CN113156835B - Modeling simulation method for operation control of electricity-heat comprehensive energy system - Google Patents
Modeling simulation method for operation control of electricity-heat comprehensive energy system Download PDFInfo
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- 238000004088 simulation Methods 0.000 title claims abstract description 78
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- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical group [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 108
- 239000000243 solution Substances 0.000 claims description 70
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 26
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Abstract
The invention relates to a modeling simulation method for operation control of an electricity-heat comprehensive energy system, which comprises the following steps: establishing a combined heat and power generation unit model, acquiring each component of the combined heat and power generation unit and respectively establishing corresponding models; establishing an absorption refrigerator model, acquiring each component of the absorption refrigerator, and respectively establishing a corresponding static model and a corresponding dynamic model; establishing a thermodynamic network model; and forming an electric-thermal comprehensive energy system transient simulation model based on the cogeneration unit model, the absorption chiller model and the thermal network model, and realizing real-time control simulation of the electric-thermal comprehensive energy system. The method of the invention builds a model for each unit of the electric-thermal comprehensive energy system, combines the models to form an electric-thermal comprehensive energy system transient simulation model, can simulate the operation control of the electric-thermal comprehensive energy system, and realizes the real-time control simulation of the electric-thermal comprehensive energy system.
Description
Technical Field
The invention relates to modeling simulation of an electricity-heat integrated energy system, in particular to a modeling simulation method for operation control of the electricity-heat integrated energy system.
Background
Under the influence of global warming, the demand for reducing the emission of greenhouse gases is increasing, and it is common knowledge in the industry to reduce the use of fossil fuels and promote the development of renewable energy technology and energy internet technology. Under the background, the comprehensive planning of an electricity-heat comprehensive energy system becomes a hotspot of current research and engineering application, wherein a cogeneration unit can recover and utilize heat energy from exhaust gas discharged by a turbonator while producing electric energy, so as to provide heat for a heat load of a building, thereby achieving the purposes of saving energy, reducing emission and improving the overall efficiency of the comprehensive energy system; the absorption refrigerator can generate refrigeration water by means of heat recovered by a cogeneration unit and supply the refrigeration water to a cold load, and compared with the traditional electric refrigerator, the absorption refrigerator also has the characteristics of energy conservation, emission reduction and higher efficiency.
At present, in the research of the academic world on the electric-thermal integrated energy system, the established model and algorithm are difficult to check. In order to research the operation control of the electric-thermal comprehensive energy system, firstly a simulation model of the electric-thermal comprehensive energy system needs to be established, and how to establish the model to realize the real-time control simulation of the electric-thermal comprehensive energy system becomes a problem which needs to be solved urgently.
Disclosure of Invention
The invention aims to overcome the defect that an electric-thermal integrated energy system in the prior art is difficult to build a simulation model, and provides a modeling simulation method for operation control of the electric-thermal integrated energy system.
In order to achieve the purpose, the invention adopts the following technical scheme:
a modeling simulation method for operation control of an electric-thermal integrated energy system includes:
establishing a combined heat and power generation unit model, acquiring each component of the combined heat and power generation unit and respectively establishing corresponding models;
establishing an absorption refrigerator model, acquiring each component of the absorption refrigerator, and respectively establishing a corresponding static model and a corresponding dynamic model;
establishing a thermodynamic network model;
and forming an electric-thermal comprehensive energy system transient simulation model based on the cogeneration unit model, the absorption refrigerator model and the thermal network model, and realizing real-time control simulation of the electric-thermal comprehensive energy system.
Compared with the prior art, the invention has the beneficial effects that:
the method of the invention builds a model for each unit of the electricity-heat comprehensive energy system, simultaneously builds corresponding models for each component in the cogeneration unit, builds corresponding static models and dynamic models for each component of the absorption refrigerator, combines a thermal network model to form an electricity-heat comprehensive energy system transient simulation model, can simulate the operation control of the electricity-heat comprehensive energy system, and realizes the real-time control simulation of the electricity-heat comprehensive energy system.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
Fig. 1 is a schematic view of an electric-thermal integrated energy system according to an embodiment of the present invention.
Fig. 2 is a model diagram of an absorption chiller according to an embodiment of the present invention, wherein 1-absorber flow direction lithium bromide solution to solution pump, 2-solution pump flow direction lithium bromide solution to heat exchanger, 3-heat exchanger flow direction lithium bromide solution to generator, 4-generator flow direction lithium bromide solution to heat exchanger, 5-heat exchanger flow direction lithium bromide solution to absorber, 6-generator flow direction water vapor to condenser, 7-condenser flow direction water to evaporator, 8-evaporator flow direction water vapor to absorber, 9-absorber cooling water inlet, 10-absorber cooling water outlet/condenser cooling water inlet, 11-condenser cooling water outlet, 12-generator hot steam inlet, 13-generator hot steam outlet, 14-evaporator cooling water inlet, 15-evaporator cooling water outlet.
Fig. 3 is a schematic structural diagram of a thermal network according to an embodiment of the present invention.
Fig. 4 is a diagram of a thermodynamic network model based on graph theory for the thermodynamic network in fig. 2.
Fig. 5 is a simulation model diagram of a gas turbine in the cogeneration unit according to the embodiment of the present invention.
Fig. 6 is a simulation model diagram of a heat recovery device in a cogeneration unit according to an embodiment of the invention.
Fig. 7 is a simulation model diagram of an absorption chiller according to an embodiment of the present invention.
Fig. 8 is a simulated model diagram of a thermal conduit in a thermal network in accordance with an embodiment of the present invention.
Fig. 9 is a simulation model diagram of thermal load in a thermal network according to an embodiment of the present invention.
FIG. 10 is a diagram of a thermal load simulation model of the simplified version of FIG. 9.
Fig. 11 is a diagram of a load simulation model of the house in fig. 9.
Fig. 12 is a diagram of a simulation model of the building load in fig. 9.
FIG. 13 is a simulation model diagram of the power subsystem of the present invention.
Fig. 14 is a simulation model diagram of the thermal subsystem of the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention.
As shown in fig. 1 to 14, an embodiment of the present invention provides a modeling simulation method for operation control of an electric-thermal integrated energy system, including the following steps:
and 102, establishing a combined heat and power generation unit model, acquiring each component of the combined heat and power generation unit and respectively establishing corresponding models.
The cogeneration is to recover the heat in the exhaust heat and smoke discharged from the steam turbine while the generator generates electricity, and is used for producing hot water or hot steam and supplying heat to users. Specifically, the cogeneration machine comprises a gas turbine, a generator and a heat recovery device, so that a mathematical model of the gas turbine, a mathematical model of the heat recovery device and a mathematical model of the generator need to be correspondingly established, and the mathematical model of the generator in simulation software such as Matlab/Simulink is known and can be directly introduced. The heat power P recovered by the heat recovery device from the waste heat flue gas of the gas turbine can be calculated based on the establishment of a mathematical model of the gas turbine and a mathematical model of the heat recovery device hr Directly used for heat supply and has heat power P hr1 And inputting the thermal power of the absorption chiller to establish a relationship with the model of the absorption chiller. The heat supply mode is that a waste heat boiler produces hot water or directly utilizes steam to supply heat energy to building load.
Specifically, a gas turbine mathematical model is established based on a Rowen model, wherein the gas turbine mathematical model comprises a speed controller model, a waste heat flue gas temperature controller model, an acceleration controller model, a fuel system model, and a compressor and turbine model.
1.1.1 Speed controller model
The main function of the speed controller is to schedule a command P according to the power set And the actual output P of the generator e Adjusting the output power of the generator to ensure that the cogeneration unit works according to the power dispatching instruction; at the same time, according to the rated rotation speed omega ref With the actual speed omega of the generator r And the rotation speed of the prime motor is adjusted to keep the frequency of the generator stable.
Based on the functions, a speed instruction formula output by the speed controller is established, and the speed instruction formula specifically comprises the following steps:
wherein, V ce0 Speed command, K, output for speed controller Droop Is the droop coefficient, T is the time constant, K p And K i Proportional and integral parameters for PI regulation.
1.1.2 Waste heat flue gas temperature controller model
The waste heat flue gas temperature controller model is linked with the compressor and turbine model, the waste heat flue gas temperature calculated by the compressor and turbine model is used as input, and the function of the waste heat flue gas temperature controller model is to enable the waste heat flue gas temperature T to be T exhaust Maintained at the temperature reference value T ref 。
The waste heat flue gas temperature controller model comprises a radiation shielding module, a thermal coupling module and a PI controller module, wherein the radiation shielding module and the thermal coupling module are used for simulating time delay caused by corresponding modules in an actual temperature measuring device;
based on a waste heat flue gas temperature controller model, the speed instruction upper limit value V output by a speed controller ce_limit1 :
Wherein, T rs1 、T rs2 ,T th For radiation shielding and thermal coupling coefficients, K p And K i Proportional and integral parameters adjusted for the PI controller module.
1.1.3 Acceleration controller model
The acceleration controller model has two functions, namely, the thermal stress is reduced by limiting the acceleration of the rotor when the gas turbine is started, in addition, in the operation process of the gas turbine, the acceleration controller model can inhibit the over-high rotating speed of the rotor of the generator and ensure the normal operation of the unit, and if the operation speed of the generator is close to the rated speed of the generator, the function of the acceleration controller model can be ignored.
Based on the acceleration controller model, the speed command upper limit value V output by the speed controller ce_limit2 :
Wherein, T inertia Is the inertia constant of the rotor of the generator.
Speed command V of speed regulator ce0 After amplitude limiting, the final speed regulating signal V is obtained ce Min represents taking the minimum value:
V ce =min{V ce0 ,V ce_limit1 ,V ce_limit2 }。
1.1.4 Fuel system model
The fuel system model has the main function of calculating the consumed power of the fuel in the gas turbine according to the control command of the speed controller and by considering the delay of a gas valve in the actual system and the efficiency conditions of the fuel at different temperatures
The fuel system model comprises a valve regulation module and a fuel regulation module; wherein the power consumption is related to the delay of the gas valve. Gas turbine doing work W on gas turbine f The method specifically comprises the following steps:
wherein, T vp Is the time constant of the valve regulating module, T fs Being fuel regulating modulesTime constant, reflecting the time delay of the two processes, K init Is the minimum per unit work done value of the gas turbine.
Taking into account the ambient temperature T atm To fuel combustion efficiency eta fuel Influence of η fuel And T atm The relation between the two is described by a function, and the work of the gas turbine on the gas turbine is calculated to be W under a certain environmental temperature f Fuel P required by gas turbine fuel . When the output of the cogeneration unit is P e When it is used, its electrical efficiency is eta ele The specific function is:
based on the above function, the thermal power P in the waste heat flue gas exhaust Is composed of
P exhaust =P fuel (1-η fuel )
1.1.5 Compressor and turbine models
The main functions of the compressor and the turbine model are to execute a fuel control signal instruction issued by the fuel system and calculate the torque T output by the turbine m And the temperature T of the exhaust gas exhaust The method specifically comprises the following steps:
wherein, K HHV A typical value for an enthalpy-related coefficient is 1.3,t ref The reference temperature of the waste gas is a set value, and particularly 510 ℃ can be taken; t is CR Delay time for combustion reaction, T TD For delay of transit time of turbine exhaust system, T CD Is the time constant of the compressor displacement.
1.2 To establish a mathematical model of a heat recovery device
The heat recovery device of the cogeneration unit can recover the heat of the waste heat flue gas discharged by the gas turbine, produce hot water by a waste heat boiler or directly supply heat energy to the building load by using steam, and can also be input into an absorption refrigerating unit for refrigeration. A mathematical model of the heat recovery device in the cogeneration unit can be established according to the basic laws of energy conservation and thermodynamics.
The energy conservation equation of the cogeneration unit is as follows:
P fuel =W f +P loss +P exhaust
wherein, P fuel As fuel combustion power, W f Power for steam to work gas turbine, P exhaust Is the thermal power, P, of the waste heat flue gas of a gas turbine loss Is the power loss;
the energy conservation equation of the heat recovery device is as follows:
P hr =P exhaust ×η hr
P hr1 =(1-δ)P hr
P hr1 =C pw f w (T w,out -T w,in )
wherein, P hr Thermal power, P, recovered for the heat recovery device hr1 The thermal power input to the waste heat boiler model or the thermal load model, delta is the proportion of the recovered heat flowing to the absorption refrigerating unit model, eta hr For the efficiency of the heat recovery device model, C pw Is the specific heat capacity of water, f w Is the flow rate of water in the heat distribution pipeline, T w,in ,T w,out The water inlet temperature and the water outlet temperature of the heat recovery device model are respectively.
Efficiency eta of heat recovery device in consideration of temperature hr Assuming the inlet and outlet flue gas temperatures of the heat recovery unit are constant, the heat recovery unit efficiency η hr Only with ambient temperature T atm Related to the ambient temperature T atm The improvement will result in a heat recovery efficiency eta hr The efficiency equation of the heat recovery device is as follows
The efficiency equation of the heat recovery device is as follows
Thermal efficiency eta of cogeneration unit heat Is composed of
Total efficiency eta of combined heat and power generation unit CHP Is composed of
Step 102, establishing an absorption chiller model, acquiring each component of the absorption chiller, and respectively establishing a corresponding static model and a corresponding dynamic model.
The cogeneration unit recovers heat in the exhaust-heat flue gas discharged from the gas turbine, and can be input into the absorption refrigeration unit for refrigeration and supply to a cold load, besides flowing to an exhaust-heat boiler and other equipment for producing hot water and supplying to a heat load, thereby forming a combined cooling, heating and power system.
The absorption refrigerator comprises a heat exchanger, a solution pump, an absorber, a condenser, a generator and an evaporator;
respectively establishing static models of the heat exchanger, the solution pump, the absorber, the condenser, the generator and the evaporator, respectively solving based on the static models, and respectively calculating heat transfer coefficients UA of the absorber, the generator, the condenser and the evaporator a ,UA g ,UA c And UA e And establishing a heat transfer coefficient model of each component of the absorption refrigerator, thereby obtaining a dynamic model of the absorption refrigerator.
2.1 Constructing a static model of an absorption chiller
As shown in fig. 2, each component constructs a static mathematical model based on the mass conservation principle and the energy conservation principle. The working medium in the absorption refrigerator is a lithium bromide aqueous solution.
2.1.1 Static mathematical model for constructing absorbers
In the absorber, the lithium bromide concentrated solution absorbs the water vapor generated in the evaporator to form a lithium bromide dilute solution, and the heat generated by dilution of the lithium bromide solution is absorbed by cooling water; circulating lithium bromide dilute solution driven by the solution pump through the heat exchanger to the generator; this process follows the equation of conservation of energy, Q a The total heat released in the absorber per second is equal to the heat absorbed by the cooling water flowing through the absorber, and is also equal to the difference between the enthalpy of the substance flowing into the absorber and the enthalpy of the substance flowing out of the absorber, i.e.:
this process follows conservation of mass, including conservation of mass of the lithium bromide solution and conservation of mass of the lithium bromide solute, namely:
wherein, T 10 Is the temperature of the cooling water outlet of the absorber/cooling water inlet of the condenser, T c,in Temperature of cooling water flowing into the absorber, f c For the flow of cooling water, C pc Is the specific heat capacity of the cooling water.
2.1.2 ) constructing a static mathematical model of the generator
In the generator, the lithium bromide dilute solution is driven by the solution pump, flows in from the absorber through the heat exchanger, is heated and evaporated in the generator, is separated into water vapor and lithium bromide concentrated solution, the water vapor flows into the condenser, and the lithium bromide concentrated solution flows back to the absorber through the heat exchanger; this process follows conservation of energy, Q g The total heat absorbed in the generator per second is equal to the heat released by the heating water and also equal to the difference between the enthalpy of the substance flowing out of the generator and the enthalpy of the substance flowing into the generator, i.e.:
Q g =f g C pg (T g,in -T g,out )
Q g =f 4 h 4 +f 6 h 6 -f 3 h 3
this process follows conservation of mass, including conservation of mass of the lithium bromide solution and conservation of mass of the lithium bromide solute, namely:
wherein, f g For heating the flow of water, C pg For heating the specific heat capacity of the water, T g,in 、R g,out The temperatures of the heated water flowing into and out of the generator, respectively.
2.1.3 ) constructing a static mathematical model of a condenser
In the condenser, the water vapor flowing from the generator is condensed and then flows toward the evaporator; specifically, the surface temperature of the cooling water pipe is low, and water vapor flowing from the generator condenses into small droplets and adheres to the surface of the cooling water pipe, and then drops to the collecting device and flows to the evaporator. This process follows conservation of energy, Q c The total heat released in the condenser per second is equal to the heat absorbed by the cooling water flowing through the condenser, and is also equal to the difference between the enthalpy of the water vapor flowing into the condenser and the enthalpy of the condensed water flowing out of the condenser, i.e.:
this process follows the conservation of mass of the water species, namely: f. of 6 =f 7 ;
Wherein f is c For cooling water flow, C pc For the specific heat capacity of the cooling water, T 10 Is the temperature, T, of the absorber cooling water outlet/condenser cooling water inlet c,out The temperature of the outlet of the cooling water for the condenser.
2.1.4 ) constructing a static mathematical model of the evaporator
The evaporator is close to the vacuum environment,the boiling point of water is low, and the water flows into the evaporator from the condenser and then is rapidly cooled and evaporated to absorb a large amount of heat. The refrigerating water pipeline flows through the evaporator, heat is absorbed to generate refrigerating water, and the refrigerating water flows through the building load for cooling and then flows into the evaporator again for refrigerating to complete refrigerating water circulation. In the evaporator, water flows into the evaporator from the condenser to be cooled and evaporated, and heat is absorbed from a refrigerating water pipeline, the refrigerating water in the refrigerating water pipeline forms a refrigerating cycle, water vapor formed in the evaporator is absorbed by the lithium bromide concentrated solution in the absorber to enter the absorber, and the next cycle is started; this process follows conservation of energy, Q e The total heat absorbed in the evaporator per second is equal to the heat released by the cooling water flowing through the evaporator and also equal to the difference between the enthalpy of the water vapor leaving the evaporator and the enthalpy of the condensed water flowing into the evaporator, i.e.:
this process follows the conservation of mass of the water species, namely: f. of 7 =f 8 ;
Wherein f is e For the flow of refrigerating water, C pe Specific heat capacity of refrigerating water, T e,out 、T e,in Respectively the inflow temperature and the outflow temperature of the chilled water flowing through the evaporator.
2.1.5 ) constructing a static mathematical model of a solution pump
The dilute lithium bromide solution is driven by the solution pump, flows from the absorber to the generator through the heat exchanger, and the process follows the mass conservation equation, including the mass conservation of the lithium bromide solution and the mass conservation of the lithium bromide solute, namely:
f 1 =f 2 ,X 1 =X 2
this process follows conservation of energy, namely:
wherein, W p Electric power consumed for solution pump, P c Is the ambient pressure, P, of the heat exchanger e Is the ambient pressure of the absorber, eta p Is the efficiency of the solution pump.
2.1.6 Constructing a static mathematical model of a heat exchanger
In the heat exchanger, the lithium bromide concentrated solution from the generator and the lithium bromide dilute solution from the absorber are subjected to heat exchange, so that the temperature of the lithium bromide dilute solution flowing into the generator is increased, and the energy Q required for heating the lithium bromide dilute solution in the generator is reduced g Thereby increasing the coefficient of performance (COP) of the system cool
This process follows the conservation of energy that the dilute lithium bromide solution flowing from the absorber to the generator absorbs an amount of heat equal to the amount of heat given off by the concentrated lithium bromide solution flowing from the generator back to the absorber, i.e. that is
f 3 h 3 -f 2 h 2 =f 4 h 4 -f 5 h 5
The mass conservation of the lithium bromide solution and the lithium bromide solute in the process is shown in the following equation
f 2 =f 3 X 2 =X 3
f 4 =f 5 ,X 4 =X 5 。
The temperature of the solution in the heat exchanger is related to the heat exchanger coefficient epsilon, and the equation is as follows
T 1 =T 2
T 5 =T 4 -ε(T 4 -T 2 )。
2.1.7 Calculating the refrigeration coefficient
Based on the above formula, the COP of the absorption refrigerator can be calculated cool (ii) a Coefficient of performance COP cool Equal to the refrigerating capacity Q of the absorption refrigerator e Energy Q required for producing heating water with absorption refrigerator g And the solution pump consumes energy W p The ratio of (A) to (B) is as follows:
Q e +Q g +W p =Q a +Q c
2.2 Dynamic model for constructing absorption chiller model
Based on the above-established static model of each component, the working point temperature T 1 ,T 4 ,T 7 ,T 8 Calculating heat transfer coefficients UA of the absorber, the generator, the condenser and the evaporator respectively based on the solution results of the static models of the components by introducing a logarithmic mean temperature LMTD for the set value a ,UA g ,UA c And UA e And establishing a heat transfer coefficient model of each component in the absorption refrigerator model so as to obtain a dynamic model of the absorption refrigerator.
2.2.1 Mathematical model of absorber)
Q a =UA a LMTD a
Wherein, UA a Is the heat transfer coefficient of the absorber, LMTD a Is the logarithmic mean temperature difference of the absorber;
2.2.2 Mathematical model of generator
Q g =UA g LMTD g
Therein, UA g For the heat transfer coefficient of the generator, LMTD g Is the logarithmic mean temperature difference of the generator;
2.2.3 Mathematical model of condenser
Q c =UA c LMTD c
In which UA c As heat transfer coefficient of condenser, LMTD c Is the logarithmic mean temperature difference of the condenser;
2.2.4 Mathematical model of evaporator
Q e =U e A e LMTD e
Therein, UA e As heat transfer coefficient of evaporator, LMTD e Is the logarithmic mean temperature difference of the evaporator;
2.2.5 Efficiency calculation
Wherein the COP cool Refrigeration coefficient, P, for absorption chiller model cool Eta when the energy for producing the heating water is derived from the heat recovered by the model of the cogeneration unit for absorbing the refrigerating power of the model of the refrigerating machine cool To consume the refrigeration efficiency of the fuel with respect to the cogeneration unit model.
2.2 Constructing a dynamic model of an absorption chiller
Based on the above-established static model of each component, its operating point temperature T 1 ,T 4 ,T 7 ,T 8 For the set point, the absorber is calculated respectively based on the solution results of the static model of each component by introducing the log mean temperature LMTDHeat transfer coefficient UA of generator, condenser and evaporator a ,UA g ,UA c And UA e And establishing a heat transfer coefficient model of each component in the absorption refrigerator model so as to obtain a dynamic model of the absorption refrigerator.
2.2.1 Mathematical model of absorber)
Q a =UA a LMTD a
Therein, UA a Is the heat transfer coefficient of the absorber, LMTD a For the logarithmic mean temperature difference of the absorber, in the actual setting, LMTD can be set a Is 9.692K, UA a Is 45.192kW/K.
2.2.2 Mathematical model of generator
Q g =UA g LMTD g
Wherein, UA g For the heat transfer coefficient of the generator, LMTD g For the logarithmic mean temperature difference of the generator, in the actual setting, the LMTD can be set g Is 21.120K, UA g Is 21.448kW/K.
2.2.3 Mathematical model of condenser
Q c =UA c LMTD c
In which UA c Is the heat transfer coefficient of the condenser, LMTD c For the logarithmic mean temperature difference of the condenser, in the actual setting, LMTD can be set c Is 11.469K, UA c Is 33.770kW/K.
2.2.4 Mathematical model of evaporator
Q e =U e A e LMTD e
Wherein, UA e As heat transfer coefficient of evaporator, LMTD e For the logarithmic mean temperature difference of the evaporator, in the actual setting, LMTD can be set e Is 3.641K, UA e Is 102.416kW/K.
2.2.5 Efficiency calculation
P cool =Q e
Wherein the COP cool Refrigeration coefficient, P, for absorption chiller model cool Eta when the energy for producing the heating water is derived from the heat recovered by the model of the cogeneration unit for absorbing the refrigerating power of the model of the refrigerating machine cool To consume the refrigeration efficiency of the fuel with respect to the cogeneration unit model.
And step 103, establishing a thermal network model.
In particular, the heat network transfers heat energy to a heat load through a heat pipe by means of a heat medium, which commonly includes steam or hot water. The heat network model of the embodiment comprises a heat source module, a pipeline module and a building load, wherein the heat source module is hot water directly generated by the cogeneration unit module or generated by a gas boiler, the heat network takes water as a medium, the hot water is transported to the building load through the pipeline module to supply heat to a user, and the cooled water flows back to the cogeneration unit module or the gas boiler through the pipeline module to be continuously heated, so that the circulation of the heat network is realized. At this time, the pipeline module is divided into a heat distribution pipeline and a water return pipeline.
In the embodiment, a heat source module and a building load in a thermal network model are set as a plurality of nodes, a pipeline module is set as a plurality of sides to form a graph theory, and the thermal network model is established based on the graph theory.
Taking the example that the constructed thermodynamic network comprises a cogeneration unit, a gas boiler, a water pump, two building loads and eight thermodynamic pipelines, abstracting the thermodynamic network into a graph, abstracting the thermodynamic pipelines into sides, abstracting the building loads, the cogeneration unit, the gas boiler and the like into nodes, and because the electric energy consumed by the water pump is extremely small relative to the system, the electric energy can be ignored, so that the thermodynamic network is represented into the graph consisting of six nodes and eight sides.
3.1.1 ) basic correlation matrix
Based on the graph theory knowledge, for a directed graph containing m nodes and n edges, each node and each edge of the thermodynamic network structure graph can be represented by an incidence matrix A of m multiplied by n orders, wherein a matrix element a ij Is determined by
The thermodynamic network can be represented by a correlation matrix A of order 6 × 8
Taking a certain node in the incidence matrix A as a reference node, and removing the row in which the node is positioned from A to obtain a basic incidence matrix A of (m-1) multiplied by n orders c . In the above thermodynamic network, the node v of the cogeneration unit 1 As a reference node, the parameters of flow, temperature, pressure and the like are set to known quantities, so that a basic correlation matrix A of 5 x 8 orders can be used c To represent
3.1.2 Basic loop matrix
Based on the knowledge of graph theory, for a graph containing m nodes and n edges and having n-m +1 basic loops, the relation between the basic loops and the edges of the graph can be described by a (n-m + 1) × n-order basic loop matrix B, wherein the matrix element B kj Is determined by
Representing the heat power network basic loop matrix B; specifically, the above thermodynamic network can be represented by a basic loop matrix B of 3 × 8 order
3.1.3 Traffic distribution in the thermal network
Constructing a flow balance equation which is A c F =0, where F is the flow vector in each pipe;
constructing a pressure balance equation, namely B delta H =0, wherein delta H is a pressure loss vector in each pipeline;
constructing a pressure loss vector equation, namely delta H = K | F | F, wherein K is a resistance coefficient matrix of each pipeline;
the equations are combined to obtain a thermodynamic network equation set, and the flow and pressure loss of each branch in the thermodynamic network can be obtained by solving:
taking the above thermal network as an example, the above equations are constructed.
(1) Equation of flow balance
According to the flow continuity of the thermodynamic network, that is, the water flow injected into each node is equal to the water flow flowing out of each node, we can obtain: a. The c F =0, wherein F = [ F = [ ] 1 f 2 f 3 f 4 f 5 f 6 f 7 f 8 ] T Is the flow vector of the pipeline, f 1 ,f 2 ,...,f 8 Are respectively an edge e 1 ,e 2 ,...,e 8 The flow rate of (c).
(2) Equation of pressure equilibrium
In one elementary circuit, the sum of the pressure losses of the water flowing in the various pipes is equal to zero, i.e. B Δ H =0, where Δ H = [ Δ H = [ ] 1 ΔH 2 ΔH 3 ΔH 4 ΔH 5 ΔH 6 ΔH 7 ΔH 8 ] T As vector of pressure loss in the pipe, Δ H 1 ,ΔH 2 ,...,ΔH 8 Are respectively an edge e 1 ,e 2 ,...,e 8 Pressure loss of (3).
(3) Vector equation of pressure loss
ΔH=K|F|F
Where K = diag { K } 1 K 2 K 3 K 4 K 5 K 6 K 7 K 8 Is a pipeline resistance coefficient matrix of the thermodynamic network, K 1 ,K 2 ,...,K 8 Are respectively a pipe e 1 ,e 2 ,...,e 8 The coefficient of resistance of (a).
And (3) obtaining a thermodynamic network equation set in a simultaneous manner, wherein the equation set comprises 16 equations and 16 variables, and solving to obtain the flow and pressure loss of each branch in the thermodynamic network:
3.1.4 Thermodynamic network temperature calculation
Constructing a temperature balance equation, and constructing A based on that the temperature at the initial end of the pipeline minus the temperature at the tail end of the pipeline is equal to the temperature drop on the pipeline 1 ,A 2 A matrix, wherein,
A 1 element a of ij ' satisfy
A 2 Element a of ij "satisfy
Wherein T is out =[T i,out ] T Is the return water temperature vector of the node, T i,out Is the return water temperature, T, of each node in =[T i,in ] T Supply water temperature vector of node, T i,in The temperature of the water supply for each node; taking the above thermodynamic network as an example, T out =[T 1,out T 2,out T 3,out T 4,out T 5,out T 6,out ] T Is the return water temperature vector of the node, T i,out Is the return water temperature, T, of each node in =[T 1,in T 2,in T 3,in T 4,in T 5,in T 6,in ] T Supply water temperature vector of node, T i,in The temperature of the water supply for each node.
Constructing a model of the thermal pipeline module for simulating a transmission link of heat energy; assuming that the thermal conduit has a conduit radius of R p A heat transfer coefficient of K p (W/m 2 DEG C) at an ambient temperature of T atm The hot water temperature at the head end of the pipeline is T s Then the hot water temperature T at l from the head end of the pipeline satisfies the following equation:
C p fdT=(T-T atm )K p ·2πR p dl
wherein C is p Is the specific heat capacity of water, and f is the flow rate of water. If the length of the pipeline is L p The temperature T of the hot water at the end of the pipe e Is composed of
For the thermodynamic network, the temperature drop Δ T of the jth pipe j Is composed of
Constructing a thermodynamic node power equation, wherein the thermodynamic node comprises a heat load node, a heat source node and a pipeline junction node;
for the pipeline junction node, the following requirements are met: t is i,in =T i,out ;
For the thermal load node, the thermal power consumed by the load is assumed to be P tli ,f vi For the water flow to the injection node, P is tli =C p f vi (T i,in -T i,out );
For the heat source node, assume that the thermal power produced is P tsi Then there is P tsi =C p f vi (T i,out -T i,in );
Node power equation of thermodynamic network can be constructed by integrating nodes at junctions of heat load, heat source and pipeline
P=C p F v (T in -T out )
Wherein P = [ P = i ] T As a node power vector, P i For the injection power of each node, the node of the heat load is a positive value, the node of the heat source is a negative value, and the node of the pipeline intersection is zero;
node traffic matrix F v =diag{f vi Can be obtained from the following formula
F v ′=A 1 F=-A 2 F=[f v1 ] T
F v =diag(F v ′)
Taking the above thermodynamic network as an example, P = [ P = [ P ] 1 P 2 P 3 P 4 P 5 P 6 ] T As a node power vector, P i For the injected power of each node, the node for the heat load is a positive value, the node for the heat source is a negative value, and the node at the intersection of the pipelines is zero. Node traffic matrix F v =diag{f v1 f v2 f v3 f v4 f v5 f v6 Can be obtained from the following formula
F v '=A 1 F=-A 2 F=[f v1 f v2 f v3 f v4 f v5 f v6 ] T
F v =diag(F v ')。
3.2 Modeling thermal loads
The heat load in this embodiment is mainly a building load, and for the building load, heat exchange between the indoor air and the hot water in the heat supply pipeline needs to be considered, and heat exchange between the indoor air and the external environment through the roof and the wall needs to be considered.
3.2.1 Heat transfer from indoor air to hot water pipes
Suppose that the supply water temperature to the building load is T in Return water temperature of T out Indoor air temperature of T room Then there is
P i =k·A·(T in -T room )
P i =C p f vi (T in -T out )
Wherein, P i The heat power transferred by the hot water to the indoor air of the ith node is k, the heat convection coefficient between the hot water and the indoor air is k, and A is the area of heat convection;
3.2.2 ) heat transfer of indoor air to the outside environment
Including heat transfer from the ambient environment to the shroud, and from the shroud to the indoor air; constructing a heat transfer expression and a heat balance equation based on the different shades and their heat transfer coefficients to obtain the indoor air temperature T of the building load room 。
In practical applications, the shelter is mainly used as a roof, a wall, a window, etc. medium through which indoor air is heat exchanged with the external environment, and the heat transfer forms include heat conduction and heat convection. This heat exchange can be divided into two sub-processes, the heat transfer between the external environment and the roof, walls, windows, etc., and the heat transfer between the roof, walls, windows and the indoor air. This heat transfer process is described below using a wall as an example.
Suppose outdoor ambient temperature is T atm Wall temperature of T wall The heat transfer between the wall and the outdoor environment can be expressed by the following equation
Q wall-atm,1 =k wall,1 ·A wall ·(T wall -T atm )
Q wall-atm =Q wall-atm,1 +Q wall-atm,2
Wherein Q is wall-atm For heat power transferred from the wall to the outdoor environment, Q wall-atm,1 Thermal power, Q, transferred to the outdoor environment by the wall in the form of thermal convection wall-atm,2 Heat power, k, transferred to the outdoor environment by the wall in the form of heat conduction wall,1 Is the thermal convection coefficient, k, between the wall and the air wall,2 Is the coefficient of thermal conductivity between the wall and the air, A wall Is the wall area, D wall Is the wall thickness.
The heat transfer process between the wall and the indoor air can be expressed by the following formula
Q room-wall,1 =k wall,1 ·A wall ·(T room -T wall )
Q room-wall =Q room-wall,1 +Q room-wall,2
Wherein Q is room-wall Is the indoor air directionThermal power, Q, transferred through the wall room-wall,1 For transferring heat power, Q, to the wall in the form of heat convection to the room air room-wall,2 For the heat power transferred from the indoor air to the wall in the form of heat conduction, the heat balance equation of the wall is
Wherein c is wa ll is the specific heat capacity of the wall, m wall In order to be the quality of the wall,is the rate of change of the wall temperature.
Similarly, for a roof, the heat transfer process with the outdoor environment can be expressed by
Q roof-atm,1 =k roof,1 ·A roof ·(T roof -T atm )
Q roof-atm =Q roof-atm,1 +Q roof-atm
The heat transfer process between the roof and the indoor air can be expressed by the following formula
Q room-roof,1 =k roof,1 ·A roof ·(T room -T roof )
Q room-roof =Q room-roof,1 +Q room-roof,2
For a window, its heat transfer process with the outdoor environment can be expressed by
Q win-atm,1 =k win,1 ·A win ·(T win -T atm )
Q win-atm =Q win-atm,1 +Q win-atm,2
The heat transfer process between the window and the indoor air can be expressed by the following formula
Q room-win,1 =k win,1 ·A win ·(T room -T win )
Q room-win =Q room-win,1 +Q room-win,2
The thermal equilibrium equation of the window isThe naming of the parameters in the above equations may refer to the naming in the wall equation to determine the meaning of each parameter.
Indoor air temperature T of building load room Can be obtained from the following formula
Wherein c is the specific heat capacity of air, m is the mass of indoor air,is the rate of change of the indoor air temperature.
And 104, forming an electric-thermal integrated energy system transient simulation model based on the combined heat and power generation unit model, the absorption refrigerator model and the thermal network model, and realizing real-time control simulation of the electric-thermal integrated energy system.
4.1. Building simulation model of cogeneration unit
Building a simulation model of the cogeneration unit on Simulink based on a mathematical model of the cogeneration unit;
as shown in fig. 5 and fig. 6, the simulation model of the cogeneration unit includes a gas turbine model, a heat recovery device model and a generator model, wherein the heat recovery device model calculates a thermal power P recovered by the heat recovery device from the waste heat flue gas hr And thermal power P directly used therein for heat supply hr1 The heat supply mode can be that a waste heat boiler produces hot water or directly utilizes steam to supply heat energy to the building load, and the process of producing the hot water can be simulated according to the requirement; specifically, the heat recovery device model calculates the thermal power P recovered by the heat recovery device from the waste heat flue gas hr And thermal power P directly used therein for heat supply hr1 And combining P hr1 Inputting a controlled heat flow source model which can be directly quoted from a Simulink element library as a control signal and outputting thermal power P by the controlled heat flow source model hr1 Inputting the heat exchanger model, wherein the controlled heat source model receives an input signal that sets the amount of heat output by the controlled heat source model and is therefore represented by the same symbol; the other end of the heat exchanger model is connected into a hot water pipeline network, so that the process of producing hot water is simulated. In addition, the generator model comprises a synchronous generator and an excitation system thereof in a Simscape component library of Simulink, and the generator model, the gas turbine model and the heat recovery device model together form a simulation model of the cogeneration unit.
4.2 construction of absorption chiller simulation model
As shown in fig. 7, based on a mathematical model of an absorption refrigerator, a simulation model of a lithium bromide absorption refrigerator is constructed on Simulink, models are respectively constructed for an absorber, a generator, a condenser and an evaporator according to mathematical formulas thereof, for solving a nonlinear equation set therein, the nonlinear equation set is firstly input into an m function file, the function file is input into an interpolated Matlab Fcn of a Simulink component library, variables to be solved of the nonlinear equation set and initial values thereof are connected with an interpolated Matlab Fcn module, and when parameters of the interpolated Matlab Fcn module are set, a fsolve function of Matlab is selected to iteratively solve the nonlinear equation set.
4.3 construction of thermal network simulation model
As shown in fig. 8, the established mathematical model of the thermal pipeline adopts pipe elements in a thermal liquid library of Simulink to construct a simulation model of the thermal pipeline and simulate a transmission link of thermal energy; the model considers the temperature drop phenomenon caused by heat exchange between hot water and the external environment, and different actual pipe network conditions can be simulated by changing parameters such as the radius, the length and the like of the model. And simulating a consumption link of heat energy through the building load simulation model to establish a heat load model.
As shown in fig. 9, the model is based on the basic law of thermodynamics, and considers heat transfer modes such as heat conduction and heat convection, including energy exchange between windows, walls, roofs and the like in buildings and the outside, wherein links such as heat convection and heat conduction are mainly built by Thermal Elements in the Simscape element library of Simulink. The energy exchange process between the window, wall, roof, etc. in the model and the outside is equivalent to the same energy exchange process, and a simplified thermal load simulation model can be obtained, as shown in fig. 10.
As shown in fig. 11, a heat load model is established by simulating a consumption link of heat energy through a building load simulation model, the heat load model is packaged into a house model, and the three house models are combined and packaged into a building model, so that a final building load simulation model is obtained. And constructing a thermal network simulation model in Simulink based on the thermal pipeline simulation model and the thermal load simulation model established above.
As shown in fig. 12, the model includes a cogeneration unit, a gas boiler, two building loads, and a multi-stage heat distribution pipeline, wherein the gas boiler model is formed by using a boiler model in the House heating system calculation in the Simulink example library.
4.4 construction of simulation model of electric-thermal comprehensive energy system
As shown in fig. 13 and 14, an electric-thermal integrated energy system simulation model is constructed in Simulink based on the cogeneration unit simulation model, the absorption chiller simulation model, the thermal network simulation model, and the component models in the Simulink component library. Specifically, photovoltaic equipment, electric energy storage equipment, an electric load equipment model and a gas turbine of the cogeneration unit model in the Simulink component library are all connected to a 10kV bus and are connected with a 35kV power distribution network through a transformer; and the heat recovery device model of the cogeneration unit model is connected into the thermal network model, and the absorption refrigerator model produces heat for heating water and the heat comes from the heat recovery device model of the cogeneration unit.
Before the simulation model of the comprehensive energy system runs, the following data input needs to be ensured to be acquired: simulation time length t sim Default value is 86400s, time of day; the CHP output plan is a set value of the output power of a cogeneration unit in one day, the photovoltaic array power plan is a set value of the photovoltaic output power in one day, the energy storage charging and discharging plan is a set value of the charging and discharging power in one day, an electric load curve is a predicted value of the electric load size in one day, 15 minutes are taken as a time unit, 96 data points are contained in one day, and data are input into the simulation system in an excel spreadsheet mode; environmental temperature T in combined heat and power generation unit model and heat load model atm Varying in relation to a cosine function by varying its base value T bias Amplitude of fluctuation T amp When the temperature conditions of the simulation are changed, the indoor temperature target values of the buildings in the thermal load model are respectively T set1 And T set2 。
The above embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, and any insubstantial changes and substitutions made by those skilled in the art based on the present invention are within the protection scope of the present invention.
Claims (7)
1. A modeling simulation method for operation control of an electric-thermal comprehensive energy system is characterized in that,
the method comprises the following steps:
establishing a combined heat and power generation unit model, acquiring each component of the combined heat and power generation unit and respectively establishing corresponding models;
establishing an absorption refrigerator model, acquiring each component of the absorption refrigerator, and respectively establishing a corresponding static model and a corresponding dynamic model;
establishing a thermodynamic network model;
forming an electric-thermal comprehensive energy system transient simulation model based on the cogeneration unit model, the absorption chiller model and the thermal network model to realize real-time control simulation of the electric-thermal comprehensive energy system,
the establishing of the cogeneration unit model comprises the following steps:
the combined heat and power generator comprises a gas turbine, a generator and a heat recovery device; correspondingly, establishing a mathematical model of the gas turbine based on the Rowen model; establishing a mathematical model of the heat recovery device; establishing a mathematical model of the generator; calculating the heat power P recovered by the heat recovery device from the waste heat smoke hr Directly used for heat supply hr1 Inputting the thermal power of the absorption refrigerator, wherein the heat supply mode is to input a waste heat boiler to produce hot water or directly utilize steam to supply heat energy to the building load;
1.1 Establishing a mathematical model of the gas turbine based on the Rowen model, wherein the mathematical model of the gas turbine comprises a speed controller model, a waste heat flue gas temperature controller model, an acceleration controller model, a fuel system model, and a compressor and turbine model;
1.1.1 The speed controller model is used for scheduling the command P according to the power set And the actual output P of the generator e Adjusting the output power of the generator to enable the cogeneration unit to work according to a power dispatching instruction; and also for the dependence on the nominal speed omega ref With the actual speed omega of the generator r Adjusting the rotation speed of a prime mover to keep the frequency of the generator stable; the method specifically comprises the following steps:
wherein, V ce0 Speed command, K, output for speed controller Droop Is the droop coefficient, T is the time constant, K p And K i Proportional parameters and integral parameters for PI regulation;
1.1.2 The waste heat flue gas temperature controller model is linked with the compressor and turbine model, and the waste heat flue gas temperature calculated by the compressor and turbine model is used as input to ensure the waste heat flue gas temperature T exhaust Maintained at a temperature reference value T ref ;
The waste heat flue gas temperature controller model comprises a radiation shielding module, a thermal coupling module and a PI controller module, wherein the radiation shielding module and the thermal coupling module are used for simulating time delay caused by corresponding modules in an actual temperature measuring device;
based on the waste heat flue gas temperature controller model, the speed instruction upper limit value V output by the speed controller ce_limit1 :
Wherein, T rs1 、T rs2 ,T th For radiation shielding and thermal coupling coefficients, K p And K i Proportional parameters and integral parameters adjusted by the PI controller module;
1.1.3 The acceleration controller model is used to reduce thermal stress by limiting the acceleration of the rotor at the start-up of the gas turbine and also to limit the generator rotor speed during operation of the gas turbine;
based on the acceleration controller model, the speed command upper limit value V output by the speed controller ce_limit2 :
Wherein, T inertia Is the inertia constant of the rotor of the generator;
speed command V of speed regulator ce0 After amplitude limiting, the final speed regulating signal V is obtained ce ,min represents taking the minimum value:
V ce =min{V ce0 ,V ce_limit1 ,V ce_limit2 };
1.1.4 The fuel system model is used for calculating the consumed power of the fuel of the gas turbine according to the control instruction of the speed controller and comprises a valve regulation module and a fuel regulation module;
wherein the power consumption is related to the delay of the gas valve and the gas turbine performs work W on the gas turbine f The method specifically comprises the following steps:
wherein, T vp Is the time constant of the valve regulating module, T fs Time constant, K, of fuel regulating module init Is the minimum per unit value of work done for the gas turbine;
taking into account the ambient temperature T atm To fuel combustion efficiency eta fuel Influence of η fuel And T atm The relation between the two is described by a function, and the work of the gas turbine on the gas turbine is calculated to be W under a certain environmental temperature f Fuel P required by gas turbine fuel (ii) a When the output of the cogeneration unit is P e When it is used, its electrical efficiency is eta ele The specific function is:
based on the above function, the thermal power P in the waste heat flue gas exhaust Is composed of
P exhaust =P fuel (1-η fuel )
1.1.5 Compressor and turbine models used to perform the fuel system dispatchFuel control signal command to calculate the torque T output by the turbine m And the temperature T of the exhaust gas exhaust The method specifically comprises the following steps:
wherein, K HHV Is a coefficient related to enthalpy, T ref Is the exhaust gas reference temperature, is the set value, T CR Delay time for combustion reaction, T TD For delay of transit time of turbine exhaust system, T CD A time constant for the compressor displacement;
1.2 To establish a mathematical model of a heat recovery device
The heat recovery device is used for recovering the heat of the waste heat flue gas generated by the gas turbine mathematical model, and part of the heat is input into a waste heat boiler model or a heat load model and part of the heat is input into the absorption refrigeration unit model; establishing a mathematical model of the heat recovery device based on the basic laws of energy conservation and thermodynamics;
the energy conservation equation of the cogeneration unit is as follows:
P fuel =W f +P loss +P exhaust
wherein, P fuel As fuel combustion power, W f Power, P, for the steam to work the gas turbine exhaust Is the thermal power, P, of the waste heat flue gas of a gas turbine loss Is the power loss;
the energy conservation equation of the heat recovery device is as follows:
P hr =P exhaust ×η hr
P hr1 =(1-δ)P hr
P hr1 =C pw f w (T w,out -T w,in )
wherein,P hr thermal power, P, recovered for the heat recovery device hr1 Delta is the proportion of the recovered heat which flows to the absorption refrigerating unit, eta is the thermal power for supplying heat hr For the efficiency of the heat recovery device, C pw Is the specific heat capacity of water, f w Flow rate of water in the heat distribution pipe, T w,in ,T w,out The temperature of a water inlet and the temperature of a water outlet of the heat recovery device are respectively;
the efficiency equation of the heat recovery device is as follows
Wherein, T ex,in For the gas temperature at the inlet of the heat recovery device, T ex,out For the gas temperature at the outlet of the heat recovery device, T atm Is ambient temperature;
thermal efficiency eta of cogeneration unit heat Is composed of
Total efficiency eta of combined heat and power generation unit CHP Is composed of
2. The method of claim 1, wherein the establishing an absorption chiller model, obtaining components of the absorption chiller and establishing corresponding static and dynamic models, respectively, comprises:
the absorption refrigerator comprises a heat exchanger, a solution pump, an absorber, a condenser, a generator and an evaporator;
establishing said heat exchanger, said solution pump, said absorber, said condenser, said generator and said evaporator separatelyA static model, and respectively calculating heat transfer coefficients UA of the absorber, the generator, the condenser and the evaporator based on the solution of the static model a ,UA g ,UA c And UA e And establishing a heat transfer coefficient model of each component of the absorption refrigerator, thereby obtaining a dynamic model of the absorption refrigerator.
3. The method of claim 2, comprising:
the working medium in the absorption refrigerator is a lithium bromide aqueous solution, and each component constructs a static mathematical model based on a mass conservation principle and an energy conservation principle;
2.1 Constructing a static model of an absorption chiller
2.1.1 Static mathematical model for constructing an absorber
In the absorber, the lithium bromide concentrated solution absorbs the water vapor generated in the evaporator to form a lithium bromide dilute solution, and the heat generated by diluting the lithium bromide solution is absorbed by cooling water; the lithium bromide dilute solution is driven by the solution pump to flow to the generator through the heat exchanger, so as to start circulation; this process follows the equation of conservation of energy, Q a The total heat released in the absorber per second is equal to the heat absorbed by the cooling water flowing through the absorber, and is also equal to the difference between the enthalpy of the substance flowing into the absorber and the enthalpy of the substance flowing out of the absorber, i.e.:
Q a =f c C pc (T 10 -T c,in )
Q a =f 5 h 5 +f 8 h 8 -f 1 h 1
this process follows conservation of mass, including conservation of mass of the lithium bromide solution and conservation of mass of the lithium bromide solute, namely:
f 1 =f 5 +f 8
f 1 X 1 =f 5 X 5
wherein, T 10 Is the temperature of the cooling water outlet of the absorber/cooling water inlet of the condenser, T c,in Temperature of cooling water flowing into the absorber, f c For the flow rate of cooling water, C pc The specific heat capacity of the cooling water;
2.1.2 ) constructing a static mathematical model of the generator
In the generator, the lithium bromide dilute solution is driven by the solution pump, flows in from the absorber through the heat exchanger, is heated and evaporated in the generator, is separated into water vapor and lithium bromide concentrated solution, the water vapor flows in the condenser, and the lithium bromide concentrated solution flows back to the absorber through the heat exchanger; this process follows conservation of energy, Q g The total heat absorbed in the generator per second is equal to the heat released by the heating water and also equal to the difference between the enthalpy of the substance flowing out of the generator and the enthalpy of the substance flowing into the generator, i.e.:
Q g =f g C pg (T g,in -T g,out )
Q g =f 4 h 4 +f 6 h 6 -f 3 h 3
this process follows conservation of mass, including conservation of mass of the lithium bromide solution and conservation of mass of the lithium bromide solute, namely:
f 3 =f 4 +f 6
f 3 X 3 =f 4 X 4
wherein f is g For heating the flow of water, C pg For heating the specific heat capacity of the water, T g,in 、T g,out The temperatures of the heated water flowing into and out of the generator, respectively;
2.1.3 Constructing a static mathematical model of a condenser
In the condenser, the water vapor flowing from the generator is condensed and then flows toward the evaporator; this process follows conservation of energy, Q c The total quantity of heat released in the condenser per second is equal to the quantity of heat absorbed by the cooling water flowing through the condenser, and is also equal to the difference between the enthalpy of the water vapor flowing into the condenser and the enthalpy of the condensed water flowing out of the condenser, i.e., the difference is
Q c =f c C pc (T c,out -T 10 )
Q c =f 6 h 6 -f 7 h 7
This process follows the conservation of mass of the water species, namely:
f 6 =f 7
wherein f is c For cooling water flow, C pc For the specific heat capacity of the cooling water, T 10 Is the temperature of the cooling water outlet of the absorber/cooling water inlet of the condenser, T c,out The temperature of the cooling water outlet of the condenser;
2.1.4 ) constructing a static mathematical model of the evaporator
In the evaporator, water flows into the evaporator from the condenser to cool and evaporate, and heat is absorbed from a refrigerating water pipeline, the refrigerating water in the refrigerating water pipeline forms a refrigerating cycle, water vapor formed in the evaporator is absorbed by the lithium bromide concentrated solution in the absorber to enter the absorber, and the next cycle is started; this process follows conservation of energy, Q e The total heat absorbed in the evaporator per second is equal to the heat released by the cooling water flowing through the evaporator and also equal to the difference between the enthalpy of the water vapor leaving the evaporator and the enthalpy of the condensed water flowing into the evaporator, i.e.:
Q e =f e C pe (T e,out -T e,in )
Q e =f 8 h 8 -f 7 h 7
this process follows the conservation of mass of the water species,
f 7 =f 8
wherein f is e For the flow of refrigerating water, C pe Specific heat capacity of refrigerating water, T e,out 、T e,in The inflow temperature and the outflow temperature of the refrigeration water flowing through the evaporator are respectively;
2.1.5 ) constructing a static mathematical model of a solution pump
The dilute lithium bromide solution is driven by the solution pump, flows from the absorber to the generator through the heat exchanger, and the process follows the mass conservation equation, including the mass conservation of the lithium bromide solution and the mass conservation of the lithium bromide solute, namely:
f 1 =f 2
X 1 =X 2
this process follows conservation of energy, namely:
wherein, W p Electric power consumed for solution pumps, P c Is the ambient pressure, P, of the heat exchanger e Is the ambient pressure of the absorber, eta p The efficiency of the solution pump;
2.1.6 Constructing a static mathematical model of a heat exchanger
In a heat exchanger, the lithium bromide concentrated solution from the generator exchanges heat with the lithium bromide dilute solution from the absorber, and this process follows conservation of energy, and the amount of heat absorbed by the lithium bromide dilute solution flowing from the absorber to the generator is equal to the amount of heat released by the lithium bromide concentrated solution flowing from the generator back to the absorber, i.e. the amount of heat is equal to the amount of heat released by the lithium bromide concentrated solution flowing from the generator back to the absorber
f 3 h 3 -f 2 h 2 =f 4 h 4 -f 5 h 5
The mass conservation of the lithium bromide solution and the lithium bromide solute in the process is shown in the following equation
f 2 =f 3 X 2 =X 3
f 4 =f 5 ,X 4 =X 5
The temperature of the solution in the heat exchanger is related to the heat exchanger coefficient epsilon, and the equation is as follows
T 1 =T 2
T 5 =T 4 -ε(T 4 -T 2 )
2.1.7 Calculating the refrigeration coefficient
Coefficient of performance COP cool Equal to the refrigerating capacity Q of the absorption refrigerator e Energy Q required for producing heating water with absorption refrigerator g And the solution pump consumes energy W p The ratio of (A) to (B) is as follows:
Q e +Q g +W p =Q a +Q c
2.2 Constructing a dynamic model of an absorption chiller
Based on the above-established static model of each component, its operating point temperature T 1 ,T 4 ,T 7 ,T 8 Calculating heat transfer coefficients UA of the absorber, the generator, the condenser and the evaporator respectively based on the solution results of the static models of the components by introducing a logarithmic mean temperature LMTD for the set value a ,UA g ,UA c And UA e Establishing a heat transfer coefficient model of each component in the absorption refrigerator model so as to obtain a dynamic model of the absorption refrigerator;
2.2.1 Mathematical model of absorber)
Q a =UA a LMTD a
Therein, UA a Is the heat transfer coefficient of the absorber, LMTD a Is the logarithmic mean temperature difference of the absorber;
2.2.2 Mathematical model of generator
Q g =UA g LMTD g
Wherein, UA g For the heat transfer coefficient of the generator, LMTD g Is the logarithmic mean temperature difference of the generator;
2.2.3 Mathematical model of condenser
Q c =UA c LMTD c
In which UA c Is the heat transfer coefficient of the condenser, LMTD c Is the logarithmic mean temperature difference of the condenser;
2.2.4 Mathematical model of evaporator
Q e =U e A e LMTD e
Therein, UA e As heat transfer coefficient of evaporator, LMTD e Is the logarithmic mean temperature difference of the evaporator;
2.2.5 Efficiency calculation
P cool =Q e
Wherein the COP cool Refrigeration coefficient, P, for absorption chiller model cool Eta, for absorbing the refrigerating power of the model of the refrigerating machine, when the energy for producing the heating water comes from the heat recovered by the model of the cogeneration unit cool For consuming fuel in relation to a cogeneration unit modelThe refrigeration efficiency of the material.
4. The method of claim 1, wherein the establishing a thermal network model comprises:
the heat network model comprises a heat source module, a pipeline module and a building load, wherein the heat source module is steam directly generated by the cogeneration unit module or hot water generated by a gas boiler and is transported to the building load through the pipeline module, and the cooled water flows back to the cogeneration unit module or the gas boiler through the pipeline module to be continuously heated, so that heat network circulation is realized;
setting a heat source module and a building load in the thermal network model as a plurality of nodes, setting a pipeline module as a plurality of edges to form a graph theory, and establishing the thermal network model based on the graph theory.
5. The method of claim 4, wherein said modeling a thermodynamic network further comprises
3.1.1 ) basic correlation matrix
Based on the graph theory knowledge, for a directed graph containing m nodes and n edges, an incidence matrix A of m multiplied by n orders can be used for representing each node and each edge of the structure graph of the thermodynamic network, wherein a matrix element a ij Is determined by
Node v of the combined heat and power generation unit model 1 Setting the parameters of the combined heat and power generation unit model as known quantities to obtain a basic incidence matrix A as reference nodes c ;
3.1.2 Basic loop matrix
Based on the knowledge of graph theory, for a graph containing m nodes and n edges and having n-m +1 basic loops, the relation between the basic loops and the edges of the graph can be described by a (n-m + 1) × n-order basic loop matrix B, wherein the matrix element B kj Is determined by
Representing the heat power network basic loop matrix B;
3.1.3 Traffic distribution in the thermal network
Constructing a flow balance equation of
A c F=0
Wherein F is the flow vector in each pipeline;
constructing a pressure balance equation of
BΔH=0
Wherein Δ H is the pressure loss vector in each pipe;
constructing a vector equation of pressure loss, i.e.
ΔH=K|F|F
Wherein K is a resistance coefficient matrix of each pipeline;
the equations are combined to obtain a thermodynamic network equation set, and the flow and pressure loss of each branch in the thermodynamic network can be obtained by solving:
3.1.4 Thermodynamic network temperature calculation
Constructing a temperature balance equation, and constructing A based on that the temperature at the initial end of the pipeline minus the temperature at the tail end of the pipeline is equal to the temperature drop on the pipeline 1 ,A 2 A matrix, wherein,
A 1 element a of (1) ij ' satisfy
A 2 Element a of (1) ij "satisfy
Let A' = [ A ] 1 A 2 ]
A' T T=ΔT
Then T = [ T = [) out T in ]
Wherein T is out =[T i,out ] T Is the return water temperature vector of the node, T i,out Is the return water temperature, T, of each node in =[T i,in ] T Supply water temperature vector of node, T i,in The temperature of the water supply for each node;
constructing a model of the thermal pipeline module for simulating a transmission link of heat energy; assuming that the thermal conduit has a conduit radius of R p A heat transfer coefficient of K p Unit W/m 2 DEG C, the ambient temperature is T atm The hot water temperature at the head end of the pipeline is T s Then the hot water temperature T at a distance of l from the head end of the pipeline satisfies the following equation
C p fdT=(T-T atm )K p ·2πR p dl
Wherein C is p Is the specific heat capacity of water, f is the flow rate of water; if the length of the pipeline is L p The temperature T of the hot water at the end of the pipe e Is composed of
For the thermodynamic network, the temperature drop Δ T of the jth pipe j Is composed of
Constructing a thermodynamic node power equation, wherein the thermodynamic nodes comprise heat load nodes, heat source nodes and pipeline junction nodes;
for the pipeline junction node, satisfy
T i,in =T i,out
For the thermal load node, the thermal power consumed by the load is assumed to be P tli ,f vi For the water flow to fill the node, there are
P tli =C p f vi (T i,in -T i,out )
For the heat source node, assume that the thermal power produced is P tsi Then there is
P tsi =C p f vi (T i,out -T i,in )
Node power equation of thermodynamic network can be constructed by integrating nodes at junctions of heat load, heat source and pipeline
P=C p F v (T in -T out )
Wherein P = [ P = i ] T As a node power vector, P i For the injection power of each node, the node of the heat load is a positive value, the node of the heat source is a negative value, and the node of the pipeline intersection is zero;
node traffic matrix F v =diag{f vi Can be obtained by the following formula
F v '=A 1 F=-A 2 F=[f v1 ] T
F v =diag(F v ′);
3.2 Modeling thermal loads
3.2.1 Heat transfer from indoor air to hot water pipes
Suppose that the supply water temperature to the building load is T in Return water temperature of T out Indoor air temperature of T room Then there is
P i =k·A·(T in -T room )
P i =C p f vi (T in -T out )
Wherein, P i Heating power delivered to indoor air at i-th node for hot waterThe ratio, k, is the thermal convection coefficient between the hot water and the indoor air, and A is the area of thermal convection;
3.2.2 ) heat transfer of indoor air to the outside environment
Including heat transfer from the ambient environment to the shroud, and from the shroud to the indoor air; constructing a heat transfer expression and a heat balance equation based on the different shades and their heat transfer coefficients to obtain the indoor air temperature T of the building load room 。
6. The method according to claim 1, wherein the forming an electric-thermal integrated energy system transient simulation model based on the cogeneration unit model, the absorption chiller model and the thermal network model, and the implementing the real-time control simulation of the electric-thermal integrated energy system comprises:
4.1 ) constructing a simulation model of a cogeneration unit
Building a simulation model of the cogeneration unit on Simulink based on a mathematical model of the cogeneration unit;
the simulation model of the cogeneration unit comprises a gas turbine model, a heat recovery device model and a generator model, wherein the heat recovery device model calculates the thermal power P recovered by the heat recovery device from the waste heat and the flue gas hr And thermal power P directly used therein for heat supply hr1 And simulating the process of producing hot water;
the generator model comprises a synchronous generator and an excitation system thereof in a Simscape element library of Simulink;
4.2 Constructing an absorption chiller simulation model
Based on a mathematical model of the absorption refrigerator, constructing a simulation model of the lithium bromide absorption refrigerator on Simulink, iterating a nonlinear equation set in the model by using a fsolve function of Matlab, inputting a nonlinear equation set function file into an Interpreted Matlab Fcn of a Simulink element library, connecting corresponding input quantity and providing an initial value of a variable to be solved, and solving the nonlinear equation set;
4.3 Constructing a thermal network simulation model
The established mathematical model of the thermal pipeline adopts pipe elements in a thermal liquid library of Simulink to construct a simulation model of the thermal pipeline and simulate a transmission link of heat energy;
simulating a consumption link of heat energy through a building load simulation model, establishing a heat load model, packaging the heat load model into a house model, and packaging the three house models into a building model in a combined manner, thereby obtaining a final building load simulation model;
constructing a thermal network simulation model in Simulink based on the thermal pipeline simulation model and the thermal load simulation model established above;
4.4 To construct an electric-thermal integrated energy system simulation model
And an electric-thermal comprehensive energy system simulation model constructed in the Simulink is based on the combined heat and power generation unit simulation model, the absorption refrigeration machine simulation model, the thermal power network simulation model and the component models in the Simulink component library.
7. The method of claim 6, further comprising,
the electric-thermal comprehensive energy system simulation model is constructed, and the following data are input:
simulation time length t sim ;
Ambient temperature T varying as a function of the cosine atm Including the associated parameter base value T bias And the fluctuation amplitude T amp ;
The indoor temperature target value of the building is T set1 And T set2 ;
The CHP output plan is a set value of the output power of the cogeneration unit in one day;
photovoltaic array output plan, namely a set value of photovoltaic output power in one day;
an energy storage charging and discharging plan, namely a set value of charging and discharging power in one day;
the electrical load curve is a predicted value of the electrical load in a day.
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