RU2805727C2 - Device and method of sedimentation of solid sediments - Google Patents

Abstract

FIELD: deposition of solid sediments.

SUBSTANCE: invention relates in particular to the desalination of wastewater with a high salt content. The device includes a housing, a flow inlet, a discharge outlet and a substrate located in the inner chamber of the said housing. The substrate configuration is suitable for the solid to be deposited and loaded onto it. The substrate is solid particles. The device also includes an internal element in the inner chamber of the housing. The internal element contains a hollow tube coaxial with the central axis of the housing, and a partition located above the tube. The upper and lower ends of the hollow tube are open.

EFFECT: stable operation over a long period, effective removal of salts from wastewater, ability to desalinate wastewater with a high salt content.

36 cl, 4 dwg, 12 ex

Description

FIELD OF TECHNOLOGY TO WHICH THE INVENTION RELATES

The present invention relates to a solid sedimentation apparatus, in particular to a desalination apparatus for wastewater with a high salt content. The present invention also relates to a method for carrying out sedimentation of solids by said sedimentation apparatus.

BACKGROUND OF THE ART

High salt wastewater refers to wastewater with a total salt content by weight of at least 1%. The salt content of wastewater discharged from some industrial processes, such as petroleum production processes, printing and dyeing, papermaking, pharmaceuticals, chemical industry and the like, is generally about 15-25%, and the wastewater contains various substances ( including salt, oil, organic substances, heavy metals and radioactive substances), and if wastewater is directly released without treatment, the wastewater can cause great harm to aquatic organisms, domestic drinking water and water from industrial and agricultural production.

At present, research on high-salinity wastewater at home and abroad mainly contains biological methods, physicochemical methods and the like. The biological method shows a higher organic matter removal rate when treating wastewater with high salt content, but highly concentrated salt substances have an inhibitory effect on microorganisms, and the salt content of the influent water needs to be controlled. The physico-chemical method mainly contains the evaporation method, the electrochemical method, the ion exchange method, the membrane separation technology and the like, but they all have problems associated with high investment costs, high operating costs, the tendency for secondary pollution of reclaimed wastewater, and the like, and the expected cleansing effect is difficult to achieve.

CN105461134A discloses a method and apparatus for treating high-salt wastewater in the coal chemical industry, which recovers water, sodium chloride and sodium sulfate in industrial wastewater through three units: a nanofiltration salt separation unit, a multiple evaporation unit with double inlet and double outlet , and a unit for processing the mother liquor (lye) by aging.

CN104326615A discloses an energy-saving system and method for treating high-salinity wastewater. The system includes a device for concentrating salts by positive osmosis and a multiple evaporator, and the device for concentrating salts by positive osmosis includes a closed exchange unit with a membrane of the filtrate formed during reverse osmosis, a recovery device for extraction with a pulling solution and a device for extracting clean water, providing at least At least one stage of the closed exchange unit with a membrane of the filtrate formed during reverse osmosis, the recovery extraction device with a pulling solution is connected, respectively, to all stages of the closed exchange unit with a membrane of the filtrate formed during reverse osmosis by means of electric valves; the clean water extraction device is connected to the recycling device by extraction with a pulling solution; All stages of the closed exchange unit with a reverse osmosis filtrate membrane are connected in series through an electric liquid discharge valve, and all are connected to a multiple mother liquor evaporator through electric bypass valves.

CN105110542A discloses a zero-release salt separation and purification method for high-salinity industrial wastewater. The method includes stages in which sodium sulfate is first extracted in strong brine by a cooling process, the released brine is passed through an evaporator to further increase the brine concentration to 25-30%, the brine is passed into a crystallizer with forced circulation when the solid phase content in the crystallizer reaches 30 -35%, begin unloading into the hydrocyclone separator with a circulation pump to carry out preliminary separation of solid and liquid phases, pass the separated crystals containing a small amount of mother liquor into a centrifuge to complete the separation of solid and liquid phases, and pass the mother liquor, which is removed by centrifuge, directly into the mother liquor reservoir.

SUMMARY OF THE INVENTION

The inventors of the present invention have discovered a device and method for sedimentation of solid sludge through industrial research, and the said device and said method, particularly when used for desalination of wastewater with high salt content, can meet the requirements of stable operation for a long period, can effectively remove salts from wastewater, and solve the problems of difficult desalination of wastewater with a high salt content, easy clogging, and the like.

Specifically, the present invention relates to the following aspects:

1. A device for sedimentation of solid sediments (in particular, a desalination device) contains a housing (for example, a vertical housing, in particular a vertical cylindrical housing), an inlet for a flow (for example, solution, sea water or wastewater, in particular salt-containing wastewater water or high-salt wastewater that contains a solvent and a dissolved substance), a discharge outlet (namely, a flow outlet), and a support located in the inner chamber of said housing, wherein the configuration of said support is suitable for a solid that must be deposited and loaded onto it.

2. A solids deposition apparatus according to any of the above or subsequent aspects, which operates under supercritical conditions (in particular, under supercritical conditions of said solvent such as water).

3. A solid deposit deposition apparatus according to any of the above or subsequent aspects, wherein said support is selected from at least one of: solid particles (for example, selected from at least one of crystal seeds, inorganic particles such as an alumina sphere, a sphere silica, sand, quartz sand, refractory material particles such as ceramic particles, and solid waste such as slag), plates (such as non-porous plate and porous plate), gratings, meshes, cages, fibers and strips, preferably solid particles .

4. A method according to any of the above or subsequent aspects, wherein the amount (by volume) of said solid particles used comprises 1/4-3/4 (preferably 1/4-1/2) of the total volume of the inner chamber of said housing and/or equivalent the diameter of said solid particle is 0.1-1.0 mm (preferably 0.2-0.7 mm) and/or the specific surface area of said solid particle is 100-300 m ² /g and/or the bulk density of said solid particle is 0.6-0.7 g/ ^cm3 .

5. A solid precipitation deposition device according to any of the above or subsequent aspects, also comprising an internal element located in (in particular, the upper part of) an internal chamber of said housing, and said internal element contains a hollow tube substantially coaxial with the central axis of said housing, the upper and lower ends of said hollow tube are open, said hollow tube comprises an upper straight tube section and a lower conical diffusion section, there is a gap (called a first gap, in particular an annular gap) between an inner wall of said body and an outer wall of said hollow tube, said internal the element also includes a partition (such as an umbrella cap, said partition being preferably substantially coaxial with the central axis of said body) located above said hollow tube, there being a gap (called a second gap, in particular an annular gap) between said partition and the upper edge of said of a hollow tube, and there is a gap (called a sixth gap, in particular an annular gap) between said partition and the inner wall of said housing.

6. A solid precipitation apparatus according to any of the above or subsequent aspects, wherein said umbrella cap is coaxial with said hollow tube and has a conical angle of 30-150° (preferably 60-120°), and/or an outer diameter of said straight tube section of said of the hollow tube is 60-80% (preferably 67-73%) of the inner diameter of said body, and/or the height of the straight tube section of said hollow tube is
10-30% of the height of the inner chamber of said body, and/or the maximum outer diameter of said conical diffusion section of said hollow tube is 75-90% of the inner diameter of said body, and/or the height of said conical diffusion section of said hollow tube is 3-10% of the height of the inner chamber of said housing, and/or the height of said partition is 5-20% of the height of the inner chamber of said housing.

7. A solid precipitation deposition device according to any of the above or subsequent aspects, which also comprises a guide structure disposed around an inner wall of said body (preferably, its longitudinal section along the central axis of said body is a trapezoid, wherein the overlap angle is Alpha and the friction angle Beta of said trapezoid are an acute angle (preferably 5-70°)), said guide structure surrounds the inner chamber of said housing to form a channel that is open at the top and bottom (in particular, a cylindrical channel called a guide hole), said guide structure is located under said hollow tube and above said flow inlet, there is a gap (called a third gap, in particular an annular gap) between said guide structure and the lower edge of said hollow tube, and/or said guide hole substantially coaxial with the central axis of said body, and/or said the guide structure is located in the upper part of the inner chamber of the said housing.

8. A solids deposition apparatus according to any of the above or subsequent aspects, wherein said flow inlet is located at the bottom or bottom of said housing, wherein said flow inlet is designed to spray said flow into an inner chamber of said housing (said outlet structure is the flow opening is preferably a nozzle or liquid distributor), and/or said discharge outlet is located on top or at the top of said housing (preferably located above said baffle), and/or the ratio of the height of the inner chamber of said housing (unit is m ) to the inner diameter (unit of measurement - m) is 7-17, preferably 10-14, and/or the inner diameter of said guide hole is 60-80% of the inner diameter of said body, and/or the height of said guide hole is 5-15% the height of the inner chamber of the said housing.

9. A solids deposition apparatus according to any of the above or subsequent aspects, which further comprises an inlet for loading a substrate and an outlet for discharging a substrate, and/or said inlet for loading a substrate is located on top or at the top of said housing (preferably located above said guide structure, more preferably located above said baffle), and/or said substrate discharge outlet located at the bottom of said housing (preferably located below said flow inlet).

10. A solids deposition apparatus according to any of the above or subsequent aspects, which further comprises a heating agent inlet, wherein said heating agent inlet is located at the bottom or lower portion of said housing, the design of said heating agent inlet is suitable for a heating agent (e.g. , air, oxygen gas or heating gas) for spraying into the inner chamber of said housing (the structure of said heating agent inlet is preferably a nozzle or gas distributor), and/or said heating agent inlet is located above or below said flow inlet (preferably located below said flow inlet).

11. A solid precipitation deposition apparatus according to any of the above or subsequent aspects, which also comprises an inner tube (for example, a straight tubular or horn-shaped tube, in particular a straight cylindrical, said inner tube preferably being substantially coaxial with the central axis of said body), said a heating agent inlet is located at the bottom of said body, there is a gap between the inner wall of said body and the outer wall of said inner tube (called a fourth gap, in particular an annular gap), there is a gap between the bottom edge or inner wall of said inner tube and said inlet heating agent (called a fifth gap, particularly an annular gap), said fifth gap communicates with said fourth gap and the interior of said inner tube, said inner tube is configured such that said heating agent imported from said heating agent inlet is essentially completely enters the interior space of said inner tube, said flow inlet is located in said fourth gap and under the upper edge of said inner tube, and/or the space of the inner chamber of said housing located under the upper edge of said inner tube is called a buffer zone, hereinafter referred to the buffer zone contains 25-40% or
20-60% of the total volume of the inner chamber of said housing, and/or the structure of said heating agent inlet is a gas distributor (preferably substantially coaxial with the central axis of said housing), and said inner tube is located above or contains said gas distributor , both separated by said fifth gap, and/or said inner tube is located under said guide structure, and/or said flow inlet is 100-500 mm below the upper edge of said inner tube in the vertical direction, and/or the outer diameter of said inner tube is 60-80% (preferably 67-73%) of the inner diameter of said body, and/or the height of said inner tube is 20-60% (preferably 30-50%) of the height of the inner chamber of said body, and/or said inner tube is located in the lower parts of the inner chamber of said housing.

12. A solids deposition method (in particular, a desalination method), which comprises the step of passing a stream containing a solute (such as an inorganic salt) and a solvent (such as water) into a solids deposition device according to any of the above or subsequent aspects to cause at least a portion of the solute to precipitate (eg, precipitate due to a precipitation reaction or due to supersaturation) and load onto said support located in the inner chamber of said housing.

13. A method of solid precipitation according to any of the above or subsequent aspects, in which said stream is held in a subcritical state (in particular, below the supercritical temperature of said solvent, for example, from room temperature to a temperature of 1-15) before entering said solid precipitation device °C, 4-10°C or 6-8°C below the supercritical temperature of said solvent (in particular water), more, in particular, at or above the supercritical pressure of said solvent, but below the supercritical temperature of said solvent, e.g. room temperature to a temperature of 1-15°C, 4-10°C or 6-8°C below the supercritical temperature of said solvent (in particular water), and/or the temperature of said substrate above the supercritical temperature of said solvent (for example, a temperature of 1 -15°C, 4-10°C or 6-8°C above said supercritical temperature), and/or a substrate is added to the inner chamber of said housing, and the temperature of said substrate is higher than the supercritical temperature of said solvent (for example, a temperature of 1-15 °C, 4-10°C or 6-8°C of the above-mentioned supercritical temperature), and/or said substrate and said stream are in such a proportion that, after mixing them, the temperature of said stream reaches or exceeds the supercritical temperature of said solvent.

14. A solid precipitation method according to any of the above or subsequent aspects, wherein the operating conditions for the inner chamber of said housing include: operating pressure 23-35 MPa gauge (preferably 25-30 MPa gauge), operating temperature 350-650 °C (preferably 380-650°C, 450-600°C or 450-550°C), flow retention time 10-1800 seconds (preferably 60-600 seconds), and flow rate 1.5-270 h ^-1 .

15. A method of deposition of solid precipitates according to any of the above or subsequent aspects, wherein a heating agent is added to an inner chamber of said housing, and said heating agent is used in such an amount that said flow, after entering the inner chamber of said housing, forms a supercritical state (for example , reaches or exceeds the supercritical temperature of said solvent), and/or said stream is a salt-containing wastewater or a wastewater with a high salt content (in particular, an organic wastewater with a high salt content), said heating agent is an oxidizing gas (for example, oxygen gas or air), and/or said heating agent and said stream are in such proportion that, after mixing thereof, the temperature of said stream reaches or exceeds the supercritical temperature of said solvent, and/or said heating agent and said stream are in such proportion that the temperature of said stream upon exiting the upper edge of said inner tube reaches or exceeds the supercritical temperature of said solvent, and/or the amount of said heating agent used is 100-500%, preferably 150-350% of the theoretical oxygen demand for oxidation of said stream.

16. A method for settling solids according to any of the above or subsequent aspects, wherein a pH adjusting agent is added to said flow and/or into an inner chamber of said housing, and said pH adjusting agent is used in such an amount that the pH value contents in the inner chamber of said housing was maintained at 9-13.

17. A method for depositing solids according to any of the above or subsequent aspects, wherein said stream enters a lower portion of an inner chamber of said housing from said stream inlet, said substrate enters an upper portion of an inner chamber of said housing from said substrate loading inlet, and then enters the lower portion of the inner chamber of said housing through said first gap, said third gap and said guide hole, said flow causes said substrate to be in a fluid state, at least a portion of said solute is deposited and loaded onto said substrate to form a loaded substrate , a portion of said loaded substrate is moved to the bottom of the inner chamber of said housing, and discharged from the inner chamber of said housing from said substrate discharge outlet, another portion of said loaded substrate is moved to the top of the inner chamber of said housing along with said flow, from which at least As much as a portion of the solute is removed (called a purified stream), passes through said guide orifice, enters said straight section of tubing from said conical diffusion section, and is then discharged from said second gap, said loaded substrate flows to the bottom of the inner chamber of said housing through said a first gap, said third gap and said guide hole, said purified stream is moved up the inner chamber of said housing through said sixth gap, and discharged from the inner chamber of said housing from said discharge outlet,

or,

said substrate enters the upper portion of the inner chamber of said housing from said substrate loading inlet, and then enters the lower portion of the inner chamber of said housing through said first gap, said third gap, and said guide hole,

said flow enters said fourth gap from said flow inlet and then enters the interior of said inner tube through said fifth gap and mixes with said heating agent which enters the interior of said inner tube from said heating agent inlet to form a mixture which is discharged from said inner tube from an upper edge of said inner tube after the temperature has risen to reach or exceed the supercritical temperature of said solvent,

a portion of said mixture flows back into the interior of said inner tube through said fourth gap and said fifth gap (forming an internal recycle), another portion of said mixture causes said substrate to be in a fluid state, at least a portion of said solute is deposited and loaded onto said substrate to form a loaded substrate, a portion of said loaded substrate is moved to the bottom of the inner chamber of said housing through said fourth gap, and discharged from the inner chamber of said housing from said substrate discharge outlet, another portion of said loaded substrate is moved to the top of the inner chamber of said housing together with said mixture from which at least a portion of the solute is removed (called the purified mixture), passes through said guide hole, enters said straight section of tubing from said conical diffusion section, and is then discharged from said second gap, said loaded substrate flows back to the bottom of the inner chamber of said body through said first gap, said third gap and said guide hole, said purified mixture is moved up the inner chamber of said body through said sixth gap, and discharged from the inner chamber of said body from said discharge outlet.

18. A method of settling solid sludge according to any of the above or subsequent aspects, wherein said stream is a high-salt wastewater (in particular, a high-salt organic wastewater), said high-salt wastewater having a TDS of no higher than 20% wt. (preferably 5-20% wt.), and a COD greater than 20,000 mg/L (preferably 20,000-200,000 mg/L or 20,000-40,000 mg/L).

On the other hand, the present invention relates to the following aspects:

1. A method for treating organic wastewater with high salt content, which is characterized by the presence of the following contents: organic wastewater with high salt content and an oxidizing agent are introduced into a fluidized bed reactor to carry out the reaction under supercritical water oxidation conditions, the salt in the wastewater is deposited on the solid particles of the reactor fluidized bed, and the post-reactive stream meets the emission requirements after gas-liquid separation.

2. A method according to any of the above or subsequent aspects, which is characterized in that: in organic wastewater with a high salt content, the COD is of the order of tens of thousands of mg/l to hundreds of thousands of mg/l, preferably 20,000-200,000 mg/l, TDS is no more than 20% by weight, preferably 5% by weight - 20% by weight.

3. A method according to any of the above or subsequent aspects, characterized in that: the oxidizing agent is at least one of air and oxygen gas, and the amount used is 100%-500%, preferably 150%-350% of the theoretical requirement for oxygen for wastewater oxidation.

4. A method according to any of the above or subsequent aspects, characterized in that: the solid particle in the fluidized bed reactor is at least one of an alumina ceramic pellet and a silicon pellet.

5. A method according to any of the above or subsequent aspects, characterized in that: the solid particle has a diameter of 0.1-1.0 mm, preferably 0.2-0.7 mm, a specific surface area of 100-300 m ² /g, and bulk density 0.6-0.7 g/ ^cm3 .

6. A method according to any of the above or subsequent aspects, characterized in that: solid particles are added in an amount of 1/4-3/4 of the reactor volume.

7. A method according to any of the above or subsequent aspects, characterized in that: the fluidized bed reactor is provided with a real-time solids loading and unloading system, and the solids are periodically loaded into and discharged from the fluidized bed reactor.

8. A method according to any of the above or subsequent aspects, characterized in that: the discharged salt-containing solid particles are subjected to ultrasonication, high-temperature stirring, polishing and the like to extract salt deposited on the particles to effect regeneration of the particles.

9. A method according to any of the above or subsequent aspects, which is characterized in that: the operating pressure of supercritical water oxidation is 23 MPa-30 MPa, the operating temperature is 380°C-650°C, preferably 450°C-600°C, and reaction time ranges from 10 seconds to 180 seconds.

10. A method according to any of the above or subsequent aspects, characterized in that: the supercritical water oxidation stream enters a gas-liquid separation tank, the liquid phase is discharged after heat exchange with the incoming reactor wastewater, or the incoming wastewater is diluted, the COD content of the incoming into the supercritical water oxidation reactor remains stable, and the reaction is carried out stably, avoiding large temperature fluctuations in the reactor.

11. A method according to any of the above or subsequent aspects, characterized in that: an appropriate amount of alkaline solution is added to the influent wastewater, and the pH of the influent water is controlled to 9-13.

12. A method according to any of the above or subsequent aspects, characterized in that: the alkaline solution is at least one of a sodium hydroxide solution and a potassium hydroxide solution.

Technical result

The present invention may achieve at least one of the following technical results.

(1) The solid precipitation deposition apparatus and method, in particular, the desalination apparatus and method according to the present invention, provides easy operation, can meet the requirements of stable operation for a long period (such as continuous operation for 20 days or more, preferably continuous operation for 30 days or more, 50 days or more, or 100 days or more), can realize highly efficient desalination of wastewater, and solve the problems of difficult desalination of wastewater with high salt content and easy sedimentation or clogging in the device and pipelines.

(2) The solids sedimentation apparatus and method, in particular, the desalination apparatus and method according to the present invention uses specific internal elements to achieve highly efficient separation of solids and demineralized stream, avoids large transfer of solids, and at the same time can ensure stable operation for a long period (eg, continuous running for 20 days or more, preferably continuous running for 30 days or more, 50 days or more, or 100 days or more).

(3) The solid sediment precipitation device and method, in particular, the desalination device and method according to the present invention arranges a buffer zone and uses the heat generated from the oxidation of organic matter in wastewater to increase the reaction temperature, so the salt precipitation area is controlled, not only organic matter can be decomposed and removed, but also avoid sedimentation and clogging at the bottom of the desalination device, so achieve the effect of killing two birds with one stone.

(4) According to one preferred embodiment of the present invention, taking into account the properties of organic wastewater with high salt content, a fluidized bed reactor is combined with supercritical water oxidation technology to treat organic wastewater with high salt content. After treatment, the desalination rate of wastewater is above 95%, the COD removal rate can reach 99% or more, the COD of discharged water is <60 mg·L, and the requirement for direct discharge is met.

BRIEF DESCRIPTION OF THE DRAWINGS

Fig. 1 is a flow diagram of one embodiment of the desalination method of the present invention,

on which 1 is a heat exchanger, 2 is a fluidized bed reactor, 3 is a gas-liquid separation tank, 4 is a real-time solids loading system and 5: a real-time solids unloading system.

Fig. 2 is a block diagram of an embodiment of the desalination apparatus of the present invention,

on which 1 - wastewater inlet, 2 - outlet for discharging solid particles, 3 - liquid distributor, 4 - solid particle, 5 - device body, 6 - guide hole, 7 - guide structure, 8 - hollow tube, 9 - umbrella cap, 10 – outlet for unloading, 11 – inlet for loading solid particles.

Fig. 3 is a block diagram of another embodiment of the desalination apparatus of the present invention,

on which 1 – gas inlet, 2 – outlet for unloading solid particles, 3 – gas distributor, 4 – solid particle, 5 – device body,
6 – guide hole, 7 – guide structure, 8 – hollow tube,
9 – umbrella cap, 10 – outlet for unloading, 11 – inlet for loading solids, 12 – inner tube, 13-1,2 – wastewater inlet.

Fig. 4 is a block diagram of another embodiment of the desalination apparatus of the present invention,

on which 1 - gas inlet, 2 - outlet for discharging solid particles, 3 - gas distributor, 4 - inner tube, 5-1, 2 - waste water inlet, 6 - device body, 7 - hollow tube, 8 - umbrella cap, 9 – outlet for unloading, 10: inlet for loading solids.

DETAILED DESCRIPTION

Reference will now be made in detail to the present embodiments of the present invention, but it is to be understood that the scope of the invention is not limited to the embodiments, but rather is defined by the appended claims.

All publications, patent applications, patents and other references mentioned in this specification are hereby incorporated by reference in their entirety. Unless otherwise defined, all technological and scientific terms used herein have the same meanings as commonly understood by those skilled in the art to which this invention relates. In the event of a conflict, this description, including definitions, will control.

When the description establishes a material, substance, method, step, device, element, and the like by such an expression as “known to those skilled in the art,” “prior art,” or similar term, it is intended that the subject matter of the invention so stated covers subject matter conventionally used in the art at the time this application is filed, but also includes subject matter of the invention which may not be in general use at the present time but will become known in the art to be suitable for a similar purpose.

As used herein, the term “substantially” means allowing for the presence of variation acceptable to those skilled in the art or considered reasonable by those skilled in the art, e.g., within ±10%, within ±5%, within ±1%, within within ±0.5% or within ±0.1%.

In the context of the present description, normal temperature refers to 25°C.

In the context of the present description, COD is determined using the analytical method provided by HJ828-2017, TDS is determined using the analytical method provided by HJT51-1999, and bulk density is determined using the analytical method provided by GB/T6286-1986.

In the context of the present description, the size and shape of the various gaps (for example, from the first gap to the sixth gap, described in the following text of the present description) are not particularly limited as long as they function as a communicating passage allowing various materials (such as thread, substrate , loaded substrate, heating agent and the like described in the following text of the present description) flow through it.

All percentages, parts, ratios, and the like referred to herein are by weight and pressures are gauge pressures unless otherwise indicated.

As used herein, any two or more embodiments of the present invention may be combined in any combination, and the resulting process solution forms part of the original disclosure of this specification and is within the scope of the present invention.

According to one embodiment of the present invention, this relates to a solid precipitation deposition apparatus. Herein, a solid precipitation apparatus may be specifically mentioned as, for example, any apparatus suitable for a case where it is necessary to precipitate at least a portion of a solute in a stream including a solvent and a solute in solid form. for physical changes (for example, decreased solubility to form a precipitate); and more specifically, for example, a desalination device and a crystallization device, and in particular a desalination device, may be listed. In the context of the present description, the solid precipitation apparatus of the present invention is explained and illustrated in detail, particularly taking the desalination apparatus as an example, but it is obvious that the present invention is not limited to the desalination apparatus.

According to an embodiment of the present invention, as said stream, for example, solution, seawater or wastewater, in particular saline wastewater or wastewater with a high salt content, in particular wastewater containing organic substances with high salt content (also known as high salt organic wastewater). However, the present invention is not limited to these specific streams, and any stream that includes a solvent and a solute and is designed to contain at least a portion of the solute precipitated in solid form, as described earlier herein, is suitable for use in the present invention. Here, since wastewater with high salt content is mentioned, its TDS is generally not higher than 20 wt.%, preferably 5-20 wt.%. In the case of organic matter content, the COD of said high salt wastewater is generally greater than 20,000 mg/l, preferably 20,000-200,000 mg/l or 20,000-40,000 mg/l.

According to one embodiment of the present invention, said stream remains in a subcritical state before entering said solids deposition device, in particular at a supercritical temperature of said solvent, more particularly at or above a supercritical solvent pressure (such as 23-35 MPa gauge, preferably 25-30 MPa gauge), but below the supercritical temperature of said solvent. Herein, as the temperature of said stream, may be listed, for example, any temperature below the supercritical temperature of said solvent, in particular, a temperature in the range from normal temperature to a temperature that is 1-15°C, 4-10°C or 6 -8°C below the supercritical temperature of said solvent (specifically water).

According to one embodiment of the present invention, said solid precipitation deposition apparatus includes a housing (namely, a device body), a flow inlet, a discharge outlet (namely, a flow outlet), and a substrate located in an inner chamber of said housing.

According to one embodiment of the present invention, the housing may be specifically listed as, for example, a vertical housing, in particular a vertical cylindrical housing.

According to one embodiment of the present invention, the ratio of the height of the inner chamber of said housing (unit is m) to the inner diameter (unit of m) is 7-17, preferably 10-14.

According to one embodiment of the present invention, said substrate is configured such that solid matter (e.g., the various precipitates described above herein) is deposited and loaded thereon, thereby forming a core-shell structure (also referred to as a loaded substrate) with sediment as the outer shell and a substrate as the inner core. When the loaded substrate grows to a predetermined size (namely, the substrate is loaded with a predetermined amount of precipitation), it must be removed or unloaded from the solids deposition device according to the circumstances, simultaneously or thereafter, the removed or unloaded substrate is replaced with a new substrate to continue the solids deposition process precipitation. Herein, the support may be any design and shape capable of achieving the purpose, and specifically, for example, solid particles, plates, lattices, meshes, cages, fibers, strips and the like may be listed, and preferably solid particles.

In the context of the present description, the so-called "in which the configuration of said support is suitable for depositing and loading solid matter thereon" means that such configuration, such as the shape or design of the support, is designed such that a significant portion of the solid matter (for example, 80% by weight) or more, 90% by weight or more, 95% by weight or more, or 98% by weight or more of the total solids) is deposited and loaded onto it, either specifically or intentionally.

According to one embodiment of the present invention, as mentioned solid particles, specifically for example, the following may be listed: crystal seeds such as inorganic salt particles, which are particularly suitable for desalination or crystallization; inorganic particles, in particular refractory material particles, specifically alumina spheres, silica spheres, sand, quartz sand, ceramic particles and the like, which are particularly suitable for desalination using inorganic particles as a mediator; solid waste such as slag and solid waste, which are particularly suitable for waste treatment.

According to one embodiment of the present invention, in order to achieve an optimal settling and loading effect, said solid particles are contacted with said flow in said solid settling apparatus to produce a fluidizing or boiling state. Thus, said solid precipitation apparatus is sometimes also called a fluidized bed reactor or a fluidized bed reactor.

According to one embodiment of the present invention, said solid particle can be of any size and shape suitable for packaging in said solid precipitation device, in particular the equivalent diameter of said solid particle is generally 0.1-1.0 mm, preferably 0. 2-0.7 mm. Moreover, the specific surface area of said solid particles is generally 100-300 m ² /g, and the bulk density is generally 0.6-0.7 g/cm ³ .

According to one embodiment of the present invention, as the loading amount of said solid particles into said solid precipitation device, specifically, for example, the used amount (by volume) of said solid particles generally contains 1/4-3/4, preferably 1/4- 1/2 of the total volume of the internal chamber of the mentioned housing.

According to one embodiment of the present invention, as said plate, lattice, mesh, cage, fiber, strip and the like, they may be of any suitable design and shape for installation in said solid precipitation apparatus, and are not particularly limited. For example, as said plate, the following may be listed in particular: a non-porous plate wherein said sediment is loaded onto the plates; or a porous plate, where said sediment is loaded onto the plates and into the pores.

According to the present invention, when said solid particles are used as a substrate, the substrate is particularly suitable for continuous operation, that is, the substrate is continuously added to said solid precipitation device and the simultaneously loaded substrate is continuously discharged, or is particularly suitable for periodic operation, i.e., the substrate is periodically replaced according to the degree of sediment load; When plates, grids, meshes, cages, fibers, strips and the like are used as a support, the support is particularly suitable for batch operation, i.e. the substrate is periodically replaced according to the degree of sediment load.

According to one embodiment of the present invention, the loaded substrate discharged from said solid deposition apparatus is subjected to ultrasonication, high temperature stirring, polishing and the like to recover sediment deposited on the substrate to effect regeneration of the substrate.

According to one embodiment of the present invention, in the inner chamber of said housing, the flow retention time is generally 10-1800 seconds, preferably 60-600 seconds or 10-180 seconds, and the flow rate is generally 1.5-270 h ^{- 1} .

According to one embodiment of the present invention, the inner chamber of the body of said sediment deposition device operates under supercritical conditions, in particular under supercritical conditions of said solvent such as water. Herein, as said supercritical conditions, the following may be specifically listed, for example: operating pressure 23-35 MPa gauge, preferably 25-30 MPa gauge, and operating temperature 350-650°C, preferably 450-600°C C or 450-550°C.

According to one embodiment of the present invention, to implement said supercritical conditions, said substrate can be located in the inner chamber of said housing and its temperature is set to a temperature higher than the supercritical temperature of said solvent, for example a temperature of 1-15°C, 4-10 °C or 6-8°C above the mentioned supercritical temperature. Herein, said substrate and said stream are in such proportion that, after mixing, the temperature of said stream reaches or exceeds the supercritical temperature of said solvent.

According to one embodiment of the present invention, to implement said supercritical conditions, said substrate may be further added to the inner chamber of said housing, and the temperature of said substrate is higher than the supercritical temperature of the solvent, for example a temperature of 1-15°C, 4-10°C or 6-8°C above supercritical temperature. Herein, said substrate and said stream are in such proportion that, after mixing, the temperature of said stream reaches or exceeds the supercritical temperature of said solvent.

According to one embodiment of the present invention, said sedimentation device also includes an internal element located in (in particular, the upper part) of the inner chamber of said housing. Herein, said internal element comprises a hollow tube substantially coaxial with the central axis of said body, in particular a hollow cylinder. There must be a gap (called the first gap) between the inner wall of the shell of said device and the outer wall of said hollow tube. In addition, said internal element also contains a partition located above said hollow tube. Preferably, said partition is substantially coaxial with the central axis of said housing. In addition, there must be a gap (called a second gap) between said partition and the upper edge of said hollow tube, and there must be a gap (called a sixth gap) between said partition and the inner wall of said housing, which will be used as an input/output channel for the respective flows.

Among the above-described gaps, annular gaps are preferred.

According to one embodiment of the present invention, said internal element is located in the upper part of the inner chamber of said housing.

According to one embodiment of the present invention, specifically, for example, a plate-like structure or a cap-like structure, in particular an umbrella cap, may be listed as said partition. Preferably, said umbrella cap is coaxial with said hollow tube, with a conical angle of typically 30-150°, preferably 60-120°. In addition, although not particularly limited, the height of said partition is generally 5-20% of the height of the inner chamber of said housing.

According to one embodiment of the present invention, the upper and lower ends of said hollow tube are open, and said hollow tube comprises an upper straight tube section and a lower conical diffusion section. Herein, the outer diameter of said straight tube section of said hollow tube is generally 60-80%, preferably 67-73% of the inner diameter of said body. Although not particularly limited, the height of the straight tube section of said hollow tube is generally 10-30% of the height of the inner chamber of said housing.

Although not particularly limited, the maximum outer diameter of said conical diffusion section of said hollow tube (namely, the outer diameter of the cone bottom) is generally 75-90% of the inner diameter of said body. Although not particularly limited, the height of the straight conical diffusion section of said hollow tube is generally 3-10% of the height of the inner chamber of said housing.

According to one embodiment of the present invention, said sedimentation device also includes a guide structure located around the inner wall of said housing. said guide structure surrounds the inner chamber of said housing to form a channel that is open at the top and bottom (called a guide hole), in particular to form a cylindrical channel that is open at the top and bottom. It is preferable that the longitudinal section of said guide structure along the central axis of said body is a trapezoid, and the overlap angle Alpha and the friction angle Beta of said trapezoid is an acute angle, preferably 5-70°. According to the present invention, there should be a gap (called a third gap) between said guide structure and a lower edge of said hollow tube. Preferably, said guide hole is substantially coaxial with the central axis of said housing.

As said third gap, the annular gap is particularly preferred.

According to one embodiment of the present invention, the internal diameter of said guide hole is generally 60-80% of the internal diameter of said housing. Moreover, the height of said guide hole is generally 5-15% of the height of the inner chamber of said housing.

According to one embodiment of the present invention, said guide structure is located below said hollow tube and above said flow inlet, and is located in the upper part of the inner chamber of said housing.

According to one embodiment of the present invention, said flow inlet is located at the bottom or lower part of said housing. Herein, the design of said flow inlet is suitable for spraying said flow into an inner chamber of said housing. As the structure mentioned, for example, a nozzle or a liquid distributor, preferably a liquid distributor, in particular a liquid distribution plate, can be listed.

According to one embodiment of the present invention, said discharge outlet is located at the top or upper part of said housing, in particular located on top of said housing. Preferably, said discharge outlet is located above said partition.

According to one embodiment of the present invention, said solid depositing apparatus also includes an inlet for loading the substrate and an outlet for discharging the substrate. Herein, said substrate loading inlet is generally located on top or at the top of said housing, preferably located on top of said housing. Preferably, said substrate loading inlet is located above said guide structure, more preferably located above said baffle. In addition, said substrate discharge outlet is generally located at the bottom of said housing, preferably located below said flow inlet.

According to one embodiment of the present invention, to implement said supercritical conditions, said sedimentation apparatus may also include a heating agent inlet. Herein, said heating agent inlet is located at the bottom or bottom of said housing, preferably located at the bottom of said housing. Moreover, the structure of said heating agent inlet is suitable for spraying said heating agent into the inner chamber of said housing. As said structure, for example, a gas nozzle or a gas distributor, preferably a gas distributor, in particular a gas distribution plate, can be listed. It is preferable that said gas distributor be substantially coaxial with the central axis of said housing.

According to one embodiment of the present invention, said heating agent is capable of increasing the temperature of the stream to achieve or exceed the supercritical temperature of the solvent through physical heat exchange or chemical heat generation, or the like. As said heating agent, specifically, for example, an oxidizing gas such as air and oxygen gas, or an oxidizing liquid such as hydrogen peroxide and a persalt aqueous solution (generally called an oxidizing agent), or a heating gas such as steam ( for example, vapor of the mentioned solvent). Preferably, said heating agent is used in such an amount that said stream, upon entering the inner chamber of said housing, forms a supercritical state, for example, reaches or exceeds the supercritical temperature of said solvent. For example, said heating agent and said stream are in such a proportion that upon mixing thereof, the temperature of said stream rises to reach or exceed the supercritical temperature of said solvent. As used herein, chemical heat generation, for example, may refer to the case where said heating agent chemically reacts with a certain component or components contained in said stream to generate heat. Particularly, when the stream is salt-containing wastewater or high-salt wastewater, said heating agent is an oxidizing gas, the oxidizing gas and organic impurities in the salt-containing wastewater or high-salt wastewater are subjected to an oxidation reaction to generate heat, thereby thereby increasing the temperature of the saline wastewater or wastewater with a high salt content to achieve or exceed the supercritical water temperature, or when the saline wastewater or wastewater with a high salt content remains in a subcritical state before entering the sedimentation device, its temperature is increased by 4 °C or higher (preferably 6-8°C) to achieve or exceed supercritical water temperature.

According to one embodiment of the present invention, said stream is saline wastewater or wastewater with high salt content, in particular organic wastewater with high salt content, said heating agent is said oxidizing gas, the amount of said heating agent used is 100- 500%, preferably 150-350% of the theoretical oxygen demand for oxidation of said stream. Here, the theoretical oxidation oxygen demand represents the amount of oxygen required to completely oxidize COD in organic wastewater.

According to one embodiment of the present invention, conditions such as temperature and pressure when said heating agent is loaded into said inner chamber are not particularly limited. Herein, as the temperature mentioned, specifically, for example, any temperature from room temperature to the supercritical temperature of the solvent (especially water) may be listed. As said pressure, for example, any pressure capable of causing said heating agent to be loaded into said inner chamber may be listed, and more specifically, for example, a pressure substantially identical to the pressure of said flow may be listed.

According to one embodiment of the present invention, in particular when said stream is a saline wastewater or a high salt wastewater (especially a high salt organic wastewater) having a COD greater than 20,000 mg/l (preferably 20,000-200,000 mg/l). l or 20000-40000 mg/l), and said heating agent is said oxidizing gas, even if the temperature of said heating agent is much lower than the supercritical temperature of said solvent (especially water), for example at substantially normal temperature, it is capable of increasing the temperature of said stream to reach or exceed the supercritical temperature of said solvent, and therefore the expected technological effect of the present invention can be effectively realized.

According to one embodiment of the present invention, in order to avoid large temperature fluctuation in said sedimentation device, other organic wastewater, such as high salt organic wastewater with higher or lower COD, can be added to said stream according to circumstances so that the COD content of said stream upon entering said sedimentation device remains substantially constant.

According to one embodiment of the present invention, said heating agent inlet is located above or below said flow inlet, preferably located below said flow inlet.

According to one embodiment of the present invention, said sedimentation device also comprises an inner tube (also in a hollow tubular structure). As the inner tube mentioned, for example, straight tubular or horn-shaped tubular, especially straight cylindrical, can be listed. Preferably, said inner tube is substantially coaxial with the central axis of said housing.

According to one embodiment of the present invention, the outer diameter of said inner tube is generally 60-80%, preferably
67-73%, of the internal diameter of the said housing. Moreover, the height of said inner tube is generally 20-60%, preferably 30-50%, of the height of the inner chamber of said housing.

According to one embodiment of the present invention, said inner tube is located under said guide structure. Moreover, said inner tube is preferably located in the lower part of the inner chamber of said housing.

According to one embodiment of the present invention, there is a gap between the inner wall of said body and the outer wall of said inner tube (called the fourth gap), in particular an annular gap. In addition, there is a gap between the lower edge or inner wall of said inner tube and said heating agent inlet (called the fifth gap), especially the annular gap. Herein, said fifth gap communicates with said fourth gap and the interior of said inner tube. Preferably, said flow inlet is located in said fourth gap and below the upper edge of said inner tube. It is further preferable that said flow inlet is 100-500 mm below the upper edge of said inner tube in the vertical direction.

According to one embodiment of the present invention, said inner tube is configured such that said heating agent imported from said heating agent inlet substantially completely enters the interior of said inner tube. Specifically, with reference to FIG. 3 or fig. 4, the structure of said heating agent inlet is a gas distributor, and said inner tube is located above said gas distributor or contains said gas distributor, both of which are separated by said fifth gap. In the first case, said inner tube has a protrusion on the gas distributor in the vertical direction, all the holes of the gas nozzle of the gas distributor are located in the area of the protrusion. The present invention is not limited to this and those skilled in the art can envision any possible configurations based on this requirement for the inner tube.

According to one embodiment of the present invention, the space of the inner chamber of said housing located below the upper edge of said inner tube is called a buffer zone, then said buffer zone generally contains 25-40% or 20-60% of the total volume of the inner chamber of said housing.

According to one embodiment of the present invention, in said buffer zone, said heating agent and said flow are in such proportion that the temperature of said flow upon exiting the upper edge of said inner tube (namely leaving said buffer zone) rises until it reaches or exceeds supercritical temperature of said solvent. In particular, if said stream is saline wastewater or wastewater with high salt content, and said heating agent is said oxidizing gas, then heat of reaction is generated during the oxidative decomposition of organic contaminants in the wastewater, resulting in when the wastewater are in the said buffer zone, their temperature is below the supercritical temperature of the water, and when they leave the said buffer zone, their temperature rises until it reaches or exceeds the supercritical temperature of the water, thereby avoiding the deposition of salts in the buffer zone.

According to one embodiment of the present invention, as a method of operation of said solid precipitation apparatus, for example, the following steps may be listed, in which: said flow enters the lower part of the inner chamber of said housing from said flow inlet, said substrate enters the upper part of the inner chamber of said housing from said substrate loading inlet, and then enters the lower portion of the inner chamber of said housing through said first gap, said third gap, and said guide hole, said flow causes said substrate to be in a fluid state, at least a portion of said of solute is deposited and loaded onto said substrate to form a loaded substrate, a portion of said loaded substrate is moved to the bottom of an inner chamber of said housing and discharged from an inner chamber of said housing from said substrate discharge outlet, another portion of said loaded substrate is moved to the top of the inner chamber of said housing together with said stream from which at least a portion of the solute is removed (called the purified stream), passes through said guide orifice, enters said straight tube section from said conical diffusion section, and is then discharged from said second gap, said loaded the substrate flows to the bottom of the inner chamber of said housing through said first gap, said third gap and said guide hole, said purified flow moves up the inner chamber of said housing through said sixth gap, and is discharged from the inner chamber of said housing from said discharge outlet.

According to one embodiment of the present invention, as another method of operating said solid deposit deposition apparatus, for example, the following may be listed as follows: said substrate enters the upper portion of the inner chamber of said housing from said substrate loading inlet, and then enters the lower part of the inner chamber of said housing through said first gap, said third gap and said guide hole; said flow enters said fourth gap from said flow inlet, and then enters the interior of said inner tube through said fifth gap, and mixes with said heating agent, which enters the interior of said inner tube from said heating agent inlet to form a mixture that is discharged from said inner tube from an upper edge of said inner tube after increasing the temperature to reach or exceed the supercritical temperature of said solvent; a portion of said mixture flows into the interior of said inner tube through said fourth gap and said fifth gap (forming an internal recycle), another portion of said mixture causes said substrate to be in a fluid state, at least a portion of said solute is deposited and supplied to said substrate to formation of a loaded substrate, a portion of said loaded substrate is moved to the bottom of the inner chamber of said housing through said fourth gap and discharged from the inner chamber of said housing from said substrate outlet, another portion of said loaded substrate is moved to the upper part of the inner chamber of said housing along with said a mixture from which at least a portion of the solute is removed (referred to as the purified mixture), passes through said guide hole, enters said straight section of tubing from said conical diffusion section, and is then discharged from said second gap, said loaded substrate flowing into the lower portion of the inner chamber of said body through said first gap, said third gap and said guide hole, said purified mixture is moved up the inner chamber of said body through said sixth gap, and discharged from the inner chamber of said body from said discharge outlet.

According to one embodiment of the present invention, according to circumstances, a pH adjusting agent may be added to said stream and/or into an inner chamber of said housing, and said pH adjusting agent is used in such an amount that the pH value of the contents in the inner chamber of said housing was maintained at 9-13. Herein, as the pH adjusting agent, any agent that can be used to adjust the pH value in the art may be listed, and specifically, for example, sodium hydroxide, potassium hydroxide and the like may be listed, without being particularly limited. For this reason, said sedimentation device may be further provided with a pH control device to regulate the flow in an alkaline environment, thereby preventing the device from corrosion.

According to one embodiment of the present invention, as appropriate, said sedimentation device may also be provided with heat exchange equipment. Said heat exchange equipment is used to extract heat between the discharge stream of said sediment settling device (e.g., a purified stream discharged from said stream outlet) and the solid sediment entering said sediment device (e.g., a stream loaded from said stream inlet).

According to one embodiment of the present invention, it will be apparent to those skilled in the art that any component contained in said sediment deposition apparatus, such as a body of the apparatus, an internal member, and the like, may be resistant in material and construction to supercritical conditions (in particular, high temperature and high pressure) solvent. For this reason, especially when used for desalination of wastewater with high salt content, the design pressure of these components is generally at least 35 MPa and the design temperature is generally at least 650°C.

According to one embodiment of the present invention, this also applies to a solid precipitation method, especially a desalination method. The method includes allowing a stream, as described in any of the previous aspects of the present description, to enter the sediment deposition apparatus, as described in any of the previous aspects of the present description, and allowing the sediment to be deposited and loaded onto the substrate.

The present invention will be specifically described below, taking high salt wastewater desalination as an example, with reference to the accompanying drawings, but the present invention is not limited thereto.

The desalination method of the present invention will be described in more detail with reference to FIG. 1.

The wastewater first enters the heat exchanger 1, exchanges heat with the high-temperature liquid after separating the gas from the liquid, then enters the fluidized bed reactor 2 for supercritical water oxidation treatment, and the oxidized wastewater can reach the standard after separating the gas from the liquid, and is discharged. The fluidized bed reactor used is a reactor conventional in the art, and in particular contains conventional components such as a reactor shell, a gas-liquid distribution disk, solid particles and the like. Solids in the fluidized bed reactor are periodically loaded into and discharged from the fluidized bed reactor by a real-time loading and releasing system, which includes a real-time solids loading system 4 and a real-time solids discharge system 5. The real-time solids loading system 4 includes a loading hopper, a loading reservoir and a valve. When it is necessary to load solids into the reactor, the valve between the loading tank and the reactor is first closed, then the emptying valve is opened to empty the loading tank, the solids in the loading hopper are loaded into the charging tank by gas transfer or liquid transfer or by gravity, then the valve on the pipeline is closed , and nitrogen is charged into the charging tank through the nitrogen pressurization valve so that the pressure in the charging tank is substantially equal to the reactor pressure. Then, the valve of the connecting pipeline between the loading tank and the reactor is opened, and the particles enter the reactor by gravity. The real-time solids discharge system 5 includes a solids discharge tank and a valve. Before unloading the salt-containing solids from the reactor, the connecting pipeline valve between the bottom of the reactor and the salt-containing solids discharge tank is first closed, the tank is filled with incoming wastewater, then high-pressure nitrogen gas is introduced to the reaction pressure, the connecting pipeline valve between the bottom of the reactor and the salt-containing solids discharge tank The solids are opened and the particles are allowed to flow into the solids discharge tank from the bottom of the reactor due to the action of gravity.

The design features and operating principle of the desalination apparatus of the present invention are given below with reference to FIG. 2:

The design features and operating principle of the desalination apparatus of the present invention are given below with reference to FIG. 2: The hollow tube 8 and the umbrella cap 9 located above the hollow tube are located above the guide structure 7, the upper and lower ends of the said hollow tube are open, the said hollow tube has a lower conical diffusion section, and the umbrella cap 9 is concentric with the hollow tube 8. The lower the hole of the hollow tube 8 is a flow direction hole 6, the annular hole formed by the bottom hole of the hollow tube and the inner wall of the desalination device is the solids outflow inlet of the desalination device, and the separated solids return to the bottom of the desalination device.

Wastewater with a high salt content is introduced from the inlet 1 of the inflow, passed through the liquid distributor 3, and then uniformly enters the desalination device, so that the solid particles 4 are in a fluid state. Under the action of the flow, the bed of particles expands to a certain height, and a desalination reaction is carried out in the desalination device so that salt is deposited on the particles. The reacted flow can entrain some of the particles to enter the hollow tube 8 and the umbrella cap 9 through the guide hole 6 surrounded by the guide structure 7 for separation, the separated particles flow to the bottom of the desalination device through the outside of the inner member of the tubular structure, and the demineralized wastewater is discharged from the desalination device through the discharge outlet 10. To timely discharge the crystallized saturated solids from the desalination device and supplement with fresh particles, fresh particles can be supplemented into the reaction system through the solids loading inlet 11 located at the top of the desalination device, and the solids can be discharged from the reaction system through the outlet 2 for unloading solid particles, located at the bottom of the desalination device.

The design features and operating principle of the desalination apparatus of the present invention are given below with reference to FIG. 3.

Based on FIG. 2, the inner tube 12 and the gas distributor 3 are located at the bottom of the desalination device, the gas distributor replaces the liquid distributor, the inner tube 12 is located above the gas distributor, the wastewater inlet 13 is located on the two sides of the bottom of the desalination device, and the wastewater symmetrically enters the annular the gap between the inner tube of the buffer zone and the inner wall of the device body.

High-salinity wastewater enters the annular gap between the inner tube of the buffer zone and the inner wall of the device body from two symmetrical wastewater inlets 13 located at the bottom of the desalination device, internal recycling is generated in the buffer zone during operation, gas enters the buffer zone through the inlet gas holes 1 and gas distributor 3, the solid particles are in a fluid state under the action of gas and liquid, the temperature rises by 4-8°C after the reaction in the buffer zone, wastewater with high salt content enters the upper zone and reacts at a certain temperature and pressure, the salt in the high salt wastewater is precipitated on the solid particles, the solid particles having the precipitated salt move down to the solids discharge outlet along with the reaction, the post-reaction stream undergoes gas-solid two-phase separation, the solid phase is returned to desalination device, and the gas phase is discharged from the desalination device.

The design features and operating principle of the desalination apparatus of the present invention are given below with reference to FIG. 4.

Said desalination device includes a device body 6 and internal elements of the desalination device, wherein the internal elements of the desalination device include a hollow tube 7, an inner tube 4 and an umbrella cap 8. Both the upper and lower ends of the hollow tube are open.

Wastewater with a high salt content enters the annular gap between the inner tube 4 and the outer wall of the device through two or more pairs of symmetrical inlet openings located at the bottom of the device. The gas phase enters the device from the bottom of the inner tube 4, solid particles enter the device from the top of the device, internal recycling is formed due to the different gas content inside and outside the inner tube, at the top of the inner tube, one part is gas-liquid-solid the mixture flows upward to enter the hollow tube 7, and the other part of the gas-liquid-solid mixture enters the annular gap between the inner tube 4 and the outer wall of the device and enters the inner part of the hollow tube through the fourth gap and the third gap. The gas-liquid-solid mixture entering the hollow tube 7 flows upward, the gas-liquid-solid three-phase separation is performed after the gas-liquid-solid mixture reaches the top of the hollow tube 7, solid particles and part of the liquid phase enter the annular gap between the hollow tube 7 and the outer wall of the device through the second gap and the first gap, and flow into the lower part of the device. The gas phase and part of the liquid phase are discharged from the device through a discharge outlet 9 located in the upper part of the device for separating gas from liquid.

EXAMPLES

The present invention will be described in further detail below by examples and comparative examples, but the present invention is not limited to the following examples.

In the following examples and comparative examples, all testing methods used, unless otherwise noted, were conventional in the art, and all testing materials used, unless otherwise described, were purchased from conventional biomechanical stores.

Example 1

Taking the flow diagram shown in FIG. 1, in organic wastewater with high salt content, the COD concentration was 92600 mg/L, TDS was 13.5 wt%, and pH was 8.5.

Organic wastewater with a high salt content and oxygen were introduced into the fluidized bed reactor, and the solid particles in the fluidized bed reactor were alumina ceramic pellets with a diameter of 0.4 mm, bulk density
0.65 g/cm ³ , a specific surface area of 260 m ² /g, and the additional amount of solid particles was 1/2 of the reactor volume. The amount of oxidizer introduced was 300% of the theoretical oxygen requirement for wastewater oxidation. The supercritical oxidation conditions were as follows: reaction temperature 600°C, reaction pressure 28 MPa, and reaction retention time 30 seconds. The amount of loaded and unloaded solid particles during the reaction was 75 g h ^-1 l ^-1 of water being poured. The salt in the wastewater was deposited on the solid particles in the fluidized bed reactor, the post-reactive stream was subjected to gas-liquid separation, the liquid phase could be discharged after heat exchange with the wastewater entering the reactor, or the incoming wastewater was diluted, the content of COD entering the reactor supercritical water oxidation was kept stable, and the reaction was carried out stably, avoiding large temperature fluctuations in the reactor.

After the above treatment, the discharged water had a COD concentration of 46 mg/L, and a TDS of 25 mg/L, which met the requirement for direct discharge.

Example 2

Taking the flow diagram shown in FIG. 1, in high salt organic wastewater, the COD concentration was 21700 mg/L, the TDS was 5.3 wt%, and the pH was 8.

Organic wastewater with high salt content and oxygen were introduced into the fluidized bed reactor, and the solid particles in the fluidized bed reactor were alumina ceramic pellets with a diameter of 0.2 mm, a bulk density of 0.67 g/cm ³ , a specific surface area of 100 m ² / g, and the additional amount of solid particles was 1/3 of the reactor volume. The amount of oxidizer introduced was 150% of the theoretical oxygen requirement for wastewater oxidation. The supercritical oxidation conditions were as follows: reaction temperature 380°C, reaction pressure 23 MPa, and reaction retention time 150 seconds. The amount of loaded and unloaded solid particles during the reaction was 58 g·h ^-1 ·l ^-1 of water being poured. The salt in the wastewater was deposited on solid particles in the fluidized bed reactor, the organic matter in the wastewater was decomposed by oxidation to carbon dioxide and water, the after-reaction stream was subjected to gas-liquid separation, the liquid phase could be released after heat exchange with the wastewater entering the reactor, or influent wastewater was diluted, the content of COD entering the supercritical water oxidation reactor was kept stable, and the reaction was carried out stably, avoiding large temperature fluctuations in the reactor.

After the above treatment, the discharged water had a COD concentration of 58 mg/L and a TDS of 113 mg/L, which met the requirement for direct discharge.

Example 3

Taking the flow diagram shown in FIG. 1, in high-salt organic wastewater, the COD concentration was 137200 mg/L, the TDS was 14.3 wt%, and the pH was 8.7.

Organic wastewater with high salt content and oxygen were introduced into the fluidized bed reactor, and the solid particles in the fluidized bed reactor were alumina ceramic pellets with a diameter of 0.7 mm, a bulk density of 0.62 g/cm ³ , a specific surface area of 300 m ² / g, and the additional amount of solid particles was 1/2 of the reactor volume. The amount of oxidizer introduced was 350% of the theoretical oxygen requirement for wastewater oxidation. The supercritical oxidation conditions were as follows: reaction temperature 650°C, reaction pressure 30 MPa, and reaction retention time 30 seconds. The amount of loaded and unloaded solid particles during the reaction was 79 g·h ^-1 ·l ^-1 of water being poured. The salt in the wastewater was deposited on solid particles in the fluidized bed reactor, the organic matter in the wastewater was decomposed by oxidation to carbon dioxide and water, the after-reaction stream was subjected to gas-liquid separation, the liquid phase could be released after heat exchange with the wastewater entering the reactor, or influent wastewater was diluted, the content of COD entering the supercritical water oxidation reactor was kept stable, and the reaction was carried out stably, avoiding large temperature fluctuations in the reactor.

After the above treatment, the discharged water had a COD concentration of 54 mg/L and a TDS of 23 mg/L, which met the requirement for direct discharge.

Example 4

A similar procedure was performed according to Example 1, except that air was used as the oxidizing agent.

After the above treatment, the released water had a COD concentration of 59 mg/L and a TDS of 26 mg/L.

Example 5

A similar procedure was performed as in Example 1, except that the solid particles were silicon pellets with a diameter of 0.5 mm, and a specific surface area of 230 m ² /g.

After the above treatment, the released water had a COD concentration of 53 mg/L and a TDS of 62 mg/L.

Example 6

A similar procedure was performed as in Example 1, except that sodium hydroxide was added to the influent wastewater to control the pH of the influent water to 11. After the above treatment, the COD and TDS in the outlet water did not change much. However, the pH value of the influent water was controlled to be alkaline, and alkaline substances in the wastewater can neutralize the acidic substances created during the reaction process, thereby preventing corrosion of the reactor.

Example 7

The desalination apparatus of the present invention was used as shown in FIG. 2, wherein the device had an inner chamber height of 2 m and an inner diameter of 0.17 m, the outer diameter of the straight tube section of the hollow tube was 0.12 m, the height of the straight tube section of the hollow tube was 0.4 m, and the conical angle of the umbrella cap was 100° , the height of the umbrella cap was 0.25 m, the outer diameter of the umbrella cap was 0.14 m, the maximum outer diameter of the conical diffusion section was 0.14 m, the height of the conical diffusion section was 0.15 m, the guide structure was a ring structure having trapezoidal section with a height of 0.2 m, the inner diameter of the guide hole was 0.13 m, the overlap angle Alpha was 45°, the friction angle Beta was 45°. In organic wastewater with high salt content, TDS was 13.5 wt%, and The pH was 8.5.

Organic wastewater with high salt content (temperature: 360°C, pressure: 30 MPa) was introduced into the desalination device, and the solid particles in the desalination device were alumina ceramic pellets with a diameter of 0.4 mm, bulk density of 0.65 g/ ^cm3 , and a specific surface area of 260 m ² /g, and the additional amount of solid particles was 1/2 of the reactor volume. In the internal chamber of the device, the operating temperature was 600°C, the pressure was 28 MPa, and the retention time was 30 seconds. The amount of loading and unloading solid particles was 75 g·h ^-1 ·l ^-1 of water being poured. After treatment, the released water had a TDS of 113 mg/L.

After 100 days of continuous operation, no blockage occurred in the device or pipes.

Example 8

The desalination apparatus of the present invention was used as shown in FIG. 3, and the device had an inner chamber height of 2 m and an internal diameter of 0.17 m, the outer diameter of the straight tube section of the hollow tube was 0.12 m, the height of the straight tube section of the hollow tube was 0.4 m, the conical angle of the umbrella cap was 100° , the height of the umbrella cap was 0.25 m, the outer diameter of the umbrella cap was 0.14 m, the maximum outer diameter of the conical diffusion section was 0.14 m, the height of the conical diffusion section was 0.15 m, the guide structure was a ring structure having trapezoidal section with a height of 0.2 m, the inner diameter of the guide hole was 0.13 m, the overlap angle Alpha was 45°, the friction angle Beta was 45°, the inner tube had an outer diameter of 0.12 m and a height of 0.7 m, the high salt wastewater inlet was 200mm below the top edge of the inner tube in the vertical direction. In the high-salinity organic wastewater, the COD concentration was 92,600 mg/L, the TDS was 13.5 wt%, and the pH was 8.5.

Organic wastewater with high salt content (temperature: normal temperature, pressure: 30 MPa) and oxygen gas (temperature: normal temperature, pressure: 30 MPa) were introduced into the desalination device, and the solid particles in the desalination device were alumina ceramic pellets with a diameter of 0 .4 mm, a bulk density of 0.65 g/cm ³ , and a specific surface area of 260 m ² /g, and the additional amount of solid particles was 1/2 of the reactor volume. The amount of oxygen gas introduced was 300% of the theoretical oxygen requirement for wastewater oxidation. In the internal chamber of the device, the operating temperature was 600°C, the pressure was 28 MPa, and the retention time was 30 seconds. The amount of loading and unloading solid particles was 75 g·h ^-1 ·l ^-1 of water being poured. After the above treatment, the discharged water had a COD concentration of 54 mg/L and a TDS of 63 mg/L, which met the requirement for direct discharge.

After 100 days of continuous operation, no blockage occurred in the device or pipes.

Example 9

The desalination apparatus of the present invention was used as shown in FIG. 4, and the device has an inner chamber height of 2 m and an inner diameter of 0.17 m, the outer diameter of the straight tube section of the hollow tube was 0.12 m, the height of the straight tube section of the hollow tube was 0.4 m, the conical angle of the umbrella cap was 100° , the height of the umbrella cap was 0.25 m, the outer diameter of the umbrella cap was 0.12 m, the inner tube had an outer diameter of 0.12 m and a height of 0.7 m, the high salt organic wastewater inlet was 150 mm lower the upper edge of the inner tube in the vertical direction. In the high-salinity organic wastewater, the COD concentration was 92,600 mg/L, the TDS was 13.5 wt%, and the pH was 8.5.

Organic wastewater with high salt content (temperature: normal temperature, pressure: 30 MPa) and oxygen gas (temperature: normal temperature, pressure: 30 MPa) were introduced into the desalination device, and the solid particles in the desalination device were alumina ceramic pellets with a diameter of 0 .4 mm, a bulk density of 0.65 g/cm ³ , and a specific surface area of 260 m ² /g, and the additional amount of solid particles was 1/2 of the reactor volume. The amount of oxygen gas introduced was 300% of the theoretical oxygen requirement for wastewater oxidation. In the internal chamber of the device, the operating temperature was 600°C, the pressure was 28 MPa, and the retention time was 30 seconds. The amount of loading and unloading solid particles was 75 g·h ^-1 ·l ^-1 of water being poured. After the above treatment, the discharged water had a COD concentration of 46 mg/L and a TDS of 43 mg/L, which met the requirement for direct discharge.

After 100 days of continuous operation, no blockage occurred in the device or pipes.

Example 10

A similar procedure was performed as in Example 8, except that the solids were silica pellets with a diameter of 0.5 mm and a specific surface area of 230 m ² /g. After the above treatment, the released water had a COD concentration of 53 mg/L and a TDS of 62 mg/L.

Example 11

A similar procedure was performed as in Example 8, except that sodium hydroxide was added to the high-salt organic wastewater feed to control the pH of the feed water to 11. After the above treatment, the COD and TDS of the discharge water did not change much. However, the pH value of the influent water was controlled to be alkaline, and alkaline substances in the wastewater can neutralize the acidic substances created in the desalination process, thereby preventing corrosion of the device.

Example 12

A similar procedure was performed as in Example 7, except that the hollow tube, umbrella cap and guide structure were not provided. After the above treatment, the released water had a TDS of 436 mg/L.

After 30 days of continuous operation, slight blockage occurred in the device and in the pipelines.

Comparative example 1

A similar procedure was performed as in Example 1, except that a conventional reactor was used rather than a fluidized bed reactor. After the above treatment, the discharged water had a COD concentration of 96 mg/L and a TDS of 138,700 mg/L, and clogging occurred in both the reactor and the pipelines.

Comparative example 2

A similar procedure was carried out as in Example 1, except that the treatment was carried out by a fluidized bed reactor under the conditions of a reaction temperature of 270 °C, a reaction pressure of 9.0 MPa and a retention time of 1 hour. After the above treatment, the released the water had a COD concentration of 13,790 mg/L and a TDS of 14,270 mg/L.

Comparative example 3

A similar procedure was performed as in Example 7, except that no solids were added to the device. After the above treatment, the released water had a TDS of 138,700 mg/L. After only 1 day of continuous operation, serious blockage occurred in the device and in the pipelines.

Claims (41)

1. A solid depositing apparatus comprising a housing, a flow inlet, a flow outlet and a substrate disposed in an inner chamber of said housing, said substrate being configured to accommodate a solid to be deposited and loaded thereon, said substrate being solid particles, said device also contains an internal element located in the inner chamber of said housing, said internal element contains a hollow tube substantially coaxial with the central axis of said housing, the upper and lower ends of said hollow tube are open, said internal element also contains a partition, located above said hollow tube. 2. The sedimentation device according to claim 1, wherein said sedimentation device is a desalination device, and/or said housing is a vertical housing, and/or said flow is a solution, seawater or wastewater containing a solvent and solute. 3. The solid sediment settling device according to claim 2, wherein said body is a vertical cylindrical body and/or said stream is saline wastewater or wastewater with a high salt content. 4. The solid precipitation deposition device according to claim 1, which operates under supercritical solvent conditions. 5. The solid precipitation apparatus according to claim 4, wherein said solvent is water. 6. The solid precipitation apparatus according to claim 1, wherein said solid particles are selected from at least one of crystal seeds, inorganic particles such as an alumina sphere, a silica sphere, sand, quartz sand, refractory material particles such as ceramic particles, and solid waste such as slag. 7. The solid precipitation deposition device according to claim 6, in which the used amount by volume of said solid particles contains 1/4-3/4 of the total volume of the inner chamber of said housing, and/or the equivalent diameter of said solid particle is 0.1-1, 0 mm, and/or the specific surface area of said solid particles is 100-300 m ² /g, and/or the bulk density of said solid particles is 0.6-0.7 g/cm ³ . 8. A device for deposition of solid precipitation according to claim 7, in which the used amount by volume of said solid particles contains 1/4-1/2 of the total volume of the internal chamber of said housing and/or the equivalent diameter of said solid particle is 0.2-0.7 mm. 9. The solid precipitation deposition apparatus of claim 1, wherein said hollow tube comprises an upper straight tube section and a lower conical diffusion section, there is a gap called a first gap between an inner wall of said body and an outer wall of said hollow tube, there is a gap called a second gap, between said partition and the upper edge of said hollow tube, and there is a gap, called a sixth gap, between said partition and the inner wall of said housing. 10. The solid precipitation deposition device according to claim 9, wherein said internal element is located in the upper part of the inner chamber of said housing, and/or said first gap is an annular gap, and/or said partition is an umbrella cap, and/or said the partition is substantially coaxial with the central axis of said housing, and/or said second gap is an annular gap, and/or the sixth gap is an annular gap. 11. The solid precipitation deposition device according to claim 10, wherein said umbrella cap is coaxial with said hollow tube and has a conical angle of 30-150°, and/or the outer diameter of said straight tube section of said hollow tube is 60-80% of the inner diameter of said body, and/or the height of the straight tube section of said hollow tube is 10-30% of the height of the inner chamber of said body, and/or the maximum outer diameter of said conical diffusion section of said hollow tube is 75-90% of the inner diameter of said body, and/or the height said conical diffusion section of said hollow tube is 3-10% of the height of the inner chamber of said body, and/or the height of said baffle is 5-20% of the height of the inner chamber of said body. 12. The solid precipitation deposition device according to claim 11, wherein said umbrella cap has a conical angle of 60-120° and/or the outer diameter of said straight tube section of said hollow tube is 67-73% of the inner diameter of said body. 13. The sediment deposition apparatus of claim 9, which further comprises a guide structure disposed around an inner wall of said housing, said guide structure surrounds an inner chamber of said housing to form a channel that is open at the top and bottom called a guide hole, said guide structure is located below said hollow tube and above said flow inlet, there is a gap, called a third gap, between said guide structure and the lower edge of said hollow tube, and/or said guide hole substantially coaxial with the central axis of said housing, and/or said guide structure located in the upper part of the inner chamber of the said housing. 14. The solid precipitation deposition device according to claim 13, in which the longitudinal section of the guide structure along the central axis of said body is a trapezoid, and/or the overlap angle alpha and the friction angle beta of said trapezoid are 5-70°, and/or the specified guide hole is a cylindrical channel, and/or said third gap is an annular gap. 15. The solid sediment settling apparatus of claim 1, wherein said flow inlet is located at the bottom or bottom of said housing, said flow inlet is designed to spray said flow into an inner chamber of said housing, and/or said outlet for unloading is located on top or in the upper part of the said housing, and/or the ratio of the height of the inner chamber of the said housing, unit of measurement - m, to the internal diameter, unit of measurement - m, is 7-17 or 10-14, and/or the internal diameter of the mentioned guide the hole is 60-80% of the inner diameter of said housing, and/or the height of said guide hole is 5-15% of the height of the inner chamber of said housing. 16. The solids deposition apparatus of claim 15, wherein the structure of said flow inlet is a nozzle or liquid distributor and/or said outlet is located above said baffle. 17. The solid precipitation deposition device according to claim 1, which further comprises an inlet for loading the substrate and an outlet for unloading the substrate, and/or said inlet for loading the substrate is located on top or at the top of said housing, and/or said outlet. for unloading the substrate is located at the bottom of the mentioned housing. 18. The solids deposition apparatus of claim 17, wherein said substrate loading inlet is located above said baffle and/or said substrate discharge outlet is located below said flow inlet. 19. The sediment settling apparatus of claim 1, further comprising a heating agent inlet, wherein said heating agent inlet is located at the bottom or lower portion of said housing, said heating agent inlet being designed to be sprayed into the inner chamber. said housing and/or said heating agent inlet is located above or below said flow inlet. 20. The solid precipitation deposition apparatus according to claim 19, wherein said heating agent is selected from at least one of air, oxygen gas or heating gas, and/or the structure of said heating agent inlet is a nozzle or a gas distributor, and/or said heating agent inlet is located below said flow inlet. 21. The sediment settling device according to claim 19, which also includes an inner tube, said heating agent inlet is located at the bottom of said body, there is a gap between the inner wall of said body and the outer wall of said inner tube, called the fourth gap, there is a gap between the lower by an edge or inner wall of said inner tube and said heating agent inlet, called a fifth gap, said fifth gap communicates with said fourth gap and the interior of said inner tube, said inner tube is configured such that said heating agent is imported from said inlet heating agent substantially completely enters the interior of said inner tube, said flow inlet is located in said fourth gap and below the upper edge of said inner tube and/or the space of the inner chamber of said housing located below the upper edge of said inner tube is called a buffer zone , further mentioned buffer zone contains 25-40% or 20-60% of the total volume of the inner chamber of the said housing, and/or said heating agent inlet structure is a gas distributor, and said inner tube is located above said gas distributor or contains said gas distributor, both separated by said fifth gap, and/or said inner tube is located below said guide structure, and/or said flow inlet is 100-500 mm below the top edge of said inner tube in the vertical direction, and/or the outer diameter of said inner tube is 60-80% of the inner diameter of said body, and/or the height of said inner tube is 20-60% of the height an inner chamber of said housing, and/or said inner tube is located in a lower part of the inner chamber of said housing. 22. The solid precipitation deposition device according to claim 21, wherein the inner tube is a straight tubular or horn-shaped tubular shape, and/or said inner tube is substantially coaxial with the central axis of said body, and/or said fourth gap is an annular gap, and/or said fifth gap is an annular gap, and/or said gas distributor is substantially coaxial with the central axis of said body, and/or the outer diameter of said inner tube is 67-73% of the inner diameter of said body, and/or the height of said inner tube tube is 30-50% of the height of the inner chamber of the said housing. 23. A method for sedimentation of solids, which comprises the step of passing a stream containing a solute and a solvent into the sedimentation apparatus of claim 1 to cause at least a portion of the solute to be deposited and loaded onto said substrate located in the internal camera of the said housing. 24. The solid precipitation method according to claim 23, wherein said solid precipitation method is a desalination method, and/or said solute is an inorganic salt, and/or said solvent is water, and/or the solute is precipitated due to precipitation reactions or due to supersaturation. 25. The solids deposition method according to claim 23, wherein said stream, before entering said solids deposition device, is held in a subcritical state, and/or the temperature of said substrate is above the supercritical temperature of said solvent, and/or the substrate is added to the inner chamber said body and the temperature of said substrate is above the supercritical temperature of said solvent, and/or said substrate and said stream are in such proportion that, after mixing, the temperature of said stream reaches or exceeds the supercritical temperature of said solvent. 26. The solids deposition method according to claim 25, wherein said stream, before entering said solids deposition device, is held at a temperature below the supercritical temperature of said solvent, and/or the temperature of said substrate is a temperature of 1-15°C, 4-10°C or 6-8°C above said supercritical temperature, and/or said solvent is water. 27. The solids deposition method of claim 26, wherein said stream, before entering said solids deposition device, is held at or above a supercritical pressure of said solvent, but below a supercritical temperature of said solvent. 28. The solids sedimentation method according to claim 26 or 27, wherein said stream, before entering said solids sedimentation device, is held at a temperature of from room temperature to a temperature of 1-15°C, 4-10°C or 6-8 °C lower than the supercritical temperature of the said solvent. 29. The method of deposition of solid sediments according to claim 23, in which the operating conditions for the inner chamber of said housing include: operating pressure of 23-35 MPa on a manometer, operating temperature of 350-650°C, flow retention time of 10-1800 seconds and volumetric speed 1.5-270 h ^-1 . 30. The method of deposition of solid sediments according to claim 29, in which the operating pressure is 25-30 MPa on the pressure gauge, and/or the operating temperature is 450-550°C, and/or the flow retention time is 60-600 seconds. 31. The method for deposition of solid deposits according to claim 23, in which a heating agent is added to the inner chamber of said housing and said heating agent is used in such an amount that said flow, after entering the inner chamber of said housing, forms a supercritical state, and/or said the stream is a salt-containing wastewater or a wastewater with a high salt content, said heating agent is an oxidizing gas, and/or said heating agent and said stream are in such proportion that, after mixing, the temperature of said stream reaches or exceeds the supercritical temperature of said solvent and/or said heating agent and said stream are in such proportion that the temperature of said stream, upon exiting the upper edge of said inner tube, reaches or exceeds the supercritical temperature of said solvent, and/or the amount of said heating agent used is 100-500% or 150-350% of the theoretical oxygen demand for the oxidation of said stream. 32. The method for settling solid sediments according to claim 31, wherein said stream, after entering the inner chamber of said housing, reaches or exceeds the supercritical temperature of said solvent, and/or said stream is organic wastewater with a high salt content, and/or said heating the agent is oxygen gas or air. 33. The method for settling solid sediments according to claim 23, wherein a pH adjusting agent is added to said stream and/or into an inner chamber of said housing and said pH adjusting agent is used in such an amount that the pH value of the contents in the inner chamber of said housing was maintained at 9-13. 34. The solids deposition method of claim 23, wherein said stream enters a lower portion of an inner chamber of said housing from said stream inlet, said substrate enters an upper portion of an inner chamber of said housing from said substrate loading inlet, and then enters into the lower portion of the inner chamber of said housing through said first gap, said third gap and said guide hole, said flow causes said substrate to be in a fluid state, at least a portion of said solute is deposited and loaded onto said substrate to form a loaded substrate, a portion of said of loaded substrate is moved to the bottom of the inner chamber of said housing and discharged from the inner chamber of said housing from said outlet to unload the substrate, another portion of said loaded substrate is moved to the top of the inner chamber of said housing along with said flow, from which at least a portion of the solute is removed, called the purified stream, passes through said guide hole, enters said straight tube section from said conical diffusion section, and is then discharged from said second gap, said loaded substrate flowing to the bottom of the inner chamber of said housing through said first gap, said third gap and said guide hole, said purified stream moves up the inner chamber of said housing through said sixth gap and is discharged from the inner chamber of said housing from said discharge outlet or said substrate enters the upper portion of the inner chamber of said housing from said substrate loading inlet, and then enters the lower portion of the inner chamber of said housing through said first gap, said third gap, and said guide hole, said flow enters said fourth gap from said flow inlet and then enters the interior of said inner tube through said fifth gap and mixes with said heating agent which enters the interior of said inner tube from said heating agent inlet to form a mixture which is discharged from said inner tube from an upper edge of said inner tube after the temperature has risen to reach or exceed the supercritical temperature of said solvent, a portion of said mixture flows into the interior of said inner tube through said fourth gap and said fifth gap to form an internal recycling, another portion of said mixture causes said substrate to be in a fluid state, at least a portion of said solute is deposited and loaded onto said substrate to formation of a loaded substrate, a portion of said loaded substrate is moved to the bottom of the inner chamber of said housing through said fourth gap and discharged from the inner chamber of said housing from said substrate discharge outlet, another portion of said loaded substrate is moved to the top of the inner chamber of said housing along with said a mixture from which at least a portion of the solute is removed, called the purified mixture, passes through said guide hole, enters said straight tube section from said conical diffusion section, and is then discharged from said second gap, said loaded substrate flowing to the bottom of the inner chambers of said housing through said first gap, said third gap and said guide hole, said purified mixture is moved up the inner chamber of said housing through said sixth gap and discharged from the inner chamber of said housing from said discharge outlet. 35. The solid sedimentation method according to claim 23, wherein said stream is a high-salt wastewater, said high-salt wastewater having a TDS of not more than 20 wt.% and a COD of more than 20,000 mg/l. 36. The solid sediment sedimentation method according to claim 35, wherein said stream is organic wastewater with a high salt content and/or said wastewater with a high salt content has a TDS of 5-20 wt.% and a COD of 20000-40000 mg/l .