DE4109267C1 - Hydrogen sulphide, ammonia and hydrogen cyanide absorption from process gas - by using circulating wash contg. aq. ammonium soln. and clean water and working up loaded absorption soln. obtd. from hydrogen sulphide absorber by reverse osmosis - Google Patents
Hydrogen sulphide, ammonia and hydrogen cyanide absorption from process gas - by using circulating wash contg. aq. ammonium soln. and clean water and working up loaded absorption soln. obtd. from hydrogen sulphide absorber by reverse osmosisInfo
- Publication number
- DE4109267C1 DE4109267C1 DE4109267A DE4109267A DE4109267C1 DE 4109267 C1 DE4109267 C1 DE 4109267C1 DE 4109267 A DE4109267 A DE 4109267A DE 4109267 A DE4109267 A DE 4109267A DE 4109267 C1 DE4109267 C1 DE 4109267C1
- Authority
- DE
- Germany
- Prior art keywords
- absorption
- absorber
- reverse osmosis
- soln
- permeate
- Prior art date
- 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.)
- Expired - Fee Related
Links
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 44
- 239000006096 absorbing agent Substances 0.000 title claims abstract description 29
- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims description 70
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title claims description 55
- 238000000034 method Methods 0.000 title claims description 32
- 229910021529 ammonia Inorganic materials 0.000 title claims description 5
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 title claims description 4
- 239000007789 gas Substances 0.000 title claims 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 title 1
- 239000012466 permeate Substances 0.000 claims abstract description 14
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 10
- 239000012528 membrane Substances 0.000 claims abstract description 9
- 239000012465 retentate Substances 0.000 claims abstract description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 3
- 229920002396 Polyurea Polymers 0.000 claims abstract 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 claims description 30
- 239000000571 coke Substances 0.000 claims description 5
- 230000002745 absorbent Effects 0.000 claims description 4
- 239000002250 absorbent Substances 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims 20
- 239000000243 solution Substances 0.000 claims 8
- 239000007864 aqueous solution Substances 0.000 claims 1
- 239000004760 aramid Substances 0.000 claims 1
- 229920003235 aromatic polyamide Polymers 0.000 claims 1
- 239000003990 capacitor Substances 0.000 claims 1
- 239000003245 coal Substances 0.000 claims 1
- 238000007670 refining Methods 0.000 claims 1
- 238000005406 washing Methods 0.000 claims 1
- 239000004952 Polyamide Substances 0.000 abstract 2
- 229920002647 polyamide Polymers 0.000 abstract 2
- 235000011114 ammonium hydroxide Nutrition 0.000 abstract 1
- 238000004140 cleaning Methods 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 238000003795 desorption Methods 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 229920001600 hydrophobic polymer Polymers 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000010626 work up procedure Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- 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
- B01D53/14—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 absorption
- B01D53/1418—Recovery of products
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
-
- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Water Supply & Treatment (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Nanotechnology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
Die Erfindung bezieht sich auf ein Verfahren gemäß Oberbegriff des Hauptanspruchs.The invention relates to a method according to the preamble of the main claim.
Ein derartiges Verfahren ist beispielsweise in der DE-A 36 31 251 beschrieben. Dabei wird der H₂S-Gehalt des gesamten oder eines Teils des in einer Abtreiber-Kolonne entsäuerten NH₃- Kreislaufwassers vor dessen Eintritt in die Kreislaufwäsche in einer Trennstufe mit poröser hydrophober Polymermembran ver ringert. Mit Hilfe dieser Porenmembranmodule lassen sich aber nur bereits aufgearbeitete bzw. regenerierte Absorptionslösungen bestimmter Qualität weiter aufkonzentrieren.Such a method is for example in DE-A 36 31 251 described. The H₂S content of the whole or part of the NH₃- deacidified in a stripping column Circulating water before it enters the cycle wash in a separation stage with porous hydrophobic polymer membrane ver wrestles. With the help of these pore membrane modules, however only processed or regenerated absorption solutions of a certain quality.
Aufgabe der Erfindung ist es nun, ein Verfahren vorzuschlagen, bei dem auch bereits die aus dem H₂S-Absorber ablaufende bela dene Absorptionslösung unter deutlicher Energieeinsparung auf gearbeitet werden kann.The object of the invention is now to propose a method in which also the bela running out of the H₂S absorber absorption solution with significant energy savings can be worked.
Zur Lösung dieser Aufgabe werden die im Kennzeichen des An spruchs 1 aufgezeigten Verfahrensschritte vorgeschlagen. Es hat sich gezeigt, daß mit Hilfe geeigneter Umkehr-Osmose-Mem branen sich die in der beladenen Absorptionslösung enthaltenen gelösten, leicht flüchtigen Komponenten wie H₂S, CO₂, HCN und NH₃ in der Flüssigkeitsphase selektiv trennen lassen. Die Se lektivität wird hierbei in der Hauptsache von den ParameternTo solve this task, those in the license plate of the To Proposition 1 suggested process steps. It has been shown that with the help of suitable reverse osmosis mem branches contained in the loaded absorption solution dissolved, volatile components such as H₂S, CO₂, HCN and Selectively separate NH₃ in the liquid phase. The Se Selectivity is mainly determined by the parameters
- pH-Wert
- Konzentrationen
- Membranmaterial
- Temperatur- PH value
- concentrations
- membrane material
- temperature
beeinflußt. Durch die erfindungsgemäße Maßnahme wird der Ener gieaufwand in Form von Dampf für die Regenerierung der beladenen Absorptionslösung deutlich gesenkt. Die Versuchsergebnisse mit Betriebslösungen zeigen, daß der erreichbare Regenera tionsgrad mit dem erfindungsgemäßen Verfahren deutlich höher ist als bei dem bekannten thermischen Regenerationsverfahren. Durch Einsatz der Umkehr-Osmose-Trennstufe läßt sich das bis herige zweistufige Desorbersystem deutlich reduzieren und zwar in der Weise, daß sich die thermisch zu regenerierende Menge praktisch halbiert und sich gegebenenfalls ein Desorber ein sparen läßt.influenced. The measure is the Ener Gi expenditure in the form of steam for the regeneration of the loaded Absorption solution significantly reduced. The test results with operating solutions show that the attainable Regenera tion degree significantly higher with the inventive method than in the known thermal regeneration process. By using the reverse osmosis separation stage this can be done up to significantly reduce the previous two-stage desorber system in such a way that the amount to be thermally regenerated practically halved and possibly a desorber can save.
Weitere günstige Verfahrensschritte sind in den Unter ansprüchen 2 bis 14 aufgeführt.Further favorable process steps are in the sub claims 2 to 14 listed.
Die besonderen Vorteile des erfindungsgemäßen Verfahrens beste hen darin, daßThe particular advantages of the method according to the invention are the best hen in that
- 1. der thermische Regenerationsaufwand bezogen auf das absor biertes H₂S sich deutlich auf 20 kg Dampf/kg H₂S reduziert, während vergleichsweise die bisherige z. Z. allgemein ange wendete klassische A/S-Wäsche noch einen Dampfverbrauch von 33 kg/kg H₂S sowie zusätzlich noch 0,29 kg NaOH/kg H₂S be nötigt; dagegen steht nur ein geringer erhöhter Aufwand an elektrischer Energie von +0,6 kWh/kg H₂S für die Umkehr- Osmose-Stufe; die Differenz zwischen Dampfeinsparung und Strommehrverbrauch bedeutet einen Energiegewinn von 8000 kcal/kg H₂S und somit eine äquivalente CO₂-Reduzierung für die Umwelt;1. the thermal regeneration effort based on the absorber free H₂S is significantly reduced to 20 kg steam / kg H₂S, while comparatively the previous z. Currently generally stated classic A / S laundry still used steam 33 kg / kg H₂S and an additional 0.29 kg NaOH / kg H₂S compels; on the other hand, there is only a slight increase in effort electrical energy of +0.6 kWh / kg H₂S for the reverse Osmosis level; the difference between steam saving and Additional electricity consumption means an energy gain of 8000 kcal / kg H₂S and thus an equivalent CO₂ reduction for the environment;
- 2. mittels der stufenweisen Permeatgewinnung eine Anpassung an die Konzentrationsebenen im Absorber erfolgen kann, ohne daß eine Ausgasung des Absorptionsmittels NH₃ im Absorber erfolgt und das Absorptionsgleichgewicht gestört wird;2. an adaptation by means of the gradual permeate extraction the concentration levels in the absorber can be done without that a degassing of the absorbent NH₃ in the absorber occurs and the absorption balance is disturbed;
- 3. bei einem Entschwefelungsgrad auf 0,2 g H₂S/Nm³ kein NaOH benötigt wird und somit die Salzfracht im Abwasser der De sorption deutlich reduziert wird;3. at a desulfurization level to 0.2 g H₂S / Nm³ no NaOH is needed and thus the salt load in the wastewater of the De sorption is significantly reduced;
- 4. existierende Systeme nachgerüstet werden können.4. Existing systems can be retrofitted.
Die Erfindung wird an Hand der Fig. 1 bis 4 bei spielsweise näher erläutert.The invention is explained in more detail with reference to FIGS . 1 to 4 in example.
Fig. 1 zeigt ein Prozeßschema mit Umkehr-Osmose-Stufe und zweistufiger Desorption; Fig. 1 shows a process diagram with reverse osmosis stage and two-stage desorption;
Fig. 2 zeigt ein Prozeßschema mit Umkehr-Osmose-Stufe und einstu figer Desorption; Fig. 2 shows a process diagram with reverse osmosis stage and one-stage desorption;
Fig. 3 zeigt ein Prozeßschema des Verfahrens nach An spruch 13; Fig. 3 shows a process diagram of the method according to claim 13;
Fig. 4 zeigt ein Prozeßschema des Verfahrens nach An spruch 14. Fig. 4 shows a process diagram of the method according to claim 14.
Kokereigas bzw. Koksofengas (KOG) in einer Menge von 50 000 Nm³/h soll bei einer Temperatur vn 24°C und einem Druck von 1,12 bar auf einen Restgehalt von 0,2 g H₂S/Nm³ entschwefelt werden. Das Kokereigas ist vor der Entschwefelungsstufe (H₂S- Absorber) beladen mit:Coke oven gas or coke oven gas (KOG) in an amount of 50,000 Nm³ / h should be at a temperature of 24 ° C and a pressure of 1.12 bar desulphurized to a residual content of 0.2 g H₂S / Nm³ will. The coke oven gas is before the desulphurization stage (H₂S- Absorber) loaded with:
Die Absorption der H₂S-Menge vn 340 kg/h erfolgt in zwei Stufen:The absorption of the H₂S amount of 340 kg / h takes place in two Stages:
- 1. Im selektiven H₂S-Absorber (Stufe 1) erfolgt die Absorption nahezu isotherm mittels Zwischenkühler für das Absorptions mittel bei 24/25°C. Die Absorptionsselektivität von H₂S gegenüber CO₂ hat einen Wert von 1 kg CO₂ pro kg H₂S.1. In the selective H₂S absorber (level 1), the absorption takes place almost isothermal by means of an intercooler for the absorption medium at 24/25 ° C. The absorption selectivity of H₂S compared to CO₂ has a value of 1 kg CO₂ per kg H₂S.
- 2. Im NH₃-Absorber erfolgt die Restabsorption von H₂S und die NH₃-Entfernung auf einen Endwert von <0,03 g/Nm³ mittels NH₃-Absorptionswasser, dessen Restgehalt an flüchtigem NH₃ <50 mg/l ist.2. In the NH₃ absorber, the residual absorption of H₂S and NH₃ removal to a final value of <0.03 g / Nm³ by means of NH₃ absorption water, the residual content of volatile NH₃ <50 mg / l.
Das beladene Kokereigas durchströmt den H₂S-Absorber im Gegen strom zu dem NH₃-haltigen Absorptionsmittel. Das bisherige Konzept der H₂S-Absorption bei der Ammoniak/Schwefelwasser stoff-Kreislaufwäsche benutzt einen regenerierten NH₃-Wasser strom mit einem NH₃-Gehalt von 14,1 g/l, wobei die rückgeführte Absorptionsmittelmenge 70 m³/h betragen muß. Die Absorptions mittelmenge für den H₂S-Absorber beträgt 43 m³/h und hat einen NH₃-Gehalt von 4,88-g/l-Lösung. Der Dampfverbrauch dieses Absorptionskonzeptes beträgt etwa 120 kg/m³ Zulauf bzw. 13 560 kg/h.The loaded coke oven gas flows through the H₂S absorber in the counter current to the NH₃-containing absorbent. The previous one Concept of H₂S absorption in the ammonia / sulfur water Fabric cycle wash uses a regenerated NH₃ water current with an NH₃ content of 14.1 g / l, the recirculated Absorbent amount must be 70 m³ / h. The absorption average amount for the H₂S absorber is 43 m³ / h and an NH₃ content of 4.88 g / l solution. The steam consumption of this Absorption concept is about 120 kg / m³ inflow or 13 560 kg / h.
Das neue Verfahrenskonzept reduziert diesen Energieverbrauch deutlich, indem ein Teil des rückgeführten effektiven Absorp tions-NH₃ bereits vor der thermischen Regeneration (dem H₂S-Desorber) mittels einer Umkehr-Osmose-Stufe aus der beladenen Absorptionslösung gewonnen wird. Durch diese Maßnahme redu ziert sich die Menge für die thermische Regeneration nahezu auf die Hälfte. Aus der aus dem H₂S-Absorber ablaufenden be ladenen Absorptionslösung (110 m³/h) werden 55 m³/h Permeat mit einem Ammoniakgehalt von 468 kg/h gewonnen. Die notwendige Restmenge an NH₃ beträgt nur noch 507 kg/h, die als thermisch regenerierte Absorptionslösung mit einem NH₃-Gehalt von 14,1 g/l in einer Menge von 36 m³/h zum H₂S-Absorber zurückgeführt wird.The new process concept reduces this energy consumption clearly by adding part of the returned effective absorb tion NH₃ even before thermal regeneration (the H₂S desorber) by means of a reverse osmosis stage from the loaded Absorption solution is obtained. With this measure redu the amount for thermal regeneration almost adorns itself in half. From the expiring from the H₂S absorber loaded absorption solution (110 m³ / h) become 55 m³ / h permeate obtained with an ammonia content of 468 kg / h. The necessary Remaining amount of NH₃ is only 507 kg / h, which is considered thermal regenerated absorption solution with an NH₃ content of 14.1 g / l returned in an amount of 36 m³ / h to the H₂S absorber becomes.
Für die Umkehr-Osmose-Stufe ergibt sich folgende Bilanz- Tabelle:The following balance results for the reverse osmosis stage Table:
Der Dampfverbrauch des erfindungsgemäßen Verfahrens für die Strippung beträgt ca. 6600 kg/h und ist etwa halb so groß wie bei den bisherigen Verfahren.The steam consumption of the method according to the invention for the Stripping is about 6600 kg / h and is about half the size with previous procedures.
Im Vergleich zu Beispiel 1 erfolgt die thermische Regenerie rung der Absorptionslösung nicht in dem bekannten NH₃-H₂S-De sorber-System. Statt dessen wird die fehlende Absorptions- NH₃-Restmenge durch eine partielle Absorptions-Kondensation aus dem Sauergas des Desorbers gewonnen. Der apparative Vor teil besteht darin, daß der Entsäurer entfallen kann und nur ein Stripper für die Restentfernung von NH₃, H₂S, CO₂ und HCN aus dem Wasserstrom notwendig ist. Der Kopfdampf aus dem NH₃- Desorber wird dabei dem Absorptionskondensator zugeführt und aus dem Absorptionskondensator wird eine thermisch regenerierte Absorptionslösung von 37,5 m³/h mit einem NH₃-Gehalt von 22,8 g/l und einem H₂S-Gehalt von 3,28 g/l zum H₂S-Absorber zurückgeführt. Gleichzeitig wird dem Absorptionskondensator aus dem H₂S-Absorber eine Menge von 36 m³/h mit einem NH₃-Ge halt von 8,5 g/l und einem H₂S-Gehalt von 1,53 g/l zugeführt. Die in diesem Beispiel erforderliche Dampfmenge beträgt ca. 6800 kg/h.In comparison to example 1, the thermal regeneration takes place tion of the absorption solution is not in the known NH₃-H₂S-De sorber system. Instead, the missing absorption NH₃ residual amount by a partial absorption condensation won from the sour gas of the desorber. The Apparative Vor Part is that the deacidifier can be omitted and only a stripper for the residual removal of NH₃, H₂S, CO₂ and HCN from the water flow is necessary. The head steam from the NH₃- Desorber is fed to the absorption condenser and the absorption condenser becomes a thermally regenerated one Absorption solution of 37.5 m³ / h with an NH₃ content of 22.8 g / l and an H₂S content of 3.28 g / l to the H₂S absorber returned. At the same time, the absorption condenser a quantity of 36 m³ / h with an NH₃-Ge from the H₂S absorber hold of 8.5 g / l and an H₂S content of 1.53 g / l supplied. The amount of steam required in this example is approx. 6800 kg / h.
In Fig. 3 ist nur der H₂S-Absorber dargestellt, wobei die daraus ablaufende beladene Absorptionslösung in drei nachein ander angeordneten Umkehr-Osmose-Stufen aufgearbeitet wird und das jeweils anfallende Permeat (P₁, P₂, P₃) an verschiedenen Stellen des H₂S-Absorbers mit entsprechendem NH₃/H₂S-Massen verhältnis (α) von 20, 12 bzw. 6 aufgegeben wird.In Fig. 3 only the H₂S absorber is shown, the resulting loaded absorption solution is worked up in three successively arranged reverse osmosis stages and the respective permeate (P₁, P₂, P₃) at different points in the H₂S absorber corresponding NH₃ / H₂S mass ratio (α) of 20, 12 or 6 is abandoned.
In Fig. 4 ist die zusätzliche Aufarbeitung der thermisch re generierten Lösung in zwei nacheinander angeordneten Umkehr- Osmose-Stufen dargestellt, wobei ebenfalls die Permeatströme mit einem bestimmten α-Wert an entsprechenden Stellen des H₂S-Absorbers aufgegeben werden und das Retentat der Endstufe der beladenen Absorptionslösung zugemischt wird.In Fig. 4, the additional workup of the thermally re-generated solution is shown in two successive reverse osmosis stages, the permeate streams with a certain α value are also given up at corresponding points in the H₂S absorber and the retentate of the final stage of the loaded Absorption solution is added.
Claims (14)
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4109267A DE4109267C1 (en) | 1991-03-21 | 1991-03-21 | Hydrogen sulphide, ammonia and hydrogen cyanide absorption from process gas - by using circulating wash contg. aq. ammonium soln. and clean water and working up loaded absorption soln. obtd. from hydrogen sulphide absorber by reverse osmosis |
ITMI920618A IT1254524B (en) | 1991-03-21 | 1992-03-17 | PROCEDURE FOR THE ABSORPTION OF H2S, NH3 AND HCN FROM THE COAL REFINING GAS |
FR9203283A FR2674252B1 (en) | 1991-03-21 | 1992-03-19 | PROCESS FOR ABSORBING H2S, NH3 AND HCN FROM GAS FROM THE RECOVERY OF COAL. |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4109267A DE4109267C1 (en) | 1991-03-21 | 1991-03-21 | Hydrogen sulphide, ammonia and hydrogen cyanide absorption from process gas - by using circulating wash contg. aq. ammonium soln. and clean water and working up loaded absorption soln. obtd. from hydrogen sulphide absorber by reverse osmosis |
Publications (1)
Publication Number | Publication Date |
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DE4109267C1 true DE4109267C1 (en) | 1992-10-08 |
Family
ID=6427874
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DE4109267A Expired - Fee Related DE4109267C1 (en) | 1991-03-21 | 1991-03-21 | Hydrogen sulphide, ammonia and hydrogen cyanide absorption from process gas - by using circulating wash contg. aq. ammonium soln. and clean water and working up loaded absorption soln. obtd. from hydrogen sulphide absorber by reverse osmosis |
Country Status (3)
Country | Link |
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DE (1) | DE4109267C1 (en) |
FR (1) | FR2674252B1 (en) |
IT (1) | IT1254524B (en) |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT404802B (en) * | 1997-09-01 | 1999-03-25 | Voest Alpine Ind Anlagen | Process for gas purification |
CN101837223A (en) * | 2009-03-11 | 2010-09-22 | 通用电气公司 | Use solvent collection CO 2System, method and apparatus |
EP2433700A1 (en) * | 2010-09-23 | 2012-03-28 | Alstom Technology Ltd | Trace component removal in CO2 removal processes by means of a semipermeable membrane |
CN109205941A (en) * | 2018-10-09 | 2019-01-15 | 浙江奇彩环境科技股份有限公司 | A kind of recycling processing method of high ammonia-nitrogen wastewater with high salt |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
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DE3631251A1 (en) * | 1986-09-13 | 1988-03-24 | Still Carl Gmbh Co Kg | Process for scrubbing hydrogen sulphide and ammonia out of gases |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS513393A (en) * | 1974-06-29 | 1976-01-12 | Nippon Kokan Kk | Ryukasuisoo jokyosuru hoho |
US4444571A (en) * | 1983-03-07 | 1984-04-24 | Bend Research, Inc. | Energy-efficient process for the stripping of gases from liquids |
CA1248462A (en) * | 1983-06-22 | 1989-01-10 | Virgil L. Brundige, Jr. | Method and arrangement for the selective removal of acid gases from a feed gas |
-
1991
- 1991-03-21 DE DE4109267A patent/DE4109267C1/en not_active Expired - Fee Related
-
1992
- 1992-03-17 IT ITMI920618A patent/IT1254524B/en active
- 1992-03-19 FR FR9203283A patent/FR2674252B1/en not_active Expired - Fee Related
Patent Citations (1)
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DE3631251A1 (en) * | 1986-09-13 | 1988-03-24 | Still Carl Gmbh Co Kg | Process for scrubbing hydrogen sulphide and ammonia out of gases |
Cited By (13)
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AT404802B (en) * | 1997-09-01 | 1999-03-25 | Voest Alpine Ind Anlagen | Process for gas purification |
CN101837223A (en) * | 2009-03-11 | 2010-09-22 | 通用电气公司 | Use solvent collection CO 2System, method and apparatus |
EP2229996A1 (en) * | 2009-03-11 | 2010-09-22 | General Electric Company | Systems, methods, and apparatus for capturing CO2 using a solvent |
JP2010208936A (en) * | 2009-03-11 | 2010-09-24 | General Electric Co <Ge> | System, method and apparatus for capturing co2 by using solvent |
US8007570B2 (en) | 2009-03-11 | 2011-08-30 | General Electric Company | Systems, methods, and apparatus for capturing CO2 using a solvent |
CN101837223B (en) * | 2009-03-11 | 2013-09-11 | 通用电气公司 | Systems, methods, and apparatus for capturing CO2 using a solvent |
WO2012038794A1 (en) * | 2010-09-23 | 2012-03-29 | Alstom Technology Ltd | Trace component removal in c02 removal processes by means of a semipermeable membrane |
CN103228340A (en) * | 2010-09-23 | 2013-07-31 | 阿尔斯通技术有限公司 | Trace component removal in CO2 removal processes by means of a semipermeable membrane |
EP2433700A1 (en) * | 2010-09-23 | 2012-03-28 | Alstom Technology Ltd | Trace component removal in CO2 removal processes by means of a semipermeable membrane |
US20130333568A1 (en) * | 2010-09-23 | 2013-12-19 | Alstom Technology, Ltd. | Trace component removal in co2 removal processes by means of a semipermeable membrane |
US9463410B2 (en) | 2010-09-23 | 2016-10-11 | General Electric Technology Gmbh | Trace component removal in CO2 removal processes by means of a semipermeable membrane |
CN109205941A (en) * | 2018-10-09 | 2019-01-15 | 浙江奇彩环境科技股份有限公司 | A kind of recycling processing method of high ammonia-nitrogen wastewater with high salt |
CN109205941B (en) * | 2018-10-09 | 2021-11-02 | 浙江奇彩环境科技股份有限公司 | Resourceful treatment method for high-salt high-ammonia nitrogen wastewater |
Also Published As
Publication number | Publication date |
---|---|
FR2674252A1 (en) | 1992-09-25 |
IT1254524B (en) | 1995-09-25 |
FR2674252B1 (en) | 1994-03-18 |
ITMI920618A1 (en) | 1993-09-17 |
ITMI920618A0 (en) | 1992-03-17 |
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