發(fā)電廠原則性熱力完整系統(tǒng)計算

1、發(fā)電廠原則性熱力系統(tǒng)計算已知條件1.汽輪機形式和參數(shù)制造廠家：哈爾濱汽輪機廠型號：N30016.7/538/538型型式：業(yè)臨界、一次中間再熱、單軸、雙缸、雙排汽、反動凝汽式汽輪機額定功率：300MW最大功率：330MW初蒸汽參數(shù)：p0=16.67MPa,t0=538C再熱蒸汽參數(shù)：冷段壓力P2=P；h=3.653MPa,冷段溫度圳=320.6C.outout熱段壓力prh=3.288MPa，熱段溫度trh=538C低壓缸排汽參數(shù)：P=0.0299MPa,L=32.1C,h=ccc2329.8kJ/kg給水泵小汽輪機耗汽份額：:st=0.0432機組發(fā)電機實際發(fā)出功率：'Pe=300M

2、W給水泵出口壓力：Ppu=20.81MPa凝結(jié)水泵出口壓力：1.78MPa機組機電效率：098mgmg0.98加熱器效率：h=0.99額定排汽量：543.8t/h給水溫度：273.6C冷卻水溫度：20C最高冷卻水溫度：34C額定工況時熱耗率：（計算）7936.2Kj/KW.h（保證）7955Kj/KW.h額定工況時汽耗率主蒸汽最大進汽量：工作轉(zhuǎn)速：旋轉(zhuǎn)方向：3.043Kg/KW.h1025t/h3000r/min順時針（從汽輪機向發(fā)電機看）48.550.5Hz取大允許條筑吊彼擺動:空負荷時額定轉(zhuǎn)速波動：土1r/min噪音水平：90db通流級數(shù)：36級表(1)機組回?zé)峒訜崞鲄?shù)項目單位回?zé)峒訜崞?/p>

3、H1H2H3H4H5H6H7H8回抽汽壓力PjMPa5.8523.6531.6950.8680.3360.1340.0650.025執(zhí)八、抽抽汽溫度tjC383.9320.6437343.3240.1141.987.965.3x=0.957汽'加熱器壓力PjMPa5.3843.3611.5590.7990.3090.1230.0600.023加熱器水側(cè)壓力pwMPa18.8318.8318.830.8242.652.652.652.65水加熱器進口水溫度twj+1C243.3201.7171.7135.3103.783.861.4側(cè)加熱器出口水溫度t.uWj0C273.6243.320

4、1.7171.7135.3103.783.861.4加熱器疏水溫度td.UWJoC251.3209.7179.72.鍋爐形式和參數(shù)型號：HG1025/18.2YM11型型式亞臨界、自然循環(huán)、中間一次再熱、燃煤汽包鍋爐、單爐膛緊閉取大連續(xù)烝發(fā)里：D1025t/hb過熱蒸汽出口參數(shù)：<5Pb=18.2MPa,tb=541C再熱蒸汽進口參數(shù)：P；h（b）=3.92MPa,t；h（b）=320C再熱蒸汽出口參數(shù)：P°h（b）=3.72Mpa,螺=541C省煤器進口給水參數(shù)：Pfw=27.5MPa,t=278.9C,hfw=1234.00KJ/kgDi,Db1,Dd按電力技術(shù)管理法規(guī)(試

5、行)的規(guī)格選取，即D1=(1.5%3.5%)Db,Db1=(1%5%)Db,Dd=(1%3%)D0相應(yīng)選取結(jié)果如下：鍋爐連續(xù)排污量：Db1=0.02Db全廠汽水損失：D1=°.03Db至鍋爐減溫水量:Dd=0.015D0,hd=594kJ/kg解：整理原始數(shù)據(jù)的計算點汽水粉值機組發(fā)電機功率pe=300MW表（2）機組回?zé)嵯到y(tǒng)計算點汽水參數(shù)項目單位回?zé)峒訜崞骷訜崞骶幪朒1H2H3H4H5H6H7H8SG排汽C加執(zhí)八、器抽汽抽汽壓力PjMPa5.8523.6531.6950.8680.3360.1340.0650.0250.0299抽汽壓損Apj%88888888'加熱器汽側(cè)壓力

6、pjMPa5.3843.3611.5590.7990.3090.1230.0600.023抽汽溫度tjC383.9320.6437343.3240.1141.987.965.3X=0.975'pj下飽和水溫度tsjC274.6244.3202.7172.7136.3104.784.862.432.1抽汽粉hjkJ/kg3138.073025.553332.163145.482945.472757.232656.372516.572329.8.一.一.p下飽和水粉hjkJ/kg1177.641038.48853.07720.97565.90442.33359.91264.22411.51

7、45.5被加執(zhí)八、水加熱器端差8jC11111111加熱器出口水溫度t-wjC273.6243.3201.7171.7135.3103.783.861.4加熱器水側(cè)壓力pwMPa18.8318.8318.830.8242.652.652.652.65進口水粉hwj4ikJ/kg1054.92867.33726.57570.62436.58352.94259.22出口水粉hwjkJ/kg1199.371054.92867.33726.57570.62436.58352.94259.22疏水疏水冷卻命端差8C888疏冷器出口水粉hwjkJ/kg1091.57896.77771.26根據(jù)p,t查水蒸

8、汽表得新蒸汽粉值h°=3396.75kJ/kg,排汽粉值處=2329.8kJ/kgh；h=3025.55kJ/kg,hOut=3537.10kJ/kgqrh=hOut-h；h=3537.10-3025.55=511.55kJ/kg全廠物質(zhì)平衡-'-汽輪機總耗氣重D=D00'鍋爐蒸發(fā)量Db=D0D1=D00.03DbDb=1.030928D0(1) 鍋爐給水量Dm=DbDb1=Db0.02Db=1.02Db=1.051547D0鍋爐連續(xù)排污量Db1=0.02Db=0.020619D0'未回收排污水量Db1=Db1=0.020619D0補充水量'Dma=D

9、iDb1=0.03DbDb1=0.03Db0.02Db1=0.05Db=0.051547Do計算回?zé)岢槠禂?shù)與凝汽系數(shù)高壓加熱器H1:由H1熱平衡式求«1，K-hWh=hw1-hw23138.07T091.57=0.071297hw1一hw2h1199.37T054.920.99h1hWH1的疏水系數(shù)二d1=二1=0.071297(2) 高壓加熱器H2:l：2h2-h=2d1hW1-hW2>h=hw2-hw3=hw2-hw3hfdi思-思1054.92-867.330.99-0.0712971091.57-896.77=0.0824873025.55-896.77H2的疏水系數(shù)

10、:d2=：d1：2=0.0712970.082487=0.153784再熱蒸汽系數(shù):rh:rh=1-：2=1-0.153784=0.846216(3) 高壓加熱器H3先計算給水泵粉升AhWU。除氧器水位高度為20m，則給水泵的進口壓力為pin=PghE0*+0.92p4=20x0.0098+0.868、0.92=0.99456MPa，取給水的平均比容為vav=0.0011m3/kg，給水泵效率11pu=0.83,則3pWU10vavPout一Pinnpu1030.001120.8V0.99456=26.3kJkg0.83由H3得熱平衡式得hhdhd-hd。-h-hhpu3h3hw3-d2hw2

11、hw3hhw3hw4hwhw3(hw4+hwu"%-2此2土83)h3-hw3=0.037610867.33-726.5726.3】0.99-0.153784896.77-771.263332.16-771.26H3的疏水系數(shù)：d3=：d2：3=0.1537840.037610=0.191394除氧器HD'第四段抽汽a4由除氧器加熱烝汽a4和汽動給水泵用汽apu兩部分組成，即'a=a+a,44st由除氧器的物質(zhì)平衡可知除氧器的進水系數(shù)a為C4'ctciT-ads-J(1)除氧器熱平衡式為'dhhhh仁w444d3w3c4'W5將式(1)代入，則

12、眉4-hw5=-4h4-hw5-d3眉3-hw5考慮nh,則熱平衡式為hw4一hw5.h='4h4一hw5'd3hw3一hw5一.=，hw4-hw5h-d3隊3-hw5h4一hw5726.57-570.620.99-0.191394771.26-570.62=0.0462643145.48-570.62：c4=1一：d3一：4=1一0.191394-0.046264=0.762342'_：4=：4：st=0.0462640.0432=0.089464(4) 低壓加熱器H5:由H5的熱平衡式得a5：5h5-Ih5h"c4hw5-hw6_c4hw5-hw6hCX.

13、5h5-h5=0.762342570.62-436.580.9900433762945.47-565.90.(5) H5的疏水系統(tǒng):d5=：5=0.043376低壓加熱器H6:L6h6-h6：d5h5-h6>h=：c4hw6-hw7-c4hw6一hw7h一d5h5一h6：6='h6f0.762342436.58-352.940.99-0.043376565.90-422.33=0.0251322757.23-442.33H6的疏水系統(tǒng):d6=：d5：6=0.0433760.025132=0.068508UOUkJO低壓加熱器H71?7h7-h；,：d6h6-h；>h=c4h

14、w7hw8=:c4hw7-hw8h-d6h6-h7一7一h7-h70.762342352.94-259.220.99-0.068508442.33-359.91=0.0289672656.37-359.91H7的疏水系數(shù)-d7=：d6：7=0.0685080.028967=0.097475低壓加熱器H8與軸封加熱器(SG)將H8與SG作為一個整體考慮，采用圖所示的熱平衡范圍列物質(zhì)平衡和熱平衡式。由熱井的物質(zhì)平衡式，得aasac-ada8(2)熱平衡式為'':c4h8=:8h8：d7h7：c：sthc代入式,考慮h，并整理成以ac4吸熱為基礎(chǔ)以進水粉hc為基準的熱平衡式，得L8屈

15、-星：d7h7-hc"h=：c4hw8-星:c4眉8-hch-：d7h7-hc'h8-hc0.0281180.762342259.22-145.50.99-0.097475359.91-145.52516.57-145.5凝氣系數(shù)a的計算與物質(zhì)平衡校核c由熱井的物質(zhì)平衡計算arca=o(cc4d78st=0.762342-0.097475-0.028118-0.0432=0.593549由汽輪機通流部分物質(zhì)平衡來計算a以校核計算的準確性c=1-0.0712970.0824870.0376100.0894640.0433760.0251320.0289670.028118=0.

16、593549兩者計算結(jié)果相同，表明以上計算正確。4,.新汽量D°計算及功率校核根據(jù)抽汽做功不足多耗新汽的公式來計算D0(8D°=Dco用=Dco/1-"jYj/<1J(i)計算Do凝汽的比內(nèi)功f為iCic=h0qrh-hc=3396.75511.55-2329.8Dco10一33600Pe3600300000”_310=1578.50.98(2)計算D0各級抽汽做功不足系數(shù)Yj如下:h1qrh-hc3138.07511.55-2329.8Y1=ic1578.57h2qrh-hc3025.55511.55-2329.8Y2=二2*1578.5=1578.5kJ

17、/kg698.1570t/h=0.836123=0.764840h3一1%=3332.16-2329.81578.5=0.635008Y3co.ic3145.48-2329.81578.5丫5h5-hcic0.516744丫6h6-hcic丫7COic丫82945.47-2329.81578.52757.23-2329.81578.52656.37-2329.81578.5h8-hc_2516.57-2329.8ic1578.5=0.3900350.2707820.206886=0.118321ajhj尸jYj和Dj的計算數(shù)據(jù)見下表(3)表(3)jhj,0jYj和Dj的計算數(shù)據(jù)ajhja.hj

18、jYjaYjjDj(t.hDj=D0%)%=0.071297h1=3138.07=223.734977Y1=0.836123a1Y1=0.059613D1=64.298943a2=0.082487h2=3025.55a2h2=249.568543Y2=0.764840«2Y2=0.063089D2=74.390604a3=0.037610h3=3332.16a3h3=125.322538Y3=0.635008a3Y3=0.023883D3=33.918443a4=0.089464h4=3145.48a4h4=281.407223Y4=0.516744a4Y4=0.046230D4=8

19、0.682786a.=0.0433765h5=2945.47a5h5=127.762707Y5=0.390035&5Y5=0.016918D5=39.118489a6=0.025132h6=2757.23口6h6=69.294704Y6=0.270782«6丫6=0.006805D6=22.665204a7=0.028967h7=2656.37口7h7=76.947070Y7=0.206886«7Y7=0.005993D7=26.123785o(8=0.028118h8=2516.57a8h8=70.760915Y8=0.11832108Y8=0.003327D8=

20、25.358117ar=0.593549chc=2329.8ah=1382.850460ccD=535.290028cZah=2607.649137£口Y=0.225858D0=901.846399則，抽汽做功不足汽耗增加系數(shù)P為p=l/1-£aY=1.291753/I1J1-0.225858則汽輪機新汽耗量D。為D0=Dc0：=698.15701.291753=901.846399t/h功率校核1kg新汽比內(nèi)功氣為8、寸+%qrh一"hj+七hc<1)=3396.750.846216511.55-2607.649137=1221.982658kJ/kg據(jù)此

21、，可得汽輪發(fā)電機的功率已為R=D0mg3600=901.8463991221.9826580.983600=299.999957MW計算誤差珞一珞300-299.9999571a=乂100%=Lx100%=0.000014%Pe300誤差非常小，在工程允許范圍內(nèi)，表示上述計算正確。5,熱經(jīng)濟指標計算1kg新汽的比粉耗q0q0=h0:rhqrh一hfw=h0：rhqrh一hw1=3396.750.846216511.55-1199.37=2630.261795kJ/kg汽輪機絕對內(nèi)效率ji1221.982658=46.4586%q02630.261795汽輪發(fā)電機組絕對電效率n=聽聽聽eimgi

22、mg=0.4645860.98=45.5294%汽輪發(fā)電機組熱耗率q3600q=ne3600=7906.978787kJ/(kWh)0.455294汽輪發(fā)電機組汽耗率d.q7906.978787d=3.006157kg/(kWh)q02630.2617954.各汽水流量絕對值計算由Dj=D°aj求出各處Dj,見表（3）除氧器的選擇：1. 除氧器額定出力的計算：計算額定工況下的出力，根據(jù)質(zhì)量平衡原則，除氧器在額定工況下的出力DM為式中DmDnDmaD.gjDd.djDcDM=DnD額定出力(t/h);進入除氧器主凝結(jié)水量補充水流量(t/h);高壓加熱器疏水流量低壓加熱器疏水流量加熱蒸汽

23、量(t/h);maDgjDdjDc(t/h)(t/h);(t/h);(t/h);則有DM=DnDD.magjDh.djDc(t/h)cD0%4+Dma+D0%3+D0%5D0叩D0%40.051547印3由5勾9018463990.7623420.05154701913940.043760.0462642. 987.45(t/h)除氧器水箱有效容積的計算：有效貯水容積是指正常水位至出水管頂部水位之間的貯水量，它是根據(jù)發(fā)電廠全部鍋爐額定負荷下的最大給水消耗量來確定的。根據(jù)我國水利電力部1984年新公布的火力發(fā)電廠設(shè)計技術(shù)規(guī)程SDJI84的規(guī)定，除氧水箱的有效總?cè)莘e宜按下列要求確定：(1) 汽輪機

24、單機容量為200MW及以下機組為1015min的鍋爐最大連續(xù)連續(xù)蒸發(fā)量時的給水消耗量(2) 汽輪機單機容量為200MW以上機組為510min的鍋爐最大連續(xù)連續(xù)蒸發(fā)量時的給水消耗量。則有效容積為：Db(t/h)8min=Db(t/h)0.133333(h)=10250.133333=136.67(t)有效容積水箱的有效容積應(yīng)占幾何容積的80%85%。取口心=80%則幾何容積為何何容積170.83(t)查取火力發(fā)電設(shè)備技術(shù)手冊，選擇除氧器型號根據(jù)上述計算結(jié)果，由火力發(fā)電設(shè)備技術(shù)手冊選取的除氧器應(yīng)滿足以下條件：銘牌出力應(yīng)大于額定出力Dm=987.45,除氧器水箱容積應(yīng)大于除氧器水箱幾何容積170.8

25、3(t)。除氧器技術(shù)規(guī)范如下：制造廠家上海電站輔機廠除氧器型號GC1000銘牌出力1000t/h結(jié)構(gòu)形式箱式頭部直徑2.5m霧化區(qū)局2.5m設(shè)計壓力0.981MPa設(shè)計溫度350C工作壓力0.785MPa進水溫度147.7C出水溫度174.5C運行方式滑壓噴嘴工作壓降0.0588MPa噴嘴組成74只X16t/h填料材料填料高度不銹鋼Q形填料除氧器內(nèi)徑2.5m除氧器長度8.6m水箱容積3180m3機組容量300MW汽動給水泵的選擇；1.汽動給水泵流量的計算：在每一個給水系統(tǒng)，給水泵(不包括備用給水泵)出口的總流量(即最大給水消耗量)應(yīng)保證供給其所連接的系統(tǒng)的全部鍋爐在最大連續(xù)蒸發(fā)量時所需的給水量，即鍋筒鍋爐：鍋爐最大連續(xù)蒸發(fā)量的110%直流鍋爐：鍋爐最大連續(xù)蒸發(fā)量的105%對中間再熱機組，給水泵入口的總流量，還應(yīng)加上供再熱蒸汽調(diào)溫用的從泵中間級抽出的流量，以及漏出和注入給水泵軸封的流量差。汽動給水泵流量為:Dfw1.051547D0v=v=1.051547901.84639910320.0012163=576.73(m3/h)1. 汽動給水泵揚程的計算:給水泵揚程應(yīng)為下列各項之和：(1) .從除氧器給水箱出口到省煤器進口介質(zhì)流動總阻力(