• 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:
    A method for increasing the hydrogen sulfide concentration in a gas stream, particularly a stream to be fed to a Claus unit, is disclosed. The method is characterized by the measurement of the flow of the gas stream to an absorption system, and in response to such measurement, separation of a portion of the acid gas leaving the regenerator of the system, and selective absorption of the H2S in the portion, with passage of the loaded absorbent to the regenerator.
    公开号:SU1069619A3
    申请号:SU782567996
    申请日:1978-01-24
    公开日:1984-01-23
    发明作者:Верлоп Ян；Вильхельмус Йоханнес；Мариа Брам Теодорус
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    a: with
    C5
    2. The method according to Claim 1, about t and chayush and with the fact that when the value of the gas flow supplied
    In a process less than the first predetermined value, a regenerated absorbent is first fed to the second absorber, and then a gas stream.
    3. The method according to claims 1 and 2, characterized in that the supply of the absorbent to the second absorber is controlled depending on the flow rate of the gas supplied to the second absorber
    4. Method according to Claims 1 and 2, about tl, which means that when the value of the flow rate of the feed gas is exceeded by a second predetermined value, the flow of the gas is first stopped, and then the regenerated absorbent.
    5. The method according to claims 1-4, about tl and h ay u and with the fact that the flow of gas into the second absorber regulate
    depending on the concentration of hydrogen sulfide in the gas after the regenerator.
    The invention relates to the automatic control of the gas treatment process in the production of sulfur and can be used in the chemical industry.
    There is a known method for automatically controlling the desorption process by adjusting the steam flow rate with a correction for the content of acidic components in the regenerated solution and the minimum loss of the amount of the regenerated solution l.
    There is also known a method for automatically adjusting an absorber by adjusting an absorber mode depending on a monitored process variable 2,
    A common disadvantage of the known methods is that they do not provide high precision of the process control. This leads to a decrease in the concentration of hydrogen sulfide in the acid gas.
    The aim of the invention is to increase the concentration of hydrogen sulfide in the acid gas by increasing the accuracy of the process control.
    The goal is achieved in that according to the proposed method, when the value of the gas flow supplied to the process is less than the first predetermined value, a part of the gas released from the absorbent and regenerated absorbent after the regenerator is directed to the second absorber, and when the second preset gas flow value is exceeded The values for the flow of gas and regenerated absrbent to the second absorber stop.
    When the value of the gas stream supplied to the process is less than the first specified value, the regenerated absorbent is first fed to the second absorber, and then the gas stream.
    The flow of absorbent in the second absorber regulate depending on the flow rate of the gas supplied to the second absorber.
    When the value of the feed gas flow exceeds a second setpoint value, the flow of gas is first stopped, and then the regenerated absorbent.
    The flow of gas in the second absorber regulate depending on the concentration of hydrogen sulfide in the gas after the regenerator.
    The magnitude of the gas flow determines, among other things, the degree of absorption by the ab carbon dioxide sorbent: if the gas flow is small, the CO is absorbed by the naive more than with a large flow. The gas separated from the absorbent after regeneration contains not only hydrogen sulfide, but also carbon dioxide. If, for example, hydrogen sulphide is only 2%. it is undesirable to direct such a gas stream to the Claus process.
    Part of the gas entering the absorbent goes to the second absorber, in which the conditions are selected in such a way that H2S is absorbed by the absorbent, i.e. selectively removed from the gas stream.
    The saturated absorbent thus obtained from the second absorber also enters the regenerator, where the gas is separated from the absorbent, just as the gas from the saturated absorbent of the first absorber. The combined gas stream exiting the regenerator in this way has a higher content of sulfur, hydrogen than the gas exiting the regenerator before using the second absorber. A new equilibrium is set at the desired concentration of HjiS. If the amount of gas going to the first absorber, will start
    increase again, at some point the situation will become such that the measured value exceeds the second specified value and the flow of gas flow to the second absorber stops.
    Preferably, / the second predetermined value is chosen greater than the first, in order to ensure stable control of the automatically proceeding process.
    At the moment when the value of the inlet gas stream becomes too small and the concentration of rijS in the outgoing gas reaches. the value at which the quantity in the feed gas remains reasonably constant, the effect of the reduced gas supply 6yjcieT feel at the outlet of the plant after some time. Therefore, the regulation of the gas flow to the second absorber should begin only some time after the moment of reduced supply. In order to have the second absorber in working condition at the moment when the gas starts to flow into this absorber, the circulation of the absorbent usually must begin immediately after the amount of gas entering the first absorber falls below a certain desired value. A signal will pass through the delay device to open a line through which the gas enters the second absorber.
    If the concentration of hydrogen sulfide in the stream going to the first absorber is not constant, then it is preferable to compare the concentration of the hydrogen sulfide in the gas released from the absorbent when comparing the quantity characterizing the flow quantity with the specified value. In this way, it is possible to assess the quality of the gas, i.e. H2S concentration in the released gas, within certain limits.
    Figure 1 shows a schematic diagram of the implementation of the proposed method; figure 2 - dependence of the values of various streams on the magnitude of the gas stream supplied to the installation.
    Acid gas is fed to absorber 1 through inlet 2, and absorbent through inlet 3. The absorbent saturated with the acidic constituents of the gas is withdrawn from the lower part 4 of the absorber by means of a pump 5. From the upper part 6 of the absorber, the remaining gas flows, which is sent along line 7, for example, to a combustion furnace (not shown). The liquid level in the absorber 1 is controlled by a level 8 regulator and a valve 9 installed in the output line 10 of the pump 5.
    The saturated absorbent through line 10 is fed to the upper part of the regenerator 11, in which the acid components of the gas are again separated from the absorbent. As a result, the pure absorbent leaves the regenerator through its lower part 12, and the components of the acid gas, mainly hydrogen sulfide and carbon dioxide, leave the regenerator 13 through the top 13. This acid gas mixture is fed through line 1, for example, in a Claus process (not shown), where hydrogen sulfide is converted to elemental sulfur. Line 15, through which the acid gas is supplied to the absorber 1, is provided with a flow meter and a sensor 16, which determines the gas flow and generates the appropriate signal, a, which is fed to the input of the computing device 17. The device 17 also receives a signal 5 from the meter and A sensor 18, which is installed in line 14 and determines the concentration of hydrogen sulfide in the gas flowing along this line. The output signal 6 from the computing device 17 is in the following dependence on the signals a and 6;
    B + (2 g
    where k., and constant ..
    The signal enters the solenoid valve 19, which allows the signal to pass to the flow controller 20 when the valve is opened by the action of a signal that is generated at the output of the switch 21 if it is greater than the first predetermined value. If then it becomes lower than the second setpoint, the switch 22 will produce a signal that closes the valve. The signal generated at the output of the switch 21, on its way to the valve 19, passes the delay device 23, as a result of which some time passes between the signal reaching the input of the specified element, its output and, consequently, the valve 19. The output of the switch 21 next with a solenoid valve 24, which opens with a signal coming from switch 21, and this signal also serves to start pump 25 through switch 26. As soon as valve 19 opens, the signal passes through it to flow controller 20, which controls the cell apan 27 installed in the branch 28 of the gas line 14 so that when it opens, the gas goes through line 28 to position 29, where it enters the second absorber 30.
    The flow meter measures the amount of gas flow in branch 28, with the result that the input of the computational device 31 arrives from the corresponding signal r, and in the indicated device 31 with the help of a given set value fi signal 3 is generated in accordance with the following expression: dr-fe r + tr, where k is constant. The signal passes through the already open valve 24 to the flow controller 32, which opens the valve 33 in a line 34 connected in position with the upper part of the absorber 30. The net absorbent is discharged from the regenerator 11 to the som 36 via line 37 to the line 38, which branches into lines 34 and 39, with line 39 entering the absorber 1 through inlet 3. The flow controller 4, together with the corresponding control valve 41, ensures the constant flow of the absorbent. The amount of absorbent going to the second absorber 30 is controlled by the regulator 32 together with the corresponding control valve 33. The saturated absorbent leaves the absorber 30 through its lower part 42 and is pumped by the pump 25 through the discharge line 43 to the line 1 along which this absorbent falls into the regenerator 11. The level of the absorber fluid by means of the regulator 44 of the level and the corresponding control valve 45. is maintained at a certain minimum value. The method is carried out as follows. If the amount of gas flowing into the first absorber 1 decreases, the signal c will decrease, and the signal B will therefore increase until it exceeds a certain predetermined value, after which the valve 24 is opened by the switch 21. The signal 3 passes to the regulator 32 which opens the valve 33, which allows the flow of the absorbent to pass to the absorber 30 at position 35. Some time later, as a result of the action of the restraining device 23, the valve 19 opens. Part of the gas flow that is transported via line 14 in accordance with The corresponding process, for example, the Claus process, will now go through line 28 to absorber 30. In it, essentially, the weight of hydrogen sulfide is absorbed from the gas by the absorbent, and most of the carbon dioxide is removed through position 46 to line 47 and further to discharge line 7, which leads, for example, to a combustion furnace (not shown). The superhigh absorbent passes to the regenerator 11, where the gas is separated from the absorbent, with the result that the sulfur concentration in the gas stream exiting the regenerator 11 through the top 13 will increase. In this way, an equilibrium is set in which the concentration of hydrogen sulfide will be higher than if the gas was not directed to the second absorber 30. Using the sensor 18, the gas quality is maintained at a constant level, i.e. content in this gas is in certain limit ah. Instead of a relatively expensive gas quality controller, you can use a flow controller if the quality of the gas introduced through line 15 to the first absorber 1 through inlet 2 is constant. If the gas flow to the plant increases again, the signal becomes less. As soon as a certain minimum value is exceeded, switch 22 is activated. A switch to: Switch 22 is directly connected to valve 19, which is now in the closed position, with the result that valve 27 is also closed and therefore the gas flow through line 28 is stopped. This output of the switch 22 is further connected via a delay device 48 to the valve 24, which after some time after the gas flow stops, closes at the same time as the pump 25 is turned off. The valve 24 is installed with a needle valve 49, which provides a slow attenuation of the set signal, resulting in a valve 33 absorbent lines 34 also close slowly. The magnitude of the various streams acts as a function of the design capacity of the gas treatment facility supplied to this installation via line 15. Curve A (FIG. 2) describes the amount of gas that should theoretically be recycled, i.e. flow in line 28, curve B - the amount of theoretically required absorbent, which could be introduced into the absorber 1 through line 3; curve B - the amount of theoretically necessary absorbent, which could be introduced into the absorber 30 through line 34; curve G is the algebraic sum of these two absorbent flows, in other words, the flow in line 38. These curves characterize the theoretically necessary quantities that approximate to practical quantities using a regulating system. The value of the actual flows will therefore depend linearly on the specified percentage of the estimated capacity of the installation. The lines A., ,, T, A-, B and B., and G, are each valid relationship that may exist between the specified quantities. The ka of FIG. 2 shows the situation in which the valve 27 in line 28 opens as soon as the amount of gas flowing through line 15 into the installation drops to only 80% of the estimated capacity of the installation. Then the valve 27 will open so much that the quantity K of the gas will enter the absorber 30, in which the quantity K of the absorbent already circulates. Assume that the quality of the gas going on line 14, i.e. its content is at the desired level, since the composition of the gas in line 14 is characterized by signal 5 and, therefore, by signal in according to the equation, and + b. In Fig. 2, this ratio is illustrated for three S values: for the desired - line A, for the lowest allowable - line Aj, for the maximum allowable - line A.
     The situation is also shown in which the valve 27 closes, interrupting the gas flow to the second absorber, as soon as the gas supply through line 15 reaches the value at which signal 6 will change the magnitude of the signal Dy, causing the solenoid valve 19 to close and after some delay close the valve 24, as a result of which the circulation of the absorbent in the second absorber - will gradually stop.
    The theoretically required amount of absorbent can be determined using curves B and C for the first and second absorber, and the total required amount is the algebraic sum of the quantities mentioned and can be determined using curve G.
    In practice, it is preferable to keep the total amount of absorbent in the installation continuously constant. In this case, the graph is
    a constant amount of absorbent will be reflected essentially horizontal line G.
    If the second K absorber begins to circulate the amount of K absorbed, that is, then it will correspond to
     the amount initially circulated in the first absorber, so that the amount will be reduced to a value of 0, which, however, is quite sufficient.
    The proposed method allows deviations from the essence of the invention to control the amount of gas going to the second absorber, depending on the gas flow going to the first absorber, characterized by signal a, and the quality of the output gas, characterized by signal 5, according to the equation where type is constant.
    The meter 18 for the composition of the outgoing gas does not necessarily have to be a device for measuring the concentration in the outgoing gas. Providing constant. the characteristics of the gas supplied to the first absorber, meter 18 may be a flow meter.
     This meter, however, is not obsolete since measuring the amount of gas supplied to the plant with its constant quality provides ample information regarding the gas output.
    The use of the invention makes it possible to increase the content of hydrogen sulfide in the acid gas.
    t4
    权利要求:
    Claims (6)
    [1]
    1. METHOD OF GAS PREPARATION PROCESS CONTROL. IN THE PRODUCTION OF SULFUR, including absorbers and regenerators, by adjusting the absorber mode in independence from the controlled process parameter, characterized in that, in order to increase the concentration of hydrogen sulfide in acid gas by increasing the accuracy of process control, when the value of the gas flow supplied to the process is less than the first predetermined value, a part of the gas freed from the absorbent and the regenerated absorbent after the regenerator is sent to the second ber, and when exceeding values of the feed gas stream a second predetermined value and the gas supply flow of regenerated absorbent in a second absorber is stopped.
    SU „„ 1069619
    [2]
    2. The method according to π.1, characterized in that when the value of the gas flow supplied to the process is less than the first predetermined value, the regenerated absorbent is first supplied to the second absorber, and then the gas flow.
    [3]
    3. The method according to claims 1 and 2, characterized in that the supply of absorbent to the second absorber is controlled depending on the flow rate of the gas flow supplied to the second absorber.
    [4]
    4. The method according to claims 1 and 2, characterized in that when exceeding the value of the flow rate of the supplied gas of the second predetermined
    [5]
    5 values first stop the flow of gas, and then the regenerated absorbent.
    5. The method according to claims 1 to 4, about l and chaga and with the fact that the flow
    [6]
    10 of the gas in the second absorber is regulated depending on the concentration of hydrogen sulfide in the gas after the regenerator.
    ί
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3333398A|1967-08-01|Absorption flow control |
    US2614904A|1946-12-04|1952-10-21|Koppers Co Inc|Gas separation|
    BE626408A|1961-12-27|
    JPS496297B1|1969-03-15|1974-02-13|
    IT1048269B|1973-03-01|1980-11-20|Shell Int Research|PROCESS TO REDUCE THE TOTAL CONTENT OF EXHAUST GAS SULFUR OF THE CLAUS PROCESS|DE2854060C2|1978-12-14|1991-07-11|Linde Ag, 6200 Wiesbaden, De|
    US4397661A|1980-06-27|1983-08-09|Monsanto Company|Gas permeation apparatus having permeate rate controlled valving|
    US4289738A|1980-07-22|1981-09-15|The Dow Chemical Company|Process for removing H2 S from sour gases with generation of a Claus feed gas|
    GB2100471B|1981-05-28|1985-03-06|British Gas Corp|Automatic coi removal system and operation thereof|
    US5266274A|1992-10-13|1993-11-30|Tpa, Inc.|Oxygen control system for a sulfur recovery unit|
    US5556606A|1994-10-07|1996-09-17|Khanmamedov; Tofik K.|Method and apparatus for controlling the hydrogen sulfide concentration in the acid gas feedstock of a sulfur recovery unit|
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    US6506349B1|1994-11-03|2003-01-14|Tofik K. Khanmamedov|Process for removal of contaminants from a gas stream|
    US6372126B1|1999-07-19|2002-04-16|Gary R. Reeves|Chlorinator for aerobic waste treatment systems|
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    US8226893B2|2008-06-24|2012-07-24|Mclauchlan Robert A|Automated sulfur recovery loop|
    US20100219061A1|2009-03-02|2010-09-02|Saudi Arabian Oil Company|Enhancement of acid gas enrichment process|
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    JP5494754B2|2012-07-31|2014-05-21|住友金属鉱山株式会社|Hydrogen sulfide gas production plant system and method of recovering and using hydrogen sulfide gas|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL7701175A|NL7701175A|1977-02-04|1977-02-04|METHOD FOR INCREASING THE CONCENTRATION OF HYDROGEN HYDROGEN IN AN ACID GAS|
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