Disclosed is a catalyst capable of producing an olefin from an alkyl halide, the catalyst comprising a silicoaluminophosphate (SAPO) having a chabazite zeolite structure with the following chemical composition (Si.sub.xAl.sub.yP.sub.z)O.sub.2, where x, y, and z represent the mole fractions of silicon, aluminum, and phosphorus, respectively, present as tetrahedral oxides, x is 0.01 to 0.30 and the sum of x+y+z is 1, and where the catalyst comprises silicon tetrahedral oxides that are connected with three or less aluminum tetrahedral oxide as shown by .sup.29Si magic angle spinning (MAS) nuclear magnetic resonance (NMR) spectroscopy peak(s) with peak(s) maxima between −93 ppm and −115 ppm.

A phosphorous modified zeolite (A) can be made by a process that includes selecting a zeolite, steaming the zeolite, leaching the zeolite, separating solids from liquid, and calcining. An olefin product can be made from an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock by contacting the feedstock with the phosphorous modified zeolite (A) in an XTO reactor under conditions effective to convert at least a portion of the feedstock to olefin products. The XTO reactor effluent can include light olefins and a heavy hydrocarbon fraction. The light olefins can be separated from the heavy hydrocarbon fraction. The heavy hydrocarbon fraction can be contacted in an OCP reactor at conditions effective to convert at least a portion of the heavy hydrocarbon fraction to light olefins.

A phosphorous modified zeolite (A) can be made by a process that includes selecting a zeolite, steaming the zeolite, leaching the zeolite, separating solids from liquid, and calcining. An olefin product can be made from an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock by contacting the feedstock with the phosphorous modified zeolite (A) in an XTO reactor under conditions effective to convert at least a portion of the feedstock to olefin products. The XTO reactor effluent can include light olefins and a heavy hydrocarbon fraction. The light olefins can be separated from the heavy hydrocarbon fraction. The heavy hydrocarbon fraction can be contacted in an OCP reactor at conditions effective to convert at least a portion of the heavy hydrocarbon fraction to light olefins.

A phosphorous modified zeolite (A) can be made by a process that includes selecting a zeolite, steaming the zeolite, leaching the zeolite, separating solids from liquid, and calcining. An olefin product can be made from an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock by contacting the feedstock with the phosphorous modified zeolite (A) in an XTO reactor under conditions effective to convert at least a portion of the feedstock to olefin products. The XTO reactor effluent can include light olefins and a heavy hydrocarbon fraction. The light olefins can be separated from the heavy hydrocarbon fraction. The heavy hydrocarbon fraction can be contacted in an OCP reactor at conditions effective to convert at least a portion of the heavy hydrocarbon fraction to light olefins.

The present application relates to methods for the reduction of halogenated hydrocarbons using compounds of Formula (I): ##STR00001##
wherein the reduction of the halogenated compounds is carried out, for example, under ambient conditions without the need for a transition metal containing co-factor. The present application also relates to methods of recovering precious metals using compounds of Formula (I) that are absorbed onto a support material.

The present application relates to methods for the reduction of halogenated hydrocarbons using compounds of Formula (I): ##STR00001##
wherein the reduction of the halogenated compounds is carried out, for example, under ambient conditions without the need for a transition metal containing co-factor. The present application also relates to methods of recovering precious metals using compounds of Formula (I) that are absorbed onto a support material.

This method for producing a fullerene derivative is a method for producing a fullerene derivative having a partial structure shown by formula (1) by reacting a predetermined halogenated compound and two carbon atoms adjacent to each other for forming a fullerene skeleton in a mixed solvent of an aromatic solvent and an aprotic polar solvent having a C═O or S═O bond in the presence of at least one metal selected from the group comprising manganese, iron, and zinc;

##STR00001##

(in formula (1), C* are each carbon atoms adjacent to each other for forming a fullerene skeleton, A is a linking group having 1-4 carbon atoms for forming a ring structure with two C*, in which a portion thereof may be a substituted or condensed group).

This method for producing a fullerene derivative is a method for producing a fullerene derivative having a partial structure shown by formula (1) by reacting a predetermined halogenated compound and two carbon atoms adjacent to each other for forming a fullerene skeleton in a mixed solvent of an aromatic solvent and an aprotic polar solvent having a C═O or S═O bond in the presence of at least one metal selected from the group comprising manganese, iron, and zinc;

##STR00001##

(in formula (1), C* are each carbon atoms adjacent to each other for forming a fullerene skeleton, A is a linking group having 1-4 carbon atoms for forming a ring structure with two C*, in which a portion thereof may be a substituted or condensed group).

Production apparatus of triptane includes: carbon dioxide recovery unit configured to recover carbon dioxide from air; hydrogen generation unit configured to electrolyze water by renewable electricity to generate hydrogen; carbon monoxide generation unit configured to generate carbon monoxide from recovered carbon dioxide and hydrogen generated; methanol generation unit configured to generate methanol from carbon monoxide generated and hydrogen generated; acetic acid generation unit configured to generate acetic acid by reacting methanol generated with recovered carbon dioxide or with carbon monoxide generated; acetone generation unit configured to generate acetone and carbon dioxide from acetic acid generated; pinacolone generation unit configured to generate pinacolone from acetone generated; Grignard reagent generation unit configured to generate Grignard reagent from methanol generated; trimethyl butanol generation unit configured to generate 2,3,3-trimethyl-2-butanol by reacting pinacolone generated with Grignard reagent generated; and triptane generation unit configured to generate 2,2,3-trimethylbutane from 2,3,3-trimethyl-2-butanol generated.

Production apparatus of triptane includes: carbon dioxide recovery unit configured to recover carbon dioxide from air; hydrogen generation unit configured to electrolyze water by renewable electricity to generate hydrogen; carbon monoxide generation unit configured to generate carbon monoxide from recovered carbon dioxide and hydrogen generated; methanol generation unit configured to generate methanol from carbon monoxide generated and hydrogen generated; acetic acid generation unit configured to generate acetic acid by reacting methanol generated with recovered carbon dioxide or with carbon monoxide generated; acetone generation unit configured to generate acetone and carbon dioxide from acetic acid generated; pinacolone generation unit configured to generate pinacolone from acetone generated; Grignard reagent generation unit configured to generate Grignard reagent from methanol generated; trimethyl butanol generation unit configured to generate 2,3,3-trimethyl-2-butanol by reacting pinacolone generated with Grignard reagent generated; and triptane generation unit configured to generate 2,2,3-trimethylbutane from 2,3,3-trimethyl-2-butanol generated.