CA2256209A1 - Process and device for recovery of thermal energy from contaminated vapor while simultaneously separating volatile organic substances - Google Patents
Process and device for recovery of thermal energy from contaminated vapor while simultaneously separating volatile organic substances Download PDFInfo
- Publication number
- CA2256209A1 CA2256209A1 CA002256209A CA2256209A CA2256209A1 CA 2256209 A1 CA2256209 A1 CA 2256209A1 CA 002256209 A CA002256209 A CA 002256209A CA 2256209 A CA2256209 A CA 2256209A CA 2256209 A1 CA2256209 A1 CA 2256209A1
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- CA
- Canada
- Prior art keywords
- vapor
- heat exchanger
- condensate
- heat
- substances
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A process for recovery of thermal energy from contaminated vapor while simultaneously separating volatile organic substances is described, in which the vapor is introduced into a heat exchanger and a heat-absorbing medium is introduced into the heat exchanger, and a heat-absorbed medium is withdrawn therefrom. The vapor is introduced into the lower part of the heat exchanger, and a gas phase enriched with said substances is withdrawn from the top of the heat exchanger, and the condensate poor in said substances is withdrawn from the bottom of the heat exchanger. A device for carrying out the process is described, including a heat exchanger, an inlet for the contaminated vapor, a condensate outlet and an outlet for the volatile substances. The inlet for the contaminated vapor is arranged in the lower part of the heat exchanger, and the outlet for the condensate is arranged at the bottom of the heat exchanger.
Description
CA 022~6209 1998-12-1~
PROCESS AND DEVICE FOR RECOVERY OF THERMAL ENERGY
FROM CONTAMINATED VAPOR WHILE SIMULTANEOUSLY
SEPARATING VOLATILE ORGANIC SUBSTANCES
Field of the Invention The present invention generally relates to recovery of thermal energy from contaminated vapor while simulta-neously separating volatile noxious organic substances which would otherwise be present in the vapor condensate.
More specifically, the invention concerns recovery of thermal energy from vapor generated in thermal treatment of wood, especially fuel wood, while simultaneously achieving such a quality of the discharged condensate so as to allow it to be directly supplied to conventional installations for water purification without any risk of damaging these.
Background Art In thermal treatment of wood, such as fuel wood, volatile substances, e.g. terpenes, other extractive sub-stances and, in case of increased temperature and time, other decomposition products in gas phase escape. This means that flue gases or exhaust air from drying of wood contain these substances. If the flue gas or the air is scrubbed with water for the purpose of cleaning and/or recovering heat, the substances will be found in the scrubber water. When drying in vapor atmosphere, the volatile components of the wood will be found in the excess vapor from the vapor drier. Especially terpenes are well-functioning antiseptics, i.e. they aim at pro-tecting the living wood from decay damage and bacteria.
These substances therefore interfere with the common bio-logical wastewater purification, and the nitrification step in modern wastewater treatment is particularly sen-sitive.
CA 022~6209 1998-12-1~
The vapor emanating from vapor drying of e.g. fuel wood contains a considerable amount of heat which is recoverable.
Summary of the Invention An object of the invention is to recover in one and the same process heat from contaminated vapor, especially vapor obtained in vapor drying of fuel wood, at the same time achieving a sufficient quality of the condensate, i.e. water, that is obtained in the process to make it possible for this to be immediately subjected to conven-tional purification including biological purification.
A further example is evaporation of water in, for instance, black liquor evaporation in the pulp and paper-making industry. The process can in this case replace or supplement the stripping of terpenes whlch is made by the condensates in a so-called condensate stripper.
The process can also be applied in the evaporation of wastewater, e.g. consumed oil emulsions in which vola-tile components such as ammonia, ethanol, methanol, ace-tic acid and the like together with volatile solventstend to contaminate the condensates obtained in the evaporation step. In many cases the heat exchanger is arranged in the evaporator for recovery of heat by so-called mechanical vapor compression. The vapor driven off from the wastewater is then compressed in one or more fans or compressors to a higher pressure. The higher pressure results in a higher condensation temperature and allows the vapor to condensate to heat the evaporator.
If the vapor is supplied to the lower part of the heat exchanger, the volatile contaminants can be made to bleed off in a concentrated state at the top while the purified condensate flows out from the bottom.
A further object of the invention is to provide a device for carrying out the process.
With a view to achieving these objects, the process and the device have been given the characteristic fea-tures that appear from the appended claims.
CA 022~6209 1998-12-1~
The heat exchanger used in the inventive process and included in the inventive device is of a type having one or more heat exchanger packages comprising, for instance, tubes or lamellae of a conventional design, and being of the encased type, i.e. the heat exchanger having an outer casing or shell. In conventional fashion, the heat exchanger has an inlet and an outlet for a medium, such as distant heating water, feed water, which flows through the heat exchanger to absorb heat. According to a prefer-red embodiment, the height of the heat exchanger isgreater than its width, and the packages are arranged concentrically about the vertical axis of the heat exchanger. When the contaminated vapor is supplied to the lower part of the heat exchanger, rectification takes place, i.e. enrichment in the same way as in dis-tillation. Water vapor condenses when moving upwards while volatile components are evaporated from the con-densate which flows downwards. The presence of the vapor also causes some components to be steam-stripped, i.e.
their volatility increases in the presence of water vapor. At the top of the heat exchanger there is a gas phase which is enriched with volatile components, and in the bottom there is a condensate which is poor in similar components. From the top, the gas/ vapor mixture can be condensed in a separate condenser or conducted to combus-tion. With a view to reinforcing the procedure described above, there are arranged, according to a preferred embo-diment, elements which increase the effective contact surface between gas and liquid, for instance Raschig rings, in the respective spaces between the outer wall and the outer boundary surface of the packages. This pro-cedure contributes essentially to the provision of the feature according to the invention, viz. the provision of a condensate of such a purity to allow it to be imme-diately supplied to a wastewater purification plant.
CA 022~6209 1998-12-1~
According to a preferred embodiment of the inven-tion, the vapor has, when entering the heat exchanger, a pressure of 1-5 bar and a temperature of 110-180~C.
Brief Description of the Drawings The invention will now be described in more detail with reference to a preferred embodiment while referring to the accompanying drawing which is a schematic view of a preferred embodiment of a device according to the invention.
Description of the Preferred Embodiment of the Invention Vapor from a fuel drier with a pressure of about 3-4 bar and a temperature of 140-150~C is supplied to the lower part towards the casing side of the heat exchanger.
At the same time a heat-absorbing medium, in this case water, is supplied through an inlet (not shown) and is allowed to flow through the tubes or lamellae in the heat exchanger packages and is withdrawn through an outlet (not shown) for use as distant heating water or feed water. The vapor introduced as described above condenses on its way upwards on the inner surfaces of the casing and also on the surfaces of the heat exchanger packages while more volatile components are evaporated from the condensate flowing downwards. This condensate accumulates on the bottom of the heat exchanger and is withdrawn in the lower part thereof. The condensate is cooled before being supplied to a conventional municipal wastewater purification plant. The gas phase enriched in the top of the heat exchanger and containing volatile components can either be condensed in a separate condenser as shown in the drawing, or be conducted to combustion (not shown).
According to the invention, a combination of distil-lation-condensation-heat exchange has now surprisingly resulted in the essential advantage that in one and the same process on the one hand a condensate is obtained which has such a purity that it can immediately be sup-plied to a water purification plant and, on the other hand, heat is recovered from the contaminated vapor. In CA 022~6209 1998-12-1~
other words, the condensate satisfies the specifications required for precisely such as plant.
Below follow the results of nitrification-inhibiting experiments involving nitrifying sludge and test water carried out according to modified ISO 9509-1989 (E).
Samples Marking of samples: MG 11331 (condensates withdrawn at the bottom of the heat exchanger according to the invention) and MG 11332 (samples withdrawn from "top con-densates").
The samples were stored in chilled state up to thetime of the analysis.
Materials and Methods Test Method The experiment was carried out at room temperature.
The method is simplified since only two sample concen-trations were examined. The test principle implies brief-ly that different volumes of test water and a synthetic medium are mixed in a number of cylinders. The mixtures are diluted with distilled water to amount to 125 ml.
Then 125 ml of nitrifying sll-dge are added, and the cylinders are incubated at room temperature for about 4 h during airing. Samples for analysis of the amount of nitrite and nitrate are withdrawn from each cylinder both before and after incubation. The amount of nitrite and nitrate formed in the cylinders which have contained sam-ples, is compared with the amount formed in cylinders which have not contained any sample.
Preparation of Samples The samples were adjusted in respect of pH to about 7.6 before the experiment.
The following test concentrations (vol%) of the sam-ple were examined: 20 and 40.
Inoculum The nitrifying sludge was supplied by Klagshamns Wastewater Treatment Plant and was aerated until it was used.
CA 022~6209 1998-12-1 Analysis After filtration (Whatman GF/A) the nitrite and nitrate nitrogen content of the filtrate was analyzed according to Swedish Standard SS 028133-2.
Results Table 1 Amount of nitrite and nitrate nitrogen formed. Samples compared with blind sample and inhibitor.
Sample marking Sample (vol%) Oxide N (mg/l) Inhibition (%) Blind sample 0 29.9*
MG 11331 20 24.7 17 MG 11331 40 17.3** 42 MG 11332 20 0.0 100 MG 11332 40 0.45** 98 Inhib*** - 0 100 * Average of three blind samples ** Average of double samples *** Reference inhibitor: Allyl thiourea 8 mg/l The proportion of suspended substance in the experi-ment was 1.52 g/l.
The specific nitrification rate of the sludge was measured to be 7.9 mg/N/(g.h). Owing to the high nitrifi-cation rate of the sludge, the time of the experiment was shortened to 2.5 h.
The results show that samples marked with MG 11331 exhibited 17% inhibition at a concentration of 20% and 42% inhibition at a concentration of 40%. For municipal purification a limit of 20% inhibition at a concentration of 20% is stated, which means that the condensate obtain-ed according to the invention can be finally purified in municipal wastewater treatment plants.
On the other hand, samples marked with MG 11332 caused a considerable inhibition of the nitrification in relation to the tested inoculum. The inhibition was total (100%) when 20 vol% of sample was added.
CA 022~6209 1998-12-1~
An analysis of the above samples especially in respect of COD (chemical oxygen demand) and BOD (bio-chemical oxygen demand) was carried out:
Sample: MG 11331 Property of analysis Result Unit KRUT-code pH 3.6 PH-25 Conductivity 10.3 mS/m COND-25 Biochemical oxygen 193 mg/l BOD7-NAE
demand, BOD7 Chemical oxygen demand, 400 mg/l CODCR-NH
chromate Suspended substances 51 mg/l STR-STG
5 Sample: MG 11332 Property of analysis Result Unit KRUT-code pH 3.9 PH-25 Conductivity 18.1 mS/m COND-25 Biochemical oxygen 3400 mg/l BOD7-NAE
demand, BOD7 Chemical oxygen demand, 13700 mg/l CODCR-NH
chromate Suspended substances 50 mg/l STR-STG
Acceptable values of condensates for biological purification are:
COD 1000-5000 mg/l BOD 800-3000 mg/l Conclusion:
The bottom condensate satisfies the above criteria.
PROCESS AND DEVICE FOR RECOVERY OF THERMAL ENERGY
FROM CONTAMINATED VAPOR WHILE SIMULTANEOUSLY
SEPARATING VOLATILE ORGANIC SUBSTANCES
Field of the Invention The present invention generally relates to recovery of thermal energy from contaminated vapor while simulta-neously separating volatile noxious organic substances which would otherwise be present in the vapor condensate.
More specifically, the invention concerns recovery of thermal energy from vapor generated in thermal treatment of wood, especially fuel wood, while simultaneously achieving such a quality of the discharged condensate so as to allow it to be directly supplied to conventional installations for water purification without any risk of damaging these.
Background Art In thermal treatment of wood, such as fuel wood, volatile substances, e.g. terpenes, other extractive sub-stances and, in case of increased temperature and time, other decomposition products in gas phase escape. This means that flue gases or exhaust air from drying of wood contain these substances. If the flue gas or the air is scrubbed with water for the purpose of cleaning and/or recovering heat, the substances will be found in the scrubber water. When drying in vapor atmosphere, the volatile components of the wood will be found in the excess vapor from the vapor drier. Especially terpenes are well-functioning antiseptics, i.e. they aim at pro-tecting the living wood from decay damage and bacteria.
These substances therefore interfere with the common bio-logical wastewater purification, and the nitrification step in modern wastewater treatment is particularly sen-sitive.
CA 022~6209 1998-12-1~
The vapor emanating from vapor drying of e.g. fuel wood contains a considerable amount of heat which is recoverable.
Summary of the Invention An object of the invention is to recover in one and the same process heat from contaminated vapor, especially vapor obtained in vapor drying of fuel wood, at the same time achieving a sufficient quality of the condensate, i.e. water, that is obtained in the process to make it possible for this to be immediately subjected to conven-tional purification including biological purification.
A further example is evaporation of water in, for instance, black liquor evaporation in the pulp and paper-making industry. The process can in this case replace or supplement the stripping of terpenes whlch is made by the condensates in a so-called condensate stripper.
The process can also be applied in the evaporation of wastewater, e.g. consumed oil emulsions in which vola-tile components such as ammonia, ethanol, methanol, ace-tic acid and the like together with volatile solventstend to contaminate the condensates obtained in the evaporation step. In many cases the heat exchanger is arranged in the evaporator for recovery of heat by so-called mechanical vapor compression. The vapor driven off from the wastewater is then compressed in one or more fans or compressors to a higher pressure. The higher pressure results in a higher condensation temperature and allows the vapor to condensate to heat the evaporator.
If the vapor is supplied to the lower part of the heat exchanger, the volatile contaminants can be made to bleed off in a concentrated state at the top while the purified condensate flows out from the bottom.
A further object of the invention is to provide a device for carrying out the process.
With a view to achieving these objects, the process and the device have been given the characteristic fea-tures that appear from the appended claims.
CA 022~6209 1998-12-1~
The heat exchanger used in the inventive process and included in the inventive device is of a type having one or more heat exchanger packages comprising, for instance, tubes or lamellae of a conventional design, and being of the encased type, i.e. the heat exchanger having an outer casing or shell. In conventional fashion, the heat exchanger has an inlet and an outlet for a medium, such as distant heating water, feed water, which flows through the heat exchanger to absorb heat. According to a prefer-red embodiment, the height of the heat exchanger isgreater than its width, and the packages are arranged concentrically about the vertical axis of the heat exchanger. When the contaminated vapor is supplied to the lower part of the heat exchanger, rectification takes place, i.e. enrichment in the same way as in dis-tillation. Water vapor condenses when moving upwards while volatile components are evaporated from the con-densate which flows downwards. The presence of the vapor also causes some components to be steam-stripped, i.e.
their volatility increases in the presence of water vapor. At the top of the heat exchanger there is a gas phase which is enriched with volatile components, and in the bottom there is a condensate which is poor in similar components. From the top, the gas/ vapor mixture can be condensed in a separate condenser or conducted to combus-tion. With a view to reinforcing the procedure described above, there are arranged, according to a preferred embo-diment, elements which increase the effective contact surface between gas and liquid, for instance Raschig rings, in the respective spaces between the outer wall and the outer boundary surface of the packages. This pro-cedure contributes essentially to the provision of the feature according to the invention, viz. the provision of a condensate of such a purity to allow it to be imme-diately supplied to a wastewater purification plant.
CA 022~6209 1998-12-1~
According to a preferred embodiment of the inven-tion, the vapor has, when entering the heat exchanger, a pressure of 1-5 bar and a temperature of 110-180~C.
Brief Description of the Drawings The invention will now be described in more detail with reference to a preferred embodiment while referring to the accompanying drawing which is a schematic view of a preferred embodiment of a device according to the invention.
Description of the Preferred Embodiment of the Invention Vapor from a fuel drier with a pressure of about 3-4 bar and a temperature of 140-150~C is supplied to the lower part towards the casing side of the heat exchanger.
At the same time a heat-absorbing medium, in this case water, is supplied through an inlet (not shown) and is allowed to flow through the tubes or lamellae in the heat exchanger packages and is withdrawn through an outlet (not shown) for use as distant heating water or feed water. The vapor introduced as described above condenses on its way upwards on the inner surfaces of the casing and also on the surfaces of the heat exchanger packages while more volatile components are evaporated from the condensate flowing downwards. This condensate accumulates on the bottom of the heat exchanger and is withdrawn in the lower part thereof. The condensate is cooled before being supplied to a conventional municipal wastewater purification plant. The gas phase enriched in the top of the heat exchanger and containing volatile components can either be condensed in a separate condenser as shown in the drawing, or be conducted to combustion (not shown).
According to the invention, a combination of distil-lation-condensation-heat exchange has now surprisingly resulted in the essential advantage that in one and the same process on the one hand a condensate is obtained which has such a purity that it can immediately be sup-plied to a water purification plant and, on the other hand, heat is recovered from the contaminated vapor. In CA 022~6209 1998-12-1~
other words, the condensate satisfies the specifications required for precisely such as plant.
Below follow the results of nitrification-inhibiting experiments involving nitrifying sludge and test water carried out according to modified ISO 9509-1989 (E).
Samples Marking of samples: MG 11331 (condensates withdrawn at the bottom of the heat exchanger according to the invention) and MG 11332 (samples withdrawn from "top con-densates").
The samples were stored in chilled state up to thetime of the analysis.
Materials and Methods Test Method The experiment was carried out at room temperature.
The method is simplified since only two sample concen-trations were examined. The test principle implies brief-ly that different volumes of test water and a synthetic medium are mixed in a number of cylinders. The mixtures are diluted with distilled water to amount to 125 ml.
Then 125 ml of nitrifying sll-dge are added, and the cylinders are incubated at room temperature for about 4 h during airing. Samples for analysis of the amount of nitrite and nitrate are withdrawn from each cylinder both before and after incubation. The amount of nitrite and nitrate formed in the cylinders which have contained sam-ples, is compared with the amount formed in cylinders which have not contained any sample.
Preparation of Samples The samples were adjusted in respect of pH to about 7.6 before the experiment.
The following test concentrations (vol%) of the sam-ple were examined: 20 and 40.
Inoculum The nitrifying sludge was supplied by Klagshamns Wastewater Treatment Plant and was aerated until it was used.
CA 022~6209 1998-12-1 Analysis After filtration (Whatman GF/A) the nitrite and nitrate nitrogen content of the filtrate was analyzed according to Swedish Standard SS 028133-2.
Results Table 1 Amount of nitrite and nitrate nitrogen formed. Samples compared with blind sample and inhibitor.
Sample marking Sample (vol%) Oxide N (mg/l) Inhibition (%) Blind sample 0 29.9*
MG 11331 20 24.7 17 MG 11331 40 17.3** 42 MG 11332 20 0.0 100 MG 11332 40 0.45** 98 Inhib*** - 0 100 * Average of three blind samples ** Average of double samples *** Reference inhibitor: Allyl thiourea 8 mg/l The proportion of suspended substance in the experi-ment was 1.52 g/l.
The specific nitrification rate of the sludge was measured to be 7.9 mg/N/(g.h). Owing to the high nitrifi-cation rate of the sludge, the time of the experiment was shortened to 2.5 h.
The results show that samples marked with MG 11331 exhibited 17% inhibition at a concentration of 20% and 42% inhibition at a concentration of 40%. For municipal purification a limit of 20% inhibition at a concentration of 20% is stated, which means that the condensate obtain-ed according to the invention can be finally purified in municipal wastewater treatment plants.
On the other hand, samples marked with MG 11332 caused a considerable inhibition of the nitrification in relation to the tested inoculum. The inhibition was total (100%) when 20 vol% of sample was added.
CA 022~6209 1998-12-1~
An analysis of the above samples especially in respect of COD (chemical oxygen demand) and BOD (bio-chemical oxygen demand) was carried out:
Sample: MG 11331 Property of analysis Result Unit KRUT-code pH 3.6 PH-25 Conductivity 10.3 mS/m COND-25 Biochemical oxygen 193 mg/l BOD7-NAE
demand, BOD7 Chemical oxygen demand, 400 mg/l CODCR-NH
chromate Suspended substances 51 mg/l STR-STG
5 Sample: MG 11332 Property of analysis Result Unit KRUT-code pH 3.9 PH-25 Conductivity 18.1 mS/m COND-25 Biochemical oxygen 3400 mg/l BOD7-NAE
demand, BOD7 Chemical oxygen demand, 13700 mg/l CODCR-NH
chromate Suspended substances 50 mg/l STR-STG
Acceptable values of condensates for biological purification are:
COD 1000-5000 mg/l BOD 800-3000 mg/l Conclusion:
The bottom condensate satisfies the above criteria.
Claims (8)
1. A process for recovery of thermal energy from contaminated vapor while simultaneously separating volatile organic substances, wherein the vapor is introduced into a heat exchanger and a heat-absorbing medium is introduced into the heat exchanger, and a heat-absorbed medium is withdrawn therefrom, comprising the steps of introducing the vapor in the lower part of the heat exchanger, the vapor condensing when moving upwards, while the volatile substances are evaporated from the condensate flowing downwards, withdrawing a gas phase enriched with said substances from the top of the heat exchanger, and withdrawing the condensate poor in said substances from the bottom of the heat exchanger.
2. A process as claimed in claim 1, wherein the contaminated vapor is vapor from a drier for thermal treatment of wood, preferably fuel wood.
3. A method as claimed in claim 1, wherein the heat exchanger is encased and the vapor is introduced towards the casing side.
4. A device for recovery of thermal energy from contaminated vapor while simultaneously separating volatile organic substances, comprising a heat exchanger having an inlet for a heat-absorbing medium and an outlet for a heat-absorbed medium, an inlet for the contaminated vapor, a condensate outlet and an outlet for the volatile substances, said inlet for the contaminated vapor being arranged in the lower part of the heat exchanger, and the outlet for the condensate being arranged at the bottom of the heat exchanger.
5. A device as claimed in claim 4, wherein the heat exchanger is encased, and the vapor inlet is arranged at the casing side.
6. A device as claimed in claim 4, wherein the contaminated vapor is vapor from a drier for thermal treatment of wood, preferably fuel wood.
7. A device as claimed in claim 4, wherein the introduced vapor has a pressure of 1-5 bar and a temperature of 110-180°C.
8. A device as claimed in claim 4, wherein the heat exchanger is included in an evaporating plant.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE9704700A SE518647C2 (en) | 1997-12-17 | 1997-12-17 | Heat exchanger for recovering heat from contaminated steam generated by e.g. steam dryer for timber, effluent heating plant or black liquor cooker |
| SE9704700-5 | 1997-12-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2256209A1 true CA2256209A1 (en) | 1999-06-17 |
Family
ID=20409418
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002256209A Abandoned CA2256209A1 (en) | 1997-12-17 | 1998-12-15 | Process and device for recovery of thermal energy from contaminated vapor while simultaneously separating volatile organic substances |
Country Status (2)
| Country | Link |
|---|---|
| CA (1) | CA2256209A1 (en) |
| SE (1) | SE518647C2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018236282A1 (en) * | 2017-06-21 | 2018-12-27 | Rosenblad Design Aktiebolag | Apparatus and method for separation of components with different volatility in a mixed fluid |
-
1997
- 1997-12-17 SE SE9704700A patent/SE518647C2/en not_active IP Right Cessation
-
1998
- 1998-12-15 CA CA002256209A patent/CA2256209A1/en not_active Abandoned
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018236282A1 (en) * | 2017-06-21 | 2018-12-27 | Rosenblad Design Aktiebolag | Apparatus and method for separation of components with different volatility in a mixed fluid |
| US11097200B2 (en) | 2017-06-21 | 2021-08-24 | Rosenblad Design Aktiebolag | Apparatus and method for separation of components with different volatility in a mixed fluid |
Also Published As
| Publication number | Publication date |
|---|---|
| SE518647C2 (en) | 2002-11-05 |
| SE9704700D0 (en) | 1997-12-17 |
| SE9704700L (en) | 1999-06-18 |
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| FZDE | Dead |