CN111477285A - Method for obtaining thermal neutral oxygen carrier in chemical looping combustion process - Google Patents
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 123
- 239000001301 oxygen Substances 0.000 title claims abstract description 123
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 123
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 55
- 239000000126 substance Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 38
- 230000007935 neutral effect Effects 0.000 title claims abstract description 27
- 239000000446 fuel Substances 0.000 claims abstract description 110
- 239000004480 active ingredient Substances 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 238000010438 heat treatment Methods 0.000 claims abstract description 15
- 238000010521 absorption reaction Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 19
- 239000002245 particle Substances 0.000 claims description 19
- 239000000969 carrier Substances 0.000 claims description 18
- 238000002309 gasification Methods 0.000 claims description 8
- 238000000197 pyrolysis Methods 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 4
- 238000005469 granulation Methods 0.000 claims description 3
- 230000003179 granulation Effects 0.000 claims description 3
- 150000004706 metal oxides Chemical class 0.000 claims description 3
- 229910052755 nonmetal Inorganic materials 0.000 claims description 3
- 229910000314 transition metal oxide Inorganic materials 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 13
- 238000012546 transfer Methods 0.000 abstract description 3
- 238000012423 maintenance Methods 0.000 abstract description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 14
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 7
- 229910052802 copper Inorganic materials 0.000 description 7
- 239000010949 copper Substances 0.000 description 7
- 229910052742 iron Inorganic materials 0.000 description 7
- 239000004449 solid propellant Substances 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 238000006722 reduction reaction Methods 0.000 description 4
- 238000004458 analytical method Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000011161 development Methods 0.000 description 2
- 238000004455 differential thermal analysis Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- 238000011946 reduction process Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000392035 Oreas Species 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000001747 exhibiting effect Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000033116 oxidation-reduction process Effects 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 238000005563 spheronization Methods 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
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Abstract
The invention belongs to the technical field related to chemical looping combustion, and particularly discloses a method for obtaining a thermal neutral oxygen carrier in a chemical looping combustion process. The method comprises the following steps: (a) determining the oxygen carrier active ingredient required in the reaction process according to the chemical looping combustion reaction, and constructing a relational expression of the ratio of the oxygen carrier circulation amount to the oxygen carrier active ingredient in the chemical looping combustion reaction process; (b) and (3) constructing a heat balance equation of the heat absorption and release reactions involved in the fuel reactor, and calculating the proportion of each component of the active component of the oxygen carrier required by the fuel reactor for maintaining self-heating operation, thereby realizing the acquisition of the thermal neutral oxygen carrier. The resulting thermally neutral oxygen carrier can satisfy the balance of heat absorption and heat release in the fuel reactor, i.e., achieve a thermal self-balance. By the invention, the limitation that the oxygen carrier circulation quantity needs to meet the oxygen transfer of the rated active lattice and the heat maintenance of the fuel reactor at the same time is removed, the temperature of the fuel reactor is prevented from being reduced in the chemical looping combustion process, and the self-heating operation of the fuel reactor is realized.
Description
Technical Field
The invention belongs to the technical field related to chemical looping combustion, and particularly relates to a method for acquiring a thermal neutral oxygen carrier in a chemical looping combustion process.
Background
Chemical looping Combustion (Chemical L piping Combustion) is based on CO2A novel combustion technology provided by a near zero emission concept. The technology avoids direct contact between fuel and air by means of the cyclic oxidation-reduction of solid oxygen carrier particles between an air reactor and a fuel reactor, and can realize CO in the fuel conversion process2Intrinsic separation of (1).
The oxygen carrier is used as a carrier carrying oxygen and heat, and the physical and chemical properties of the oxygen carrier directly determine the transfer efficiency of the oxygen and the heat in the reaction process, so that the operation of the whole chemical-looping combustion system is influenced. In chemical looping combustion systems, a strongly exothermic reaction process generally occurs within the air reactor, while the fuel reactor may be endothermic or exothermic depending on the type of fuel and oxygen carrier. In particular, in the chemical looping combustion process of solid fuel such as coal, the pyrolysis and gasification process of the solid fuel is a strong endothermic reaction, and at this time, the heat carried by the oxygen carrier often has difficulty in maintaining the reaction temperature in the fuel reactor relatively stable. Therefore, to achieve autothermal operation of a large solid fuel chemical looping combustion reactor, the first to be solved is the problem of endothermic heat compensation in the fuel reactor.
In a chemical looping fuel reactor, the reduction reaction process between different oxygen carriers and fuel gas has different heat absorption and release characteristics. Three conventional oxygen carriers CuO and Fe2O3And NiO in a mixture with a different fuel gas (CH)4CO or H2) The heat absorption and release amounts in the reduction reaction process of (a) are significantly different, wherein CuO has a strong heat release characteristic as a whole, and Fe2O3And NiO, the whole body has endothermic or slightly exothermic characteristics, and based on the characteristics, the corresponding oxygen carrier material is expected to be directionally designed by regulating the types and the proportions of active components so as to maintain the self-heating operation of the fuel reactor. At present, chemical looping combustion collarMost scholars in the field have focused their research on the development of high performance oxygen carriers, and little research has been associated with achieving autothermal operation of large chemical looping combustion devices. In fact, in the chemical looping combustion process of the solid fuel, if the heat compensation of the pyrolysis and gasification reactions with strong heat absorption in the fuel reactor is realized only by improving the circulation flow of the oxygen carrier to strengthen the heat exchange with the air reactor, the operation load of the reactor is greatly improved, thereby increasing the operation cost of the system and even shortening the service life of the reactor. Therefore, the development of a thermally neutral oxygen carrier has a significant driving role in the realization of industrial operation of chemical looping combustion technology.
Disclosure of Invention
In view of the above drawbacks and needs of the prior art, the present invention provides a method for obtaining thermally neutral oxygen carriers during chemical looping combustion, wherein the obtaining of thermally neutral oxygen carriers is achieved by solving the proportion of oxygen carrier active ingredients required for maintaining the self-heating operation of a fuel reactor by constructing the relationship between the circulation amount of oxygen carriers and the proportion of oxygen carrier active ingredients in the chemical looping combustion reaction and the thermal equilibrium equation of the heat absorption and heat release reactions involved in the fuel reactor. The method avoids the fuel reactor from absorbing or releasing extra heat by reasonably regulating the type and proportion of the active components of the oxygen carrier, and realizes the self-heating operation of the fuel reactor.
To achieve the above object, according to the present invention, there is provided a method for obtaining a thermally neutral oxygen carrier in a chemical looping combustion process, the method comprising the steps of:
(a) determining the oxygen carrier active component required in the reaction process according to the chemical looping combustion reaction, and constructing the ratio C of the oxygen carrier circulation amount to the oxygen carrier active component in the chemical looping combustion reaction processoxThe relation (one);
(b) based on the self-heating operation of the fuel reactor in the chemical looping combustion reaction, constructing a heat balance equation (II) of the heat absorption and release reactions involved in the fuel reactor, and solving the distribution ratio of each component in the oxygen carrier active ingredients for maintaining the self-heating operation of the fuel reactor according to the relational expression (I) and the equation (II) so as to further realize the acquisition of the heat neutral oxygen carrier; the obtained thermal neutral oxygen carrier can satisfy the balance of heat absorption and heat release in the fuel reactor, namely, the self-balance of the whole heat is realized.
Further preferably, in step (a), the relation (one) is preferably performed as follows:
wherein m is1The circulation flow rate of the oxygen carrier required for complete combustion of the fuel;
is the molar mass of oxygen; m isfuelIs the fuel flow rate; srStoichiometric ratio of oxygen required for complete combustion per mole of fuel; Δ X is the difference in the conversion of the oxygen carrier in the air reactor and the fuel reactor; coxIs the proportion of active ingredients in the oxygen carrier; mfuelIs the molar mass of the fuel.
Further preferably, in step (b), the equation (two) is preferably performed in the following manner:
mfuelΔHre+m1ΔHOC+mfuelΔHp+mFGΔHFG+ΔHLeither as 0 (two)
Wherein, Δ HreThe heat absorbed or released by the complete reaction of the fuel and the oxygen carrier in unit flow; Δ HOCThe oxygen carrier particles carry heat from the air reactor into the fuel reactor as a unit of circulation flow; Δ HpThe heat absorbed for pyrolysis and gasification of fuel per unit flow rate (gaseous fuel may not take this into account); Δ HFGThe heat absorbed by the low-temperature fluidizing gas with unit flow; Δ HLIs the system heat loss; m isFGIs the flow of the fluidizing gas in the fuel reactor.
Further preferably, the Δ HOCPreferably according to the following relationship:
ΔHOC＝cOC(TOC,AR-TOC,FR)
wherein, cOCIs the specific heat capacity of the oxygen carrier; t isOC,ARAnd TOC,FRThe temperature of the oxygen carrier particles in the air reactor and the fuel reactor, respectively.
Further preferably, the Δ HFGPreferably according to the following relationship:
ΔHFG＝cFG(TFR-T0)
wherein, cFGThe specific heat capacity of the fluidizing gas; t isFRIs the operating temperature of the fuel reactor; t is0Is the initial temperature of the fluidizing gas.
Further preferably, the active ingredient in the oxygen carrier is one or more, and for the oxygen carriers of multiple active ingredients, the mixing mode comprises physical mixing or granulation technology so that multiple active ingredients are contained in one particle.
Further preferably, the active ingredient raw material of the oxygen carrier is solid particles or a solution.
Further preferably, the active component in the oxygen carrier is a transition metal oxide or a non-metal oxide.
Generally, compared with the prior art, the technical scheme of the invention has the following beneficial effects:
the invention combines the fuel type, the heat required by the complete conversion of the fuel, the temperature of the fuel reactor and the air reactor, the circulation flow of the oxygen carrier required by the complete combustion of the fuel, the type of the active components of the oxygen carrier, the temperature of the reactor, the specific heat capacity of the oxygen carrier particles and the like, reasonably regulates and controls the type and the proportion of the active components in the oxygen carrier based on the energy balance principle, can remove the strict limitation that the circulation flow of the oxygen carrier needs to simultaneously meet the rated active lattice oxygen transfer and the heat maintenance of the fuel reactor, avoids the temperature reduction of the fuel reactor in the chemical-looping combustion process, is favorable for realizing the self-heating operation of the chemical-looping fuel reactor, thereby reducing the operation cost of the system and prolonging the service life.
Drawings
FIG. 1 is a flow chart of a thermal neutral oxygen carrier capture process constructed in accordance with a preferred embodiment of the present invention;
FIG. 2 is a graph of the ratio of the mass of iron ore to copper ore (80: 20) to 25% H of a copper/iron ore mixed oxygen carrier synthesized according to the method of preparation described in example 1 and constructed in accordance with a preferred embodiment of the present invention2+35％CO+40％CO2Thermogravimetric differential thermal analysis curves during four cycles of redox reactions of syngas fuel;
FIG. 3 is a graph of the trend of fuel reactor tail gas concentration over time in a chemical looping combustion performance test with coal for a thermally neutral complex oxygen carrier synthesized according to the method of preparation described in example 1.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention. In addition, the technical features involved in the embodiments of the present invention described below may be combined with each other as long as they do not conflict with each other.
Referring to fig. 1, the method for obtaining thermal neutral oxygen carriers in a chemical looping combustion process of the present invention includes the following steps:
according to the type of fuel in the chemical looping combustion fuel reactor, the heat required by complete conversion of the fuel, the operating temperatures of the fuel reactor and an air reactor, the circulating flow rate of oxygen carriers required by complete combustion of the fuel, the type of oxygen carrier active ingredients, the temperature and the flow rate of fluidizing gas, the specific heat capacity of oxygen carrier particles and the like, the proportion of the oxygen carrier active ingredients required for maintaining the self-heating operation of the fuel reactor (namely, the temperature of the fuel reactor can be kept unchanged based on the existing energy flow and material flow) is calculated through an energy balance principle, and then the acquisition of the thermally neutral oxygen carriers is realized.
Oxygen carrier circulation flow m for complete conversion of fuel in fuel reactor1As shown in the formula (one),
wherein m is1The circulation flow rate of the oxygen carrier required for complete combustion of the fuel;
is the molar mass of oxygen; m isfuelIs the fuel flow rate; srStoichiometric ratio of oxygen required for complete combustion per mole of fuel; Δ X is the difference in the conversion of the oxygen carrier in the air reactor and the fuel reactor; coxIs the proportion of active ingredients in the oxygen carrier; mfuelIs the molar mass of the fuel.
In order to realize the self-heating operation of the fuel reactor, the heat absorption and release processes involved in the fuel reactor need to reach heat balance, as shown in the formula (II),
mfuelΔHre+m1ΔHOC+mfuelΔHp+mFGΔHFG+ΔHLeither as 0 (two)
ΔHOC＝cOC(TOC,AR-TOC,FR) (III)
ΔHFG＝cFG(TFR-T0) (IV)
Wherein, Δ HreThe heat absorbed or released by the complete reaction of the fuel and the oxygen carrier in unit flow; Δ HOCThe oxygen carrier particles carry heat from the air reactor into the fuel reactor per unit circulation flow rate, cOCIs the specific heat capacity of the oxygen carrier; t isOC,ARAnd TOC,FRThe temperature of the oxygen carrier particles in the air reactor and the fuel reactor, respectively; Δ HpThe heat absorbed for pyrolysis and gasification of fuel per unit flow rate (gaseous fuel may not take this into account); Δ HFGM is the heat absorbed by the low temperature fluidizing gas per unit flowFGIs the flow of the fluidized gas in the fuel reactor; c. CFGThe specific heat capacity of the fluidizing gas; t isFRIs the operating temperature of the fuel reactor; t is0Is the initial temperature of the fluidizing gas; Δ HLIs a system heat loss.
To ensure complete combustion of the fuel, the oxygen carrier in the fuel reactor should provide oxygen in an amount greater than or equal to the amount of oxygen required for complete combustion of the fuel. According to the type and input amount of the fuel and the type of the oxygen carrier, the minimum oxygen carrier circulation flow required by the complete combustion of the fuel can be calculated by the formula (I). By comprehensively considering the heat carried by the oxygen carrier from the air reactor into the fuel reactor, the heat absorbed by pyrolysis and gasification of the solid fuel, the heat absorbed by low-temperature fluidizing gas and the heat loss (such as system heat leakage) possibly existing in the chemical looping combustion system, the heat balance of the whole process in the fuel reactor is realized by utilizing the heat absorption and release characteristics of different types of oxygen carriers when reacting with the fuel, as shown in formula (II).
As a further preference, the oxygen carrier active ingredient may be one or more, the active ingredient may react with combustible gas (gaseous fuel, or pyrolysis and gasification product of solid fuel, etc.) endothermically or exothermically, but the overall endothermy may be compensated for, keeping the temperature of the chemical looping fuel reactor constant;
as a further preference, the oxygen carrier active ingredient raw material may be solid particles, or may be a precursor solution;
as a further preference, the oxygen carrier active ingredient may be various transition metal oxides or non-metal oxides (e.g., CaSO)4Etc.), either as chemically pure chemicals or as ores and industrial wastes;
as a further preference, multiple oxygen carrier active ingredients can be provided inside the same particle by physical mixing means, or by various granulation techniques (e.g. extrusion spheronization, spray drying, cement binding, etc.) to achieve a thermo-neutral effect;
as a further preference, the present invention is not only suitable for the capture of oxygen carriers for chemical looping combustion processes, but also for the capture of oxygen carriers for other chemical looping processes.
The present invention will be further illustrated with reference to specific examples.
Examples
(1) Selecting copper ore and iron oreAs an oxygen carrier raw material, the composition analysis of which is shown in table 2, a representative coal gasification product was selected as a fuel: 25% H2+35％CO+40％CO2，TAR、TFRBoth at 950 ℃ with fluidizing gas at 50 vol.% H2O+50vol.％N2And T0At 20 ℃, the mass ratio of the iron ore to the copper ore is calculated to be about 80:20 based on the formulas (I), (II), (III) and (IV), and the complete combustion of the fuel and the self-heating operation of the fuel reactor can be simultaneously satisfied;
table 2 chemical composition analysis of iron and copper ores.
(2) Pretreatment: putting the copper ore powder and the iron ore powder into a drying box with the temperature of 105 ℃ for drying for 12h, then respectively heating the powders to 1000 ℃ in the air atmosphere at the heating rate of 5 ℃/min and calcining for 10 h. After cooling to room temperature, crushing and screening to obtain 0.15-0.35mm particles for later use;
(3) preparation: in the embodiment, a mechanical mixing mode is adopted, and the pretreated raw materials are fully mixed according to the mass ratio of 80:20 of iron ore to copper ore to obtain the overall thermally neutral oxygen carrier.
Results analysis results of differential thermal analysis of oxygen carriers during four cycles of redox reactions the results are shown in fig. 2, with the upward peak corresponding to an exothermic process and the downward peak corresponding to an endothermic process. Wherein the first two weaker exothermic peaks are corresponding to the oxygen carrier to generate reduction reaction in the fuel reactor, and the stronger exothermic peaks are corresponding to the oxygen carrier to perform oxidation process in the air reactor. As can be seen from fig. 2, the endothermic and exothermic process heat addition for the reduction process carried out in the fuel reactor is close to zero, overall exhibiting thermal neutrality.
The thermal neutral oxygen carrier particles prepared in the examples were tested for their coal chemical looping combustion reaction performance by a batch fluidized bed experiment. The coal type adopted in the experiment is high-grade anthracite, and the concrete working conditions of the experiment are as follows: reactor temperature 950 ℃, peroxide coefficient 1.0, reduction process atmosphere 50 vol.% H2O+50vol.％N2. In the experimental process, the CO in the tail gas is recorded by an on-line flue gas analyzer2、CO、CH4And H2The reactivity of the oxygen carrier particles was examined as shown in fig. 3. As can be seen from FIG. 3, the concentration of unconverted combustible gas during the reaction was at a lower level, indicating that the oxygen carrier particles produced had better reactivity.
It will be understood by those skilled in the art that the foregoing is only a preferred embodiment of the present invention, and is not intended to limit the invention, and that any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (8)
1. A method for obtaining thermal neutral oxygen carriers in a chemical looping combustion process, the method comprising the steps of:
(a) determining the oxygen carrier active component required in the reaction process according to the chemical looping combustion reaction, and constructing the ratio C of the oxygen carrier circulation amount to the oxygen carrier active component in the chemical looping combustion reaction processoxThe relation (one);
(b) based on the self-heating operation of the fuel reactor in the chemical looping combustion reaction, constructing a heat balance equation (II) of the heat absorption and release reactions involved in the fuel reactor, and solving the distribution ratio of each component in the oxygen carrier active ingredients for maintaining the self-heating operation of the fuel reactor according to the relational expression (I) and the equation (II) so as to further realize the acquisition of the heat neutral oxygen carrier; the obtained thermal neutral oxygen carrier can satisfy the balance of heat absorption and heat release in the fuel reactor, namely, the self-balance of the whole heat is realized.
2. The method for obtaining thermally neutral oxygen carriers in a chemical looping combustion process as claimed in claim 1, wherein in step (a), said relation (one) is preferably performed in the following manner:
wherein m is1The circulation flow rate of the oxygen carrier required for complete combustion of the fuel;
is the molar mass of oxygen; m isfuelIs the fuel flow rate; srStoichiometric ratio of oxygen required for complete combustion per mole of fuel; Δ X is the difference in the conversion of the oxygen carrier in the air reactor and the fuel reactor; coxIs the proportion of active ingredients in the oxygen carrier; mfuelIs the molar mass of the fuel.
3. The method for obtaining thermally neutral oxygen carriers in a chemical looping combustion process as claimed in claim 1, wherein in step (b), said equation (two) is preferably performed in the following manner:
mfuelΔHre+m1ΔHOC+mfuelΔHp+mFGΔHFG+ΔHLeither as 0 (two)
Wherein, Δ HreThe heat absorbed or released by the complete reaction of the fuel and the oxygen carrier in unit flow; Δ HOCThe oxygen carrier particles carry heat from the air reactor into the fuel reactor as a unit of circulation flow; Δ HpHeat absorbed for pyrolysis and gasification of fuel per flow rate; Δ HFGThe heat absorbed by the low-temperature fluidizing gas with unit flow; Δ HLIs the system heat loss; m isFGIs the flow of the fluidizing gas in the fuel reactor.
4. The method of claim 3, wherein Δ H is the level of the carrier of heat neutral oxygen in a chemical looping combustion processOCPreferably according to the following relationship:
ΔHOC＝cOC(TOC,AR-TOC,FR)
wherein, cOCIs the specific heat capacity of the oxygen carrier; t isOC,ARAnd TOC,FRThe temperature of the oxygen carrier particles in the air reactor and the fuel reactor, respectively.
5. The method of claim 3, wherein Δ H is the level of the carrier of heat neutral oxygen in a chemical looping combustion processFGPreferably according to the following relationship:
ΔHFG＝cFG(TFR-T0)
wherein, cFGThe specific heat capacity of the fluidizing gas; t isFRIs the operating temperature of the fuel reactor; t is0Is the initial temperature of the fluidizing gas.
6. The method for obtaining the thermally neutral oxygen carrier in the chemical looping combustion process as claimed in claim 1, wherein the active ingredients in the oxygen carrier are one or more, and for the oxygen carriers of multiple active ingredients, the mixing mode comprises physical mixing or granulation technology to make multiple active ingredients in one particle.
7. The method for obtaining the thermally neutral oxygen carrier in the chemical looping combustion process according to claim 1, wherein the active ingredient raw material in the oxygen carrier is solid particles or solution.
8. The method of claim 1, wherein the active component of the oxygen carrier is a transition metal oxide or a non-metal oxide.
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