CN1451642A - Method for producing methanol and synthetic ammonia - Google Patents
Method for producing methanol and synthetic ammonia Download PDFInfo
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- CN1451642A CN1451642A CN 02113606 CN02113606A CN1451642A CN 1451642 A CN1451642 A CN 1451642A CN 02113606 CN02113606 CN 02113606 CN 02113606 A CN02113606 A CN 02113606A CN 1451642 A CN1451642 A CN 1451642A
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- synthetic
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- methanol
- ammonia
- synthetic ammonia
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Abstract
A process for preparing both methanol and synthetic ammonia includes separated two systems for respectively preparing methanol and synthetic ammonia. The system for preparing methanol includes converting to prepare synthetic gas, synthesizing methanol while releasing gas and rectifying. The system for preparing synthetic ammonia from said released gas includes mixing with air, steam, or oxygen, two-stage conversion, transformation, decarborizing and methanation. Its advantages are simple process, and no N2 in the synthetic gas for preparing methanol.
Description
One, technical field
The invention belongs to the production method of methyl alcohol and synthetic ammonia, particularly a kind of method of methanol with joint production of synthetic ammonia.
Two, background technology
On the combination producing of methyl alcohol and synthetic ammonia, the general at present synthetic ammonia coproducing methanol that adopts, promptly the reforming gas with synthetic ammonia is the raw material synthesizing methanol, its operational path both can be in parallel, it can be again series connection, can also be series connection and parallel connection combine (see " big nitrogenous fertilizer ", 2000 the 23rd roll up P372).Technical process shown in Figure 1 is a kind of method that generally adopts of synthetic ammonia coproducing methanol, as can be seen from Figure 1, through one section conversions, two sections conversions prepared contain N
2A reforming gas part as the unstripped gas of synthetic ammonia, a part extracts synthesizing methanol, the synthetic tail gas that produces of methyl alcohol returns synthetic ammonia installation again as syngas for synthetic ammonia.There is following shortcoming in above-mentioned alcohol technology: 1, a large amount of nitrogen circulate in system for methanol synthesis, cause methanol synthesis loop huge, have increased facility investment and circulator power; 2, reforming gas should be as the unstripped gas of synthetic ammonia, and again as the synthetic gas of methyl alcohol, thereby gas making operation load increases, and facility investment increases, the also corresponding increase of power of reforming gas compression simultaneously; 3, reforming gas should satisfy the processing requirement of synthetic ammonia, satisfies the processing requirement of methyl alcohol again, thereby the operation easier of gas making operation is bigger; 4, ammonia synthesis process system and methanol technics system influence each other seriously.
Three, summary of the invention
The present invention is directed to the deficiency that prior art exists, a kind of method of methanol with joint production of synthetic ammonia is provided, with save energy, minimizing investment, and it is few to make methyl alcohol and synthetic ammonia two systems lead connection mutually, stable operation.
Method provided by the invention is to be two relatively independent operational systems with methanol process and Ammonia Production technological design; Methanol production adopts common process, and processing step mainly contains and transforms the preparation synthetic gas, methyl alcohol is synthetic and methanol rectification; Ammonia Production is a raw material with the synthetic off-gas that produces of methyl alcohol, can make full use of the characteristics that contain a large amount of hydrogen in the off-gas, this off-gas and air, steam or oxygen are prepared into reforming gas by two sections conversions, carry out ammonia synthesis through conversion, decarburization, methanation then.
Better for the production effect that makes synthetic ammonia, the present invention has also taked following technical scheme:
1, the synthetic off-gas decompression that produces of methyl alcohol or etc. be depressed into two sections and send into synthetic ammonia installation again after transforming desired pressure.
2, after the off-gas of sending into synthetic ammonia installation adds steam, send into secondary reformer and carry out two sections conversions through being heated to 500～700 ℃.
3, two sections when transforming, the H in the synthetic gas that the add-on of air forms after with methanation
2: N
2=(2.5～3): 1 control.
4, two sections methane contents that transform in the reforming gas for preparing are 0.5～1.0%.
The present invention has the following advantages and beneficial effect:
1, with the synthetic high H that produces of methyl alcohol
2, low CH
4The off-gas of content is the unstripped gas of synthetic ammonia, has reduced the load of ammonia operation, thereby ammonia only needs secondary reformer, can remove traditional primary reformer and desulfurizing and purifying system, and technical process is simplified, and facility investment reduces.
2, do not contain a large amount of nitrogen in the synthetic gas of methyl alcohol, thereby the compression work of having avoided nitrogen to circulate being brought waste and equipment is huge in the methanol production system.
3, methanol process and Ammonia Production technology are two relatively independent systems, and methanol production is operated under the operating mode of the best, are not subjected to the influence of Ammonia Production.
4,, thereby saved the technology steam that transforms in a large number because the hydrogen concentration height in the off-gas descends the steam/hydrocarbons ratio of conversion significantly.
5, off-gas is sent into synthetic ammonia installation after decompression, has utilized its high pressure, the power consumption of natural gas compression in the time of can saving conventional Ammonia Production.
6, avoided the synthetic off-gas that produces of methyl alcohol to act as a fuel and the energy wastage that causes.
7, existing ammonia production system is transformed, can be reduced fuel, gas making consumption of raw materials greatly; If keep original primary reformer of ammonia production system, then can improve the gas making ability greatly.
Adopting method construction scale provided by the invention is 100,000 tons/year methanol device, can coproduction 2～60,000 ton/year synthetic ammonia (output is adjustable); To can be according to the methanol device of the supporting corresponding scale of ability of synthetic ammonia less than 40,000 tons/year existing synthetic ammonia installation; To the synthetic ammonia installation greater than 100,000 tons/year the supporting corresponding scale of methanol device, economic benefit can be better.The chemical plant of every existing synthetic ammonia installation methanol device again adopts method provided by the invention all can realize purpose energy-conservation and the minimizing investment.
Four, description of drawings
Fig. 1 is a kind of process flow sheet of synthetic ammonia coproducing methanol;
Fig. 2 is a kind of process flow sheet according to methanol with joint production of synthetic ammonia proposed by the invention.
Five, embodiment
Embodiment 1:
100,000 tons/year of the methanol production scales of present embodiment, 30,000 tons/year of Ammonia Production scales, technical process is as shown in Figure 2.Methanol production is raw material with the natural gas, adopts conventional technical process and corollary apparatus and is operational system independently, and processing step mainly contains and transforms the preparation synthetic gas, methyl alcohol synthesizes and methanol rectification.Ammonia Production is a raw material with the synthetic off-gas that produces of methyl alcohol, and the pressure of off-gas is that 4.7MPa, temperature are 40 ℃, H
2Be 82%, CH
4Be 10.5%; above-mentioned off-gas does not need reduced pressure treatment; directly to 4.4MPa, enter synthetic ammonia installation; add process steam through being heated to 350 ℃; further being heated to 500 ℃ then ℃ sends into secondary reformer with the heat exchange to 600 of secondary reformer exit gas again and transforms; process air is preheated to 600 ℃ and sends into secondary reformer with protection steam, the H in the synthetic gas that the add-on of process air forms after with methanation
2: N
2=3: 1 control, in secondary reformer, off-gas-mixture of steam mixes, and airborne oxygen and hydrogen, methane generation oxidizing reaction are CO, H with the hydrocarbon conversion
2Emit a large amount of heat simultaneously and at high temperature carry out degree of depth conversion for remaining methane, obtaining methane content is the reforming gas of 0.50% (butt), the reforming gas that goes out secondary reformer adopts conventional ammonia synthesis process and corollary apparatus to produce synthetic ammonia after reforming gas interchanger, reforming gas boiler reclaim heat, and processing step comprises conversion, decarburization, methanation, ammonia synthesis.
Embodiment 2:
100,000 tons/year of the methanol production scales of present embodiment, 60,000 tons/year of Ammonia Production scales, technical process is as shown in Figure 2.The raw material of methanol production, technical process are identical with embodiment 1.The used off-gas pressure of Ammonia Production is that 4.7MPa, temperature are 40 ℃, H
2Be 75%, CH
4Be 17%, above-mentioned off-gas enters synthetic ammonia installation after being decompressed to 3.4MPa, mix with water vapor after be preheated to 650 ℃ and enter secondary reformer and transform, the oxygen and the next process air of compression section that are come by the methyl alcohol air separation facility mix, after being preheated to 650 ℃, enter secondary reformer, the H in the synthetic gas that the add-on of process air forms after with methanation
2: N
2=2.5: 1 control, the content that secondary reformer transforms the methane in the reforming gas for preparing is 0.9% (butt), the reforming gas that goes out secondary reformer adopts conventional ammonia synthesis process and corollary apparatus to produce synthetic ammonia after reforming gas interchanger, waste heat boiler reclaim heat, and processing step comprises conversion, decarburization, methanation, ammonia synthesis.
Claims (6)
1, a kind of method of methanol with joint production of synthetic ammonia, it is characterized in that methanol process and Ammonia Production technology are two relatively independent operational systems, the methanol process step comprises conversion preparation synthetic gas, methyl alcohol is synthetic and methanol rectification, Ammonia Production technology is raw material with the synthetic off-gas that produces of methyl alcohol, this off-gas and air, steam or oxygen are prepared into reforming gas by two sections conversions, carry out ammonia synthesis through conversion, decarburization, methanation then.
2, the method for methanol with joint production of synthetic ammonia according to claim 1 is characterized in that the synthetic off-gas decompression that produces of methyl alcohol or waits and send into synthetic ammonia installation after being depressed into two sections desired pressure of conversion.
3, the method for methanol with joint production of synthetic ammonia according to claim 2 after the off-gas that it is characterized in that sending into synthetic ammonia installation adds steam, is sent into secondary reformer and is carried out two sections conversions through being heated to 500～700 ℃.
4, according to the method for claim 1 or 2 or 3 described methanol with joint production of synthetic ammonia, the H in the synthetic gas that the add-on that it is characterized in that two sections air when transforming forms after with methanation
2: N
2=(2.5～3): 1 control.
5,, it is characterized in that two sections methane contents that transform in the reforming gas for preparing are 0.5～1.0% according to the method for claim 1 or 2 or 3 described methanol with joint production of synthetic ammonia.
6, the method for methanol with joint production of synthetic ammonia according to claim 4 is characterized in that two sections methane contents that transform in the reforming gas for preparing are 0.5～1.0%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02113606 CN1451642A (en) | 2002-04-15 | 2002-04-15 | Method for producing methanol and synthetic ammonia |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02113606 CN1451642A (en) | 2002-04-15 | 2002-04-15 | Method for producing methanol and synthetic ammonia |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1451642A true CN1451642A (en) | 2003-10-29 |
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ID=29220909
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|---|---|---|---|
| CN 02113606 Pending CN1451642A (en) | 2002-04-15 | 2002-04-15 | Method for producing methanol and synthetic ammonia |
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| CN (1) | CN1451642A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1326821C (en) * | 2004-11-19 | 2007-07-18 | 朱宗林 | Process of coarse methanol from synthetized ammonia |
| CN101602649A (en) * | 2009-07-27 | 2009-12-16 | 福州大学 | A kind of mesolow alcohol, ether hydrazine production process |
| CN102050699A (en) * | 2010-11-04 | 2011-05-11 | 茌平信祥化工有限公司 | Process for co-producing methanol and ammonia by utilizing calcium carbide tail gas |
| CN102180767A (en) * | 2011-03-10 | 2011-09-14 | 庞玉学 | Method and device for jointly producing methanol, ammonia and acetic acid by using coal and natural gas |
| CN102229434A (en) * | 2011-04-05 | 2011-11-02 | 宁波金远东工业科技有限公司 | Apparatus for joint production of methanol and synthetic ammonia by using exhaust gas from methanol synthesis |
| CN102482183A (en) * | 2009-08-20 | 2012-05-30 | 沙特基础工业公司 | Process for methanol and ammonia co-production |
| CN102580490A (en) * | 2012-01-16 | 2012-07-18 | 重庆市万利来化工股份有限公司 | Methanol purge gas recycling process |
| CN103896306A (en) * | 2012-12-26 | 2014-07-02 | 昭和电工株式会社 | High-purity ammonia, method and device for manufacturing same |
| CN108863724A (en) * | 2018-07-30 | 2018-11-23 | 河南心连心化肥有限公司 | A kind of device and technique of synthetic ammonia coproducing methanol |
-
2002
- 2002-04-15 CN CN 02113606 patent/CN1451642A/en active Pending
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1326821C (en) * | 2004-11-19 | 2007-07-18 | 朱宗林 | Process of coarse methanol from synthetized ammonia |
| CN101602649A (en) * | 2009-07-27 | 2009-12-16 | 福州大学 | A kind of mesolow alcohol, ether hydrazine production process |
| CN102482183A (en) * | 2009-08-20 | 2012-05-30 | 沙特基础工业公司 | Process for methanol and ammonia co-production |
| CN102482183B (en) * | 2009-08-20 | 2015-07-01 | 沙特基础工业公司 | Process for methanol and ammonia co-production |
| CN102050699A (en) * | 2010-11-04 | 2011-05-11 | 茌平信祥化工有限公司 | Process for co-producing methanol and ammonia by utilizing calcium carbide tail gas |
| CN102050699B (en) * | 2010-11-04 | 2013-07-24 | 茌平信祥化工有限公司 | Process for co-producing methanol and ammonia by utilizing calcium carbide tail gas |
| CN102180767A (en) * | 2011-03-10 | 2011-09-14 | 庞玉学 | Method and device for jointly producing methanol, ammonia and acetic acid by using coal and natural gas |
| CN102229434A (en) * | 2011-04-05 | 2011-11-02 | 宁波金远东工业科技有限公司 | Apparatus for joint production of methanol and synthetic ammonia by using exhaust gas from methanol synthesis |
| CN102580490A (en) * | 2012-01-16 | 2012-07-18 | 重庆市万利来化工股份有限公司 | Methanol purge gas recycling process |
| CN103896306A (en) * | 2012-12-26 | 2014-07-02 | 昭和电工株式会社 | High-purity ammonia, method and device for manufacturing same |
| CN103896306B (en) * | 2012-12-26 | 2016-02-24 | 昭和电工株式会社 | High purity ammonia and manufacture method thereof and high purity ammonia manufacturing installation |
| CN108863724A (en) * | 2018-07-30 | 2018-11-23 | 河南心连心化肥有限公司 | A kind of device and technique of synthetic ammonia coproducing methanol |
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