CN210740681U - Gas boiler system - Google Patents
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- CN210740681U CN210740681U CN201921081082.1U CN201921081082U CN210740681U CN 210740681 U CN210740681 U CN 210740681U CN 201921081082 U CN201921081082 U CN 201921081082U CN 210740681 U CN210740681 U CN 210740681U
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Abstract
The utility model discloses a gas boiler system, gas boiler system includes single chemical chain combustion reactor, and chemical chain combustion reactor includes chemical chain combustion reaction room and first heat medium room, chemical chain combustion reaction room's one end and gas pipeline and air conduit link to each otherThe other end of the chemical-looping combustion reaction chamber is communicated with a flue gas pipeline, and an oxygen carrier is filled in the chemical-looping combustion reaction chamber; alternately introducing fuel and air into the chemical looping combustion reaction chamber, and alternately performing a reduction reaction process of an oxidation state oxygen carrier and an oxidation regeneration reaction process of a reduction state oxygen carrier, wherein the time of the oxidation regeneration reaction process is longer than that of the reduction reaction process; the heat medium in the heat medium chamber absorbs the reaction heat released in the reduction reaction process and the oxidation regeneration reaction process. The utility model discloses a gas boiler system has that the system is simple reliable, long service life, cost are low, energy utilization efficiency is high and NOxZero emission.
Description
Technical Field
The utility model relates to a boiler technical field, in particular to gas boiler system.
Background
The problems with conventional gas boilers can be summarized in three aspects, one being the low efficiency of energy utilization. This is because the dew point of water vapor in combustion flue gas is low (about 55 ℃), so that the latent heat of water vapor generated by combustion is hardly utilized, and the combustion flue gas amount is large, resulting in a large sensible heat loss. Second is NOxThe discharge amount of (a) is difficult to satisfy the discharge standard. The higher combustion temperature and direct mixing of the gas with air results in thermal NOxAnd rapid NOxIs generated. Thirdly, the CO in the gas fume2Low concentration (about 8% when the gas is natural gas), so CO2The energy consumption of the trapping process is large.
Around the problems of the conventional gas boiler, the chinese utility model patent No. zl201610222192.x discloses a gas boiler system as shown in fig. 1, which can improve the energy utilization efficiency of the gas boiler and realize NOxZero emission and CO2Near zero energy consumption CO capture2. However, the technology adopts two chemical-looping combustion reactors which are mutually switched, when one reactor carries out the reduction reaction process of the oxygen carrier in the oxidation state, the other reactor carries out the oxidation regeneration reaction process of the oxygen carrier in the reduction state, and when the two reactors respectively finish the reduction reaction process and the oxidation regeneration reaction process, the switching is carried out. This requires that the time required for completing the reduction of all the oxygen carriers in an oxidized state is the same as the time required for completing the oxidative regeneration of all the oxygen carriers in a reduced state, and the exothermic amount of the oxidative regeneration reaction of the oxygen carriers in a reduced state is obviously more than that of the reduction reaction of the oxygen carriers in an oxidized state, so that the temperature of the oxygen carriers rises sharply during the oxidative regeneration reaction, the temperature distribution of the oxygen carrier packed bed is also deteriorated remarkably, and the oxygen carriers are sintered at high temperature to cause the oxygen carriers to be sintered at high temperature to generate oxygen carriersThe service life is shortened. In addition, the above patent also has problems of complex system, poor reliability and high cost.
SUMMERY OF THE UTILITY MODEL
In view of this, the embodiment of the utility model provides a gas boiler system, the main objective is to simplify the system, improve system reliability and reduce system cost, avoids the temperature surge of oxygen carrier packed bed simultaneously, improves the temperature distribution of packed bed to improve the life of oxygen carrier.
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 gas boiler system, including a single chemical looping combustion reactor, where the chemical looping combustion reactor includes a chemical looping combustion reaction chamber and a first heat medium chamber, one end of the chemical looping combustion reaction chamber is communicated with a gas pipeline and an air pipeline, the other end of the chemical looping combustion reaction chamber is communicated with a flue gas pipeline, and an oxygen carrier is filled in the chemical looping combustion reaction chamber; gas and air are respectively and alternately introduced into the chemical-looping combustion reaction chamber through a gas pipeline and an air pipeline, the gas reacts with the oxidation-state oxygen carrier to generate reduction reaction product gas when the gas is introduced, the reduction reaction product gas is discharged through a flue gas pipeline, and meanwhile, the oxidation-state oxygen carrier is reduced into a reduction-state oxygen carrier; when air is introduced, the reduced oxygen carrier is oxidized and regenerated into an oxidized oxygen carrier by oxygen in the air, and the gas of the oxidation reaction product is discharged through a flue gas pipeline; the first heat medium chamber is connected with a first heat medium leading-in pipeline and a first heat medium leading-out pipeline.
Further, wherein the chemical looping combustion reactor is a shell-and-tube chemical looping combustion reactor, the shell-and-tube chemical looping combustion reactor comprises a first tube side and a first shell side, the first tube side is a chemical looping combustion reaction chamber, and the first shell side is a first heat medium chamber.
Further, a flue gas heat exchanger and a gas-water separator are arranged on the flue gas pipeline.
Further, the lower part of the oxygen carrier packed bed of the chemical looping combustion reaction chamber is filled with a heat accumulator; the lower end enclosure of the shell-and-tube chemical looping combustion reactor can be used as a gas-water separator.
Further, wherein the below of shell and tube type chemical chain combustion reactor be connected with shell and tube type gas heater, shell and tube type gas heater includes second tube side and second shell side, the second tube side with the chemical chain combustion reaction chamber communicates with each other, the second shell side is the second heat medium room, and it is connected with the leading-in pipeline of second heat medium and the pipeline is derived to the second heat medium, shell and tube type gas heater's low head is gas water separator, be equipped with the comdenstion water discharge pipeline on the low head.
Further, the second tube side of the shell-and-tube flue gas heat exchanger is filled with a heat accumulator.
Further, a one-way valve or an electromagnetic valve is respectively arranged on the gas pipeline and the air pipeline.
Further, a fuel component concentration sensor is arranged on the smoke pipeline.
Further, the oxygen carrier is a copper-based oxygen carrier or a multi-component oxygen carrier comprising a copper-based oxygen carrier.
Further, wherein the gas pipeline is provided with a gas fan, the air pipeline is provided with an air fan, the flue gas pipeline is provided with a three-way valve and a flue gas circulating pipeline, one end of the flue gas circulating pipeline is connected with a suction inlet of the air fan, and the other end of the flue gas circulating pipeline is connected with the three-way valve on the flue gas pipeline.
Compared with the prior art, the beneficial effects of the utility model reside in that:
the utility model discloses a gas boiler system is because single chemical chain combustion reactor has been adopted, still adopted simultaneously gas and air to let in from the same end of chemical chain combustion reaction chamber and the same mode of flow direction, therefore with the chemical chain combustion reactor who adopts two intercomwitches, and gas and air let in from the different end of chemical chain combustion reaction chamber and the prior art difference that the flow direction is opposite, need not to set up a lot of pipelines and solenoid valve or motorised valve (especially set up poor reliability on the high temperature flue gas pipeline, short service life, high-cost high temperature resistant solenoid valve or motorised valve), also only need set up a flue gas heat exchanger that is used for the gaseous waste heat recovery of reaction product simultaneously, and then, through filling the heat accumulator below the oxygen carrier that fills the bed in chemical chain combustion reaction chamber or connecting pipe shell type flue gas heat exchanger in the below of shell-and-tube type chemical chain combustion reactor, and the lower seal head of the shell-and-tube chemical looping combustion reactor or the lower seal head of the shell-and-tube flue gas heat exchanger is used as a gas-water separator, so that the external pipelines of the system are further reduced, the integration level of the system is improved, and the system is extremely simple and reliable and has low manufacturing cost.
In addition, 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.
The utility model discloses consider along with the lapse of gas boiler system operation duration, oxygen carrier's performance can deteriorate gradually and lead to partial fuel composition to discharge from flue gas pipeline, when the fuel composition concentration that fuel composition concentration sensor on flue gas pipeline measured is higher than fuel composition concentration setting value, take the method of starting the flow setting value of combustible component in the gas of small amplitude reduction reaction process from next reduction reaction process to guarantee that the gas obtains complete burning in the whole life cycle of gas boiler system.
In order to avoid forming mixed gas with explosion danger at an inlet of the chemical-looping combustion reactor during switching, after the reduction reaction process is completed, starting the air fan and switching a three-way valve on a flue gas pipeline to enable the reduction reaction product gas to flow back to the upper part of the chemical-looping combustion reactor through a flue gas circulating pipeline, flushing the fuel gas at the upper part of the chemical-looping combustion reactor, switching the three-way valve, and then leading air into the chemical-looping combustion reactor; similarly, after the oxidation regeneration reaction process is completed, the three-way valve on the flue gas pipeline is switched to enable the oxidation regeneration reaction product gas to flow back to the upper part of the chemical-looping combustion reactor through the flue gas circulation pipeline, the air on the upper part of the chemical-looping combustion reactor is washed, then the three-way valve is switched and the air fan is stopped, and then the fuel gas is led into the chemical-looping combustion reactor.
When the gas and the air are introduced from the same end of the chemical looping combustion reaction chamber, the gas and the air are usually normal temperature gas, and the exothermic quantity of the reaction at the inlet of the packed bed is gradually reduced to zero along with the gradual advance of the chemical looping combustion reaction from the inlet of the packed bed to the downstream, so that the temperature of the oxygen carrier bed layer at the inlet is reduced to be below the minimum temperature required for the chemical looping combustion reaction, namely the initiation temperature, so that the reaction in the next oxidation state oxygen carrier reduction reaction process or the reduction state oxygen carrier oxidation regeneration reaction process cannot occur, and finally the whole chemical looping combustion cannot be maintained. Therefore, the utility model discloses under the condition outside the explosion limit of gas all the time guaranteeing the gas of chemical chain combustion reactor entrance, adopted and mixed a small amount of air in the gas that lets in among oxidation state oxygen carrier reduction reaction process, and the method of mixing a small amount of gas in the air that lets in among reduction state oxygen carrier oxidation regeneration process, the oxygen carrier bed that makes oxygen carrier filling bed entrance side carries out chemical chain combustion reaction all the time and releases the reaction heat to can maintain the temperature on this oxygen carrier layer more than the initiation temperature of chemical chain combustion reaction all the time.
In addition, in the prior art that two groups of identical chemical looping combustion reactors are switched with each other, the reduction reaction process of the oxidation state oxygen carrier and the oxidation regeneration reaction process of the reduction state oxygen carrier must adopt the same proceeding time, otherwise, the two reactors cannot simultaneously maintain continuous chemical looping combustion reaction, reaction temperature and external heat supply. That is, it is necessary to complete the reduction of all the oxygen carriers in the oxidation state and the oxidation regeneration of the oxygen carriers in the reduction state in the same time, so that the reaction heat release power of the oxidation regeneration reaction process of the oxygen carriers in the reduction state is significantly higher than that of the oxidation reaction process of the oxygen carriers in the oxidation state (when the fuel gas is natural gas and the oxygen carriers are copper-based oxygen carriers, the reaction heat release power of the oxidation regeneration reaction process of the oxygen carriers in the reduction state is about 3.0 times of that of the reduction reaction process of the oxygen carriers in the oxidation regeneration process), and thus the oxygen carrier packed bed is inevitably subjected to temperature surge and temperature distribution deterioration in the oxidation regeneration process, so that the oxygen carriers are rapidly deteriorated by sintering and the bed pressure loss is rapidly increased, and the service life of the oxygen carriers is greatly reduced.
Taking methane 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 750 ℃ are as follows:
4CuO+CH4(g)＝4Cu+CO2(g)+2H2O(g)
△H＝-201.0kJ/mol
4Cu+2O2(g)＝4CuO
△H＝-599.9kJ/mol
different from the prior art, the utility model discloses an adopt single chemical chain combustion reactor for the reduction reaction process of oxidation state oxygen carrier and the oxidation regeneration reaction process of reduction state oxygen carrier adopt different time of carrying on separately for the possibility. Thus, under the condition that the proceeding time of the reduction reaction process of the oxidation state oxygen carrier is given, the proceeding time of the oxidation regeneration reaction process of the reduction state oxygen carrier which is longer than the proceeding time of the reduction reaction process of the oxidation state oxygen carrier is adopted to reduce the air flow of the oxidation regeneration process of the reduction state oxygen carrier, so that the reaction heat release power of the oxidation regeneration process can be reduced and even close to the reaction heat release power of the reduction process, the temperature surge of the oxygen carrier filling bed is avoided, the temperature distribution of the oxygen carrier filling bed is kept unchanged in the whole reduction reaction process and the oxidation regeneration reaction process, the service life of the oxygen carrier is greatly prolonged, and the stability of the external heat supply power is improved.
The utility model discloses gas boiler system because the dew point of reduction reaction process product gas is higher, so the latent heat of the vapor as gas combustion product can be retrieved basically. Therefore, the utility model discloses have apparent energy-conserving effect and economic benefits.
The gas boiler system of the embodiment of the utility model has the advantages that because the reaction temperature of the reduction reaction process and the oxidation regeneration reaction process of the oxygen carrier is lower,so that NO is not generatedxThereby realizing NOxAnd (4) zero emission. Therefore, the utility model discloses have apparent environmental benefit.
Drawings
FIG. 1 is a schematic view of a prior art gas boiler system.
Fig. 2 is a schematic view of a gas boiler system according to embodiment 1 of the present invention.
Fig. 3 is a schematic view of a gas boiler system according to embodiment 2 of the present invention.
Fig. 4 is a schematic view of a gas boiler system according to embodiment 3 of the present invention.
Fig. 5 is a schematic view of a gas boiler system according to embodiment 4 of the present invention.
Fig. 6 is a schematic view of a gas boiler system according to embodiment 5 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 gas boiler system according to embodiment 1 of the present invention. Referring to fig. 2, the present embodiment provides a gas boiler system including a single chemical looping combustion reactor 1;
the chemical looping combustion reactor 1 includes a chemical looping combustion reaction chamber 14 and a first heat medium chamber 15, and the first heat medium chamber 15 is used for accommodating a first heat medium which exchanges heat with the chemical looping combustion reaction chamber 14.
One end of the chemical-looping combustion reaction chamber 14 is communicated with the gas pipeline 6 and the air pipeline 8, the other end of the chemical-looping combustion reaction chamber is communicated with the flue gas pipeline 9, and an oxygen carrier is filled in the chemical-looping combustion reaction chamber 14.
Gas and air are respectively and alternately introduced into the chemical looping combustion reaction chamber 14 through a gas pipeline 6 and an air pipeline 8, the gas reacts with the oxidation state oxygen carrier to generate reduction reaction product gas when the gas is introduced, and the reduction reaction product gas is discharged through a flue gas pipeline 9, and meanwhile, the oxidation state oxygen carrier is reduced into a reduction state oxygen carrier; when air is introduced, the reduced oxygen carrier is oxidized by oxygen in the air to regenerate into an oxidized oxygen carrier, and the gas of the oxidation reaction product is discharged through a flue gas pipeline 9.
The first heating medium chamber 15 is connected to a first heating medium introduction pipe 10 and a first heating medium discharge pipe 11.
Chemical chain combustion reactor 1 be shell and tube type chemical chain combustion reactor, shell and tube type chemical chain combustion reactor includes first tube side 2 and first shell side 4, first tube side 2 is chemical chain combustion reaction chamber 14, first shell side 4 is first heat medium chamber 15.
The oxygen carrier is a copper-based oxygen carrier or a multi-component oxygen carrier comprising a copper-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 both strong exothermic reactions, and the characteristic is very favorable for maintaining the reaction temperature required by the reduction process by the reaction heat of the copper-based oxygen carrier and realizing the external heat supply. 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 components that should be provided as needed, which are not mentioned in the embodiments of the gas boiler system of the present invention, should be known to those skilled in the art. A gas fan 5 is arranged on the gas pipeline 6 to feed gas into the combustion reactor. An air blower 7 is arranged on the air pipeline 8 to send air into the combustion reactor. The fuel gas includes various kinds of gas such as natural gas, coal gasification gas, blast furnace gas, coke oven gas, converter blow-off gas, biomass gas, biogas, and gasification gas of various kinds of liquid fuels such as methanol.
When the gas and the air are introduced from the same end of the chemical looping combustion reaction chamber, the gas and the air are usually normal temperature gas, and the reaction heat release at the inlet of the oxygen carrier packed bed is gradually reduced to zero along with the gradual propulsion of the chemical looping combustion reaction from the inlet of the oxygen carrier packed bed to the downstream, so that the temperature of the oxygen carrier bed at the inlet is reduced to be below the minimum temperature required for the chemical looping combustion reaction, namely the initiation temperature, so that the reaction in the next oxidation state oxygen carrier reduction reaction process or the reduction state oxygen carrier oxidation regeneration reaction process cannot occur, and finally the whole chemical looping combustion cannot be maintained. Therefore, the embodiment of the utility model provides a under the condition that the gas of guaranteeing chemical chain combustion reactor entrance is outside the explosion limit of gas all the time, adopted and mixed a small amount of air in the gas that lets in oxidation state oxygen carrier reduction reaction process, and mixed a small amount of gas in the air that lets in the oxidation regeneration process of reduction state oxygen carrier, made the oxygen carrier bed layer of the inlet side of oxygen carrier bed 3 carry out chemical chain combustion reaction all the time and release the reaction heat to can maintain the temperature on this oxygen carrier layer above the initiation temperature of chemical chain combustion reaction all the time.
On the other hand, an embodiment of the present invention provides an operation method of a gas boiler system, please refer to fig. 2, the operation method includes the following steps:
s1, a reduction reaction process: in the chemical looping combustion reaction chamber 14, the fuel gas introduced through the fuel gas pipeline 6 reacts with the oxidation state oxygen carrier to generate reduction reaction product gas, the reduction reaction product gas is discharged through the flue gas pipeline 9, and meanwhile, the oxidation state oxygen carrier is reduced into a reduction state oxygen carrier; in the first heat medium chamber 15, the heat medium introduced through the first heat medium introduction pipe 10 absorbs the reaction heat of the reduction reaction, and then is discharged through the first heat medium discharge pipe 11; the time for the reduction reaction process to be carried out is set as t1, and the flow rate of combustible components in the fuel gas is set as F1;
s2, an oxidation regeneration reaction process: in the chemical looping combustion reaction chamber 14, oxygen in the air introduced through the air pipeline 8 reacts with the reduced oxygen carrier, the reduced oxygen carrier is oxidized and regenerated into an oxidized oxygen carrier, and the gas of the oxidized reaction product is discharged through the flue gas pipeline 9; in the first heat medium chamber 15, the heat medium introduced through the first heat medium introduction pipe 10 absorbs the reaction heat of the oxidation regeneration reaction, and then is discharged through the first heat medium discharge pipe 11; the time of the oxidation regeneration reaction process is set to t2, and the air flow rate is set to F2; controlling the time set value t2 of the oxidation and regeneration reaction process to be more than 1.0 time of the time set value t1 of the reduction reaction process, and controlling the air flow set value F2 to be less than 9.5 times of the flow set value F1 of combustible components in the fuel gas so as to reduce the reaction exothermic power of the oxidation and regeneration reaction process and enable the reaction exothermic power of the oxidation and regeneration reaction process to be close to the reaction exothermic power of the reduction reaction process;
s3, switching: when the reduction reaction process is carried out at t1, stopping introducing the fuel gas into the chemical looping combustion reaction chamber 14, and simultaneously introducing air with the flow rate of F2 into the chemical looping combustion reaction chamber 14 through the air pipeline 8; when the oxidation regeneration reaction process is carried out t2, the air feeding into the chemical looping combustion reaction chamber 14 is stopped, and meanwhile, the fuel gas with the flow rate of F1 is fed into the chemical looping combustion reaction chamber 14 through the fuel gas pipeline 6.
In specific implementation, the time set value t2 of the oxidation regeneration reaction process can be controlled to be 1.1-4.0 times of the time set value t1 of the reduction process, and the air flow set value F2 of the oxidation regeneration reaction process can be controlled to be 2.1-6.0 times of the flow set value F1 of combustible components in fuel gas of the reduction reaction process, so that the reaction exothermic power of the oxidation regeneration reaction process is close to the reaction exothermic power of the reduction reaction process. Preferably, the time set value t1 of the reduction reaction process is set to be 5-30 minutes.
In the specific implementation process, when the reduction reaction process is carried out, the gas with the flow rate of F1 is introduced, and simultaneously, the air with the flow rate of F3 is introduced, so that the inlet temperature of the oxygen carrier packed bed 3 is always kept above the minimum temperature required by the reduction state oxygen carrier oxidation regeneration reaction; when the oxidation regeneration reaction process is carried out, air with the flow rate of F2 is introduced, and simultaneously, fuel gas with the flow rate of F4 is introduced, so that the inlet temperature of the oxygen carrier packed bed 3 is always kept above the minimum temperature required by the reduction reaction of the oxygen carrier in an oxidation state. Preferably, the set value of the air flow F3 is set to be 0.5-15.0% of the set value of the flow F1 of combustible components in the fuel gas; and the set flow value F4 of combustible components in the fuel gas is set to be 0.5-4.0% of the set flow value F2.
In specific implementation, the reaction temperature of the reduction reaction process of the oxidation state oxygen carrier is preferably 300-800 ℃, and the reaction temperature of the oxidation regeneration process of the reduction state oxygen carrier is preferably 300-800 ℃. In the embodiment, the reaction temperature is controlled below 1000 ℃, and NO is not generated in the reaction productxThus, NO can be realizedxZero emission of (2).
Example 2
Fig. 3 is a schematic structural view of a 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 flue gas pipeline 9 is provided with a flue gas heat exchanger 20 and a gas-water separator 23.
The flue gas heat exchanger 20 is connected with a second heat medium leading-in pipeline 21 and a second heat medium leading-out pipeline 22; the gas-water separator 23 is provided with a condensed water discharge pipe 24 to discharge the condensed water.
The first heating medium and the second heating medium may be the same heating medium or different heating media.
On the other hand, the present embodiment further provides an operation method of a 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 condensate water produced in the flue gas heat exchanger is discharged through a condensate water discharge duct 24.
In specific implementation, the first heat medium and the second heat medium comprise water, heat conduction oil, saturated steam, superheated steam, air, various process gases and the like, so that a gas hot water boiler system, a gas heat conduction oil boiler system, a gas saturated steam boiler system, a gas superheated steam heating system, a gas hot air furnace system and the like are formed.
Example 3
Fig. 4 is a schematic structural view of a gas boiler system according to embodiment 3 of the present invention. Referring to fig. 4, the present embodiment is different from embodiment 1 in that the present embodiment further includes:
and a heat accumulator 32 is filled below the oxygen carrier filling bed 3 of the chemical looping combustion reaction chamber 14 and used for enhancing the heat exchange between the flue gas and the first heating medium so as to recover the heat of the flue gas. The heat accumulator of this example is a honeycomb ceramic.
The lower end enclosure 34 of the shell-and-tube chemical looping combustion reactor can be used as a gas-water separator, so that the external pipelines of the system are further reduced, and the integration level of the system is improved, so that the system is extremely simple and reliable and has low manufacturing cost; the lower head 34 is provided with a condensed water discharge pipe 24 to discharge condensed water.
The gas pipeline 6 and the air pipeline 8 are respectively provided with a one-way valve or an electromagnetic valve 12 and 13 to prevent the gas and the air from being mixed.
The present embodiment further provides an operation method of a gas boiler system, referring to fig. 4, which is different from embodiment 1 in that the operation method of the present embodiment further includes:
exchanging heat between the flue gas generated in the reduction reaction process of the step S1 and the oxidation regeneration reaction process of the step S2 and a second heating medium to recover heat from the flue gas;
in the reduction reaction process of step S1 and the oxidation regeneration reaction process of step S2, the gas and air are prevented from being mixed by installing check valves or electromagnetic valves 12, 13 on the gas pipe 6 and the air pipe 8, respectively;
water generated during the reduction reaction of step S1 and the oxidation regeneration reaction of step S2 is discharged through the condensed water discharge pipe 24.
Example 4
Fig. 5 is a schematic structural view of a gas boiler system according to embodiment 4 of the present invention. Referring to fig. 4, the present embodiment is different from embodiment 1 in that the present embodiment further includes:
a shell-and-tube flue gas heat exchanger 30 is connected to the lower part of the shell-and-tube chemical looping combustion reactor 1, the shell-and-tube flue gas heat exchanger 30 comprises a second tube pass 31 and a second shell pass 33, the second tube pass 31 is communicated with the chemical looping combustion reaction chamber 14, the second shell pass 33 is a second heat medium chamber 35 and is connected with a second heat medium introducing pipeline 21 and a second heat medium leading-out pipeline 22, and a lower end enclosure 34 of the shell-and-tube flue gas heat exchanger 30 can be used as a gas-water separator, so that the external pipeline of the system is further reduced, the integration level of the system is improved, and the system is extremely simple and reliable and has low manufacturing cost; the lower head 34 is provided with a condensed water discharge pipe 24 to discharge condensed water. Preferably, the first shell pass and the second shell pass are respectively provided with a liquid baffle plate for heating media so as to enhance the heat exchange capacity of the heating media.
The second tube side 31 of the shell-and-tube flue gas heat exchanger 30 is filled with a heat accumulator 32 to enhance the heat recovery of the flue gas and improve the utilization rate of energy to the maximum extent.
The flue gas pipeline 9 is provided with a fuel component concentration sensor 40 for detecting the concentration of the fuel components in the flue gas pipeline, and when the concentration of the fuel components is higher than the set value of the concentration of the fuel components, a method of slightly reducing the set value of the flow of combustible components in the fuel gas in the reduction reaction process from the next reduction reaction process is adopted to ensure that the fuel gas is completely combusted in the whole service life cycle of the gas-fired boiler system.
In specific implementation, the fuel component concentration sensor may be CH according to the type of the fuel gas4Concentration sensor, CO concentration sensor or H2A concentration sensor.
The gas pipeline 6 and the air pipeline 8 are respectively provided with a one-way valve or an electromagnetic valve 12 and 13 to prevent the mixing of gas and air.
The present embodiment further provides an operation method of a gas boiler system, referring to fig. 5, which is different from embodiment 1 in that steps S1-S2 of the operation method of the present embodiment are:
s1, a reduction reaction process: in the chemical looping combustion reaction chamber 14, the fuel gas introduced through the fuel gas pipeline 6 reacts with the oxidation state oxygen carrier to generate reduction reaction product gas, the reduction reaction product gas is discharged through the flue gas pipeline 9, and meanwhile, the oxidation state oxygen carrier is reduced into a reduction state oxygen carrier; in the first heat medium chamber 15, the heat medium introduced through the first heat medium introduction pipe 10 and the second heat medium introduction pipe 21 absorbs the reaction heat of the reduction reaction, and then is discharged through the first heat medium discharge pipe 11 and the second heat medium discharge pipe 22; the time for the reduction reaction process to be carried out is set as t1, and the flow rate of combustible components in the fuel gas is set as F1;
s2, an oxidation regeneration reaction process: in the chemical looping combustion reaction chamber 14, oxygen in the air introduced through the air pipeline 8 reacts with the reduced oxygen carrier, the reduced oxygen carrier is oxidized and regenerated into an oxidized oxygen carrier, and the gas of the oxidized reaction product is discharged through the flue gas pipeline 9; in the first heat medium chamber 15, the heat medium introduced through the first heat medium introduction pipe 10 and the second heat medium introduction pipe 21 absorbs the reaction heat of the oxidation regeneration reaction, and then is discharged through the first heat medium discharge pipe 11 and the second heat medium discharge pipe 22; the time of the oxidation regeneration reaction process is set to t2, and the air flow rate is set to F2; the time set value t2 of the oxidation regeneration reaction process is controlled to be more than 1.0 time of the time set value t1 of the reduction reaction process, and the air flow set value F2 is controlled to be less than 9.5 times of the flow set value F1 of combustible components in the fuel gas, so that the reaction exothermic power of the oxidation regeneration reaction process is reduced, and the reaction exothermic power of the oxidation regeneration reaction process is close to the reaction exothermic power of the reduction reaction process.
In specific implementation, the time set value t2 of the oxidation regeneration reaction process can be controlled to be 1.1-4.0 times of the time set value t1 of the reduction process, and the air flow set value F2 of the oxidation regeneration reaction process can be controlled to be 2.1-6.0 times of the flow set value F1 of combustible components in fuel gas of the reduction reaction process, so that the reaction exothermic power of the oxidation regeneration reaction process is close to the reaction exothermic power of the reduction reaction process. Preferably, when the oxygen carrier is a copper-based oxygen carrier and the fuel gas is natural gas, t2 is controlled to be about 3.1 times of t1, and F2 is controlled to be about 3.1 times of F1. Preferably, the time set value t1 of the reduction reaction process is set to be 5-30 minutes.
In the specific implementation process, when the reduction reaction process is carried out, the gas with the flow rate of F1 is introduced, and simultaneously, the air with the flow rate of F3 is introduced, so that the inlet temperature of the oxygen carrier packed bed 3 is always kept above the minimum temperature required by the reduction state oxygen carrier oxidation regeneration reaction; when the oxidation regeneration reaction process is carried out, air with the flow rate of F2 is introduced, and simultaneously, fuel gas with the flow rate of F4 is introduced, so that the inlet temperature of the oxygen carrier packed bed 3 is always kept above the minimum temperature required by the reduction reaction of the oxygen carrier in an oxidation state. Preferably, the set value of the air flow F3 is set to be 0.5-15.0% of the set value of the flow F1 of combustible components in the fuel gas; and the set flow value F4 of combustible components in the fuel gas is set to be 0.5-4.0% of the set flow value F2.
In specific implementation, the reaction temperature of the reduction reaction process of the oxidation state oxygen carrier is preferably 300-800 ℃, and the reaction temperature of the oxidation regeneration process of the reduction state oxygen carrier is preferably 300-800 ℃. In the embodiment, the reaction temperature is controlled below 1000 ℃, and NO is not generated in the reaction productxThus, NO can be realizedxZero emission of (2).
In specific implementation, when the fuel component concentration measured by the fuel component concentration sensor 40 on the flue gas pipeline 9 is higher than the fuel component concentration set value, the flow set value F1 of combustible components in the fuel gas in the reduction reaction process is reduced from the next reduction reaction process.
Preferably, the set concentration of the fuel component is 0.1-2.0% by volume, and the set flow F1 of the combustible component in the fuel gas in the reduction reaction process is 0.1-1.0% by volume.
In the reduction reaction process of step S1 and the oxidation regeneration reaction process of step S2, the gas pipe 6 and the air pipe 8 are respectively provided with check valves or electromagnetic valves 12 and 13 to prevent the gas and the air from mixing.
In practice, water generated during the reduction reaction of step S1 and the oxidation regeneration reaction of step S2 is discharged through the condensed water discharge line 24.
In specific implementation, the flue gas generated in the reduction reaction process of the step S1 and the oxidation regeneration reaction process of the step S2 exchanges heat with the second heating medium, so that the flue gas is subjected to heat recovery.
Example 5
Fig. 6 is a schematic structural view of a gas boiler system according to embodiment 5 of the present invention. Referring to fig. 5, the present embodiment is different from embodiment 4 in that the present embodiment further includes:
a three-way valve 50 and a flue gas circulating pipeline 60 are arranged on the flue gas pipeline 9, one end of the flue gas circulating pipeline 60 is connected with a suction inlet of the air fan 7, and the other end of the flue gas circulating pipeline 60 is connected with the three-way valve 50 on the flue gas pipeline 9; the three-way valve 50 can be used for conducting corresponding pipelines according to reaction requirements, and control is easy to realize. Of course, valves may be provided in each branch.
The present embodiment further provides an operation method of a gas boiler system, referring to fig. 6, which is different from embodiment 4 in that step S1 of the operation method of the present embodiment further includes:
in order to avoid forming mixed gas with explosion danger at the inlet of the chemical-looping combustion reactor during switching, after the reduction reaction process is carried out at t1, the air fan 7 is started, the three-way valve 50 on the flue gas pipeline 9 is switched, so that the product gas of the reduction reaction flows back to the upper part of the chemical-looping combustion reactor through the flue gas circulating pipeline 60, the fuel gas at the upper part of the chemical-looping combustion reactor is washed, and after the set time t3 of the fuel gas washing, the three-way valve 50 is switched, so that the air with the flow rate of F2 is introduced into the chemical-looping combustion reactor; after the oxidation regeneration reaction process is carried out at t2, the three-way valve 50 on the flue gas pipeline 9 is switched to make the oxidation regeneration reaction product gas flow back to the upper part of the chemical-looping combustion reactor through the flue gas circulation pipeline 60, the air at the upper part of the chemical-looping combustion reactor is flushed, after the set time t4 of air flushing, the three-way valve 50 is switched and the air fan 7 is stopped, so that the fuel gas with the flow rate of F1 is introduced into the chemical-looping combustion reactor.
Preferably, in this embodiment, the set value of the gas flushing time t3 is 0.1-1.0 min; the set value of the air flushing time t4 is 0.1-0.5 minutes.
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. A gas boiler system is characterized by comprising a single chemical-looping combustion reactor, wherein the chemical-looping combustion reactor comprises a chemical-looping combustion reaction chamber and a first heating medium chamber, one end of the chemical-looping combustion reaction chamber is communicated with a gas pipeline and an air pipeline, the other end of the chemical-looping combustion reaction chamber is communicated with a flue gas pipeline, and an oxygen carrier is filled in the chemical-looping combustion reaction chamber; gas and air are respectively and alternately introduced into the chemical-looping combustion reaction chamber through a gas pipeline and an air pipeline, the gas reacts with the oxidation-state oxygen carrier to generate reduction reaction product gas when the gas is introduced, the reduction reaction product gas is discharged through a flue gas pipeline, and meanwhile, the oxidation-state oxygen carrier is reduced into a reduction-state oxygen carrier; when air is introduced, the reduced oxygen carrier is oxidized and regenerated into an oxidized oxygen carrier by oxygen in the air, and the gas of the oxidation reaction product is discharged through a flue gas pipeline; the first heat medium chamber is connected with a first heat medium leading-in pipeline and a first heat medium leading-out pipeline.
2. A gas boiler system according to claim 1, characterized in that the chemical looping combustion reactor is a shell and tube chemical looping combustion reactor, which comprises a first tube side and a first shell side, the first tube side being a chemical looping combustion reaction chamber and the first shell side being a first heating medium chamber.
3. A gas boiler system according to claim 1, characterized in that a flue gas heat exchanger and a gas-water separator are arranged on the flue gas duct.
4. A gas boiler system according to claim 2, characterized in that the chemical looping combustion reaction chamber is filled with a heat accumulator below the oxygen carrier packed bed.
5. The gas boiler system according to claim 2, wherein a shell-and-tube type flue gas heat exchanger is connected to a lower portion of the shell-and-tube type chemical looping combustion reactor, the shell-and-tube type flue gas heat exchanger includes a second tube pass and a second shell pass, the second tube pass is communicated with the chemical looping combustion reactor, and the second shell pass is a second heat medium chamber, and a second heat medium introducing pipe and a second heat medium discharging pipe are connected to the second heat medium chamber.
6. A gas boiler system according to claim 5, characterized in that the second tube side of the shell-and-tube flue gas heat exchanger is filled with a thermal mass.
7. A gas boiler system as claimed in any one of claims 1 to 6, wherein the gas pipeline and the air pipeline are respectively provided with a check valve or an electromagnetic valve.
8. A gas boiler system as set forth in any of claims 1-6, characterized in that a fuel component concentration sensor is provided on said flue gas duct.
9. A gas boiler system as claimed in any one of claims 1 to 6, wherein the oxygen carrier is a copper-based oxygen carrier or a multi-component oxygen carrier comprising copper-based oxygen carriers.
10. A gas boiler system as claimed in any one of claims 1 to 6, wherein an air blower is provided on the air pipeline, a three-way valve and a flue gas circulation pipeline are provided on the flue gas pipeline, one end of the flue gas circulation pipeline is connected with a suction inlet of the air blower, and the other end of the flue gas circulation pipeline is connected with the three-way valve on the flue gas pipeline.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110319574A (en) * | 2019-07-11 | 2019-10-11 | 北京联力源科技有限公司 | A kind of gas-fired Boiler System and its operation method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110319574A (en) * | 2019-07-11 | 2019-10-11 | 北京联力源科技有限公司 | A kind of gas-fired Boiler System and its operation method |
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