CN115025824A - Ion exchanger - Google Patents
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- CN115025824A CN115025824A CN202210568943.9A CN202210568943A CN115025824A CN 115025824 A CN115025824 A CN 115025824A CN 202210568943 A CN202210568943 A CN 202210568943A CN 115025824 A CN115025824 A CN 115025824A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
Abstract
The invention discloses an ion exchanger, and belongs to the technical field of purification equipment. The device comprises a shell, an upper top plate, a lower bottom plate, a pull brace rod, an upper distributor, a lower distributor and a filling layer, wherein the upper top plate and the lower bottom plate are respectively arranged at the upper side and the lower side of the shell along the radial direction; the upper distributor penetrates through one side of the shell and is fixedly connected with part or all of the stay bars, and an inlet pipe of the upper distributor is formed at one side of the upper distributor; the lower distributor penetrates through one side of the shell and is fixedly connected with part or all of the stay bars, and an inlet pipe of the lower distributor is formed at one side of the lower distributor; the filling layer is arranged above the lower bottom plate, and the filling height of the filling layer is higher than the upper horizontal tangent line of the lower distributor. It is suitable for large-scale industrial production and can save the regenerant and reduce the generation of sewage.
Description
Technical Field
The invention relates to the technical field of purification equipment, in particular to an ion exchanger.
Background
The ion exchange method is a method of exchanging a solid phase exchanger containing a certain ion with a certain ion in a solution. The method has the advantages of strong selectivity and high concentration multiple as a unique separation technology, and is applied in various fields. The ion exchange reaction is the exchange between ions, i.e. one ion in solution is adsorbed onto the exchanger while displacing an equivalent amount of the same type of ion. An ion exchanger is a reaction bed for performing an ion exchange reaction, and has two functions: exchange and regeneration. The exchange is to pass the material to be purified through an ion exchanger, and the unnecessary ions in the material are exchanged with the ions needed on the exchange resin. The regeneration is that after the ion exchange resin is saturated, the needed ions and the full and unneeded ions absorbed by the resin are exchanged by the regenerant, so that the resin can be reused. According to the above, there are two cycles of exchange and regeneration in the ion exchanger.
Disclosure of Invention
In view of the above, the present invention provides an ion exchanger, which is suitable for large-scale industrial production and can save regenerant and reduce sewage generation, thereby being more practical.
In order to achieve the first object, the technical scheme of the ion exchanger provided by the invention is as follows:
the invention provides an ion exchanger, which comprises a shell (1), an upper top plate (2), a lower bottom plate (3), a pull brace rod (4), an upper distributor (6), a lower distributor (7) and a filling layer (5),
the upper top plate (2) and the lower bottom plate (3) are respectively arranged at the upper side and the lower side of the shell (1) along the radial direction, and accommodation spaces 'are formed inside the shell (1), the upper top plate (2) and the lower bottom plate (3) in a surrounding manner'
The pull support rod (4) is supported between the upper distributor (6) and the lower distributor (7);
the upper distributor (6) penetrates through one side of the shell (1) and is fixedly connected with part or all of the stay bars (4), and an inlet pipe of the upper distributor (6) is formed on one side of the upper distributor (6);
the lower distributor (7) penetrates through one side of the shell (1) and is fixedly connected with part or all of the stay bars (4), and an inlet pipe of the lower distributor (7) is formed on one side of the lower distributor (7);
the filling layer (5) is arranged above the lower bottom plate (3), and the filling height of the filling layer (5) is higher than the upper horizontal tangent of the lower distributor (7).
The ion exchanger provided by the invention can be further realized by adopting the following technical measures.
Preferably, the ion exchanger is applied to anion exchange or cation exchange, and the material for manufacturing the ion exchanger is selected according to two application working conditions.
Preferably, the shell is made of a metal material, the metal material is selected from one of carbon steel, stainless steel, metal titanium and cast iron alloy, the diameter is larger than or equal to 1.5m, the height is larger than or equal to 1.5m, the wall thickness is larger than or equal to the calculated thickness plus 2mm, and when the shell is contacted with a corrosive medium, the shell needs to be subjected to anti-corrosion lining glue treatment.
Preferably, the tension stay bar (4) is made of the same material as the shell (1), is welded between the upper top plate (2) and the lower bottom plate (3), and needs to be subjected to anti-corrosion lining glue treatment when contacting with a corrosive medium.
Preferably, the pull support rods (4) are uniformly distributed in the accommodating space, the number of the pull support rods is determined according to the diameter of the shell and the design pressure, the distance between the pull support rods (4) and the shell (1) and the farthest distance between two adjacent pull support rods (4) are less than 30 times of the diameter of the pull support rods (4), and the number of the pull support rods is a positive integer larger than or equal to 1.
Preferably, the sectional area of a single stay bar (4) is calculated according to the following formula:
a is the cross section area of the stay bar, mm 2 ；
W is the axial load of a single tension brace rod, N;
[ Sigma ] -allowable stress of tension stay bar material at design temperature, MPa
Preferably, the upper top plate (2) and the lower bottom plate (3) are of flat plate structures, the materials of the upper top plate and the lower bottom plate are the same as those of the shell (1), the upper top plate and the lower bottom plate are welded with the shell (1), and when the upper top plate and the lower bottom plate are contacted with corrosive media, the upper top plate and the lower bottom plate need to be subjected to anti-corrosion rubber lining treatment.
Preferably, the upper top plate (2) and the lower bottom plate (3) are provided with holes with the same number and positions as the pull stay bars (4), and the pull stay bars penetrate through the holes to be welded with the upper top plate (2) and the lower bottom plate (3).
Preferably, the thicknesses of the upper top plate (2) and the lower bottom plate (3) are calculated according to the following formula:
delta-thickness of the upper top plate (2) and the lower bottom plate (3), mm;
l is the distance between the pull brace rod (4) and the shell (1), and the farthest distance between two adjacent pull brace rods (4), namely mm;
pc-design pressure, MPa;
[ sigma ] -allowable stress, MPa, of the bottom plate (3) material at design temperature;
k is the coefficient of the connecting method of the upper top plate (2) and the lower bottom plate (3);
preferably, the lower distributor (7) is positioned above the lower bottom plate (3), and the tangential distance between an inlet pipe of the lower distributor (7) and the lower bottom plate (3) is 0-20 mm;
when the device is applied to non-corrosive media, the material of the lower distributor (7) is the same as that of the shell (1), and an inlet pipe of the lower distributor (7) is welded on the shell (1); when the lower distributor (7) needs to be contacted with a corrosive medium, the lower distributor is made of an acid-resistant material and is connected and sealed with the shell (1) by a stuffing box.
Preferably, the upper distributor (6) is positioned below the upper top plate (2), and the tangential distance between the inlet pipe of the upper distributor (6) and the upper top plate (2) is calculated according to the following formula:
H＝HL×0.18+200
h is the tangential distance, mm, between the upper distributor (6) and the upper top plate (2);
HL-height of the housing (1), mm;
when the distributor is applied to non-corrosive media, the material of the upper distributor (6) is the same as that of the shell (1), and an inlet pipe of the upper distributor (6) is welded on the shell (1); when corrosive media need to be contacted, the upper distributor (6) is made of acid-resistant materials and is connected and sealed with the shell (1) by a stuffing box.
Preferably, the lower distributor (7) and the upper distributor (6) are distributed in a calandria manner, the calandria includes linear calandria or circular calandria, preferably circular calandria, the calandria is selected from one or more of a microporous pipe, a macroporous pipe covered gauze and a wire winding pipe, preferably the wire winding pipe manner, the gap of each calandria pipe is selected from 0.15 mm-0.2 mm, the discharge flow rate of the upper distributor (6) and the lower distributor (7) to the accommodating space is selected from 0.05 m/s-0.1 m/s according to the maximum exchange or regeneration flow rate, and the total flow rate of the distributors is selected from 1 m/s-1.5 m/s.
Preferably, the filling layer (5) is one or more of acid and alkali resistant anthracite particles, ceramic beads, glass beads and plastic beads, preferably ceramic beads, and the specific gravity of the filling particles is more than or equal to 1.5g/cm 3 The particle size of the particles is 5-10 times of the pore diameter of the micropores, the meshes of the coating net and the gaps of the wire winding pipe.
Preferably, the ion exchanger is further provided with one or more conventional container components selected from a manhole, a hand hole, a safety valve, an exhaust hole and a window.
Preferably, the ion exchanger is used for filling chlorine type ion exchange resin to the central line of the upper distributor (6) in anion exchange, and is used for filling sodium type ion exchange resin to the central line of the upper distributor (6) in cation exchange.
It can be seen from the above manufacturing method that the ion exchanger provided by the present invention is different from the conventional technology in three main aspects:
one is as follows: the invention gets rid of the dependence of the conventional technology on the upper and lower end sockets and replaces two flat plates, thus saving 25-30% of regenerant, but bringing about the problem that the flat plate structure is easy to deform under stress.
And the second step is as follows: the invention solves the problem of internal distribution of large-scale ion exchangers, utilizes the filling layer to isolate resin and the distributor for secondary distribution besides designing a special distributor, solves the problems of uneven distribution of the conventional ion exchanger, broken resin stopper water cap and the like, and improves the utilization rate of the resin and the exchange effect.
And thirdly: the invention is suitable for large-scale ion exchangers, and solves the problem that a large-scale project needs a plurality of sets of parallel ion exchangers because the conventional ion exchangers have small volumes.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic diagram showing the structure of an ion exchanger provided by an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a linear calandria distributor for an ion exchanger according to an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a circular calandria distributor for an ion exchanger according to an embodiment of the present invention;
fig. 4 is a schematic top view illustrating an arrangement of tie-rods in a regular triangle arrangement for an ion exchanger according to an embodiment of the present invention.
Detailed Description
In view of the above, the present invention provides an ion exchanger, which is suitable for large-scale industrial production and can save regenerant and reduce sewage generation, thereby being more practical.
The inventors have made diligent observation and found that when the ion exchange process is determined, users often have two desires, one is to improve the ion exchange effect and the other is to save regenerant.
The improvement of the ion exchange effect is sought by most users, for example, in the energy and power industry, the improvement of the ion exchange effect means that the service life of a boiler and power generation equipment is longer and the efficiency is higher, and in the propylene glycol purification field, the improvement of the ion exchange effect means that the product purity is high and the application field is wider; the improvement of the ion exchange effect in the field of dairy products means that the heavy metal ions in food are lower and the food is safer.
Saving regenerants is required for cost and emission reduction. The regenerant is required to provide the ions needed for purification on the resin and to replace the harmful ions saturated on the resin. Usually acids, bases and salts, and when acids are used as regenerants, H is supplied to the resin + Ions, metal ions and cations are replaced, and the regenerated waste liquid needs to be neutralized by alkali; when regenerated with base, OH is supplied to the resin - Ions are replaced by anions, and the regenerated waste liquid needs to be neutralized by acid; when regenerated with salt, the salt needs to be selected according to the ions required by the purification solution. The saving of regenerant means a reduction in regenerant cost and a reduction in wastewater cost.
The traditional manufacturing method of the industrial ion exchanger adopts a container comprising an upper elliptical end socket and a lower elliptical end socket as a main structure, a branch pipe capable of discharging waste regenerant is filled with resin with about 50% of equipment capacity when in use, and quartz stone and quartz sand with certain thickness are placed on the lower end socket of the early-stage ion exchanger to be used as a filter material for bearing the resin, because the resin is always lost, the manufacturing mode is gradually eliminated, and a filter plate for bearing the resin is used instead, so that the problem of resin loss is solved. This type of technology mainly involves the following four disadvantages:
first, there is no special distributor during exchange and regeneration, and for large diameter ion exchanger, exchange liquid or regenerant will permeate through the path with the least resistance, i.e. the permeable amount is more in the center of the ion exchanger and less in the periphery, resulting in low resin utilization rate during exchange and differential resin regeneration effect during regeneration, affecting the use effect.
Secondly, in order to ensure the exchange quality, most of ion exchange processes select countercurrent regeneration, namely, the regenerant enters the ion exchanger from bottom to top, and due to structural limitation, when the regeneration is finished, part of new regenerant is left in the end socket and is not contacted with resin, and the regenerant is discharged as waste acid and alkali without playing a role, so about 20% of the regenerant is wasted, and simultaneously, 20% of sewage is generated.
Thirdly, when the regeneration is finished, in order to remove the regenerated waste regenerant on the upper part of the resin layer, the waste regenerant passes through the resin layer again, and at the moment, a part of harmful ions in the waste regenerant returns to the resin to form reverse regeneration.
And fourthly, the material receiving port, the supporting leg and the bearing resin filter plate are limited by stress, the ion exchanger is difficult to be made to be very large, and a set of large water treatment and purification system needs a plurality of identical devices to operate.
From the above description, it is known that the development of an ion exchanger which can be large-sized, economical and efficient can solve the above problems, and achieve the purposes of saving production cost and reducing sewage discharge.
The existing ion exchanger comprises a container with an upper elliptical end socket and a lower elliptical end socket as a main body structure, and a resin bearing filter plate and a branch pipe capable of discharging waste regenerant are arranged in the container. The last disadvantage is that this structure is difficult to make large due to the limitations of leg stress, bottom head stress, and resin carrier stress. The inventor of the present invention has found that it is difficult to achieve the desired effect by merely adding a distributor while studying to improve the effect of large-scale ion exchange and save the regenerant, and that the real waste is derived from the use of a new regenerant and the discharge of a waste regenerant by an ion exchanger, and the distributor plays a very important role as a part of improving the use efficiency of the regenerant.
To further illustrate the technical means and effects of the present invention adopted to achieve the predetermined objects, the following detailed description of an ion exchanger according to the present invention with reference to the accompanying drawings and preferred embodiments will be made to describe the detailed embodiments, structures, features and effects thereof. In the following description, different "one embodiment" or "an embodiment" refers to not necessarily the same embodiment. Furthermore, the particular features, structures, or characteristics may be combined in any suitable manner in one or more embodiments.
The term "and/or" herein is only one kind of association relationship describing the association object, and means that three relationships may exist, for example, a and/or B, and is specifically understood as follows: both a and B may be included, a may be present alone, or B may be present alone, and any of the three cases can be provided.
Referring to fig. 1-3, the ion exchanger provided by the invention is composed of the following structures:
a1, the ion exchanger mainly comprises a shell 1, an upper top plate 2, a lower bottom plate 3, a bracing rod 4, an upper distributor 6, a lower distributor 7 and a filling layer 5;
a2, the other parts except the filling layer 5 are connected together in a welding mode or a stuffing box mode;
a3, the infill layer 5 was hand laid onto the lower plate 3.
The shell 1 is a main body for containing ion exchange resin and supporting equipment and is made of metal materials, wherein the metal materials comprise carbon steel, stainless steel, metal titanium, cast iron alloy and the like, the diameter is larger than or equal to 1.5m, and the height is larger than or equal to 1.5 m.
Further, since the resin type is different and the material to be purified is different, the resin packing shape required for the process is also different, and the resin packing amount and the aspect ratio required for the process are not within the confirmation range of the present invention, the present invention only provides that the ion exchanger is designed on the premise that the packing amount and the aspect ratio are known.
Further, when the shape of the resin filling layer 5 is determined, firstly, the diameter of the resin filling layer 5 is larger than or equal to 1.5m, and after the parameter is satisfied, according to the formula: h is calculated as HL × 0.18+200, HL is (HT +200)/0.82
H is the tangential distance, mm, between the upper distributor 6 and the upper top plate 2;
HL-housing 1 height, mm;
HT-resin filling height, mm, wherein the ion exchanger needs to be filled with resin when in use, and the resin filling height refers to the filling height of the ion exchanger filled with resin inside when in use;
the height of the housing can be calculated according to the above formula. It should be noted that the present invention is different from the general technique in that the resin filling height is half of the height of the straight barrel section of the ion exchanger, which can be simply understood as HL ═ HT × 2, and the filling ratio of the present invention is larger.
When the solution penetrates through the resin layer, the resin layer generates resistance, i.e. pressure is required to ensure a certain flow rate to penetrate through the resin layer, so that internal pressure exists in the exchange process, and the pressure has a great relationship with the type of the resin, the material to be purified and the flow rate and is not within the confirmation range of the invention. The shell needs to bear radial pressure, and shell 1 thickness can calculate shell 1's calculation thickness according to GB150-2011, for guarantee and distributor pipe and go up roof 2 and lower plate 3 welding abundant to solve and appear local loss problem after operation a period, increase 2mm in the shell 1 wall thickness need calculate the thickness.
The stay bar 4 is used for increasing the stability of the upper top plate 2 and the lower bottom plate 3, and is uniformly distributed in the ion exchanger, and when the number of the stay bars 4 is determined, three conditions are mainly met:
the number is more than or equal to 1;
the number is determined according to the diameter of the shell 1 and the design pressure, and the distance (L) between the stay bar 4 and the shell 1 and the farthest distance (L) between two adjacent stay bars 4 are less than 30 times of the diameter (d) of the stay bar 4.
The calculation formula of the sectional area of the single pull brace 4 is as follows:
a-the cross section area of the stay bar 4 is mm 2 ；
W-axial load of single brace 4, N;
[ Sigma ] -allowable stress of material of tension stay 4 at design temperature, MPa
Further, the distance between the tension brace 4 and the shell 1 and the farthest distance (L) between two adjacent tension braces 4 determine the load of the tension brace 4, the most economical mode is that the distance between the tension brace 4 and the shell 1 is equal to that between two adjacent tension braces 4, therefore, the invention recommends to adopt a triangular arrangement mode, and the quantity and the arrangement are as shown in figure 4, so that the stress of each tension brace 4 is the same.
When designing the stay bars 4, according to the above conditions, the initial number of the stay bars 4 is given, then the calculation is performed, and the back calculation is performed, and usually 2-3 times of calculation can obtain the number, diameter and arrangement mode of the stay bars 4.
After the number of the tension stay bars 4 is determined, the thicknesses of the upper top plate 2 and the lower bottom plate 3 are calculated according to the following formula:
δ — thickness of upper top plate 2 and lower bottom plate 3, mm;
l is the distance between the tension brace 4 and the shell 1, and the farthest distance between two adjacent tension braces 4, namely mm;
pc-design pressure, MPa;
[ sigma ] -allowable stress of the material at design temperature, MPa; (Upper top plate 2 and lower bottom plate 3)
K is the coefficient of the connecting method of the upper top plate 2 and the lower bottom plate 3;
where the value of K can be found in GB 150-2011.
The mode of the invention for improving the ion exchange efficiency is mainly to control the flow range of the solution (regenerant) through a lower distributor 6 and an upper distributor 7, the distributors are distributed in a calandria way, and the calandria can be composed of linear calandria or circular calandria, as shown in figure 2 and figure 3, and is preferably circular calandria. The calandria can be made by three modes of covering gauze with a microporous pipe and a macroporous pipe and winding a wire pipe, and the mode of the wire pipe is preferred. The pore diameter of the micropore, the mesh of the coated net and the gap of the wire winding pipe are selected to be between 0.15mm and 0.2mm, the discharge flow rate of the distributor to the ion exchanger is selected to be between 0.05m/s and 0.1m/s according to the maximum exchange or regeneration flow rate, and the total flow rate of the distributor is selected to be between 1m/s and 1.5 m/s. When the exchange or regeneration process is determined, the distributor can be determined based on the above parameters.
After passing through the lower distributor 7, the solution (regenerant) firstly passes through the filling layer 5, the filling layer 5 is composed of particles with large particle size, after passing through the filling layer 5, the solution (regenerant) is distributed again and then enters the resin layer, and in order to ensure the distribution effect, the specific gravity of the filling particles is more than or equal to 1.5g/cm 3 And selecting an actual gap of the distributor with the particle size of 5-10 times.
The ion exchanger does not need to be in a high floating state when resin is regenerated, and does not need the resin to move at high speed to drive the resin layer to prevent the resin from being broken, so that the resin filling height of the ion exchanger is the central line of the upper distribution pipe, and a large amount of waste regenerant is prevented from being stored in the ion exchanger.
The preparation and use of the ion exchanger of the present invention will be further illustrated by the following examples. However, the ion exchanger provided in the present invention is not limited to the solutions mentioned in the following examples, and aqueous solutions purified by ion exchange resins and ion exchangers in the existing industries are all applicable to the present invention.
Example 1:
lyocell fibre solvent purification is a representative field of ion exchanger applications, and the solvent to be purified is a 15% to 25% aqueous solution of N-methyl-morpholine oxide, which is organic amine in nature.
The invention is provided withA large-sized anion exchanger is designed and applied to the field, and the exchanger can be filled with 0.55mm of a uniform particle type anion exchange resin 160m 3 The design pressure is 0.6MPa, the shape of the resin layer is phi 5500 multiplied by 6800, and S304 is selected as the manufacturing material.
The length of the housing 1 is calculated according to the formula HL (HT +200)/0.82, HL 8537 mm. The thickness of the outer shell 1 was calculated as +2mm, the calculated thickness was 14.2mm in terms of the inner pressure container, and the thickness of the outer shell 1 was 16.2 mm.
The stay bars are arranged in a regular triangle shape, 19 stay bars are taken, and the stay bars are arranged according to a formula
The diameter of the pull brace 4 is between 64mm and 77mm, the diameter of the pull brace 4 is 70mm, and the farthest distance between adjacent pull braces 4 is 917mm, which is less than 30 times of the diameter of the pull brace 4.
The thickness of the upper top plate 2 and the lower bottom plate 3 is according to the formula
Calculated to be 41 mm.
An upper distributor 6 and a lower distributor 7 are manufactured according to the schematic diagram 3, the distributors are made of S304 distributor materials, branch pipes are made of metal wire winding pipes, and the upper distributor 6 and the lower distributor 7 are welded on the shell 1 of the ion exchanger.
After the ion exchanger is manufactured and installed according to the conditions, ceramic sand with the specific gravity of more than or equal to 2.2g/cm3 and the thickness of 1.5mm is paved on the lower bottom plate 3 and is paved on the lower distributor 7.
When in use, the upper horizontal tangent line of the upper distributor 6 is filled with 0.55mm of the homogeneous anion exchange resin, and the filling amount is about 160m 3 For mixing, 336m 3 Regenerating the resin with 4.5% sodium hydroxide (2.1 times of bed volume), washing until the effluent water is neutral, purifying 15% N-methyl-morpholine oxide water solution, wherein the chroma after purification is less than or equal to 10PCU, the conductivity is 5 mus/cm, and the purified bed volume is saturated after reaching 300BV and then carrying out regeneration treatment.
The conductivity detection method comprises the following steps: on-line conductivity meter
The chroma detection method comprises the following steps: on-line colorimeter
In this example, the ion exchanger was fabricated to be filled with 160m 3 The conventional equipment is limited by the stress of the resin bearing plate and the end socket, and the maximum length of the anion exchange resin can be 30m 3 In the case of requiring 6 conventional ion exchangers, only 1 ion exchanger of this example was required. In the embodiment, 4.5% sodium hydroxide with 2.1 times of bed volume is adopted as the regenerant to regenerate the resin, 4.5% sodium hydroxide with 3 times of bed volume is usually adopted in the conventional exchanger, but the regenerant actually contacting with the resin is only 2.4 bed volume, the conductivity reaches 5 mus/cm after being used for purifying sewage, 10 mus/cm is better than the conventional one, the volume of the exchange bed can reach 300, which is 7% higher than the common 280 bed volume, therefore, the regeneration and exchange effects of the embodiment are better than the conventional technology, and 30% of the regenerant is saved.
Example 2:
the invention relates to an important field of application of an ion exchanger in the field of sewage purification, which designs and manufactures a large cation exchanger to be applied in the field, and the exchanger can be filled with 0.65mm of uniform particle type cation exchange resin 60m 3 The design pressure is 0.4MPa, the shape of the resin layer is phi 4000 multiplied by 4800, Q235B is selected as a main material, and natural rubber is lined for anti-corrosion treatment.
The length of the housing 1 is calculated according to the formula HL (HT +200)/0.82, HL 6098 mm. The thickness of the shell 1 is calculated as the thickness +2mm, the calculated thickness is 8.4mm according to the calculation of the inner pressure container, the thickness of the shell 1 is 10.4mm, and the shell can be made of a steel plate with the nominal thickness of 12 mm.
The pull stay bars 4 are arranged in a regular triangle shape, 7 pull stay bars are taken, and the formula is adopted
The diameter of each pull support rod is 62-75 mm, the diameter of each pull support rod 4 is 65mm, and the farthest distance between every two adjacent pull support rods 4 is 1000mm and is less than 30 times of the diameter of each pull support rod 4.
The thickness of the upper top plate 2 and the lower bottom plate 3 is according to the formula
Calculated to 40 mm.
Conventional container fittings such as a manhole, an exhaust hole, a safety valve hole and the like are added on the basis of the main body data, and then corrosion-resistant and acid-resistant glue is lined, wherein the manhole refers to a device used for entering people during maintenance of the container.
An upper distributor 6 and a lower distributor 7 are manufactured according to a schematic diagram 2, the distributors adopt titanium tubes as supporting materials, a plurality of holes with the diameter of 20mm are formed in branch pipes, polypropylene filter screens with the hole diameter of 0.15mm are used for covering the branch pipes, the branch pipes are connected with an ion exchanger main body by using stuffing boxes, the distributors are fixed, and sealing is kept.
After the ion exchanger is installed, 2mm glass beads are spread on the lower base plate 3 and spread on the lower distributor 7.
When in use, the material is filled with a 0.65mm homogeneous particle type cation exchange resin to the upper horizontal tangent line of the upper distributor, and the filling amount is about 60m 3 Then, the mixture is regenerated by using 135m 35% hydrochloric acid (the volume of the bed is 2.25 times of the volume of the mixture), and the mixture is washed until effluent water is neutral, and is used for carrying out regeneration treatment after the conductivity reaches 0.75 mu s/cm after the water exchange of the purified anion exchange resin is carried out, and the conductivity reaches 1 mu s/cm after the volume of the purified bed reaches 16000 BV.
The detection method comprises the following steps: an on-line conductivity meter.
In this example, the ion exchanger thus produced was filled with 60m 3 The conventional equipment is limited by the stress of the resin bearing plate and the end socket, and the maximum length of the cation exchange resin can be 30m 3 In the case where two conventional ion exchangers are required, only one of the ion exchangers of example 1 is required. In the embodiment, 5% hydrochloric acid with 2.25 times of bed volume is adopted as the regenerant to regenerate the resin, and a conventional exchanger generally adopts 5% hydrochloric acid with 3 times of bed volume to regenerate the resin, but the actual regenerant contacting the resin is only 2.4 bed volumes, so that the electric conductivity reaches 0.75 Mus/cm after the regenerant is used for purifying sewage, the electric conductivity is better than the conventional 1 Mus/cm, the bed volume is 16000BV and is better than the conventional 15000BV, therefore, the regeneration and exchange effects of the embodiment are not lower than the conventional technology, and 25% of the regenerant is saved.
Example 3:
food purification is a brand new field of application of ion exchangers, the substance to be purified is mannitol aqueous solution, and macroporous anion exchange resin is adopted to purify the mannitol aqueous solution.
The invention designs and manufactures a medium-sized anion exchanger to be applied to the field, and the exchanger can be filled with 0.35 mm-0.85 mm of macroporous anion exchange resin 4.8m 3 The design pressure is 0.5MPa, the shape of the resin layer is phi 1600 multiplied by 2400, and S316L is selected as the manufacturing material.
The housing length is calculated according to the formula HL (HT +200)/0.82, HL 2644 mm. The shell thickness was calculated as +2mm, calculated from the internal pressure vessel, and calculated as 4.0mm, and the shell thickness was 6.0 mm.
1 brace rod is taken according to the formula
The diameter of the tension brace is between 55mm and 66mm, the diameter of the tension brace is 60mm, and the distance between the tension brace and the outer wall is 800mm which is less than 30 times of the diameter of the tension brace.
The thickness of the upper top plate and the lower bottom plate is according to the formula
Calculated 35.3 mm.
An upper distributor and a lower distributor are manufactured according to the schematic diagram 2, the distributor adopts S316L as a material, a branch pipe adopts a woven microporous pipe, and the upper distributor and the lower distributor are welded on an ion exchanger shell.
After the ion exchanger is manufactured and installed according to the conditions, the lower bottom plate is paved with 2.5 mm-3 mm materials with specific gravity more than or equal to 1.5g/cm 3 Anthracite particles are spread on the lower distributor.
When in use, the macroporous anion exchange resin with the diameter of 0.35mm to 0.85mm is filled, the upper horizontal tangent line of the upper distributor is filled, and the filling amount is about 4.8m 3 Using 10.6m 3 Regenerating the resin with 4% sodium hydroxide (2.2 times of bed volume), washing until the effluent water is neutral, purifying 10% mannitol water solution with chroma less than or equal to 5PCU, and regenerating after the purified bed volume reaches 180 BV.
The chroma detection method comprises the following steps: on-line colorimeter
In this example, 4.0% sodium hydroxide with 2.2 bed volumes is used as regenerant to regenerate resin, 4.0% sodium hydroxide with 3 bed volumes is used as regenerant to regenerate resin in conventional exchanger, but the regenerant actually contacting the resin is only 2.4 bed volumes, after purifying mannitol aqueous solution, the chroma is the same as that of conventional ion exchanger, the exchange bed volume can reach 180BV, which is the same as that of conventional ion exchanger, therefore, the regeneration and exchange effect of this example is not lower than that of conventional technology, and 27% of regenerant is saved.
As can be seen from the above embodiments, the embodiments of the present invention achieve the following technical effects:
after adopting the flat-plate type container structure, compared with the conventional ion exchanger with upper and lower end enclosures, the regeneration agent can be saved by about 20 percent, meanwhile, the reverse regeneration of the resin layer by the waste regeneration agent is prevented, and the regeneration agent can be saved by 25 to 30 percent relatively.
After the special distributor and secondary distribution are adopted, the exchange and regeneration effects can be improved, and the purification quality can be improved.
The invention gets rid of the mechanical processing and mechanical limitation of the traditional elliptical end socket and the traditional bearing plate, can be manufactured according to the process requirement, and avoids the phenomena of large occupied area, high investment and difficult operation caused by the parallel arrangement of a plurality of ion exchangers in large-scale engineering.
While preferred embodiments of the present invention have been described, additional variations and modifications in those embodiments may occur to those skilled in the art once they learn of the basic inventive concepts. Therefore, it is intended that the appended claims be interpreted as including preferred embodiments and all such alterations and modifications as fall within the scope of the invention.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (10)
1. An ion exchanger is characterized by comprising a shell (1), an upper top plate (2), a lower bottom plate (3), a pull brace rod (4), an upper distributor (6), a lower distributor (7) and a filling layer (5),
the upper top plate (2) and the lower bottom plate (3) are respectively arranged at the upper side and the lower side of the shell (1) along the radial direction, and accommodation spaces 'are formed inside the shell (1), the upper top plate (2) and the lower bottom plate (3) in a surrounding manner'
The pull support rod (4) is supported between the upper distributor (6) and the lower distributor (7);
the upper distributor (6) penetrates through one side of the shell (1) and is fixedly connected with part or all of the stay bars (4), and an inlet pipe of the upper distributor (6) is formed on one side of the upper distributor (6);
the lower distributor (7) penetrates through one side of the shell (1) and is fixedly connected with part or all of the stay bars (4), and an inlet pipe of the lower distributor (7) is formed on one side of the lower distributor (7);
the filling layer (5) is arranged above the lower bottom plate (3), and the filling height of the filling layer (5) is higher than the upper horizontal tangent of the lower distributor (7).
2. The ion exchanger of claim 1, wherein the ion exchanger is used for anion exchange or cation exchange, and the material for making the ion exchanger is selected according to two application conditions.
3. The ion exchanger of claim 1, wherein the housing is made of a metal material selected from one of carbon steel, stainless steel, metallic titanium, and cast iron alloy, having a diameter of 1.5m or more, a height of 1.5m or more, and a wall thickness of 2mm or more, and is treated with an anti-corrosive lining when contacting a corrosive medium.
4. The ion exchanger according to claim 1, wherein the tie-rod (4) is made of the same material as the housing (1), is welded between the upper top plate (2) and the lower bottom plate (3), and is treated with an anti-corrosion lining glue when contacting a corrosive medium.
5. The ion exchanger according to claim 1 or 4, wherein the tie-stay rods (4) are uniformly distributed in the accommodating space, the quantity is determined according to the diameter of the shell and the design pressure, the distance between the tie-stay rod (4) and the shell (1) and the farthest distance between two adjacent tie-stay rods (4) are less than 30 times of the diameter of the tie-stay rod (4), and the quantity is a positive integer greater than or equal to 1.
6. The ion exchanger according to claim 4 or 5, wherein the cross-sectional area of a single tie-rod (4) is calculated according to the following formula:
a is the cross section area of the stay bar, mm 2 ；
W is the axial load of a single tension brace rod, N;
[ Sigma ] -allowable stress of the stay bar material at design temperature, MPa.
7. The ion exchanger as claimed in claim 1, wherein the upper top plate (2) and the lower bottom plate (3) are of flat plate structure, are made of the same material as the housing (1), and are welded to the housing (1) and need to be treated with anti-corrosion lining glue when contacting corrosive media.
8. The ion exchanger according to claim 1 or 4, wherein the upper top plate (2) and the lower bottom plate (3) are provided with holes having the same number and positions as the stay rods (4), and the stay rods penetrate through the holes and are welded with the upper top plate (2) and the lower bottom plate (3).
9. The ion exchanger according to claim 4 or 8, wherein the thicknesses of the upper top plate (2) and the lower bottom plate (3) are calculated by the following formula:
delta-thickness of the upper top plate (2) and the lower bottom plate (3), mm;
l is the distance between the pull brace rod (4) and the shell (1), and the farthest distance between two adjacent pull brace rods (4), namely mm;
pc-design pressure, MPa;
[ sigma ] -allowable stress of the material of the soleplate (3) at the design temperature, MPa;
k is the coefficient of the connecting method of the upper top plate (2) and the lower bottom plate (3).
10. The ion exchanger according to claim 1, wherein the lower distributor (7) is located above the lower base plate (3), and the tangential distance between the inlet pipe of the lower distributor (7) and the lower base plate (3) is 0-20 mm;
when the device is applied to non-corrosive media, the material of the lower distributor (7) is the same as that of the shell (1), and an inlet pipe of the lower distributor (7) is welded on the shell (1); when corrosive media need to be contacted, the lower distributor (7) is made of acid-resistant materials and is connected and sealed with the shell (1) by a stuffing box;
preferably, the upper distributor (6) is positioned below the upper top plate (2), and the tangential distance between the inlet pipe of the upper distributor (6) and the upper top plate (2) is calculated according to the following formula:
H＝HL×0.18+200
h is the tangential distance, mm, between the upper distributor (6) and the upper top plate (2);
HL-height of the housing (1), mm;
when the device is applied to non-corrosive media, the material of the upper distributor (6) is the same as that of the shell (1), and an inlet pipe of the upper distributor (6) is welded on the shell (1); when corrosive media need to be contacted, the upper distributor (6) is made of acid-resistant materials and is connected and sealed with the shell (1) by a stuffing box;
preferably, the lower distributor (7) and the upper distributor (6) are distributed in a calandria manner, the calandria includes linear calandria or circular calandria, preferably circular calandria, the calandria is selected from one or more of a microporous pipe, a macroporous pipe covered gauze and a wire winding pipe, preferably the wire winding pipe manner, the gap of each calandria pipe is selected from 0.15 mm-0.2 mm, the discharge flow rate of the upper distributor (6) and the lower distributor (7) to the accommodating space is selected from 0.05 m/s-0.1 m/s and the flow rate of a distributor main pipe is selected from 1 m/s-1.5 m/s according to the exchange or regeneration maximum flow rate;
preferably, the filling layer (5) is one or more of acid and alkali resistant anthracite particles, ceramic beads, glass beads and plastic beads, preferably the ceramic beads, and the specific gravity of the filling particles is more than or equal to 1.5g/cm 3 The particle size of the particles is 5-10 times of the pore diameter of the micropores, the meshes of the coating net and the gaps of the wire winding pipe;
preferably, the ion exchanger is also provided with one or more conventional container components of a manhole, a hand hole, a safety valve, an exhaust hole and a window;
preferably, the ion exchanger is used for filling chlorine type ion exchange resin to the central line of the upper distributor (6) in anion exchange, and is used for filling sodium type ion exchange resin to the central line of the upper distributor (6) in cation exchange.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210568943.9A CN115025824A (en) | 2022-05-24 | 2022-05-24 | Ion exchanger |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210568943.9A CN115025824A (en) | 2022-05-24 | 2022-05-24 | Ion exchanger |
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| CN115025824A true CN115025824A (en) | 2022-09-09 |
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| CN202210568943.9A Pending CN115025824A (en) | 2022-05-24 | 2022-05-24 | Ion exchanger |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB9102057D0 (en) * | 1991-01-31 | 1991-03-13 | Permutit Co Ltd | Ion exchange apparatus |
| EP0621239A2 (en) * | 1993-04-17 | 1994-10-26 | Judo Wasseraufbereitung GmbH | Small water treatment unit based on ion exchangers with possibility to regeneration and thermal desinfection |
| CN2530715Y (en) * | 2002-03-04 | 2003-01-15 | 南通市南宝石墨设备厂 | Filtering cap type chelating resin tower |
| CN202366713U (en) * | 2011-11-30 | 2012-08-08 | 河北瑞晶康生物科技有限公司 | Ion exchange column distributor |
| CN202440541U (en) * | 2012-01-18 | 2012-09-19 | 金柯有色金属有限公司 | Distributor sieve plate device |
| CN203922760U (en) * | 2014-07-03 | 2014-11-05 | 江西省鑫盛钨业有限公司 | A kind of ion exchange unit of producing ammonium paratungstate |
| CN205035106U (en) * | 2015-08-25 | 2016-02-17 | 浙江华强环境科技有限公司 | High -efficient carbon ware that removes |
| CN207347223U (en) * | 2017-09-30 | 2018-05-11 | 常州海源恒业水处理设备有限公司 | The flat bottom cover cation and anion exchange device of a kind ofization water system equipment |
-
2022
- 2022-05-24 CN CN202210568943.9A patent/CN115025824A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB9102057D0 (en) * | 1991-01-31 | 1991-03-13 | Permutit Co Ltd | Ion exchange apparatus |
| EP0621239A2 (en) * | 1993-04-17 | 1994-10-26 | Judo Wasseraufbereitung GmbH | Small water treatment unit based on ion exchangers with possibility to regeneration and thermal desinfection |
| CN2530715Y (en) * | 2002-03-04 | 2003-01-15 | 南通市南宝石墨设备厂 | Filtering cap type chelating resin tower |
| CN202366713U (en) * | 2011-11-30 | 2012-08-08 | 河北瑞晶康生物科技有限公司 | Ion exchange column distributor |
| CN202440541U (en) * | 2012-01-18 | 2012-09-19 | 金柯有色金属有限公司 | Distributor sieve plate device |
| CN203922760U (en) * | 2014-07-03 | 2014-11-05 | 江西省鑫盛钨业有限公司 | A kind of ion exchange unit of producing ammonium paratungstate |
| CN205035106U (en) * | 2015-08-25 | 2016-02-17 | 浙江华强环境科技有限公司 | High -efficient carbon ware that removes |
| CN207347223U (en) * | 2017-09-30 | 2018-05-11 | 常州海源恒业水处理设备有限公司 | The flat bottom cover cation and anion exchange device of a kind ofization water system equipment |
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