CN104484568B - Backheat work done ratio and backheat ratio of profit increase assay method during non-reheat unit having heaters radiation loss - Google Patents
Backheat work done ratio and backheat ratio of profit increase assay method during non-reheat unit having heaters radiation loss Download PDFInfo
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Abstract
The invention discloses backheat work done ratios during a kind of non-reheat unit having heaters radiation loss and backheat ratio of profit increase assay method, 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 respectively with the first order, the second level is connected with third level heater, primary heater is surface heater, its hydrophobic row is to second level heater, second level heater is contact(-type) heater, third level heater is surface heater, its hydrophobic row is to condenser hotwell, backheat work done is as follows than with the determination step of backheat ratio of profit increase during non-reheat unit having heaters radiation loss：Obtain dimensionless heat consumption rate of the reheating without extraction cycle, equivalent backheat steam flow work done and equivalent condensing stream work done；Determine backheat work done ratio and backheat ratio of profit increase during non-reheat unit having heaters radiation loss.Assay method of the present invention realizes hard measurement of the backheat work done than the high-precision low cost with backheat ratio of profit increase.
Description
Technical field
Backheat work done when backheat ratio of profit increase when being directed to non-reheat unit having heaters radiation loss the present invention relates to one kind
Assay method, the measure of backheat work done when backheat ratio of profit increase when can realize non-reheat unit having heaters radiation loss,
Belong to hard measurement field.
Background technology
The extraction cycle being made of heater is the important component of reheating embrittlement, and backheat effect is to influence reheating embrittlement
One of principal element of the thermal 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 that the work done of backheat steam flow is shared in steam turbine internal strength (the sum of the work done of backheat steam flow and condensing stream work done)
Ratio, backheat ratio of profit increase refer to efficiency relative growth rate of the backheat compared to no backheat.Backheat work done ratio is bigger, backheat ratio of profit increase
Bigger, 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 when heater heat-insulating property is bad,
Heater radiation loss can be generated, cause traditional backheat work done when backheat ratio of profit increase measuring method failure.
The content of the invention
It is an object of the invention to provide backheat work done ratio during a kind of non-reheat unit having heaters radiation loss and backheats
The assay method of ratio of profit increase, backheat work done when backheat ratio of profit increase when can realize non-reheat unit having heaters radiation loss
In high precision, inexpensive hard measurement.
The present invention realizes by following technical solution：
Backheat work done ratio and backheat ratio of profit increase assay method, described non-during a kind of non-reheat unit having heaters radiation loss
Reheating embrittlement is made of a cylinder, three-level steam extraction number consecutively be the first order, the second level and third level steam extraction, and respectively with
The first order, the second level are connected with third level heater, and primary heater is surface heater, and hydrophobic row adds to the second level
Hot device, second level heater are contact(-type) heater, and third level heater is surface heater, and hydrophobic row is hot to condenser
Well, which is characterized in that backheat work done with the measure of backheat ratio of profit increase than walking during the non-reheat unit having heaters radiation loss
It is rapid as follows：
Step 1：Obtain dimensionless heat consumption rate HR of the reheating without extraction cycleRK, equivalent backheat steam flow work doneIt is coagulated with equivalent
Steam flow work done
Step 2：According to：
Determine backheat work done ratio and backheat ratio of profit increase during non-reheat unit having heaters radiation loss.
The equivalent backheat steam flow work doneWith equivalent 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), j-th stage heater usage factor ηj；
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；Low pressure (LP) cylinder exhaust steam 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 is obtained,
Step 2.2：Condensing fraction volume α can be obtained by mass balance equationc,
αc=1- α1-α2-α3 (4)
Step 3：Calculate backheat air-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) (5)
Condensing stream work done is,
wc=αc·(h0-hc) (6)
Step 4：Calculate conversion condensing stream amount of work Δ wc
The radiation loss that primary heater generates：
The radiation loss that second level heater generates：
The radiation loss that third level heater generates：
Conversion condensing share Δ α is can be calculated by (7) (8) (9)c,
Conversion condensing stream amount of work is can be calculated by (10),
Δwc=Δ αc·(h0-hc) (11)
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 reheating without extraction cycle：
Wherein, h0For main steam enthalpy, hwcFor condensation water enthalpy, hcFor actual steam discharge enthalpy.
Assuming that during non-reheat unit having heaters radiation loss, the series of regenerative steam is n, and j-th stage heater goes out
Water proportion is Aj, the feed-water enthalpy rise of j-th stage heater is τj, j-th stage heater usage factor is ηj, 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。
Heater generate radiation loss be：
Heater radiation loss conversion condensing share be：
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 non-reheat unit having heaters radiation loss, additional 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 hard measurement of the backheat work done than the high-precision low cost with backheat ratio of profit increase.(2) originally
The backheat work done proposed is invented than the assay method with backheat ratio of profit increase, the result of calculation checked with heat balance method is complete
Unanimously.
Description of the drawings
Fig. 1 is the non-reheat backheat steam turbine structure figure that the present invention uses.
Fig. 2 is the calculation process schematic diagram of assay method of the present invention.
Specific embodiment
Backheat work done ratio and backheat ratio of profit increase assay method, calculate during a kind of non-reheat unit having heaters radiation loss
Model is the non-reheat unit for having three-level backheat for one.The steam turbine is made of a cylinder, and three-level steam extraction is successively
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 heater
For surface heater, hydrophobic row is to the 2nd grade of heater, and the 2nd grade of heater is contact(-type) heater, and 3rd level heater is
Surface heater, hydrophobic row is to condenser hotwell.
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), j-th stage heater usage factor ηj。
Step 1.2：From the database of SIS in Thermal Power PlantQ SIS or distributed monitoring control system, obtain such as
Lower data：Non-reheat unit main steam temperature t0With main steam pressure p0；Condenser pressure pwc；1st grade of extraction temperature t1And steam 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 t2And steam 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
Grade 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.Low pressure (LP) cylinder steam 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 classical IAPWS-IF97, saliva enthalpy is calculated out
hw2。
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, steam extraction part of the 1st grade of heater is obtained
Volume,
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 is obtained,
Step 2.2：Condensing fraction volume α can be obtained by mass balance equationc,
αc=1- α1-α2-α3 (4)
Step 3：Calculate backheat air-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) (5)
Condensing stream work done is,
wc=αc·(h0-hc) (6)
Step 4：Calculate conversion condensing stream amount of work Δ wc
The radiation loss that 1st grade of heater generates：
The radiation loss that 2nd grade of heater generates：
The radiation loss that 3rd level heater generates：
Conversion condensing share Δ α is can be calculated by (7) (8) (9)c,
Conversion condensing stream amount of work is can be calculated by (10),
Δwc=Δ αc·(h0-hc) (11)
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 is can be calculated by (12) (13)：
Step 6：Calculate backheat ratio of profit increase δ ηRG
By taking unit shown in scheming as an example, computation model be one have three-level steam extraction backheat non-reheat unit heat device by
Number is 1~3 to its extraction pressure respectively from high to low, and the 1st grade of heater is surface heater, and the 2nd grade of heater is mixing
Formula heater, 3rd level heater are surface heater.
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%；
J-th stage heater usage factor ηjFor 0.98；
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；
Exhaust enthalpy of turbine hcFor 2207.697kJ/kg；
Condensation water enthalpy hwcFor 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),
Condensing fraction volume is calculated to obtain by formula (4),
(3), backheat air-flow work done w is calculatedr, condensing stream work done wc
Backheat air-flow work done is calculated to obtain by formula (5),
wr=α1·(h0-h1)+α2·(h0-h2)+α3·(h0-h3)=171.20712kJ/kg
Air-flow work done must be coagulated by being calculated by formula (6),
wc=αc·(h0-hc)=756.01849kJ/kg
(4), conversion condensing stream amount of work Δ w is calculatedc
The radiation loss that generates of 1st grade of heater is calculated to obtain by formula (7)：
The radiation loss that generates of 2nd grade of heater is calculated to obtain by formula (8)：
By formula (9) calculate 3rd level heater generate radiation loss：
Conversion condensing share Δ α can be calculated by formula (10)c,
Conversion condensing stream work done is calculated by formula (11),
Δwc=Δ αc·(h0-hc)=11.53808kJ/kg
(5) calculate backheat work done and compare xr
Equivalent backheat air-flow work done is calculated by formula (12)：
Equivalent solidifying air-flow work done is calculated by formula (13)：
Backheat work done ratio is calculated by formula (14)：
Obtain backheat ratio of profit increase：
The thermal efficiency η of the non-reheat backheat unit is acquired using heat Balance CalculationRGFor 0.41560, unit during no backheat
Thermal efficiency ηRKFor 0.37056, calculate backheat ratio of profit increase exact value δ ηRGFor 0.10839.In tradition is calculated, without considering adding
When hot device radiation loss influences, X is compared in the backheat work done for calculating gainedrFor 0.18464, backheat ratio of profit increase δ ηRGFor 0.11622.It can
To find out, traditional backheat ratio of profit increase results of measuring differs larger with exact value, and what assay method provided by the present invention acquired returns
Hot thermal efficiency gain is identical with exact value, as a result accurately.
Claims (1)
1. backheat work done ratio and backheat ratio of profit increase assay method during a kind of non-reheat unit having heaters radiation loss, it is described it is non-again
Heat engine group 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 respectively with the
Level-one, the second level are connected with third level heater, and primary heater is surface heater, and hydrophobic row heats to the second level
Device, second level heater are contact(-type) heater, and third level heater is surface heater, and hydrophobic row is hot to condenser
Well, which is characterized in that backheat work done with the measure of backheat ratio of profit increase than walking during the non-reheat unit having heaters radiation loss
It is rapid as follows：
Step 1：Obtain dimensionless heat consumption rate HR of the reheating without extraction cycleRK, equivalent backheat steam flow work doneWith equivalent condensing stream
Work done
Step 2：According to：
Determine backheat work done ratio and backheat ratio of profit increase during non-reheat unit having heaters radiation loss；
The equivalent backheat steam flow work doneWith equivalent 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
δpj, wherein, j=1,2,3, j-th stage heater usage factor ηj；
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；Low pressure (LP) cylinder exhaust steam 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,
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 is obtained,
Step 2.2：Condensing fraction volume α can be obtained by mass balance equationc,
αc=1- α1-α2-α3 (4)
Step 3：Calculate backheat air-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) (5)
Condensing stream work done is,
wc=αc·(h0-hc) (6)
Step 4：Calculate conversion condensing stream amount of work Δ wc
The radiation loss that primary heater generates：
The radiation loss that second level heater generates：
The radiation loss that third level heater generates：
In formula, τ1For the feed-water enthalpy rise of the 1st grade of heater；τ2For the feed-water enthalpy rise of the 2nd grade of heater；τ3For 3rd level heater
Feed-water enthalpy rise；
Conversion condensing share Δ α is can be calculated by (7) (8) (9)c,
Conversion condensing stream amount of work is can be calculated by (10),
Δwc=Δ αc·(h0-hc) (11)
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 reheating without extraction cycle：
Wherein, h0For main steam enthalpy, hwcFor condensation water enthalpy, hcFor actual steam discharge enthalpy, σ recepts the caloric for reheater.
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