CN106582272A - Desulfuration purification process for acidic waste water steam stripping ammonia gas - Google Patents
Desulfuration purification process for acidic waste water steam stripping ammonia gas Download PDFInfo
- Publication number
- CN106582272A CN106582272A CN201611149118.6A CN201611149118A CN106582272A CN 106582272 A CN106582272 A CN 106582272A CN 201611149118 A CN201611149118 A CN 201611149118A CN 106582272 A CN106582272 A CN 106582272A
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- CN
- China
- Prior art keywords
- desulfurizing
- ammonia
- sulfur
- purifying
- water
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 211
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 22
- 238000000746 purification Methods 0.000 title abstract description 11
- 239000002351 wastewater Substances 0.000 title abstract description 4
- 230000002378 acidificating effect Effects 0.000 title abstract 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 70
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 claims abstract description 44
- 125000001741 organic sulfur group Chemical group 0.000 claims abstract description 40
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 38
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 37
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 37
- 239000011593 sulfur Substances 0.000 claims abstract description 37
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 27
- 230000008929 regeneration Effects 0.000 claims abstract description 23
- 238000011069 regeneration method Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 229910000069 nitrogen hydride Inorganic materials 0.000 claims abstract description 12
- 239000002912 waste gas Substances 0.000 claims abstract description 10
- 238000002485 combustion reaction Methods 0.000 claims abstract description 9
- 230000003647 oxidation Effects 0.000 claims abstract description 9
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 9
- 238000011084 recovery Methods 0.000 claims abstract description 9
- 238000001179 sorption measurement Methods 0.000 claims abstract description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 8
- 230000003197 catalytic effect Effects 0.000 claims abstract description 6
- 230000003009 desulfurizing effect Effects 0.000 claims description 135
- 229910021529 ammonia Inorganic materials 0.000 claims description 93
- 239000003795 chemical substances by application Substances 0.000 claims description 72
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 62
- 229910001868 water Inorganic materials 0.000 claims description 58
- 238000000034 method Methods 0.000 claims description 50
- 150000004053 quinones Chemical class 0.000 claims description 34
- 230000008569 process Effects 0.000 claims description 25
- 238000004064 recycling Methods 0.000 claims description 23
- 238000010521 absorption reaction Methods 0.000 claims description 22
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 230000023556 desulfurization Effects 0.000 claims description 16
- 239000000498 cooling water Substances 0.000 claims description 15
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 9
- 238000011049 filling Methods 0.000 claims description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 230000007062 hydrolysis Effects 0.000 claims description 7
- 238000006460 hydrolysis reaction Methods 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 239000005864 Sulphur Substances 0.000 claims description 5
- 230000008021 deposition Effects 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 3
- 238000006555 catalytic reaction Methods 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 2
- 238000009826 distribution Methods 0.000 claims description 2
- 239000008187 granular material Substances 0.000 claims description 2
- 239000012629 purifying agent Substances 0.000 claims 1
- LOUPRKONTZGTKE-WZBLMQSHSA-N Quinine Chemical compound C([C@H]([C@H](C1)C=C)C2)C[N@@]1[C@@H]2[C@H](O)C1=CC=NC2=CC=C(OC)C=C21 LOUPRKONTZGTKE-WZBLMQSHSA-N 0.000 abstract 4
- 235000001258 Cinchona calisaya Nutrition 0.000 abstract 2
- LOUPRKONTZGTKE-UHFFFAOYSA-N cinchonine Natural products C1C(C(C2)C=C)CCN2C1C(O)C1=CC=NC2=CC=C(OC)C=C21 LOUPRKONTZGTKE-UHFFFAOYSA-N 0.000 abstract 2
- 229960000948 quinine Drugs 0.000 abstract 2
- 235000001508 sulfur Nutrition 0.000 description 29
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 21
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 21
- 239000003245 coal Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000012535 impurity Substances 0.000 description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 230000002159 abnormal effect Effects 0.000 description 5
- 239000000796 flavoring agent Substances 0.000 description 5
- 235000019634 flavors Nutrition 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 230000000149 penetrating effect Effects 0.000 description 3
- 150000002989 phenols Chemical class 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- AZQWKYJCGOJGHM-UHFFFAOYSA-N 1,4-benzoquinone Chemical compound O=C1C=CC(=O)C=C1 AZQWKYJCGOJGHM-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000005202 decontamination Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 230000036541 health Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 229910052573 porcelain Inorganic materials 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 210000000952 spleen Anatomy 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- AQGDXJQRVOCUQX-UHFFFAOYSA-N N.[S] Chemical compound N.[S] AQGDXJQRVOCUQX-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 241000736911 Turritella communis Species 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 125000003636 chemical group Chemical group 0.000 description 1
- -1 class Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 125000001165 hydrophobic group Chemical group 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0423—Beds in columns
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/76—Gas phase processes, e.g. by using aerosols
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40086—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by using a purge gas
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Dispersion Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
The invention provides a desulfuration purification process for acidic waste water steam stripping ammonia gas. Main equipment comprises two catalytic oxidation, adsorption and desulfuration purification towers capable of being connected in series or in parallel, the towers are filled with a desulfuration purifier capable of achieving thermal regeneration, and heat exchange tubes are arranged in a bed; the operating temperature ranges from 10 DEG C to 60 DEG C, H2S in the treated ammonia gas is smaller than or equal to 3 ug/g, SO2 in the treated ammonia gas is smaller than or equal to 3 ug/g, organic sulfur in the treated ammonia gas is smaller than or equal to 3 ug/g, and basically no phenol/quinine or cyanogen or hydrocarbon is contained; during thermal regeneration of the desulfuration purification towers, adsorbed and precipitated elemental sulfur is condensed into liquid sulfur to be recycled, and waste gas containing organic sulfur, phenol/quinine, cyanogen, hydrocarbon, NH3 and CO2 is merged into an H2S gas-rich pipeline at the top of a steam stripping tower, enters a sulfur recovery unit combustion furnace to be treated, or enters a torch pipeline to be burned up and exhausted.
Description
Technical field
The present invention relates to a kind of ammonia decontamination purifying technique, and in particular to a kind of sour water strips the desulfurizing and purifying of ammonia
Technique.
Background technology
Oil plant, coal plant, coking of coal factory, the sour water produced by natural gas from coal factory, are separated by stripping, can
Obtain hydrogen sulfide air-flow and ammonia air-flow.
Sour water is stripped in separating obtained ammonia, and such as sour water Single-tower stripping is separated and Jing three-levels condensation gained ammonia
Gas, usually contains the H such as 1% or so2S, general Jing circulate washing method by most of H2S washes ammonia and returns stripper and divides again
From, or make NH4HS crystalline products or solution are sold, or are directly down to low temperature formation NH without ammonia scrubbing4HS crystallizations will be big
Part H2S is removed；Remaining a small amount of H in ammonia2Again by desulfurizing agent adsorption treatment, ammonia can reach H to S after process2S≤10ug/
The level of g or even≤3ug/g.
In some sour water occasions, gained ammonia main component such as NH398-99% or so, hydrogen sulfide 0.7% or so, but
Contained organic sulfur, volatile phenol/quinones, cyanogen class, hydro carbons are more, and smell component is more, the process of Jing said methods, gained NH4HS is tied
Brilliant or solution exist color, abnormal flavour and impurity, purity problem and purposes is limited or cannot sell, use；Desulfurizing agent is to contained
Organic sulfur such as COS, mercaptan, thioether, CS2And volatile phenol/quinones, cyanogen class, no clean-up effect or not ideal enough, sometimes
The etching problem of ammonia following process equipment such as compressor, prepared ammonia or liquefied ammonia is caused to there is also color, contaminant problem；Essence
Discharged during desulfurizer regeneration containing organic sulfur, volatile phenol/quinones, cyanogen class waste gas, generally send torch burning to empty, and torch pair
The combustion efficiency of this kind of waste gas is general, often remaining significantly abnormal flavour and pollution.
The content of the invention
To solve above-mentioned technical problem, the present invention provides the desulfurizing and purifying technique that a kind of sour water strips ammonia, along ammonia
Air-flow to capital equipment include two can series-parallel catalysis oxidation adsorb and arrange in desulfurizing and purifying tower, desulfurizing and purifying tower and can fill
Divide the heat exchanger tube of drop mild heat desulfurizing agent bed, desulfurizing and purifying tower lower part outlet connection regeneration condenser, regeneration condenser bottom
Portion has can accomplished continuously or intermittently discharge liquid elemental sulfur but not discharge the sulfur outlet of gas；
Ammonia is entered before absorption desulfurizing and purifying tower to be allocated oxygen into and fully mixes, and the amount of allocating of oxygen is slightly more than anti-with sulfide
O needed for elemental sulfur should be generated2Amount, the sulfide concentration on-line determination in ammonia；
The filling of absorption desulfurizing and purifying tower can hot recycling catalytic oxidation adsorption desulfurizer, operation temperature 10-60 DEG C, by contained by ammonia
A small amount of organic sulfur, phenol/quinones, cyanogen class, hydro carbons absorption, by contained very small amount SO2With contained H2S reactions are converted into elemental sulfur and inhale
It is attached, by remaining H2S be oxidized to elemental sulfur and adsorb in endoporus and between granule；H in ammonia after process2S≤3ug/g, SO2≤
3ug/g, organic sulfur≤3ug/g is substantially free of phenol/quinones, cyanogen class, hydro carbons；
One of sulfide, phenol/quinones, cyanogen class, hydro carbons that desulfurizing and purifying tower operates into outlet ammonia exceedes after setting, desulfurization
Purifying column cuts out carries out elemental sulfur, sulfide, phenol/quinones, cyanogen class, hydro carbons that hot recycling blows down absorption deposition；Arrange during hot recycling
The material that goes out, gas enter regeneration condenser, and wherein molten sulfur and sulfur vapor is condensed into liquid sulfur, solid-state sulfur recovery, containing organic sulfur, phenol/
Quinones, cyanogen class, hydrocarbon, NH3、CO2Waste gas be incorporated to stripper overhead richness H2S gas pipelines, go combustion furnace of sulfur recovery device to process,
Or enter flare line and go to burn emptying.
It is described can hot recycling catalytic oxidation adsorption desulfurizer, can be by activated carbon supported Fe, Mn, Cu, Zn, Co etc. into
Divide the modified catalytic oxidation adsorption desulfurizer for preparing, the Sulfur capacity with >=20% (quality), and the H of≤1ug/L2S removes precision,
It is preferred that there are tempreture organic sulphur hydrolysis to convert the catalytic oxidation adsorption desulfurizer of removing ability, can also be by with higher H2S removings are held
The desulfurizing agent and the desulfurizing agent collocation with tempreture organic sulphur hydrolysis conversion removing ability of amount and precision is used, described with organic sulfur water
The desulfurizing agent of solution conversion removing ability also can substantially recover its performance by hot recycling, to improve COS, CS2, mercaptan etc. penetrates
Time, wherein COS are hydrolyzed to H2S is simultaneously further oxidized to elemental sulfur absorption deposition removing, and mercaptan is converted into that molecular weight is bigger, inhales
The bigger disulphide of attached amount, the disulphide also can blow away during hot recycling, so as to improve absorption desulfurizing and purifying
Tower accommodates the ability of organic sulfur before penetrating.The specific surface area of absorbent charcoal carrier is very big, with a large amount of hydrophobic groups, has to major part
Machine sulfur, phenol/quinones, cyanogen class, hydro carbons have stronger absorbability,
In the decontamination process of absorption desulfurizing and purifying tower, dominant response is H to ammonia2S、O2Reaction generates elemental sulfur, and this is anti-
Should there are heat release, every 1% volume H2S matches somebody with somebody aequum O2It is 60 DEG C or so that reaction generates the adiabatic temperature rise of elemental sulfur, in desulfurizing agent bed
The purpose for arranging heat exchanger tube and water-cooled is to avoid bed temperature from rising to decline with an absorption property caused by institute；In ammonia containing organic
When sulfur, phenol/quinones, cyanogen class, hydrocarbon are more, desulfurizing and purifying tower should adopt appropriate operation temperature, take into account the hydrolysis of organic sulfur
With residual organic sulfur, phenol/quinones, cyanogen class, hydrocarbon absorption, experience be 40-50 DEG C or so preferably.
Heat exchange in desulfurizing and purifying tower, except common spiral coil can be adopted, it is preferred to use vertical pipes heat exchange structure, its
The bed temperature difference is little when advantage is mainly desulfurizing and purifying, easy temperature control, and the heating higher than bed temperature permissible value can be adopted during regeneration
Medium temperature, stops a leak easily by shutting one or a few sleeve pipe during leakage, and agent is easily unloaded when desulfurizing decontaminating agent is scrapped.
The desulfurizing and purifying tower with vertical pipes heat exchange structure, with the lower slightly cooling water of temperature as shifting thermal medium,
Water inlet, draining and its to the distribution in sleeve pipe, collecting from sleeve pipe, are all disposed within intake chamber, the row of desulfurizing and purifying top of tower
Hydroecium；Sleeve pipe extends down into desulfurizing decontaminating agent bed, until the bottom of desulfurizing decontaminating agent bed, desulfurizing decontaminating agent bed it
, used as support, the quantity and heat exchange area of heat exchange sleeve is enough, to ensure exchange capability of heat for lower filling inert ceramic balls；It is described vertical
Sleeve pipe is formed by inner and outer tubes nesting, and inner tube, the upper port of outer tube connect respectively intake chamber, drip chamber, end closure under outer tube,
Inner tube lower end extends to outer tube lower end and is open, and to dirty, outer tube water is to upstream, inner tube, outer tube water, the stream of soda pop for inner tube water
To being formed by cooling water circulation pump power；By the shifting for controlling the entrance, the temperature difference of discharge and flow or sleeve pipe of cooling water
Heat energy power, can preferably control bed temperature during desulfurizing decontaminating agent normal operating, reach the little temperature difference, the degree of easy temperature control.By
Preferable in 40-50 DEG C of desulfurizing decontaminating agent bed temperature, 30 DEG C or so of cooling water inlet temperature of control, 40 DEG C or so of temperature at discharging condensate are i.e.
Can, except directly using the public recirculated water of plant area as cooling water, also can separately set, cooling water heat exchanger plant area is public to follow
Ring water gives indirect heat exchange, and the advantage of indirect heat exchange is easily found when cooling water leaks into ammonia or ammonia inleakage of cooling water, also
Cooling water can be done using pure water or deionized water.
When desulfurizing and purifying tower adopts above-mentioned vertical pipes heat exchange structure, heat exchange is there is also between inner and outer tubes, this is
It is different from a feature of spiral coil.Cooling water flow is identical, out temperature be all respectively 35 DEG C, 45 DEG C of premise
Under, when inner tube water flow to outer pipe bottom and started cooling effect, its temperature has had been raised to 39 DEG C, it is clear that the bed for being obtained
The temperature difference is less；Such case is more notable in desulfurizing agent hot recycling, especially can adopt in desulfurizing agent bed temperature-rise period
Higher heating medium inlet temperature.
In the desulfurizing and purifying tower with vertical pipes heat exchange structure, the vertical water cold sleeve should have it is appropriate between
Away from heat exchange area, move heat energy power, especially should try one's best using same casing size and spacing in ammonia entrance, in case surpassing
Temperature.Heat exchange sleeve gos deep into the height 0.5-10m of desulfurizing decontaminating agent bed, tube pitch 0.05-0.10m, heat exchange area 5-30m2/m3
Desulfurizing decontaminating agent.The positions and dimensions of desulfurizing decontaminating agent filling pipe should be appropriately arranged with, it is to avoid impact closes on the spacing of heat exchange sleeve,
Ensure that the desulfurizing decontaminating agent bed temperature below desulfurizing decontaminating agent filling pipe meets the requirements.
The structure of the desulfurizing and purifying tower desulfurizing decontaminating agent bed can be the axially or radially reaction according to ammonia flow direction
The structure of device can make desulfurizing decontaminating agent be easier to from reactor bottom draw off when scrapping, and new agent is filled from reactor head or upper lateral part
Fill out.Wherein preferably, reason is H to the axial arrangement of ammonia upper entering and lower leaving2S and O2Response speed quickly, is reacted and heat release set of regions
In, each vertical pipes water-cooled all plays at any time shifting heat effect during axial arrangement, thus temperature control and reaction effect are more preferable.
As H in outlet ammonia or follow-up ammonia product2One of S, organic sulfur, phenol/quinones, cyanogen class, hydrocarbon close setting
When, absorption desulfurizing and purifying tower carries out hot recycling process.Before desulfurizing agent hot recycling, can be first with nitrogen by the ammonia in desulfurizing and purifying tower
It is purged in the sour water before stripper entrance and is absorbed, but should takes appropriate measures and such as allocate into before sour water is passed through
Air or nitrogen, prevent sour water from quickly inhaling ammonia and flow backwards into desulfurizing and purifying tower, or are slowly blown in stripper suitable tower
Board position；And the water in hydroecium, drip chamber, sleeve pipe heat-tranferring system is released, is blown out.
250-300 DEG C of the hot regeneration temperature of desulfurizing and purifying tower.During hot recycling, to hydroecium be passed through 250-350 DEG C plus
Thermal medium such as hot blast, steam or conduction oil, using higher heat carrier temperature when desulfurizing decontaminating agent bed temperature is relatively low, afterwards
It is gradually lowered；It is gradually that desulfurization is net plus thermal medium from bottom to top returns drip chamber from top to bottom, then from outer tube from the inner tube of sleeve pipe
Agent bed is heated, and the most of absorption in desulfurizing decontaminating agent bed is deposited into branch's fusing, vaporization, flows through again from lower part outlet
Raw and cold condenser is collected and condenses elemental sulfur, containing organic sulfur, phenol/quinones, cyanogen class, hydrocarbon, NH3、CO2Waste gas be incorporated to stripper overhead
Rich H2S gas pipelines, go combustion furnace of sulfur recovery device to process, and can also enter flare line and go to burn emptying.During hot recycling to
Be passed through nitrogen, carbon dioxide in desulfurizing decontaminating agent bed continuously to be purged, will desorption thing blowout, further empty surface and interior
Hole, recovers desulfurizing and purifying performance.Can lead to cooling water in hydroecium, drip chamber, sleeve pipe heat-tranferring system after the completion of hot recycling and be down to 40 DEG C
It is stand-by below or come into operation, if it is necessary, can use the ammonia after purification to enter line replacement before coming into operation, deliver to stripper after ammonia displacement and enter
Absorbed in sour water before mouthful, but air or the nitrogen of such as allocate into before sour water is passed through that should taking appropriate measures, prevent
Only sour water is quickly inhaled ammonia and is flow backwards into desulfurizing and purifying tower；Or suitable tray location is slowly blown in stripper.
In the present invention, condenser is regenerated, preferably with somewhat larger inner space and heat exchange tube pitch, hot material porch
First half can condensing trapping liquid sulfur, the latter half of waste gas outlet further can condense to form solid-state sulfur, by will
Cooling water flow carries out appropriate height weave control, and the solid-state sulfur interval that latter half cooling tube surface condensation is formed melts
Discharge, separate elemental sulfur and waste gas and reach satisfied degree.Control condensator outlet EGT is not higher than 100 DEG C.
Regeneration condenser discharge molten sulfur, the container of molten sulfur storage tank or haulage vehicle can be flowed into, due to quantity it is less, generally
It is more excellent except the not high purposes of individual requests such as produces sulphuric acid again containing impurity such as some organic sulfurs, phenol/quinones, cyanogen class, hydrocarbon
Choosing is transported to the sulfur recovery facility with combustion furnace and processes, and organic sulfur conversion is entered into sulfur product for elemental sulfur, by phenol/quinone
The burn impurities such as class, cyanogen class, hydrocarbon are removed, and so as to the liquid sulfur is converted into into standard compliant sulfur product, and do not cause environment
Pollution；The liquid sulfur that condenser is discharged also can be cooled down directly makes block storage, transport.A small amount of waste water collected by condenser goes
Sour water pipeline or storage tank before stripper.
If more containing impurity such as organic sulfur, phenol/quinones, cyanogen class, the hydrocarbon for being difficult to convert in ammonia, desulfurizing and purifying Ta Yifa
Give birth to penetrating and being not susceptible to H for organic sulfur, phenol/quinones, cyanogen class, hydrocarbon etc.2When penetrating of S, it is contemplated that individually carry out such as 150 DEG C of left sides
Right impurity blows down, and at this time elemental sulfur will not blow out substantially, but organic sulfur, phenol/quinones, cyanogen class, the hydrocarbon major part adsorbed
Can deviate from, nitrogen, carbon dioxide now should be passed through in desulfurizing decontaminating agent bed and be continuously purged, desorption thing blowout is entered
One step empties surface and endoporus, recovers adsorption cleaning performance.
It is pointed out that moisture increased in the ammonia in the present invention after desulfurizing and purifying, incrementss mainly take
The certainly H in raw material ammonia2S contents.
When adsorption desulfurizing agent is through the use of long period, hydraulic performance decline is unloaded to a certain extent before agent scraps, and can be carried out again
It is raw to process, by the elemental sulfur for being adsorbed, organic sulfur, phenol/quinones, cyanogen class, NH3、CO2Blow down Deng gasification, the useless agent after process is basic
Without abnormal flavour, agent process safety health, basic nonhazardouss are unloaded.Useless agent does not have abnormal flavour and murder by poisoning because basic, without sulfur, it is easy to should
With or storage, transport, process, can be used for it is less demanding absorption or refined purposes, can also enter boiler and burn, containing going back for cobalt
Receive metal.
In the desulfurizing and purifying technique of sour water stripping ammonia of the present invention, the amount of oxygen is allocated in purification process into, it is less slightly
In and H2When S generates the amount needed for simple substance reaction of Salmon-Saxl, ammonia can reach O after purification2The level of≤10ug/g, desulfurization precision is constant,
Simply adsorb the desulfurizing and purifying tower regeneration period slightly shorter；Generally control remnants O2Both desulfurization essence had been can guarantee that during 100-800ug/g
Degree, and the longer absorption desulfurizing and purifying tower regeneration period can be obtained.
In the desulfurizing and purifying technique of sour water stripping ammonia of the present invention, contained H in ammonia2S、SO2、COS、CS2Can base
Elemental sulfur is changed on this, elemental sulfur blowout and the collection of condensed device, discharge during hot recycling；End conversion contained in ammonia is organic
Sulfur, phenol/quinones, cyanogen class, hydrocarbon, are blown, except small part Jing in absorption desulfurizing and purifying tower during absorption retention removing, hot recycling
Regeneration condenser enters the elemental sulfur of condensation, and remaining is mostly as exhaust gas component Jing stripper overheads richness H2S gas pipelines, desulfuration
Sulphur retracting device combustion furnace is processed, or removes torch burning and exhausting.
The desulfurizing and purifying technique of sour water of the present invention stripping ammonia is relatively simple, in normal operation can unmanned, far
Journey Monitoring and Controlling, because having the collection of liquid sulfur, accumulating problem and supplying heat problem during regeneration, need personnel on site's operation and
Control.
The sour water of the present invention strips the desulfurizing and purifying technique of ammonia, with advantages below：
1st, ammonia sulfur content is low after purifying, and the impurity such as organic sulfur, phenol/quinones, cyanogen class, hydrocarbon is substantially free of, to postorder process equipment
Corrosion such as compressor mitigates；
2nd, ammonia after purifying, impurity level can reach H2S≤3ug/g, SO2≤ 3ug/g, organic sulfur≤3ug/g；Can be further
Liquefied ammonia is prepared, the requirement of Liquid Anhydrous Ammonia GB536-88 Grade A standards, and water white transparency is easily reached；
3rd, contained in ammonia end conversion organic sulfur, phenol/quinones, cyanogen class, hydrocarbon, absorption retention removing in Jing absorption desulfurizing and purifying towers
Afterwards, it is blown during hot recycling, mostly as exhaust gas component Jing stripper overheads richness H2S gas pipelines, remove sulfur recovery facility
Combustion furnace is processed, or removes torch burning and exhausting, solves a difficult problem for puzzlement this class device；
4th, purification process is reliable and stable, easy to control, and treating capacity is big, normal operation unmanned；
5th, the whereabouts such as impure molten sulfur, regeneration tail gas rationally, is discharged or even three-waste free discharge, non-environmental-pollution without waste gas and waste liquid,
Site environment is preferable；
6th, easily draw off when desulfurizing decontaminating agent is scrapped, unload agent process safety health, useless agent does not have abnormal flavour, basic nonhazardouss substantially,
It is easy to apply or store, transport, process.
This purification Technological adaptability is strong, can be used to process containing a small amount of SO2, COS, organic sulfur such as mercaptan, thioether, CS2And contain
Organic sulfur, phenol/quinones, cyanogen class, the sour water stripping ammonia of hydrocarbon, purification effect is preferable；The sour water includes oil plant, coal
Sour water and partial hydrogenation produced by chemical plant, coking of coal factory, natural gas from coal factory and portion of natural gas processing unit (plant)
The aqueous solution of device recycle hydrogen process gained sulfide hydrogen and ammonia.
Description of the drawings
Fig. 1, ammonia desulfurizing and purifying process flow diagram.
Fig. 2, adsorbs ammonia desulfurizing and purifying process flow diagram when desulfurizing and purifying tower regenerates.
Fig. 3, the radial flow desulfurizing and purifying tower sketch with vertical pipes heat exchange structure.
Fig. 4, the downflow system desulfurizing and purifying tower sketch with vertical pipes heat exchange structure.
Legend：1 desulfurizing and purifying tower shell, 2 desulfurizing decontaminating agent beds, 3 desulfurizing decontaminating agents filling pipe, 4 intake chambers, 5 heat exchange
Sleeve pipe inner tube, 6 heat exchange sleeve outer tubes, 7 dividing plates, the radial direction reaction bed container of 8 side cornice passages, 9 radial directions with passage
Reaction bed inner tube, 10 vertical water-cooled heat exchange sleeves, 11 support porcelain ball, 12 discharge outlet, 13 water inlets, 14 desulfurizing decontaminating agents to unload agent
Mouthful, 15 ammonia import or exports, 21 drip chambers, 22 coolings/condenser.
Specific embodiment
Embodiment
A set of ammonia desulfurization purifier, its technological process such as accompanying drawing 1 are set up in coal plant sour water stripper plant
It is shown.
Ammonia desulfurization purifier, along the H that airflow direction mainly includes being sequentially connected2S concentration in-line analyzers, oxygen are matched somebody with somebody
Enter pipe and static mixer, two can connection in series-parallel and the 20M that can cut out3Downflow system desulfurization with vertical pipes heat exchange structure is net
Change tower；Desulfurizing and purifying tower bottom outlet one 1M of connection3Simple substance sulfur condenser（Water-cooled, heat exchange area 15M2）, the condenser can use
Make ammonia cooling or condense elemental sulfur when regenerating；Wherein the overall structure of desulfurizing and purifying tower as shown in Figure 4, under ammonia is enterprising
Go out.
In ammonia desulfurization purifier, desulfurizing and purifying tower includes reactor body, water vapor heat-tranferring system, reactor body
Do not connect with water vapor heat-tranferring system；Reactor body includes that housing 1, reactive desulfurizing agent bed 2, ammonia import and export 15, desulfurization
Agent filling pipe 3, desulfurizing agent unloads agent mouth 14；Desulfurizing agent bed bottom is supported by porcelain ball 11；Water vapor heat-tranferring system includes intake chamber
4th, drip chamber 21, vertical water-cooled move thermal sleeve 10, move thermal sleeve and are formed by inner tube 5 is nested with outer tube 6, and outer tube upward opening is in row
Hydroecium base plate, extends downwardly under desulfurizing agent bed position and in lower end closure；Inner tube lower end extends to outer pipe bottom, upper end
Extend to outside outer tube upper port；The height 4.5m of desulfurizing agent bed；Move spacing 56mm of thermal sleeve, sleeve pipe inner tube Φ
19x2mm, outer tube Φ 38x3mm, sleeve pipe radical 680, the m of heat exchange area 3603；Reactor diameter Φ 2600mm, total high 7500mm.
Load 10M in desulfurizing and purifying tower middle and upper part3XDS-2 ammonia desulfurizing agents, bottom filling 9M3XDS-1 ammonia desulfurizing agents, bottom
Load 0.6M in portion3Inert ceramic balls are supported.Two kinds of ammonia desulfurizing agents of described XDS-2, XDS-1 are that Shandong is fast limited up to Chemical Group
The product grade of company, is all activated carbon modified Fine Desulfurizer at Ambient Temperature, mainly by by H2S and O2Reaction generates elemental sulfur simultaneously
Absorption is deposited and removes the H contained by ammonia2S, in H2S 0-2%（Volume）Relative broad range in, with slightly many O2And fully mix
When can process to H2S≤3ug/g, wherein working sulfur capacity >=20% (quality), XDS-1 ammonias desulfurizing agent also have certain organic
Sulfur hydrolysis ability, can be by COS, CS2It is hydrolyzed to H2S simultaneously further generates elemental sulfur adsorbing and removing；Both ammonia desulfurizing agents
Can also adsorbing and removing end conversion organic sulfur and phenol/quinones, cyanogen class, hydrocarbon, removing precision can be usually reached Organic substance≤3ug/g's
Level；In 40-50 DEG C or so of temperature conditionss, two kinds of desulfurizing agents in above-mentioned filling ratio, the conversion of its tempreture organic sulphur hydrolysis with
The overall performance that residual organic sulfur, phenol/quinones, cyanogen class, hydrocarbon adsorb is preferable.Two kinds of ammonia desulfurizing agents of described XDS-2, XDS-1, also
Can be purged by 250-300 DEG C of hot recycling and indifferent gas, elemental sulfur, organic sulfur and phenol/quinones, the cyanogen of deposition is adsorbed in blowing
The compositions such as class, hydrocarbon, recover its desulfurizing and purifying performance substantially.
The main operating process conditions of ammonia desulfurization purifier are：
The basic composition of stripping ammonia（Volume content）And flow：H2S0.8-1.0%, COS0.005-0.01%, CS20.01-
0.03%th, H2O 1.0-1.5%, it is remaining for ammonia, flow 300- containing other organic sulfurs, phenol/quinones, cyanogen class, hydrocarbon 300-600ppm
400NM3/h；According to H2The amount of S allocates oxygen into O2Excessive about 0.02%；
33 DEG C of the ammonia inlet temperature of desulfurizing and purifying tower, 33 DEG C of room temperature of water inlet, 41 DEG C of draining room temperature, desulfurizing decontaminating agent bed
3 DEG C of the temperature difference of 46 DEG C of temperature, differing heights and diameter key position；Work off one's feeling vent one's spleen composition permissible value H2S≤3ug/g NH3, SO2≤
1ug/g NH3, O250-200 ug/g NH3, organic sulfur≤3 ug/g NH3, phenol/quinones+cyanogen class+hydrocarbon≤10 ug/g NH3。
After ammonia desulfurization purifier comes into operation, desulfurizing and purifying tower single-tower operation, another tower is standby, has operated 25 for the first time
My god, to H2The close permissible value upper limits of S, period organic sulfur, phenol/quinones, cyanogen class, hydrocarbon are qualified.After incision stand-by still, cut out with rear tower
Regeneration.Before the regeneration of desulfurizing and purifying tower, the ammonia in desulfurizing and purifying tower is first purged to the acidity before stripper entrance with nitrogen dirty
Absorbed in water, allocate into before sour water is passed through a small amount of air prevent sour water quickly inhale ammonia flow backwards enter desulfurizing and purifying
Tower；The water of intake chamber, drip chamber is blown out as far as possible with purification wind, is collected into water pot.
During the hot recycling of desulfurizing and purifying tower, with the 280-350 DEG C of hot blast preheated in heating furnace circulation heating, hot blast are beaten
Enter sleeve pipe inner tube from intake chamber dirty, then from outer pipe bottom upstream returning drainage room, 350 DEG C of hot blast temperature when regeneration starts, with bed
The rising of layer temperature is gradually decreased to 300 DEG C, 280 DEG C of hot blast temperature during constant temperature；Being passed through nitrogen in desulfurizing decontaminating agent bed is carried out
Continuous purging, reactivation outlet material, gas enter condenser, and initial stage condensation waste water removes Water Tank before stripper, fusing, the list of gasification blowout
Matter sulfur is condensed and collected, containing organic sulfur, phenols, cyanogen class, hydrocarbon, NH3、CO2The condensed device air vent of waste gas to connect stripper overhead rich
H2S gas pipelines, go combustion furnace of sulfur recovery device to process.After being regenerated to 250 DEG C of temperature of working off one's feeling vent one's spleen, stop Hot-blast Heating, continue
After nitrogen purge 10 hours, desulfurizing and purifying tower intake chamber, drip chamber use instead it is cooling water circulation stop nitrogen after being cooled to 50 DEG C,
Switchback carries out ammonia desulfurizing and purifying, and another tower cuts out standby.It is continuing with as ammonia cooler after the drained molten sulfur of condenser.Heat is again
The raw molten sulfur discharged of collecting is condensed into bulk, and gross weight 2800kg illustrates desulfurization capacity of the desulfurizing agent under above-mentioned use condition extremely
It is less 20%（Quality）.
The desulfurizing and purifying tower completes after first time hot recycling comes into operation, to have passed through 10 regeneration periods, every time the operating of regeneration
Time, all at 25 days or so, is all H2The close permissible value upper limits of S, period organic sulfur, phenol/quinones, cyanogen class, hydrocarbon are all qualified, place
Ammonia is processed further the liquefied ammonia for producing after reason, and total S≤1ug/g, water white transparency reaches Liquid Anhydrous Ammonia GB536-88 Grade As
The requirement of standard, illustrates XDS-2, XDS-1 desulfurizing agent effect used in the ammonia desulfurization purifier operation process of the present invention
Preferably, its performance is recovered substantially after hot recycling, also illustrates the ammonia desulfurization purifier of the present invention to H2S, organic sulfur, phenols,
Cyanogen class, hydrocarbon removing clean-up effect it is preferable.
The ammonia desulfurization purifier of the present invention, its technology controlling and process and obtained ammonia, the quality of liquefied ammonia, are all substantially better than
The NH for adopting before4The old technique of HS crystallization+desulfurizing agents, the NH of old technique4HS crystalline qualities are general, to organic sulfur, phenols, cyanogen class,
The process of hydrocarbon and its whereabouts arrange not reasonable.
Claims (10)
1. a kind of sour water strips the desulfurizing and purifying technique of ammonia, and flowing to capital equipment along ammonia can be series-parallel including two
Catalysis oxidation adsorbs setting in desulfurizing and purifying tower, desulfurizing and purifying tower can fully drop the heat exchanger tube of mild heat desulfurizing agent bed,
Desulfurizing and purifying tower lower part outlet connection regeneration condenser, regeneration condenser bottom has can accomplished continuously or intermittently discharge liquid elemental sulfur
But do not discharge the sulfur outlet of gas；
Ammonia is entered before absorption desulfurizing and purifying tower to be allocated oxygen into and fully mixes, and the amount of allocating of oxygen is slightly more than anti-with sulfide
O needed for elemental sulfur should be generated2Amount, the sulfide concentration on-line determination in ammonia；
The filling of absorption desulfurizing and purifying tower can hot recycling catalytic oxidation adsorption desulfurizer, operation temperature 10-60 DEG C, by contained by ammonia
A small amount of organic sulfur, phenol/quinones, cyanogen class, hydro carbons absorption, by contained very small amount SO2With contained H2S reactions are converted into elemental sulfur and inhale
It is attached, by remaining H2S be oxidized to elemental sulfur and adsorb in endoporus and between granule；H in ammonia after process2S≤3ug/g, SO2≤
3ug/g, organic sulfur≤3ug/g is substantially free of phenol/quinones, cyanogen class, hydro carbons；
One of sulfide, phenol/quinones, cyanogen class, hydro carbons that desulfurizing and purifying tower operates into outlet ammonia exceedes after setting, desulfurization
Purifying column cuts out carries out elemental sulfur, sulfide, phenol/quinones, cyanogen class, hydro carbons that hot recycling blows down absorption deposition；Arrange during hot recycling
The material that goes out, gas enter regeneration condenser, and wherein molten sulfur and sulfur vapor is condensed into liquid sulfur, solid-state sulfur recovery, containing organic sulfur, phenol/
Quinones, cyanogen class, hydrocarbon, NH3、CO2Waste gas be incorporated to stripper overhead richness H2S gas pipelines, go combustion furnace of sulfur recovery device to process,
Or enter flare line and go to burn emptying.
2. sour water as claimed in claim 1 strips the desulfurizing and purifying technique of ammonia, it is characterised in that catalysis oxidation is adsorbed
There are desulfurizing agent tempreture organic sulphur hydrolysis to convert removing ability, and can substantially recover its performance by hot recycling.
3. sour water as claimed in claim 2 strips the desulfurizing and purifying technique of ammonia, it is characterised in that by described with having
Machine sulfur hydrolysis remove the desulfurizing agent of ability and have higher H2The desulfurizing agent and collocation of S removing capacity and precision is used.
4. sour water as claimed in claim 1 strips the desulfurizing and purifying technique of ammonia, it is characterised in that in desulfurizing and purifying tower
Using vertical pipes heat exchange structure.
5. sour water as claimed in claim 4 strips the desulfurizing and purifying technique of ammonia, it is characterised in that described with vertical
The desulfurizing and purifying tower of sleeve heat exchange structure, with the lower slightly cooling water of temperature as shifting thermal medium, water inlet, draining and its in sleeve pipe
Distribution, collecting from sleeve pipe, be all disposed within intake chamber, the drip chamber of desulfurizing and purifying top of tower；Sleeve pipe is extended down into
Desulfurizing decontaminating agent bed, until the bottom of desulfurizing decontaminating agent bed；The vertical pipes are formed by inner and outer tubes nesting, interior
Pipe, the upper port of outer tube connect respectively intake chamber, drip chamber, and end closure under outer tube, inner tube lower end extends to outer tube lower end and opens
Mouthful, to dirty, outer tube water is formed inner tube water to upstream, inner tube, outer tube water, the flow direction of soda pop by cooling water circulation pump power.
6. sour water as claimed in claim 5 strips the desulfurizing and purifying technique of ammonia, it is characterised in that the vertical water-cooled
Sleeve pipe gos deep into the height 0.5-10m of desulfurizing decontaminating agent bed, tube pitch 0.05-0.10m, heat exchange area 5-30m2/m3Desulfurizing and purifying
Agent.
7. sour water as claimed in claim 1 strips the desulfurizing and purifying technique of ammonia, it is characterised in that desulfurizing decontaminating agent bed
The structure of layer is axially or radially according to ammonia flow direction.
8. sour water as claimed in claim 7 strips the desulfurizing and purifying technique of ammonia, it is characterised in that desulfurizing decontaminating agent bed
Layer is the axial arrangement of ammonia upper entering and lower leaving.
9. sour water as claimed in claim 1 strips the desulfurizing and purifying technique of ammonia, it is characterised in that desulfurizing decontaminating agent bed
Inert ceramic balls are loaded under layer as support.
10. sour water as claimed in claim 1 strips the desulfurizing and purifying technique of ammonia, it is characterised in that desulfurizing and purifying tower
250-300 DEG C of hot regeneration temperature, and be passed through nitrogen, carbon dioxide in desulfurizing decontaminating agent bed and continuously purged.
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| CN106947539A (en) * | 2017-05-08 | 2017-07-14 | 淄博赢信达知识产权咨询服务有限公司 | The technique for preparing low hydrogen CO gas |
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| CN106986341A (en) * | 2017-05-08 | 2017-07-28 | 淄博赢信达知识产权咨询服务有限公司 | A kind of technique for preparing CO gas |
| CN110937648A (en) * | 2019-12-25 | 2020-03-31 | 浙江工业大学 | Process and device for continuously treating high-concentration organic wastewater |
| CN115259259A (en) * | 2022-07-18 | 2022-11-01 | 陕西未来能源化工有限公司 | Conversion condensate treatment system and process |
| CN115724407A (en) * | 2021-08-31 | 2023-03-03 | 中国石油化工股份有限公司 | Liquid sulfur degassing device and method |
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