CN215102490U - Ash water ash removal hardness reducing system - Google Patents
Ash water ash removal hardness reducing system Download PDFInfo
- Publication number
- CN215102490U CN215102490U CN202121225121.8U CN202121225121U CN215102490U CN 215102490 U CN215102490 U CN 215102490U CN 202121225121 U CN202121225121 U CN 202121225121U CN 215102490 U CN215102490 U CN 215102490U
- Authority
- CN
- China
- Prior art keywords
- cross
- hydrocyclone
- permeation
- ash removal
- flow filter
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The present disclosure provides a grey water ash removal hardness reduction system, which includes: a settling tank, a hydrocyclone, a cross-flow filter and a cross-flow circulating pump; wherein, the hydrocyclone is respectively communicated with the settling tank and the cross-flow filter; the cross-flow circulating pump is connected with the cross-flow filter in parallel and forms a closed loop path; in the ash removal and hardness reduction state, the ash water is crystallized and settled in a settling tank and then enters a hydrocyclone for separation; the separation liquid separated by the hydrocyclone and the permeation thick slurry pumped by the cross flow circulating pump respectively enter the cross flow filter and are mixed to form a mixed liquid, and a permeation clear liquid and the permeation thick slurry are formed after the permeation separation in the cross flow filter; wherein, the high-temperature high-pressure purified water is formed after the penetrating clear liquid is discharged; pumping part of the separated permeation thick slurry serving as the permeation thick slurry pumped by the cross-flow circulating pump into the cross-flow filter again; the ash water ash removal hardness reducing system disclosed by the invention can effectively remove ash and reduce hardness, and meets the requirements of high solid content and high separation precision.
Description
Technical Field
The utility model belongs to the technical field of high temperature high pressure coal gasification buck cooling, in particular to grey water ash removal hardening system.
Background
At present, most domestic and foreign coal chemical industry slag water units adopt a multi-stage flash evaporation process, the existing process adopts three stages of flash evaporation of a high-pressure flash evaporation tank, a low-pressure flash evaporation tank and a vacuum flash evaporation tank, and the effect of a flash evaporation system can be summarized as follows: reducing temperature and pressure, recovering heat, concentrating liquid, and removing fine ash and high-concentration calcium and magnesium ions in the ash water through a settling tank and normal-pressure desalting and hardening reduction technologies (such as ion exchange, normal-pressure dosing and the like) after flash evaporation so as to meet the requirement of recycling of circulating water.
The flash evaporation process has the advantages of rapid and efficient cooling and the disadvantages of serious scouring and ash entrainment. The internal structure of the flash tank is simple, after the black water enters the flash tank, the black water is subjected to reduced pressure flash evaporation and liquid-solid sedimentation separation, flash steam is discharged from an upper outlet, and liquid is discharged from a lower outlet. The flash steam is condensed to recover heat and liquid through cooling heat exchange.
In the field, a technical means for removing hardness and separating particles by an electrochemical method also exists, and the electrochemical method is difficult to apply to the working conditions of high temperature and high pressure due to electrode plates, power supply devices and the like; the ash water from the washing tower is gradually cooled and depressurized due to the fact that the washing tower cannot work at high temperature and high pressure, and is subjected to dust removal and then is pressurized to the pressure of the washing tower by a high-speed pump for recycling, so that equipment and power consumption are increased; in addition, because the dust can not be removed at high temperature, the heat exchanger can not be used for heat exchange and cooling in the cooling process, so that the cooling and pressure reduction can only be carried out by a flash evaporation method, and the equipment investment, the occupied area and the civil engineering cost are greatly increased.
In addition, in the field, a cyclone permeator, a separator, a slurry cooling tank and a centrifuge can be adopted to perform solid-liquid separation on the high-parameter black water to obtain thick slurry and clear water, the high-parameter thick slurry is separated again to obtain slurry clear water, the separated clear water can meet the requirement of clear water recycling, and the slurry is directly treated by the centrifuge to obtain ash, so that the black water treatment efficiency is improved. Although a three-stage flash system can be replaced by solid-liquid separation, the aim of improving the energy efficiency is fulfilled. However, only solid-liquid separation at high temperature and high pressure can be realized, but desalting and hardness reduction at high temperature and high pressure cannot be realized, and for high-hardness grey water, equipment such as a gasification furnace, a washing tower and the like can be scaled due to hardness improvement, and high-temperature and high-pressure recycling of washing water still cannot be realized; secondly, the commonly adopted vertical cyclone permeator is a single vertical separator with large treatment capacity, which cannot solve the contradiction between the treatment capacity and the separation efficiency and cannot realize effective separation on smaller solid particles, thereby increasing the burden of a rear-end cross flow filter and causing frequent parking; in addition, in the prior art, cross-flow filtration is usually configured as a permeate circulation system, which causes the flow velocity at the rear end of the membrane of the cross-flow filter to be too low, thereby forming a filter cake on the surface of the filter, greatly reducing the treatment capacity of the filter, and increasing the pressure drop.
SUMMERY OF THE UTILITY MODEL
In view of the above-mentioned problem that exists among the prior art, the utility model provides a desalt and fall hard, solid-liquid separation and cyclic utilization grey water ash removal and fall hard system.
In order to achieve the above object, the embodiment of the present invention adopts the following technical solutions:
the present disclosure provides a grey water ash removal hardness reduction system, which includes: a settling tank, a hydrocyclone, a cross-flow filter and a cross-flow circulating pump; wherein the hydrocyclone is respectively communicated with the settling tank and the cross-flow filter; the cross-flow circulating pump is connected with the cross-flow filter in parallel and forms a closed loop path; under the ash removal and hardness reduction state, the grey water is crystallized and settled in the settling tank and then enters the hydrocyclone for separation; the separation liquid separated by the hydrocyclone and the permeation thick slurry pumped by the cross-flow circulating pump respectively enter the cross-flow filter and are mixed to form a mixed liquid, and a permeation clear liquid and the permeation thick slurry are formed after permeation separation in the cross-flow filter; wherein, the high-temperature high-pressure purified water is formed after the penetrating clear liquid is discharged; and pumping part of the separated permeation concentrated slurry serving as the permeation concentrated slurry pumped by the cross-flow circulating pump into the cross-flow filter again through the cross-flow circulating pump.
In some embodiments of the present disclosure, the grey water ash removal and hardness reduction system further comprises an alkali liquor tank and a feed pump; the alkali liquor tank is communicated with the settling tank through the feed pump, and the hardness reducing agent is pumped into the settling tank through the feed pump.
In some embodiments of the present disclosure, the grey water ash removal hardness reduction system further comprises a horizontal decanter centrifuge; the horizontal screw centrifuge is respectively communicated with the hydrocyclone and the cross-flow filter; under the ash removal and hardness reduction state, solid particles separated by the hydrocyclone are sent to the horizontal screw centrifuge; and feeding the other part of the separated permeation concentrated slurry into the horizontal screw centrifuge, and carrying out solid-liquid separation on the separated solid particles in the horizontal screw centrifuge.
In some embodiments of the present disclosure, the cross-flow filter comprises a housing with end caps at both ends and a ceramic filtration membrane core; the shell and the end cover enclose a closed accommodating space; the ceramic filter membrane core is arranged in the shell, and two ends of the ceramic filter membrane core face to the end covers respectively; and under the state of ash removal and hardness reduction, the mixed solution permeates through the ceramic filtering membrane core to form a permeated clear solution.
In some embodiments of the present disclosure, the ceramic filtration membrane core comprises at least two tubular ceramic membranes.
In some embodiments of the present disclosure, the ceramic filtration membrane core comprises three tubular ceramic membranes.
In some embodiments of the present disclosure, the accommodating space is sequentially divided into a mixing chamber, a clear liquid chamber and a thick slurry chamber; two ends of the tubular ceramic membrane are respectively communicated with the mixing cavity and the thick slurry cavity; and under the state of ash removal and hardness reduction, the mixed solution permeates through the tubular ceramic membrane to form a permeated clear solution, and the permeated clear solution enters the clear solution cavity and is discharged out of the shell.
In some embodiments of the present disclosure, the cross-flow filter comprises a separation fluid inlet, a permeate concentrate inlet, a permeate supernatant outlet, and a permeate concentrate outlet; wherein the separation liquid inlet and the permeate thick slurry inlet are respectively positioned close to the end covers of the mixing cavity; the penetrating clear liquid outlet is positioned in the shell of the clear liquid cavity; the penetrating thick slurry outlet is positioned close to an end cover of the thick slurry cavity; the cross-flow filter is communicated with the hydrocyclone through the separation liquid inlet; two ends of the cross flow circulating pump are respectively communicated with the permeation concentrated slurry inlet and the permeation concentrated slurry outlet; the permeate concentrated slurry flowing out of the permeate concentrated slurry outlet is pumped into the cross-flow filter again through the permeate concentrated slurry inlet via the cross-flow circulating pump; the permeate clear liquid flows out through the permeate clear liquid outlet.
In some embodiments of the present disclosure, the hydrocyclone includes a mixed grey water inlet, an overflow clear liquid outlet, and an underflow concentrate outlet; the hydrocyclone is correspondingly communicated with a mixed grey water outlet of the settling tank through the mixed grey water inlet; the hydrocyclone is connected with a separation liquid inlet of the cross-flow filter through a separation liquid outlet; the hydrocyclone is connected with the underflow thick slurry inlet of the horizontal screw centrifuge through the underflow thick slurry outlet.
In some embodiments of the present disclosure, the hydrocyclone comprises at least two cyclones arranged in parallel.
Compared with the prior art, the beneficial effects of the utility model reside in that:
the ash water ash removal hardening reduction system can effectively reduce the pressure of an ash water treatment system, thereby reducing the power consumption of an ash water circulating system and reducing the energy consumption and equipment investment of an ash water circulating pump; a flash evaporation system, a settling tank and normal temperature and pressure desalting and hardness reducing technology are replaced by the combination of high-temperature and high-pressure desalting and solid-liquid separation means; in addition, the recycling of the circulating water under high temperature and high pressure is realized through the high temperature and high pressure desalting and hardness reducing technology, the temperature loss and the pressure loss of the system are reduced, the energy efficiency of the system is greatly improved, and the requirements of high solid content and high separation precision are met.
Finally, the equipment volume, the occupied area and the civil engineering cost are greatly reduced by utilizing the hydrocyclone, the cross flow filter and the horizontal screw centrifuge to replace multi-stage flash evaporation.
Drawings
In the drawings, which are not necessarily drawn to scale, like reference numerals may describe similar components in different views. Like reference numerals having letter suffixes or different letter suffixes may represent different instances of similar components. The drawings illustrate various embodiments generally by way of example and not by way of limitation, and together with the description and claims serve to explain the disclosed embodiments. The same reference numbers will be used throughout the drawings to refer to the same or like parts, where appropriate. Such embodiments are illustrative, and are not intended to be exhaustive or exclusive embodiments of the present apparatus or method.
FIG. 1 is a schematic diagram of a grey water ash removal hardness reducing system according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a cross-flow filter of a grey water ash removal and hardness reduction system according to an embodiment of the present invention.
Description of the reference numerals
1-a settling tank; 2-a hydrocyclone; 3-a cross-flow filter; 4-horizontal decanter centrifuge; 5-cross-flow circulation pump;
6-lye tank; 7-a feed pump; 8-a shell; 9-end cap; 10-ceramic filtration membrane core;
11-a tubular ceramic membrane; 12-a mixing chamber; 13-clear liquid chamber; 14-dense slurry cavity
A-a separation liquid inlet;
b-a permeate thick slurry inlet;
c-a permeate clear liquid outlet;
d-permeation thick slurry outlet
Detailed Description
The following detailed description of the embodiments of the present invention is provided with reference to the accompanying drawings, but not intended to limit the invention thereto. Embodiments of the present disclosure are described in further detail below with reference to the figures and the detailed description, but the present disclosure is not limited thereto.
All terms (including technical or scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs unless specifically defined otherwise. It will be further understood that terms, such as those defined in commonly used dictionaries, should be interpreted as having a meaning that is consistent with their meaning in the context of the relevant art and will not be interpreted in an idealized or overly formal sense unless expressly so defined herein.
Techniques, methods, and apparatus known to those of ordinary skill in the relevant art may not be discussed in detail but are intended to be part of the specification where appropriate.
At present, at coal gasification grey water cooling technical field, the in-process that carries out the high temperature solid-liquid separation of high temperature high pressure grey water and desalt and fall the hardness, the ubiquitous filter handling capacity is not enough, and power consumption is big, and equipment investment, area and civil engineering cost increase scheduling problem, for overcoming above-mentioned problem, the embodiment of the utility model provides a following technical scheme specially.
Before introducing the embodiment of the utility model, simply introduce required operational environment, grey water ash removal falls hard system and goes on under high temperature high pressure condition, has both satisfied its operation demand, can also improve separation efficiency. In addition, the grey water described herein is a grey water having a high temperature and pressure, and only under such conditions can the requirements for proper operation and separation of the ash removal and hardness reduction system be met.
The term "mixed liquor" is used herein for purposes of illustration.
The expression "mixed liquid" in the embodiments of the present application means a liquid formed by chemically reacting two different substances or simply mixing the two different substances. For example, the liquid formed after the reaction between the grey water in the settling tank 1 and the hardness reducing agent is a mixed liquid; in addition, the separation liquid separated by the hydrocyclone 2 is sent to the cross-flow filter 3, and then is directly mixed with the permeating thick slurry pumped into the cross-flow filter 3 again through the cross-flow circulating pump 5 to form a liquid which is a mixed liquid. For the convenience of reading, a part of the mixed liquid is not further distinguished in the following description, and since the mixed liquid is only used as the liquid to be treated, the mixed liquid does not substantially affect the connection relationship between the structural features in the embodiment of the present application, and is only treated for the purpose of concise text description. If the situation is not limited, the structural characteristics of the context can be directly related, and the following steps are carried out.
Referring to FIG. 1, a grey water ash removal hardness reduction system, comprising: a settling tank 1, a hydrocyclone 2, a cross-flow filter 3 and a cross-flow circulating pump 5; wherein, the hydrocyclone 2 is respectively communicated with the settling tank 1 and the cross-flow filter 3; the cross-flow circulating pump 5 is connected with the cross-flow filter 3 in parallel and forms a closed loop path; in the ash removal and hardness reduction state, the ash water is crystallized and settled in a settling tank 1 and then enters a hydrocyclone 2 for separation; the separation liquid separated by the hydrocyclone 2 and the permeation thick slurry pumped by the cross flow circulating pump 5 respectively enter the cross flow filter 3 and are mixed to form a mixed liquid, and a permeation clear liquid and the permeation thick slurry are formed after the permeation separation in the cross flow filter 3; wherein, the high-temperature high-pressure purified water is formed after the penetrating clear liquid is discharged; part of the separated permeate concentrated slurry is pumped into the cross flow filter 3 again as the permeate concentrated slurry pumped by the cross flow circulating pump 5 through the cross flow circulating pump 5. By the ash water ash removal and hardness reduction system provided by the embodiment of the utility model, about 60% of heat consumption and about 4MPa of circulating power consumption can be saved; meanwhile, the occupied area of the system and the civil engineering cost are greatly reduced. In this embodiment, through grey water ash removal system of hardening that falls, can remove the salt through high temperature high pressure and fall the hardening and solid-liquid separation replace black water flash distillation and ordinary pressure flocculation, and can reduce circulation energy consumption and calorific loss. In addition, the requirements of high solid content and high separation precision can be simultaneously met by a series solid-liquid separation combination mode of the hydrocyclone 2 and the cross flow filter 3.
In the present example, the settling tank 1 is primarily used for homogeneously mixing the hardness-reducing agent with the grey water, carrying out chemical reactions and crystallization in the course of thorough mixing, wherein the resulting product is formedSalt crystallization forms solid precipitates on the fine ash, thereby reducing the hardness of the grey water. For example, by sodium hydroxide (NaOH) and sodium dihydrogen phosphate (NaH)2PO4) The hardness reducing agent reacts with calcium and magnesium ions in the ash water to generate carbonate or phosphate, and the carbonate or the phosphate is crystallized and precipitated, so that the hardness is reduced due to the reduction of the calcium and magnesium ions. Because the ash water contains a large amount of condensed nuclei such as fine ash, carbonate or phosphate is crystallized on the fine ash, the separation difficulty is reduced, and the blocking risk is reduced.
In the present embodiment, the hydrocyclone 2 mainly uses the flow velocity of the separation liquid to form a high-speed rotating flow field therein, and performs primary separation on solid particles in the separation liquid through centrifugal force. In particular, since the hydrocyclone 2 does not include moving parts and has a simple structure, it is particularly suitable for high-temperature and high-pressure liquid-solid separation. According to the results of simulation and experiment, the separation efficiency can reach 95% for solid particles larger than 5 microns. The hydrocyclone 2 can greatly reduce the amount of fine ash entering the cross-flow filter 3 and increase the processing capacity of the cross-flow filter 3.
In this embodiment, the cross-flow circulation pump 5 is a high-flow low-lift circulation pump, which is mainly used to provide power for the circulation of the cross-flow filter 3. The hydrocyclone 2 and the cross-flow filter 3 are both high-temperature and high-pressure equipment.
In one embodiment, referring to fig. 1, the grey water ash removal and hardness reduction system further comprises an alkali liquor tank 6 and a feed pump 7; the alkali liquor tank 6 is communicated with the settling tank 1 through a feed pump 7, and the hardness reducing agent is pumped into the settling tank 1 through the feed pump 7. In this embodiment, the configuration may be made, for example, the lye tank 6 is provided with an outlet, the feed pump 7 is provided with an inlet and an outlet, and the settling tank 1 is provided with a chemical feeding inlet; the lye tank 6 is communicated with the inlet of the feed pump 7 through the outlet thereof. The lye tank 6 is arranged as a normal pressure device and is mainly used for storing the hardness-reducing medicament (or called as a desalting medicament). The feed pump 7 is communicated with the medicine feeding inlet of the settling tank 1 through the outlet thereof. The charging pump 7 is mainly used for pressurizing the solution containing the hardness reducing agent, meets the requirement of the operating pressure of the system and charges the settling tank 1.
In an embodiment, referring to FIG. 1, the grey water ash removal and hardness reduction system further comprises a horizontal decanter centrifuge 4; the horizontal screw centrifuge 4 is respectively communicated with the hydrocyclone 2 and the cross flow filter 3; under the state of ash removal and hardness reduction, solid particles separated by the hydrocyclone 2 are sent to a horizontal screw centrifuge 4; and the other part of the separated permeation concentrated slurry is sent into a horizontal screw centrifuge 4, and is subjected to solid-liquid separation with the separated solid particles in the horizontal screw centrifuge 4. In this embodiment, the horizontal decanter centrifuge 4 is mainly used for further solid-liquid separation of a mixed liquid composed of solid particles from the hydrocyclone 2 and a permeated concentrated slurry from the cross-flow filter 3, and the separated filter cake and waste salt are made to meet the transportation requirements, and simultaneously, the separated clear liquid is recycled. The clear liquid separated by the horizontal decanter centrifuge 4 and the permeating clear liquid permeated by the cross flow filter 3 are both high-temperature high-pressure purified water which can be recycled.
In one embodiment, with reference to fig. 1 and 2, cross-flow filter 3 comprises a housing 8 with end caps 9 at both ends and a ceramic filter membrane core 10; the shell 8 and the end cover 9 enclose a closed accommodating space; the ceramic filtering membrane core 10 is arranged in the shell 8, and two ends of the ceramic filtering membrane core face to the end covers 9 respectively; in the ash-removed and hardened state, the mixed solution permeates through the ceramic filtration membrane core 10 to form a permeated clear solution.
In one embodiment, the ceramic filter membrane core 10 comprises at least two tubular ceramic membranes 11.
In one embodiment, the ceramic filter membrane core 10 comprises three tubular ceramic membranes 11. In this embodiment, micropores are distributed on the tube wall of the tubular ceramic membrane, and under the action of pressure, the mixed solution flows in the tube cavity of the tubular ceramic membrane, the permeated clear solution (or small molecular substances) permeates the micropores on the tube wall, and the permeated concentrated slurry (or large molecular substances) is intercepted by the micropores, so that the purposes of separation, concentration, purification, environmental protection and the like are achieved. The tubular ceramic membrane has many advantages of high separation efficiency, stable effect, good chemical stability, acid and alkali resistance, organic solvent resistance, bacteria resistance, high temperature resistance, pollution resistance, high mechanical strength, good regeneration performance, simple separation process, low energy consumption, simple and convenient operation and maintenance, long service life and the like, and the detailed beneficial effects are not further described herein.
In an embodiment, with reference to fig. 1 and 2, the accommodating space is sequentially divided into a mixing chamber 12, a clear liquid chamber 13 and a thick liquid chamber 14; two ends of the tubular ceramic membrane 11 are respectively communicated with the mixing chamber 12 and the thick slurry chamber 14; in the state of ash removal and hardness reduction, the mixed solution permeates through the tubular ceramic membrane 11 to form a permeated clear solution, and the permeated clear solution enters the clear solution cavity 13 and is discharged out of the shell 8. In this embodiment, the inner diameter of each ceramic membrane is 10mm, the length is adjustable within a range of 1-2m, and the specific structural characteristics can be adjusted correspondingly according to actual requirements, which is not further limited herein. In addition, the arrangement of the ceramic membranes can adopt a triangular or square arrangement mode.
In one embodiment, with reference to fig. 1 and 2, the cross-flow filter 3 comprises a separation liquid inlet a, a permeate concentrate inlet B, a permeate clear liquid outlet C, and a permeate concentrate outlet D; wherein, the separation liquid inlet A and the permeation thick slurry inlet B are respectively positioned at the end cover 9 close to the mixing cavity 12; the permeate clear liquid outlet C is positioned in the shell 8 of the clear liquid cavity 13; the permeate thick liquid outlet D is positioned at the end cover 9 close to the thick liquid cavity 14; the cross-flow filter 3 is communicated with the hydrocyclone 2 through a separation liquid inlet A; two ends of the cross-flow circulating pump 5 are respectively communicated with a permeation concentrated slurry inlet B and a permeation concentrated slurry outlet D; the permeating concentrated slurry flowing out of the permeating concentrated slurry outlet D passes through the permeating concentrated slurry inlet B and is pumped into the cross flow filter 3 again through the cross flow circulating pump 5; the permeate clear solution flows out through permeate clear solution outlet C.
In this embodiment, in the ash removal and hardness reduction state, the separation liquid separated by the hydrocyclone 2 enters the mixing chamber 12 through the separation liquid inlet a, the osmotic thick slurry pumped by the cross-flow circulating pump 5 enters the mixing chamber 12 through the osmotic thick slurry inlet B, and the separation liquid and the osmotic thick slurry are mixed in the mixing chamber 12 to form a mixed liquid; the mixed liquid enters the tubular ceramic membrane 11, permeates the micropores on the tube wall of the tubular ceramic membrane 11 and permeates the tube cavity of the tubular ceramic membrane 11 to enter the thick liquid cavity 14 under the driving of the internal and external pressure difference of the tubular ceramic membrane 11, and then is discharged through the clear liquid permeating outlet C. In the process of permeating the mixed solution through the micropores, fine ash in the mixed solution is intercepted by the tubular ceramic membrane 11, so that the solid concentration in the mixed solution continuously rises, and further a permeating thick slurry is formed, flows in the tube cavity of the tubular ceramic membrane 11 under the action of pressure, flows out of the tubular ceramic membrane 11, enters the thick slurry cavity 14, is further collected and then is discharged from a permeating thick slurry outlet D.
In the above embodiment, the mixed liquid should have a certain flow rate in the tube cavity of the tubular ceramic membrane 11 during the filtration process, so as to prevent fine ash in the mixed liquid from depositing to form a filter cake, thereby reducing the filtration efficiency. Once fine ash deposition occurs to form a filter cake, backwashing is required. In the back washing process, the separation liquid inlet A is closed, the back washing liquid enters from the clear permeate outlet C, and seeps into the tube cavity from the tube cavity of the tubular ceramic membrane 11 under the action of reverse pressure difference, so that the filter cake is washed, and the washed permeate thick slurry enters the thick slurry cavity 14 and is discharged from the thick permeate slurry outlet D.
In addition, in order to ensure a high flow rate of the permeate concentrated slurry, a part of the permeate concentrated slurry is circularly pressurized by the cross flow circulating pump 5, enters the cross flow filter 3 through the permeate concentrated slurry inlet B and circulates. The cross-flow filter 3 mainly forms a cross-flow filtering mode by using a plurality of tubular ceramic membranes 11, so that fine solid particles which cannot be separated by the hydrocyclone 2 can be intercepted, and filter cake deposition can be prevented through high flow rate of mixed liquid in the tube cavities of the tubular ceramic membranes 11, and the purpose of liquid-solid separation under high temperature and high pressure is achieved.
In one embodiment, referring to FIG. 1, hydrocyclone 2 includes a mixed grey water inlet (not shown), an overflow supernatant outlet (not shown), and an underflow slurry outlet (not shown); the hydrocyclone 2 is correspondingly communicated with a mixed grey water outlet of the settling tank 1 through the mixed grey water inlet; the hydrocyclone 2 is connected with a separation liquid inlet A of the cross flow filter 3 through a separation liquid outlet; the hydrocyclone 2 is connected with the underflow thick slurry inlet of the horizontal screw centrifuge 4 through the underflow thick slurry outlet.
In an embodiment, the hydrocyclone 2 comprises at least two cyclones (not shown in the figure) arranged in parallel. The hydrocyclone 2 usually adopts a parallel combination mode of a plurality of cyclones, for example, the cyclones are arranged in parallel in a circle or a radial mode, separation liquid enters an inner cavity of each cyclone through an inlet of each cyclone, and then an upper outlet and a lower outlet of each cyclone are collected respectively and then discharged. The specific structure of the cyclones is not further described, and for example, the cyclone includes a central pipe, an upper header pipe and a lower header pipe, and the separation liquid flows from the central pipe into the inlet of each cyclone, is separated, then is collected into the upper header pipe and the lower header pipe, and is discharged through the upper outlet and the lower outlet. In this embodiment, the cyclones can be arranged in circumferential parallel or linear parallel, so that the flow velocity of each cyclone is ensured to be equal, and the separation efficiency of the cyclones is increased.
In order to fully understand the technical solution of the grey water ash removal and hardness reduction system of the embodiment of the present invention and to clearly understand the detailed process of ash removal and hardness reduction, in particular, the following will be described by dividing specific steps with reference to fig. 1 and 2, as follows:
firstly, grey water enters a settling tank 1 from an external pipe network, is fully mixed with a hardness reducing agent from an alkali liquor tank 6 and pumped into the settling tank 1 through a feed pump 7, and undergoes a chemical reaction to form a mixed solution;
secondly, the mixed solution is sent into a hydrocyclone 2 and is separated into separated liquid and solid particles under the action of centrifugal force; wherein, the separation liquid is sent into a cross flow filter 3, and the solid particles are sent into a horizontal screw centrifuge 4;
thirdly, the separation liquid and the permeation thick slurry pumped in by the cross flow circulating pump 5 respectively enter the cross flow filter 3 and are mixed to form a mixed liquid;
fourthly, the mixed solution is subjected to permeation separation in the cross flow filter 3, one part of the mixed solution is discharged in a permeation clear solution mode, and the other part of the mixed solution is discharged in a permeation thick slurry mode;
fifthly, permeating thick slurry in the previous step, wherein one part of the thick slurry is pumped into the cross flow filter 3 again through the cross flow circulating pump 5; one part is sent into a horizontal screw centrifuge 4 to be mixed with solid particles;
sixthly, mixing the permeating concentrated slurry and the solid particles in a horizontal screw centrifuge 4, and then separating; wherein a part is discharged in the form of a clear liquid; a portion is discharged in the form of a filter cake and waste salts.
After the steps, the process of removing ash and reducing hardness is finished.
Moreover, although illustrative embodiments have been described herein, the scope includes any and all embodiments having equivalent elements, modifications, omissions, combinations (e.g., of aspects across various embodiments), adaptations or alterations based on the present disclosure. The elements in the claims are to be interpreted broadly based on the language employed in the claims and not limited to examples described in the specification or during the life of the application. Further, the steps of the disclosed methods may be modified in any manner, including by reordering steps or inserting or deleting steps. It is intended, therefore, that the description be regarded as examples only, with a true scope being indicated by the following claims and their full scope of equivalents.
The above description is intended to be illustrative and not restrictive. For example, the above-described examples (or one or more aspects thereof) may be used in combination with each other. Other embodiments may be utilized, for example, by one of ordinary skill in the art, upon reading the above description. Also, in the foregoing detailed description, various features may be combined together to simplify the present disclosure. This should not be interpreted as intending that an unclaimed disclosed feature is essential to any claim. Thus, the following claims are hereby incorporated into the detailed description as examples or embodiments, with each claim standing on its own as a separate embodiment, and it is contemplated that these embodiments may be combined with each other in various combinations or permutations. The scope of the invention should be determined with reference to the appended claims, along with the full scope of equivalents to which such claims are entitled.
Claims (10)
1. An ash water ash removal hardness reduction system, comprising: a settling tank, a hydrocyclone, a cross-flow filter and a cross-flow circulating pump; wherein the content of the first and second substances,
the hydrocyclone is respectively communicated with the settling tank and the cross-flow filter;
the cross-flow circulating pump is connected with the cross-flow filter in parallel and forms a closed loop path;
under the ash removal and hardness reduction state, the grey water is crystallized and settled in the settling tank and then enters the hydrocyclone for separation;
the separation liquid separated by the hydrocyclone and the permeation thick slurry pumped by the cross-flow circulating pump respectively enter the cross-flow filter and are mixed to form a mixed liquid, and a permeation clear liquid and the permeation thick slurry are formed after permeation separation in the cross-flow filter; wherein, the high-temperature high-pressure purified water is formed after the penetrating clear liquid is discharged; and pumping part of the separated permeation concentrated slurry serving as the permeation concentrated slurry pumped by the cross-flow circulating pump into the cross-flow filter again through the cross-flow circulating pump.
2. The grey water ash removal hardness reduction system of claim 1, further comprising an lye tank and a feed pump; the alkali liquor tank is communicated with the settling tank through the feed pump, and the hardness reducing agent is pumped into the settling tank through the feed pump.
3. The grey water ash removal hardness reduction system of claim 1, further comprising a horizontal decanter centrifuge; the horizontal screw centrifuge is respectively communicated with the hydrocyclone and the cross-flow filter;
under the ash removal and hardness reduction state, solid particles separated by the hydrocyclone are sent to the horizontal screw centrifuge; and feeding the other part of the separated permeation concentrated slurry into the horizontal screw centrifuge, and carrying out solid-liquid separation on the separated solid particles in the horizontal screw centrifuge.
4. The grey water ash removal hardness reduction system of claim 1, wherein the cross-flow filter comprises a housing with end caps at both ends and a ceramic filter membrane core; the shell and the end cover enclose a closed accommodating space; the ceramic filter membrane core is arranged in the shell, and two ends of the ceramic filter membrane core face to the end covers respectively;
and under the state of ash removal and hardness reduction, the mixed solution permeates through the ceramic filtering membrane core to form a permeated clear solution.
5. The grey water ash removal hardness reduction system of claim 4, wherein the ceramic filtration membrane core comprises at least two tubular ceramic membranes.
6. The grey water ash removal hardness reduction system of claim 5, wherein the ceramic filtration membrane core comprises three tubular ceramic membranes.
7. The grey water ash removal hardness reducing system according to claim 5, wherein the accommodating space is sequentially divided into a mixing chamber, a clear liquid chamber and a thick liquid chamber; two ends of the tubular ceramic membrane are respectively communicated with the mixing cavity and the thick slurry cavity;
and under the state of ash removal and hardness reduction, the mixed solution permeates through the tubular ceramic membrane to form a permeated clear solution, and the permeated clear solution enters the clear solution cavity and is discharged out of the shell.
8. The grey water ash removal hardness reduction system of claim 7, wherein the cross-flow filter comprises a separation fluid inlet, a permeate thick slurry inlet, a permeate clear fluid outlet, and a permeate thick slurry outlet; wherein the separation liquid inlet and the permeate thick slurry inlet are respectively positioned close to the end covers of the mixing cavity; the penetrating clear liquid outlet is positioned in the shell of the clear liquid cavity; the penetrating thick slurry outlet is positioned close to an end cover of the thick slurry cavity;
the cross-flow filter is communicated with the hydrocyclone through the separation liquid inlet;
two ends of the cross flow circulating pump are respectively communicated with the permeation concentrated slurry inlet and the permeation concentrated slurry outlet; the permeate concentrated slurry flowing out of the permeate concentrated slurry outlet is pumped into the cross-flow filter again through the permeate concentrated slurry inlet via the cross-flow circulating pump;
the permeate clear liquid flows out through the permeate clear liquid outlet.
9. The grey water ash removal hardness reduction system of claim 3, wherein the hydrocyclone comprises a mixed grey water inlet, an overflow clear liquid outlet, and an underflow concentrate outlet;
the hydrocyclone is correspondingly communicated with a mixed grey water outlet of the settling tank through the mixed grey water inlet;
the hydrocyclone is connected with a separation liquid inlet of the cross-flow filter through a separation liquid outlet;
the hydrocyclone is connected with the underflow thick slurry inlet of the horizontal screw centrifuge through the underflow thick slurry outlet.
10. The grey water ash removal hardness reduction system of any of claims 1 to 9, wherein the hydrocyclone comprises at least two cyclones arranged in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121225121.8U CN215102490U (en) | 2021-06-02 | 2021-06-02 | Ash water ash removal hardness reducing system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121225121.8U CN215102490U (en) | 2021-06-02 | 2021-06-02 | Ash water ash removal hardness reducing system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215102490U true CN215102490U (en) | 2021-12-10 |
Family
ID=79302826
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202121225121.8U Active CN215102490U (en) | 2021-06-02 | 2021-06-02 | Ash water ash removal hardness reducing system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215102490U (en) |
-
2021
- 2021-06-02 CN CN202121225121.8U patent/CN215102490U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101306885B (en) | Resource process method for coking sulfur-containing waste water | |
| CN103663547A (en) | Treatment and recovery process of acid wastewater in titanium dioxide production process | |
| CN103041705B (en) | Device and method for coupling catalyst recovery process with dynamic disc membrane separation process | |
| CN102423637B (en) | Membrane separation system and purification method for purifying camphorsulfonic acid solution | |
| CN101392417A (en) | Method for recovering ion liquid solvent from cellulose spinning by combination method | |
| CN101570503B (en) | Method for concentrating low-concentration caprolactam water solution | |
| CN204614460U (en) | Boron-containing radioactive waste liquid deep purifying reclaims the equipment of boric acid simultaneously | |
| CN203545801U (en) | Boron-containing radioactive wastewater treatment device | |
| CN102633378A (en) | Method and system for recycling catalyst from coal chemical liquid waste | |
| CN215102490U (en) | Ash water ash removal hardness reducing system | |
| CN103663774A (en) | Method for treating low-concentration ammonia-containing wastewater by use of membrane separation technology | |
| CN210140501U (en) | System for handle coal gasification buck | |
| CN115432844A (en) | Ash water ash removal hardness reducing system | |
| CN104810071B (en) | Method and equipment for deep purifying of boron-containing radioactive waste liquid and recovery of boric acid | |
| CN110451529A (en) | A kind of method of purification of sodium chloride for injection | |
| CN110143710A (en) | Formation foil production line Sewage treatment utilizes method | |
| WO2022222452A1 (en) | Zero-discharge and resource recycling process for seawater desalination | |
| CN215102628U (en) | Processing system of concentrated water resourceization of high salt | |
| CN210945083U (en) | Ceramic membrane sewage treatment system convenient to regenerate | |
| CN103420520A (en) | Processing method of vanadium-containing aluminum-containing wastewater | |
| CN103435015B (en) | Technique and device for extracting sulfuric acid (H2SO4) from acid mine water | |
| CN217498959U (en) | Polymer-containing water resource recycling system | |
| CN217498967U (en) | Treatment system for battery-grade iron phosphate production wastewater | |
| CN212640040U (en) | Novel ammonium nitrate process condensate liquid processing system | |
| CN218232078U (en) | System for recovering sulfur and ammonia nitrogen in waste water of thiocarbohydrazide production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |