CN1298629C - Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification - Google Patents
Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification Download PDFInfo
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- CN1298629C CN1298629C CNB2005100106577A CN200510010657A CN1298629C CN 1298629 C CN1298629 C CN 1298629C CN B2005100106577 A CNB2005100106577 A CN B2005100106577A CN 200510010657 A CN200510010657 A CN 200510010657A CN 1298629 C CN1298629 C CN 1298629C
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- ammonia
- ammoniacal liquor
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- acid
- phenol
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- 238000000034 method Methods 0.000 title claims abstract description 27
- 235000011114 ammonium hydroxide Nutrition 0.000 title claims description 34
- 238000002309 gasification Methods 0.000 title claims description 7
- 239000003077 lignite Substances 0.000 title claims description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 79
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 38
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 34
- 238000010521 absorption reaction Methods 0.000 claims abstract description 23
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000007788 liquid Substances 0.000 claims abstract description 15
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 12
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims abstract description 11
- 239000002253 acid Substances 0.000 claims abstract description 10
- 239000003463 adsorbent Substances 0.000 claims abstract description 10
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 6
- 238000004064 recycling Methods 0.000 claims abstract description 4
- 239000012266 salt solution Substances 0.000 claims abstract description 3
- 239000002594 sorbent Substances 0.000 claims description 22
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 claims description 18
- 235000011089 carbon dioxide Nutrition 0.000 claims description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 10
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 7
- 229910052760 oxygen Inorganic materials 0.000 claims description 7
- 239000001301 oxygen Substances 0.000 claims description 7
- 230000001172 regenerating effect Effects 0.000 claims description 7
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 5
- 229910017604 nitric acid Inorganic materials 0.000 claims description 5
- 230000008929 regeneration Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- 230000002572 peristaltic effect Effects 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 102000004316 Oxidoreductases Human genes 0.000 claims description 2
- 108090000854 Oxidoreductases Proteins 0.000 claims description 2
- 238000009835 boiling Methods 0.000 claims description 2
- 230000005587 bubbling Effects 0.000 claims description 2
- 238000011049 filling Methods 0.000 claims description 2
- 230000007420 reactivation Effects 0.000 claims description 2
- 238000010792 warming Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 4
- XABJJJZIQNZSIM-UHFFFAOYSA-N azane;phenol Chemical compound [NH4+].[O-]C1=CC=CC=C1 XABJJJZIQNZSIM-UHFFFAOYSA-N 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 9
- 238000000746 purification Methods 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 5
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 4
- QLULGSLAHXLKSR-UHFFFAOYSA-N azane;phosphane Chemical compound N.P QLULGSLAHXLKSR-UHFFFAOYSA-N 0.000 description 4
- 239000013078 crystal Substances 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 4
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 3
- 230000008025 crystallization Effects 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003599 detergent Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000012855 volatile organic compound Substances 0.000 description 1
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- Industrial Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention relates to a method for recycling dirty liquid ammonia containing volatile phenol, carbon dioxide, hydrogen sulfide and other volatile substances. Under a heating condition, dirty liquid ammonia is boiled, the top temperature of a rectifying tower is controlled, most of water back flows and ammonia, the volatile phenol, the carbon dioxide, the hydrogen sulfide and other volatile substances become gases. In an absorption tower filled with adsorbent, the volatile phenol, the hydrogen sulfide and other volatile substances are selectively absorbed by the adsorbent. The carbon dioxide and the ammonia enter acid absorption liquid. The ammonia and the acid react to generate corresponding ammonium salt solution. The carbon dioxide does not react with the acid and escapes out, and thus, the ammonia is recycled. The present invention has the advantages that the recycling rate of ammonia reaches more than 90%, the content of the ammonium salt phenol is less than 0.00015%, the adsorbent can be regenerated and utilized, the production cost is low, etc.
Description
(1) technical field: dirty ammoniacal liquor is recycled
(2) background technology: domestic in recent years many scholars have carried out more research to the method that contains assorted ammoniacal liquor recovery ammonia; wherein many scientific research institutions and enterprise are for recovery and the existing patent of utilization and the bibliographical information of ammonia; these processing modes that contain assorted ammoniacal liquor of conclude have following four kinds: (1) to carbonated ammoniacal liquor only, NH is studying in southization Group Co.,Ltd and Shanghai Chemical Research Inst
3-CO
2-H
2On the O ternary system basis, desorb, rectifying and anti-crystallization technique are combined, develop integrated isolation technique, and successfully use it for the transformation of carbon containing ammoniacal liquor retrieving arrangement, obtain purified gas ammonia or liquefied ammonia; (2) precipitation desulfurization, fractionation by distillation absorption process are the precipitation agent desulfurization to ammonia water containing sulfur with the ferrous sulfate, and ammoniacal liquor synthesizes with carbonic acid gas through fractionation by distillation and absorption again after the desulfurization, belongs to a kind of treatment method with comprehensive utilization; (3) film absorption method equipment is simple, and is easy to operate, and no burn into is pollution-free, and along with the development of membrane technique, the application of this method has the trend that progressively enlarges; (4) phosphorus ammonium selectivity absorption process reclaims the ammonia in the weak ammonia with gas sewage extracting and dephenolizing, ammonia still process treatment process.To containing CO
2, H
2The dirty ammoniacal liquor of volatile organic compounds such as S and phenol, aniline, pyridine, (1), (2) class methods obviously can not be suitable for, and the film absorption method mainly adopts PP, PP/CAB film, can not intercept organism fully to penetrate, and the application of present heavy industrialization is still few.In phosphorus ammonium selectivity absorption process, the volatile organic matter in the ammoniacal liquor will be with NH in the ammonia still process process
3, H
2O enters into the phosphorus ammonium, and during desorb, organism can be with NH in desorption tower for phosphorus ammonium pregnant liquor
3Enter strong aqua, can not solve the purifying problem of ammonia.
At containing CO
2, H
2Multiple organic dirty ammoniacal liquor such as S, oil, phenol, pyridine and aniline, if adopting under the condition of heating is evaporated the ammonia in the dirty ammoniacal liquor, directly carry out neutralization reaction with acid (nitric acid or sulfuric acid) absorption liquid, generate the technology of corresponding ammonium salt, in absorption process, following variation will take place in the absorption liquid color: colourless → yellowish → pale yellow → Huang → orange → reddish brown → brownish black, and absorption liquid off-odor enrichment progressively, evaporative crystallization obtains ammonium salt, and denseer stink is arranged.Here it is, and our gas phase purifying that proposes is recycled the processing method of ammonia, carries out the purification of ammonia and recycles, and reclaims in the product not contain organism substantially, and waste water obtains purification to a certain degree.
(3) summary of the invention
The objective of the invention is to contain CO at brown coal pressurized gasification
2, H
2Multiple organic dirty ammoniacal liquor such as S, oil, phenol, pyridine, the dirty ammoniacal liquor gas phase purifying of proposition is recycled the method for ammonia, and the ammonium salt product that recovery ammonia is produced does not contain other organism, and quality reaches agricultural first grade requirement, and waste water obtains corresponding purification.
Fig. 1 is that the dirty ammoniacal liquor of the present invention purifies the recovery process synoptic diagram,
Dirty ammoniacal liquor purifies the recovery process device as shown in Figure 1, and dirty ammoniacal liquor is from raw material ammonia tank 1 (main component the dirty ammoniacal liquor: NH
3Content 50～200g/L, CO
2Content 10～80g/L, phenol content 0～6g/L, H
2S content 0～3g/L, pyridine content 0～0.3g/L, pH value 10-11), squeeze into still kettle 4 by peristaltic pump 3 meterings, dirty ammoniacal liquor input speed 3-6mL/min ammoniacal liquor in still kettle is heated to boiling, regulate 95～100 ℃ of thermal source 9 control still temperature, regulate rectifying tower 5 chuck cooling water flows, 60～80 ℃ of control tower top temperatures, make ammonia, phenol, carbonic acid gas, pyridine, hydrogen sulfide and other volatile matter enter gas phase, it is in 75～90 ℃ the absorption column 6 of filling sorbent material that this gas phase is introduced temperature, most of hydrogen sulfide, phenol, pyridine and other volatile organic matter are adsorbed agent absorption, carbonic acid gas, remaining hydrogen sulfide, ammonia enters acid and absorbs liquid bath 7, and (acid is nitric acid, concentration 40%～60% or sulfuric acid, concentration 60%～98%), ammonia and acid-respons generate corresponding ammonium salt solution, and carbonic acid gas is not overflowed with acid-respons, hydrogen sulfide has been realized the recycling of ammonia by acid oxidase.Waste water after the ammonia still process is got waste liquid tank 2 by peristaltic pump, because ammonia wherein, phenol, carbonic acid gas, hydrogen sulfide and other volatile matter have been deviate from distillation, has also correspondingly obtained purification.After adsorbents adsorb is saturated, reusable through regeneration.
Adsorbent reactivation is that the preparation reproducing adsorbent is filled in regeneratory furnace, feed carbon dioxide gas, the control carbon dioxide flow is 380 ℃ ± 15 ℃ of 2～15 times of sorbent material volume amount/min, temperature, with 3～5 ℃ of temperature rise rates regeneratory furnace is warming up to 380 ℃ ± 15 ℃, bubbling air mixed with carbon dioxide gas after sorbent material heated 4h, regulate the oxygen level 4～5% of air, regulate the content 5-7.5% of atmospheric oxygen behind the reheat 2h, after continuing heating 1h, close air, carbonic acid gas successively, regeneratory furnace treats that sorbent material reduces to room temperature, regeneration ending.
The present invention has ammonia recovery and reaches more than 90%, does not contain organism in the absorption liquid substantially, and ammonium salt phenol content is less than 0.00015%, sorbent material reproducible utilization, advantage such as production cost is low.
(4) description of drawings
Fig. 1 is that dirty ammoniacal liquor of the present invention purifies the recovery process synoptic diagram.1 is the dirty ammonia vessel, the 2nd of raw material among the figure, waste liquid ammonia vessel, the 3rd, and peristaltic pump, the 4th, still kettle, the 5th, rectifying tower, the 6th, absorption column, the 7th, acid absorbs liquid bath, the 8th, cooling water jecket, the 9th, thermal source.
(5) embodiment
Embodiment 1
Dirty ammoniacal liquor NH
3Content 126.1g/L, phenol 4.26g/L, pH value 11.Sorbent material is a ZX-15 type gac, loadings 17g, 96 ℃ of still kettle temperature, 67 ℃ of rectifying tower top temperature, dirty ammoniacal liquor input speed 5.5mL/min is behind the charging 1300mL, concentration 50% nitric acid absorption liquid begins variable color, especially it is obvious to absorb the variable color of mouth of pipe place, shows that adsorption tube begins to penetrate, processed waste water NH
3Content 11.1g/L, pH value 9.5, ammonia recovery reaches 91.2%.The 17g sorbent material is purified ammonia 149.5g altogether, the about 8.79g NH of the detergent power of sorbent material
3/ g sorbent material.Analyze in the absorption liquid and do not contain organism substantially, obtain not having stink white ammonium nitrate crystal behind the condensing crystal, analytical results shows that its phenol content is less than 0.00015%, and all the other index ' s qualities meet the agricultural crystallization ammonium nitrate acceptable end product index of " GB2945-1989 ammonium nitrate " regulation.
Embodiment 2
Dirty ammoniacal liquor NH
3Content 95.1g/L, phenol 3.56g/L, pH value 10.The sorbent material CAN-230-B type gac of regenerating 10 times, loadings 11.2g, 96 ℃ of still kettle temperature, 80 ℃ of rectifying tower top temperature, behind the dirty ammoniacal liquor input speed 3.2mL/min charging 1300mL, concentration 80% sulfuric acid absorption liquid begins variable color, processed waste water NH
3Content 4.4g/L, pH value 8.5, ammonia recovery 91.8%.11.2g sorbent material is purified ammonia 62.5g altogether, the about 5.6g NH of the detergent power of sorbent material
3/ g sorbent material, purification efficiency reach 65% of novel sorbents.The absorption liquid condensing crystal obtains the ammonium salt crystal, and analytical results indicates that its phenol content is less than 0.00015%, and all the other index ' s qualities meet agricultural crystallization sulphur ammonium acceptable end product index.
Embodiment 3
To prepare reproducing adsorbent (CAN-230-B gac) 14.5315g, fill in tube furnace, control carbon dioxide flow 200mL/min, and be heated to 380 ℃, tube furnace is heated to 380 ℃ with 3～5 ℃ of temperature rise rates, aerating oxygen mixes with carbon-dioxide flow behind the heating 4h, regulate oxygen level 4～5%, continue to regulate oxygen level 6.5～7.5% behind the heating 2h, after continuing to heat 1h, close air, carbonic acid gas successively, tube furnace, treat that sorbent material reduces to room temperature, regeneration ending, reproducing adsorbent 13.2554g.This sorbent material is used for purified ammonia, and purification efficiency reaches 75.7% of novel sorbents.
Claims (4)
1, the dirty ammoniacal liquor recoverying and utilizing method of a kind of brown coal pressurized gasification, it is characterized in that, dirty ammoniacal liquor is squeezed into still kettle (4) from raw material ammonia tank (1) by peristaltic pump (3) metering, dirty ammoniacal liquor input speed 3-6mL/min, ammoniacal liquor is heated to boiling in still kettle (4), regulate 95～100 ℃ of thermal source (9) control still temperature, regulate rectifying tower (5) chuck cooling water flow, 60～80 ℃ of control tower top temperatures, make ammonia, phenol, pyridine, carbonic acid gas, hydrogen sulfide and other volatile matter enter gas phase, it is in 75～90 ℃ the absorption column (6) of filling sorbent material that this gas phase is introduced temperature, most of hydrogen sulfide, phenol, pyridine and other volatile organic matter are adsorbed agent absorption, carbonic acid gas, residue hydrogen sulfide, ammonia enters acid and absorbs liquid bath (7), and ammonia and acid-respons generate corresponding ammonium salt solution, and carbonic acid gas is not overflowed with acid-respons, hydrogen sulfide has been realized the recycling of ammonia by acid oxidase.
2, the dirty ammoniacal liquor recoverying and utilizing method of brown coal pressurized gasification according to claim 1 is characterized in that main component: NH in the described dirty ammoniacal liquor
350～200g/L, CO
210～80g/L, phenol 0～6g/L, H
2S 0～3g/L, pyridine 0～0.3g/L, pH value 10-11.
3, the dirty ammoniacal liquor recoverying and utilizing method of brown coal pressurized gasification according to claim 1 is characterized in that described absorption liquid is nitric acid or sulfuric acid liquid, concentration of nitric acid 40%～60%, sulfuric acid concentration 60%～98%.
4, the dirty ammoniacal liquor recoverying and utilizing method of brown coal pressurized gasification according to claim 1, it is characterized in that, this method also comprises the regeneration of sorbent material, adsorbent reactivation is that reproducing adsorbent is filled in the regeneratory furnace, feed carbonic acid gas, the control carbon dioxide flow is 2～15 times of sorbent material volume amount/min, 380 ℃ ± 15 ℃ of temperature, with 3～5 ℃ of temperature rise rates regeneratory furnace is warming up to 380 ℃ ± 15 ℃, bubbling air mixed with carbon-dioxide flow after sorbent material heated 4h, regulate the oxygen level 4～5% of air, regulate the content 5-7.5% of atmospheric oxygen behind the reheat 2h, after continuing heating 1h, close air successively, carbonic acid gas, regeneratory furnace, treat that sorbent material reduces to room temperature, regeneration ending.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100106577A CN1298629C (en) | 2005-02-17 | 2005-02-17 | Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100106577A CN1298629C (en) | 2005-02-17 | 2005-02-17 | Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification |
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| Publication Number | Publication Date |
|---|---|
| CN1657411A CN1657411A (en) | 2005-08-24 |
| CN1298629C true CN1298629C (en) | 2007-02-07 |
Family
ID=35007145
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|---|---|---|---|
| CNB2005100106577A Expired - Fee Related CN1298629C (en) | 2005-02-17 | 2005-02-17 | Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101362620B (en) * | 2007-08-09 | 2010-09-22 | 谢建中 | Phenolic waste water treatment technology from hydroxyphenylglycine synthesis process |
| CN101863523B (en) * | 2010-05-21 | 2012-07-11 | 赛鼎工程有限公司 | Method for treating ammonia-containing waste water from crushed coal pressure gasification |
| CN105110350B (en) * | 2015-08-13 | 2017-08-01 | 神华集团有限责任公司 | Ammonia recovery system and ammonia recovery method |
| CN109650631B (en) * | 2019-02-16 | 2021-07-20 | 中铝矿业有限公司 | Method for controlling ammonia water concentration in coal gas production process |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB552843A (en) * | 1941-01-07 | 1943-04-28 | Percy Parrish | Improvements in or relating to the manufacture of 25 to 30% liquor ammonia |
| CN86104483A (en) * | 1986-06-28 | 1988-03-02 | 贵阳市科学技术情报研究所 | From ammoniacal liquor, reclaim the novel process of ammonia |
| CN1056893A (en) * | 1991-07-04 | 1991-12-11 | 东北煤气化设计研究所 | Gas sewage extracting and dephenolizing, ammonia still process treatment process |
| CN1167084A (en) * | 1996-05-14 | 1997-12-10 | 中国石化茂名石油化工公司 | Technology for refining ammonia |
| JPH1060449A (en) * | 1996-08-22 | 1998-03-03 | Nippon Steel Corp | Purification of coke oven gas |
| JPH10297919A (en) * | 1997-04-23 | 1998-11-10 | Nissan Chem Ind Ltd | Production of high purity ammonia water |
| US6585807B2 (en) * | 2000-04-28 | 2003-07-01 | Mitsubishi Gas Chemical Company, Inc. | Recovery method of ammonia from gaseous mixture |
-
2005
- 2005-02-17 CN CNB2005100106577A patent/CN1298629C/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB552843A (en) * | 1941-01-07 | 1943-04-28 | Percy Parrish | Improvements in or relating to the manufacture of 25 to 30% liquor ammonia |
| CN86104483A (en) * | 1986-06-28 | 1988-03-02 | 贵阳市科学技术情报研究所 | From ammoniacal liquor, reclaim the novel process of ammonia |
| CN1056893A (en) * | 1991-07-04 | 1991-12-11 | 东北煤气化设计研究所 | Gas sewage extracting and dephenolizing, ammonia still process treatment process |
| CN1167084A (en) * | 1996-05-14 | 1997-12-10 | 中国石化茂名石油化工公司 | Technology for refining ammonia |
| JPH1060449A (en) * | 1996-08-22 | 1998-03-03 | Nippon Steel Corp | Purification of coke oven gas |
| JPH10297919A (en) * | 1997-04-23 | 1998-11-10 | Nissan Chem Ind Ltd | Production of high purity ammonia water |
| US6585807B2 (en) * | 2000-04-28 | 2003-07-01 | Mitsubishi Gas Chemical Company, Inc. | Recovery method of ammonia from gaseous mixture |
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| CN1657411A (en) | 2005-08-24 |
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