A ship with a flue gas carbon dioxide capture and storage plant has a main engine such as a slow running diesel engine providing flue gas. The flue gas is led via a flue gas heat exchanger with a thermal fluid exit to a re-boiler and arranged for cooling said flue gas. Further cooled flue gas is led into a turbine compressor compressing it up to a compressed flue gas. A combustion chamber is provided with a fuel feed and a pre-mix gas burner for afterburning said compressed flue gas which also burns remaining methane from the diesel engine, resulting in hot afterburned compressed flue gas enriched in CO.sub.2. The CO2-absorber (20) leading said CO.sub.2-enriched absorber solution to a CO.sub.2-stripper (21), operating at e.g. 1 Bar and exporting CO2 to a CO2-compressor (26) to a CO.sub.2-export line (28) to onboard CO.sub.2 pressure tanks.

The present disclosure provides a multiple-compression system and a process for capturing carbon dioxide (CO.sub.2) from a flue gas stream containing CO.sub.2. The disclosure also provides a process for regeneration of the carbon dioxide capture media.

A method, apparatus and system for cooling compressed gases at a well site without the need for fans. Wherein produced liquids act as a continuously-flowing heat sink for gases entering stages of compression. Heat sinks can be automatically bypassed such that gases are compressed without first cooling them based upon outputs of temperature sensors.

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 system for removing carbon dioxide from a carbon dioxide laden gas mixture, the system comprising two groups of carbon dioxide removal structures, each removal structure within each group comprising a porous solid mass substrate supported on the structure and a sorbent that is capable of adsorbing or binding to carbon dioxide, to remove carbon dioxide from a gas mixture, the sorbent being supported upon the surfaces of the porous mass substrate solid; an endless loop support for each of the groups of the removal structures, the endless loop support being so arranged as to move the support structures of each group along a closed curve while being exposed to a stream of the gas mixture; and a sealable regeneration box at one location along each of the endless loop supports, in which, when a porous solid mass substrate is sealed in place therein, carbon dioxide adsorbed upon the sorbent is stripped from the sorbent and the sorbent regenerated; each removal structural supporting a porous substrate in a position to be exposed to a flow of carbon dioxide laden gas mixture so as to allow for the removal of CO.sub.2 from the gas mixture; the number of removal structures to the number of regeneration boxes being directly determined by the ratio of the time to adsorb CO.sub.2, from a base level to desired level on the sorbent, to the time to strip the CO.sub.2 from the desired level back to the base level.

Disclosed herein are methods for treating an exhaust stream comprising NOx, the methods comprising receiving an exhaust stream and combining it with at least one nitrogen-containing reagent to form a combined stream, heating the combined stream to a reaction temperature ranging from about 870 C. to about 1100 C. to react at least a portion of the nitrogen-containing component, cooling the reacted stream in a first cooling step to a first temperature, and optionally further cooling the reacted stream in a second cooling step to a second temperature, wherein the first cooling step comprises heat exchange between at least a portion of the exhaust stream and at least a portion of the reacted stream. Exhaust treatment systems are also disclosed herein.

Wet-type carbon dioxide capturing equipment includes a CO.sub.2 absorption tower where CO.sub.2 of an exhaust gas reacts with an absorbent, a CO.sub.2 stripping tower where CO.sub.2 is separated from a rich solution absorbed the CO.sub.2 in the CO.sub.2 absorption tower, a reboiler for supplying thermal energy to the CO.sub.2 stripping tower to separate the CO.sub.2 from the rich solution in the CO.sub.2 stripping tower, a first heat exchanger for heating the rich solution by exchanging heat between a lean solution having the CO.sub.2 separated therefrom in the CO.sub.2 stripping tower and the rich solution, a mechanical vapor recompressor (MVR) for compressing a CO.sub.2 gas separated in the CO.sub.2 stripping tower, and a second heat exchanger for separating a portion of CO.sub.2 from the rich solution by heating the rich solution by exchanging heat between the CO.sub.2 gas compressed in the MVR and the rich solution passing through the first heat exchanger, in which the rich solution having CO.sub.2 that is not separated in the second heat exchanger is input to the CO.sub.2 stripping tower where the CO.sub.2 is separated.

A method for gas processing, in particular for processing biogas of a biogas plant in which in one method step a membrane process or a reactive process is executed, and in at least one further method step an adsorption and/or absorption process is executed.

The invention relates to contactors suitable for use, for example, in manufacturing and chemical refinement processes. In an aspect is a hybrid indirect/direct contactor for thermal management of counter-current processes, the contactor comprising a vertical reactor column, an array of interconnected heat transfer tubes within the reactor column, and a plurality of stream path diverters, wherein the tubes and diverters are configured to block all straight-line paths from the top to bottom ends of the reactor column.

Embodiments of the present disclosure are directed to systems and methods for regenerating a sorbent material of a scrubber, configured for scrubbing a contaminant from indoor air from an enclosed space. Some embodiments include a sorbent material portion (SMP) including a sorbent material, which may be configured to be cycled between an adsorption phase for adsorbing a contaminant from indoor air, and a regeneration phase configured for releasing at least a portion of the contaminant adsorbed by the sorbent material during the adsorption phase thereof, via temperature swing adsorption, into a purging airflow.