Process and system for treating gaseous effluents containing acidic non-condensable gases and applications, method for recovering sulfur

Abstract

The present application relates to the field of acid non-condensable gas treatment, and discloses a treatment method and treatment system for ammonia-containing acid non-condensable gas, application and a sulfur recovery method, the method comprising: (1) mixing ammonia-containing acid non-condensable gas with hydrogenation tail gas, and then sequentially performing quenching treatment and sulfur absorption treatment to obtain tail gas I and rich liquid; (2) performing high-temperature Claus reaction on the tail gas I to obtain tail gas II; (3) performing desulfurization on the tail gas II; wherein the method further comprises, before, at the same time as or after step (2), regenerating the rich liquid to obtain lean liquid and regenerated gas, and performing reflux condensation separation on the regenerated gas after cooling to obtain regenerated acid gas; the content of hydrogen sulfide in the ammonia-containing acid non-condensable gas is 0.01-5% by volume fraction. The treatment method can completely treat ammonia, hydrogen sulfide, hydrogen and other components in the ammonia-containing acid non-condensable gas, and realize ultra-low SO2 emission of tail gas.

Description

Technical Field

[0001] This invention relates to the field of acidic noncondensable gas treatment technology, specifically to a method and system for treating amino acid-containing noncondensable gas and its application, as well as a method for sulfur recovery. Background Technology

[0002] Currently, petrochemical enterprises lack comprehensive environmental protection measures for the acidic non-condensable gases generated in the black water treatment unit (hydrogen 22.63%, carbon monoxide 21.36%, carbon dioxide 44.06%, hydrogen sulfide 1.52%) and the conversion unit (hydrogen 59.94%, carbon dioxide 38.94%, hydrogen sulfide 0.05%) of POX units (coal coke to hydrogen). Emissions are mostly handled through flare incineration or on-site venting, which has a certain impact on the surrounding environment. The main method for treating lean acidic gases with H2S below 5% is direct oxidation. However, in recent years, with increasingly stringent domestic environmental protection requirements, the national standard "Integrated Emission Standard for Air Pollutants" stipulates that the first-level emission standard for H2S is 0.03 mg / m³. 3 The emission standard for newly built, expanded, or renovated facilities is 0.06 mg / m³. 3 The existing device has a concentration of 0.1 mg / m³. 3 The emission standard for newly built, expanded, or renovated facilities is 0.32 mg / m³. 3 The existing device has a concentration of 0.6 mg / m³. 3 .

[0003] The direct combustion of low-concentration acidic gases using a flare increases SO2 emissions from the plant, polluting the atmosphere. Furthermore, the reaction temperature for complete ammonia conversion exceeds 1250℃, placing higher demands on the burners and increasing the consumption of fuel gas for flare combustion, thus raising both investment and operating costs. Moreover, the acidic non-condensable gases produced by POX plants can no longer be discharged at high altitudes on-site; they must be treated. A common treatment technique involves mixing the POX acidic non-condensable gases with high-concentration acidic gases before processing them in a sulfur recovery unit.

[0004] The literature "Analysis of the sulfur recovery pathway for low-concentration acidic gas in coal gasification hydrogen production process" Guangdong Chemical Industry, 2013, 40(14):251-252. It analyzes how to send low-concentration acidic gas from the coal gasification hydrogen production process back to the sulfur recovery unit for treatment. However, in the acidic non-condensable gas of the POX unit, the hydrogen sulfide concentration is extremely low (only 1%), and the main components are N2 and CO2. The entry of inert components is not conducive to the high-temperature Claus reaction. At the same time, excessive CO2 components will promote the side reaction in the sulfur reactor, produce COS, and reduce the sulfur recovery rate.

[0005] The method of mixing low-concentration acidic gas with high-concentration acidic gas and then introducing them into the sulfur recovery unit poses a risk. The acidic non-condensable gas produced during the POX unit's production process contains a certain amount of ammonia. When the temperature is below 85℃, this ammonia readily reacts with H2S in the acidic gas to form ammonium salt crystals, causing blockages in pipelines and valves, and threatening the stable operation of the unit.

[0006] The literature "A New Approach to Hydrogen Sulfide Tail Gas Treatment in Low-Temperature Methanol Washing Process", Energy Conservation and Environmental Protection, 2003, 10: 39-40, describes a new approach to hydrogen sulfide tail gas treatment. This approach involves concentrating and purifying the tail gas from the low-temperature methanol washing process, where the hydrogen sulfide content is 20%-30% (V / V), and then using it to produce DMSO. Summary of the Invention

[0007] The purpose of this invention is to overcome the shortcomings of treating ammonia-containing lean acidic gas, which can easily cause blockage of pipelines and valves, threaten stable production of the equipment, reduce sulfur recovery rate, and cause excessive SO2 emissions in flue gas. This invention provides a method for treating ammonia-containing lean acidic gas.

[0008] As mentioned above, the current method for treating ammonia-poor acidic gas, especially when H2S content is no higher than 5%, is direct incineration. The inventors have found that this method increases environmental pressure, fuel consumption, and CO2 emissions. Alternatively, the method involves mixing the gas with high-concentration acidic gas before introducing it into a sulfur recovery unit. The inventors have found that the presence of excessive CO2 components in this method promotes side reactions in the sulfur reactor, producing COS, reducing sulfur recovery rate, and causing blockages in pipelines and valves, threatening the stable operation of the unit.

[0009] Based on the above findings, the first aspect of the present invention provides a method for treating amino acid-containing noncondensable gases, the method comprising:

[0010] (1) After mixing amino acid-containing non-condensable gas with hydrogenated tail gas, the mixture is subjected to rapid cooling and sulfur absorption treatment in sequence to obtain tail gas I and rich liquid.

[0011] (2) Tail gas I undergoes a high-temperature Claus reaction to produce tail gas II;

[0012] (3) Desulfurization is performed on exhaust gas II;

[0013] The method further includes, before, simultaneously or after step (2), regenerating the rich liquid to obtain a lean liquid and regenerated gas, and then cooling the regenerated gas and refluxing and condensing it to obtain regenerated acidic gas; the hydrogen sulfide content in the amino acid-containing non-condensable gas is 0.01-5% by volume fraction.

[0014] A second aspect of the present invention provides a system for treating amino acid-containing noncondensable gases, the system comprising:

[0015] An amino acid-containing noncondensable gas supply unit is used to supply amino acid-containing noncondensable gas into the system.

[0016] The sulfur recovery unit comprises a quench tower, an absorption tower, and a regeneration tower connected in sequence. The quench tower is used to quench the mixture of amino acid-containing non-condensable gas and hydrogenated tail gas. The absorption tower is used to absorb sulfur after quenching to obtain tail gas I and rich liquid. The regeneration tower is used to regenerate the rich liquid to obtain lean liquid and regeneration gas. A reflux tank is also connected after the regeneration tower for reflux condensation and separation of the regeneration gas to obtain regeneration acid gas.

[0017] An incinerator is used to perform a high-temperature Claus reaction on tail gas I to obtain tail gas II.

[0018] The desulfurization tower is used to desulfurize the tail gas II obtained from incineration.

[0019] The third aspect of the present invention provides the application of the above-mentioned method for treating amino acid-containing noncondensable gases in the treatment of POX-containing amino acid-containing noncondensable gases.

[0020] The fourth aspect of this invention provides a sulfur recovery method, which includes: generating sulfur from the regenerated acid gas obtained by the above method through a sulfur recovery process.

[0021] Compared with the prior art, the present invention has at least the following beneficial effects:

[0022] 1. This invention mixes amino acid-containing non-condensable gas with hydrogenation tail gas, and then performs rapid cooling and sulfur absorption treatment in sequence to obtain tail gas I and rich liquid. This avoids the risk of ammonium salt crystallization of amino acid-containing gas at low temperature, which may block pipelines and other facilities. At the same time, it reduces the ammonia consumption in the rapid cooling process itself, and avoids the disadvantage of the high temperature required for direct combustion of amino acid-containing non-condensable gas, thereby reducing fuel gas consumption and CO2 generation.

[0023] 2. In this invention, the amino acid-containing non-condensable gas is mixed with the hydrogenated tail gas and then subjected to rapid cooling and sulfur absorption treatment in sequence to obtain tail gas I and rich liquid. Tail gas I undergoes a high-temperature Claus reaction to obtain tail gas II, which reduces the H2S content in the tail gas. After the tail gas is incinerated, it is treated by a desulfurization tower to achieve ultra-low SO2 emissions from the flue gas.

[0024] 3. The processing method of the present invention reduces CO2 production and makes the combustion heat of hydrogen components in amino acid-containing noncondensable gases available for utilization.

[0025] 4. The H2S content in the acidic noncondensable gas produced by the POX unit (coal coke to hydrogen) is not higher than 5%. The treatment method of the present invention can completely treat the components such as ammonia, hydrogen sulfide and hydrogen in the acidic noncondensable gas produced by the POX unit, achieve ultra-low SO2 emissions in the tail gas, and at the same time reduce burner temperature and fuel gas consumption. Attached Figure Description

[0026] Figure 1 This is a schematic diagram of the treatment process of an amino acid-containing noncondensable gas in one embodiment of the present invention, specifically in the treatment of POX-containing amino acid-containing noncondensable gas.

[0027] Explanation of reference numerals in the attached figures

[0028] 1. Heat exchanger 2. Quenching tower

[0029] 3. Absorption tower; 4. Three-stage incinerator

[0030] 5. Superheater 6. Waste heat boiler

[0031] 7. Desulfurization tower 8. Chimney

[0032] 9. Rich liquid pump 10. Regeneration tower

[0033] 11. Reflux tank A, POX containing amino acids, non-condensable gas

[0034] B. Hydrogenation tail gas Detailed Implementation

[0035] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0036] The first aspect of this invention provides a method for treating amino acid-containing noncondensable gases, the method comprising:

[0037] (1) After mixing amino acid-containing non-condensable gas with hydrogenated tail gas, the mixture is subjected to rapid cooling and sulfur absorption treatment in sequence to obtain tail gas I and rich liquid.

[0038] (2) Tail gas I undergoes a high-temperature Claus reaction to produce tail gas II;

[0039] (3) Desulfurization is performed on exhaust gas II;

[0040] The method further includes, before, simultaneously or after step (2), regenerating the rich liquid to obtain a lean liquid and regenerated gas, and then cooling the regenerated gas and refluxing and condensing it to obtain regenerated acidic gas; the hydrogen sulfide content in the amino acid-containing non-condensable gas is 0.01-5% by volume fraction.

[0041] As mentioned earlier, existing methods for amino acid-containing noncondensable gases with a hydrogen sulfide content of less than 5% mostly employ direct oxidation. However, this method increases SO2 emissions from the plant, polluting the atmosphere. The inventors discovered that direct oxidation lowers the burner temperature of the equipment, and without additional flare-fired fuel gas, the hydrogen sulfide content after treatment is reduced. According to this invention, by mixing the amino acid-containing noncondensable gas with hydrogenated tail gas and sequentially subjecting it to quenching and sulfur absorption treatment to obtain tail gas I and rich liquid, the H2S content in tail gas I is reduced. After incineration, the tail gas is treated by a desulfurization tower, achieving ultra-low SO2 emissions from the flue gas. Furthermore, the system of this invention reduces the ammonia injection consumption of all quenching towers in the sulfur unit and avoids the high temperature required for direct combustion of amino acid-containing noncondensable gases, reducing fuel gas consumption and CO2 generation. Simultaneously, the treatment method of this invention allows the low-concentration, ammonia-containing acidic noncondensable gas to be treated without affecting the CLAUS unit reaction.

[0042] According to some preferred embodiments of the present invention, the hydrogen sulfide content in the amino acid-containing noncondensable gas is 0.05-3% by volume (e.g., 0.05%, 0.12%, 0.32%, 0.68%, 1.52%, 1.7%, 2%, 2.5%, 3%, and any combination of the above values).

[0043] According to the present invention, the temperature of the amino acid-containing noncondensable gas is not limited as long as the purpose of the present invention can be achieved. In some embodiments, the temperature of the amino acid-containing noncondensable gas is greater than or equal to 85°C, preferably 90-100°C (e.g., 90°C, 95°C, 100°C, and any combination of the above values). Using the aforementioned embodiments, the amino acid-containing noncondensable gas and the hydrogenation tail gas can be mixed better.

[0044] According to the present invention, the inlet pressure of the amino acid-containing noncondensable gas is not limited as long as the objective of the present invention can be achieved. In some embodiments, the inlet pressure of the amino acid-containing noncondensable gas is greater than 20 kPa, preferably 20-100 kPa, more preferably 20-40 kPa (e.g., 20 kPa, 25 kPa, 30 kPa, 35 kPa, 40 kPa, and any combination of the above values). Using the aforementioned embodiments not only better fixes the ammonia composition and reduces the ammonia consumption of the quench tower itself in the sulfur unit, but also allows for a better pressure of tail gas I in the subsequent high-temperature Claus reaction, which is beneficial to the high-temperature Claus reaction. According to the present invention, "inlet pressure of the amino acid-containing noncondensable gas" refers to the pressure at which the amino acid-containing noncondensable gas enters the equipment undergoing quenching treatment.

[0045] Claus tail gas produced by Claus sulfur production still contains 5%-10% unrecovered sulfur. According to the present invention, "hydrogenated tail gas" refers to Claus tail gas mixed with a certain flow rate of hydrogen and entering the bed of a hydrogenation reactor (300°C, 8kPa) containing a catalyst. Under the action of the catalyst, elemental sulfur and sulfur dioxide in Claus tail gas are reduced to hydrogen sulfide, and COS and CS2 are hydrolyzed to generate CO2 and H2S.

[0046] According to the present invention, the composition of the hydrogenation tail gas is not limited as long as the purpose of the present invention can be achieved. In some preferred embodiments, the hydrogenation tail gas includes: 0.8-5% hydrogen, 0-2% hydrogen sulfide, 60-90% nitrogen, 15-38% water, and the balance being carbon dioxide.

[0047] According to the present invention, in some embodiments, the temperature of the hydrogenation tail gas is greater than 120°C, preferably 130-170°C (e.g., 130°C, 140°C, 150°C, 160°C, 170°C, and any combination of the above values). By employing the aforementioned embodiments, the risk of ammonium salt crystallization at low temperatures, which could clog pipelines and other facilities, can be avoided. Simultaneously, the combination of quenching treatment can fix the ammonia component, reducing ammonia consumption in the quench tower of the sulfur plant and avoiding the high temperature required for direct combustion of the amino acid-containing non-condensable gas, thus reducing fuel gas consumption and CO2 generation.

[0048] According to the present invention, as long as the purpose of the present invention can be achieved, the flow rates of the amino acid-containing noncondensable gas and the hydrogenation tail gas in step (1) are not limited. In some embodiments, the flow rate of the amino acid-containing noncondensable gas is 1000-6000 Nm³. 3 / h (e.g., 1000 Nm) 3 / h, 1500Nm 3 / h, 2000Nm 3 / h, 3000Nm 3 / h, 4500Nm 3 / h, 5500Nm 3 / h, 6000Nm 3 / h, and any combination of the above values), preferably 2000-3500 Nm 3 / h; In some implementations, the flow rate of the hydrogenation tail gas is 40-50t / h.

[0049] According to some preferred embodiments of the present invention, the flow rate ratio of the amino acid-containing noncondensable gas to the hydrogenation tail gas is (45-75) Nm³. 3 / h: 1t / h (e.g., 45Nm) 3 / h: 1t / h, 50Nm 3 / h: 1t / h, 55Nm3 / h: 1t / h, 60Nm 3 / h: 1t / h, 70Nm 3 / h: 1t / h, 75Nm 3 / h: 1t / h, and any combination of the above values).

[0050] According to the present invention, in some embodiments, in step (1), the quenching conditions include: an operating pressure of 10-15 kPaG (e.g., 10 kPaG, 11 kPaG, 12 kPaG, 13 kPaG, 14 kPaG, 15 kPaG, and any combination of the above values).

[0051] According to the present invention, quenching treatment uses quenching water as a cooling medium to reduce the temperature, and can also absorb the ammonia component in amino acid-containing non-condensable gases. In some embodiments, the quenching treatment conditions include: a quenching water circulation rate greater than 150 t / h, preferably 250-350 t / h (e.g., 250 t / h, 260 t / h, 270 t / h, 290 t / h, 300 t / h, 320 t / h, 350 t / h, and any combination of the above values).

[0052] According to the present invention, in some embodiments, the quenching conditions include: a quench water temperature of 25-38°C (e.g., 25°C, 30°C, 32°C, 35°C, and any combination of the above values).

[0053] According to some embodiments of the present invention, the quenching conditions include: the pH value of the quenching water is 8-9.

[0054] According to the present invention, the aforementioned quenching conditions can better fix the ammonia components, while reducing the temperature of the gas after mixing the amino acid-containing non-condensable gas and the hydrogenated tail gas. This reduces the ammonia injection consumption of the quenching tower itself in the sulfur unit, and avoids the disadvantage of the high temperature required for the direct high-temperature Claus reaction of the amino acid-containing non-condensable gas. It also reduces fuel gas consumption and CO2 generation, and is more conducive to subsequent sulfur absorption treatment, reducing the H2S content in the tail gas.

[0055] According to the present invention, in some embodiments, in step (1), the sulfur absorption treatment conditions include: an operating pressure of 7-10 kPaG (e.g., 7 kPaG, 8 kPaG, 9 kPaG, 10 kPaG, and any combination of the above values).

[0056] According to the present invention, in some embodiments, the sulfur absorption treatment conditions include: an operating temperature of 25-35°C (e.g., 25°C, 28°C, 32°C, 34°C, 35°C, and any combination of the above values).

[0057] According to the present invention, any solution capable of absorbing hydrogen sulfide can be used for sulfur absorption treatment. In some embodiments, an aqueous solution of MDEA is used for sulfur absorption treatment.

[0058] According to some preferred embodiments of the present invention, the circulation rate of the MDEA aqueous solution is 120-140 t / h (e.g., 120 t / h, 125 t / h, 130 t / h, 135 t / h, 138 t / h, 140 t / h, and any combination of the above values).

[0059] According to some preferred embodiments of the present invention, the concentration of the MDEA aqueous solution is 30-40 wt% (e.g., 30 wt%, 35 wt%, 38 wt%, 40 wt%, and any combination of the above values).

[0060] According to the present invention, the aforementioned sulfur absorption treatment can reduce the H2S content in the exhaust gas. After the exhaust gas is incinerated, it is treated by a desulfurization tower to achieve ultra-low SO2 emissions from the flue gas, while further avoiding the influence of water vapor and CO2 on the high-temperature Claus reaction.

[0061] According to the present invention, it is understood that the high-temperature Claus reaction is carried out in an incinerator (reactor). In some embodiments, the high-temperature Claus reaction conditions include: the incinerator (reactor) burner temperature is greater than or equal to 1250°C, preferably 1250-1500°C (e.g., 1250°C, 1300°C, 1350°C, 1400°C, 1500°C, and any combination of the above values).

[0062] According to the present invention, in some embodiments, the high-temperature Claus reaction conditions include: an incineration pressure of 5-7 kPa (e.g., 5 kPa, 6 kPa, 7 kPa, and any combination of the above values).

[0063] According to the present invention, in some preferred embodiments, the incinerator uses a three-stage gas-air combustion; more preferably, the first stage gas-air combustion uses 80-90% gas equivalent combustion air, the second stage gas-air combustion uses 20-30% gas equivalent combustion air, and the third stage gas-air combustion uses 15-25% gas equivalent combustion air. The gas content in the gas-air mixture refers to the content where the gas equivalent is equal to the air equivalent.

[0064] According to the present invention, after the amino acid-containing noncondensable gas and the hydrogenated tail gas are mixed and subjected to rapid cooling treatment in sequence, and then subjected to sulfur absorption treatment under the aforementioned sulfur absorption treatment conditions, the H2S content in the tail gas can be better reduced. After the tail gas is incinerated, it is treated by a desulfurization tower to achieve ultra-low SO2 emissions from the flue gas. This allows the combustion heat value of the hydrogen components in the amino acid-containing noncondensable gas and the hydrogenated tail gas to be utilized, thereby reducing the consumption of fuel gas in the incinerator and the generation of CO2.

[0065] According to the present invention, the exhaust gas after incineration in the incinerator contains a certain amount of sulfur dioxide (18 mg / m³). A certain amount of sulfur dioxide may be generated during the high-temperature Claus reaction. In order to reduce the sulfur dioxide content, in some embodiments, the desulfurization conditions include: using a 20 wt% alkaline solution for circulating desulfurization. Preferably, the circulation rate of the alkaline solution is 300-400 t / h (e.g., 300 t / h, 320 t / h, 350 t / h, 375 t / h, 400 t / h, and any combination of the above values). Using the aforementioned embodiments, the trace amounts of sulfur dioxide in the exhaust gas obtained after rapid cooling, sulfur absorption, and incineration in the incinerator can be better removed.

[0066] According to the present invention, the pH value of the alkaline solution is not required as long as the purpose of the present invention can be achieved. In some embodiments, the pH value of the alkaline solution is 7.5-9.

[0067] According to the present invention, there is no requirement for the specific type of alkaline solution. The present invention uses NaOH aqueous solution as the alkaline solution to illustrate the preferred embodiment of the present invention, but the alkaline solution of the present invention is not limited to NaOH aqueous solution.

[0068] According to some preferred embodiments of the present invention, the desulfurization conditions include an operating pressure and temperature of 50-70°C.

[0069] According to some preferred embodiments of the present invention, the desulfurization conditions include an operating pressure of 1-3 kPa.

[0070] According to the present invention, in order to improve the recovery of high-concentration H2S acidic gas, in some embodiments, the regeneration conditions include: a bottom temperature of 115-120°C and a pressure of 65-70 kPaG in the regeneration tower; in some embodiments, the regeneration conditions include: a top temperature of 100-110°C and a pressure of 0.03-0.08 MPaG in the regeneration tower. Using the aforementioned embodiments, H2S acidic gas with a concentration of not less than 35% can be obtained, and the H2S acidic gas can be directly sent to a sulfur recovery unit to generate sulfur.

[0071] According to the present invention, while achieving the purpose of the present invention, resource utilization is further realized. In some embodiments, the method of the present invention further includes, after step (2) and before step (3), exhaust gas II is cooled and overheated and waste heat is utilized as needed.

[0072] According to the present invention, there are no restrictions on the method of cooling the regenerated gas in step (3), including but not limited to air cooling.

[0073] According to the present invention, it is understood that the method of the present invention further includes the gas after desulfurization in step (3) being directly discharged into the chimney at high altitude.

[0074] According to the present invention, in some embodiments, the method of the present invention further includes the sulfur absorption treatment step of the lean liquor obtained in step (3).

[0075] According to the present invention, as long as regenerated acidic gas can be obtained, there are no restrictions on the method of reflux condensation separation, and it will not be described in detail in the present invention.

[0076] According to the present invention, the SO2 emission of the gas obtained by the treatment method of the present invention can be controlled at 0.1 mg / m³. 3 about.

[0077] In accordance with the present invention, unless otherwise specified, all pressures referred to in the present invention are absolute pressures.

[0078] A second aspect of the present invention provides a system for treating amino acid-containing noncondensable gases, the system comprising:

[0079] An amino acid-containing noncondensable gas supply unit is used to supply amino acid-containing noncondensable gas into the system.

[0080] The sulfur recovery unit comprises a quench tower, an absorption tower, and a regeneration tower connected in sequence. The quench tower is used to quench the mixture of amino acid-containing non-condensable gas and hydrogenated tail gas. The absorption tower is used to absorb sulfur after quenching to obtain tail gas I and rich liquid. The regeneration tower is used to regenerate the rich liquid to obtain lean liquid and regeneration gas. A reflux tank is also connected after the regeneration tower for reflux condensation and separation of the regeneration gas to obtain regeneration acid gas.

[0081] An incinerator is used to perform a high-temperature Claus reaction on tail gas I to obtain tail gas II.

[0082] The desulfurization tower is used to desulfurize the tail gas II obtained from incineration.

[0083] According to the present invention, in some embodiments, a boundary valve is provided at the connection pipe between the amino acid-containing noncondensable gas supply unit and the quench tower; in order to better control the flow rate of amino acid-containing noncondensable gas supplied by the amino acid-containing noncondensable gas supply unit, in some preferred embodiments, a flow control valve is provided after the boundary valve.

[0084] According to the present invention, in some preferred embodiments, the sulfur recovery unit is equipped with an interlocking action. Using the aforementioned embodiments, when the sulfur recovery unit trips, the sulfur recovery unit interlocks, minimizing the output of the interlocking action, i.e., reducing the output of the flow control valve to its lowest value.

[0085] According to the present invention, in some embodiments, the system of the present invention further includes a heat exchanger for heat exchange of the hydrogenation tail gas to the required temperature.

[0086] According to the present invention, in some embodiments, the incinerator is a three-stage incinerator.

[0087] According to the present invention, in order to realize the resource utilization of waste heat, in some embodiments, a superheater and a waste heat boiler are connected in sequence after the incinerator.

[0088] According to the present invention, the equipment such as the three-stage incinerator, desulfurization tower, quench tower, absorption tower, regeneration tower, and reflux tank are all well known to those skilled in the art. For example, depending on the regeneration conditions, a reboiler can be installed at the bottom of the regeneration tower to heat the steam to the required temperature for regeneration. This will not be elaborated further here. At the same time, the various material inlets or outlets in the present invention can be cross-connected, and the various devices can be connected through pipelines. In some embodiments, in order to maintain the temperature of the amino acid-containing non-condensable gas at greater than or equal to 85°C, a heat tracing line can be installed on the medium pipeline as needed. In some embodiments, when the material enters the equipment, it can be introduced by a pump. For example, when the rich liquid enters the regeneration tower for regeneration, it can be introduced into the regeneration tower by a rich liquid pump. The present invention has no special requirements for this, and will not be elaborated further here.

[0089] The third aspect of the present invention provides the application of the above-mentioned method for treating amino acid-containing noncondensable gases in the treatment of POX-containing amino acid-containing noncondensable gases.

[0090] The inventors discovered that petrochemical plants currently lack comprehensive environmental protection measures for the acidic non-condensable gases (NCVs) and amino acid-containing NCVs generated in black water treatment and conversion units. These gases are often discharged via flare incineration or on-site venting, which impacts the surrounding environment. Alternatively, they are mixed with high-concentration acidic gases and introduced into the sulfur recovery unit, but this method can cause pipeline and valve blockages, threatening stable operation. This invention addresses this issue by treating NCVs from POX plants using a method that ensures sulfur recovery in the Claus process. This significantly reduces environmental pressure, fuel consumption and CO2 emissions, and the risk of ammonium salt crystallization clogging pipelines, achieving cleaner production in POX units.

[0091] According to the present invention, in some embodiments, the POX amino acid-containing noncondensable gas includes amino acid-containing noncondensable gas generated by the black water treatment unit and / or the conversion unit of the POX device.

[0092] According to some embodiments of the present invention, the non-condensable gas containing amino acids produced by the black water treatment unit of the POX device, by volume fraction, comprises: 15-25% hydrogen, 15-23% carbon monoxide, 30-50% carbon dioxide, 0.05%-2.0% hydrogen sulfide, with the balance being ammonia components and other unavoidable gaseous components.

[0093] According to the present invention, in some embodiments, the amino acid-containing non-condensable gas generated by the POX device conversion unit comprises: 48-63% hydrogen, 0-1.2% carbon monoxide, 30-50% carbon dioxide, 0.05%-0.2% hydrogen sulfide, with the balance being ammonia components and other unavoidable gaseous components.

[0094] According to the present invention, other unavoidable gases include nitrogen and water vapor, etc.

[0095] According to the present invention, when treating POX amino acid-containing non-condensable gas, the amino acid-containing non-condensable gas generated by the black water treatment unit or the conversion unit of the POX device can be treated separately, or the amino acid-containing non-condensable gas generated by the black water treatment unit and the conversion unit of the POX device can be mixed and treated together.

[0096] According to the present invention, when the amino acid-containing non-condensable gases generated by the black water treatment unit and the conversion unit of the POX device are mixed and treated together, as long as the purpose of the present invention can be achieved, the ratio of the amino acid-containing non-condensable gases generated by the black water treatment unit and the conversion unit of the POX device is not limited. In some embodiments, the volumetric flow rate of the acidic non-condensable gases generated by the black water treatment unit of the POX device is less than the volumetric flow rate of the acidic non-condensable gases generated by the conversion unit of the POX device. Preferably, the volumetric flow rate ratio of the acidic non-condensable gases generated by the black water treatment unit of the POX device to the acidic non-condensable gases generated by the conversion unit of the POX device is 1:(1.1-2).

[0097] The fourth aspect of the present invention provides a sulfur recovery method. The present invention does not provide a new sulfur recovery method. The method includes: generating sulfur from the sulfur recovery process of the regenerated acid gas obtained by the above method.

[0098] According to the present invention, there are no limitations on the sulfur recovery process as long as the purpose of the present invention can be achieved, and all sulfur recovery processes in the art are used to regenerate acidic gas to generate sulfur.

[0099] According to the present invention, in some embodiments, the sulfur recovery method includes: regenerated acid gas and air simultaneously enter a high-temperature reactor (1200-1300℃, 30-40kPa) to undergo a high-temperature Claus reaction, where 1 / 3 volume of H2S in the regenerated acid gas is burned to generate SO2, ensuring that the H2S:SO2 ratio in the process gas is 2:1. The process gas passes through a steam generator and a sulfur cooler, and is cooled to 160℃, where the sulfur in the process gas is condensed into liquid sulfur. The unreacted process gas is then fed to a reactor (first-stage reactor bed temperature 280-320℃, second-stage reactor bed temperature 200-250℃) to undergo a low-temperature Claus reaction, recovering sulfur. A sulfur condenser is installed in the middle of the process to recover sulfur step by step. The amount of oxygen is only required to ensure that all H2S is converted into elemental sulfur, and there are no special restrictions on its specific amount, which will not be elaborated upon in this invention.

[0100] According to the present invention, in some embodiments, combined with Figure 1 The present invention describes the treatment process of amino acid-containing noncondensable gases in the treatment of POX-containing amino acid-containing noncondensable gases:

[0101] POX containing amino acid noncondensable gas A is obtained by mixing the POX containing amino acid noncondensable gas produced by the black water treatment unit of the POX unit and the POX containing amino acid noncondensable gas produced by the conversion unit of the POX unit. POX containing amino acid noncondensable gas A is mixed with hydrogenated tail gas B after being heated by heat exchanger 1, and then enters the quench tower 2 of the sulfur recovery unit for quench treatment, and enters the absorption tower 3 of the sulfur recovery unit for sulfur absorption treatment to obtain tail gas I and rich liquid.

[0102] Tail gas I enters the three-stage incinerator 4 for a high-temperature Claus reaction to obtain tail gas II. Tail gas II passes through the superheater 5 and the waste heat boiler 6 in sequence before entering the desulfurization tower 7 to obtain desulfurized gas. The desulfurized gas directly enters the chimney 8 for high-altitude emission.

[0103] The rich liquid is pumped into the regeneration tower 10 of the sulfur recovery unit by the rich liquid pump 9 to regenerate into lean liquid and regeneration gas. The lean liquid obtained at the bottom of the regeneration tower 10 is returned to the absorption tower for sulfur absorption treatment. The regeneration gas obtained at the top of the regeneration tower 10 is air-cooled and then enters the reflux tank 11 for reflux condensation and separation to obtain regenerated acid gas. The regenerated acid gas is then used in the sulfur recovery process.

[0104] During the process, when the sulfur recovery unit trips, the sulfur recovery unit interlocks, causing the interlock action to minimize the output, i.e., the flow control valve output is at its lowest.

[0105] The present invention will be described in detail below through embodiments. In the following embodiments,

[0106] The flow rate of POX ammonia-containing non-condensable acidic gas entering the inlet device is used to determine the blockage status of the low-pressure gas pipeline.

[0107] The content of SO2, H2S and CO2 in the desulfurized gas was tested using an online spectrometer.

[0108] The volumetric content of H2S in regenerated acidic gas was determined by the length-to-volume method.

[0109] Example 1

[0110] like Figure 1 As shown, POX amino acid-containing noncondensable gas A is obtained by mixing POX produced by the black water treatment unit of the POX unit (by volume fraction, hydrogen 22.63%, carbon monoxide 21.36%, carbon dioxide 44.06%, hydrogen sulfide 1.52%, with the balance being ammonia and other unavoidable gas components) and POX produced by the conversion unit of the POX unit (by volume fraction, hydrogen 59.94%, carbon dioxide 38.94%, hydrogen sulfide 0.05%, with the balance being ammonia and other unavoidable gas components). The flow ratio of the amino acid-containing noncondensable gas produced by the black water treatment unit of the POX unit to that produced by the conversion unit of the POX unit is 1:1.6.

[0111] POX containing amino acids, non-condensable gas A, at a temperature of 95℃ (flow rate of 3000 Nm³) 3 The mixture of hydrogenated tail gas B (1.5% hydrogen, 0.5% hydrogen sulfide, 62% nitrogen, 36% water vapor, and a flow rate of 47t / h) at a temperature of 150℃ after being heated by heat exchanger 1 (at an inlet pressure of 30kPa) and hydrogenated tail gas B (by volume fraction, 1.5% hydrogen, 0.5% hydrogen sulfide, 62% nitrogen, and 36% water vapor, with a flow rate of 47t / h) is then introduced into the quench tower 2 of the sulfur recovery unit for quenching (quenching conditions include: operating pressure of 12kPaG, quench water circulation rate of 300t / h, and quench water temperature of 32℃), and then into the absorption tower 3 of the sulfur recovery unit for sulfur absorption (sulfur absorption conditions include: operating pressure of 8kPaG, operating temperature of 30℃, using 35wt% MDEA aqueous solution for sulfur absorption, and a circulation rate of 130t / h for MDEA aqueous solution) to obtain tail gas I and rich liquid.

[0112] The exhaust gas I enters the three-stage incinerator 4 for a high-temperature Claus reaction (the conditions for the high-temperature Claus reaction include: incinerator burner temperature of 1400℃, combustion pressure of 6kPa, 85% gas equivalent combustion air volume for the first stage gas-air combustion, 25% gas equivalent combustion air volume for the second stage gas-air combustion, and 20% gas equivalent combustion air volume for the third stage gas-air combustion) to obtain exhaust gas II. Exhaust gas II passes through the superheater 5 and the waste heat boiler 6 in sequence and then enters the desulfurization tower 7 for desulfurization (the conditions for desulfurization include: circulation of a 20wt% NaOH aqueous solution with a pH of 8.2, a circulation rate of 350t / h, an operating pressure and temperature of 60℃, and an operating pressure of 2kPa) to obtain desulfurized gas. The desulfurized gas directly enters the chimney 8 for high-altitude emission.

[0113] The rich liquor enters the regeneration tower 10 of the sulfur recovery unit via the rich liquor pump 9. The reboiler in the regeneration tower 10 heats the liquor to 118°C using steam for regeneration, yielding lean liquor and regeneration gas. The bottom temperature of the regeneration tower is 118°C and the pressure is 68 kPaG, while the top temperature is 105°C and the pressure is 0.05 MPaG. The lean liquor from the bottom of the regeneration tower 10 is returned to the absorption tower for sulfur absorption. The regeneration gas from the top of the regeneration tower 10 is air-cooled and then enters the reflux tank 11 for reflux condensation and separation to obtain regenerated acidic gas. This regenerated acidic gas is then used in the sulfur recovery process.

[0114] After one month of operation, the pressure gauge at the inlet of the POX amino acid-containing non-condensable gas device showed a pressure of <200 kPa, indicating that there was no blockage.

[0115] The SO2 emissions, H2S content, and volumetric H2S content in the regenerated acid gas after desulfurization are shown in Table 1.

[0116] Example 2

[0117] like Figure 1 As shown, POX amino acid-containing noncondensable gas A is obtained by mixing POX produced by the black water treatment unit of the POX unit (15.62% hydrogen, 22.51% carbon monoxide, 49.52% carbon dioxide, and 1.84% hydrogen sulfide, with the balance being ammonia and other unavoidable gases, based on 100% volume fraction) and POX produced by the conversion unit of the POX unit (60.35% hydrogen, 30.65% carbon dioxide, and 0.12% hydrogen sulfide, with the balance being ammonia and other unavoidable gases, based on 100% volume fraction); wherein the flow ratio of amino acid-containing noncondensable gas produced by the black water treatment unit of the POX unit to that produced by the conversion unit of the POX unit is 1:1.1;

[0118] POX containing amino acids, non-condensable gas A at 95℃ (flow rate 2100 Nm³)3 The mixture of hydrogenated tail gas B (1.5% hydrogen, 0.5% hydrogen sulfide, 62% nitrogen, 36% water vapor, and a flow rate of 40t / h) after being heated by heat exchanger 1 at a temperature of 150℃ and a flow rate of 23kPa inlet pressure) is then introduced into the quench tower 2 of the sulfur recovery unit for quenching treatment (quenching conditions include: operating pressure of 10kPaG, quench water circulation rate of 350t / h, and quench water temperature of 25℃), and then into the absorption tower 3 of the sulfur recovery unit for sulfur absorption treatment (sulfur absorption conditions include: operating pressure of 7kPaG, operating temperature of 30℃, using 40wt% MDEA aqueous solution for sulfur absorption treatment, and MDEA aqueous solution circulation rate of 140t / h) to obtain tail gas I and rich liquid.

[0119] The exhaust gas I enters the three-stage incinerator 4 for a high-temperature Claus reaction (the high-temperature Claus reaction conditions include: incinerator burner temperature of 1400℃, combustion pressure of 7kPa, the first stage gas-air combustion using 85% gas equivalent combustion air, the second stage gas-air combustion using 25% gas equivalent combustion air, and the third stage gas-air combustion using 20% ​​gas equivalent combustion air) to obtain exhaust gas II. Exhaust gas II passes through the superheater 5 and the waste heat boiler 6 in sequence and then enters the desulfurization tower 7 for desulfurization (the desulfurization conditions include: circulation of a 20wt% NaOH aqueous solution with a pH of 8.2, a circulation rate of 350t / h, an operating pressure and temperature of 60℃, and an operating pressure of 2kPa) to obtain desulfurized gas. The desulfurized gas directly enters the chimney 8 for high-altitude emission.

[0120] The rich liquor enters the regeneration tower 10 of the sulfur recovery unit via the rich liquor pump 9. The reboiler in the regeneration tower 10 heats the liquor to 118°C using steam for regeneration, yielding lean liquor and regeneration gas. The bottom temperature of the regeneration tower is 118°C and the pressure is 68 kPaG, while the top temperature is 105°C and the pressure is 0.05 MPaG. The lean liquor from the bottom of the regeneration tower 10 is returned to the absorption tower for sulfur absorption. The regeneration gas from the top of the regeneration tower 10 is air-cooled and then enters the reflux tank 11 for reflux condensation and separation to obtain regenerated acidic gas. This regenerated acidic gas is then used in the sulfur recovery process.

[0121] After one month of operation, the pressure gauge at the inlet of the POX amino acid-containing non-condensable gas device showed a pressure of <200 kPa, indicating that there was no blockage.

[0122] The SO2 emissions, H2S content, and volumetric H2S content in the regenerated acid gas after desulfurization are shown in Table 1.

[0123] Example 3

[0124] like Figure 1As shown, POX amino acid-containing noncondensable gas A is obtained by mixing POX produced by the black water treatment unit of the POX unit (containing 23.32% hydrogen, 16.20% carbon monoxide, 31.50% carbon dioxide, and 0.25% hydrogen sulfide, with the balance being ammonia and other unavoidable gases, based on a 100% volume fraction) and POX produced by the POX unit shift unit (containing 53.74% hydrogen, 48.64% carbon dioxide, and 0.05% hydrogen sulfide, with the balance being ammonia and other unavoidable gases, based on a 100% volume fraction). The flow ratio of the amino acid-containing noncondensable gas produced by the black water treatment unit of the POX unit to that produced by the POX unit shift unit is 1:2.

[0125] POX containing amino acids, non-condensable gas A at 95℃ (flow rate 3300 Nm³) 3 The mixture of hydrogenated tail gas B (1.5% hydrogen, 0.5% hydrogen sulfide, 62% nitrogen, 36% water vapor, and a flow rate of 50t / h) at a temperature of 150℃ after being heated by heat exchanger 1 (at an inlet pressure of 38kPa) and hydrogenated tail gas B (by volume fraction, 1.5% hydrogen, 0.5% hydrogen sulfide, 62% nitrogen, and 36% water vapor, with a flow rate of 50t / h) is then introduced into the quench tower 2 of the sulfur recovery unit for quenching (quenching conditions include: operating pressure of 15kPaG, quench water circulation rate of 250t / h, and quench water temperature of 36℃), and then into the absorption tower 3 of the sulfur recovery unit for sulfur absorption (sulfur absorption conditions include: operating pressure of 10kPaG, operating temperature of 30℃, using 30wt% MDEA aqueous solution for sulfur absorption, and a circulation rate of 120t / h for MDEA aqueous solution) to obtain tail gas I and rich liquid.

[0126] The exhaust gas I enters the three-stage incinerator 4 for a high-temperature Claus reaction (the conditions for the high-temperature Claus reaction include: incinerator burner temperature of 1400℃, combustion pressure of 5kPa, the first stage gas-air combustion using 85% gas equivalent combustion air, the second stage gas-air combustion using 25% gas equivalent combustion air, and the third stage gas-air combustion using 20% ​​gas equivalent combustion air) to obtain exhaust gas II. Exhaust gas II passes through the superheater 5 and the waste heat boiler 6 in sequence and then enters the desulfurization tower 7 for desulfurization (the desulfurization conditions include: circulation of a 20wt% NaOH aqueous solution with a pH of 8.2, a circulation rate of 350t / h, an operating pressure and temperature of 60℃, and an operating pressure of 2kPa) to obtain desulfurized gas. The desulfurized gas directly enters the chimney 8 for high-altitude emission.

[0127] The rich liquor enters the regeneration tower 10 of the sulfur recovery unit via the rich liquor pump 9. The reboiler in the regeneration tower 10 heats the liquor to 118°C using steam for regeneration, yielding lean liquor and regeneration gas. The bottom temperature of the regeneration tower is 118°C and the pressure is 68 kPaG, while the top temperature is 105°C and the pressure is 0.05 MPaG. The lean liquor from the bottom of the regeneration tower 10 is returned to the absorption tower for sulfur absorption. The regeneration gas from the top of the regeneration tower 10 is air-cooled and then enters the reflux tank 11 for reflux condensation and separation to obtain regenerated acidic gas. This regenerated acidic gas is then used in the sulfur recovery process.

[0128] After one month of operation, the pressure gauge at the inlet of the POX amino acid-containing non-condensable gas device showed a pressure of <200 kPa, indicating that there was no blockage.

[0129] The SO2 emissions, H2S content, and volumetric H2S content in the regenerated acid gas after desulfurization are shown in Table 1.

[0130] Example 4

[0131] The method is the same as in Example 1, except that the inlet pressure of the POX amino acid-containing noncondensable gas A is 100 kPa.

[0132] After one month of operation, the pressure gauge at the POX amino acid-containing non-condensable gas inlet device read <200 kPa, indicating no blockage.

[0133] The SO2 emissions, H2S content, and volumetric H2S content in the regenerated acid gas after desulfurization are shown in Table 1.

[0134] Example 5

[0135] The method is the same as in Example 1, except that the inlet pressure of the POX amino acid-containing noncondensable gas A is 10 kPa.

[0136] After one month of operation, the pressure gauge at the inlet of the POX amino acid-containing non-condensable gas device showed a pressure of <200 kPa, indicating that there was no blockage.

[0137] The SO2 emissions, H2S content, and H2S volume content in the desulfurized gas are shown in Table 1. The increased flow rate of the regenerated acidic gas compared to Example 1 indicates a decrease in sulfur recovery rate.

[0138] Example 6

[0139] The method is the same as in Example 1, except that the flow rate of hydrogenated tail gas B is 85 t / h; otherwise, it is the same as in Example 1.

[0140] The SO2 emissions, H2S content, and H2S volume content in the desulfurized gas are shown in Table 1. The increased flow rate of the regenerated acidic gas compared to Example 1 indicates a decrease in sulfur recovery rate.

[0141] Comparative Example 1

[0142] The method is the same as in Example 1, except that...

[0143] POX-containing amino acid noncondensable gas A and hydrogenated tail gas B are not subjected to quenching treatment, but are directly passed through the absorption tower 3 of the sulfur recovery unit for sulfur absorption treatment to obtain tail gas I and rich liquid.

[0144] Table 1 shows the SO2 emissions, H2S content, and H2S volume content in the desulfurized gas. The increased sulfur dioxide content in the flue gas indicates a decrease in sulfur recovery rate.

[0145] Comparative Example 2

[0146] The method is the same as in Example 1, except that: the hydrogenated tail gas B, after being heated by heat exchanger 1 and reaching a temperature of 150°C, sequentially enters the quench tower 2 of the sulfur recovery unit for quenching treatment, and then enters the absorption tower 3 of the sulfur recovery unit for sulfur absorption treatment to obtain tail gas I and rich liquid; tail gas I reacts with POX amino acid-containing non-condensable gas A (flow rate of 3000 Nm³) at a temperature of 95°C. 3 After being mixed (at an inlet pressure of 30 kPa), the mixture enters the three-stage incinerator 4 for a high-temperature Claus reaction.

[0147] The rest is the same as in Example 1.

[0148] Table 1 shows the SO2 emissions, H2S content, and H2S volume content in the desulfurized gas. The increased sulfur dioxide content in the flue gas indicates a decrease in sulfur recovery rate.

[0149] Comparative Example 3

[0150] The method is the same as in Example 1, except that...

[0151] Amino acid-containing noncondensable gas A, Claus tail gas (by 100% volume fraction, hydrogen 15.62%, carbon monoxide 22.51%, carbon dioxide 49.52%, hydrogen sulfide 1.84%, balance being monomers and other unavoidable components) and hydrogen (flow rate 100 Nm³) 3After mixing, the mixture enters a hydrogenation reactor bed (bed volume of 41 cubic meters, hydrogenation conditions including temperature of 300℃) containing a supported cobalt-molybdenum catalyst (active components: 2wt% cobalt oxide and 3wt% molybdenum oxide) for hydrogenation reaction to obtain hydrogenated gas. The hydrogenated gas then enters the quench tower 2 of the sulfur recovery unit for quenching treatment, and then enters the absorption tower 3 of the sulfur recovery unit for sulfur absorption treatment to obtain tail gas I and rich liquid.

[0152] The SO2 emissions, H2S content, and H2S volume content in the desulfurized gas are shown in Table 1. The increased flow rate of the regenerated acidic gas compared to Example 1 indicates a decrease in sulfur recovery rate.

[0153] Sulfur recovery example

[0154] The regenerated acid gas from Examples 1-6 and Comparative Examples 1-3 was introduced into a sulfur recovery unit for sulfur recovery. Specifically, the regenerated acid gas and air were simultaneously introduced into a high-temperature reactor (1250°C, 35 kPa) to undergo a high-temperature Claus reaction. One-third of the volume of H2S in the regenerated acid gas was burned to generate SO2, ensuring that the H2S:SO2 ratio in the process gas was 2:1. The process gas was cooled to 160°C by a steam generator and a sulfur cooler, and the sulfur in the process gas was condensed into liquid sulfur. The unreacted process gas was introduced into a reactor (bed temperature of 300°C in the first-stage reactor and 230°C in the second-stage reactor) to undergo a low-temperature Claus reaction to recover sulfur. A sulfur condenser was installed in the middle of the process to recover sulfur step by step.

[0155] The sulfur recovery rates in Examples 1-6 and Comparative Examples 1-3 are shown in Table 1.

[0156] Table 1

[0157]

[0158] As can be seen from the results in Table 1, the process described in Examples 1-6 of this invention for treating amino acid-containing non-condensable gases can better reduce the sulfur dioxide content in the desulfurized gas and increase the sulfur recovery rate.

[0159] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for treating amino acid-containing noncondensable gases, characterized in that, The method includes: (1) After the amino acid-containing non-condensable gas is mixed with the hydrogenated tail gas, it is subjected to rapid cooling and sulfur absorption treatment in sequence to obtain tail gas I and rich liquid; (2) Tail gas I undergoes a high-temperature Claus reaction to produce tail gas II; (3) The exhaust gas is desulfurized (II); The method further includes, before, simultaneously or after step (2), regenerating the rich liquid to obtain the lean liquid and regenerated gas, and then cooling the regenerated gas and refluxing and condensing it to obtain regenerated acidic gas. The hydrogen sulfide content in the amino acid-containing noncondensable gas is 0.01-5% by volume. The temperature of the amino acid-containing non-condensable gas is greater than or equal to 85°C. The temperature of the hydrogenation tail gas is greater than 120°C; Hydrogenated tail gas refers to Claus tail gas mixed with a certain flow rate of hydrogen. Under the action of a catalyst, elemental sulfur and sulfur dioxide in Claus tail gas are reduced to hydrogen sulfide, and COS and CS2 are hydrolyzed to produce CO2 and H2S.

2. The processing method according to claim 1, wherein, The hydrogen sulfide content in the amino acid-containing noncondensable gas is 0.05-3% by volume; and / or The temperature of the amino acid-containing non-condensable gas is 90-100℃; and / or The inlet pressure of the amino acid-containing noncondensable gas is greater than 20 kPa; and / or The hydrogen sulfide content in the hydrogenation tail gas is 0.05-3% by volume. and / or The temperature of the hydrogenation tail gas is 130-170℃.

3. The processing method according to claim 2, wherein, By volume fraction, the amino acid-containing noncondensable gas contains 10-60% hydrogen, 10-40% carbon monoxide, 20-50% carbon dioxide, and 0.05-3% hydrogen sulfide, with the balance being ammonia and other unavoidable gaseous components; and / or The inlet pressure of the amino acid-containing noncondensable gas is 20-40 kPa; and / or The hydrogen sulfide content in the hydrogenation tail gas is 1-1.9% by volume; and / or The hydrogenation tail gas, by volume fraction, comprises: 0.8-5% hydrogen, 0-2% hydrogen sulfide, 60-90% nitrogen, 15-38% water vapor, and the balance being carbon dioxide.

4. The processing method according to claim 1, wherein, In step (1), the flow rate of the acid gas containing ammonia is 1000-6000 Nm 3 / h; and / or In step (1), the flow rate of the hydrogenation tail gas is 40-50 t / h; And / or, In step (1), the quenching conditions include: Operating pressure is 10-15 kPaG; and / or The quench water circulation rate is greater than 150 t / h; and / or The quench water temperature is 25-38℃; and / or The pH of the quench water is 8-9; and / or In step (1), the sulfur absorption treatment conditions include: The operating pressure is 7-10 kPaG; and / or the operating temperature is 25-35℃; and / or sulfur absorption treatment is performed using an aqueous MDEA solution.

5. The processing method according to claim 4, wherein, In step (1), the flow rate of the acid gas containing ammonia is 2000-3500 Nm 3 / h; and / or The flow rate ratio of the amino acid-containing noncondensable gas to the hydrogenated tail gas is (45-75) Nm³. 3 / h: 1t / h; And / or, The quench water circulation rate is 250-350 t / h; and / or The circulation rate of the MDEA aqueous solution is 120-140 t / h. The concentration of the MDEA aqueous solution is 30-40 wt%.

6. The processing method according to claim 1, wherein, In step (2), the high-temperature Claus reaction conditions include: The high-temperature Claus reaction is carried out in an incinerator with a burner temperature greater than or equal to 1250°C; and / or The incineration pressure is 5-7 kPa; And / or, in step (3), the desulfurization conditions include: Desulfurization is carried out using 15-25wt% alkaline solution in a circulating manner; Operating pressure and temperature: 50-70℃; and / or The operating pressure is 1-3 kPa.

7. The processing method according to claim 6, wherein, The burner temperature of the incinerator is 1250-1500℃; and / or The incinerator uses a three-stage gas-air combustion process; The circulation rate of the alkaline solution is 300-400 t / h; The pH value of the alkaline solution is 7.5-9.

8. The processing method according to claim 7, wherein, The first stage of gas-air combustion uses 80-90% gas equivalent combustion air, the second stage uses 20-30% gas equivalent combustion air, and the third stage uses 15-25% gas equivalent combustion air.

9. The processing method according to claim 1, wherein, Regeneration conditions include: The bottom temperature of the regeneration tower is 115-120℃, and the pressure is 65-70 kPaG; and / or The regeneration tower top temperature is 100-110℃, and the pressure is 0.03-0.08 MPaG; and / or The method further includes, after step (2) and before step (3), cooling and superheating of exhaust gas II as needed, and waste heat utilization; and / or The method also includes the direct emission of the desulfurized gas from step (3) into the chimney at high altitude; and / or The method also includes returning the lean liquor obtained in step (3) to the sulfur absorption treatment step.

10. A system for treating amino acid-containing noncondensable gases, characterized in that, The system includes: An amino acid-containing noncondensable gas supply unit is used to supply amino acid-containing noncondensable gases into the system. The sulfur recovery unit comprises a quench tower, an absorption tower, and a regeneration tower connected in sequence. The quench tower is used to quench the mixture of amino acid-containing non-condensable gas and hydrogenated tail gas. The absorption tower is used to absorb sulfur after quenching to obtain tail gas I and rich liquid. The regeneration tower is used to regenerate the rich liquid to obtain lean liquid and regeneration gas. A reflux tank is also connected after the regeneration tower for reflux condensation and separation of the regeneration gas to obtain regeneration acid gas. An incinerator is used to perform a high-temperature Claus reaction on tail gas I to obtain tail gas II. The desulfurization tower is used to desulfurize the tail gas II obtained from incineration; Hydrogenated tail gas refers to Claus tail gas mixed with a certain flow rate of hydrogen. Under the action of a catalyst, elemental sulfur and sulfur dioxide in Claus tail gas are reduced to hydrogen sulfide, and COS and CS2 are hydrolyzed to produce CO2 and H2S.

11. The system according to claim 10, wherein, A boundary valve is provided at the connection pipe between the amino acid-containing non-condensable gas supply unit and the quench tower. The sulfur recovery unit is equipped with interlocking mechanisms; and / or The system also includes a heat exchanger for heating the hydrogenation tail gas to the required temperature; and / or The incinerator is a three-stage incinerator; and / or The incinerator is connected in sequence to a superheater and a waste heat boiler.

12. The system according to claim 11, wherein, A flow control valve is provided after the boundary valve.

13. The application of the method for treating amino acid-containing noncondensable gases according to any one of claims 1-9 in the treatment of POX-containing amino acid-containing noncondensable gases.

14. The application according to claim 13, wherein, The POX-containing amino acid-containing noncondensable gas includes amino acid-containing noncondensable gas generated by the black water treatment unit and / or the conversion unit of the POX device.

15. The application according to claim 14, wherein, By volume fraction, the non-condensable gas containing amino acids produced by the black water treatment unit of the POX device comprises: 15-25% hydrogen, 15-23% carbon monoxide, 30-50% carbon dioxide, 0.05%-2.0% hydrogen sulfide, with the balance being ammonia and other unavoidable gaseous components; and / or By volume fraction, the amino acid-containing non-condensable gas generated by the POX device conversion unit comprises: 48-63% hydrogen, 0-1.2% carbon monoxide, 30-50% carbon dioxide, 0.05%-0.2% hydrogen sulfide, with the remainder being ammonia components and other unavoidable gaseous components.

16. The application according to claim 15, wherein, The volumetric flow rate of acidic noncondensable gas generated by the black water treatment unit of the POX device is less than that generated by the conversion unit of the POX device.

17. The application according to claim 16, wherein, The volumetric flow rate ratio of the acidic noncondensable gas generated by the black water treatment unit of the POX device to that generated by the conversion unit of the POX device is 1:(1.1-2).

18. A method for sulfur recovery, characterized in that, The method includes: The sulfur is generated by the sulfur recovery process of the regenerated acid gas obtained by the method of any one of claims 1-9.

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