CN101987755B - Supercritical water treatment system of organic wastewater with low salt content - Google Patents
Supercritical water treatment system of organic wastewater with low salt content Download PDFInfo
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- CN101987755B CN101987755B CN2010105167633A CN201010516763A CN101987755B CN 101987755 B CN101987755 B CN 101987755B CN 2010105167633 A CN2010105167633 A CN 2010105167633A CN 201010516763 A CN201010516763 A CN 201010516763A CN 101987755 B CN101987755 B CN 101987755B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 109
- 239000002351 wastewater Substances 0.000 title claims abstract description 39
- 150000003839 salts Chemical class 0.000 title claims abstract description 22
- 239000010815 organic waste Substances 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000010612 desalination reaction Methods 0.000 claims description 24
- 238000003860 storage Methods 0.000 claims description 23
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 13
- 239000011780 sodium chloride Substances 0.000 claims description 13
- 239000003513 alkali Substances 0.000 claims description 8
- 239000013505 freshwater Substances 0.000 claims description 7
- 238000009826 distribution Methods 0.000 claims description 5
- 239000008399 tap water Substances 0.000 claims description 5
- 235000020679 tap water Nutrition 0.000 claims description 5
- 210000000056 organ Anatomy 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 2
- 235000019600 saltiness Nutrition 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 24
- 229910017053 inorganic salt Inorganic materials 0.000 abstract description 11
- 239000000463 material Substances 0.000 abstract description 7
- 238000000034 method Methods 0.000 abstract description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 5
- 238000000926 separation method Methods 0.000 abstract description 5
- 239000003054 catalyst Substances 0.000 abstract description 4
- 230000000694 effects Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 abstract description 2
- 238000011033 desalting Methods 0.000 abstract 2
- 239000003344 environmental pollutant Substances 0.000 abstract 1
- 231100000719 pollutant Toxicity 0.000 abstract 1
- 239000002699 waste material Substances 0.000 abstract 1
- 238000007600 charging Methods 0.000 description 13
- 239000012530 fluid Substances 0.000 description 9
- 238000009284 supercritical water oxidation Methods 0.000 description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000004062 sedimentation Methods 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 239000010808 liquid waste Substances 0.000 description 3
- 238000000197 pyrolysis Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005115 demineralization Methods 0.000 description 1
- 230000002328 demineralizing effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002277 temperature effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a supercritical water treatment system and method of organic wastewater with low salt content. In the system, the heat after reaction is fully recycled by a heat exchanger to generate hot water; liquid and gas after reaction are separated and recycled by a gas-liquid separator; according to the characteristics of different materials, an optimal supercritical water treatment mode is flexibly selected by controlling the air flow; on the basis of reserving a tubular reactor, a tank reactor is connected in parallel; the treatment effect of ammonia nitrogen and the like is improved and the conditions required for the supercritical reaction are reduced by adding catalysts; a desalting buffer tank is provided for realizing the desalting operation in a supercritical state; and the clogging problem of a feeding pipeline caused by preheating can be effectively avoided by controlling the preheating temperature of the wastes. The system of the invention integrates removal of COD, inorganic salt and ammonia nitrogen, integrates the pretreatment, mixing, reaction, product separation and product collection of materials, and is widely applied to the harmless treatment processes of pollutants such as high-concentration organic waste which can not be biochemically degraded easily and the like.
Description
Technical field
The present invention relates to a kind of system that utilizes supercritical water bio-refractory organic waste water to be carried out harmless treatment, the super critical water treatment system of particularly a kind of low saline salinity (1-2%) organic waste water as reaction medium.
Background technology
Supercritical water (Supercritical Water, be called for short SCW) be meant temperature and pressure all be higher than its stagnation point (T=374.15 ℃, the water of special state P=22.12MPa).Have only a spot of hydrogen bond to exist under this state, specific inductivity is similar to organic solvent, has high spread coefficient and low viscosity.Organism, oxygen can dissolve each other by arbitrary proportion and SCW, thereby make inhomogeneous reaction become homogeneous reaction, have reduced the resistance of mass transfer, heat transfer greatly.And inorganics particularly the solubleness of salt in SCW is extremely low, easily it is separated.
The supercritical water treatment technology of organic waste water comprises supercritical water oxidation technology (Supercritical Water Oxidation; Abbreviation SCWO), supercritical water gasification technology (Supercritical Water Gasification; Be called for short SCWG) and supercritical water partial oxidation technology (Supercritical Water Partial Oxidation is called for short SCWPO).
SCWO is a special property of utilizing water under supercritical state, to be had, makes organism and oxygenant that oxidizing reaction take place rapidly in supercritical water and comes thorough decomposing organic matter, realizes organic harmless treatment.
SCWG is a special property of utilizing water under supercritical state, to be had, and under the condition of oxidizer not, reactions such as hydrolysis, pyrolysis take place in supercritical water organism, and generating with hydrogen is main flammable gonosome.
SCWPO is a special property of utilizing water under supercritical state, to be had, and under the prerequisite that the partially oxidation agent is provided, organism being decomposed generate with hydrogen is main inflammable gas.The adding of oxygenant makes the material that originally in gasification, is difficult to decompose to decompose, and improves vaporization rate, and simultaneously, oxygenant also can make the generation of tar be inhibited, and reduces the latch up phenomenon of reactor drum.
Though the supercritical water treatment technology has obtained very much progress, still have some problems that need solution, show:
1) the SCWO process is a thermopositive reaction, and when organic massfraction reaches 1～2%, just can realize self-heating.But because the recovery and the optimization problem of supercritical water oxidation treatment system energy do not have fine solution, so the running cost of supercritical water treatment process is still higher.
2) in the lower supercritical water of density, the solubleness of inorganic salt in water significantly reduces.Therefore the salt that generates in material and the reaction process is easy to from supercritical water, separate out the formation salt sedimentation.Salt sedimentation can cause the pipeline and the reactor plugs of system, can make the heat transfer deterioration of equipment such as interchanger simultaneously, finally causes system normally to move.And existing demineralization plant or system are limited by operational condition, are not suitable under the supercritical state, safety, desalination easily.
3) reactor drum that is used for supercritical water treatment at present mainly is a tubular reactor.The structure of tubular reactor is simple relatively, be widely used, and is prone to stifled, uncontrollable exothermic heat of reaction, is difficult to distinguish shortcomings such as pressure influence and temperature effect but have the salt deposition.Though and existing evaporation wall type reactor drum can effectively be avoided problems such as salt sedimentation, corrosion, has the low problem of energy utilization efficiency also.
4) during supercritical water oxidation was handled, the oxidation of ammonia nitrogen is difficulty comparatively.There are some researches show: when catalyst-free, when temperature was lower than 640 ℃, any degraded did not take place in ammonia; And reach 680 ℃, 24.8MPa when reaction conditions, the residence time is when being 10s, has only 10% ammonia oxidized.Other there are some researches show: promptly use MnO
2/ CeO
2As catalyzer, when reaction conditions is 450 ℃, 27.6MPa, the residence time, the degradation rate of ammonia also had only 40% when being 0.8s.
Summary of the invention
The objective of the invention is to overcome the existing existing deficiency of super critical water treatment system, a kind of novel super critical water treatment system is provided, can be widely used in the harmless treatment and the recycling process of low saline salinity organic waste water.
For reaching above purpose, the present invention takes following technical scheme to be achieved:
A kind of super critical water treatment system of low saline salinity organic waste water; It is characterized in that; Comprise air preheater, the inlet end of said air preheater shell-side connects high-pressure air, and the exit end of air preheater shell-side is communicated with a mixer entrance end; Another inlet end of this mixing tank is communicated with the outlet of waste water preheater shell-side, and waste water preheater shell-side inlet is communicated with the waste water storage device; The outlet of said mixing tank links to each other with the inlet of first tubular reactor; The outlet of first tubular reactor links to each other with the inlet of second tubular reactor; The outlet of second tubular reactor is divided into two-way; One the tunnel links to each other with the inlet end of three-tube type reactor drum, and another road links to each other with the inlet end of tank reactor; It is to be communicated with the inlet end of preheating of air organ pipe side after one the tunnel that the exit end of three-tube type reactor drum and the water side of tank reactor are converged; The outlet of preheating of air organ pipe side is communicated with the entrance and exit of waste water preheater tube side respectively, realizes the distribution between the two-way flow through the variable valve on the pipeline; The outlet of waste water preheater tube side is communicated with the inlet of hot water generator pipe side, and the outlet of hot water generator pipe side is communicated with a gas-liquid separator through back pressure valve; The shell-side of hot water generator is communicated with the thermal water utilization device; Be equipped with well heater on said first tubular reactor and second tubular reactor.
In the such scheme, said tank reactor is the baffling tank reactor, and its bottom salt outlet is communicated with blow-off line through a desalination surge tank.
Said thermal water utilization device comprises the clear water storage tank that connects tap water; Its outlet is communicated with a fresh water pump; This clear water pump outlet is divided into two-way through threeway, and one the tunnel is communicated with the inlet end of hot water generator shell-side, and another road is communicated with the outlet at bottom end of desalination surge tank; The exit end of hot water generator shell-side is communicated with a hot water storage tank's inlet end.
Said waste water storage device comprises and has the storage tank that adds the alkali jar that its inlet end connects raw material waste water through valve; Exit end is communicated with the inlet end of waste water preheater shell-side through a product pump.Be provided with whisking appliance in the storage tank.
Be provided with line strainer between the outlet of said hot water generator pipe side and the back pressure valve.
The major advantage of system of the present invention is:
1, through air preheater, waste water preheater preheating material, produce life through hot water generator and use hot water, make full use of fluidic heat after the reaction.Electric heater starts or reacts and can not come into operation during self-heating in system, and replenishment system normally moves institute's heat requirement.Through to the reacted heat of abundant recycling, effectively reduce the running cost of the super critical water treatment system of low saline salinity organic waste water.
2, on the basis of tubular reactor, increased the baffling tank reactor, can be through increasing the speed that catalyzer improves supercritical water reaction.
3, owing to adopted the baffling tank reactor, utilize inorganic salt in reactor drum, to carry out the first step salt at the low dissolution characteristics of overcritical water electrode and separate, the salt sedimentation after the separation is at reactor bottom.The tank reactor lower end connects the desalination surge tank; Close desalination surge tank outlet at bottom valve; Open the valve between tank reactor and the desalination surge tank, the inorganic salt that are deposited on reactor bottom through pressure reduction and action of gravity are brought in the desalination surge tank, and intermittent type ground opens and closes desalination surge tank two ends valve up and down; Realize the intermittent type removal of inorganic salt; Avoided because of the caused blockage problem of salt sedimentation, the liquid after having guaranteed to handle is saliferous or contain the salt of minute quantity not, has satisfied the desalination requirement.
Pre-treatment, mixing, reaction, the gas-liquid separation of system of the present invention collection charging are collected in one, and the integrated performance of system is good.Can choose suitable supercritical water treatment mode flexibly to different feeds, under the prerequisite that guarantees charging harmless treatment (COD reduction of discharging, desalination), realize the purpose of its recycling (product hydrogen).
Description of drawings
Below in conjunction with accompanying drawing and embodiment the present invention is done further detailed description.
Fig. 1 is the structural representation of system of the present invention.
Among the figure: 1 is High-Pressure Compressor; 2 is surge tank; 3 is air preheater; 4 for adding the alkali jar; 5 is storage tank; 6 is product pump; 7 is the waste water preheater; 8 is mixing tank; 9 is first tubular reactor; 10 is second tubular reactor; 11 is the three-tube type reactor drum; 12 is tank reactor; 13 is the desalination surge tank; 14 is the clear water storage tank; 15 is fresh water pump; 16 is hot water generator; 17 is the hot water storage tank; 18 is line strainer; 19 is back pressure valve; 20 is gas-liquid separator.
Legend implication among Fig. 1 is seen table 1
Instrument code implication among Fig. 1 is seen table 2.
Table 1
Table 2
| Code | The code meaning | Code | The code meaning |
| FIC | Flow shows control | TIC | Temperature shows control |
| PIC | Pressure display control | LIC | Liquid level shows control |
| ELEC1 | Electric heater 1 | ELEC2 | Electric heater 2 |
Embodiment
With reference to shown in Figure 1, equipment connection mode is following in the super critical water treatment system of low saline salinity organic waste water:
High-Pressure Compressor 1 is communicated with the inlet end of surge tank 2, and the exit end of surge tank 2 is communicated with the inlet end of air preheater 3 shells, and the exit end of air heat exchanger 3 shell-sides is communicated with mixing tank 8 inlet ends.
The outlet that adds alkali jar 4 links to each other with the inlet of storage tank 5; The exit end of storage tank 5 is communicated with the inlet end of product pump 6; The exit end of product pump 6 is communicated with the inlet end of waste water preheater 7 shell-sides, the outlet of waste water preheater 7 shell-sides be communicated with another inlet end of mixing tank 8.
The outlet of mixing tank 8 links to each other with the inlet of first tubular reactor 9, and the outlet of first tubular reactor 9 links to each other with the inlet of second tubular reactor 10.Arrange first step electric heater (ELEC1) on first tubular reactor 9, arrange second stage electric heater (ELEC2) on second tubular reactor 10.The outlet of second tubular reactor 10 is divided into two-way, and one the tunnel is communicated with the inlet end of three-tube type reactor drum 11, and another road links to each other with the inlet end of tank reactor 12.During normal the operation, having only wherein one tunnel work, does not work in another road.It is one the tunnel that the water side of the exit end of three-tube type reactor drum 11 and tank reactor 12 is converged, and is communicated with the inlet end of air preheater 3 pipe sides.The pipe side outlet of air preheater 3 is divided into two-way, and one the tunnel is communicated with the inlet end of waste water preheater 7 pipe sides, and one the tunnel is communicated with exit end that waste water preheater 7 is managed sides, through the distribution between the realization of the variable valve on the pipeline two-way flow.The outlet of waste water preheater 7 pipe sides is communicated with the inlet of hot water generator 16 pipe sides; The outlet of hot water generator 16 pipe sides links to each other with the inlet of line strainer 18; The outlet of line strainer 18 is communicated with the inlet of back pressure valve 19, and the outlet of back pressure valve 19 is communicated with the inlet of gas-liquid separator 20.
The bottom salt outlet of tank reactor 12 is communicated with the inlet end of desalination surge tank 13, and the exit end of desalination surge tank 13 connects blow-off line.
The outlet of clear water storage tank 14 is communicated with the inlet of fresh water pump 15, and the exit end of fresh water pump 15 is divided into two-way through threeway, and one the tunnel is communicated with the inlet end of the shell-side of hot water generator 16, and another road is communicated with the outlet at bottom end of desalination surge tank 13.The exit end of hot water generator 16 shell-sides is communicated with hot water storage tank 17 inlet end.
The super critical water treatment system principle of work of low saline salinity organic waste water shown in Figure 1 is following:
1) air is after High-Pressure Compressor 1 pressurization and regulating; Get into surge tank 2 and reduce flow rate fluctuation; Get into the shell-side of airheater 3 then, be heated to about 300 ℃ of direct mixing tanks 8 that get into by the outlet fluid of reactor drum 11 or 12 and mix with charging (organic liquid waste).
2) according to the physicochemical property of charging, select suitable alkali and add alkali number, be stored in alkaline solution and add in the alkali jar 4; Unlatching adds alkali jar 4 and is exported to the valve between storage tank 5 inlets; Start the whisking appliance be arranged in the storage tank 5 mixed and monitored parallel feeding to charging pH, charging get into product pump 6 pressurized with regulating after, get into the shell-side of waste water preheater 7 again; Reacted hot-fluid by the pipe side is preheated to about 200 ℃, then gets into mixing tank 8.
3) high-pressure air (what participate in reaction mainly is oxygen), organism charging get into first tubular reactor 9 behind the thorough mixing in mixing tank 8, then second get into tubular reactor 10.Through managing more than the supercritical temperature of outer heating with tube fluid heat temperature raising to water.If the ammonia nitrogen of organic liquid waste and inorganic salt content is lower, supercutical fluid optionally gets into three-tube type reactor drum 11, does not carry out the desalination operation; If the higher (NH of the ammonia nitrogen of organic liquid waste and inorganic salt content
3-N＞50mg/L), supercutical fluid optionally gets into tank reactor 12, and wherein tank reactor 12 inside have catalyst tank can lay pellet type catalyst.In tank reactor 12; Rely on the characteristic of salt utmost point low solubility in supercritical water; To reactor bottom, the reacting fluid adverse current of a large amount of cleanings upwards flows and flows out through the water side from tank reactor 12 bottoms behind the catalyst bed reaction inorganic salt through gravity settling.
4) the pipe side that gets into air preheater 3, waste water preheater 7, hot water generator 16 successively from reactor drum 11 or 12 effusive hot-fluids is removed preheated air, waste water, and obtains hot water.Wherein the pipe side outlet of air preheater 3 is divided into two-way; One the tunnel is communicated with the inlet end of waste water preheater 7 pipe sides; One the tunnel is communicated with the exit end of waste water preheater 7 pipe sides; Realize the distribution between the two-way flow through the variable valve on the pipeline, guarantee that the temperature after the waste water preheating is about 200 ℃, be lower than the temperature of waste water generation pyrolysis and coking.Hot water generator 16 pipe side outlet place fluid temperature (F.T.)s are reduced to about 80 ℃.Cooled fluid is decompressed to normal atmosphere through line strainer 18 through back pressure valve 19, gets into gas-liquid separator 20 then and carries out gas-liquid separation.
5) tap water is stored in the clear water storage tank 14 in advance, and tap water is divided into two-way after fresh water pump 15 pressurizations, and one the road flows into the shell-side of hot water generator 16, obtains life through heat exchange and uses hot water, and be stored among the hot water storage tank 17; Another road clear water flows into the salt discharge outlet conduit of desalination surge tank 13, is used for the desalination operation.
System of the present invention has carried out optimization process to energy-recuperation system, has utilized reaction back fluidic heat.Through air preheater 3, waste water preheater 7 preheating materials heat is brought in the system again, produces life through hot water generator 16 and use hot water, make full use of reaction back fluidic heat.Start or reaction can not self-heating the time in system, electrically heated ELEC1, ELEC2 come into operation, and replenishment system normally moves institute's heat requirement.When reaction can self-heating, then close electrically heated ELEC1, ELEC2.Through to the reacted heat of abundant recycling, reduced the running cost of the super critical water treatment system of low saline salinity organic waste water.
Reactor drum 12 in the system of the present invention is the baffling tank reactor, utilizes inorganic salt extremely low dissolution characteristics in supercritical water, and inorganic salt at first are deposited in the bottom of reactor drum 12.Open fresh water pump 15 and make the tap water that is full of normal temperature and pressure in the desalination snubber 13.Open the valve between tank reactor 12 to the desalination snubber 13, the salt of tank reactor 12 bottoms gets into desalination surge tank 13 under the effect of initial pressure reduction, gravity.Then close the valve of desalination surge tank 13 inlet ends, open the exit end valve, inorganic salt in the jar are discharged.The salt discharge process can intermittent type, carry out repeatedly, thereby has realized the function of the continuous desalination of system, intermittent type salt discharge, has avoided the caused blockage problem of salt sedimentation, and the liquid after having guaranteed to handle is saliferous or contain the salt of minute quantity not, has satisfied processing requirements.
The pipe side outlet of system of the present invention air preheater 3 is divided into two-way, and one the tunnel is communicated with the inlet end of waste water preheater 7 pipe sides, and one the tunnel is communicated with exit end that waste water preheater 7 is managed sides.Exit end at waste water preheater 7 shell-sides is provided with thermopair, according to the preheating temperature of waste water, regulates through the variable valve on the pipeline automatically and realizes the distribution between the two-way flow, and the temperature after the assurance wastewater heat exchange is lower than the temperature of waste water generation pyrolysis and coking.Air mixes with charging in mixing tank 8, can increase the flow velocity of charging, carries out initial reaction with charging simultaneously, reduces the generation of easy obstruction materials such as tar.The blockage problem that these measures have effectively avoided feeding preheating to be easy to generate in the pyroprocess.
The supply of the air in the system of the present invention can be regulated through bypass emptying; To different chargings; The start and stop of add-on through regulating air and electrically heated ELEC1, ELEC2 can be selected different supercritical water treatment modes flexibly, and the easy to handle organism is preferentially selected SCWG; More unmanageable organism can be selected SCWPO, and the organism of intractable is selected SCWO.System of the present invention can guarantee to realize as much as possible under the prerequisite of charging harmless treatment the purpose of its recycling, has multifunctionality.The pre-treatment, mixing, reaction, the gas-liquid separation that collect charging simultaneously are collected in one, and the integrated performance of system is good.
Claims (5)
1. the super critical water treatment system of a low saline salinity organic waste water; Be that saltiness is the super critical water treatment system of the organic waste water of 1-2%, it is characterized in that, comprise air preheater; The inlet end of said air preheater shell-side connects high-pressure air; The exit end of air preheater shell-side is communicated with a mixer entrance end, and another inlet end of this mixing tank is communicated with the outlet of waste water preheater shell-side, and waste water preheater shell-side inlet is communicated with the waste water storage device; The outlet of said mixing tank links to each other with the inlet of first tubular reactor; The outlet of first tubular reactor links to each other with the inlet of second tubular reactor; The outlet of second tubular reactor is divided into two-way; One the tunnel links to each other with the inlet end of three-tube type reactor drum, and another road links to each other with the inlet end of tank reactor; It is to be communicated with the inlet end of preheating of air organ pipe side after one the tunnel that the exit end of three-tube type reactor drum and the water side of tank reactor are converged; The outlet of preheating of air organ pipe side is communicated with the entrance and exit of waste water preheater tube side respectively, realizes the distribution between the two-way flow through the variable valve on the pipeline; The outlet of waste water preheater tube side is communicated with the inlet of hot water generator pipe side, and the outlet of hot water generator pipe side is communicated with a gas-liquid separator through back pressure valve; The shell-side of hot water generator is communicated with the thermal water utilization device; Be equipped with well heater on said first tubular reactor and second tubular reactor.
2. the super critical water treatment system of low saline salinity organic waste water as claimed in claim 1 is characterized in that, said tank reactor is the baffling tank reactor, and its bottom salt outlet is communicated with blow-off line through a desalination surge tank.
3. the super critical water treatment system of low saline salinity organic waste water as claimed in claim 2; It is characterized in that; Said thermal water utilization device comprises the clear water storage tank that connects tap water, and its outlet is communicated with a fresh water pump, and this clear water pump outlet is divided into two-way through threeway; One the tunnel is communicated with the inlet end of hot water generator shell-side, and another road is communicated with the outlet at bottom end of desalination surge tank; The exit end of hot water generator shell-side is communicated with a hot water storage tank's inlet end.
4. the super critical water treatment system of low saline salinity organic waste water as claimed in claim 1 is characterized in that, said waste water storage device comprises and have the storage tank that adds the alkali jar that its inlet end connects raw material waste water through valve; Exit end is communicated with the inlet end of waste water preheater shell-side through a product pump, is provided with whisking appliance in the storage tank.
5. the super critical water treatment system of low saline salinity organic waste water as claimed in claim 1 is characterized in that, is provided with line strainer between the outlet of said hot water generator pipe side and the back pressure valve.
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| CN2010105167633A CN101987755B (en) | 2010-10-22 | 2010-10-22 | Supercritical water treatment system of organic wastewater with low salt content |
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| CN111760517A (en) * | 2020-07-01 | 2020-10-13 | 西安交通大学 | Supercritical hydrothermal synthesis system and method capable of switching multi-material mixing mode and sequence |
| CN114790026B (en) * | 2022-04-29 | 2023-07-21 | 西安交通大学 | Supercritical water oxidation treatment method and system |
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| US6171509B1 (en) * | 1998-06-12 | 2001-01-09 | Chematur Engineering Ab | Method and apparatus for treating salt streams |
| CN1137861C (en) * | 1998-10-22 | 2004-02-11 | 孙传经 | Waste water treatment process by super-critical aqueous oxidation |
| CN1186273C (en) * | 2000-12-30 | 2005-01-26 | 深圳市宝利达实业有限公司 | Supercritical water oxiding method and device for flowing sewage treatment and power supply |
| CN1323748A (en) * | 2001-06-22 | 2001-11-28 | 田江霞 | Supercritical sewage oxidizing treater |
| CN1318326C (en) * | 2005-06-07 | 2007-05-30 | 中国科学院山西煤炭化学研究所 | Method of sewage oxidation treatment using supercritical water |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| EP4063470A1 (en) * | 2021-03-24 | 2022-09-28 | Paul Scherrer Institut | Process for catalytic supercritical water gasification equipped with several sulfur removal steps |
| WO2022199943A1 (en) * | 2021-03-24 | 2022-09-29 | Paul Scherrer Institut | Process for catalytic supercritical water gasification equipped with several sulfur removal steps |
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