An engine system includes an engine configured to combust liquid natural gas and generate an exhaust gas comprising methane; a catalytic reactor coupled downstream of the engine and configured to convert methane into a product through one or more of oxidative coupling of methane (OCM) reaction and steam methane reforming (SMR) reaction; and a recirculation loop configured to recirculate at least a part of the product back to the engine.

The disclosure is directed to a process and an apparatus for providing a feedstock. A gaseous feed stream comprising at least one hydrocarbon is passed to a reforming unit followed by a water gas shift reaction zone to provide a first gaseous stream comprising H.sub.2, CO, and CO.sub.2. The first gaseous stream is fed a hydrogen separation zone to separate it into a hydrogen enriched stream and a second gaseous stream comprising CO, CO.sub.2 and H.sub.2. The second gaseous stream is fed to a CO.sub.2 to CO conversion system to produce a third gaseous stream comprising H.sub.2 and CO having a H.sub.2:CO molar ratio of less than 5:1. The third gaseous stream is fed as the feedstock for a gas fermentation unit to have increased stability and product selectivity.

Systems and methods are provided for using oxycombustion to provide heat within a reverse flow reactor environment. The oxygen for the oxycombustion can be provided by oxygen stored in an oxygen storage component in the reactor. By using an oxygen storage component to provide the oxygen for combustion during the regeneration step, heat can be added to a reverse flow reactor while reducing or minimizing addition of diluents and while avoiding the need for an air separation unit. As a result, a regeneration flue gas can be formed that is substantially composed of CO.sub.2 and/or H.sub.2O without requiring the additional cost of creating a substantially pure oxygen-containing gas flow.

According to this disclosure, there is provided a pyrolysis reaction system and a direct non-oxidative methane coupling process using the same by which it is possible to reach the selectivity for good C.sub.≤10 hydrocarbons and at the same time to inhibit coke from being generated while a good methane conversion is maintained during direct conversion of methane into C.sub.2+ hydrocarbons through non-oxidative pyrolysis.

What is proposed is a process and a plant for parallel production of methanol and ammonia by heterogeneously catalyzed reaction of hydrogen and carbon oxides on the one hand and hydrogen and nitrogen on the other hand. This includes producing a raw synthesis gas stream and dividing it into two portions. A first raw synthesis gas substream is used as input for a methanol synthesis to obtain raw methanol and a methanol synthesis purge stream. A second raw synthesis gas substream is subjected to a CO conversion, a carbon dioxide separation and a liquid nitrogen scrubbing and then sent to an ammonia synthesis. According to the invention at least a portion of the methanol synthesis purge stream is sent to the ammonia synthesis and at least one substream obtained from the second raw synthesis gas substream is passed to the methanol synthesis.

A synthesis gas plant for producing synthesis gas, said synthesis gas plant including an electrically heated reforming reactor system including a first catalyst active for catalyzing steam methane reforming reaction, said electrically heated reforming reactor system being arranged to receive a feed gas comprising hydrocarbons and outletting a first synthesis gas stream. The synthesis gas plant also includes a post converter downstream the electrically heated reforming reactor system, said post converter housing a second catalyst active for catalyzing steam methane reforming/methanation reactions and reverse water gas shift reaction, said post converter being arranged to receive at least part of said first synthesis gas stream and outletting a second synthesis gas stream. Furthermore, the synthesis gas plant includes means for adding a heated CO.sub.2 rich gas stream to the at least part of the first synthesis gas stream upstream the post converter and/or into the post converter.

A hydrogen reforming system is provided and includes a steam reforming system, a dry reforming system, and a water supply device. The steam reforming system is configured to (i) receive a raw material gas and react the raw material gas with water to generate a first mixed gas containing hydrogen and carbon monoxide, (ii) react the first mixed gas with the water to generate hydrogen and carbon dioxide, and (iii) discharge hydrogen and carbon dioxide. The dry reforming system is configured to (i) receive and react the raw material gas and the carbon dioxide discharged from the steam reforming system to generate a second mixed gas containing hydrogen, (ii) react the second mixed gas with the water to generate hydrogen and carbon dioxide, and (iii) discharge hydrogen and carbon dioxide. The water supply device is configured to supply the water to the steam reforming system and the dry reforming system.

The present disclosure relates to a process and a system for producing synthesis gas. The carbonaceous feedstock is gasified, in the presence of at least one of oxygen and steam, in a first reactor to obtain a gaseous mixture comprising H2, CO, CH4, CO2, H2O, tar and char. The gaseous mixture is treated in a second reactor, in the presence of a catalyst, to obtain synthesis gas. The system comprises a first reactor, a connecting conduit, a second reactor, at least one cyclone separator, at least one heat exchanger and at least one synthesis gas filter unit. The process and the system of the present disclosure are capable of producing synthesis gas with comparatively higher conversion of the unreacted char.

A system for producing CO and CO.sub.2 to achieve an efficient oil recovery operation having de minimis undesirable gaseous emissions is provided. The system includes a portable CO producing device and a portable CO.sub.2 producing device located proximate to the reservoir and a gas collecting device configured to receive CO and CO.sub.2 and selectively distribute a desired ratio of CO and CO.sub.2 dynamically based on current reservoir conditions. Producing CO.sub.2 proximate to the reservoir comprises reforming carbon based fuel within oxygen. Electrical energy generated is used to selectively distribute the desired ratio of CO/CO.sub.2 to the reservoir with de minimis greenhouse gases produced transmitted into the atmosphere. The system is an energy efficient arrangement that recycles and reuses by-products and unused products from the process. Greenhouse gas emissions are significantly reduced compared to conventional processes by-products are fully utilized. Hydrogen produced can be used to generate electricity, as can heat generated from other sources within the process.

Provided is a hydrogen supply system that supplies hydrogen. The hydrogen supply system includes: a dehydrogenation reaction unit that subjects a raw material including a hydride to a dehydrogenation reaction to obtain a hydrogen-containing gas; a hydrogen purification unit that removes a dehydrogenation product from the hydrogen-containing gas obtained in the dehydrogenation reaction unit to obtain a purified gas including high-purity hydrogen; and a degassing unit that removes an inorganic gas contained in the raw material on an upstream side of the dehydrogenation reaction unit in a flow of the raw material.