Integrated method for the production of dimethyl ether from a hydrocarbon gases

 

Usage: petrochemistry. The essence: a comprehensive method for the production of dimethyl ether (DME) from hydrocarbon gases, natural and casing-head gas, containing mainly CH4and other hydrocarbon and non-hydrocarbonaceous gases, comprising three main stages of processing of hydrocarbon gases in DME: (a) obtaining a synthesis gas with a molar ratio of hydrogen (H2) to carbon monoxide (CO), approximately equal to 1.0, according to the method of non-catalytic partial oxidation of hydrocarbon gases with oxygen in high-temperature Converter, with correction of the primary products of partial oxidation due to entry into the reaction zone fluxes of carbon dioxide (CO2) and water vapor (H2On subsequent disposal of the excess enthalpy of the flow of convertible gases at the output of the Converter in steam and hot water boilers; b) synthesis of dimethyl ether from synthesis gas in a reactor using a mixed catalyst for methanol synthesis and dehydration of methanol, with recirculation of the unreacted synthesis gas) fractionation products of synthesis and the production of goods DME with purity not less than 95 wt.%. Technical result: getting cheap fuel DME with a purity of not IU the forge part)to

Claims

1. Integrated method for the production of dimethyl ether (DME) from hydrocarbon gases, natural and casing-head gas, containing mainly of CH4and other hydrocarbon and non-hydrocarbonaceous gases, comprising three main stages of processing of hydrocarbon gases in DME: a) a synthesis gas with a molar ratio of hydrogen (H2) to carbon monoxide (CO), approximately equal to 1.0, according to the method of non-catalytic partial oxidation of hydrocarbon gases with oxygen in high-temperature Converter with correction of the primary products of partial oxidation due to entry into the reaction zone fluxes of carbon dioxide (CO2) and water vapor (H2O), with subsequent recycling of the excess enthalpy of the flow of convertible gases at the outlet of the Converter in steam and hot water boilers; b) synthesis of dimethyl ether from synthesis gas in a reactor using a mixed catalyst for methanol synthesis and dehydration of methanol, with recirculation of the unreacted synthesis gas) fractionation products of synthesis and obtaining trade DME with purity not less than 95 wt.%, in which the process of partial oxidation is performed in a two converte or non-equilibrium combustion of hydrocarbon gas and oxygen with a ratio of the number of moles of oxygen to the number of carbon atoms in the hydrocarbon source gas in the range of 0.6 - 0.8 and at a pressure of 2.0 - 5.5 MPa, with corrective gases introduced into the reaction zone a ramjet combustor, almost without affecting the area of the actual combustion in the boundary layer in this zone or at the outlet of the combustion chamber, when the ratio of the number of moles of CO2and a pair of N2On the number of carbon atoms in the hydrocarbon source gas of 0.6 - 0.8 and 0 - 0.15, respectively, providing a residence time of combustion products of hydrocarbon gas in the oxygen prior to their mixing with threads CO2and a pair of H2Oh, in the range of 0.005-0.05 s, and the residence time of the total flow, including CO2and pairs of N2Oh, before entering the second stage Converter is 0.1-0.2 s, and the second stage of the Converter in the chamber high temperature suacide and correction of composition, made in the form of a nozzle of small particles of refractory material such as Al2O3that will filter the soot, steam gasification and CO2the correction of the composition of the reaction gases by the reaction of water gas to ensure the reaction gases in the volume of the nozzle in the range of 0.1 - 0.5 C.

2. Comprehensive method under item 1, characterized in that the process stage (a) is performed with almost 100% recycling and beneficial use for receipt is onverter, including the heat of condensation of the reaction water formed in the Converter at a partial oxidation and correction of the composition, with the utilization of carry out switching in the path of the converted gas at the outlet of the Converter, in addition to the steam boiler, heat exchanger, end of boiler-heat exchanger with a flow rate of cooling water with a temperature not exceeding 20C, about 10 times larger than the flow rate of water vapor in the cooled converted gas, and is approximately equal to the total water consumption, going to power steam boiler-heat exchanger stage of synthesis gas production and power heat transfer section of the synthesis reactor boiling water.

3. Comprehensive method under item 1, characterized in that the second process stage is the synthesis of dimethyl ether is carried out in horizontal gas-phase reactor with mnogopotochnoy catalytic nozzle at a pressure of 5.0-10.0 MPa, in the temperature range of 250-300C, with successive passage of the synthesis gas and the formed products of the synthesis of all the shelves - sealed catalyst baskets, the total number of which is chosen in the range 4-40, while the reaction gases after passing each basket and prior to their submission to the next basket is cooled in an individual heat exchanger, the

4. Comprehensive method under item 1 or 3, characterized in that the fractionation of the products of synthesis from the output of the reactor is first cooled in a water heat exchanger to a temperature at which when selected pressure is condensed 50 - 90 wt.% water and methanol and not more than 10 wt.% DME contained in the products of synthesis, and which, after separation send in a small distillation unit methanol condensate, from which the methanol solution is directed to the combustion section of the energy supply, and DME is directed to a highway commodity DME, and passed through the separator methanol condensate gas-vapor stream is additionally cooled in a consistent system of heat exchangers, using as a cooler of cold water, cold unreacted synthesis gas from the output of the absorber CO2and supercooled in refrigerating machines DME ranging from +5 to -40C, after which the liquid phase DME and CO2is subjected to rectification in the column average pressure of 3.0 - 4.0 MPa, after which the DME is sent to the highway commodity DME and highway DME absorption CO2and the gas phase outlet of the separator DME and CO2sent to the absorber CO2irrigated supercooled liquid pressure, and the gas flow from the output of the absorber containing unreacted synthesis gas and a small amount of CO2send in the contour of the recycle reactor synthesis gas compressor with intermediate cleaning this thread from CO2using monoethanolamine or without treatment, with all of the selected reaction CO2return in this branch of the synthesis gas.

 

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FIELD: hydrocarbon manufacturing.

SUBSTANCE: natural gas is brought into reaction with vapor and oxygen-containing gas in at least one reforming zone to produce syngas mainly containing hydrogen and carbon monoxide and some amount of carbon dioxide. Said gas is fed in Fisher-Tropsh synthesis reactor to obtain crude synthesis stream containing low hydrocarbons, high hydrocarbons, water, and unconverted syngas. Then said crude synthesis stream is separated in drawing zone onto crude product stream containing as main component high hydrocarbons, water stream, and exhaust gas stream, comprising mainly remained components. Further at least part of exhaust gas stream is vapor reformed in separated vapor reforming apparatus, and reformed exhaust gas is charged into gas stream before its introducing in Fisher-Tropsh synthesis reactor.

EFFECT: increased hydrocarbon yield with slight releasing of carbon dioxide.

7 cl, 3 dwg, 1 tbl, 5 ex

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