CN1248963C - Ammonia refining combined process - Google Patents
Ammonia refining combined process Download PDFInfo
- Publication number
- CN1248963C CN1248963C CN 200410060461 CN200410060461A CN1248963C CN 1248963 C CN1248963 C CN 1248963C CN 200410060461 CN200410060461 CN 200410060461 CN 200410060461 A CN200410060461 A CN 200410060461A CN 1248963 C CN1248963 C CN 1248963C
- Authority
- CN
- China
- Prior art keywords
- ammonia
- tower
- gas ammonia
- water
- washing tower
- 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.)
- Active
Links
Images
Landscapes
- Industrial Gases (AREA)
- Separation Of Gases By Adsorption (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The present invention provides an ammonia refining combination technology, particularly a technology for gas ammonia containing hydrogen sulfide and water generated by acidic water stripping devices of oil refineries, which belongs to the field of gas refining. Raw material gas ammonia containing hydrogen sulfide and water is cooled to 5 to 10 DEG C by a cooler to enter a first separating tank for separation according to the present invention, gas ammonia exhausted from the top of the first separating tank enters a washing tower to contact concentrated ammonia liquor for washing, the operating temperature of the washing tower is controlled between-10 DEG C and 0 DEG C, gas ammonia exhausted from the top of the washing tower is separated through a secondary separating tank and then enters an adsorption tank for adsorption, and adsorbed gas ammonia passes through a compressor, a third separating tank and a refined desulfurization tank and then enters refined liquid ammonia finished product tank through a liquid ammonia cooler. The present invention solves the defects of complicated flow path, large discharge of concentrated ammonia liquor containing sulfur and complicated operation existing in the prior art. The purity of refined liquid ammonia reaches 99.9%, and the content of hydrogen sulfide is smaller than 1 ppm.
Description
Technical field
The invention belongs to the gas purification field, relate to a kind of sulfide hydrogen of refinery acidic water stripping device generation and the gas ammonia process for refining of water.
Background technology
Chinese patent specification sheets CN1047366C discloses a kind of gas ammonia process for refining, adopt washing-crystallization-absorption-fine desulfurizing technology flow process, the sulfide hydrogen that sewage from oil refinery stripper plant stripping is come out and the gas ammonia of water are cooled to below 40 ℃ behind the separatory, hydrogen sulfide in the gas ammonia and water-content are stabilized in about 1 weight % enter washing tower, the temperature of washing tower is controlled at below 10 ℃, the content of hydrogen sulfide and water is lower than 200ppm in the gas ammonia of washing back, enter the crystallisation adsorption jar again, carry out smart desulfurization at last, the purity of the refining liquefied ammonia that obtains can reach 99.8%, hydrogen sulfide content is below 1ppm.This technology is owing to the gas ammonia temperature that enters washing tower is higher, cause hydrogen sulfide and water-content in the gas ammonia higher, the cyclic ammonia water concentration of washing usefulness is reduced, for guaranteeing washing effect, must often replenish liquefied ammonia, the sulfur-bearing strong aqua of Pai Chuing is also more simultaneously, increases the quantity discharged of sulfur-bearing strong aqua, and the sour water load is increased.This technology is also deposited crystallisation adsorption and need be interrupted discharge opeing in addition, and operation is complicated.Also there is the flow process complexity in this technology, and required equipment is more, takes up an area of big shortcoming.
Summary of the invention
The present invention is directed to the shortcoming of the big and complicated operation of the quantity discharged of flow process complexity that prior art exists, sulfur-bearing strong aqua, provide the ammonia that a kind of flow process is simple, the quantity discharged of sulfur-bearing strong aqua is few and easy to operate refining combination process, liquefied ammonia purity after making ammonia refining reaches 99.9%, and hydrogen sulfide content is less than 1ppm.
Technical scheme of the present invention is: the refining combination process of a kind of ammonia is the raw material gas ammonia with sulfide hydrogen and water, be cooled to 5～10 ℃ through water cooler and enter first fen flow container separatory, first fen flow container working pressure 0.3～0.35MPa, 5～10 ℃ of temperature, the effusive gas ammonia of the first separatory tank deck enters washing tower and contacts washing with strong aqua, the service temperature of washing tower is controlled at-10～0 ℃, entered adsorption tanks absorption behind the flow container separatory again through second minute from the effusive gas ammonia of scrubber overhead, the compressed machine of gas ammonia after the absorption, behind the 3rd fen flow container and the smart digester, advance to make with extra care liquefied ammonia finished product jar through the liquefied ammonia water cooler.
The further technical characterictic of the present invention is, utilizes the refining liquefied ammonia of the present invention to cool off the raw material gas ammonia of sulfide hydrogen and water as the heat-eliminating medium of water cooler.
The technical characterictic of another optimization of the present invention is, washing tower of the present invention adopts the big structural shape in little bottom, top, the top tower diameter is 0.5～0.8: 1 with the ratio of bottom tower diameter, top minor diameter tower height degree and bottom major diameter tower aspect ratio are 4～5: 1,2～4 sections fillers are housed in the minor diameter tower of top, this filler is for existing washing tower customary filler, as DN50 multi-saddle ring filler.
Utilize the liquefied ammonia purity after the present invention can make ammonia refining to reach 99.9%, hydrogen sulfide content is less than 1ppm.The beneficial effect that the present invention compared with prior art produces is embodied in:
1) the present invention is cooled to 5～10 ℃ with the gas ammonia of sulfide hydrogen and water through water cooler and enters first fen flow container, can make the water in the gas ammonia reduce to 0.14 weight %, hydrogen sulfide in the gas ammonia is fixed on liquid phase at low temperatures simultaneously, can be below 0.16 weight % from the hydrogen sulfide content of the effusive gas ammonia of the first separatory tank deck.And in the prior art gas ammonia of sulfide hydrogen and water being cooled to separatory below 40 ℃, hydrogen sulfide behind the separatory in the gas ammonia and water-content are stabilized in about 1 weight %.The present invention is by the low temperature separatory like this, make that the content of hydrogen sulfide and water reduces greatly in the gas ammonia that enters washing tower, the concentration of compared with prior art washing the cyclic ammonia water of usefulness reduces slower, must often not replenish liquefied ammonia, the sulfur-bearing strong aqua of Pai Chuing is also less simultaneously, and the sour water load is little.
2) service temperature of washing tower of the present invention is at-10～0 ℃, and about 30ppm, and the temperature of prior art washing tower is controlled at below 10 ℃ from the effusive gas ammonia hydrogen sulfide content of scrubber overhead, and the content of hydrogen sulfide is lower than 200ppm in the gas ammonia of washing back.Owing to the content of hydrogen sulfide in the washing tower outlet gas ammonia in the prior art is higher, need hydrogen sulfide content is reduced to below the 30ppm through a crystallisation process, advance adsorption tower again.Hydrogen sulfide content is about 30ppm in the washing tower of the present invention outlet gas ammonia, only need simple ammoniacal liquor separating tank separatory after, just can enter adsorption tanks absorption, compared with prior art saved a crystallisation process, make the minimizing of appliance arrangement amount, simplified control.
3) the present invention has low-temperature receiver and is easy to get, the effect that expense is cheap if the refining liquefied ammonia of employing self cools off the raw material gas ammonia as heat-eliminating medium.
4) minor diameter tower section effect in the preferred washing tower structure of the present invention top is a washing desulphurization hydrogen, and bottom major diameter tower section effect is settlement separate.Has reduced investment, the effect of reinforcing desulfuration.
Description of drawings
Accompanying drawing is the present invention's one typical flowchart.
Among the figure: the 1-water cooler; First fen flow container of 2-; The 3-washing tower; Second fen flow container of 4-; The 5-adsorption tanks; The 6-compressor; The 3rd fen flow container of 7-; The smart digester of 8-; 9-liquefied ammonia water cooler; 10-makes with extra care liquefied ammonia finished product jar.
Embodiment
As shown in the figure: with the raw material gas ammonia of sulfide hydrogen and water, be cooled to 5～10 ℃ through water cooler 1 and enter first fen flow container 2, the working pressure of first fen flow container 2 is 0.3～0.35MPa, temperature is 5～10 ℃, made the water in the raw material gas ammonia reduce to 0.14 weight % in the flow container 2 at first minute, hydrogen sulfide in the raw material gas ammonia is fixed in the liquid phase at low temperatures simultaneously, hydrogen sulfide content in the effusive gas ammonia in first fen flow container, 2 tops is 0.16 weight %, water-content is at 0.14 weight %, enter washing tower 3, the service temperature of washing tower is controlled at-10～0 ℃, pushes up effusive gas ammonia hydrogen sulfide content at 30ppm from washing tower 3; Enter adsorption tanks 5 again through second fen flow container 4, behind the compressed machine of the gas ammonia after the absorption 6, the 3rd minute flow container 7, smart digester 8 and the cold liquid ammonia condenser 9, advance to make with extra care liquefied ammonia finished product jar 10.Hydrogen sulfide content in the purified liquefied ammonia is at 1ppm, and purity can reach 99.9%.
With reference to the accompanying drawings, but autofining liquefied ammonia finished product jar 10 extraction units are divided liquefied ammonia, make the heat-eliminating medium of water cooler 1, with the laggard compressor 6 of raw material gas ammonia heat exchange.
With reference to the accompanying drawings, optional 0.6～1.5 meter of the upper diameter of washing tower 3, lower diameter is 1.25～2 times of upper diameter, top minor diameter tower height degree and bottom major diameter tower aspect ratio are 4～5: 1,3 sections fillers are housed in the minor diameter tower of top, this filler is for existing washing tower customary filler, as DN50 MSR Stainless Steel Helices.
Be one group of concrete operations data of technology of the present invention below:
Raw material ammonia 1360.5kg/h
90 ℃ of temperature
Pressure 0.4Mpa
Hydrogen sulfide content 2.7 weight %
Water-content 10.4 weight %
First fen flow container 2 outlet ammonia
10 ℃ 8 ℃ 5 ℃ of temperature
Pressure 0.35Mpa 0.35Mpa 0.35Mpa
Hydrogen sulfide content 0.16 weight % 0.15 weight % 0.14 weight %
Water-content 0.14 weight % 0.12 weight % 0.11 weight %
Washing tower 3
0 ℃-5 ℃-10 ℃ of temperature
Pressure 0.25Mpa 0.25Mpa 0.25Mpa
Hydrogen sulfide content 30ppm 22ppm 15ppm
The water-content vestige
Adsorption tanks 5
0 ℃-5 ℃-10 ℃ of temperature
Pressure 0.23Mpa 0.23Mpa 0.23Mpa
Hydrogen sulfide 10ppm 5ppm 2ppm
130 ℃ of temperature
Pressure 1.6Mpa
Hydrogen sulfide content 1ppm
Ammonia purity 99.9%
Claims (3)
1, a kind of ammonia is made with extra care combination process, it is characterized in that: with the raw material gas ammonia of sulfide hydrogen and water, be cooled to 5～10 ℃ through water cooler and enter first fen flow container separatory, first fen flow container working pressure 0.3～0.35MPa, 5～10 ℃ of temperature, the effusive gas ammonia of the first separatory tank deck enters washing tower and contacts washing with strong aqua, the service temperature of washing tower is controlled at 0～-10 ℃, entered adsorption tanks absorption behind the flow container separatory again through second minute from the effusive gas ammonia of scrubber overhead, the compressed machine of gas ammonia after the absorption, behind the 3rd fen flow container and the smart digester, advance to make with extra care liquefied ammonia finished product jar through the liquefied ammonia water cooler.
2, according to the refining combination process of the described ammonia of claim 1, it is characterized in that: autofining liquefied ammonia finished product jar extension liquefied ammonia cools off the raw material gas ammonia as the heat-eliminating medium of water cooler.
3, according to the refining combination process of the described ammonia of claim 1, it is characterized in that: described washing tower adopts the structural shape that top is little, the bottom is big, the top tower diameter is 0.5～0.8: 1 with the ratio of bottom tower diameter, top minor diameter tower height degree and bottom major diameter tower aspect ratio are 4～5: 1, and 2～4 sections fillers are housed in the minor diameter tower of top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410060461 CN1248963C (en) | 2004-08-16 | 2004-08-16 | Ammonia refining combined process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410060461 CN1248963C (en) | 2004-08-16 | 2004-08-16 | Ammonia refining combined process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1587045A CN1587045A (en) | 2005-03-02 |
| CN1248963C true CN1248963C (en) | 2006-04-05 |
Family
ID=34603466
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410060461 Active CN1248963C (en) | 2004-08-16 | 2004-08-16 | Ammonia refining combined process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1248963C (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103523798B (en) * | 2013-10-31 | 2016-06-29 | 青岛科技大学 | A kind of apparatus and method of the ammonia scrubbing method dephenolize desulfurization of improvement |
| CN104326485A (en) * | 2014-10-12 | 2015-02-04 | 陕西创联工业技术有限公司 | Ammonia refining treatment process |
| CN106277145A (en) * | 2016-08-30 | 2017-01-04 | 宁波中金石化有限公司 | The apparatus and method that a kind of aromatic hydrocarbons cleaning produces |
| CN106398752A (en) * | 2016-10-18 | 2017-02-15 | 山东宝塔新能源有限公司 | Device for supplementing sulfur for hydrogenation reaction by means of collecting tower top hydrogen sulfide from hydrogen sulfide removal stripping towers for hydrogenation reaction on coal tar |
| CN107777708A (en) * | 2017-09-28 | 2018-03-09 | 华陆工程科技有限责任公司 | A kind of method of thick ammonia refining in acidic water stripping device |
| CN109248564B (en) * | 2018-11-15 | 2021-01-05 | 山东海科化工集团有限公司 | Recycling device and process for coarse ammonia water generated by acidic water treatment device of petrochemical refinery |
| CN110395746B (en) * | 2019-08-20 | 2021-06-04 | 中国石油化工股份有限公司 | Device and method for refining and decoloring liquid ammonia |
-
2004
- 2004-08-16 CN CN 200410060461 patent/CN1248963C/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN1587045A (en) | 2005-03-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1248963C (en) | Ammonia refining combined process | |
| CN102309914A (en) | Treatment method for stinky waste gas discharged by storage tank | |
| FR2987368A1 (en) | PROCESS FOR REMOVING MERCURY FROM HYDROCARBON LOAD WITH HYDROGEN RECYCLE | |
| CN104326485A (en) | Ammonia refining treatment process | |
| CN113336225B (en) | Production device and process for preparing electronic grade carbon monoxide from synthetic ammonia tail gas | |
| CN102653505A (en) | Propylene refining method | |
| CN101653688A (en) | Process flow for removing CO2 and H2S in gas mixture | |
| JP2022534554A (en) | Direct oxidation of hydrogen sulfide in hydrotreating recycle gas streams by hydrogen refining | |
| CN1900232A (en) | Liquefied gas desulfurizing method | |
| CN1775924A (en) | Liquefied gas desulfurizing and refining method | |
| RU56207U1 (en) | INSTALLING OIL CLEANING (OPTIONS) | |
| CN1380274A (en) | Alcohol refining process for producing several products | |
| CN106395857A (en) | Liquid ammonia refining decolorization system and method | |
| CN104624019A (en) | Treatment method for alkali liquor oxidation regeneration tail gas containing mercaptide | |
| CN1257838C (en) | Hydrocarbon trap method for carbon dioxide for foodstuff | |
| CN101634515B (en) | Method for extracting high-yield pure krypton and pure xenon by full distillation | |
| CN1090590C (en) | Multisection stripping process for treating acid sewage from oil refinery | |
| CN110791327B (en) | Device and process for deeply removing purified gas sulfide of low-temperature methanol washing system | |
| CN217578331U (en) | Production device for preparing electronic-grade carbon monoxide from synthesis ammonia tail gas | |
| CN203095914U (en) | Device for removing high-boiling-point sulphide in methyl tertiary butyl ethers | |
| CN201567231U (en) | Hydrogen chloride desorption tower device for recycling polycrystalline silicon production tail gas | |
| CN209537347U (en) | A kind of system removed for sulfide non-hydrogen in cracking c_5 olefin component | |
| CN105085146A (en) | Refining method and system for preparing polymerization-grade propylene from refinery crude propylene | |
| CN208362221U (en) | Remove the device of higher boiling sulfur compound in methyl tertiary butyl ether(MTBE) | |
| CN1047366C (en) | Technology for refining ammonia |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: China Petrochemical Group Corp. Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: China Petrochemical Group Corp. |
|
| ASS | Succession or assignment of patent right |
Owner name: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORAT Free format text: FORMER OWNER: SINOPEC GROUP Effective date: 20130326 Free format text: FORMER OWNER: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORATION Effective date: 20130326 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 100029 CHAOYANG, BEIJING TO: 471003 LUOYANG, HENAN PROVINCE |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20130326 Address after: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Patentee before: China Petrochemical Group Corp. Patentee before: Luoyang Petrochemical Engineering Corporation /SINOPEC |