WO2024017202A1 - Shift condensate treatment system and process - Google Patents

Shift condensate treatment system and process Download PDF

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Publication number
WO2024017202A1
WO2024017202A1 PCT/CN2023/107744 CN2023107744W WO2024017202A1 WO 2024017202 A1 WO2024017202 A1 WO 2024017202A1 CN 2023107744 W CN2023107744 W CN 2023107744W WO 2024017202 A1 WO2024017202 A1 WO 2024017202A1
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WIPO (PCT)
Prior art keywords
ammonia
condensate
ammonia water
low
tower
Prior art date
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PCT/CN2023/107744
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French (fr)
Chinese (zh)
Inventor
柳永兵
高玉林
和露霞
张海龙
田佰起
陈志远
原仲凯
张帅帅
张艳
高宇
郭江
白延佳
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陕西未来能源化工有限公司
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Priority to AU2023296338A priority Critical patent/AU2023296338B2/en
Publication of WO2024017202A1 publication Critical patent/WO2024017202A1/en

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors

Definitions

  • the invention relates to the technical field of coal chemical industry, and in particular to a switching condensate treatment system and process.
  • Shift condensate refers to low-temperature condensate and sulfur-containing low-concentration ammonia water.
  • Low-temperature condensate refers to gasified water gas ⁇ 215°C. After partial shift reaction, it undergoes step-by-step cooling and is separated when the shift gas drops below 90°C.
  • the condensate contains ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, iron ions, etc.; sulfur-containing low-concentration ammonia water means that the low-temperature condensate is further steam-stripped through a transformation stripping tower, and the liquid phase is sent to gasification, and the gas phase After condensation and desalted water washing, the sulfur-containing low-concentration ammonia water produced is dissolved in H 2 S, CO 2 , CO, H 2 and iron ions.
  • the low-temperature condensate produced by the condensation of the water gas in the conversion system is stripped through the stripping tower.
  • the gas phase is then condensed and desalted and washed, and then the low-concentration ammonia water is sent to the boiler flue gas ammonia removal method.
  • low-concentration ammonia contains H 2 S, CO 2 , CO, H 2 and iron ions, it affects the efficiency of flue gas desulfurization and the quality of by-product ammonium sulfate, and destroys ammonia balance and water balance, causing excess ammonia and Escape; when changing the stripping tower to process low-temperature condensate at the same time, the equipment is in poor working condition, corrosion and leakage often occur, and a single tower cannot be exited during maintenance, which affects the long-term stable operation of the system.
  • the purpose of the embodiments of the present invention is to provide a switching condensate treatment system to solve the problems of water balance and ammonia balance in the boiler desulfurization system, improve the quality of ammonium sulfate, and solve the problem of switching stripping tower during maintenance.
  • the problem of being unable to exit a single tower ensures the stable operation of the system.
  • a shifting condensate treatment system including: at least two shifting stripping towers and an ammonia recovery device; the inlets of the two shifting stripping towers are respectively connected to shifting low-temperature condensate pipelines, and the outlets are sulfur-containing low-concentration ammonia water pipelines.
  • Each of the converted low-temperature condensate pipelines is provided with a first pipeline connected to the inlet of the ammonia recovery device, and a second pipeline is provided in the sulfur-containing low-concentration ammonia water pipeline connected to the inlet of the ammonia recovery device.
  • the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline, and the sulfur-containing low-concentration ammonia water pipeline is used to connect to the boiler ammonia desulfurization equipment.
  • an ammonia water tower is installed on the sulfur-containing low-concentration ammonia water pipeline, there are three shifting stripping towers, and the outlets of the three shifting stripping towers are all connected to the ammonia water towers.
  • the ammonia recovery device includes a stripping tower, and the steam There is a switching condensate inlet in the middle of the stripping tower, and the switching condensate inlet corresponds to multiple switching condensate pipes. There is an acid gas vent pipe at the top of the stripping tower, and a purified water discharge pipe at the bottom.
  • the ammonia recovery device further includes a three-stage partial condenser, and the outlet pipe in the middle of the stripping tower is connected to the three-stage partial condenser.
  • the ammonia recovery device further includes a raw water tank, and the bottom of the third-stage decondenser is connected to the raw water tank.
  • the ammonia recovery device further includes a refining tower.
  • the upper part of the three-stage decondenser is connected to a refining tower.
  • the refining tower is divided into two sections. At least 95% of carbon dioxide and hydrogen sulfide are stored in the lower section. Removal, the solution is circulated and absorbed; the upper section uses fresh low-temperature concentrated ammonia water to deeply remove the remaining carbon dioxide and hydrogen sulfide.
  • the ammonia recovery device further includes an ammonia water preparation device.
  • the leading pipe at the top of the refining tower is connected to the ammonia water preparation device.
  • the ammonia water preparation device is used to make ammonia water of different concentrations.
  • Embodiments of the present invention also provide a method for treating shift condensate, which includes: converting the shift low-temperature condensate into sulfur-containing low-concentration ammonia water through a shift stripping tower, and the sulfur-containing low-concentration ammonia water is used for ammonia desulfurization, wherein the shift stripping step There are at least two towers; according to the operating conditions, part or all of the low-temperature condensate is selected to enter the ammonia recovery unit without changing the stripping tower and then used for ammonia desulfurization after purification; according to the operating conditions, part or all of the sulfur-containing low-concentration ammonia water is selected to enter The ammonia recovery device is purified and then used for ammonia desulfurization.
  • the purification of the ammonia recovery device includes: changing the condensate flow into the stripping tower, extracting ammonia-rich gas with part of the acid gas removed from the middle of the stripping tower, and entering The three-stage partial condenser further separates the acidic gas in the third-stage partial condenser, and then the crude ammonia gas is obtained at the top, which enters the refining tower, where the acidic gas is deeply removed.
  • the refined ammonia gas in the refining tower is sent to the ammonia water making device, and the ammonia water prepared in the ammonia water making device is sent to the boiler ammonia desulfurization or ammonia water sales. .
  • the present invention uses a shifting stripper stripping process to process the shifted condensate.
  • the low-temperature condensate pipelines are more than the corresponding shift stripper pipelines, and the corresponding ammonia recovery process pipelines are added. Multiple shifted low-temperature condensate pipelines are mixed to ammonia
  • the recovery process stripping tower treatment reduces the processing capacity of the changing stripping tower.
  • the low-temperature condensate can be processed through the ammonia recovery unit or other changing stripping towers, solving the problem of a single changing stripping tower.
  • the problem that one set of changing stripping towers cannot be exited makes the operation of three sets of parallel changing condensate systems more flexible.
  • Transformation and heat recovery eliminate the fluctuations caused by shutdowns in the system.
  • the sulfur-containing low-concentration ammonia water treated by shift stripping is mixed with the low-temperature condensate and sent to the ammonia recovery device for treatment.
  • high-purity ammonia is extracted and sent to the boiler for ammonia desulfurization, which solves the problem of water balance and ammonia balance in the boiler desulfurization system and improves the efficiency of ammonium sulfate.
  • the quality ensures the continuous and stable operation of the conversion and heat recovery system and boiler desulfurization system.
  • the present invention multiple sets of transformations are realized to freely distribute the low-temperature condensate according to the operating conditions of the condensate stripping tower.
  • the ammonia recovery device realizes the transformation of the transformation condensate by optimizing the combination of low-temperature condensate and sulfur-containing dilute ammonia water.
  • Liquid purification treatment produces high-purity gas ammonia and ammonia water of different concentrations, which solves the problem of water balance and ammonia balance in the boiler desulfurization system and greatly improves the efficiency of the boiler desulfurization system.
  • the shift condensate treatment process and the ammonia recovery process of the present invention cooperate with each other to meet the shift condensate treatment requirements in the three systems, that is, the flexible operation of the shift condensate treatment capacity and exit, and the shift condensate becomes waste after purification treatment
  • the diversification and multiple needs of ammonia products meet the urgency and practicality of industrial production.
  • Figure 1 is a schematic diagram of the switching condensate treatment process according to the embodiment of the present invention.
  • Figure 2 is a schematic diagram of the ammonia recovery process according to the embodiment of the present invention.
  • f1 the first valve; f2, the second valve; f3, the third valve; f4, the first delivery valve; f5, the second delivery valve; f6, the third delivery valve; f7, the first ammonia Recovery valve; f8, the second ammonia recovery valve; f9, the first desulfurization valve; f10, the second desulfurization valve; 1. Change to the first stripper; 2. Change to the second stripper; 3. Change to the third stripper; 4. Ammonia water tower; 5. Raw water tank; 6. Stripping tower; 7. Three-stage decondenser; 8. Refining tower; 9. Ammonia water preparation device;
  • each part is exaggerated to show the location of each part, and the schematic diagram is for illustrative purposes only.
  • shifted condensate can be a fixed connection, a detachable connection, or an integral body; it can be a mechanical connection, It can be a direct connection, or it can be an indirect connection through an intermediary. It can be an internal connection between two elements, or an interactive relationship between two elements.
  • shifted condensate In the field of chemical industry, shifted low-temperature condensate and sulfur-containing low-concentration ammonia are collectively referred to as shifted condensate.
  • low-concentration ammonia contains H 2 S, CO 2 , CO, H 2 and iron ions, etc., which affects the efficiency of flue gas desulfurization and the quality of by-product ammonium sulfate, and destroys ammonia balance and water balance, causing Ammonia excess and escape; when changing the stripping tower to process low-temperature condensate at the same time, maintenance cannot allow a single tower to exit, which affects the long-term stable operation of the system.
  • the present invention proposes a switching condensate treatment system.
  • one embodiment of the present invention describes a shifting condensate treatment system, which includes: at least two shifting stripping towers and an ammonia recovery device; the inlets of the two shifting stripping towers are respectively connected to the shifting low temperature
  • the outlet of the condensate pipeline is a sulfur-containing low-concentration ammonia water pipeline.
  • a first pipeline is provided in the two conversion low-temperature condensate pipelines and is connected to the inlet of the ammonia recovery device.
  • the second pipeline is connected to the inlet of the ammonia recovery device, and the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline.
  • the sulfur-containing low-concentration ammonia water pipeline is used to connect to the boiler. Ammonia desulfurization equipment.
  • the shift stripper stripping process is used to process the shifted condensate.
  • the low-temperature condensate pipelines are more than the corresponding shift stripper pipelines.
  • Corresponding ammonia recovery process pipelines are added, and the multiple shifted low-temperature condensate pipelines are mixed to the ammonia recovery process for stripping. tower treatment, reducing the processing capacity of the shift stripping tower.
  • the low-temperature condensate can be processed through the ammonia recovery unit or other shift stripping towers, solving the problem of a single set of shift stripping towers. The problem that the tower cannot exit allows greater flexibility in the operation of the three parallel conversion condensate systems.
  • the sulfur-containing low-concentration ammonia water treated by shift stripping is mixed with low-temperature condensate and sent to the ammonia recovery device for processing. After processing, high-purity ammonia is extracted and sent to the boiler for ammonia desulfurization to maintain the continuous and stable operation of the shift system and boiler desulfurization system.
  • the number of low-temperature condensate conversion processes is 1.5 times the stripping process.
  • There are 2 sets of stripping treatment processes described in this embodiment one set of stripping towers for changing one, two, and three, and one stripping tower for ammonia recovery, corresponding to 3 sets of changing low-temperature condensate processes ( That is, transformation I, transformation II, transformation III in Figure 1); or each set of transformation stripping towers handles low-temperature condensate and reduces the load to 60%, or a single set of transformation stripping tower system exits.
  • the three sets of changing low-temperature condensates correspond to the three sets of changing stripping tower processing operations, the first valve f1, the second valve f2, and the third valve f3
  • Fully open operation by adding three sets of changing low-temperature condensate in the processing pipeline, can enter the ammonia recovery device, or by adjusting the opening of the first valve f1, the second valve f2, the third valve f3, and the first ammonia recovery valve f7 To adjust the operation or withdrawal of three sets of conversion stripping towers under different loads;
  • the sulfur-containing low-concentration ammonia water after the low-temperature condensate is processed by the shift stripper corresponds to the desulfurization operation of the boiler ammonia valve, and the first desulfurization valve f9 is fully open.
  • the second ammonia recovery valve f8 Through the added processing pipeline and the second ammonia recovery valve f8, it can enter the ammonia recovery device for processing.
  • the refined ammonia water can enter the boiler ammonia desulfurization operation through the added pipeline and the second desulfurization valve f10; it can also pass through the second ammonia recovery valve f8.
  • the first desulfurization valve f9 adjusts the ammonia recovery device to operate under different loads.
  • the improved process pipeline of three sets of conversion condensate pipelines means that the three sets of conversion system low-temperature condensation pipelines are respectively connected to an outgoing condensate pipeline in front of the first valve f1, the second valve f2, and the third valve f3, and the three pipelines are connected.
  • the pipeline in front of the first desulfurization valve f9 is connected to an ammonia recovery and treatment pipeline.
  • the ammonia recovery and treatment of the transfer condensate is refined into concentrated ammonia water and connected to the pipeline after the first desulfurization valve f9.
  • the ammonia recovery device includes a stripping tower 6 for processing shifted condensate.
  • a stripping tower 6 for processing shifted condensate.
  • the liquid phase inlet of the stripping tower 6 also includes a raw water tank 5 for optimal combination of the converted condensate; there is an acid gas vent pipe at the top of the stripping tower 6; and a purified water discharge pipe at the bottom.
  • a pipeline is drawn from the middle part of the stripping tower 6, and the middle part of the stripping tower 6 is connected to the partial condenser 7 for transporting rich ammonia gas to the partial condenser 7.
  • the upper part of the three-stage decondenser 7 is connected to the refining tower 8 for transporting crude ammonia gas to the refining tower 8 .
  • Decondenser 7 and fine The production tower 8 is used to further remove acid gases such as H 2 S and CO 2 .
  • Pipes are drawn from the top of the refining tower 8, which are respectively connected to the boiler desulfurization device and the ammonia water preparation device 9; the ammonia water preparation device 9 is made into ammonia water of different concentrations, and is connected to the boiler desulfurization device or the ammonia water for external sale.
  • the shift condensate (low-temperature condensate and sulfur-containing low-concentration ammonia water) enters from the middle of the stripping tower 6 after an optimized combination.
  • the shift condensate is first The hydrogen sulfide and carbon dioxide in the condensate are stripped from the top of the stripping tower 6.
  • the temperature of the stripping tower 6 is changed by the bottom steam, the different temperatures of the condensate after heat exchange into the tower, and the cold feed at the top of the tower.
  • Tower 6 forms a temperature gradient from top to bottom.
  • the temperature is controlled at 150-155°C to extract ammonia in a side line.
  • a temperature-changing and pressure-changing three-stage decondenser 7 is used to obtain purer ammonia gas. , and then further remove acidic gases such as H 2 S and CO 2 through the refining tower 8 to prepare high-purity ammonia, which is sent to the user or made into ammonia water of different concentrations and then sent to the user.
  • each set of modified condensate corresponds to a different treatment process
  • the treatment load in the improved first stripper 1, second stripper 2, and third stripper 3 is reduced, and the operating conditions and operations are also relatively optimized. , reduce steam consumption, and the rest is processed through the ammonia recovery unit.
  • the operating load of the three sets of switching stripping towers and the operating load of the ammonia recovery unit can be flexibly adjusted according to operational needs.
  • the processing capacity of the switching stripping tower is reduced and system corrosion is reduced; on the other hand, the converted condensate treated by the ammonia recovery device can achieve ammonia separation from acidic gases, making the ammonia product purer, producing high-purity gas ammonia and ammonia water of different concentrations, solving the problems of water balance and ammonia balance in the boiler desulfurization system. It also greatly improves the quality of ammonium sulfate, and part of the gas ammonia produced is used for boiler desulfurization and denitrification.
  • ammonia gas enriched in the middle of stripping tower 6 Due to the presence of carbon dioxide, ammonia and water vapor, the ammonia gas enriched in the middle of stripping tower 6 Now, if ammonia gas is obtained through one-time cooling, ammonium salt crystals will be generated, which will not only affect the recovery rate of ammonia, but also block equipment and pipelines. Therefore, the method of gradually lowering the temperature and pressure is used to separate ammonia and carbon dioxide, that is, the three-stage decondenser 7 is used for separation.
  • the bottom of the third-stage decondenser 7 is connected to the raw water tank 5 for reprocessing.
  • the refining tower 8 is divided into two sections. More than 95% of the carbon dioxide and hydrogen sulfide are removed in the lower section, and the solution is circulated Absorption; the upper section uses fresh low-temperature concentrated ammonia water to deeply remove remaining carbon dioxide and hydrogen sulfide.
  • the gas phase outlet at the upper part of the refining tower 8 is used to connect users.
  • the refining tower 8 is connected to an ammonia water preparation device 9 to prepare ammonia water of different concentrations, which can be desulfurized or sold by the user's boiler ammonia method, depending on the process requirements or user needs.
  • the outlet pipe in the middle of the stripping tower is connected to the partial condenser, and the partial condenser is connected to the refining tower.
  • the refining tower is desulfurized and decarbonized again to produce high-purity gas ammonia.
  • the gas ammonia is fed into the flue gas SCR for denitrification, and into the ammonia water extractor all the way, and is recycled.
  • the concentrated ammonia water is used for ammonia desulfurization all the way, and is fed into the ammonia water storage tank all the way to realize the delivery of ammonia water of different concentrations.
  • This embodiment provides a method for treating shift condensate, which includes: converting the shift low-temperature condensate into sulfur-containing low-concentration ammonia water through a shift stripping tower, and the sulfur-containing low-concentration ammonia water is used for ammonia desulfurization, wherein the shift stripping tower at least There are two; according to the operating conditions, part or all of the low-temperature condensate is selected to enter the ammonia recovery unit without changing the stripping tower and then used for ammonia desulfurization after purification; according to the operating conditions, part or all of the sulfur-containing low-concentration ammonia water is selected to enter the ammonia recovery The device is purified and then used for ammonia desulfurization.
  • liquid ammonia is 3,465 yuan/ton
  • the annual purchase cost of liquid ammonia is reduced by 22.6472 million yuan, deducting
  • the operating cost will be reduced by 4.5189 million yuan, and it is expected to generate benefits of 18.1283 million yuan per year.
  • the unit price increases by 40 yuan/ton. Based on the average output of 60 tons/day, the improvement in product quality increases product benefits by 792,000 yuan/year; the total benefit generated by the two is 18.9203 million yuan/year.
  • switching low-temperature condensation can only be processed through respective switching stripping towers.
  • the sulfur-containing low-concentration ammonia water is sent to the boiler for ammonia desulfurization.
  • the condensate stripping tower has a higher operating load and greater corrosion, resulting in Sulfur-containing low-concentration ammonia water is high in acid gas components and metal ions and other impurities, which seriously affects the water balance desulfurization effect of the desulfurization system. It is difficult to achieve the ammonia balance of the system, resulting in secondary pollution of ammonia escape and waste of resources. By-products such as ammonium sulfate are of poor quality. , affecting the stable operation of the boiler desulfurization system.
  • three sets of transformations are realized to freely distribute low-temperature condensate according to the operating conditions of the condensate stripping tower, which reduces the processing capacity of the transformation condensate stripping tower and solves the problem that a single set of transformation stripping tower cannot exit.
  • Realize the flexible operation of the switching condensate system saving 100,000 yuan/time in start-up and shutdown costs.
  • the ammonia recovery device realizes the purification treatment of the switching condensate through the optimized combination of low-temperature condensate and sulfur-containing dilute ammonia water, and produces high-purity gas ammonia and ammonia water of different concentrations, solving the water balance and ammonia balance of the boiler desulfurization system.

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Abstract

The present invention relates to the technical field of the coal chemical industry, and specifically to a shift condensate treatment system and process. The shift condensate treatment system comprises at least two shift stripping towers and an ammonia recovery device, wherein inlets of the two shift stripping towers are respectively connected to shift low-temperature condensate pipes, and outlets of same are connected to sulfur-containing low-concentration ammonia water pipes; first pipes are respectively arranged on the two shift low-temperature condensate pipes and are connected to an inlet of the ammonia recovery device; second pipes are arranged on the sulfur-containing low-concentration ammonia water pipes and are connected to the inlet of the ammonia recovery device; an outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipes by means of third pipes; and the sulfur-containing low-concentration ammonia water pipes are configured to connect to a boiler ammonia desulfurization apparatus. The system solves the problems of water balance and ammonia balance of a boiler desulfurization system, thus improving the quality of ammonium sulfate; and the system solves the problem of it not being possible for a single tower to be out of service during maintenance of shift stripping towers, thus ensuring stable operation of the system.

Description

一种变换冷凝液处理系统及工艺A switching condensate treatment system and process
本发明要求于2022年7月18日提交中国专利局、申请号为202210842707.1、发明名称为“一种变换冷凝液处理系统及工艺”的中国专利申请的优先权，其全部内容通过引用结合在本发明中。This invention claims the priority of the Chinese patent application submitted to the China Patent Office on July 18, 2022, with the application number 202210842707.1 and the invention title "A switching condensate treatment system and process", the entire content of which is incorporated herein by reference. Inventing.
技术领域Technical field
本发明涉及煤化工技术领域，尤其涉及一种变换冷凝液处理系统及工艺。The invention relates to the technical field of coal chemical industry, and in particular to a switching condensate treatment system and process.
背景技术Background technique
公开该背景技术部分的信息仅仅旨在增加对本发明的总体背景的理解，而不必然被视为承认或以任何形式暗示该信息构成已经成为本领域一般技术人员所公知的现有技术。The information in this Background section is disclosed solely for the purpose of increasing understanding of the general background of the invention and is not necessarily considered to be an admission or in any way implying that the information constitutes prior art that is already known to a person of ordinary skill in the art.
变换冷凝液是指低温冷凝液和含硫低浓氨水，低温冷凝液是指气化来的水煤气～215℃，通过部分变换反应后，经过逐级冷却，变换气降至90℃以下时分离掉的冷凝液，冷凝液中含有氨、氢气、一氧化碳、二氧化碳、硫化氢及铁离子等；含硫低浓氨水是指将低温冷凝液进一步经变换汽提塔蒸汽汽提，液相送气化，气相经冷凝和脱盐水洗涤，所产生的含硫低浓度氨水，该氨水中溶有H2S、CO2、CO、H2及铁离子等。Shift condensate refers to low-temperature condensate and sulfur-containing low-concentration ammonia water. Low-temperature condensate refers to gasified water gas ~215°C. After partial shift reaction, it undergoes step-by-step cooling and is separated when the shift gas drops below 90°C. The condensate contains ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, iron ions, etc.; sulfur-containing low-concentration ammonia water means that the low-temperature condensate is further steam-stripped through a transformation stripping tower, and the liquid phase is sent to gasification, and the gas phase After condensation and desalted water washing, the sulfur-containing low-concentration ammonia water produced is dissolved in H 2 S, CO 2 , CO, H 2 and iron ions.
变换系统水煤气经冷凝产生的低温冷凝液通过汽提塔汽提，气相再经冷凝和脱盐水洗涤处理后将低浓度的氨水送至锅炉烟气氨法脱 硫系统，由于低浓度的氨水含有H2S、CO2、CO、H2及铁离子等，影响烟气脱硫的效率和副产品硫铵的质量，并且破坏氨平衡和水平衡，造成氨过剩和逃逸；同时变换汽提塔处理低温冷凝液时，设备工况较差，常有腐蚀泄漏现象，维护保养时无法单塔退出，影响系统长周期稳定运行的问题。The low-temperature condensate produced by the condensation of the water gas in the conversion system is stripped through the stripping tower. The gas phase is then condensed and desalted and washed, and then the low-concentration ammonia water is sent to the boiler flue gas ammonia removal method. In the sulfur system, because low-concentration ammonia contains H 2 S, CO 2 , CO, H 2 and iron ions, it affects the efficiency of flue gas desulfurization and the quality of by-product ammonium sulfate, and destroys ammonia balance and water balance, causing excess ammonia and Escape; when changing the stripping tower to process low-temperature condensate at the same time, the equipment is in poor working condition, corrosion and leakage often occur, and a single tower cannot be exited during maintenance, which affects the long-term stable operation of the system.
发明内容Contents of the invention
针对现有技术存在的不足，本发明实施例的目的是提供一种变换冷凝液处理系统，解决锅炉脱硫系统水平衡和氨平衡问题，提高硫酸铵的品质；解决变换汽提塔在维护保养时无法单塔退出的问题，保证了系统的稳定运行。In view of the shortcomings of the existing technology, the purpose of the embodiments of the present invention is to provide a switching condensate treatment system to solve the problems of water balance and ammonia balance in the boiler desulfurization system, improve the quality of ammonium sulfate, and solve the problem of switching stripping tower during maintenance. The problem of being unable to exit a single tower ensures the stable operation of the system.
为了实现上述目的，本发明实施例提供了如下技术方案：In order to achieve the above objects, embodiments of the present invention provide the following technical solutions:
一种变换冷凝液处理系统，包括：至少两个变换汽提塔和氨回收装置；两个变换汽提塔入口分别连接变换低温冷凝液管路，出口为含硫低浓氨水管路，在两个所述变换低温冷凝液管路分别设置第一管路连接到所述氨回收装置入口，在所述含硫低浓氨水管路设置第二管路连接到所述氨回收装置入口，所述氨回收装置出口通过第三管路连接到含硫低浓氨水管路上，所述含硫低浓氨水管路用于连接到锅炉氨法脱硫设备。A shifting condensate treatment system, including: at least two shifting stripping towers and an ammonia recovery device; the inlets of the two shifting stripping towers are respectively connected to shifting low-temperature condensate pipelines, and the outlets are sulfur-containing low-concentration ammonia water pipelines. Each of the converted low-temperature condensate pipelines is provided with a first pipeline connected to the inlet of the ammonia recovery device, and a second pipeline is provided in the sulfur-containing low-concentration ammonia water pipeline connected to the inlet of the ammonia recovery device. The outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline, and the sulfur-containing low-concentration ammonia water pipeline is used to connect to the boiler ammonia desulfurization equipment.
在另一优选的实施方式中，所述含硫低浓氨水管路上设置氨水塔，所述变换汽提塔为三个，三个所述变换汽提塔出口均连接到所述氨水塔。In another preferred embodiment, an ammonia water tower is installed on the sulfur-containing low-concentration ammonia water pipeline, there are three shifting stripping towers, and the outlets of the three shifting stripping towers are all connected to the ammonia water towers.
在另一优选的实施方式中，所述氨回收装置包括汽提塔，所述汽 提塔中部具有变换冷凝液入口，所述变换冷凝液入口对应多路变换冷凝液管道，所述汽提塔顶部有酸性气放空管道，底部有净化水排放管道。In another preferred embodiment, the ammonia recovery device includes a stripping tower, and the steam There is a switching condensate inlet in the middle of the stripping tower, and the switching condensate inlet corresponds to multiple switching condensate pipes. There is an acid gas vent pipe at the top of the stripping tower, and a purified water discharge pipe at the bottom.
在另一优选的实施方式中，所述氨回收装置还包括三级分凝器，所述汽提塔中部引出管道连接所述三级分凝器。In another preferred embodiment, the ammonia recovery device further includes a three-stage partial condenser, and the outlet pipe in the middle of the stripping tower is connected to the three-stage partial condenser.
在另一优选的实施方式中，所述氨回收装置还包括原料水罐，所述三级分凝器底部连接所述原料水罐。In another preferred embodiment, the ammonia recovery device further includes a raw water tank, and the bottom of the third-stage decondenser is connected to the raw water tank.
在另一优选的实施方式中，所述氨回收装置还包括精制塔，所述三级分凝器上部连接精制塔，所述精制塔分为两段，至少95％的二氧化碳及硫化氢在下段脱除，溶液循环吸收；上段使用新鲜低温浓氨水对剩余二氧化碳及硫化氢进行深度脱除。In another preferred embodiment, the ammonia recovery device further includes a refining tower. The upper part of the three-stage decondenser is connected to a refining tower. The refining tower is divided into two sections. At least 95% of carbon dioxide and hydrogen sulfide are stored in the lower section. removal, the solution is circulated and absorbed; the upper section uses fresh low-temperature concentrated ammonia water to deeply remove the remaining carbon dioxide and hydrogen sulfide.
在另一优选的实施方式中，所述氨回收装置还包括制取氨水器，所述精制塔顶部引出管道连接制取氨水器，所述制取氨水器用于制成不同浓氨水。In another preferred embodiment, the ammonia recovery device further includes an ammonia water preparation device. The leading pipe at the top of the refining tower is connected to the ammonia water preparation device. The ammonia water preparation device is used to make ammonia water of different concentrations.
本发明实施例还提供了一种变换冷凝液处理方法，包括：变换低温冷凝液经变换汽提塔转换为含硫低浓氨水，含硫低浓氨水用于氨法脱硫，其中，变换汽提塔至少具有两个；根据运行状况，选择部分或全部低温冷凝液不经变换汽提塔而进入氨回收装置净化后用于氨法脱硫；根据运行状况，选择部分或全部含硫低浓氨水进入氨回收装置净化后再用于氨法脱硫。Embodiments of the present invention also provide a method for treating shift condensate, which includes: converting the shift low-temperature condensate into sulfur-containing low-concentration ammonia water through a shift stripping tower, and the sulfur-containing low-concentration ammonia water is used for ammonia desulfurization, wherein the shift stripping step There are at least two towers; according to the operating conditions, part or all of the low-temperature condensate is selected to enter the ammonia recovery unit without changing the stripping tower and then used for ammonia desulfurization after purification; according to the operating conditions, part or all of the sulfur-containing low-concentration ammonia water is selected to enter The ammonia recovery device is purified and then used for ammonia desulfurization.
在另一优选的实施方式中，氨回收装置净化包括：变换冷凝液经过进入汽提塔中，从汽提塔中部抽出去除部分酸性气的富氨气，进入 三级分凝器，在三级分凝器中进一步与酸性气进行分离后顶部得粗氨气，进入精制塔，在精制塔中对酸性气进行深度脱除。In another preferred embodiment, the purification of the ammonia recovery device includes: changing the condensate flow into the stripping tower, extracting ammonia-rich gas with part of the acid gas removed from the middle of the stripping tower, and entering The three-stage partial condenser further separates the acidic gas in the third-stage partial condenser, and then the crude ammonia gas is obtained at the top, which enters the refining tower, where the acidic gas is deeply removed.
在另一优选的实施方式中，将精制塔中精制后的氨气送入制取氨水器中，制取氨水器配制的氨水送至锅炉氨法脱硫或氨水销售。。In another preferred embodiment, the refined ammonia gas in the refining tower is sent to the ammonia water making device, and the ammonia water prepared in the ammonia water making device is sent to the boiler ammonia desulfurization or ammonia water sales. .
本发明实施例中提供的一个或多个技术方案，至少具有如下技术效果或优点：One or more technical solutions provided in the embodiments of the present invention have at least the following technical effects or advantages:
1、本发明采用变换汽提塔汽提工艺处理变换冷凝液，所述低温冷凝液管道多于对应的变换汽提塔管道，增加对应氨回收工艺管道，多条变换低温冷凝液管线混合至氨回收工艺汽提塔处理，减少了变换汽提塔的处理量，当一套变换汽提塔出现问题停工时，低温冷凝液可以通过氨回收装置处理或其它变换汽提塔来处理，解决了单套变换汽提塔无法退出的问题，使得并行的三套变换冷凝液系统运行有了更大的灵活性，在运行方式上有了多种选择，降低不必要的开、停车费用，避免了因变换及热回收开停车对系统造成的波动。经变换汽提处理的含硫低浓氨水与低温冷凝液混合至氨回收装置处理，处理后提取高纯度氨送锅炉氨法脱硫，解决了锅炉脱硫系统水平衡和氨平衡问题，提高了硫酸铵的品质，保证了变换及热回收系统和锅炉脱硫系统的持续稳定运行。1. The present invention uses a shifting stripper stripping process to process the shifted condensate. The low-temperature condensate pipelines are more than the corresponding shift stripper pipelines, and the corresponding ammonia recovery process pipelines are added. Multiple shifted low-temperature condensate pipelines are mixed to ammonia The recovery process stripping tower treatment reduces the processing capacity of the changing stripping tower. When a set of changing stripping towers has problems and shuts down, the low-temperature condensate can be processed through the ammonia recovery unit or other changing stripping towers, solving the problem of a single changing stripping tower. The problem that one set of changing stripping towers cannot be exited makes the operation of three sets of parallel changing condensate systems more flexible. It has a variety of choices in operation modes, reduces unnecessary startup and parking costs, and avoids unnecessary costs. Transformation and heat recovery eliminate the fluctuations caused by shutdowns in the system. The sulfur-containing low-concentration ammonia water treated by shift stripping is mixed with the low-temperature condensate and sent to the ammonia recovery device for treatment. After treatment, high-purity ammonia is extracted and sent to the boiler for ammonia desulfurization, which solves the problem of water balance and ammonia balance in the boiler desulfurization system and improves the efficiency of ammonium sulfate. The quality ensures the continuous and stable operation of the conversion and heat recovery system and boiler desulfurization system.
2、本发明中实现了多套变换根据冷凝液汽提塔的运行状况对低温冷凝液的自由分配，同时氨回收装置通过对低温冷凝液和含硫稀氨水的优化组合，实现了将变换凝液净化处理，产出高纯度的气氨和不同浓度的氨水，解决了锅炉脱硫系统水平衡和氨平衡问题，也大大提 高硫酸铵的品质，产出的部分气氨供锅炉脱销使用，降低了锅炉外购液氨的成本，同时过剩的氨制成氨水外卖，大大降低了生产成本，满足了系统稳定运行。经过测试，产生的效益为1892.03万元/年。2. In the present invention, multiple sets of transformations are realized to freely distribute the low-temperature condensate according to the operating conditions of the condensate stripping tower. At the same time, the ammonia recovery device realizes the transformation of the transformation condensate by optimizing the combination of low-temperature condensate and sulfur-containing dilute ammonia water. Liquid purification treatment produces high-purity gas ammonia and ammonia water of different concentrations, which solves the problem of water balance and ammonia balance in the boiler desulfurization system and greatly improves the efficiency of the boiler desulfurization system. Due to the high quality of ammonium sulfate, part of the gas ammonia produced is used by the boiler when it is out of stock, which reduces the cost of purchasing liquid ammonia for the boiler. At the same time, the excess ammonia is made into ammonia water for take-out, which greatly reduces the production cost and satisfies the stable operation of the system. After testing, the benefits generated were 18.9203 million yuan/year.
3、本发明的变换冷凝液处理工艺与氨回收工艺相互配合，满足了三套系统中变换冷凝液处理需求，即灵活操作变换汽提塔处理量及退出，且变换冷凝液净化处理后变废为宝，氨产品的多样化和多需求满足工业化生产的迫切性，实用性。3. The shift condensate treatment process and the ammonia recovery process of the present invention cooperate with each other to meet the shift condensate treatment requirements in the three systems, that is, the flexible operation of the shift condensate treatment capacity and exit, and the shift condensate becomes waste after purification treatment For treasure, the diversification and multiple needs of ammonia products meet the urgency and practicality of industrial production.
附图说明Description of drawings
构成本发明的一部分的说明书附图用来提供对本发明的进一步理解，本发明的示意性实施例及其说明用于解释本发明，并不构成对本发明的不当限定。The description and drawings that constitute a part of the present invention are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention.
图1是本发明实施例的变换冷凝液处理工艺示意图；Figure 1 is a schematic diagram of the switching condensate treatment process according to the embodiment of the present invention;
图2是本发明实施例的氨回收工艺示意图；Figure 2 is a schematic diagram of the ammonia recovery process according to the embodiment of the present invention;
图中：f1、第一阀门；f2、第二阀门；f3、第三阀门；f4、第一外送阀门；f5、第二外送阀门；f6、第三外送阀门；f7、第一氨回收阀门；f8、第二氨回收阀门；f9、第一脱硫阀门；f10、第二脱硫阀门；1、变一汽提塔；2、变二汽提塔；3、变三汽提塔；4、氨水塔；5、原料水罐；6、汽提塔；7、三级分凝器；8、精制塔；9、制取氨水器；In the picture: f1, the first valve; f2, the second valve; f3, the third valve; f4, the first delivery valve; f5, the second delivery valve; f6, the third delivery valve; f7, the first ammonia Recovery valve; f8, the second ammonia recovery valve; f9, the first desulfurization valve; f10, the second desulfurization valve; 1. Change to the first stripper; 2. Change to the second stripper; 3. Change to the third stripper; 4. Ammonia water tower; 5. Raw water tank; 6. Stripping tower; 7. Three-stage decondenser; 8. Refining tower; 9. Ammonia water preparation device;
为显示各部位位置而夸大了互相间间距或尺寸，示意图仅作示意使用。The spacing or size of each part is exaggerated to show the location of each part, and the schematic diagram is for illustrative purposes only.
具体实施方式Detailed ways
为了方便叙述，本发明中如果出现“上”、“下”、“左”“右”字样， 仅表示与附图本身的上、下、左、右方向一致，并不对结构起限定作用，仅仅是为了便于描述本发明和简化描述，而不是指示或暗示所指的设备或元件必须具有特定的方位，以特定的方位构造和操作，因此不能理解为对本发明的限制。本发明中的术语“安装”、“相连”、“连接”、“固定”等术语应作广义理解，例如，可以是固定连接，也可以是可拆卸连接，或为一体；可以是机械连接，可以是直接连接，也可以是通过中间媒介间接相连，可以是两个元件内部连接，或者两个元件的相互作用关系，对于本领域的普通技术人员而言，可以根据具体情况理解术语在本发明的具体含义。在化工领域内，变换低温冷凝液和含硫低浓氨水统称变换冷凝液。For convenience of description, if the words "upper", "lower", "left" and "right" appear in the present invention, It only shows that the upper, lower, left and right directions are consistent with the drawings themselves, and does not limit the structure. It is only for the convenience of describing the present invention and simplifying the description, and does not indicate or imply that the equipment or components referred to must have specific characteristics. Orientation, is constructed and operates in a specific orientation and therefore should not be construed as limiting the invention. The terms "installation", "connection", "connection", "fixing" and other terms in the present invention should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral body; it can be a mechanical connection, It can be a direct connection, or it can be an indirect connection through an intermediary. It can be an internal connection between two elements, or an interactive relationship between two elements. For those of ordinary skill in the art, the terminology used in the present invention can be understood according to the specific circumstances. specific meaning. In the field of chemical industry, shifted low-temperature condensate and sulfur-containing low-concentration ammonia are collectively referred to as shifted condensate.
正如背景技术所介绍的，低浓度的氨水含有H2S、CO2、CO、H2及铁离子等，影响烟气脱硫的效率和副产品硫铵的质量，并且破坏氨平衡和水平衡，造成氨过剩和逃逸；同时变换汽提塔处理低温冷凝液时，维护保养无法单塔退出，影响系统长周期稳定运行的问题。为了解决如上的技术问题，本发明提出了一种变换冷凝液处理系统。As introduced in the background technology, low-concentration ammonia contains H 2 S, CO 2 , CO, H 2 and iron ions, etc., which affects the efficiency of flue gas desulfurization and the quality of by-product ammonium sulfate, and destroys ammonia balance and water balance, causing Ammonia excess and escape; when changing the stripping tower to process low-temperature condensate at the same time, maintenance cannot allow a single tower to exit, which affects the long-term stable operation of the system. In order to solve the above technical problems, the present invention proposes a switching condensate treatment system.
如图1-图2所示，本发明一实施例中记载了一种变换冷凝液处理系统，包括：至少两个变换汽提塔和氨回收装置；两个变换汽提塔入口分别连接变换低温冷凝液管路，出口为含硫低浓氨水管路，在两个所述变换低温冷凝液管路分别设置第一管路连接到所述氨回收装置入口，在所述含硫低浓氨水管路设置第二管路连接到所述氨回收装置入口，所述氨回收装置出口通过第三管路连接到含硫低浓氨水管路上，所述含硫低浓氨水管路用于连接到锅炉氨法脱硫设备。 As shown in Figures 1 and 2, one embodiment of the present invention describes a shifting condensate treatment system, which includes: at least two shifting stripping towers and an ammonia recovery device; the inlets of the two shifting stripping towers are respectively connected to the shifting low temperature The outlet of the condensate pipeline is a sulfur-containing low-concentration ammonia water pipeline. A first pipeline is provided in the two conversion low-temperature condensate pipelines and is connected to the inlet of the ammonia recovery device. In the sulfur-containing low-concentration ammonia water pipe The second pipeline is connected to the inlet of the ammonia recovery device, and the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline. The sulfur-containing low-concentration ammonia water pipeline is used to connect to the boiler. Ammonia desulfurization equipment.
采用变换汽提塔汽提工艺处理变换冷凝液，所述低温冷凝液管道多于对应的变换汽提塔管道，增加对应氨回收工艺管道，多条变换低温冷凝液管线混合至氨回收工艺汽提塔处理，减少了变换汽提塔的处理量，当一套变换汽提塔出现问题停工时，低温冷凝液可以通过氨回收装置处理或其它变换汽提塔来处理，解决了单套变换汽提塔无法退出的问题，使得并行的三套变换冷凝液系统运行有了更大的灵活性，在运行方式上有了多种选择，降低不必要的开、停车费用，避免了因变换及热回收开停车对系统造成的波动。经变换汽提处理的含硫低浓氨水与低温冷凝液混合至氨回收装置处理，处理后提取高纯度氨送锅炉氨法脱硫，保持变换系统和锅炉脱硫系统的持续稳定运行。The shift stripper stripping process is used to process the shifted condensate. The low-temperature condensate pipelines are more than the corresponding shift stripper pipelines. Corresponding ammonia recovery process pipelines are added, and the multiple shifted low-temperature condensate pipelines are mixed to the ammonia recovery process for stripping. tower treatment, reducing the processing capacity of the shift stripping tower. When a set of shift stripping towers has problems and shuts down, the low-temperature condensate can be processed through the ammonia recovery unit or other shift stripping towers, solving the problem of a single set of shift stripping towers. The problem that the tower cannot exit allows greater flexibility in the operation of the three parallel conversion condensate systems. It has multiple choices in operation modes, reduces unnecessary startup and parking costs, and avoids the need for conversion and heat recovery. Fluctuations caused by driving and stopping on the system. The sulfur-containing low-concentration ammonia water treated by shift stripping is mixed with low-temperature condensate and sent to the ammonia recovery device for processing. After processing, high-purity ammonia is extracted and sent to the boiler for ammonia desulfurization to maintain the continuous and stable operation of the shift system and boiler desulfurization system.
在原有工艺的基础上，将变换多条低温冷凝液管道与汽提工艺入口连通，并在每条管道上增加阀门，同时每条管道混合与新增处理工艺连接(氨回收装置)；低温冷凝液处理后得含硫低浓氨水在原有工艺基础上，将含硫低浓氨水管线与新增处理工艺连接(氨回收装置)，并在管道上增加阀门，随时切换处理方式。On the basis of the original process, multiple low-temperature condensate pipelines will be connected to the inlet of the stripping process, and valves will be added to each pipeline. At the same time, each pipeline will be mixed and connected to the new treatment process (ammonia recovery unit); low-temperature condensation After liquid treatment, sulfur-containing low-concentration ammonia water is obtained. Based on the original process, the sulfur-containing low-concentration ammonia water pipeline is connected to the new treatment process (ammonia recovery device), and valves are added to the pipeline to switch the treatment method at any time.
变换低温冷凝液工艺数目为汽提处理工艺1.5倍。本实施例中所述汽提处理工艺为2套(其中变一、变二、变三汽提塔为一套，氨回收中汽提塔为一套)，对应3套变换低温冷凝液工艺(即图1中变换I、变换II、变换III)；或，每套变换汽提塔处理低温冷凝液降低负荷至60％，或则单套变换汽提塔系统退出。The number of low-temperature condensate conversion processes is 1.5 times the stripping process. There are 2 sets of stripping treatment processes described in this embodiment (one set of stripping towers for changing one, two, and three, and one stripping tower for ammonia recovery), corresponding to 3 sets of changing low-temperature condensate processes ( That is, transformation I, transformation II, transformation III in Figure 1); or each set of transformation stripping towers handles low-temperature condensate and reduces the load to 60%, or a single set of transformation stripping tower system exits.
如图1所示，以三套变换冷凝液为例，三套变换低温冷凝液对应三套变换汽提塔处理运行，第一阀门f1、第二阀门f2、第三阀门f3 全开运行，通过增加处理管道三套变换的低温冷凝液，可以进入氨回收装置，也可以通过调整第一阀门f1、第二阀门f2、第三阀门f3、第一氨回收阀门f7的开度来调整三套变换汽提塔不同负荷下运行或退出运行；As shown in Figure 1, taking three sets of changing condensates as an example, the three sets of changing low-temperature condensates correspond to the three sets of changing stripping tower processing operations, the first valve f1, the second valve f2, and the third valve f3 Fully open operation, by adding three sets of changing low-temperature condensate in the processing pipeline, can enter the ammonia recovery device, or by adjusting the opening of the first valve f1, the second valve f2, the third valve f3, and the first ammonia recovery valve f7 To adjust the operation or withdrawal of three sets of conversion stripping towers under different loads;
现有技术中低温冷凝液经变换汽提塔处理后的含硫低浓氨水对应锅炉氨阀脱硫运行，第一脱硫阀门f9全开运行。通过增加的处理管道、第二氨回收阀门f8，可以进入氨回收装置处理，精制后的氨水通过增加的管道、第二脱硫阀门f10，进入锅炉氨法脱硫运行；也可以通过第二氨回收阀门f8、第一脱硫阀门f9调整氨回收装置在不同负荷下运行。In the prior art, the sulfur-containing low-concentration ammonia water after the low-temperature condensate is processed by the shift stripper corresponds to the desulfurization operation of the boiler ammonia valve, and the first desulfurization valve f9 is fully open. Through the added processing pipeline and the second ammonia recovery valve f8, it can enter the ammonia recovery device for processing. The refined ammonia water can enter the boiler ammonia desulfurization operation through the added pipeline and the second desulfurization valve f10; it can also pass through the second ammonia recovery valve f8. The first desulfurization valve f9 adjusts the ammonia recovery device to operate under different loads.
进一步，三套变换冷凝液管线改良的工艺管线是指，三套变换系统低温冷凝管线分别在第一阀门f1、第二阀门f2、第三阀门f3前连接一条外送冷凝液管线，三条管线连接在一条外送变换冷凝液总管上；在第一脱硫阀门f9前管线连接一条至氨回收处理管线，氨回收处理完的变换冷凝液，精制成浓氨水连接至第一脱硫阀门f9后管线。Furthermore, the improved process pipeline of three sets of conversion condensate pipelines means that the three sets of conversion system low-temperature condensation pipelines are respectively connected to an outgoing condensate pipeline in front of the first valve f1, the second valve f2, and the third valve f3, and the three pipelines are connected. On an external transfer condensate main pipe; the pipeline in front of the first desulfurization valve f9 is connected to an ammonia recovery and treatment pipeline. The ammonia recovery and treatment of the transfer condensate is refined into concentrated ammonia water and connected to the pipeline after the first desulfurization valve f9.
如图2所示，氨回收装置包括汽提塔6，用于处理变换冷凝液，所述汽提塔6中部有变换冷凝液入口，所述变换冷凝液入口对应多路变换冷凝液管道；所述汽提塔6液相入口处还包括原料水罐5，用于对变换冷凝液的优化组合；所述汽提塔6顶部有酸性气放空管道；底部有净化水排放管道。所述汽提塔6中部引出管道，所述汽提塔6中部连接分凝器7，用于向分凝器7中输送富的氨气。所述三级分凝器7上部连接精制塔8，用于向精制塔8中输送粗氨气。分凝器7和精 制塔8均用于进一步脱除H2S、CO2等酸性气体。所述精制塔8顶部引出管道，分别连接锅炉脱销装置、制取氨水器9；制取氨水器9制成不同浓氨水，连接锅炉脱硫装置或氨水外售。As shown in Figure 2, the ammonia recovery device includes a stripping tower 6 for processing shifted condensate. There is a shifted condensate inlet in the middle of the stripping tower 6, and the shifted condensate inlet corresponds to a multi-channel shifted condensate pipeline; so The liquid phase inlet of the stripping tower 6 also includes a raw water tank 5 for optimal combination of the converted condensate; there is an acid gas vent pipe at the top of the stripping tower 6; and a purified water discharge pipe at the bottom. A pipeline is drawn from the middle part of the stripping tower 6, and the middle part of the stripping tower 6 is connected to the partial condenser 7 for transporting rich ammonia gas to the partial condenser 7. The upper part of the three-stage decondenser 7 is connected to the refining tower 8 for transporting crude ammonia gas to the refining tower 8 . Decondenser 7 and fine The production tower 8 is used to further remove acid gases such as H 2 S and CO 2 . Pipes are drawn from the top of the refining tower 8, which are respectively connected to the boiler desulfurization device and the ammonia water preparation device 9; the ammonia water preparation device 9 is made into ammonia water of different concentrations, and is connected to the boiler desulfurization device or the ammonia water for external sale.
应当理解的是，所述变换冷凝液(低温冷凝液和含硫低浓氨水)优化组合后从汽提塔6中部进入，根据硫化氢与二氧化碳的相对挥发度高于氨的特性，先将变换冷凝液的硫化氢与二氧化碳从汽提塔6塔顶汽提出去，汽提塔6温度通过底部蒸汽、进塔的变换冷凝液换热后的不同温度及塔顶的冷进料，使汽提塔6形成从上到下形成温度梯度，在汽提塔的中部控制温度在150～155℃对氨进行侧线抽出，使用变温、变压的三级分凝器7的方法获得较纯的氨气，再经过精制塔8进一步脱除H2S、CO2等酸性气体，制取高纯度氨气，送至用户或制成不同浓度氨水，再送至用户。It should be understood that the shift condensate (low-temperature condensate and sulfur-containing low-concentration ammonia water) enters from the middle of the stripping tower 6 after an optimized combination. According to the characteristics that the relative volatility of hydrogen sulfide and carbon dioxide is higher than that of ammonia, the shift condensate is first The hydrogen sulfide and carbon dioxide in the condensate are stripped from the top of the stripping tower 6. The temperature of the stripping tower 6 is changed by the bottom steam, the different temperatures of the condensate after heat exchange into the tower, and the cold feed at the top of the tower. Tower 6 forms a temperature gradient from top to bottom. In the middle of the stripping tower, the temperature is controlled at 150-155°C to extract ammonia in a side line. A temperature-changing and pressure-changing three-stage decondenser 7 is used to obtain purer ammonia gas. , and then further remove acidic gases such as H 2 S and CO 2 through the refining tower 8 to prepare high-purity ammonia, which is sent to the user or made into ammonia water of different concentrations and then sent to the user.
由于改良后每套变换冷凝液对应不同的处理工艺，因此改良后的变一汽提塔1、变二汽提塔2、变三汽提塔3中处理负荷降低，操作工况和运行也相对优化，降低蒸汽用量，其他通过氨回收装置处理，根据运行需要可以灵活调整三套变换汽提塔的运行负荷及氨回收装置运行负荷，一方面减少变换汽提塔处理量减少系统腐蚀；另一方面，氨回收装置处理后的变换冷凝液，能够实现酸性气和的氨分离，氨产品更纯，产出高纯度的气氨和不同浓度的氨水，解决了锅炉脱硫系统水平衡和氨平衡问题，也大大提高硫酸铵的品质，产出的部分气氨供锅炉脱销使用，很好的满足锅炉脱硫脱硝的使用。Since each set of modified condensate corresponds to a different treatment process, the treatment load in the improved first stripper 1, second stripper 2, and third stripper 3 is reduced, and the operating conditions and operations are also relatively optimized. , reduce steam consumption, and the rest is processed through the ammonia recovery unit. The operating load of the three sets of switching stripping towers and the operating load of the ammonia recovery unit can be flexibly adjusted according to operational needs. On the one hand, the processing capacity of the switching stripping tower is reduced and system corrosion is reduced; on the other hand, , the converted condensate treated by the ammonia recovery device can achieve ammonia separation from acidic gases, making the ammonia product purer, producing high-purity gas ammonia and ammonia water of different concentrations, solving the problems of water balance and ammonia balance in the boiler desulfurization system. It also greatly improves the quality of ammonium sulfate, and part of the gas ammonia produced is used for boiler desulfurization and denitrification.
由于汽提塔6中部富集的氨气由于二氧化碳、氨及水蒸气的存 在，若一次性降温获得氨气则会生成铵盐结晶，既影响氨的回收率，同时生成的铵盐结晶堵塞设备和管道。因此采用逐次降低温度和压力的办法进行氨与二氧化碳的分离，即三级分凝器7进行分离。Due to the presence of carbon dioxide, ammonia and water vapor, the ammonia gas enriched in the middle of stripping tower 6 Now, if ammonia gas is obtained through one-time cooling, ammonium salt crystals will be generated, which will not only affect the recovery rate of ammonia, but also block equipment and pipelines. Therefore, the method of gradually lowering the temperature and pressure is used to separate ammonia and carbon dioxide, that is, the three-stage decondenser 7 is used for separation.
所述三级分凝器7底部连接原料水罐5，重新处理。The bottom of the third-stage decondenser 7 is connected to the raw water tank 5 for reprocessing.
由于三级分凝器7上部的粗氨气还有部分酸性气的存在，需要进一步进行脱硫脱碳，精制塔8分为两段，95％以上的二氧化碳及硫化氢在下段脱除，溶液循环吸收；上段使用新鲜低温浓氨水对剩余二氧化碳及硫化氢进行深度脱除。Since the crude ammonia gas in the upper part of the third-stage partial condenser 7 still contains some acid gas, further desulfurization and decarbonization are required. The refining tower 8 is divided into two sections. More than 95% of the carbon dioxide and hydrogen sulfide are removed in the lower section, and the solution is circulated Absorption; the upper section uses fresh low-temperature concentrated ammonia water to deeply remove remaining carbon dioxide and hydrogen sulfide.
优选的，所述精制塔8上部气相出口，用于连接用户。Preferably, the gas phase outlet at the upper part of the refining tower 8 is used to connect users.
所述精制塔8连接制取氨水器9，制取不同浓度氨水，用户锅炉氨法脱硫或销售，具体视工艺要求或用户需求而定。汽提塔中部引出管道连接分凝器，分凝器连接精制塔，精制塔再次脱硫脱碳产出高纯度气氨，气氨一路进烟气SCR脱硝、一路进制取氨水器，循环制取浓氨水一路用于氨法脱硫、一路进氨水储罐，实现外卖不同浓度的氨水。The refining tower 8 is connected to an ammonia water preparation device 9 to prepare ammonia water of different concentrations, which can be desulfurized or sold by the user's boiler ammonia method, depending on the process requirements or user needs. The outlet pipe in the middle of the stripping tower is connected to the partial condenser, and the partial condenser is connected to the refining tower. The refining tower is desulfurized and decarbonized again to produce high-purity gas ammonia. The gas ammonia is fed into the flue gas SCR for denitrification, and into the ammonia water extractor all the way, and is recycled. The concentrated ammonia water is used for ammonia desulfurization all the way, and is fed into the ammonia water storage tank all the way to realize the delivery of ammonia water of different concentrations.
本实施例提供了一种变换冷凝液处理方法，包括：变换低温冷凝液经变换汽提塔转换为含硫低浓氨水，含硫低浓氨水用于氨法脱硫，其中，变换汽提塔至少具有两个；根据运行状况，选择部分或全部低温冷凝液不经变换汽提塔而进入氨回收装置净化后用于氨法脱硫；根据运行状况，选择部分或全部含硫低浓氨水进入氨回收装置净化后再用于氨法脱硫。This embodiment provides a method for treating shift condensate, which includes: converting the shift low-temperature condensate into sulfur-containing low-concentration ammonia water through a shift stripping tower, and the sulfur-containing low-concentration ammonia water is used for ammonia desulfurization, wherein the shift stripping tower at least There are two; according to the operating conditions, part or all of the low-temperature condensate is selected to enter the ammonia recovery unit without changing the stripping tower and then used for ammonia desulfurization after purification; according to the operating conditions, part or all of the sulfur-containing low-concentration ammonia water is selected to enter the ammonia recovery The device is purified and then used for ammonia desulfurization.
经过测试，氨回收装置外送纯氨量为823kg/h，则每年减少采购 液氨6584吨，扣除锅炉运行尾气指标波动每年补充48吨，每年需采购液氨6536吨；按照同统一计算标准即液氨按照3465元/吨，则每年减少采购液氨费用2264.72万元，扣减运行费用451.89万元，预计每年可产生效益1812.83万元。硫铵产品质量提升后单价提高40元/吨，按照平均产量60吨/天，产品质量提升增加产品效益79.2万元/年；二者合计产生的效益为1892.03万元/年。After testing, the amount of pure ammonia delivered by the ammonia recovery device is 823kg/h, so annual purchases will be reduced. Liquid ammonia is 6,584 tons. After deducting the fluctuation of boiler operation exhaust gas index, 48 tons are replenished every year, and 6,536 tons of liquid ammonia need to be purchased every year. According to the same unified calculation standard, that is, liquid ammonia is 3,465 yuan/ton, then the annual purchase cost of liquid ammonia is reduced by 22.6472 million yuan, deducting The operating cost will be reduced by 4.5189 million yuan, and it is expected to generate benefits of 18.1283 million yuan per year. After the quality improvement of ammonium sulfate products, the unit price increases by 40 yuan/ton. Based on the average output of 60 tons/day, the improvement in product quality increases product benefits by 792,000 yuan/year; the total benefit generated by the two is 18.9203 million yuan/year.
现有技术中变换低温冷凝只能通过各自的变换汽提塔处理，含硫低浓氨水送至锅炉氨法脱硫，受流程及工艺影响冷凝液汽提塔运行负荷较高腐蚀较大，产生的含硫低浓度氨水中酸性气体成分及金属离子等杂质高，严重影响脱硫系统的水平衡脱硫效果，系统的氨平衡难以实现，形成氨逃逸二次污染和资源浪费，硫酸铵等副产品品质较差，影响锅炉脱硫系统的稳定运行。而本发明中实现了三套变换根据冷凝液汽提塔的运行状况对低温冷凝液的自由分配，减少了变换冷凝液汽提塔处理量，解决了单套变换汽提塔无法退出的问题，实现变换冷凝液系统灵活运行，节约开停车费用10万/次。同时氨回收装置通过对低温冷凝液和含硫稀氨水的优化组合，实现了将变换凝液净化处理，产出高纯度的气氨和不同浓度的氨水，解决了锅炉脱硫系统水平衡和氨平衡问题，也大大提高硫酸铵的品质，产出的部分气氨供锅炉脱销使用，降低了锅炉外购液氨的成本，同时过剩的氨制成氨水外卖，大大降低了生产成本，满足了系统稳定运行。In the existing technology, switching low-temperature condensation can only be processed through respective switching stripping towers. The sulfur-containing low-concentration ammonia water is sent to the boiler for ammonia desulfurization. Affected by the process and technology, the condensate stripping tower has a higher operating load and greater corrosion, resulting in Sulfur-containing low-concentration ammonia water is high in acid gas components and metal ions and other impurities, which seriously affects the water balance desulfurization effect of the desulfurization system. It is difficult to achieve the ammonia balance of the system, resulting in secondary pollution of ammonia escape and waste of resources. By-products such as ammonium sulfate are of poor quality. , affecting the stable operation of the boiler desulfurization system. In the present invention, three sets of transformations are realized to freely distribute low-temperature condensate according to the operating conditions of the condensate stripping tower, which reduces the processing capacity of the transformation condensate stripping tower and solves the problem that a single set of transformation stripping tower cannot exit. Realize the flexible operation of the switching condensate system, saving 100,000 yuan/time in start-up and shutdown costs. At the same time, the ammonia recovery device realizes the purification treatment of the switching condensate through the optimized combination of low-temperature condensate and sulfur-containing dilute ammonia water, and produces high-purity gas ammonia and ammonia water of different concentrations, solving the water balance and ammonia balance of the boiler desulfurization system. problem, it also greatly improves the quality of ammonium sulfate. Part of the gas ammonia produced is used by the boiler when it is out of stock, which reduces the cost of purchasing liquid ammonia for the boiler. At the same time, the excess ammonia is made into ammonia water for take-out, which greatly reduces the production cost and satisfies the system stability. run.
无论采用何种方式改进变换冷凝液处理管道及工艺，只要最终能够实现三套变换冷凝液可以对应不同的处理方式，实现灵活转换，即 可实现相同的效果。No matter what method is used to improve the switching condensate treatment pipeline and process, as long as it can finally achieve three sets of switching condensate that can correspond to different treatment methods and achieve flexible conversion, that is The same effect can be achieved.
上述虽然结合附图对本发明的具体实施方式进行了描述，但并非对本发明保护范围的限制，所属领域技术人员应该明白，在本发明的技术方案的基础上，本领域技术人员不需要付出创造性劳动即可做出的各种修改或变形仍在本发明的保护范围以内。 Although the specific embodiments of the present invention have been described above in conjunction with the accompanying drawings, they do not limit the scope of the present invention. Those skilled in the art should understand that based on the technical solutions of the present invention, those skilled in the art do not need to perform creative work. Various modifications or variations that can be made are still within the protection scope of the present invention.

Claims (7)

  1. 一种变换冷凝液处理系统，其特征在于，包括：至少两个变换汽提塔和氨回收装置；A shift condensate treatment system, characterized by including: at least two shift stripping towers and an ammonia recovery device;
    变换汽提塔入口连接变换低温冷凝液管路，出口为含硫低浓氨水管路，在所述变换低温冷凝液管路设置第一管路连接到所述氨回收装置入口，在所述含硫低浓氨水管路设置第二管路连接到所述氨回收装置入口，所述氨回收装置出口通过第三管路连接到含硫低浓氨水管路上，所述含硫低浓氨水管路用于连接到锅炉氨法脱硫设备；The inlet of the conversion stripping tower is connected to a conversion low-temperature condensate pipeline, and the outlet is a sulfur-containing low-concentration ammonia water pipeline. A first pipeline is provided in the conversion low-temperature condensate pipeline and is connected to the inlet of the ammonia recovery device. The sulfur-containing low-concentration ammonia water pipeline is provided with a second pipeline connected to the inlet of the ammonia recovery device, and the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline. The sulfur-containing low-concentration ammonia water pipeline is For connection to boiler ammonia desulfurization equipment;
    所述含硫低浓氨水管路上设置氨水塔，所述氨回收装置包括汽提塔，所述汽提塔中部具有变换冷凝液入口，所述变换冷凝液入口对应多路变换低温冷凝液管路，所述汽提塔顶部有酸性气放空管道，底部有净化水排放管道，所述氨回收装置还包括三级分凝器，所述汽提塔中部引出管道连接所述三级分凝器，所述氨回收装置还包括精制塔，所述三级分凝器上部连接精制塔。An ammonia water tower is installed on the sulfur-containing low-concentration ammonia water pipeline. The ammonia recovery device includes a stripping tower. The stripping tower has a switching condensate inlet in the middle. The switching condensate inlet corresponds to a multi-channel switching low-temperature condensate pipeline. , there is an acid gas vent pipe at the top of the stripping tower, and a purified water discharge pipe at the bottom. The ammonia recovery device also includes a three-stage partial condenser, and the outlet pipe in the middle of the stripping tower is connected to the third-stage partial condenser. The ammonia recovery device also includes a refining tower, and the upper part of the three-stage decondenser is connected to the refining tower.
  2. 如权利要求1所述的变换冷凝液处理系统，其特征在于，所述变换汽提塔为三个，三个所述变换汽提塔出口均连接到所述氨水塔。The shifting condensate treatment system of claim 1, wherein there are three shifting stripping towers, and the outlets of the three shifting stripping towers are all connected to the ammonia water tower.
  3. 如权利要求1所述的变换冷凝液处理系统，其特征在于，所述氨回收装置还包括原料水罐，所述三级分凝器底部连接所述原料水罐。The switching condensate treatment system of claim 1, wherein the ammonia recovery device further includes a raw water tank, and the bottom of the third-stage decondenser is connected to the raw water tank.
  4. 如权利要求1所述的变换冷凝液处理系统，其特征在于，所述精制塔分为两段，至少95％的二氧化碳及硫化氢在下段脱除，溶液循环吸收；上段使用新鲜低温浓氨水对剩余二氧化碳及硫化氢进行深度脱除。 The switching condensate treatment system according to claim 1, characterized in that the refining tower is divided into two sections, at least 95% of carbon dioxide and hydrogen sulfide are removed in the lower section, and the solution is recycled and absorbed; the upper section uses fresh low-temperature concentrated ammonia water to The remaining carbon dioxide and hydrogen sulfide are deeply removed.
  5. 如权利要求4所述的变换冷凝液处理系统，其特征在于，所述氨回收装置还包括制取氨水器，所述精制塔顶部引出管道连接制取氨水器，所述制取氨水器用于制成不同浓氨水。The switching condensate treatment system according to claim 4, characterized in that the ammonia recovery device further includes an ammonia water preparation device, the leading pipe at the top of the refining tower is connected to the ammonia water preparation device, and the ammonia water preparation device is used for making ammonia water. into different concentrations of ammonia.
  6. 一种利用如权利要求1-5任一项所述的变换冷凝液处理系统的变换冷凝液处理方法，其特征在于，包括：A switching condensate treatment method utilizing the switching condensate treatment system according to any one of claims 1 to 5, characterized in that it includes:
    变换低温冷凝液经变换汽提塔转换为含硫低浓氨水，其中，变换汽提塔至少具有两个；The shift low-temperature condensate is converted into sulfur-containing low-concentration ammonia water through a shift stripping tower, wherein there are at least two shift stripping towers;
    根据运行状况，选择部分或全部变换低温冷凝液不经变换汽提塔而进入氨回收装置净化后用于氨法脱硫；According to the operating conditions, select part or all of the converted low-temperature condensate to enter the ammonia recovery unit for purification without passing through the conversion stripper, and then be used for ammonia desulfurization;
    根据运行状况，选择部分或全部含硫低浓氨水进入氨回收装置净化后再用于氨法脱硫；According to the operating conditions, some or all of the sulfur-containing low-concentration ammonia water is selected to enter the ammonia recovery device for purification and then used for ammonia desulfurization;
    氨回收装置净化包括：变换低温冷凝液进入汽提塔中，从汽提塔中部抽出去除部分酸性气的富氨气，进入三级分凝器，在三级分凝器中进一步与酸性气进行分离后顶部得粗氨气，进入精制塔，在精制塔中对酸性气进行深度脱除。The purification of the ammonia recovery unit includes: changing the low-temperature condensate into the stripping tower, extracting the ammonia-rich gas with part of the acid gas removed from the middle of the stripping tower, entering the third-stage partial condenser, and further reacting with the acid gas in the third-stage partial condenser. After separation, crude ammonia gas is obtained at the top and enters the refining tower, where the acid gas is deeply removed.
  7. 如权利要求6所述的变换冷凝液处理方法，其特征在于，将精制塔中精制后的氨气送入制取氨水器中，制取氨水器配制的氨水送至锅炉氨法脱硫或氨水销售。 The conversion condensate treatment method according to claim 6, characterized in that the refined ammonia gas in the refining tower is sent to an ammonia water making device, and the ammonia water prepared in the ammonia water making device is sent to the boiler ammonia desulfurization or ammonia water sales .
PCT/CN2023/107744 2022-07-18 2023-07-17 Shift condensate treatment system and process WO2024017202A1 (en)

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