CN106595351B - Anti- scale removal fluid-bed heat exchanger - Google Patents
Anti- scale removal fluid-bed heat exchanger Download PDFInfo
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- CN106595351B CN106595351B CN201510666027.9A CN201510666027A CN106595351B CN 106595351 B CN106595351 B CN 106595351B CN 201510666027 A CN201510666027 A CN 201510666027A CN 106595351 B CN106595351 B CN 106595351B
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- heat exchanger
- liquid
- scale removal
- solid
- tube box
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Classifications
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F19/00—Preventing the formation of deposits or corrosion, e.g. by using filters or scrapers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28G—CLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
- F28G1/00—Non-rotary, e.g. reciprocated, appliances
- F28G1/12—Fluid-propelled scrapers, bullets, or like solid bodies
Abstract
The present invention relates to a kind of anti-scale removal fluid-bed heat exchangers, mainly to solve the easy fouling of synthetic ammonia installation decarburization alkali solution cooler tube side in traditional technology, the technical issues of long period is declined using rear heat transfer effect.The present invention includes lower tube box 1 by using one kind, heat exchanger tube 2, upper tube box 3, liquid-solid separator 4, down-comer 5, solid particle slot 6, liquid storage groove 7, liquid circulation pump 8, it is distributed case 9, ball plug 10, baffle 11, distributing disc 12, distribution grid 13, tubule 14, it is lower along casing 15, it is distributed case 9 and exports connecting hole 14, heat exchanger tube 2 connects upper tube box 3, upper tube box 3 connects liquid-solid separator 4, solid phase enters solid particle slot 6 by down-comer 5, liquid phase enters liquid storage groove 7, the technical solution for the anti-scale removal fluid-bed heat exchanger that solid phase and liquid phase circulation return lower tube box 1 preferably solves above-mentioned technical problem, it can be used for extending the cycle of operation of synthetic ammonia installation decarburization alkali solution cooler.
Description
Technical field
The invention belongs to chemical fields, specifically, belonging to chemical industry heat transmission equipment long-term operation field, are related to one kind and prevent and kill off
Dirty fluid-bed heat exchanger is widely used in solution tube side and walks liquid phase, and tube side is easy to happen the shell-and-tube heat exchanger of fouling and clogging
Long-term operation problem.
Background technology
Heat exchanger is widely used in industries such as oil, chemical industry, the energy.However, with the increase of usage time, heat exchanger
Inevitably there are dirt adhesions, are reduced so as to cause the heat exchange efficiency of heat exchanger, resistance increases, and influences heat exchanger
Normal operation.It develops anti-scale removal fluid-bed heat exchanger and replaces traditional heat exchangers, heat exchanger heat transfer effect can be improved, effectively extend
Device run time has great economic benefit.Document US005676201A discloses a kind of external circulation fluidized bed heat exchanger.
The fluid-bed heat exchanger does not fully consider that solid particle is evenly distributed with problem, thus maintains heat-transfer effect indifferent under long period.Text
It offers CN202709856U and discloses a kind of horizontal solid Circulating Fluidized Bed Heat Exchanger using Kenics static mixers.The fluidisation
Bed heat exchanger solid particle is unable to Efficient Cycle and is evenly distributed with, and is only used for horizontal heat exchanger.Document CN102840578A is disclosed
A kind of compact parallel connection type built-in fluid bed heat exchanger, but the fluid-bed heat exchanger do not consider that solid particle is evenly distributed with problem yet.It is comprehensive
It is upper described, solve the problems, such as that the uniformly distributed of solid particle is to enhance one of the key technology that heat-transfer capability is maintained under its long period.And show
There is technology to fail to solve the problems, such as this very well.
The present invention provides a kind of anti-scale removal fluid-bed heat exchanger, by being distributed case, tubule, lower along casing, ball plug, gear
The multiple equipments such as plate, distributing disc and distribution grid realize solid particle being evenly distributed in fluid-bed heat exchanger tube side, targetedly
Solve the above problem.
Invention content
The technical problem to be solved by the present invention is to the easy fouling of heat exchanger in the prior art, long period uses rear heat transfer effect
It is decreased obviously, a kind of anti-scale removal fluid-bed heat exchanger is provided, which has solid particulate distributions uniform,
The advantage that long period maintains heat-transfer effect ability strong.
In order to solve the above technical problems, the technical solution adopted in the present invention is as follows：A kind of anti-scale removal fluid-bed heat exchanger,
The anti-scale removal fluid-bed heat exchanger is by lower tube box 1, heat exchanger tube 2, upper tube box 3, liquid-solid separator 4, down-comer 5, solid
Grain slot 6, liquid storage groove 7, liquid circulation pump 8, tubule 14 and it is lower along casing 15 form.Wherein, lower tube box 1 includes distribution case 9, ball
Shape plug 10, baffle 11, distributing disc 12, distribution grid 13, ball plug 10 are mounted at distribution 9 lower inlet of case, and baffle 11 is mounted on
On ball plug 10, distributing disc 12 is mounted on baffle 11, and distribution grid 13 is mounted on distributing disc 12, is distributed 9 upper end of case
Exit connecting hole 14 is connected along casing 15, heat exchanger tube 2 with upper tube box 3 under the installation of 2 lower end of heat exchanger tube, upper tube
Case 3 connects liquid-solid separator 4, and liquid-solid separator 4 branches away two-way, and solid phase connects solid particle slot 6 by down-comer 5 all the way,
Another way liquid phase connect liquid storage groove 7, liquid storage groove 7 by liquid circulation pump 8 connect distribution case 9, solid particle slot 6 be connected into from
Pipeline of the liquid circulation pump 8 to distribution case 9.
In above-mentioned technical proposal, the distribution case 9 is the tubaeform or conical of upper and lower opening.Divide 9 osculum of cloth case
Diameter is identical as 1 entrance caliber of lower tube box, and distribution case 9 osculum end connects 1 entrance of lower tube box, distribution 9 big mouthfuls of diameters of case with
1 diameter of lower tube box is identical, distribution 9 big opening end of case arrangement tubule 14.It is distributed 0.1~0.3 that 9 height of case is the length of heat exchanger tube 2
Times.
In above-mentioned technical proposal, the tubule 14 is pipe.1.2~3 times of 14 a diameter of Solids Particle Diameter of tubule, carefully
14 length of pipe is 8mm~15mm, and 14 quantity of tubule is 2~4 times of 2 quantity of heat exchanger tube, and sealing plate can be installed additional on tubule 14.
It is described lower along 0.4 times~0.6 times that 15 caliber of casing is heat exchanger tube 2 in above-mentioned technical proposal, it is lower along casing
15 length are 15mm~50mm.It is lower to be gradually increased along 15 length of casing from heat exchanger center to heat exchanger surrounding.Heat exchanger most in
The lower of the heart does not set groove, not trepanning along casing 15.Heat exchanger surrounding it is lower along casing 15 setting groove, bevel angle are obliquely
It is 15 degree~60 degree, lower to be tapered into along 15 bevel angle of casing from heat exchanger center to heat exchanger surrounding.Under heat exchanger surrounding
At least one hole is opened along 15 outer wall of casing, open pore size is 1.2~1.5 times of solid particle average grain diameter.
In above-mentioned technical proposal, 1.2~2 times of 10 a diameter of lower tube box of the ball plug, 1 entrance caliber.
In above-mentioned technical proposal, the baffle 11 is flat, roof type, anti-roof type, square bevel-type, negative side's bevel-type or spiral shell
One kind in rotary propeller type.11 central shaft of baffle and distribution 9 central shaft of case and 1 center overlapping of axles of lower tube box.Baffle 11 is vertically thrown
The maximum length of shadow is less than or equal to 0.3 times of 1 diameter of lower tube box.
In above-mentioned technical proposal, the distributing disc 12 is the rotary body that aperture is opened on periphery, and wherein rotary body is cylinder, circle
One kind in cone, round platform or semi-round ball.1 center overlapping of axles of 12 central shaft of distributing disc and lower tube box.12 upright projection of distributing disc
Maximum length is less than or equal to 0.3 times of 1 diameter of lower tube box.12 height of distributing disc is less than or equal to the maximum length of its upright projection.
12 percent opening of distributing disc is 40%~70%, and open pore size is 1.5~2 times of solid particle average grain diameter.12 distance of distributing disc
The distance of baffle 11 is more than or equal to 30mm.
In above-mentioned technical proposal, the distribution grid 13 is porous plate.13 Facad structure of distribution grid is round, ring-like, fin
One kind in type or grizzly bar type.13 side structure of distribution grid is in plane, upper convex, lower convex, convex lens type or recessed type
It is a kind of.The distance that distribution grid 13 leaves distributing disc 12 is more than or equal to 30mm.13 a diameter of baffle 11 of distribution grid and distributing disc 12 hang down
Deliver directly shadow maximum length the greater 1.5~2 times.13 thickness of fabric swatch is 5mm~10mm.13 percent opening of fabric swatch be 50%~
80%, opening diameter is more than or equal to 2 times of solid particle average grain diameter, for any two trepanning, 13 center of range distribution plate
Remote open pore size is more than or equal to the close open pore size in 13 center of range distribution plate.
In above-mentioned technical proposal, the liquid-solid separator 4 is one kind of gravity sedimentation type or cyclone separator.
In above-mentioned technical proposal, solid particle used in the anti-scale removal fluid-bed heat exchanger is inert particle, specifically
Refer to heap density and be more than density of liquid phase, there is certain degree of hardness and intensity, and do not consolidate with what medium in use occasion system reacted
Body particle, preferably zirconium silicate pearl, corundum ball, porcelain ball, alumina bead, zirconium silicate pearl, bead, steel ball, engineering plastics, polyformaldehyde
It is one or more in particle, polytetrafluoroethylgranule granule, handstone, the wire of chopping, glueballs, more preferable bead, oxidation
Aluminium pill and zirconium silicate pearl.Solid particle average grain diameter is 2mm~5mm.Solid particle is in the anti-scale removal fluid-bed heat exchanger
Average external volume solid holdup be 3%~8%.
In order to solve the above technical problems, using a kind of method of anti-scale removal fluid-bed heat exchanger.Anti- scale removal fluidized bed heat exchanger
Recirculated water in device tubulation 2, shell side cycle synthesis ammonia lean solution.
In the above method, water squeezes into distribution case 9 from liquid storage groove 7 after liquid circulation pump 8, with solid in distribution case 9
After grain mixing, solid particle is fluidized；Liquid-solid mixture passes through baffle 11, distributing disc 12, distribution successively after squeezing ball plug 10
Plate 13, lower along casing 15 by entering after tubule 14, solid particle enters heat exchanger tube 2 along casing 15 along lower, is fluidizing
2 wall surface of heat exchanger tube is washed away under state repeatedly, under the washing away of solid particle, dirt is not easy viscous in 2 wall surface of heat exchanger tube
It is attached and tie poly-；Synthesis ammonia lean solution in tube side in water and shell side completes heat exchange.
In the above method, solid particle and water recycle in anti-scale removal fluid-bed heat exchanger.
In the above method, operated in flow rate ranging from 1.5m/s~4m/s of water in anti-scale removal fluid-bed heat exchanger tubulation 2.
It is described lower along casing 15, distribution case 9, ball plug 10, baffle 11, distribution in technical scheme of the present invention and method
The material of disk 12, distribution grid 13 and tubule 14 is stainless steel or inert material, preferably 316L stainless steels or tetrafluoroethene.The present invention
Technical solution and method in, Numerical heat transfer coefficient is come with the temperature difference and heat flux of inner wall temperature and mainstream temperature, with dimension
The time length changing rule of certain heat transfer coefficient is held to judge the fouling condition of fluid-bed heat exchanger, to as under long period
Maintain the basis for estimation of heat-transfer effect ability.
Technical solution using the present invention, it is a kind of by lower tube box 1, heat exchanger tube 2, upper tube box 3, liquid-solid separator 4, under
Drop pipe 5, solid particle slot 6, liquid storage groove 7, liquid circulation pump 8, tubule 14, it is lower along casing 15 form, lower tube box 1 include point
Cloth case 9, ball plug 10, baffle 11, distributing disc 12 and distribution grid 13, preventing and kill off along casing 15 under the installation of 2 lower end of heat exchanger tube
Dirty fluid-bed heat exchanger, achieve continuous operation after 124 days heat transfer coefficient be still maintained original 95% preferable technique effect.
Description of the drawings
Fig. 1 is the schematic diagram of anti-scale removal fluid-bed heat exchanger of the present invention.
Fig. 2 is the distribution case and tubule connection diagram of anti-scale removal fluid-bed heat exchanger of the present invention.
Fig. 3 is the lower along casing schematic diagram of anti-scale removal fluid-bed heat exchanger of the present invention.
Fig. 4 is the baffle schematic diagram of anti-scale removal fluid-bed heat exchanger of the present invention.
Fig. 5 is the distributing disc schematic diagram of anti-scale removal fluid-bed heat exchanger of the present invention.
Fig. 6 is the distribution grid schematic diagram of anti-scale removal fluid-bed heat exchanger of the present invention.
In Fig. 1,1 is lower tube box；2 be heat exchanger tube；3 be upper tube box；4 be liquid-solid separator；5 be down-comer；6 be solid
Body particle slot；7 be liquid storage groove；8 be liquid circulation pump；9 be distribution case；10 be ball plug；11 be baffle；12 be distributing disc；
13 be distribution grid；14 be tubule；15 be lower along casing.Wherein, ball plug 10, baffle 11, distributing disc 12 and distribution grid 13 are installed
Within distribution case 9.Ball plug 10 is mounted at distribution 9 lower inlet of case, and ball plug 10 installs overhead gage 11, pacifies on baffle 11
Distributing disc 12 is filled, distribution grid 13 is installed on distributing disc 12, is distributed connecting hole 14 at 9 upper end outlet of case, 2 lower end of heat exchanger tube
It is connected with upper tube box 3 along casing 15,2 upper end of heat exchanger tube under installation, upper tube box 3 connects liquid-solid separator 4, liquid-solid separator
4 out divide two-way, and solid phase connects solid particle slot 6 by down-comer 5 all the way, and another way liquid phase connects liquid storage groove 7, liquid storage
Slot 7 connects lower tube box 1 by liquid circulation pump 8, and solid particle slot 6 is connected into the pipeline from liquid circulation pump 8 to lower tube box 1.
Liquid squeezes into lower tube box 1 from liquid storage groove 7 after liquid circulation pump 8, and solid particle introduces after lower tube box 1 and liquid
It mixes, into distribution case 9, after squeezing ball plug 10, sequentially enters baffle 11, distributing disc 12 and distribution grid 13, then lead to
Cross tubule 14 enter it is lower along casing 15, hence into and wash away heat exchanger tube 2, solid particle enters upper tube box 3 after coming out, then
Into liquid-solid separator 4, liquid phase and solid phase separation in liquid-solid separator 4, liquid phase circulation returns liquid storage groove 7, under solid phase is passed through
Enter solid particle slot 6 after dropping pipe 5, the solid particle and circulation fluid to get off from solid particle slot 6 mixes, and is again introduced into down tube
Case 1 completes solid particle cycle.As shown in figure 3, lower use undergauge pattern along casing, local decompression is formed, makes solid particle more
It is easily accessible.It the lower groove along casing and opens aperture and is further ensured that solid particulate distributions are uniform.
The trepanning mode of distributing disc 12 and distribution grid 13 of the present invention does not terminate in shown in Fig. 5 and Fig. 6.
Below by embodiment and comparative example, the present invention is further elaborated, but the method for the present invention is not limited in
This.
Specific implementation mode
With reference to embodiment, the method that further illustrates the present invention.
【Embodiment 1】
Using anti-scale removal fluid-bed heat exchanger shown in FIG. 1, using Mr. Yu's synthetic ammonia installation decarbonization system alkali solution cooler,
442 heat exchanger tubes, every pipe range 4800mm are set in the anti-scale removal fluid-bed heat exchanger, caliber is 22 × 1.5mm of Φ, pipe
In equilateral triangle arrangement.Solid particle uses bead, and average grain diameter 5mm, solid particle is in the anti-scale removal fluid-bed heat exchanger
Interior average external volume solid holdup is 3%.Liquid phase is water, flow velocity 1.5m/s.It is cone shown in Fig. 2 to be distributed case.It is high to be distributed case
Spend 480mm.It is distributed tubule 1768, diameter 6mm, length 8mm.It is lower along casing caliber 12mm, arranging is：It is 1 most intermediate, length
15mm, square groove, not trepanning；7 layers totally 183, length 20mm intermediate, 60 degree of groove opens a hole, aperture 6mm, 4 layers of outside
Totally 258, length 30mm, 45 degree of groove opens two holes, aperture 7.5mm.2 times of a diameter of lower tube box import caliber of ball plug.
Baffle is flat shown in Fig. 4, and upright projection maximum length is 0.1 times of lower tube box diameter.Distributing disc is cylinder shown in Fig. 5
Type, diameter and height are 0.1 times of lower tube box diameter, percent opening 40%, aperture 8mm, apart from baffle 30mm.Distribution grid is figure
The fin-type porous plate of single layer plane shown in 6, a diameter of 0.15 times of lower tube box diameter, thickness 5mm, percent opening 50%, minimum-value aperture
10mm, range distribution disk 40mm.Under this condition, continuous operation after 92 days heat transfer coefficient be still original 95%.
【Embodiment 2】
It is cold using Mr. Yu's synthetic ammonia installation decarbonization system lye using anti-scale removal fluid-bed heat exchanger identical with embodiment 1
But device, solid particle use bead, average grain diameter 2mm, average body of the solid particle in the anti-scale removal fluid-bed heat exchanger
Product solid holdup is 8%.Liquid phase is water, flow velocity 4m/s.It is tubaeform shown in Fig. 2 to be distributed case.It is distributed case height 1440mm.Distribution
Tubule 1768, a diameter of 6mm, length 15mm.It is lower along casing caliber be 7.5mm, arranging is：Most intermediate 1, length 20mm,
Square groove, not trepanning；Intermediate 7 layers totally 183, length 30mm, 30 degree of groove opens a hole, aperture 3mm, 4 layers of outside totally 258
Root, length 50mm, 15 degree of groove open two holes, aperture 2.5mm.1.2 times of a diameter of lower tube box import caliber of ball plug.Gear
Plate is anti-roof type shown in Fig. 4, and upright projection maximum length is 0.3 times of lower tube box diameter.Distributing disc is circular cone shown in Fig. 5
Type, bottom diameter and height are 0.3 times of lower tube box diameter, percent opening 70%, aperture 4mm, apart from baffle 40mm.Distribution
Plate is convex rounded porous plate on single layer shown in Fig. 6, a diameter of 0.6 times of lower tube box diameter, thickness 10mm, percent opening 80%, most
Small-bore 6mm, range distribution disk 30mm.Under this condition, continuous operation after 110 days heat transfer coefficient be still original 95%.
【Embodiment 3】
It is cold using Mr. Yu's synthetic ammonia installation decarbonization system lye using anti-scale removal fluid-bed heat exchanger identical with embodiment 1
But device, solid particle use alumina bead, average grain diameter 5mm, solid particle being averaged in the anti-scale removal fluid-bed heat exchanger
Volume solid holdup is 3%.Liquid phase is water, flow velocity 1.5m/s.It is cone shown in Fig. 2 to be distributed case.It is distributed case height 480mm.
It is distributed tubule 1326, diameter 6mm, length 8mm.It is lower along casing caliber be 12mm diameters, arranging is：It is 1 most intermediate, length
15mm, square groove, not trepanning；Totally 183, length 20mm, middle layer 7,60 degree of groove open a hole, aperture 6mm, 4 layers of outside
Totally 258, length 30mm, 30 degree of groove opens a hole, aperture 6mm.2 times of a diameter of lower tube box import caliber of ball plug.Gear
Plate is propeller type shown in Fig. 4, and upright projection maximum length is 0.1 times of lower tube box diameter.Distributing disc is round platform shown in Fig. 5
Type, a diameter of 0.1 times of lower tube box diameter of going to the bottom, is highly 0.08 times of lower tube box diameter, percent opening 40%, aperture 8mm, away from
From baffle 30mm.Distribution grid is convex grizzly bar type porous plate under single layer shown in Fig. 6, a diameter of 0.15 times of lower tube box diameter, thickness
10mm, percent opening 50%, minimum-value aperture 10mm, range distribution disk 30mm.Under this condition, heat transfer coefficient is still after 86 days for continuous operation
It is original 95%.
【Embodiment 4】
It is cold using Mr. Yu's synthetic ammonia installation decarbonization system lye using anti-scale removal fluid-bed heat exchanger identical with embodiment 1
But device, solid particle use alumina bead, average grain diameter 2mm, solid particle being averaged in the anti-scale removal fluid-bed heat exchanger
Volume solid holdup is 8%.Liquid phase is water, flow velocity 4m/s.It is tubaeform shown in Fig. 2 to be distributed case.It is distributed case height 1440mm.Point
Cloth tubule 884, diameter 6mm, length 15mm.It is lower along casing caliber be 7.5mm, arranging is：Most intermediate 1, length 20mm, nothing
Groove, not trepanning；Intermediate 7 layers totally 183, length 30mm, 45 degree of groove opens two holes, aperture 3mm, 4 layers of outside totally 258,
Length 50mm, 15 degree of groove open two holes, aperture 3mm.1.2 times of a diameter of lower tube box import caliber of ball plug.Baffle is figure
Negative side's bevel-type shown in 4, upright projection maximum length are 0.3 times of lower tube box diameter.Distributing disc is semicircle ball-type shown in Fig. 5,
A diameter of 0.3 times of lower tube box diameter is highly 0.25 times of lower tube box diameter, percent opening 70%, aperture 4mm, apart from baffle
40mm.Distribution grid is the recessed type circular ring type porous plate of single layer shown in Fig. 6, a diameter of 0.6 times of lower tube box diameter, thickness 5mm, trepanning
Rate 80%, minimum-value aperture 6mm, range distribution disk 40mm.Under this condition, continuous operation after 124 days heat transfer coefficient be still original
95%.
【Comparative example 1】
Mr. Yu's synthetic ammonia installation decarbonization system alkali solution cooler, fluid-bed heat exchanger ginseng are applied using fluid-bed heat exchanger
According to the identical anti-scale removal fluid-bed heat exchanger with embodiment 1, it is only not provided with distribution case, ball plug, baffle, distributing disc, distribution
Plate, tubule and lower along casing, solid particle uses bead, and average grain diameter 2mm, solid particle is in the fluid-bed heat exchanger
Average external volume solid holdup is 8%.Liquid phase is water, flow velocity 4m/s.Under this condition, continuous operation after 71 days heat transfer coefficient become former
95% come.
【Comparative example 2】
Using certain traditional synthetic ammonia installation decarbonization system alkali solution cooler, liquid phase is water, flow velocity 4m/s, continuous operation
Heat transfer coefficient is just 95% originally after only 34 days.
Claims (10)
1. a kind of anti-scale removal fluid-bed heat exchanger, which is characterized in that anti-scale removal fluid-bed heat exchanger is by lower tube box (1), heat exchanger
Tubulation (2), upper tube box (3), liquid-solid separator (4), down-comer (5), solid particle slot (6), liquid storage groove (7), liquid circulation
Pump (8), tubule (14), it is lower along casing (15) form, wherein lower tube box (1) include distribution case (9), ball plug (10), baffle
(11), distributing disc (12), distribution grid (13), ball plug (10) are mounted at distribution case (9) lower inlet, and baffle (11) is mounted on
On ball plug (10), distributing disc (12) is mounted on baffle (11), and distribution grid (13) is mounted on distributing disc (12), point
Connecting hole (14) at cloth case (9) upper end outlet, along casing (15), heat exchanger tube (2) under the installation of heat exchanger tube (2) lower end
It is connected with upper tube box (3), upper tube box (3) connects liquid-solid separator (4), and liquid-solid separator (4) branches away two-way, and solid phase is logical all the way
Down-comer (5) connection solid particle slot (6) is crossed, another way liquid phase connects liquid storage groove (7), and liquid storage groove (7) is followed by liquid
Ring pumps (8) connection distribution case (9), and solid particle slot (6) is connected into the pipeline from liquid circulation pump (8) to distribution case (9).
2. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that the distribution case (9) is to open up and down
Mouthful it is tubaeform or conical, distribution case (9) osculum diameter it is identical with lower tube box (1) entrance caliber, distribution case (9) osculum end
Lower tube box (1) entrance is connected, the big mouth diameter of distribution case (9) is identical as lower tube box (1) diameter, distribution case (9) big opening end arrangement
Tubule (14)；Distribution case (9) is highly long 0.1~0.3 times of heat exchanger tube (2)；Tubule (14) is pipe, and tubule (14) is straight
Diameter is 1.2~3 times of Solids Particle Diameter, and tubule (14) length is 8mm~15mm, and tubule (14) quantity is heat exchanger tube
(2) 2~4 times of quantity, tubule can install sealing plate additional on (14).
3. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that described lower to be along casing (15) caliber
0.4 times~0.6 times of heat exchanger tube (2) caliber；It is lower along casing (15) length be 15mm~50mm；From heat exchanger center to changing
Hot device surrounding, it is lower to be gradually increased along casing (15) length；The lower of heat exchanger bosom does not set groove, not trepanning along casing (15)；
Heat exchanger surrounding it is lower along casing (15) setting groove obliquely, bevel angle is 15 degree~60 degree, from heat exchanger center to changing
Hot device surrounding, it is lower to be tapered into along casing (15) bevel angle；The lower of heat exchanger surrounding opens at least one along casing (15) outer wall
A hole, open pore size are 1.2~1.5 times of solid particle average grain diameter.
4. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that under the ball plug (10) is a diameter of
1.2~2 times of bobbin carriage (1) entrance caliber.
5. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that the baffle (11) be it is flat,
One kind in roof type, anti-roof type, square bevel-type, negative side's bevel-type or propeller type；In baffle (11) central shaft and distribution case (9)
Mandrel and lower tube box (1) center overlapping of axles；The maximum length of baffle (11) upright projection is less than or equal to lower tube box (1) diameter
0.3 times；The distributing disc (12) is the rotary body that aperture is opened on periphery, and wherein rotary body is in cylinder, circular cone, round platform or semi-round ball
One kind；Distributing disc (12) central shaft and lower tube box (1) center overlapping of axles；The maximum length of distributing disc (12) upright projection is less than
Equal to 0.3 times of lower tube box (1) diameter；Distributing disc (12) is highly less than or equal to the maximum length of its upright projection；Distributing disc
(12) percent opening is 40%~70%, and open pore size is 1.5~2 times of solid particle average grain diameter；Distributing disc (12) distance gear
The distance of plate (11) is more than or equal to 30mm.
6. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that the distribution grid (13) is porous
Plate；Distribution grid (13) Facad structure is one kind in round, ring-like, fin-type or grizzly bar type；Distribution grid (13) side structure is
One kind in plane, upper convex, lower convex, convex lens type or recessed type；The distance of distribution grid (13) range distribution disk (12) is big
In equal to 30mm；The 1.5~2 of distribution grid (13) a diameter of baffle (11) and distributing disc (12) upright projection maximum length the greater
Times；Distribution grid (13) thickness is 5mm~10mm；Distribution grid (13) percent opening is 50%~80%, and opening diameter is more than or equal to solid
2 times of body mean particle size, for any two trepanning, the remote open pore size in range distribution plate (13) center be more than or equal to away from
The open pore size close from distribution grid (13) center.
7. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that the liquid-solid separator (4) is weight
One kind of power decanter type or cyclone separator.
8. anti-scale removal fluid-bed heat exchanger according to claim 1, which is characterized in that the anti-scale removal fluid-bed heat exchanger
The solid particle used is that heap density is more than density of liquid phase, and the inertia not reacted with medium in use occasion system
Grain；Solid particle average grain diameter is 2mm~5mm；Average external volume of the solid particle in the anti-scale removal fluid-bed heat exchanger is solid
It is 3%~8% containing rate.
9. a kind of method preventing synthetic ammonia installation decarburization alkali solution cooler fouling, using any one in claim 1~8
Anti- scale removal fluid-bed heat exchanger, it is characterised in that heat exchanger tube (2) interior recirculated water, shell side cycle synthesis ammonia lean solution；Water is from liquid
Body storage tank (7) squeezes into distribution case (9) after liquid circulation pump (8), after being mixed with distribution case (9) interior solid particle, by solid
Grain fluidisation；Liquid-solid mixture passes through baffle (11), distributing disc (12), distribution grid (13) successively after squeezing ball plug (10), passes through
Enter heat exchanger tube (2) along casing (15) along lower after tubule (14), solid particle washes away heat exchange repeatedly under fluidized state
Device tubulation (2) wall surface, under the washing away of solid particle, dirt is not easy to adhere to and tie poly- in heat exchanger tube (2) wall surface；In tube side
Synthesis ammonia lean solution in water and shell side completes heat exchange；Solid particle and water recycle in anti-scale removal fluid-bed heat exchanger.
10. the method according to claim 9 for preventing synthetic ammonia installation decarburization alkali solution cooler fouling, which is characterized in that
Operated in flow rate ranging from 1.5m/s~4m/s of the interior water of the heat exchanger tube (2).
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| CN107394964A (en) * | 2017-08-08 | 2017-11-24 | 北京必可测科技股份有限公司 | A kind of descaling and antiscaling engine cooler and antiscaling method |
| CN107421347A (en) * | 2017-08-18 | 2017-12-01 | 北京必可测科技股份有限公司 | Save antiscale condenser arrangement |
| CN109654912B (en) * | 2017-10-12 | 2020-08-07 | 中国石油化工股份有限公司 | Horizontal fluidized bed heat exchanger with particle shell pass |
| CN109654924B (en) * | 2017-10-12 | 2020-08-07 | 中国石油化工股份有限公司 | Vertical fluidized bed heat exchanger with particle shell pass |
| CN109748253A (en) * | 2018-12-19 | 2019-05-14 | 安徽节源环保科技有限公司 | A method of improving wet-process phosphoric acid concentration heat exchanger fouling |
| CN111686463A (en) * | 2019-03-12 | 2020-09-22 | 天津大学 | Automatic particle adding technology in scale prevention and removal and heat transfer enhancement of circulating fluidized bed |
| CN114076527B (en) * | 2020-08-13 | 2024-03-26 | 中国石油化工股份有限公司 | Fluidized bed heat exchanger |
| CN116045724B (en) * | 2023-01-04 | 2023-08-08 | 浙江兰通空调设备有限公司 | Plate heat exchanger |
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