CN210741117U - Diffusion gas boiler system and converter gas system comprising same - Google Patents
Diffusion gas boiler system and converter gas system comprising same Download PDFInfo
- Publication number
- CN210741117U CN210741117U CN201921081492.6U CN201921081492U CN210741117U CN 210741117 U CN210741117 U CN 210741117U CN 201921081492 U CN201921081492 U CN 201921081492U CN 210741117 U CN210741117 U CN 210741117U
- Authority
- CN
- China
- Prior art keywords
- gas
- looping combustion
- pipeline
- chemical looping
- steam
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Air Supply (AREA)
Abstract
The utility model discloses a diffuse gas boiler system and include its converter gas system, diffuse gas boiler system includes first chemical chain combustion reactor, and first chemical chain combustion reactor includes first chemical chain combustion reaction room and first heatThe upper part of the first chemical looping combustion reaction chamber is communicated with a first diffused gas pipeline and an air pipeline, the lower part of the first chemical looping combustion reaction chamber is communicated with a flue gas pipeline, and a first oxygen carrier is filled in the first chemical looping combustion reaction chamber; when gas is diffused, the diffused gas is led into a first chemical-looping combustion reaction chamber to carry out reduction reaction of a first oxygen carrier; when no coal gas is diffused, introducing air into the first chemical-looping combustion reaction chamber to perform oxidation regeneration reaction of the first oxygen carrier; the first heating medium in the first heating medium chamber absorbs the reaction heat of the reduction reaction and the oxidation regeneration reaction. The utility model discloses realize the effective utilization of diffusion coal gas and reduce environmental pollution, still have that the system is simple reliable and the cost is low, oxygen carrier is longe-lived and NOxZero emission.
Description
Technical Field
The utility model relates to a diffuse utilization of coal gas technical field, in particular to diffuse coal gas boiler system and include its converter gas system.
Background
In industrial fields such as steel and petrochemical industry, there are cases where a gas containing combustible components is discharged. For example, in the converter steelmaking process in the steel industry, the converter gas components do not reach the standard (for example, the volume fraction of CO is less than or equal to 20 percent, O is not more than2The volume fraction of the coal gas is more than or equal to 2 percent), and the effective utilization of the coal gas diffused by the converter is related to the economic benefit and the environmental responsibility of steel enterprises. However, since the converter off-gas is difficult to be used by the conventional technology due to intermittent generation, low calorific value and large fluctuation of calorific value, the off-gas is generally off-discharged directly to the atmosphere or off-discharged by igniting combustion using ignition fuel and combustion-supporting fuel having high calorific value, thereby causing serious problems of energy waste and air pollution.
FIG. 1 is a schematic diagram of a conventional converter gas treatment system. The converter gas generated by the converter 101 is subjected to heat recovery by a waste heat recovery device 102, is dedusted by a dedusting device 103, is blown into a gas component analyzer 105 by a gas fan 104, and is analyzed by the gas component analyzer 105, if the gas components reach the standard (for example, CO is more than or equal to 20%, O is more than or equal to 20%)2Less than or equal to 2 percent), opening the recovery side of the three-way valve 106 and closing the diffusion side, and sending the converter gas into a gas tank 107 for recycling; if the coal gas does not reach the standard, the diffusing side of the three-way valve 106 is opened, the recycling side is closed, and the converter diffused coal gas is sent to the diffusing tower 109 through a diffused coal gas pipeline 115 to be ignited, combusted and diffused or directly diffused. If various emergencies such as the gas tank 107 being full or the analyzer 105 being out of order occur, the need for the analyzer is highA large amount of converter gas which can be recycled in a cabinet and has extremely high CO concentration is also diffused, so that the problems of energy waste and environmental pollution exist, and the risks of CO poisoning and explosion also exist.
SUMMERY OF THE UTILITY MODEL
In view of this, the embodiment of the utility model provides a diffuse gas boiler system and include its converter gas system, the main objective is that the realization system is simple reliable and cost is low, reaction temperature controllability is good, energy utilization efficiency is high, oxygen carrier long service life, NOxZero emission, and can treat the diffused gas with large sudden amount and extremely high concentration of combustible components.
In order to achieve the above object, the utility model mainly provides the following technical scheme:
in one aspect, an embodiment of the present invention provides a bleeding gas boiler system, including a first chemical looping combustion reactor, where the first chemical looping combustion reactor includes a first chemical looping combustion reaction chamber and a first heat medium chamber, an upper portion of the first chemical looping combustion reaction chamber is communicated with a first bleeding gas pipeline and an air pipeline, a lower portion of the first chemical looping combustion reaction chamber is communicated with a flue gas pipeline, and a first oxygen carrier is filled in the first chemical looping combustion reaction chamber; the lower part of the first heat medium chamber is connected with a first heat medium leading-in pipeline, and the upper part of the first heat medium chamber is connected with a first heat medium leading-out pipeline.
Further, wherein first chemical looping combustion reactor is first shell and tube chemical looping combustion reactor, first shell and tube chemical looping combustion reactor includes first tube side and first shell side, first tube side is first chemical looping combustion reaction chamber, first shell side is first heat medium chamber.
Further, wherein diffuse gas boiler system still includes first steam-water separator, first heat medium is water, first steam-water separator's middle part with first heat medium is derived the pipe connection, first steam-water separator's top is equipped with first saturated steam and derives the pipeline, first steam-water separator's bottom is equipped with first water circulating line, first water circulating line with the middle part of first heat medium chamber is connected.
Further, the first chemical-looping combustion reaction chamber comprises a first oxygen carrier packed bed, and a second oxygen carrier is filled below the first oxygen carrier packed bed.
Further, a second shell-and-tube chemical looping combustion reactor is connected below the first shell-and-tube chemical looping combustion reactor, and the second shell-and-tube chemical looping combustion reactor comprises a second tube side and a second shell side; the second tube side is a second chemical looping combustion reaction chamber, a second oxygen carrier is filled in the second chemical looping combustion reaction chamber, and the second chemical looping combustion reaction chamber is communicated with the first chemical looping combustion reaction chamber; the second shell pass is a second heat medium chamber, the lower portion of the second heat medium chamber is connected with a second heat medium leading-in pipeline, and the upper portion of the second heat medium chamber is connected with a second heat medium leading-out pipeline.
Further, wherein the diffusion gas boiler system further comprises a second steam-water separator, the second heating medium is water, the middle of the second steam-water separator is connected with the second heating medium leading-out pipeline, a second saturated steam leading-out pipeline is arranged at the top of the second steam-water separator, a second water circulating pipeline is arranged at the bottom of the second steam-water separator, and the second water circulating pipeline is connected with the middle of the second heating medium chamber.
Further, an air fan and a one-way valve or an electromagnetic valve are arranged on the air pipeline.
Further, the first oxygen carrier and the second oxygen carrier are copper-based oxygen carriers or multi-component oxygen carriers comprising copper-based oxygen carriers and iron-based oxygen carriers.
On the other hand, the embodiment of the utility model provides a converter gas system including above-mentioned diffusion gas boiler system, converter gas system still includes converter gas processing subsystem; the converter gas treatment subsystem comprises a converter, a waste heat recovery device, a dust removal device, a gas fan, a gas component analyzer, a first three-way valve, a gas cabinet, a second three-way valve and a diffusion tower; the converter, the waste heat recovery device, the dust removal device, the coal gas fan, the coal gas component analyzer, the first three-way valve and the coal gas cabinet are sequentially connected through a converter coal gas pipeline; the first three-way valve, the second three-way valve and the diffusing tower are sequentially connected through a second diffusing gas pipeline; the second three-way valve is connected with the first diffused gas pipeline, and the second diffused gas pipeline is connected with the flue gas pipeline at a position between the second three-way valve and the diffusing tower.
Furthermore, a one-way valve or an electromagnetic valve is arranged on the smoke pipeline.
Compared with the prior art, the beneficial effects of the utility model reside in that:
the chemical-looping combustion boiler system for the diffused gas in the embodiment of the utility model adopts the shell-and-tube chemical-looping combustion reactor and the second chemical-looping combustion reaction chamber integrated with the shell-and-tube chemical-looping combustion reactor, so that the system is simple and reliable and has low manufacturing cost;
because water is used as a heating medium and the steam-water separator is arranged, high-temperature water at the bottom of the steam-water separator is circulated to the middle part of the heating medium chamber to guide low-temperature supplemented water into the lower part of the heating medium chamber, so that the chemical-looping combustion reaction chamber forms temperature distribution with the temperature rising along with the height increase, in addition, the temperature required by the chemical-looping combustion reaction can be ensured by controlling the pressure and the temperature of saturated steam (the pressure and the temperature of the first saturated steam are higher than those of the second saturated steam), thereby fully utilizing combustible components in the diffused coal gas, and simultaneously realizing more thorough heat recovery of reaction product gas. In addition, the service life of the oxygen carrier is prolonged by preventing the temperature of the oxygen carrier from rising sharply;
furthermore, by filling a second oxygen carrier having a higher active component loading amount than the first oxygen carrier below the first oxygen carrier filling bed, or by providing a second chemical-looping combustion reactor filled with the second oxygen carrier, safe handling and utilization of the released gas having a large amount of burstiness and an extremely high combustible component concentration is realized. In the case where there is no sudden large amount of the purge gas having a high combustible component concentration, an inexpensive heat storage body (for example, a honeycomb ceramic heat storage body) may be used instead of the second oxygen carrier.
In addition, by adopting the copper-based oxygen carrier containing the strong exothermic reaction of the reduction reaction and the oxidation regeneration reaction or the multi-component oxygen carrier containing the copper-based oxygen carrier and utilizing the heat storage function of the oxygen carrier, the contradiction between the intermittence of the released coal gas and the requirement on the continuity of the energy supply is solved;
taking CO and a copper-based oxygen carrier as an example, the calorific values of the reduction reaction of the oxidation state oxygen carrier and the oxidation regeneration reaction of the reduction state oxygen carrier at 400 ℃ are as follows:
CuO+CO(g)＝Cu+CO2(g)
△H＝-130.3kJ/mol
Cu+0.5O2(g)＝CuO
△H＝-153.1kJ/mol
in addition, because of the low temperature of the chemical looping combustion reaction, NO is not generated in the utilization of the diffused gasX。
Therefore, the utility model discloses economic and environmental benefit that has showing.
Drawings
FIG. 1 is a schematic diagram of a conventional converter gas treatment system.
Fig. 2 is a schematic view of a diffused gas chemical looping combustion boiler system according to embodiment 1 of the present invention.
Fig. 3 is a schematic view of a diffused gas chemical looping combustion boiler system according to embodiment 2 of the present invention.
Fig. 4 is a schematic view of a diffused gas chemical looping combustion boiler system according to embodiment 3 of the present invention.
Fig. 5 is a schematic view of a diffused gas chemical looping combustion boiler system according to embodiment 4 of the present invention.
Fig. 6 is a schematic view of a diffused gas chemical looping combustion boiler system according to embodiment 5 of the present invention.
Figure 7 is a schematic view of a converter gas system including a blow-off gas chemical looping combustion boiler according to example 6 of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following specific examples, which should not be construed as limiting the invention. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.
Example 1
Fig. 2 is a schematic structural view of a bleeding gas boiler system according to embodiment 1 of the present invention. Referring to fig. 2, the present embodiment provides a bleed gas boiler system comprising a first chemical looping combustion reactor 1;
the first chemical looping combustion reactor 1 comprises a first chemical looping combustion reaction chamber 5 and a first heating medium chamber 13, the upper part of the first chemical looping combustion reaction chamber 5 is communicated with a first diffused gas pipeline 6 and an air pipeline 8, the lower part of the first chemical looping combustion reaction chamber 5 is communicated with a flue gas pipeline 9, and a first oxygen carrier is filled in the first chemical looping combustion reaction chamber 5; a first heat medium introducing pipe 10 is connected to a lower portion of the first heat medium chamber 13, and a first heat medium discharging pipe 11 is connected to an upper portion of the first heat medium chamber 13.
First chemical looping combustion reactor 1 is first shell and tube chemical looping combustion reactor, first shell and tube chemical looping combustion reactor includes first tube side 2 and first shell side 4, first tube side 2 is first chemical looping combustion reaction chamber 5, first shell side 4 is first heat medium chamber 13.
The first chemical looping combustion reaction chamber 5 comprises a first oxygen carrier packed bed 3.
The first oxygen carrier is a copper-based oxygen carrier or a multi-component oxygen carrier comprising a copper-based oxygen carrier and an iron-based oxygen carrier, such as a copper-iron-based binary oxygen carrier or a copper-iron-nickel-based ternary oxygen carrier. By using the copper-based oxygen carrier or the multi-component oxygen carrier containing the copper-based oxygen carrier, although only one chemical looping combustion reactor alternately performs the reduction reaction process of the oxidation state oxygen carrier and the oxidation regeneration reaction process of the reduction state oxygen carrier, continuous and stable external heat supply can be realized.
In the oxygen carrier of the embodiment, the reduction reaction and the oxidation regeneration reaction of the copper-based oxygen carrier are strong exothermic reactions, and the characteristic is very favorable for maintaining the reduction process by self reaction heatThe required reaction temperature and the supply of heat to the outside are realized. With the component CH of fuel gas4CO and H2For example, the oxidation states of copper-based, iron-based, and nickel-based oxygen carriers are respectively associated with CH4CO and H2And the reduced state of (a) and (b) are respectively reacted with O2The reaction equation of the oxidative regeneration reaction of (1) and the heat of reaction at 600 ℃ are as follows:
4CuO+CH4(g)＝4Cu+CO2(g)+2H2O(g) △H＝-194.7kJ/mol
CuO+CO(g)＝Cu+CO2(g) △H＝-131.9kJ/mol
CuO+H2(g)＝Cu+H2O(g) △H＝-95.5kJ/mol
12Fe2O3+CH4(g)＝8Fe3O4+CO2(g)+2H2O(g) △H＝190.3kJ/mol
3Fe2O3+CO(g)＝2Fe3O4+CO2(g) △H＝-29.6kJ/mol
3Fe2O3+H2(g)＝2Fe3O4+H2O(g) △H＝6.6kJ/mol
4NiO+CH4(g)＝4Ni+CO2(g)+2H2O(g) △H＝144.3kJ/mol
NiO+CO(g)＝Ni+CO2(g) △H＝-46.8kJ/mol
NiO+H2(g)＝Ni+H2O(g) △H＝-10.6kJ/mol
2Cu+O2(g)＝2CuO △H＝-302.5kJ/mol
4Fe3O4+O2(g)＝6Fe2O3△H＝-494.9kJ/mol
2Ni+O2(g)＝2NiO △H＝-472.0kJ/mol
as can be seen from the above reaction formula, among the three oxygen carriers, only the reduction reaction of the oxidation state of the copper-based oxygen carrier is a strongly exothermic reaction. In addition, the skilled person in the art should know the components that should be arranged as required, which are not mentioned in the embodiments of the inventive bleeding gas boiler system. An air blower 7 is provided in said air duct 8 to feed air into the combustion reactor.
In another aspect, the present embodiment further provides an operation method of a diffusion gas boiler system, and referring to fig. 2, the operation method of the present embodiment includes the following steps:
s1, a reduction reaction process: when gas is diffused, the diffused gas is introduced into a first chemical-looping combustion reaction chamber 5 through a first diffused gas pipeline 6, combustible components in the diffused gas react with the oxidation state of a first oxygen carrier to generate reduction reaction product gas, the reduction reaction product gas is discharged through a flue gas pipeline 9, and meanwhile, the oxidation state of the first oxygen carrier is reduced to a reduction state; if the diffused coal gas contains oxygen, the oxygen reacts with the generated reduction-state oxygen carrier to generate an oxidation-state oxygen carrier;
s2, an oxidation regeneration reaction process: when no gas is released, starting an air fan 7, introducing air into the first chemical-looping combustion reaction chamber 5 through an air pipeline 8, oxidizing and regenerating the reduction state of the first oxygen carrier into an oxidation state by oxygen in the air, and discharging the oxidation reaction product gas through a flue gas pipeline 9;
s3, reaction heat absorption process: in the first heat medium chamber 13, the first heat medium introduced through the first heat medium introduction pipe 10 absorbs the reaction heat of the reduction reaction and the oxidation regeneration reaction, and is then discharged through the first heat medium discharge pipe 11.
In specific implementation, the reaction temperature of the reduction reaction and the oxidation regeneration reaction of the first oxygen carrier is more than 250 ℃.
Example 2
Fig. 3 is a schematic structural view of a bleeding gas boiler system according to embodiment 2 of the present invention. Referring to fig. 3, the present embodiment is different from embodiment 1 in that the present embodiment further includes:
the diffusion gas boiler system further comprises a first steam-water separator 30, the first heating medium is water, the middle of the first steam-water separator 30 is connected with the first heating medium leading-out pipeline 11, the top of the first steam-water separator 30 is provided with a first saturated steam leading-out pipeline 31, the bottom of the first steam-water separator 30 is provided with a first water circulation pipeline 33, and the first water circulation pipeline 33 is connected with the middle of the first heating medium chamber 13. The first saturated steam outlet pipeline 31 is provided with a first saturated steam pressure regulating valve 32 to regulate the pressure of the first saturated steam. A first saturated steam pressure sensor 34 is arranged on one side of the upper part of the first steam-water separator 30.
On the other hand, the present embodiment further provides an operation method of a diffusion gas boiler system, referring to fig. 3, which is different from embodiment 1 in that the operation method of the present embodiment further includes the following steps after the step S2:
s4, a first saturated steam generation process: the first heating medium is water, the first heating medium is introduced into the lower part of the first heating medium chamber 13 through a first heating medium introducing pipeline 10, the first heating medium absorbs the reaction heat of the reduction reaction and the oxidation regeneration reaction and generates a steam-water mixture, the steam-water mixture is introduced into the middle part of the first steam-water separator 30 from the upper part of the first heating medium chamber 13 through a first heating medium leading-out pipeline 11 for steam-water separation, the separated first saturated steam is sent out through a first saturated steam leading-out pipeline 32, and the water is reinjected to the middle part of the first heating medium chamber 13 through a first water circulating pipeline 33; the reaction temperature of the reduction reaction and the oxidation regeneration reaction of the first oxygen carrier is controlled by adjusting the pressure of the first saturated steam in the first steam-water separator 30, and the liquid level of the first steam-water separator 30 is controlled by adjusting the flow rate of the first heating medium.
Example 3
Fig. 4 is a schematic structural view of a bleeding gas boiler system according to embodiment 3 of the present invention. Referring to fig. 4, the present embodiment is different from embodiment 2 in that the present embodiment further includes:
the first chemical looping combustion reaction chamber 5 comprises a first oxygen carrier packed bed 3, and a second oxygen carrier or a heat accumulator is filled below the first oxygen carrier packed bed 3.
The air pipeline 8 is also provided with a one-way valve 12 or an electromagnetic valve 12.
The second oxygen carrier is a copper-based oxygen carrier or a multi-component oxygen carrier comprising a copper-based oxygen carrier and an iron-based oxygen carrier, such as a copper-iron-based binary oxygen carrier or a copper-iron-nickel-based ternary oxygen carrier, and the like, and the active component loading amount of the second oxygen carrier is higher than that of the first oxygen carrier; the rest of the process is the same as that of embodiment 1, and the description thereof is omitted. In this embodiment, the thermal mass may be a honeycomb ceramic thermal mass.
On the other hand, the present embodiment further provides an operation method of a diffusion gas boiler system, referring to fig. 4, which is different from the embodiment 2 in that steps S1 to S4 of the operation method of the present embodiment are:
s1, a reduction reaction process: when gas is diffused, the diffused gas is introduced into a first chemical-looping combustion reaction chamber 5 through a first diffused gas pipeline 6, combustible components in the diffused gas react with the oxidation state of a first oxygen carrier to generate reduction reaction product gas, the reduction reaction product gas is discharged through a flue gas pipeline 9, and meanwhile, the oxidation state of the first oxygen carrier is reduced to a reduction state;
s2, an oxidation regeneration reaction process: when no gas is released, starting an air fan 7, introducing air into the first chemical-looping combustion reaction chamber 5 through an air pipeline 8, oxidizing and regenerating the reduction states of the first oxygen carrier and the second oxygen carrier by oxygen in the air into an oxidation state, and discharging the oxidation reaction product gas through a flue gas pipeline 9;
s4, a first saturated steam generation process: the first heating medium is water, the first heating medium is introduced into the lower part of the first heating medium chamber 13 through a first heating medium introducing pipeline 10, the first heating medium absorbs the reaction heat of the reduction reaction and the oxidation regeneration reaction and generates a steam-water mixture, the steam-water mixture is introduced into the middle part of the first steam-water separator 30 from the upper part of the first heating medium chamber 13 through a first heating medium leading-out pipeline 11 for steam-water separation, the separated first saturated steam is sent out through a first saturated steam leading-out pipeline 32, and the water is reinjected to the middle part of the first heating medium chamber 13 through a first water circulating pipeline 33; the reaction temperature of the reduction reaction and the oxidation regeneration reaction of the first oxygen carrier and the second oxygen carrier is controlled by adjusting the pressure of the first saturated steam in the first steam-water separator 30, and the liquid level of the first steam-water separator 30 is controlled by adjusting the flow rate of the first heating medium.
In specific implementation, when the diffusion time of the coal gas is prolonged and/or the concentration of combustible components in the diffused coal gas is increased, unreacted combustible components in the reduction product gas at the outlet of the first oxygen carrier filling bed enter the second oxygen carrier filling bed to react with the oxidation state of the second oxygen carrier to generate reduction reaction product gas, and the oxidation state of the second oxygen carrier is reduced to the reduction state; when the gas diffusion time in the previous reduction reaction process is prolonged and/or the concentration of combustible components in the diffused gas is increased, the air flow is increased in the following two or more oxidation regeneration reaction processes, so that the reduction state of the second oxygen carrier is gradually oxidized and regenerated into an oxidation state by unreacted oxygen in the oxidation regeneration reaction products at the outlet of the first oxygen carrier filling bed; and after the reduction state of the second oxygen carrier is completely oxidized and regenerated into an oxidation state, the air flow is adjusted back to the original flow value.
In the reduction reaction process, when the diffusion time of the coal gas is prolonged and/or the concentration of combustible components in the diffused coal gas is increased, the air fan is started while the diffused coal gas is introduced, and air is introduced to maintain the inlet temperature of the second oxygen carrier packed bed 22 at more than 250 ℃.
In specific implementation, the air flow is 5-50% of the flow of combustible components in the diffused coal gas.
In specific implementation, the reaction temperature of the reduction reaction and the oxidation regeneration reaction of the first oxygen carrier and the second oxygen carrier is more than 250 ℃.
In the reduction reaction process, when the diffusion time of the coal gas is not prolonged and/or the concentration of combustible components in the diffused coal gas is not increased, the second oxygen carrier or the heat accumulator plays a role in enhancing the heat exchange between the oxidation regeneration reaction product gas and the reduction reaction product gas and the first heating medium or the second heating medium.
Example 4
Fig. 5 is a schematic structural view of a bleeding gas boiler system according to embodiment 4 of the present invention. Referring to fig. 5, the present embodiment is different from embodiment 3 in that the present embodiment further includes:
a second shell-and-tube chemical looping combustion reactor is connected below the first shell-and-tube chemical looping combustion reactor; the second shell-and-tube chemical looping combustion reactor comprises a second tube side 21 and a second shell side 23; the second tube side 21 is a second chemical looping combustion reaction chamber 24, a second oxygen carrier is filled in the second chemical looping combustion reaction chamber 24, the second chemical looping combustion reaction chamber 24 comprises a second oxygen carrier filling bed 22, and the second chemical looping combustion reaction chamber 24 is communicated with the first chemical looping combustion reaction chamber 5; the second shell pass 23 is a second heat medium chamber 25, a second heat medium introducing pipe 26 is connected to the lower part of the second heat medium chamber 25, and a second heat medium leading-out pipe 27 is connected to the upper part of the second heat medium chamber 25.
On the other hand, the present embodiment further provides an operation method of a diffused gas boiler system, referring to fig. 5, which is different from embodiment 3 in that step S4 of the operation method of the present embodiment is specifically:
first saturated steam generation process: the first heat medium is water, the first heat medium and the second heat medium are respectively introduced to the lower parts of the first heat medium chamber 13 and the second heat medium chamber 25 through the first heat medium introduction pipeline 10 and the second heat medium introduction pipeline 26, the first heat medium and the second heat medium respectively absorb the reaction heat of the reduction reaction and the oxidation regeneration reaction and generate a steam-water mixture, the steam-water mixture is introduced from the upper part of the first heat medium chamber 13 through the first heat medium derivation pipeline 11 into the middle part of the first steam-water separator 30 for steam-water separation, the separated first saturated steam is delivered through the first saturated steam derivation pipeline 32, the water is reinjected to the middle part of the first heat medium chamber 13 through the first water circulation pipeline 33, or the steam-water mixture is delivered through the second heat medium derivation pipeline 27; the reaction temperature of the reduction reaction and the oxidation regeneration reaction of the first oxygen carrier and the second oxygen carrier is controlled by adjusting the pressure of the first saturated steam in the first steam-water separator 30, and the liquid level of the first steam-water separator 30 is controlled by adjusting the flow rate of the first heating medium.
Example 5
Fig. 6 is a schematic structural view of a bleeding gas boiler system according to embodiment 5 of the present invention. Referring to fig. 6, the present embodiment is different from embodiment 4 in that the present embodiment further includes:
the diffuse gas boiler system still include second steam-water separator 40, the second heat medium is water, the middle part of second steam-water separator 40 with the second heat medium is derived pipeline 27 and is connected, the top of second steam-water separator 40 is equipped with second saturated steam and derives pipeline 41, the bottom of second steam-water separator 40 is equipped with second water circulating line 43, second water circulating line 43 with the middle part of second heat medium chamber is connected.
On the other hand, the present embodiment further provides an operation method of a diffusion gas boiler system, referring to fig. 6, which is different from embodiment 4 in that the operation method of the present embodiment further includes the following steps after the step S4:
s5, a second saturated steam generation process: the second heating medium is water, the second heating medium is introduced into the lower part of the second heating medium chamber 25 through a second heating medium introducing pipeline 26, the second heating medium absorbs heat of reduction reaction product gas and oxidation regeneration reaction product gas entering the second chemical-looping combustion reaction chamber 24 and generates a steam-water mixture, the steam-water mixture is introduced into the middle part of the second steam-water separator 40 from the upper part of the second heating medium chamber 25 through a second heating medium leading-out pipeline 27 for steam-water separation, the separated second saturated steam is sent out through a second saturated steam leading-out pipeline 41, and the water is reinjected to the middle part of the second heating medium chamber 25 through a second water circulating pipeline 43; the flue gas temperature at the outlet of the second chemical looping combustion reactor is controlled by adjusting the pressure of saturated steam in the second steam-water separator 40, and the liquid level of the second steam-water separator 40 is controlled by adjusting the flow of the second heating medium.
Example 6
Figure 7 is a schematic view of a converter gas system including a blow-off gas chemical looping combustion boiler according to example 6 of the present invention. Referring to fig. 7, the present embodiment is different from embodiment 5 in that the present embodiment further includes: a subsystem for treating the coal gas of the converter,
the converter gas treatment subsystem comprises a converter 101, a waste heat recovery device 102, a dust removal device 103, a gas fan 104, a gas component analyzer 105, a first three-way valve 106, a gas tank 107, a second three-way valve 110 and a diffusion tower 109; the converter 101, the waste heat recovery device 102, the dust removal device 103, the gas fan 104, the gas component analyzer 105, the first three-way valve 106 and the gas tank 107 are sequentially connected through a converter gas pipeline 108, and the first three-way valve 106, the second three-way valve 110 and the diffusion tower 109 are sequentially connected through a second diffusion gas pipeline 112; the second three-way valve 110 is connected with the first diffusion gas pipeline 6, the second diffusion gas pipeline 112 is connected with the flue gas pipeline 9 at a position between the second three-way valve 110 and the diffusion tower 109, and the flue gas pipeline 9 is provided with a one-way valve 111 or an electromagnetic valve 111.
On the other hand, the present embodiment further provides an operation method of a converter gas treatment system including a blow-off gas chemical looping combustion boiler, referring to fig. 7, which is different from the embodiment 5 in that steps S1 to S2 of the operation method of the present embodiment are:
s1, a reduction reaction process: the converter gas generated by the converter 101 is subjected to heat recovery by a waste heat recovery device 102, is dedusted by a dedusting device 103, is blown into a gas component analyzer 105 by a gas fan 104, and is analyzed by the gas component analyzer 105, if the gas components reach the standard (for example, the volume fraction of CO is more than or equal to 10%, O is more than or equal to 10%)2The volume fraction is less than or equal to 2%), the recovery side of the first three-way valve 106 is opened, the diffusion side is closed, and the converter gas is sent into a gas tank 107 for recycling; if the gas components do not reach the standard, opening the diffusion side of a first three-way valve 106 and closing the recovery side, opening the first diffusion gas pipeline side of a second three-way valve 110 and closing the diffusion tower side, introducing the converter diffusion gas into a first chemical chain combustion reaction chamber 5 and a second chemical chain combustion reaction chamber 24 through a first diffusion gas pipeline 6, respectively reacting combustible components in the diffusion gas with the oxidation states of a first oxygen carrier and a second oxygen carrier to generate reduction reaction product gas, discharging the reduction reaction product gas to a diffusion tower 109 through a flue gas pipeline 9 and a second diffusion gas pipeline 112 for discharging, and simultaneously respectively reducing the oxidation states of the first oxygen carrier and the second oxygen carrier to the reduction states;
s2, an oxidation regeneration reaction process: when no gas is diffused, the diffusing tower side of the second three-way valve 110 is opened to close the first diffusing gas pipeline side, the air fan is started, air is introduced into the first chemical-looping combustion reaction chamber 5 and the second chemical-looping combustion reaction chamber 24 through the air pipeline 8, the reduction states of the first oxygen carrier and the second oxygen carrier are oxidized and regenerated into oxidation states by oxygen in the air, and the oxidation reaction product gas is discharged through the flue gas pipeline 9, the second diffusing gas pipeline 112 and the diffusing tower 109.
In the foregoing embodiments, the descriptions of the respective embodiments have respective emphasis, and for parts that are not described in detail in a certain embodiment, reference may be made to related descriptions of other embodiments.
The features of the invention claimed in the claims and/or in the description may be combined, but the combination is not limited to the combination defined in the claims by the reference. The technical solution obtained by combining the technical features in the claims and/or the specification is also the scope of the present invention.
The above description is only for the specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art can easily think of the changes or substitutions within the technical scope of the present invention, and all should be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. The diffused gas boiler system is characterized by comprising a first chemical looping combustion reactor, wherein the first chemical looping combustion reactor comprises a first chemical looping combustion reaction chamber and a first heating medium chamber, the upper part of the first chemical looping combustion reaction chamber is communicated with a first diffused gas pipeline and an air pipeline, the lower part of the first chemical looping combustion reaction chamber is communicated with a flue gas pipeline, and a first oxygen carrier is filled in the first chemical looping combustion reaction chamber; the lower part of the first heat medium chamber is connected with a first heat medium leading-in pipeline, and the upper part of the first heat medium chamber is connected with a first heat medium leading-out pipeline.
2. The bleed gas boiler system of claim 1, wherein the first chemical looping combustion reactor is a first shell-and-tube chemical looping combustion reactor comprising a first tube-side and a first shell-side, the first tube-side being a first chemical looping combustion reaction chamber and the first shell-side being a first heating medium chamber.
3. The bleeding gas boiler system according to claim 2, further comprising a first steam-water separator, wherein the first heating medium is water, the middle portion of the first steam-water separator is connected to the first heating medium outlet pipe, a first saturated steam outlet pipe is provided at the top of the first steam-water separator, a first water circulation pipe is provided at the bottom of the first steam-water separator, and the first water circulation pipe is connected to the middle portion of the first heating medium chamber.
4. The bleeding gas boiler system of claim 3, wherein the first chemical looping combustion reaction chamber comprises a first packed bed of oxygen carriers, the first packed bed of oxygen carriers being packed with a second oxygen carrier or thermal mass below.
5. The bleed gas boiler system of claim 4, wherein a second shell-and-tube chemical looping combustion reactor is connected below the first shell-and-tube chemical looping combustion reactor, and the second shell-and-tube chemical looping combustion reactor comprises a second tube side and a second shell side; the second tube pass is a second chemical looping combustion reaction chamber, a second oxygen carrier or a heat accumulator is filled in the second chemical looping combustion reaction chamber, and the second chemical looping combustion reaction chamber is communicated with the first chemical looping combustion reaction chamber; the second shell pass is a second heat medium chamber, the lower portion of the second heat medium chamber is connected with a second heat medium leading-in pipeline, and the upper portion of the second heat medium chamber is connected with a second heat medium leading-out pipeline.
6. The bleeding gas boiler system according to claim 5, further comprising a second steam-water separator, wherein the second heating medium is water, the middle part of the second steam-water separator is connected to the second heating medium outlet pipe, a second saturated steam outlet pipe is provided at the top of the second steam-water separator, a second water circulation pipe is provided at the bottom of the second steam-water separator, and the second water circulation pipe is connected to the middle part of the second heating medium chamber.
7. The bleeding gas boiler system of claim 6, wherein said air duct is provided with an air blower and a one-way valve or a solenoid valve.
8. The bleed gas boiler system of claim 7, wherein the first and second oxygen carriers are copper-based oxygen carriers or multi-element oxygen carriers comprising copper-based and iron-based oxygen carriers.
9. A converter gas system comprising the bleeding gas boiler system of any one of claims 1 to 8, further comprising a converter gas treatment subsystem; the converter gas treatment subsystem comprises a converter, a waste heat recovery device, a dust removal device, a gas fan, a gas component analyzer, a first three-way valve, a gas cabinet, a second three-way valve and a diffusion tower; the converter, the waste heat recovery device, the dust removal device, the coal gas fan, the coal gas component analyzer, the first three-way valve and the coal gas cabinet are sequentially connected through a converter coal gas pipeline; the first three-way valve, the second three-way valve and the diffusing tower are sequentially connected through a second diffusing gas pipeline; the second three-way valve is connected with the first diffused gas pipeline, and the second diffused gas pipeline is connected with the flue gas pipeline at a position between the second three-way valve and the diffusing tower.
10. The converter gas system according to claim 9, wherein a one-way valve or an electromagnetic valve is provided on the flue gas conduit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921081492.6U CN210741117U (en) | 2019-07-11 | 2019-07-11 | Diffusion gas boiler system and converter gas system comprising same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921081492.6U CN210741117U (en) | 2019-07-11 | 2019-07-11 | Diffusion gas boiler system and converter gas system comprising same |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210741117U true CN210741117U (en) | 2020-06-12 |
Family
ID=70980833
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921081492.6U Active CN210741117U (en) | 2019-07-11 | 2019-07-11 | Diffusion gas boiler system and converter gas system comprising same |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210741117U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110319708A (en) * | 2019-07-11 | 2019-10-11 | 北京联力源科技有限公司 | Emission coal gas boiler system, its operation method and the converter gas system including it |
| CN116753528A (en) * | 2023-08-18 | 2023-09-15 | 河北富莱尔环保节能工程有限公司 | Converter gas high-efficiency utilization and power generation system |
-
2019
- 2019-07-11 CN CN201921081492.6U patent/CN210741117U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110319708A (en) * | 2019-07-11 | 2019-10-11 | 北京联力源科技有限公司 | Emission coal gas boiler system, its operation method and the converter gas system including it |
| CN116753528A (en) * | 2023-08-18 | 2023-09-15 | 河北富莱尔环保节能工程有限公司 | Converter gas high-efficiency utilization and power generation system |
| CN116753528B (en) * | 2023-08-18 | 2023-11-21 | 河北富莱尔环保节能工程有限公司 | Converter gas high-efficiency utilization and power generation system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111655609B (en) | Fuel chemical-looping hydrogen production system and method | |
| CN106247323B (en) | A kind of chemical chain combustion apparatus and its method based on tower bubbling fluidized bed fuel reactor | |
| CN210741117U (en) | Diffusion gas boiler system and converter gas system comprising same | |
| JP6453349B2 (en) | Carbon dioxide combustion method using in situ oxygen generation and chemical loop combustion | |
| CN105757641B (en) | Gas-fired Boiler System and its operation method | |
| WO2018162675A4 (en) | Method and system for gas capture comprising by circulating sorbent | |
| JP5165832B2 (en) | Hydrogen generating apparatus and method | |
| CN101349423B (en) | Double-circulating fluid bed system for chemical chain combustion | |
| US9314740B2 (en) | Chemical looping removal of ventilation air methane | |
| US11697157B2 (en) | Incineration apparatus and method | |
| CN110319708A (en) | Emission coal gas boiler system, its operation method and the converter gas system including it | |
| WO2010091642A1 (en) | Chemical-looping combustion method and system | |
| CN210740681U (en) | Gas boiler system | |
| CN110319574A (en) | A kind of gas-fired Boiler System and its operation method | |
| JP6913822B2 (en) | Acid gas processing and power generation process | |
| CN115143455A (en) | Novel chemical looping combustion method comprising hydrogen production process | |
| US20210197158A1 (en) | Reactor for Heating a Gas and Uses Thereof | |
| CN210237115U (en) | Raw material gas conversion heat supply system for ammonia synthesis process | |
| CN109266373A (en) | A kind of coal chemical industry power polygenerations systeme based on Cabase compound | |
| TWI747571B (en) | Interconnected fluidized bed reactor | |
| CN203147748U (en) | Solid fuel chemical-looping combustion device of circulating fluidized bed | |
| CN203147747U (en) | Solid fuel half-pressurizing chemical-looping combustion device of circulating fluidized bed | |
| WO2023286721A1 (en) | Gas production device, gas production system, and gas production method | |
| US20240116757A1 (en) | Methods for chemical process heating with carbon capture | |
| CN208952077U (en) | A kind of burning chemistry chains system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |