CN105347311A - Method used for generating elemental sulfur via selective oxidation of H2S - Google Patents
Method used for generating elemental sulfur via selective oxidation of H2S Download PDFInfo
- Publication number
- CN105347311A CN105347311A CN201510814964.4A CN201510814964A CN105347311A CN 105347311 A CN105347311 A CN 105347311A CN 201510814964 A CN201510814964 A CN 201510814964A CN 105347311 A CN105347311 A CN 105347311A
- Authority
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- China
- Prior art keywords
- selective oxidation
- elemental sulfur
- air
- processing method
- road
- 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.)
- Granted
Links
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 48
- 230000003647 oxidation Effects 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims abstract description 21
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000005864 Sulphur Substances 0.000 claims abstract description 11
- 229910052814 silicon oxide Inorganic materials 0.000 claims abstract description 11
- 239000011148 porous material Substances 0.000 claims abstract description 8
- 239000007921 spray Substances 0.000 claims abstract description 6
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000003672 processing method Methods 0.000 claims description 14
- 210000000952 spleen Anatomy 0.000 claims description 12
- 239000011229 interlayer Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000010410 layer Substances 0.000 claims description 8
- 229910052717 sulfur Inorganic materials 0.000 abstract description 15
- 239000011593 sulfur Substances 0.000 abstract description 15
- 238000005516 engineering process Methods 0.000 abstract description 7
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 24
- 235000001508 sulfur Nutrition 0.000 description 16
- 238000011084 recovery Methods 0.000 description 11
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 5
- 150000003463 sulfur Chemical class 0.000 description 4
- 239000003245 coal Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation 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
- C01B17/0426—Preparation 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 characterised by the catalytic conversion
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a method used for generating elemental sulfur via selective oxidation of H2S. A device of the method comprises a heater, a selective oxidation reactor, a middle temperature condenser, a low temperature condenser, and a molten sulphur groove; the selective oxidation reactor is filled with 5 to 12% of a Fe2O3/silicon oxide H2S selective oxidation catalyst with an average pore diameter ranging from 30 to 50nm in a plurality of layers, an air spray inlet and a cooling coil pipe is arranged between each pair of layers respectively; the temperature of the catalyst layers, air adding total amount, and air distribution amount at each air spray inlet are controlled to be appropriate so as to realize complete oxidation of H2S in a process gas containing 0.5 to 2% H2S, SO2 with a concentration of 200mg/m<3> or lower is generated, the other element sulfur is conversed into elemental sulfur, and strict discharge standards of the industry or the area are satisfied. Technological process is short and simple; SO2 emission concentration is low; and technology operation is stable.
Description
Technical field
The present invention relates to a kind of recovery technology of sulfur method, be specifically related to a kind of H
2s selective oxidation generates the processing method of elemental sulfur.
Background technology
In petrochemical complex, Coal Chemical Industry, coal gasification course, a part of sulphur contained by raw material can change into H usually
2s, is formed containing H through being separated
2the sour gas of S, this sour gas generally processes through recovery technology of sulfur, by H
2s is converted into elemental sulfur as much as possible.
Recovery technology of sulfur device, in operation process, through the tail gas that chimney is emptying, its SO
2concentration is continuous monitoring project, although the higher limit of existing discharge standard of air pollutants GB16297-1996 is as 700mg/m
3be not difficult to reach, but also may there is more strict emission standard in place industry or location; H
2s is one of odor pollution material included by emission standard for odor pollutants GB14554-93, and emission limit is more strict, the accurate higher limit of factory's boundary mark as three grades be 0.45/0.80mg/m
3, 100 meters of smoke stack emission amount higher limits are 14kg/h.
Along with the raising of environmental protection standard, increasingly strict to the requirement of recovery technology of sulfur tail gas, thus, when the recovery technology of sulfur of pre-treatment sour gas, its back segment often comprises H
2the step of S selective oxidation, will come from the lower H as 0.5-2% of content in preceding step Process Gas
2s, and the O allocated into
2reaction, selective oxidation generates elemental sulfur.
H
2s selective oxidation reaction, object product is elemental sulfur, is separated and enters liquid-state sulfur groove, finally form sulfur product; Side reaction is SO
2.Usually to H in tail gas
2s, SO
2the requirement of content is generally as far as possible not containing H
2s, SO
2content is as far as possible low, thus, if do not have other treatment step directly to discharge as steps such as catalyzed oxidation adsorption desulfurizes after selective oxidation, then and should at H
2s selective oxidation step is by H
2s transforms entirely, is converted into elemental sulfur as much as possible, reduces SO simultaneously as far as possible
2selectivity.
H
2s selective oxidation generates in the reaction of elemental sulfur, reduces by product SO
2optionally method, except suitable control O
2the amount of allocating into and temperature of reaction, also to adopt the Fe that the active lower catalyzer of Crouse is as larger in aperture
2o
3/ silicon oxide catalyst, but at guarantee H
2while S transforms entirely, prior art not easily accomplishes SO
2content is lower than 200mg/m
3and even 100mg/m
3, 50mg/m
3level, thus not easily reach place industry or area may exist comparatively strict emission standard.
Summary of the invention
For overcoming above-mentioned technological deficiency, the invention provides a kind of H
2s selective oxidation generates the processing method of elemental sulfur, for the treatment of containing H
2the process gas of S0.5-2%, at guarantee H
2while S transforms entirely, make SO
2content is lower than 200mg/m
3and even 100mg/m
3, 50mg/m
3, thus reach place industry or area may exist comparatively strict emission standard.
Technical scheme of the present invention is: a kind of H
2s selective oxidation generates the processing method of elemental sulfur, comprises well heater, selective oxidation reaction device, middle temperature condenser and subcooling condenser, Molten sulphur groove; The 5-12%Fe of average pore diameter 30-50nm is loaded in reactor
2o
3/ silicon oxide H
2s catalyst for selective oxidation, catalyzer divides multilayer to load, interlayer Ge She mono-road air entrance and a road temperature-reducing coil; By suitably control each reaction bed temperature, air allocate total amount and the sendout at each gas inlet into, by the H in Process Gas
2s is all oxidized, except generation≤200mg/m
3sO
2, all the other are all converted into elemental sulfur;
Containing H
2the unstripped gas of S volume content 0.5-2%, and measure the air mixed allocated into, after heater via is preheating to 180 ~ 210 DEG C, enter selective oxidation reaction device by top, between catalyst layer, entrance sprays into the air of metering; Regulate the air capacity of each bed and coil pipe cooling degree, control middle and upper part bed temperature 180-220 DEG C, bottom bed temperature 220-240 DEG C, not containing H in making to work off one's feeling vent one's spleen
2s, SO
2volume content≤200mg/m
3; Work off one's feeling vent one's spleen and enter middle temperature condenser, be cooled to 140-160 DEG C, the elemental sulfur of generation is separated and enters Molten sulphur groove, and middle temperature condenser overhead is worked off one's feeling vent one's spleen, then is cooled to after the 40-60 DEG C of micro-elemental sulfur of removing residue through subcooling condenser, emptying through chimney.
H of the present invention
2s selective oxidation generates in the processing method of elemental sulfur, and preferably, selective oxidation reaction device inner catalyst divides 4-10 layer to load, and interlayer establishes 3-9 road gas inlet, together with the gas inlet allocating unstripped gas before well heater into, establishes 4-10 road gas inlet altogether.
H of the present invention
2s selective oxidation generates in the processing method of elemental sulfur, preferably, air entrance set by selective oxidation reaction device inner catalyst interlayer, there is high speed spout, supersonic speed spout is better, more preferably every road gas inlet has multiple mouths, to enable sprayed into air and Process Gas mix better faster, described high speed spout, supersonic speed spout have the jet size matched with air straying quatity.
H of the present invention
2s selective oxidation generates the processing method of elemental sulfur, has the following advantages:
1) technique is comparatively brief, SO
2emission concentration is lower
The 5-12%Fe of average pore diameter 30-50nm is loaded in reactor
2o
3/ silicon oxide H2S catalyst for selective oxidation, and catalyzer divides multilayer to load, interlayer Ge She mono-road air entrance and a road temperature-reducing coil; By suitably control each reaction bed temperature, air allocate total amount and the sendout at each gas inlet into, make temperature of reaction lower, make O in reactant gases
2concentration lower, thus while being all oxidized by the H2S in Process Gas, achieve lower SO
2generation, all the other are all converted into elemental sulfur, SO in emptying tail gas
2content is lower than 200mg/m
3and even 100mg/m
3, 50mg/m
3, not containing other sulfide, thus reach place industry or area may exist comparatively strict emission standard; Fe used
2o
3it is active that/silicon oxide catalyst has lower Crouse, is a key;
2) process runs well
In reactor load Fe
2o
3/ silicon oxide catalyst, can give play to selective oxidation H in longer operational process
2s generates the stability of elemental sulfur, and reason is the stability of its silica support, the average pore diameter of catalyzer 30-50nm and the low O of low temperature
2fe under condition
2o
3not easily there is the character of sulphating: silica support acid resistance, water tolerance are better, not by H under 180 ~ 240 DEG C of temperature of reaction conditions
2s, SO
2erosion; Catalyzer there is the average pore diameter of 30-50nm, make the liquid sulfur that formed in internal gutter less, the blocking formed is less; At the low O of the low temperature of this processing method
2under condition, the Fe of catalyzer
2o
3active ingredient can in the operation of several years less generation sulphating.
Accompanying drawing explanation
Accompanying drawing 1 is H of the present invention
2s selective oxidation generates the concise and to the point flow process of the processing method of elemental sulfur, and wherein device numbering is followed successively by 1 well heater, 2 selective oxidation reaction devices, warm condenser in 3,4 subcooling condensers, 5 Molten sulphur grooves, 6 chimneys.
Embodiment
Embodiment 1
A set of sulfur recovery facility, comprises well heater, selective oxidation reaction device, middle temperature condenser and subcooling condenser, Molten sulphur groove; Selective oxidation reaction device filling Fe
2o
3/ silicon oxide H
2s catalyst for selective oxidation 60m
3, catalyzer divides 6 layers respectively to fill 10m
3, interlayer Ge She mono-road gas inlet and temperature-reducing coil, every road air has 5 high speed spouts; Described Fe
2o
3/ silicon oxide catalyst Fe
2o
3content 5%, average pore diameter 50nm, profile is the column-shape strip of Ф 3x5-10mm; The elementary operation condition of this device is:
Unstripped gas 20000m
3/ hr, H
2s volume content 0.5%, all the other are N mainly
2, CO
2, COS≤20mg/m
3, without other sulfide, allocate air total amount 250m into
3about/hr reacts; Unstripped gas allocates 70m into
3the air of about/hr, enters selective oxidation reaction device by top after being preheating to 210 DEG C, all the other 180m
3the air of about/hr distributes between 5 road entrances between catalyst layer, and metering sprays into; Regulate the air capacity of each bed and coil pipe cooling degree, control upper part 3 bed temperature 210-220 DEG C, lower part 3 bed temperature 230-240 DEG C, not containing H in making to work off one's feeling vent one's spleen
2s, SO
2volume content≤100mg/m
3, not containing other sulfide; Work off one's feeling vent one's spleen and enter middle temperature condenser, be cooled to 150 DEG C, the elemental sulfur of generation is separated and enters Molten sulphur groove; Middle temperature condenser overhead is worked off one's feeling vent one's spleen, and is cooled to 40 DEG C of micro-elemental sulfurs of removing residue through subcooling condenser, emptying through chimney.
This sulfur recovery facility, in 1 year that puts into operation, this sulfur recovery facility smooth running, not containing H in air-discharging
2s, SO
2volume content≤100mg/m
3, wherein most of the time≤50mg/m
3, not containing other sulfide.
Embodiment 2
A set of sulfur recovery facility, comprises well heater, selective oxidation reaction device, middle temperature condenser and subcooling condenser, Molten sulphur groove; Selective oxidation reaction device filling Fe
2o
3/ silicon oxide H
2s catalyst for selective oxidation 50m
3, catalyzer divides 8 layers respectively to fill 6.25m
3, interlayer Ge She mono-road gas inlet and temperature-reducing coil, every road air has 5 high speed spouts; Described Fe
2o
3/ silicon oxide catalyst Fe
2o
3content 12%, average pore diameter 30nm, profile is the column-shape strip of Ф 3x5-10mm; The elementary operation condition of this device is:
Unstripped gas 10000m
3/ hr, H
2s volume content 1.8%, all the other are N mainly
2, CO
2, COS≤20mg/m
3, without other sulfide, allocate air total amount 450m into
3about/hr reacts; Unstripped gas allocates 100m into
3the air of about/hr, enters selective oxidation reaction device by top after being preheating to 180 DEG C, all the other 350m
3the air of about/hr distributes between 7 road entrances between catalyst layer, and metering sprays into; Regulate the air capacity of each bed and coil pipe cooling degree, control 5, middle and upper part bed temperature 200-220 DEG C, 3, bottom bed temperature 230-240 DEG C, not containing H in making to work off one's feeling vent one's spleen
2s, SO
2volume content≤100mg/m
3, not containing other sulfide; Work off one's feeling vent one's spleen and enter middle temperature condenser, be cooled to 150 DEG C, the elemental sulfur of generation is separated and enters Molten sulphur groove; Middle temperature condenser overhead is worked off one's feeling vent one's spleen, and is cooled to 60 DEG C of micro-elemental sulfurs of removing residue through subcooling condenser, emptying through chimney.
This sulfur recovery facility, in 1 year that puts into operation, this sulfur recovery facility smooth running, not containing H in air-discharging
2s, SO
2volume content≤100mg/m
3, wherein most of the time≤50mg/m
3, not containing other sulfide.
Claims (5)
1. a H
2s selective oxidation generates the processing method of elemental sulfur, comprises well heater, selective oxidation reaction device, middle temperature condenser and subcooling condenser, Molten sulphur groove; The 5-12%Fe of average pore diameter 30-50nm is loaded in reactor
2o
3/ silicon oxide H
2s catalyst for selective oxidation, catalyzer divides multilayer to load, interlayer Ge She mono-road air entrance and a road temperature-reducing coil; By suitably control each reaction bed temperature, air allocate total amount and the sendout at each gas inlet into, by the H in Process Gas
2s is all oxidized, except generation≤200mg/m
3sO
2, all the other are all converted into elemental sulfur;
Containing H
2the unstripped gas of S volume content 0.5-2%, and measure the air mixed allocated into, after heater via is preheating to 180 ~ 210 DEG C, enter selective oxidation reaction device by top, between catalyst layer, entrance sprays into the air of metering; Regulate the air capacity of each bed and coil pipe cooling degree, control middle and upper part bed temperature 180-220 DEG C, bottom bed temperature 220-240 DEG C, not containing H in making to work off one's feeling vent one's spleen
2s, SO
2volume content≤200mg/m
3; Work off one's feeling vent one's spleen and enter middle temperature condenser, be cooled to 140-160 DEG C, the elemental sulfur of generation is separated and enters Molten sulphur groove, and middle temperature condenser overhead is worked off one's feeling vent one's spleen, then is cooled to after the 40-60 DEG C of micro-elemental sulfur of removing residue through subcooling condenser, emptying through chimney.
2. H as claimed in claim 1
2s selective oxidation generates the processing method of elemental sulfur, and it is characterized in that, oxidation reactor inner catalyst divides 4-10 layer to load, and interlayer establishes 3-9 road gas inlet, together with the gas inlet allocating unstripped gas before well heater into, establishes 4-10 road gas inlet altogether.
3. H as claimed in claim 1
2s selective oxidation generates the processing method of elemental sulfur, and it is characterized in that, the air entrance set by selective oxidation reaction device inner catalyst interlayer, has high speed spout, and described high speed spout has the jet size matched with air straying quatity.
4. H as claimed in claim 3
2s selective oxidation generates the processing method of elemental sulfur, and it is characterized in that, described high speed spout is supersonic speed spout.
5. the arbitrary H as described in claim 1-4
2s selective oxidation generates the processing method of elemental sulfur, and it is characterized in that, the every road gas inlet set by selective oxidation reaction device inner catalyst interlayer has multiple mouths.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510814964.4A CN105347311B (en) | 2015-11-23 | 2015-11-23 | H2S selective oxidations generate the process of elemental sulfur |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510814964.4A CN105347311B (en) | 2015-11-23 | 2015-11-23 | H2S selective oxidations generate the process of elemental sulfur |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105347311A true CN105347311A (en) | 2016-02-24 |
| CN105347311B CN105347311B (en) | 2018-05-08 |
Family
ID=55323409
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510814964.4A Active CN105347311B (en) | 2015-11-23 | 2015-11-23 | H2S selective oxidations generate the process of elemental sulfur |
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| Country | Link |
|---|---|
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106698361A (en) * | 2016-12-14 | 2017-05-24 | 山东迅达化工集团有限公司 | Sulfur recycling process for acid gas |
| CN109789394A (en) * | 2016-09-26 | 2019-05-21 | 雅各布斯荷兰有限公司 | Improved catalyst for selective oxidation of sulfureted hydrogen |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1049320A (en) * | 1989-07-21 | 1991-02-20 | Veg气体研究所公司 | Catalyst for selective oxidation of sulfide to elemental sulfur, its preparation method and method for selective oxidation of sulfide to elemental sulfur |
| CN1909950A (en) * | 2004-01-15 | 2007-02-07 | 科诺科飞利浦公司 | Catalytic Partial Oxidation of H2S by Staged Oxygen Feeding Method |
-
2015
- 2015-11-23 CN CN201510814964.4A patent/CN105347311B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1049320A (en) * | 1989-07-21 | 1991-02-20 | Veg气体研究所公司 | Catalyst for selective oxidation of sulfide to elemental sulfur, its preparation method and method for selective oxidation of sulfide to elemental sulfur |
| CN1909950A (en) * | 2004-01-15 | 2007-02-07 | 科诺科飞利浦公司 | Catalytic Partial Oxidation of H2S by Staged Oxygen Feeding Method |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109789394A (en) * | 2016-09-26 | 2019-05-21 | 雅各布斯荷兰有限公司 | Improved catalyst for selective oxidation of sulfureted hydrogen |
| CN109789394B (en) * | 2016-09-26 | 2022-03-01 | 沃利荷兰有限公司 | Improved catalyst for selective oxidation of hydrogen sulfide |
| CN106698361A (en) * | 2016-12-14 | 2017-05-24 | 山东迅达化工集团有限公司 | Sulfur recycling process for acid gas |
| CN106698361B (en) * | 2016-12-14 | 2019-04-05 | 山东迅达化工集团有限公司 | The recovery technology of sulfur of sour gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105347311B (en) | 2018-05-08 |
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