CN205948388U - Flash distillation of tower tray formula heat transfer integration equipment - Google Patents
Flash distillation of tower tray formula heat transfer integration equipment Download PDFInfo
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- CN205948388U CN205948388U CN201620536662.5U CN201620536662U CN205948388U CN 205948388 U CN205948388 U CN 205948388U CN 201620536662 U CN201620536662 U CN 201620536662U CN 205948388 U CN205948388 U CN 205948388U
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Abstract
The utility model discloses a flash distillation of tower tray formula heat transfer integration equipment, including a tower body, the tower body divide into the evaporating chamber of lower part and the hot water room on upper portion through the tower body baffle, the inside of equipment still is equipped with the tower tray, the tower tray is located the heat transfer section of hot water room, the tower tray is located the below of water inlet distributor, the tower tray still includes downspout and cover cap. The utility model discloses the processes such as flash distillation, solid -phase separation and clean water intensification that contain solid waste water that have realized simultaneously in single tower have effectively improved heat transfer area and efficiency of heat transfer in the tower, have still overcome the shortcoming that the easy scale deposit of current indirect heating equipment of the same type was blockked up, and very big degree has alleviateed to change washs the maintenance work and the expense of packing, and the no environmental pollution scheduling problem has good technological economic benefits and environmental protection profit.
Description
Technical field
This utility model is related to a kind of tower disc type flash distillation-heat-exchange integrated equipment.
Background technology
Air flow bed with Hydrocarbon as raw material produces the (multiinjector pair as East China University of Science's exploitation in course of gas
Put formula Coal Gasification Technology, patent No. US7862632B2, ZL98110616.1, ZL01210097.8, ZL200510111484.8,
ZL200810039551.3), from gasification furnace synthesis gas out after supercooled water gradient cooling and washing, folded in synthesis gas
The lime-ash almost all of band is transferred in liquid phase, and this contains pulp water and is also referred to as Heisui River；These nearly saturated slag water temperature are 220
～250 DEG C, solid concentration about 1wt%, pressure is 2.0～10.0MPa.For saving water resource and minimizing discharge, should containing pulp water
Recycle.But the restriction due to flocculant heat resistance in water technology, only has containing pulp water and just enables to purify after lowering the temperature.
Accordingly, it would be desirable to separate with solid slag to carrying out heat recovery containing pulp water, to realize the effectively utilizes of energy, save water resource.
In slag inclusion hydro-thermal amount recovery technology, the Chinese patent CN94117093.4 of Texaco Development Corporation's application (authorizes public
Announcement CN1037503C) disclose a kind of multistage flash evaporation (high pressure flash, middle pressure flash distillation, low pressure flash and vacuum flashing) and multistage
Heat exchanger carrys out the process of recovery process slag inclusion waste water heat with reference to knockout drum；Whole Slag-water system technological process is more
Complexity, and due to the steam that flashes off will necessarily entrainment portions fine slag, when dividing wall type heat exchanger reclaims heat, fine slag surely can
Stagnate and accumulate on heat exchanger surface, directly affect heat transfer effect, therefore must clear up in time, thus bring very big maintenance work
Measure.
East China University of Science apllied Chinese patent CN01239007.0 (Authorization Notice No. CN2474538Y) discloses
A kind of hot-water tower reclaiming slag inclusion waste water heat, the hot hydroecium of eddy flow flash chamber and direct contact heat transfer is coupling in a tower
Interior；This choice of technology filler as augmentation of heat transfer tower internals although its Mass and heat transfer effect is preferable, but life-time service meeting
Lead to filler surface accumulation fine slag to block, so that gas liquid interfacial area reduces, affect Mass and heat transfer efficiency, therefore work people
Member needs to carry out stopping cleaning after the usage cycles (a year about) of 3～4 nozzles and changes filler.The cleaning of filler is not
But need water under high pressure, and the loading and unloading amount of filler is larger, expend a large amount of manpowers, in addition filler also can cause to site environment
Certain impact.
Utility model content
To be solved in the utility model is that prior art is difficult to meet slag inclusion waste water heat recovery, buck utilization simultaneously, gives up
The technological requirement of three aspects such as slag separation, and heat exchanger blocking, the problem of replacement, there is provided one kind is used for high pressure belt temperature
Flash distillation-heat-exchange integrated equipment containing solid wastewater energy reuse.
This utility model mainly solves above-mentioned technical problem by the following technical programs：
A kind of tower disc type flash distillation-heat-exchange integrated equipment, including a tower body (1), described tower body (1) passes through tower body dividing plate
(2) it is divided into the vaporization chamber (3) of bottom and the hot hydroecium (4) on top, described tower body (1) is additionally provided with the pipe of water inlet containing solid waste
(11), steam (vapor) outlet (12), water inlet (13), hot water outlet (14), discharge of wastewater mouth (15) and waste residue outlet (17), described tower
The inside of body (1) is provided with riser (31)；The inside of described tower disc type flash distillation-heat-exchange integrated equipment is additionally provided with tower tray (5), institute
State tower tray (5) to be located in the heat exchanging segment (41) of described hot hydroecium (4), described tower tray (5) is located under water inlet distributor (42)
Side, described tower tray (5) also includes downspout (51) and cap (52).
In this utility model, tower tray, as vapor-liquid contacting elements, is arranged on dividing plate top using conventional mechanical means
Hot water is indoor, and its Main Function is so that the steam of rising and the liquid declining is fully contacted on column plate, improves heat and mass effect
Rate, most of steam is condensed by liquid, and a small amount of steam and incoagulable gas are discharged from tower top, and liquid is most of to be flowed to from downflow weir
Next block tower tray, is finally discharged by hot water outlet, enters system circulation and uses.
It is preferred that described tower tray (5) is one of solid valve tower tray, sieve tray, float valve tray or jet tray.
It is preferred that the number of plates of described tower tray (5) is 1-10 it is therefore preferable to 2-5.
It is preferred that the height of weir of described tower tray (5) is 30-120mm it is therefore preferable to 40-80mm.
It is preferred that the weir length of described tower tray (5) compares l with tower diameterw/ D is 0.40-0.90 it is therefore preferable to 0.65-0.75.
It is preferred that the aperture d of described tower tray (5)0For 10-100mm it is therefore preferable to 30-60mm.
It is preferred that the hole centre-to-centre spacing of described tower tray (5) and aperture ratio t/d0For 2.0-6.0 it is therefore preferable to 2.5-3.5.
It is preferred that the perforate height of described tower tray (5) is 2-20mm it is therefore preferable to 6-15mm.
It is preferred that the gas phase loading factor F of described tower tray (5) is 6-15 it is therefore preferable to 7-12；Described gas phase loading factor
Computational methods those skilled in the art all know that it is this area conventional method, as follows：F=W0×(ρV)1/2, wherein F is
Gas phase loading factor, W0For gas phase superficial velocity, ρVFor density of gas phase.
The hole count of described tower tray (5) is commonly used in the art, be generally based on described gas phase loading factor and according to
The fixed range of flow of actual production target, is calculated by this area conventional method；Determine a gas phase loading factor F first,
Obtain gas phase superficial velocity W according to the computational methods of described gas phase loading factor0, remove further according to the fixed total flow of productive target
With gas phase superficial velocity W0Obtain hole count with the product in aperture；In actual production process the difference according to concrete fluid situations and
The difference of the fitting formula being adopted, can determine described hole count using conventional try and error method based on the above method.
It is preferred that the width of described downspout (51) compares W with tower diameterd/ D is 0.04-0.3 it is therefore preferable to 0.12-0.18.
It is preferred that the area of described downspout (51) compares A with column areaf/ATFor 0.015-0.25 it is therefore preferable to 0.075-
0.095.
It is preferred that the height of base slot of the downcomer of described downspout (51) is 20-150mm it is therefore preferable to 30-70mm.
In this utility model, the top of described vaporization chamber (3) is provided with the pipe of water inlet containing solid waste (11), uses by this area is conventional
In be passed through through air relief valve decompression after high pressure belt temperature water containing solid waste；The described pipe of water inlet containing solid waste (11) presses this area usual manner
Setting, both can press tower body radial symmetric formal distribution by two inlet tubes, and also can only arrange single inlet tube, with practical situation be
Accurate.
In this utility model, described riser (31) is arranged according to a conventional method, for producing vaporization chamber (3) vacuum flashing
Steam water conservancy diversion send in top hot hydroecium (4).
It is preferred that the bottom of described riser (31) is located in described vaporization chamber (3), the upper bit of described riser (31)
In described hot hydroecium (4), the lower section of described tower tray (5), the top of described riser (31) is provided with cloth vapour cap (32)；More preferably
Ground, the quantity of described riser (31) is 1-5, because upflowing vapor also has part lime-ash, the quantity of riser (31) is unsuitable many；
More preferably, the top of described tower body dividing plate (2) is provided with the rib (33) of fixing described riser (31)；More preferably, described cloth vapour
Cap (32) be shaped as square or taper it is therefore preferable to taper.
In this utility model, described water inlet distributor (42) is by the routine of this area located at described water inlet (13)
Lower section, the cleaner low temperature water energy for making entrance tower body is uniformly distributed.
It is preferred that described water inlet distributor (42) is tubular liquid distributor, tank type liquid distributor, disc type liquid dividing
One of cloth device or injecting type liquid distribution trough.
In this utility model, the inside of described hot hydroecium (4) preferably is provided with demister (43), described demister (43) position
Between described water inlet (13) and the described steam (vapor) outlet (12), carry secretly for removing not coagulating in acid vapors of device for transferring
Mist, system burden after mitigation；More preferably, described demister (43) is one of wire mesh demister or spiral board demister.
In this utility model, it is preferred that the diameter of described vaporization chamber (3) and described hot hydroecium (4) a diameter of isometrical or
Reducing.
In this utility model, described steam (vapor) outlet (12) by the routine of this area located at the top of tower body (1), for arranging
The incoagulability steam producing during going out wastewater energy reuse.
In this utility model, described water inlet (13) is by the routine of this area in the hot hydroecium (4) of tower body (1)
Portion, for being passed through water at low temperature in tower body.
In this utility model, described hot water outlet (14) heat exchanging segment located at hot hydroecium (4) by the routine of this area
(41) below, the clear hot-water for absorbing almost all steam heat leaves this equipment, realizes the process system of water purification
Circulating and recovering.
In this utility model, described discharge of wastewater mouth (15) located at the bottom of vaporization chamber (3), is used by the routine of this area
In waste discharge.
It is preferred that the cone section side of described vaporization chamber (3) is provided with a standby discharge of wastewater mouth (16), give up for additional discharge
Water.
In this utility model, described waste residue exports (17) by the routine of this area located at the cone section bottom of vaporization chamber (3),
For the waste residue producing during waste discharge energy reuse.
On the basis of meeting common sense in the field, above-mentioned each optimum condition, can combination in any, obtain final product this utility model each relatively
Good example.
Positive effect of the present utility model is：
(1) vaporization chamber is coupled by this utility model with hot hydroecium, using eddy flow guide type flash steam entrance and structure simple,
There is the tower tray pattern of self-cleaning function, be simultaneously achieved the flash distillation containing solid waste water in single tower, solid phase separates and clean water
The process such as intensification, each process is interrelated, and device integration is high, enormously simplify the technological process containing solid waste Water circulation；
(2) this utility model also effectively increases the heat transfer area in tower and heat transference efficiency, also overcomes dividing wall type and changes
The easy fouling of hot device, the shortcoming of blocking, high degree alleviates replacings, the maintenance work cleaning filler and expense, has excellent
Adaptability, reliability and larger operating flexibility, improve the quality of system recycle-water, further increase the energy profit of system
With rate, reduce the problems such as system water circulation amount, energy saving, reduction consumption, non-environmental-pollution；
To sum up, this utility model is with the gas as raw material containing hydrocarbon substance such as coal, petroleum coke, biomass, trade waste
Fluidized bed produces slag inclusion waste water or other industrial circle mesohigh band temperature comprehensive recycling containing solid waste water in course of gas and provides one
Plant long period, the technology ensuring of safe and stable operation, there is good technical economic benefit and environmental benefit.
Brief description
Fig. 1 is the structural representation of this utility model preferred embodiment.
Specific embodiment
Mode below by embodiment further illustrates this utility model, but is not therefore limited in this utility model
Among described scope of embodiments.
As shown in figure 1, a kind of tower disc type flash distillation-heat-exchange integrated equipment, including a tower body 1, described tower body 1 passes through tower body
Dividing plate 2 is divided into the vaporization chamber 3 of bottom and the hot hydroecium 4 on top, and described tower body 1 is additionally provided with the pipe of water inlet containing solid waste 11, steam
Outlet 12, water inlet 13, hot water outlet 14, discharge of wastewater mouth 15, standby discharge of wastewater mouth 16 and waste residue outlet 17, described tower body
1 inside is provided with riser 31；The inside of described tower disc type flash distillation-heat-exchange integrated equipment is additionally provided with tower tray 5, described tower tray 5
In the heat exchanging segment 41 of described hot hydroecium 4, described tower tray 5 is located at the lower section of water inlet distributor 42, and described tower tray 5 also includes
Downspout 51 and cap 52；The inside of described tower body 1 is provided with a riser 31, and the bottom of described riser 31 is located at described evaporation
In room 3, the top of described riser 31 is located in described hot hydroecium 4, the lower section of described tower tray 5, the top of described riser 31
It is provided with cloth vapour cap 32；The top of described tower body dividing plate 2 is provided with the rib 33 of fixing described riser 31；The shape of described cloth vapour cap 32
Shape is taper；The inside of described hot hydroecium 4 is provided with demister 43, and described demister 43 is located at described water inlet 13 and described steam
Between outlet 12.
Above-mentioned tower disc type flash distillation-heat-exchange integrated equipment operation method is as follows：
Through being arranged on after air relief valve decompression before the pipe of water inlet containing solid waste 11, eddy flow enters evaporation to the water containing solid waste of high pressure belt temperature
Room 3, due to abrupt pressure reduction and under cyclonic action, in water containing solid waste, a large amount of instantaneous flash distillations of liquid phase water are more clean steam,
This flash-off steam also can carry fraction fine ash, and the sensible heat containing solid waste water is also converted into steam latent heat simultaneously；In density effect
Under, steam after cloth vapour cap 32 water conservancy diversion of riser 31 and its epimere even into the hot hydroecium 4 positioned at vaporization chamber 3 top,
Slag inclusion waste water after concentration enters the liquid phase main body storage tank of vaporization chamber 3 lower section, is discharged by discharge of wastewater mouth 15 or 16, enters follow-up
Workshop section；
Steam enters the heat exchanging segment 41 in hot hydroecium 4 and passes through tower tray 5, divides through water inlet 13 and water inlet with from top
The relatively low clean water of temperature that cloth device 42 flows down directly is contacted on column plate, and mass-and heat-transfer process simultaneously occurs, and steams
Contain in vapour flying dust major part got off by clean water washing, clean water absorb steam latent heat after by downspout 51 to
Tower tray flowing underneath, the clean water of higher temperature flows out equipment by hot water outlet 14, recycles as system recycle-water, on a small quantity
Incoagulable gas is discharged from steam (vapor) outlet 12 through demister 43 by tower top.
Embodiment 1
The concrete structure setting of the tower disc type flash distillation of the present embodiment-heat-exchange integrated equipment is as shown in Figure 1；In addition,
The a diameter of 3400mm of tower body, the vaporization chamber of bottom and the hot hydroecium on top adopt same footpath, vaporization chamber height 7300mm, and hot hydroecium is high
Degree 13200mm；Set up 2 bore 600mm of water inlet containing solid waste same week, the pipe of water inlet containing solid waste inserts cylinder depth
450mm, 70 ° of semicylinder guide openings angle；Draft tube diameter 700mm, length about 8000mm, totally 1；Hot hydroecium's heat exchanging segment
Interior 7 layers of solid valve tower tray of setting, plate spacing 700mm, every layer of tower tray there is 420-600 perforate height be 8-12mm, aperture is 38-
The solid valve of 50mm, hole centre-to-centre spacing and aperture ratio t/d0For 4.0；The height of weir 90mm of every layer of tower tray, height of base slot of the downcomer 70mm, weir is long
2157mm；Downspout width 387mm, downspout area 0.45m2；One spiral board demister is set between tower tray and gas outlet.
So that day processes 2000 tons of coal water slurry gasification systems as a example, with single above-mentioned tower tray come high pressure whole in processing system
Containing solid Heisui River.From front system containing solid Heisui River total flow 230t/h, solid content～0.9%, pressure 4.08-3.96MPa, temperature
220-225℃；Described divide two strands containing solid Heisui River, the reducing pressure angle valve through being arranged on the pipe of water inlet containing solid waste front end is decompressed to
After 0.45MPa, enter flash chamber from the pipe of water inlet containing solid waste, steam carries Heisui River and produces rotation along vaporization chamber barrel, in centrifugation
In the presence of power, the Heisui River containing lime-ash contacts formation liquid film with barrel, flows downward in evaporation；The air-flow of rotation is carried out simultaneously
Evaporation process.Evaporation capacity maximum determines, the steam flow flashing off is about by evaporating pressure, temperature, import discharge
40220Nm3/ h (32.5t/h), 155 DEG C of temperature；The lime-ash overwhelming majority in Heisui River enters the liquid phase after concentrating, this black water stream
Flow 198t/h, 155 DEG C of temperature, pressure 0.45MPa, solid content 1.1%, from discharge of wastewater mouth enter postorder vacuum flashing
Device carries out further flash separation process.
Flash-off steam containing higher latent heat out enters hot hydroecium through riser from cloth vapour cap；And cold water stream to be heated
Measure as 156t/h, temperature is～78 DEG C, then enter hot hydroecium from hot hydroecium's top water inlet after tank type liquid distributor distribution
Heat exchanging segment.On 7 layers of tower tray being arranged on heat exchanging segment, up steam carries out directly contact with descending cold water, and heat occurs
Transmittance process while amount, quality, the cold water absorbing steam latent heat becomes hot water, and flow increases as 179t/h, and temperature then goes up
Rise to 153 DEG C, this strand contains certain potential temperature, clean hot water leaves hot hydroecium from hot water outlet, uses for preamble system circulation, and
A small amount of steam (9.5t/h) containing incoagulable gas then leaves from overhead vapours outlet, through after system to process laggard sour gas fiery
Torch is vented.
Embodiment 2
The concrete structure setting of the tower disc type flash distillation of the present embodiment-heat-exchange integrated equipment is as shown in Figure 1；In addition,
The a diameter of 2500mm of tower body, the vaporization chamber of bottom and the hot hydroecium on top adopt same footpath, vaporization chamber height 6300mm, and hot hydroecium is high
Degree 9200mm；Set up 2 bore 300mm of water inlet containing solid waste same week, the pipe of water inlet containing solid waste inserts cylinder depth
330mm, 30 ° of semicylinder guide openings angle；Draft tube diameter 350mm, length 4000mm, totally 4, circularize and be distributed in tower
Interior；1 layer of sieve tray of setting, plate spacing 500mm in hot hydroecium's heat exchanging segment, every layer of tower tray have 220-300 perforate height be
2-6mm, aperture are the sieve aperture of 10mm, hole centre-to-centre spacing aperture ratio t/d0For 2.0；The height of weir 30mm of every layer of tower tray, height of base slot of the downcomer
20mm, the long 1000mm in weir；Downspout width 100mm, downspout area 0.073m2；One silk screen is set between tower tray and gas outlet
Demister.
So that day processes 600 tons of coal water slurry gasification systems as a example, with single above-mentioned tower tray come high pressure whole in processing system
Containing solid Heisui River.From front system containing solid Heisui River total flow 156t/h, solid content～0.6%, pressure 3.95MPa, temperature 214
℃；Described divide two strands containing solid Heisui River, the reducing pressure angle valve through being arranged on the pipe of water inlet containing solid waste front end is decompressed to after 0.50MPa, from
The pipe of water inlet containing solid waste enters flash chamber, and steam carries Heisui River and produces rotation along vaporization chamber barrel, under the influence of centrifugal force, contains
The Heisui River of lime-ash contacts formation liquid film with barrel, flows downward in evaporation；The air-flow of rotation is evaporated process simultaneously.Evaporation
Amount maximum determines, the steam flow flashing off is about 24700Nm by evaporating pressure, temperature, import discharge3/h(20.0t/
H), 158 DEG C of temperature；The lime-ash overwhelming majority in Heisui River enters the liquid phase after concentrating, the flow 144t/h of this black water stream, temperature
158 DEG C, pressure 0.50MPa, solid content 0.8%, the vacuum flash vaporizer entering postorder from discharge of wastewater mouth is further dodged
Steam separating treatment.
Flash-off steam containing higher latent heat out enters hot hydroecium through riser from cloth vapour cap；And cold water stream to be heated
Measure as 109t/h, temperature is～75 DEG C, then enter hot hydroecium from hot hydroecium's top water inlet after the distribution of tubular liquid distributor
Heat exchanging segment.On 5 layers of tower tray being arranged on heat exchanging segment, up steam carries out directly contact with descending cold water, and heat occurs
Transmittance process while amount, quality, the cold water absorbing steam latent heat becomes hot water, and flow increases as 127t/h, and temperature then goes up
Rise to 156 DEG C, this strand contains certain potential temperature, clean hot water leaves hot hydroecium from hot water outlet, uses for preamble system circulation, and
A small amount of steam (2.0t/h) containing incoagulable gas then leaves from overhead vapours outlet, through after system to process laggard sour gas fiery
Torch is vented.
Embodiment 3
The concrete structure setting of the tower disc type flash distillation of the present embodiment-heat-exchange integrated equipment is as shown in Figure 1；In addition,
The a diameter of 3800mm of tower body, the vaporization chamber of bottom and the hot hydroecium on top adopt same footpath, vaporization chamber height 7800mm, and hot hydroecium is high
Degree 9800mm；Set up 2 bore 600mm of water inlet containing solid waste same week, the pipe of water inlet containing solid waste inserts cylinder depth
400mm, 45 ° of semicylinder guide openings angle；Draft tube diameter 550mm, length about 7500mm, totally 5；Hot hydroecium's heat exchanging segment
10 layers of float valve tray of interior setting, plate spacing 700mm, every layer of tower tray there is 250-520 perforate height be 15-20mm, aperture is
The float valve of 100mm, hole centre-to-centre spacing and aperture ratio t/d0For 6.0；The height of weir 120mm of every layer of tower tray, height of base slot of the downcomer 150mm, weir is long
3420mm；Downspout width 1140mm, downspout area 2.83m2；One spiral board demister is set between tower tray and gas outlet.
So that day processes 3100 tons of coal water slurry gasification systems as a example, with single above-mentioned tower tray come high pressure whole in processing system
Containing solid Heisui River.From front system containing solid Heisui River total flow 318t/h, solid content～1.6%, pressure 3.90MPa, temperature 222
℃；Described divide two strands containing solid Heisui River, the reducing pressure angle valve through being arranged on the pipe of water inlet containing solid waste front end is decompressed to after 0.50MPa, from
The pipe of water inlet containing solid waste enters flash chamber, and steam carries Heisui River and produces rotation along vaporization chamber barrel, under the influence of centrifugal force, contains
The Heisui River of lime-ash contacts formation liquid film with barrel, flows downward in evaporation；The air-flow of rotation is evaporated process simultaneously.Evaporation
Amount maximum determines, the steam flow flashing off is about 53700Nm by evaporating pressure, temperature, import discharge3/h(43.5t/
H), 158 DEG C of temperature；The lime-ash overwhelming majority in Heisui River enters the liquid phase after concentrating, the flow 272.4t/h of this black water stream, temperature
158.8 DEG C of degree, pressure 0.50MPa, solid content 1.8%, the vacuum flash vaporizer entering postorder from discharge of wastewater mouth is carried out further
Flash separation process.
Flash-off steam containing higher latent heat out enters hot hydroecium through riser from cloth vapour cap；And cold water stream to be heated
Measure as 248t/h, temperature is～74 DEG C, then enter hot hydroecium from hot hydroecium's top water inlet after the distribution of disc type liquid distribution trough
Heat exchanging segment.On 7 layers of tower tray being arranged on heat exchanging segment, up steam carries out directly contact with descending cold water, and heat occurs
Transmittance process while amount, quality, the cold water absorbing steam latent heat becomes hot water, and flow increases as 288t/h, and temperature then goes up
Rise to 156 DEG C, this strand contains certain potential temperature, clean hot water leaves hot hydroecium from hot water outlet, uses for preamble system circulation, and
A small amount of steam (5.6t/h) containing incoagulable gas then leaves from overhead vapours outlet, through after system to process laggard sour gas fiery
Torch is vented.
Effect example 1
, will answer in embodiment 1 and Chinese patent CN01239007.0 taking single series 6.5MPa coal water slurry gasifying device as a example
With applying in the material filling type hot-water tower (prior art 1) of flash distillation-direct heat transfer technology and Chinese patent CN94117093.4
The operation key data comparative result of the commercial plant (prior art 2) of flash distillation-indirect heat exchange technology is as shown in table 1.
Table 1 6.5MPa coal water slurry gasifying device slag water treatment system primary operational data compares
From table 1, apply the material filling type hot-water tower of flash distillation-direct heat transfer technology, embodiment 1 compared to existing technology in 1
The concentration of suspension of buck that reclaims of tower disc type flash distillation-heat-exchange integrated equipment is low, water quality preferably, and heat exchange in embodiment 1
The a little higher than prior art of grey coolant-temperature gage 1 that obtains it is contemplated that in prior art 1 material filling type hot-water tower maintenance cost, embodiment 1
Tower disc type device structure operation and maintenance cost all relatively low, and the technique effect even slightly above prior art 1 can be reached, because
This than prior art 1 have more practical application meaning.
And compared to existing technology 2 flash distillation-indirect heat exchange technological process, embodiment 1 flash-off steam amount is big, though to be heated
Grey coolant-temperature gage is 77 DEG C, lower than 109 DEG C of the grey coolant-temperature gage that prior art 2 is obtained by indirect heat exchange, but through heat recovery
Afterwards, the saturation temperature of embodiment 1 output buck is 172 DEG C, and prior art 2 reclaims the buck saturation temperature obtaining and is only 123
DEG C, after gasification system runs a period of time, this temperature can be further reduced to about 50 DEG C；The gasification scale of prior art 2 is less,
But effect is not so good as embodiment 1 on the contrary；Additionally, the synthesis gas WGR that embodiment 1 goes out the battery limit (BL) that gasifies is 1.50, and prior art 2
For 1.31, embodiment 12 improves 15% compared to existing technology, and gasification battery limit (BL) energy-conservation converts into about 1.4 ten thousand tons/year of coal of mark；To sum up,
Embodiment 12 more energy efficient subtracts consumption compared to existing technology.
As described above, the water containing solid waste of high pressure belt temperature is after the flash distillation-heat-exchange integrated equipment of embodiment 1, simultaneously real
Heat recovery, water purification reuse and useless solid separation are showed, this process flow is simple, reduced investment, is an energy-saving consumption-reducing, has well
The technology of environmental benefit.
In description of the present utility model it is to be understood that term " on ", D score, "front", "rear", "left", "right",
The orientation of instruction such as " vertical ", " level ", " top ", " bottom ", " interior ", " outward " or position relationship be based on orientation shown in the drawings or
Position relationship, is for only for ease of and describes this utility model and simplify description, rather than instruction or the device or the unit that imply indication
Part must have specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to restriction of the present utility model.
Although the foregoing describing specific embodiment of the present utility model, it will be appreciated by those of skill in the art that
These are merely illustrative of, and protection domain of the present utility model is defined by the appended claims.Those skilled in the art
Member, on the premise of without departing substantially from principle of the present utility model and essence, can make numerous variations or repair to these embodiments
Change, but these changes and modification each fall within protection domain of the present utility model.
Claims (32)
1. a kind of tower disc type flash distillation-heat-exchange integrated equipment, including a tower body (1), described tower body (1) passes through tower body dividing plate (2)
It is divided into the vaporization chamber (3) of bottom and the hot hydroecium (4) on top, described tower body (1) is additionally provided with the pipe of water inlet containing solid waste (11), steams
Vapor outlet (12), water inlet (13), hot water outlet (14), discharge of wastewater mouth (15) and waste residue outlet (17), described tower body (1)
Inside is provided with riser (31)；It is characterized in that, the inside of described tower disc type flash distillation-heat-exchange integrated equipment is additionally provided with tower tray
(5), described tower tray (5) is located in the heat exchanging segment (41) of described hot hydroecium (4), and described tower tray (5) is located at water inlet distributor
(42) lower section, described tower tray (5) also includes downspout (51) and cap (52).
2. tower disc type flash distillation as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described tower tray (5) is solid valve
One of tower tray, sieve tray, float valve tray or jet tray.
3. tower disc type flash distillation as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the column plate of described tower tray (5)
Number is 1-10.
4. tower disc type flash distillation as claimed in claim 3-heat-exchange integrated equipment is it is characterised in that the column plate of described tower tray (5)
Number is 2-5.
5. tower disc type flash distillation as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the height of weir of described tower tray (5)
For 30-120mm.
6. tower disc type flash distillation as claimed in claim 5-heat-exchange integrated equipment is it is characterised in that the height of weir of described tower tray (5)
For 40-80mm.
7. tower disc type flash distillation as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the weir of described tower tray (5) is long
Compare l with tower diameterw/ D is 0.40-0.90.
8. tower disc type flash distillation as claimed in claim 7-heat-exchange integrated equipment is it is characterised in that the weir of described tower tray (5) is long
Compare l with tower diameterw/ D is 0.65-0.75.
9. tower disc type flash distillation as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the aperture of described tower tray (5)
d0For 10-100mm.
10. tower disc type flash distillation as claimed in claim 9-heat-exchange integrated equipment is it is characterised in that the hole of described tower tray (5)
Footpath d0For 30-60mm.
11. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the hole of described tower tray (5)
Centre-to-centre spacing and aperture ratio t/d0For 2.0-6.0.
12. tower disc type flash distillations as claimed in claim 11-heat-exchange integrated equipment is it is characterised in that the hole of described tower tray (5)
Centre-to-centre spacing and aperture ratio t/d0For 2.5-3.5.
13. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the opening of described tower tray (5)
Hole height is 2-20mm.
14. tower disc type flash distillations as claimed in claim 13-heat-exchange integrated equipment is it is characterised in that the opening of described tower tray (5)
Hole height is 6-15mm.
15. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that the gas of described tower tray (5)
Phase kinetic energy factor is 6-15.
16. tower disc type flash distillations as claimed in claim 15-heat-exchange integrated equipment is it is characterised in that the gas of described tower tray (5)
Phase kinetic energy factor is 7-12.
17. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described downspout (51)
Width compares W with tower diameterd/ D is 0.04-0.3.
18. tower disc type flash distillations as claimed in claim 17-heat-exchange integrated equipment is it is characterised in that described downspout (51)
Width compare W with tower diameterd/ D is 0.12-0.18.
19. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described downspout (51)
Area compares A with column areaf/ATFor 0.015-0.25.
20. tower disc type flash distillations as claimed in claim 19-heat-exchange integrated equipment is it is characterised in that described downspout (51)
Area compare A with column areaf/ATFor 0.075-0.095.
21. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described downspout (51)
Height of base slot of the downcomer is 20-150mm.
22. tower disc type flash distillations as claimed in claim 21-heat-exchange integrated equipment is it is characterised in that described downspout (51)
Height of base slot of the downcomer be 30-70mm.
23. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described riser (31)
Bottom is located in described vaporization chamber (3), and the top of described riser (31) is located in described hot hydroecium (4), described tower tray (5)
Lower section, the top of described riser (31) is provided with cloth vapour cap (32).
24. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described riser (31)
Quantity is 1-5.
25. tower disc type flash distillations as claimed in claim 23-heat-exchange integrated equipment is it is characterised in that described tower body dividing plate (2)
Top be provided with the rib (33) of fixing described riser (31).
26. tower disc type flash distillations as claimed in claim 23-heat-exchange integrated equipment is it is characterised in that described cloth vapour cap (32)
Be shaped as square or taper.
27. tower disc type flash distillations as claimed in claim 26-heat-exchange integrated equipment is it is characterised in that described cloth vapour cap (32)
Be shaped as taper.
28. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described water inlet distributor
(42) it is one of tubular liquid distributor, tank type liquid distributor, disc type liquid distribution trough or injecting type liquid distribution trough.
29. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described hot hydroecium (4)
Inside is provided with demister (43), and described demister (43) is located between described water inlet (13) and described steam (vapor) outlet (12).
30. tower disc type flash distillations as claimed in claim 29-heat-exchange integrated equipment is it is characterised in that described demister (43)
It is one of wire mesh demister or spiral board demister.
31. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described vaporization chamber (3)
Diameter and a diameter of isometrical or reducing of described hot hydroecium (4).
32. tower disc type flash distillations as claimed in claim 1-heat-exchange integrated equipment is it is characterised in that described vaporization chamber (3)
Cone section is provided with a standby discharge of wastewater mouth (16).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620536662.5U CN205948388U (en) | 2016-06-03 | 2016-06-03 | Flash distillation of tower tray formula heat transfer integration equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620536662.5U CN205948388U (en) | 2016-06-03 | 2016-06-03 | Flash distillation of tower tray formula heat transfer integration equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205948388U true CN205948388U (en) | 2017-02-15 |
Family
ID=57966741
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620536662.5U Withdrawn - After Issue CN205948388U (en) | 2016-06-03 | 2016-06-03 | Flash distillation of tower tray formula heat transfer integration equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205948388U (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106621415A (en) * | 2016-06-03 | 2017-05-10 | 华东理工大学 | Integrated column tray type flash evaporation-heat exchange apparatus |
| CN108452547A (en) * | 2017-02-22 | 2018-08-28 | 清华大学山西清洁能源研究院 | A kind of water coal slurry pressure gasification dirt vapor recovery utilizes new technological process and device |
| CN111664436A (en) * | 2019-03-07 | 2020-09-15 | 中石化广州工程有限公司 | Sieve plate tower disc type periodical pollution discharge flash tank |
| EP4140557A1 (en) | 2021-08-31 | 2023-03-01 | Air Products And Chemicals, Inc. | Integrated heat exchanger and sour water stripper |
| WO2023244572A1 (en) * | 2022-06-16 | 2023-12-21 | Lanzatech, Inc. | Liquid distributor system and process of liquid distribution |
| CN117379807A (en) * | 2023-10-11 | 2024-01-12 | 湖北圣灵科技有限公司 | Pyran production system for glutaraldehyde synthesis |
-
2016
- 2016-06-03 CN CN201620536662.5U patent/CN205948388U/en not_active Withdrawn - After Issue
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106621415A (en) * | 2016-06-03 | 2017-05-10 | 华东理工大学 | Integrated column tray type flash evaporation-heat exchange apparatus |
| CN106621415B (en) * | 2016-06-03 | 2019-06-04 | 华东理工大学 | Tower disc type flash distillation-heat-exchange integrated equipment |
| CN108452547A (en) * | 2017-02-22 | 2018-08-28 | 清华大学山西清洁能源研究院 | A kind of water coal slurry pressure gasification dirt vapor recovery utilizes new technological process and device |
| CN111664436A (en) * | 2019-03-07 | 2020-09-15 | 中石化广州工程有限公司 | Sieve plate tower disc type periodical pollution discharge flash tank |
| EP4140557A1 (en) | 2021-08-31 | 2023-03-01 | Air Products And Chemicals, Inc. | Integrated heat exchanger and sour water stripper |
| WO2023244572A1 (en) * | 2022-06-16 | 2023-12-21 | Lanzatech, Inc. | Liquid distributor system and process of liquid distribution |
| CN117379807A (en) * | 2023-10-11 | 2024-01-12 | 湖北圣灵科技有限公司 | Pyran production system for glutaraldehyde synthesis |
| CN117379807B (en) * | 2023-10-11 | 2024-03-12 | 湖北圣灵科技有限公司 | Pyran production system for glutaraldehyde synthesis |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20170215 Effective date of abandoning: 20190604 |
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| AV01 | Patent right actively abandoned |