CN105384147A - Ammonia-synthesis and carbon-containing-chemical combinative production technology - Google Patents
Ammonia-synthesis and carbon-containing-chemical combinative production technology Download PDFInfo
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- CN105384147A CN105384147A CN201510742603.3A CN201510742603A CN105384147A CN 105384147 A CN105384147 A CN 105384147A CN 201510742603 A CN201510742603 A CN 201510742603A CN 105384147 A CN105384147 A CN 105384147A
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- C—CHEMISTRY; METALLURGY
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
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- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
- C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
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- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
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- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
- C01B2203/0261—Processes for making hydrogen or synthesis gas containing a partial oxidation step containing a catalytic partial oxidation step [CPO]
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/068—Ammonia synthesis
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1052—Nickel or cobalt catalysts
- C01B2203/1058—Nickel catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
Abstract
The invention discloses an ammonia-synthesis and carbon-containing-chemical combinative production technology. The combinative production technology includes the steps that a gas source containing carbon passes through a methane reforming unit and then passes through a purification unit, or the gas source containing carbon directly passes through the purification unit, the molar ratio of H2 to CO in the gas is allowed to meet the requirements of synthetic oil or low carbon alcohol or low carbon olefin, and the gas source enters a reactor to be subjected to a synthetic oil reaction or a low carbon alcohol reaction or a low carbon olefin reaction; products are separated through a separating device, residual tail gas is fed into a CO conversion device, and then CO2 is removed through a decarburizing device; or the CO2 in the residual tail gas is directly removed through the decarburizing device, then high-purity hydrogen is obtained through a PSA hydrogen extracting device and sent into an ammonia-synthesis work section, and meanwhile nitrogen in a proper proportion is sent into the ammonia-synthesis work section through an air separation device. The ammonia-synthesis and carbon-containing-chemical combinative production technology has the advantages that the use ratio of carbon is high, and efficiency and economic benefits are good.
Description
Technical field
The present invention relates to a kind of technique of synthetic ammonia coproducing carbon containing chemical.
Background technology
Since entering 2013, along with the release successively of newly-increased production capacity, the situation of national synthetic ammonia production capacity surplus progressively highlights, and enterprise goes into operation decline, and price declines is serious.According to Chinese nitrogen fertilizer industry association statistics, in 2013, industry average productivity utilization ratio drops to 80%, and price has declined nearly 30% apart from height point last year.According to current development trend, expect " 12 " end, national urea production capacity is by breakthrough 9,000 ten thousand tons, and the market requirement is about 6,230 ten thousand tons of (wherein industrial requirements 1,930 ten thousand tons, agricultural needs amount about 4,300 ten thousand tons, not containing outlet), urea production capacity surplus is close to 3,000 ten thousand tons.Because current farm crop are in higher level to amount of application of nitrogen fertilizer, the increasing degree that nitrogenous fertilizer will be consumed at agriculture field from now on tends towards stability substantially; Thermoelectricity, cement industry denitration and exhaust gas from diesel vehicle process etc. pull larger field to urea requirement, then after the quick growth (average annual growth reaches 11.6%) of 2013-2017, will obviously slow down the demand speedup of urea.Visible, the coming years, urea production capacity surplus will present the situation of expansion, and Fertilizer Industry in China is the crisis of immersal structure production capacity surplus.
Current domestic middle-size and small-size ammonia enterprise is lower due to the higher general working rate of cost, and the technological improvement and the product that how to perform middle-size and small-size ammonia enterprise adjust important realistic meaning.From a policy perspective, although government progressively tightens up Modern Coal-based Chemical project, encourage traditional coal chemical industry technological transformation upgrading.Since 2012, government has promulgated a series of policies and regulations, encourages the relevant items such as coal poly-generation, coke(oven)gas LNG, synthetic ammonia traditional coal chemical industry technological transformation upgrading.Synthetic ammonia with only the H in synthetic gas
2, and do not make full use of other gaseous fractions such as CO.By coproduction synthetic oil, low-carbon alcohol and low-carbon alkene, the available gas component of synthetic gas can be made full use of, realize the maximization of economic benefit.
China develops the combined production of methanol ammonia synthesis process technology with independent intellectual property right, experienced by semicentennial development, and connection alcohol Technology has been tending towards ripe at present.Synthetic ammonia coproducing methanol is that fertilizer industry institute of China is peculiar, and coal-based alcohol production capacity about 1,110 ten thousand tons/year in 2012, accounts for 21.5% of methyl alcohol aggregated capacity, is the important component part of China's methyl alcohol industry.But China's methyl alcohol aggregated capacity is also seriously superfluous in recent years, and current methanol production enterprise-wide working rate is on the low side.Therefore need to develop synthetic ammonia coproducing other products with the low problem of the working rate solving middle-size and small-size synthetic ammonia.
Summary of the invention
For the problems referred to above, the invention provides utilizing of a kind of carbon high, the technique of synthetic ammonia coproducing fischer-tropsch product/low-carbon alcohol/low-carbon alkene that efficiency is good in economic efficiency.
Present invention process concrete steps are as follows
By carbon containing source of the gas, first through methane reforming unit, then through clean unit; Or carbon containing source of the gas is directly through clean unit, make H in gas
2/ CO mol ratio meets the requirement of synthetic oil or low-carbon alcohol or low-carbon alkene, enter reactor carry out synthetic oil reaction or low-carbon alcohol reaction or low-carbon alkene reaction; Product is separated through tripping device, and residual exhaust sends into CO changing device, then takes off CO through decarbonization device
2, or residual exhaust directly takes off CO through decarbonization device
2, then carry hydrogen production device through PSA and obtain highly purified hydrogen, send into synthetic ammonia workshop section, by air separation facility, the nitrogen of proper ratio is sent into synthetic ammonia workshop section simultaneously.
As mentioned above, source of the gas of the present invention is the one of coal based synthetic gas, bio-based synthetic gas, Sweet natural gas, coal-seam gas, shale gas
As mentioned above, methane reforming unit of the present invention is selectable unit, if the source of the gas of workshop section meets the requirement of follow-up workshop section above, then need not convert, if the source of the gas of workshop section does not meet the requirement of follow-up workshop section above, then needs to be converted into and meets the requirement of follow-up workshop section.Described methane reforming process adopts methane portion oxidation synthesis gas technique, filling non-noble metal Ni-Al
2o
3catalyzer, reaction conditions: normal pressure, 600-800 DEG C, volume space velocity 1000-3000h
-1.
As mentioned above, clean unit of the present invention is the index requiring to control objectionable impurities according to the purification of follow-up workshop section, specific as follows: F-T synthesis unit will be obtained sulphur and arsenic total content in scavenging tower gas and be less than 0.1ppm, CO+CO
2total content is less than 10ppm; Higher alcohols synthesis unit will be obtained sulphur content in scavenging tower gas and be less than 0.05ppm, and arsenic content is less than 0.05ppm; Low-carbon alkene synthesis unit will be obtained sulphur content in scavenging tower gas and be less than 0.2ppm, and arsenic content is less than 0.1ppm.
As mentioned above, F-T synthesis unit of the present invention adopts the SMDS Technology of Shell company, filling Co/SiO
2catalyzer, reaction conditions: H
2/ CO=2-4 (V/V), 2.0-4.0MPa, 200-240 DEG C.
As mentioned above, the Sygmo1 technique that higher alcohols synthesis unit of the present invention adopts Dow chemical company of the U.S. and UCC to develop jointly, filling MoS
2catalyzer, reaction conditions: 290-310 DEG C, 8-10MPa, 5000-7000h
-1, H
2/ CO=1.1-1.3 (V/V).
As mentioned above, low-carbon alkene synthesis unit of the present invention adopt Dalian Chemical Physics Research Institute Technology, filling Fe-Mn/MgO catalyzer, reaction conditions: 300-400 DEG C, 1.0-2.0MPa, 1000-2000h
-1, H
2/ CO=2 (V/V).
As mentioned above, CO converter unit of the present invention is selectable unit, if meet synthetic ammonia requirement without CO or CO content in tail gas, then without the need to conversion, adopt high water/gas than conversion process, convert at water-gas ratio 1.8-2. (mol/mol) 3,340-400 DEG C.
As mentioned above, decarburization unit of the present invention adopts the strange low-temp methanol washing process technology in Shandong, major control index: becoming owner of the poor methanol temperature of washing tower is-40 ~-60 DEG C, goes out master and washes COS+H in the purified gas of tower
2s≤0.1ppm, CO
2≤ 3% (V/V), the water-content <1% (V/V) in poor methanol, total sulfur content <100ppm, NH in hot recycling tower backflash
3<5g/L, goes out Crouse's gas H of workshop section
2s concentration>=25% (V/V).
As mentioned above, PSA of the present invention puies forward the PSA Technology that hydrogen unit adopts Sichuan Tianyi Science & Technology Co., Ltd, major control index: H
2>=99.9% (V/V), CH
4≤ 0.1% (V/V), CO+CO
2≤ 20PPm, goes out unit temp 40 DEG C, goes out device pressure 2.4MPa.
As mentioned above, synthetic ammonia unit of the present invention adopts U.S. Kellogg ammonia synthesis process technology, processing condition 400-520 DEG C, 15-20MPa, 20000-30000h
-1, H
2/ CO=2.8-2.9 (V/V).
As mentioned above, air separation unit of the present invention adopts the space division technique technology of Linde Co, major control index: O
2≤ 10ppm.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention.
As shown in the figure: 1 is source of the gas, 2 is methane reformings, and 3 is purifications, and 4 is F-T synthesis, and 5 is synthesis of low-carbon alcohol, and 6 is synthesizing low-carbon alkene, and 7 is product separation, and 8 is CO conversion, and 9 is decarburizations, and 10 is that PSA carries hydrogen, and 11 is synthetic ammonia, and 12 is empty point.
Joint process of the present invention achieve synthetic ammonia and production synthetic oil/low-carbon alcohol/low-carbon alkene, greatly enhance the utilising efficiency of carbon.Joint process of the present invention reduces the depth requirements of conversion, the overall investment of synthetic ammonia installation reduces, thus reduce the production cost of synthetic ammonia, substantially increase the efficiency of carbon conversion of full factory, and can produce according to market requirement flexible, improve the economic benefit of full factory, have important meaning for cleaner production, energy-saving and emission-reduction.
Embodiment
In order to make object of the present invention, technical scheme and advantage clearly understand, by embodiment, the present invention is further elaborated below.Should be appreciated that specific embodiment described herein only in order to explain the present invention, be not intended to limit the present invention.
Embodiment 1
Take Sweet natural gas as source of the gas, adopt methane portion oxidation preparing synthetic gas by reforming, filling non-noble metal Ni-Al
2o
3catalyzer, normal pressure, 700 DEG C, volume space velocity 2000h
-1, obtain H
2the synthetic gas of/CO=3 (V/V), enters purification section, and going out sulphur and arsenic total content in scavenging tower gas is 0.08ppm, CO+CO
2total content is 7ppm, then enters Fischer-Tropsch synthesis device, adopts the SMDS Technology of Shell company, filling Co/SiO
2catalyzer, reaction conditions: H
2/ CO=3 (V/V), 2.8MPa, 220 DEG C; Out the product of reactor obtains hard wax, soft wax, heavy oil, light oil and liquefied petroleum gas (LPG) through separation, and the CO gas single-pass conversion through fischer-tropsch reaction is complete, and without the need to carrying out CO conversion, employing PSA carries the H in hydrogen technique extraction tail gas
2(H
2>=99.9% (V/V), CH
4≤ 0.1% (V/V), CO+CO
2≤ 5ppm), then converge the N of Kong Fen workshop section
2(O
2≤ 10ppm), adopt U.S. Kellogg technology to carry out synthetic ammonia, reaction conditions: 460 DEG C, 20MPa, 20000h
-1, H
2/ CO=2.8 (V/V).
Embodiment 2
From Shell crushed coal pressurized-gasification furnace H out
2the synthetic gas of/CO=1.2, does not need through conversion section, directly enters purification section, go out sulphur content in scavenging tower gas and be less than 0.04ppm, arsenic content is 0.03ppm, then enters low-carbon alcohol reactor, adopt the Sygmo1 technique that Dow chemical company of the U.S. and UCC develop jointly, filling MoS
2catalyzer, processing condition: 300 DEG C, 8MPa, 5500h
-1, H
2/ CO=1.2 (V/V); Out the product of reactor obtains methyl alcohol, ethanol, propyl alcohol, butanols and amylalcohol through separation; Unreacted CO gas, adopts high water/gas than conversion process, in water-gas ratio 2.0, carries out CO conversion at 380 DEG C, then removes CO with the strange low-temp methanol washing process in Shandong
2, go out CO in tower purified gas
2≤ 0.3% (V/V), adopts PSA to put forward hydrogen technique and obtains H
2(H
2>=99.8% (V/V), CH
4≤ 0.03% (V/V), CO+CO
2≤ 10ppm); Finally converge the N of Kong Fen workshop section
2(O
2≤ 10ppm), adopt U.S. Kellogg technology to carry out synthetic ammonia, reaction conditions: 470 DEG C, 18MPa, 30000h
-1, H
2/ CO=2.9 (V/V).
Embodiment 3
From texaco coal-water slurry gasification stove H out
2the synthetic gas of/CO=2, do not need through conversion section, directly enter purification section, going out sulphur content in scavenging tower gas is 0.15ppm, and arsenic content is 0.09ppm, then low-carbon alkene synthesis reactor is entered, adopt the Technology of Dalian Chemical Physics Research Institute, filling Fe-Mn/MgO catalyzer, reaction conditions 370 DEG C, 1.2MPa, 1200h
-1, H
2/ CO=2 (V/V); Out the product of reactor obtains ethene, propylene and butylene through separation, unreacted CO gas, adopts high water/gas than conversion process, in water-gas ratio 1.9, carries out CO conversion at 400 DEG C, then removes CO with the strange low-temp methanol washing process in Shandong
2, go out CO in tower purified gas
2≤ 0.5% (V/V), adopts PSA technique to obtain H
2(H
2>=99.99% (V/V), CH
4≤ 0.05% (V/V), CO+CO
2≤ 10ppm); Finally converge the N of Kong Fen workshop section
2(O
2≤ 8ppm), adopt U.S. Kellogg technique to carry out synthetic ammonia, reaction conditions: 450 DEG C, 16MPa, 25000h
-1, H
2/ CO=2.8 (V/V).
Claims (12)
1. a technique for synthetic ammonia coproducing carbon containing chemical, is characterized in that comprising the steps:
By carbon containing source of the gas, first through methane reforming unit, then through clean unit; Or carbon containing source of the gas is directly through clean unit, make H in gas
2/ CO mol ratio meets the requirement of synthetic oil or low-carbon alcohol or low-carbon alkene, enter reactor carry out synthetic oil reaction or low-carbon alcohol reaction or low-carbon alkene reaction; Product is separated through tripping device, and residual exhaust sends into CO changing device, then takes off CO through decarbonization device
2, or residual exhaust directly takes off CO through decarbonization device
2, then carry hydrogen production device through PSA and obtain highly purified hydrogen, send into synthetic ammonia workshop section, by air separation facility, the nitrogen of proper ratio is sent into synthetic ammonia workshop section simultaneously
.
2., as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described source of the gas is the one in coal based synthetic gas, bio-based synthetic gas, Sweet natural gas, coal-seam gas, shale gas.
3. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described methane reforming process adopts methane portion oxidation synthesis gas technique, filling non-noble metal Ni-Al
2o
3catalyzer, reaction conditions: normal pressure, 600-800 DEG C, volume space velocity 1000-3000h
-1.
4. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described clean unit is the index requiring to control objectionable impurities according to the purification of follow-up workshop section, specific as follows: F-T synthesis unit will be obtained sulphur and arsenic total content in scavenging tower gas and be less than 0.1ppm, CO+CO
2total content is less than 10ppm; Higher alcohols synthesis unit will be obtained sulphur content in scavenging tower gas and be less than 0.05ppm, and arsenic content is less than 0.05ppm; Low-carbon alkene synthesis unit will be obtained sulphur content in scavenging tower gas and be less than 0.2ppm, and arsenic content is less than 0.1ppm.
5. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described F-T synthesis unit adopts the SMDS Technology of Shell company, filling Co/SiO
2catalyzer, reaction conditions: H
2/ CO volume ratio=2-4,2.0-4.0MPa, 200-240 DEG C.
6., as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described higher alcohols synthesis unit adopts the Sygmo1 technique of Dow chemical company of the U.S. and UCC joint development, filling MoS
2catalyzer, reaction conditions: 290-310 DEG C, 8-10MPa, 5000-7000h
-1, H
2/ CO volume ratio=1.1-1.3.
7. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described low-carbon alkene synthesis unit adopt Dalian Chemical Physics Research Institute Technology, filling Fe-Mn/MgO catalyzer, reaction conditions: 300-400 DEG C, 1.0-2.0MPa, 1000-2000h
-1, H
2/ CO volume ratio=2.
8., as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described CO converts and adopt high water/gas than conversion process, convert at aqueous vapor mol ratio 1.8-2.3,340-400 DEG C.
9. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described decarburization unit adopts the strange low-temp methanol washing process technology in Shandong, major control index: becoming owner of the poor methanol temperature of washing tower is-40 ~-60 DEG C, goes out master and washes COS+H in the purified gas of tower
2s≤0.1ppm, CO
2≤ 3V%, the water-content <1V% in poor methanol, total sulfur content <100ppm, NH in hot recycling tower backflash
3<5g/L, goes out Crouse's gas H of workshop section
2s concentration>=25V%.
10., as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described PSA puies forward the PSA Technology that hydrogen unit adopts Sichuan Tianyi Science & Technology Co., Ltd, major control index: H
2>=99.9V%, CH
4≤ 0.1V%, CO+CO
2≤ 20PPm, goes out unit temp 40 DEG C, goes out device pressure 2.4MPa.
11. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described synthetic ammonia unit adopts U.S. Kellogg ammonia synthesis process technology, processing condition 400-520 DEG C, 15-20MPa, 20000-30000h
-1, H
2/ CO volume ratio=2.8-2.9.
12. as the technique of a claim 1 synthetic ammonia coproducing carbon containing chemical, it is characterized in that described air separation unit adopts the space division technique technology of Linde Co, major control index: O
2≤ 10ppm.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106542962A (en) * | 2016-10-17 | 2017-03-29 | 中石化上海工程有限公司 | With synthesis gas as the method for raw material combined production of methanol, synthesis ammonia and low-carbon alcohols |
| CN106542963A (en) * | 2016-10-17 | 2017-03-29 | 中石化上海工程有限公司 | The continuous producing method of synthesis gas combined production of methanol and low-carbon alcohols |
| CN107043089A (en) * | 2017-05-19 | 2017-08-15 | 福州大学化肥催化剂国家工程研究中心 | A kind of isobaric technique of the ammonia synthesis co-production containing carbon chemicals |
| CN111116294A (en) * | 2018-10-30 | 2020-05-08 | 中国石油化工股份有限公司 | Device and method for product separation and byproduct utilization of olefin prepared from synthesis gas |
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