A liquid desiccant system including a high desorber, a low desorber, and an absorber that are in fluid communication with a working solution, where the high desorber provides rejected water vapor from the working fluid for condensation in a condenser of the low desorber that provides heat for rejection of additional water from the working solution in the low desorber effectively multiplying the heat provided for desorption. The low desorber provided the concentrated working solution to the absorber where water from ambient air is condensed into the concentrated working solution to provide a dilute working solution within a working solution conduit of the absorber that is thermally coupled to an internal cooler of the absorber. In some embodiments, the working solution can be an aqueous solution of at least one ionic liquid.

A process for the production of synthetically produced methane (57)/gaseous and/or liquid hydrocarbons (114, 115, 116, 117). For this purpose, hydrogen (44, 84, 150) from an electrolytic arrangement (41, 81, 151, 159) which is operated by means of regeneratively generated electric energy and carbon dioxide (19, 46, 86) are synthesized in a methane synthesis (FIGS. 2-48) or Fischer-Tropsch synthesis (FIGS. 3-96) or other suitable hydrocarbon synthesis, the carbon dioxide (19, 46, 86) being produced from an air/gas flow (3, 134) by means of a carbon dioxide recovery system (FIG. 1). The carbon dioxide (19, 46, 86) is obtained from the air/gas flow (3, 134) in the carbon dioxide recovery system (FIG. 1) by way of a reversible adsorption process. Also a production system (57) for the production of synthetically produced methane/gaseous and/or liquid hydrocarbons (114, 115, 116, 117), in particular for carrying out the production process according to the invention, comprising an electrolytic arrangement (41, 81, 151, 159) which is operated by means of regeneratively generated electric energy (42, 82, 153) for producing hydrogen (44, 84, 150), a carbon dioxide recovery system (FIG. 1) for producing carbon dioxide (19, 46, 86) from an air/gas flow (3, 134) and a methane (FIG. 2) or Fischer-Tropsch synthesis (FIG. 3) or any other suitable hydrocarbon synthesis for synthesizing hydrogen (44, 84, 150) and carbon dioxide (19, 45, 86) to methane (57)/gaseous and/or liquid hydrocarbons (114, 115, 116, 117).

A method and plant for capturing CO.sub.2 from a CO.sub.2 containing exhaust gas (1), where the exhaust gas is compressed (10) and thereafter cooled (13, 15, 22) before the exhaust gas is introduced into an absorber (30), where the exhaust gas is brought in counter-current flow with an aqueous CO.sub.2 absorbent solution (49), to give a lean exhaust gas (31) that is withdrawn from the absorber (30), reheated 22, 13) against incoming compressed exhaust gas, and thereafter expanded (34) and released into the atmosphere (4), where the aqueous CO.sub.2 absorbent solution is an aqueous potassium carbonate solution, and that the steam and CO.sub.2 withdrawn from the regenerator (40) is cooled in a direct contact cooler (61) by counter-current flow of cooling water (62), to generate a gaseous flow (70) of cooled CO.sub.2 and steam that is withdrawn for compression and drying of the CO.sub.2, and a liquid flow (64) of cooling water and condensed steam that is withdrawn and flashed (80), to give a cooled liquid phase (84) that is recycled as cooling water for the direct contact cooler (61) for the withdrawn CO.sub.2 and steam, and a gaseous phase (81) that is compressed (82) and thus heated, and introduced into the regenerator (40) as stripping steam (83).

A packed bed for a heat exchanger may comprise a frame and a first fin layer disposed within the frame. A second fin layer may be disposed within the frame. A first perforated sheet may be disposed between the first fin layer and the second fin layer. A sorbent material may be disposed within a volume of at least one of the first fin layer or the second fin layer.

A continuous solid organic matter pyrolysis polygeneration system and method for using the system is disclosed. The pyrolysis polygeneration system mainly includes a processing system, a drying furnace, a pyrolysis furnace, a cooling furnace, a tail gas treatment system, and a gas treatment system and a protective gas circulation system cooperate with each other to realize the multi-level rational utilization of energy, and are suitable for the continuous and rapid pyrolysis and carbonization of various solid organic matter in the actual production. While realizing the polygeneration of coke, wood vinegar and tar, the maximum utilization of overall heat is realized through process optimization.

Systems for generation of liquid water are provided. In embodiments, the systems comprise a thermal desiccant unit comprising a porous hygroscopic material located within a housing including a fluid inlet and a fluid outlet, a working fluid that accumulates heat and water vapor upon flowing from fluid inlet of the housing, through the porous hygroscopic material, and to the fluid outlet of the housing, a condenser comprising a fluid inlet and a fluid outlet for condensing water vapor from the working fluid; an enthalpy exchange unit operatively coupled between the thermal desiccant unit and the condenser, wherein the enthalpy exchange unit transfers enthalpy between the working fluid output from the thermal desiccant unit and the working fluid input to the thermal desiccant unit, and, wherein the enthalpy exchange unit transfers enthalpy between the working fluid output from the condenser and the working fluid input to the condenser.

Various embodiments disclosed herein include a system and method for processing an exhaust gas. The system comprises a regenerative thermal oxidizer (RTO), a bypass flow module in parallel with the RTO, and a mixing module disposed downstream of the RTO; wherein the RTO is configured to oxidize a first part of the exhaust gas and produce a hot tail gas and deliver a predetermined amount of the hot tail gas outside of the RTO, and the mixing module is configured to receive the predetermined amount of the hot tail gas; and wherein the bypass flow module is configured to receive and bypass a second part of the exhaust gas around the RTO into the mixing module; and wherein the second part of the exhaust gas absorbs sufficient heat from the predetermined amount of the hot tail gas in the mixing module for oxidizing and decomposing an organic compound therein.

A system for simultaneous heat recovery and flue gas cleaning, comprising at least one heat pump (300), at least one combined heat recovery and flue gas cleaning unit (1) comprising a heat exchanger (10), said unit having an inlet (20) directing a flow of flue gas into said unit, an outlet (40) for allowing said flow of flue gas to leave said unit, wherein said heat pump is adapted to deliver a flow of cooling media to the heat exchanger at a temperature in the interval of about 4 to about +4 C. This system is compact, efficient and easy to operate. The system can easily be expanded thanks to a modular concept, and it is well suited for mobile applications. A method for heat recovery and flue gas cleaning is also disclosed.

The invention relates to a system for the regenerative thermal oxidation of crude gas, comprising a combustion chamber (29) and a plurality of regenerators (30, 32, 34, 36, 38, 40, 41) which each have a regenerator chamber (42, 44, 46, 48, 50, 52, 54) that communicates with the combustion chamber (29) and contains a heat exchanger (56). The system contains a supply line (58) for feeding crude gas into a crude gas line (60) and has a clean gas line (62) for giving off clean gas, wherein a regenerator chamber (42, 44, 46, 48, 50, 52, 54) of a regenerator (30, 32, 34, 36, 38, 40, 41), in each case independently of the regenerator chambers (42, 44, 46, 48, 50, 52, 54) of the rest of the regenerators (30, 32, 34, 36, 38, 40, 41), can be optionally connected to the crude gas line (60) and separated from the crude gas line (60) via an adjustable crude gas shut-off device (64, 66, 68, 70, 72, 74, 75), as well as optionally connected to the clean gas line (62) and separated from the clean gas line (62) via an adjustable clean gas shut-off device (76, 78, 80, 82, 84, 86, 88). According to the invention, the system comprises a separating device (90) for separating suspended particles in crude gas fed into the crude gas line (60) from the supply line (58).

A hydrocarbon burner for an enclosed environment includes a heat exchanger having a first heat exchanger inlet connected to an inlet of the hydrocarbon burner and a first heat exchanger outlet connected to a heater, and a second heat exchanger inlet connected to a reactor outlet and a second heat exchanger outlet connected to an outlet of the hydrocarbon burner. A reactor includes a reactor inlet, the reactor outlet, and a catalyst mixture disposed in a reactor bed between the reactor inlet and the reactor outlet. The heater connects the first heat exchanger outlet to the reactor inlet. The reactor is a low temperature reactor configured to convert at least one hydrocarbon to at least one of H2O and CO2.