CN104636593B - Backheat work done ratio and backheat ratio of profit increase assay method during reheating embrittlement having heaters radiation loss - Google Patents
Backheat work done ratio and backheat ratio of profit increase assay method during reheating embrittlement having heaters radiation loss Download PDFInfo
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Abstract
The invention discloses backheat work done ratio during a kind of reheating embrittlement having heaters radiation loss and backheat ratio of profit increase assay method, there is the reheating embrittlement three-level to draw gas backheat, and the steam turbine of reheating embrittlement is made up of high pressure cylinder, intermediate pressure cylinder and low pressure (LP) cylinder；High pressure cylinder steam discharge is in addition to the heating as primary heater is drawn gas, remaining reheated device enters intermediate pressure cylinder, intermediate pressure cylinder steam discharge as the second level in addition to drawing gas, and remainder enters low pressure (LP) cylinder, and backheat work done is as follows than with the determination step of backheat ratio of profit increase during the reheating embrittlement having heaters radiation loss：Obtain equivalent backheat steam flow work done, the dimensionless heat consumption rate of equivalent condensing stream work done and reheating without extraction cycle of reheating embrittlement having heaters radiation loss；Determine the backheat work done of reheating embrittlement having heaters radiation loss when backheat ratio of profit increase.Backheat work done of the present invention realizes backheat work done than high-precision, the inexpensive hard measurement with backheat ratio of profit increase than the assay method with backheat ratio of profit increase.
Description
Technical field
The present invention relates to it is a kind of be directed to reheating embrittlement having heaters radiation loss when backheat work done when backheat ratio of profit increase
Assay method, it is possible to achieve the measure of backheat work done when backheat ratio of profit increase during reheating embrittlement having heaters radiation loss, belongs to
Hard measurement field.
Background technology
The extraction cycle being made up of heater is the important component of reheating embrittlement, and backheat effect is 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 (work done of backheat steam flow with condensing stream work done sum)
Ratio, backheat ratio of profit increase refers to backheat compared to the efficiency relative growth rate without backheat.Backheat work done is than 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
Circulation, 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 produced, cause traditional backheat work done when backheat ratio of profit increase measuring method failure.
The content of the invention
Increase it is an object of the invention to provide backheat work done ratio during a kind of reheating embrittlement having heaters radiation loss and backheat
The assay method of beneficial rate, backheat work done when backheat ratio of profit increase is high-precision when can realize reheating embrittlement having heaters radiation loss
Degree, inexpensive hard measurement.
The present invention is realized by following technical solution：
Backheat work done ratio and backheat ratio of profit increase assay method, the reheating during a kind of reheating embrittlement having heaters radiation loss
There is unit three-level to draw gas backheat, and the steam turbine of reheating embrittlement is made up of high pressure cylinder, intermediate pressure cylinder and low pressure (LP) cylinder；High pressure cylinder steam discharge,
Intermediate pressure cylinder steam discharge and low pressure (LP) cylinder number consecutively of drawing gas are drawn gas for the first order, the second level and the third level, and respectively with the first order, second
Level is connected with third level heater, and primary heater is surface heater, and its hydrophobic row is to second level heater, the second level
Heater is contact(-type) heater, and third level heater is surface heater, and its hydrophobic row is to condenser hotwell；High pressure cylinder is arranged
Vapour is in addition to the heating as primary heater is drawn gas, and remaining reheated device enters intermediate pressure cylinder, and intermediate pressure cylinder steam discharge, which is removed, is used as second
Outside level is drawn gas, remainder enters low pressure (LP) cylinder, it is characterised in that：Backheat work done during the reheating embrittlement having heaters radiation loss
It is as follows than with the determination step of backheat ratio of profit increase：
Step 1：Obtain the equivalent backheat steam flow work done of reheating embrittlement having heaters radiation lossEquivalent condensing stream is made
Work(And dimensionless heat consumption rate HR of the reheating without extraction cycleRK,
Step 2：According to：
Determine that X is compared in the backheat work done of reheating embrittlement having heaters radiation lossrAnd backheat ratio of profit increase δ ηRG。
The equivalent backheat steam flow work done of the reheating embrittlement having heaters radiation lossEquivalent condensing stream work done's
Acquisition methods are as follows：
Step 1：The calculating of therrmodynamic system carbonated drink parameter
Step 1.1：Take heat consumption to ensure under operating mode, low pressure (LP) cylinder internal efficiency ratio ηLP, 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：Reheating embrittlement main steam temperature t0With main steam pressure p0；Exhaust temperature of HP
thcWith exhaust steam pressure phc；Reheat steam temperature trWith reheated steam pressure pr；Low pressure (LP) cylinder throttle (steam) temperature tlEnter vapour pressure with low pressure (LP) cylinder
Power pl；Condenser pressure pwc；First order extraction temperature t1With extraction pressure p1；Primary heater drain temperature td1, go out saliva
Temperature 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；Third level extraction temperature t3With extraction pressure p3；Third level heater condensate temperature td3, exit water temperature degree tw3
With go out water pressure pw3；
Step 1.3：By reheating embrittlement 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 property association proposes, calculating obtains main steam enthalpy h0；By high pressure cylinder steam discharge
Temperature thcWith exhaust steam pressure phc, the industrial water and steam heat proposed according to international water and steam property association in 1997
Power property model, calculating obtains exhaust enthalpy value hhc；By reheat steam temperature trWith reheated steam pressure pr, according to the world in 1997
The industrial properties of water and steam model that water and steam property association proposes, calculating obtains reheated steam hr；By low
Cylinder pressure throttle (steam) temperature tlWith initial steam pressure pl, the industrial water and water proposed according to international water and steam property association in 1997
Steam thermodynamic properties model, calculating obtains low pressure (LP) cylinder steam admission enthalpy hlEnter the entropy s of vapour with low pressure (LP) cylinderl, it is correspondingly made available low pressure (LP) cylinder constant entropy
Steam discharge entropy sc *=sl；Low pressure (LP) cylinder exhaust steam pressure pcWith condenser pressure pwcIt is identical, by low pressure (LP) cylinder exhaust steam pressure pcWith constant entropy steam discharge
Entropy sc *, the industrial properties of water and steam model proposed according to international water and steam property association in 1997, calculating
Obtain constant entropy exhaust enthalpy hc *；By the low pressure (LP) cylinder internal efficiency ratio η takenLP, calculate actual exhaust enthalpy hc=hr-ηLP·(hr-
hc *)；By condenser pressure pwc, the industrial water and steam heat proposed according to international water and steam property association in 1997
Power property model, calculating obtains condensate enthalpy hwc；
By first order extraction temperature t1And pressure p1, the industry proposed according to international water and steam property association in 1997
Use properties of water and steam model, calculating obtains the first order and drawn gas enthalpy h1；By first order extraction pressure p1And taken
One-level extraction line crushing rate δ p1, calculate the hydrophobic pressure p of primary heaterd1=p1·(1-δp1), dredged by primary heater
Coolant-temperature gage td1With hydrophobic pressure pd1, the industrial water and steam proposed according to international water and steam property association in 1997
Thermodynamic properties model, calculating obtains the hydrophobic enthalpy h of primary heaterd1；By primary heater exit water temperature degree tw1And outlet
Water pressure pw1, the industrial properties of water and steam model proposed according to international water and steam property association in 1997,
Calculating obtains outlet water enthalpy hw1；
By second level extraction temperature t2With extraction pressure p2, proposed according to international water and steam property association in 1997
Industrial properties of water and steam model, the second level must be arrived and draw gas enthalpy h by calculating2；By second level heater outlet coolant-temperature gage
tw2With go out water pressure pw2, the industrial water and steam heating power proposed according to international water and steam property association in 1997
Property model, calculating obtains outlet water enthalpy hw2；
By third level extraction temperature t3With extraction pressure p3, proposed according to international water and steam property association in 1997
Industrial properties of water and steam model, calculating obtains the third level and drawn gas enthalpy h3；By third level extraction pressure p3And take
Third level extraction line crushing rate δ p3, calculate third level heater condensate pressure pd3=p3·(1-δp3), heated by the third level
Device drain temperature td3With hydrophobic pressure pd3, the industrial water and water proposed according to international water and steam property association in 1997
Steam thermodynamic properties model, calculating obtains third level heater condensate enthalpy hd3；By third level heater outlet coolant-temperature gage tw3With
Go out water pressure pw3, the industrial properties of water and steam mould proposed according to international water and steam property association in 1997
Type, calculating obtains outlet water enthalpy hw3；
Step 2：Heaters at different levels are calculated to draw gas share αj(j=1,2,3), condensing stream part volume αc
Step 2.1：According to the thermal balance and flux balance equations of primary heater, part of drawing gas of primary heater is obtained
Volume,
According to the thermal balance and flux balance equations of second level heater, the share of drawing gas of second level heater is obtained,
According to the thermal balance and flux balance equations of third level heater, the share of drawing gas of third level heater is obtained,
Step 2.2：Condensing stream part volume α can be obtained by mass balance equationc,
αc=1- α1-α2-α3 (4)
Step 3：Calculate backheat steam flow work done wr, condensing stream work done wc
Unit share reheated steam recepts the caloric σ=h in reheaterr-h1；
Backheat steam flow work done is,
wr=α1·(h0-h1)+α2·(h0-h2-σ)+α3·(h0-h3-σ) (5)
Condensing stream work done is,
wc=αc·(h0-hc+σ) (6)
Step 4：Calculate conversion condensing stream amount of work Δ wc
The radiation loss that primary heater is produced,
The radiation loss that second level heater is produced,
The radiation loss that third level heater is produced,
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+σ) (11)
Step 5：Calculate backheat work done and compare 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：
Defined according to heat consumption rate, obtain dimensionless heat consumption rate of the reheating without extraction cycle：
Wherein, h0For main steam enthalpy, hwcFor condensate enthalpy, hcFor the actual steam discharge enthalpy of low pressure (LP) cylinder, σ inhales for reheater
Heat, σ=hr-hhc, hhcFor high pressure cylinder steam discharge enthalpy, hrFor reheated steam enthalpy.
Assuming that during reheating embrittlement having heaters radiation loss, the series of its regenerative steam is n, the water outlet of j-th stage heater
Share 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, reheating vapour enthalpy
For hr, it is σ that unit share reheated steam recepts the caloric in reheater, and low pressure (LP) cylinder exhaust enthalpy is hc, it is h that condenser, which goes out saliva enthalpy,wc,
J-th stage, which is drawn gas, share and draws gas work done enthalpy drop respectively αjAnd Hj, condensing stream part volume and condensing stream work done enthalpy drop are respectively αcWith
Hc。
Heater produce radiation loss be：
Heater radiation loss conversion condensing share be：
The conversion condensing stream amount of work of the additional cold source energy is：
Δwc=Δ αc·(h0-hc+σ) (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, and it is defined as：
In formula, ηRGFor the thermal efficiency of reheating backheat unit, ηRKThe thermal efficiency of unit during for without backheat.
By defining for heat consumption rate：
HRRG=HRRK-Xr·(HRRK-1) (10)
In formula, HRRGFor the dimensionless heat consumption rate of backheat unit, HRRKThe dimensionless heat consumption rate of unit during for without backheat,
Formula (10), (11), (12) substitution formula (9) are calculated backheat ratio of profit increase and be：
The advantage of the invention is that：
(1) when heater heat-insulating property is bad, heater radiation loss can be produced.Traditional backheat work done when backheat
Ratio of profit increase measuring method does not consider above-mentioned shadow due to being calculated according only to backheat work done than the definition with backheat ratio of profit increase
Ring, cause its results of measuring mistake.Above-mentioned influence is not considered, causes its results of measuring mistake.The present invention combine above-mentioned influence because
Element, proposes that a kind of new backheat work done, than the assay method with backheat ratio of profit increase, realizes backheat work done ratio and backheat ratio of profit increase
High-precision, inexpensive hard measurement；(2) backheat work done proposed by the invention is than the assay method with backheat ratio of profit increase, with
The result of calculation that heat balance method checking computations are obtained is completely the same.
Brief description of the drawings
Fig. 1 is the heat flow diagrams with three-level regenerative steam；
Fig. 2 is calculation flow chart of the invention.
Embodiment
Backheat work done ratio and backheat ratio of profit increase assay method during a kind of reheating embrittlement having heaters radiation loss, it calculates mould
Type is the reheating embrittlement for a backheat of being drawn gas with three-level.The steam turbine is made up of high pressure cylinder, intermediate pressure cylinder and low pressure (LP) cylinder；It is high
Cylinder pressure steam discharge, intermediate pressure cylinder steam discharge and low pressure (LP) cylinder number consecutively of drawing gas are drawn gas for the 1st grade, the 2nd grade and 3rd level, and respectively with the 1st
Level, the 2nd grade be connected with 3rd level heater, the 1st grade of heater is surface heater, and its hydrophobic row is to the 2nd grade of heater, the 2nd
Level heater is contact(-type) heater, and 3rd level heater is surface heater, and its hydrophobic row is to condenser hotwell；High pressure cylinder
Steam discharge is in addition to the heating as the 1st grade of heater is drawn gas, and remaining reheated device enters intermediate pressure cylinder, and intermediate pressure cylinder steam discharge, which is removed, is used as the 2nd
Outside level is drawn gas, remainder enters low pressure (LP) cylinder.Determination step is as follows,
Step 1：The calculating of therrmodynamic system carbonated drink parameter
Step 1.1：Take under THA (Turbine Heat Acceptance, heat consumption ensures operating mode), low pressure (LP) cylinder is relatively interior
Efficiency etaLP, 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 SIS in Thermal Power PlantQ (SIS) or the database of scattered control system (DCS), obtain
Take following data：Reheating embrittlement main steam temperature t0With main steam pressure p0；Exhaust temperature of HP thcWith exhaust steam pressure phc；Again
Vapours temperature trWith reheated steam pressure pr；Low pressure (LP) cylinder throttle (steam) temperature tlWith low pressure (LP) cylinder initial steam pressure pl；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 draws gas temperature
Spend t3With extraction pressure p3；3rd level heater condensate temperature td3, exit water temperature degree tw3With go out water pressure pw3；
Step 1.3：By reheating embrittlement main steam temperature t0With main steam pressure p0, according to international water and steam in 1997
The industrial properties of water and steam model IAPWS-IF97 (hereinafter referred to as IAPWS-IF97) that property association proposes, calculates
Obtain main steam enthalpy h0；By exhaust temperature of HP thcWith exhaust steam pressure phc, according to IAPWS-IF97, calculating obtains exhaust enthalpy
Value hhc；By reheat steam temperature trWith reheated steam pressure pr, according to IAPWS-IF97, calculating obtains reheated steam hr.By low pressure
Cylinder throttle (steam) temperature tlWith initial steam pressure pl, according to IAPWS-IF97, calculating obtains low pressure (LP) cylinder steam admission enthalpy hlEnter the entropy of vapour with low pressure (LP) cylinder
sl, it is correspondingly made available low pressure (LP) cylinder constant entropy steam discharge entropy sc *=sl.Low pressure (LP) cylinder exhaust steam pressure pcWith condenser pressure pwcIt is identical, by low pressure
Cylinder exhaust steam pressure pcWith constant entropy steam discharge entropy sc *, according to IAPWS-IF97, calculating obtains constant entropy exhaust enthalpy hc *.By the low pressure (LP) cylinder taken
Internal efficiency ratio ηLP, calculate actual exhaust enthalpy hc=hr-ηLP·(hr-hc *)；By condenser pressure pwc, according to IAPWS-
IF97, calculating obtains condensate enthalpy hwc。
By the 1st grade of extraction temperature t1And pressure p1, according to IAPWS-IF97, calculating obtains the 1st grade of enthalpy h that draws gas1；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, calculating obtains the 1st grade of heater and dredged
Water enthalpy hd1；By the 1st grade of heater outlet coolant-temperature gage tw1With go out water pressure pw1, according to IAPWS-IF97, calculating is exported
Water enthalpy hw1。
By the 2nd grade of extraction temperature t2With extraction pressure p2, according to IAPWS-IF97, calculating obtains the 2nd grade of enthalpy h that draws gas2；By
2nd grade of heater outlet coolant-temperature gage tw2With go out water pressure pw2, according to IAPWS-IF97, calculating obtains outlet water enthalpy hw2。
By 3rd level extraction temperature t3With extraction pressure p3, according to IAPWS-IF97, calculating obtains 3rd level and drawn gas enthalpy h3；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, calculating obtains 3rd level
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：Heaters at different levels are calculated to draw gas share αj(j=1,2,3), condensing stream part volume αc
Step 2.1：According to the thermal balance and flux balance equations of the 1st grade of heater, part of drawing gas 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 share of drawing gas of the 2nd grade of heater is obtained,
According to the thermal balance and flux balance equations of 3rd level heater, the share of drawing gas of 3rd level heater is obtained,
Step 2.2：Condensing stream part volume α can be obtained by mass balance equationc,
αc=1- α1-α2-α3 (4)
Step 3：Calculate backheat steam flow work done wr, condensing stream work done wc
Unit share reheated steam recepts the caloric σ=h in reheaterr-h1。
Backheat steam flow work done is,
wr=α1·(h0-h1)+α2·(h0-h2-σ)+α3·(h0-h3-σ) (5)
Condensing stream work done is,
wc=αc·(h0-hc+ σ) (6) step 4：Calculate conversion condensing stream amount of work Δ wc
The radiation loss that 1st grade of heater is produced,
The radiation loss that 2nd grade of heater is produced,
The radiation loss that 3rd level heater is produced,
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+σ) (11)
Step 5：Calculate backheat work done and compare 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 Fig. 1 as an example, its computation model is the reheating embrittlement of a backheat of being drawn gas with three-level, steam turbine portion
Divide and be made up of high pressure cylinder, intermediate pressure cylinder and low pressure (LP) cylinder, numbering is 1~3 to heater respectively from high to low by its extraction pressure, the 1st grade
Heater is surface heater, and the 2nd grade of heater is contact(-type) heater, and 3rd level heater is surface heater.
Detailed calculation procedure is as follows：
(1), low pressure (LP) cylinder internal efficiency ratio ηLPFor 0.84；
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 plant level supervisory information system (SIS) real-time data base, reading it is main in real time
Data are as follows：
Main steam temperature t0For 535 DEG C；
Main steam pressure p0For 13.5MPa；
Exhaust temperature of HP thcFor 415.2 DEG C；
High pressure cylinder exhaust steam pressure phcFor 6.080MPa；
Reheat steam temperature trFor 535 DEG C；
Reheated steam pressure prFor 5.594MPa；
Low pressure (LP) cylinder throttle (steam) temperature tlFor 359.9 DEG C；
Low pressure (LP) cylinder initial steam pressure plFor 1.6MPa；
Low pressure (LP) cylinder exhaust steam pressure pcFor 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 359.9 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 152.7 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 IAPWS-IF97 and computation model：
Main steam enthalpy h0For 3426.274kJ/kg；
High pressure cylinder exhaust enthalpy hhcFor 3215.414kJ/kg；
Reheated steam enthalpy hrFor 3509.948kJ/kg；
Low pressure (LP) cylinder exhaust enthalpy hcFor 2327.895kJ/kg；
Condensate enthalpy hwcFor 137.765kJ/kg；
The 1st grade of enthalpy h that draws gas1For 3215.414kJ/kg；
1st grade of heater condensate enthalpy hd1For 1207.950kJ/kg；
1st grade of heater outlet water enthalpy hw1For 1195.240kJ/kg；
The 2nd grade of enthalpy h that draws gas2For 3167.643kJ/kg；
2nd grade of heater outlet water enthalpy hw2For 852.023kJ/kg；
3rd level draws gas enthalpy h3For 2774.591kJ/kg；
3rd level heater condensate enthalpy hd3For 500.602kJ/kg；
3rd level heater outlet water enthalpy hw3For 493.080kJ/kg；
(2) each heater, is calculated to draw gas share αj(j=1,2,3), condensing stream part volume αc
The 1st grade of heater is calculated by formula (1) to draw gas share：
The 2nd grade of heater is calculated by formula (2) to draw gas share：
3rd level heater is calculated by formula (3) to draw gas share：
Condensing stream part volume is calculated by formula (4)：
(3) backheat steam flow work done w, is calculatedr, condensing stream work done wc
Backheat steam flow work done is calculated by formula (5)：
wr=α1·(h0-h1)+α2·(h0-h2+σ)+α3·(h0-h3+ σ)=182.40250kJ/kg
Condensing stream work done is calculated by formula (6)：
wc=αc·(h0-hc+ σ)=883.28947kJ/kg
(4) conversion condensing stream amount of work Δ w, is calculatedc
The radiation loss that 1st grade of heater is produced is calculated by formula (7)：
The radiation loss that 2nd grade of heater is produced is calculated by formula (8)：
The radiation loss of 3rd level heater generation is calculated by formula (9)：
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+ σ)=12.50440kJ/kg
(5), calculate backheat work done and compare xr
Equivalent backheat steam flow work done is calculated by formula (12)：
Equivalent condensing stream 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 reheating backheat unit is tried to achieve using heat Balance CalculationRGFor 0.43072, the heat of unit during no backheat
Efficiency etaRKFor 0.38875, the exact value δ η of backheat ratio of profit increase are calculatedRGFor 0.09745.In tradition measuring and calculating, heating is not considered
When device radiation loss influences, X is compared in the backheat work done obtained by calculatingrFor 0.20650, backheat ratio of profit increase δ ηRGFor 0.12623.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 is tried to achieve
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 heat engine again during a kind of reheating embrittlement having heaters radiation loss
There is group three-level to draw gas backheat, and the steam turbine of reheating embrittlement is made up of high pressure cylinder, intermediate pressure cylinder and low pressure (LP) cylinder；High pressure cylinder steam discharge, in
Cylinder pressure steam discharge and low pressure (LP) cylinder number consecutively of drawing gas are drawn gas for the first order, the second level and the third level, and respectively with the first order, the second level
It is connected with third level heater, primary heater is surface heater, its hydrophobic row is to second level heater, and the second level adds
Hot device is contact(-type) heater, and third level heater is surface heater, and its hydrophobic row is to condenser hotwell；High pressure cylinder steam discharge
In addition to the heating as primary heater is drawn gas, remaining reheated device enters intermediate pressure cylinder, and intermediate pressure cylinder steam discharge, which is removed, is used as the second level
Draw gas outer, remainder enters low pressure (LP) cylinder, it is characterised in that：Backheat work done ratio during the reheating embrittlement having heaters radiation loss
Determination step with backheat ratio of profit increase is as follows：
Step 1：Obtain the equivalent backheat steam flow work done of reheating embrittlement having heaters radiation lossEquivalent condensing stream work done
And dimensionless heat consumption rate HR of the reheating without extraction cycleRK,
Step 2：According to：
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Determine that X is compared in the backheat work done of reheating embrittlement having heaters radiation lossrAnd backheat ratio of profit increase δ ηRG；
The equivalent backheat steam flow work done of the reheating embrittlement having heaters radiation lossEquivalent condensing stream work doneAcquisition
Method is as follows：
Step 1：The calculating of therrmodynamic system carbonated drink parameter
Step 1.1：Take heat consumption to ensure under operating mode, low pressure (LP) cylinder internal efficiency ratio ηLP, j-th stage heater extraction line crushing rate
δpj(j=1,2,3), j-th stage heater usage factor ηj；
Step 1.2：Obtain following data：Reheating embrittlement main steam temperature t0With main steam pressure p0；Exhaust temperature of HP thcWith
Exhaust steam pressure phc；Reheat steam temperature trWith reheated steam pressure pr；Low pressure (LP) cylinder throttle (steam) temperature tlWith low pressure (LP) cylinder initial steam pressure pl；
Condenser pressure pwc；First order extraction temperature t1With extraction pressure p1；Primary heater drain temperature td1, exit water temperature degree tw1
With go out water pressure pw1；Second level extraction temperature t2With extraction pressure p2；Second level heater outlet coolant-temperature gage tw2With go out saliva
Pressure pw2；Third level extraction temperature t3With extraction pressure p3；Third level heater condensate temperature td3, exit water temperature degree tw3And outlet
Water pressure pw3；
Step 1.3：By reheating embrittlement main steam temperature t0With main steam pressure p0, according to international water and steam property in 1997
The industrial properties of water and steam model that association proposes, calculating obtains main steam enthalpy h0；By exhaust temperature of HP
thcWith exhaust steam pressure phc, the industrial water and steam heating power proposed according to international water and steam property association in 1997
Matter model, calculating obtains exhaust enthalpy value hhc；By reheat steam temperature trWith reheated steam pressure pr, according to international water in 1997 and
The industrial properties of water and steam model that steam properties association proposes, calculating obtains reheated steam hr；By low pressure (LP) cylinder
Throttle (steam) temperature tlWith initial steam pressure pl, the industrial water and steam proposed according to international water and steam property association in 1997
Thermodynamic properties model, calculating obtains low pressure (LP) cylinder steam admission enthalpy hlEnter the entropy s of vapour with low pressure (LP) cylinderl, it is correspondingly made available low pressure (LP) cylinder constant entropy steam discharge
Entropy sc *=sl；Low pressure (LP) cylinder exhaust steam pressure pcWith condenser pressure pwcIt is identical, by low pressure (LP) cylinder exhaust steam pressure pcWith constant entropy steam discharge entropy sc *,
The industrial properties of water and steam model proposed according to international water and steam property association in 1997, calculating is obtained
Entropy exhaust enthalpy hc *；By the low pressure (LP) cylinder internal efficiency ratio η takenLP, calculate actual exhaust enthalpy hc=hr-ηLP·(hr-hc *)；By coagulating
Vapour device pressure pwc, the industrial properties of water and steam mould proposed according to international water and steam property association in 1997
Type, calculating obtains condensate enthalpy hwc；
By first order extraction temperature t1And pressure p1, the industrial water proposed according to international water and steam property association in 1997
With water vapour thermodynamic properties model, calculating obtains the first order and drawn gas enthalpy h1；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, the industrial water and steam heating power proposed according to international water and steam property association in 1997
Property model, calculating obtains the hydrophobic enthalpy h of primary heaterd1；By primary heater exit water temperature degree tw1With outlet hydraulic pressure
Power pw1, the industrial properties of water and steam model proposed according to international water and steam property association in 1997, calculating
Obtain out saliva enthalpy hw1；
By second level extraction temperature t2With extraction pressure p2, the industry proposed according to international water and steam property association in 1997
Properties of water and steam model is used, the second level must be arrived and draw gas enthalpy h by calculating2；By second level heater outlet coolant-temperature gage tw2With
Go out water pressure pw2, the industrial properties of water and steam mould proposed according to international water and steam property association in 1997
Type, calculating obtains outlet water enthalpy hw2；
By third level extraction temperature t3With extraction pressure p3, the industry proposed according to international water and steam property association in 1997
Use properties of water and steam model, calculating obtains the third level and drawn gas enthalpy h3；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), dredged by third level heater
Coolant-temperature gage td3With hydrophobic pressure pd3, the industrial water and steam proposed according to international water and steam property association in 1997
Thermodynamic properties model, calculating obtains third level heater condensate enthalpy hd3；By third level heater outlet coolant-temperature gage tw3And outlet
Water pressure pw3, the industrial properties of water and steam model proposed according to international water and steam property association in 1997,
Calculating obtains outlet water enthalpy hw3；
Step 2：Heaters at different levels are calculated to draw gas share αj(j=1,2,3), condensing stream part volume αc
Step 2.1：According to the thermal balance and flux balance equations of primary heater, the share of drawing gas of primary heater is obtained,
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According to the thermal balance and flux balance equations of second level heater, the share of drawing gas of second level heater is obtained,
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According to the thermal balance and flux balance equations of third level heater, the share of drawing gas of third level heater is obtained,
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Step 2.2：Condensing stream part volume α can be obtained by mass balance equationc,
αc=1- α1-α2-α3 (4)
Step 3：Calculate backheat steam flow work done wr, condensing stream work done wc
Unit share reheated steam recepts the caloric σ=h in reheaterr-h1；
Backheat steam flow work done is,
wr=α1·(h0-h1)+α2·(h0-h2-σ)+α3·(h0-h3-σ) (5)
Condensing stream work done is,
wc=αc·(h0-hc+σ) (6)
Step 4：Calculate conversion condensing stream amount of work Δ wc
The radiation loss that primary heater is produced,
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The radiation loss that second level heater is produced,
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The radiation loss that third level heater is produced,
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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,
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Conversion condensing stream amount of work is can be calculated by (10),
Δwc=Δ αc·(h0-hc+σ) (11)
Step 5：Calculate backheat work done and compare Xr
Equivalent backheat steam flow work done is：
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Equivalent condensing stream work done is：
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The dimensionless heat consumption rate HRRKAcquisition methods it is as follows：
Defined according to heat consumption rate, obtain dimensionless heat consumption rate of the reheating without extraction cycle：
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Wherein, h0For main steam enthalpy, hwcFor condensate enthalpy, hcFor the actual steam discharge enthalpy of low pressure (LP) cylinder, hrFor reheated steam enthalpy
Value.
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| "再热机组热力循环效果的评价及其算法研究";王培红 等;《中国电机工程学报》;20020331;第22卷(第3期);68-71 * |
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