Our IP
Below is our published intellectual property. The portfolio is evolving as our research is progressing. Please check WIPO Patentscope or a similar search tool for the most up to date information.
The hydrocarbon feed enters a reactor with a proprietary zeolite-based catalyst. The reactor contains at least two reaction zones, separated by a zone and implements for mixing the products of the previous reaction zone with an oxygenate and olefin-containing co-feed. The reactor effluent is separated into gasoline blendstock, reaction water and the off gas. The results are: (1) increased RON the produced gasoline; (2) reduced content of compounds with high melting points and prone to crystallization, e.g. durene or 2,6-dimethylnaphthalene; (3) reduced content of benzene; (4) increased yield of the produced gasoline.
The group of inventions relates to a process of co-converting hydrocarbon feedstock with a high content of unsaturated hydrocarbons and aliphatic alcohols into components of high octane gasolines or aromatic hydrocarbons, as well as to catalysts of such a co-conversion. The method of co-converting hydrocarbon fractions and oxygenates into high octane components of fuels or aromatic hydrocarbons includes contacting a hydrocarbon stream with oxygenates over a proprietary catalyst under a certain pressure and temperature. The catalyst contains the HZSM-5 zeolite that passed thermal and steam treatment. The invented composition of the catalyst allows (1) conversion at high temperatures, (2) resistance to water vapor, at the same time providing (3) increased catalyst cycle length that may otherwise be shortened by feedstocks like pyrolysis gasoline, oligomer-gasoline and catalytically cracked gasoline with high olefin content.
The feed passes through two consecutive reaction units containing a proprietary pentasil zeolite catalyst. The effluent is separated into liquid and gas fractions, and the latter is fed back to the reaction units. The gas fraction is separated into a hydrogen-rich gas (HRG) and light naphtha including olefins; the HRG is fed into an oxygenate synthesis unit. The resultant oxygenates return to both reaction units while the light naphtha with olefins is fed only to the inlet of the first reaction unit. The invention (1) improves the efficiency of producing concentrates of aromatic hydrocarbons and (2) increases the yield of alkylbenzenes, especially xylenes.
The feed, including methanol, is heated in a mixer and then enters a reactor where it is converted into aromatic hydrocarbons in the presence of a catalyst. The effluent is separated into liquid and gas; the gas is recirculated into the mixer, and the liquid is additionally separated into liquid hydrocarbons and water. The hydrocarbon liquids enter a rectification column to be separated into an aromatic hydrocarbon concentrate and reflux which is recirculated to the mixer, and the water is removed. The composition of the liquid aromatic hydrocarbons, which are fed into the rectification column, is measured. Depending on result, the flow rate of the feed to the mixer is adjusted, as can be the temperature of the rectification column. The result is an increased efficiency of producing concentrates of aromatic hydrocarbons with elevated content of alkylbenzenes, particularly xylenes.
Synthesis gas (syngas) made with natural gas in a syngas production unit is subsequently converted into methanol. Then the methanol is converted into aromatic hydrocarbons in the presence of a proprietary catalyst in two consecutive reactors: (1) low-temperature isothermal reactor for synthesizing aromatic and aliphatic hydrocarbons, and (2) high-temperature adiabatic reactor for synthesizing aromatic and aliphatic hydrocarbons from aliphatic hydrocarbons formed in the first reactor. The effluent from the second reactor enters a separation and stabilization unit, where water is removed and liquid hydrocarbons are separated from gas. Hydrogen-rich gas from the stabilization unit is recirculated to syngas unit to adjust the H2:CO ratio therein to 1.8-2.3:1 and make the syngas by autothermal reforming. The result is an increased efficiency of producing concentrates of aromatic hydrocarbons.
The C3-C4 hydrocarbon gases, light low-octane hydrocarbons and oxygenates (C1-C3 aliphatic alcohols) and/or mixtures thereof are converted into aromatic hydrocarbons over the proprietary catalyst. The catalyst is a mechanical mixture of two zeolites, the first of which has the SiO2/Al2O3 ratio of 20, pre-treated with an aqueous alkali solution and modified with oxides of rare-earth elements at 0.5 to 2.0 wt.%. The second zeolite has the SiO2/Al2O3 ratio of 82. It has residual sodium oxide at 0.04wt.%, and is modified with magnesium oxide at 0.5 to 5.0 wt.%. The zeolites are used in the weight ratio from 1.7:1 to 2.8:1, and the binder, at 20-25% of the weight of the catalyst, includes silicon oxide. The conversion process with the proposed catalyst occurs in an isothermal reactor without recirculation of the gases from the separation stage, by contacting gaseous feedstock (evaporated and heated in a preheater) with a fixed bed of the catalyst. The results are (1) a higher yield of aromatic hydrocarbons with (2) an almost complete conversion of the hydrocarbon feed and oxygenates, (3) an increased selectivity towards xylenes, and (4) a simplification of the process by using a reduced pressure.
