容器设备常用计算表

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压力容器体积计算

手写输入手写输入手写输入标准椭圆形封头该值为2
验证设备长度双椭圆封头设备容积 1.999545857
手写输入手写输入手写输入
L=
2000.053
封头其它相关计算
封头直边段高度 h1 直边段容积椭圆封头内容积（包括直边段）椭圆形周长计算椭圆形面积计算 mm 立方米立方米 mm L=2π b+4(a-b) 平方毫米 s=π ab V=π aa*h1 25.00 0.03 0.25 3769.80 1130940.00
无折边锥形封头计算
封头直边段高度 h1 大直边段容积圆锥角小圆锥半径封头厚度大圆椎半径大圆椎高度小圆椎高度小直边段容积平截圆锥体容积(阴影部分) 大圆椎侧表面积 mm mm mm mm mm R H h mm 立方米 V=π *R*R*h1 α r 25.00 0.0283 30.00 25.00 8.00 600.00 1039.27 43.30 0.0000 0.39 2261946.71
带双折边锥形封头相关计算
带双折边锥形封头容积带双折边锥形封头表面积带双折边锥形封头重量(碳钢) 带双折边锥形封头重量(不锈钢) 立方米平方毫米 kg kg 0.42 2356194.48 147.97 148.91
椭圆形封头+双折边锥形封头容器容积V
椭圆形封头+双折边锥形封头容器容积V 2.17
椭圆形封头容器的体积计算
压力容器直径Di（内径）长径比椭圆封头a值椭圆封头b值椭圆封头深度h值（不包括直边段）椭圆体体积公式设备容积 a:长半轴长度 h：椭圆体的高 b：短半轴长度且a>b>0 L/d （d=Di） Di/2h 毫米毫米毫米立方米立方米 a=Di/2 b=Di/2 h=Di/C4/2 V=4/3π abh v=4/3π abh+π aaL 椭圆形封头长短轴比值毫米 1200.00 1.14 2.00 600.00 600.00 300.00 0.45 2.00

容器支腿计算

设备的水平力 FH(N)=Max( P1,Fk1)+Fh'
垂直地震影响系数α vmax=0.65 αmax
0.00
支腿系数tg θ=3/8*Do/h
593.78 5256.21
水平弯距引起垂直力 FL1(N)=FH/2 tgθ
垂直最大受拉力 FL(N)=FL1+ Fv/n-W/nFv'/n
63.91 158.79
地震影响系数衰减系数γ =0.9+(0.05ξ)/(0.5+5ξ)
设备水平地震力 Fk1(N)=α1*η k1*W*g
当量质量 meq(Kg)=0.75*W
设备垂直地震力 (N)Fv0-0=α vmax*meqg
单根支腿的水平反力 Q(N)=FH/n
垂直最大受压力 FY(N)=max(FL1+(F v+W+Fv')/n,Wt/n)
输入数据筒体长度H(mm)
设备外径Do(mm)
设备质量W(kg) 支腿底板到设备重心距离h(mm) 底板到支腿与壳体焊接支腿类型
支腿周向截面的惯性矩x I1(mm4)
支腿截面积 AT(mm2)
壳体外壁到支腿重心处的距离 e(mm)
支腿的弹性模量 E(MPa)
支腿材料的许用拉弯应力[σ]b,MPa
支腿与壳体焊缝剪力τ (Mpa)=max(FY/Aw 1,FL/Aw1) 焊接接头弯曲应力σ=QLw1/Zw1 支腿与底板焊缝剪力τ(Mpa)
0.37
底板计算厚度,δb （mm） =a0(3B/[σ])
0.5
4749.55
地脚螺栓根径 db （mm）
14.04 σB≤[σ]
0.00

容器支座计算

1、计算条件容器设计压力p=0.6MPa 容器壳设计温度t=50℃设计温度下材质许用应σ]=容器筒体内直径Di=2800mm 容器总高度Ho= 容器筒体名义厚度δn=12mm 支撑高度/支座底板离地面厚度附加量C=C1+C2=1mm 支座底板到壳体质心壳体保温层厚度δt=0mm 偏心载荷Ge= 操作状态下设备总质量mo=35000kg 偏心距Se=2、水平风载荷实取风载作用外直径D0=2824mm考虑到公式计算值可能不全面风载作用外设置地区10m高度处的基本风压qo=550N/m2 查GB50009 壳体质心距地面高度H t=附录E中表E.5风载荷Pw=12114.96N 风压高度变化3、水平地震力重力加速度g=9.81m/s2 地震载荷Pe= 地震影响系数a=0.24按表20选取水平载荷P=4、支座承受载荷选用支座型号:A1JB/T4712.3表3～表5支座数量n= 支座的筋板和底板材料:Q235A 支座本体允许载荷[Q]=250KN不均匀系数k= b2=280mm计算支座安装尺寸D = l2=300mm 查JB/T4712.3表3～表5s1=130mm实际支座安装尺寸D =δ3=14mm 支座实际承受=5、支座处圆筒所受支座弯矩校核(带垫板支座)支座载荷校设计温度下筒体材料许用应力[σ]=113mm支座处圆筒所受的支座筒体有效厚度δe=11mm 由此查找[ML]设计压力p=0.6MPa 壳体许用弯矩[ML]=支座处圆筒所受的支座弯矩校支座尺寸容器壳体材质:Q235B许用应力[σ]=113MPa 查许用应力表容器总高度Ho=6500mm离地面高度H=5000mm体质心距离h=1500mm偏心载荷Ge=10000N偏心距Se=2000mm作用外直径D0=2824mm体质心距地面高度H t=6500mm 按此值及地面类别选取系数fi 度变化系数fi=1按Ht及地面类别查表22地震载荷Pe=82404N水平载荷P=85432.74N支座数量n=4一般为4个,承受静力载荷,直径≤700mm的容器可以采用2个不均匀系数k=0.83支座安装尺寸D=3178.222mm支座安装尺寸D=3178mm际承受载荷Q=153.0478KN载荷校核结论:合格!的支座弯矩ML=26.01813KN.m用弯矩[ML]=37.34KN.m 以[σ]、δe、p查JB/T4712.3附录B中表B.1～B.4并采用内插法弯矩校核结论:合格!内插法公式：X1=0.8 Y1=0.026968X=0.866667 Y=0.032675X2=0.9 Y2=0.035529。

矩形容器计算(ABCDE型通用)V1.1

设计压力，MPa 常压加固柱型号HW300X300X12X12设计温度，℃50加固柱截面系数，cm³1115容器长L，mm 10000加固柱间距L p，mm450容器宽W，mm 6000型钢和宽度W方向水平布置，底板型钢支撑实际跨距，mm200容器高H，mm 8000加固圈型号等边角钢50X50X5型钢材料Q235A 加固圈惯性矩，cm411.21壁板材料Q235A 顶边加固件型号等边角钢50X50X5设温壁板材料许用应力[σ]t，MPa 135顶边加固件惯性矩，cm411.21常温型钢许用应力[σ]b，MPa135介质名称水材料弹性模量E t，MPa 191000介质密度ρ，Kg/m31000顶板加强筋型号等边角钢100X100X12顶板加强筋沿L方向上的间距A=L T，mm200钢板负偏差C1，mm0.8钢材密度ρM=，Kg/m³7850顶板加强筋截面系数，cm³29.48顶板加强筋沿W方向上的间距B=W T，mm200腐蚀裕量C2， mm2底板厚度δbn，mm8拉杆近似直径，m m 26.2211623拉杆直径，mm加速度g，N/Kg9.81顶板名义厚度δT ，mm4实际的加固圈数量及各段间距H1，mm H2，mm H3，mm H4，mm H5，mm H6，mm4250016001500130011000推荐的加固圈数量及各段间距H1H2H3H4H5H61480032000000 2360024002000000 3296020001680136000 4248016801440128011200各段壁板厚度δin，mm 101618181801.设计条件示意图。

压力容器设计常用计算表格╱常用金属材料的比重参考表

8.9
55-3-1锰黄铜
8.5
0.6白铜
8.9
59-1-1铁黄铜
8.5
5白铜
8.9
58-1-1铁黄铜
8.5
19白铜
8.9
80-3硅黄铜
8.6
30白铜
8.9
65-5镍黄铜
8.65
3-12锰白铜
8.4
4-3锡青铜
8.8
40-1.5锰白铜
8.9
4-4-2.5锡青铜
8.75
40-0.5锰白铜
8.9
4-4-4锡青铜
8.8
77-2B铝黄铜
8.6
3.5-3-1.5硅铁青铜
8.8
67-2.5铝黄铜
8.5
1.5锰青铜
8.8
60-1-1铝黄铜
8.4
5锰青铜
8.6
59-3-2铝黄铜
8.4
1.0镉青铜
8.8
66-6-3-2铝黄铜
8.5
0.5铬青铜
8.9
58-2锰黄铜
8.5
0.2锆青铜
8.9
57-3-1锰黄铜
8.5
0.4锆青铜
常用金属材料的比重参考表
名称或牌号
密度g/cm3
名称或牌号
密度g/cm3
灰口铸造
6.6～7.4
锰脱氧铜
8.89
白口铸造
7.4～7.7
96黄铜
8.85
可锻铸造
7.2～7.4
90黄铜
8.73
工业纯铁
7.87
85黄铜
8.7
钢材
7.85
80黄铜
8.66
铸钢
7.8
68黄铜
8.5

压力容器设计常用计算表格设备重量估算

总重
0
材料密度
7.93
0
7.93
0
7.93
0
7.93
0
7.93
7.35
15
7.93
0.00 ☆★☆★☆ ☆★☆★☆
0
7.85
△▲△
△▲△
1986
单重
150
总重
总重
0 600
15 备注
0
0
0 顶部板式 13.7 27.4 侧壁板式
0 轴式
导程h
75
盘管密度
7.85
盘管壁厚
3.2
279.0
672
1100
80
160
80
93
180
100
112
200
125
137
250
150
163
300
200
223
400
250
277
480
300
329
550
350
391
620
400
430
680
450
484
760
500
534
840
600
634
980
w=0.7854* (D^2d2^2)*s*7 .85/10^6
计算：
单重
0.0 0.0 0.0 0.00 0.00
项目名
设计项目：
类别序号名称
1 壳体-1
2 壳体-2
3 壳体-3
壳
4 底板 5 顶板
直径壁厚
长度
数量
体
6 椭圆封头-1 250
10
2
7 椭圆封头-2 8 变径段

注册化工工程师必备-常压容器设备筒体强度及补强计算书自动计算-带计算公式

t
简图
0 997 10 1860 0.019 0.019 80 1500 06Cr19Ni10 137 137 130 0.3 0 0.85 壁厚计算
Mpa kg/m3 N/kg mm Mpa Mpa ℃ mm Mpa Mpa Mpa mm mm
Di
δ
碳钢低合金钢≥ 不锈钢≥ 0.13 0.3 2.30 6 5.7 液压试验时应力效核
0.38 4.56 4.94 8 3.44 液压试验时应力效核 0.08 0.05 16.58 179.78 可行压力计算
mm mm mm mm mm Mpa Mpa Mpa Mpa
液压试验压力（取较大值）
0.075858696
试验压力下封头的应力 σT=PT(Di+δe)/2δe= 许用值 σT≤0.9φReL σT≤0.9φReL
常压容器设备强度计算书
内压圆筒体 (NB/T47003.1-2009) 单位
P ρ g h ρgh PC t Di ReL [σ] [σ] C1 C2 φ
t
设计条件
设计压力物料密度重力加速度液面高度液注静压力计算压力 P+ρgh 设计温度筒体内径筒体材料试验温度下屈服强度常温下材料许用应力设计温度下材料许用应力钢板厚度负偏差腐蚀裕量焊接接头系数壳体最小厚度 min (mm) （不包括腐蚀裕量）计算厚度 δ = Pc Di / 2 [σ] φ=
最大允许设计压力[P]=2 [σ]t φ δhe / K Dhi=
0.36
Mpa
设计温度下圆筒计算应力许用值 σ≤φ[σ]t σ≤φ[σ]t
盛水试验时应力效核 σ=PcDi/2δhe 8.69 78.2 可行

常压设备计算

0.85
193000.0
MPa
第 2 页，共 8 页
二、设计依据标准。 DESIGN STANDA RD
*《钢制焊接常压容器》
NB/T 47003.12《00S9TEEL WELDE D ATMOSP HERIC PRESSU RE VESSEL S》
三、容器顶板厚度 VESSEL TOP PLATE THICKN ESS
第二道横向加固件距顶边距离
SECOND TRANSVERSE REINFORCEMENT DISTANCE FROM THE TOP EDGE
第一道加固圈单位长度上载荷
LOAD PER UNIT LENGTH ON FIRST TRANSVERSE REINFORCEMENT
第一道加固圈所需惯性矩
ACTUAL INERTIA MOMENT OF FIRST TRANSVERSE
Gi
容器主体材质 VESSEL MATERIAL
主体材质的材料屈服极限 MATERIAL YIELD
S
设计温度下材料的许用应力 ALLOWABLE STRESS
OF MATERIAL FOR DESIGN TEMPERATURE
[σ]t
设计温度下材料的许用压缩应力 ALLOWABLE
COMPRESS STRESS OF MATERIAL FOR DESIGN TEMPERATURE
1）顶边加固件计算 TOP EDGE STIFFENING RIB CALCULATION
第 3 页，共 8 页
第一道横向加固件距顶边距离
FIRST TRANSVERSE REINFORCEMENT DISTANCE
h1
FROM THE TOP EDGE

压力容器封头重量重量计算表

压力容器标准椭圆封头重量计算表《JB4746-2002》
序号 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 设备名称封头位封头内径置 (mm) 4000 4000 2400 1800 1800 2000 2000 2400 2400 2400 2400 2600 2600 3200 3200 1000 1000 1500 1500 1000 1000 1800 1800 4000 4000 4000 4500 4500 5000 5000 5000 5000 6000 2700 材料密度封头坯料厚封头直边 kg/m3 度(mm) 高度(mm) 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 7850 20 20 16 12 12 12 12 12 12 12 12 12 12 12 12 14 14 14 14 26 26 54 54 36 28 24 18 20 20 18 16 18 60 40 40 40 40 40 40 40 40 40 40 40 40 40 40 40 40 40 40 40 50 50 50 50 40 40 40 40 40 40 40 40 40 80 封头总深度(mm) 1040 1040 640 0 490 490 540 540 640 640 640 640 690 690 840 840 290 290 415 415 300 300 500 500 1040 1000 1040 0 1165 0 1165 0 1290 0 1290 0 1290 0 1290 0 1540 0 755 0 新蒸汽冷凝水上封头自蒸发器下封头冷凝器上封头下封头

卧式容器计算表

0第1页共11页01020304050607080910111213141516171819202122232425262728a 29r 30r 31323334常温许用应力材料密度材料数据地脚螺栓材料许用应力地震设防烈度试验压力焊接接头系数9本文件内容为北京石油化工设计院技术成果，未经本院许可，不得转让或复制给第三方。

T h i s d o c u m e n t i s t h e p r o p e r t y o f B P D I . U n a u t h o r i z e d d i s c l o s u r e t o a n y t h i r d p a r t y o r d u p l i c a t i o n i s n o t p e r m i t t e d .许用应力1400设计基本地震加速度计算条件（一）设计温度版次计算压力100设计压力0.85校核审定审核例题设备图号13.001工程名称设备位号卧式容器计算表（JB/T4731-2005）容委会详细设计设计阶段V111E511编制170设计温度下的弹性模量7850材料密度度0.125-0.1-0.10.40g0.323452.05E+052.05E+05设计温度下的许用应力常温屈服强度0.1基本数据17016MnR圆筒材料常温弹性模量常温许用应力7140厚度附加量椭圆封头103尺寸数据一名义厚度半球形封头鞍座封头封头类型有效厚度材料碟形封头封头材料设计温度下的许用应力16MnRQ235-A.FQ235-A170n ny 0封头曲面深度6501707850[]tσ[]σ1αφTp c p pTeL R EtE sγMPa MPa MPaC ︒MPa MPa MPa MPa MPaMPa MPa[]h σ[]t hσhγMPa []saσmm mm mm mmmmheδhδhC MPa []btσ3/m kg 3/m kg ih mm。

Vessel Volumes (各种容器体积excel计算表)

1) a.b.2)3)4)5)6)7)This is especially true in the case of Hemispherical heads.head if a flush fit is required between the two inside diameters. This occurs because the required head thickness for a given design pressure is usually less than for the corresponding cylindrical section.more economical to use an ellipsoidal type.head thickness. A typical head flange length is about 1.5" to 2".Try to stay away from the immediate area of the knuckle radius with respect to locating nozzles or doing other welding, cutting or grinding. The need to locate a nozzle, insulation ring, clips or other item near the knuckle radius should be consulted with a mechanical or fabrication engineer.Be aware of the fact that the outside diameter of the cylindrical section may be bigger than that of the higher localized stresses at the knuckle radius as compared to the ellipsoidal type. The pressure rating of these heads is increased by forming the head so that the knuckle radius is made at least equal to 3times the plate thickness. For code construction, the radius should in no case be less than 6% of the inside diameter.ASME F&D heads are used for pressure vessels in the general range of from 15 to about 200 psig .Although these heads may be used for higher pressures, for pressures in excess of 200 psig it may be range of 100 psig and for most vessels designed for pressures over 200 psig. Their inside depth of dish (IDD ) is defined as half of the minor axis and is equal to 1/4 of the inside diameter of the head.Flanged and dished heads are inherently shallower (smaller IDD) than comparable ellipsoidal heads. These heads (like the ellipsoidal) are formed from a flat plate into a dished shape consisting of two radii:the "crown" radius or radius of the dish and the inside-corner radius, sometimes referred to as the "knuckle" radius. Because of the relative shallow dish curvature, ASME F&D heads are subject tohistorically expected that graduate engineers will learn this information using their own efforts.any plate rolling, longitudinal weld seam, and reducing the possibility of stress relief. Thisoption should be rejected only if required alloy, wall thickness, or diameter is not available.Own a copy of Eugene Megyesy's "Pressure Vessel Handbook " as published by Pressure Vessel Handbook Publishing Inc.; P.O. Box 35365; Tulsa, OK 74153. This is probably the most useful and These type of heads are used in preference to ASME Flanged and Dished heads for pressures in the Ellipsoidal heads are designed and fabricated on the basis of using the inside diameter as their nominal diameter.ASME F&D (also called Torispherical) heads are designed and fabricated in the USA on the basis of using the outside diameter as their nominal diameter.The following are some guidelines and experienced hints for the design and utilization of process vessels.Standard pipe caps. These are usually available off-the-shelf in carbon steel, as well as stainless,Standard seamless pipe. This is basic material that can be readily found available today. Always make this your first priority in selecting the vessel shell because of the convenience of eliminating in sizes up to 42" and in various pipe schedule thicknesses.This information is never taught nor discussed in University courses or academic circles. It has been practical engineering book ever published in the USA. It clearly belongs on every process plantengineer's desk. Study it thoroughly and your project problems will start to fade away.The straight flange that forms part of each vessel head is part of the cylindrical vessel portion and should be accounted for as such in calculating the vessel volume. These flanges vary in length depending on the Ellipsoidal 2:1 heads have, by definition, 50% of the volumetric capacity of a hemispherical head with the same internal diameter.Always try to design around existing or available standard materials such as:8)9)10)11)12) 1.2.3.4.5.6.7.as welded spherical segments. This requires more manual intensive work and results in a higher cost.Hemispherical heads are the strongest of the formed heads for a given thickness. A sphere is thestrongest known vessel shape. However, the main trade-off here is that all spheres have to be fabricated Always be cognizant of the need for vessel entry into a vessel as well as vessel internal parts such as trays, baffles, agitators, dip pipes, downcomers, separator vanes, demister pads, etc. Sometimes these items directly affect not only the height of a vessel, but also the diameter. A chemical engineer should take these factors into consideration even though they normally are not considered while doing process operations. Many times some of these nozzles are not identified early in a project and their introduction later requires costly change orders or, worse, vessel field modifications after the vessel is installed. Some of these nozzles are: manways, inspection ports, drains, cleaning (spraying) ports, auxiliary levelqualified structural or mechanical engineer should be commissioned to design this critical need.calculations and simulations. Often, if not in the majority of cases, these factors and items are thecontrolling parameters that practically establish the diameter and height of the fabricated vessel regardless of what the simulation program output states.As you consider the physical dimensions of a process vessel, always keep in mind that you must have,required vessel insulation can be applied in the field without obstructing nozzle flanges and bolts.It is always advisable for the process Chemical Engineer to participate in the specification of the ultimate insulation requirements and type since he/she are the most informed people of the temperature ranges and insulation types compatible with the vessel material, temperature, and service. Again, if this is not instrument nozzle, liquid temperature probe, sample(s) probe, top head vents, critical high and low level probes, etc. Process Chemical Engineers are the best qualified to identify this need and specify the location and size. Never expect to lift a vessel by its nozzles. Lifting lugs are required for this, and a Do not forget to allow for insulation support rings. You must allow sufficient nozzle length so that anyas a minimum, certain required nozzles built into the vessel - besides those required for basic process This Workbook was originally compiled to organize and utilize the techniques, formulas, basic data,and other information that I saved and used over the course of approximately 40 years of experience in Chemical Engineering. Users will probably find it useful for carrying out day-to-day process plant projects such as:considered initially and is found to be required later, project timing and costs will suffer due to field vessel modifications that could involve an ASME "R" stamp procedure.Calculating the location of critical liquid levels on a vessel for alarms and shutdown;Calculating the weight of a process vessel for cost estimates or foundation work;Calculating the "Line Pack", or volume content, of a piping system with fittings.There are probably more uses or applications for this Workbook, but the above should suffice to Calculating the maximum volume capacity of a vessel;Calculating the partial volumes of a vessel at different levels ("Strapping" a vessel);Calculating the required vessel size for a given partial volume;Calculating the surface area of a vessel for primer, painting and insulation purposes;computer and a spreadsheet to organize and distribute it for use and exploitation by others. I hope this helps others - especially young, striving, and determined engineers who earnestly want to do a successful and safe project.Arthur Montemayorindicate the utilitarian value of this information to a Process or Project Engineer - especially in an operating process plant in the field. Most of the basic information contained here was kept by me for years in notes, 3-ring binders, between pages of text books, in formal calculations, etc. Thanks to God for giving me the good common sense to save and document this information and for giving us the digital。

压力容器-设备通-计算软件

760
8.47 12.7 16.9
21.2
25.4 29.6 33.9 38.1 42.3
840
10.1 15.6 20.7
25.9
31.3 36.3 41.5 46.7 51.8
980
13.8 20.6 27.5
34.4
41.3 48.2 55.1 62 68.9
HG/T20592-2009法兰标准
40
1 1/2
48.0 3.50
3.84
4.25 4.58
50
2
60.0 3.50 4.88
4.50 6.16
65
2 1/2
75.5 3.75
6.64
4.50 7.88
80
3
88.5 4.00 8.34
4.75 9.81
100
4
114.0 4.00 10.85 5.00 13.44
125
5
140.0 4.50 15.04 5.50 18.24
350 按图1 2.23 3.34 4.46
5.57
6.69
7.8 8.92 10 11.1
400 中的 2.72 4.08 5.44
6.8
8.16 9.52 10.9 12.2 13.6
440 型式 3.24 4.87 6.49
8.11
9.74 11.4 13 14.6 16.2
480 确定 3.79 5.68 7.58
积
筒体封头容积
度封头坯料厚度材料负
14.4
14.3
封头成型减薄
2400
7850 8
0.25 0.85
碳钢 401.0 不锈钢 405.1

压力容器计算常用表

拉杆孔螺纹深度 L2 拉杆孔深度 L2+5
拉杆侧管板到第一块折流板距离长拉杆长度短拉杆长度
设备法兰密封面密封面处高度设备法兰厚度螺母型号螺母厚度单颗重量管板厚度
管板延长法兰厚度差螺柱长度+15 螺柱长度圆整数量单根重量螺柱总重螺母总重
S22253
25 mm
2 mm
5000 mm
0.642
求圈数换热面积管外径
中径
圈数
4 57 1200
5.925
计算根数
换热面积
管外径
2
长度
根数
500 25 1000
6366.198
`
计算盘管圈数换热面积管外径盘管圆直径
盘管圈数
0.600 32 500
求管径换热面积
圈数中径
管外径
4 6 1200
56.290
计算长度换热面积
管外径根数
盘管计算
求面积盘管外径盘管中径盘管圈数
管道
1200 6
换热面积
#VALUE!
列管计算
计算面积管外径根数长度
68 30 6250
换热面积厚度碳钢不锈钢
40.055 2.5
757.1851887 764.9017257
盘管换热面积计算面积管外径盘管圆直径盘管圈数
换热面积
26 500 5
800 mm
48 mm 2 mm 233.86 根
16 mm 22 mm 70 mm 2 mm M16 8颗
24 mm 29 mm
300 mm 4315 mm 3880 mm
FM 10.5 mm
50 mm M24

卧式容器强度计算

kK F 在横截面最低 5 5 -64.2 点处 eb2 无垫板或 L/Ra≥8 时, 垫板 F 3K6 F 6 不起 4eb2 2e2 在鞍座 -122.853 加强边角处作用 L/Ra<8 时, 时 12K 6 FRa F 6 4 e b2 L e2
MPa
6
4e re b2
F
F

2 2e2 re
3K6 F

-45.289

MPa
6
4e re b2

2 Le2 re
12 K6 FRm
MPa
L/Ra≥8 时,
6 鞍座垫板边 6 4 e b2 2 e2 -122.853272

圆筒中间处截面上的弯矩
压力试验
F L 1 2 Ra2 hi2 / L2 4 A = 5.5842e+08 MT1 4h 4 L 1 i 3L
N·mm

操作工况：
A Ra2 hi2 1 L 2 AL -3.15646411e+06 M 2 F A1 4 h 1 i 3L
MPa
MPa
全国化工设备设计技术中心站
3
过程设备强度计算书
SW6-2011
封头应力校核圆筒封头圆筒, 封头, 鞍圆筒的有效宽度无加强圈圆筒
椭圆形封头, KPc Di h 2 he 65.672 MP c Rh 碟形封头, h 2 he 半球形封头, Pc Di h 4 he [] = 0.8 [ ] = 112

支腿计算-立式容器

DN W 2t2 DB W 2 2n n 2 2
2 2
符号
名称水平风载荷计算风压高度变化系数（按设备质心所处高度选取） 10m高度处的基本风压值，容器外径，有保温时取保温层外径容器壳体总长度水平风载荷Pw=1.2fi*qo*Do*Ho*10-6 地震作用标准值计算地震影响系数设备操作质量重力加速度水平地震作用标准值Pe=ae*mo*g 载荷的确定
b B *
3* C1

Cb
【σ 】 Cb δ A.7 σ
f
支腿装配焊缝的弯曲应力
支腿装配焊缝的强度计算 σ f=R*L1/Z
Z hf1 tf1 τ A1 σ
z 1
焊缝的抗弯截面模量 Z=2*(hf1)2/6*tf1/(2)1/2 每条装配焊缝的计算长度 hf1=hf-10 焊缝的焊脚高度支腿装配焊缝的剪切应力焊缝的横截面积 τ 1=FL2/A1
c b 1 cr b
A.5 σ Db nbt Abt d1 Cbt tb 【σ A.5.1 τ
bt】
地脚螺栓的强度验算地脚螺栓的拉应力，当计算的值小于0时，其值为0
bt
bt
4F * HC 1 ( H W1 ) N * nbt * Abt Db
地脚螺栓的中心圆直径，取Db等于DB 一个支腿的地脚螺栓数一个地脚螺栓的有效截面积地脚螺栓的内径地脚螺栓腐蚀裕度地脚螺栓螺距地脚螺栓的许用拉应力，对于普通碳钢常温下的【σ 地脚螺栓的拉应力验算：σ
c
0.227 ReL
2
支腿的稳定验算：σ c≤【σ cr】支腿剪切计算 τ =FH/(N*A) 支腿的稳定验算：τ ≤【τ 】支腿的许用剪切应力【τ 】=0.6【σ 】t 支腿的弯曲计算

卧式容器三鞍座的设计和计算

1
= 0.7603
=
19 mm
=
187.5 mm
5.1.
中间支座处
支座处横截面最低点:σ 7=-kK5FB/(δ ob2)
其中: k
K5(GB150) δo 圆筒
的有效宽度,b2=1.56( Rmδo)^1/2
因为 σ7 ≤ [σ]t
5.1. 3
边支座鞍座边角处
(L-2A)/Rm≥ 8时,σ8=FA/(4δob2)3K6FA/(2δo2)
其中,K2(GB150 -89 表8-1)
因为 σ6
≤
min.([σ] t,B)
4 4.1
4.1. 1
筒体切向剪应力计算边支座处横截面上
壳体未被封头加强时 (A/Rm>0.5): τ1=K3Q/(Rm δo)
其中,Q1=q(2/3* H+A)
Q2=1/2*q*(L/ 2-A)+(MBMA)/(L/2-A)
= 因此σ10校核不需计算
200 mm
=
-39.9 MPa
因此σ9校核不需计算
=
38.7 MPa
因此σ10校核不需计算
=
内
=
15.0 MPa
=
1
= 0.0581
=
0.271
=
200 mm
对中心轴的惯性矩，Io
一个支座的加强环及有效宽度内筒体壁的组合截面积,Ao
因为靠近支座
无加强圈
=
40000 mm2
因此σ9校核不需计算
=
13.6 MPa
=
1
组合截面中心轴到加强环最远点距离，d
因为支座处无加强圈

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424 55.418
重量计算
长度不锈钢
4500 2159.58
长度碳钢
1000 53.23
厚度不锈钢
8 405.06
厚度 C1 C4 不锈钢
8 0.22 0.01 385.60
板厚不锈钢
3 0.50
内径不锈钢
976 9.29
厚度不锈钢
50 55.982
板厚
板厚不锈钢直边高
直边高 C2
容积 1.55 1.60
内表面积 6.00
123
截面积
5.08938E-07
6
台计算
mm mm mm mm mm mm rad m2 kg
筒体筒体直径
碳钢
2400 2137.79
夹套
筒体直径
500
距筒端距离
100Байду номын сангаас
椭圆封头直径碳钢
标准椭圆 2400 400.97
碟形封头直径
θ(弧度) C3 碳钢
标准10:1 2400 1.11 0.04 380.27
钢管外径碳钢
57 0.49
环板外径碳钢
1096 9.20
圆板直径碳钢
总深度
长度
板厚
8
4 53.78
40
40 -0.14
505
容积表面积计算
锥台计算
容积 20.36
夹套间距 50
容积 1.99
内表面积 33.93
内表面积 6.55
板厚δ 大端内径φ2 小端内径φ1 锥台高h 斜边长a 展开长b 展开角θ 面积S 重量w
20 2000 800 2000 2200 3703.3 1.7 7.6 1193.8