Systems of producing hydrogen and biochar from biomass assisted by iron and steel slag extract
Systems of producing hydrogen and biochar from biomass assisted by iron and steel slag extract include: a pretreatment system that the reactants, including the biomass, iron-based catalyst and alkaline reagent, are pretreated and fully mixed at specific ratios in the pretreatment system; thermal reactor that the mixed reactants from the pretreatment device are transferred into and fully reacted in the thermal reactor; a solid residue collector that the solid residue is collected by the solid residue collector at the discharge outlet of the thermal reactor after the reacted mixture is separated; a gas collection system that he generated hydrogen-based gas is collected by the gas collection system from the exhaust port of the thermal reactor.
1. A system of producing hydrogen and biochar from biomass assisted by an iron and steel slag extract, comprising:
a pretreatment system, wherein the pretreatment system is configured to pretreat the biomass, an iron-based catalyst, and an alkaline reagent, and mix the biomass, the iron-based catalyst, and the alkaline reagent at a stoichiometric specific ratio to obtain a mixed reactant, wherein the pretreatment system further comprises:
an iron-based catalyst collecting system, wherein the iron-based catalyst collecting system comprises:
a pre-washing device, wherein industrial solid waste, minerals, or mine tailings are continuously added and fully mixed with an auxiliary reagent and water at a specific ratio into the pre-washing device to obtain a washed slurry;
a reactor, wherein the washed slurry from the pre-washing device is continuously transferred into the reactor by using a pump unit, carbon dioxide is continuously bubbled into the reactor under a specific pressure in order to be fully mixed and reacted with the washed slurry to obtain a treated slurry, and the treated slurry is continuously discharged from the reactor;
a multistage solid-liquid separator, wherein the multistage solid-liquid separator is configured to perform a solid-liquid separation on the treated slurry continuously discharged from the reactor to obtain a filtrate, wherein unreacted solids obtained by the solid-liquid separation are recycled as feedstock into a next stage of reaction and separation; and
a purifier, wherein besides target ions of calcium and magnesium, the filtrate from the multistage solid-liquid separator further contains impurity ions comprising ions, the filtrate from the multistage solid-liquid separator is continuously transferred into the purifier, the impurity ions are removed from the filtrate via a precipitation by physically and/or chemically changing a pH value of the filtrate to obtain an iron-containing precipitate, and the iron-based catalyst is obtained by collecting the iron-containing precipitate; and
an alkaline reagent separation system, wherein the alkaline reagent separation system comprises:
a product preparation unit, wherein the product preparation unit is configured to produce a Ca/Mg-based product based on the filtrate containing the target ions of calcium and magnesium obtained by the multistage solid-liquid separator; and
a thermal decomposition unit, wherein the Ca/Mg based product is calcined and decomposed in the thermal decomposition unit to form a Ca/Mg alkaline reagent;
a thermal reactor, wherein the thermal reactor is configured to allow the mixed reactant to fully react;
a solid residue collector, wherein the solid residue collector is in communication with a discharge outlet of the thermal reactor, and the solid residue collector is configured to collect solid residue produced in a reaction from the thermal reactor; and
a gas collection system, wherein the gas collection system is in communication with an exhaust port of the thermal reactor, and the gas collection system is configured to collect a hydrogen-based gas produced in the reaction from the thermal reactor.
2. The system according to claim 1 , wherein the pretreatment system further comprises a biomass dehydration treatment unit to adjust the moisture content of the biomass.
3. The system according to claim 1 , wherein the pretreatment system is further configured to reduce the iron-based catalyst in the hydrogen at 500° C. for 2 hours.
4. The system according to claim 1 , wherein the biomass and the alkaline reagent are mixed according to the specific stoichiometric ratio, and an amount of the iron-based catalyst added in a reaction is between 5% and 15% by weight of a total mass of the biomass and the alkaline reagent.
5. The system according to claim 1 , wherein the thermal reactor is further configured to fully react the mixed reactant either at 500° C. for 1 hour or at 300° C. for 2 hours.
6. The system according to claim 5 , wherein additional steam is needed for keeping a humidity of a reaction environment between 10% and 30% when the biomass is relatively dry.
7. The system according to claim 1 , wherein the solid residue is a mixture of the biochar, calcium magnesium carbonate, and the iron-based catalyst.
8. The system according to claim 7 , further comprising an iron-making sintering system, wherein the solid residue is mixed with raw materials at a ratio of no more than 30% by weight for a preparation of the raw materials for a sintering and a blast furnace reduction reaction in the iron-making sintering system.
9. The system according to claim 1 , further comprising a gas separation and purification system, wherein the gas separation and purification system is configured to separate and purify the hydrogen-based gas collected by the gas collection system to obtain a high-purity hydrogen product.
10. The system according to claim 1 , further comprising a mixed gas reuse system, wherein the mixed gas reuse system is configured to collect and transfer the hydrogen-based gas into an iron-making blast furnace for a direct iron ore reduction, engaging in a heating reaction and a reduction reaction.
11. The system according to claim 2 , wherein the mixed reactant is fully reacted either at 500° C. for 1 hour or at 300° C. for 2 hours in the thermal reactor.
12. The system according to claim 3 , wherein the mixed reactant is fully reacted either at 500° C. for 1 hour or at 300° C. for 2 hours in the thermal reactor.
13. The system according to claim 4 , wherein the mixed reactant is fully reacted either at 500° C. for 1 hour or at 300° C. for 2 hours in the thermal reactor.
14. The system according to claim 2 , wherein the solid residue is a mixture of the biochar, calcium magnesium carbonate, and the iron-based catalyst.
15. The system according to claim 3 , wherein the solid residue is a mixture of the biochar, calcium magnesium carbonate, and the iron-based catalyst.
16. The system according to claim 4 , wherein the solid residue is a mixture of the biochar, calcium magnesium carbonate, and the iron-based catalyst.
17. The system according to claim 2 , further comprising a mixed gas reuse system, wherein the mixed gas reuse system is configured to collect and transfer the hydrogen-based gas into an iron-making blast furnace for a direct iron ore reduction, engaging in a heating reaction and a reduction reaction.
18. The system according to claim 3 , further comprising a mixed gas reuse system, wherein the mixed gas reuse system is configured to collect and transfer the hydrogen-based gas into an iron-making blast furnace for a direct iron ore reduction, engaging in a heating reaction and a reduction reaction.