CN204039202U - A kind of thick-oil waste water pre-treatment and evaporative desalination system - Google Patents
A kind of thick-oil waste water pre-treatment and evaporative desalination system Download PDFInfo
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- CN204039202U CN204039202U CN201420481135.XU CN201420481135U CN204039202U CN 204039202 U CN204039202 U CN 204039202U CN 201420481135 U CN201420481135 U CN 201420481135U CN 204039202 U CN204039202 U CN 204039202U
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Abstract
A kind of thick-oil waste water pre-treatment and evaporative desalination system, two-stage chemical reaction clarification pretreatment system is set before vaporizer, effectively removes the silicon-dioxide in thick-oil waste water and hardness, coordinate high temperature Scale inhibitors, avoid the fouling of evaporator heat exchange face, vaporizer long-term stability is run; The dense water of vaporizer discharge, after evaporation pond spontaneous evaporation is disposed, can realize the wastewater zero discharge of process system.The utility model employing evaporation technology makes full use of the heat energy in high-heat heavy crude waste water, and in the water of condensation that falling-film evaporator produces, saltiness and organism significantly reduce, and after follow-up organic matter removal and deep desalting treatment, can be used for station boiler supplementary feed.In addition, the silicon-dioxide in the utility model employing secondary chemical reaction removal thick-oil waste water and hardness, in conjunction with adding Scale inhibitors to avoid the fouling of evaporator heat exchange face, evaporator condensation water saltiness is low, reaches thick-oil waste water pro desalting target.
Description
Technical field
The utility model belongs to Industrial Wastewater Treatment and resource circulation utilization technical field, is specifically related to a kind of thick-oil waste water pre-treatment and evaporative desalination system.
Background technology
There is abundant viscous crude resource in China, and emphasis is distributed in the oil fields such as triumph, the Liaohe River, Henan, Xinjiang.Because viscosity of thickened oil is high, poor fluidity, needs to use a large amount of high pressure, high-quality steam to heat oil reservoir in viscous oil recovery process, improves its mobility and makes it be easy to exploitation.Use that steam carries out a large amount of high temperature of association in the process of heavy crude heat extraction, high salt, high silicon, high organic thick-oil waste water need to dispose.At present, routine techniques be thick-oil waste water is carried out oil removing, softening after, reach in " viscous crude field recovered water is used for vapour generator Water purification design specifications " (SY/T0097-2000) " injection boiler feedwater quality index ", be back to distributed Sweet natural gas arcola.Because reuse water quality is lower, boiler blowdown rate is high, and energy waste is very large, and steam quality is lower, can not meet the growth requirement of heavy crude heat extraction technology.
Adopt high-parameters coal burning boiler of power station to substitute Sweet natural gas arcola, produce superheated vapour for oil field note well in cogeneration mode, generate electricity simultaneously, there is good economic benefit.But station boiler is very high to supplementary feed water quality requirement, the requirement that boiler replenishing water need reach " thermal power generation unit and apparatus of steam power plants Water Vapor Quality " (GB/T12145-2008).Because thick-oil waste water water quality is very complicated, temperature, organism, saltiness etc. are higher, and fouling tendency is strong, and the difficulty of it being carried out to total demineralization process is high, there is not yet successful Engineering Projects report.
Utility model content
The purpose of this utility model is to provide a kind of thick-oil waste water pre-treatment and evaporative desalination system, and the thick-oil waste water passing through this system process can realize the pro desalting of thick-oil waste water, reduces the organic content in thick-oil waste water simultaneously; And namely can be used for station boiler supplementary feed through follow-up organic matter removal and deep desalting treatment.
In order to achieve the above object, the technical solution adopted in the utility model is: comprise thick-oil waste water pond and the A reactor that is communicated with successively with thick-oil waste water pond and primary-clarifiers, and A reactor is provided with the first dispensing mouth for adding silica removal chemical agent; The liquid exit of described primary-clarifiers is connected with Secondary clarifier with second reactor successively, and second reactor is provided with the second dispensing mouth for adding deliming chemical agent; The solid outlet of I and II settler is divided into two-way, returns the entrance of A reactor after a road is connected with pressure filter, and another road is connected with the entrance of corresponding I and II reactor; The liquid exit of Secondary clarifier is connected with falling-film evaporator, falling-film evaporator with for providing the heat power supply device of thermal source to be connected for the first single-effect evaporator of falling-film evaporator, the dense water out of end effect of falling-film evaporator is connected with evaporation pond, the condensation-water drain of each single-effect evaporator of falling-film evaporator is connected with condensation water tank, and end effect vapour outlet is connected with condensation water tank through condenser.
Flasher is provided with between described thick-oil waste water pond and A reactor.
The vapour outlet of described flasher is connected with the first single-effect evaporator of falling-film evaporator, and liquid exit is connected with A reactor.
Described pressure filter adopts plate and frame(type)filter press or centrifugal drier.
Filtering basin are provided with between the liquid exit of described Secondary clarifier and falling-film evaporator.
Described filtering basin adopt multi-medium filtering pond, sand filter, variable orifice gap filtering basin or fibrous filtering pool.
Described falling-film evaporator is provided with the 3rd dosing mouth for adding Scale inhibitors, and falling-film evaporator adopts 2 effect ~ 4 effect plate-type down-film evaporator or tube-type down-flow evaporators.
Described heat power supply device adopts station boiler steam turbine, and the low pressure (LP) cylinder exhaust steam outlet of station boiler steam turbine is connected with the first single-effect evaporator of falling-film evaporator.
Described condenser adopts recirculated water cooling condensing device, direct current water-cooled condenser, direct air cooled condenser or indirect air cooling condenser.
Compared with prior art, the beneficial effects of the utility model are:
1, because thick-oil waste water has high temperature, high salt, high silicon, high organic feature, its water temperature is at 80 DEG C or higher, according to biological treatment-embrane method desalination process process thick-oil waste water, must first lower the temperature, heat energy then in thick-oil waste water can not get effective utilization, and the utility model adopts falling-film evaporator process thick-oil waste water, effectively make use of the heat energy in waste water.
2, because silica concentration in thick-oil waste water is very high, can 250mg/L ~ 300mg/L be reached, direct evaporation process, i.e. a large amount of fouling about Waste water concentrating to 4 times, and tie silicates dirt layer and be difficult to cleaning and remove; The utility model is provided with A reactor, primary-clarifiers, second reactor, Secondary clarifier (i.e. two-stage reaction clarification pretreatment system) before falling-film evaporator, A reactor and primary-clarifiers are for removing the silicon-dioxide in thick-oil waste water, and second order reaction settler is for removing the Ca in thick-oil waste water
2+, in product water, silica concentration is lower than 50mg/L, Ca
2+concentration, lower than 0.1mmol/L, makes thick-oil waste water evaporation concentration to 20 times ~ 30 times; And the precipitation body refuse after primary-clarifiers and Secondary clarifier solid-liquid separation can also recycle.
3, the thick-oil waste water of the utility model after falling-film evaporator process, its water of condensation saltiness is lower than 50mg/L, COD is lower than 100mg/L, deliver to condensation water tank storage, after follow-up organic matter removal and deep desalting treatment, can be used for station boiler supplementary feed, and the dense water of falling-film evaporator discharge is after evaporation pond spontaneous evaporation is disposed, and can realize the wastewater zero discharge of process system.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Wherein, 1-thick-oil waste water pond, 2-flasher, 3-A reactor, 4-primary-clarifiers, 5-second reactor, 6-Secondary clarifier, 7-filtering basin, 8-falling-film evaporator, 9-condensation water tank, 10-station boiler steam turbine, 11-condenser, 12-evaporation pond, 13-pressure filter; A-silica removal medicament, b-pH adjusting agent, c-flocculation agent, d-coagulant aids, e-sodium carbonate, f-Scale inhibitors.
Embodiment
Below in conjunction with accompanying drawing, the utility model is described in further details.
See Fig. 1, the flasher 2 that the pre-treatment of the utility model thick-oil waste water and evaporative desalination system comprise thick-oil waste water pond 1 and be connected with thick-oil waste water pond 1, the vapour outlet of flasher 2 is connected with the first single-effect evaporator of falling-film evaporator 8, liquid exit is connected with two-stage reaction clarification system, and two-stage reaction clarification system is made up of A reactor 3, primary-clarifiers 4, second reactor 5 and Secondary clarifier 6, A reactor 3 is provided with the first dispensing mouth for adding silica removal chemical agent; Second reactor 5 is provided with the second dispensing mouth for adding deliming chemical agent; A reactor 3 is connected with primary-clarifiers 4, the liquid exit of primary-clarifiers 4 is connected with Secondary clarifier 6 with second reactor 5 successively, and I and II settler 4, the solid outlet of 6 is divided into two-way, one tunnel returns the entrance of A reactor 3 after being connected with pressure filter 13, another road is connected with the entrance of corresponding I and II reactor 3,5; The liquid exit of Secondary clarifier 6 is connected with falling-film evaporator 8 through filter tank 7, the falling-film evaporator 8 that falling-film evaporator 8 adopts 2 effect ~ 4 to imitate, falling-film evaporator 8 is provided with the 3rd dosing mouth for adding Scale inhibitors, station boiler steam turbine 10 is for providing thermal source (i.e. heating steam) for the first single-effect evaporator of falling-film evaporator 8, and the low pressure (LP) cylinder exhaust steam outlet of station boiler steam turbine 10 is connected with the first single-effect evaporator of falling-film evaporator 8; The dense water out of end effect of falling-film evaporator 8 is connected with evaporation pond 12, and the condensation-water drain of each single-effect evaporator of falling-film evaporator 8 is connected with condensation water tank 9, and end effect vapour outlet is connected with condensation water tank 9 through condenser 11.
Wherein, pressure filter 13 adopts plate and frame(type)filter press or centrifugal drier, and condenser 11 adopts recirculated water cooling condensing device, direct current water-cooled condenser, direct air cooled condenser or indirect air cooling condenser; Filtering basin 7 adopt multi-medium filtering pond, sand filter, variable orifice gap filtering basin or fibrous filtering pool; Falling-film evaporator 8 adopts 2 effect ~ 4 to imitate plate-type down-film evaporator or tube-type down-flow evaporators, its single-action heat transfer temperature difference about 2.5 DEG C ~ 3.5 DEG C, the heating steam that the secondary steam of last effect is imitated as next, makes full use of the heat energy in thermal source primary steam; Further, the pH value of Secondary clarifier water outlet of the present utility model controls more than 10, and water inlet and the circulation material liquid pH of falling-film evaporator 8 control more than 10, to reduce silicon-dioxide fouling tendency; Circulation feed liquid herein refers to the circulation feed liquid of every 1st effective evaporator inside, and be heating steam and circulation feed liquid respectively in heat-transfer surface both sides, heating steam condensation becomes time condensation water, and the evaporation of circulation feed liquid part generates secondary steam.
In addition, A reactor 3 of the present utility model and second reactor 5 are divided into rapid reaction zone and slow reaction district, and rapid reaction zone can adopt mechanic whirl-nett reaction or microvovtex aggregation, rapid reaction zone residence time 5min ~ 10min; Slow reaction district adopts large discharge low rate mixing recirculation reactor, slow reaction district residence time 10min ~ 15min; Bottom of clarifier establishes sludge circulation pipe, by sludge circulation pump, active sludge is back to reactor, to promote the carrying out of chemical reaction;
The utility model proposes a kind of thick-oil waste water pre-treatment and evaporative desalination system and method, realized the pro desalting of thick-oil waste water by evaporation technology, reduce the organic content in thick-oil waste water simultaneously; Two-stage chemical reaction clarification pretreatment system is set before vaporizer, effectively removes the silicon-dioxide in thick-oil waste water and hardness, coordinate high temperature Scale inhibitors, avoid the fouling of evaporator heat exchange face, vaporizer long-term stability is run; The dense water of vaporizer discharge, after evaporation pond spontaneous evaporation is disposed, can realize the wastewater zero discharge of process system.And the utility model adopts evaporation technology to make full use of heat energy in high-heat heavy crude waste water, utilize station boiler steam turbine do work after exhaust steam as vaporizer thermal source, improve energy utilization efficiency; Make the thick-oil waste water after pre-treatment avoid fouling in evaporative process, in evaporator condensation water, saltiness and organism significantly reduce, and after follow-up organic matter removal and deep desalting treatment, can be used for station boiler supplementary feed.In addition, the utility model adopts the measures such as flash distillation, multiple-effect falling film evaporation, station boiler turbine low pressure cylinder exhaust steam utilization, effectively utilizes the heat energy in thick-oil waste water, reduces the energy consumption of evaporative process, makes technique have good economy.
Based on thick-oil waste water pre-treatment and the evaporative desalination method of above-mentioned thick-oil waste water pre-treatment and evaporative desalination system, the thick-oil waste water be stored in thick-oil waste water pond 1 after oil removing is delivered in flasher 2 and carries out flash distillation, the flash-off steam that flasher 2 produces delivers to the heat energy that falling-film evaporator 8 is used as the thermal source of the first single-effect evaporator to reclaim wherein, thick-oil waste water after the flash distillation cooling that flasher 2 is discharged delivers to A reactor 3, to A reactor 3, add silica removal medicament a from the first dispensing mouth simultaneously, pH adjusting agent b, flocculation agent c and coagulant aids d, enter primary-clarifiers 4 after thick-oil waste water after flash distillation cooling reacts in A reactor 3 to carry out solid-liquid separation and also to control in the primary-clarifiers water outlet obtained silica concentration lower than 50mg/L, the primary-clarifiers precipitation body refuse part obtained returns in A reactor 3 and participates in chemical reaction as crystal seed, another part is sent in pressure filter 13 and is carried out press filtration process, the filtrate produced after press filtration process returns A reactor 3 and continues process, primary-clarifiers water outlet is sent in second reactor 5, from the second dispensing mouth, in second reactor 5, add sodium carbonate e simultaneously, flocculation agent c and coagulant aids d, primary-clarifiers water outlet enters Secondary clarifier 5 and carries out solid-liquid separation after reacting in second reactor 5, and control Ca in the Secondary clarifier water outlet obtained
2+concentration is lower than 0.1mmol/L, the Secondary clarifier precipitation body refuse part obtained returns in second reactor 5 and participates in chemical reaction as crystal seed, another part is sent in pressure filter 13 and is carried out press filtration process, the filtrate produced after press filtration process returns A reactor 3 and continues process, and the solid sludges outward transport that pressure filter 13 produces after processing I and II settler precipitation body refuse is disposed, Secondary clarifier water outlet control ph after filtering basin 7 filter is more than or equal to 10, and sends in falling-film evaporator 8 and process, and adds efficient scale inhibitor f to control fouling, to reduce the heat-transfer surface scaling rate of falling-film evaporator from the 3rd dosing mouth simultaneously, due to the falling-film evaporator that falling-film evaporator 8 adopts 2 ~ 4 to imitate, therefore, the heating steam that the secondary steam of the last effect of falling-film evaporator of the present utility model is imitated as next, the low pressure (LP) cylinder exhaust steam of the station boiler steam turbine 10 low pressure exhaust steam of discharging provides primary steam (first heating steam) for the Secondary clarifier water outlet entering falling-film evaporator 8, and compare use Steam Turbine Through IP Admission draw gas as the vapo(u)rization system of thermal source, its evaporation energy consumption is low, Secondary clarifier water outlet obtains by the dense water of end effect after falling-film evaporator 8 processes after falling-film evaporator 10 concentrates 20 times ~ 30 times, dense for this end effect water is delivered to evaporation pond 12 with spontaneous evaporation, collect in condensation water tank 9 after the secondary steam that last evaporator produces delivers to condenser 11 condensation, the time condensation Water Sproading of each single-effect evaporator generation of falling-film evaporator 8 is in condensation water tank 9, and control is sent to the saltiness of the water of condensation in condensation water tank 9 lower than 50mg/L, COD is lower than 100mg/L, water of condensation saltiness in condensation water tank and organic concentration significantly reduce, reach thick-oil waste water pro desalting target.Finally all water of condensation collected in condensation water tank 9 are carried out organic matter removal and deep desalting treatment.
Wherein, silica removal medicament a is magnesium chloride, magnesium oxide or magnesium sulfate, and pH adjusting agent b is sodium hydroxide, calcium hydroxide or calcium oxide, and flocculation agent c is polymerize aluminum chloride, bodied ferric sulfate or iron trichloride; Coagulant aids d is polyacrylamide.
The evaporative desalination treatment system of certain oil-field thick-oil waste water, design water quality is in table 1.
Certain oil-field thick-oil waste water quality of table 1
Adopt treatment process of the present utility model, thick-oil waste water after oil removal treatment is stored in thick-oil waste water pond 1, delivers in flasher 2 and carries out flash distillation, flasher import thick-oil waste water temperature 80 DEG C, flash off water temp 63 DEG C, flash-off steam delivers to falling-film evaporator 8 as thermal source, A reactor 3 is delivered in flash distillation water outlet, magnesium chloride is added in A reactor 3, lime (CaO), polymerize aluminum chloride and polyacrylamide, the concentration of magnesium chloride in flash distillation water outlet is made to be 350mg/L, the concentration of lime is 600mg/L, the concentration of polymerize aluminum chloride is 40mg/L, the concentration of polyacrylamide is 0.5mg/L, send in primary-clarifiers 4 through abundant reacted thick-oil waste water and carry out solid-liquid separation, partly precipitated body refuse returns A reactor and does 3 for crystal seed participation chemical reaction, and residue body refuse is delivered to pressure filter 13 and carried out press filtration process, second reactor 5 is sent in the primary-clarifiers water outlet that primary-clarifiers 4 produces, sodium carbonate is added in second reactor 5, polymerize aluminum chloride, polyacrylamide and the concentration controlling sodium carbonate in primary-clarifiers water outlet is 800mg/L, the concentration of polymerize aluminum chloride is 30mg/L, the concentration of polyacrylamide is 0.4mg/L, after fully reacting, send into Secondary clarifier 6 carry out solid-liquid separation, partly precipitated body refuse returns second reactor and participates in chemical reaction as crystal seed, residue body refuse is delivered to pressure filter 13 and is carried out press filtration process, the filtrate that pressure filter 13 produces returns A reactor 3 and continues process, the solid sludges outward transport that pressure filter 13 produces is disposed, the Secondary clarifier water outlet that Secondary clarifier 6 produces is sent in variable orifice gap filtering basin 7 and is filtered, the product water pH value obtained controls more than 10, and this product water is delivered to falling-film evaporator 8, falling-film evaporator 8 uses the board-like vertically moving membrane vaporizer of 2 effect, the primary steam of falling-film evaporator 8 adopts the low pressure exhaust steam of station boiler steam turbine 10 mesolow cylinder discharge, steam parameter is 70 DEG C, 30kPa, the secondary steam that first single-effect evaporator produces, as the heating steam of the second effect, is collected into condensation water tank 9 after the secondary steam of the second single-effect evaporator delivers to direct air cooled condenser condensation, and the water of condensation that first and second single-effect evaporator produces also is collected into condensation water tank 9, in falling-film evaporator 8, add Scale inhibitors control fouling, the dense water that the second single-effect evaporator produces is delivered to evaporation pond 12 spontaneous evaporation and is disposed, water of condensation in condensation water tank 9 can be used for station boiler supplementary feed after delivering to follow-up organic matter removal and the process of deep desalting treatment system.
Implementation result: adopt art breading thick-oil waste water of the present utility model, in vaporizer water inlet, silicon-dioxide is 45mg/L, Ca after pretreatment
2+for 0.05mmol/L; After evaporation process, thick-oil waste water is concentrated into 20 times, and vaporizer is without fouling; Evaporation time condensation water saltiness 40mg/L, COD is 80mg/L, achieves thick-oil waste water evaporation pro desalting, can be used for station boiler supplementary feed after subsequent disposal.
Claims (9)
1. a thick-oil waste water pre-treatment and evaporative desalination system, it is characterized in that: comprise thick-oil waste water pond (1) and the A reactor (3) that is communicated with successively with thick-oil waste water pond (1) and primary-clarifiers (4), and A reactor (3) is provided with the first dispensing mouth for adding silica removal chemical agent; The liquid exit of described primary-clarifiers (4) is connected with Secondary clarifier (6) with second reactor (5) successively, and second reactor (5) is provided with the second dispensing mouth for adding deliming chemical agent; I and II settler (4,6) solid outlet is divided into two-way, one tunnel returns the entrance of A reactor (3) after being connected with pressure filter (13), another road is connected with the entrance of corresponding I and II reactor (3,5); The liquid exit of Secondary clarifier (6) is connected with falling-film evaporator (8), falling-film evaporator (8) with for providing the heat power supply device of thermal source to be connected for the first single-effect evaporator of falling-film evaporator (8), the dense water out of end effect of falling-film evaporator (8) is connected with evaporation pond (12), the condensation-water drain of each single-effect evaporator of falling-film evaporator (8) is connected with condensation water tank (9), and end effect vapour outlet is connected with condensation water tank (9) through condenser (11).
2. thick-oil waste water pre-treatment according to claim 1 and evaporative desalination system, is characterized in that: be provided with flasher (2) between described thick-oil waste water pond (1) and A reactor (3).
3. thick-oil waste water pre-treatment according to claim 2 and evaporative desalination system, it is characterized in that: the vapour outlet of described flasher (2) is connected with the first single-effect evaporator of falling-film evaporator (8), and liquid exit is connected with A reactor (3).
4. thick-oil waste water pre-treatment according to claim 1 and evaporative desalination system, is characterized in that: described pressure filter (13) adopts plate and frame(type)filter press or centrifugal drier.
5. thick-oil waste water pre-treatment according to claim 1 and evaporative desalination system, is characterized in that: be provided with filtering basin (7) between the liquid exit of described Secondary clarifier (6) and falling-film evaporator (8).
6. thick-oil waste water pre-treatment according to claim 5 and evaporative desalination system, is characterized in that: described filtering basin (7) adopt multi-medium filtering pond, sand filter, variable orifice gap filtering basin or fibrous filtering pool.
7. thick-oil waste water pre-treatment according to claim 1 and evaporative desalination system, it is characterized in that: described falling-film evaporator (8) is provided with the 3rd dosing mouth for adding Scale inhibitors, and falling-film evaporator (8) adopts 2 effect ~ 4 effect plate-type down-film evaporator or tube-type down-flow evaporators.
8. thick-oil waste water pre-treatment according to claim 1 and evaporative desalination system, it is characterized in that: described heat power supply device adopts station boiler steam turbine (10), and the low pressure (LP) cylinder exhaust steam outlet of station boiler steam turbine (10) is connected with the first single-effect evaporator of falling-film evaporator (8).
9. thick-oil waste water pre-treatment according to claim 1 and evaporative desalination system, is characterized in that: described condenser (11) adopts recirculated water cooling condensing device, direct current water-cooled condenser, direct air cooled condenser or indirect air cooling condenser.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104176870A (en) * | 2014-08-25 | 2014-12-03 | 西安热工研究院有限公司 | Viscous oil wastewater pretreatment and evaporation desalting system and method |
| CN110131702A (en) * | 2019-06-13 | 2019-08-16 | 西安西热水务环保有限公司 | A kind of wet slag removing system pulp water cyclic utilization system and method |
| CN111410351A (en) * | 2019-01-07 | 2020-07-14 | 湖南军信环保股份有限公司 | Method for treating high-salinity wastewater |
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2014
- 2014-08-25 CN CN201420481135.XU patent/CN204039202U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104176870A (en) * | 2014-08-25 | 2014-12-03 | 西安热工研究院有限公司 | Viscous oil wastewater pretreatment and evaporation desalting system and method |
| CN104176870B (en) * | 2014-08-25 | 2016-06-15 | 西安热工研究院有限公司 | A kind of thick-oil waste water pre-treatment and evaporative desalination system and method |
| CN111410351A (en) * | 2019-01-07 | 2020-07-14 | 湖南军信环保股份有限公司 | Method for treating high-salinity wastewater |
| CN111410351B (en) * | 2019-01-07 | 2022-05-31 | 湖南军信环保股份有限公司 | Method for treating high-salinity wastewater |
| CN110131702A (en) * | 2019-06-13 | 2019-08-16 | 西安西热水务环保有限公司 | A kind of wet slag removing system pulp water cyclic utilization system and method |
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