An H.sub.2-rich fuel gas production plant comprising a syngas production unit can be advantageously integrated with an olefins production plant comprising a steam cracker in at least one of the following: (i) fuel gas supply and consumption; (ii) feed supply and consumption; and (iii) steam supply and consumption, to achieve considerable savings in capital and operational costs, enhanced energy efficiency, and reduced CO.sub.2 emissions, compared to operating the plants separately.

The present disclosure relates to systems and methods useful for power production. In particular, a power production cycle utilizing CO.sub.2 as a working fluid may be configured for simultaneous hydrogen production. Beneficially, substantially all carbon arising from combustion in power production and hydrogen production is captured in the form of carbon dioxide. Further, produced hydrogen (optionally mixed with nitrogen received from an air separation unit) can be input as fuel in a gas turbine combined cycle unit for additional power production therein without any atmospheric CO.sub.2 discharge.

A process for producing syngas that uses the syngas product from an oxygen-fired reformer to provide all necessary heating duties, which eliminates the need for a fired heater. Without the flue gas stream leaving a fired heater, all of the carbon dioxide produced by the reforming process is concentrated in the high-pressure syngas stream, allowing essentially complete carbon dioxide capture.

A process for producing syngas that uses the syngas product from a partial oxidation reactor to provide all necessary heating duties, which eliminates the need for a fired heater. Soot is removed from the syngas using a dry filter to avoid a wet scrubber quenching the syngas stream and wasting the high-quality heat. Without the flue gas stream leaving a fired heater, all of the carbon dioxide produced by the reforming process is concentrated in the high-pressure syngas stream, allowing essentially complete carbon dioxide capture.

There is disclosed a furnace (10), a fluid feed component, a fluid reforming system, and a method of reforming a fluid (20). The furnace (10) comprises a vessel (12) that defines a chamber (14) for holding a body of liquid (16). A fluid inlet (18) is provided for introducing a fluid (20) into the chamber (14) below a level (22) of the body of liquid (16) to cause the fluid (20) to interact with the liquid (16) and to migrate therethrough towards an outlet (24) for discharging a product (26) of the interaction from the chamber (14). A liquid circulation passage (28) is implemented, having a weir (30) which is operatively located near the level of the body of liquid (16), and a port (34) which is located remote from the weir (30) and in fluid (20) communication with the fluid inlet (18) so as to enable the liquid (16) to flow over the weir (30) through the liquid circulation passage (28) and through the port (34).

The present disclosure relates to systems and methods useful for power production. In particular, a power production cycle utilizing CO.sub.2 as a working fluid may be configured for simultaneous hydrogen production. Beneficially, substantially all carbon arising from combustion in power production and hydrogen production is captured in the form of carbon dioxide. Further, produced hydrogen (optionally mixed with nitrogen received from an air separation unit) can be input as fuel in a gas turbine combined cycle unit for additional power production therein without any atmospheric CO.sub.2 discharge.

A hydrocarbon is reacted with water in the presence of a catalyst to form hydrogen, carbon monoxide, and carbon dioxide. Hydrogen is selectively allowed to pass through a hydrogen separation membrane to a permeate side of a reactor, while water and carbon-containing compounds remain in a retentate side of the reactor. An outlet stream is flowed from the retentate side to a heat exchanger. The outlet stream is cooled to form a cooled stream. The cooled stream is separated into a liquid phase and a vapor phase. The liquid phase is flowed to the heat exchanger and heated to form steam. The vapor phase is cooled to form condensed water and a first offgas stream. The first offgas stream is cooled to form condensed carbon dioxide and a second offgas stream. The steam and the second offgas stream are recycled to the reactor.

A hydrogen reforming system includes: a reformer that generates first mixed gas through a reforming reaction between fuel gas and water; a transformer that is fed with the first mixed gas and generates second mixed gas from which carbon monoxide is removed by a water gas shift reaction; a pressure swing adsorption that purifies and separate hydrogen from the second mixed gas generated in the transformer; a heat exchanger that is provided between the reformer and the transformer and between the transformer and the PSA unit to control temperatures of the first mixed gas and the second mixed gas through heat exchange with water; a water feeder that communicates with the heat exchanger and supplies water to the heat exchanger; and a control value that is provided on a line through which water is discharged from the water feeder and adjusts a flow rate of water.

A steam methane reformer (SMR) system includes an outer tube, wherein a first end of the outer tube is closed; an inner tube disposed in the outer tube, wherein a first end of the inner tube is open. A flow channel is defined within the inner tube and an annular space is defined between the outer tube and the inner tube, the flow channel being in fluid communication with the annular space. The SMR system includes a catalytic foam disposed in the annular space between the outer tube and the inner tube, the catalytic foam comprising a catalyst.

A process for producing syngas from pre-treated recovery plastic polymers comprising:

a) gasifying said recovery pre-treated polymers according to the following reaction scheme R1:

[—CH.sub.2—]+H.sub.2O═CO+2H.sub.2;  R1:

b) hydrogenating said pre-treated polymers to higher hydrocarbons and methane by using hydrogen produced in R1, according to the following reaction scheme R3:

[—CH.sub.2—].sub.n+H.sub.2═C.sub.nH.sub.(2n+2)  R3:

wherein n is an integer of from 1 to 3, said reaction being optionally combined with oligomers and olefin formation reactions;
c) steam reforming of methane according to the following reaction scheme R4:

CH.sub.4+H.sub.2O═CO+3H.sub.2;  R4:

and optionally
d) reforming reaction of methane according to the following reaction scheme R5:

CH.sub.4+CO.sub.2=2CO+2H.sub.2;  R5:

said process being carried out in a plant (10), (20), (30), (40), (50) comprising a gasification section (11), (21), (31), (41), (51) and a reforming section (12), (22), (32), (42), (52) comprising a tube bundle (13), (23), (33), (43), (53) provided with a catalyst wherein,
i) said gasification (11), (21), (31) and reforming sections (12),(22), (32) are part of a sole reactive unit (10), (20), (30), or said gasification (41), (51) and reforming section (42), (52) are two physically distinct reactive units (40), (50),
ii) the gasification section (11), (21) or the reactive unit (41) provides respectively the energetical support to the reforming section (12), (22) or to the reforming reactive unit (42), thanks to the exothermic combustion reaction scheme R2:

[—CH.sub.2-]+1.5O.sub.2═CO.sub.2+H.sub.2O;  R2:

or in alternative: the reforming section (