A number of variations may include a product including a fluid additive including at least one asphaltene dispersant/inhibitor including a branched dendritic core and at least one carboxylic acid moiety.

A two-step process for the oligomerization and hydration of a mixed butenes feed is provided and is implemented in a two-stage system. The two-step process yields a product consisting of diisobutenes (DIBs) and mixed butanols. The DIBs are produced via the selective oligomerization of isobutene in a first stage and the mixed butanols are produced via the hydration, in a second stage, of mixed butenes that remain unreacted in the first stage.

The invention relates generally to a charcoal ignition fluid that is composed of a cellulose ether polymer, butanol, and water. The charcoal ignition fluid has performance characteristics similar to petroleum distillate but is more sustainable. Additionally, the charcoal ignition fluid can include ethanol and/or an alcohol to reduce the water content. Moreover, the charcoal ignition fluid can include an acetate salt to increase the visible flame for safety purposes. The charcoal ignition fluid may also include an organic ester to enhance the odor of the ignition fluid.

A compression ignition engine fuel includes 98.0% to 99.9% by weight of methanol and 0.01% to 2.0% by weight of an alkyl nitrate or mixture of alkyl nitrates.

In a method of enhancing the dry grinding efficiency of petcoke including adding additives to the petcoke and dry grinding the petcoke together with the additives. The additives may include a combination of at least one organic additive and at least one inorganic additive.

A diesel fuel substitute composition includes an alcohol, an acetal, and an additive comprising a component selected from the group consisting of C.sub.3-8 dialkyl ethers, alkylated phenols, RNO.sub.2, and combinations thereof. A method for forming the diesel fuel substitute is also provided.

A process for generating a main fuel composition comprising methanol and water and not more than 20% by weight dimethyl ether, and a fumigant comprising dimethyl ether, the process comprising: providing a pre-fuel composition comprising methanol and dimethyl ether, adding water to the pre-fuel composition to cause or aid evaporation of at least a portion of the dimethyl ether from the pre-fuel composition, collecting the portion of dimethyl ether evaporated from the pre-fuel composition for use as a fumigant, and using the remainder of the pre-fuel composition comprising methanol and water as a main fuel composition. The water may be at a temperature above ambient.

The present invention provides a process for preparing a branched ester, comprising reacting a branched primary alcohol composition, having from 8 to 28 carbon atoms and an average number of branches per molecule of from 0.7 to 3.0, said branching comprising methyl and ethyl branches, with an acid. In another aspect, the invention provides a process for preparing a branched ester, pour point depressants for use in fuels, and the use of a branched primary alcohol composition.

A diesel fuel substitute composition includes an alcohol, an acetal, and an additive comprising a component selected from the group consisting of C.sub.3-8 dialkyl ethers, alkylated phenols, RNO.sub.2, and combinations thereof. A method for forming the diesel fuel substitute is also provided.

The disclosure provides a gasification process for the production of a methane-rich syngas at temperatures exceeding 400 C. through the use of an alkali hydroxide MOH, using a gasification mixture comprised of at least 0.25 moles and less than 2 moles of water for each mole of carbon, and at least 0.15 moles and less than 2 moles of alkali hydroxide MOH for each mole of carbon. These relative amounts allow the production of a methane-rich syngas at temperatures exceeding 400 C. by enabling a series of reactions which generate H.sub.2 and CH.sub.4, and mitigate the reforming of methane. The process provides a methane-rich syngas comprised of roughly 20% (dry molar percentage) CH.sub.4 at temperatures above 400 C., and may effectively operate within an IGFC cycle at reactor temperatures between 400-900 C. and pressures in excess of 10 atmospheres.