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WO1994016990A1 - Method for removing sulfide with catalytic carbon - Google Patents

Method for removing sulfide with catalytic carbon Download PDF

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Publication number
WO1994016990A1
WO1994016990A1 PCT/US1994/000884 US9400884W WO9416990A1 WO 1994016990 A1 WO1994016990 A1 WO 1994016990A1 US 9400884 W US9400884 W US 9400884W WO 9416990 A1 WO9416990 A1 WO 9416990A1
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WO
WIPO (PCT)
Prior art keywords
char
temperature
catalytically
nitrogen
carbonaceous
Prior art date
Application number
PCT/US1994/000884
Other languages
French (fr)
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WO1994016990B1 (en
Inventor
Richard A. Hayden
Original Assignee
Calgon Carbon Corporation
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Calgon Carbon Corporation filed Critical Calgon Carbon Corporation
Priority to JP6517278A priority Critical patent/JP2572206B2/en
Publication of WO1994016990A1 publication Critical patent/WO1994016990A1/en
Publication of WO1994016990B1 publication Critical patent/WO1994016990B1/en

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Classifications

    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8603Removing sulfur compounds
    • B01D53/8606Removing sulfur compounds only one sulfur compound other than sulfur oxides or hydrogen sulfide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8603Removing sulfur compounds
    • B01D53/8612Hydrogen sulfide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/18Carbon
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/02Preparation of sulfur; Purification
    • C01B17/04Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/046Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process without intermediate formation of sulfur dioxide
    • C01B17/0469Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process without intermediate formation of sulfur dioxide at least one catalyst bed operating below the dew-point of sulfur
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00Carbon; Compounds thereof
    • C01B32/30Active carbon
    • C01B32/312Preparation
    • C01B32/336Preparation characterised by gaseous activating agents

Definitions

  • the present invention relates to the use of a highly -catalytically-active carbonaceous char for the removal of sulfide from gas or liquid media in the presence of oxygen .and water.
  • extrinsic parameters can include particle size distribution, pore volume distribution, and contact time. It is further the object of the present invention to produce and employ such carbonaceous chars at minimal cost and hazard when compared to prior art
  • the present invention comprises the removal of sulfides and mercaptans from media containing oxygen and water by the catalytic action of carbonaceous chars.
  • These chars are prepared by the low-temperature carbonization and oxidation of a nitrogen-poor feedstock.
  • the oxidized low- temperature char is then subjected to a nitrogen-containing compound at high temperatures during the initial calcination or calcination/activation.
  • high-temperature carbonaceous chars are those produced by thermal treatment at temperatures greater than 700 C.
  • Low temperature carbonaceous chars are those that have not experienced temperatures greater than 700 C.
  • the preferred nitrogen-poor feedstock is a bituminous coal or a bituminous coal-like material such as those derived from higher or lower rank bitumens, coals, or lignocellulose materials by various chemical treatments.
  • higher rank coals include anthracite or semi-anthracite coals
  • lower rank coals include peat, lignite, and sub-bituminous coals.
  • chemical treatment of these feedstocks include alkali metal treatment of the high rank materials and zinc chloride or phosphoric acid treatment of the low rank materials. These types of treatments can also be applied to lignocellulose materials .
  • the feedstock material is pulverized, mixed if necessary with small amounts of a suitable binder such as pitch, briquetted or otherwise formed, and sized.
  • the sized material is then extensively oxidized at temperatures less than 700 C, preferably less than 400 C. The oxidation is continued until additional gains in the catalytic activity of the final product are no longer evident.
  • the oxidation is well beyond that typically required to remove the coking properties of bituminous coals and produces an optimally oxidized char.
  • Other convenient means of oxidation can also be used to effect the low-temperature oxidation and carbonization of the starting material.
  • the oxidized low-temperature carbonaceous char is then exposed to small amounts of an inexpensive, abundant, and relatively non-toxic nitrogen-containing compound such as urea during, not after, the initial calcination and condensation of the carbon structure.
  • the amounts of nitrogen-containing compounds used are typically small, preferably less than 5% by weight of the oxidized low-temperature carbonaceous char or such that additional gains in the catalytic activity of the final product are no longer evident.
  • the treatment is carried out by heating the oxidized low-temperature char to high temperatures, preferably between 850 C and 950 C, in the presence of the nitrogen-containing compound. This heating is preferably conducted under an atmosphere that is inert except for the gases and vapors attributable to the char and/or the nitrogen-containing compound.
  • the heating rate and temperatures are preferably selected such that additional gains in the catalytic activity of the final product are no longer evident.
  • the nitrogen-treated high-temperature carbonaceous char may then be activated to the desired density at temperatures above 700 C in steam and/or carbon dioxide, with or without the addition of other gasifying agents such as air.
  • the calcined or calcined/activated carbonaceous char is then cooled in an oxygen-free or otherwise inert atmosphere to temperatures less than 400 C, preferably less than 200 C. Additional gains in catalytic activity may be realized by repeating the oxidation/exposure to nitrogen- containing compounds/calcination or calcination/activation/inert cooling as many times as may be desired.
  • any other method known to generate catalytic activity in high temperature carbonaceous chars may be applied to the resultant product to further enhance its catalytic activity.
  • the catal tically-active carbonaceous char prepared according to the above method is then contacted with a sulflde-containing media in the presence of water and oxygen. Sulfide is removed from the media by catalytic oxidation to primarily sulfates and elemental sulfur.
  • the operating temperature is between about 0 C and 300 C and preferably between about 0 C and 100 C and more preferably between about 25 C and 90 C.
  • Example 1 demonstrates the H 2 S removal capacity of a specific mesh size fraction of a commercial activated carbon.
  • Example 2 demonstrates the H- ⁇ S removal capacity of the invention. Comparison of these two examples shows that the performance of the invention greatly exceeds that of a typical activated carbon.
  • a commercially available activated carbon, BPL manufactured by Calgon Carbon Corporation, Pittsburgh PA
  • BPL manufactured by Calgon Carbon Corporation, Pittsburgh PA
  • This carbon showed an Apparent Density ( Test Method TM-7, Calgon Carbon Corporation, Pittsburgh PA) of 0.504 grams per cc and a CC1 4 Number ( Test Method TM-6, Calgon Carbon Corporation, Pittsburgh PA ) of 55.1 %.
  • the sized carbon was loaded into a column having an inside diameter of approximately 0.73 inches to give a bed depth of 9 inches. Column loading was done in such a manner as to achieve a packing density equivalent to the Apparent Density.
  • a gas stream having a relative humidity of greater than 509c, an oxygen content of greater than 17 v/v%, and a known HjS concentration of approximately 1 v/v% was passed through this column at a flow rate of 1450 +/- 20 cc/minute under ambient conditions.
  • the effluent from this column was monitored and the elapsed time required to achieve a 50 ppm H_S breakthrough was measured. For this carbon sample the elapsed time period was equal to 9 minutes.
  • Bituminous coal was pulverized, mixed with about 4 to 6% coal tar pitch, and briquetted.
  • the resultant briquettes were crushed and sized to produce an approximately less than 4 mesh size and greater than 10 mesh size (U.S. Standard Series sieves) material.
  • this material was oxidized by heating from 100 C to 200 C at a rate of 200 C per hour, then from 200 C to
  • the resultant oxidized material was cooled to near ambient temperatures in a low oxygen content atmosphere, sized to produce an approximately less than 5 and greater than 6 mesh size (U.S. Standard Series sieves) material, and subsequently impregnated with an aqueous urea solution and dried.
  • the quantity of urea solution used was sufficient to produce a 4% urea loading on a dry weight basis. After impregnation, portions of the oxidized, impregnated low-temperature char were rapidly heated to 950 C under an inert gas atmosphere.
  • the resultant materials were activated with steam at 950 C for a sufficient period of time to achieve the desired yield. After activation, the materials were cooled to ambient temperature under an inert atmosphere.
  • the catalytically-active activated carbonaceous chars so produced when combined and sized to less than 5 mesh (U.S. Standard Series) and greater than 6 mesh (U.S. Standard Series) exhibited an Apparent Density (Test Method TM- 7, Calgon Carbon Corporation, Pittsburgh PA) of 0.495 grams per cc.
  • the CC Number of the sized, combined chars was 55.5%.
  • the H 2 S removal ability of the sized, catalytically-active, activated high-temperature carbonaceous char prepared as described above was determined using conditions identical to those described in Example 1. For this sample of catalytically-active activated carbonaceous char the elapsed time period required to achieve a 50 ppm H 2 S breakthrough was equal to 326 minutes.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Catalysts (AREA)

Abstract

An improved process is provided for the selective removal of sulfide from gas or liquid media containing oxygen and water by contacting said media with a catalytically-active carbonaceous char. The improvement is provided by the use of a catalytically-active carbonaceous char prepared by low-temperature carbonization and oxidation of a bituminous coal or bituminous coal-like material followed by exposure to a nitrogen containing compound at high-temperatures during the initial calcination and/or activation of the oxidized material.

Description

TITLE METHOD FOR REMOVING SULFTDE WITH CATALYTIC CARBON
FIELD OF THE INVENTION
The present invention relates to the use of a highly -catalytically-active carbonaceous char for the removal of sulfide from gas or liquid media in the presence of oxygen .and water.
BACKGROUND OF THE INVENTION
Various methods of removing H2S using .carbonaceous chars are known. For example, it has been known that charcoal has the ability to catalyze the oxidation of hydrogen sulfide. Activated carbon has been used for the removal of hydrogen sulfide and various mercaptans from a humidified, oxygen-containing gaseous stream. Improvements in the removal capabilities of the carbonaceous char have been realized by the addition of a base, such as ammonia or hydroxide, to the char surface during the removal process. It has been found that the addition of certain halogens and/or transition metal impregnants to carbonaceous char substrates also enhances the removal of hydrogen sulfide and mercaptans from humid air streams. However, none of these improvements altered the inherent properties of a carbonaceous char which are fundamentally responsible for the observed phenomenon in the absence of promoters such as sodium hydroxide, potassium iodide, or other compounds.
Some improvements in the pore size distribution of .activated carbons have been described wherein a high-temperature activated carbonaceous char is treated with a urea or melamine compound and calcined at high temperatures. Chars prepared in this manner have enhanced hydrogen sulfide adsorption capabilities; however, the ability of such chars to remove hydrogen sulfide by catalytic oxidation was not tested or reported. The production of a carbonaceous chars suitable for catalytic hydrogen sulfide oxidation has been taught wherein a high-temperature activated carbon or coke is oxidized and exposed to a nitrogen-containing ammonium salt at temperatures above 350 C. Such prior art methods have certain disadvantages which limit their application. The use of commercially-available uni pregnated activated carbons for catalytic hydrogen sulfide removal suffers from low rates of removal, and consequently, low hydrogen sulfide breakthrough capacities. The use of promoters in the presence of such carbonaceous chars also entails certain disadvantages. For example, the use of ammonia requires added cost and hazard in the installation and control of measured ammonia additions. The use of sodium hydroxide and other metal salts also involves added costs as well as an increased risk of thermal excursion due to the lowering of the char ignition temperature.
Accordingly, it is the object of the present invention to provide a carbonaceous char which is catalytically .active for sulfide and meπ^ptan removal in the presence of oxygen and water when compared to other unimpregnated chars and apart from those extrinsic parameters known to affect such removal. For example, extrinsic parameters can include particle size distribution, pore volume distribution, and contact time. It is further the object of the present invention to produce and employ such carbonaceous chars at minimal cost and hazard when compared to prior art
SUMMARY OF THE INVENTION
Generally, the present invention comprises the removal of sulfides and mercaptans from media containing oxygen and water by the catalytic action of carbonaceous chars. These chars are prepared by the low-temperature carbonization and oxidation of a nitrogen-poor feedstock. The oxidized low- temperature char is then subjected to a nitrogen-containing compound at high temperatures during the initial calcination or calcination/activation. In all cases, high-temperature carbonaceous chars are those produced by thermal treatment at temperatures greater than 700 C. Low temperature carbonaceous chars are those that have not experienced temperatures greater than 700 C.
The preferred nitrogen-poor feedstock is a bituminous coal or a bituminous coal-like material such as those derived from higher or lower rank bitumens, coals, or lignocellulose materials by various chemical treatments. Examples of higher rank coals include anthracite or semi-anthracite coals, while examples of lower rank coals include peat, lignite, and sub-bituminous coals. Examples of the chemical treatment of these feedstocks include alkali metal treatment of the high rank materials and zinc chloride or phosphoric acid treatment of the low rank materials. These types of treatments can also be applied to lignocellulose materials . In a preferred embodiment of this invention, the feedstock material is pulverized, mixed if necessary with small amounts of a suitable binder such as pitch, briquetted or otherwise formed, and sized. The sized material is then extensively oxidized at temperatures less than 700 C, preferably less than 400 C. The oxidation is continued until additional gains in the catalytic activity of the final product are no longer evident.
The oxidation is well beyond that typically required to remove the coking properties of bituminous coals and produces an optimally oxidized char. Other convenient means of oxidation can also be used to effect the low-temperature oxidation and carbonization of the starting material.
The oxidized low-temperature carbonaceous char is then exposed to small amounts of an inexpensive, abundant, and relatively non-toxic nitrogen-containing compound such as urea during, not after, the initial calcination and condensation of the carbon structure. The amounts of nitrogen-containing compounds used are typically small, preferably less than 5% by weight of the oxidized low-temperature carbonaceous char or such that additional gains in the catalytic activity of the final product are no longer evident. The treatment is carried out by heating the oxidized low-temperature char to high temperatures, preferably between 850 C and 950 C, in the presence of the nitrogen-containing compound. This heating is preferably conducted under an atmosphere that is inert except for the gases and vapors attributable to the char and/or the nitrogen-containing compound. The heating rate and temperatures are preferably selected such that additional gains in the catalytic activity of the final product are no longer evident.
The nitrogen-treated high-temperature carbonaceous char may then be activated to the desired density at temperatures above 700 C in steam and/or carbon dioxide, with or without the addition of other gasifying agents such as air. The calcined or calcined/activated carbonaceous char is then cooled in an oxygen-free or otherwise inert atmosphere to temperatures less than 400 C, preferably less than 200 C. Additional gains in catalytic activity may be realized by repeating the oxidation/exposure to nitrogen- containing compounds/calcination or calcination/activation/inert cooling as many times as may be desired. Alternatively, any other method known to generate catalytic activity in high temperature carbonaceous chars may be applied to the resultant product to further enhance its catalytic activity.
The catal tically-active carbonaceous char prepared according to the above method is then contacted with a sulflde-containing media in the presence of water and oxygen. Sulfide is removed from the media by catalytic oxidation to primarily sulfates and elemental sulfur. The operating temperature is between about 0 C and 300 C and preferably between about 0 C and 100 C and more preferably between about 25 C and 90 C.
PRESENTLY PREFERRED EMBODIMENTS
The utility of the invention is illustrated by the following two examples. In each example, equivalent mesh size fractions of the carbonaceous chars were evaluated to negate any particle size effects. The chars used in these examples have approximately the same densities and CO, activities. This near equivalence indicates that the pore volumes of both chars are nearly equivalent Therefore the benefits of the present invention are evident as the extrinsic properties affecting sulfide removal are nearly equivalent for these samples. Example 1 demonstrates the H2S removal capacity of a specific mesh size fraction of a commercial activated carbon. Example 2 demonstrates the H-^S removal capacity of the invention. Comparison of these two examples shows that the performance of the invention greatly exceeds that of a typical activated carbon.
EXAMPLE 1
A commercially available activated carbon, BPL (manufactured by Calgon Carbon Corporation, Pittsburgh PA) was sized to less than 5 and greater than 6 mesh (U.S. Standard Series sieves). When so sized this carbon showed an Apparent Density ( Test Method TM-7, Calgon Carbon Corporation, Pittsburgh PA) of 0.504 grams per cc and a CC14 Number ( Test Method TM-6, Calgon Carbon Corporation, Pittsburgh PA ) of 55.1 %. The sized carbon was loaded into a column having an inside diameter of approximately 0.73 inches to give a bed depth of 9 inches. Column loading was done in such a manner as to achieve a packing density equivalent to the Apparent Density. A gas stream having a relative humidity of greater than 509c, an oxygen content of greater than 17 v/v%, and a known HjS concentration of approximately 1 v/v% was passed through this column at a flow rate of 1450 +/- 20 cc/minute under ambient conditions. The effluent from this column was monitored and the elapsed time required to achieve a 50 ppm H_S breakthrough was measured. For this carbon sample the elapsed time period was equal to 9 minutes.
EXAMPLE 2
Bituminous coal was pulverized, mixed with about 4 to 6% coal tar pitch, and briquetted. The resultant briquettes were crushed and sized to produce an approximately less than 4 mesh size and greater than 10 mesh size (U.S. Standard Series sieves) material. In the presence of large quantities of excess air, this material was oxidized by heating from 100 C to 200 C at a rate of 200 C per hour, then from 200 C to
350 C at a rate of 100 C per hour, then held at 350 C for 4 hours, and finally heated from 350 C to 450 C at a rate of 100 C per hour. The resultant oxidized material was cooled to near ambient temperatures in a low oxygen content atmosphere, sized to produce an approximately less than 5 and greater than 6 mesh size (U.S. Standard Series sieves) material, and subsequently impregnated with an aqueous urea solution and dried. The quantity of urea solution used was sufficient to produce a 4% urea loading on a dry weight basis. After impregnation, portions of the oxidized, impregnated low-temperature char were rapidly heated to 950 C under an inert gas atmosphere. Immediately following this calcination treatment the resultant materials were activated with steam at 950 C for a sufficient period of time to achieve the desired yield. After activation, the materials were cooled to ambient temperature under an inert atmosphere. The catalytically-active activated carbonaceous chars so produced, when combined and sized to less than 5 mesh (U.S. Standard Series) and greater than 6 mesh (U.S. Standard Series) exhibited an Apparent Density (Test Method TM- 7, Calgon Carbon Corporation, Pittsburgh PA) of 0.495 grams per cc. The CC Number of the sized, combined chars was 55.5%.
The H2S removal ability of the sized, catalytically-active, activated high-temperature carbonaceous char prepared as described above was determined using conditions identical to those described in Example 1. For this sample of catalytically-active activated carbonaceous char the elapsed time period required to achieve a 50 ppm H2S breakthrough was equal to 326 minutes.
While a presently preferred embodiment of the invention has been described, it may be otherwise embodied within the scope of the appended claims.

Claims

WHAT IS CLAIMED IS:
1. A process for the removal of sulfides from gas or liquid media which comprises contacting said media, in the presence of oxygen and water, with a catalytically-active carbonaceous char, said char being prepared from a bituminous coal or bituminous coal-like material carbonized and oxidized at temperatures below 700° C and which is subjected thereafter to nitrogen-containing compounds during an initial exposure to temperatures above 700° C.
2. A process as set forth in Claim 1 wherein said catalytically-active carbonaceous char has been activated at temperatures above 700° C using at least one of steam, carbon dioxide, and oxygen.
3. The process of Claim 1 wherein the sulfide is hydrogen sulfide.
4. The process of Claim 1 wherein said process is operated at a temperature of between 0° C and 300° C to remove said sulfides.
5. The process of Claim 1 wherein said process is operated at a temperature of between about 25° C and 90° C to remove said sulfides.
6. A process as set forth in Claim 1 wherein said nitrogen-containing compounds are urea and urea-like compounds.
PCT/US1994/000884 1993-01-21 1994-01-21 Method for removing sulfide with catalytic carbon WO1994016990A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP6517278A JP2572206B2 (en) 1993-01-21 1994-01-21 Removal method of sulfide by catalytic carbon

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US872393A 1993-01-21 1993-01-21
US08/008,723 1993-01-21

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WO1994016990B1 WO1994016990B1 (en) 1994-09-01

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0795351A3 (en) * 1996-03-11 1997-12-03 Calgon Carbon Corporation Process for the catalytic oxidation of ferrous iron in liquid media
KR101512562B1 (en) 2013-08-20 2015-04-16 대전대학교 산학협력단 A process for producing biomass adsorbent from platanus leaves
EP3302761A4 (en) * 2015-06-01 2018-12-26 Calgon Carbon Corporation Method for inerting activated carbon in biogas purification equipment

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101439504B1 (en) 2012-10-09 2014-09-15 주식회사 포스코 Method of active carbon for removing hydrogen sulfide and active carbon manufactured by the same

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US737579A (en) * 1902-12-06 1903-09-01 Ernst Burschell Process of purifying gas.
GB411918A (en) * 1932-01-04 1934-06-18 Franz Krczil Improvements in the methods and means for producing active charcoal or for re-activating spent charcoal
US3630959A (en) * 1969-06-04 1971-12-28 Standard Oil Co Ohio Carbonization of bituminous coals
JPS5220395A (en) * 1975-08-08 1977-02-16 Mitsubishi Petrochem Co Ltd Process for producing porous carbonaceous particles
US5256384A (en) * 1991-03-26 1993-10-26 Metallgesellschaft Aktiengesellschaft Activated carbon process for removing hydrogen sulfide from gases

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US737579A (en) * 1902-12-06 1903-09-01 Ernst Burschell Process of purifying gas.
GB411918A (en) * 1932-01-04 1934-06-18 Franz Krczil Improvements in the methods and means for producing active charcoal or for re-activating spent charcoal
US3630959A (en) * 1969-06-04 1971-12-28 Standard Oil Co Ohio Carbonization of bituminous coals
JPS5220395A (en) * 1975-08-08 1977-02-16 Mitsubishi Petrochem Co Ltd Process for producing porous carbonaceous particles
US5256384A (en) * 1991-03-26 1993-10-26 Metallgesellschaft Aktiengesellschaft Activated carbon process for removing hydrogen sulfide from gases

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Removal by Adsorption of Hydrogen Sulfide by a New Type of Activated Carbon Containing Nitrogen", BOKI et al., JAPANESE JOURNAL OF HYGIENE, Vol. 38, No. 5, December 1983, pgs. 877-882. *

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0795351A3 (en) * 1996-03-11 1997-12-03 Calgon Carbon Corporation Process for the catalytic oxidation of ferrous iron in liquid media
KR101512562B1 (en) 2013-08-20 2015-04-16 대전대학교 산학협력단 A process for producing biomass adsorbent from platanus leaves
EP3302761A4 (en) * 2015-06-01 2018-12-26 Calgon Carbon Corporation Method for inerting activated carbon in biogas purification equipment
US10633307B2 (en) 2015-06-01 2020-04-28 Calgon Carbon Corporation Method for inerting activated carbon in biogas purification equipment
US11958803B2 (en) 2015-06-01 2024-04-16 Calgon Carbon Corporation Method for inerting activated carbon in biogas purification equipment

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JPH07505116A (en) 1995-06-08
CA2131987A1 (en) 1994-08-04
JP2572206B2 (en) 1997-01-16

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