WO2003092859A1 - Verfahren zur reinigung von gas - Google Patents
Verfahren zur reinigung von gas Download PDFInfo
- Publication number
- WO2003092859A1 WO2003092859A1 PCT/DE2002/001872 DE0201872W WO03092859A1 WO 2003092859 A1 WO2003092859 A1 WO 2003092859A1 DE 0201872 W DE0201872 W DE 0201872W WO 03092859 A1 WO03092859 A1 WO 03092859A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- liquid
- cooled
- fed
- pollutants
- Prior art date
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/006—Layout of treatment plant
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/40—Intercepting solids by cyclones
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/40—Sorption with wet devices, e.g. scrubbers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/70—Condensing contaminants with coolers
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Definitions
- the invention relates to a process for the purification of gas, in particular process gas from allothermal gasification processes, the gas being cooled in successive steps and pollutants from the gas being condensed in the individual steps and pollutants being additionally removed chemically from the gas in at least one step.
- DD 110 050 discloses a process for the production of gases containing hydrogen and / or carbon oxide, in which the main focus is on the effective use of liquid in gas cleaning.
- a method for cleaning gas is known, in which the gas to be cleaned passes through two heat exchangers connected in series, which cool the gas. Furthermore, liquid is supplied to the gas in spray zones, which are located at the inlet and outlet of the second heat exchanger.
- High-temperature cracking of the process gas is not desirable in terms of energy, since gasification processes, in particular for biomass, are optimized for an operating temperature of 800 ° C.
- a disadvantage of all of the aforementioned methods is that the individual process steps are not coordinated with one another in such a way that undesired reactions in the process gas are suppressed between the individual process steps.
- the present invention is therefore based on the object of designing and developing a method of the type mentioned at the outset in such a way that problem-free and effective gas cleaning can be implemented while preventing undesired reactions.
- a method for cleaning gas is characterized in that the gas after whose generation for solids removal is carried out under adjustable physical conditions by a cyclone and is cooled suddenly in succession by a heat exchanger coupled to the cyclone and by finely sprayed water droplets produced when passing through a swirling water bath.
- a second sudden cooling of the gas takes place through liquid contact.
- the contact of the gas with hot walls is prevented in a particularly refined way by passing through a swirling liquid bath and the generation of finely sprayed liquid droplets. Induction of after-reactions by hot walls is almost impossible.
- the finest drops not only cool the gas abruptly due to their large heat exchange surface, but also effectively clean them, since the drops function as condensation nuclei to which pollutants and dirt accumulate.
- the physical conditions in the cyclone could be chosen so that the gas is subjected to isothermal, isochoric, isobaric or adiabatic changes in state. It is also conceivable that the gas maintains its physical properties assumed during gas generation when it passes through the cyclone. In addition, it is conceivable that individual physical properties of the gas are changed in the cyclone as a result of physical conditions suitably set by the operator. This means that the cyclone can be used variably. Other cyclones of this type are also conceivable within the gas generator, possibly for the pre-separation of solids.
- the gas could be cooled to the condensation temperatures of selected gas components. This ensures that certain reactions can be selectively excluded, whereas other reactions take place.
- the gas could be cooled by a tube bundle heat exchanger.
- This configuration has the advantage that high turbulence is generated in the individual tubes by high speeds, which ensures high heat transfer rates. Steam is generated on the secondary side.
- the tube bundle heat exchanger could be designed in the sense of a "transfer line exchanger".
- the gas could be cooled from approx. 800 ° C to approx. 310 ° C in the first step.
- This embodiment of the method ensures quenching or freezing of Boudouard back reactions, the synthesis products of which are extremely temperature-dependent.
- This special embodiment of the method can rule out an unfavorable carbon monoxide to carbon dioxide ratio in the process gas.
- the gas could be introduced into a funnel-shaped tube and the liquid could be supplied tangentially to produce a rotating liquid.
- This embodiment of the method has the advantage that a Conical surface of the tube is flushed with liquid, which prevents the accumulation of condensing gas components on possibly tearing open liquid films at the inlet of the hot gas.
- the rotation of the liquid prevents dry spots from forming which act as reaction nuclei for undesired reactions. In this respect, induction of undesirable reactions is effectively prevented.
- the liquid could be passed through a narrowest point of the funnel-shaped tube designed as an annular gap, the liquid being atomized into extremely fine droplets by increasing the speed.
- This has the advantage that the gas is quickly cooled in direct liquid contact, which allows the gas to absorb the liquid until it is completely saturated.
- the heat of vaporization of the liquid supplied - for example water - ultimately leads to the cooling of the gas.
- This special design leads to the formation of a sufficient number of condensation nuclei in the form of saturated water vapor and water droplets, which serve for the attachment and binding of particles and compounds to be washed out, such as sulfur and nitrogen compounds.
- long- and short-chain hydrocarbons as well as fine particles of residual ash and similar particles that could not be separated from the upstream cyclone can be deposited.
- the increase in speed of the liquid creates a relative speed between the gas flow and the liquid droplets, as a result of which liquid droplets and pollutant particles collide and adhere to one another.
- the gas could be passed through a Venturi scrubber.
- the use of such a device has the advantage of easy commercial availability.
- the gas could be cooled from approximately 310 ° C to approximately 75 ° C in the second step. The combination of the rapid cooling of the gas in the heat exchanger and the sudden cooling to 75 ° C reduces the possibility of new formation of dioxin compounds.
- the pH of the liquid could be adjusted depending on the pollutants to be precipitated. This measure enables selective washing out of pollutants.
- Acidic liquid preferably at a pH of about 5 or 6, could be used. Using this pH enables effective removal of alkaline compounds.
- the liquid could contain sulfuric acid to precipitate ammonia.
- sulfuric acid is advantageous in that sulfuric acid is easily available, can be stored and can be transported by trained laboratory personnel. In this respect, only the usual safety precautions must be taken, which are prescribed when handling common acids.
- the gas could be passed through a droplet separator. This ensures that entrained liquid drops can be removed from the gas.
- the gas could be led upwards and exposed to centrifugal forces by baffles so that contaminated liquid droplets are deposited on the outer wall of the droplet separator.
- the liquid could be fed to a circulation container.
- the liquid can advantageously be used several times by being supplied to the gas again.
- a first partial flow of the liquid could be fed to the funnel-shaped tube or, if necessary, to a venturi scrubber.
- this configuration enables the liquid to be separated into two partial flows, only the less heavily contaminated partial flow being fed back into the gas. As a result, the degree of separation can be increased.
- the second partial flow could be fed to a failure device and a separation basin. This measure advantageously ensures that heavy metals, dust particles or tar components can be separated from the cleaning liquid.
- the gas could be cooled by liquid. This enables pollutants remaining in the gas to be absorbed again by liquid.
- the gas could be passed through a swirling liquid bath.
- the provision of a swirling liquid bath ensures that hot gas almost does not come into contact with hot reactor walls, which can reduce undesired reactions.
- the gas could be cooled from about 75 ° C to about 40 ° C. Cooling to this temperature enables water and similar liquids in the gas to condense out, the condensation temperature of which is below 75 ° C. at the given process pressures.
- the pH of the liquid could be regulated depending on the pollutants to be precipitated. This enables a selective washing out of remaining pollutants in the gas.
- Alkaline liquid preferably at a pH of about 8 or 9, could be used.
- the use of a liquid basic environment enables neutralization of acidic components in the gas.
- Sodium hydroxide solution could be added to the liquid to absorb acidic components.
- the use of caustic soda does not exceed the usual requirements for the prescribed safety precautions when operating a process plant. Laboratory staff or chemists do not have to be trained in how to use the cleaning fluid.
- the gas could be introduced tangentially into a cylindrical body.
- the tangential introduction advantageously causes larger particles that are in the gas to be separated by centrifugal forces that arise.
- the gas could be passed from bottom to top in countercurrent with the liquid through the cylindrical body in such a way that a highly turbulent fluidized bed is created.
- This embodiment of the method advantageously has the effect that the gas is contacted with a large mass transfer area. As a result, a very high degree of separation of remaining pollutants in the gas is achieved.
- the gas could be passed through baffles arranged one above the other. This special guidance of the gas enables the formation of streamlines, through which very special entrainment effects are brought about, which ultimately realize an optimal speed distribution in the entire gas stream.
- the gas could be greatly accelerated by stacking vane rings before leaving the cylindrical body. This step has the effect that, in addition to centrifugal forces, especially inertial forces act on small droplets and separate them in the cylindrical body.
- the separated liquid could be passed through a cone with a built-in vortex brake.
- the separated liquid is collected and discharged effectively without any further fluid droplets being generated by possible turbulence, which return to the gas that has already been freed from liquid.
- the liquid could be collected in a circulation container and fed to washing liquid coolers in a quantity-controlled manner. This measure enables the liquid to be reused as required in individual process steps that use the liquid for cooling or cleaning purposes. After cooling, the liquid could be fed back into the gas at the head of the cylindrical body. In a very particularly advantageous manner, liquid contaminated with only a few pollutants can be used primarily for cooling already largely cleaned gas.
- the liquid could be cooled to about 40 ° C.
- the choice of this temperature enables a circulation of already separated liquid only for cooling purposes. Economical use of fluids can be achieved here in a particularly effective manner.
- the excess liquid from the circulation tank could be fed to a circulation tank used for the second cooling step.
- this step realizes that liquid can be exchanged between individual process steps as required.
- Light hydrocarbons could be supplied to the circulation tank through the excess liquid, which increases the concentration of light hydrocarbons and aromatics in the circulation tank.
- the hydrocarbons and aromatics are not separated in order to feed them to another recycle tank for further applications.
- this process step enables light hydrocarbons and aromatics in particular to be used selectively in further process steps.
- the light hydrocarbons and aromatics contained in the liquid could be used as extractants. This eliminates the need for external extraction agents, which considerably simplifies the process. Components that have already been extracted from the gas are used in a refined way to extract remaining pollutants from the gas. As a result, a particularly effective process step is indicated both in ecological and in economic terms.
- the extractant could be used for tars contained in the gas. A targeted and highly efficient washing out of the tars without the addition of external extraction agents is advantageously ensured.
- Diesel oil could be used as an additional extractant.
- the use of diesel oil represents a process step that is characterized by the fact that the extractant is readily available and disposable. In addition, it is easily possible to reuse the diesel oil used.
- the gas could leave the cylindrical body at its dew point.
- the choice of the dew point as the temperature at the time the gas escapes from the cylindrical body enables liquids saturated in the gas to condense out when the gas leaves.
- the gas could be fed to a bladder in which an alkaline liquid supply is pumped out to wash out the gas.
- a bladder advantageously allows the gas to be treated on a small volume. In addition, little investment is required to use the bladder to perform the procedure effectively.
- the use of an alkaline liquid supply enables the removal of hydrogen sulfide still remaining in the gas.
- the pH value can be adjusted by adding lye to the pumped liquid.
- the gas could be led out of the bladder through a container with a liquid receiver containing a deionized water.
- a liquid receiver containing a deionized water As a result, lye droplets that are entrained in the bladder apparatus can be retained.
- this process step contributes to the process gas at the outlet of this container being cleaned of all contaminants.
- the gas could be cooled with a refrigeration system.
- the gas saturated with liquid after the liquid washing is cooled with a refrigeration system, so that remaining liquids can be effectively condensed out.
- the use of a refrigeration system prevents the gas from coming into contact with other liquids.
- the gas could be cooled to around 5 ° C to 15 ° C.
- the use of this particular temperature is essentially determined by the hydrate point of the gas, which can be different for different gas compositions and different operating temperatures of the gas generator. The use of this special temperature enables optimum gas purity, which enables the cleaned gas to be used safely in a downstream gas engine.
- the cooling system could be operated to cool the gas with thermal energy obtained from the upstream process. In terms of process economy, this ensures an advantageous embodiment, since almost no external energy has to be used.
- the cleaned gas could be fed to a fixed bed to crack dioxins and furans. This can remove extremely toxic gas components.
- the temperature of the gas could be raised above its dew point. This ensures that suitable reaction conditions are present in the cracking of dioxins and furans, which ensure effective removal of the gas from dioxins and furans.
- the heat energy absorbed in circulation tanks or separating tanks could be used as domestic heat via heat exchangers.
- thermal energy generated during the process is used particularly advantageously, as a result of which the use of external energy is minimized.
- Catalytic materials could be added to the circuit.
- the use of catalytic materials selectively enables certain reactions to be accelerated without the need to replace the catalysts.
- the catalytic materials contained in the circulation containers can be circulated.
- the components contained in the circulation containers could be separated off by means of filtration systems, in particular ultrafiltration systems. These outcomes The process is designed to filter heavy metals and compounds that are difficult to dispose of.
- the filters also enable separated components to be selectively removed from the circulating liquid, which enables the circulating liquid to be used again.
- Heavy metals could be collected from residual sludge and concentrated to a small residual volume using used heat in filter press processes. In terms of process economics, this process step not only generates energy, but rather specifies a process that considerably simplifies the disposal of heavy metals due to their highly concentrated accumulation in small volumes.
- Fig. 1 is a schematic diagram of a first embodiment of the method for purifying gas
- Fig. 2 is a schematic diagram of a second embodiment of the method for purifying gas according to the invention.
- FIG. 3 shows a schematic diagram for gas purification.
- FIG. 1 shows a schematic diagram of the first exemplary embodiment of the method for purifying gas 1 according to the invention.
- the gas 1 which is generated in the gas generator is removed through a cyclone 2 to remove solids under adjustable physical conditions.
- the physical conditions in Cyclone 2 are matched to the gas to be cleaned.
- the pipe connections from the gas generator to the cyclone 2 are very well insulated and made of heat-resistant material.
- the pipe dimensions are selected so that high flow velocities are generated and the pressure loss of the gas 1 is optimized with regard to the downstream process.
- the heat exchanger 3 is arranged downstream of the cyclone 2 in such a way that the gas 1 enters the heat exchanger 3 after leaving the cyclone 2.
- the hot gas 1 with a temperature between 700 ° C and 900 ° C is suddenly cooled to about 300 ° C in the heat exchanger 3. This is done by passing the gas 1 through a tube bundle of thin tubes.
- the heat exchanger 3 is designed as a “transfer line exchanger”. High speeds in the individual tubes generate high turbulence, so that high heat transfer rates are generated. Steam is generated on the secondary side.
- the gas 1 cooled in the heat exchanger 3 enters the venturi scrubber 4 immediately after leaving the heat exchanger 3 and is saturated in direct contact with injected washing water and thereby suddenly cooled again to approx. 75 ° C.
- the gas 1 is introduced into a funnel-shaped tube 5, to which water is supplied tangentially to produce a swirling water bath.
- the water is passed through a narrowest point of the funnel-shaped tube 5, which is designed as an annular gap 6 and is atomized into extremely fine droplets by increasing the speed.
- the saturated and partially cleaned gas 1 enters a droplet separator 7.
- the gas 1 is guided from bottom to top through the droplet separator 7 and is subjected to centrifugal forces by guide plates in such a way that liquid droplets containing pollutants are deposited on the outer wall of the droplet separator 7.
- the deposited liquid is fed to a circulation container 8.
- a partial flow of the liquid is fed to the venturi scrubber 4 from the circulation tank 8.
- On second partial flow is fed to a failure device and a separation basin 14.
- the gas 1 enters the droplet separator 7 into the cylindrical body 9, which is designed as a washing column.
- the gas 1 is introduced tangentially into the cylindrical body 9. This creates centrifugal forces that separate larger particles still in gas 1.
- the gas 1 flows in countercurrent with circulating water through the cylindrical body 9.
- the pH of the circulating water is adjusted to approximately 8 to 9 by metering in sodium hydroxide solution. As a result, acidic components contained in the gas are absorbed.
- the gas 1 is guided from bottom to top in countercurrent with the circulating water through the cylindrical body 9 in such a way that a highly turbulent water fluidized bed is formed.
- the gas 1 is passed through baffles 10 arranged one above the other. Pollutants to be separated are bound to the circulating water and run off together with the droplets on the wall of the cylindrical body 9.
- the gas 1 is greatly accelerated by stacked vane rings, whereby remaining small drops are separated.
- the separated water is led over a cone with a built-in vortex brake.
- the separated water is collected in a circulation tank 11 and fed to washing water coolers 12 in a quantity-controlled manner.
- the water is fed to the gas 1 again after cooling to about 40 ° C. at the top of the cylindrical body 9. Furthermore, an excess of the water from the circulation tank 11 is fed to the circulation tank 8 in a quantity-controlled manner, so that the water in the venturi scrubber 4 can be used again.
- Condensed tars and residual ash components are concentrated in the circulating water of the Venturi scrubber 4. Due to the excess water that occurs during gas cooling, a wastewater flow is discharged from the circuit of the Venturi scrubber in a level-controlled manner. This stream is fed through a backwashable filter system. This involves solid components and tars deposited. When the pressure rises, the filter automatically backflushes to a hydrocyclone 13. The solid components separated there are fed to a separation basin 14 via a double-valve system. The waste water stream is passed into the separating tank 15, where liquid hydrocarbons are separated. The remaining waste water is discharged into the sewage system to the waste water system.
- the excess water portion of the gas 1 condenses out in the cylindrical body 9.
- the gas 1 leaves the cylindrical body 9 at its head at about 40 ° C. after cooling by the circulating water.
- the cleaned gas 1 is free from tars, acidic and alkaline constituents and essentially consists only of hydrogen, methane, carbon monoxide and carbon dioxide.
- the gas is fed directly to gas turbines, gas engines or high-temperature fuel cells. Part of the gas 1 is used to heat burners.
- FIG. 2 schematically shows a diagram of the second exemplary embodiment of the method according to the invention for purifying gas 1.
- the gas 1 is washed via the Venturi scrubber 4 and the droplet separator 7.
- the wash water is kept slightly acidic, with a pH of 5 to 6 being adjusted by adding sulfuric acid.
- the gas 1 is cooled by saturation with liquid and ammonia is completely absorbed. Solids are also discharged.
- a slight hydrocarbon fraction occurs in the cylindrical body 9 during the condensation.
- the hydrocarbon fraction is returned to the Venturi scrubber 4. led, whereby an increased concentration of light hydrocarbons in the gas stream between Venturi scrubber 4 and cylindrical body 9 is formed.
- the light hydrocarbons have an extractive effect on the tars contained in the gas 1 and wash the tars both in the washing circuit of the Venturi scrubber 4 or droplet separator 7 and in the washing circuit of the cylindrical body 9.
- the gas 1 leaves the cylindrical body 9 at its dew point. Here there is still hydrogen sulfide in the gas 1.
- the hydrogen sulfide is removed in a bubble device 16.
- a slightly alkaline water supply is pumped around in the bubble device 16. The pH value is adjusted by adding lye to the pumped water. The excess of the pumped water is led to the separating tank 15.
- the gas 1 flows from the bladder 16 through a further container 17, which contains a water reservoir with a deionized water.
- the container 17 holds back entrained lye droplets.
- the gas 1 leaves the container 17 and is free of all contaminants.
- FIG. 3 schematically shows a diagram for gas purification, which is subordinated to the method steps already explained.
- the gas 1 is cooled to about 5 ° C. to 15 ° C. by a refrigeration system 18.
- the refrigeration system 18 is operated with thermal energy from the process, so that no external energy has to be used.
- the condensed liquid portion is passed into the separating tank 15.
- the cooled, finely cleaned gas is reheated in the cooler 20 and is available for use in burners, gas engines or other energy generation devices.
- the finely cleaned gas 1 is free from contaminants and tars and enables long operating times and low maintenance of the gas engines.
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP02745077A EP1549412A1 (de) | 2002-05-03 | 2002-05-23 | Verfahren zur reinigung von gas |
AU2002317158A AU2002317158A1 (en) | 2002-05-03 | 2002-05-23 | Method for purifying gas |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10220000 | 2002-05-03 | ||
DE10220000.9 | 2002-05-03 | ||
DE10223030A DE10223030A1 (de) | 2002-05-03 | 2002-05-22 | Verfahren zur Reinigung von Gas |
DE10223030.7 | 2002-05-22 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003092859A1 true WO2003092859A1 (de) | 2003-11-13 |
Family
ID=29403583
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/DE2002/001872 WO2003092859A1 (de) | 2002-05-03 | 2002-05-23 | Verfahren zur reinigung von gas |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP1549412A1 (de) |
AU (1) | AU2002317158A1 (de) |
WO (1) | WO2003092859A1 (de) |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
NL8101446A (nl) * | 1981-03-24 | 1981-11-02 | Shell Int Research | Werkwijze voor het zuiveren van een vliegas bevattend gas. |
EP0208156A1 (de) * | 1985-06-11 | 1987-01-14 | von Beckerath, Kurt, Dr.rer.nat.,Dipl.-Chem. | Verfahren und Anlage zur weitgehenden Restentfernung von Schadstoffen aus Abgasen von Verbrennungsanlagen |
US4704972A (en) * | 1986-01-14 | 1987-11-10 | Societe Dite: Sogea | Method and apparatus for reducing acid pollutants in smoke |
US4738835A (en) * | 1985-05-22 | 1988-04-19 | A. Ahlstrom Corporation | Method of recovering alkali chemicals from flue gases containing alkali metal vapor |
DE4424367A1 (de) * | 1994-07-11 | 1996-01-18 | Siemens Ag | Verfahren und Einrichtung zur Reinigung von Rauchgas |
-
2002
- 2002-05-23 EP EP02745077A patent/EP1549412A1/de not_active Withdrawn
- 2002-05-23 AU AU2002317158A patent/AU2002317158A1/en not_active Abandoned
- 2002-05-23 WO PCT/DE2002/001872 patent/WO2003092859A1/de not_active Application Discontinuation
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
NL8101446A (nl) * | 1981-03-24 | 1981-11-02 | Shell Int Research | Werkwijze voor het zuiveren van een vliegas bevattend gas. |
US4738835A (en) * | 1985-05-22 | 1988-04-19 | A. Ahlstrom Corporation | Method of recovering alkali chemicals from flue gases containing alkali metal vapor |
EP0208156A1 (de) * | 1985-06-11 | 1987-01-14 | von Beckerath, Kurt, Dr.rer.nat.,Dipl.-Chem. | Verfahren und Anlage zur weitgehenden Restentfernung von Schadstoffen aus Abgasen von Verbrennungsanlagen |
US4704972A (en) * | 1986-01-14 | 1987-11-10 | Societe Dite: Sogea | Method and apparatus for reducing acid pollutants in smoke |
DE4424367A1 (de) * | 1994-07-11 | 1996-01-18 | Siemens Ag | Verfahren und Einrichtung zur Reinigung von Rauchgas |
Also Published As
Publication number | Publication date |
---|---|
AU2002317158A1 (en) | 2003-11-17 |
EP1549412A1 (de) | 2005-07-06 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE3121206C2 (de) | Verfahren zum Vergasen fester Abfälle | |
DE69405841T2 (de) | Energiewirksame Filtration von Synthesegas Kühl- und Waschwässern | |
DE3784692T2 (de) | Verfahren zur verbesserung der qualitaet des wassers angewendet zum kuehlen und waschen eines ungereinigten synthesegases. | |
DE69913994T2 (de) | Flash-pyrolyse in einem zyklon | |
DE60207735T2 (de) | Verfahren und anlage zur vergasung von biomassen | |
DE2914937A1 (de) | Verfahren zum herstellen eines sauberen, praktisch hcn-freien synthesegases | |
DE4240196C2 (de) | Verfahren zur Kühlung und Reinigung von ultrafeine Partikel enthaltendem Gas, insbesondere Gichtgas oder Generatorgas und Vorrichtung zu seiner Durchführung | |
EP0412587B1 (de) | Verfahren zum Reinigen von Rohbrenngas aus der Vergasung fester Brennstoffe | |
EP2262875B1 (de) | Verfahren und vorrichtung zur behandlung von bei der vergasung anfallenden fluidströmen | |
DE3102819A1 (de) | Verfahren fuer die rueckgwinnung von waerme bei der kohlevergasung und vorrichtung dafuer | |
EP0975414A1 (de) | Verfahren zum regenerieren einer beladenen waschflüssigkeit aus einer anlage zur gasentschwefelung | |
DE2609320B2 (de) | Kohlevergasungseinrichtung | |
DE2726552A1 (de) | Destillierverfahren und zugehoerige vorrichtung | |
DE2129231C3 (de) | Verfahren zur Abscheidung von Schwefeldioxid aus den Rauchgasen schwefelhaltiger Brennstoffe | |
EP2134648A2 (de) | Verfahren zur schwefelsäureerzeugung und anlage zur durchführung des verfahrens | |
EP3792216B1 (de) | Wärmeintegration bei der synthesegaserzeugung durch partialoxidation | |
DE2735090A1 (de) | Verfahren zur herstellung von wasserstoff und kohlenoxid enthaltenden prozessgasen | |
DE202015106840U1 (de) | Vorrichtung zur Behandlung von Feststoff beladenem Prozessabwasser | |
EP1549412A1 (de) | Verfahren zur reinigung von gas | |
EP0586837B1 (de) | Vorrichtung zur Kühlung von heissen Gasen | |
DE10223030A1 (de) | Verfahren zur Reinigung von Gas | |
DE3024469A1 (de) | Verfahren und einrichtung zur partialoxidation von kohlenstoffhaltigen feststoffen | |
DE10049227B4 (de) | Verfahen zur Gasreinigung von Prozeßgas aus Vergasungsverfahren | |
EP0515950B1 (de) | Herstellung von Synthesegas aus aschereichen Kohlenwasserstoffen | |
WO2014180923A1 (de) | Vorrichtung und verfahren zur behandlung von kondensat aus vergasungsanlagen |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CO CR CU CZ DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ OM PH PL PT RO RU SD SE SG SI SK SL TJ TM TN TR TT TZ UA UG US UZ VN YU ZA ZM ZW |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application | ||
WWE | Wipo information: entry into national phase |
Ref document number: 2002745077 Country of ref document: EP |
|
WWP | Wipo information: published in national office |
Ref document number: 2002745077 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: JP |
|
WWW | Wipo information: withdrawn in national office |
Country of ref document: JP |
|
WWW | Wipo information: withdrawn in national office |
Ref document number: 2002745077 Country of ref document: EP |