CN114804269B - Online desalting and discharging system and method for organic waste supercritical water treatment equipment - Google Patents
Online desalting and discharging system and method for organic waste supercritical water treatment equipment Download PDFInfo
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- CN114804269B CN114804269B CN202210468312.XA CN202210468312A CN114804269B CN 114804269 B CN114804269 B CN 114804269B CN 202210468312 A CN202210468312 A CN 202210468312A CN 114804269 B CN114804269 B CN 114804269B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
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Abstract
The invention discloses an online desalting and discharging system and method for supercritical water treatment equipment for organic wastes. The outside of the spiral conveyor of the salt discharge section, the flash tank and the outside of the external spiral conveyor are all provided with water cooling sleeves for cooling and protecting the equipment, and simultaneously, steam is generated. The control method comprises the steps of salt elimination section starting, salt elimination section starting and capacity expansion pressure control. The invention effectively solves the problem of salt deposition in the supercritical water technology and realizes online desalination and salt discharge.
Description
Technical Field
The invention belongs to the technical field of supercritical water technology desalination and salt discharge, and particularly relates to an online desalination and salt discharge system and method of organic waste supercritical water treatment equipment.
Background
Supercritical water refers to water with temperature not less than 374.15 deg.C and pressure not less than 22.12MPa (i.e. higher than the critical point of water). Compared with normal water, supercritical water has the unique properties of reduced density, reduced viscosity, increased diffusion coefficient, reduced hydrogen bond stability and quantity, and dielectric constant far smaller than that of normal water, and presents the characteristics of non-polar solvent with high diffusivity and good mass transfer. In addition, when supercritical water participates in reaction, unlike normal water, water is generally decomposed into ions to participate in reaction, free radicals in a supercritical water reaction system are increased, and the ionic reaction is weakened. Therefore, a series of supercritical water related technologies, such as supercritical water oxidation, supercritical water gasification, supercritical water thermal modification and supercritical water thermal synthesis, are derived, and a plurality of achievements are achieved in the fields of efficient clean conversion of fossil energy, harmless treatment of wastewater, petroleum development and processing, nano material synthesis and the like.
Supercritical water is an excellent mass transfer medium that enables normally water-insoluble organic and gases to dissolve in supercritical water, but has reduced solubility for inorganic species, thereby creating one of the important challenges in supercritical water technology-inorganic salt deposition. Due to the ion accumulation of water and the change of water density, inorganic salts in water cannot be dissolved in water and are separated out, and further equipment and pipelines are blocked. When the temperature of the discharged water is reduced to the subcritical condition after the reaction, the inorganic salt deposited in the reactor will be dissolved again. Therefore, most reactor designs or operating techniques developed to mitigate salting-out precipitation are associated with operations to cool the effluent after the reaction, such as counter-current flow reactors with brine ponds, evaporation wall reactors, adsorption/reaction on fluidized solid phases, counter-current flow reactors, centrifugal reactors, high-velocity flow, mechanical brushes, rotating scrapers, reactor flushing, additives, low-turbulence/homogeneous precipitation, cross-flow filtration, density separation, extreme pressure operations. It is still necessary to periodically clean the reactor (and any other affected piping or components) of salt deposits. If the cleaning operations are performed too frequently, the down time resulting from system shut down, cleaning, reassembly, pressure testing, and restart may reduce the economics of supercritical water technology or be detrimental to a particular application.
Disclosure of Invention
The technical problem to be solved by the invention is to provide an online desalting and discharging system and method of organic waste supercritical water treatment equipment, aiming at overcoming the defects in the prior art, solving the industrial requirement of online continuous desalting and discharging of salt in the supercritical water technology, and realizing safe and effective control of the system.
The invention adopts the following technical scheme:
the utility model provides an organic waste supercritical water treatment equipment's online desalination system, including row salt section auger delivery ware, row salt section auger delivery ware's input and supercritical water reaction system deposit salt tube coupling, row salt section auger delivery ware's output is divided two the tunnel through the flash vessel, be connected with condenser and outside auger delivery ware respectively, realize online desalination and arrange salt according to the liquid level of control flash vessel and the pressure differential of supercritical water reaction system deposit salt pipeline and row salt section auger delivery ware outlet line, through the aperture of control steam line back pressure valve, realize salt water mixture's flash separation.
Specifically, a salt discharge section screw conveyor outlet control valve and a salt discharge section screw conveyor outlet regulating valve are sequentially arranged on a connecting pipeline between the salt discharge section screw conveyor and the flash tank.
Furthermore, pressure difference detecting instruments are arranged on the supercritical water reaction system precipitated salt pipeline and the outlet pipeline of the salt discharging section screw conveyer and are arranged in an interlocking mode with the outlet regulating valve of the salt discharging section screw conveyer.
Specifically, a flash tank steam outlet control valve is arranged on a connecting pipeline between the condenser and the flash tank.
Specifically, water cooling jackets are arranged outside the salt discharge section screw conveyor, the flash tank and the external screw conveyor.
Furthermore, a water cooling jacket of the external screw conveyor is connected with a water cooling jacket of the spiral conveyor of the salt discharge section through a pipeline sequentially passing through the shell side of the condenser and the water cooling jacket of the flash tank.
Specifically, a flash tank salt discharge outlet regulating valve is arranged on a connecting pipeline between the external spiral conveyor and the flash tank.
Furthermore, the external screw conveyor and the salt discharge outlet regulating valve of the flash tank are interlocked with a liquid level detection instrument arranged in the flash tank.
The invention also provides a working method of the online desalination and discharge system of the supercritical water treatment equipment for organic wastes, which comprises the following steps:
controlling a motor of the spiral conveyor at the salt discharge section to rotate reversely, closing an outlet of the spiral conveyor at the salt discharge section, and observing the pressure difference change conditions at the outlets of the supercritical water system and the spiral conveyor at the salt discharge section in real time; when the pressure difference is larger than a set value, opening an outlet of the spiral conveyor of the salt discharge section, and adjusting the spiral conveyor of the salt discharge section to convey salt slurry downwards; controlling the pressure difference to be within the range of 10-15 MPa by utilizing a valve arranged at the outlet of the spiral conveyor at the salt discharge section;
observing the liquid level change in the flash tank in real time, and controlling the liquid level in the flash tank to be within 20-40% of the set liquid level by using valves arranged at an external spiral conveyor and a salt discharge outlet of the flash tank when the liquid level in the flash tank is greater than the set lowest liquid level;
the flash tank is maintained in the set pressure range of 10-15 MPa by adjusting the opening of a valve arranged at a steam outlet of the flash tank.
Specifically, when the pressure difference is smaller than the lower limit of the set pressure range, the opening degree of an outlet of the spiral conveyor at the salt discharge section is reduced; when the pressure difference is larger than the upper limit of the set pressure range, the opening degree of the outlet of the spiral conveyor of the salt discharging section is increased;
when the liquid level in the flash tank is smaller than the lower limit of the set liquid level range, reducing the rotating speed of the external screw conveyor and reducing the opening of a salt discharge outlet of the flash tank; when the liquid level in the flash tank is larger than the upper limit of the set liquid level range, the rotating speed of the external screw conveyor is increased, and the opening degree of the salt discharge outlet of the flash tank is increased.
Compared with the prior art, the invention at least has the following beneficial effects:
according to the online desalting and discharging system of the supercritical water treatment equipment for the organic wastes, disclosed by the invention, inorganic salts precipitated in a supercritical water reaction device are discharged through the spiral conveyor at the desalting section, so that the safety risks of blockage of the device, uneven temperature distribution and the like are avoided; the inorganic salt solution discharged from the supercritical water reaction device is separated into steam and inorganic salt rich solution after adiabatic expansion in the flash tank; the separated steam is cooled by a condenser, and the separated inorganic salt rich solution is output by an external screw conveyor for treatment or enters a next-stage salt discharge system for further pressure reduction and enrichment.
Furthermore, according to the deposition amount of inorganic salt of the supercritical water reaction device, the intermittent operation and the continuous operation of the salt discharge system are switched by the outlet control valve of the salt discharge section screw conveyor so as to select the operation mode; the pressure difference between the front end and the rear end of the spiral conveyor at the salt discharge section is controlled by an outlet regulating valve of the spiral conveyor at the salt discharge section, so that the starting and the regulation of the salt discharge section are realized.
Further, the pressure difference of the input end and the output end of the spiral conveyor of the salt discharge section is displayed through a pressure difference detection instrument so as to confirm whether the deposited salt of the supercritical water reaction device has a proper pressure discharge device or not; when the pressure difference detection instrument displays that the pressure difference is greater than the rated pressure difference (set according to the number of salt discharge systems), the stable operation of the system is easily influenced, and the opening degree of an outlet regulating valve of the spiral conveyor at the salt discharge section is reduced; when the pressure difference detection instrument displays that the pressure difference is smaller than the rated pressure difference, the discharge of deposited salt is easily influenced, and the opening degree of the outlet regulating valve of the spiral conveyor at the salt discharging section is increased.
Furthermore, the pressure of the adiabatic expansion process in the flash tank is maintained (set according to the system level number of salt discharge systems) through a flash tank steam outlet control valve, so that the separation efficiency of the saline solution is adjusted, and the operation safety of the flash tank is maintained.
Furthermore, water cooling sleeves are arranged outside the salt discharge section screw conveyor, the flash tank and the external screw conveyor to cool and protect the equipment, and steam is generated at the same time.
Furthermore, according to the 'temperature butt' principle, the cooling water is arranged for sectional heat exchange, and the low-temperature section sequentially flows through the high-temperature section for heat exchange (namely sequentially flows through the water cooling jacket of the external screw conveyor, the shell side of the condenser, the water cooling jacket of the flash tank and the water cooling jacket of the salt discharge section screw conveyor), so that the heat exchange efficiency is improved, and the heat energy is reasonably utilized.
Furthermore, the liquid level of the flash tank with a certain liquid level is maintained through the flash tank salt discharge outlet regulating valve, and the heat loss is reduced.
Furthermore, the liquid level of the flash tank is displayed through the liquid level detection instrument, when the liquid level of the flash tank exceeds the rated range, the liquid level of the flash tank is maintained within the rated range by adjusting the opening of the regulating valve of the salt discharge outlet of the flash tank, and the start of flash tank salt discharge and online desalting salt discharge are realized.
A working method of an online desalting and discharging system of organic waste supercritical water treatment equipment comprises the following steps of firstly, increasing the pressure difference at the outlets of a supercritical water system and a salt discharging section screw conveyor through the motor reversal of the salt discharging section screw conveyor so as to form rated pressure difference and enable deposited salt to be smoothly discharged from the supercritical water system; then, the inorganic salt solution is expanded, depressurized and separated in the flash tank, and a certain amount of water is maintained in the flash tank in advance to prevent the temperature from rising suddenly in the flash tank expansion process; and finally, the flash pressure in the flash tank is controlled by adjusting the opening of a valve arranged at the steam outlet of the flash tank, so that the reasonable separation of the saline solution is realized.
Furthermore, the pressure difference between the supercritical water system and the outlet of the spiral conveyor at the salt discharge section is monitored, inorganic salt cannot be effectively discharged when the pressure difference is too small, and the safety risk of the system operation is increased when the pressure difference is too large, so that the pressure difference needs to be controlled to be maintained within a rated range through the opening degree of the outlet of the spiral conveyor at the salt discharge section; liquid level in the monitoring flash tank, the liquid level is too high can reduce flash tank effective volume and influence the separation of salt solution, and the liquid level is too high can promote the flash distillation temperature in the flash tank and increase the safe risk of system operation, consequently need the aperture control liquid level of the rotational speed and flash tank salt discharge outlet through outside auger delivery ware to maintain in rated range.
In conclusion, the invention can effectively improve the problems that inorganic salt is easy to separate out and is blocked in a device or a pipeline in the supercritical water technology, and can effectively separate the saline water solution, thereby obtaining the inorganic salt rich solution and recovering the waste heat; the operability is strong, and the intermittent or continuous operation and the one-stage or multi-stage salt discharge operation can be selected according to the process requirements.
The technical solution of the present invention is further described in detail by the accompanying drawings and embodiments.
Drawings
Fig. 1 is a schematic diagram of the overall structure of the system of the present invention.
Wherein: 1. a salt discharge section screw conveyor; 2. a flash tank; 3. a condenser; 4. an external screw conveyor; v001, an outlet control valve of the spiral conveyor at the salt discharging section; v002, adjusting a valve at the outlet of the spiral conveyor at the salt discharge section; v003. Flash tank steam outlet control valve; and V004, adjusting a salt discharge outlet of the flash tank.
Detailed Description
The technical solutions of the present invention will be described clearly and completely below, and it should be apparent that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the present invention, all the embodiments and preferred methods mentioned herein can be combined with each other to form a new technical solution, if not specifically stated.
In the present invention, all the technical features mentioned herein and preferred features may be combined with each other to form a new technical solution, if not specifically stated.
In the present invention, the percentage (%) or parts means the weight percentage or parts by weight with respect to the composition, if not otherwise specified.
In the present invention, the components referred to or the preferred components thereof may be combined with each other to form a novel embodiment, if not specifically stated.
In the present invention, unless otherwise stated, the numerical range "a-b" represents a shorthand representation of any combination of real numbers between a and b, where a and b are both real numbers. For example, a numerical range of "6 to 22" indicates that all real numbers between "6 to 22" have been listed herein, and "6 to 22" is only a shorthand representation of the combination of these numbers.
The "ranges" disclosed herein may have one or more lower limits and one or more upper limits, respectively, in the form of lower limits and upper limits.
As used herein, the term "and/or" refers to any and all possible combinations of one or more of the associated listed items and includes such combinations.
In the present invention, unless otherwise specified, the individual reactions or operation steps may be performed sequentially or may be performed in sequence. Preferably, the reaction processes herein are carried out sequentially.
Unless otherwise defined, technical and scientific terms used herein have the same meaning as is familiar to those skilled in the art. In addition, any methods or materials similar or equivalent to those described herein can also be used in the present invention.
The invention provides an online desalting and discharging system of supercritical water treatment equipment for organic wastes, wherein a salt discharging section screw conveyor is used for online conveying salt to play a role in reducing pressure, a flash tank is used for flash evaporation and desalination, and a condenser is used for condensing flash evaporation gas; the outside of the spiral conveyor of the salt discharge section, the flash tank and the outside of the external spiral conveyor are all provided with water cooling sleeves for cooling and protecting the equipment, and simultaneously, steam is generated. The control method comprises the steps of salt discharge section starting, salt discharge section starting and expansion pressure control. The invention can effectively solve the problem of salt deposition in the supercritical water technology and realize online desalination and salt discharge.
Referring to fig. 1, the on-line desalting and discharging system of supercritical water treatment equipment for organic wastes of the present invention includes a salt discharging screw conveyor 1, a flash tank 2, a condenser 3 and an external screw conveyor 4.
The entry and the supercritical water reaction system deposit salt tube coupling of salt discharge section auger delivery ware 1, the export of salt discharge section auger delivery ware 1 and the entry linkage of flash tank 2, the steam outlet of flash tank 2 passes through the exit linkage of pipeline and condenser 3, and the salt discharge export of flash tank 2 passes through the pipeline and is connected with outside auger delivery ware 4.
Wherein, a connecting pipeline between the salt discharging section screw conveyor 1 and the flash tank 2 is sequentially provided with a salt discharging section screw conveyor outlet control valve V001 and a salt discharging section screw conveyor outlet regulating valve V002.
And a pressure difference detection instrument PIA001 is arranged on the outlet pipeline of the deposition salt pipeline of the supercritical water reaction system and the salt discharge section screw conveyor 1, and the pressure difference detection instrument PIA001 and the salt discharge section screw conveyor outlet regulating valve V002 are arranged in an interlocking manner.
A flash tank steam outlet control valve V003 is arranged on a connecting pipeline between the condenser 3 and the flash tank 2.
A flash tank salt discharging outlet regulating valve V004 is arranged on a connecting pipeline between the external screw conveyor 4 and the flash tank 2.
The inside of flash vessel 2 is provided with liquid level detection instrument LIC002, and liquid level detection instrument LIC002 sets up with the motor of outside auger 4 and flash vessel salt discharging outlet governing valve V004 interlocking respectively.
The shells of the salt discharging section screw conveyor 1, the flash tank 2 and the external screw conveyor 4 are all provided with water cooling sleeves, and helical blades are arranged in the salt discharging section screw conveyor 1 and the external screw conveyor 4 and connected with a motor.
The online desalting and discharging system of the supercritical water treatment equipment for organic wastes can be designed into a one-stage, two-stage or multi-stage desalting system according to the calculation of the capacity expansion and salt discharge and pressure reduction processes of an actual system; the method comprises the following specific steps:
before system start
The outlet control valve V001 of the salt discharging section screw conveyor and the steam outlet control valve V003 of the flash tank are in a closed state, the motors of the salt discharging section screw conveyor 1 and the external screw conveyor 4 are in a closed state, and the steam outlet pipeline backpressure valve of the flash tank is in a fully-opened state.
Salt rejection segment start-up
Controlling a motor of the salt discharging section screw conveyor 1 to reversely rotate, enabling a conveying screw to reversely rotate upwards, closing an outlet regulating valve V002 of the salt discharging section screw conveyor, opening an outlet control valve V001 of the salt discharging section screw conveyor, and observing the pressure difference change of a pressure difference detection instrument PIA001 at the outlet of the supercritical water system and the salt discharging section screw conveyor 1 in real time (set according to process requirements, for example, for a first-stage salt discharging system, the pressure difference detection instrument PIA001 can be set to be 10-15 MPa, but is not limited to the range);
when the pressure difference of the pressure difference detection instrument PIA001 is larger than a set value (10 MPa), an outlet regulating valve V002 of the salt discharge section screw conveyor is opened, and the motor of the salt discharge section screw conveyor 1 is regulated to rotate forward to convey salt slurry downwards; meanwhile, the outlet regulating valve V002 of the salt discharge section screw conveyor is utilized to control the pressure difference of the pressure difference detection instrument PIA001 to be within a set pressure range (10-15 MPa).
If the pressure difference of the pressure difference detection instrument PIA001 is smaller than the lower limit (10 MPa) of the set pressure range, the opening degree of an outlet regulating valve V002 of the spiral conveyor of the salt discharging section is reduced;
and if the pressure difference of the pressure difference detection instrument PIA001 is larger than the upper limit (15 MPa) of the set pressure range, increasing the opening of the outlet regulating valve V002 of the salt discharging section screw conveyor.
Capacity expansion salt discharge start
Observing the liquid level change in the flash tank 2 in real time by using a liquid level detection instrument LIC002, and opening an external screw conveyor 4 and a flash tank steam outlet control valve V003 to convey salt slurry outwards when the liquid level is greater than a set lowest liquid level; and simultaneously, the liquid level in the flash tank 2 is controlled to be within a set liquid level range (20-40 percent) by utilizing the motor speed (rough adjustment) of the external screw conveyor 4 and the flash tank salt discharge outlet regulating valve V004 (fine adjustment).
And if the liquid level in the flash tank 2 is less than the lower limit of the set liquid level range, reducing the rotating speed of the motor of the external screw conveyor 4 and reducing the opening of the flash tank salt discharge outlet regulating valve V004.
And if the liquid level in the flash tank 2 is larger than the upper limit of the set liquid level range, increasing the rotating speed of the motor of the external screw conveyor 4 and increasing the opening of the flash tank salt discharge outlet regulating valve V004.
Capacity expansion pressure control
The flash tank 2 is maintained within a set pressure range (10 to 15 MPa) by opening control of the flash tank vapor outlet control valve V003.
If the pressure reduction of the first-stage salt discharge system is small or the separation effect of the saline solution is poor, a two-stage or multi-stage salt discharge system can be arranged according to the process requirements; the flash tank 2 in the first-stage salt removing system is called a first-stage flash tank, the external screw conveyor 4 is called a first-stage screw conveyor, the outlet end of the first-stage screw conveyor is connected with the inlet section of the second-stage flash tank, the steam outlet end of the second-stage flash tank is connected with the condenser 3, the solution outlet end of the second-stage flash tank is connected with the second-stage screw conveyor, and the rest is called a multi-stage salt removing system; the sequence of salt discharge of each stage is that after the pressure reduction of the screw conveyor of the previous stage, the flash evaporation is carried out in the flash tank to separate steam and salt-rich solution, the steam is cooled by the condenser, and the salt-rich solution enters the screw conveyor of the current stage and is reduced in pressure to enter the flash tank of the next stage or is discharged.
The invention can discharge more than 95% of deposited salt in a supercritical water system on line, and finally obtain rich solution with the salt content of more than 90 wt.%.
In summary, the online desalting and discharging system and method for the supercritical water treatment equipment for organic wastes provided by the invention have the advantages that the salt discharging section screw conveyor, the flash tank, the condenser and the external screw conveyor are arranged, so that the industrial requirement of online continuous desalting and discharging of salts in the supercritical water technology is met, and the safe and effective control of the system is realized.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (9)
1. The utility model provides an online desalination system's that organic waste supercritical water treatment equipped working method, a serial communication port, the online desalination system that organic waste supercritical water treatment equipped includes salt discharge section auger delivery ware (1), the input and the supercritical water reaction system deposit salt tube coupling of salt discharge section auger delivery ware (1), the output of salt discharge section auger delivery ware (1) divides two the tunnel through flash vessel (2), be connected with condenser (3) and outside auger delivery ware (4) respectively, realize online desalination and salt discharge according to the liquid level of control flash vessel (2) and the pressure differential of supercritical water reaction system deposit salt tube way and salt discharge section auger delivery ware (1) outlet line, through the aperture of control steam line back pressure valve, realize the flash separation of salt water mixture, concrete working method includes:
controlling a motor of the spiral conveyor at the salt discharge section to rotate reversely, closing an outlet of the spiral conveyor at the salt discharge section, and observing the pressure difference change conditions at the outlets of the supercritical water system and the spiral conveyor at the salt discharge section in real time; when the pressure difference is larger than a set value, opening an outlet of the spiral conveyor of the salt discharge section, and adjusting the spiral conveyor of the salt discharge section to convey salt slurry downwards; controlling the pressure difference within the range of 10 to 15MPa by using a valve arranged at the outlet of the spiral conveyor of the salt discharge section;
observing the liquid level change in the flash tank in real time, and controlling the liquid level in the flash tank to be within 20% -40% of the set liquid level by utilizing valves arranged at an external spiral conveyor and a salt discharging outlet of the flash tank when the liquid level in the flash tank is greater than the set lowest liquid level;
the opening of a valve arranged at a steam outlet of the flash tank is adjusted to keep the flash tank within a set pressure range of 10 to 15MPa.
2. The working method of the on-line desalination system of supercritical water treatment equipment of organic waste of claim 1, wherein when the pressure difference is less than the lower limit of the set pressure range, the opening degree of the outlet of the screw conveyor of the salt discharge section is reduced; when the pressure difference is larger than the upper limit of the set pressure range, the opening degree of the outlet of the spiral conveyor of the salt discharging section is increased;
when the liquid level in the flash tank is less than the lower limit of the set liquid level range, reducing the rotating speed of the external spiral conveyor and reducing the opening of a salt discharge outlet of the flash tank; when the liquid level in the flash tank is larger than the upper limit of the set liquid level range, the rotating speed of the external spiral conveyor is increased, and the opening degree of a salt discharge outlet of the flash tank is increased.
3. The operating method of the on-line desalination and salt-removal system of supercritical water treatment equipment for organic wastes according to claim 1, wherein a connection pipeline between the salt-removal section screw conveyor (1) and the flash tank (2) is sequentially provided with a salt-removal section screw conveyor outlet control valve (V001) and a salt-removal section screw conveyor outlet regulating valve (V002).
4. The working method of the on-line desalination and salt-removal system of supercritical water treatment equipment for organic wastes according to claim 3, wherein a pressure difference detection instrument (PIA 001) is arranged on the supercritical water reaction system precipitated salt pipeline and the outlet pipeline of the salt-removal section screw conveyor (1), and the pressure difference detection instrument (PIA 001) and the salt-removal section screw conveyor outlet regulating valve (V002) are arranged in an interlocking manner.
5. The operating method of an on-line desalination and salt-removal system of supercritical water treatment equipment for organic wastes as claimed in claim 1, wherein a flash tank steam outlet control valve (V003) is provided on a connection pipeline between the condenser (3) and the flash tank (2).
6. The working method of the on-line desalination and discharge system of supercritical water treatment equipment for organic wastes according to claim 1, characterized in that a water cooling jacket is arranged outside the salt discharge section screw conveyor (1), the flash tank (2) and the external screw conveyor (4).
7. The working method of the on-line desalination and salt-removal system of supercritical water treatment equipment for organic wastes according to claim 6, characterized in that the water cooling jacket of the external screw conveyor (4) is connected with the water cooling jacket of the salt-removal section screw conveyor (1) through pipelines sequentially passing through the shell side of the condenser (3) and the water cooling jacket of the flash tank (2).
8. The working method of the on-line desalination system of organic waste supercritical water treatment equipment of claim 1, wherein a flash tank salt discharge outlet regulating valve (V004) is arranged on a connecting pipeline between the external screw conveyor (4) and the flash tank (2).
9. The working method of the on-line desalination system of supercritical water treatment equipment for organic wastes according to claim 8, characterized in that the external screw conveyor (4) and the flash tank salt discharge outlet regulating valve (V004) are interlocked with a liquid level detection instrument (LIC 002) arranged in the flash tank (2).
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| JPH09314155A (en) * | 1996-03-25 | 1997-12-09 | Japan Organo Co Ltd | Method and apparatus for oxidizing supercritical water |
| CN102642947B (en) * | 2012-04-23 | 2013-11-13 | 西安交通大学 | Supercritical water oxidization treatment system for high-salinity organic waste water |
| CN102633351B (en) * | 2012-04-23 | 2013-07-10 | 西安交通大学 | Desalting and salt discharging control method for supercritical water oxidation systems |
| CN113958940B (en) * | 2021-11-30 | 2024-01-23 | 西安热工研究院有限公司 | Maintenance system and method for high-energy water recovery of supercritical unit |
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