WO1987003506A2 - PROCESS FOR SINGLE OR MULTI-PHASE PREFERABLY SIMULTANEOUS SO2 AND NOx SEPARATION FROM FLUE GASES IN A WET PROCESS - Google Patents
PROCESS FOR SINGLE OR MULTI-PHASE PREFERABLY SIMULTANEOUS SO2 AND NOx SEPARATION FROM FLUE GASES IN A WET PROCESS Download PDFInfo
- Publication number
- WO1987003506A2 WO1987003506A2 PCT/EP1986/000693 EP8600693W WO8703506A2 WO 1987003506 A2 WO1987003506 A2 WO 1987003506A2 EP 8600693 W EP8600693 W EP 8600693W WO 8703506 A2 WO8703506 A2 WO 8703506A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- washing
- lime
- liquid
- wash water
- nox
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
-
- 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
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Definitions
- a method for simultaneous S02 and NOx separation from the flue gases of combustion boilers has already been proposed, a liquid containing additives such as limestone or hydrated lime and EDTA or NTA and / or polycarboxylic acids and CaS04 or CaS03 for washing is used, is activated as a partial quantity via a solid-liquid separation stage with delivery of the inactive liquid into a reaction vessel in which reduced additives are added, and is returned via an inlet level and / or via a pump and the wash water reservoir Nozzle pairs are made available again directly for the washing process, a part of the filtrate water being charged with N + S salts being introduced into the combustion chamber of the combustion boiler before it is activated and / or the fuel coal being fed into the combustion boiler before being supplied .
- additives such as limestone or hydrated lime and EDTA or NTA and / or polycarboxylic acids and CaS04 or CaS03 for washing is used
- Sodium bisulfite, ascorbic acid, sodium dithionite and similar reducing agents are preferably used as reducing agents in this process.
- the EDTA is precipitated and returned to the washing water circuit. This valuable feed product is thus returned to the scrubbing liquid circuit, which makes the process very economical, with only the actual waste water with the N + S compounds, which contribute to the S02 increase in the process, returning to the combustion chamber via the coal, so that the stoichiometric ratio of S02 to NOx is available to the desired extent.
- the EDTA is precipitated at a pH of 1 within the course of the wash water process in order to be able to reuse this valuable residue product.
- the washing liquid is reduced to a pH value 1 before the gypsum is separated without the supply of oxidizing air and that EDTA is precipitated and that the washing liquid is separated from the solids after the separation stage substances CaS03 and CaS04 freed, preferably by adding lime, raised to a pH value of neutral greater than 6 and with the N + S salts for setting the necessary ratio of S02 to NOx, preferably after being fed onto the coal, is fed to the combustion boiler.
- the mixture of CaS03 and CaS04 is fed in after oxidation.
- the neutralization with lime takes place, among other things, to prevent corrosion formation in the boiler.
- the pH of the gypsum sludge is reduced to 1 and EDTA is precipitated and that gypsum sludge treated in this way after neutralization, preferably with lime, optionally with the addition of gypsum Setting the necessary ratio of S02 to NOx, preferably on the fuel coal, is added before being fed into the boiler.
- the pH is reduced to 1 by adding a small amount of acid, for example sulfuric acid.
- This process according to the invention ensures that the valuable feed product EDTA can be recovered and returned to the washing cycle.
- S02 is released during their thermal decomposition after introduction into the combustion boiler, so that the ratio of S02 to NOx in the raw gas stream and thus relevant to the process can be precisely controlled without external additives , such as Pyrosulfite, sodium sulfite, SO 2 rich gas, elemental sulfur or other highly sulfur-containing compounds which participate in the combustion process and produce SO 2 must be added.
- the invention it is therefore proposed not to introduce NH3 into this area, but rather to add ammonium salts of organic or inorganic bonds above the furnace bed.
- the granulate has a certain size, which, with a certain humidity, guarantees that the zone of the best conversion is always passed above after the ember bed.
- the ammonium salts are prepared in such a way that they are fed in according to the gas velocity in the boiler above the ember bed in order to pass through a long zone with a long residence time.
- the invention proposes that hydrated lime or limestone be added to the suction line of the washing water circulation pump.
- the amount of lime added is controlled stoichiometrically in accordance with the amount of flue gas pollutant.
- a part of the water from the main wash water circuit is fed to a gravity separator for the separation of solids.
- the partial flow of water freed from solids is returned to the sump. This partial amount of water is circulated in a closed circuit.
- the solid (approx. 30%) thickened in a gravity separator is dewatered via a dewatering station.
- the drained Solid is discharged and fed to an oxidation station in order to convert the calcium sulfite portion into calcium sulfate dihydrate.
- the filtrate is returned to the gravity separator.
- the addition of reducing agents takes place in the inner jacket of the gravity separator, since it was found that a sufficient residence time is very advantageous for the reduction of iron-III to iron-II.
- the lime addition must not be added to a partial water cycle with a precipitation tank, since otherwise the lime load per liter of wash water is too high (eg 1.5-6.0 g Ca (OH) 2 / l wash water). This can result in local pH values up to pH 12 in the wash water and can lead to a disruption of the sulfite-sulfate ratio. In addition, there may also be little iron degradation from the iron chelate complex.
- the lime is added over the entire wash water circuit. This is advantageously done via the metering into the suction line or in the pump reservoir of the wash water circulation pumps.
- the washing water circuit with solids (CaS04 x 2 H20 / CaS03 x 1/2 H20) as seed crystals prevents plaster oversaturation of the washing solution.
- a wet separator is switched to the wash water circuit of which calcium hydrate is metered in, calcium sulfite and calcium sulfate being formed from the sulfur oxides.
- trimercapto-triazine is added to the wash water as active substance.
- trimercapto-s-triazine is expediently used in the form of the sodium salt.
- the solids formed consisting of the residue product CaS03, CaS04, the free Ca0H2 with the heavy metals bound to trimercapto-s-triazine, mercury, cadmium and nickel, form poorly soluble stable compounds in water.
- This mercury compound for example, only decomposes above 210 ° C., even under these conditions no mercury is released, but other more stable compounds are formed. It has been shown from the deposited products that mercury does not leach out.
- nitrogen oxides from exhaust gases by aqueous solutions e.g. Contain iron-II-ethylenediamine tetraacetate or other complex compounds of iron or cobalt, can be absorbed.
- nitrous oxide (N20) and nitrogen-sulfur compounds such as nitrilotrisulfonic acid, smidosulfonic acid, amidosulfonic acid, hydroxysulfonic acid and similar compounds, are formed in addition to nitrogen (N2).
- reaction (1) By adding a sufficient amount of ammonium ions to the solution which contains the metal complex and which absorbs the nitrogen oxides from the exhaust gases, the reaction (1) can take place in a known manner at temperatures of about 40-90 degrees C.
- ammonium sulfate is first added to the solution.
- the further consumption of ammonium can be supplemented by gaseous ammonia, ammonium hydroxide or urea.
- the iron III complex oxidized by oxygen from the exhaust gas can advantageously be reduced electronically in electrolysis cells, but also in a known manner by means of other reducing agents, v / ie hydrazine or dithionite.
- the nitrogen oxide reduction is independent of the S02-N0 molar ratio.
- the process can be used behind existing flue gas desulfurization plants. 3.
- the method can additionally be used in the case of simultaneous washing methods if the S02-NO molar ratio is not sufficient and has to be adjusted by cost-intensive measures.
- the process is free of waste water if the iron reduction is carried out electrochemically by means of electrolysis and NH3 is metered in such that no residual products remain.
- the method can be used for S02-free or S02-poor flue gases.
- this is achieved by ultrasonically stimulating the liquid and / or by vibrating the liquid, which is attached to the walls, to set both into vibrations, i.e. the washing liquid and the individual electrolysis elements; additionally also the membranes, which are now continuously pulsed around by the ultrasound-excited and thus vibrating washing liquid, and which make it possible for incrustations to fall off.
- excitation of the liquid and the cleaning and excitation of the membranes and the insertion elements are preferred effected in the cell with ultrasound and thus not subjected to material fatigue as is the case with vibrators.
- the invention it is therefore proposed to use a two-stage separation of SO2 and NOx, in which In the first stage, the normal known S02 washing takes place over limestone or hydrated lime, and in the second stage, according to the invention, a sodium hydroxide washing solution is used for NOx separation, in which the residual emission S02 from the first stage is reduced with the NOx via the electrolysis in such a way that Cleaved N2 is transferred to the atmosphere and sodium sulfate is discharged as the end product.
- the sodium hydroxide solution is provided with an EDTA complex, which is approximately 40 g / l and etv / a has 6 g iron complex, this iron complex being kept active according to the invention with the washing solution via an electrolysis cell by reducing iron III to iron II .
- a second washing stage is operated, which is operated with sodium hydroxide solution, in which an EDTA or NTA complex is mixed in, preferably by 40 g / l, this EDTA complex preferably having at least one Contains 6 g iron complex and the entire washing liquid for reducing the iron is passed through an electrolysis cell.
- the electrolytic cell does not end in a flat bottom, as is known, but instead a swamp-like device arrangement is provided at the end of the cell surfaces, which is provided with a sludge opening valve which is opened in corresponding time amplitudes In order to remove the solid which settles in the lower part of the electrolysis cell - preferably by sink separation - increased by ultrasound and / or vibration to open the controlled valve in the sludge of the electrolysis cell and to hand it over to the process.
- the sump is also emptied by a density measuring device in corresponding time amplitudes, so that even with very strong solids-containing washing liquids to be treated electrolytically electrolytic treatment with high solids density is feasible.
- s is known to bind flue gas by dry hydrated lime in the area of a spray absorber or a contact section.
- the separation of e.g. around 95% S02 means in spray absorbers that a moisture is added which cools the gas almost to the dew point, and consequently a reheating is necessary for the gas to be released into the chimney after the filter.
- a two-stage decision Ab ⁇ provide before a fabric filter, said dry process in the first stage and in the second Stage the rest is separated by wet technology, the gas being cooled only as far as is necessary for the separation, and thus flue gases with temperatures of, for example, 140 degrees C after the boiler only have to be cooled to about 90 degrees C and not, as in wet spray absorption, for example up to 70 degrees C, in order to achieve a deposition of 95%.
- this separation system is achieved in spite of the high temperature maintenance by the fact that, for gas separation with a low temperature drop, the hydrated lime in front of the fabric filter causes a separation performance of about 70% and more, based on the raw gas load, and the used lime from the fabric filter only slightly moistened is passed to the spray absorber in order to be separated from it as used lime from the process.
- FIG. 1 shows a process with integrated water treatment and lime addition
- Figure 2 is a view of an electrolytic cell and FIG. 3 shows a two-stage deposition process in front of a fabric filter.
- the scrubber 1 As can be seen from FIG. 1, in the scrubber 1 the incoming raw gas 2 is washed with circulated wash water via a pump and the wash circuit line 4 and leaves, freed from pollutants, via the clean gas line 3 the scrubber.
- Lime hydrate or limestone 5 is added to the suction line of the wash water circulation pump 6.
- the amount of lime added is controlled stoichiometrically according to the amount of flue gas.
- a part of the water from the main wash water circuit for the separation of solids is fed via line 7 to a gravity separator 13.
- the partial flow of water freed from solids is returned to the laundry sump.
- the bypassing of this partial water quantity is a closed cycle.
- the solid (approx. 30%) thickened in the gravity separator 13 is dewatered via a dewatering station 9.
- the dewatered solid is discharged at 10 and one oxidation station in order to convert the calcium sulfite portion into calcium sulfate dihydrate.
- the fil is returned via line 11 to the gravity separator.
- the lime is added over the entire wash water circuit. This is advantageously done via the metering in the suction line or in the pump reservoir 5 of the wash water circulation pumps.
- 21 denotes the housing of an electrolysis cell.
- the electrolytic cell there are, for example, two electrolytic cell bodies 22 arranged at a distance from one another.
- the electrolytic cell bodies 22 are superimposed by the diaphragm 23.
- the washing liquid 24 to be treated electrolytically is located inside the housing.
- a conical sump 25 is provided below the electrolytic cells.
- the outlet of the conical sump 25 has a controllable sump slide 26.
- the vibration exciter attached to the housing 21 of the cell body is designated by 27.
- An ultrasound device 28 is arranged above the electrolysis cells.
- a further ultrasonic device 29 is located on the conical sump 25.
- the density measuring devices 30 extend into the conical sump 25.
- the raw gas is 31, a spray absorber 32, a fresh lime supply 33. with 34 a fabric filter, with 35 a lime moistening station, with 36 the supply of lime into the spray absorption and with 37 the separation of the used lime.
- this separation system is achieved by entering hydrated lime at 33 dry, and here with e.g. 60-70% separation in the contact section 33 and in the filter 34 is achieved without adding moisture and without lowering the temperature, since these surfaces of the contact section and the filter are insulated, so that only a deposit of less than 30% in the spray absorber at low humidity is achieved must be given.
- a temperature e.g. by 90 degrees C, which is sufficient to transfer the cleaned exhaust gases to the chimney according to the dispersion calculation without reheating.
- a two-stage separation of S02 at a low temperature drop is achieved by introducing the limestone at 33 with the highest contact separation performance into the contact section 33 using dry technology, and after contacting below the filter at 35, the used lime is moistened and is fed to spray absorption at 36.
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Abstract
Description
Claims
Applications Claiming Priority (18)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DEP3542907.0 | 1985-12-04 | ||
DE19853542907 DE3542907A1 (en) | 1984-08-11 | 1985-12-04 | Process for simultaneously separating out SO2 and NOx from the flue gases of combustion boilers |
DEP3600270.4 | 1986-01-08 | ||
DE19863600270 DE3600270A1 (en) | 1986-01-08 | 1986-01-08 | Simultaneous SO2 and NOx separation in the high temperature region and in the simultaneous wet technique region |
DEP3601454.0 | 1986-01-20 | ||
DE19863601454 DE3601454A1 (en) | 1986-01-20 | 1986-01-20 | Process for removing HCl, HF, SO3, SO2 and NOx from combustion exhaust gases by simultaneous wet scrubbing with controlled scrubbing water circulation and specific addition of lime |
DEP3603984.5 | 1986-02-08 | ||
DEP3604063.0 | 1986-02-08 | ||
DE19863604063 DE3604063A1 (en) | 1986-02-08 | 1986-02-08 | Gas purification downstream of waste incineration plants |
DE19863603984 DE3603984A1 (en) | 1986-02-08 | 1986-02-08 | Process for separating off nitrogen oxides from exhaust gases |
DEP3604801.1 | 1986-02-15 | ||
DE19863604801 DE3604801A1 (en) | 1986-02-15 | 1986-02-15 | Electrolysis with vibratory agglomeration for preferably gypsum-containing residues in the scrubbing solution |
DE19863607282 DE3607282A1 (en) | 1986-03-06 | 1986-03-06 | Process for separating off SO2 and NOx from flue gases |
DEP3607282.6 | 1986-03-06 | ||
DEP3609807.8 | 1986-03-22 | ||
DE3609807 | 1986-03-22 | ||
DEP3610408.6 | 1986-03-27 | ||
DE19863610408 DE3610408A1 (en) | 1986-03-27 | 1986-03-27 | Two-stage semi-dry desulphurisation process |
Publications (2)
Publication Number | Publication Date |
---|---|
WO1987003506A2 true WO1987003506A2 (en) | 1987-06-18 |
WO1987003506A3 WO1987003506A3 (en) | 1987-07-16 |
Family
ID=27575910
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1986/000693 WO1987003506A2 (en) | 1985-12-04 | 1986-11-29 | PROCESS FOR SINGLE OR MULTI-PHASE PREFERABLY SIMULTANEOUS SO2 AND NOx SEPARATION FROM FLUE GASES IN A WET PROCESS |
Country Status (2)
Country | Link |
---|---|
EP (1) | EP0248855A1 (en) |
WO (1) | WO1987003506A2 (en) |
Cited By (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0531726A1 (en) * | 1991-08-29 | 1993-03-17 | Dravo Lime Company | Process for removing sulfur dioxide and nitrogen oxides from flue gases |
WO2005035103A1 (en) * | 2003-08-19 | 2005-04-21 | Wuhan Kaidi Electric Power Co., Ltd. | A reaction tower for dry desulfurizating flue gas |
CN102614735A (en) * | 2012-04-13 | 2012-08-01 | 大连华氏流体设备有限公司 | Device and method for smoke desulphurization and waste recycle |
CN103611384A (en) * | 2013-12-10 | 2014-03-05 | 中国石油大学(华东) | Ultrasonic-assisted spraying drainage and atomization dust removal device |
CN105080317A (en) * | 2014-05-05 | 2015-11-25 | 淮南市明月环保科技有限责任公司 | Method for simultaneously reclaiming sulfur and nitrate |
CN105251330A (en) * | 2015-11-09 | 2016-01-20 | 武汉钢铁(集团)公司 | Technology of synchronous desulfurization and denitration through flue gas ammonia method based on electrolytic regeneration iron removal |
CN105833696A (en) * | 2016-05-06 | 2016-08-10 | 陈佐会 | Ultrasonic desulfuration, denitration and dust removal method |
CN109233775A (en) * | 2018-09-25 | 2019-01-18 | 中国石油化工股份有限公司 | A kind of scavenger and preparation method thereof of thick oil thermal extraction sulfur-bearing gas with foreign flavor |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2919235A (en) * | 1956-11-06 | 1959-12-29 | Paul S Roller | Electrolytic method and apparatus for the production of metal hydroxide |
GB1245854A (en) * | 1968-08-31 | 1971-09-08 | Montedison Spa | Removal of nitric oxide from industrial gases |
US3755161A (en) * | 1970-02-05 | 1973-08-28 | Osaka Soda Co Ltd | Treatment process for removal of metals and treating agent therefor |
DE2703157A1 (en) * | 1976-01-26 | 1977-07-28 | Babcock Hitachi Kk | Nitrogen oxide and sulphur oxide removal from combustion gas - by treatment with lime suspension contg. ferrous chelate and oxidn. of calcium sulphite formed |
FR2486818A1 (en) * | 1980-07-18 | 1982-01-22 | Rhone Poulenc Ind | Nitrogen oxide removal from waste gas - by contact with aq. tetra:valent cerium salt and nitrate ions in redox reactions |
DE3418285A1 (en) * | 1983-05-20 | 1984-12-20 | Hölter, Heinz, Dipl.-Ing., 4390 Gladbeck | Process for scrubbing out SO2, HCL, HF, NOx and other pollutants from the flue gas downstream of, preferably, fossil-fuel power stations |
DE3324668A1 (en) * | 1983-07-08 | 1985-01-17 | Ekkehard Prof. Dr.-Ing. 4300 Essen Weber | Process for the disposal of nitrogen oxide using organic nitrogen compounds |
WO1985003238A2 (en) * | 1984-01-25 | 1985-08-01 | Hoelter Heinz | Process for stripping nitrogen oxides and sulphur oxides as well as optionally other noxious elements of flue gas from combustion plants |
-
1986
- 1986-11-29 WO PCT/EP1986/000693 patent/WO1987003506A2/en not_active Application Discontinuation
- 1986-11-29 EP EP87900093A patent/EP0248855A1/en not_active Ceased
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2919235A (en) * | 1956-11-06 | 1959-12-29 | Paul S Roller | Electrolytic method and apparatus for the production of metal hydroxide |
GB1245854A (en) * | 1968-08-31 | 1971-09-08 | Montedison Spa | Removal of nitric oxide from industrial gases |
US3755161A (en) * | 1970-02-05 | 1973-08-28 | Osaka Soda Co Ltd | Treatment process for removal of metals and treating agent therefor |
DE2703157A1 (en) * | 1976-01-26 | 1977-07-28 | Babcock Hitachi Kk | Nitrogen oxide and sulphur oxide removal from combustion gas - by treatment with lime suspension contg. ferrous chelate and oxidn. of calcium sulphite formed |
FR2486818A1 (en) * | 1980-07-18 | 1982-01-22 | Rhone Poulenc Ind | Nitrogen oxide removal from waste gas - by contact with aq. tetra:valent cerium salt and nitrate ions in redox reactions |
DE3418285A1 (en) * | 1983-05-20 | 1984-12-20 | Hölter, Heinz, Dipl.-Ing., 4390 Gladbeck | Process for scrubbing out SO2, HCL, HF, NOx and other pollutants from the flue gas downstream of, preferably, fossil-fuel power stations |
DE3324668A1 (en) * | 1983-07-08 | 1985-01-17 | Ekkehard Prof. Dr.-Ing. 4300 Essen Weber | Process for the disposal of nitrogen oxide using organic nitrogen compounds |
WO1985003238A2 (en) * | 1984-01-25 | 1985-08-01 | Hoelter Heinz | Process for stripping nitrogen oxides and sulphur oxides as well as optionally other noxious elements of flue gas from combustion plants |
Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0531726A1 (en) * | 1991-08-29 | 1993-03-17 | Dravo Lime Company | Process for removing sulfur dioxide and nitrogen oxides from flue gases |
TR27881A (en) * | 1991-08-29 | 1995-10-11 | Dravo Lime Co | The method for removing sulfur dioxide and nitrogen oxides from flue gases. |
WO2005035103A1 (en) * | 2003-08-19 | 2005-04-21 | Wuhan Kaidi Electric Power Co., Ltd. | A reaction tower for dry desulfurizating flue gas |
CN102614735A (en) * | 2012-04-13 | 2012-08-01 | 大连华氏流体设备有限公司 | Device and method for smoke desulphurization and waste recycle |
CN103611384A (en) * | 2013-12-10 | 2014-03-05 | 中国石油大学(华东) | Ultrasonic-assisted spraying drainage and atomization dust removal device |
CN105080317A (en) * | 2014-05-05 | 2015-11-25 | 淮南市明月环保科技有限责任公司 | Method for simultaneously reclaiming sulfur and nitrate |
CN105080317B (en) * | 2014-05-05 | 2018-01-16 | 淮南市明月环保科技有限责任公司 | Method that is a kind of while reclaiming sulphur and nitre |
CN105251330A (en) * | 2015-11-09 | 2016-01-20 | 武汉钢铁(集团)公司 | Technology of synchronous desulfurization and denitration through flue gas ammonia method based on electrolytic regeneration iron removal |
CN105833696A (en) * | 2016-05-06 | 2016-08-10 | 陈佐会 | Ultrasonic desulfuration, denitration and dust removal method |
CN106422713A (en) * | 2016-05-06 | 2017-02-22 | 陈佐会 | Method for desulfuration, denitration and dust removal through ultrasonic atomization |
CN109233775A (en) * | 2018-09-25 | 2019-01-18 | 中国石油化工股份有限公司 | A kind of scavenger and preparation method thereof of thick oil thermal extraction sulfur-bearing gas with foreign flavor |
CN109233775B (en) * | 2018-09-25 | 2020-11-27 | 中国石油化工股份有限公司 | Removing agent for sulfur-containing peculiar smell gas of heavy oil thermal production well and preparation method thereof |
Also Published As
Publication number | Publication date |
---|---|
WO1987003506A3 (en) | 1987-07-16 |
EP0248855A1 (en) | 1987-12-16 |
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