CN108571905A - A kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device - Google Patents
A kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device Download PDFInfo
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- CN108571905A CN108571905A CN201810620956.XA CN201810620956A CN108571905A CN 108571905 A CN108571905 A CN 108571905A CN 201810620956 A CN201810620956 A CN 201810620956A CN 108571905 A CN108571905 A CN 108571905A
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- 239000002006 petroleum coke Substances 0.000 title claims abstract description 99
- 239000002918 waste heat Substances 0.000 title claims abstract description 82
- 238000011084 recovery Methods 0.000 title claims abstract description 81
- 230000005484 gravity Effects 0.000 claims abstract description 10
- 238000000034 method Methods 0.000 claims abstract description 10
- 239000011329 calcined coke Substances 0.000 claims description 105
- 230000000694 effects Effects 0.000 claims description 6
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 4
- 239000010962 carbon steel Substances 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 abstract description 22
- 238000009826 distribution Methods 0.000 description 28
- 238000010586 diagram Methods 0.000 description 18
- 239000002245 particle Substances 0.000 description 16
- 239000007789 gas Substances 0.000 description 13
- 239000000571 coke Substances 0.000 description 9
- 230000002708 enhancing effect Effects 0.000 description 5
- 238000005242 forging Methods 0.000 description 5
- 238000005728 strengthening Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 230000005540 biological transmission Effects 0.000 description 4
- 230000001965 increasing effect Effects 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 238000004088 simulation Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 239000003610 charcoal Substances 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 238000010025 steaming Methods 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000011868 grain product Nutrition 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
- F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F21/00—Constructions of heat-exchange apparatus characterised by the selection of particular materials
- F28F21/08—Constructions of heat-exchange apparatus characterised by the selection of particular materials of metal
- F28F21/081—Heat exchange elements made from metals or metal alloys
- F28F21/082—Heat exchange elements made from metals or metal alloys from steel or ferrous alloys
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
A kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device provided by the invention, including hopper and one group of heat-transfer pipe；It is arranged if one group of heat-transfer pipe is in dried layer from top to bottom, and adjacent layer heat-transfer pipe is staggered.The present invention also provides a kind of high temperature after-smithing petroleum coke high-grade exhaust heat recovering methods.The high temperature after-smithing petroleum coke high-grade waste-heat recovery device is of simple structure and low cost, easy to use, using gravity structure, use cooling means from inside to outside so that the temperature inside after-smithing petroleum coke is more uniformly distributed, and ensure that the quality and yield of product.
Description
Technical field
The present invention relates to charcoal element technique petroleum coke apparatus field, more particularly to a kind of high temperature after-smithing petroleum coke high-grade waste heat
Retracting device.
Background technology
Temperature is up to the high-quality waste heat of 1000 DEG C of high temperature after-smithing petroleum coke and does not obtain so far fully in charcoal element technique
It utilizes.The adjoint thermal energy of high temperature calcined coke accounts for about the 33.5% of charcoal element production total energy.In order to ensure the product matter of after-smithing petroleum coke
Amount, often so that calcined coke closing cooling, makes its outlet temperature drop to 200 DEG C or less.The companion in the production process of after-smithing petroleum coke
With the discharge of a large amount of high temperature calcined coke grain products, currently, mostly using water-cooling jacket merely to high temperature after-smithing petroleum coke greatly
Cooling is without efficiently using the partial heat；The problem of bringing simultaneously is the waste of high-grade heat source, and calcined coke cools down not
Uniformly, outlet part influences product quality because of the excessively high generation oxidative phenomena of temperature.Using to high-temperature particle water quenching cooling or nature
The mode of cooling causes the waste of high-grade heat source.
In technique, the calcined coke hopper of conventional water cooling nested structure can be adopted sometimes for the quality of guarantee calcined coke
It takes the discharge velocity for reducing calcined coke or lengthens the height dimension of water leg, after-smithing petroleum coke is extended in water leg hopper with this
The interior residence time.Although the quality of calcined coke product has reached industrial requirements as a result, high-grade high temperature calcined coke it is remaining
Thermal resource is not recycled well, and there are still a large amount of energy wastes.
Invention content
Technical problem：In order to solve the defects of prior art, the present invention provides a kind of high temperature after-smithing petroleum coke high-grades
Waste-heat recovery device.
Technical solution：A kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device provided by the invention, including hopper
And one group of heat-transfer pipe；It is arranged if one group of heat-transfer pipe is in dried layer from top to bottom, and adjacent layer heat-transfer pipe is staggered.
It is arranged as an improvement, the heat-transfer pipe is in multilayer from top to bottom.
As an improvement, the heat-transfer pipe, the center spacing of every layer of adjacent tubes and the spacing of adjacent layer are that 2-3 times of heat transfer is straight
Diameter pipe.
It is improved as another kind, the heat-transfer pipe is carbon steel heat-transfer pipe.
The present invention also provides a kind of high temperature after-smithing petroleum coke high-grade exhaust heat recovering method, using above-mentioned retracting device,
Method is：Using gravity structure, high temperature calcined coke flows from above to below in hopper under the effect of gravity, while with
It exchanges heat between every layer of heat-transfer pipe.
Advantageous effect：High temperature after-smithing petroleum coke high-grade waste-heat recovery device provided by the invention is simple in structure, at low cost
It is honest and clean, easy to use, cooling means from inside to outside is used using gravity structure so that the temperature inside after-smithing petroleum coke
Degree is more uniformly distributed, and ensure that the quality of product.
The present invention uses gravity structure, high temperature calcined coke to flow from above to below under the effect of gravity；Utilize heat transfer
Pipe recycles high temperature after-smithing petroleum coke sensible heat, with direct heat transfer between saturated water and high temperature after-smithing petroleum coke, generates saturated vapor, can use
In power generation.
Since the flow velocity of calcined coke is smaller, although calcined coke is solid particle but minimum to the abrasion of heat-transfer pipe metallic walls,
Ordinary carbon steel material need to be only used, keeps the cost of evaporator relatively low.
Description of the drawings
Fig. 1 is the structural schematic diagram one of high temperature after-smithing petroleum coke high-grade waste-heat recovery device；
Fig. 2 is the structural schematic diagram two of high temperature after-smithing petroleum coke high-grade waste-heat recovery device；
Calcined coke Temperature Distribution cloud atlas in the wrong row's evaporators of Fig. 3-1；
The temperature profile of calcined coke in the wrong row's evaporators of Fig. 3-2；
Calcined coke Temperature Distribution cloud atlas in Fig. 3-3 in-line arrangement evaporators；
The temperature profile of calcined coke in Fig. 3-4 in-line arrangement evaporators；
Fig. 3-5 flow velocitys are to going out the influence diagram of calcined coke mouth temperature；
Influence diagram of Fig. 3-6 flow velocitys to heat transfer coefficient；
Influence diagram of Fig. 3-7 flow velocitys to waste heat recovery efficiency；
Influence diagram of Fig. 3-8 voidages to after-smithing petroleum coke outlet temperature；
Influence diagram of Fig. 3-9 voidages to Composite Walls；
Influence diagram of Fig. 3-10 voidages to waste heat recovery evaporator heat recovery efficiency；
The temperature profile of after-smithing petroleum coke in Fig. 3-11 difference pipe row's evaporators；
Influence diagram of Fig. 3-12 pipes number of rows to after-smithing petroleum coke outlet temperature；
Influence diagram of Fig. 3-13 pipes number of rows to heat transfer coefficient；
Influence diagram of Fig. 3-14 pipes number of rows to waste heat recovery evaporator waste heat recovery efficiency；(a)0.15m；(b)0.18m；
(c)0.21m；
Fig. 3-15 difference tube spacing temperature profiles；
Influence diagram of Fig. 3-16 tube spacing to after-smithing petroleum coke outlet temperature；
Influence diagram of Fig. 3-17 tube spacing to heat transfer coefficient；
Fig. 3-18 tube spacing exchanges the influence diagram of heat regenerator heat recovery efficiency；(a) wrong row；(b) in-line arrangement；
The temperature profile of Fig. 3-19 after-smithing petroleum coke temperature；
Fig. 3-20 after-smithing petroleum cokes outlet temperature with flow velocity variation diagram；
Fig. 3-21 pipes arrange influence diagram of the mode to heat transfer coefficient；
Fig. 3-22 pipes arrange influence diagram of the mode to waste heat recovery evaporator waste heat recovery efficiency.
Specific implementation mode
High temperature after-smithing petroleum coke high-grade waste-heat recovery device of the present invention is further illustrated below.
High temperature after-smithing petroleum coke high-grade waste-heat recovery device is shown in Fig. 1 and 2, including hopper 1 and one group of heat-transfer pipe 2；
It is arranged if one group of heat-transfer pipe 2 is in dried layer from top to bottom, and adjacent layer heat-transfer pipe 2 is staggered.
Heat-transfer pipe 2 is carbon steel heat-transfer pipe.
High temperature after-smithing petroleum coke high-grade exhaust heat recovering method, using above-mentioned retracting device, method is：Using flow by gravity
Formula structure, high temperature calcined coke flow from above to below in hopper 1 under the effect of gravity, at the same with every layer of heat-transfer pipe (2) it
Between exchange heat.
Present invention research heat-transfer pipe arranges the total heat transfers of the factors to evaporator such as mode, tube spacing, pipe number of rows, calcined coke flow velocity
The affecting laws of characteristic.
1, heat-transfer pipe arrangement mode influences the temperature of after-smithing petroleum coke
The Temperature Distribution of after-smithing petroleum coke in 1.1 wrong exhaust recovery evaporators
Fig. 3-1 is the Temperature Distribution cloud atlas of calcined coke in wrong row's evaporator, and Y-axis indicates the height of calcined coke evaporator, X-axis
Then indicate the sectional width of evaporator.Evaporator box height is 1.5m, width 0.42m, the pipe number of rows in particle flow direction
It is 8, often arranges three branch pipes, a diameter of 0.068m of heat-transfer pipe, tube hub spacing is 0.12m, and row's center spacing is 0.18m.Mistake row's knot
The left side heat transfer tube hub of structure is 0.06m with a distance from left wall face, and the right heat transfer tube hub is 0.12m with a distance from right wall.
Pressure of steaming 1.0MPaG (corresponding saturation temperature is 183 DEG C, i.e. 456K).
Evaporator takes Temperature Distribution layer along coordinate Y-axis, and a Temperature Distribution layer is taken between every two pipes row, totally 7 layers.In y=
First layer Temperature Distribution point is chosen at 0.24m, and one layer of Temperature Distribution point is chosen every 0.18m along Y direction.Every layer along X-axis
Direction takes 6 points, and the position of first point is x=0.02m, and a temperature spot is read every 0.08m along X-direction.Forge rear stone
Oil coke inlet temperature is set as 1073K, flow velocity 0.02mm/s.Temperature of the after-smithing petroleum coke in wrong comb waste heat recovery evaporator point
Cloth is as shown in figure 3-2.
By Fig. 3-2 it is found that high temperature after-smithing petroleum coke is after entering evaporator, by first row heat-transfer pipe cooling down, temperature
Degree distribution is not very uniformly.Compared to other temperature spots of same layer, the calcined coke temperature close to region at x=0.4m is very high, this can
It is wrong row's arrangement that can be primarily due to heat-transfer pipe, and first row 3 is unsymmetrical arrangement between heat-transfer pipe and babinet, and the 1st branch pipe is from a left side
Side box body wall surface is closer, and the 3rd branch pipe farther out from right side babinet wall surface, causes to be formed between the 3rd branch pipe and right side babinet wall surface wider
Path, laterally disturbance is small for calcined coke, and heat transfer coefficient is low, and calcined coke cannot be cooled in time, therefore, the temperature difference in the layer at first row
It is maximum.As after-smithing petroleum coke continues the heat exchange that flows downward, tend to be steady along the gradual cloth of X-direction temperature point, at the 7th row
Layer in the temperature difference it is minimum, illustrate after after-smithing petroleum coke flows through multi coil row, because it is horizontal plunder heat-transfer pipe when disturbance mix so that it is warm
Degree distribution is more uniform, and the influence of the different distance between the heat-transfer pipe and babinet wall surface of the right and left is smaller and smaller.After-smithing petroleum coke
Along the greenhouse cooling gradient relative equilibrium of Y direction, this may be because heat-transfer pipe is transverse pipe row and constant temperature in evaporator
Tube wall will not lead to vertical temperature distribution gradients uneven phenomenon because of the heat transferring medium temperature difference.
The Temperature Distribution of after-smithing petroleum coke in 1.2 in-line arrangement pipe waste heat recovery evaporators
Fig. 3-3 is the Temperature Distribution cloud atlas along calcined coke in pipe waste heat recovery evaporator, and Y-axis indicates that calcined coke evaporator is high
Degree, X-axis then indicate the sectional width of evaporator.Evaporator box height be 1.5m, width 0.42m, particle flow direction
Pipe number of rows is 8, often arranges three branch pipes, a diameter of 0.068m of heat-transfer pipe, and heat transfer tube hub spacing is 0.12m, and pipe row's center spacing is
0.18m.The left and right both sides heat transfer tube hub of in-line arrangement structure is 0.03m with a distance from wall surface.
Evaporator takes Temperature Distribution layer along coordinate Y-axis, and a Temperature Distribution layer is taken between every two pipes row, totally 7 layers.In y=
First layer Temperature Distribution point is chosen at 0.24m, and one layer of Temperature Distribution point is chosen every 0.18m along Y direction.Every layer along X-axis
Direction takes 7 points, and the position of first point is x=0.02m, along X-direction temperature spot be respectively 0.02m, 0.09m, 0.15m,
0.21m、0.21m、0.33m、0.4m.After-smithing petroleum coke inlet temperature is set as 1073K, flow velocity 0.2mm/s.After-smithing petroleum coke is suitable
Temperature Distribution in comb waste heat recovery evaporator is as shown in Figure 3-4.
By Fig. 3-4 it is found that first, high temperature after-smithing petroleum coke cools down cold after entering evaporator by first row heat-transfer pipe
But, Temperature Distribution is not very uniformly.All temperature spots of same row are compared along Y-axis, close to area at x=0.15m and x=0.27m
The calcined coke temperature in domain is very high.It is in-line arrangement arrangement that this, which may be primarily due to heat-transfer pipe, to be arranged symmetrically between heat-transfer pipe and babinet,
1st and the 2nd row pipe row between, the 2nd and the 3rd row pipe row between spacing it is all larger, form the calcined coke runner of relative short-circuit,
Disturb relatively small, the heat transmission of calcined coke is few, so close to x=0.15m and close to every layer of temperature at x=0.27m and 0.27m
Other opposite points of degree are higher.Secondly, in every layer at tank wall side, two row of x=0.02m and x=0.4m of calcined coke temperature
Minimum, the main reason for forming such result, may be, since the spacing of heat-transfer pipe and tank wall is smaller than tube center distance, at two row
The local velocity of after-smithing petroleum coke is larger, and disturbance is stronger, enhances transverse movement of the calcined coke in evaporator, strengthens after forging
Convection current heat transfer, burnt intergranular transmission of heat by contact and gas and the burnt intergranular convection current of burnt internal gas are conducted heat, and are reduced simultaneously
Heat transfer resistance between tube wall and calcined coke, heat exchange amount relative increase, temperature are lower.Again, close to evaporator center x=
For calcined coke temperature at 0.21m than slightly higher at close tank wall both sides, and than low among two tubulations, this may be to be monitored
Calcined coke temperature spot is among neighbouring heat-transfer pipe, and disturbance enhances heat transfer.Finally, high temperature after-smithing petroleum coke is entering
After evaporator cools, wrong cooling grid is compared, in-line arrangement pipe evaporator Exit temperature distribution is relatively uneven, close to runner
It is higher to locate temperature, and babinet both sides temperature has been reduced to tube wall temperature, reason is equally due to the larger formation of tube spacing between row
Runner reduce heat transfer, and side pipe with tank wall spacing is smaller enhances heat transfer.
From the point of view of the calcined coke Temperature Distribution of the above wrong cooling grid and in-line arrangement pipe evaporator, in other conditions all same
Under the premise of, to obtain more uniform calcined coke Temperature Distribution, it is preferred to use the structure of wrong cooling grid.
2, the influence that after-smithing petroleum coke flow velocity heat exchanging device heat transfer property influences
It is respectively 0.14mm/s, 0.16mm/s, 0.18mm/s, 0.2mm/ to take after-smithing petroleum coke to enter evaporator inlet speed
s、0.22mm/s、0.24mm/s、0.26mm/s.Above-mentioned wrong row's evaporator model is calculated, the import temperature of after-smithing petroleum coke
Degree is still set as 1073K, and tube wall temperature is set as 456K.The flow velocity of analysis after-smithing petroleum coke goes out temperature, overall heat-transfer coefficient to calcined coke
With the influence of heat exchanger waste heat recovery efficiency.
(1) flow velocity of after-smithing petroleum coke influences calcined coke outlet temperature
Fig. 3-5 shows the variation that calcined coke goes out temperature with flow velocity.By 3-5 it is found that the flow velocity with after-smithing petroleum coke increases
Greatly, after-smithing petroleum coke outlet temperature is gradually increasing, and the outlet temperature of after-smithing petroleum coke gradually rises.Because when calcined coke speed increases
After big, after-smithing petroleum coke shortens in the residence time of waste heat recovery evaporator, and heat cannot shed, cause to forge rear oil in time
Coke cannot be cooled down accordingly, and outlet temperature gradually increases the total heat output of calcined coke and reduces, so outlet temperature increases.
(2) influence of the flow velocity of after-smithing petroleum coke to overall heat-transfer coefficient
Fig. 3-6 shows influence of the flow velocity to overall heat-transfer coefficient of after-smithing petroleum coke.By Fig. 3-6 it is found that as flow velocity increases
Greatly, it forges rear oil waste heat recovery evaporator overall heat-transfer coefficient gradually to increase, when reason may be that after-smithing petroleum coke speed increases, pass
Heat pipe, which disturbs after-smithing petroleum coke, to be enhanced, and transverse movement enhancing of the calcined coke in evaporator strengthens calcined coke internal gas
Convection current heat transfer, burnt intergranular transmission of heat by contact and gas conduct heat with burnt intergranular convection current, while reducing tube wall and forging
Heat transfer resistance between coke afterwards, heat exchange amount relative increase, heat transfer coefficient increase.
(3) influence of the flow velocity of after-smithing petroleum coke to waste heat recovery evaporator waste heat recovery efficiency
Fig. 3-7 is influence of the flow velocity of after-smithing petroleum coke to waste heat recovery evaporator waste heat recovery efficiency.It can by Fig. 3-7
Know, as flow velocity gradually increases, the waste heat recovery efficiency of waste heat recovery heat of evaporation continuously decreases, and reason may be due to calcined coke
Flow velocity increases, although heat transfer coefficient is increased, reduces the residence time that calcined coke cools so that total heat exchange amount
Reduce, that is to say, that heat transfer coefficient increase caused by heat exchange amount increase be less than by residence time reduce reduction heat exchange
Amount so that the outlet temperature of calcined coke is got higher, and the totality of waste heat recovery efficiency in waste heat recovery evaporator is caused to become smaller.
3, the influence of after-smithing petroleum coke voidage heat exchanging device heat transfer property
The after-smithing petroleum coke voidage is taken to be respectively：0.581,0.662,0.718,0.747,0.794, still to above-mentioned wrong comb
Evaporator model carries out simulation calculating, and after-smithing petroleum coke inlet temperature is set as 1073K, flow velocity 0.2mm/s, and tube wall temperature is set as
456K.Changed according to the voidage of calcined coke, calculates effective specific heat capacity, effective thermal conductivity and the accumulation of corresponding calcined coke
The apparent physical parameter such as density.Still by taking above-mentioned wrong cooling grid as an example, the voidage of after-smithing petroleum coke is analyzed to calcined coke
The influence of outlet temperature and influence to evaporator overall heat-transfer coefficient, waste heat recovery efficiency.
(1) influence of the voidage of after-smithing petroleum coke to calcined coke outlet temperature
Fig. 3-8 be after-smithing petroleum coke influence of the voidage to calcined coke outlet temperature by Fig. 3-8 it is found that forging rear oil
Burnt mean outlet temperature and highest outlet temperature is reduced with the increase of calcined coke voidage, and reason may be as follows, forges
The apparent physical parameter of petroleum coke is related with voidage afterwards, and when voidage increases, the bulk density of calcined coke reduces, and compares simultaneously
Thermal capacitance reduces, under identical speed of the discharging of the coke, since bulk density reduces, and to which after-smithing petroleum coke mass flow is reduced, calcined coke
The unit mass heat of institute's band is also opposite to be reduced, therefore as voidage increases, the outlet temperature of after-smithing petroleum coke continuously decreases.
(2) influence of the voidage of after-smithing petroleum coke to evaporator overall heat-transfer coefficient
Fig. 3-9 is influence of the voidage of after-smithing petroleum coke to evaporator overall heat-transfer coefficient.By Fig. 3-9 it is found that with forging
The gradual increase of burnt voidage, the overall heat-transfer coefficient of waste heat recovery evaporator are gradually reduced afterwards.According to packed particle associated hot object
Property parameter calculation formula, when voidage increases, the bulk density of calcined coke reduces, and effective specific heat capacity reduces, effective system
Number reduces, and therefore, total heat transfer efficiency of waste heat recovery evaporator can reduce with the increase of voidage.
(3) influence of the voidage of after-smithing petroleum coke to evaporator waste heat recovery efficiency
Fig. 3-10 is influence of the voidage of after-smithing petroleum coke to evaporator waste heat recovery efficiency.By Fig. 3-10 it is found that with
The gradual increase of calcined coke voidage, the waste heat recovery efficiency of waste heat recovery evaporator gradually increases.Comparison diagram 3-9 it is found that
Although the overall heat-transfer coefficient of evaporator is reduced with the increase of calcined coke voidage, the heat that calcined coke is totally brought into also subtracts therewith
It is small, while the outlet temperature of calcined coke also reduces so that the waste heat recovery efficiency of waste heat recovery evaporator increases.
4, influence of the heat-transfer pipe pipe number of rows to evaporator heat transfer performance
Influence for research heat-transfer pipe pipe number of rows to evaporator heat transfer performance, it is respectively 6 rows, 8 to select heat-transfer pipe pipe number of rows
Row and 10 rows.The model of stagger arrangement pipe evaporator is established according to different pipe numbers of rows, the center tube spacing of heat-transfer pipe is 0.12m, row
Spacing is 0.18m, and when 6 rows, 8 rows and 10 row, corresponding evaporator total height was respectively 1.2m, 1.5m and 2.0m.After-smithing petroleum coke
Inlet temperature is still set as 1073K, and tube wall temperature is set as 456K, and the voidage of after-smithing petroleum coke takes 0.718.Sunykatuib analysis difference pipe
Influence of the number of rows to calcined coke outlet temperature, overall heat-transfer coefficient and heat exchanger waste heat recovery efficiency in each evaporator.
(1) influence of the pipe number of rows to calcined coke outlet temperature
Fig. 3-11 is the Temperature Distribution cloud atlas of the calcined coke in each evaporator when flow velocity is 0.2mm/s, and Fig. 3-12 is each steaming
The outlet temperature of calcined coke in device is sent out with the variation of flow velocity.By Fig. 3-11 and Fig. 3-12 it is found that when in waste heat recovery evaporator
When pipe number of rows is 6 row, the outlet temperature highest of calcined coke, and as after-smithing petroleum coke flow velocity increases, with 8 cooling grids
Gradually increase with the outlet temperature difference of 10 cooling grids.Calcined coke outlet temperature when pipe number of rows is 10 row is minimum, and with stream
The increase of speed, outlet temperature variation are little.Main cause may be that total heat conduction area when pipe number of rows is 6 row is minimum, and because of pipe
Number of rows is reduced, and residence time of the after-smithing petroleum coke in heat exchanger is reduced, and the heat exchange amount of waste heat recovery evaporator also reduces therewith,
It results in as pipe number of rows reduces, the increased result of outlet temperature of after-smithing petroleum coke.When pipe number of rows number increases, waste heat recovery
The total heat conduction area of evaporator increases, and total heat exchange amount of after-smithing petroleum coke increases, and the outlet temperature of after-smithing petroleum coke gradually tends to
Stablize.
(2) influence of the pipe number of rows to waste heat recovery evaporator overall heat-transfer coefficient
Fig. 3-13 be when calcined coke flow velocity 0.14mm/s, 0.16mm/s, 0.18mm/s, 0.2mm/s, 0.22mm/s,
Influence of the pipe number of rows to waste heat recovery evaporator overall heat-transfer coefficient when 0.24mm/s, 0.26mm/s.By Fig. 3-13 it is found that with pipe
The increase of number of rows, overall heat-transfer coefficient reduce, but the influence of the managed number of rows of overall heat-transfer coefficient is not very big.Main cause may be because
Total heat exchange amount of the increase of total heat exchange area in after-smithing petroleum coke waste heat recovery evaporator, after-smithing petroleum coke increases, and always exchanges heat
When area is increased to a certain extent, the outlet temperature of calcined coke reduces, and the temperature difference between calcined coke and cooling medium reduces therewith, by
It can not possibly be less than the temperature of cooling medium in the outlet temperature of calcined coke so that the outlet temperature of calcined coke gradually tends towards stability,
Total heat exchange amount is caused to also tend to stablize.
(3) influence of the pipe number of rows to evaporator waste heat recovery efficiency
Influence of the pipe number of rows to evaporator waste heat recovery efficiency when Fig. 3-14 is different in flow rate.By Fig. 3-14 it is found that waste heat
Organic efficiency increases with the increase of pipe number of rows, and the efficiency of 6 rows is minimum, the efficiency highest of 10 rows.Master is this is because work as pipe number of rows
When too low, total heat conduction area is very few, and residence time of the calcined coke in evaporator is too short, and total heat exchange amount is on the low side, forges rear oil
Burnt outlet temperature is excessively high, and the waste heat recovery efficiency of waste heat recovery evaporator is caused to reduce.
Although pipe number of rows increases, waste heat recovery efficiency becomes larger, and when pipe number of rows is excessive, after-smithing petroleum coke outlet temperature is gradual
It reduces, close to the temperature of Cooling Heat Transfer tube wall, eventually results in the waste of heat transfer area, influence the economy of evaporator.
6,8,10 row's heat-transfer pipe numbers of rows of comparison influence the heat transfer property of waste heat recovery evaporator respectively, avoid forging rear oil
Coke considers economic interests and production efficiency because of the excessively high generation oxidation reaction of temperature, oil after recommendation is forged in above-mentioned condition
8 comb numbers of rows of burnt waste heat recovery evaporator are best.
5, the influence of heat transfer tube spacing heat exchanging device heat transfer property
In order to determine the optimum height range of heat exchanger, herein select three kinds heat transfer tube spacing, respectively 0.15m, 0.18,
0.21m.Research heat transfer tube spacing goes out temperature, overall heat-transfer coefficient and heat exchanger waste heat recovery efficiency to different pipe numbers of rows to calcined coke
Influence.
The evaporator box height that simulation calculates is 2m, and the pipe number of rows in particle flow direction is 8, often arranges three branch pipes, is conducted heat
Pipe diameter is 0.068m, and row's center spacing is 0.18m.The inlet temperature 1073K of calcined coke.In the left side heat-transfer pipe of mistake row's structure
The heart is 0.06m with a distance from left wall face, and the right heat transfer tube hub is 0.12m with a distance from right wall.Tube wall temperature is set as 456K,
The voidage of after-smithing petroleum coke takes 0.718.
(1) influence of the tube spacing to calcined coke outlet temperature
Calcined coke Temperature Distribution cloud atlas of the Fig. 3-15 when being the flow velocity 0.2mm/s of calcined coke under the conditions of various tube spacing is (horizontal
The directions coordinate x are dimensionless coordinate), Fig. 3-16 is calcined coke outlet temperature under the conditions of various tube spacing with the variation of flow velocity.By
Shown in Fig. 3-15 and Fig. 3-16, tube spacing be 0.15m when calcined coke outlet temperature it is minimum, tube spacing be 0.21m when forge after
Burnt outlet temperature highest, calcined coke outlet temperature when tube spacing is 0.18m are between the two.Main cause may be, with
The reduction of tube spacing, the local velocity of after-smithing petroleum coke increases, disturbance enhancing, to transverse movement of the calcined coke in heat exchanger
Enhancing, convection current heat transfer, burnt intergranular transmission of heat by contact and gas and the coke for strengthening calcined coke internal gas are intergranular right
Heat is spread, while reducing the heat transfer resistance between tube wall and calcined coke, heat exchange amount relative increase, calcined coke outlet temperature is lower.
(2) influence of the tube spacing to evaporator overall heat-transfer coefficient
Fig. 3-17 is influence of the tube spacing to waste heat recovery evaporator overall heat-transfer coefficient.By Fig. 3-17 it is found that between pipe
Away from increase, the overall heat-transfer coefficient of evaporator can reduce, but overall heat-transfer coefficient variation when three kinds of tube spacing is little.Main cause
May be that with the reduction of tube spacing, the local velocity of after-smithing petroleum coke increases, disturbance enhancing, strengthen after-smithing petroleum coke with
The convection current of heat-transfer pipe is conducted heat so that overall heat-transfer coefficient increases.But due to being the arrangement mode of wrong comb, even if tube spacing increases,
The lateral level of disruption of calcined coke particle is barely affected so that the variation unobvious of overall heat-transfer coefficient.
(3) influence of the tube spacing to evaporator waste heat recovery efficiency
Fig. 3-18 is influence of the tube spacing to evaporator waste heat recovery efficiency.By Fig. 3-18 it is found that subtracting with tube spacing
Small, the waste heat recovery efficiency of waste heat recovery evaporator increases, but change between the efficiency of three kinds of tube spacing it is little, this be mainly because
For, tube spacing is smaller, local dip enhancing, heat exchange efficiency increase, calcined coke outlet temperature reduce, waste heat recovery evaporator it is total
Heat exchange amount becomes larger, therefore the waste heat recovery efficiency of heat exchanger increases therewith.Similarly, since be the arrangement mode of wrong comb, even if
Tube spacing increases, and the lateral level of disruption of calcined coke particle is barely affected so that the variation unobvious of total heat transfer property are led
The waste heat recovery efficiency change unobvious of induced evaporation device.
Although the reduction of tube spacing strengthens the coefficient of heat transfer, but tube spacing is too small can increase flow resistance, causes to conduct heat
Pipe wall abrasion.When simulation calculates, after-smithing petroleum coke is considered with fluid analogy theory, without in view of after-smithing petroleum coke particle
Diameter.Therefore, while selecting tube spacing, it is also contemplated that actual conditions, suitable pipe is selected according to calcined coke particle size
Spacing avoids in practical engineering application because of the local choking phenomenon of the excessive appearance of burnt particle diameter.
6, the influence of heat-transfer pipe arrangement mode heat exchanging device heat transfer property
Under identical flow velocity, simulation different heat transfer pipe arrangement mode is to calcined coke outlet temperature, overall heat-transfer coefficient and heat exchange
The influence of device waste heat recovery efficiency.Analog study is carried out herein for two kinds of pipe row's modes of mistake row and in-line arrangement, selecting pipe number of rows is
8, the evaporator box height for simulating calculating is 1.5m, width 0.42m, often arranges three branch pipes, a diameter of 0.068m of heat-transfer pipe, pipe
Center spacing is 0.12m, and row's center spacing is 0.18m.The inlet temperature of calcined coke is still 1073K, and tube wall may be configured as constant temperature
456K.Mistake row structure the left side conduct heat tube hub with a distance from left wall face be 0.06m, the right conduct heat tube hub from right wall away from
From for 0.12m；For in-line arrangement structure to be symmetrical, arranged on left and right sides heat transfer tube hub is 0.09m with a distance from wall surface.Forge rear stone
The voidage of oil coke takes 0.718.
(1) influence of the pipe row arrangement mode to calcined coke outlet temperature
Fig. 3-19 is the cloud of calcined coke Temperature Distribution in evaporator of two kinds of arrangement mode calcined coke flow velocitys when being 0.2mm/s
Figure, Fig. 3-20 be two kinds of arrangement modes when evaporator calcined coke outlet temperature with flow velocity variation.By Fig. 3-19 and Fig. 3-20
It is found that the difference of the calcined coke Temperature Distribution of two kinds of different pipe row modes is clearly, after-smithing petroleum coke in wrong cooling grid
Temperature is gradually uniformly reduced as flow velocity increases, and Exit temperature distribution is uniform；And the calcined coke temperature inside in-line arrangement heat exchanger point
Cloth is uneven, and along Y-axis, high-temperature region is concentrated mainly among every two tubulation, and after-smithing petroleum coke Exit temperature distribution is uneven, part
There is the phenomenon that temperature is excessively high.In-line arrangement heat exchange of heat pipe discharge of the coke mean temperature than wrong comb arrange it is much higher, but with flow velocity increase the temperature difference
More apparent (Fig. 3-20).Reason may be as follows：Wrong comb is more strong to calcined coke perturbation action, strengthen particle and gas with
Heat transfer between tube wall, while the convection current heat transfer for strengthening gas itself, reduce tube wall surface air-film thickness, reduce total heat transfer
Result caused by thermal resistance.
(2) influence of the pipe row arrangement mode to evaporator overall heat-transfer coefficient
Fig. 3-21 is that pipe arranges influence of the arrangement mode to waste heat recovery evaporator overall heat-transfer coefficient.By Fig. 3-21 it is found that
Identical to discharge of the coke under speed, the overall heat-transfer coefficient of wrong comb waste heat recovery evaporator is higher than in-line arrangement.This may be due to wrong comb
Arrangement is more strong to the perturbation action of calcined coke, strengthens the transverse movement of calcined coke, reduces the gas of tube wall surface
Film thickness reduces total heat exchanged thermoresistance, pair for strengthening the heat exchange between particle and gas and tube wall, while strengthening gas itself
Stream heat exchange, particle and intergranular heat transfer, it is higher than in-line arrangement pipe so as to cause the overall heat-transfer coefficient of wrong cooling grid.
(3) influence of the pipe row arrangement mode to evaporator waste heat recovery efficiency
Fig. 3-22 is that pipe arranges influence of the arrangement mode to evaporator waste heat recovery efficiency.By Fig. 3-22 it is found that it is identical go out
Under burnt speed, the waste heat recovery efficiency of wrong cooling grid is higher than in-line arrangement.It is since wrong comb is to calcined coke that this is equally possible
Perturbation action is more strong, reduces tube wall surface air-film thickness, reduces total heat transfer resistance, strengthens particle and gas and pipe
Heat exchange between wall, while the convection current heat transfer for strengthening gas itself, it is suitable so as to cause the overall heat-transfer coefficient ratio of wrong cooling grid
The calcined coke outlet temperature of the height of row, wrong cooling grid is low, then total heat exchange amount increases, and is returned so as to cause the waste heat of evaporator
The rate of producing effects increases.
After-smithing petroleum coke waste heat recovery evaporator selects in-line arrangement or wrong row, not only to consider in practical engineering application
Overall heat-transfer coefficient, waste heat recovery efficiency and after-smithing petroleum coke flow velocity etc., while being also contemplated that mill of the calcined coke particle to heat-transfer pipe
Erosion situation, mistake row compare in-line arrangement, and tube wall is more easy to be worn.
In above example, heat-transfer pipe 2 from top to bottom, multilayer setting, the specific number of plies according to high temperature after-smithing petroleum coke into
Material temperature degree and the pressure of steaming of waste heat recovery, are determined, it is preferable that heat-transfer pipe 2 is set in 6 to 10 layers from top to bottom by thermodynamic metering
It sets, more preferably 8 layers setting；Heat-transfer pipe 2, the center spacing of every layer of adjacent tubes and the spacing of adjacent layer are 2-3 times of biography
Heat pipe diameter is 0.15-0.21m in above example；High temperature calcined coke flowing velocity is 0.14mm/s-0.26mm/s；It is preferred that
Ground, flowing velocity 0.14mm/s-0.20mm/s；High temperature calcined coke voidage is 0.581-0.794；Preferably, after high temperature is forged
Burnt voidage is 0.718-0.794.
Claims (5)
1. a kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device, it is characterised in that：Including hopper (1) and one group of biography
Heat pipe (2)；One group of heat-transfer pipe (2) is if be in that dried layer is arranged, and adjacent layer heat-transfer pipe (2) is staggered from top to bottom.
2. a kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device according to claim 1, it is characterised in that：It is described
From top to bottom, multilayer setting, the specific number of plies is according to the feeding temperature of high temperature after-smithing petroleum coke and the production of waste heat recovery for heat-transfer pipe (2)
Steam pressure is determined by thermodynamic metering.
3. a kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device according to claim 1, it is characterised in that：It is described
Heat-transfer pipe (2), the center spacing of every layer of adjacent tubes and the spacing of adjacent layer are 2-3 times of heat transfer pipe diameter.
4. a kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device according to claim 1, it is characterised in that：It is described
Heat-transfer pipe (2) is carbon steel heat-transfer pipe.
5. a kind of high temperature after-smithing petroleum coke high-grade exhaust heat recovering method, it is characterised in that：Use any one of claims 1 to 33
The retracting device, method are：Using gravity structure, high temperature calcined coke is under the effect of gravity in hopper (1)
It flows from above to below, while exchanging heat between every layer of heat-transfer pipe (2).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115854745A (en) * | 2023-01-09 | 2023-03-28 | 坤洋翰光能源技术(江苏)有限公司 | High-temperature solid slag heat collector and heat collection method thereof |
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| CN208505076U (en) * | 2018-04-12 | 2019-02-15 | 南京华电节能环保设备有限公司 | A kind of high temperature after-smithing petroleum coke high-grade waste-heat recovery device |
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| JP2001066077A (en) * | 1999-08-24 | 2001-03-16 | Babcock Hitachi Kk | Heat-recovering device |
| CN202993144U (en) * | 2012-12-31 | 2013-06-12 | 张茂勇 | Internally-buried heat pipe type waste heat recovery and steam production device for charcoal ink factory calcining furnace calcined coke |
| CN204005897U (en) * | 2014-06-13 | 2014-12-10 | 盐城市锅炉制造有限公司 | High-temp solid heat recovery waste heat boiler |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115854745A (en) * | 2023-01-09 | 2023-03-28 | 坤洋翰光能源技术(江苏)有限公司 | High-temperature solid slag heat collector and heat collection method thereof |
| CN115854745B (en) * | 2023-01-09 | 2023-11-14 | 江苏坤洋翰光能源技术集团有限公司 | High-temperature slag fixing heat collector and heat collecting method thereof |
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