TWI671492B - Chemical looping reactor with shared partial reactor vessels - Google Patents

Abstract

A chemical loop reactor with a common structure includes a first reduction reactor, a second reduction reactor, and a common oxidation reactor. The common oxidation reactor is disposed in the first and second reduction reactors. between. In this way, the present invention uses a fluidized bed with an internal formula in a chemical circuit combustion process to perform a single redox reaction of oxygen carriers (metal oxides such as nickel or copper), and the first and second reduction reactors can each process themselves Reaction, reactants, so that two different sources can be processed simultaneously in a chemical loop reactor, and the oxygen carrier can be independently circulated independently, so that the oxygen in the oxygen carrier can be completely released, thereby obtaining high purity Carbon dioxide can also be expanded to produce hydrogen, which has the effect of simplifying the reaction mechanism, fast output rate, high operation efficiency and low cost.

Description

Chemical loop reactor with shared structure

The invention relates to a chemical loop reactor with a shared structure, in particular to a chemical circuit combustion process using an internally generalized fluidized bed, in particular to sharing the reaction zones of the two groups of fluidized beds with the same function for common use. The way is integrated and placed in the middle of the overall structure.

At present, the most common chemical loop reactors include fluidized-bed reactors (FBR) and moving-bed reactors (MBR). The bed volume of traditional fluidized bed reactors is large. Although recently developed Interconnected Fluidized Bed (IFB) patents have been proposed for use in chemical circuits, such as the Republic of China I544180, 201741246 and the US 9,903,584 and other patents. Only one source can be processed at a time. If there are two types of feed to be processed, there may be two types of reactors for processing. For example: Suppose there are two different sources now, but these two sources are not suitable to be sent to the same reactor for processing. They may affect each other because of burning time, temperature, or some other substances in it. When two different sources are to be processed at the same time, as in the structure shown in Figure 1B of the patent I544180, the structure of the two Figure 1B is disassembled, and there will be 4 + 4 = 8 reaction mechanisms in total, which will cause the bed to occupy land. Large area and increased equipment costs. Therefore, the aforementioned patents are deficient in failing to deal with two different sources at the same time.

In view of the huge market potential for domestic energy demand, such as energy conservation, carbon reduction, waste recycling, and circular economy, the country has set phase reduction targets and is actively promoting green energy to account for 20%. but It can be known from the above-mentioned technologies that although there are currently international invention patents related to energy-saving and carbon-reduction development technologies, there are also patents related to fluidized bed chemical circuit technology. However, as far as the IFB fluidized bed in the sub-field is concerned, with the exception of the IFB fluidized bed patent application previously filed by the applicant, such related technologies have not yet had the same applications and concepts as the patent in this case; The system cannot meet the user's needs of applying the internal fluidized bed in the chemical circuit combustion program in actual use to achieve the simplified reaction mechanism, fast output rate, high operating efficiency and low cost.

The main purpose of the present invention is to overcome the above-mentioned problems encountered in the conventional art and provide a single-oxidation reduction of oxygen carriers (metal oxides such as nickel or copper) by applying an internal-general fluidized bed in a chemical circuit combustion process. For the reaction, the first and second reduction reactors can process their own reactions and reactants, so that they can simultaneously process two different sources in a chemical loop reactor, and the oxygen carriers can independently circulate independently, so that the oxygen can be carried separately. The oxygen in the body can be completely released to obtain high-purity carbon dioxide, and it can also be expanded to produce hydrogen. It has a chemical structure reaction with a shared structure that simplifies the reaction mechanism, fast output rate, high operation efficiency and low cost. Device.

To achieve the above object, the present invention is a chemical loop reactor with a shared structure, including: a first reduction reactor having a first sparse bed and a first dense bed, and the top side of the first sparse bed A first weir exit is provided, and a first orifice communicating with the first sparse bed is provided at the bottom side of the first dense bed. The first reduction reactor contains an oxygen carrier in a first oxidation state. Air is injected into the first dense bed as a transport gas, the oxygen carrier in the first oxidation state is transported from the first dense bed and enters the first sparse bed through the first orifice, the first sparse bed The bed is injected with a first hydrocarbon fuel and a fluidized gas, and the first oxygen state oxygen carrier reacts with the first hydrocarbon fuel to reduce to a first metal state oxygen carrier, and generates carbon dioxide (CO2) and steam. The first metal state oxygen carrier in the first sparse bed is driven upward by the fluidized gas to the upper end and then passes over the first weir embankment exit; a second reduction reactor having a second thinning Bed and a second dense bed, the second dilute A second weir exit is provided on the side of the top of the bed, and a second orifice communicating with the second sparse bed is provided on the side of the bottom of the second dense bed. The second reduction reactor contains a second oxidation state. Oxygen carrier, inject air into the second dense bed as the transport gas, transport the oxygen carrier in the second oxidation state from the second dense bed and enter the second sparse bed through the second orifice, The second sparse bed is injected with a second hydrocarbon fuel and a fluidized gas, and the oxygen carrier in the second oxidation state reacts with the second hydrocarbon fuel to be reduced to the oxygen carrier in the second metal state and generates carbon dioxide and steam. The formed gas, the second metal state oxygen carrier is driven upward by the fluidized gas in the second sparse bed to the upper end and then passes over the second weir embankment exit; and a common oxidation reactor is provided in the The first and second reduction reactors are in communication with the first and second reduction reactors. The common oxidation reactor has a sparse bed and a dense bed, and a hole communicating with the sparse bed is provided at the bottom side of the dense bed. Mouth, and the top of the dense bed is two The sides are connected to the first and second sparse beds through the first and second weir embankment exits, and the two sides of the top of the sparse bed are each provided with a weir exit that communicates with the first and second dense beds. The first The oxygen carriers in the two and two metal states respectively pass through the outlets of the first and second weir banks and enter the dense bed to settle down and accumulate, and inject carbon dioxide into the dense bed as a transport gas to transfer the first and two metal oxygen carriers The body is transported from the dense bed and enters the sparse bed through the orifice, and the sparse bed is injected with air to cause the air to react with the first and second metal oxygen carriers to oxidize into the first and second oxide Oxygen and produce a gas composed of nitrogen (N ₂ ) and oxygen (O ₂ ). The first and second oxygen carriers are driven upward by the air in the sparse bed, and each crosses both sides. The weir embankment exit enters the first and second dense beds to form a loop respectively, so as to supply the first and second oxygen carriers to the first and second reduction reactors again and again to complete the cycle. Oxidation and reduction cycle.

In the above embodiments of the present invention, the first and second hydrocarbon fuels may be the same or different sources.

In the above embodiments of the present invention, the oxygen carriers in the first and second oxidation states are metal oxides capable of being oxidized and reduced or powders and granules containing metal oxides.

In the above embodiments of the present invention, the fluidized gas is carbon dioxide, steam, or air.

1‧‧‧first reduction reactor

11‧‧‧ the first sparse bed

111‧‧‧ the first weir exit

12‧‧‧ the first dense bed

121‧‧‧ the first orifice

2‧‧‧Second reduction reactor

21‧‧‧Second sparse bed

211‧‧‧Second weir exit

22‧‧‧Second dense bed

221‧‧‧Second orifice

3‧‧‧shared oxidation reactor

31‧‧‧ sparse bed

311‧‧‧ weir exit

32‧‧‧ dense bed

321‧‧‧ orifice

4a‧‧‧ metal oxygen carrier

4b‧‧‧ Oxygen carrier in oxidation state

5‧‧‧stack height

6‧‧‧ fluidized gas

FIG. 1 is a schematic diagram of the internal structure of a chemical loop reactor with a shared structure according to the present invention.

Figure 2 is a schematic diagram of the three-dimensional and oxygen carrier flow of a chemical loop reactor with a shared structure according to the present invention.

Please refer to "Figure 1 and Figure 2", which are schematic diagrams of the internal structure of the chemical loop reactor with a common structure according to the present invention, and three-dimensional and oxygen carrier flow diagrams of the chemical loop reactor with a common structure according to the present invention, respectively. As shown in the figure, the present invention is a chemical loop reactor with a common structure, which includes a first reduction reactor 1, a second reduction reactor 2, and a common oxidation reactor 3. The common oxidation reactor The 3 series is installed between the first and second reduction reactors 1 and 2.

The first reduction reactor 1 mentioned above has a first sparse bed 11 and a first dense bed 12. A first weir bank outlet 111 is provided on the top side of the first sparse bed 11 and a bottom side of the first dense bed 12. A first opening 121 is formed on the side and communicates with the first sparse bed 11. The first reduction reactor 1 contains an oxygen carrier in a first oxidation state. Air is injected into the first dense bed 12 as a transport gas, and the oxygen carrier in the first oxidation state is removed from the first dense bed. 12 and transported through the first orifice 121 into the first sparse bed 11, the first sparse bed 11 is injected with a first hydrocarbon fuel and a fluidized gas 6 (such as carbon dioxide or steam or air), and the first oxidation The oxygen carrier in the first state reacts with the first hydrocarbon fuel to be reduced to the oxygen carrier in the first metal state, and generates a gas composed of carbon dioxide (CO ₂ ) and steam. The first sparse bed 11 is driven upward by the fluidized gas 6 to the upper end, and then passes through the first weir bank outlet 111 and enters the common oxidation reactor 3.

The second reduction reactor 2 has a second sparse bed 21 and a second dense bed 22. A second weir outlet 211 is provided on the top side of the second sparse bed 21, and a bottom weir is provided on the bottom side of the second dense bed 22. A second orifice 221 communicating with the second sparse bed 21. The second reduction reactor 2 contains an oxygen carrier in a second oxidation state. Air is injected into the second dense bed 22 as a transport gas, and the oxygen carrier in the second oxidation state is removed from the second dense bed. 22 and transported through the second orifice 221 into the second sparse bed 21, the second sparse bed 21 is injected with a second hydrocarbon fuel and a fluidized gas 6 (such as carbon dioxide or steam or air), and the second oxidation The oxygen carrier in the state is reacted with the second hydrocarbon fuel to be reduced to the oxygen carrier in the second metal state, and a gas composed of carbon dioxide and steam is generated. The oxygen carrier in the second metal state is in the second sparse bed. 21 is driven upward by the fluidized gas 6 to the upper end, and then passes through the second weir bank outlet 211 and enters the common oxidation reactor 3.

The common oxidation reactor 3 is in communication with the first and second reduction reactors 1, 2 and has a sparse bed 31 and a dense bed 32. A bottom side of the dense bed 32 is provided with a communication with the sparse bed 31. Orifice 321, and the two sides of the top of the dense bed 32 are connected to the first and second sparse beds 11, 21 through the first and second weir embankment outlets 111 and 211, and the two sides of the top of the sparse bed 31 are provided There is a weir bank outlet 311 connected to the first and second dense beds 12 and 22. The first and second metal oxygen carriers respectively pass through the first and second weir embankment exits 111 and 211 and enter the dense bed 32 to sink and accumulate, and carbon dioxide is injected into the dense bed 32 as a transport gas. Oxygen carriers in the first and second metal state are transported from the dense bed 32 and enter the sparse bed 31 through the orifice 321. The sparse bed 31 is injected with air to make the air and the first and second metal state oxygen carriers The reaction is oxidized to form an oxygen carrier in the first and second oxidation states, and a gas composed of nitrogen (N ₂ ) and oxygen (O ₂ ) is generated. The oxygen carrier in the first and second oxidation states is in the sparse bed 31. Driven by the air, they respectively pass through the weir bank exits 311 on both sides and enter the first and second dense beds 12, 22 to form a loop respectively, so as to provide the first and second oxidation states again. The oxygen carrier is repeatedly cycled to the first and second reduction reactors 1 and 2 to complete the oxidation and reduction cycle. If so, a new chemical loop reactor with a common structure is formed by the disclosed structure.

The chemical loop reactor with a shared structure of the present invention is connected to at least one feeding module (not shown) to provide the first and two hydrocarbon fuels, and the first and two hydrocarbon fuels can be supplied. For the same or different sources.

The chemical loop reactor with a shared structure provided by the present invention is suitable for single-stage (step) oxidation-reduction of oxygen carriers. It can be nickel, copper, or other single-reaction metal oxides. It can also be used in three-stage reactions with iron. It is different in unity. Figures 1 and 2 use nickel as an example. When used, the present invention shares the two bed bodies of the block that converts metallic nickel into nickel oxide, and sets it in the middle of the chemical loop reactor in the form of a common oxidation reactor 3, and then sets the first on both sides. The two reduction reactors 1, 2 integrate the reaction mechanism that originally had 8 beds and integrate the reaction zone with the same function in the middle, that is, set in the middle of the overall structure in a way that the middle 2 bed system can be shared repeatedly. . When two different sources are to be processed at the same time, the first and second reduction reactors 1 and 2 on the left and right sides can each process their own reactions with their sources, and The oxygen carriers can be circulated independently, so that the oxygen in the oxygen carriers can be completely released, thereby obtaining high-purity carbon dioxide, and also can be expanded to produce hydrogen. It has a simplified reaction mechanism, fast output rate, high operating efficiency and The effect of low cost. As shown in Figure 2, the hydrocarbon fuel in Figure 1 is omitted here to mainly explain the flow and reaction of oxygen carriers. The stacking height 5 in the figure indicates that in a dense bed, the oxygen carriers will accumulate to a certain level. The height, in addition to increasing the driving force to the sparse bed, also isolates the gas from the sparse bed to the dense bed. The fluidized gas (carbon dioxide or steam or air) and air injected into the device are collectively referred to as the fluidized gas 6. It can be seen from FIG. 2 that the oxygen carrier 4a in the metal state will enter the sparse bed 31, which is also the oxidation section, through the orifice 321 at the bottom of the dense bed 32, which is the common oxidation reactor 3. In the sparse bed 31, which is also the oxidation section, It is driven upward by the fluidized gas 6 and reacts with the oxygen in the fluidized gas 6 to generate an oxygen carrier 4b in an oxidized state. The oxygen carrier 4b in the oxidized state is transported to the upper weir bank outlet 311, and Over the weir embankment exit 311 and pile up to the first and second dense beds 12, 22 of the first and second reduction reactors 1, 2 and then pass through the first and second holes of the first and second dense beds 12, 22 of the reduction zone. The ports 121, 221 enter the first and second sparse beds 11, 21 of this reduction zone. The oxygen carrier in the oxidation state reacts with the first and two hydrocarbon fuels in the first and second sparse beds 11, 21, and the oxygen carrier in the oxidation state loses oxygen and is reduced to the oxygen carrier in the metal state. Dihydrocarbon fuels have a combustion reaction due to the acquisition of oxygen. Since the reaction only returns oxygen atoms, no nitrogen is involved. That is, the generated gas is high-purity carbon dioxide and water, which can be obtained by appropriate separation. Carbon dioxide of purity. The oxygen carrier is repeatedly cycled in the reactor to complete the oxidation and reduction cycle.

The effects of the chemical loop reactor with a shared structure of the present invention are:

1. When two different sources are to be processed at the same time, the operation units of two sets of fluidized beds with oxidation and reduction (ie, oxygen-enriched combustion and carbon capture technology) can be simplified to reduce the cost. In the future, the reaction mechanism of 8 beds will be shared in the middle of the 2 beds. A common oxidation reactor is set in the middle of the overall structure, and a reduction reactor is set on each of the two sides. Originally there would be a total of 8 reaction mechanisms. The two beds in this block only need to be converted from the metal state to the oxidized state to achieve the effect of processing two different sources at the same time, which can greatly reduce the land area and equipment costs. .

2. Apply the internal fluidized bed in the chemical circuit combustion process to carry out a single redox reaction of oxygen carriers (metal oxides such as nickel or copper). The first and second reduction reactors can each process their own reactions and reactants. Therefore, two different feed sources can be processed simultaneously in a chemical loop reactor. The oxygen carrier can also be independently circulated independently, so that the oxygen in the oxygen carrier can be completely released, thereby obtaining high-purity carbon dioxide. Expanding the production of hydrogen has the effect of simplifying the reaction mechanism, fast output rate, high operation efficiency and low cost.

To sum up, the present invention is a chemical loop reactor with a shared structure, which can effectively improve the various shortcomings. It uses an internal-general fluidized bed in the chemical loop combustion process to carry out oxygen carriers (nickel or copper, etc.) Metal oxide) single redox reaction, the first and second reduction reactors can process their own reactions and reactants, so that two different sources can be processed in a chemical loop reactor at the same time, and the oxygen carrier can be the same Independent circulation, so that the oxygen in the oxygen carrier can be completely released to obtain high-purity carbon dioxide, and it can also be expanded to produce hydrogen. It has the effect of simplifying the reaction mechanism, fast output rate, high operating efficiency and low cost. So that the production of the present invention can be more advanced, more practical, and more in line with the needs of users, it has indeed met the requirements for invention patent applications, and filed patent applications according to law.

However, the above are only the preferred embodiments of the present invention, and the scope of implementation of the present invention cannot be limited by this; therefore, any simple equivalent changes and modifications made in accordance with the scope of the patent application and the contents of the invention specification of the present invention , All should still fall within the scope of the invention patent.

Claims (6)

A chemical loop reactor with a shared structure is an internally generalized fluidized bed used in a chemical loop combustion process. The reaction zones with the same function in two sets of fluidized beds are integrated in a shared manner and set in the middle of the overall structure. A chemical loop reactor with a common structure includes: a first reduction reactor having a first sparse bed and a first dense bed, a first weir embankment outlet is provided on the top side of the first sparse bed, and the first dense bed A first orifice communicating with the first sparse bed is provided at the bottom side; a second reduction reactor has a second sparse bed and a second dense bed, and a first sparse bed is provided with a first The second weir embankment exit, a second orifice communicating with the second sparse bed is provided at the bottom side of the second dense bed; and a common oxidation reactor is provided between the first and second reduction reactors and communicates with The first and second reduction reactors communicate with each other, the common oxidation reactor has a third sparse bed and a third dense bed, and a third orifice communicating with the third sparse bed is provided at the bottom side of the third dense bed. , And the The two sides of the top of the three dense beds are connected to the first and second sparse beds through the first and second weir embankment outlets, and one of the sides of the top of the third sparse bed is provided to communicate with the first and second dense beds. The third weir exit. The chemical loop reactor with a shared structure according to item 1 of the scope of the patent application, wherein the first reduction reactor contains an oxygen carrier in a first oxidation state and is injected into the first dense bed to be fluidized. The gas is used as a transport gas, and the oxygen carrier in the first oxidation state is transported from the first dense bed and enters the first sparse bed through the first orifice, and the first sparse bed is injected with the first hydrocarbon fuel and Fluidized gas, the first oxygen state oxygen carrier reacts with the first hydrocarbon fuel to reduce to a first metal state oxygen carrier, and generates a gas composed of carbon dioxide (CO ₂ ) and steam, the first The oxygen carrier in the metal state is driven upward by the fluidized gas in the first sparse bed to the upper end and then passes over the exit of the first weir; the second reduction reactor contains the oxygen carrier in the second oxidation state. A fluidized gas is injected into the second dense bed as a transport gas, and the oxygen carrier in the second oxidation state is transported from the second dense bed and enters the second sparse bed through the second orifice. Two sparse beds injected with second hydrocarbon fuel and fluidized gas The second oxygen state oxygen carrier reacts with the second hydrocarbon fuel to reduce to a second metal state oxygen carrier, and generates a gas composed of carbon dioxide and steam. The second metal state oxygen carrier is The second sparse bed is driven upward by the fluidized gas to the upper end and then passes over the second weir embankment exit; and in the common oxidation reactor, the first and second metal oxygen carriers pass through the first and second, respectively The weir embankment enters the third dense bed and sinks and accumulates, and a fluidized gas is injected into the third dense bed as a transport gas, and the first and dimetallic oxygen carriers are transported from the third dense bed. And enters the third sparse bed through the third orifice, and the third sparse bed is injected with a fluidized gas to cause the fluidized gas to react with the first and dimetallic oxygen carriers to oxidize into the first and second oxides State of the oxygen carrier and generate a gas composed of nitrogen (N ₂ ) and oxygen (O ₂ ). The first and second oxygen state oxygen carriers are driven upward by the fluidized gas in the third sparse bed. , And then cross the third weir exit on both sides to enter A loop is formed in each of the first and second dense beds, so as to provide the oxygen carrier in the first and second oxidation states to the first and second reduction reactors again and again to complete the oxidation and reduction cycle. . According to the chemical loop reactor with a shared structure described in item 2 of the scope of the patent application, the first and second hydrocarbon fuels may be the same or different sources of each other. According to the chemical loop reactor with a shared structure described in item 2 of the scope of the patent application, wherein the oxygen carriers in the first and second oxidation states are metal oxides that can be oxidized and reduced. According to the chemical loop reactor with a shared structure described in item 4 of the scope of the patent application, wherein the oxygen carriers in the first and second oxidation states are powders and granules containing the metal oxide. . The chemical loop reactor with a common structure according to item 2 of the scope of the patent application, wherein the fluidized gas is carbon dioxide or steam or air.