Catalytic Partial Oxidation for Synthesis Gas Production
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Solution Overview
Problem
Current methods for producing synthesis gas and hydrogen from liquid hydrocarbons, such as Steam Reforming and non-catalytic Partial Oxidation, face challenges with high energy consumption, investment costs, and limited flexibility in using various hydrocarbon feedstocks, especially those containing sulfurated and nitrogenous compounds, and are inefficient in producing hydrogen from heavy or extra-heavy oils.
Innovation Solution
A catalytic partial oxidation process that nebulizes and vaporizes liquid hydrocarbon streams using a gaseous propellant, followed by a catalytic reaction with structured catalytic beds, allowing for flexible use of different hydrocarbon feedstocks and reducing energy and investment costs by controlling temperature and oxygen consumption.
Engineering Contradictions & Design Principles
Engineering Contradiction Analysis
1Productivity
If Steam Reforming or non-catalytic Partial Oxidation is used to produce synthesis gas from liquid hydrocarbons, then synthesis gas production is achieved, but energy consumption and investment costs are high
Solution Approach 1:
A catalytic bed with structured catalyst is introduced as an intermediary between the hydrocarbon feedstock and the reforming process. The catalyst facilitates the partial oxidation reaction, enabling synthesis gas production at lower temperatures and with reduced energy input compared to conventional Steam Reforming or non-catalytic Partial Oxidation methods
Solution Approach 2:
The process operates at lower temperatures and pressures compared to traditional methods by utilizing catalytic action. The structured catalyst modifies the reaction parameters, allowing efficient synthesis gas production under milder conditions that reduce energy consumption and equipment investment costs
2Adaptability or versatility
If non-catalytic Partial Oxidation is used to process heavy hydrocarbon residues, then synthesis gas can be produced from low-quality feedstocks, but oxygen consumption is high and temperatures reach about 1,400°C
Solution Approach 1:
The structured catalyst acts as an intermediary that enables the partial oxidation of heavy hydrocarbon residues at lower oxygen concentrations. The catalyst promotes the reaction efficiency, allowing versatile feedstock processing while significantly reducing oxygen consumption compared to non-catalytic methods
Solution Approach 2:
The catalytic process changes the operating parameters by conducting the reaction at lower temperatures (avoiding 1,400°C) and lower oxygen partial pressures. This maintains the ability to process diverse feedstocks including heavy residues while reducing oxygen consumption and energy input
3Productivity
If catalytic beds with conventional catalysts are used, then synthesis gas production is achieved, but carbonaceous residues form and catalyst deactivation occurs
Solution Approach 1:
The structured catalyst is composed of multiple components with complementary functions: active catalytic sites for promoting partial oxidation, and structural components that provide mechanical strength and resistance to carbon deposition. This composite structure maintains catalyst stability and prevents deactivation while ensuring continuous synthesis gas production
Solution Approach 2:
The structured catalyst utilizes porous materials with controlled pore sizes and distributions. The porous structure facilitates reactant access to active sites while preventing carbonaceous residue accumulation through appropriate pore design, thereby maintaining catalyst activity and reliability over extended operation periods
Applied Scientific Principles
This section explains which scientific principles are used to turn an abstract innovation direction into a practical engineering solution.
Function Achieved in This Case
This process effectively produces synthesis gas and hydrogen with lower energy and investment costs, improved flexibility in feedstock use, and reduced oxygen consumption, enabling efficient hydrogen production from a wide range of hydrocarbon streams, including those previously unsuitable for traditional methods.
Implementation Method 1
passage through one or more structured catalytic beds with contact times ranging from 0.01 to 100 ms, thereby promoting the partial oxidation reactions
Implementation Method 2
The liquid hydrocarbon stream is mixed with a stream of a gaseous propellant selected from gaseous hydrocarbons and/or vapour and is then nebulized/vaporized
Data Source
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AI summary
A process is described for producing synthesis gas and hydrogen starting from liquid hydrocarbon feedstocks, possibly also mixed with gaseous hydrocarbon streams, comprising at least the following operations: 1) nebulizing/vaporizing a stream of a liquid hydrocarbon feedstock consisting of one or more of the following hydrocarbons: naphthas, various kinds of gas oils, such as LCO, HCO and VGO, other products of refining cycles and oil up-grading, such as DAO, other heavy residues, at a temperature ranging from 50 to 500?C and a pressure of 2 to 50 atm, the nebulization also being effected with the help of a gaseous propellant, possibly with the addition of CO2, selected from vapour and/or a gaseous hydrocarbon and resulting in the formation of a nebulized/ vaporized liquid hydrocarbon stream; 2) mixing the nebulized/vaporized liquid hydrocarbon stream coming from phase 1) with: a) an oxidizing stream, possibly mixed with vapour, b) possibly a gaseous hydrocarbon stream at a temperature ranging from 50 to 500?C and a pressure of 2 to 50 atm, with the formation of a possibly biphasic liquid-gas reaction mixture; 3) passing the reaction mixture coming from phase 2) through at least a first structured catalytic bed with the formation of a mixture of reaction products comprising H2 and CO, said structured catalytic bed comprising a catalytic partial oxidation catalyst, arranged on one or more layers, the reaction mixture flowing through each of the layers with a contact time varying from 0.01 to 100 ms, preferably from 0.1 to 10 ms; 4) cooling the mixture of reaction products coming from phase 3). The relative equipment for effecting said process is also described.