SYSTEM AND METHOD FOR PRODUCING HYDROGEN USING BY PRODUCT GAS

Abstract

Disclosed is a system for producing hydrogen from a byproduct gas generated during a steelmaking process or a coal chemistry process, including a reformer for reforming the byproduct gas using steam (H.sub.2O), a separator for separating a reformed gas supplied from the reformer into a reduction gas and hydrogen gas (H.sub.2), a first reactor for reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) using the reduction gas supplied from the separator, and a second reactor for producing ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2) by mixing the ferrous oxide (FeO) supplied from the first reactor with steam (H.sub.2O), wherein the concentration of hydrogen gas (H.sub.2) in the reformed gas discharged from the reformer is higher than the concentration of hydrogen gas (H.sub.2) in the byproduct gas.

Claims

1. A system for producing hydrogen from a byproduct gas generated during a steelmaking process or a coal chemistry process, the system comprising: a reformer for reforming the byproduct gas using steam (H.sub.2O); a separator for separating a reformed gas supplied from the reformer into a reduction gas and hydrogen gas (H.sub.2); a first reactor for reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) using the reduction gas supplied from the separator; and a second reactor for producing ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2) by mixing the ferrous oxide (FeO) supplied from the first reactor with steam (H.sub.2O), wherein a concentration of hydrogen gas (H.sub.2) in the reformed gas discharged from the reformer is higher than a concentration of hydrogen gas (H.sub.2) in the byproduct gas.

2. The system of claim 1, further comprising a third reactor, which is connected to the first reactor and the second reactor, wherein the third reactor is configured such that the ferrous-ferric oxide (Fe.sub.3O.sub.4) supplied from the second reactor is mixed with oxygen (O.sub.2) and is thus oxidized into ferric oxide (Fe.sub.2O.sub.3) and supplied to the first reactor.

3. The system of claim 1, wherein an internal temperature of the reformer is 600 C. to 900 C.

4. The system of claim 1, wherein the separator includes a pressure swing adsorption (PSA) unit.

5. The system of claim 1, wherein a portion of the steam (H.sub.2O) fed to the second reactor is supplied from the first reactor.

6. The system of claim 1, wherein the byproduct gas includes a coke oven gas (COG).

7. The system of claim 1, wherein, in the byproduct gas, a steam-to-carbon ratio (H.sub.2O/CH.sub.4) is 2.5 to 3.5.

8. The system of claim 1, wherein the reduction gas includes at least one selected from the group consisting of hydrogen gas (H.sub.2), carbon monoxide (CO), methane gas (CH.sub.4) and combinations thereof.

9. A method of producing hydrogen, comprising: generating a reformed gas by reforming a byproduct gas generated during a steelmaking process or a coal chemistry process with steam (H.sub.2O); separating the reformed gas into a reduction gas and hydrogen gas (H.sub.2); reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) using the reduction gas; and producing ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2) by reacting the ferrous oxide with steam (H.sub.2O), wherein, in the generating the reformed gas, a concentration of hydrogen gas (H.sub.2) in the reformed gas is higher than a concentration of hydrogen gas (H.sub.2) in the byproduct gas.

10. The method of claim 9, wherein the reducing the ferric oxide (Fe.sub.2O.sub.3) into the ferrous oxide (FeO) includes a reaction represented by Scheme 1 below:
4Fe.sub.2O.sub.3+CH.sub.4.fwdarw.8FeO+2H.sub.2O+CO.sub.2.[Scheme 1]

11. The method of claim 9, wherein the producing the ferrous-ferric oxide (Fe.sub.3O.sub.4) and the hydrogen gas (H.sub.2) includes a reaction represented by Scheme 2 below:
8FeO+ 8/3H.sub.2O.fwdarw. 8/3Fe.sub.3O.sub.4+ 8/3H.sub.2.[Scheme 2]

12. The method of claim 9, wherein, in the reducing the ferric oxide (Fe.sub.2O.sub.3) into the ferrous oxide (FeO) using the reduction gas, a portion of the ferric oxide (Fe.sub.2O.sub.3) includes ferric oxide obtained by mixing oxygen (O.sub.2) with ferrous-ferric oxide (Fe.sub.3O.sub.4) resulting from the producing the ferrous-ferric oxide (Fe.sub.3O.sub.4) and the hydrogen gas (H.sub.2).

13. The method of claim 12, wherein the ferrous-ferric oxide (Fe.sub.3O.sub.4) and the oxygen (O.sub.2), which are mixed, are formed into ferric oxide (Fe.sub.2O.sub.3) through a reaction represented by Scheme 3 below:
8/3Fe.sub.3O.sub.4+O.sub.2.fwdarw.4Fe.sub.2O.sub.3.[Scheme 3]

14. The method of claim 9, wherein the separating the reformed gas into the reduction gas and the hydrogen gas (H.sub.2) includes a pressure swing absorption (PSA) process.

15. The method of claim 9, wherein the generating the reformed gas is performed at a temperature of 600 C. to 900 C.

16. The method of claim 9, wherein the byproduct gas includes a coke oven gas (COG).

17. The method of claim 9, wherein, in the byproduct gas, a steam-to-carbon ratio (H.sub.2O/CH.sub.4) is 2.5 to 3.5.

18. The method of claim 9, wherein the reduction gas includes at least one selected from the group consisting of hydrogen gas (H.sub.2), carbon monoxide (CO), methane gas (CH.sub.4) and combinations thereof.

19. The method of claim 9, wherein, in the producing the ferrous-ferric oxide (Fe.sub.3O.sub.4) and the hydrogen gas (H.sub.2), a portion of the steam (H.sub.2O) includes steam resulting from the reducing the ferric oxide (Fe.sub.2O.sub.3) into the ferrous oxide (FeO).

Description

DRAWINGS

[0034] In order that the disclosure may be well understood, there will now be described various forms thereof, given by way of example, reference being made to the accompanying drawings, in which:

[0035] FIG. 1 schematically shows a hydrogen production system according to some forms of the present disclosure;

[0036] FIG. 2 schematically shows a hydrogen production system and process according to some forms of the present disclosure;

[0037] FIG. 3 schematically shows a hydrogen production system and process in Example 1;

[0038] FIG. 4 schematically shows a hydrogen production process in Example 1 and Comparative Examples 1 and 2;

[0039] FIG. 5 is a graph showing the hydrogen yield depending on the temperature in Example 1;

[0040] FIG. 6 is a graph showing the methane conversion rate depending on the temperature in Example 1;

[0041] FIG. 7 shows a tester for evaluating the conversion into a reformed gas when the byproduct gas used is coke oven gas (COG);

[0042] FIG. 8 is a graph showing the results of measurement of concentration and thermodynamic equilibrium value depending on the temperature in order to evaluate reforming performance in Example 1;

[0043] FIG. 9 is a graph showing the results of measurement of methane conversion rate and thermodynamic equilibrium value depending on the temperature in order to evaluate reforming performance in Example 1;

[0044] FIG. 10 is a graph showing absolute amounts of hydrogen gas (H.sub.2) and carbon monoxide (CO) used for a reduction test using a reference material; and

[0045] FIG. 11 is a graph showing the results of the reduction test of FIG. 10.

[0046] The drawings described herein are for illustration purposes only and are not intended to limit the scope of the present disclosure in any way.

DETAILED DESCRIPTION

[0047] The following description is merely exemplary in nature and is not intended to limit the present disclosure, application, or uses. It should be understood that throughout the drawings, corresponding reference numerals indicate like or corresponding parts and features.

[0048] Hereinafter, aspects of the present disclosure will be described in detail with reference to the accompanying drawings. The advantages and features of the present disclosure, as well as how to accomplish them, will become apparent with reference to the forms described in detail below with reference to the accompanying drawings. However, the present disclosure is not limited to the forms disclosed below, but may be embodied in various forms. Throughout the drawings, the same reference numerals will refer to the same or like elements.

[0049] Unless defined otherwise, all terms (including technical and scientific terms) used herein may be used in a sense that is commonly understood by those skilled in the art to which the present disclosure belongs. Also, commonly used predefined terms are not to be ideally or excessively interpreted unless explicitly defined otherwise.

[0050] Furthermore, the terminology used herein is for the purpose of illustrating forms and is not intended to limit the present disclosure. In this specification, singular forms include plural forms unless the context clearly dictates otherwise. It will be further understood that the terms comprise and/or include, when used in this specification, specify the presence of stated elements, features, numbers, steps, and/or operations, but do not preclude the presence or addition of one or more other elements, features, numbers, steps, and/or operations. Here, the term and/or includes each of the mentioned items and all combinations of one or more thereof.

[0051] Also, it will be understood that when an element such as a layer, film, area, or sheet is referred to as being on another element, it can be directly on the other element, or intervening elements may be present therebetween. In contrast, when an element such as a layer, film, area, or sheet is referred to as being under another element, it can be directly under the other element, or intervening elements may be present therebetween.

[0052] Unless otherwise specified, all numbers, values, and/or representations that express the amounts of components, reaction conditions, polymer compositions, and mixtures used herein are to be taken as approximations including various uncertainties affecting the measurements that occur in obtaining these values, among others, and thus should be understood to be modified by the term about in all cases. Furthermore, when a numerical range is disclosed in this specification, the range is continuous, and includes all values from the minimum value of said range to the maximum value thereof, unless otherwise indicated. Moreover, when such a range pertains to integer values, all integers including the minimum value to the maximum value are included, unless otherwise indicated.

[0053] In the present specification, when a range is described for a variable, it will be understood that the variable includes all values including the end points described within the stated range. For example, the range of 5 to 10 will be understood to include any subranges, such as 6 to 10, 7 to 10, 6 to 9, 7 to 9, and the like, as well as individual values of 5, 6, 7, 8, 9 and 10, and will also be understood to include any value between valid integers within the stated range, such as 5.5, 6.5, 7.5, 5.5 to 8.5, 6.5 to 9, and the like. Also, for example, the range of 10% to 30% will be understood to include any subranges, such as 10% to 15%, 12% to 18%, 20% to 30%, etc., as well as all integers including values of 10%, 11%, 12%, 13% and the like up to 30%, and will also be understood to include any value between valid integers within the stated range, such as 10.5%, 15.5%, 25.5%, and the like.

[0054] As used herein, the ratio is to be understood as indicating a stoichiometric ratio, unless otherwise stated.

[0055] Hereinafter, a detailed description will be given of the present disclosure with reference to the appended drawings.

[0056] FIGS. 1 and 2 schematically show a hydrogen production system and a hydrogen production process according to some forms of the present disclosure.

[0057] With reference to FIG. 1, the hydrogen production system 1 for producing hydrogen from a byproduct gas generated during a steelmaking process or a coal chemistry process according to the present disclosure may include a reformer 50, a separator 70, and reactors 100, 200, 300. In the reformer 50, the byproduct gas (e.g. byproduct gas containing methane (CH.sub.4)) may be converted into a reformed gas, and in the separator 70, hydrogen (H.sub.2) may be separated from the reformed gas. In the reactors 100, 200, 300, oxidation and reduction may be carried out. In particular, such oxidation and reduction may include reduction of ferric oxide (Fe.sub.2O.sub.3) or oxidation of ferrous ferric oxide (Fe.sub.3O.sub.4).

[0058] More specifically, with reference to FIG. 2, the hydrogen production system 1 according to the present disclosure includes a reformer 50 for reforming the byproduct gas using steam (H.sub.2O), a separator 70 for separating the reformed gas supplied from the reformer 50 into a reduction gas and hydrogen gas (H.sub.2), a first reactor 100 for reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) using the reduction gas supplied from the separator 70, and a second reactor 200 for producing ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2) by mixing steam (H.sub.2O) with ferrous oxide (FeO) supplied from the first reactor.

[0059] In particular, the hydrogen production system 1 according to the present disclosure is characterized in that the concentration of hydrogen gas (H.sub.2) in the reformed gas discharged from the reformer 50 is higher than the concentration of hydrogen gas (H.sub.2) in the byproduct gas. Specifically, the byproduct gas supplied to the reformer 50 may react with steam (H.sub.2O), and may thus be converted into a reformed gas whose hydrogen (H.sub.2) concentration is amplified.

[0060] In the hydrogen production system 1 according to the present disclosure, hydrogen (H.sub.2) primarily obtained from the separator 70 and hydrogen (H.sub.2) secondarily obtained through separation from the second reactor 200 are included, ultimately affording an increased amount of hydrogen (H.sub.2).

[0061] The hydrogen production system 1 according to an form of the present disclosure may further include a third reactor 300, which is connected to the first reactor 100 and the second reactor 200. The third reactor 300 allows ferrous-ferric oxide (Fe.sub.3O.sub.4) supplied from the second reactor 200 to be mixed with oxygen (O.sub.2) to thus be oxidized into ferric oxide (Fe.sub.2O.sub.3). Simultaneously, the third reactor 300 may be configured to supply the oxidized ferric oxide (Fe.sub.2O.sub.3) to the first reactor 100. In the hydrogen production system 1 according to the present disclosure, the first reactor 100 to the third reactor 300 may constitute a looping process. Thus, hydrogen may be produced at a high yield from the supplied byproduct gas and the generation of byproducts may be decreased compared to conventional cases.

[0062] More specifically, a hydrogen production method, which is performed in the hydrogen production system 1 according to an form of the present disclosure, may include generating a reformed gas by reforming a byproduct gas generated during a steelmaking process or a coal chemistry process with steam (H.sub.2O), separating the reformed gas into a reduction gas and hydrogen gas (H.sub.2), reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) using the reduction gas, and producing ferrous ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2) by allowing the reduced ferrous oxide to react with steam (H.sub.2O). In the step of generating the reformed gas, the concentration of hydrogen gas (H.sub.2) in the reformed gas may be higher than that of hydrogen gas (H.sub.2) in the byproduct gas.

[0063] The step of generating the reformed gas may be performed using the reformer 50, and the step of separating the reformed gas into the reduction gas and the hydrogen gas (H.sub.2) is performed using the separator 70.

[0064] Moreover, the step of reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) may be performed using the first reactor 100. More specifically, the step of reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) may include the reaction represented by Scheme 1 below.

4Fe.sub.2O.sub.3+CH.sub.4.fwdarw.8FeO+2H.sub.2O+CO.sub.2[Scheme 1]

[0065] In Scheme 1, methane (CH.sub.4) may function as a reducing agent, and in the hydrogen production system and method according to the present disclosure, the methane (CH.sub.4) conversion rate may be 85% or more, but is not limited thereto.

[0066] Also, the step of producing the ferrous-ferric oxide (Fe.sub.3O.sub.4) and the hydrogen gas (H.sub.2) may be performed using the second reactor 200. More specifically, the step of producing the ferrous-ferric oxide (Fe.sub.3O.sub.4) and the hydrogen gas (H.sub.2) may include the reaction represented by Scheme 2 below.

8FeO+ 8/3H.sub.2O.fwdarw. 8/3Fe.sub.3O.sub.4+ 8/3H.sub.2[Scheme 2]

[0067] In the step of reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO) using the generated reduction gas, a portion of the ferric oxide (Fe.sub.2O.sub.3) may include ferric oxide obtained by mixing oxygen (O.sub.2) with ferrous-ferric oxide (Fe.sub.3O.sub.4) resulting from the step of producing ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2). More specifically, ferrous-ferric oxide (Fe.sub.3O.sub.4) and oxygen (O.sub.2), which are mixed, may be formed into ferric oxide (Fe.sub.2O.sub.3) through the reaction represented by Scheme 3 below.

8/3Fe.sub.3O.sub.4+O.sub.2.fwdarw.4Fe.sub.2O.sub.3[Scheme 3]

[0068] Also, mixing of ferrous-ferric oxide (Fe.sub.3O.sub.4) with oxygen (O.sub.2) may be conducted using the third reactor 300.

[0069] Thus, the overall process including oxidation and reduction using the first reactor 100, the second reactor 200, and the third reactor 300 may be performed as represented by Scheme 4 below.

First reactor: 4Fe.sub.2O.sub.3+CH.sub.4.fwdarw.8FeO+2H.sub.2O+CO.sub.2

Second reactor: 8FeO+ 8/3H.sub.2O.fwdarw. 8/3Fe.sub.3O.sub.4+ 8/3H.sub.2

Third reactor: 8/3Fe.sub.3O.sub.4+O.sub.2.fwdarw.4Fe.sub.2O.sub.3

Overall process reaction: CH.sub.4+H.sub.2+O.sub.2.fwdarw. 8/3H.sub.2+CO.sub.2[Scheme 4]

[0070] The internal temperature of the reformer 50 may be 600 C. or higher. For example, the internal temperature of the reformer 50 may fall in the range of 600 C. to 900 C. In one aspect, the internal temperature of the reformer 50 is 700 C. or higher. For example, the internal temperature of the reformer 50 may fall in the range of 700 C. to 900 C. Thus, in the hydrogen production method according to the present disclosure, the step of generating the reformed gas may be performed at a temperature of 600 C. to 900 C.

[0071] In the hydrogen production system 1 according to a form of the present disclosure, the separator 70 may further include a pressure swing adsorption (PSA) unit. Accordingly, the step of separating the reformed gas into the reduction gas and the hydrogen gas (H.sub.2) may include a PSA process. Specifically, hydrogen (H.sub.2) is strongly adsorbed from the reformed gas supplied from the reformer 50 using an adsorbent (or a membrane) selected under increased pressure compared to other components, thereby separating hydrogen (H.sub.2). For example, the separation efficiency of the adsorbent may be 80% or more, and thus the recovery rate of hydrogen (H.sub.2) that is separated may be 80% or more. Furthermore, PSA may be performed under increased pressure of 10 bar.

[0072] In the hydrogen production system 1 according to the present disclosure, a portion of the steam (H.sub.2O) fed to the second reactor 200 may be supplied from the first reactor 100. Specifically, during the production of ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2) by reacting the reduced ferrous oxide with steam (H.sub.2O), a portion of the steam (H.sub.2O) may include steam resulting from the step of reducing ferric oxide (Fe.sub.2O.sub.3) into ferrous oxide (FeO). Accordingly, the steam (H.sub.2O) formed through the reaction of the first reactor 100 (Scheme 1) is supplied to the second reactor 200, and is thus used for the reaction of the second reactor 200 (Scheme 2), thereby reducing the supply of steam (H.sub.2O) from the outside, and thus the hydrogen production system 1 may be made more environmentally friendly by increasing the production efficiency using limited resources.

[0073] Meanwhile, examples of the byproduct gas used in the hydrogen production system 1 according to the present disclosure may include coke oven gas (COG) generated during a coal chemistry process, Linz-Donawitz converter gas (LDG), finex-off gas (FOG), and blast furnace gas (BFG). In one aspect, the byproduct gas includes coke oven gas (COG). The COG may include the gas composition shown in Table 1 below.

TABLE-US-00001 TABLE 1 Hydro- Carbon Carbon Oxy- gen Methane monoxide Nitrogen dioxide Ethylene gen (H.sub.2) (CH.sub.4) (CO) (N.sub.2) (CO.sub.2) (C.sub.2H.sub.4) (O.sub.2) 58.32 26.06 6.74 4.22 2.07 1.84 0.75 Composition unit: vol. %

[0074] In order to increase the production efficiency of hydrogen (H.sub.2), a steam-to-carbon ratio (SCR) (H.sub.2O/CH.sub.4) in the byproduct gas used in the hydrogen production system 1 according to the present disclosure may be 2.5 to 3.5. In one aspect, the SCR (H.sub.2O/CH.sub.4) may be 3.0.

[0075] In the step of separating the reformed gas into the reduction gas and the hydrogen gas (H.sub.2) in the hydrogen production method according to the present disclosure, the reduction gas may include at least one selected from the group consisting of hydrogen gas (H.sub.2), carbon monoxide (CO), methane gas (CH.sub.4) and combinations thereof. Thus, in the hydrogen production system 1 according to the present disclosure, the reduction gas separated from the reformed gas using the separator 70 may include at least one selected from the group consisting of hydrogen gas (H.sub.2), carbon monoxide (CO), methane gas (CH.sub.4) and combinations thereof.

[0076] A better understanding of the present disclosure will be given through the following Examples and Comparative Examples. However, the following Examples are set forth to illustrate the present disclosure but are not to be construed as limiting the scope of the present disclosure.

EXAMPLE 1

[0077] With reference to FIG. 3, in Example 1, 100 kmol/hr of COG, serving as a byproduct gas, was fed to a reformer. Here, the COG had a gas composition as shown in Table 1.

[0078] Using the reformer, the COG was reformed under conditions of a SCR (H.sub.2O/CH.sub.4) of 3.0, a reaction temperature of 800 C., and a reaction pressure of 1 atm, thus generating a reformed gas whose hydrogen (H.sub.2) concentration was amplified (methane (CH.sub.4) conversion rate: 97%).

[0079] The resulting reformed gas was transferred from the reformer into a separator (using PSA, membrane efficiency: 80%, pressure: 10 bar), thus primarily separating 119.47 kmol/hr of hydrogen (H.sub.2) (recovery rate: 80%).

[0080] The reduction gas (including 28.84 kmol/hr of hydrogen gas (H.sub.2), 32.45 kmol/hr of carbon monoxide (CO), and 0.67 kmol/hr of methane gas (CH.sub.4)), which was not separated but remained in the reformer, was transferred to a fuel reactor, and was then allowed to react with a sufficient amount of a ferric oxide (Fe.sub.2O.sub.3) catalyst (i.e. an amount able to sufficiently use the supplied reduction gas) introduced into the fuel reactor (a Gibbs reactor) at a reaction temperature of 800 C. and a reaction pressure of 1 atm. For example, 116.94 kmol/hr of ferrous oxide (FeO) was formed through reaction with 30 kmol/hr of the ferric oxide (Fe.sub.2O.sub.3) catalyst (a reduction reaction, Fe.sub.2O.sub.3 reduction rate: 95%).

[0081] The ferrous oxide (FeO) formed in the fuel reactor was transferred to a steam reactor, and was then allowed to react with steam (H.sub.2O) to produce ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2), thereby secondarily separating 38.98 kmol/hr of hydrogen gas (H.sub.2). Here, a portion of the steam (H.sub.2O) fed to the steam reactor may be obtained from the fuel reactor.

[0082] The amounts of the components fed to the respective units are shown in Table 2 below.

TABLE-US-00002 TABLE 2 Reformer Reformer Fuel reactor Fuel reactor Composition inlet outlet inlet outlet H.sub.2 59.45 149.34 28.84 0.14 CO.sub.2 2.06 8.78 4.91 37.85 CO 6.83 29.00 29.00 0.18 H.sub.2O 76.89 41.27 N.sub.2 4.27 4.27 4.27 4.27 CH.sub.4 25.63 0.67 0.67 2.04E10 FeO 0 0 0 116.94 Fe.sub.2O.sub.3 0 0 60 0.62 C.sub.2H.sub.4 1.76 2.67E07 2.67E07 3.44E22 O.sub.2 0 8.01E18 0 1.18E11 Total Flow 176.89 233.33 131.14 160 Inlet and outlet units: kmol/hr COG gas has a composition excluding water vapor(H2O) from the reformer intake amount. Process simulation was performed for chemistry processes including COG gas reforming process and actual iron oxide reduction process. Production of about 150 kmol/hr of hydrogen from 100 kmol/hr of COG was confirmed. Conversion of 60 kmol/hr of Fe.sub.2O.sub.3 into about 116.94 kmol/hr of FeO through reduction was confirmed.

[0083] Also, ferrous-ferric oxide (Fe.sub.3O.sub.4) formed in the steam reactor was transferred to an air reactor, and was then allowed to react with oxygen (O.sub.2), thus obtaining ferric oxide (Fe.sub.2O.sub.3). Furthermore, a looping process was performed in a manner in which ferric oxide (Fe.sub.2O.sub.3) formed in the steam reactor was transferred again to the fuel reactor and allowed to react with the added reduction gas (H.sub.2, CH.sub.4, CO).

[0084] Consequently, the total amount of hydrogen (H.sub.2) that was primarily and secondarily produced was 158.45 kmol/hr.

Comparative Example 1

[0085] With reference to FIG. 4, the reformer 50 was not used in Comparative Example 1, unlike Example 1, in which primary separation of hydrogen (S1) was performed using the reformer and the separator. Thus, COG was not reformed with steam (H.sub.2O), but 47.56 kmol/hr of hydrogen (H.sub.2) was primarily produced directly from COG using the separator 70 (S2), and 76.79 kmol/hr of hydrogen (H.sub.2) was secondarily produced by feeding the separated residual reduction gas (including 11.89 kmol/hr of hydrogen gas (H.sub.2), 6.83 kmol/hr of carbon monoxide (CO), and 25.63 kmol/hr of methane gas (CH.sub.4)) to oxidation and reduction reactors 100, 200 (S2).

[0086] Consequently, the total amount of hydrogen (H.sub.2) that was primarily and secondarily produced was 124.35 kmol/hr.

Comparative Example 2

[0087] With reference to FIG. 4, the reformer 50 and the separator 70 were not used in Comparative Example 2, unlike S1 of Example 1 or S2 of Comparative Example 1. Thus, COG (including 59.45 kmol/hr of hydrogen gas (H.sub.2), 6.83 kmol/hr of carbon monoxide (CO), and 25.63 kmol/hr of methane gas (CH.sub.4)), serving as a reduction gas, was directly fed to oxidation and reduction reactors 100, 200, thus producing 106.91 kmol/hr of hydrogen (H.sub.2) (S3).

Evaluation Example 1: Total Amount of Hydrogen (H.SUB.2.) Produced

[0088] The total amounts of hydrogen (H.sub.2) produced in Example 1 and Comparative Examples 1 and 2 are shown in Table 3 below.

TABLE-US-00003 TABLE 3 Primarily Secondarily produced H.sub.2 produced H.sub.2 Total H.sub.2 (kmol/hr) (kmol/hr) (kmol/hr) Example 1 119.47 38.98 158.45 Comparative 47.56 76.79 124.35 Example 1 Comparative 0 106.91 106.91 Example 2

[0089] Therefore, hydrogen (H.sub.2) was produced at the highest yield (158.45 kmol/hr) in Example 1, in which hydrogen was primarily produced using both the reformer and the separator and hydrogen was secondarily produced using a redox process.

Evaluation Example 2: Evaluation of Yield of Hydrogen (H.SUB.2.) Depending on Temperature

[0090] In order to evaluate the yield of hydrogen (H.sub.2) depending on the temperature in the reforming process, the reforming process was performed using COG of Table 1 under the same conditions as in Example 1. Here, among the operation conditions of the reformer, the temperature was changed from 500 C. to 1000 C. The composition of the resulting reformed gas is shown FIG. 5, and the results of the methane (CH.sub.4) conversion rate are shown in FIG. 6.

[0091] With reference to FIG. 5, the composition and a high hydrogen (H.sub.2) yield were obtained at, in one aspect, 600 C. or higher, and in one aspect between 600 C. to 900 C. With reference to FIG. 6, the methane (CH.sub.4) conversion rate was about 80% or more at, in one aspect, 600 C. or higher. The yield of hydrogen (H.sub.2) was confirmed through thermodynamic calculation.

Evaluation Example 3: Verification of Reforming Performance of COG Depending on Temperature

Verification Tester

[0092] With reference to FIG. 7, a tester for verifying the reforming performance of the byproduct gas (COG) is shown. Such a tester may be configured to include a COG reformer 410, a temperature detector 420, pressure detectors 500, 501, and a back pressure regulator 600.

Verification of Reforming Performance

[0093] The thermodynamic composition and the methane (CH.sub.4) conversion rate depending on the temperature using the verification tester are shown in FIGS. 8 and 9, respectively. Here, the test conditions were as follows: 4 ml of a steam reforming (SR) catalyst, a gas hourly space velocity (GHSV) of 5000/h, and a steam-to-carbon ratio (SCR, H.sub.2O/CH.sub.4) of 3.0.

[0094] With reference to FIG. 8, reforming performance close to the thermodynamic equilibrium value was confirmed from a temperature of, in one aspect, 700 C. (hydrogen (H.sub.2) yield: 80%, dry basis).

[0095] With reference to FIG. 9, the methane (CH.sub.4) conversion rate was 90% or more at a temperature of 700 C. or higher, from which it was confirmed that the target methane (CH.sub.4) conversion rate exceeded 85%.

Evaluation Example 4: Verification of Redox Reaction Using Oxidation and Reduction Reactors

[0096] In order to evaluate the applicability to an oxidation reactor and a reduction reactor (e. G., a fuel reactor and a steam reactor), reduction reactor testing was performed using a ferric oxide (Fe.sub.2O.sub.3) reference material. Based on the test results, process design parameters for ferric oxide (Fe.sub.2O.sub.3) application in the process of the present disclosure were derived.

Reduction Reactor Test Conditions

[0097] Table 4 below shows the absolute amount of the reactive gas, and Table 5 below shows the detailed test conditions.

TABLE-US-00004 TABLE 4 Composition Blank Reactor (mmol/min) H.sub.2 0.211 CO.sub.2 0.045 CO 0.286 H.sub.2O N.sub.2 0.045 CH.sub.4 0.001

TABLE-US-00005 TABLE 5 Test conditions Catalyst amount 23.4 g/15 mL GHSV 75/h Temperature 830 C. Measurement Real-time measurement with uGC Catalyst Fe.sub.2O.sub.3 Moisture Removal with moisture absorbent

Verification Results of Reduction Reaction

[0098] The absolute amounts of hydrogen (H.sub.2) and carbon monoxide (CO) used in the reduction are shown in FIG. 10, and the reduction reactor test results are shown in FIG. 11.

[0099] With reference to FIG. 10, 4.78 mmol/g of the reduction gas was used for catalyst reduction. In the case of a ferric oxide (Fe.sub.2O.sub.3) reference material, 5.0 mmol/g of ferric oxide (Fe.sub.2O.sub.3) participated in reduction by a stoichiometric ratio of about 0.95. Thus, process design parameters may be presented based on the above test results. The absolute amounts of gases used in the reduction reaction are shown in Table 7 below.

TABLE-US-00006 TABLE 7 Total Reduction Gas (mmol) H.sub.2 50.75 CO 61.27 Tot. 112.02 Result 4.78 mmol/g catal.

[0100] Therefore, in the hydrogen production system and method according to the present disclosure, the byproduct gas (especially, COG) was reformed under conditions of the specific SCR (H.sub.2O/CH.sub.4), reaction temperature and pressure using the reformer, thus generating a reformed gas whose hydrogen (H.sub.2) concentration was amplified (methane (CH.sub.4) conversion rate: 97%), from which hydrogen (H.sub.2) was then separated, thus primarily producing hydrogen (H.sub.2) at a high yield (i.e. 80%).

[0101] Moreover, in the reforming process, the residual reduction gas (including hydrogen gas (H.sub.2), carbon monoxide (CO) and methane gas (CH.sub.4)) was transferred to the oxidation and reduction reactors, followed by reaction with the ferric oxide (Fe.sub.2O.sub.3) catalyst in a sufficient amount thereof at a specific reaction temperature and pressure, whereby the reduction was progressed to form ferrous oxide (FeO) at a high yield. The ferrous oxide (FeO) thus obtained was allowed to react with steam (H.sub.2O) to afford ferrous-ferric oxide (Fe.sub.3O.sub.4) and hydrogen gas (H.sub.2), whereby hydrogen gas (H.sub.2) was secondarily separated. Accordingly, hydrogen (H.sub.2) was produced at a high yield through this dual process.

[0102] As a portion of the steam (H.sub.2O) fed to the steam reactor, steam resulting from the reduction reaction may be recycled, thereby producing environmentally friendly hydrogen (H.sub.2).

[0103] Although forms of the present disclosure have been described with reference to the accompanying drawings, those skilled in the art will appreciate that the present disclosure may be embodied in other specific forms without changing the technical spirit or features thereof. Thus, such modifications should not be understood individually from the technical ideas or views of the present disclosure.