CA2911135A1 - Process for treatment of high contaminated waters - Google Patents
Process for treatment of high contaminated waters Download PDFInfo
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- CA2911135A1 CA2911135A1 CA2911135A CA2911135A CA2911135A1 CA 2911135 A1 CA2911135 A1 CA 2911135A1 CA 2911135 A CA2911135 A CA 2911135A CA 2911135 A CA2911135 A CA 2911135A CA 2911135 A1 CA2911135 A1 CA 2911135A1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
- B01D1/289—Compressor features (e.g. constructions, details, cooling, lubrication, driving systems)
- B01D1/2893—Driving systems
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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
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- 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
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
A process is invented for treating contaminated water from natural sources i.e sea, lake, river, well, etc and contaminated wastewaters produced from industrial and oil & gas operations. The process is based on three selected relevant kind and types of membranes followed by evaporation and desalination technologies. The contaminated water is passed through a pretreatment system and thereafter through the selected membranes, to remove and reduce the amount of contaminations; thereby the maximum possible amount of reusable water is recovered. For producing potable water, a Nano filtration system is also essential to be incorporated. The from the membrane process rejected concentrate, containing much higher amount of contaminants is then processed further by using evaporation and distillation technologies. The total recovered and cleaned water from this new process is exceeding 90 % of the total contaminated water and wastewaters processed.
The main advantages of this process The main advantages of this process are a- By using membrane technology with high throughput but low capital and operating costs, high volumes of contaminated water can be treated;
b- The distillation technology, with high facility and operating costs, is used for relatively low amounts of concentrate, remaining from membrane systems, c- With using UF, NF, RO and distillation technologies combined, much higher volumes of reusable water, can be produced.
d- With using UF, NF, RO and distillation technologies combined makes the recovery of high volumes of reusable water much more economical;
e- The amount of final rejected concentrate is low; therefore the high storage cost for the said concentrate is accordingly low.
f- The process can be used for treating contaminated wastewaters produced from industrial and oil & gas operations and for production of potable water from different sources as well.
The main advantages of this process The main advantages of this process are a- By using membrane technology with high throughput but low capital and operating costs, high volumes of contaminated water can be treated;
b- The distillation technology, with high facility and operating costs, is used for relatively low amounts of concentrate, remaining from membrane systems, c- With using UF, NF, RO and distillation technologies combined, much higher volumes of reusable water, can be produced.
d- With using UF, NF, RO and distillation technologies combined makes the recovery of high volumes of reusable water much more economical;
e- The amount of final rejected concentrate is low; therefore the high storage cost for the said concentrate is accordingly low.
f- The process can be used for treating contaminated wastewaters produced from industrial and oil & gas operations and for production of potable water from different sources as well.
Description
Description High amounts of different wastewaters are produced from industrial and oil &
gas operations every day. For example, the amount of different wastewaters, generated from Steam Assisted Gravity Drainage (SAGD) by oil & gas production, is in some cases thousands of cubic meters by each operation per day. With regulatory restrictions for controlling the usage of water, especially in industrial and oil & gas operations, the wastewater must be treated and reused.
Also in the areas with water shortage, saving water is necessary. Therefore the wastewater must be treated on required quality for reuse. Water from natural sources such as sea, lake, river, well, etc. used for production of potable water must be cleaned to required standards prior to utilization. The industrial and also the oil & gas wastewaters must be treated, by removing the unwanted substances, to meet the requirements for reuse. By conventional methods for water treatment, different technologies are used. The most methods used are membrane technologies and distillation processes.
The membrane technologies are effective to recover useable water but the treatment is restricted by the amounts of contaminants and the recovery is maximum up to around 70 % of contaminated water. Their facility cost and the operating expensed are relatively low.
The distillation processes can treat different contaminated waters containing high amounts of contaminants and recover higher amount of clean water;
maximum up to around 85 % of the contaminated water used. But their facility cost and operating expenses are quite high.
The New Invention The new invention is a process based on:
a. Pretreatment system;
b. Ultra filtration technology;
c. Nano filtration technology;
d. Reverse osmosis filtration technology;
e. Vacuum Evaporation/distillation technologies;
f. Thermal Vapour Compression;
g. Mechanical Vapour Compression.
Pretreatment system Pretreatment system is used as water softener and includes also Induced Gas Flotation (IGF), walnut shells filtration, etc. for removal of large particles, silica, oils, etc. In most cases, if the amount of contaminants in feed water exceeds i.e. 100 ppb total oil and grease, 3 ppm TOC, 20 ppm TSS, 50 NTU turbidity then a pretreatment of the feed water is necessary.
Ultra Filtration (UF):
UF is used for removal of the remaining entrained oils, suspended solids, bacteria, algae and some soluble organic species, etc. The UF membranes have a nominal pore size of 0.04 micron and with using nominal pressure between 2 to 4 bar (30 to 60 psi), silica in colloidal form and materials greater than 50,000 molecular-weights can be removed.
Feed water temperature must be maintained at manufacturers' requirements since high temperatures damage and reduce the life of the membranes.
Therefore a cooling tower or heat exchangers is needed to assure the right feed water temperature is maintained. Another alternative is using high
gas operations every day. For example, the amount of different wastewaters, generated from Steam Assisted Gravity Drainage (SAGD) by oil & gas production, is in some cases thousands of cubic meters by each operation per day. With regulatory restrictions for controlling the usage of water, especially in industrial and oil & gas operations, the wastewater must be treated and reused.
Also in the areas with water shortage, saving water is necessary. Therefore the wastewater must be treated on required quality for reuse. Water from natural sources such as sea, lake, river, well, etc. used for production of potable water must be cleaned to required standards prior to utilization. The industrial and also the oil & gas wastewaters must be treated, by removing the unwanted substances, to meet the requirements for reuse. By conventional methods for water treatment, different technologies are used. The most methods used are membrane technologies and distillation processes.
The membrane technologies are effective to recover useable water but the treatment is restricted by the amounts of contaminants and the recovery is maximum up to around 70 % of contaminated water. Their facility cost and the operating expensed are relatively low.
The distillation processes can treat different contaminated waters containing high amounts of contaminants and recover higher amount of clean water;
maximum up to around 85 % of the contaminated water used. But their facility cost and operating expenses are quite high.
The New Invention The new invention is a process based on:
a. Pretreatment system;
b. Ultra filtration technology;
c. Nano filtration technology;
d. Reverse osmosis filtration technology;
e. Vacuum Evaporation/distillation technologies;
f. Thermal Vapour Compression;
g. Mechanical Vapour Compression.
Pretreatment system Pretreatment system is used as water softener and includes also Induced Gas Flotation (IGF), walnut shells filtration, etc. for removal of large particles, silica, oils, etc. In most cases, if the amount of contaminants in feed water exceeds i.e. 100 ppb total oil and grease, 3 ppm TOC, 20 ppm TSS, 50 NTU turbidity then a pretreatment of the feed water is necessary.
Ultra Filtration (UF):
UF is used for removal of the remaining entrained oils, suspended solids, bacteria, algae and some soluble organic species, etc. The UF membranes have a nominal pore size of 0.04 micron and with using nominal pressure between 2 to 4 bar (30 to 60 psi), silica in colloidal form and materials greater than 50,000 molecular-weights can be removed.
Feed water temperature must be maintained at manufacturers' requirements since high temperatures damage and reduce the life of the membranes.
Therefore a cooling tower or heat exchangers is needed to assure the right feed water temperature is maintained. Another alternative is using high
2 , temperature resistant membranes, which increase the amount of the facility cost.
Nano Membrane Technology:
Nano filtration (NF) technology is a relatively recent development and has greater selectivity of ions. Nano membranes have great resistance to fouling, a high degree of selectivity and physical durability which is needed for industrial wastewater treatment. Nano filtration is used for removal of natural organics, pesticide, hardness, sulfates, desalting, etc. Nano membranes are also used for hardness removal in place of water softeners. For potable water production, NF is essential to be incorporated in the new invented process.
Reverse Osmosis Technology:
Reverse osmosis filtration has been used for decades for water treatment especially for potable water production. RO membranes are capable of rejecting practically all particles, bacteria and organics > 200 Dalton molecular weight (including pyrogens). Only solvent (i.e., water molecules) can pass through the semi-permeable RO membrane. All ions and dissolved molecules, including salts, effluent materials and organic molecules such as sugars, are retained in the rejected concentrate.
The NF and RO membrane systems can remove around 99 % of all unwanted substances including salts and metal ions. Therefore, a combination of the two technologies is essential in critical cases i.e. for producing potable water.
The treated water will be suitable for direct reuse.
Evaporation/distillation Technologies:
Evaporation and distillation technologies are one of the oldest methods used for removal of unwanted particles and contaminants from natural source waters and also from wastewaters produced from industrial and oil & gas operations.
Nano Membrane Technology:
Nano filtration (NF) technology is a relatively recent development and has greater selectivity of ions. Nano membranes have great resistance to fouling, a high degree of selectivity and physical durability which is needed for industrial wastewater treatment. Nano filtration is used for removal of natural organics, pesticide, hardness, sulfates, desalting, etc. Nano membranes are also used for hardness removal in place of water softeners. For potable water production, NF is essential to be incorporated in the new invented process.
Reverse Osmosis Technology:
Reverse osmosis filtration has been used for decades for water treatment especially for potable water production. RO membranes are capable of rejecting practically all particles, bacteria and organics > 200 Dalton molecular weight (including pyrogens). Only solvent (i.e., water molecules) can pass through the semi-permeable RO membrane. All ions and dissolved molecules, including salts, effluent materials and organic molecules such as sugars, are retained in the rejected concentrate.
The NF and RO membrane systems can remove around 99 % of all unwanted substances including salts and metal ions. Therefore, a combination of the two technologies is essential in critical cases i.e. for producing potable water.
The treated water will be suitable for direct reuse.
Evaporation/distillation Technologies:
Evaporation and distillation technologies are one of the oldest methods used for removal of unwanted particles and contaminants from natural source waters and also from wastewaters produced from industrial and oil & gas operations.
3 = Water is first heated to the boiling point for producing vapor followed by a cooling process. The water vapor is passed through a condenser where the vapor is condensed to water and collected for reuse. Most of the containing materials remain behind in the boiling vessel solution. However, inorganic materials such as silica, sodium, tin, copper, etc. can migrate and must be controlled.
Organics with boiling points lower than 100 C will automatically be transferred to the distillate, and even organics with a boiling point over 100 C can dissolve in water vapor and pass into the distillate. Distillation is a slow process and requires large amounts of energy. This process requires regular cleaning of the boiling vessel as well. The waste concentrate, from the distillation process, is then rejected while the clean water is stored for reuse. Although the principals of the distillation procedures are simple, the cost for the facility is quite considerable. Also the operating expenses, due to high energy consumption, are relatively high. Considering that natural gas cannot be always available, especially in remote areas, the energy costs will be even more expensive. The Distillation technology, producing high quality of clean water, is more suitable for the production of potable water.
Vacuum Evaporation technology:
Vacuum Evaporation technology is a further development of the conventional, evaporation technology described above. The major difference is crating vacuum in the boiler vessel and thereby reducing the boiling temperature of water. A portion of the solution, in the boiler vessel, is discharged by a vacuum pump creating vacuum in the vessel. By reducing the boiling temperature of water, causes reduction of energy consumption and thereby less energy costs by this process.
Organics with boiling points lower than 100 C will automatically be transferred to the distillate, and even organics with a boiling point over 100 C can dissolve in water vapor and pass into the distillate. Distillation is a slow process and requires large amounts of energy. This process requires regular cleaning of the boiling vessel as well. The waste concentrate, from the distillation process, is then rejected while the clean water is stored for reuse. Although the principals of the distillation procedures are simple, the cost for the facility is quite considerable. Also the operating expenses, due to high energy consumption, are relatively high. Considering that natural gas cannot be always available, especially in remote areas, the energy costs will be even more expensive. The Distillation technology, producing high quality of clean water, is more suitable for the production of potable water.
Vacuum Evaporation technology:
Vacuum Evaporation technology is a further development of the conventional, evaporation technology described above. The major difference is crating vacuum in the boiler vessel and thereby reducing the boiling temperature of water. A portion of the solution, in the boiler vessel, is discharged by a vacuum pump creating vacuum in the vessel. By reducing the boiling temperature of water, causes reduction of energy consumption and thereby less energy costs by this process.
4 = Additional Equipment:
For reducing energy consumption and/or producing additional amountsw of steam needed by oil & gas operations, additional technologies, such as Thermal Vapour Recompression (TVR) and Mechanical Vapour Recompression (MVT) technologies are used as well.
Thermal Vapour Compression (TVC) For boiling contaminated slurry in distillation process high pressure steam is used. By using TVC, high pressure steam is mixed with low pressure excess steam, from oil & gas operations, for heating the slurry in the evaporation vessel and thereby saving high pressure steam. Average amount of steam used for producing 3 kg vapor, by conventional distillation, is without TVC 0.45 kg while with using TVC is 0.23 kg.
Mechanical Vapour Compression (MVC) The thermal TEC, described above, can be replaced by MVC system which is mostly used where high pressure steam is not available. The compressors used are:
Turbo compressors, (axial; single and multi-stage);
Radial (single and multi-stage);
iii. High pressure Fans;
iv. Piston types and Roots compressors.
For reducing energy consumption and/or producing additional amountsw of steam needed by oil & gas operations, additional technologies, such as Thermal Vapour Recompression (TVR) and Mechanical Vapour Recompression (MVT) technologies are used as well.
Thermal Vapour Compression (TVC) For boiling contaminated slurry in distillation process high pressure steam is used. By using TVC, high pressure steam is mixed with low pressure excess steam, from oil & gas operations, for heating the slurry in the evaporation vessel and thereby saving high pressure steam. Average amount of steam used for producing 3 kg vapor, by conventional distillation, is without TVC 0.45 kg while with using TVC is 0.23 kg.
Mechanical Vapour Compression (MVC) The thermal TEC, described above, can be replaced by MVC system which is mostly used where high pressure steam is not available. The compressors used are:
Turbo compressors, (axial; single and multi-stage);
Radial (single and multi-stage);
iii. High pressure Fans;
iv. Piston types and Roots compressors.
5 Referrals and Abbreviations (Alphabetical):
- Contaminated water from natural sources i.e. sea, lake, river, well, etc.
referred to as contaminated waters;
- Contaminated wastewaters produced from industrial and oil & gas operations referred to as contaminated wastewaters.
- BWS: Back Wash Slurry;
- CIP: Clean in Place;
- DSP: Discharge Slurry Pump;
- DVP discharge vacuum pump;
- DWP: Discharge Water Pump;
- EHE: Effect Heat Exchanger;
- FVVT: Feed Water Tank;
- FWP: Feed Water Pump;
- IGF Induced Gas Flotation;
- MFW: Main Feed Water;
- MVC: Mechanical Vapour Compression;
- NF: Nano Filtration;
- NFS: Nano Filtration System;
- ORF Oil Removal Flotation;
- OTSG: Once Through Steam Generator;
- PTS: Pre Treatment system;
- RC: Rejected Concentrate;
- RCT: Reject Concentrate Tank;
- RO: Reverse Osmosis;
- ROS: Reverse Osmosis System;
- SCS: Steam Condenser System;
- TVC: Thermo Vapour Compression;
- UF: Ultra Filtration;
- UFS: Ultra Filtration System;
- VES: Vacuum Evaporation System;
The System of the Invention The System of the Invention consists of:
a. Pretreatment system 2;
b. Discharge water pump 4 for storage tank 5;
c. Storage tank 5 as feed water tank for UF system 8;
d. Discharge water pump 7 for discharging the water from storage tank 5 into UF system 8;
e. UF system 8;
f. Clean in Place (CIP) 9 for UF system 8;
g. Slurry pump 11 for discharge of Backwash wastewater from UF system into PTU system 2;
h. Discharge water pump 14 for discharge of treated water from UF system 8 into storage tank 15 as feed water tank for NF system 18;
i. Feed water pump 17 for discharge of the said treated water from storage tank 15 into NF system 18;
j. NF system 18;
k. Slurry pump 23 for discharge of rejected concentrate from NF system 8 into the concentrate storage tank 24;
I. Clean in place (CIP) 19 for NF system 18;
m. Slurry pump 21 for discharge of backwash wastewater from NF system into NF system feed water tank 15;
n. Discharge water pump 28 for discharge of treated water from NF system 18 into storage tank 27 as RO system feed water tank;
o. Feed water pump 28 for discharge of treated water from storage tank 27 into RO system;
p. RO system 30;
q. CIP 31 for RO system 30;
r. Discharge slurry pump 33 for discharge of backwash wastewater into RO system feed water tank 27;
s. Slurry pump 36 for discharge of rejected concentrate from RO system 30 into concentrate storage tank 24;
t. Discharge water pump 38 for discharge of recovered clean water into storage tank 40 for reuse (i.e. as OTSG feed water tank);
u. Slurry pump 42 for discharge of rejected concentrate from RCT tank into vacuum evaporation system 43;
v. Vacuum evaporation system 43;
w. Vacuum slurry pump 46;
x. Steam condenser 50;
y. Thermal Vapour Compression (TV) system 60;
z. Heat exchanger effects 61 for providing heat into vapor boiler 43;
Process Description The contaminated main feed water (MFW) 1 is discharged into a conventional pre-treatment system (PTS) 2 which also includes Induced Gas Flotation (IGF) with or without walnut shells, for removal of oils, silica and large particle solids, etc. The pre-treated water 3 is then discharged, via discharge water pump (DWP) 4, into the storage tank 5 as feed water tank for ultra filtration system (UFS) 8. The UFS feed water 6 from UFS feed water tank 5 is then discharged, via feed water pump 7, into UFS 8 for further treatment. The Back Wash wastewater 10, along with waste water from UFS-CIP 9, is returned, via slurry pump 11, to PTS for reprocessing.
The rejected slurry, from UFS is discharged, via slurry pump 12, into the UFS feed water tank 5 for reprocessing. The, in UFS 8 treated water stream 13, is then discharged, via discharge water pump 14, into storage tank 15 as feed water tank for NFS 18. The, by UFS 8 treated water, in storage tank 15, is used as feed water for NFS 18. The feed water stream 16 from storage tank 15 is then discharged , via feed water pump 17, into the NFS 18, to be treated further. The by NFS 18 treated water stream 25 is discharged, via discharge water pump 26, into storage tank 27 as feed water tank for ROS 30. The back wash and wastewater slurry 20 from CIP
19 of NFS 18, is discharged, via discharge slurry pump 21, into NFS feed water tank 15 for reprocessing. The rejected concentrate slurry 22 from NFS
is discharged, via discharge slurry pump 23, into reject concentrate tank 24.
The, by NFS treated water from ROS feed water tank 27 is discharged 29, via feed water pump 28, into ROS 30 for final treatment. The cleaned water st5ream 37 from ROS 30 is then discharged 39, via discharge water pump 38 into storage tank 40 for reuse (i.e. for "Once Through Steam Generator"
= OTSG). The rejected concentrate slurry 35, from ROS 30, is discharged, via discharge slurry pump 36, into the reject-concentrate tank (RCT) 24 as feed slurry tank for vacuum evaporation system (VES) 43. The rejected concentrate stream 41, from RCT, is then discharged, via feed slurry pump 42, into the said VES vessel 43. A portion of the slurry 44, collected in the VES vessel, is discharged 47 via vacuum discharge pump 46 to create vacuum in the said vessel and thereby reducing the water boiling temperature. The slurry 44, collected in VES is then heated and most of the water containing in the said slurry 44 will be evaporated 48 and collected on top of the VES vessel. The vapor from VES 43 is then injected into steam condenser system (SCS) 50 to be discharged as distilled water 53 for reuse.
Cooling water 51 is passed through the SCS as cooling aggregate and then is discharged 52. The final waste concentrate 47 from VES 43 is discharged, via discharge vacuum slurry pump 46, for disposal and thereby creating vacuum in the vessel 43 for reducing the boiling temperature and saving energy consumption.
To make the process more economical, a "Thermo Vapour Compression"
(TVC) 60 is used. High pressure steam 54 is passed, through the TVS 60 and at the same time low pressure excessive steam 55 is injected into the low pressure steam-chamber 56 of TVC 60. Through venture effect the high pressure steam 54 and the low pressure steam 55 are mixed in the mixing chamber 58. The steam mixture 59 is passed, through the heat exchanger effects 61 for heating the slurry 44 in the VES vessel 43, and then is discharged 62 for recirculation.
- Contaminated water from natural sources i.e. sea, lake, river, well, etc.
referred to as contaminated waters;
- Contaminated wastewaters produced from industrial and oil & gas operations referred to as contaminated wastewaters.
- BWS: Back Wash Slurry;
- CIP: Clean in Place;
- DSP: Discharge Slurry Pump;
- DVP discharge vacuum pump;
- DWP: Discharge Water Pump;
- EHE: Effect Heat Exchanger;
- FVVT: Feed Water Tank;
- FWP: Feed Water Pump;
- IGF Induced Gas Flotation;
- MFW: Main Feed Water;
- MVC: Mechanical Vapour Compression;
- NF: Nano Filtration;
- NFS: Nano Filtration System;
- ORF Oil Removal Flotation;
- OTSG: Once Through Steam Generator;
- PTS: Pre Treatment system;
- RC: Rejected Concentrate;
- RCT: Reject Concentrate Tank;
- RO: Reverse Osmosis;
- ROS: Reverse Osmosis System;
- SCS: Steam Condenser System;
- TVC: Thermo Vapour Compression;
- UF: Ultra Filtration;
- UFS: Ultra Filtration System;
- VES: Vacuum Evaporation System;
The System of the Invention The System of the Invention consists of:
a. Pretreatment system 2;
b. Discharge water pump 4 for storage tank 5;
c. Storage tank 5 as feed water tank for UF system 8;
d. Discharge water pump 7 for discharging the water from storage tank 5 into UF system 8;
e. UF system 8;
f. Clean in Place (CIP) 9 for UF system 8;
g. Slurry pump 11 for discharge of Backwash wastewater from UF system into PTU system 2;
h. Discharge water pump 14 for discharge of treated water from UF system 8 into storage tank 15 as feed water tank for NF system 18;
i. Feed water pump 17 for discharge of the said treated water from storage tank 15 into NF system 18;
j. NF system 18;
k. Slurry pump 23 for discharge of rejected concentrate from NF system 8 into the concentrate storage tank 24;
I. Clean in place (CIP) 19 for NF system 18;
m. Slurry pump 21 for discharge of backwash wastewater from NF system into NF system feed water tank 15;
n. Discharge water pump 28 for discharge of treated water from NF system 18 into storage tank 27 as RO system feed water tank;
o. Feed water pump 28 for discharge of treated water from storage tank 27 into RO system;
p. RO system 30;
q. CIP 31 for RO system 30;
r. Discharge slurry pump 33 for discharge of backwash wastewater into RO system feed water tank 27;
s. Slurry pump 36 for discharge of rejected concentrate from RO system 30 into concentrate storage tank 24;
t. Discharge water pump 38 for discharge of recovered clean water into storage tank 40 for reuse (i.e. as OTSG feed water tank);
u. Slurry pump 42 for discharge of rejected concentrate from RCT tank into vacuum evaporation system 43;
v. Vacuum evaporation system 43;
w. Vacuum slurry pump 46;
x. Steam condenser 50;
y. Thermal Vapour Compression (TV) system 60;
z. Heat exchanger effects 61 for providing heat into vapor boiler 43;
Process Description The contaminated main feed water (MFW) 1 is discharged into a conventional pre-treatment system (PTS) 2 which also includes Induced Gas Flotation (IGF) with or without walnut shells, for removal of oils, silica and large particle solids, etc. The pre-treated water 3 is then discharged, via discharge water pump (DWP) 4, into the storage tank 5 as feed water tank for ultra filtration system (UFS) 8. The UFS feed water 6 from UFS feed water tank 5 is then discharged, via feed water pump 7, into UFS 8 for further treatment. The Back Wash wastewater 10, along with waste water from UFS-CIP 9, is returned, via slurry pump 11, to PTS for reprocessing.
The rejected slurry, from UFS is discharged, via slurry pump 12, into the UFS feed water tank 5 for reprocessing. The, in UFS 8 treated water stream 13, is then discharged, via discharge water pump 14, into storage tank 15 as feed water tank for NFS 18. The, by UFS 8 treated water, in storage tank 15, is used as feed water for NFS 18. The feed water stream 16 from storage tank 15 is then discharged , via feed water pump 17, into the NFS 18, to be treated further. The by NFS 18 treated water stream 25 is discharged, via discharge water pump 26, into storage tank 27 as feed water tank for ROS 30. The back wash and wastewater slurry 20 from CIP
19 of NFS 18, is discharged, via discharge slurry pump 21, into NFS feed water tank 15 for reprocessing. The rejected concentrate slurry 22 from NFS
is discharged, via discharge slurry pump 23, into reject concentrate tank 24.
The, by NFS treated water from ROS feed water tank 27 is discharged 29, via feed water pump 28, into ROS 30 for final treatment. The cleaned water st5ream 37 from ROS 30 is then discharged 39, via discharge water pump 38 into storage tank 40 for reuse (i.e. for "Once Through Steam Generator"
= OTSG). The rejected concentrate slurry 35, from ROS 30, is discharged, via discharge slurry pump 36, into the reject-concentrate tank (RCT) 24 as feed slurry tank for vacuum evaporation system (VES) 43. The rejected concentrate stream 41, from RCT, is then discharged, via feed slurry pump 42, into the said VES vessel 43. A portion of the slurry 44, collected in the VES vessel, is discharged 47 via vacuum discharge pump 46 to create vacuum in the said vessel and thereby reducing the water boiling temperature. The slurry 44, collected in VES is then heated and most of the water containing in the said slurry 44 will be evaporated 48 and collected on top of the VES vessel. The vapor from VES 43 is then injected into steam condenser system (SCS) 50 to be discharged as distilled water 53 for reuse.
Cooling water 51 is passed through the SCS as cooling aggregate and then is discharged 52. The final waste concentrate 47 from VES 43 is discharged, via discharge vacuum slurry pump 46, for disposal and thereby creating vacuum in the vessel 43 for reducing the boiling temperature and saving energy consumption.
To make the process more economical, a "Thermo Vapour Compression"
(TVC) 60 is used. High pressure steam 54 is passed, through the TVS 60 and at the same time low pressure excessive steam 55 is injected into the low pressure steam-chamber 56 of TVC 60. Through venture effect the high pressure steam 54 and the low pressure steam 55 are mixed in the mixing chamber 58. The steam mixture 59 is passed, through the heat exchanger effects 61 for heating the slurry 44 in the VES vessel 43, and then is discharged 62 for recirculation.
Claims (10)
PROPERTY OR PRIVILAGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1- A process for treating and thereby removing the unwanted materials and substances from contaminated waters, generated from natural sources such as sea, lake, river, well, etc. and wastewaters produced from industrial and oil and gas operations, comprising the steps of:
A- providing a pretreatment system (PTS) having specifications, according to the description of the invention for initial treatment, consisting of:
a. a conventional pretreatment unit for removal of oil, large particulates, silica, etc;
b. a water tank for storage of pretreated water and as feed water tank for UF system;
c. a water pump for discharge of the pre treated water into the UF feed water tank;
B- providing an ultra filtration system (UFS) having specifications, according to the description of the invention, for removal of remaining entrained oils, solids, suspended solids, bacteria, algae and soluble organic species, etc. consisting of:
a. an UF membrane unit for further treatment of the pretreated water produced from the said pre treatment system;
b. a storage tank for permeate produced by UF membranes and also used as a feed water tank for NF system;
c. a feed water pump for discharge of UF feed water, from UF
feed water tank into the said UF membrane unit;
d. a clean in place (CIP) for the UF system;
e. a discharge slurry pump for discharge of backwash and wastewater from UF system into pretreatment system for recycling;
f. a discharge slurry pump for discharge of rejected concentrate, produced by UF membranes, into the said UF feed water tank for recycling;
C- providing a nano filtration system having specifications according to the description of the invention, for removal of natural organics, pesticides, hardness, sulfates, desalting, hardness etc. from permeate produced by ultra filtration; consisting of:
a. a nano membrane unit for treatment of permeate produced from the said ultra filtration;
b. a storage tank for permeate produced by nano membranes and also used as feed water tank for RO system;
c. a feed water pump for discharge of UF permeate from NF feed water tank, into the said NF membrane unit;
d. a CIP for NF system;
e. a discharge slurry pump for discharge of backwash and wastewater from NF system into NF feed water tank for recycling;
f. a discharge slurry pump for discharge of rejected concentrate, produced by NF membranes, into a storage tank as a feed slurry tank for further treatment by distillation process.
D- providing a reverse osmosis RO filtration system, having specifications according to the description of the invention, for removal of particles, bacteria, organics > 200 Dalton molecular weight (including pyrogens), and all ions and dissolved molecules, including salts, effluent materials and organic molecules such as sugars, etc., consisting of:
a. an RO membrane unit for treatment of permeate produced from the said NF filtration;
b. a storage water tank for clean water produced by RO
membranes and also used as reusable water tank c. a feed water pump for discharge of NF permeate from NF feed water tank, into the said RO membrane unit;
d. a CIP for RO system;
e. a slurry pump for discharge of backwash and wastewater from RO system into RO system feed water tank for recycling;
f. a discharge slurry pump for discharge of rejected concentrate, produced by RO membranes, into a storage tank as a distillation system feed tank for further treatment by distillation process.
E- providing a vacuum evaporation system according to the specifications, indicated in the description of the invention for separation of water from unwanted particles and substances, contained in the rejected concentrate generated from membrane processes; consisting of:
a. a vacuum vaporation vessel for boiling the said rejected concentrate from said distillation system feed tank ;
b. a slurry pump for discharge the slurry from rejected concentrate tank into distillation boiling vessel;
c. a thermal vapour compression (TVC), according to the description of the invention, for mixing high and low pressure steam and passing the said steam mixture into a heat exchanger located in the boiler vessel;
d. a heat exchanger according to the description of the invention, for heating the rejected slurry in the said boiling vessel;
e. a slurry vacuum pump for discharge of final remaining concentrate and at the same time creating vacuum in the boiler vessel, thereby reducing the boiling temperature and saving energy consumption;
f. a condenser, according to the description of the invention, for cooling the vapor from the said boiling vessel and thereby producing clean water for reuse;
g. a mechanical vapour compression for replacing the said TVC
in cases that high pressure steam is not available.
A- providing a pretreatment system (PTS) having specifications, according to the description of the invention for initial treatment, consisting of:
a. a conventional pretreatment unit for removal of oil, large particulates, silica, etc;
b. a water tank for storage of pretreated water and as feed water tank for UF system;
c. a water pump for discharge of the pre treated water into the UF feed water tank;
B- providing an ultra filtration system (UFS) having specifications, according to the description of the invention, for removal of remaining entrained oils, solids, suspended solids, bacteria, algae and soluble organic species, etc. consisting of:
a. an UF membrane unit for further treatment of the pretreated water produced from the said pre treatment system;
b. a storage tank for permeate produced by UF membranes and also used as a feed water tank for NF system;
c. a feed water pump for discharge of UF feed water, from UF
feed water tank into the said UF membrane unit;
d. a clean in place (CIP) for the UF system;
e. a discharge slurry pump for discharge of backwash and wastewater from UF system into pretreatment system for recycling;
f. a discharge slurry pump for discharge of rejected concentrate, produced by UF membranes, into the said UF feed water tank for recycling;
C- providing a nano filtration system having specifications according to the description of the invention, for removal of natural organics, pesticides, hardness, sulfates, desalting, hardness etc. from permeate produced by ultra filtration; consisting of:
a. a nano membrane unit for treatment of permeate produced from the said ultra filtration;
b. a storage tank for permeate produced by nano membranes and also used as feed water tank for RO system;
c. a feed water pump for discharge of UF permeate from NF feed water tank, into the said NF membrane unit;
d. a CIP for NF system;
e. a discharge slurry pump for discharge of backwash and wastewater from NF system into NF feed water tank for recycling;
f. a discharge slurry pump for discharge of rejected concentrate, produced by NF membranes, into a storage tank as a feed slurry tank for further treatment by distillation process.
D- providing a reverse osmosis RO filtration system, having specifications according to the description of the invention, for removal of particles, bacteria, organics > 200 Dalton molecular weight (including pyrogens), and all ions and dissolved molecules, including salts, effluent materials and organic molecules such as sugars, etc., consisting of:
a. an RO membrane unit for treatment of permeate produced from the said NF filtration;
b. a storage water tank for clean water produced by RO
membranes and also used as reusable water tank c. a feed water pump for discharge of NF permeate from NF feed water tank, into the said RO membrane unit;
d. a CIP for RO system;
e. a slurry pump for discharge of backwash and wastewater from RO system into RO system feed water tank for recycling;
f. a discharge slurry pump for discharge of rejected concentrate, produced by RO membranes, into a storage tank as a distillation system feed tank for further treatment by distillation process.
E- providing a vacuum evaporation system according to the specifications, indicated in the description of the invention for separation of water from unwanted particles and substances, contained in the rejected concentrate generated from membrane processes; consisting of:
a. a vacuum vaporation vessel for boiling the said rejected concentrate from said distillation system feed tank ;
b. a slurry pump for discharge the slurry from rejected concentrate tank into distillation boiling vessel;
c. a thermal vapour compression (TVC), according to the description of the invention, for mixing high and low pressure steam and passing the said steam mixture into a heat exchanger located in the boiler vessel;
d. a heat exchanger according to the description of the invention, for heating the rejected slurry in the said boiling vessel;
e. a slurry vacuum pump for discharge of final remaining concentrate and at the same time creating vacuum in the boiler vessel, thereby reducing the boiling temperature and saving energy consumption;
f. a condenser, according to the description of the invention, for cooling the vapor from the said boiling vessel and thereby producing clean water for reuse;
g. a mechanical vapour compression for replacing the said TVC
in cases that high pressure steam is not available.
2- A process according to claim 1 that one or more other additional systems and/or equipment are incorporated;
3- A process according to claim 1 wherein one or more of PTS , UFS, NFS, ROS, VES, and TVC are modified;
4- A process according to claim 1 that one or more of Pretreatment -, UF-, NF-, RO-, Distillation-, and thermal vapour recompression-systems are eliminated;
5- A process, according to claim 1 wherein pretreatment system, UFS
system, NF system, RO system and distillation system are combined for other purposes than water treatment;
system, NF system, RO system and distillation system are combined for other purposes than water treatment;
6- A process, according to claim 1, wherein conventional pretreatment system is modified or replaced by a new version of pretreatment system;
7- A process, according to claim 1, wherein another evaporation method, technology, and/or system is used,
8- A process, according to claim 1, wherein another heating material for evaporation purposes is used;
9- A process, according to claim 1, wherein another cooling material is used for cooling the vapor in place of water;
10- A process, according to claim 1, wherein thermal vapour recompression is replaced with mechanical vapor recompression;
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA2911135A CA2911135A1 (en) | 2015-11-04 | 2015-11-04 | Process for treatment of high contaminated waters |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA2911135A CA2911135A1 (en) | 2015-11-04 | 2015-11-04 | Process for treatment of high contaminated waters |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2911135A1 true CA2911135A1 (en) | 2017-05-04 |
Family
ID=58646025
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2911135A Abandoned CA2911135A1 (en) | 2015-11-04 | 2015-11-04 | Process for treatment of high contaminated waters |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107217709A (en) * | 2017-07-19 | 2017-09-29 | 六安合益智能家居科技有限公司 | A kind of purifier handled applied to floor wastewater |
| CN110590041A (en) * | 2019-09-30 | 2019-12-20 | 大唐郓城发电有限公司 | Method for treating desulfurization wastewater |
| CN111051253A (en) * | 2017-09-12 | 2020-04-21 | 奥加诺株式会社 | Apparatus and method for treating silica-containing water |
| CN111533308A (en) * | 2020-05-09 | 2020-08-14 | 江苏澳特克环境科技有限公司 | Water treatment process for emulsifying and cooling mixed wastewater liquid |
| CN111762946A (en) * | 2020-07-03 | 2020-10-13 | 西安航天华威化工生物工程有限公司 | Advanced treatment method for desulfurization wastewater of power plant |
| CN115140899A (en) * | 2022-07-15 | 2022-10-04 | 浙江红狮环保股份有限公司 | Treatment technology of high organic matter and high salt wastewater |
-
2015
- 2015-11-04 CA CA2911135A patent/CA2911135A1/en not_active Abandoned
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107217709A (en) * | 2017-07-19 | 2017-09-29 | 六安合益智能家居科技有限公司 | A kind of purifier handled applied to floor wastewater |
| CN111051253A (en) * | 2017-09-12 | 2020-04-21 | 奥加诺株式会社 | Apparatus and method for treating silica-containing water |
| CN110590041A (en) * | 2019-09-30 | 2019-12-20 | 大唐郓城发电有限公司 | Method for treating desulfurization wastewater |
| CN111533308A (en) * | 2020-05-09 | 2020-08-14 | 江苏澳特克环境科技有限公司 | Water treatment process for emulsifying and cooling mixed wastewater liquid |
| CN111762946A (en) * | 2020-07-03 | 2020-10-13 | 西安航天华威化工生物工程有限公司 | Advanced treatment method for desulfurization wastewater of power plant |
| CN115140899A (en) * | 2022-07-15 | 2022-10-04 | 浙江红狮环保股份有限公司 | Treatment technology of high organic matter and high salt wastewater |
| CN115140899B (en) * | 2022-07-15 | 2024-02-23 | 浙江红狮环保股份有限公司 | Treatment method of high-organic matter and high-salt wastewater |
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