CN102810128A - Design calculation method for single-strand spiral wound heat exchanger - Google Patents

Design calculation method for single-strand spiral wound heat exchanger Download PDF

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Publication number
CN102810128A
CN102810128A CN2012102978151A CN201210297815A CN102810128A CN 102810128 A CN102810128 A CN 102810128A CN 2012102978151 A CN2012102978151 A CN 2012102978151A CN 201210297815 A CN201210297815 A CN 201210297815A CN 102810128 A CN102810128 A CN 102810128A
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pipe
formula
heat
shell
layer
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张周卫
汪雅红
张小卫
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Abstract

A design calculation method for a single-strand spiral wound heat exchanger is for the heat exchange process design computational process of a single-strand spiral wound heat exchanger, and comprises the following four main heat exchange process calculation processes: velocity calculation of the tube side of the single-strand spiral wound heat exchanger, velocity calculation of the shell side of the single-strand spiral wound heat exchanger, total heat-transfer coefficient calculation of the single-strand spiral wound heat exchanger and pressure calibration. The design calculation method can be used in the technical fields of -161 DEG C rock gas low-temperature liquification, -197 DEG C air low-temperature liquification and separation, -197 DEG C low-temperature liquid nitrogen washing process, -70 DEG C low-temperature methanol washing process and other gas low-temperature purification and low-temperature liquification and separation. Together with the heat exchange process calculation result and the inlet and outlet parameters, the basic structure and pipeline arrangement method of wound tubes can be determined, the total heat-transfer coefficient, the total heat-transfer area, the effective heat exchange height, the pressure loss and other important parameters of the wound heat exchanger can be simply and quickly calculated, and the integral design process of the spiral wound heat exchanger is facilitated.

Description

Sub-thread stream spiral winding pipe formula design of heat exchanger computing method
Technical field
The present invention relates to a kind of sub-thread stream spiral winding pipe formula design of heat exchanger computing method; Be mainly used in the low-temperature gas liquefaction separation field, comprise that the liquefaction of-161 ℃ of natural gas in low temperature ,-197 ℃ of air low temperature liquefaction separate ,-197 ℃ of low temperature liquid nitrogens are washed technology ,-70 ℃ of gas low temperatures such as low-temp methanol washing process purify, the low-temperature liquefaction separation technology field.
Background technology
Sub-thread stream spiral winding pipe formula heat interchanger is a kind of single tube bundle helical disk cast heat-exchange apparatus that a kind of heat exchange pipeline forms after twining layer by layer; Mainly support critical pieces such as (5) constitutes under (2), tube bank (3), core tube (4), the tube bank by supporting in housing (1), the tube bank; For most basic sub-thread stream heat interchanger in the wrap-round tubular heat exchanger, be mainly used in the heat transfer process that there is big temperature difference fluids in tube side.Sub-thread stream spiral winding pipe formula heat interchanger is with its compact conformation; Unit volume has bigger heat transfer area; The thermal expansion of heat-transfer pipe can compensate voluntarily; Realize easily maximizing, can reduce advantage such as table of equipment number and become the visual plant in low temperature purification, the liquefaction process such as natural gas liquefaction, cryogenic air separation, low-temperature rectisol.Because spiral winding pipe formula heat interchanger is applied to low temperature environment mostly, volume is bigger, and generally the form with the heat transfer tower occurs; Can reach seven, 80 meters, general heat interchanger is also at two, 30 meters, and internal pipeline twines complicated; There is not general design criterion; Do not have unified heat-exchanging process design and calculation method yet,, brought difficulty therefore for spiral winding pipe formula heat interchanger standardisation process along with technological process or physical parameter characteristics are different and exist than big difference.In addition,, do not have unified pipeline winding pattern and Design Theory computing method to be used for the computer aided calculation process, brought obstacle for the scientific computing process of spiral winding pipe formula heat interchanger because spiral winding pipe formula heat exchanger tube (3) winding method is a lot.Be standardization and the science computational problem that solves spiral winding pipe formula heat interchanger better; The present invention has provided a kind of simple and direct design and calculation method of sub-thread stream spiral winding pipe formula heat interchanger from most basic sub-thread stream spiral winding pipe formula heat interchanger heat-exchanging process designing and calculating.
Summary of the invention
Sub-thread stream spiral winding pipe formula design of heat exchanger computing method comprise that mainly the tube side flow velocity calculates, the shell side flow velocity calculates, overall heat transfer coefficient is calculated and pressure is checked four main processes; After the tube side flow velocity calculate to be accomplished,, confirm to twine tube bank (3) basic parameter, totally manage radical and overall pipe root aligning method according to known given design parameter; Housing (1) intensity computation process can be with reference to existing national standard design such as GB150, GB151.
Technical solution of the present invention:
1, the tube side flow velocity calculates
Comprise calculated population number of tubes such as heat exchanging fluid flow, out temperature, inlet and outlet pressure, design temperature, design pressure, pipeline material and specification according to the Known designs parameter
n=G i /[3600 πρv i( d i/2) 2]
In the formula:
n---number of tubes;
G i---mass rate in the pipe, kg/s;
ρ---fluid density, kg/m 3
v i---tube fluid flow velocity, m/s;
d i---internal diameter of the pipeline, m;
Confirm helical pipe specification, radial layer spacing, tube axial spacing and pitch; Confirm core tube (4) diameter and arrange pipeline layer by layer around core tube (4) by arithmetic progression; Ground floor row arranges second layer pipeline with the reverse acting spiral ascending angle in full back; Second layer row of conduits completely back is arranged the 3rd layer with the transport screw ascending angle; The 3rd layer of row of conduits completely arranged the 4th layer with the reverse acting spiral ascending angle in the back ... Positive reciprocal permutation to the i layer; Supply and form whole tube bank (3) by arithmetic progression when i layer row is discontented; Again number of tubes and according to statistical magnitude in the statistics tube bank (3) nRecomputate velocity in pipes
v i ?=G i /[3600 πρ i n?( d i/2) 2]
Be used to calculate overall heat transfer coefficient;
2, the shell side flow velocity calculates
The shell side total cross-sectional area
A Always= π( D/ 2) 2
In the formula:
D---housing (1) internal diameter, m 2
Core tube (4) total cross-sectional area
A Core= π( d Core/ 2) 2
In the formula:
d Core---core tube (4) external diameter, m 2
The pipeline gross section A PipeBe each layer of pipeline projected area sum vertically, promptly
A Pipe= A Layer 1+ A Layer 2+ A Layer 3 A Layer (n-1)- A Layer n
The arbitrary layer of pipeline is projected area vertically
A Layer i=π ( D Layer i+ d 0/ 2) 2/ 4-π ( D Layer i- d 0/ 2) 2/ 4
In the formula:
D Layer i---i layer pipe layers diameter, m;
d 0---outer diameter tube, m;
The circulation gross section
A Shell= A- A Pipe- A Core
The shell-side mass rate
G 0= v 0 ρ 0 A Shell
In the formula:
G 0---shell-side mass rate, kg/s;
ρ 0---shell fluid density, kg/m 3
v 0---shell fluid flow velocity, m/s;
The shell-side flow velocity
v 0 =G 0 /(3600 ρ 0 A Shell)
Can be used for calculating overall heat transfer coefficient;
3, overall heat transfer coefficient is calculated
Manage outer Reynolds number
Re 0v 0 ρ 0 d 0 0
In the formula:
μ 0---manage outer viscosity coefficient, Pa.s;
Manage outer convection transfer rate
h ?0=0.297( λ 0/ d 0)Re 0.609Pr 0.3
In the formula:
h 0---shell-side convection transfer rate, W/ (m 2K);
λ 0---shell fluid coefficient of heat conductivity, W/ (mK);
Manage outer Prandtl number
Pr 0μ 0 C p 0
In the formula:
C p---specific heat at constant pressure, kJ/kg;
The intraductal heat transfer coefficient
h i=0.038( λ i /d i)(Re 0.75-180)Pr 0.42
In the formula:
h i---pipe side convection transfer rate, W/ (m 2K);
λ i---pipe side liquid coefficient of heat conductivity, W/ (mK);
Reynolds number in the pipe
Re iv i ρ i d i i
In the formula:
ρ i---tube fluid density, kg/m 3
v i---tube fluid flow velocity, m/s;
d i---internal diameter of the pipeline, m;
μ i---viscosity coefficient in the pipe, Pa.s;
Prandtl number in the pipe
Pr iμC p/ λ i
Overall heat transfer coefficient
K=1/{1/ h 0+1× d 0/( d i× h i)+ R 0+ R i d 0/ d i+ δd 0/( λd m)}
In the formula:
K---overall heat transfer coefficient, W/ (m 2K);
δ---duct thickness, m;
R i---sealing factor in the pipe, (m 2K)/W;
R 0---manage outer sealing factor, (m 2K)/W;
Total heat transfer
Q=C p mΔ t
In the formula:
Q---total heat transfer, W;
m---mass rate, kg/s;
Δ t---the temperature difference, K;
Total heat conduction area by
Q=KΔ t m ?A
In the formula:
Δ t m---log-mean temperature difference, K;
Calculate
A=Q/KΔ t m
Every pipe range
L=A/( πd 0 n)
The effective heat exchange height of heat interchanger
HLsin α
In the formula:
α---the spiral coil ascending angle;
Effectively heat exchange does not highly comprise end socket, bobbin carriage, adapter and skirt equal altitudes;
4, pressure is checked
Shell pressure check according to
Δ P 0≤0.125 P od?[σ 0]/?[σ 0] t
In the formula:
P Od---shell-side design pressure, MPa;
0]---shell-side permissible stress under the test temperature, MPa;
0] t---shell-side permissible stress under the design temperature, MPa;
Δ P 0---shell pressure loss, MPa;
Check; Work as Δ P 0Reduce the shell-side flow velocity when losing and calculate Δ according to the calculating of sub-thread stream spiral winding pipe formula heat interchanger shell-side flow velocity, the calculating of sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger, sub-thread stream spiral winding pipe formula heat interchanger Calculation of pressure loss step again greater than the shell-side allowable pressure P 0Press v oThe 0.1m/s speed of at every turn successively decreasing double counting is until Δ P 0Lose less than the shell-side allowable pressure; According to the given cross-flow coil pipe computing formula of Gilli
Δ P 0=0.337 C t C i C n nG 2/(2 g c ρ 0)
In the formula:
ρ 0---the density of shell fluid, kg/m 3
Δ P 0---shell pressure loss, kg/m 2
n---the pipe row number (writhing number of each root heat-transfer pipe) of flow direction;
C i---heat-transfer pipe inclination (winding angle of heat-transfer pipe coil pipe) correction factor;
C i=(cos β) -1.81(cos φ) 1.356
In the formula:
β---fluid flow direction and axially between angle;
βα×(1- α/90°)(1- K 0.25)
φαβ
K---tube bank (3) performance mumber that the coil pipe layer is made into, twine a tubing heat exchanger left side and twine and twine the coil pipe layer with the right side and hand over and mend when arranging, K=1, therefore β=0 only twine by a left side right or in the heat exchanger formed of any one winding direction coil pipe, K=0;
φ---the angle between fluid actual flow direction and the heat-transfer pipe Z-axis;
C n---pipe row number correction factor;
C n=0.9524(1+0.375/ n)
C t---pipe is arranged correction factor;
C t=( C in-line+ C staggerd)?/2;
In the formula:
C In-line---the correction factor during in upright arrangement the layout;
C Staggerd---the correction factor when regular stagger arrangement is arranged;
The pipe wall pressure check according to
Δ P i≤0.125 P id?[σ i]/?[σ i] t
In the formula:
P Id---pipe side design pressure, MPa;
i]---pipe side permissible stress under the test temperature, MPa;
i] t---pipe side permissible stress under the design temperature, MPa;
Δ P i---the loss of pipe wall pressure, MPa;
Check; Work as Δ P iReduce to manage effluent speed when losing and also calculate Δ according to the calculating of sub-thread stream spiral winding pipe formula Tube Sheet of Heat Exchanger effluent speed, the calculating of sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger, sub-thread stream spiral winding pipe formula heat interchanger Calculation of pressure loss step again greater than pipe side allowable pressure P iAccording to v iThe 0.1m/s speed of at every turn successively decreasing double counting is until Δ P iLess than the loss of pipe side allowable pressure; According to the given coil pipe internal pressure loss computing formula of Schmidt
Δ P i =f i G i 2 ?nl?/(2 g c ρ i d i)
f i=0.3164?[1+(28800/Re i)( d i /d m) ?0.62]?/Re i 0.25
In the formula:
Δ P i---the loss of pipe inside pressure, kg/m 2
ρ i---the density of side liquid in the pipe, kg/m 3
l---heat transfer pipe range, m;
g c---gravity reduction coefficient 1.27 * 10 8M/ h 2
f i---friction factor.
Sub-thread stream spiral winding pipe formula heat exchanger shell (1) and other accessory can carry out designing and calculating with reference to design standardss such as GB150, GB151.
The problems of principle that scheme is related:
Sub-thread stream spiral winding pipe formula heat interchanger is mainly used in low-temperature gas liquefaction to be separated and the gas purification field; Like technical fields such as gas low temperature purification, low-temperature liquefaction separation such as natural gas in low temperature liquefaction, air low temperature liquefaction separation, low-temperature rectisols; So have the low-temperature heat exchange characteristic, be calculating in the present cryogenic high pressure heat transmission equipment, design, heat interchanger that manufacture difficulty is bigger.The present invention uses thermal conduction study and principles of fluid mechanics; A kind of sub-thread stream spiral winding pipe formula heat interchanger heat-exchanging process design and calculation method has been proposed; And through experimental verification and basic engineering parameter makeover process; Can be applicable to complicated process of mathematical modeling of twining tube bank (3); And building mathematical model and corresponding three-dimensional physical model be applied to the Calculation of Heat Transfer process of spiral winding pipe formula heat interchanger, and obtain spiral winding pipe formula heat interchanger complicated tube bank (3) structural parameters and relevant heat transfer model, design whole spiral winding pipe formula heat interchanger with this; Make spiral winding pipe formula heat interchanger that a definite method for designing arranged, help the standardisation process of spiral winding pipe formula heat interchanger.
Technical characterstic of the present invention:
Through four step rule is that sub-thread stream spiral winding pipe formula heat interchanger tube side velocimeter is calculated, sub-thread stream spiral winding pipe formula heat exchanger shell pass flow velocity calculates, sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger calculates and sub-thread stream spiral winding pipe formula heat interchanger pressure is checked four main processes; Simplify spiral winding pipe formula heat interchanger technology Calculation process, obtain sub-thread stream low temperature spiral winding pipe formula heat exchanger tube (3) model and winding arrangement Parameter of Overall Design; The complete sub-thread stream wrap-round tubular heat exchanger heat-exchanging process computation model of one cover is proposed; Can the winding method that sub-thread flows spiral winding pipe formula heat interchanger be applied to modeling process; And with institute's established model and the corresponding three-dimensional physical model technology Calculation process that is applied to conduct heat; Obtain sub-thread stream spiral winding pipe formula heat exchanger tube (3) and twine model and process calculation model; Design whole sub-thread stream spiral winding pipe formula heat interchanger with this, make sub-thread stream spiral winding pipe formula heat interchanger that definite design and calculation method arranged.
Description of drawings
Shown in Figure 1 is that sub-thread flows spiral winding pipe formula heat interchanger critical piece pie graph.
Winding tube bank 3-D solid structure sketch for sub-thread stream spiral winding pipe formula heat interchanger shown in Figure 2.
Embodiment
According to known import and export parameter, confirm heat exchange pipeline material and size, suppose the pipeline fluid flow velocity; Calculate heat exchange pipeline quantity, according to the selected core tube (4) of number of tubes, by confirming that good tube pitch, interlamellar spacing and winding angle twine; Guarantee in the winding process that number of tubes increases progressively by arithmetic progression from inside to outside between layer and the layer; And when end layer number of tubes is not enough,, accomplish the whole pipe winding process by waiting difference to supply; According to the overall number of tubes of supplying after last layer, inverse pipeline fluid flow velocity; Twine mathematical model according to the tube bank of having built up (3), calculate the shell-side fluid flow velocity; According to tube side fluid flow velocity and shell-side fluid flow velocity, calculate overall heat transfer coefficient and total heat conduction area, confirm the effective heat exchange height of heat interchanger; Check the pipeline fluid and the shell-side fluid pressure loss,, accomplish the The whole calculations process if the calculating pressure loss is then supposed pipe flow speed again greater than the allowable pressure loss, until the calculating pressure loss less than the allowable pressure loss for extremely; After the heat transfer technology Calculation is accomplished, carry out housing (1) intensity according to prior art again and calculate; Calculate and intensity computation process in conjunction with heat-exchanging process, accomplish the design calculation process of whole sub-thread stream spiral winding pipe formula heat interchanger.

Claims (5)

1. sub-thread stream spiral winding pipe formula design of heat exchanger computing method comprise that sub-thread stream spiral winding pipe formula heat interchanger tube side velocimeter is calculated, sub-thread stream spiral winding pipe formula heat exchanger shell pass flow velocity calculates, sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger calculates and sub-thread stream spiral winding pipe formula heat interchanger pressure is checked four main heat-exchanging process computation processes.
2. according to claim 1Described sub-thread stream spiral winding pipe formula heat interchanger tube side velocimeter is calculated process, it is characterized in that:
Comprise calculated population number of tubes such as heat exchanging fluid flow, out temperature, inlet and outlet pressure, design temperature, design pressure, pipeline material and specification according to the Known designs parameter
n=G i /[3600 πρv i( d i/2) 2]
In the formula:
n---number of tubes;
G i---mass rate in the pipe, kg/s;
ρ---fluid density, kg/m 3
v i---tube fluid flow velocity, m/s;
d i---internal diameter of the pipeline, m;
Confirm helical pipe specification, radial layer spacing, tube axial spacing and pitch; Confirm core tube (4) diameter and arrange pipeline layer by layer around core tube (4) by arithmetic progression; Ground floor row arranges second layer pipeline with the reverse acting spiral ascending angle in full back; Second layer row of conduits completely back is arranged the 3rd layer with the transport screw ascending angle; The 3rd layer of row of conduits completely arranged the 4th layer with the reverse acting spiral ascending angle in the back ... Positive reciprocal permutation to the i layer; Supply and form whole tube bank (3) by arithmetic progression when i layer row is discontented; Again number of tubes and according to statistical magnitude in the statistics tube bank (3) nRecomputate velocity in pipes
v i ?=G i /[3600 πρ i n?( d i/2) 2]
Be used to calculate overall heat transfer coefficient.
3. according to claim 1Described sub-thread stream spiral winding pipe formula heat exchanger shell pass flow velocity computation process is characterized in that:
The shell side total cross-sectional area
A Always= π( D/ 2) 2
In the formula:
D---housing (1) internal diameter, m 2
Core tube (4) total cross-sectional area
A Core= π( d Core/ 2) 2
In the formula:
d Core---core tube (4) external diameter, m 2
The pipeline gross section A PipeBe each layer of pipeline projected area sum vertically, promptly
A Pipe= A Layer 1+ A Layer 2+ A Layer 3 A Layer (n-1)- A Layer n
The arbitrary layer of pipeline is projected area vertically
A Layer i=π ( D Layer i+ d 0/ 2) 2/ 4-π ( D Layer i- d 0/ 2) 2/ 4
In the formula:
D Layer i---i layer pipe layers diameter, m;
d 0---outer diameter tube, m;
The circulation gross section
A Shell= A- A Pipe- A Core
The shell-side mass rate
G 0= v 0 ρ 0 A Shell
In the formula:
G 0---shell-side mass rate, kg/s;
ρ 0---shell fluid density, kg/m 3
v 0---shell fluid flow velocity, m/s;
The shell-side flow velocity
v 0 =G 0 /(3600 ρ 0 A Shell)
Can be used for calculating overall heat transfer coefficient.
4. according to claim 1Described sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger computation process is characterized in that:
Manage outer Reynolds number
Re 0v 0 ρ 0 d 0 0
In the formula:
μ 0---manage outer viscosity coefficient, Pa.s;
Manage outer convection transfer rate
h ?0=0.297( λ 0/ d 0)Re 0.609Pr 0.3
In the formula:
h 0---shell-side convection transfer rate, W/ (m 2K);
λ 0---shell fluid coefficient of heat conductivity, W/ (mK);
Manage outer Prandtl number
Pr 0μ 0 C p 0
In the formula:
C p---specific heat at constant pressure, kJ/kg;
The intraductal heat transfer coefficient
h i=0.038( λ i /d i)(Re 0.75-180)Pr 0.42
In the formula:
h i---pipe side convection transfer rate, W/ (m 2K);
λ i---pipe side liquid coefficient of heat conductivity, W/ (mK);
Reynolds number in the pipe
Re iv i ρ i d i i
In the formula:
ρ i---tube fluid density, kg/m 3
v i---tube fluid flow velocity, m/s;
d i---internal diameter of the pipeline, m;
μ i---viscosity coefficient in the pipe, Pa.s;
Prandtl number in the pipe
Pr iμC p/ λ i
Overall heat transfer coefficient
K=1/{1/ h 0+1× d 0/( d i× h i)+ R 0+ R i d 0/ d i+ δd 0/( λd m)}
In the formula:
K---overall heat transfer coefficient, W/ (m 2K);
δ---duct thickness, m;
R i---sealing factor in the pipe, (m 2K)/W;
R 0---manage outer sealing factor, (m 2K)/W;
Total heat transfer
Q=C p mΔ t
In the formula:
Q---total heat transfer, W;
m---mass rate, kg/s;
Δ t---the temperature difference, K;
Total heat conduction area by
Q=KΔ t m ?A
In the formula:
Δ t m---log-mean temperature difference, K;
Calculate
A=Q/KΔ t m
Every pipe range
L=A/( πd 0 n)
The effective heat exchange height of heat interchanger
HLsin α
In the formula:
α---the spiral coil ascending angle;
Effectively heat exchange does not highly comprise end socket, bobbin carriage, adapter and skirt equal altitudes.
5. according to claim 1Described sub-thread stream spiral winding pipe formula heat interchanger pressure is checked computation process, it is characterized in that:
Shell pressure check according to
Δ P 0≤0.125 P od?[σ 0]/?[σ 0] t
In the formula:
P Od---shell-side design pressure, MPa;
0]---shell-side permissible stress under the test temperature, MPa;
0] t---shell-side permissible stress under the design temperature, MPa;
Δ P 0---shell pressure loss, MPa;
Check; Work as Δ P 0Reduce the shell-side flow velocity when losing and calculate Δ according to the calculating of sub-thread stream spiral winding pipe formula heat interchanger shell-side flow velocity, the calculating of sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger, sub-thread stream spiral winding pipe formula heat interchanger Calculation of pressure loss step again greater than the shell-side allowable pressure P 0Press v oThe 0.1m/s speed of at every turn successively decreasing double counting is until Δ P 0Lose less than the shell-side allowable pressure; According to the given cross-flow coil pipe computing formula of Gilli
Δ P 0=0.337 C t C i C n nG 2/(2 g c ρ 0)
In the formula:
ρ 0---the density of shell fluid, kg/m 3
Δ P 0---shell pressure loss, kg/m 2
n---the pipe row number (writhing number of each root heat-transfer pipe) of flow direction;
C i---heat-transfer pipe inclination (winding angle of heat-transfer pipe coil pipe) correction factor;
C i=(cos β) -1.81(cos φ) 1.356
In the formula:
β---fluid flow direction and axially between angle;
βα×(1- α/90°)(1- K 0.25)
φαβ
K---the performance mumber of the tube bank that the coil pipe layer is made into, twine a tubing heat exchanger left side and twine and twine the coil pipe layer with the right side and hand over and mend when arranging, K=1, therefore β=0 only twine by a left side right or in the heat exchanger formed of any one winding direction coil pipe, K=0;
φ---the angle between fluid actual flow direction and the heat-transfer pipe Z-axis;
C n---pipe row number correction factor;
C n=0.9524(1+0.375/ n)
C t---pipe is arranged correction factor;
C t=( C in-line+ C staggerd)?/2;
In the formula:
C In-line---the correction factor during in upright arrangement the layout;
C Staggerd---the correction factor when regular stagger arrangement is arranged;
The pipe wall pressure check according to
Δ P i≤0.125 P id?[σ i]/?[σ i] t
In the formula:
P Id---pipe side design pressure, MPa;
i]---pipe side permissible stress under the test temperature, MPa;
i] t---pipe side permissible stress under the design temperature, MPa;
Δ P i---the loss of pipe wall pressure, MPa;
Check; Work as Δ P iReduce to manage effluent speed when losing and also calculate Δ according to the calculating of sub-thread stream spiral winding pipe formula Tube Sheet of Heat Exchanger effluent speed, the calculating of sub-thread stream spiral winding pipe formula total exchange coefficient of the heat exchanger, sub-thread stream spiral winding pipe formula heat interchanger Calculation of pressure loss step again greater than pipe side allowable pressure P iAccording to v iThe 0.1m/s speed of at every turn successively decreasing double counting is until Δ P iLess than the loss of pipe side allowable pressure; According to the given coil pipe internal pressure loss computing formula of Schmidt
Δ P i =f i G i 2 ?nl?/(2 g c ρ i d i)
f i=0.3164?[1+(28800/Re i)( d i /d m) ?0.62]?/Re i 0.25
In the formula:
Δ P i---the loss of pipe inside pressure, kg/m 2
ρ i---the density of side liquid in the pipe, kg/m 3
l---heat transfer pipe range, m;
g c---gravity reduction coefficient 1.27 * 10 8M/ h 2
f i---friction factor.
CN2012102978151A 2012-08-21 2012-08-21 Design calculation method for single-strand spiral wound heat exchanger Pending CN102810128A (en)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101338984A (en) * 2008-08-08 2009-01-07 西安交通大学 Spiral traverse baffle shell type heat exchanger design method
CN102261968A (en) * 2011-06-14 2011-11-30 南京工业大学 Method and device for predicting node temperature of shell and tube heat exchanger

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101338984A (en) * 2008-08-08 2009-01-07 西安交通大学 Spiral traverse baffle shell type heat exchanger design method
CN102261968A (en) * 2011-06-14 2011-11-30 南京工业大学 Method and device for predicting node temperature of shell and tube heat exchanger

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102999707A (en) * 2012-12-07 2013-03-27 张周卫 Low-temperature methanol-methanol winding tubular heat exchanger design and calculation method
CN103148732A (en) * 2013-03-26 2013-06-12 牛玉振 Gas/liquid-phase fluid uniform distribution device of high-pressure wound-tube type heat exchanger
CN104748612A (en) * 2013-12-31 2015-07-01 中国石油天然气股份有限公司 Method and device for acquiring structural size of spiral baffle heat exchanger
CN104748612B (en) * 2013-12-31 2017-04-12 中国石油天然气股份有限公司 Method and device for acquiring structural size of spiral baffle heat exchanger
CN106196613B (en) * 2016-07-25 2019-10-01 青岛新奥清洁能源有限公司 A kind of hot-water boiler blowdown cool-down method and system
CN106196613A (en) * 2016-07-25 2016-12-07 新奥泛能网络科技股份有限公司 A kind of hot-water boiler blowdown cool-down method and system
CN107704645A (en) * 2016-08-09 2018-02-16 林德股份公司 Determine the method and its manufacture method of the intensity of tube-bundle heat exchanger
CN109614712A (en) * 2018-12-12 2019-04-12 东北大学 A kind of spiral winding tube type heat exchanger HEAT EXCHANGE ANALYSIS system
CN110852564A (en) * 2019-10-09 2020-02-28 天津大学 Comprehensive performance evaluation method for movable internal combustion engine flue gas waste heat exchanger
CN110765645A (en) * 2019-11-06 2020-02-07 国网四川省电力公司电力科学研究院 Design method of built-in coil type compressed air heat exchange system
CN110765645B (en) * 2019-11-06 2023-05-23 国网四川省电力公司电力科学研究院 Design method of built-in coil type compressed air heat exchange system
CN112611252A (en) * 2021-01-11 2021-04-06 曹雁青 Running diagnosis method and system for circulating water system
CN113190924A (en) * 2021-03-26 2021-07-30 内蒙古中煤蒙大新能源化工有限公司 Modeling and scaling analysis method and system for circulating water system of coal chemical industry enterprise
CN113190924B (en) * 2021-03-26 2024-01-23 中煤鄂尔多斯能源化工有限公司 Modeling and scaling analysis method and system for circulating water system of coal chemical industry enterprise

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Application publication date: 20121205