1、合成氨全算1.2m合成流程簡圖1=11-氨冷器2-冷交3-循環機4-合成塔5-熱交6-廢熱鍋爐7-軟水預熱器8-水冷器9-氨分10-液氨儲罐合成氨物料衡算一已知條件及設計條件1、合成原料氣體（精煉來氣）成分（氫氮比3）成分H2N2ch4Ar合計百分含量73.5%24.5%1.5%0.5%100%2、合成甲烷控制14.5%3、進塔氨含量2.5%，出塔氨含量13.2%4、催化劑填裝量11.24 M35、水冷器的出口氣體溫度35 C6、1.2m合成系統設計生產負荷15t/h7、系統工作壓力31.4Mpa8、計算標準1tNH3衡算數據查詢有限，有的時候采用了資料上現成的數據，沒有符合當前的系統狀態。二

2、計算1、合成進塔氣體成分CH4N2H2Arnh30.1450.2250.5950.010.025注：甲烷為操作值，氫為表測值，氨為實驗值，氬為假設值，氮氣為反推值，在這個氣體成 分下，氫氮比為2.6為合理值。2、合成塔出口氣體成分假設合成塔的進口氣體量為A mol,則有出塔氨量為A*(13.2%-2.5%)1 +13.2%=0.09452A mol除去氨外出塔的氣體量為A-0.09452A=0.90547AmolyNH3=13.2%yCH4=0.145A/0.90547A=0.1601=16.01%0.225A - (0.0945A *0.5) yd=0.90547 A=19.63%0.595

3、A - (0.0945A *1.5) yH2=0.90547 A=50.05%CH4N2H2Arnh30.16010.19630.50050.0110.132yAr=0.01A/0.90547A=1.10%塔出口氣體成分表：3、合成率合成率0.09452A * 2A *(1 0.145 0.01 0.025)=23.05%4、氨分出口氣體成分分離下有物料總衡算式F總=V氣+L液兩相平衡有K(i)= 空，是組分食是液相中分比?是氣相中的分比K(i)為組分i的相平 x(i)衡常數(四)K (i) =(知)1 LF (i) Lx(i)VLX(i)L(F (i)Lx(i)1)推出旦) 1 = (-)K

4、(i)Lx(i)L,、F (i),、公式變形 Lx(i) = -= L(i)(了) K (i) +1L = L(i).氣態組分x(i)=L(i)F (i) - L(i)V假定氨分進料量為A mol氨分入口氣體成分為叫N2H2Arnh30.16010.19630.50050.0110.132在35C, 29Mpa時有相平衡常數表Kch 4Kn2Kh 2KaKnh38.20034.527.528.20.098假設 V/L=21.36T . F (i)Li =1 + (V/L) K (i)LNH3=0.04267315A molLCH4=0.000913983A molLAr=1.82315E-05

5、A molLH2=0.000850612A molLN2=0.000266018A mol液相總和 L=0.044721994A； V=A-L新的 V/L=21.36036244V/L誤差=-1.69684E-05，驗證氣液比正確液相中各成分含量為xNH3=LNH3/L=0.95418709=95.42%xCH4=0.020437=2.04%xAr=0.000407663=0.04%xH2=0.019019989=1.901%xN2=0.005948259=0.059%氣相中的各成分含量yNH3=VNH3/V=9.351%yCH4=16.758%yAr=1.150%yH2=52.304%yN2

6、=20.521%液相中的氨含量95.419%氣相中的氨含量9.351%液相中的甲烷2.044%氣相中的甲烷16.758%液相中的氬0.041%氣相中的氬1.150%液相中的氫1.902%氣相中的氫52.304%液相中的氮0.595%氣相中的氮20.521%5、冷交出液相成分引用數據，此數據我沒有查（-10C, 28Mpa相平衡常數）Kch4Kn Kh 2KaKnh32728075510.0254合成塔入塔氣體成分CH4N2H2Arnh30.1450.2250.5950.010.025x(i)=y(i)/K(i)由合成塔入塔氣體成分可得xCH4xN2xH2xArxNH30.537%0.281%0

7、.793%0.020%98.425%6、球罐出口氣相與液相成分氨分和冷交共同放氨，進入球罐則氨分分離的氨G%=(1云進塔氨)*界出塔氨含量氨分出口氨含量七(y出塔氨含量-y進塔氨含量)* (1 - y氨分出口氨含量)y為氣相G%=40.676%即氨分的分離量為40.676%，冷交分離量為59.324%進入球罐的混合物的成分為W(i)=0.406氨分液相(i)+0.593冷交液相(i) i為成分可根據各公式求得混合之后的液相的成分為Xch4 Xn2 Xh2 XaT Xnh30.0114988760.0040880.0124429440.0002820.972023假定進料量為Amol球罐溫度為1

8、7攝氏度，壓力為1.5Mpa時的各成分的相平衡常數是KCH4Kn2Kh2KArKNH31706205755400.598F(i)1 + （V/L）K（i）設球罐的氣液比為V/L=0.071LNH3= 0.932433729A molLch4= 0.000879792A molLAr= 7.16828E-06A molLh2= 0.0002975A molLn2= 9.08041E-05A mol液相總和 L=0.044721994A； V=A-L新的 V/L=0.070997503V/L誤差二0.00352%，驗證氣液比正確液相中各成分含量為xNH3=LNH3/L=99.863%xCH4=0.

9、094%xAr=0.001%xH2=0.032%xN2=0.010%氣相（馳放氣）中的各成分含量yNH3=VNH3/V=59.720%yCH4=16.019%液相中的氨含量99.863%液相中的甲烷0.094%液相中的氬0.001%液相中的氫0.032%液相中的氮0.010%yAr=0.415%yH2=i8.321%yN2=6.030%氣相中的氨含量59.720%氣相中的甲烷16.019%氣相中的氬0.415%氣相中的氫18.321%氣相中的氮6.030%7、球罐物料衡算以1tNH3為標準計算轉換為氣態標準體積有球罐中液相成分為液相中的氨含量99.863%液相中的甲烷0.094%液相中的氬0.

10、001%液相中的氫0.032%液相中的氮0.010%1tNH3 存在的必要體積=1000/(17/22.4)/99.863%=1319.449NM3噸氨中的各成分體積為在必要體積中的百分占有量即必要體積乘以百分比噸氨中的成分單位NM3NH31317.647059CH41.243257035Ar0.010129683H20.420405432N20.128317686球罐中氣液比為V/L=0.071馳放氣量=0.071*1319.449二 93.68089馳放氣中成分單位NM3NH355.9466263CH415.00664015Ar0.388385723H217.16365537N25.648

11、74318總體積=噸氨各成分+馳放氣各成分=1413.603219NM3反向核算個成分百分比=(噸氨中i成分量+馳放氣中i成分量)/總體積NH3%=(1317.647059+55.9466263)/ 1413.603219=0.971696772 同理其他成分有表各入口成分核算百分比NH30.971696772CH40.011495374Ar0.000281915H20.012439177進入球罐液體成分xCH4xN2xH2xArxNH3百分比0.0114990.0040880.0124430.0002820.972023N20.004086763兩表比較有各成分比例大概相同。核算結果為入口成

12、分計算準確。8、合成系統物料衡算新鮮氣1入塔氣體2出塔氣體3馳放氣4放空氣5球罐中氨6NH300.0250.1320.597200.093510.99863CH40.0150.1450.1610.160190.167580.00094Ar0.0050.010.0110.004150.011500.00001H20.7350.5950.50050.183210.523040.00032N20.2450.2250.19630.060300.205210.00010以下的代表的都是相對應的成分含量值氫VyH=VyH+ V5yH2 +3 V4yNH3 + 3 V5yNH3 +3 V6yNH3 TOC

13、o 1-5 h z 1-24-2-222（2）氮-1 ,- 1 -1 ,-VyN=VyN+ V5yN2 +_ V4yNH3 + _ V5yNH3 +_ V6yNH31242222甲烷+氬V1（yCH4+yAr）=V4（yCH4+yAr）+ V5（yCH4+yAr）氨V3yNH3-V2yNH3=V4yNH3+V5yNH3+V6yNH3（5）總物料V2=V3+V1-V4-V5-V6yNH3已知 V4= 93.68089NM3 V6= 1319.449NM3聯立（1）（2）（3）得 V1= 2819NM3 V5= 228NM3V1，V2 帶入（4）（5）聯立得 V2= 11852NM3 V3= 10

14、532NM38、合成塔進出口物料合成塔進口物料NM3NH3296.3CH41718.54Ar118.52H27051.94N22666.7合成塔出口物料NM3NH31390.224CH41695.652Ar115.852H2N25271.2662067.4329、鍋爐，熱交預熱器都是換熱，未發生液化的設備，進出口物料為合成塔出口 物料合成塔出口物料NH31390.224CH41695.652Ar115.852H25271.266N22067.432總1053210、水冷器物料水冷器進口物料水冷器進口物料NH31390.224CH41695.652Ar115.852H25271.266N2206

15、7.432總10532在氨分計算是得出的氣液比為V/L=21.36則有方程V出口 = 21.36L出口V出口 + L出口 = V進總水冷器出口氣相V10060.98水冷器出口液相L471.0196785氣相組分物料量液相物料量NH39.351%940.7896449.434355CH416.758%1686.0259.627406354Ar1.150%115.65990.19210542H252.304%5262.3038.962805548N220.521%2064.6282.8033343811、氨分物料氨分進口物料量=水冷器出口物料，且成分一致氣相組分氣相物料量液相物料量NH39.351

16、%940.7896449.434355CH416.758%1686.0259.627406354Ar1.150%115.65990.19210542H252.304%5262.3038.962805548N220.521%2064.6282.80333438合10060.98471.0196785進口物料總量=V水冷器出+L水冷器出= 10532NM3氨分出口氣相和液相是水冷器后分離開的，固然組成和水冷器的時候一致氨分還有一部分用去調節系統氣體成分的放空氣V放空氣=228NM3成分表為氨分出口放空 氣組分物料量NM3NH30.09350874821.31999458CH40.167580553

17、38.20836612Ar0.0114958882.621062358H20.523040817119.2533062N20.20521144746.78820995合22812、冷交二入二出物料衡算冷交二入的物料總量為氨分出口氣相減去放空氣的量 冷交二入物料量=10060.98-228NM3=9832.98NM3冷交二入成分物料量NM3NH30.093508748919.4696505CH40.1675805531647.816228Ar0.011495888113.0388322H20.5230408175143.049888N20.2052114472017.840056合9832.98

18、冷交而出工況：出口溫度15攝氏度，壓力28Mpa,查表有此時的平衡氨含量為5.9%，過飽和度為1.1則為6.5%假設二出的氨量為A NM3A/(9832.98-919.469+A)=0.0649得到 A=618.645NM3氣體從二入到二出的過程中冷凝的氨=919.46-618.645=300.82NM3冷交二出氣相物料量NM3氣相組分液相物料量NM3NH3618.64508330.064844842300.8245672CH41647.8162280.1727200050Ar113.03883220.011848450H25143.0498880.5390817190N22017.84005

19、60.2115049840合9540.3900871300.824567213、氨冷器物料衡算進入氨冷器的物料氣相量為冷交二出氣體和補入新鮮氣液相為冷交二出液相量進氨冷器物料表氨冷器進口成分氣相物料量NM3氣相組分液相物料量NM3NH3618.64508330.064844842300.8245672CH41647.8162280.1727200050來源冷Ar113.03883220.011848450交二出H25143.0498880.5390817190N22017.8400560.2115049840合9540.3900871300.8245672NH3000CH442.2850.01

20、50來源補Ar14.0950.0050入氣體H22071.9650.7350N2690.6550.2450合281910NH3618.64508330.050054661300.8245672CH41690.1012280.1367463290己Ar127.13383220.0102864160總、計H27215.0148880.5837678750N22708.4950560.2191447180合12359.390091300.8245672氫氮比二0.583767/0.219144=2.6638氨冷器進口物料總量二12359.39+300.8245=12660.21NM3出口氣體中氣態氨

21、含量為2.5%假設氨冷器出口氨量為A NM3則有A/(12359-618.645)=0.025有 A=293.53有氨冷器出口物料表氨冷器出口氣相物料NM3組分液相物料NM3NH3293.53036580.024391196625.9392846CH41690.1012280.1404406310Ar127.13383220.0105643110H27215.0148880.599538790N22708.4950560.2250650720合12034.275371625.9392846氨冷器出口氨含量為2.439%出口物料總量二12034.27+625.939=12660.21NM314、

22、冷交一入一出物料衡算冷交一入物料為氨冷器出口物料量冷交一入氣相物料NM3組分液相物料NM3NH3293.53036580.024391196625.9392846CH41690.1012280.1404406310Ar127.13383220.0105643110H27215.0148880.599538790N22708.4950560.2250650720合12034.275371625.9392846進入冷交之后，有部分的氨在冷交內冷凝留在液相中 冷交一出一入冷交放氨平衡方程L出+V出二一入總量 注：l為冷交內液相，V為冷交一出氣相L出yNH3+V出xNH3二入總量乘以氨含量冷交二出的總

23、氨量=293.53+625.93=919.47NM3冷交一入總物料=12340.27+625.939=12660.21NM3冷交一入氨含量=919.47/12660.21=0.07262一出物料表冷交一出氣相%NM3/tNH3NM3/hKmol/hNH3 0.025285.1394277.085190.9413CH4 0.1451653.80624807.091107.46Ar 0.01114.05561710.83476.37652H2 0.5956786.308101794.64544.403N2 0.2252566.25138493.761718.472合11405.5615、球罐物料衡

24、算核算氨產171083.47637.652馳放氣中的氨為93.68*0.5972=55.94球罐中氨為1009.569702NM3氨分至球罐液相物料NM3冷交至球罐液相物料NM3471.0200067625.9392846氨分出組分物料量NM3NH30.954172537449.434355CH40.0204394859.62740635Ar0.000407850.19210542H20.0190285038.96280555N20.0059516252.80333438合1471.020007冷交出組分物料量NM3NH30.984251969616.081973CH40.005370373.

25、36152579Ar0.0001960780.12273319H20.0079333334.96578499N20.00281251.76045424合1625.939285總氨量16、物料衡算匯總表1065.516328女右計山 I /口乂 LU /口%NM3/tNH3NM3/hKmol/h.%NM3/tNH3NM3/hKmol/hNH30.02439293.530374402.95549196.56051 .NH30.02500285.139004277.08498190.94129CH40.140441690.1012325351.518411131.76421 .CH40.145001

26、653.8061924807.092891107.45950Ar0.01056127.133831907.0074885.13426 .Ar0.01000114.055601710.8339976.37652H20.599547215.01489108225.223324831.48318 .H20.595006786.30817101794.622574544.40279N20.225072708.4950640627.425841813.72437 I.N20.225002566.2509938493.764841718.47164合1.0000012034.27537180514.130

27、548058.66654 .k11405.55995171083.399287637.65175合成塔一入合成塔二出%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH30.02500296.300004444.50000198.41518 .NH30.132001390.2240020853.36000930.95357CH40.145001718.5400025778.100001150.80804 .CH40.161001695.6520025434.780001135.48125Ar0.01000118.520001777.8000079.36607 .

28、Ar0.01100115.852001737.7800077.57946H20.595007051.94000105779.100004722.28125 I.H20.500505271.2660079068.990003529.86563N20.225002666.7000040000.500001785.73661 I.N20.196302067.4316031011.474001384.44080合1.0000011852.00000177780.000007936.60714 .k1.0008010532.00000157980.000007052.67857水冷器出口氣相水冷器出口液

29、相%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH30.09351940.7896514111.84468629.99307 I.NH30.95417449.434356741.51532300.96051CH40.167581686.0245925290.368901129.03433 .CH40.020449.62741144.411106.44692Ar0.01150115.659891734.8984277.45082 .Ar0.000410.192112.881580.12864H20.523045262.3031978934.547923523.

30、86375 .H20.019038.96281134.442086.00188N20.205212064.6282730969.423981382.56357 I.N20.005952.8033342.050021.87723合1.0008410060.98000150914.700006737.26339 .卜1.00000471.019687065.29518315.41496氨分出口氣相放空氣%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH30.09351940.7896514111.84468629.99307 I.NH30.0935121.3199

31、9319.7999214.27678CH40.167581686.0245925290.368901129.03433 .CH40.1675838.20837573.1254925.58596Ar0.01150115.659891734.8984277.45082 .Ar0.011502.6210639.315941.75518H20.523045262.3031978934.547923523.86375 .H20.52304119.253311788.7995979.85712N20.205212064.6282730969.423981382.56357 I.N20.2052146.78

32、821701.8231531.33139合1.0008410060.98000150914.700006737.26339 .卜1.00084228.000003420.00000152.67857氨分出口液相冷交二入%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH30.95419449.441216741.61814300.96510 .NH30.09351919.4696513792.044761209.82849CH40.020449.62624144.393546.44614 .CH40.167581647.8162324717.243412168.

33、17925Ar0.000410.192022.880260.12858 .Ar0.01150113.038831695.58248148.73531H20.019028.95880134.381935.99919 .H20.523045143.0498977145.748326767.17091N20.005952.8017542.026231.87617 .N20.205212017.8400630267.600842655.05270合1.00000471.020017065.30010315.41518 .卜9832.98000147494.7000012938.13158冷交二出氣相冷

34、交二出液相%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH30.06484618.645089279.67625414.27126 .NH31.00000300.824574512.36851201.44502CH40.172721647.8162324717.243411103.44837 CH40.000000.000000.000000.00000Ar0.01185113.038831695.5824875.69565 .Ar0.000000.000000.000000.00000H20.539085143.0498977145.748323444.0

35、0662 I.H20.000000.000000.000000.00000N20.211502017.8400630267.600841351.23218 .N20.000000.000000.000000.00000合1.000009540.39009143105.851316388.65408 .卜1.00000300.824574512.36851201.44502冷交出口液氨氨冷器進口氣相%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH30.98425616.081979241.22960412.55489 .NH30.05005618.645089

36、279.67625414.27126CH40.005373.3615350.422892.25102 .CH40.136751690.1012325351.518411131.76421Ar0.000200.122731.841000.08219 .Ar0.01029127.133831907.0074885.13426H20.007934.9657874.486773.32530 .H20.583777215.01489108225.223324831.48318N20.002811.7604526.406811.17888 .N20.219142708.4950640627.425841813.72437合1.00000625.939289389.08927419.15577 .p1.0000012359.39009185390.851318276.37729氨冷器進口液相球罐進口液相%NM3/tNH3NM3/hKmol/h%NM3/tNH3NM3/hKmol/hNH31.00000300.824574512.36851201.44502 .NH30.971021065.5163315982.74492713.51540CH40.000000.000000.000000.00000