CN102659201A - Treatment device and method for reclaiming oil extraction waste water by using waste heat of oil-gas field united station - Google Patents
Treatment device and method for reclaiming oil extraction waste water by using waste heat of oil-gas field united station Download PDFInfo
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- CN102659201A CN102659201A CN201210126238XA CN201210126238A CN102659201A CN 102659201 A CN102659201 A CN 102659201A CN 201210126238X A CN201210126238X A CN 201210126238XA CN 201210126238 A CN201210126238 A CN 201210126238A CN 102659201 A CN102659201 A CN 102659201A
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Abstract
Disclosed are a treatment device and a method for reclaiming oil extraction waste water by using waste heat of an oil-gas field united station. The waste heat of the united station is used for evaporating and concentrating the oil extraction water to recycle fresh water, wherein any evaporator can be sued; the mass fraction of salts is controlled to be 25-35% after the waste water is concentrated and discharged from the evaporator, wherein crystallization of salts is definitely guaranteed not to be precipitated at the normal temperature; and high temperature fresh water steam and high temperature concentrated salt water discharged from the evaporator are subjected to heat exchange with the oil extraction waste water through heat exchangers and cooled to the normal temperature, the fresh water formed by the cooled water steam is reclaimed, and when each of indexes (such as suspended solid and the like) of the concentrated salt water after cooling meets the water quality requirement of reinjection water, the concentrated salt water is reinjected. The treatment device and the method for reclaiming the oil extraction waste water by using the waste heat of the oil-gas field united station has the advantages of being capable of not only effectively solving the problem of waste salt rubbish produced by the fact that lots of oil extraction waste water is difficult to completely reinject, but also effectively using oilfield waste heat resources to obtain the fresh water and achieving good environment benefits and economical benefits and particularly applicable to oilfields in water-deficient areas of deserts.
Description
Technical field
The present invention relates to a kind of fld joint station used heat (like torch, other form used heat) that utilizes oil extraction waste water is carried out processing equipment for recycling and method.
Background technology
The oil extraction waste water generation of fld joint station is big; Has higher saltiness (massfraction is 10～25%); Sodium chloride content low (massfraction is 50～75%) in the saline admixture; Become the difficult problem that land disposal can't crack, therefore, general fld have to adopt the way of re-injection that it is disposed.But because the water yield is excessive; Re-injection still can not be under its situation about disposing fully; The waste water of re-injection have to not be pumped to and shine the salt pond and carry out the nature volatilization in the hope of minimizing; But stayed a large amount of mixing salt that has no use value (except sodium-chlor, also having calcium chloride, magnesium chloride etc.) and become new refuse harm environment.
Up to now, do not find as yet than the better recycling processing method of supersalinity oil extraction waste water.
Summary of the invention
The object of the present invention is to provide a kind of treatment unit and method of utilizing fld joint station used heat to the oil extraction waste water resource utilization.
For achieving the above object, the inventive system comprises: comprise first interchanger that the is connected in parallel combination, the combination of second interchanger that are connected with the normal temperature oil extraction waste water, and the vaporizer that is connected with the outlet of the combination of first interchanger, the combination of second interchanger; The fire end of said vaporizer links to each other with oil field used heat heating system; Through the entering vaporizer that confluxes after the combination of first interchanger, the preliminary heat exchange heating of second interchanger combination oil extraction waste water; Waste water carries out becoming high temperature fresh water steam and the concentrated salt solution of high temperature after the evaporation concentration in vaporizer; Formation normal temperature fresh water reclaimed after high temperature fresh water steam made up cooling through first interchanger, formed the concentrated salt solution of normal temperature after the concentrated salt solution of high temperature is lowered the temperature through the combination of second interchanger and carried out re-injection.
Described first interchanger combination, second heat exchanger package are combined into shell and tube heat exchanger, plate-type heat exchanger, spiral tube heat exchanger or coil heat exchanger.
Described normal temperature oil extraction waste water makes up through first, second interchanger that is connected in parallel through arm shunting back by 10: 1～1: 10 throughput ratio.
Described first, second interchanger combination is composed in series by 3～8 interchanger respectively, and low temperature oil extraction waste water and high temperature fresh water, high temperature concentrate the brinish temperature difference and is controlled at 5 ℃～30 ℃.
Describedly be controlled at 60 ℃～100 ℃ by first, second interchanger combination wastewater temperature that gets into vaporizer that confluxes.
Described oil extraction waste water salt massfraction is 1～25%.
Described fresh water yield is controlled to be 20～80% of former oil extraction waste water, concentrates brinish salt massfraction and is controlled to be 25～35%.
The present invention utilizes fld joint station used heat to the oil extraction waste water recycling processing method: to the system of steady-state operation; Oil extraction waste water at normal temperatures carries out preliminary heat exchange heating by arm shunting back through first, second heat exchanger package merging that is connected in parallel by 10: 1～1: 10 throughput ratio; Conflux after the waste water of preliminary heat exchange heating makes up through first, second interchanger and get into vaporizer by the oil field waste heating; Waste water carries out becoming high temperature fresh water steam and the concentrated salt solution of high temperature after the evaporation concentration in vaporizer; Formation normal temperature fresh water reclaimed after high temperature fresh water steam made up the heat exchange cooling through first interchanger, formed the concentrated salt solution of normal temperature after the concentrated salt solution of high temperature is lowered the temperature through second interchanger combination heat exchange and carried out re-injection.
Described first, second interchanger combination is composed in series by 3～8 interchanger respectively, and low temperature oil extraction waste water and high temperature fresh water, high temperature concentrate the brinish temperature difference and is controlled at 5 ℃～30 ℃; And make up the wastewater temperature that gets into vaporizer that confluxes by first, second interchanger and be controlled at 60 ℃～100 ℃.
Described fresh water yield is controlled to be 20～80% of oil extraction waste water, concentrates brinish salt massfraction and is controlled to be 25～35%.
The invention reside in and utilize joint station used heat (like torch, waste hot steam etc.) that supersalinity oil extraction waste water (salt massfraction 1～25%) is carried out evaporation concentration (no matter adopting which kind of vaporizer) recovery fresh water; Concentrating back waste water salt massfraction brings up to concentration and is 25～35% (note: definitely will guarantee that crystallization salt-free under its normal temperature separate out) discharges from vaporizer; The high temperature fresh water steam that vaporizer is discharged, high temperature concentrate salt solution and carry out the heat exchange postcooling to normal temperature through interchanger and oil extraction waste water respectively; The fresh water that water vapor cooling back forms reclaims, and the cooling back concentrates the water quality requirement that salt solution each item index (like SS etc.) satisfies re-injection water and carries out re-injection.
Meaning of the present invention is both can effectively to solve that a large amount of oil extraction waste waters are difficult to complete re-injection and the abraum salt garbage problem that produces can utilize the oil gas field waste thermal resource to obtain fresh water again efficiently; Not only have good benefits in environment, and have good economic benefits.The present invention is particluarly suitable for the oil field of water-deficient area, desert and carries out.
Description of drawings
Fig. 1 is a system flow synoptic diagram of the present invention.
Embodiment
Below in conjunction with synoptic diagram the present invention is done further explain.
Referring to Fig. 1, the present invention includes and draw together the interchanger that the is connected in parallel combination 1, the interchanger combination 2 that are connected with the former oil extraction waste water of normal temperature, and the vaporizer that is connected of the outlet of interchanger combination 1, interchanger combination 2; The fire end of said vaporizer links to each other with oil field used heat heating system.Make up the entering vaporizer that confluxes after the preliminary heat exchange of 2 oil extraction waste waters is heated through interchanger combination 1, interchanger; Waste water carries out becoming high temperature fresh water steam and the concentrated salt solution of high temperature after the evaporation concentration in vaporizer; Formation normal temperature fresh water reclaimed after high temperature fresh water steam made up 1 cooling through interchanger, formed the concentrated salt solution of normal temperature after the concentrated salt solution of high temperature is lowered the temperature through interchanger combination 2 and carried out re-injection.
Interchanger combination 1 of the present invention is composed in series by 3～8 interchanger respectively with interchanger combination 2, and low temperature oil extraction waste water and high temperature fresh water, high temperature concentrate the brinish temperature difference and is controlled at 5 ℃～30 ℃.And be controlled at 60 ℃～100 ℃ by interchanger combination 1 and interchanger combination 2 wastewater temperature that gets into vaporizer that confluxes.
The oil recovery re-injection water salt massfraction that the present invention adopted is 1～25%.
Recovery method of the present invention is following: to the system of steady-state operation; Oil extraction waste water at normal temperatures by 10: 1～1: 10 throughput ratio by arm shunting back through the interchanger combination 1 that is connected in parallel with interchanger combination 2 and carry out preliminary heat exchange heating; The waste water of preliminary heat exchange heating makes up to conflux after 2 through interchanger combination 1 and interchanger and gets into the vaporizer by the oil field waste heating; Waste water carries out becoming high temperature fresh water steam and the concentrated salt solution of high temperature after the evaporation concentration in vaporizer; High temperature fresh water steam makes up the recovery of 1 heat exchange cooling back formation normal temperature fresh water through interchanger, and the concentrated salt solution of high temperature makes up the concentrated salt solution of 2 heat exchange cooling back formation normal temperature through interchanger and carries out re-injection.Fresh water yield is controlled to be 20～80% of former oil extraction waste water quality, and it is 25～35% that concentrated brinish salt massfraction is controlled to be.
High-temperature vapor and high temperature concentrate salt solution (massfraction 25～35%) carry out heat exchange through interchanger combination 1, interchanger combination 2 respectively after; Self be cooled to normal temperature (0 ℃～30 ℃); Form to reclaim fresh water and concentrate salt solution, the concentrated salt solution each item water-quality guideline under the normal temperature (like SS etc.) is carried out re-injection after satisfying the water quality requirement of re-injection water.Simultaneously normal temperature oil extraction waste water down made up 2 o'clock at the interchanger combination 1 of flowing through, interchanger, also concentrated the salt solution entering vaporizer that carries out confluxing after heat exchange is tentatively heated with vaporizer effusive high temperature fresh water steam and high-temperature respectively and carried out evaporation concentration.
Claims (10)
1. utilize fld joint station used heat to oil recovery re-injection recycling of water resource treatment unit; It is characterized in that: comprise first interchanger that the is connected in parallel combination (1), second interchanger combination (2) that are connected with the normal temperature oil extraction waste water, and the vaporizer that is connected with the outlet of first interchanger combination (1), second interchanger combination (2); The fire end of said vaporizer links to each other with oil field used heat heating system; Through the entering vaporizer that confluxes after first interchanger combination (1), the preliminary heat exchange heating of second interchanger combination (2) oil extraction waste water; Waste water carries out becoming high temperature fresh water steam and the concentrated salt solution of high temperature after the evaporation concentration in vaporizer; High temperature fresh water steam passes through first interchanger and makes up the recovery of (1) cooling back formation normal temperature fresh water, and the concentrated salt solution of high temperature makes up the concentrated salt solution of (2) cooling back formation normal temperature through second interchanger and carries out re-injection.
2. the fld joint station used heat that utilizes according to claim 1 is characterized in that the oil extraction waste water processing equipment for recycling: described first interchanger combination (1), second interchanger combination (2) are shell and tube heat exchanger, plate-type heat exchanger, spiral tube heat exchanger or coil heat exchanger.
3. the fld joint station used heat that utilizes according to claim 1 is characterized in that the oil extraction waste water processing equipment for recycling: described normal temperature oil extraction waste water makes up (1,2) through arm shunting back through first, second interchanger that is connected in parallel by 10: 1～1: 10 throughput ratio.
4. the fld joint station used heat that utilizes according to claim 1 is to the oil extraction waste water processing equipment for recycling; It is characterized in that: described first, second interchanger combination (1,2) is composed in series by 3～8 interchanger respectively, and low temperature oil extraction waste water and high temperature fresh water, high temperature concentrate the brinish temperature difference and is controlled at 5 ℃～30 ℃.
5. the fld joint station used heat that utilizes according to claim 1 is characterized in that the oil extraction waste water processing equipment for recycling: describedly be controlled at 60 ℃～100 ℃ by first, second interchanger combination (1,2) wastewater temperature that gets into vaporizer that confluxes.
6. the fld joint station used heat that utilizes according to claim 1 is characterized in that the oil extraction waste water processing equipment for recycling: described oil extraction waste water salt massfraction is 1～25%.
7. the fld joint station used heat that utilizes according to claim 1 is to the oil extraction waste water processing equipment for recycling, and it is characterized in that: described fresh water yield is controlled to be 20～80% of former oil extraction waste water, concentrates brinish salt massfraction and is controlled to be 25～35%.
One kind according to claim 1 the device utilize fld joint station used heat to the oil extraction waste water recycling processing method,
It is characterized in that: to the system of steady-state operation; Oil extraction waste water is at normal temperatures made up (1,2) through first, second interchanger that is connected in parallel and is carried out preliminary heat exchange heating by arm shunting back by 10: 1～1: 10 throughput ratio; The waste water of the preliminary heat exchange heating vaporizer of entering that conflux after through first, second interchanger combination (1,2) by the oil field waste heating; Waste water carries out becoming high temperature fresh water steam and the concentrated salt solution of high temperature after the evaporation concentration in vaporizer; High temperature fresh water steam passes through first interchanger and makes up the recovery of (1) heat exchange cooling back formation normal temperature fresh water, and the concentrated salt solution of high temperature makes up the concentrated salt solution of (2) heat exchange cooling back formation normal temperature through second interchanger and carries out re-injection.
9. the fld joint station used heat that utilizes according to claim 8 is to oil recovery re-injection recycling of water resource treatment process; It is characterized in that: described first, second interchanger combination (1,2) is composed in series by 3～8 interchanger respectively, and low temperature oil extraction waste water and high temperature fresh water, high temperature concentrate the brinish temperature difference and is controlled at 5 ℃～30 ℃; And be controlled at 60 ℃～100 ℃ by first, second interchanger combination (1,2) wastewater temperature that gets into vaporizer that confluxes.
10. the fld joint station used heat that utilizes according to claim 8 is to oil recovery re-injection recycling of water resource treatment process, and it is characterized in that: described fresh water yield is controlled to be 20～80% of oil extraction waste water, concentrates brinish salt massfraction and is controlled to be 25～35%.
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| CN201210126238XA CN102659201A (en) | 2012-04-26 | 2012-04-26 | Treatment device and method for reclaiming oil extraction waste water by using waste heat of oil-gas field united station |
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| CN201210126238XA CN102659201A (en) | 2012-04-26 | 2012-04-26 | Treatment device and method for reclaiming oil extraction waste water by using waste heat of oil-gas field united station |
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Citations (4)
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| US4032412A (en) * | 1971-07-23 | 1977-06-28 | Deutsche Texaco Aktiengesellschaft | Process for optimal pressure control in a multi-stage evaporation unit |
| CN101318716A (en) * | 2007-06-07 | 2008-12-10 | 天津工业大学 | Film evaporating concentration liquid processing system and processing method |
| CN101774747A (en) * | 2010-03-04 | 2010-07-14 | 成都金池塘科技有限公司 | Device for performing reduction treatment on drilling waste water by using diesel exhaust and treatment method thereof |
| CN102329036A (en) * | 2011-09-06 | 2012-01-25 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
-
2012
- 2012-04-26 CN CN201210126238XA patent/CN102659201A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4032412A (en) * | 1971-07-23 | 1977-06-28 | Deutsche Texaco Aktiengesellschaft | Process for optimal pressure control in a multi-stage evaporation unit |
| CN101318716A (en) * | 2007-06-07 | 2008-12-10 | 天津工业大学 | Film evaporating concentration liquid processing system and processing method |
| CN101774747A (en) * | 2010-03-04 | 2010-07-14 | 成都金池塘科技有限公司 | Device for performing reduction treatment on drilling waste water by using diesel exhaust and treatment method thereof |
| CN102329036A (en) * | 2011-09-06 | 2012-01-25 | 江苏中圣高科技产业有限公司 | High-efficiency method for recovery treatment of saliferous wastewater under zero emission through residual heat utilization |
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Inventor after: Sun Genxing Inventor after: Liu Ruoyang Inventor after: Chen Yuanyuan Inventor after: Si Jun Inventor after: Fu Wei Inventor before: Sun Genxing Inventor before: Si Jun Inventor before: Liu Ruoyang Inventor before: Chen Yuanyuan Inventor before: Fu Wei |
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Effective date of registration: 20121113 Address after: 710021 Shaanxi province Xi'an Weiyang University Park No. 1 Applicant after: Shaanxi University of Science and Technology Address before: 710021 Shaanxi province Xi'an Weiyang University Park No. 1 Applicant before: Shaanxi University of Science and Technology Applicant before: Beijing Huasheng Kuntai Environmental Protection Co., Ltd. |
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Application publication date: 20120912 |