Looping Reaction Hydrogen Production System and Hydrogen Production Method

Abstract

A looping reaction hydrogen production system includes a reduction reaction device, a primary separation device, a hydrogen production reaction device, a secondary separation device, a primary heat transfer device and a cooling purification device. Based on looping combustion reaction mechanism, the system makes MeO/Me circularly flow between the hydrogen production reaction device and the reduction reaction device to respectively generate a reduction/oxidation chemical reaction, and to convert the conventional carbon-based solid fuel into the high-purity clean hydrogen energy. Compared with the conventional hydrogen production technology from water-gas shift reaction of syngas, the system reduces water consumption, energy consumption and environmental pollution of the hydrogen production process; converts conventional carbon-based fuel into clean hydrogen energy by use of renewable energy sources, such as solar energy; and achieves efficient capture and storage of gaseous CO.sub.2.

Claims

1. A looping reaction hydrogen production system, characterized by comprising: a reduction reaction device in which high-temperature MeO undergoes a reduction reaction with CO reducing gas generated by a reaction of high-temperature CO.sub.2 with carbon-based fuel to obtain a Me-containing solid product and a CO.sub.2-containing gaseous product; a primary separation device receiving the solid product and the gaseous product from the reduction reaction device and conducting separation to obtain the Me, carbonous particles and CO.sub.2-containing reaction product syngas; a hydrogen production reaction device receiving the Me from the primary separation device, in which the Me undergoes an oxidation reaction with high-temperature steam to obtain a MeO-containing solid product and an H2-containing gaseous product; a secondary separation device receiving the solid product and the gaseous product from the hydrogen production reaction device and conducting separation to obtain the MeO and the H2-containing gaseous product; a primary heat transfer device receiving the MeO from the secondary separation device and extraneous MeO, heating, and transporting to the reduction reaction device; a cooling purification device receiving the gaseous product from the secondary separation device and conducting separation to obtain the H.sub.2; wherein, the MeO is an oxidized metal oxide, and the Me is a reduced metal or a reduced metal oxide.

2. The looping reaction hydrogen production system according to claim 1, characterized in that the primary separation device comprises a carbon separator and a primary gas-solid separator, the carbon separator is connected with the reduction reaction device to achieve effective separation of the metal oxide Me from the carbonous particles and the CO.sub.2-containing reaction product syngas, and the primary gas-solid separator is connected with the carbon separator to achieve effective separation of the carbonous particles from the CO.sub.2-containing reaction product syngas.

3. The looping reaction hydrogen production system according to claim 1, characterized in that the looping reaction hydrogen production system also including a feedback device connected to the primary separation device and the reduction reaction device; the feedback device receiving carbon particles from the primary separation device and returning the carbon particles to the reduction reaction device.

4. The looping reaction hydrogen production system according to claim 1, characterized in that the looping reaction hydrogen production system also including a heat exchanging device connected to the primary separation device, the heat transfer device receives the reaction product syngas from the primary separation device, and controls the heat exchange between the reaction product syngas and water/steam to obtain low-temperature reaction product syngas and high-temperature water/steam medium.

5. The looping reaction hydrogen production system according to claim 4,characterized in that the outlet of gas from the heat transfer device is divided into two paths, one of which is connected to a cooling refinement device to purify and recover part of CO.sub.2inlow-temperature reaction product syngas, and the other of which is connected with a recirculation compressor and a secondary heat transfer device to pressurize and heat the remaining low-temperature reaction product syngas, and then transport it to the reduction reaction device as high-temperature CO.sub.2.

6. The looping reaction hydrogen production system according to claim 1, characterized in that the looping reaction hydrogen production system also comprises a feed water pump and a tertiary heat transfer device connected with the feed water pump and the hydrogen production reaction device; the tertiary heat transfer device receives water from the feed water pump, gets it heated and sends the resulting high-temperature steam to the hydrogen production reaction device.

7. The looping reaction hydrogen production system according to claim 6, characterized in that the cooling purification device is connected with the feedwater pump, and the feedwater pump receives extraneous water and condensate from the cooling purification device and sends to the tertiary heat transfer device as feed water.

8. A looping reaction hydrogen production method, characterized in that hydrogen is produced by use of a looping reaction hydrogen production system described in claim 1, comprising the following steps: S1: feeding high-temperature CO.sub.2, carbon-based fuel and high-temperature MeO into a reduction reaction device, performing a reaction to obtain a Me-containing solid product and a CO.sub.2-containing gaseous product; S2: conducting separation on the Me-containing solid product and the CO.sub.2-containing gaseous product by use of a primary separation device to obtain Me, carbonous particles and CO.sub.2-containing reaction product syngas; S3: sending high-temperature steam and the obtained Me into a hydrogen production reaction device, performing a reaction to obtain a MeO-containing solid product and an H2-containing gaseous product; S4: conducting separation on the obtained MeO-containing solid product and the H2-containing gaseous product by use of a secondary separation device to obtain MeO and the H2-containing gaseous product; and S5: cooling and clarifying the H2-containing gaseous product to obtain the hydrogen, and sending the high-temperature MeO obtained by heating the obtained MeO and extraneous MeO into the reduction reaction device by use of a primary heat transfer device, and repeating the steps S1 to S5 in turn.

9. The looping reaction hydrogen production method according to claim 8, characterized in that after heat exchange with the CO.sub.2-containing reaction product syngas obtained in the step S2, part of the obtained CO.sub.2-containing reaction product syngas is cooled and purified, and the remaining part is compressed and heated, and then sent into the reduction reaction device as the high-temperature CO.sub.2; the carbonous particles obtained in the Step S2 are returned to the reduction reaction device; and the condensate obtained by cooling and clarifying the H2-containing gaseous product in the Step S4 is heated together with the extraneous water and sent to the hydrogen production reaction device as the high-temperature steam.

10. The looping reaction hydrogen production method according to claim 8, characterized in that the carbon-based fuel is coal, biomass or petroleum coke, the MeO is Fe.sub.3O.sub.4 or FeO, and the Me is FeO or Fe; and solar energy or power fuel is used as a heat source to obtain the high-temperature MeO at 800-1100° C., the high-temperature CO.sub.2 at 300-450° C. and the high-temperature steam at 150-300° C. separately.

Description

BRIEF DESCRIPTION OF THE DRAWING

[0032] The FIGURE is a structural diagram of a looping reaction hydrogen production system according to an exemplary embodiment of the present invention.

[0033] Description of reference numerals in attached drawing:

[0034] 1-hydrogen production reaction device, 2-reduction reaction device, 3-carbon separator, 4-gas-solid separator, 5-feedback device, 6-heat exchanging device, 7-recirculation compressor, 8-secondary heat transfer device, 9-cooling refinement device, 10-secondary separation device, 11-cooling purification device, 12-feedwater pump, 13-tertiary heat transfer device, 14-primary heat transfer device.

DETAILED DESCRIPTION OF EMBODIMENTS

[0035] All of the features disclosed in the Description, or all of the steps of any method or process so disclosed, may be combined in any way, except combinations where such features and/or steps are mutually exclusive.

[0036] Any feature disclosed in the Description can be replaced with other equivalent or similar features, unless otherwise specified. That is, each feature is only an example of series of equivalent or similar features, unless otherwise specified.

[0037] In order to solve the problems in the prior art, based on the looping combustion reaction mechanism, the present invention achieves the efficient capture and storage of gaseous product CO.sub.2 by converting the conventional carbon-based solid fuel into the high-purity clean hydrogen energy, and prepares high-quality water/steam for production heating or power generation by use of the physical sensible heat of the high-temperature gas generated by the reaction.

[0038] A looping reaction hydrogen production system of the present invention will be described in detail below. Wherein, the equations of main looping chemical reactions in the looping reaction hydrogen production system are as follows: [0039] reduction reaction: C+CO.sub.2+2MeO ==== 2Me+2CO.sub.2, ΔH,.sub.C=Q.sub.1 KJ/mol (endothermic reaction); [0040] hydrogen production reaction: Me+H.sub.2O ==== H.sub.2+MeO, ΔH, .sub.H2=Q.sub.2 KJ/mol (endothermic or exothermic reaction); [0041] integrated reaction: C+CO.sub.2+2H.sub.2O ==== 2H.sub.2+2CO.sub.2 (endothermic reaction). wherein, the MeO is an oxidized metal oxide, such as Fe.sub.3O.sub.4 or FeO; the Me is a reduced metal or a reduced metal oxide, such as FeO or Fe.

[0042] As shown above, the overall chemical reaction integrating the looping combustion reactions is an endothermic reaction, so it is necessary to provide heat for the looping hydrogen production system by use of other kinds of energy (such as solar energy or power fuel).

[0043] The figure is a structural diagram of a looping reaction hydrogen production system according to an exemplary embodiment of the present invention.

[0044] Referring to the figure, according to the exemplary embodiment of the present invention, the looping reaction hydrogen production system includes a reduction reaction device 2, a primary separation device, a hydrogen production reaction device 1, a secondary separation device 10, a primary heat transfer device 14, a cooling purification device 11 and other components, makes oxidized metal oxide MeO/reduced metal or reduced metal oxide Me circularly flow between the hydrogen production reaction device 1 and the reduction reaction device 2 to respectively generate an oxidation chemical reaction and a reduction chemical reaction, and prepares hydrogen by use of carbon-based fuel to achieve efficient and clean utilization of the energy resources.

[0045] Particularly, the reduction reaction device 2 is the main component for realizing a reduction reaction on the MeO, and it may be an existing device, such as a fluidized bed. High-temperature MeO undergoes a reduction reaction in the reduction reaction device 2 with CO reducing gas generated by a reaction of high-temperature CO.sub.2 with the carbon-based fuel to obtain a Me-containing solid product and a CO.sub.2-containing gaseous product.

[0046] The carbon-based fuel of the present invention is coal, biomass, petroleum coke and the like, and the CO reducing gas is produced by reaction of the high-temperature CO.sub.2 at 300-450° C. with the carbon-based fuel; the CO reducing gas and a small amount of volatile gas (e.g., CO, H.sub.2 and CH.sub.4) generated from the carbon-based fuel undergo the reduction reaction with the high-temperature MeO at 800-1100° C. to reduce the oxidized metal oxide MeO to the reduced metal or reduced metal oxide Me. In addition, some unburned carbonous particles and generated gaseous products such as CO.sub.2 and H.sub.2O (a small amount) are produced.

[0047] The primary separation device receives the solid product and the gaseous product from the reduction reaction device 1 and conducts separation to obtain Me, carbonous particles and CO.sub.2-containing reaction product syngas.

[0048] Particularly, the primary separation device includes a carbon separator 3 and a gas-solid separator 4. The carbon separator 3 is connected with the reduction reaction device 2 to achieve effective separation of the metal oxide Me from the carbonous particles and the CO.sub.2-containing reaction product syngas, to be specific, to achieve effective separation of the reduced metal or reduced metal oxide Me from the unburned carbonous particles, and the obtained reduced metal or reduced metal oxide Me is sent to the hydrogen production reaction device 1 for subsequent reactions, and the reaction product syngas (mostly CO.sub.2, with a small amount of H.sub.2O and other impurities) and the carbonous particles (unburned C) are lifted to the gas-solid separator 4; the gas-solid separator 4 is connected with the carbon separator 3 to achieve effective separation of the carbonous particles from the CO.sub.2-containing reaction product syngas, namely, gas-solid separation. Optionally, the carbon separator 3 can be a spouted bed device, and the gas-solid separator 4 can be a cyclone separator.

[0049] Referring to the figure, preferably, the looping reaction hydrogen production system also includes a feedback device 5 connected with the primary separation device and the reduction reaction device 2, and the feedback device 5 receives the carbonous particles from the primary separation device and returns the carbonous particles to the reduction reaction device 2 to continue the reduction reaction with the high-temperature CO.sub.2.

[0050] Further, the looping reaction hydrogen production system also includes a heat exchanging device 6 connected with the primary separation device, the heat exchanging device 6 receives the reaction product syngas from the primary separation device and controls the heat exchange between the reaction product syngas and water/steam medium to obtain low-temperature reaction product syngas and high-temperature water/steam medium. Optionally, the heat exchanging device 6 can be a tubular heat exchanging device, and the obtained high-temperature water/steam medium can be used for production heating or power generation.

[0051] Preferably, the gas outlet of the heat exchanging device is divided into two paths. One is connected with a cooling refinement device 9 to purify and recover part of CO.sub.2 in the low-temperature reaction product syngas for further recycling, and the other is connected with a recirculation compressor 7 and a secondary heat transfer device 10 to pressurize and heat the remaining low-temperature reaction product syngas and transport to the reduction reaction device 2 to participate in the reaction as high-temperature CO.sub.2, thus achieving CO.sub.2 recycling.

[0052] The hydrogen production reaction device of the present invention receives the Me from the primary separation device, in which the Me undergoes an oxidation reaction with the high-temperature steam to obtain a MeO-containing solid product and an H2-containing gaseous product. Optionally, the hydrogen production reaction device is a bubbling fluidized bed.

[0053] The secondary separation device 10 receives the solid product and the gaseous product from the hydrogen production reaction device 1 and conducts separation to obtain the MeO and the H2-containing gaseous product. Preferably, the secondary separation device 10 is a gas-solid separation device, such as a cyclone separator.

[0054] The primary heat transfer device 14 receives the MeO from the secondary separation device 10 and extraneous MeO, heats, and transports it to the reduction reaction device 1 to participate in the reduction reaction. The primary heat transfer device 14 provides stable energy for the oxidation-reduction reaction in the looping hydrogen production system. The cooling purification device 11 receives the gaseous product from the secondary separation device 10 and conducts separation to obtain the H.sub.2. That is, for the gaseous product from the secondary separation device 10, H.sub.2Ois condensed to get high-purity hydrogen.

[0055] In addition, the looping reaction hydrogen production system also includes a feedwater pump 12 and a tertiary heat transfer device 13 connected with the feedwater pump 12 and the hydrogen production reaction device 1, the tertiary heat transfer device 13 receives water from the feedwater pump 12, heats and transports the obtained high-temperature steam to the hydrogen production reaction device 1 to participate in the reaction as the raw material.

[0056] The cooling purification device 11 is connected with the feedwater pump 12, and the feedwater pump 12 receives extraneous water and the condensate from the cooling purification device 11 and sends to the tertiary heat transfer device 13 as feed water. As a result, the condensate from the cooling purification device 11 and the extraneous water pass through the feedwater pump 12 and the secondary heat transfer device 13 sequentially, and then enter the hydrogen production reaction device 1 to participate in the reaction in the form of steam.

[0057] Wherein, preferably, the primary heat transfer device 14, the secondary heat transfer device 8 and the tertiary heat transfer device 13 of the present invention are solar heat transfer devices by use of the solar energy or power fuel heat transfer devices by use of the power fuel. According to the present invention, the solar energy or the power fuel is used to provide heat for the looping hydrogen production system to realize high-efficiency and low-cost hydrogen production.

[0058] When the system is used, the high-temperature MeO and the carbon-based fuel undergo the reduction reaction in the reduction reaction device 2 to produce the solid products (mostly, the Me) and the gaseous products (mostly, the CO.sub.2); the Me is separated from the carbonous particles and other impurities in the carbon separator, the obtained Me undergoes the oxidation reaction with the steam to produce the MeO and the H.sub.2 in the hydrogen production reaction device, and the gas (hydrogen and steam) is separated from the MeO in the secondary separation device, then the MeO is sent to the reduction reaction device after heating in the primary heat transfer device; the gas (hydrogen and steam) is clarified in the cooling purification device to obtain the high-purity hydrogen, and the condensate is heated by the feedwater pump and the tertiary heat transfer device, and then sent to the hydrogen production reaction device; the separated carbonous particles are returned to the reduction reaction device through the feedback device, and the high-temperature CO.sub.2 and other gases transfer heat to the water/steam medium through the heat exchanging device to generate high-quality water/steam; and the low-temperature gases including CO.sub.2 are pressurized by the recirculation compressor and heated by the secondary heat transfer device, and then introduced into the reduction reaction device.

[0059] The present invention further provides a looping reaction hydrogen production method for preparing hydrogen by use of the looping reaction hydrogen production system, which includes the following steps:

[0060] S1: high-temperature CO.sub.2, carbon-based fuel and high-temperature MeO are fed into a reduction reaction device 2 to obtain a Me-containing solid product and a CO.sub.2-containing gaseous product through reaction. Wherein, the carbon-based fuel is coal, biomass or petroleum coke, the MeO is Fe.sub.3O.sub.4 or FeO, and the Me is FeO or Fe.

[0061] S2: separation is conducted on the Me-containing solid product and the CO.sub.2-containing gaseous product by use of a primary separation device to obtain Me, carbonous particles and CO.sub.2-containing reaction product syngas; wherein, after heat exchange with the obtained CO.sub.2-containing reaction product syngas, part of the obtained CO.sub.2-containing reaction product syngas is cooled and purified, and the remaining part is compressed and heated, and then sent into the reduction reaction device as the high-temperature CO.sub.2, and the obtained carbonous particles are returned to the reduction reaction device.

[0062] S3: the high-temperature steam and the obtained Me is sent into a hydrogen production reaction device 1 to obtain a MeO-containing solid product and an H2-containing gaseous product through reaction.

[0063] S4: separation is conducted on the obtained MeO-containing solid product and the H2-containing gaseous product by use of a secondary separation device 10 to obtain MeO and the H2-containing gaseous product; wherein, condensate obtained by cooling and clarifying the H2-containing gaseous product is heated together with extraneous water and sent to the hydrogen production reaction device as the high-temperature steam.

[0064] S5: the H2-containing gaseous product is cooled and clarified to obtain the hydrogen, and the high-temperature MeO obtained by heating the obtained MeO and extraneous MeO is sent into the reduction reaction device 1 by use of a primary heat transfer device 14, and the steps S1 to S5 are repeated in turn.

[0065] With this method, the solar energy or the power fuel is used as a heat source to obtain the high-temperature MeO at 800-1100° C., the high-temperature CO.sub.2 at 300-450° C. and the high-temperature steam at 150-300° C. separately. According to the present invention, a circulating flux of the MeO/Me and an addition ratio of the carbon-based fuel are adjusted to control the reduction degree of the oxidized metal oxide, and a steam flow to the hydrogen production reaction device is regulated to control the oxidation degree of the reduced metal or the reduced metal oxide, so as to control the whole system and produce the hydrogen.

[0066] The present invention will be further described in detail with reference to an embodiment.

[0067] Referring to the figure, the embodiment includes: a Fe.sub.3O.sub.4/FeO granular metal oxide with a particle size ranging from 125 .Math.m to 180 .Math.m is used as a circulating medium, with a mass fraction of Fe.sub.3O.sub.4 being 30%, and lignite is used as carbon-based fuel.

[0068] A reduction reaction device: the lignite is sent into a high-temperature reduction reaction device at 1000° C. to produce coal gas (e.g., H.sub.2/CO) and coke by destructive distillation; the coke undergoes a reduction reaction with high-temperature CO.sub.2 to form CO reducing gas; as inside the reduction reaction device happens an endothermic reaction and exists high-temperature CO.sub.2 with sensible heat, the temperature of the reduction reaction device drops by about 100° C.

[0069] The chemical equations are as follows:

##STR00001##

the Fe.sub.3O.sub.4 undergoes a reaction with reducing gas (mostly, CO) to produce CO.sub.2, H.sub.2O and FeO, with chemical equations shown as follows:

##STR00002##

[0070] A carbon separator: the reduced FeO circulating particles are separated from carbonous particles (e.g., unburned coke and ash), the FeO is sent to a hydrogen production reaction unit, and the reaction syngas (mostly CO.sub.2, with a small amount of H.sub.2O) and the solid particles are lifted to a gas-solid separator. The reaction syngas is effectively separated from the carbonous particles, and the carbonous particles are captured and returned to the reduction reaction device through a feedback device to undergo the reaction with the recirculated high-temperature CO.sub.2 (referring to Equation 1).

[0071] The high-temperature syngas at 900° C. from the gas-solid separator exchanges heat with water medium in a heat exchanging device. To be specific, on one hand, the reaction syngas is cooled to 200° C.; on the other hand, the water medium is heated to generate high-quality steam (at 540° C., 11.8 MPa) for production. A part of the cooled syngas is heated to 400° C. through a recirculation compressor and a secondary heat transfer device, and then sent to the reduction reaction device. The remaining syngas is sent to a cooling refinement device to obtain gaseous CO.sub.2 with a purity of more than 95% for convenient capture and storage.

[0072] A hydrogen production reaction device: the FeO circulating particles at 900° C. from the carbon separator undergo an oxidation reaction with the steam heated by a tertiary heat transfer device to produce H.sub.2 and Fe.sub.3O.sub.4. The hydrogen production reaction device conducts an exothermic reaction, and the temperature of the reduction reaction device rises by about 34° C. The chemical equation is as follows:

##STR00003##

[0073] The gas (H.sub.2 and H.sub.2O) is efficiently separated from the Fe.sub.3O.sub.4 through a secondary separation device, and the separated gas is sent to a cooling purification device to obtain a high-purity H.sub.2 with a purity of more than 98%. In addition, the 934° C. Fe.sub.3O.sub.4 obtained by the secondary separation device is heated together with newly added Fe.sub.3O.sub.4 to 1000° C. by a primary heat transfer device and then sent to the reduction reaction device for circulation reaction.

[0074] For carbon-based fuel, the equation of the main integrated reaction is as follows:

##STR00004##

[0075] The hydrogen production reaction between the carbon-based fuel and the steam is endothermic. Theoretically, it takes at least 102.6 KJ of heat energy to convert 1 mol C into 2 mol H.sub.2. In this embodiment, solar energy is used to provide heat energy for the looping hydrogen production system, which achieves the conversion from 1 mol C into 2 mol H.sub.2 and 1 mol CO.sub.2, and effectively separates the H.sub.2 from CO.sub.2in the syngas, thus greatly reducing the hydrogen production cost and facilitating the capture and storage of CO.sub.2.

[0076] The present invention is not limited to the foregoing specific implementations. The present invention expands to any new feature or any new combination disclosed in the Description, and steps in any new method or process or any new combination disclosed.