respectively. They are also equal to space velocities of approximately 62000 and 144000 hours−1, respectively.
The filters are then progressively loaded with dry, artificial high surface area carbon soot at a flow rate of approximately 15 scfm (space velocity approximately 85000 hr−1) and at loadings from about 0.5 grams/liter to about 4.5 grams/liter, and the pressure drops are measured at 11.25 and 26.25 scfm for each soot loading. The pressure drop versus soot loading curves for the inventive and comparative examples are shown in FIG. 1. It is evident that the unique pore microstructures of the inventive bodies enable a much lower rate of pressure drop increase with increasing soot loading than the comparative examples. Comparative filters have higher pressure drops because they do not meet both requirements that the bulk filter density be less than 0.60 g/cm3 and that the value of Pm be no greater than 3.75. The inventive examples are seen to have a much more gradual increase in pressure drop versus soot loading during loading of the initial 1 gram/liter of soot. This results in much lower pressure drops at all higher soot loadings as well.
The extrapolated pressure drops at 5 g/l soot loading and 11.25 scfm flow rate are plotted versus the pore microstructural parameter, Pm, in FIG. 2. It is evident that when the value of the parameter Pm is not more than 3.75 and bulk density of the filter is less than 0.60 g/cm3, the soot-loaded pressure drop of the filter is of a desirable low value.
The extrapolated pressure drops at 5 g/l soot loading and 11.25 scfm flow rate are also plotted versus the percentage of total porosity between 10 and 50 μm in FIG. 3. It is apparent that very low pressure drops can be achieved even when the amount of porosity between 10 and 50 μm is much less than 75% of the total amount of porosity in the ceramic. Thus, the pressure drop of a filter cannot be predicted from the amount of porosity between 10 and 50 μm.
The extrapolated pressure drops at 5 g/l soot loading and 11.25 scfm flow rate are plotted versus the raw material parameter, Rm, in FIG. 4. It is seen that when the raw materials and pore forming agent are selected according to the present invention so that the value of Rm is not more than −2.64, the soot-loaded pressure drop is desirably low.
Therefore, the present invention is advantageous in providing a lower pressure drop cordierite diesel particulate filter relative to commercially available filters due to improved pore connectivity. The improved pore connectivity is a consequence of the narrow pore size distribution and high %porosity. The inventive filters are especially suitable for applications in which the filter is coated with a catalyst system, however may be used in uncatalyzed applications. The lower pressure drop will enable more efficient operation of the diesel engine and improved fuel economy. Despite having a high porosity, the inventive filters possess a high filtration efficiency since a low pressure drop can be achieved without requiring coarse porosity that would allow the passage of soot particles through the filter walls. The inventive filters also have excellent strength due to the absence of coarse pores, despite a high porosity.
It should be understood that while the present invention has been described in detail with respect to certain illustrative and specific embodiments thereof, it should not be considered limited to such but may be used in other ways without departing from the spirit of the invention and the scope of the appended claims.







TABLE 1







Raw material properties










Median Particle
Density of Pore


Raw Material
Diameter (μm)
Former (g/cm3)












Talc A
24.2
—


Talc B
21.6
—


Talc C
15.4
—


Talc D
68.8
—


Alumina A
6.8
—


Alumina B
1.8
—


Aluminum hydroxide A
13.2
—


Aluminum hydroxide B
5.0
—


Boehmite
<0.15
—


Kaolin
3.2
—


Silica
23.4
—


Graphite A
124
2.2


Graphite B
49.0
2.2


Graphite C
36.3
2.2


Graphite D
9.0
2.2


Graphite E
28.6
2.2


Potato starch
45.0
1.5


Corn starch
14.6
1.5


Coconut shell flour
36.6
1.3


Walnut shell flour
75
1.3


Porous polyacrylate beads A
8.1
0.8


Porous polyacrylate beads B
41.9
0.8
















TABLE 2







Comparative Examples









Example Number













C1
C2
C3
C4
C5
















Talc A
39.96
40.7
40.7
40.7
0


Talc B
0
0
0
0
40.7


Alumina A
21.54
0
0
0
0


Alumina B
0
14.8
14.8
14.8
14.8


Aluminum Hydroxide B
16.35
16.0
16.0
16.0
16.0


Kaolin
0
16.0
16.0
16.0
16.0


Silica
22.15
12.5
12.5
12.5
12.5


Graphite A
0
20.0
0
0
0


Graphite C
10.0
0
0
0
20.0


Graphite E
0
0
20.0
20.0
0


Rm parameter
−2.35
−2.03
−2.41
−2.41
−2.34


Total Intrusion (ml/g)
0.3912
0.3877
0.4246
0.4181
0.3896


% Porosity
47.4
46.6
50.4
49.5
47.2


d10 pore size (μm)
7.1
2.0
5.1
5.1
3.0


d50 pore size (μm)
12.4
11.1
11.4
11.9
7.1


d90 pore size (μm)
23.9
31.2
28.3
35.7
15.4


(d90 − d10)/d50
1.35
2.62
2.03
2.56
1.74


(d90 − d50)/d50
0.92
1.80
1.47
1.99
1.16


(d50 − d10)/d50
0.43
0.82
0.56
0.57
0.58


Pm parameter
3.93
4.75
3.96
4.13
4.15


Pore volume ≧80 μm (ml/g)
0.0103
0.0120
0.0175
0.0219
0.0053


Pore volume ≧60 μm (ml/g)
0.0136
0.0164
0.0217
0.0270
0.0070


Pore volume ≧50 μm (ml/g)
0.0170
0.0216
0.0256
0.0323
0.0089


Pore volume ≧40 μm (ml/g)
0.0204
0.0268
0.0294
0.0375
0.0107


Pore volume ≧20 μm (ml/g)
0.0553
0.0800
0.0677
0.0831
0.0265


Pore volume ≧10 μm (ml/g)
0.2781
0.2176
0.2567
0.2613
0.0880


Pore volume ≧4 μm (ml/g)
0.3882
0.3121
0.3982
0.3920
0.3166


Pore volume ≧2 μm (ml/g)
0.3905
0.3499
0.4161
0.4094
0.3740


Percent of total porosity <10 μm
28.9
43.9
39.5
37.5
77.4


Percent of total porosity >10 μm, <50 μm
66.7
50.6
54.4
54.8
20.3


Percent of total porosity >50 μm
4.3
5.6
6.0
7.7
2.3


Diameter (cm)
5.10
5.05
4.92
5.02
5.20


Length (cm)
15.53
15.18
15.53
15.43
15.97


Cells per square inch
180.6
182
213
198
185


Wall thickness (10−3 inches)
19.5
10.9
20.5
13.9
20.5


Filter bulk density (g/cm3)
0.68
0.43
0.70
0.60
0.71


Clean pressure drop at 11.25 scfm (kPa)
0.73
0.52
1.00
0.49
0.92


Pressure drop at 1 g/L, 11.25 scfm (kPa)
1.62
2.34
2.08
1.45
2.04


Pressure drop at 5 g/L, 11.25 scfm (kPa)
2.97
3.37
3.30
2.24
3.43


Pressure drop at 10 g/L, 11.25 scfm (kPa)
4.83
4.60
5.07
3.22
5.30


Clean pressure drop at 26.25 scfm (kPa)
2.66
1.61
3.62
1.63
2.72


Pressure drop at 1 g/L, 26.25 scfm (kPa)
4.72
6.05
6.21
3.85
5.46


Pressure drop at 5 g/L, 26.25 scfm (kPa)
8.18
8.81
9.61
5.97
9.05


Pressure drop at 10 g/L, 26.25 scfm (kPa)
12.79
11.93
14.27
8.50
13.81


Pressure drop at 1 g/l soot loading minus clean
0.89
1.82
1.08
0.96
1.12


pressure drop, both at 11.25 scfm (kPa)


CTE, 25-800° C. (10−7° C.−1)
9.1
3.5
4.7
3.5
6.6


Modulus of rupture on cellular bar (lbs/in2)
1136
320
—
—
600
















TABLE 3







Comparative Examples









Example Number













C6
C7
C8
C9
C10
















Talc A
0
0
0
0
20.35


Talc B
0
40.7
0
0
0


Talc C
40.7
0
40.7
40.7
0


Talc D
0
0
0
0
20.35


Alumina B
14.8
14.8
14.8
14.8
14.8


Aluminum Hydroxide B
16.0
16.0
16.0
16.0
16.0


Kaolin
16.0
16.0
16.0
16.0
16.0


Silica
12.5
12.5
12.5
12.5
12.5


Graphite A
0
0
0
0
40.0


Graphite C
20.0
0
40.0
0
0


Graphite D
0
20.0
0
40.0
0


Rm parameter
−2.04
−2.22
−2.49
−2.37
−2.44


Total Intrusion (ml/g)
0.3838
0.4103
0.5167
0.4868
0.5624


% Porosity
45.6
49.1
52.7
52.7
59.7


d10 pore size (μm)
3.5
2.2
4.1
3.7
6.9


d50 pore size (μm)
9.4
4.8
9.9
8.4
22.6


d90 pore size (μm)
27.4
11.3
35.0
35.1
55.8


(d90 − d10)/d50
2.55
1.92
3.11
3.75
2.16


(d90 − d50)/d50
1.92
1.38
2.53
3.20
1.46


(d50 − d10)/d50
0.63
0.54
0.59
0.56
0.7


Pm parameter
4.51
4.23
3.93
3.91
3.94


Pore volume ≧80 μm (ml/g)
0.0109
0.0074
0.0170
0.0168
0.0275


Pore volume ≧60 μm (ml/g)
0.0145
0.0091
0.0248
0.0228
0.048


Pore volume ≧50 μm (ml/g)
0.0191
0.0107
0.0334
0.0313
0.0777


Pore volume ≧40 μm (ml/g)
0.0237
0.0123
0.0419
0.0397
0.1073


Pore volume ≧20 μm (ml/g)
0.0603
0.0224
0.1015
0.0951
0.3243


Pore volume ≧10 μm (ml/g)
0.1774
0.0483
0.2555
0.2056
0.476


Pore volume ≧4 μm (ml/g)
0.3309
0.2517
0.4691
0.4247
0.5285


Pore volume ≧2 μm (ml/g)
0.3700
0.3776
0.5062
0.4779
0.5443


Percent of total porosity <10 μm
53.8
88.2
50.6
57.8
15.4


Percent of total porosity >10 μm, <50 μm
41.2
9.2
43.0
35.8
70.8


Percent of total porosity >50 μm
5.0
2.6
6.5
6.4
13.8


Diameter (cm)
—
5.37
—
—
5.08


Length (cm)
—
15.15
—
—
15.19


Cells per square inch
—
186
—
—
196


Wall thickness (10−3 inches)
—
14.0
—
—
19.9


Filter bulk density (g/cm3)
—
0.59
—
—
0.52


Clean pressure drop at 11.25 scfm (kPa)
—
1.02
—
—
0.65


Pressure drop at 1 g/L, 11.25 scfm (kPa)
—
1.78
—
—
1.4


Pressure drop at 5 g/L, 11.25 scfm (kPa)
—
3.19
—
—
2.67


Pressure drop at 10 g/L, 11.25 scfm (kPa)
—
5.34
—
—
3.96


Clean pressure drop at 26.25 scfm (kPa)
—
2.85
—
—
2.43


Pressure drop at 1 g/L, 26.25 scfm (kPa)
—
4.67
—
—
4


Pressure drop at 5 g/L, 26.25 scfm (kPa)
—
7.75
—
—
7.52


Pressure drop at 10 g/L, 26.25 scfm (kPa)
—
12.15
—
—
11.32


Pressure drop at 1 g/l soot loading minus clean
—
0.76
—
—
0.75


pressure drop, both at 11.25 scfm (kPa)


CTE, 25-800° C. (10−7° C.−1)
6.4
3.7
8.1
8.6
9.4


Modulus of rupture on cellular bar (lbs/in2)
—
601
—
—
—
















TABLE 4







Inventive Examples









Example Number














1
2
3
4
5
6

















Talc A
40.70
40.70
40.70
39.96
39.96
39.96


Alumina A
0
0
14.80
0
21.54
21.54


Alumina B
14.80
14.80
0
21.54
0
0


Aluminum Hydroxide B
16.00
16.00
16.00
16.35
16.35
16.35


Kaolin
16.00
16.00
16.00
0
0
0


Silica
12.50
12.50
12.50
22.15
22.15
22.15


Graphite A
60.0
0
0
0
0
0


Graphite B
0
0
40.0
40.0
40.0
0


Graphite C
0
0
0
0
0
40.0


Graphite D
0
40.0
0
0
0
0


Rm parameter
−2.92
−2.76
−3.03
−2.87
−3.03
−3.02


Total Intrusion (ml/g)
0.6897
0.5752
0.6140
0.6307
0.5737
0.6195


% Porosity
61.6
59.0
59.9
62.0
55.4
60.7


d10 pore size (μm)
5.3
5.0
9.1
9.3
8.7
10.0


d50 pore size (μm)
16.9
13.2
15.4
15.9
15.8
17.2


d90 pore size (μm)
38.4
39.9
45.0
39.2
35.6
42.2


(d90 − d10)/d50
1.96
2.64
2.34
1.87
1.70
1.88


(d90 − d50)/d50
1.27
2.01
1.93
1.46
1.25
1.45


(d50 − d10)/d50
0.69
0.62
0.41
0.41
0.45
0.42


Pm parameter
3.73
3.66
3.34
3.24
3.59
3.35


Pore volume ≧80 μm (ml/g)
0.0203
0.0205
0.0229
0.0250
0.0184
0.0301


Pore volume ≧60 μm (ml/g)
0.0321
0.0321
0.0379
0.0362
0.0270
0.0412


Pore volume ≧50 μm (ml/g)
0.0479
0.0448
0.0538
0.0491
0.0382
0.0538


Pore volume ≧40 μm (ml/g)
0.0637
0.0574
0.0696
0.0619
0.0495
0.0663


Pore volume ≧20 μm (ml/g)
0.2491
0.1723
0.2109
0.2195
0.1570
0.2270


Pore volume ≧10 μm (ml/g)
0.5423
0.3603
0.5326
0.5531
0.4868
0.5565


Pore volume ≧4 μm (ml/g)
0.6401
0.5462
0.6110
0.6273
0.5693
0.6180


Pore volume ≧2 μm (ml/g)
0.6728
0.5654
0.6137
0.6302
0.5728
0.6191


Percent of total porosity <10 μm
21.4
37.4
13.3
12.3
15.1
10.2


Percent of total porosity >10 μm, <50 μm
71.7
54.9
78.0
79.9
78.2
81.2


Percent of total porosity >50 μm
6.9
7.8
8.8
7.8
6.7
8.7


Diameter (cm)
5.15
—
5.12
5.19
5.27
5.34


Length (cm)
15.19
—
15.33
15.05
15.23
15.19


Cells per square inch
179
—
189
164
183
167


Wall thickness (10−3 inches)
11.3
—
14.1
13.7
14.2
12.8


Filter bulk density (g/cm3)
0.31
—
0.40
0.35
0.44
0.35


Clean pressure drop at 11.25 scfm (kPa)
0.43
—
0.43
0.31
0.37
0.30


Pressure drop at 1 g/L, 11.25 scfm (kPa)
1.05
—
0.92
0.56
0.75
0.50


Pressure drop at 5 g/L, 11.25 scfm (kPa)
1.92
—
1.80
1.10
1.70
1.09


Pressure drop at 10 g/L, 11.25 scfm (kPa)
3.01
—
2.99
1.77
2.93
1.79


Clean pressure drop at 26.25 scfm (kPa)
1.60
—
1.57
1.15
1.37
1.14


Pressure drop at 1 g/L, 26.25 scfm (kPa)
3.03
—
2.69
1.70
2.23
1.55


Pressure drop at 5 g/L, 26.25 scfm (kPa)
5.21
—
4.98
3.02
4.58
2.95


Pressure drop at 10 g/L, 26.25 scfm (kPa)
7.90
—
8.04
4.72
7.72
4.73


Pressure drop at 1 g/l soot loading minus clean
0.62
—
0.49
0.25
0.38
0.20


pressure drop, both at 11.25 scfm (kPa)


CTE, 25-800° C. (10−7° C.−1)
5.2
5.6
5.5
6.4
7.9
9.5


Modulus of rupture on cellular bar (lbs/in2)
185
—
—
—
—
305
















TABLE 5







Inventive Examples









Example Number














7
8
9
10
11
12

















Talc A
39.96
40.27
39.86
40.7
40.7
40.7


Alumina A
0
10.75
19.05
0
0
0


Alumina B
21.54
0
0
14.8
14.8
14.8


Aluminum Hydroxide B
16.35
15.83
14.01
16.0
16.0
16.0


Boehmite
0
4.95
4.99
0
0
0


Kaolin
0
15.83
0
16.0
16.0
16.0


Silica
22.15
12.37
22.09
12.5
12.5
12.5


Graphite A
0
0
0
0
20.0
0


Graphite C
0
40.0
30.0
0
0
0


Graphite D
40.0
0
0
0
0
0


Potato Starch
0
0
0
40.0
20.0
0


Corn Starch
0
0
0
0
0
40.0


Rm parameter
−2.75
−2.95
−2.75
−3.31
−2.68
−3.21


Total Intrusion (ml/g)
0.5950
0.5385
0.5339
0.6216
0.6561
0.5329


% Porosity
59.8
56.6
54.5
59.4
62.8
56.5


d10 pore size (μm)
10.8
7.9
5.0
7.0
7.2
5.0


d50 pore size (μm)
20.7
14.6
11.0
14.6
16.0
8.6


d90 pore size (μm)
53.8
39.3
30.4
29.2
35.5
34.5


(d90 − d10)/d50
2.08
2.15
2.31
1.52
1.77
3.42


(d90 − d50)/d50
1.60
1.69
1.76
1.00
1.22
2.99


(d90 − d10)/d50
0.48
0.46
0.55
0.52
0.55
0.42


Pm parameter
3.55
3.55
3.69
3.41
3.42
3.43


Pore volume ≧80 μm (ml/g)
0.0347
0.0238
0.0182
0.0140
0.0161
0.0170


Pore volume ≧60 μm (ml/g)
0.0503
0.0320
0.0246
0.0209
0.0245
0.0255


Pore volume ≧50 μm (ml/g)
0.0693
0.0420
0.0315
0.0287
0.0333
0.0340


Pore volume ≧40 μm (ml/g)
0.0882
0.0520
0.0383
0.0364
0.0421
0.0424


Pore volume ≧20 μm (ml/g)
0.3119
0.1527
0.0939
0.1457
0.1664
0.0895


Pore volume ≧10 μm (ml/g)
0.5553
0.4211
0.3042
0.4917
0.5344
0.2115


Pore volume ≧4 μm (ml/g)
0.5942
0.5305
0.5023
0.5903
0.6301
0.5091


Pore volume ≧2 μm (ml/g)
0.5942
0.5370
0.5217
0.6018
0.6422
0.5287


Percent of total porosity <10 μm
6.7
21.8
43.0
20.9
18.5
60.3


Percent of total porosity >10 μm, <50 μm
81.7
70.4
51.1
74.5
76.4
33.3


Percent of total porosity >50 μm
11.6
7.8
5.9
4.6
5.1
6.4


Diameter (cm)
—
5.14
4.92
5.16
—
5.08


Length (cm)
—
15.26
15.24
15.21
—
15.24


Cells per square inch
—
186
188
197
—
205


Wall thickness (10−3 inches)
—
13.4
12.2
11.5
—
11.7


Filter bulk density (g/cm3)
—
0.41
0.40
0.35
—
0.39


Clean pressure drop at 11.25 scfm (kPa)
—
0.37
0.43
0.40
—
0.41


Pressure drop at 1 g/L, 11.25 scfm (kPa)
—
0.67
0.87
0.97
—
0.72


Pressure drop at 5 g/L, 11.25 scfm (kPa)
—
1.34
1.62
1.95
—
1.37


Pressure drop at 10 g/L, 11.25 scfm (kPa)
—
2.23
2.58
3.26
—
2.18


Clean pressure drop at 26.25 scfm (kPa)
—
1.37
1.46
1.48
—
1.44


Pressure drop at 1 g/L, 26.25 scfm (kPa)
—
2.03
2.48
2.81
—
2.13


Pressure drop at 5 g/L, 26.25 scfm (kPa)
—
3.69
4.34
5.29
—
3.73


Pressure drop at 10 g/L, 26.25 scfm (kPa)
—
6.02
6.71
8.61
—
5.83


Pressure drop at 1 g/l soot loading minus clean

0.30
0.44
0.57
—
0.31


pressure drop, both at 11.25 scfm (kPa)


CTE, 25-800° C. (10−7° C.−1)
7.8
7.5
5.2
4.2
3.2
4.3


Modulus of rupture on cellular bar (lbs/in2)
—
409
247
253
—
236
















TABLE 6







Inventive Examples









Example Number














13
14
15
16
17
18

















Talc A
0
0
0
0
0
40.7


Talc B
40.7
40.7
0
0
40.7
0


Talc C
0
0
40.7
40.7
0
0


Alumina B
14.8
14.8
14.8
14.8
14.8
14.8


Aluminum Hydroxide B
16.0
16.0
16.0
16.0
16.0
16.0


Kaolin
16.0
16.0
16.0
16.0
16.0
16.0


Silica
12.5
12.5
12.5
12.5
12.5
12.5


Graphite A
0
0
0
0
0
30.0


Graphite C
60.0
0
60.0
0
35.0
0


Graphite D
0
60.0
0
60.0
0
0


Potato Starch
0
0
0
0
0
20.0


Rm parameter
−3.23
−3.12
−2.93
−2.82
−2.67
−2.91


Total Intrusion (ml/g)
0.6640
0.6709
0.6775
0.6081
0.5989
0.9012


% Porosity
62.2
58.4
61.3
55.7
60.0
69.7


d10 pore size (μm)
6.2
3.5
4.1
3.7
4.6
7.6


d50 pore size (μm)
11.7
6.3
9.1
7.8
12.3
18.6


d90 pore size (μm)
21.5
15.7
25.7
38.6
29.3
51.7


(d90 − d10)/d50
1.32
1.96
2.37
4.48
2.01
2.37


(d90 − d50)/d50
0.85
1.51
1.81
3.96
1.38
1.78


(d50 − d10)/d50
0.47
0.45
0.55
0.52
0.63
0.59


Pm parameter
3.04
3.21
3.29
3.70
3.52
3.34


Pore volume ≧80 μm (ml/g)
0.0092
0.0157
0.0141
0.0270
0.0139
0.0271


Pore volume ≧60 μm (ml/g)
0.0141
0.0190
0.0211
0.0369
0.0183
0.0405


Pore volume ≧50 μm (ml/g)
0.0192
0.0226
0.0290
0.0489
0.0233
0.0651


Pore volume ≧40 μm (ml/g)
0.0243
0.0261
0.0368
0.0609
0.0283
0.0898


Pore volume ≧20 μm (ml/g)
0.0791
0.0490
0.0930
0.1343
0.0874
0.3517


Pore volume ≧10 μm (ml/g)
0.4291
0.1154
0.2974
0.2499
0.3881
0.6650


Pore volume ≧4 μm (ml/g)
0.6446
0.5598
0.6093
0.6079
0.5556
0.7780


Pore volume ≧2 μm (ml/g)
0.6575
0.6574
0.6631
0.6081
0.5891
0.7962


Percent of total porosity <10 μm
35.4
82.8
56.1
58.9
35.2
26.2


Percent of total porosity >10 μm, <50 μm
61.7
13.8
39.6
33.1
60.9
66.6


Percent of total porosity >50 μm
2.9
3.4
4.3
8.0
3.9
7.2


Diameter (cm)
5.16
5.35
5.23
5.39
—
—


Length (cm)
15.22
15.23
15.20
15.22
—
—


Cells per square inch
186
190
183
202
—
—


Wall thickness (10−3 inches)
11.7
12.6
14.4
11.3
—
—


Filter bulk density (g/cm3)
0.32
0.38
0.39
0.38
—
—


Clean pressure drop at 11.25 scfm (kPa)
0.50
0.53
0.47
0.40
—
—


Pressure drop at 1 g/L, 11.25 scfm (kPa)
0.92
0.86
0.90
0.70
—
—


Pressure drop at 5 g/L, 11.25 scfm (kPa)
1.93
1.68
1.85
1.18
—
—


Pressure drop at 10 g/L, 11.25 scfm (kPa)
3.26
2.76
3.09
1.72
—
—


Clean pressure drop at 26.25 scfm (kPa)
1.78
1.76
1.62
1.40
—
—


Pressure drop at 1 g/L, 26.25 scfm (kPa)
2.71
2.54
2.61
2.11
—
—


Pressure drop at 5 g/L, 26.25 scfm (kPa)
5.28
4.50
5.01
3.46
—
—


Pressure drop at 10 g/L, 26.25 scfm (kPa)
8.64
7.13
8.18
5.04
—
—


Pressure drop at 1 g/l soot loading minus clean
0.42
0.33
0.43
0.30
—
—


pressure drop, both at 11.25 scfm (kPa)


CTE, 25-800° C. (10−7° C.−1)
6.4
5.1
7.3
—
6.3
—


Modulus of rupture on cellular bar (lbs/in2)
270
238
276
264
330
—
















TABLE 7







Inventive Examples









Example Number













19
20
21
22
23
















Talc A
40.7
40.7
40.7
40.7
40.7


Alumina B
14.8
14.8
14.8
14.8
14.8


Aluminum Hydroxide B
16.0
16.0
16.0
16.0
16.0


Kaolin
16.0
16.0
16.0
16.0
16.0


Silica
12.5
12.5
12.5
12.5
12.5


Graphite A
40.0
0
0
0
0


Potato Starch
20.0
0
0
0
0


Coconut shell flour
0
36.0
0
0
0


Walnut shell flour
0
0
36.0
0
0


Polyacrylate beads A
0
0
0
30.0
0


Polyacrylate beads B
0
0
0
0
30.0


Rm parameter
−3.13
−3.34
−3.18
−3.70
−3.83


Total Intrusion (ml/g)
0.8301
0.5862
0.6392
0.4881
0.5473


% Porosity
70.5
63.7
61.02
55.0
57.9


d10 pore size (μm)
7.0
4.9
4.9
2.4
3.6


d50 pore size (μm)
17.4
9.4
12.1
5.4
10.7


d90 pore size (μm)
36.8
15.4
23.4
17.0
23.9


(d90 − d10)/d50
1.71
1.13
1.52
2.69
1.90


(d90 − d50)/d50
1.12
0.64
0.93
2.13
1.23


(d50 − d10)/d50
0.60
0.48
0.59
0.56
0.67


Pm parameter
3.28
2.87
3.33
3.75
3.59


Pore volume ≧80 μm (ml/g)
0.0244
0.0108
0.0140
0.0091
0.0123


Pore volume ≧60 μm (ml/g)
0.0379
0.0151
0.0190
0.0126
0.0172


Pore volume ≧50 μm (ml/g)
0.0549
0.0179
0.0245
0.0157
0.0219


Pore volume ≧40 μm (ml/g)
0.0718
0.0207
0.0300
0.0188
0.0266


Pore volume ≧20 μm (ml/g)
0.2870
0.0405
0.0890
0.0393
0.0750


Pore volume ≧10 μm (ml/g)
0.6834
0.2474
0.4050
0.1086
0.3017


Pore volume ≧4 μm (ml/g)
0.7912
0.5493
0.5975
0.3216
0.4840


Pore volume ≧2 μm (ml/g)
0.8082
0.5761
0.6252
0.4579
0.5230


Percent of total porosity <10 μm
17.7
57.8
36.6
77.8
44.9


Percent of total porosity >10 μm, <50 μm
75.7
39.1
59.5
19.0
51.1


Percent of total porosity >50 μm
6.6
3.1
3.8
3.2
4.0


CTE, 25-800° C. (10−7° C.−1)
6.1
—
8.3
—
—


Modulus of rupture on cellular bar (lbs/in2)
—
—
—
—
—
















TABLE 8







Inventive Examples









Example Number












24
25
26
27















Talc A
40.7
40.7
40.7
40.7


Alumina A
16.0
16.0
0
0


Alumina B
0
0
16.0
16.0


Aluminum Hydroxide A
16.0
16.0
0
0


Aluminum Hydroxide B
0
0
16.0
16.0


Kaolin
16.0
16.0
16.0
16.0


Silica
12.5
12.5
12.5
12.5


Graphite E
20.0
40.0
40.0
60.0


Rm parameter
−2.78
−3.23
−2.86
−3.30


Total Intrusion (ml/g)
0.4820
0.6037
0.4759
0.5966


% Porosity
55.2
61.1
53.2
60.8


d10 pore size (μm)
8.2
10.1
7.8
8.8


d50 pore size (μm)
14.6
16.0
12.5
13.6


d90 pore size (μm)
29.8
32.2
28.4
29.8


(d90 − d10)/d50
1.48
1.38
1.65
1.55


(d90 − d50)/d50
1.04
1.02
1.28
1.19


(d50 − d10)/d50
0.44
0.37
0.38
0.35


Pm parameter
3.50
3.16
3.48
3.07


Pore volume ≧80 μm (ml/g)
0.0150
0.0185
0.0161
0.0188


Pore volume ≧60 μm (ml/g)
0.0208
0.0268
0.0210
0.0241


Pore volume ≧50 μm (ml/g)
0.0257
0.0340
0.0260
0.0303


Pore volume ≧40 μm (ml/g)
0.0332
0.0446
0.0318
0.0372


Pore volume ≧20 μm (ml/g)
0.0966
0.1471
0.0786
0.1052


Pore volume ≧10 μm (ml/g)
0.3988
0.5452
0.3442
0.4851


Pore volume ≧4 μm (ml/g)
0.4716
0.5941
0.4728
0.5942


Pore volume ≧2 μm (ml/g)
0.4787
0.5983
0.4752
0.5961


Percent of total porosity <10 μm
17.3
9.7
27.7
18.7


Percent of total porosity >10 μm, <50 μm
77.4
84.7
66.9
76.2


Percent of total porosity >50 μm
5.3
5.6
5.5
5.1


Diameter (cm)
—
—
5.07
—


Length (cm)
—
—
15.33
—


Cells per square inch
—
—
196
—


Wall thickness (10−3 inches)
—
—
13.7
—


Filter bulk density (g/cm3)
—
—
0.46
—


Clean pressure drop at 11.25 scfm (kPa)
—
—
0.50
—


Pressure drop at 1 g/L, 11.25 scfm (kPa)
—
—
1.18
—


Pressure drop at 5 g/L, 11.25 scfm (kPa)
—
—
2.11
—


Pressure drop at 10 g/L, 11.25 scfm (kPa)
—
—
3.30
—


Clean pressure drop at 26.25 scfm (kPa)
—
—
1.78
—


Pressure drop at 1 g/L, 26.25 scfm (kPa)
—
—
3.32
—


Pressure drop at 5 g/L, 26.25 scfm (kPa)
—
—
5.74
—


Pressure drop at 10 g/L, 26.25 scfm (kPa)
—
—
8.84
—


Pressure drop at 1 g/l soot loading minus
—
—
0.68
—


clean pressure drop, both at 11.25 scfm (kPa)


CTE, 25-800° C. (10−7° C.−1)
5.5
6.0
5.3
7.4


Modulus of rupture on cellular bar (lbs/in2)
—
—
—
—

## Claims

1. A method of making a cordierite structure for use in a diesel particulate filter, the method comprising:
forming a mixture of cordierite-forming raw materials, a pore former and organic components, the cordierite-forming raw materials including talc, silica, and an alumina-forming source, each defining a median particle size, wherein the talc median particle size, the alumina-forming source median particle size, the amount of pore former, and the pore former median particle size satisfy the relationship Rm≦−2.64, where Rm is equal to [−0.102(talc median particle diameter)+0.001466(talc median particle diameter)2−0.0491((weight percent super-addition of pore forming agent)/(density of pore forming agent))−0.00762(median particle diameter of pore forming agent)+0.0000760(median particle diameter of pore forming agent)2−0.0562(median particle diameter of the alumina-forming source)], wherein the median particle diameter is in units of micrometers;
shaping the mixture into a green structure; and,
firing the green structure at a temperature and for a time to produce a fired structure having a CTE (25-800° C.) of less than 13×10−7/° C., a bulk filter density of less than 0.60 g/cm3, a median pore diameter, d50, of less than 25 micrometers, a porosity and pore size distribution that satisfy the relationship Pm≦3.75, wherein Pm is equal to 10.2474{1/[(d50)2(% porosity/100)]}+0.0366183(d90)−0.00040119(d90)2+0.468815(100/% porosity)2+0.0297715(d50)+1.61639(d50−d10)/d50, wherein d10, and d90 are pore diameters in units of micrometers at 10% and 90% of the pore size distribution on a volumetric basis, and d10<d50<d90.

2. The method of claim 1 wherein the talc is platy and has a median particle size of between 5 and 35 micrometers.

3. The method of claim 1 wherein the median particle size of the silica is between 1 and 35 micrometers.

4. The method of claim 1 wherein the median particle size of the alumina-forming source is between 1 and 18 micrometers.

5. The method of claim 4 wherein the alumina-forming source is selected from the group consisting of corundum, aluminum hydroxide, aluminum oxide hydroxide (such as boebmite), and so-called transition aluminas such as gamma-alumina and rho-alumina.

6. The method of claim 1 wherein the pore former has a median particle size of between 5 and 90 micrometers.

7. The method of claim 6 wherein the pore former has a median particle size of between 7 and 60 micrometers.

8. The method of claim 7 wherein the pore former has a median particle size of between 20 and 50 micrometers.

9. The method of claim 1 wherein the pore former is selected from the group consisting of carbon, coke, graphite, starch, flour, cellulose, polyacrylate, polyethylene, or polystyrene.

10. The method of claim 1 wherein the organic components comprise 2% to 10% by weight of methyl cellulose, and 0.5% to 2% by weight sodium stearate.

11. The method of claim 10 wherein the organic components comprise 3% to 6% by weight methyl cellulose and 0.6% to 1% by weight sodium stearate.

12. The method of claim 1 wherein the shaping is by extrusion.

13. The method of claim 12 wherein the mixture is shaped through a die into a honeycomb body having an inlet and outlet end or face, and a multiplicity of cells extending from the inlet end to the outlet end, the cells having porous walls.

14. The method of claim 1 wherein the CTE of the honeycomb structure is less than 10×10−7/° C.

15. The method of claim 14 wherein the CTE of the honeycomb structure is less than 7×10−7/° C.

16. The method of claim 1 wherein the CTE of the honeycomb structure is greater than 4×10−7/° C. and less than 13×10−7/° C.

17. The method of claim 16 wherein the CTE of the honeycomb structure is greater than 4×10−7/° C. and less than 10×10−7/° C.

18. The method of claim 17 wherein the CTE of the honeycomb structure is greater than 4×10−7/° C. and less than 7×10−7/° C.

19. The method of claim 1 wherein the honeycomb structure has Pm≦3.50.

20. The method of claim 19 wherein the honeycomb structure has Pm≦3.30.

21. The method of claim 1 wherein the firing is at 1390° C. to 1400° C. for 4 to 25 hours.

22. The method of claim 1 further comprising the step of forming a wall-flow filter.

23. The method of claim 22 wherein in the formation of a wall-flow filter the cells of the honeycomb structure are end plugged at the inlet or outlet end to form a checkered pattern.

24. The method of claim 1 wherein the CTE of the honeycomb structure is less than 6×10−7/° C.

25. The method of claim 1 wherein the pore former comprises graphite and starch.

26. The method of claim 1 wherein the pore former comprises graphite and potato starch.

27. The method of claim 1, wherein the mixture of cordierite-forming raw materials includes kaolin.

28. A method of making a cordierite structure, comprising the steps of:
forming a mixture of cordierite-forming raw materials, a pore former and organic components, the cordierite-forming raw materials including talc, silica, and an alumina-forming source, wherein the pore former comprises a combination of graphite and starch;
shaping the mixture into a green honeycomb structure; and
firing the green structure at a temperature and for a time to produce a fired honeycomb structure;
wherein the fired structure further comprises: a CTE (25-800° C.) of less than 13×1031 7/° C., a median pore diameter, d50, of less than 25 μm; a porosity of greater than 53%; a narrow pore size distribution with a value of (d50−d10)/d50 not greater than 0.6; and a value of d90 less than 40 μm wherein d10, and d90 are pore diameters at 10% and 90% of the pore size distribution on a volumetric basis, and d10<d50<d90;
wherein the fired structure comprises a pore size distribution that satisfies the relationship Pm≦3.75, wherein Pm is equal to 10.2474 {1/[(d50)2(% porosity/100)]}+0.0366183(d90)+0.00040119 (d90)2+0.468815(100/% porosity)2+0.0297715(d50)+1.61639(d50−d10)/d50, wherein d10, and d90 are pore diameters in units of micrometers at 10% and 90% of the pore size distribution on a volumetric basis, and d10<d50<d90.

29. The method of claim 28 wherein the starch comprise a potato starch.

30. The method of claim 28, wherein the mixture of cordierite-forming raw materials includes kaolin.