CN117525493A - Method and device for controlling start-up of cascade reformer and SOFC power generation system - Google Patents
Method and device for controlling start-up of cascade reformer and SOFC power generation system Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000010248 power generation Methods 0.000 title claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 132
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 38
- 239000003546 flue gas Substances 0.000 claims description 34
- 230000008859 change Effects 0.000 claims description 15
- 238000002407 reforming Methods 0.000 abstract description 15
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 54
- 239000000446 fuel Substances 0.000 description 21
- 239000001257 hydrogen Substances 0.000 description 10
- 229910052739 hydrogen Inorganic materials 0.000 description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 9
- 230000008569 process Effects 0.000 description 7
- 238000006057 reforming reaction Methods 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000000630 rising effect Effects 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- -1 oxygen ions Chemical class 0.000 description 3
- 238000004321 preservation Methods 0.000 description 3
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
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- 238000010792 warming Methods 0.000 description 2
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- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
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- 238000009833 condensation Methods 0.000 description 1
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- 238000011217 control strategy Methods 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
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- 238000000629 steam reforming Methods 0.000 description 1
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
- H01M8/04089—Arrangements for control of reactant parameters, e.g. pressure or concentration of gaseous reactants
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/043—Processes for controlling fuel cells or fuel cell systems applied during specific periods
- H01M8/04302—Processes for controlling fuel cells or fuel cell systems applied during specific periods applied during start-up
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04313—Processes for controlling fuel cells or fuel cell systems characterised by the detection or assessment of variables; characterised by the detection or assessment of failure or abnormal function
- H01M8/0432—Temperature; Ambient temperature
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
- H01M8/04701—Temperature
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
- H01M8/04298—Processes for controlling fuel cells or fuel cell systems
- H01M8/04694—Processes for controlling fuel cells or fuel cell systems characterised by variables to be controlled
- H01M8/04746—Pressure; Flow
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- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
- H01M8/2465—Details of groupings of fuel cells
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
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Abstract
The method determines a control instruction according to the demand of the SOFC stack for reformed gas, starts the reformers step by step according to the control instruction and the gas supply quantity of each level of reformers, distributes the reformed gas flow demand of the SOFC stack to reformers of different levels, can protect the safety of the reformers and the SOFC stack to the maximum extent, obviously improves the reliability of the integral operation of the SOFC power generation system, and simultaneously improves the service life of each device of the system; the reformers at all levels are started step by step according to the gas-available quantity, so that the time for the whole system to respond to fluctuation of the reforming gas quantity is shorter, and the working efficiency of the system is greatly improved.
Description
Technical Field
The invention belongs to reformer control technology, and particularly relates to a start control method and device of a cascade reformer and an SOFC power generation system.
Background
With the rapid development of social economy, environmental pollution and continuous worsening of energy safety problems generated in the use process of traditional fossil fuels, clean energy technology is rising worldwide. The solid oxide fuel cell (Solid Oxide Fuel Cell, SOFC) is one of fuel cells, has higher comprehensive thermal efficiency and wider fuel selection, and is particularly suitable for applications requiring high-efficiency energy conversion and clean energy, such as distributed energy systems, fixed power stations, power grid peak shaving stations and the like.
The hydrogen has higher combustion efficiency, belongs to clean energy sources, and is widely applied to fuel cells, but because the hydrogen storage and transportation conditions are harsh, the hydrogen is produced by reforming methanol and is used for SOFC cells or electric pile systems.
When the SOFC electric pile is actually operated, different states exist due to different operation strategies, the electric pile system formed by the SOFC electric pile is operated with different fluctuation power, the flow of reformed gas of the methanol reformer is required to fluctuate along with the power fluctuation of the SOFC electric pile system, the repeated thermal change is not friendly to a catalyst and a reactor of the methanol reformer, the prior art has a control strategy for starting the reformer, and the thermal inertia of the electric pile system is not effectively treated, so that the response of the reformer to the electric pile system is not timely.
Disclosure of Invention
Based on this, the present invention aims to provide a method and apparatus for controlling the start-up of a cascade reformer and an SOFC power generation system, so as to at least overcome the above-mentioned drawbacks of the prior art.
In a first aspect, the present invention provides a start-up control method of a cascade reformer including at least two stages of reformers, each stage of reformers in the cascade reformer being arranged stepwise according to an suppliable amount, the start-up control method comprising:
obtaining the reformed gas demand of the SOFC stack;
generating control instructions of the cascade reformer according to the reformed gas demand;
and controlling the step-by-step starting of each level of reformers according to the control instruction and the air supply quantity of each level of reformers so as to realize the air supply to the SOFC stack.
Further, controlling the stage-wise start of the stages of reformers according to the control instruction and the gas-controllable amount of the stages of reformers comprises:
acquiring the gas-controllable quantity of each level of reformer;
based on the control instruction, each stage of reformer is started step by step from low to high in the gas supply amount.
Further, based on the control instruction, starting the reformer of each stage stepwise from low to high in the gas supply amount includes:
starting a reformer of a minimum level of the suppliable gas amount based on the control instruction;
when the gas supply amount of the reformer with the smallest gas supply amount can not meet the reformed gas demand of the SOFC stack, starting the reformers with the secondary gas supply amounts until the sum of the gas supply amounts of the reformers with the different stages meets the reformed gas demand of the SOFC stack.
Further, the start control method further includes:
acquiring temperature change information of the SOFC stack;
and determining the reformed gas demand of the SOFC stack according to the temperature change information.
Further, the start control method further includes:
and controlling the high-temperature flue gas to be led into each stage of reformers step by step from low to high according to the gas-feeding quantity.
Further, the start control method further includes:
the flow of the high-temperature flue gas is controlled to control the preheating temperature of the reformers, so that the starting time of each stage of reformers is matched with the temperature switching time of the SOFC stack.
In a second aspect, the present invention provides a start-up control device for a cascade reformer, comprising:
a reformed gas amount acquisition unit configured to acquire a reformed gas demand amount of the SOFC stack;
an instruction generation unit configured to generate a control instruction of the cascade reformer according to the reformed gas demand;
and the control unit is configured to control the step-by-step starting of each level of reformers according to the control instruction and the air-controllable quantity of each level of reformers so as to realize the air supply to the SOFC stack.
Further, the start control device further includes:
and the temperature information acquisition unit is configured to acquire temperature change information of the SOFC stack.
In a third aspect, the present invention provides a SOFC power generation system based on a cascade reformer, comprising a cascade reformer, a controller and a SOFC stack system;
the cascade reformers comprise at least two stages of reformers, all stages of reformers in the cascade reformers are arranged in a cascade mode according to the gas-controllable quantity, reformers at the same stage are connected in parallel, and reformed gas generated by each stage of reformers is distributed to the SOFC stack system under the control of the controller;
the controller is respectively connected with the cascade reformer and the SOFC stack system;
the controller uses the starting control method to control the starting of each stage of reformer in the cascade reformer so as to realize the starting of the SOFC stack system.
Further, the gas supply range of each stage of reformer is set according to the amount of reformed gas demand corresponding to the operation state of the SOFC stack and the number of SOFC stacks in the SOFC stack system.
From the above technical scheme, the invention has the following beneficial effects:
the invention provides a starting control method and a device for cascade reformers and an SOFC power generation system, wherein for cascade reformers with cascade design, the starting control method starts the reformers step by step according to the reformed gas demand of an SOFC stack and the gas-available quantity of each level of reformers, distributes the reformed gas flow demand to reformers with different levels, can protect the safety of the reformers and the SOFC stack to the maximum extent, obviously improves the reliability of the integral operation of the SOFC power generation system, and simultaneously improves the service life of each device of the system; the reformers at all levels are started step by step according to the gas-available quantity, so that the time for the whole system to respond to fluctuation of the reforming gas quantity is shorter, and the working efficiency of the system is greatly improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are required to be used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are only embodiments of the present invention, and that other drawings can be obtained according to the provided drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural diagram of an SOFC power generation system based on a cascaded methanol reformer according to an embodiment of the present invention;
FIG. 2 is a flow chart illustrating a method for controlling start-up of a cascade reformer according to an embodiment of the present invention;
FIG. 3 is a schematic diagram of a start-up control apparatus for a cascade reformer according to an embodiment of the present invention;
FIG. 4 is a schematic diagram of a start-up control apparatus for a cascade reformer according to an embodiment of the present invention;
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Solid oxide fuel cells (Solid Oxide Fuel Cell, SOFCs for short) are a type of fuel cell that use a solid oxide electrolyte that conducts negative oxygen ions from the cathode to the anode. The negative oxygen ions oxidize hydrogen or carbon monoxide electrochemically at the anode. The hydrogen in the fuel is mainly derived from fuel reforming of natural gas or the like, while the oxygen is derived from air, and typically the fuel is reacted with air and steam in a device upstream of the SOFC anode, and the reformed product comprises hydrogen (H) 2 ) Carbon monoxide (CO), carbon dioxide (CO) 2 ) Methane vapor (CH) 4 ) Etc. SOFCs can provide this endothermic reaction, steam reforming, with the exothermic heat of electrochemical oxidation inside the fuel cell, improving efficiency. SOFC stack systems using methanol as fuel produce little waste and cleaner emissions.
The fuel usually generates reforming hydrogen production reaction in the reforming reactor, the combustion reaction in the combustor or the combustion chamber provides certain energy for the reforming reaction, and high-temperature flue gas generated by the combustion in the combustor or the combustion chamber enters the reforming reactor to exchange heat with the fuel, so that the fuel reacts with air and steam to produce hydrogen under the action of the catalyst.
When the SOFC electric pile system actually operates, four states mainly comprise normal operation, standby, shutdown and starting, various fluctuation power is required to be switched according to state switching during operation, further the reformed gas flow generated by the methanol reforming module is required to fluctuate along with the power fluctuation of the SOFC electric pile system, a large-scale methanol reformer is often used at present, the gas flow change caused by all power fluctuation of the electric pile system is borne by one level or the same reformer, and particularly, the starting of the reformer and the first round of starting of the SOFC electric pile system are carried out, namely, the whole SOFC electric pile system is started from shutdown to working state, and the process lacks corresponding starting strategies, so that the thermal inertia of the system lacks effective treatment, and adverse effects are caused on the response of the electric pile system during starting.
In order to solve the technical problems, the present application provides a method and an apparatus for controlling the start of a cascade reformer, and an SOFC power generation system, where the cascade reformer is arranged in steps according to the gas supply amounts of the reformers at different stages, and the first start of the SOFC stack system is achieved by controlling the start of the cascade reformer, that is, the process of starting the reformer, supplying gas to the reformer, and triggering the start of the SOFC stack is performed.
In one embodiment, the present application provides a cascade reformer-based SOFC power generation system comprising a cascade reformer, a controller, and a SOFC stack system.
The cascade reformers comprise at least two stages of reformers, all stages of reformers in the cascade reformers are arranged in a cascade mode according to the gas-controllable quantity, reformers at the same stage are connected in parallel, and reformed gas generated by all stages of reformers is distributed to the SOFC stack system under the control of the controller.
The controller is respectively connected with the cascade reformers and the SOFC stack system, and controls the start-up and air supply of each stage of reformers in the cascade reformers so as to realize the start-up of the SOFC stack.
Specifically, the SOFC stack system generally includes more than one SOFC stack, where each SOFC stack is electrically connected, and each SOFC stack is connected to a controller, where the controller may read intrinsic parameters and timing variables of each SOFC stack, determine an operating state of the SOFC stack according to the intrinsic parameters and timing variables, and calculate an intake flow of reformed gas required by each SOFC stack according to power fluctuation data of the SOFC stack.
When the system works, each level of reformer provides reformed gas with corresponding flow to each SOFC stack according to the control instruction of the controller.
Illustratively, reformed gas generated by each stage of reformer is converged to a central pipeline, and is uniformly controlled and distributed by a controller to flow into each SOFC stack for power generation.
In a further embodiment, the air supply range of each stage of reformer is set according to the amount of reformed gas required corresponding to the operation state of the SOFC stack and the number of SOFC stacks.
Specifically, the gas flow of the reformer is positively related to the volume thereof, the reformed gas demand of each operation state of the SOFC stack is different, the gas supply of each stage of the reformer can meet the demand of starting the reformer step by designing reformers with different volumes, for example, the maximum gas supply of the reformer with the lowest stage meets the reformed gas flow required by 2 SOFC stacks in operation, the maximum gas supply of the secondary reformer meets the reformed gas flow required by 5 SOFC stacks in operation, the maximum gas supply of the reformer with the highest stage meets the reformed gas flow required by 10 SOFC stacks in operation, and the controller can determine which stage of the reformer is started according to the number of the SOFC stacks actually required to be started and the operation state of the stacks under the setting.
By way of example, fig. 1 provides a schematic structural diagram of a SOFC power generation system based on cascaded methanol reformers, and the SOFC power generation system 100 shown in fig. 1 includes a SOFC stack system 110, a controller 120 and cascaded methanol reformers 130, where the SOFC stack system includes n SOFC stacks connected in parallel, the controller 120 is electrically connected to the cascaded methanol reformers 130 and the SOFC stack system 110 respectively, the cascaded methanol reformers 130 are arranged in three steps, and include a primary reformer 131, a secondary reformer 132 and a tertiary reformer 133, where the primary reformer 131 has the largest available air supply, and the tertiary reformer 133 has the smallest available air supply.
In a further embodiment, considering that the reformers of different stages have different gas supply amounts, the gas flow of the reformers with different equipment volumes and multiple linkage stages has a larger variation range, and the combustor is required to supply the heating and heat preservation of a plurality of electric stacks, if the structural design of the internal combustor in the prior art is still adopted, the required volume of the combustor is large because the gas flow to be generated by the reformers with large gas supply amount is large, and the arrangement of the combustor in the interior of the reformers possibly leads to the larger volume of the reformers, so the combustor can be arranged externally. There are various ways of igniting the burner, such as spark; the burner and the reformer are connected through a gas flow pipeline; the reformer is provided with a high-temperature flue gas channel, and the high-temperature flue gas enters the high-temperature flue gas channel of the reformer connected with the high-temperature flue gas channel from an external burner outlet, so that the reformer is heated, and the heat condition of reforming reaction is provided.
The start-up procedure of the cascade methanol reformer controlled by the controller of the above example in this embodiment refers to the implementation of management of the reformer start-up sequence, timing, etc. during the reformer start-up process by instructions containing abstract and detailed levels for the programmable set of hard-drive devices, which management is time-ordered, with a presentation form suitable for and understood by the computer control elements.
The control device or controller mentioned in the embodiments of the present invention is capable of controlling a physical system, such as a reformer or an SOFC stack, by means of control signals, thereby allowing components in the physical system to establish, modify and adapt a motion profile, thereby successfully executing a desired motion profile and process commands.
The object manipulating part of the start control process of the cascaded methanol reformer will be described in detail below, and may be mainly expressed as a control device or a controller generating a control signal according to a control instruction to control each stage of reformer in the cascaded methanol reformer to start step by step, so as to further complete the execution step of the SOFC stack.
Fig. 2 is an alternative execution flow of a start-up control method of a cascade reformer according to an embodiment of the present application, which may include the following steps:
and S21, obtaining the reformed gas demand of the SOFC stack.
And S22, generating control instructions of the cascade reformer according to the reformed gas demand.
And S23, controlling each level of reformers to start step by step according to the control instruction and the air supply quantity of each level of reformers so as to supply air to the SOFC stack.
Specifically, controlling the stage-wise start of each stage reformer according to the control instruction and the gas-suppliable amount of each stage reformer in step S23 includes:
and S231, acquiring the air-suppliable quantity of each level of reformer.
And S232, starting the reformers at all levels step by step from low to high according to the air supply amount based on the control instruction.
Illustratively, step S232 includes:
the reformer of the minimum level of the suppliable gas amount is started based on the control instruction.
When the gas supply amount of the reformer with the smallest gas supply amount can not meet the reformed gas demand of the SOFC stack, starting the reformers with the secondary gas supply amounts until the sum of the gas supply amounts of the reformers with the different stages meets the reformed gas demand of the SOFC stack.
Specifically, when starting the reformer, a reformer with a smaller available gas supply amount, for example, the three-stage reformer 131 in the cascade reformer 130 illustrated in fig. 1, is preferentially started, and when the gas supply amount of the lower-stage reformer does not meet the flow demand of the SOFC stack for the reformed gas, the higher-stage reformer is restarted, so that the gas flow fluctuation of the cascade reformer is not too intense, and the waste of equipment resources is not easily caused. For example, when only 2 SOFC stacks need to be started to be in an operating state when the system is started in the first round, if the gas flow requirement is directly responded by the primary reformer, on the one hand, the response speed is slow, and on the other hand, the reformer supplied by a large flow rate responds to the small flow requirement, the equipment resource is inevitably wasted. After the reformer is started, the reformer generates reforming reaction to generate hydrogen-containing gas, and the SOFC stack is started.
In a further embodiment, step S231 further includes:
acquiring temperature change information of the SOFC stack;
and determining the reformed gas demand of the SOFC stack according to the temperature change information.
Specifically, generally, the operating temperature of the SOFC stack is constant, but when the SOFC stack is started at the first round, the operating temperature cannot be immediately reached, assuming that the stack is started in a shutdown state, i.e., cold start, the temperature of the SOFC stack needs to be raised from room temperature to a set operating temperature, for example, 600 ℃, a plurality of temperature intervals are required to be passed during the period to reach 600 ℃, and usually, the requirements of the SOFC stacks with different temperatures on the inlet flow of the reformed gas can be different, so that a plurality of temperature intervals can be divided between room temperature and 600 ℃ within the period of several hours, and the controller determines the required amount of the reformed gas according to each temperature interval, and further starts the reformer step by step to realize the gas supply in combination with the gas supply capability of each level of reformers.
In a further embodiment, the start control method further includes the following steps:
and controlling the high-temperature flue gas to be led into each stage of reformers step by step from low to high according to the gas-feeding quantity.
Specifically, when preheating the reformer, the high temperature flue gas is introduced from the burner outlet into the low-level reformer, and after being preheated, the high temperature flue gas sequentially enters the higher-level reformer, and the high temperature flue gas cooled by heat exchange in the low-level reformer is mixed with reformed fuel (such as H 2 ) The heat exchange is continued, so that the situation that the fuel is difficult to burn due to starting at low temperature is avoided.
Generally, the flow rate of the high-temperature flue gas required by each stage of the reformer is determined according to the volume of the reformed gas, the temperature rising rate and the heat exchange effect of the high-temperature flue gas and the reformer. Typically the type (or size) of reformer determines the upper limit of the flow of high temperature flue gas to the reformer; in order to ensure the service life of the system, the heating rate of the reformer is not too fast, and the heating rate also limits the upper limit of the flow of high-temperature flue gas; the heat exchange effect of the high-temperature flue gas and the reformer means that a heat exchange coefficient exists between the high-temperature flue gas and the reformer, and the heat exchange coefficient is often less than 1 because the heat utilization efficiency is not 100%, and can be expressed as: high temperature flue gas flow rate heat exchange coefficient = reformer high temperature flue gas flow demand value, specific numerical values are flexibly adjusted according to different reformers, so long as normal operation of the reformers can be ensured.
In a further embodiment, the start control method further includes the following steps:
the flow of the high-temperature flue gas is controlled to control the preheating temperature of the reformers, so that the starting time of each stage of reformers is matched with the temperature switching time of the SOFC stack.
Specifically, since the high-temperature flue gas flows into each stage of reformers step by step, when the low-level reformers are started, the high-level reformers are preheated to a certain temperature, when the SOFC stack is started and divided into a plurality of temperature intervals, and when the SOFC stack is heated and switched to a temperature interval with higher temperature, the controller needs to start the reformers with higher level to ensure the inlet air flow of the reformed gas, the reformers are usually heated from normal temperature to working temperature, for example, from normal temperature to 250 ℃ and the temperature span is 225 ℃, and the startup of the three-level reformers only can meet the condition that the SOFC stack is heated to 150 ℃, at this time, the two-level reformers are not started to working temperature during the duration of the temperature, and reforming reaction cannot happen, but because the high-temperature flue gas is preheated, the two-level reformers are preheated to a certain temperature, so long as the temperature at least reaches 100 ℃, the startup time of the reformers can be matched with the temperature switching time of the stack, so that the process of starting the reformer step by step matches the temperature switching time of the SOFC stack.
Taking the cascaded methanol reformer with three stages as shown in fig. 1 as an example, and assuming that the SOFC stack system is composed of 10 SOFC stacks connected in parallel, the start control of the cascaded methanol reformer will be further described below.
The operating state of the SOFC stack is divided into four types: the reforming gas flows required by each state are V1, V2, V3 and V4 respectively. For a single SOFC stack, typically V1> V2> v3≡v4, the required reformer flow at shutdown and start-up may be consistent, v3=v4, or inconsistent, v3≡v4.
Assuming that the safe variable range of the gas flow rate of a standard reformer is 50% -100%, when the reformers are arranged in a three-stage cascade structure, the relation between the maximum gas amount which can be supplied and the safe variable range of the gas supply amount of each stage of reformers and the gas flow rate ratio of the standard reformers is as follows:
the maximum gas amount which can be supplied by the primary reformer is 100%, so that the normal operation of all SOFC stacks can be satisfied, and the safe variation range of the gas supply amount is 50% -100%. In actual operation, the maximum air flow of the primary reformer can be more than 100%, and the actual flow can be only required to meet the safety change range of 50% -100%. Typically, the amount of reformate gas flow required for operation of the SOFC stack is greater than or equal to the lower gas supply limit of the primary reformer.
The maximum gas amount which can be supplied by the secondary reformer is 50%, and the normal operation of 50% of SOFC stacks can be satisfied. Meanwhile, the maximum outlet gas flow is more than or equal to the reforming gas flow required by the hot standby of all SOFC stacks, and the safe variation range of the gas supply amount is 25% -50%. In actual operation, the maximum flow rate of the secondary reformer may be greater than 50%, and the actual flow rate may be as long as the safety variation range is 25% -50%.
The maximum gas supply of the three-stage reformer is 25%. The maximum outlet gas flow is more than or equal to the reforming gas flow required by all SOFC stacks when the SOFC stacks are stopped, and the safe variation range of the gas flow which can be supplied is 12.5% -25%. Since v3≡v4 is typically the case, the three-stage reformer also meets the amount of reformate gas flow required for all SOFC stacks to reach start-up. In actual operation, the maximum flow rate of the three-stage reformer can be more than 25%, and the actual flow rate can be only required to meet the safety variation range of 12.5% -25%.
It should be noted that the above setting is merely a visual comparison with the assumed gas flow rate of one standard reformer, and is not considered as a limitation on the absolute volume and gas flow rate of the reformers, so that it is convenient to understand the differences between the reformers. In practical applications, the gas flow rate of the assumed standard reformer may be specifically designed according to the actual requirements of the SOFC stack system to which it is connected.
(1) Start-up three-stage reformer
According to the size of the equipment of the three-stage reformer, the temperature rising rate limit and the heat exchange effect of the high-temperature flue gas and the reformer, the flow N1 of the high-temperature flue gas flowing into the three-stage reformer is calculated, the flow of the high-temperature flue gas flowing into the three-stage reformer from the outlet of the combustor is controlled, and the high-temperature flue gas flowing through the three-stage reformer sequentially enters the two-stage reformer and the first-stage reformer to be preheated.
The high temperature flue gas heats the tertiary reformer to an operating temperature T0, the tertiary reformer is started and a reforming reaction occurs. At this time, the maximum allowable flow rate of the reformed gas produced by the three-stage reformer is Q1, and the flow rate Q1 can support all the SOFC stacks to reach the start-up state, i.e. if the system has 10 SOFC stacks, the flow rate required by a single SOFC stack to reach the start-up state is V s Q1 is greater than or equal to n V s . For ease of adjustment, typically Q1 is V s Is an integer multiple of (a).
And the reformed gas generated by starting the three-stage reformer is introduced into an anode channel of the SOFC stack after heat exchange and condensation, and the SOFC stack starts to be started. At this time, the burner needs to supply heat required for starting the SOFC stack in addition to the reformer.
(2) Starting a secondary reformer
Assuming that 3 SOFC stacks need to be started to an operating state in the first-round start-up, and the SOFC stacks undergo three temperature phases from the cold start-up to the operating state, the flow of reforming gas needed for the 1 stack start-up to the first temperature phase is V t1 The flow of reformate gas required for startup of 2 SOFC stacks to the first temperature stage is 2V t1 The flow of reformate gas required for the start-up of 3 SOFC stacks to the first temperature stage is 3V1 and so on, assuming 3V t1 The allowable maximum flow rate Q1 of the three-stage reformer, i.e., Q1, can support 3 stacks to heat up to the first temperature stage.
When all 3 SOFC stacks need to be warmed up to the second temperature stage, it is assumed that the flow of reforming gas required for the warming up of 1 SOFC stack to the second temperature stage is V t2 At this time 3V t2 > Q1, if 3V t2 The quotient of/Q1 is 2, which indicates that the three-stage reformer can only meet the condition that 2 SOFC stacks are heated to the second temperature stage, and the three-stage reformer needs to ensure the heating start of the 2 SOFC stacks preferentially, and has the following steps ofThe surplus reformed gas is still fed into the third SOFC stack, and the flow of the reformed gas fed into the third SOFC stack does not support the continuous heating to the second temperature stage, so that other reformers are required to be put into operation and normally perform reformed gas output to complement the insufficient reformed gas of the third SOFC stack, and the controller starts the secondary reformers according to the required amount of the reformed gas.
Similarly, when the temperature needs to be raised to the third temperature stage, the flow of reformed gas required for starting up 1 SOFC stack is increased to V t3 If V t3 =q1, meaning that a three-stage reformer can only support the warming up of 1 stack, and the reformed gas required for the start-up of the other two stacks needs to be complemented by a higher-order reformer.
Taking the foregoing three temperature phases as an example, the start-up of the secondary reformer must be implemented in the first temperature phase to ensure continuous power generation of the SOFC stack, and if the duration of the first temperature phase is t1, that is, the controller is required to implement the start-up of the secondary reformer in a period less than or equal to t 1.
The secondary reformer is preheated to a certain temperature when the tertiary reformer is started, the temperature of the secondary reformer is recorded as T1, the flow N2 of the high-temperature flue gas flowing into the secondary reformer is calculated according to the volume of the secondary reformer, the temperature rising rate limit and the heat exchange effect of the high-temperature flue gas and the reformer, and the secondary reformer is controlled to rise to the reforming reaction working temperature T0 according to a certain temperature rising rate. At this time, the high-temperature flue gas preferentially guarantees the flow required by the startup of the secondary reformer, and the high-temperature flue gas passing through the outlet of the secondary reformer is respectively used for maintaining the temperature stability of the tertiary reformer and the preheating of the primary reformer.
Assuming that the temperature rising rates of the SOFC stack and the reformer are both 5 ℃/min, the upper limit of the first temperature stage of the stack is 150 ℃, the SOFC stack is heated from normal temperature to 150 ℃, the temperature span is 125 ℃, the reformer is usually heated from normal temperature to working temperature T0, for example, from normal temperature to 250 ℃, the temperature span is 225 ℃, at this time, when the stack ends for the duration of the first temperature stage, the secondary reformer is not started to working temperature, and no reformed gas can be supplied, but by preheating the tertiary reformer, the secondary reformer is preheated to temperature T1, and as long as T1 is greater than or equal to 100 ℃, the starting time of the secondary reformer can be matched with the reformed gas flow required by temperature switching of the SOFC stack.
After the secondary reformer is started, reforming reaction occurs to generate reformed gas, and the reformed gas is introduced into the SOFC stack to support SOFC startup.
(3) Primary reformer
Similar to the start-up control of the secondary reformer, the controller needs to start up the primary reformer when both the tertiary and secondary reformers are started up and still cannot meet the reformate gas flow demand of the SOFC stack, and does not start up the primary reformer if both the secondary and tertiary reformers can be met.
In some embodiments, when all the levels of reformers are started, the air supply task is preferentially allocated to the high-level reformers according to the target operation state of the SOFC stack, that is, for example, after all the three levels of reformers are started, if the air supply amount of the first-level reformers can meet the flow of reformed air required by maintaining the target operation state of all the SOFC stacks due to the stronger air supply capability of the first-level reformers, the second-level and third-level reformers can be controlled to withdraw from air supply to the SOFC stack.
After the secondary and tertiary reformers stop the output of reformed gas, the temperature of the reformed gas is not reduced to room temperature, and high-temperature flue gas for heat preservation of the primary reformer also flows through the secondary and tertiary reformers for heat preservation, so that the reformers can respond to the change of reformed gas flow caused by the change of SOFC electric pile power in time.
The three-stage cascade methanol reformer mentioned in the above embodiments is only exemplified by the three-stage cascade arrangement, and the system may be designed as other multi-stage linkage reformer structures, such as two-stage, four-stage, five-stage, or more.
In the design of the temperature stage, the embodiments provided in the present application take only three temperature stages as an example, and in practical application, the design of the temperature stage may be a plurality of temperature stages, so long as the reformed gas provided by the reformer at the highest level can support at least 1 SOFC stack to be started to an operating state.
When referring to fuel for hydrogen production and SOFC stack power generation, any fuel may be used as long as the SOFC stack or stack system has fluctuating demand for intake air flow, and the fuel is not limited to methanol reforming, but may be reforming of other compounds, such as natural gas, and the like.
Referring to fig. 3, an embodiment of the present application further provides a start-up control apparatus 300 of a cascade reformer, including:
a reformed gas amount acquisition unit 310 configured to acquire a reformed gas demand amount of the SOFC stack;
an instruction generation unit 320 configured to generate control instructions of the cascade reformer according to the reformed gas demand;
and the control unit 330 is configured to control the stage reformers to start stage by stage according to the control instruction and the air-controllable amount of the stage reformers so as to realize air supply to the SOFC stack.
In some embodiments, as shown in fig. 4, the start-up control apparatus 300 further includes a temperature information obtaining unit 340 configured to obtain temperature change information of the SOFC stack, so that the reformed gas amount obtaining unit 310 determines the reformed gas demand of the SOFC stack according to the temperature change information.
The start-up control device 300 of the cascade reformer adopts the start-up control method provided by the above embodiments, and specific implementation logic may refer to the relevant description of the start-up control method provided by each of the foregoing embodiments, which is not repeated herein.
The embodiments described above have described the invention in particular detail with respect to possible scenarios, and those skilled in the art will recognize that the invention can be practiced with other embodiments. No particular naming of the components, case of terminology, attribute, data structure, or any other programming or structural aspect is mandatory or significant, and the mechanisms that implement the invention or its features may have different names, forms, or procedures. The system may be implemented by a combination of hardware and software (as described), entirely by hardware elements or entirely by software elements. The specific division of functionality between the various system components described herein is exemplary only and not mandatory; in contrast, functions performed by a single system component may be performed by multiple components, or functions performed by multiple components may be performed by a single component.
It will be appreciated by those skilled in the art that the various steps of the disclosed methods may be implemented by general purpose computing devices, they may be concentrated on a single computing device, or distributed across a network of computing devices, or they may alternatively be implemented in program code executable by computing devices, such that they may be stored in storage devices for execution by computing devices, or they may be separately fabricated into individual integrated circuit modules, or multiple modules or steps within them may be fabricated into a single integrated circuit module. Thus, the present disclosure is not limited to any specific combination of hardware and software.
The programs (also referred to as programs, software applications, or code) executable by these computing devices include machine instructions for a programmable processor, and may be implemented in a high-level procedural and/or object-oriented programming language, and/or in assembly/machine language. As used herein, the terms "machine-readable medium" and "computer-readable medium" refer to any computer program product, apparatus, and/or device (e.g., magnetic discs, optical disks, memory, programmable Logic Devices (PLDs)) used to provide machine instructions and/or data to a programmable processor, including a machine-readable medium that receives machine instructions as a machine-readable signal. The term "machine-readable signal" refers to any signal used to provide machine instructions and/or data to a programmable processor.
Certain aspects of the invention include the process steps and instructions described herein in the form of algorithms. It should be noted that the process steps and instructions of the present invention may be embodied in software, firmware, and/or hardware, which when implemented in software, can be downloaded to reside on and be operated from different platforms used by a variety of operating systems.
It will be appreciated by persons skilled in the art that the structures shown in the various figures are block diagrams of only some of the structures associated with the aspects of the present application and are not intended to limit the terminal device to which the aspects of the present application may be applied, and that a particular terminal device may include more or less components than those shown, or may combine some of the components, or have a different arrangement of components.
In the description of the present specification, reference to the terms "one embodiment," "some embodiments," "examples," "specific examples," or "possible designs," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present application. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
The above embodiments are only for illustrating the technical solution of the present invention, and are not limiting; although the invention has been described in detail with reference to the foregoing embodiments, those skilled in the art will appreciate that: the technical scheme described in the foregoing embodiments can be modified or some of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A startup control method of a cascade reformer, the cascade reformer including at least two stages of reformers, and each stage of reformers in the cascade reformer being cascade-arranged according to an suppliable amount, the startup control method comprising:
obtaining the reformed gas demand of the SOFC stack;
generating control instructions of the cascade reformer according to the reformed gas demand;
and controlling each level of reformers to start step by step according to the control instruction and the air supply quantity of each level of reformers so as to supply air to the SOFC stack.
2. The startup control method according to claim 1, wherein controlling stepwise startup of each stage reformer according to the control instruction and an suppliable amount of each stage reformer comprises:
acquiring the gas-controllable quantity of each level of reformer;
and starting each stage of reformer step by step from low to high according to the air-controllable quantity based on the control instruction.
3. The startup control method according to claim 2, wherein the step-wise starting up of each stage of the reformer from low to high in the gas suppliable amount based on the control instruction comprises:
starting a reformer of a minimum level of the suppliable gas amount based on the control instruction;
when the gas supply amount of the reformer with the smallest gas supply amount can not meet the reformed gas demand of the SOFC stack, starting the reformers with the secondary gas supply amount until the total gas supply amount of the cascade reformers meets the reformed gas demand of the SOFC stack.
4. The startup control method according to claim 1, characterized in that the startup control method further comprises:
acquiring temperature change information of the SOFC stack;
and determining the reformed gas demand of the SOFC stack according to the temperature change information.
5. The startup control method according to claim 1, characterized in that the startup control method further comprises:
and controlling the high-temperature flue gas to be led into each stage of reformers step by step from low to high according to the gas-controllable quantity.
6. The startup control method according to claim 1, characterized in that the startup control method further comprises:
the flow of the high-temperature flue gas is controlled to control the preheating temperature of the reformers, so that the starting time of each stage of reformers is matched with the temperature switching time of the SOFC stack.
7. A start-up control device for a cascade reformer, comprising:
a reformed gas amount acquisition unit configured to acquire a reformed gas demand amount of the SOFC stack;
an instruction generation unit configured to generate control instructions of a cascade reformer according to the reformed gas demand;
and the control unit is configured to control each stage of reformer to start step by step according to the control instruction and the air-controllable quantity of each stage of reformer so as to realize air supply to the SOFC stack.
8. The start-up control device according to claim 7, characterized in that the start-up control device further comprises:
and the temperature information acquisition unit is configured to acquire temperature change information of the SOFC stack.
9. A SOFC power generation system based on a cascade reformer, which is characterized by comprising the cascade reformer, a controller and an SOFC electric pile system;
the cascade reformers comprise at least two stages of reformers, all stages of reformers in the cascade reformers are arranged in a cascade mode according to the gas-controllable quantity, reformers at the same stage are connected in parallel, and reformed gas generated by each stage of reformers is distributed to the SOFC stack system under the control of the controller;
the controller is respectively connected with the cascade reformer and the SOFC stack system;
the controller controls the start-up of each stage of the cascade reformer using the start-up control method according to any one of claims 1 to 6 to achieve the gas supply to the SOFC stack system.
10. The SOFC power generation system of claim 9, wherein the range of supply of each stage of reformer is set according to the amount of reformed gas demand corresponding to the operating state of the SOFC stack system and the number of SOFC stacks in the SOFC stack system.
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