Patent Application
20120304530
The present application relates to upgrading bio-oils so that such products may be used as fuels. More specifically, the present application relates to a process for upgrading pyrolysis oil into a usable fuel product.
Many people have attempted to use “bio-oil,” such as Pyrolysis oil, as potential fuel source. Pyrolysis oil is extracted from biomass. As it contains carbon, hydrogen and oxygen atoms, many people have considered Pyrolysis oil as a potential hydrocarbon fuel.
However, bio-oil has many properties that make it difficult to use as a fuel. Some of these properties include its low heating value, incomplete volatility, acidity, instability, and incompatibility with standard petroleum fuels. Generally, these undesirable properties of pyrolysis oil result from the pyrolysis oil comprising oxygenated organic compounds. In other words, the presence of the oxygen-carbon bonds within these bio-oil molecules renders the bio-oil generally unsuitable for use as a hydrocarbon fuel source. Accordingly, various processes have been developed in an attempt to eliminate the oxygen atoms from the bio-oil, thereby transforming the bio-oil into usable hydrocarbon liquid fuel.
There are generally two (2) types of processes that have been attempted to eliminate oxygen atoms from the bio-oil, namely “hydro-treating” and “catalytic cracking.” In a “hydro-treating” process, the bio-oil compounds are reacted with hydrogen gas at high temperature and high pressure, thereby causing the oxygen atoms in the bio-oil to react with the hydrogen gas and form water. Unfortunately, this requirement for high temperature and high pressure hydrogen results in a process that is not economically viable. In a “catalytic cracking” process, the removal of oxygen atoms from the bio-oil occurs by using shape-selective catalysts which promote the conversion of the oxygen atoms into carbon dioxide (CO2) and water molecules.
There are generally problems associated with both hydro-treating and catalytic cracking. Catalytic cracking is considered to be the less-expensive alternative to hydro-treating. Generally, the catalysts involved in catalytic cracking may be zeolite materials, such as a ZSM5 catalyst, or other catalysts including molecular sieves (SAPOs), mordenite and HY-zeolites. However, the use of such catalysts has been limited because the fuel formed using such catalysts is of low quality.
Recently, a new type of catalytic conversion process for converting bio-oils to fuel has been investigated. This process is referred to as “hydrodeoxygenation” and involves a high temperature, high pressure process in presence of hydrogen and a catalyst to remove the oxygen atoms from the bio-oil molecules. Most of the catalysts used for hydrodeoxygenation are some variations of Co—Mo, Ni—Mo or Fe—Mo impregnated on a support. However, these new types of hydrodeoxygenation catalysts have yet to provide an economical process for upgrading bio-oil molecules into a fuel product.
Accordingly, there is a need in the art for a new type of catalyst and process that will result in an economical upgrading of pyrolysis oil into a fuel product. Such a process and catalyst is disclosed herein.
The present embodiments relate to a new type of catalyst that may be used to upgrade pyrolysis oil. As used hereinthroughout, including the appended claims, the term pyrolysis oil means any bio-oil, including without limitation oil from biomass gasification, by-product oil from the transesterification of biomass, lipids or other oils extracted from biomass, or other oils derived from the treatment of, or extraction from, biomass. These catalysts will generally include a support material, an active metal (such as, for example, copper, nickel, manganese, iron or cobalt), and a zirconia promoter material. The zirconia promoter material may be zirconia itself (ZrO2) or may be zirconia doped with d-block elements such as yttrium, scandium and ytterbium. The support material may be either an acidic support, such as alumina, or it may be a non-acidic support such as carbon, silica-gel, silicalite or even a zeolite material.
The catalysts of the present embodiments may be particularly adept at upgrading bio-oil. For example, the presence of zirconia on the surface of the catalysts improves the dispersion of the active metal (copper) throughout the surface of the catalyst. Such dispersion of copper metal results in smaller “active sites” that are more effective at converting the oxygen atoms in the bio-oil into CO2. Second, doping zirconia with d-block elements leads to a structural oxygen deficiency on the surface of the catalyst, which then will promote a continuous renewal of oxygen atoms to the active site (and hence a higher ability of the catalyst to consistently reduce the oxygen atoms). It can be observed that the oxygen deficiency created is highly ordered and will act as molecular paths for a renewal of oxygen atoms to the surface of the catalyst by carrying oxygen through the matrix to another active site. While at the active site, the oxygen atom will effectively combine with hydrogen atoms to form water. The managed oxygen deficiency on the surface of the catalyst will further enhance the cleavage of C—O bonds preferentially over C—C bond cleavage, thereby further increasing the efficiency of the process.
Referring now to
The obtained quantity of bio-oil 105 is added to a pyrolysis apparatus 112 which may operate to separate the bio-oil 105 into a gas phase 116, char 124 and a liquid phase mixture 120. The liquid phase mixture 120 may include both an organic phase and an aqueous phase. Those skilled in the art will appreciate how to construct a pyrolysis apparatus 112 that is operable to separate out these constituents according to their relative state of matter. Further, those skilled in the art will appreciate how the gas phase 116 and/or the char 124 may be disposed of, re-used, burned as a heat source, etc.
A separation step 130 may be performed on the liquid phase mixture 120. Such a separation process is known in the art and results in an organic phase 140 being removed/separated and an aqueous phase 142. The organic phase 140 may then undergo a bio-oil upgrading process 160 using the catalysts and/or other techniques/materials described herein. This upgrading process results in an upgraded bio-oil product 170. If necessary, the upgraded bio-oil 170 may be further refined 175, processed, etc., in order to obtain better and/or more concentrated fuel product. The aqueous phase 142 may undergo further processing, as known in the art, to regenerate 146 hydrogen gas. If desired, this hydrogen gas that is regenerated may be used in the bio-oil upgrading process 160.
Referring now to
The high pressure may be supplied (at least in part) by hydrogen supply 220. In other words, hydrogen supply 220 may flood the vessel 200 with hydrogen gas 219, thereby providing a quantity of hydrogen gas that may react with the organic phase during the upgrading process. Other methods of increasing the pressure within the vessel 200, such as using nitrogen or an inert gas, may also be used. Obviously, the vessel 200 may be heated in order to achieve the reaction temperatures associated with the upgrading process.
In order to perform the upgrading process 160, a quantity of the organic phase 140 of the pyrolysis oil is added to the vessel 206. In some embodiments, this organic phase may be mixed with a solvent such as tetralin to form a reaction mixture 217. Of course, other solvents may also be used in the reaction mixture 217. In other embodiments, the reaction mixture 217 does not include a solvent and is made up, almost exclusively, of the organic phase 140.
It should be noted that, in some embodiments, the aqueous phase 142 of the pyrolysis oil is not added to the vessel 200. Rather, the aqueous phase 142 of the pyrolysis oil has already been separated out from the organic phase 140. This may be important because water soluble components, such as Na, Mg and Ca, have been separated from the organic phase, thereby reducing the possibility of such materials poisoning the catalyst. Such prior separation of the aqueous phase may also mitigate corrosion of the catalyst.
Once the reaction mixture 217 is within the vessel 217, the mixture 217 may be stirred (through methods known in the art), heated and pressurized in order to promote the reaction that will upgrade the pyrolysis oil. As noted above, such upgrading of the pyrolysis oil involves removing oxygen atoms from the bio-oil. In order to perform this reaction a catalyst 222 may be used. This catalyst 222 may be loaded in a catalyst basket 210, as shown in
The catalyst 222 that may be used in the present embodiments will now be described. Specifically, a schematic of the catalyst 222 according to the present embodiments is shown in
In addition to a support material 330, the catalyst 222 may include an active metal 340. The active metal 340 may be positioned on the surface of the catalyst 222 and facilitates the upgrading reaction. In some embodiments, the active metal 340 may be selected from the group consisting of copper, iron, manganese, nickel and cobalt. In some embodiments, the active metal 340 is copper.
Further, the catalyst 222 may also include a zirconia promoter material 350. This zirconia promoter material 350 may also be positioned on the surface of the catalyst 222 proximate the active metal 340. The zirconia promoter material 350 will comprise zirconia (ZrO2). In some embodiments the zirconia promoter material 350 may be pure zirconia. In other embodiments, the zirconia promoter material 350 may be zirconia that has been doped with a d-group metal such as Sc, Y, or Yb. Thus, the zirconia promoter material may be selected from the group consisting of zirconia, zirconia doped with Y, zirconia doped with Sc and zirconia doped with Yb.
It should be note that, in some embodiments, the use of zirconia doped with d-block elements in the catalyst may be desirable. Specifically, the d-block doped zirconia may be used as a promoter for transition metal catalyst (i.e., the active metal). This catalysis scheme may have two distinct merits. First, the presence of zirconia on the surface may improve copper dispersion. In other words, smaller sites (which are promoted by the presence of zirconia with the copper) have been demonstrated to be more effective at carbon (CO2) reduction, thereby improving the performance of the catalyst. Second, zirconia doping with d-block elements may lead to a structural oxygen deficiency on the surface of the catalyst, which then will assist with continuous renewal of oxygen to the active site on the catalyst, and hence higher turnover frequency and a greater ability of the catalyst to react with oxygen atoms. It can be observed that the oxygen deficiency created is highly ordered and will act as molecular paths for surface renewal by carrying oxygen through the matrix to another active site (where the oxygen will effectively combine with hydrogen to form water). The managed oxygen deficiency will further enhance the cleavage of C—O bonds preferentially over C—C bond cleavage thereby further increasing the energy efficiency of the process.
In the embodiment shown in
Referring now to
Examples of the particular catalysts that may be formed include: Cu—ZrO2—Y2O3—Al2O3 and Cu—ZrO2—Al2O3
Carbon dioxide has been used as model compound to test the present catalysts due to its “highly oxidized state.” It is believed that a catalyst scheme effective at reducing CO2 efficiently in presence of hydrogen will also be highly active for oxygen removal from other less oxygenated compounds such as pyrolysis oil.
Copper, zirconia and Yttria were used in formulation of three different catalysts. The catalysts were synthesized using incipient wetness method. Alumina pellets procured from CoorsTek (180 m2/g, gamma) were ground to 150-250 micron range. The ground alumina was dried overnight at 100° C. Upon cooling, alumina was impregnated with zirconium nitrate then dried overnight at 100° C. followed by calcination at 400° C. for four hours. The resulting material was impregnated with copper nitrate using the same procedure. The final catalyst (Cu—ZrO2—Al2O3) was stored in a glass vial. The catalyst composition from the impregnated concentrations was calculated to be 10% Cu-1% Zr. Similar procedure was followed to prepare Cu—ZrO2—Y2O3—Al2O3, the only difference being, zirconium nitrate solution was pre-mixed with Yttrium nitrate in a 100:8 ratio. To prepare the third catalyst, co-precipitated Yttria doped zirconia (10 m2/gm area) was impregnated with Cu followed by drying and calcinations. The Cu-YDZ (Yttria doped zirconia) catalyst was mixed with Cu—ZrO2—Y2O3—Al2O3 in a 1:1 ratio (1:18 active sites). All the three catalysts were tested at 250° C., 200 CC/min net flow rate, 4:1 hydrogen to CO2 ratio. Change in carbon dioxide concentration was measured using Varian MicroGC. The results of CO2 reduction are summarized in the Table below. Carbon monoxide and methanol were observed as products of CO2 reduction.
As seen from the foregoing Table, it can be concluded that addition of Yttria to the zirconia promoter, results into order of magnitude higher conversion. These results support the hypothesis of creating oxygen-deficient promoter structure to enhance reduction of highly oxidized species by efficient oxygen removal. Further addition of Yttria-doped-zirconia to the Y—Zr promoted catalyst results in further increased conversion, and thus further asserting the hypothesis.
The present invention may be embodied in other specific forms without departing from its spirit or essential characteristics. The described embodiments are to be considered in all respects only as illustrative and not restrictive. The scope of the invention is, therefore, indicated by the appended claims rather than by the foregoing description. All changes which come within the meaning and range of equivalency of the claims are to be embraced within their scope.
This application claims the benefit of U.S. Provisional Patent Application Ser. No. 61/493,099 filed Jun. 3, 2011, entitled “Bio-Oil Upgrading Process.” This provisional application is expressly incorporated herein by reference.
| Number | Date | Country | |
|---|---|---|---|
| 61493099 | Jun 2011 | US |
