• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to a method for producing carbon monoxide from a nitrogen-contaminated gas containing mainly hydrogen, carbon monoxide and methane, and simplifies the process. The gas stream is separated at a low temperature to obtain a nitrogen-containing fraction of carbon monoxide and part of the carbon monoxide is circulated to compensate for the cold need of the process, and the remaining portion of carbon monoxide is diverted as the desired product. Nitrogen-containing carbon monoxide is separated into carbon monoxide and the nitric fraction containing carbon monoxide by means of rectification. In this case, the lower part of the distillation column (RK) is heated by circulating carbon monoxide, and carbon monoxide in the lower part of the RK in liquid form after reducing its pressure is applied during the cooling of the upper part of the RK. 2 hp f-lt, 2 ill. I SU) compiled 00 4 S1
    公开号:SU1358794A3
    申请号:SU833584200
    申请日:1983-04-27
    公开日:1987-12-07
    发明作者:Фабиан Райнер
    申请人:Линде Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to a process for producing carbon monoxide from a nitrogen-contaminated and mainly hydrogen, carbon monoxide and methane gas stream, the gas stream being separated at a low temperature to produce a nitrogen oxide-containing carbon monoxide portion of the carbon monoxide to cover the cold process requirement. is in circulation, and the remainder is disposed of as a product.
    Fig. 1 shows an installation that implements the proposed method in conjunction with methane washing; figure 2 - the same, in conjunction with partial condensation.
    The installation for implementing the method includes pipelines 1-28, heat exchangers 29-34, compressors 35-36, turboexpanders 37 and 38, valves 39-51, sumps 52-54, compressor 55, tank 56, pumps 57 and 58, cool
    The heater 59, the condensers 60-62, the heating 25 is emitted in the form of gas and the combining unit 63, the mixer 64, the washing column 65, the regeneration column 66, the columns 67 and 68, the pipelines 69-71.
    The method is implemented as follows.
    Pipeline 1 supplies gas obtained by steam reforming of natural gas, which contains, mol%: hydrogen 70.54; carbon monoxide 24.69; methane 3.49; nitrogen 1.28. The gas that is produced by the reforming of natural gas has a nitrogen content of 5 mol%. In the general case, the proposed method can process natural gases with a nitrogen content of up to about 15 mol%. If there are gases with an even higher nitrogen content, then it is more economically advantageous to use nitrogen separation before steam reforming than to use
    the proposed method.
    I
    The gas used is supplied through conduit 1 at a pressure of 14 bar and a temperature of 36 ° C. In heat exchangers 29 and 30, the gas is cooled by cold separation products to 92 K, and the methane and carbon monoxide contained in the split gas are largely condensed. The biphasic mixture is fed to the bottom of the methane wash column 65. From the remaining gas in the wash column 65, the carbon monoxide is washed out with liquid
    ten
    - 15 3587942
    methane, which is introduced through conduit 4 into the upper part of the wash column 65. Purified hydrogen is taken from the upper part of the wash column via conduit 69, which contains about 1.5 mol.% of methane, 0.2 mol.% of nitrogen and 10 as impurities. ppm carbon monoxide. This hydrogen fraction is heated in heat exchanger 30, then expanded in expander 37 to release cooling energy, and after reheating in heat exchangers 30 and 29 through conduit 2 is discharged as merchandise hydrogen.
    Wash- ing methane with all of the carbon monoxide containing the predominant part of nitrogen and a small amount of dissolved hydrogen is removed from the bottom of the effluent column 65 and in valve 39 is brought to a pressure of about 4 bar. When this is dissolved in the flushing methane
    0
    five
    Responsible equilibrium conditions are also carbon monoxide, nitrogen, and methane. The components that were dissolved in the gaseous state, where hydrogen and carbon monoxide are approximately the same, are separated in the sump 52, their pressure in the valve 40 is lowered and, after heating in the heat exchangers 30 and 29, is removed through pipeline 3 as a fraction of the heating
    gas.
    I
    In another embodiment, the sump 52 is replaced by a small distillation column, the upper part of which is cooled by circulating carbon monoxide under a pressure of 1.5 bar and at a temperature of 86 K. Due to this, the content of carbon monoxide in this fraction of heating gas decreases below
    5 to 40 mol%.
    Remaining in a settling tank 52 or in an appropriate distillation coke. The liquid is divided into two partial streams and in valves 41 and 42
    0, its pressure is reduced to 2.5 bar. The partial flow through the valve 41 is evaporated in the heat exchanger 30 and then fed to the regeneration column 66.
    5, a partial flow valve 42 is introduced directly into the regeneration tower 66 a few floors above the previous partial flow. The regeneration column 66 has a head condensation. . 3
    a torus 60 in the upper part, as well as a lower temperature detector 63, both of them are filled with carbon monoxide circulating in the circuit. Pure methane is present in the lower part of the column, the pressure in which by pump 57 is adjusted to the pressure of the incoming raw gas. Pipeline 4 branches off the methane required for methane rinsing, cools down the heat exchanger 30- and goes to the wash column 65. Methane pressure decreases in valve 46 and it is mixed with the heating gas fraction withdrawn from the sump 52.
    The product from the top of the recovery column 66 is a mixture, mol%: carbon monoxide 95.05; nitrogen 4.8; methane 0.1; hydrogen 0.05. This gas is introduced into the middle part of the distillation column 67, which also operates under a pressure of 2.5 bar (if the pressure drop is neglected). Nitrogen, which contains residual hydrogen and about 35 mol.% Carbon monoxide and is mixed with the fraction of heating gas, is taken off from the top of this distillation column through conduit 5. Pure carbon monoxide is removed from the bottom of the distillation column 67, its pressure in valve 47 drops to 1.5 bar, and the temperature decreases from 90.5 to 85 K and evaporates in the condenser 61 in the top of column 67. A small amount is fed through valve 48 the amount of liquid carbon monoxide to cover the loss of cold in the separation of nitrogen and carbon monoxide.
    The carbon monoxide selected from the bottom of the distillation column 67, which contains both the commercial product and the carbon monoxide of the circuit, after its evaporation in the condenser 61 heats up in the heat exchanger 31 supercooled liquid carbon monoxide 1; and finally it is heated in the heat exchanger 29. Carbon monoxide pressure of 1.1 bar is supplied to the compressor 35, from which a commodity product is withdrawn through line 11, carbon monoxide from the corresponding pressure level. The carbon monoxide to be supplied to the circuit, after being compressed to 30 bar, is cooled in the heat exchanger 29, condenses in the heater, the lower part of the regene 585844
     Then, the carbon dioxide is heated in a heat exchanger 31 in the heat exchanger 31, and the pressure of carbon monoxide in the tank 56 is reduced to 2.5 bar. Separate cooling stages feed on this liquid carbon monoxide.
    Pipelines 7 and 70, as well as
    10 through the valve 45, the partial flow enters the heat exchanger 30 and there the evaporated while the other partial flow through pipelines 7 and 10, as well as through the valve 43 enters the cooler 59 of the discharge column. After evaporation in heat exchanger 30 and cooler 59, both partial streams of carbon monoxide are re-combined and discharged through pipeline 9 at a pressure of 2.5 bar. This gas is mixed with the expanded gas, which is discharged through conduit 9 and through conduit 8 enters the lower part of the distillation column 67 as the heating vapor.
    The pressure of another partial stream discharged through conduit 7 from the liquid carbon monoxide tank in valve 44 is reduced to 1.5 bar and fed as cooling means to condenser 60 in the upper part of regeneration column 66. Evaporated carbon monoxide is mixed with evaporated in condenser 5 61 distillation columns are commercial and circulating carbon monoxide, and after reheating, they are again supplied to carbon monoxide compressor 35.
    The proposed method (figure 2) is advantageous for processing gas mixtures with a low methane content, since it is not provided for methane washing.
    Pipeline 12 supplies 5 gas with a high content of carbon monoxide, which contains, mol%: hydrogen 29.7; nitrogen 4.2, methane 0.1; carbon monoxide 66. The gas in the mixer 64 is mixed with the cooled gas, 0 mainly containing hydrogen and carbon monoxide, and then compressed in the compressor 36. In the heat exchangers 32 and 33 the gas is cooled to about 78 K, and condensate is formed with a high content of carbon monoxide which is separated in the sump 53. To release dissolved hydrogen, the pressure exiting through the pipeline from the condensate sump 53 decreases
    0
    in valve 49 to about 1.5 bar and it is fed to another sump 54.
     The liquid phase from the sump 54 consists of a mixture of carbon monoxide and rasa.i A partial flow of this liquid is led through line 15 and is fed into an open refrigerant circuit. The cycle is also fed through pipeline 16, released under reduced pressure by gas from sump 54, as well as by a partial flow of low pressure side of the turbine expander 38, into which gas with a high content of hydrogen from sump 53 is heated after heating in heat exchangers 33 and 32 with cooling in the expander. The mixture formed from lines 15, 16 and 14 is a very low temperature refrigerant that is heated in heat exchangers 33 and 32, cooling process flows, and finally mixed with raw gas in mixer 64.
    The main flow from sump 54 is reduced by pump 58 to a pressure of 2.6 bar and leads through pipeline 17; -, c to heat exchanger 33 and is heated, then in heat exchanger 31 is partially evaporated and through pipeline 18 is fed to nitrogen separation column 6B, where it is lowered pressure. The product from the top of column 68 is the nitrogen fraction, which is led through conduit 19 to the residual gas conduit 20, which also carries excess gas from the turboexpander outlet through conduit 13.
    heated by blowing cold Q holding 98% of carbon monoxide and only
    of carbon monoxide through pipe 27. This stream leaves the column 68 with a commercial product of carbon monoxide in a liquid state through line 21. In valve 51, the pressure of a part of this product from the bottom of the column drops to 1.5 bar and is fed through line 22 to condenser 62 at the top of column 68 and evaporated there. The evaporated carbon monoxide under low pressure through the pipeline 24 is supplied to the heat exchanger 34 and heated there, cooling
    carbon monoxide in the circuit. A partial stream of vaporized carbon monoxide through line 23 can be mixed into the rest of the product from the bottom of column 68, which, after reducing the pressure in valve 50
    is removed through conduit 71. This fraction is used in the heat exchanger 32 as an additional refrigerant, and after heating through conduit 28 it is combined with the partial flow heated in the heat exchanger 34 and is supplied to the carbon monoxide compressor 55. From the appropriate stage
    the pressure through pipeline 25 is taken commercially available carbon monoxide, while part of the circuit is withdrawn through pipeline 26, is supplied to the heat exchanger 34, in which
    it is cooled before being fed back to column 68.
    Example 1. A mixture containing,%, is fed to a column for nitrogen / carbon monoxide distillation separation:
    hydrogen 2; nitrogen 4; carbon monoxide 94. The rectification is carried out at a pressure of 1.5 bar, and the top temperature of the column is 80 K, and the bottom is 84 K.
    权利要求:
    Claims (3)
    [1]
    I
    A gas mixture containing,%: hydrogen 29, nitrogen 33, carbon monoxide 38, and a fraction of carbon monoxide containing only 2% nitrogen is withdrawn from the top of the column.
    Example 2. A mixture containing, in%: hydrogen, 0.03; nitrogen 3.97 and carbon monoxide 96. The rectification is carried out at a pressure of 3.5 bar, the temperature of the top column is 91 K, and the bottom of the column is 93 K. A gas mixture containing,%, hydrogen 1 is withdrawn from the top of the column: hydrogen 1; nitrogen 41 and carbon monoxide 58, and from the cube - oxide fraction, CO2% nitrogen.
    Formula inventions
    45 1. A method of producing carbon monoxide from a gas mixture containing nitrogen, hydrogen, carbon monoxide and methane, comprising the low-temperature rectification of the gas mixture in a column with
    5Q obtaining nitrogen fraction and carbon monoxide, the supply of carbon monoxide as a refrigerant to the circulation, followed by the removal of part of carbon monoxide to the consumer, is different from the fact that, in order to simplify the technology, the lower part of the distillation column is heated by circulating carbon monoxide and released at the bottom of the rectification
    the columns, liquid carbon monoxide, after reducing its pressure, serves to cool the upper part of the distillation column.
    [2]
    2, Method 1, characterized in that the heating of the bottom
    portions of the distillation column are carried out by heat exchange with gaseous carbon monoxide,
    [3]
    3. The method according to claim 1, characterized by the fact that the rectification is carried out at a temperature of 80-93 K.
    27
    Editor M.Blanar
    Compiled by A.Nikitin Tehred L. Serdyukova
    Order 6012/59 Tyrant 476Subscription
    BNIIPI USSR State Committee
    for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
    Production
    printing enterprise, Uzhgorod, st. Project, 4
    ((Z.2
    Proofreader I. Muska
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19823215829|DE3215829A1|1982-04-28|1982-04-28|METHOD FOR PRODUCING CARBON MONOXIDE|
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