6-1、附錄一物料平衡計(jì)算書(shū)

1、目錄12總論111223334556777999111111121214161616算的方法 方程式物2.12.22.3物算的基準(zhǔn)工藝流程圖3各工段物算 3.1 丙烷脫氫工段3.1.13.1.2丙烷脫氫工段流程圖丙烷脫氫工段物算分離精制工段分離精制工段流程圖3.2.2 分離精制工段物算羰基羰基羰基工段工段流程圖工段物算3.4 異構(gòu)物分離工段3.4.13.4.2異構(gòu)物分離工段流程圖異構(gòu)物分離工段物算3.5 醇醛縮合工段3.5.13.5.2醇醛縮合工段流程圖醇醛縮合工段物算3.6 加氫精餾工段3.6.13.6.2加氫精餾工段辛烯醛加氫精餾工段4主要設(shè)備物算 4.1 反應(yīng)器4.1.1 丙烷反應(yīng)器（R

2、-104）4.1.24.1.34.1.4選擇性加氫反應(yīng)器（R-201）1718202122222325羰基反應(yīng)器（R-302）醇醛縮合反應(yīng)器（R-501）兩相分離器塔設(shè)備-202）4.3.14.3.24.3.3丙烯精餾塔（T異構(gòu)物分離塔（T-402）辛醇預(yù)蒸餾塔（T-603）1 總論物算是以質(zhì)量守恒定律為基礎(chǔ)對(duì)物料平衡進(jìn)行計(jì)算，在工藝設(shè)計(jì)中，物算是在工藝流程確定后進(jìn)行的。其在確定項(xiàng)目生產(chǎn)工藝及流程后，通過(guò)對(duì)整個(gè)生產(chǎn)系統(tǒng)、部分重要的生產(chǎn)單元進(jìn)行物算計(jì)算出主、副產(chǎn)品的產(chǎn)量、原材料的消耗、生產(chǎn)過(guò)程中各階段的消耗量以及產(chǎn)品收率等各項(xiàng)經(jīng)濟(jì)技術(shù)指標(biāo)，進(jìn)而定量地評(píng)價(jià)初步設(shè)計(jì)所選擇的的工藝路線在技術(shù)及經(jīng)濟(jì)上的

3、合理性，為后續(xù)的熱量、其他工藝計(jì)算及設(shè)備計(jì)算打下基礎(chǔ)。2 物算的方法2.1方程式對(duì)一般的體系而言，物料分布均可表示為：（物料的累積率）=（物料進(jìn)入率）-（物料流出率）+（反應(yīng)生成率）-（反應(yīng)消耗率）特別地，當(dāng)系統(tǒng)沒(méi)有化學(xué)反應(yīng)時(shí)，則可簡(jiǎn)化為：（物料的累積率）=（物料進(jìn)入率）-（物料流出率）在穩(wěn)定狀態(tài)下有：（物料進(jìn)入率）=（物料流出率）物算包括總質(zhì)量、組分和元素。各種方法的適用情況如下：表 2-1物算的適用范圍由于項(xiàng)目過(guò)程中存在化學(xué)反應(yīng)故主要采用總質(zhì)量方法，主要采用總質(zhì)量的方法，同時(shí)列出每種組分的質(zhì)量流量以便于查找和計(jì)算。類別物算形式無(wú)化學(xué)反應(yīng)有化學(xué)反應(yīng)總式總質(zhì)量式適用適用總物質(zhì)的量式適用不適用組

4、分式組分質(zhì)量式適用不適用組分物質(zhì)的量式適用不適用元素原子式元素原子質(zhì)量式適用適用2.2 物算的基準(zhǔn)1、對(duì)于間歇式操作的過(guò)程，常采用一批原料為基準(zhǔn)進(jìn)行計(jì)算。2、對(duì)于連續(xù)式操作的過(guò)程，可以采用時(shí)間產(chǎn)品數(shù)量或原料量為基準(zhǔn)進(jìn)行計(jì)算。物算的結(jié)果應(yīng)列成原材料消耗及消耗量表。3、消耗是指以每年或是指每噸產(chǎn)品或以一定量的產(chǎn)品所消耗的原材料量；而消耗量等時(shí)間所消耗的原材料量。4、制劑車間的消耗起算入。及消耗量計(jì)算時(shí)應(yīng)把原料、輔料及主要包裝材料一物算的主要任務(wù)如下：1、保證主要產(chǎn)品丁辛醇質(zhì)量合格。2、確定對(duì)環(huán)境有危害的工業(yè)三廢的含量，并確定處理措施。3、各主要單元過(guò)程的物算，并指導(dǎo)工藝設(shè)備的尺寸確定。4、匯總?cè)?/p>

5、程物算，數(shù)據(jù)用于完成物料流程圖等后續(xù)設(shè)計(jì)任務(wù)。2.3 工藝流程圖本項(xiàng)目用丙烷、氣為原料，Pta/SAPO-34（硅磷鋁系列的分子篩）催化劑、三苯基膦氯化銠催化劑、固體堿Ca/Al2O3 催化劑、Cu-Zn-Al催化劑等等為輔助原料，設(shè)計(jì)年產(chǎn) 46 萬(wàn)噸丁辛醇，整個(gè)工藝流程由丙烷脫氫工段、分離精制工段、羰基工段、異構(gòu)物分離工段、醇醛縮合工段、加氫精餾工段六個(gè)工段組成。圖 2-1工藝流程示意圖3 各工段物算3.1 丙烷脫氫工段3.1.1 丙烷脫氫工段流程圖圖 3-1丙烷脫氫工段流程圖3.1.2 丙烷脫氫工段物算表 3-1消耗表 3-2相關(guān)物理化學(xué)常數(shù)其余物性數(shù)據(jù)選用 AspenplusV8.0 中

6、自帶的物性數(shù)據(jù)庫(kù)和整合的企業(yè)數(shù)據(jù)庫(kù)。以 AspenPlus8.0 的模擬數(shù)據(jù)為依據(jù)得到的物算的結(jié)果詳見(jiàn)下表：（注：下列表格中0.001 表示 10-310-6；TRACE 表示痕量級(jí) 10-610-9）表 3-3丙烷脫氫工段流股物料模擬結(jié)果ItemsInputOutputXSJC3H8H2ORECYCLE1C-H2OF1Temperature/25253021.52525Prere/bar1.51.51.58.51.51.5Vapor Frac110001Mole Flow kmol/hr5105980097.722766.0012339.249Mass Flow kg/hr10.079466

7、14.0514412.224221.09213799.7451457.71Volume Flow cum/hr82.70817093.2519.1389.06318.2638463.52Enlpy MMBtu/hr0.001-105.119-218.698-11.67-209.71815.038Mole Flow kmol/hr名稱數(shù)值摩爾氣體常數(shù)R=8.31433J/（molK）標(biāo)準(zhǔn)大氣壓1atm=101.325Kpa伽常數(shù)N=6.0220451023mol-1冰點(diǎn)溫度0=275.15K標(biāo)準(zhǔn)狀態(tài)下氣體摩爾體積（275.15K，101.325Kpa）V=22.4138310-3m3/mol消耗

8、噸/年丙烷370000.0Pta/SAPO-34 催化劑（硅磷鋁系列的分子篩）23.17表 3-4丙烷脫氫工段物算表3.2 分離精制工段3.2.1 分離精制工段流程圖圖 3-2分離精制工段流程圖Mass-flow kg/hrSummationInput65257.448Output65257.449Rel.diff-1.53239E-08C3H801053094.13344.45E-06108.8393C2H60601.75E-271.94E-065.763574H25004.52E-973.77E-051101.863CH400001.13E-0546.66489C3H60000.12123

9、70.000158933.4191C3H40000.1168820.00046158.44755C2H40002.93E-401.19E-070.234642C2H20005.63E-290.00027946.6664H2O008003.35007476637.350083.2.2 分離精制工段物算表 3-5分離精制工段流股物料模擬結(jié)果表 3-6 分離精制工段物算Mass-flow kghrSummationInput51578.665ItemsInputOutputF1H2SIS2FLH2T201-DRECYCLE1C3H6Temperature/252540-146.8-146.8-51.

10、521.58.2Prere/bar1.51211.2101098.57.5Vapor Frac1100.0091101Solid Frac00000000Mole Flowkmol/hr2339.249603421.471091.888.20697.7221007.726Mass Flowkg/hr51457.71120.953612.52364.7292200.9381818.2634221.09242361.123Volume Flowcum/hr38463.52124.8730.8191.0611150.696165.3889.0632721.604EnlpyGcal/hr3.790.0

11、01-2.335-0.414-1.2671.853-2.9413.967Mole Flow kmol/hrC3H8108.8393000.05542402.58E-1094.133414.65049C2H65.763574000.05874405.5777311.75E-270.1270994H21101.8636000.2555671091.89.80784.52E-971.675677CH446.664890020.07277026.5921200C3H6933.4191000.69314306.04E-080.121237990.9291C3H458.44755000.00634306.

12、48E-150.1168821.81E-09C2H40.234642000.00597600.2286642.93E-401.16E-06C2H246.6664000.322245046.000115.63E-290.3440509H2O37.350080347.87E-0603.47E-283.3500741.58E-263.3 羰基工段3.3.1 羰基工段流程圖圖 3-3羰基工段流程圖3.3.2 羰基工段物算表 3-7羰基工段流股物料模擬結(jié)果ItemsInputOutputC3H6RECYCLE4SJCHJT301-DRECYCLE3T301-WTemperature/8.233.3251

13、201014020.8Prere /bar7.51019184.81.44.9Vapor Frac1110100Solid Frac0000000Mole Flow kmol/hr1007.72641.5262087.8665154.806673.2081033.276Mass Flow kg/hr42361.121723.61430103.29174423.41542.853.56Volume Flow cum/hr2721.60491.5652748.36966.942760.60668.313107.977Enlpy Gcal/hr3.967-0.479-26.28441.84-1.04

14、142.712-56.548Output51578.665Rel.diff0.000表 3-8羰基工段物算表Mass-flow kg/hrSummationInput248611.444Output248611.374Rel.diff2.81564E-07Mole Flow kmol/hrC3H814.6504922.19871002.9368740.00575348.28498C2H60.1270990.155481000.0916641.32E-050.190884H21.6756771.1708761091.80114.54832.24E-051.175397CH40000000C3H6

15、990.929116.65887002.2156470.0050630.14362C3H41.81E-094.80E-11009.36E-111.79E-121.76E-09C2H41.16E-067.07E-07001.05E-065.78E-118.11E-07C2H20.3440510.47289000.2434467.36E-050.573315H2O1.58E-261.06E-07000.0182040.3435811.44184CO00.863857995032.251139.06E-060.87315C4H8O-105.88E-15002.1672987.353795875.46

16、27C4H8O-209.12E-15000.23560.29762373.4308C18H15P0006651.43E-09664.85330.146656C5H10O200005.27E-060.3488171.547054C8H14O0000000C8H18O0000000C4H10O-10000000C4H10O-20000000O200.005205100.0980962.22E-070.0052963.4 異構(gòu)物分離工段3.4.1 異構(gòu)物分離工段流程圖圖 3-4異構(gòu)物分離工段流程圖3.4.2 異構(gòu)物分離工段物算表 3-9異構(gòu)物分離工段流股物料模擬結(jié)果ItemsInputOutputT

17、301-WRECYCLE4L4T402-DT403-WC4-1C4-2Temperature/20.833.3-3.583.355.731.931.9Prere bar4.91051.80.20.20.2Vapor Frac0101011Solid Frac0000000Mole Flow kmol/hr1033.27641.52633.904105.3632.557149.927699.999Mass Flow kg/hr72089.561723.6141466.4467355.247258.75410810.7750474.78Volume Flowcum/hr107.97791.5652

18、.9061654.4640.32818849.2688005.96Enlpy Gcal/hr-56.548-0.479-0.611-5.072-0.243-7.389-34.499Mole Flow kmol/hrC3H848.2849822.1987120.875355.2119975.21199700表 3-10異構(gòu)物分離工段物算表Mass-flow kg/hrSummationInput72089.561Output72089.606Rel.diff-6.24224E-07C2H60.1908840.1554810.0354051.11E-091.11E-0900H21.1753971.

19、1708760.00452109.99E-3100CH40000000C3H630.1436216.6588712.879160.60552020.6055200C3H41.76E-094.80E-117.11E-111.64E-091.64E-0900C2H48.11E-077.07E-071.04E-0702.12E-1700C2H20.5733150.472890.1004491.48E-091.48E-0900H2O1.441841.06E-076.07E-071.4418391.44183900CO0.873150.8638570.00929701.61E-2600C4H8O-187

20、5.46275.88E-153.45E-1324.88496875.4627149.8895699.8244C4H8O-273.43089.12E-154.12E-1373.2188173.43080.0373950.174597C18H15P0.146656001.74E-1460.1466562.69E-651.26E-64C5H10O21.547054004.76E-721.5470542.11E-159.86E-15C8H14O0000000C8H18O0000000C4H10O-10000000C4H10O-20000000O20.0052960.0052059.08E-0502.8

21、8E-25003.5 醇醛縮合工段3.5.1 醇醛縮合工段流程圖圖 3-5醇醛縮合工段流程圖3.5.2 醇醛縮合工段物算表 3-11醇醛縮合工段流股物料模擬結(jié)果ItemsInputOutputC4-2C-INH-OUTWATERE502-OUTTemperature/31.925112.725150Prere bar0.2550.56Vapor Frac10000Solid Frac00000Mole Flow kmol/hr699.999500500335.466364.533Mass Flow kg/hr50474.789007.649007.646043.51444431.26Volum

22、e Flow cum/hr88005.9611.91912.8427.99777.196EnlpyGcal/hr-34.499-34.495-33.583-23.145-18.203Mole Flow kmol/hrC3H800000表 3-12醇醛縮合工段物算表3.6 加氫精餾工段3.6.1加氫精餾工段1加氫精餾工段流程圖Mass-flow kg/hrSummationInput59482.415Output59482.413Rel.diff3.36234E-08C2H600000H200000CH400000C3H600000C3H400000C2H400000C2H200000H2O05

23、00500335.4669.197541CO00000C4H8O-1699.8244001.58E-0610.49736C4H8O-20.174597001.73E-080.174597C18H15P1.26E-640000C5H10O29.86E-150000C8H14O0001.65E-13344.6635C8H18O00000C4H10O-100000C4H10O-200000O200000圖 3-6加氫精餾工段流程圖2加氫精餾工段物算表 3-13加氫精餾工段流股物料模擬結(jié)果ItemsInputOutputH2-1T402-DC4-1T601-DT602-DS102C4H10O-1Tem

24、perature/15083.331.9123.47682.485.1Prere/bar51.80.250.30.30.3Vapor Frac1111110Solid Frac0000000Mole Flow kmol/hr235105.363149.92726.26557.514.5158.478Mass Flow kg/hr473.7327355.24710810.771559.4194258.7911074.67411746.866Volume Flow cum/hr1657.5921654.46418849.26160.5185502.8951413.38117.684Enlpy Gc

25、al/hr0.204-5.072-7.389-1.131-3.773-0.938-11.826Mole Flow kmol/hrC3H805.21199705.211997000C2H60.00E+001.11E-0901.11E-09000H2235001.453211000CH40000000C3H600.6055200.6055202000C3H40.00E+001.64E-0901.64E-09000表 3-14加氫精餾工段物算表3.6.2 辛烯醛加氫精餾工段1辛烯醛加氫精餾工段流程圖Mass-flow kg/hrSummationInput18639.749Output18639.7

26、50Rel.diff-5.36488E-08C2H40000000C2H20.00E+001.48E-0901.48E-09000H2O01.44183901.4418391.13E-073.23E-098.90E-36CO0000000C4H8O-1024.88496149.88951.8647451.5789960.0517473.81E-18C4H8O-2073.218810.03739510.943940.0431850.0013065.79E-25C18H15P0.00E+001.74E-1462.69E-650000C5H10O20.00E+004.76E-722.11E-1500

27、00C8H14O0000000C8H18O0000000C4H10O-10000.31556493.3861969.783443157.7938C4H10O-20004.42802152.491624.6635040.6845962O20000000圖 3-7辛烯醛加氫精餾工段流程圖2辛烯醛加氫精餾工段物算表 3-15辛烯醛加氫精餾工段流股物料模擬結(jié)果ItemsInputOutputE502-OUTH2-2V6T603-DT604-WC8H18OTemperature/.8123.4123.3Prere bar66610.10.1Vapor Frac011101Solid Frac000000

28、Mole Flow kmol/hr364.53372035.32821.1810.069343.942Mass Flow kg/hr44431.2591451.43478.3881014.3588.9644780.99Volume Flow cum/hr77.1964234.211153.847650.1020.014112631.3Enlpy Gcal/hr-18.2030.626-0.01-1.071-0.006-27.422Mole Flow kmol/hrC3H8000000C2H6000000H2072035.093950.892832800CH4000000表 3-16辛烯醛加氫精

29、餾工段物算表4 主要設(shè)備物算4.1 反應(yīng)器4.1.1 丙烷反應(yīng)器（R-104）表 4-1R-104 流股物料模擬結(jié)果ItemsInputOutputR103-OUTR104-OUTTemperature/630630Mass-flow kg/hrSummationInput45882.693Output45882.693Rel.diff0.000C3H6000000C3H4000000C2H4000000C2H2000000H2O9.19754100.1779429.0195991.24E-767.28E-09CO000000C4H8O-110.4973600.04814510.386267.

30、65E-582.82E-05C4H8O-20.174596500.0011470.17344911.29E-652.80E-08C18H15P000000C5H10O2000000C8H14O344.663500.0002120.04120087.73E-152.646962C8H18O000.0065470.60493650.068802341.2949C4H10O-1003.92E-050.0628481.79E-434.45E-05C4H10O-2000000O2000000表 4-2R-104 流股物算表4.1.2 選擇性加氫反應(yīng)器（R-201）表 4-3R-201 流股物料模擬結(jié)果I

31、temsputOutputR201-INH2T202-INTemperature/26.72550Prere bar251228Mass-flow kg/hrSummationInput50845.2253Output50845.2253Rel.diff0.000Prere bar1.51.5Vapor Frac11Solid Frac00Mole Flow kmol/hr2209.0982305.25Mass Flow kg/hr50845.2350845.23Volume Flow cum/hr110653115468.5Enlpy Gcal/hr25.16528.215Mole Flow

32、 kmol/hrC3H8196.107108.839C2H65.8225.764H21009.6341101.863CH442.74346.665C3H6854.977933.419C3H453.54558.448C2H40.1770.235C2H242.74446.667H2O3.353.35表 4-4R-201 流股物算表4.1.3 羰基反應(yīng)器（R-302）表 4-5R-302 流股物料模擬結(jié)果ItemsputOutputE302-OUTR302-OUTTemperature/200100Prere bar17.217.2Mass-flow kghrSummationInput46582.

33、215Output46582.215Rel.diff0.000Vapor Frac010Solid Frac000Mole Flow kmol/hr1103.772601105.448Mass Flow kg/hr46461.26120.95346582.22Volume Flow cum/hr98.605124.873113.067Enlpy Gcal/hr0.0370.001-1.413Mole Flow kmol/hrC3H8108.78390108.7839C2H60.12709900.127099H21.67E-30601.675677CH43.50E-1500C3H6932.726

34、0991.0503C3H458.4412100.116882C2H41.16E-0601.16E-06C2H20.34405100.344051H2O3.35007303.350073表 4-6R-302 流股物算表Mass-flow kghrSummationVapor Frac0.6760.122Solid Frac00Mole Flow kmol/hr2140.8421861.29Mass Flow kg/hr248611.4248611.4Volume Flow cum/hr3120.067570.225Enlpy Gcal/hr6.661-12.976Mole Flow kmol/h

35、rC3H849.506151.2276C2H60.2825620.282562H2256.6361115.7237CH400C3H6172.150732.36433C3H41.86E-091.86E-09C2H41.86E-061.86E-06C2H20.8168350.816835H2O1.4360071.803625CO171.947533.12429C4H8O-1758.3506884.9838C4H8O-263.2906873.96402C18H15P665665C5H10O21.1375261.895876C8H14O00C8H18O00C4H10O-100C4H10O-200O20

36、.2872020.1033934.1.4 醇醛縮合反應(yīng)器（R-501）表 4-7R-501 流股物料模擬結(jié)果ItemsputOutputC4-2R501-OUTTemperature/31.9120Prere bar0.25Vapor Frac10Solid Frac00Mole Flow kmol/hr699.999699.999Mass Flow kg/hr50474.7850474.78Volume Flow cum/hr88005.9688.272Enlpy Gcal/hr-34.499-40.072Mole Flow kmol/hrC3H800C2H600H200CH400C3H60

37、0C3H400C2H400C2H200H2O0344.6635CO00C4H8O-1699.824410.49737C4H8O-20.1745970.174597Input248611.374Output248611.374Rel.diff0.000表 4-8R-501 流股物算表4.2 兩相分離器本項(xiàng)目中的兩相分離器主要為氣液分離器（F-601）。該氣液分離器的流股物流模擬結(jié)果見(jiàn)下表：表 4-9F-601 流股物料模擬結(jié)果ItemsputOutputE604-OUTV6T603-INTemperature/404040Prere bar666Vapor Frac0.08810Solid Fr

38、ac000Mole Flow kmol/hr400.5235.328365.192Mass Flow kg/hr45882.6978.38845804.3Volume Flow cum/hr220.31153.84766.464Enlpy Gcal/hr-35.042-0.01-35.033Mole Flow kmol/hrC3H8000Mass-flow kghrSummationInput50474.775Output50474.775Rel.diff0.000C18H15P1.26E-640C5H10O29.86E-150C8H14O0344.6635C8H18O00C4H10O-100

39、C4H10O-200O200表 4-10F-601 流股物算表4.3 塔設(shè)備4.3.1 丙烯精餾塔（T-202）表 4-11T-202 流股物料模擬結(jié)果ItemsInputOutputMass-flow kg/hrSummationInput45882.6921Output45882.6921Rel.diff0.000C2H6000H235.9867835.093950.892833CH4000C3H6000C3H4000C2H4000C2H2000H2O9.1975410.1779429.019599CO000C4H8O-110.434430.04814510.38629C4H8O-20.1

40、745970.0011470.173449C18H15P000C5H10O2000C8H14O2.6883750.0002122.688163C8H18O341.97510.006547341.9686C4H10O-10.0629323.92E-050.062893C4H10O-2000O2000表 4-12T-202 流股物算表4.3.2 異構(gòu)物分離塔（T-402）表 4-13T-402 流股物料模擬結(jié)果ItemsputOutputMass-flow kghrSummationInput46582.2158Output46582.2154Rel.diff8.94279711e-09T202-

41、INC3H6RECYCLE1Temperature/508.221.5Prere bar287.58.5Vapor Frac010Solid Frac000Mole Flow kmol/hr1105.4481007.72697.722Mass Flow kg/hr46582.2242361.124221.092Volume Flow cum/hr113.0672721.6049.063Enlpy Gcal/hr-1.4133.967-2.941Mole Flow kmol/hrC3H8108.783914.6504994.1334C2H60.1270990.1270991.75E-27H21.6756771.6756774.52E-97CH4000C3H6991.0503990.92910.121237C3H40.1168821.81E-090.116882C2H41.16E-061.16E-062.93E-40C2H20.3440510.3440515.63E-29H2O3.3500731.58E-263.350074T403-INT402-402-DTem