CN1053219A - Refining process for synthetic ammonia raw material gas - Google Patents
Refining process for synthetic ammonia raw material gas Download PDFInfo
- Publication number
- CN1053219A CN1053219A CN90105545A CN90105545A CN1053219A CN 1053219 A CN1053219 A CN 1053219A CN 90105545 A CN90105545 A CN 90105545A CN 90105545 A CN90105545 A CN 90105545A CN 1053219 A CN1053219 A CN 1053219A
- Authority
- CN
- China
- Prior art keywords
- gas
- refining
- raw material
- reaction
- methyl alcohol
- 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.)
- Withdrawn
Links
Images
Classifications
-
- Y02P20/121—
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of refining process for synthetic ammonia raw material gas, it is specially adapted to the coal is raw material, adopts middle-size and small-size nitrogen fertilizer plant unstripped gas refining of air, steam gas making.Unstripped gas under the 5.0-15MPa condition, is equipped with desulfurization catalyst in same segmentation after conversion, decarburization, catalyst for methanol in the treating tower of methanation catalyst, carries out desulphurization reaction, successively, respectively, continuously with H
2Generation methyl alcohol, methane reaction make refining raw-material gas.And utilizing the heat energy of the thermopositive reaction that produces in the treating process, tower gas is advanced in first preheating, enters heat regenerator again water is added thermogenesis steam, enters circulating gas heater again, constitutes a circulation process.
Description
The present invention relates to refining process for synthetic ammonia raw material gas, it is specially adapted to the coal is raw material, adopts middle-size and small-size nitrogen fertilizer plant unstripped gas refining of air, steam gas making.
Syngas for synthetic ammonia must be purified hydrogen and nitrogen, usually with air, sum total has carbon monoxide and carbonic acid gas and a small amount of hydrogen sulfide of 2-4% in the unstripped gas of the middle-size and small-size nitrogen fertilizer plant of steam gas making, the type nitrogen fertilizer plant all adopts copper to wash method (Jiang Shengjie at present, the synthetic ammonia engineering, second volume P318～368), not only to consume copper, acetic acid, raw materials such as ammonia, and consume a large amount of steam (500-600 kilogram/ton ammonia), need refrigerating capacity 5-10 ten thousand kilocalories again, and complex process, be raw material with oil or Sweet natural gas or be raw material at present with the coal, adopt the large-scale ammonia plant of steam oxygen gas making to adopt the methane method of purification (Zhang Chengfang, ammonia synthesis process and energy-conservation P273-96), but it is very high that it requires unstripped gas, i.e. H
2S≤0.1ppm CO+CO
2≤ 0.5%, therefore, single methanation process, not being suitable for the coal is raw material, with the middle-size and small-size nitrogen fertilizer plant refining process for synthetic ammonia raw material gas of air vapor gas making.
The object of the present invention is to provide a kind of both to the less demanding (CO+CO in the permission unstripped gas of unstripped gas
2Be 2～4%) do not consume industrial chemicals again, do not consume steam and refrigerating capacity, can also byproduct steam and methyl alcohol, and technology is simple, is applicable to the coal to be the process for refining of raw material with the middle-size and small-size nitrogen fertilizer plant syngas for synthetic ammonia of air vapor gas making.
Purpose of the present invention can reach by following measure: unstripped gas is after conversion, decarburization, under the 5.0-15MPa condition, be equipped with in the treating tower of desulfurization catalyst, catalyst for methanol, methanation catalyst a segmentation, carry out desulphurization reaction successively, respectively, continuously, with H
2Generate the methyl alcohol reaction and generate methane reaction, make most of carbon monoxide in the unstripped gas, carbonic acid gas generate methyl alcohol, the remaining methane that then generates, wherein methyl alcohol becomes the byproduct recovery, and methane then reclaims the usefulness that acts as a fuel after the emptying in synthetic ammonia process.Because above reaction is thermopositive reaction, can utilize its heat energy preheating to advance tower gas, and outside treating tower, be equipped with interchanger and heat reclamation device, make whole technology form the working cycle of a preheating → refining (heat release) → heat regenerator (generation steam) → recirculation heater → water cooler (methyl alcohol separation) → ammonia synthesis.
Below in conjunction with accompanying drawing the present invention is described in detail:
Accompanying drawing is a process flow sheet of the present invention.
After unstripped gas and circulation gas mix, enter carbon oil strainer [1], separate profit and carbide at this, enter circulating gas heater [3], gas is heated to 70-100 ℃, enters treating tower [4], in tower, at first pass through preheating section, gas is reacted the after heat gas heating to 200-230 ℃ at this, enters interior first section of tower then successively, H in the gas
2S removes by the following formula reaction:
After the desulfurization in the unstripped gas sulphur content can reach below the 1ppm.
Unstripped gas after the desulfurization enters second section again, CO, CO in the gas
2Generate methyl alcohol by following reaction formula;
At this moment, CO, CO in the unstripped gas
2Summation enters the 3rd section again less than 0.5%, makes remaining CO and CO by following reaction formula
2Further purify;
At this moment, CO and CO in the unstripped gas
2Summation is less than 10ppm.
Because above reaction is thermopositive reaction, therefore can reach 370-380 ℃ from the 3rd section gas temperature that comes out, enter preheating section and advance tower gas with preheating, preheating is advanced hot air temperature behind the tower gas and is dropped to 270-280 ℃ and go out tower, enter heat regenerator [2] then, water is heated and produces the steam of 0.7-0.9MPa here, temperature drops to 140-160 ℃, enter recirculation heater [3], the circulation gas temperature is heated to 100 ℃ by normal temperature, former hot gas is then reduced to 60-80 ℃, enters water cooler [5], with cold water hot gas is cooled to be lower than 40 ℃ indirectly, this moment, methanol condensed was a liquid, enter methanol separator [6], methyl alcohol is separated, but one ton of ammonia by-product of every product methyl alcohol 70-100 kilogram.Gas is divided into two strands then, and a part is sent to ammonia synthesis converter, and another part mixes with unstripped gas after circulator [7] pressurization, continues the circulation said process.
Embodiment:
Tolerance is 16050 mark rice
3In/time, pressure is that 12-13MPa contains CO2.2%, CO
20.2%, H
272.6%, N
222%, CH
42%, H
2S0.005g/m
3Unstripped gas and circulation gas enter carbon oil strainer → recirculation heater, gas is heated to 80-100 ℃, enters the scavenging tower of a high 13000mm then, earlier through preheating section, gas is heated to 200-230 ℃, enters dress zinc-manganese sweetening agent 0.5m then successively
3Desulfurization section, dress copper catalyst 2.5m
3The methyl alcohol section, dress nickel catalyzator 1m
2The methane section, go out treating tower tolerance and be 15040 mark rice
3In/time, contain H in giving vent to anger
271.56%, N
229.11%, CH
42.6%, CH
3OH2.02%, CO+CO
2≤ 10ppm, H
2S≤1ppm, gas temperature are 370-380 ℃, enter preheating section → heat regenerator → recirculation heater → water cooler → methanol separator then successively, pay and produce methyl alcohol 305m
3/ h enters ammonia synthesis converter then, produce 5 tons of ammonia/time.
The process for refining of syngas for synthetic ammonia of the present invention and copper wash method and the simple methane method of purification relatively has following advantage:
Wash method relatively with copper, the one, simplified technique, and do not consume copper, the raw materials of industry such as acetic acid, ammonia, do not consume steam and refrigerating capacity, also can pay and produce methyl alcohol and steam, reduced cost, and since gas-solid reaction than gas liquid reaction good stability, operating reliability is strong.
Compare with the simple methane method of purification, CO is no more than at most 0.5% in the unstripped gas because the simple methane method of purification requires, in order to reduce CO in the unstripped gas, must consume a large amount of steam in transformation system makes it be transformed to hydrogen, and the present invention is owing to enter the methane section through the methyl alcohol section first again, so can allow in the unstripped gas there to be than great fluctuation process (2-4%) Co content, thereby conversion consumption steam can reduce significantly, and can also by-product methyl alcohol.
Claims (2)
1, a kind of being used for the coal is raw material, adopt the refining process for synthetic ammonia raw material gas of air vapor gas making, it is characterized in that the later unstripped gas of process conversion decarburization is under the 5.0-15MPa condition, in same segmentation desulfurization catalyst is housed, in the treating tower of catalyst for methanol, methanation catalyst, carry out desulphurization reaction successively, respectively, continuously, with H
2Generate the methyl alcohol reaction and generate methane reaction, wherein methyl alcohol becomes byproduct to reclaim, and methane reclaims after the emptying in synthetic ammonia process and makes fuel.
2, according to the process for refining of the described syngas for synthetic ammonia of claim 1, it is characterized in that, the heat energy that utilizes the thermopositive reaction in the treating process to produce, tower gas is advanced in elder generation's preheating, enter heat regenerator again water is added thermogenesis 0.7-0.9MPa steam, enter circulating gas heater again, circulation gas is heated to 100 ℃ and constitute the circulation process an of preheating → refining (heat release) → heat regenerator (generation steam) → recirculation heater → water cooler (methyl alcohol separation) → ammonia synthesis from normal temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN90105545A CN1019663B (en) | 1990-09-04 | 1990-09-04 | Refining process for synthetic ammonia raw material gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN90105545A CN1019663B (en) | 1990-09-04 | 1990-09-04 | Refining process for synthetic ammonia raw material gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1053219A true CN1053219A (en) | 1991-07-24 |
| CN1019663B CN1019663B (en) | 1992-12-30 |
Family
ID=4879359
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN90105545A Expired CN1019663B (en) | 1990-09-04 | 1990-09-04 | Refining process for synthetic ammonia raw material gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1019663B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043469C (en) * | 1994-03-30 | 1999-05-26 | 湖南安淳节能技术有限公司 | Ammonia-alcohol ratio adjustable technology for refining raw-material gas for synthesis of ammonia |
| CN1090228C (en) * | 1997-06-11 | 2002-09-04 | 三菱重工业株式会社 | Fine preparation method for gas |
| CN1090670C (en) * | 1997-10-03 | 2002-09-11 | 三菱重工业株式会社 | Gas purifying method and apparatus |
| CN1092228C (en) * | 1997-08-29 | 2002-10-09 | 三菱重工业株式会社 | Coal gas purifier |
| CN1098918C (en) * | 1997-07-22 | 2003-01-15 | 三菱重工业株式会社 | Gas refinishing process and gas refinishing equipment |
| CN1299971C (en) * | 2004-12-10 | 2007-02-14 | 南化集团研究院 | Technique for deep purifying material gas for synthesizing ammonia |
| CN100339298C (en) * | 2004-05-08 | 2007-09-26 | 吕仲明 | Non-isostatic alcoholization alkylation process for purifying raw gas for ammonia synthesis |
| CN110482568A (en) * | 2019-08-12 | 2019-11-22 | 上海国际化建工程咨询有限公司 | A kind of by-product alkanol for medium and small nitrogen fertilizer factory to be transformed and the method and system of cold and hot joint purification |
| CN113479905A (en) * | 2021-06-29 | 2021-10-08 | 福州大学化肥催化剂国家工程研究中心 | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system |
-
1990
- 1990-09-04 CN CN90105545A patent/CN1019663B/en not_active Expired
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1043469C (en) * | 1994-03-30 | 1999-05-26 | 湖南安淳节能技术有限公司 | Ammonia-alcohol ratio adjustable technology for refining raw-material gas for synthesis of ammonia |
| CN1090228C (en) * | 1997-06-11 | 2002-09-04 | 三菱重工业株式会社 | Fine preparation method for gas |
| CN1098918C (en) * | 1997-07-22 | 2003-01-15 | 三菱重工业株式会社 | Gas refinishing process and gas refinishing equipment |
| CN1092228C (en) * | 1997-08-29 | 2002-10-09 | 三菱重工业株式会社 | Coal gas purifier |
| CN1090670C (en) * | 1997-10-03 | 2002-09-11 | 三菱重工业株式会社 | Gas purifying method and apparatus |
| CN100339298C (en) * | 2004-05-08 | 2007-09-26 | 吕仲明 | Non-isostatic alcoholization alkylation process for purifying raw gas for ammonia synthesis |
| CN1299971C (en) * | 2004-12-10 | 2007-02-14 | 南化集团研究院 | Technique for deep purifying material gas for synthesizing ammonia |
| CN110482568A (en) * | 2019-08-12 | 2019-11-22 | 上海国际化建工程咨询有限公司 | A kind of by-product alkanol for medium and small nitrogen fertilizer factory to be transformed and the method and system of cold and hot joint purification |
| CN113479905A (en) * | 2021-06-29 | 2021-10-08 | 福州大学化肥催化剂国家工程研究中心 | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system |
| CN113479905B (en) * | 2021-06-29 | 2022-08-05 | 福州大学化肥催化剂国家工程研究中心 | Self-deoxidization ammonia synthesis tower and renewable energy source ammonia synthesis system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1019663B (en) | 1992-12-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100526273C (en) | Method for integral production of liquid ammonia and methanol and/or dimethyl ether by using coke oven gas as raw material | |
| CA1065347A (en) | Methanol | |
| CN205035336U (en) | Resistant sulphur transform process systems of high concentration CO part | |
| CN104628508A (en) | System and process for preparing alkene from raw materials of coal and natural gas by virtue of synthesis | |
| CN103898265A (en) | System device and method for modifying coke oven gas to directly reduce iron ore | |
| CA1160020A (en) | Process for synthetising ammonia from hydro carbons | |
| CN102585951A (en) | Novel process for co-production of liquefied synthesis gas, pure hydrogen and methanol from coke-oven gas | |
| CN1053219A (en) | Refining process for synthetic ammonia raw material gas | |
| CN101993730A (en) | Multifunctional energy system based on appropriate conversion of chemical energy of fossil fuel | |
| CN102746870B (en) | FT synthesis technology | |
| CN101704714A (en) | Method for preparing synthesis gas after pure oxygen catalytic partial oxidation of purge gas in methanol synthesis loop to increase yield of methanol and device | |
| GB2098235A (en) | Process for increasing the calorific value of fuel gas mixtures containing hydrogen | |
| CN102101644B (en) | Method for preparing ammonia synthesis gas from iron alloy smoke | |
| US7947747B2 (en) | Joint process for preparing alcohol/ether mixtures alcohol/hydrocarbon mixtures, and synthesizing ammonia | |
| CN101550053B (en) | New process for producing firedamp by syngas | |
| CN201056492Y (en) | Natural gas partial oxidation series-connected heat exchange type device for washing synthetic ammonia by liquid nitrogen | |
| CN106672898A (en) | Method for synthesizing ammonia by taking byproduct tail gas in process of producing acetylene by pyrolyzing natural gas as raw material | |
| CN100408530C (en) | Method for producing methanol by using coke oven gas as raw material | |
| CN204509155U (en) | A kind of with coal and Sweet natural gas for raw material is through the system of synthetic gas alkene | |
| CN203904284U (en) | System for preparing reducing gas for shaft furnace through catalysis and gasification of coal | |
| CN102876828B (en) | Reducing gas purification process and system matched with gas-based shaft furnace | |
| US4692322A (en) | Process for producing a product gas containing carbon oxides and hydrogen from methanol | |
| CN103060035A (en) | Method for producing LNG (liquefied natural gas) by coal-based synthesis gas | |
| CN112979516B (en) | Energy-saving methyl mercaptan synthesis device | |
| CN114015481B (en) | Short-flow low-temperature methanol washing system and process thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C13 | Decision | ||
| GR02 | Examined patent application | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |