Patent RU-2678980-C1 (RU)
Inventor: MAHER DAVID W
IPC: C07C2/76
Filed: 2016-08-18
Granted: 2019-02-05
Abstract: FIELD: chemistry.SUBSTANCE: invention relates to two variants of the system for producing aromatic hydrocarbons and two variants of the method. One of the options of the system includes: (a) flavouring, configured to (i) receive a specified amount of ≥1 million standard cubic feet per day [MSCFD] (29000 NM3D) of raw materials for flavouring, where the raw material for flavouring includes C2 hydrocarbons and non-aromatic C3 + hydrocarbons and has a predetermined concentration of non-aromatic C2 + hydrocarbons in the range from 15 to 90 mol. % per mole of raw aromatization, and (ii) flavouring (A) at least part of the non-aromatic C3 + hydrocarbons of the raw material for flavouring and (B) at least part of the hydrocarbon C2 raw materials for aromatization with obtaining the outgoing reaction stream containing molecular hydrogen, non-aromatic hydrocarbons and aromatic hydrocarbons; (b) product heat exchanger in fluid communication with the flavouring agent, configured to extract at least the first and second products from the outgoing reaction stream, where the first product includes at least part of the aromatic hydrocarbons leaving the reaction stream and the second product includes a tail gas containing (i) at least part of the molecular hydrogen of the outlet reaction stream; and (ii) at least part of the non-aromatic hydrocarbons of the outlet reaction stream; and (c) raw material pretreatment unit configured for (A) receiving ≥2 MSCFD (57000 NM3D) gaseous raw materials and (B) obtaining raw materials for flavouring from gaseous raw materials, where the gaseous raw materials comprise from 0 to 98 mol. % methane, from 1 to 50 mol. % C2 hydrocarbons and from 1 to 40 mol. % non-aromatic C3 + hydrocarbons, where the installation for pre-processing of raw materials includes (i) at least one heat transfer step with (A) input in the fluid communication with the pipeline for the raw materials and (B) the output, the heat transfer stage is configured to transfer heat from the gaseous raw material in order to condense part of the gaseous raw material at a fixed dew point, and (ii) at least one vapour-liquid separator, where the vapour-liquid separator has an inlet in fluid communication with the heat transfer step, at least one drum-separator and the first and second outputs, where: (A) separator inlet is configured to receive gaseous feedstock and condensed portions from the heat transfer step, (B) drum separator is configured to separate the gaseous feedstock and the condensed portions to produce a bottom stream, including a flavouring feed, and a top stream, including separated gaseous hydrocarbons, (C) first separator outlet is configured to transfer the separated gaseous portion from the pretreatment unit, and (D) second separator outlet is configured to transfer a predetermined amount of flavouring raw material to flavouring, and where (iii) the first stage of heat transfer installation for pre-processing includes at least one heat exchanger in indirect thermal contact with the flow of the refrigerant, (iv) the first heat exchanger is adapted to indirectly transfer the first, second and third parts of heat transferred from the gaseous feedstock, where the first part is transferred to the refrigerant, the second part is transferred to the separated gaseous hydrocarbons and the third part is transferred to the raw material for flavoring, and (v) the second heat transfer stage is configured to remove some heat from the refrigerant flow, where the amount of heat varies by no more than +/-50 %, whereas the condensed part condensed from the gaseous raw material has a volume change of ≤+/-10 %.EFFECT: present invention does not require the adaptation of reactors and related equipment to the composition of a specific C2-C9 hydrocarbon source and can be carried out using standardized modules that are easily transported to remote locations.21 cl, 1 tbl, 3 dwg