초록 ▼

Embodiments of the present invention provide cost-effective systems and methods for producing a synthesis gas product using a steam reformer system and an ion transport membrane (ITM) reactor having multiple stages, without requiring inter-stage reactant injections. Embodiments of the present invent

Embodiments of the present invention provide cost-effective systems and methods for producing a synthesis gas product using a steam reformer system and an ion transport membrane (ITM) reactor having multiple stages, without requiring inter-stage reactant injections. Embodiments of the present invention also provide techniques for compensating for membrane performance degradation and other changes in system operating conditions that negatively affect synthesis gas production.

대표청구항 ▼

1. A method for producing a synthesis gas product comprising hydrogen and carbon monoxide, comprising the steps of: (a) reacting a reactant gas mixture comprising steam and a hydrocarbon in a reforming reaction in a primary reformer system to form an intermediate gas mixture having a composition com

1. A method for producing a synthesis gas product comprising hydrogen and carbon monoxide, comprising the steps of: (a) reacting a reactant gas mixture comprising steam and a hydrocarbon in a reforming reaction in a primary reformer system to form an intermediate gas mixture having a composition comprising methane, hydrogen, and carbon oxides;(b) introducing at least a portion of the intermediate gas mixture into a membrane oxidation reactor system comprising a plurality of membrane oxidation reactor stages arranged in series including a first membrane oxidation reactor stage and a second membrane oxidation reactor stage in the series, each stage comprising a membrane oxidation reactor and a catalyst, each membrane oxidation reactor comprising a reactant zone, an oxidant zone, and one or more mixed metal oxide membranes separating the reactant zone from the oxidant zone, wherein all of the intermediate gas mixture that is introduced into the membrane oxidation reactor system is introduced into the reactant zone of the first membrane oxidation reactor stage of the plurality of membrane oxidation reactor stages, and wherein each of the reactant zones of the plurality of membrane oxidation reactor stages has an effluent discharged therefrom, wherein at least a portion of the effluent from the reactant zone of the first membrane oxidation reactor stage is introduced into the reactant zone of the second membrane oxidation reactor stage as a feed thereto, and wherein the feed to the reactant zone of the second membrane oxidation reactor stage consists of the at least a portion of the effluent from the first membrane oxidation reactor stage;(c) introducing an oxygen-containing oxidant gas mixture into the oxidant zone of each of the plurality of membrane oxidation reactor stages and permeating oxygen through the one or more mixed metal oxide membranes of each of the plurality of membrane oxidation reactor stages;(d) reacting the at least a portion of the intermediate gas mixture with the oxygen that has permeated through the one or more mixed metal oxide membranes of one or more of the plurality of membrane oxidation reactor stages to form the synthesis gas product;(e) discharging the synthesis gas product as an effluent from the membrane oxidation reactor system;(f) measuring the temperature of the synthesis gas product from the membrane oxidation reactor system; and(g) controlling reaction conditions of the primary reformer system as a function of the measured temperature of the synthesis gas product from the membrane oxidation reactor system. 2. The method of claim 1, wherein step (g) comprises: adjusting an operating temperature of the primary reformer system as a function of the measured temperature of the synthesis gas product from the membrane oxidation reactor system. 3. The method of claim 1, wherein the primary reformer system comprises a fired tubular reformer and step (g) comprises: adjusting at least one of a flow rate and a composition of combustion fuel to the fired tubular reformer as a function of the measured temperature of the synthesis gas product from the membrane oxidation reactor system. 4. The method of claim 1, wherein the primary reformer system comprises at least one of an oxygen-blown reformer, an auto-thermal reformer, and a partial oxidation reactor, and step (g) comprises: adjusting a flow rate of oxygen to the primary reformer system as a function of the measured temperature of the synthesis gas product from the membrane oxidation reactor system. 5. The method of claim 1, wherein step (g) comprises: adjusting at least one of an amount of hydrocarbon contained in the reactant gas mixture, an amount of steam contained in the reactant gas mixture, and a molar ratio of steam-to-carbon contained in the reactant gas mixture. 6. The method of claim 1, wherein step (g) comprises: controlling reaction conditions of the primary reformer system to maintain the measured temperature of the synthesis gas product from the membrane oxidation reactor system while performance of the one or more mixed metal oxide membranes degrades. 7. The method of claim 1, wherein step (g) comprises: controlling reaction conditions of the primary reformer system to maintain the measured temperature of the synthesis gas product from the membrane oxidation reactor system while a production rate of synthesis gas product from the membrane oxidation reactor system is reduced. 8. The method of claim 1, wherein step (g) comprises: controlling reaction conditions of the primary reformer system to maintain the measured temperature of the synthesis gas product from the membrane oxidation reactor system while a production rate of synthesis gas product from the membrane oxidation reactor system is increased. 9. The method of claim 1 wherein the plurality of membrane oxidation reactor stages comprises n membrane oxidation reactor stages, wherein the integer n is greater than or equal to 3, wherein at least a portion of the effluent from the reactant zone of the (k−1)th membrane oxidation reactor stage is introduced into the reactant zone of the kth membrane oxidation reactor stage as a feed thereto where k takes on each integer value from 3 to n, and wherein the feed to the reactant zone of the kth membrane oxidation reactor stage consists of the at least a portion of the effluent from the (k−1)th membrane oxidation reactor stage for each integer k, the kth membrane oxidation reactor stage being arranged serially directly downstream of the (k−1)th membrane oxidation reactor stage. 10. The method of claim 1, wherein the primary reformer system comprises a fired tubular reformer. 11. The method of claim 1, wherein the primary reformer system comprises at least one of an oxygen-blown reformer, an auto-thermal reformer, and a partial oxidation reactor. 12. The method of claim 1 wherein at least one of: (i) the primary reformer system is operated such that the composition of the intermediate gas mixture is essentially at chemical equilibrium with respect to the steam reforming reaction; and(ii) the primary reformer system is operated such that the composition of the at least a portion of the intermediate gas mixture that is introduced into the membrane oxidation reactor system is essentially at chemical equilibrium with respect to the steam reforming reaction. 13. The method of claim 1, wherein the membrane oxidation reactor system is operated such that the composition of the synthesis gas product from the membrane oxidation reactor system is essentially at chemical equilibrium with respect to the steam reforming reaction. 14. The method of claim 1, further comprising: (f) determining a target operating temperature value for the intermediate gas mixture as a function of a measured temperature of the synthesis gas product from the membrane oxidation reactor system; and(g) controlling reaction conditions of the primary reformer system as a function of the target operating temperature value for the intermediate gas mixture.