CN205412613U - Facility from gas mixture separation ammonia - Google Patents
Facility from gas mixture separation ammonia Download PDFInfo
- Publication number
- CN205412613U CN205412613U CN201520796543.9U CN201520796543U CN205412613U CN 205412613 U CN205412613 U CN 205412613U CN 201520796543 U CN201520796543 U CN 201520796543U CN 205412613 U CN205412613 U CN 205412613U
- Authority
- CN
- China
- Prior art keywords
- ammonia
- heat exchanger
- waterborne liquid
- gas mixture
- liquid
- 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.)
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/12—Separation of ammonia from gases and vapours
-
- 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
- B01D53/002—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 condensation
-
- 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
- B01D53/14—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 absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
- B01D2252/103—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model relates to a facility from gas mixture separation ammonia. A facility includes for following contain ammonia gas mixture separation ammonia: tube bank heat exchanger, it has the discharge tube that is used for containing the charge -in pipeline of ammonia gas mixture and waterborne liquid and is used for double -phase solution -airmixture to be suitable for and make gas mixture and waterborne liquid mixing in order to obtain double -phase solution -airmixture and with its cooling, the separator, it establishes the low reaches at tube bank heat exchanger for separate into the liquid phase of rich ammonia and the gaseous phase of poor ammonia, the absorption tower, it establishes the low reaches at the separator about the gaseous phase to including the charge -in pipeline that is used for fresh water, be used for as the waterborne liquid load the water of ammonia the discharge tube, be used for gas purging pipeline and at least one mass transfer device of poor ammonia, the first portion of waterborne liquid with the help of the conveyor conveying through heat exchanger, in the cooling of heat exchanger department, afterwards once more on mass transfer device top loading to absorption tower, the second portion of the waterborne liquid tube bank heat exchanger that recycles.
Description
Technical field
This utility model relates to by making ammonia-containing gas mixture mix to come the facility of separation of ammonia from admixture of gas with waterborne liquid, and ammonia is at least partly absorbed by described waterborne liquid.
Background technology
Such facilities and equipment are known per se.Its a kind of important purposes is, by Sa Suoer-Lu Qi (Sasol-Lurgi) method, processes the condensate gas obtained in coal fixed bed gasification.Wherein, succeedingly process tar, oil, phenol, and succeedingly isolate sour gas and ammonia subsequently from condensate gas.These facilities are described in " gasification (GASIFICATION) " of second edition, graceful/Maltese Fan Deboge (ChristopherHigman/MaartenvanderBurgt) of Christoffer black square, bay commercial press (GulfProfessionalPublishing), 5.1.1 chapter and at " industrial chemistry encyclopaedia of Liv Ullmann (Ullmann ' sEncyclopediaofIndustrialChemistry) ", 6th edition, volume 15,6th chapter, page 430.
It practice, generally performed the separation of ammonia by absorbing ammonia in absorption tower.Ammonia-containing gas mixture flows from bottom to top by tower and is conducted through one or more, such as three packed beds.Water as absorbent passes through filler to guide from bottom to top relative to the adverse current of ammonia-containing gas mixture.First ammonia-containing gas mixture absorbs in the nethermost filler that liquid contacts with aqueous wherein, and absorb in being contacted at this due to a large amount of ammonia and dissipate relevant substantial amounts of absorption heat, and water absorbing liquid is circulated through an external heat exchanger.Generally the second packed bed is performed this measure.
When the absorbability that aqueous absorbs liquid reduces with temperature rising, it is desirable to make the temperature caused by the absorption of ammonia rising remain low by corresponding big quantity of fluid.But, which results in the region of the nethermost packed bed first contacted with admixture of gas, tower must be designed with the biggest diameter, can be uniformly distributed big quantity of fluid on packed bed.This big quantity of fluid to be recycled causes the bigger and corresponding cost of equipment size, and this reduces the economy of the method.
Utility model content
The purpose of this utility model is to provide the facility operated by above method of a kind of improvement, wherein contact in smaller size smaller and equipment that therefore price lower execution with absorbing between liquid at ammonia-containing gas mixture.
nullDescribed purpose is solved according to this utility model，Wherein，Described purpose is solved by means of making admixture of gas mix to come the facility of separation of ammonia from ammonia-containing gas mixture with waterborne liquid，Ammonia is absorbed by described waterborne liquid at least in part，Wherein，Admixture of gas and waterborne liquid are directed to dividually in the inlet shroud of tube bundle heat exchanger and are mixed wherein，To obtain biphase solution-airmixture，Wherein，Solution-airmixture then passes through the pipe of tube bundle heat exchanger，Wherein，Described solution-airmixture is cooled down by cooling medium directed in shell side，The solution-airmixture carrying out automatic heat-exchanger is subsequently communicated in separator，So that gas phase and liquid phase are carried out，Wherein，Obtain gas phase and the liquid phase of rich ammonia of lean ammonia，And the liquid phase of the gas phase of lean ammonia and rich ammonia is each is discharged for using further from separator.
According to this utility model, from the mixing of ammonia-containing gas mixture and the waterborne liquid of whole stripping towers, the absorption of ammonia and absorb heat be dissipated in tube bundle heat exchanger execution.Admixture of gas and waterborne liquid are separately introduced in the inlet shroud of tube bundle heat exchanger and mix wherein to obtain biphase solution-airmixture, wherein, solution-airmixture then passes through the pipe of pipe speed heat exchanger, wherein, solution-airmixture is cooled down by cooling medium directed in shell side.Due to ammonia-containing gas mixture with absorb liquid and jointly flow the pipe by heat exchanger, partially absorbing heat and directly dissipate during it produces, the temperature increase of liquid is lowered, and the absorbability of therefore liquid increases.Subsequently, solution-airmixture is sent in the equipment for separating gas phase and liquid phase from heat exchanger.
Preferred aspect of the present utility model
Of the present utility model it is advantageous in that, by means of at least one nozzle in the inlet shroud of tube bundle heat exchanger, waterborne liquid is incorporated in ammonia-containing gas mixture.This is a kind of straightforward procedure being evenly distributed in gas by liquid.
A kind of modification of the present utility model is, the absorption of ammonia is performed during the multistage, wherein, the first stage is implemented according to the above of the present utility model, and then in second stage, the gas phase of the lean ammonia obtained enters in absorption tower and flows by this tower from bottom to top, and wherein, fresh water is introduced in this tower, fresh water passes through absorption tower to flow from the top to the bottom relative to the adverse current of gas phase, and wherein, the gas of further lean ammonia is discharged for using further from tower, and wherein, the water being loaded with ammonia is discharged from tower as waterborne liquid and is used in the first step by introduction in the inlet shroud of tube bundle heat exchanger.
By this measure, in a usual manner, i.e. by gas phase and liquid phase contact in one or more packed beds, remaining ammonia content is removed from gas phase.Together with gas phase and waterborne liquid according to this utility model mixing in tube bundle heat exchanger, it is possible to realize the extra high separating degree of ammonia in the case of the equipment using substantially reduced size.
Another specific aspect of this utility model is characterised by, two independences, stacked mass transfer apparatus it is furnished with for the absorption tower of second stage, such as packed bed or structured packing, wherein, described aqueous phase is circulated through lower filler and is circulated throughout and is positioned at the heat exchanger outside tower for cooling.When performing in the first step according to prior art to absorb on packed bed, this aspect is particularly advantageous.
In a word, this utility model provides a kind of for the facility from ammonia-containing gas mixture separation of ammonia, comprising:
(a) tube bundle heat exchanger, described tube bundle heat exchanger is with the feed pipe for ammonia-containing gas mixture and waterborne liquid and the discharge tube for biphase solution-airmixture, described tube bundle heat exchanger is suitable for making described admixture of gas and the mixing of described waterborne liquid to obtain biphase solution-airmixture and for being cooled down by described biphase solution-airmixture
(b) separator, described separator is arranged on the downstream of described tube bundle heat exchanger, for being separated into liquid phase and the gas phase of lean ammonia of rich ammonia,
(c) absorption tower, described absorption tower is arranged on the downstream of described separator about described gas phase, described absorption tower includes the feed pipe for fresh water, discharge tube for the water being loaded with ammonia as waterborne liquid, the discharge tube of gas and at least one mass transfer apparatus for lean ammonia, wherein, the Part I of described waterborne liquid is transmitted through heat exchanger by means of conveyer device, it is cooled at described heat exchanger, and above described mass transfer apparatus, the most again it is loaded into described absorption tower, and wherein, the Part II of described waterborne liquid is recycled to described tube bundle heat exchanger.
Accompanying drawing explanation
Other development of the present utility model, advantage and potential application can also be understood according to the detailed description and the accompanying drawings of detailed description below.
In the accompanying drawings:
Fig. 1 shows the facility from the admixture of gas separation of ammonia containing ammonia and noble gas according to prior art,
Fig. 2 shows the exemplary embodiment according to facility of the present utility model.
Detailed description of the invention
First, prior art will be explained with reference to Fig. 1.Ammonia-containing gas mixture 1 is introduced at the bottom on absorption tower 2, and flows by mass transfer apparatus 3,4 and 5 successively, and mass transfer apparatus 3,4 and 5 is here designed to packed bed.Soften water 6 to be introduced in the top of tower 2 as absorbent, and pass through packed bed to flow successively relative to the adverse current of admixture of gas risen.For lower packed bed 3 and central filler bed 4, water is pumped across by means of pump 7 and 8.Via heat exchanger 9 and 10, the absorption heat generated during the absorption of ammonia from water extraction.So, it is achieved absorb more ammonia by water.At the bottom of tower 2, rich ammonia waterborne liquid 12 discharges to use further via pump 11.At the top of tower 2, lean ammonia gas 13 is discharged to use further, and lean ammonia gas 13 is to mainly contain the noble gas of nitrogen.
Due to the large volume flow of fractional load absorbent, so the packed bed 3 of particularly bottommost must be designed to the biggest.This causes the size on absorption tower 2 relatively greatly, particularly at the cross section this respect of tower.This causes again the restriction of increase and absorption tower 2 installation in complex facilities that cost puts into.Additionally, pump 7 and heat exchanger 9 must be designed to stronger accordingly.
As an example of the design according to facility of the present utility model, Fig. 2 shows how the stream 14 of ammonia-containing gas mixture 1 ' and waterborne liquid is introduced in the inlet shroud 15 of tube bundle heat exchanger 16.After it has flowed by the pipe of heat exchanger, being wherein dissipated by liquid phase scrubbing and absorption heat from the major part in the ammonia of gas phase, the biphase solution-airmixture generated is introduced in separator 18 to separate gas phase and liquid phase as stream 17 '.From there, gas phase is introduced in the bottom on absorption tower 2 ' as stream 19 and is flow to the top of tower 2 ' by packed bed 4 ' and 5 '.Introducing at the top of tower 2 ' and soften water 6 ', it takes away remaining ammonia content as absorbent from gas phase.The gas phase substantially releasing ammonia is left for processing further from tower 2 ' at top as stream 13 '.By means of pump installation 8 ', water is circulated through lower packed bed 4 ', wherein absorbs heat and dissipates via heat exchanger 10 '.Flow 14 from loop towards heat exchanger 16 branch.The rich ammonia waterborne liquid 12 ' generated discharges from separator 18, and by means of pump 11 ' supply for further using.
Commercial Application
This utility model represents a kind of low cost alternative scheme of the facility of actual employing, is the most commercially applicable.
Reference numerals list
1,1 ' ammonia-containing gas mixture
2,2 ' absorption towers
3 mass transfer apparatus
4,4 ' mass transfer apparatus
5,5 ' mass transfer apparatus
6,6 ' fresh water or softening water
7 pumps
8,8 ' pumps
9 heat exchangers
10,10 ' heat exchangers
11,11 ' pumps
12,12 ' rich ammonia waterborne liquids
13,13 ' lean ammonia noble gases
14 waterborne liquids
15 inlet shroud
16 tube bundle heat exchangers
17 ' solution-airmixtures
18 separators
19 gas phases
Claims (1)
1. the facility being used for from ammonia-containing gas mixture separation of ammonia, it is characterised in that including:
(a) tube bundle heat exchanger (16), described tube bundle heat exchanger (16) is with for ammonia-containing gas mixture (1 ') and the feed pipe of waterborne liquid (14) and for the discharge tube of biphase solution-airmixture (17 '), described tube bundle heat exchanger (16) is suitable for making described admixture of gas (1 ') and described waterborne liquid (14) mixing to obtain biphase solution-airmixture (17 ') and for described biphase solution-airmixture (17 ') being cooled down
(b) separator (18), described separator (18) is arranged on the downstream of described tube bundle heat exchanger (16), for being separated into liquid phase (12 ') and the gas phase (19) of lean ammonia of rich ammonia,
(c) absorption tower (2 '), described absorption tower (2 ') is arranged on the downstream of described separator (18) about described gas phase, described absorption tower (2 ') includes the feed pipe for fresh water (6 '), discharge tube for the water being loaded with ammonia as waterborne liquid (14), the discharge tube of gas (13 ') and at least one mass transfer apparatus (4 ') for lean ammonia, wherein, the Part I of described waterborne liquid (14) is transmitted through heat exchanger (10 ') by means of conveyer device (8 '), cooled at described heat exchanger (10 ') place, and the most again it is loaded into described absorption tower (2 ') in described mass transfer apparatus (4 ') top, and wherein, the Part II of described waterborne liquid (14) is recycled to described tube bundle heat exchanger (16).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102014115395.2A DE102014115395A1 (en) | 2014-10-22 | 2014-10-22 | Process and plant for the separation of ammonia from a gas mixture |
| DE102014115395.2 | 2014-10-22 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205412613U true CN205412613U (en) | 2016-08-03 |
Family
ID=54330719
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510664938.8A Active CN105536433B (en) | 2014-10-22 | 2015-10-15 | Method and installation for separating ammonia from a gas mixture |
| CN201520796543.9U Active CN205412613U (en) | 2014-10-22 | 2015-10-15 | Facility from gas mixture separation ammonia |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510664938.8A Active CN105536433B (en) | 2014-10-22 | 2015-10-15 | Method and installation for separating ammonia from a gas mixture |
Country Status (5)
| Country | Link |
|---|---|
| CN (2) | CN105536433B (en) |
| AU (1) | AU2015335275B2 (en) |
| DE (1) | DE102014115395A1 (en) |
| EA (1) | EA033528B1 (en) |
| WO (1) | WO2016062410A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108889093B (en) * | 2018-09-14 | 2024-03-19 | 深圳市奥图威尔科技有限公司 | Waste gas treatment device for absorbing ammonia gas by using acetone |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3155722A (en) * | 1960-01-29 | 1964-11-03 | Chemical Construction Corp | Recovery of residual ammonia and carbon dioxide in the synthesis of urea |
| US3344585A (en) * | 1967-05-12 | 1967-10-03 | Eugene G Hollowell | Method for recovering ammonia from gaseous mixture |
| DE10049227B4 (en) * | 2000-09-28 | 2007-02-01 | Bu Bioenergie & Umwelttechnik Ag | Procedures for gas purification of process gas from gasification processes |
| RU2351385C1 (en) * | 2007-10-29 | 2009-04-10 | Общество с ограниченной ответственностью "Завод полимеров Кирово-Чепецкого химического комбината" (ООО "Завод полимеров КЧХК") | Chlorine absorber |
| CN101439865A (en) * | 2008-12-22 | 2009-05-27 | 江西稀有稀土金属钨业集团有限公司 | Method for recycling ammine in ammonium paratungstate production |
| CN102087021B (en) * | 2010-12-20 | 2014-04-09 | 华北电力大学 | Integrated system for utilizing residual heat of boiler smoke and removing sulfur |
| CN203612972U (en) * | 2013-10-23 | 2014-05-28 | 河南心连心化肥有限公司 | Device for recycling ammonia from waste gas in ammonia synthetizing system |
-
2014
- 2014-10-22 DE DE102014115395.2A patent/DE102014115395A1/en not_active Withdrawn
-
2015
- 2015-10-08 AU AU2015335275A patent/AU2015335275B2/en active Active
- 2015-10-08 EA EA201790813A patent/EA033528B1/en not_active IP Right Cessation
- 2015-10-08 WO PCT/EP2015/025069 patent/WO2016062410A1/en active Application Filing
- 2015-10-15 CN CN201510664938.8A patent/CN105536433B/en active Active
- 2015-10-15 CN CN201520796543.9U patent/CN205412613U/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| AU2015335275B2 (en) | 2018-12-20 |
| CN105536433B (en) | 2020-09-22 |
| EA201790813A1 (en) | 2017-08-31 |
| EA033528B1 (en) | 2019-10-31 |
| WO2016062410A1 (en) | 2016-04-28 |
| AU2015335275A1 (en) | 2017-05-18 |
| DE102014115395A1 (en) | 2016-04-28 |
| CN105536433A (en) | 2016-05-04 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |