任何化工產(chǎn)品的制作無非是兩個過程分離過程與反應(yīng)過程

v＝p即。AAxA1/6010~10mmHg24VIVDQCLDLDFFV,IVW'LmWQB2/60ypVyipVAPVAiPVAA）pu20zH2ggA和B是兩種不同的物質(zhì)，如：a,a,aBBAAABaaaBB。AAAB若a與a或aABAABBpppix（p）00ixiiiiiip*Bx或x于01、ABBppx0ppx0pp0xAAABBBiiip、pA和BAB3/60p0、p0BABx、xBABHnHnHnH總1122iiVnVnVnV總1122ii1×n×Hi×n×Viiin、nn12iH、HH21iV總V、V、……V12ippa0iiipiipi0iaii（x則axaiiiiiiiaa，aABAABB4/60B125。第一節(jié)兩組分溶液氣液平衡6.1.1兩組分理想物系的氣液平衡FC22222PyP－nn－2－15/6012345o。CppppABABppxppxpx)000AAABBBBApf(x)p(x)AABAxp，pAABttccx(y)x(y)6/604則pppPypPyAAABBpxppx00AABBBxPypxPy00AAABBByp0xyp0x）APBPAABA又Ppppxpxpxpx)0000ABAABBAABAxPp0）BppA00AB4Pb氣相區(qū)1x2t）x7/60Pp0xtBppA00ABp、p0PxABAp0yxAPAAbppApABae°p=pXAA°BppAfApdBXAB理想溶液苯與甲苯的混合液即a點（xyy1p0P）當(dāng)x0x1pp，，0＝PABBBAABBxyppP0yxpP即1yx)p00即bP0即APAPAAAAAAAAyxtp0與p0AAABoCppx0iiip0，p0AB∴px是kii8/60xx1ABPpppxpx00ABAABBxPp0Bp0p0AABx0時Pp0x1當(dāng)Pp0即當(dāng)xABAA，x，Ppxp0當(dāng)x0得b點BAAAA當(dāng)x0xPpxp0得a點ABBBBp)在e則pAB知Pp0Pp0p0Ppx圖即0ABBAypp0xAPAPAAyxp01yx∴即AAAPAAypp0xyp10xyB∴BPBPBBBBPxBB即xP122x圖線線線9/60pp2°BpB°ApppBAAtxy）tfxtfyt、b過熱蒸氣區(qū)y℃線氣液共存區(qū)未沸騰的液體區(qū)精餾塔示意圖［］苯與甲苯氣液平衡圖P=1atm10/60P稱yyx苯-甲苯混合液在P=101.33kpa的x-y圖yxyy可＝ppAABxxABBpp0x＝p0AAxAxAAAA11/60ppxppx00AAABBBp0p0AABBp/x＝＝或則ABAApxAB/BBPy/xyxAyx＝1○AABBAPy/xBB1＝p0A0pBp0A及p0ByyxxyxA1或ABABA1y1xAAyABxABABpA0或p0p若0A較Byxp0ABByx若yAxy若1xmXy*1m)X第二節(jié)平衡蒸餾和簡單蒸餾6.2.1平衡蒸餾12/60312tfTFQte平衡蒸餾裝置G＝GGG10AAh1○DyWx2○FxFxFFW2yW3○xxDDF1F14○DDFF)xx43y5○DDF13/60DWWFD)則11＝FFq、令F1)x1xFqxq1q1xy56○F1q1q66q當(dāng)xx時，yxq1FFG＝G＋Q10L損失入出Q0∴G＝GL10入出∴Q輸入＝FCTt)①1pf輸出；0；CP0；tf0；tet以tteereWtteeDrpWCttpe輸出e輸入FCTtDrtt1qFr）2pepe出e出入DFq）t0；e。rt）e）Cp14/60x1xytf(x)e6.2.2簡單蒸餾dy*dL(y*x)Fx）1Ly*xWx2L則x則x12Fln1Wy*xx2據(jù)1x與x1xy*x21對xx到xy*x12xy1xx11xFWx1211xx211m1xbFlnln1Wm1m1xb2F1xlnln1Wm1x215/60yx)D,mWDyFx12第三節(jié)精餾原理和流程6.3.1精餾原理1txA11tJyDy與x2111y>xEt113xFxyGy>x22222tHxC43yxH13yJH3HHHJJJ110.63℃tCGF3tD2J80.1℃tA1y3yy3211216/60ABBt1（<Cyxxxx11101txy222ttC2B1'2tEx0'2xx2x'2yyy211一次部分氣化t-x-y圖t'Ey'的2y12'y'x'y'y>x與222225y3yD33y2x321、2、3-分離器；4-加熱器；5-冷凝器y1x21無中間產(chǎn)品及中間加熱器與冷凝器x4的多次部分氣化（冷凝）分離示意圖Fx117/60y1，xxtt3313x3y15y3y33y2x32y1x2xFx16.3.2精餾操作流程18/60xyn-1n°°°°xn+1n篩板塔的操作情況圖1n1nnntxtn1tt為yn1n1n1n1n1成平衡的液相濃度xyxxyn1nn1n1n1n1nx,yyxnn1nn1第四節(jié)兩組分連續(xù)精餾的計算6.4.1理論板的概念及恒摩爾流的假定nxynn19/60VVVV12nV'V'V'V'12mLLLL12nL'L'L'L'12m6.4.2物料衡算和操作線方程1○DxD2○FxFw；；；xFxDxW20/60QCL精餾塔的物料衡算QBDqFDx％DxDFxDFxDFFWx)wF1xFW1xWqFWF1xWF；；。VyLxDx）n1nDyn1nxnxD21/601L,xD,xDD1yy22nx1nn+1F精餾段操作線方程的推導(dǎo)LDyxnxLDLDn1DDL/DD/DynxnxL/DD/DL/DD/D1DLD令RR1yn1xnx）R1R1DybL=V+WL；V－；W。LxVymm1Wxmmy1m1xW22/60FV'm'x'mW）LWm1xmyxLWLWWL'令R'WR1m1xmyx）R1R1wybq1Wyxxq)q1q1FFLL）LLL）在xWqL，F(xiàn)LLL，qFq6.4.3進料狀況的影響q23/60LLL即qF、I及IIIVVLLLLFVVqLLF∴qWF；LLLLVVFqq0F，L，LLF+FqLLFFFLVLq1F0FL∵FF∴LL∵LVFL∵V∴q24/60IIVqFrmFLLFVV．FVLVL①VVLFLLLq令FIfIIVIIVLLIrxr1xr輕重mFF．FIVILIVILI②③FVLVLVILLIVVFLVFLLVFLLIFILLIVFLIILLFIILLII或④VFLIIFVFVLVIILLqqVFL令I(lǐng)IFVIIkmol進料變?yōu)轱柡驼魵馑枰臒崃縄IVFLVFII原料液的千摩爾氣化潛熱rmVIIqmVLmL'LqFL'FVLVL'LVV'(qF與⑤25/60LWm1xyxLWLWmW．．4理論板層數(shù)的求法HNhPPNTpNNTNT1y1L,xD,xDDF,xFy'1逐板計算法示意圖yxxD1Dxxx,11y1(ax26/60操作關(guān)系bya1y2Cxx1D12用操作線方程x112氣液平衡關(guān)系yR1xxR1R1n1nDR'1x'xm1yR'1R1'wmLLWWy'xx'或LWwm1m或y’22xxx（xnnFFFx'x(xmwwxx精RxyxDR1R127/60yabxDCxWxDxDDxyb聯(lián)bDR⑵LWyxxLWLWWc點wwLDyxxLDLDDLWyxxLWLWwLyxDxyDL(yx)qF(xy)W(yx)WD(xy)qF(xy)W(yx)∴DwqFy(DW)yqFx(DxWx)∵DWDWFDxWxFxDWF28/60qFyFyqFxFx∴Fqxyxq1q1Fqqqqx、yx）。qxq1FFq將q（xx從eq1FFdd，⑶qqx及qq1F29/601ya12y2f3d4ey5cb6xxxxWF1Dx求理論板層數(shù)的圖解法步驟qq，q為+1q11qq，q為“1q12q0q1q為q134qq，q為0q1qq，0q為q15xxxabxDR1DqxexF30/60dxxCwadC1求y1x1y11x1y2x1求2xy12求yx22①②③、、5幾種特殊情況時理論板數(shù)的求法qQC餾出液LD原料液FF'V,I'釜殘液WQB31/60LLVVW0'x'VyV'y'Wxm00m1wh；V0yy0。00V'V,L'W0Wx'Vy'Wxm0m1wWW或y'x'xm1VmVw00,xqC（xwwy'0,x'xxxx,0w聯(lián)m1mww'xxmwyadegxxxxwFD提餾段操作線方程32/60i。、、6回流比的影響及選擇LLRD0Rxyn1xnDR1R1Rx0DR1R1yx在n1nNmin求NminQCLDFF'V,I'L,IWQBp0yxap0p0avv）AAAyBxp0nAABBnBBnnnyxn1n33/60則yxyx或,,1yxyxaAA1DyxAABB1B1BDxxya①AAAy1xxB1B1BDyx②2A1yx③（yx）21n1nyx④AAyxB2B1xxyaa⑤AAAx1x1yBB1B2DyxaAAy2xB2B2xxaa⑥AAx12xBB2DyxAAyxB3B2xyaa⑦AAx12yBB3DxxAaAaa1⑧x2N1xBBDWaaaaN1m12N1xxaN1⑨AAxxmBBDwNNmin34/60xxlg()(N1)lgalg()AAxminxDmWBBxxlgABxxN1BA⑩DWlgamAB1xxD1xWx○N1DWlgamNmin○aa稱mxxawFyagqexxwFqD最小回流比的確定35/60ddddRRminminq．xyRtgminDqR1xxminDqxyDyxR⑴qminqqxq,yqqqggRax,xminDDR。minygabecxxxxWFD不正常平衡曲線的R的確定min⑵qx,yqq36/60axyq1a1xqq11xaxR③DD1xa1xqqxxqF1a1xxRDDa1x1xminFFaxyyy對yxqF1a1x1aayqFqqqFxyDyxxyRqDFyxminqqFq11x得R1DDmina1y1yFFyF11xaxRN，，RDD1xa1xminqq∞∞與Rminab/VV因（）D及1VVqF當(dāng)D汽V和VV(R(1)當(dāng)RVR②Rmin37/60NRRminRRRminNRminNmin0RRV與VR13321RLLL1.12.0VVR=RRminD操作min38/60、、7簡捷法求理論板層數(shù)．．．RRN及Nminmin(RR稱為：吉利蘭圖。吉利蘭圖是雙對數(shù)坐標圖，橫坐標min)R1；縱坐標表示NNminNN(NminRRNN示，0；R1N2minRRR10，N=，minminNN1。N2R為min1R；min2N；min(RR)3R1NNN2NminYXX39/60XRRR1YNNN2X、、8塔高和塔徑的計算．EMny全回B流為例yyAxy''nyyCnxnn單板效率EyxABABCn1n40/60yyBCBCEMVnn1n1yynxxABABABEMLn1nnxxABn1y*xnnx*ynnEMVEMLx與ynn1n1x*x*,ynx”n1nnxxn1ABxyC,nnn1yy*x,y*Bn1nnnyyn1x,y’nn1nx,y*nn,xyn1nyN100％。ETPNNTNP。41/60VVDu或D2s4usV[m/s]3s精餾段Vs/s。[m3wnMsVsVm3600sV[/m3vM[/ol。mpV0T0nT0nRTpTp0TppVnRT，VnVp00VV22.4V，V22.4m/kmol，V[m/s。Tp0333600Tp0ss0、T；0、p。0提餾段V'sV'M'22.4V'TpV'[m/s]03m3600'3600TpsV0VVV'DDsuss42/60、、9連續(xù)精餾裝置的熱量衡算1QVILIDIcVDLDLD）LDFV間歇精餾出全凝器的熱量＝QLIDILDCLDVIVDQ(RD(II)V(II)CVDLDVDLDQQQQQ）傳放吸損CI；VD。LDI43/60QWCCtt)CPC21WC[kJ/(kg0CCpct，tC。012QQQQQQ0）放吸C吸CLQQQQQ吸損放CC1QL'IBLMV'IQVWLWLQLQ＝Q進出WQV'IL'IQBVWLWLMLQ＝Q放傳∴QWIIBh1B2QWBIIh12WhI,I。BB12WQBrh。44/60第五節(jié)間歇精餾LDFV間歇精餾RxDRxD6.5.1回流比恒定時的間歇精餾計算RxD在x、x餾出液平均組成和xFWe在x由x和xD1D1FdxD145/60R.min1Ryn1xnxR1R1DxyR∵DFF1R1xx1xyyx∴R1（R）FDqxyxminyminFFqqxFyxFF）RminxyDmR1axF1a11恒回流比間歇精餾時x和x的關(guān)系wDxxWDRR146/60RxxDi,xR1DiDixDixxDiWiRN＝minxR1Dminxxx即DDD132xxxW3W2W1x~xDW大大x,xD即D31或小小xxDDWxx與D,W故DDxd。Wx＋dxd。WWD。○d1WdWxdx○2WWWDdd而xx）DDd將○展開2xdWdxdWdx）WWWWWWDWdWWdxWxx○3DWdWWdxWxxFWedxWxxlnFxxFFWexxDWDW47/60FWexx始終FWe1FdWxdx○4FWWxx2xW2DWF；xx。fWxw-1xDxdxFwxDwxwFxxWDWDxDm○1DxFx○2DmFW12xFWFWRVVV＝48/60lnFWedx∵Wfxxxf(x,x)xFWxxDWFDWxDW當(dāng)x(x)WDV一定，DW3.5.2餾出液組成恒定時的間歇精餾計算FxDxFDWFx(FW)xFxFDWDDWFxxW）FDxxDWDFW）xxDW在1a23y4b1RxxD49/60xxDWexyRy與xDWexminyWeWeWeWe）RR。minx（X,x，DR1DDxWex與RWxRWRx111awxyb。DR111x,xbRDD11ax。150/60設(shè)d＝(R）））dWWdxWxx（參考間歇精餾）DW參考餾出液組成恒定時FxxDWFxxDWF(Rxx)dVdxFxxD2WDWR1xVVdVFxxDxdxx2FFxW0DW)21xw+-RxD(xFwDwxxxFw氣化量積分求法Vx時的氣化總量，而xWe、、xDW第六節(jié)恒沸精餾和萃取精餾6.6.1恒沸精餾51/603.6.2萃取精餾第七節(jié)多組分精餾6.7.1流程方案選擇n6.7.2多組分系統(tǒng)的氣液平衡nn∵F－2cnxiyiiKy）iixiiKi52/60ippPyiiip0xipiiipx0iii）ypix0KiPiiiKP及ip0pK0iiiKf組分、P、t)iK值jp/xPy/xy/xKAApxAAPyxAAyxAAB///KABBBBBBBBy/xKi0iiiy/xKp0ijjjjj0xyKxpiPiiiip,Ppxpxpx而P01010i12nnp0xyiiipxpxpx0102012nnp0jxxyiijiijixxxnx1j12j2njnijii153/60∵xy○1iKiinny1i將1到x○2Kii1i1iy/(K/K)y//K○xyiijiijii12ynniny/K/Ky/iiKiijiji1i1i1i變TRTlnf0（f0xPfiiifiifi0ixiiffx0iffy0if,fiiLiVf0,f0iPtiLiVffiLiVyf0iLf0○1KixiiiVK）iffx,xfiL0f0iLiiiiLffy,yfiV0f0iViViiiV54/60．ppx0○1iiiii＝fPf0f0f＝pfp時，fp,1pippy○2ii2Pypx0ppx01iiiiiiiiypi0K