CN104462840B - Backheat work done ratio and backheat ratio of profit increase assay method when non-reheat unit has hydrophobic cold source energy - Google Patents

Backheat work done ratio and backheat ratio of profit increase assay method when non-reheat unit has hydrophobic cold source energy Download PDF

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CN104462840B
CN104462840B CN201410800503.7A CN201410800503A CN104462840B CN 104462840 B CN104462840 B CN 104462840B CN 201410800503 A CN201410800503 A CN 201410800503A CN 104462840 B CN104462840 B CN 104462840B
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msub
steam
backheat
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CN104462840A (en
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王培红
刘朝阳
苏志刚
孙文
赵佳骏
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Southeast University
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Abstract

Backheat work done ratio and backheat ratio of profit increase assay method when having hydrophobic cold source energy the invention discloses a kind of non-reheat unit, non-reheat unit has three-level steam extraction backheat, the steam turbine of non-reheat unit is made of a cylinder, its three-level steam extraction number consecutively is the first order, the second level and third level steam extraction, and be connected respectively with the first order, the second level and third level heater, backheat work done is as follows than with the determination step of backheat ratio of profit increase when non-reheat unit has hydrophobic cold source energy：Obtaining non-reheat unit has the equivalent backheat steam flow work done of hydrophobic cold source energy, the dimensionless heat consumption rate of equivalent condensing stream work done and non-reheat without extraction cycle；Determine that non-reheat unit has the backheat work done of hydrophobic cold source energy when backheat ratio of profit increase.Backheat work done of the present invention realizes backheat work done than the high-precision with backheat ratio of profit increase, inexpensive hard measurement than the assay method with backheat ratio of profit increase.

Description

Backheat work done ratio is measured with backheat ratio of profit increase when non-reheat unit has hydrophobic cold source energy Method
Technical field
The present invention relates to it is a kind of for non-reheat unit have hydrophobic cold source energy when backheat work done when backheat ratio of profit increase Assay method can realize the measure of the when backheat ratio of profit increase of backheat work done when non-reheat unit has hydrophobic cold source energy, belong to Hard measurement field.
Background technology
The extraction cycle being made of heater is the important component of non-reheating embrittlement, and backheat effect is to influence non-reheat One of principal element of generatine set heat efficiency.The key technical indexes for evaluating backheat effect is backheat work done ratio and backheat ratio of profit increase. Wherein, backheat work done ratio refers to backheat steam flow work done institute in steam turbine internal strength (the sum of the work done of backheat steam flow and condensing stream work done) The ratio accounted for, backheat ratio of profit increase refer to efficiency relative growth rate of the backheat compared to no backheat.Backheat work done ratio is bigger, and backheat increases Beneficial rate is bigger, and backheat effect is better.
In backheat the work done when Traditional calculating methods of backheat ratio of profit increase, the extraction cycle of definition belongs to no cold source energy Cycling, the corresponding backheat steam flow work done namely work done without cold source energy.But for top heater drain discharge To the non-reheat unit of condenser, hydrophobic cold source energy can be generated, causes the survey of traditional backheat work done when backheat ratio of profit increase Calculation method fails.For this purpose, when backheat increases for backheat work done when a kind of present invention proposition non-reheat unit has hydrophobic cold source energy The Accurate Determining method of beneficial rate.
The content of the invention
Backheat work done ratio increases with backheat when having hydrophobic cold source energy it is an object of the invention to provide a kind of non-reheat unit The assay method of beneficial rate can realize the high-precision of the when backheat ratio of profit increase of backheat work done when non-reheat unit has hydrophobic cold source energy Degree, inexpensive hard measurement.
The present invention realizes by following technical solution：
Backheat work done ratio and backheat ratio of profit increase assay method when a kind of non-reheat unit has hydrophobic cold source energy, it is described it is non-again Heat engine group has three-level steam extraction backheat, and the steam turbine of non-reheat unit is made of a cylinder, and three-level steam extraction number consecutively is The first order, the second level and third level steam extraction, and be connected respectively with the first order, the second level and third level heater, first order heating Device is surface heater, and for hydrophobic row to second level heater, second level heater is contact(-type) heater, and the third level is heated Device is surface heater, drain discharge to condenser, backheat work done ratio when the non-reheat unit has hydrophobic cold source energy It is as follows with the determination step of backheat ratio of profit increase：
Step 1：Obtaining non-reheat unit has the equivalent backheat steam flow work done of hydrophobic cold source energyEquivalent condensing stream is made Work(And dimensionless heat consumption rate HR of the non-reheat without extraction cycleRK,
Step 2：According to：
X is compared in the backheat work done that determining non-reheat unit has hydrophobic cold source energyrAnd backheat ratio of profit increase δ ηRG。
The equivalent backheat steam flow work doneEquivalent condensing stream work doneAcquisition methods it is as follows：
Step 1：The calculating of therrmodynamic system carbonated drink parameter
Step 1.1：It takes heat consumption to ensure under operating mode, System Turbine Relative Internal Efficiency ηri, j-th stage heater extraction line pressure Loss rate δ pj(j=1,2,3)；
Step 1.2：Obtain following data：Non-reheat unit main steam temperature t0With main steam pressure p0；Condenser pressure pwc；First order extraction temperature t1With extraction pressure p1；Primary heater drain temperature td1, exit water temperature degree tw1With outlet hydraulic pressure Power pw1；Second level extraction temperature t2With extraction pressure p2；Second level heater outlet coolant-temperature gage tw2With go out water pressure pw2；3rd Grade extraction temperature t3With extraction pressure p3；Third level heater condensate temperature td3, exit water temperature degree tw3With go out water pressure pw3；
Step 1.3：By non-reheat unit main steam temperature t0With main steam pressure p0, steamed according to international water in 1997 and water The industrial properties of water and steam model that vapour property association proposes, is calculated main steam enthalpy h0And main steam Entropy s0, it is correspondingly made available steam turbine constant entropy steam discharge entropy sc *=s0；Steam turbine exhaust pressure pcWith condenser pressure pwcIt is identical, by vapour Turbine discharge pressure pcWith constant entropy steam discharge entropy sc *, the industrial water that is proposed according to international water and steam property association in 1997 and Constant entropy exhaust enthalpy h is calculated in water vapour thermodynamic properties modelc *；By the System Turbine Relative Internal Efficiency η takenri, calculate real Border exhaust enthalpy hc=h0-ηri·(h0-hc *)；By condenser pressure pwc, carried according to international water and steam property association in 1997 The industrial properties of water and steam model gone out, is calculated condensation water enthalpy hwc；
By first order extraction temperature t1And pressure p1, according to the industry of international water and steam property association proposition in 1997 With properties of water and steam model, first order steam extraction enthalpy h is calculated1；By first order extraction pressure p1And taken Level-one extraction line crushing rate δ p1, calculate the hydrophobic pressure p of primary heaterd1=p1·(1-δp1), it is dredged by primary heater Coolant-temperature gage td1With hydrophobic pressure pd1, according to the industrial water and steam of international water and steam property association proposition in 1997 The hydrophobic enthalpy h of primary heater is calculated in thermodynamic properties modeld1；By primary heater exit water temperature degree tw1And outlet Water pressure pw1, according to the industrial properties of water and steam model that international water and steam property association in 1997 proposes, Saliva enthalpy h is calculated outw1；
By second level extraction temperature t2With extraction pressure p2, proposed according to international water and steam property association in 1997 Second level steam extraction enthalpy h is calculated in industrial properties of water and steam model2；By second level heater outlet coolant-temperature gage tw2With go out water pressure pw2, according to the industrial water and steam heating power of international water and steam property association proposition in 1997 Saliva enthalpy h is calculated out in property modelw2；
By third level extraction temperature t3With extraction pressure p3, proposed according to international water and steam property association in 1997 Third level steam extraction enthalpy h is calculated in industrial properties of water and steam model3；By third level extraction pressure p3And it takes Third level extraction line crushing rate δ p3, calculate third level heater condensate pressure pd3=p3·(1-δp3), it is heated by the third level Device drain temperature td3With hydrophobic pressure pd3, the industrial water and water that are proposed according to international water and steam property association in 1997 Third level heater condensate enthalpy h is calculated in steam thermodynamic properties modeld3；By third level heater outlet coolant-temperature gage tw3With Go out water pressure pw3, according to the industrial properties of water and steam mould of international water and steam property association proposition in 1997 Saliva enthalpy h is calculated out in typew3；
Step 2：Calculate heater steam extraction share α at different levelsj(j=1,2,3), condensing fraction volume αc
Step 2.1：According to the thermal balance and flux balance equations of primary heater, steam extraction part of primary heater is obtained Volume：
According to the thermal balance and flux balance equations of second level heater, the steam extraction share of second level heater is obtained：
According to the thermal balance and flux balance equations of third level heater, the steam extraction share of third level heater and hydrophobic is obtained Share：
βc=α3 (4)
Step 2.2：Condensing fraction volume α can be obtained by mass balance equationc：
αc=1- α1-α2-α3 (5)
Step 3：Calculate backheat steam flow work done wr, condensing stream work done wc
Backheat steam flow work done is：
wr=α1·(h0-h1)+α2·(h0-h2)+α3·(h0-h3) (6)
Condensing stream work done is：
wc=αc·(h0-hc) (7)
Step 4：Calculate conversion condensing stream amount of work Δ wc
Third level heater condensate is can be calculated by heat flow diagrams be emitted into condenser generate additional cold source energy and be：
Δqc_d=βc·(hdn-hwc) (8)
Conversion condensing share Δ α can be calculated by (8) formulac：
Conversion condensing stream amount of work is can be calculated by (9),
Δwc=Δ αc·(h0-hc) (10)
Step 5：It calculates backheat work done and compares Xr
Equivalent backheat steam flow work done is：
Equivalent condensing stream work done is：
The dimensionless heat consumption rate HRRKAcquisition methods it is as follows：
It is defined according to heat consumption rate, obtains dimensionless heat consumption rate of the non-reheat without extraction cycle：
Wherein, h0For main steam enthalpy, hwcFor condensation water enthalpy, hcFor actual steam discharge enthalpy.
Assuming that when non-reheat unit has hydrophobic cold source energy, the series of regenerative steam is n, and main vapour enthalpy is h0, steam turbine Exhaust enthalpy is hc, it is h that condenser, which goes out saliva enthalpy,wc, j-th stage steam extraction share and steam extraction work done enthalpy drop are αjAnd Hj, condensing fraction volume and Condensing stream work done enthalpy drop is αcAnd Hc, it is respectively β into the hydrophobic share of condenser and hydrophobic enthalpycAnd hdn。
When final stage drain discharge to condenser, the additional cold source energy of generation is：
Δqc_d=βc·(hdn-hwc) (1)
The condensing share of hydrophobic cold source energy conversion is：
Conversion condensing stream amount of work of the additional cold source energy is：
Δwc=Δ αc·(h0-hc) (3)
Steam turbine backheat steam flow work done is：
The condensing stream work done of steam turbine is：
wc=αc·Hc (5)
Equivalent backheat steam flow work done is:
Equivalent condensing stream work done is：
Backheat work done ratio is：
Backheat ratio of profit increase refers to efficiency relative growth rate of the backheat compared to non-backheat, is defined as：
In formula, ηRGFor the thermal efficiency of non-reheat backheat unit, ηRKFor no backheat when unit the thermal efficiency.
By defining for heat consumption rate：
HRRG=HRRK-Xr·(HRRK-1) (10)
In formula, HRRGFor the dimensionless heat consumption rate of backheat unit, HRRKFor no backheat when unit dimensionless heat consumption rate,
By formula (10), (11), (12) substitute into formula (9) calculate backheat ratio of profit increase is：
The advantage of the invention is that：
(1) when having heaters drain discharge to condenser, additional hydrophobic cold source energy can be generated.Traditional backheat work done When backheat ratio of profit increase measuring method due to being calculated according only to backheat work done than the definition with backheat ratio of profit increase, is not examined Consider above-mentioned influence, cause its results of measuring mistake.The present invention combines above-mentioned influence factor, propose a kind of new backheat work done ratio and The assay method of backheat ratio of profit increase realizes backheat work done than the high-precision with backheat ratio of profit increase, inexpensive hard measurement；(2) Backheat work done proposed by the invention is than the assay method with backheat ratio of profit increase, the result of calculation checked with heat balance method It is completely the same.
Description of the drawings
Fig. 1 is the heat flow diagrams with three-level regenerative steam；
Fig. 2 is the calculation flow chart of the present invention.
Specific embodiment
Backheat work done ratio and backheat ratio of profit increase assay method, calculate mould when a kind of non-reheat unit has hydrophobic cold source energy Type is the non-reheat unit for having three-level steam extraction backheat for one.The steam turbine is made of a cylinder, three-level steam extraction according to Secondary number is the 1st grade, the 2nd grade and 3rd level steam extraction, and is connected respectively with the 1st grade, the 2nd grade and 3rd level heater, the 1st grade of heating Device is surface heater, and hydrophobic row is to the 2nd grade of heater, and the 2nd grade of heater is contact(-type) heater, 3rd level heater For surface heater, drain discharge to condenser.Determination step is as follows,
Step 1：The calculating of therrmodynamic system carbonated drink parameter
Step 1.1：It takes under THA (Turbine Heat Acceptance, heat consumption ensure operating mode), steam turbine is relatively interior Efficiency etari, j-th stage heater extraction line crushing rate δ pj(j=1,2,3).
Step 1.2：From SIS in Thermal Power PlantQ (SIS) or the database of scattered control system (DCS), obtain Take following data：Non-reheat unit main steam temperature t0With main steam pressure p0；Condenser pressure pwc；1st grade of extraction temperature t1With Extraction pressure p1；1st grade of heater condensate temperature td1, exit water temperature degree tw1With go out water pressure pw1；2nd grade of extraction temperature t2With Extraction pressure p2；2nd grade of heater outlet coolant-temperature gage tw2With go out water pressure pw2；3rd level extraction temperature t3With extraction pressure p3； 3rd level heater condensate temperature td3, exit water temperature degree tw3With go out water pressure pw3；
Step 1.3：By non-reheat unit main steam temperature t0With main steam pressure p0, steamed according to international water in 1997 and water The industrial properties of water and steam model IAPWS-IF97 (hereinafter referred to as IAPWS-IF97) that vapour property association proposes, meter Calculation obtains main steam enthalpy h0And the entropy s of main steam0, it is correspondingly made available steam turbine constant entropy steam discharge entropy sc *=s0.Turbine discharge Pressure pcWith condenser pressure pwcIt is identical, by steam turbine exhaust pressure pcWith constant entropy steam discharge entropy sc *, according to IAPWS-IF97, calculate Obtain constant entropy exhaust enthalpy hc *.By the System Turbine Relative Internal Efficiency η takenri, calculate to obtain actual exhaust enthalpy hc=h0-ηri·(h0- hc *)；By condenser pressure pwc, according to IAPWS-IF97, condensation water enthalpy h is calculatedwc。
By the 1st grade of extraction temperature t1And pressure p1, according to IAPWS-IF97, the 1st grade of steam extraction enthalpy h is calculated1；By the 1st grade Extraction pressure p1And the 1st grade of extraction line crushing rate δ p taken1, calculate the 1st grade of heater condensate pressure pd1=p1·(1-δ p1), by the 1st grade of heater condensate temperature td1With hydrophobic pressure pd1, according to IAPWS-IF97, the 1st grade of heater is calculated and dredges Water enthalpy hd1；By the 1st grade of heater outlet coolant-temperature gage tw1With go out water pressure pw1, according to IAPWS-IF97, outlet is calculated Water enthalpy hw1。
By the 2nd grade of extraction temperature t2With extraction pressure p2, according to IAPWS-IF97, the 2nd grade of steam extraction enthalpy h is calculated2；By 2nd grade of heater outlet coolant-temperature gage tw2With go out water pressure pw2, according to IAPWS-IF97, saliva enthalpy h is calculated outw2。
By 3rd level extraction temperature t3With extraction pressure p3, according to IAPWS-IF97,3rd level steam extraction enthalpy h is calculated3；By 3rd level extraction pressure p3And the 3rd level extraction line crushing rate δ p taken3, calculate 3rd level heater condensate pressure pd3= p3·(1-δp3), by 3rd level heater condensate temperature td3With hydrophobic pressure pd3, according to IAPWS-IF97,3rd level is calculated Heater condensate enthalpy hd3；By 3rd level heater outlet coolant-temperature gage tw3With go out water pressure pw3, according to IAPWS-IF97, calculate Obtain out saliva enthalpy hw3。
Step 2：Calculate heater steam extraction share α at different levelsj(j=1,2,3), condensing fraction volume αc
Step 2.1：According to the thermal balance and flux balance equations of the 1st grade of heater, the steam extraction share of the 1st grade of heater is obtained：
According to the thermal balance and flux balance equations of the 2nd grade of heater, the steam extraction share of the 2nd grade of heater is obtained：
According to the thermal balance and flux balance equations of 3rd level heater, the steam extraction share of 3rd level heater and hydrophobic share are obtained：
βc=α3 (4)
Step 2.2：Condensing fraction volume α can be obtained by mass balance equationc：
αc=1- α1-α2-α3 (5)
Step 3：Calculate backheat steam flow work done wr, condensing stream work done wc
Backheat steam flow work done is：
wr=α1·(h0-h1)+α2·(h0-h2)+α3·(h0-h3) (6)
Condensing stream work done is：
wc=αc·(h0-hc) (7)
Step 4：Calculate conversion condensing stream amount of work Δ wc
3rd level heater condensate is can be calculated by heat flow diagrams be emitted into condenser generate additional cold source energy and be：
Δqc_d=βc·(hdn-hwc) (8)
Conversion condensing share Δ α can be calculated by (8) formulac：
Conversion condensing stream amount of work is can be calculated by (9),
Δwc=Δ αc·(h0-hc) (10)
Step 5：It calculates backheat work done and compares Xr
Equivalent backheat steam flow work done is：
Equivalent condensing stream work done is：
Backheat work done ratio can be calculated by (11) (12) formula：
Step 6：Calculate backheat ratio of profit increase δ ηRG
By taking unit shown in Fig. 1 as an example, computation model be one have three-level steam extraction backheat non-reheat unit, heater By its extraction pressure, number is 1~3 respectively from high to low, and the 1st grade of heater is surface heater, and the 2nd grade of heater is mixed Box-like heater, 3rd level heater are surface heater.The drain discharge of 3rd level heater is to condenser.
Detailed calculation procedure is as follows：
(1), System Turbine Relative Internal Efficiency ηriFor 0.85；
The extraction line crushing rate δ p of j-th stage heaterj(j=1,2,3) it is 3%；
Read related real time data from the real-time data base of plant level supervisory information system (SIS), reading it is main in real time Data are as follows：
Main steam temperature t0For 535 DEG C；
Main steam pressure p0For 13.5MPa；
Condenser pressure pwcFor 0.005MPa；
1st grade of extraction temperature t1For 415.2 DEG C；
1st grade of extraction pressure p1For 6.080MPa；
1st grade of heater condensate temperature td1For 274.5 DEG C；
1st grade of heater outlet coolant-temperature gage tw1For 272.5 DEG C；
1st grade of heater outlet water pressure pw1For 13.500MPa；
2nd grade of extraction temperature t2For 256.8 DEG C；
2nd grade of extraction pressure p2For 1.600MPa；
2nd grade of heater outlet coolant-temperature gage tw2For 199.9 DEG C；
2nd grade of heater outlet water pressure pw2For 1.552MPa；
3rd level extraction temperature t3For 120.2 DEG C；
3rd level extraction pressure p3For 0.200MPa；
3rd level heater condensate temperature td3For 119.3 DEG C；
3rd level heater outlet coolant-temperature gage tw3For 117.3 DEG C；
3rd level heater outlet water pressure pw3For 1.552MPa；
It can be obtained according to classical IAPWS-IF97 and computation model：
Main steam enthalpy h0For 3426.274kJ/kg；
Condensation water enthalpy hwcFor 137.765kJ/kg；
Exhaust enthalpy of turbine hcFor 137.765kJ/kg；
1st grade of steam extraction enthalpy h1For 3215.414kJ/kg；
1st grade of heater condensate enthalpy hd1For 1207.950kJ/kg；
1st grade of heater outlet water enthalpy hw1For 1195.240kJ/kg；
2nd grade of steam extraction enthalpy h2For 2936.266kJ/kg；
2nd grade of heater outlet water enthalpy hw2For 852.023kJ/kg；
3rd level steam extraction enthalpy h3For 2617.188kJ/kg；
3rd level heater condensate enthalpy hd3For 500.602kJ/kg；
3rd level heater outlet water enthalpy hw3For 493.080kJ/kg；
(2), each heater steam extraction share α is calculatedj(j=1,2,3), condensing fraction volume αc
1st grade of heater steam extraction share is calculated to obtain by formula (1)：
2nd grade of heater steam extraction share is calculated to obtain by formula (2)：
3rd level heater steam extraction share is calculated to obtain by formula (3)：
3rd level heater condensate share is calculated to obtain by formula (4)：
βc=α3=0.12291
Condensing fraction volume is calculated to obtain by formula (5)：
(3), backheat steam flow work done w is calculatedr, condensing stream work done wc
Backheat steam flow work done is calculated to obtain by formula (6)：
wr=α1·(h0-h1)+α2·(h0-h2)+α3·(h0-h3)=182.96895kJ/kg
Condensing stream work done is calculated to obtain by formula (7)：
wc=αc·(h0-hc)=742.39784kJ/kg
(4), conversion condensing stream amount of work Δ w is calculatedc
By formula (8) calculate 3rd level heater condensate is emitted into condenser and generates additional cold source energy：
Δqc_d=βc·(hdn-hwc)=44.59464kJ/kg
Conversion condensing share Δ α can be calculated by formula (9)c：
Conversion condensing stream work done is calculated by formula (10),
Δwc=Δ αc·(h0-hc)=26.25302kJ/kg
(5), calculate backheat work done and compare Xr
Equivalent backheat steam flow work done is calculated by formula (11)：
Equivalent condensing stream work done is calculated by formula (12)：
Backheat work done ratio is calculated by formula (13)：
Obtain backheat ratio of profit increase：
The thermal efficiency η of the non-reheat backheat unit is acquired using heat Balance CalculationRGFor 0.41477, unit during no backheat Thermal efficiency ηRKFor 0.37056, calculate backheat ratio of profit increase exact value δ ηRGFor 0.10660.In tradition is calculated, without considering dredging When water cold source energy influences, X is compared in the backheat work done for calculating gainedrFor 0.19773, backheat ratio of profit increase δ ηRGFor 0.12446.It can be with Find out, traditional backheat ratio of profit increase results of measuring differs larger with exact value, the backheat that assay method provided by the present invention acquires Ratio of profit increase is identical with exact value, as a result accurately.

Claims (1)

  1. Backheat work done ratio and backheat ratio of profit increase assay method, the non-reheat when 1. a kind of non-reheat unit has hydrophobic cold source energy Unit has three-level steam extraction backheat, and the steam turbine of non-reheat unit is made of a cylinder, and three-level steam extraction number consecutively is the Level-one, the second level and third level steam extraction, and be connected respectively with the first order, the second level and third level heater, primary heater For surface heater, hydrophobic row is to second level heater, and second level heater is contact(-type) heater, third level heater For surface heater, drain discharge to condenser, when the non-reheat unit has hydrophobic cold source energy backheat work done ratio with The determination step of backheat ratio of profit increase is as follows：
    Step 1：Obtaining non-reheat unit has the equivalent backheat steam flow work done of hydrophobic cold source energyEquivalent condensing stream work done And dimensionless heat consumption rate HR of the non-reheat without extraction cycleRK,
    Step 2：According to：
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    <mrow> <msub> <mi>&amp;delta;&amp;eta;</mi> <mrow> <mi>R</mi> <mi>G</mi> </mrow> </msub> <mo>=</mo> <msub> <mi>X</mi> <mi>r</mi> </msub> <mo>&amp;CenterDot;</mo> <mrow> <mo>(</mo> <mn>1</mn> <mo>-</mo> <mfrac> <mn>1</mn> <mrow> <msub> <mi>HR</mi> <mrow> <mi>R</mi> <mi>K</mi> </mrow> </msub> </mrow> </mfrac> <mo>)</mo> </mrow> </mrow>
    X is compared in the backheat work done that determining non-reheat unit has hydrophobic cold source energyrAnd backheat ratio of profit increase δ ηRG；
    The equivalent backheat steam flow work doneEquivalent condensing stream work doneAcquisition methods it is as follows：
    Step 1：The calculating of therrmodynamic system carbonated drink parameter
    Step 1.1：It takes heat consumption to ensure under operating mode, System Turbine Relative Internal Efficiency ηri, j-th stage heater extraction line crushing rate δpjIn formula, j=1,2,3；
    Step 1.2：Obtain following data：Non-reheat unit main steam temperature t0With main steam pressure p0；Condenser pressure pwc；The Level-one extraction temperature t1With extraction pressure p1；Primary heater drain temperature td1, exit water temperature degree tw1With go out water pressure pw1； Second level extraction temperature t2With extraction pressure p2；Second level heater outlet coolant-temperature gage tw2With go out water pressure pw2；The third level is taken out Stripping temperature t3With extraction pressure p3；Third level heater condensate temperature td3, exit water temperature degree tw3With go out water pressure pw3；
    Step 1.3：By non-reheat unit main steam temperature t0With main steam pressure p0, according to international water and steam in 1997 The industrial properties of water and steam model that matter association proposes, is calculated main steam enthalpy h0And the entropy s of main steam0, It is correspondingly made available steam turbine constant entropy steam discharge entropy sc *=s0；Steam turbine exhaust pressure pcWith condenser pressure pwcIt is identical, by steam turbine Exhaust steam pressure pcWith constant entropy steam discharge entropy sc *, the industrial water and water that are proposed according to international water and steam property association in 1997 steam Constant entropy exhaust enthalpy h is calculated in vapour thermodynamic properties modelc *；By the System Turbine Relative Internal Efficiency η takenri, calculate to obtain actual row Vapour enthalpy hc=h0-ηri·(h0-hc *)；By condenser pressure pwc, proposed according to international water and steam property association in 1997 Condensation water enthalpy h is calculated in industrial properties of water and steam modelwc；
    By first order extraction temperature t1And pressure p1, according to the industrial water of international water and steam property association proposition in 1997 With water vapour thermodynamic properties model, first order steam extraction enthalpy h is calculated1；By first order extraction pressure p1And the first order taken Extraction line crushing rate δ p1, calculate the hydrophobic pressure p of primary heaterd1=p1·(1-δp1), by the hydrophobic temperature of primary heater Spend td1With hydrophobic pressure pd1, according to the industrial water and steam heating power of international water and steam property association proposition in 1997 The hydrophobic enthalpy h of primary heater is calculated in property modeld1；By primary heater exit water temperature degree tw1With outlet hydraulic pressure Power pw1, according to the industrial properties of water and steam model that international water and steam property association in 1997 proposes, calculate Obtain out saliva enthalpy hw1；
    By second level extraction temperature t2With extraction pressure p2, according to the industry of international water and steam property association proposition in 1997 With properties of water and steam model, second level steam extraction enthalpy h is calculated2；By second level heater outlet coolant-temperature gage tw2With Go out water pressure pw2, according to the industrial properties of water and steam mould of international water and steam property association proposition in 1997 Saliva enthalpy h is calculated out in typew2；
    By third level extraction temperature t3With extraction pressure p3, according to the industry of international water and steam property association proposition in 1997 With properties of water and steam model, third level steam extraction enthalpy h is calculated3；By third level extraction pressure p3And taken Three-level extraction line crushing rate δ p3, calculate third level heater condensate pressure pd3=p3·(1-δp3), it is dredged by third level heater Coolant-temperature gage td3With hydrophobic pressure pd3, according to the industrial water and steam of international water and steam property association proposition in 1997 Third level heater condensate enthalpy h is calculated in thermodynamic properties modeld3；By third level heater outlet coolant-temperature gage tw3And outlet Water pressure pw3, according to the industrial properties of water and steam model that international water and steam property association in 1997 proposes, Saliva enthalpy h is calculated outw3；
    Step 2：Calculate heater steam extraction share α at different levelsj, wherein, j=1,2,3, condensing fraction volume αc；
    Step 2.1：According to the thermal balance and flux balance equations of primary heater, the steam extraction share of primary heater is obtained：
    <mrow> <msub> <mi>&amp;alpha;</mi> <mn>1</mn> </msub> <mo>=</mo> <mfrac> <mrow> <mo>(</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>1</mn> </mrow> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>2</mn> </mrow> </msub> <mo>)</mo> </mrow> <mrow> <mi>h</mi> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>d</mi> <mn>1</mn> </mrow> </msub> </mrow> </mfrac> <mo>-</mo> <mo>-</mo> <mo>-</mo> <mrow> <mo>(</mo> <mn>1</mn> <mo>)</mo> </mrow> </mrow>
    According to the thermal balance and flux balance equations of second level heater, the steam extraction share of second level heater is obtained：
    <mrow> <msub> <mi>&amp;alpha;</mi> <mn>2</mn> </msub> <mo>=</mo> <mfrac> <mrow> <mo>(</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>2</mn> </mrow> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>3</mn> </mrow> </msub> <mo>)</mo> <mo>-</mo> <msub> <mi>&amp;alpha;</mi> <mn>1</mn> </msub> <mo>&amp;CenterDot;</mo> <mo>(</mo> <msub> <mi>h</mi> <mrow> <mi>d</mi> <mn>1</mn> </mrow> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>3</mn> </mrow> </msub> <mo>)</mo> </mrow> <mrow> <msub> <mi>h</mi> <mn>2</mn> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>3</mn> </mrow> </msub> </mrow> </mfrac> <mo>-</mo> <mo>-</mo> <mo>-</mo> <mrow> <mo>(</mo> <mn>2</mn> <mo>)</mo> </mrow> </mrow>
    According to the thermal balance and flux balance equations of third level heater, the steam extraction share of third level heater and hydrophobic part are obtained Volume：
    <mrow> <msub> <mi>&amp;alpha;</mi> <mn>3</mn> </msub> <mo>=</mo> <mfrac> <mrow> <mo>(</mo> <mn>1</mn> <mo>-</mo> <msub> <mi>&amp;alpha;</mi> <mn>1</mn> </msub> <mo>-</mo> <msub> <mi>&amp;alpha;</mi> <mn>2</mn> </msub> <mo>)</mo> <mo>&amp;CenterDot;</mo> <mo>(</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mn>3</mn> </mrow> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mi>c</mi> </mrow> </msub> <mo>)</mo> </mrow> <mrow> <msub> <mi>h</mi> <mn>3</mn> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>d</mi> <mn>3</mn> </mrow> </msub> </mrow> </mfrac> <mo>-</mo> <mo>-</mo> <mo>-</mo> <mrow> <mo>(</mo> <mn>3</mn> <mo>)</mo> </mrow> </mrow>
    βc=α3 (4)
    Step 2.2：Condensing fraction volume α can be obtained by mass balance equationc：
    αc=1- α1-α2-α3 (5)
    Step 3：Calculate backheat steam flow work done wr, condensing stream work done wc
    Backheat steam flow work done is：
    wr=α1·(h0-h1)+α2·(h0-h2)+α3·(h0-h3) (6)
    Condensing stream work done is：
    wc=αc·(h0-hc) (7)
    Step 4：Calculate conversion condensing stream amount of work Δ wc
    Third level heater condensate is can be calculated by heat flow diagrams be emitted into condenser generate additional cold source energy and be：
    Δqc_d=βc·(hdn-hwc) (8)
    In formula, hdnTo enter the hydrophobic enthalpy of condenser；
    Conversion condensing share Δ α can be calculated by (8) formulac：
    <mrow> <msub> <mi>&amp;Delta;&amp;alpha;</mi> <mi>c</mi> </msub> <mo>=</mo> <mfrac> <mrow> <msub> <mi>&amp;Delta;q</mi> <mrow> <mi>c</mi> <mo>_</mo> <mi>d</mi> </mrow> </msub> </mrow> <mrow> <msub> <mi>h</mi> <mi>c</mi> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mi>c</mi> </mrow> </msub> </mrow> </mfrac> <mo>-</mo> <mo>-</mo> <mo>-</mo> <mrow> <mo>(</mo> <mn>9</mn> <mo>)</mo> </mrow> </mrow>
    Conversion condensing stream amount of work is can be calculated by (9),
    Δwc=Δ αc·(h0-hc) (10)
    Step 5：It calculates backheat work done and compares Xr
    Equivalent backheat steam flow work done is：
    <mrow> <msubsup> <mi>w</mi> <mi>r</mi> <mrow> <mi>e</mi> <mi>q</mi> </mrow> </msubsup> <mo>=</mo> <msub> <mi>w</mi> <mi>r</mi> </msub> <mo>-</mo> <msub> <mi>&amp;Delta;w</mi> <mi>c</mi> </msub> <mo>-</mo> <mo>-</mo> <mo>-</mo> <mrow> <mo>(</mo> <mn>11</mn> <mo>)</mo> </mrow> </mrow>
    Equivalent condensing stream work done is：
    <mrow> <msubsup> <mi>w</mi> <mi>c</mi> <mrow> <mi>e</mi> <mi>q</mi> </mrow> </msubsup> <mo>=</mo> <msub> <mi>w</mi> <mi>c</mi> </msub> <mo>+</mo> <msub> <mi>&amp;Delta;w</mi> <mi>c</mi> </msub> <mo>-</mo> <mo>-</mo> <mo>-</mo> <mrow> <mo>(</mo> <mn>12</mn> <mo>)</mo> </mrow> </mrow>
    The dimensionless heat consumption rate HRRKAcquisition methods it is as follows：
    Step 16：It is defined according to heat consumption rate, obtains dimensionless heat consumption rate of the non-reheat without extraction cycle：
    <mrow> <msub> <mi>HR</mi> <mrow> <mi>R</mi> <mi>K</mi> </mrow> </msub> <mo>=</mo> <mfrac> <mrow> <mo>(</mo> <msub> <mi>h</mi> <mn>0</mn> </msub> <mo>-</mo> <msub> <mi>h</mi> <mrow> <mi>w</mi> <mi>c</mi> </mrow> </msub> <mo>)</mo> </mrow> <mrow> <mo>(</mo> <msub> <mi>h</mi> <mn>0</mn> </msub> <mo>-</mo> <msub> <mi>h</mi> <mi>c</mi> </msub> <mo>)</mo> </mrow> </mfrac> </mrow>
    Wherein, h0For main steam enthalpy, hwcFor condensation water enthalpy, hcFor actual steam discharge enthalpy.
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