AU2014221190B2 - Process of scrubbing volatiles from evaporator water vapor - Google Patents
Process of scrubbing volatiles from evaporator water vapor Download PDFInfo
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- AU2014221190B2 AU2014221190B2 AU2014221190A AU2014221190A AU2014221190B2 AU 2014221190 B2 AU2014221190 B2 AU 2014221190B2 AU 2014221190 A AU2014221190 A AU 2014221190A AU 2014221190 A AU2014221190 A AU 2014221190A AU 2014221190 B2 AU2014221190 B2 AU 2014221190B2
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- vapor
- volatile compounds
- scrubbing
- scrubbing solution
- water
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- 238000005201 scrubbing Methods 0.000 title claims abstract description 81
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000003039 volatile agent Substances 0.000 title abstract description 3
- 150000001875 compounds Chemical class 0.000 claims abstract description 47
- 239000002699 waste material Substances 0.000 claims abstract description 38
- 239000010797 grey water Substances 0.000 claims abstract description 26
- 239000002893 slag Substances 0.000 claims abstract description 26
- 239000007787 solid Substances 0.000 claims abstract description 23
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 12
- 238000002309 gasification Methods 0.000 claims abstract description 12
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 12
- 239000012808 vapor phase Substances 0.000 claims abstract description 5
- 239000007791 liquid phase Substances 0.000 claims abstract description 4
- 238000001704 evaporation Methods 0.000 claims abstract description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 23
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 239000002253 acid Substances 0.000 claims description 15
- 238000011282 treatment Methods 0.000 claims description 13
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 12
- 150000003839 salts Chemical class 0.000 claims description 12
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 10
- 229910021529 ammonia Inorganic materials 0.000 claims description 10
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 claims description 10
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 7
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 claims description 6
- 239000004327 boric acid Substances 0.000 claims description 6
- 235000019253 formic acid Nutrition 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 4
- 239000003518 caustics Substances 0.000 claims description 3
- 239000006260 foam Substances 0.000 claims description 2
- 230000001376 precipitating effect Effects 0.000 claims 2
- 238000004064 recycling Methods 0.000 claims 1
- 239000000243 solution Substances 0.000 description 38
- 150000007513 acids Chemical class 0.000 description 11
- 239000002585 base Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 8
- 238000010791 quenching Methods 0.000 description 8
- 230000000171 quenching effect Effects 0.000 description 8
- 235000010338 boric acid Nutrition 0.000 description 6
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 4
- 239000010881 fly ash Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 229910015444 B(OH)3 Inorganic materials 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000002006 petroleum coke Substances 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 235000019270 ammonium chloride Nutrition 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 239000010866 blackwater Substances 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 239000011335 coal coke Substances 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001642 boronic acid derivatives Chemical class 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- 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
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Landscapes
- Treating Waste Gases (AREA)
Abstract
PROCESS OF SCRUBBING VOLATILES FROM EVAPORATOR WATER VAPOR A hydrocarbonaceous gasification process comprising: directing a hydrocarbonaceous feedstock and water to a gasifier (52) and producing slag and synthesis gas in the gasifier (52); removing slag from the gasifier (52); removing the synthesis gas from the gasifier (52) and scrubbing the synthesis gas with scrubbing water, and separating the scrubbing water from the synthesis gas; wherein a waste stream is formed and includes the scrubbing water and suspended solids including the slag removed from the gasifier(52); directing the waste stream to a solids separator (64) and separating at least some of the suspended solids from the waste stream and yielding a grey water effluent containing volatile compounds; directing the grey water effluent to an evaporator (12); evaporating water and volatile compounds from the grey water effluent to form vapor which contains gaseous volatile compounds; directing the vapor having a gaseous volatile compounds to a vapor scrubber (22); contacting the vapor having the gaseous volatile compounds with a scrubbing solution as the vapor passes through the vapor scrubber (22); reacting the scrubbing solution with the gaseous volatile compounds such that the gaseous volatile compounds pass from a vapor phase into a liquid phase in the scrubbing solution and form volatile compounds in the scrubbing solution; wherein reacting the scrubbing solution with the gaseous volatile compounds produces a treated vapor stream; and collecting the scrubbing solution having the volatile compounds removed from the vapor.
Description
PROCESS OF SCRUBBING VOLATILES FROM EVAPORATOR WATER VAPOR
FIELD OF INVENTION
[0001] The present invention relates to a process for treating vapor generated from a waste stream in an evaporator, and more particularly relates to removing volatile acids and/or bases from the vapor.
SUMMARY
[0001a] The present invention relates to a hydrocarbonaceous gasification process comprising: directing a hydrocarbonaceous feedstock and water to a gasifier and producing slag and synthesis gas in the gasifier; removing slag from the gasifier; removing the synthesis gas from the gasifier and scrubbing the synthesis gas with scrubbing water, and separating the scrubbing water from the synthesis gas; wherein a waste stream is formed and includes the scrubbing water and suspended solids including the slag removed from the gasifier; directing the waste stream to a solids separator and separating at least some of the suspended solids from the waste stream and yielding a grey water effluent containing volatile compounds; directing the grey water effluent to an evaporator; evaporating water and volatile compounds from the grey water effluent to form vapor which contains gaseous volatile compounds; directing the vapor having a gaseous volatile compounds to a vapor scrubber; contacting the vapor having the gaseous volatile compounds with a scrubbing solution as the vapor passes through the vapor scrubber; reacting the scrubbing solution with the gaseous volatile compounds such that the gaseous volatile compounds pass from a vapor phase into a liquid phase in the scrubbing solution and form volatile compounds in the scrubbing solution; wherein reacting the scrubbing solution with the gaseous volatile compounds produces a treated vapor stream; and collecting the scrubbing solution having the volatile compounds removed from the vapor.
[0002] There is also disclosed herein a process for treating vapor formed in an evaporator in a waste stream treatment process. The waste stream is directed to an evaporator where water from the waste stream is vaporized. As the waste stream is heated, volatile compounds in the waste stream are also vaporized. The vapor, including the volatile compounds, is directed to a vapor scrubber where the vapor is contacted with a scrubbing solution. The volatile compounds in the vapor phase react with chemicals in the scrubbing solution and pass from the vapor into the scrubbing solution. Thus, the scrubbing solution removes the volatile contaminants from the vapor.
BRIEF DESCRIPTION OF DRAWINGS
[0003] Preferred embodiments of the invention will now be described hereinafter, by way of examples only, with reference to the accompanying drawings, wherein: [0004] Figure 1 is a schematic illustrating a process for treating vapor containing volatile compounds utilizing a vapor scrubber.
[0005] Figure 2 is a schematic illustrating the process for treating vapor shown in Figure 1 applied to a gasification process.
DESCRIPTION OF EXEMPLARY EMBODIMENTS
[0006] A system for treating vapor from a waste stream is generally indicated by the numeral 10 in Figure 1. In the embodiment illustrated therein, vapor can be produced from various types of waste streams, including landfill leachate, flue gas desulfurization (FGD) waste streams, and integrated gasification combined cycle (IGCC) waste streams.
[0007] Viewing the vapor treatment system 10 in more detail, the waste stream influent is directed into an evaporator 12 through waste stream inlet 14. During this phase of the process, the waste stream influent is heated to produce vapor, distillate, and concentrated brine. Evaporator 12 may be any type of evaporator including falling film or forced circulation. Evaporator 12 includes distillate outlet 16, vapor outlet line 18, a sump 19 for collecting and holding a concentrated brine, and a concentrated brine outlet 20. As the water is evaporated from the waste stream in the evaporator, volatile acids and/or bases present in the waste stream also evaporate and form gaseous volatile compounds in the vapor. Thus, the evaporated volatile compounds that were present in the waste stream generally have volatilities, and thus, vapor pressures, similar to or greater than that of water.
[0008] The vapor, including the evaporated volatile compounds, is directed from evaporator 12, through the vapor outlet line 18, to vapor scrubber 22. In vapor scrubber 22, an aqueous scrubbing solution, in one embodiment, is sprayed through nozzles 24 into the vapor. The scrubbing solution includes either caustic and/or acidic compounds which react with the volatile compounds in the vapor.
For example, if the scrubbing solution contains caustic compounds, the scrubbing solution will react with volatile acids in the vapor. On the other hand, if the scrubbing solution contains acidic compounds, the scrubbing solution will react with volatile bases in the vapor. In either case, the scrubbing solution reacts with the volatile compounds in the vapor to form a salt, which is removed from the vapor phase and passed into the liquid of the scrubbing solution. The salts, formed from the reaction between the volatile compounds and the scrubbing solution, are water soluble and thus, dissociate in the scrubbing solution. Other means may also be used to promote the transfer of volatile acids and/or bases from the vapor to the liquid phase. Such devices include, random or structuring packing, wire mesh pads, or various types of trays, such as sieves, bubble caps, etc. Not only does the scrubbing solution react with the volatile acids and/or bases in the vapor, but the scrubbing solution also serves to break up any foam produced in the evaporator 12 that is entrained in the vapor.
[0009] In one embodiment, the vapor includes the volatile base ammonia. That is, ammonia was present in the waste stream entering the evaporator 12. As the waste stream is heated in evaporator 12, water and ammonia in the waste stream evaporate. To remove the ammonia from the vapor, the scrubbing solution, which includes an acid, such as hydrochloric acid (HCI) or sulfuric acid (H2S04), is sprayed into the vapor. The acid in the scrubbing solution reacts with the ammonia to produce either ammonium chloride or ammonium sulfate salt.
The salt formed from these reactions, dissociates in the scrubbing solution. For example: NH3 (g) + HCI (aq) -> NH4CI (aq) 2NH3 (g)+ H2SO4 (aq) -» {NH4)2S04 (aq) [0010] In another embodiment, the vapor includes formic acid (HC02H) and/or boric acid {B(OH)3). That is, formic acid and/or boric acid were present in the waste stream entering evaporator 12. As the waste stream is heated in evaporator 12, water, formic acid and/or boric acid in the waste stream evaporate. To remove the volatile acids from the vapor, the scrubbing solution, which comprises an alkali, such as sodium hydroxide (NaOH) or potassium hydroxide (KOH), is sprayed into the vapor. The alkali compounds in the scrubbing solution react with the volatile acids to produce formate and/or borate salts. The salts formed from these reactions, dissociate in the scrubbing solution. For example: HC02H (g) + NaOH (aq) NaHC02(aq) + H20 B(OH)3(g) + NaOH (aq) NaB(OH)4 (aq) HC02H (g) + KOH (aq) KHC02(aq) +H20 B(OH)3 (g) + KOH (aq) KB(OH)4 (aq) [0011] Referring again to Figure 1, the scrubbing solution is produced by adding an alkali or acid through inlet 26 to the circulating aqueous solution in the bottom portion of vapor scrubber 22. At least a portion of the scrubbing solution is then circulated toward valve 28, where it is recirculated to the spray nozzles 24 for treating the vapor. The concentration of the salts in the scrubbing solution circulated through the vapor scrubber 22 is controlled by removing a portion of the scrubbing solution as blowdown and in one embodiment directing the biowdown through valve 28 to the evaporator 12 for further treatment. In other cases, the blowdown from the vapor scrubber 22 can be directed to other treatment systems or can be disposed of in various conventional ways. For example, in a system designed for coal gasification wastewater treatment, the scrubber biowdown is directed to a separate crystallizer to precipitate out the salts formed in the scrubbing reaction.
[0012] In the embodiment illustrated in Figure 1, after passing through the sprayed scrubbing solution, the treated vapor passes through line 30 toward a mechanical vapor recompression (MVR) device 32. In one embodiment, prior to reaching the MVR 32, the treated vapor passes through mist eliminators. MVR 32 compresses the vapor which is then directed through line 34 to evaporator 12 where it is used to heat and vaporize the Incoming waste stream. As the heat from the treated vapor is transferred to the incoming waste stream, the vapor condenses and forms a distillate which exits the evaporator through outlet 16. As shown in Figure 1, at least a portion of the distillate from evaporator 12 is directed from outlet 16 to inlet 38 of the vapor scrubber 22. The distillate is then added as make-up water to the scrubbing solution. In an alternate embodiment, a portion of the treated vapor is not directed to MVR 32, but is instead directed from the vapor scrubber 22 to condenser 36.
[0013] Figure 2 is a schematic illustration of a gasification process that incorporates the system for treating a vapor stream shown in Figure 1. The gasification system shown in Figure 2 is indicated generally by the numeral 50.
As shown therein, a feedstock such as a hydrocarbonaceous feedstock is directed into a gasifier 52. Examples of hydrocarbonaceous feedstocks are coal and petroleum coke. Typically, coal or petroleum coke is pulverized and mixed with water to form a slurry and the slurry is directed into the gasifier 52. It should be appreciated that other fuels can be utilized as a feedstock in gasification processes. For example, organic waste material including plastic waste or sewage can form a feedstock. Typical gasifiers operate at high temperatures and 2014221190 02 Sep 2014 high pressures. For example, a typical temperature range for a gasifier is approximately 1,200° to approximately 1,500°C. A typical pressure range is from approximately 20 to approximately 80 atmospheres.
[0014] Gasifier 52 includes a reaction zone 52A and a quenching chamber 52B. The feedstock or slurry is fed into the reaction zone 52A. In the case of coal for example, the coal slurry is fed into the reaction zone 52A and is partially oxidized. This produces a hot effluent syngas and slag. Syngas basically comprises carbon monoxide and hydrogen. Quenching water is directed into the quenching chamber 52B. The raw syngas and slag byproduct pass to the quenching chamber 52B typically disposed at the lower end of the gasifier 52. Here, the hot syngas and molten slag are contacted with quenching water and are cooled and separated. The slag, entrained within the some of the quenching water, is removed from the gasifier 52. The syngas is directed to a syngas scrubber 56 which removes fine ash, soot, salts, and other suspended solids from the syngas. In particular, as illustrated in Figure 2, scrubbing water is introduced into the scrubbing chamber 56. As a result of the scrubbing water contacting the syngas, the scrubbing water removes fine ash, soot, salts, and other suspended solids from the syngas and this results in an aqueous waste stream (blowdown) that is directed from the syngas scrubber 56 to a settler feed tank 58. After the syngas has been scrubbed in the scrubber 56, the syngas is subjected to various other treatments, For example, water in the syngas is condensed and/or removed by a water knockout. Details of the further treatment of the syngas is not dealt with herein because such is not per se material to the present invention and further processes for treating the syngas after scrubbing are well known and appreciated by those skilled in the art. -6- [0015] Returning to the gasifier 52, as noted above, the slag byproduct combined with some of the quenching water is directed to a lockhopper 60. Lockhopper 60 removes slag from the quenching water-slag mixture and the removed slag, along with some water, is directed to a screening system 62. Screening system 62 separates the slag into coarse slag and fine slag. The coarse slag is suitable for commercial use or can be disposed in a landfill. The fine slag is directed to the settler feed tank 58 where it mixes with the scrubbing water from the syngas scrubber 56. In some cases, the aqueous solution received and held in the settler feed tank 58 is referred to as black water. In any event, the aqueous solution in the settler feed tank 58 will include suspended solids such as slag, fly ash, etc.
[0016] The black water in the settler tank 58 is fed to the clarifier or solids separator 64 which removes substantial suspended solids including slag, fly ash, and other particulate matter. The settled suspended solids from clarifier 64 may be recirculated back to the gasifier 52 for further treatment. In addition, clarifier or solids separator 64 produces a supernatant or grey water waste stream that is directed from the clarifier 64 to a holding tank 66. A portion of the grey water held in the grey water holding tank 66 is treated by the treatment system 10 shown in Figure 1.
[0017] One of the principal reasons for treating the grey water is that the grey water includes chloride salts that are of a concern since they are water soluble and tend to accumulate in recirculated process water. Furthermore, chloride is corrosive to material such as stainless steels, which are typically used in gasification process equipment. In partial oxidation gasification processes where coal, petroleum coke, or waste plastics and other chloro-organic materials are found in the feedstock, one of the most common chlorides exiting the gasifier is hydrogen chloride. In addition, partial oxidation reactions also produce ammonia from the feedstock. Ammonia and hydrogen chloride react in water systems to form an ammonium chloride solution. Thus, various chloride species might reside in the grey water and it is preferable to remove these corrosive species.
[0018] A stream of grey water is pumped from the grey water holding tank 66 by pump 68 to a recycle line 70. Recycle line 70 leads back to the syngas scrubber 56 where the grey water is utilized to scrub the syngas. A portion of the grey water is not recycled but is directed through the treatment system 10 shown in Figure 1. As illustrated in Figure 2, a portion of the grey water is directed to evaporator 12. As discussed above, evaporator 12 concentrates the waste stream and produces a vapor containing various evaporated acids and/or bases from the grey water waste stream. The vapor containing the volatile compounds is directed to the vapor scrubber 22 where it is “scrubbed” with the scrubbing solution. The volatile acids and/or bases present in the vapor react with the scrubbing solution and are removed from the vapor and dissociate as salt in the scrubbing solution. In the embodiment illustrated in Figure 2, the blowdown from the vapor scrubber is returned to the evaporator 12 for further treatment. There are other treatments that may be appropriate for treating the blowdown from the vapor scrubber 22. For example, in a gasification process such as shown in Figure 2, the blowdown from the vapor scrubber 22 can be directed to a separate crystallizer to precipitate out salts formed in the scrubbing reaction.
[0019] In some situations, it may be necessary or prudent to provide some additional means for removing suspended solids from the grey water prior to the grey water reaching the evaporator. That is, in some cases, there may be a significant concentration of suspended solids, particularly slag and fly ash, in the grey water effluent leaving the solids separator 64. This is especially true if there is an upset with respect to the solids separator 64. In these cases, it may be beneficial to remove these remaining suspended solids from the grey water effluent before reaching the evaporator 12. By removing slag and fly ash that might be contained in the grey water effluent, the fouling normally associated with the suspended solids in the evaporator is reduced or eliminated. Various means can be employed to remove the suspended solids prior to reaching the evaporator. One approach is to utilize a ceramic membrane or a group of ceramic membranes just upstream of the evaporator 12.
[0020] The present invention may, of course, be carried out in other specific ways than those herein set forth without departing from the scope and the essential characteristics of the invention. The present embodiments are therefore to be construed in all aspects as illustrative and not restrictive.
Claims (12)
1. A hydrocarbonaceous gasification process comprising: directing a hydrocarbonaceous feedstock and water to a gasifier and producing slag and synthesis gas in the gasifier; removing slag from the gasifier; removing the synthesis gas from the gasifier and scrubbing the synthesis gas with scrubbing water, and separating the scrubbing water from the synthesis gas; wherein a waste stream is formed and includes the scrubbing water and suspended solids including the slag removed from the gasifier; directing the waste stream to a solids separator and separating at least some of the suspended solids from the waste stream and yielding a grey water effluent containing volatile compounds; directing the grey water effluent to an evaporator; evaporating water and volatile compounds from the grey water effluent to form vapor which contains gaseous volatile compounds; directing the vapor having a gaseous volatile compounds to a vapor scrubber; contacting the vapor having the gaseous volatile compounds with a scrubbing solution as the vapor passes through the vapor scrubber; reacting the scrubbing solution with the gaseous volatile compounds such that the gaseous volatile compounds pass from a vapor phase into a liquid phase in the scrubbing solution and form volatile compounds in the scrubbing solution; wherein reacting the scrubbing solution with the gaseous volatile compounds produces a treated vapor stream; and collecting the scrubbing solution having the volatile compounds removed from the vapor.
2. The method of claim 1 wherein the volatile compounds in the vapor include formic acid, boric acid or ammonia, and wherein the method includes contacting the volatile compounds with sodium hydroxide, potassium hydroxide, sulfuric acid or hydrochloric acid.
3. The method of claim 1 including condensing the treated vapor stream to form a distillate and mixing at least some of the distillate with the scrubbing solution that is collected in a sump associated with the vapor scrubber.
4. The method of claim 1 wherein the scrubbing solution including the volatile compounds is collected in a sump associated with a vapor scrubber, and the method includes recycling a first portion of the collected scrubbing solution and contacting the vapor with the first portion of the collected scrubbing solution, and directing a second portion of the collected scrubbing solution to the evaporator for further treatment.
5. The method of claim 4 wherein the scrubbing solution includes a caustic or an acid for reacting with a gaseous volatile compounds in the vapor.
6. The method of claim 1 wherein the vapor includes formic or boric acid and the method includes contacting the formic or boric acid with an alkali contained in the scrubbing solution.
7. The method of claim 1 wherein the vapor includes ammonia and the method includes contacting the ammonia with an acid contained in the scrubbing solution.
8. The method of claim 7 wherein the acid contained within the scrubbing solution is hydrochloric acid or sulfuric acid.
9. The method of claim 1 further including utilizing the vapor scrubber to break up foam contained in the vapor.
10. The method of claim 1 including directing blowdown from the vapor scrubber to the evaporator for further treatment.
11. The method of claim 1 wherein a blowdown stream is produced by the vapor scrubber and the method include precipitating salts from the blowdown stream.
12. The method of claim 1 including directing a blowdown stream from the vapor scrubber to a crystallizer and precipitating salts from the blowdown stream.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2014221190A AU2014221190B2 (en) | 2010-05-25 | 2014-09-02 | Process of scrubbing volatiles from evaporator water vapor |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US12/786,665 | 2010-05-25 | ||
| AU2011258484A AU2011258484B2 (en) | 2010-05-25 | 2011-05-24 | Process of scrubbing volatiles from evaporator water vapor |
| AU2014221190A AU2014221190B2 (en) | 2010-05-25 | 2014-09-02 | Process of scrubbing volatiles from evaporator water vapor |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2011258484A Division AU2011258484B2 (en) | 2010-05-25 | 2011-05-24 | Process of scrubbing volatiles from evaporator water vapor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU2014221190A1 AU2014221190A1 (en) | 2014-09-25 |
| AU2014221190B2 true AU2014221190B2 (en) | 2016-09-15 |
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| Application Number | Title | Priority Date | Filing Date |
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| AU2014221190A Ceased AU2014221190B2 (en) | 2010-05-25 | 2014-09-02 | Process of scrubbing volatiles from evaporator water vapor |
Country Status (1)
| Country | Link |
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| AU (1) | AU2014221190B2 (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090133407A1 (en) * | 2007-11-28 | 2009-05-28 | Nrg Energy, Inc. | Plasma gasification system |
| US20090188867A1 (en) * | 2008-01-30 | 2009-07-30 | Dinh-Cuong Vuong | Methods and systems for processing waste water |
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2014
- 2014-09-02 AU AU2014221190A patent/AU2014221190B2/en not_active Ceased
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20090133407A1 (en) * | 2007-11-28 | 2009-05-28 | Nrg Energy, Inc. | Plasma gasification system |
| US20090188867A1 (en) * | 2008-01-30 | 2009-07-30 | Dinh-Cuong Vuong | Methods and systems for processing waste water |
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| Publication number | Publication date |
|---|---|
| AU2014221190A1 (en) | 2014-09-25 |
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