CN103408086A - MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof - Google Patents
MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof Download PDFInfo
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Abstract
本发明涉及一种MVR汽提脱氨系统，包括汽提脱氨塔、氨水精馏塔、冷凝器。汽提脱氨塔设有高氨氮污水输入管、蒸汽输入管Ⅰ、脱氨后的废水排放口、含氨蒸汽排放口Ⅰ并连有再沸器；高氨氮污水输入管连有废水进料预热器Ⅱ、Ⅰ；脱氨后的废水排放口分别连有废水进料预热器Ⅰ、轴流泵；含氨蒸汽排放口Ⅰ经机械蒸汽压缩机与再沸器相连；再沸器连有与氨水精馏塔相连的稀氨水储罐；氨水精馏塔设有出料口、含氨蒸汽排放口Ⅱ、蒸汽输入管Ⅱ；出料口连有精馏塔釜出料泵，并与废水进料预热器Ⅱ相连；含氨蒸汽排放口Ⅱ与冷凝器相连；浓氨水排放口连有与氨水精馏塔相连的浓氨水储罐。同时，本发明还公开了该系统的应用方法。本发明投资小、易于实施且综合利用率高。
The invention relates to an MVR stripping ammonia removal system, which comprises a stripping ammonia removal tower, an ammonia water rectification tower and a condenser. The stripping deamination tower is equipped with high ammonia nitrogen sewage input pipe, steam input pipe I, deammonized waste water discharge port, ammonia steam discharge port I and is connected with a reboiler; the high ammonia nitrogen sewage input pipe is connected with waste water feed pre Heater Ⅱ, Ⅰ; the waste water discharge port after deamination is connected with the waste water feed preheater Ⅰ and the axial flow pump respectively; the ammonia-containing steam discharge port Ⅰ is connected with the reboiler through a mechanical steam compressor; the reboiler is connected with A dilute ammonia water storage tank connected to the ammonia water rectification tower; the ammonia water rectification tower is equipped with a discharge port, an ammonia-containing steam discharge port II, and a steam input pipe II; The feed preheater II is connected; the ammonia-containing steam discharge port II is connected with the condenser; the concentrated ammonia water discharge port is connected with a concentrated ammonia water storage tank connected with the ammonia water rectification tower. At the same time, the invention also discloses the application method of the system. The invention has the advantages of small investment, easy implementation and high comprehensive utilization rate.
Description
技术领域 technical field
本发明涉及含氨废水脱氨处理技术领域，尤其涉及一种MVR汽提脱氨系统及其方法。 The invention relates to the technical field of ammonia-containing wastewater deamination treatment, in particular to an MVR stripping deamination system and a method thereof.
背景技术 Background technique
石化、冶金、食品等行业常常会产生大量的氨氮的废水。由于处理氨氮废水的成本比较高，其中蒸汽的消耗量通常在180kg/t废水以上，装置不节能，运行费用高，企业难以承受。 Petrochemical, metallurgy, food and other industries often produce a large amount of ammonia nitrogen wastewater. Due to the relatively high cost of treating ammonia nitrogen wastewater, the consumption of steam is usually above 180kg/t of wastewater, the device is not energy-saving, and the operating cost is high, which is unbearable for enterprises.
含氨废水脱除技术通常有生化法、吹脱法、汽提法、折点氯化法、离子交换法、化学沉淀法、膜分离法等。目前，在处理工业中产生的氨氮含量在500~10000ppm的高浓度氨氮废水通常采用比较成熟且广泛采用的技术是通过蒸汽汽提精馏脱氨的方法，将高氨氮废水经过汽提脱氨塔的汽提段汽提后，再经过精馏段精馏后生产一定浓度的氨水。由于汽提过程中消耗大量的蒸汽，而蒸汽通过精馏段塔顶冷凝器冷凝生产氨水，因此蒸汽消耗比较高。虽然国内有通过双效汽提脱氨工艺降低能耗的研究，通过双效汽提脱氨工艺能够使蒸汽消耗降低40~45%，然而对高氨氮废水处理来说，能耗依然比较高。 Ammonia-containing wastewater removal technologies usually include biochemical methods, stripping methods, steam stripping methods, breakpoint chlorination methods, ion exchange methods, chemical precipitation methods, membrane separation methods, etc. At present, in the treatment of high-concentration ammonia nitrogen wastewater with an ammonia nitrogen content of 500-10000ppm in the treatment industry, a relatively mature and widely used technology is usually used to remove ammonia by steam stripping and rectification. After stripping in the stripping section, ammonia water of a certain concentration is produced after rectification in the rectifying section. Because a large amount of steam is consumed in the stripping process, and the steam is condensed to produce ammonia water through the overhead condenser of the rectification section, so the steam consumption is relatively high. Although there are domestic studies on reducing energy consumption through double-effect stripping and deamination process, the steam consumption can be reduced by 40~45% through double-effect stripping and deamination process. However, the energy consumption is still relatively high for the treatment of high ammonia nitrogen wastewater.
机械蒸汽再压缩( Mechanical Vapor Recompression)技术，简称MVR 技术，在蒸发操作单元中，由于其100%循环二次蒸汽的潜热，系统本身能基本达到热平衡，新鲜蒸汽仅用于系统开始启动预热，从而大幅度减少蒸发器对外来新鲜蒸汽的消耗，相对于多效蒸发来说，是一种新型高效节能装置，现已广泛应用于工业废水、造纸黑液的浓缩减量处理，乳品、制糖、淀粉等蒸馏浓缩处理，以及海水淡化、制盐等很多生产领域。但是对于高氨氮废水来说，由于废水水质通常比较复杂，因此仅仅用MVR技术进行蒸发结晶不但蒸发量大而且得到的产品不纯，无法工业回用。 Mechanical Vapor Recompression (Mechanical Vapor Recompression) technology, referred to as MVR technology, in the evaporation operation unit, due to the latent heat of 100% circulating secondary steam, the system itself can basically reach thermal balance, and the fresh steam is only used for system startup and preheating. Thereby greatly reducing the consumption of external fresh steam by the evaporator. Compared with multi-effect evaporation, it is a new type of high-efficiency energy-saving device. It has been widely used in the concentration and reduction treatment of industrial wastewater, papermaking black liquor, dairy products, and sugar , starch and other distillation and concentration treatment, as well as seawater desalination, salt production and many other production fields. However, for high-ammonia-nitrogen wastewater, because the quality of the wastewater is usually relatively complex, the MVR technology alone for evaporation and crystallization not only has a large amount of evaporation but also produces impure products that cannot be reused industrially.
发明内容 Contents of the invention
本发明所要解决的技术问题是提供一种投资小、易于实施的MVR汽提脱氨系统。 The technical problem to be solved by the present invention is to provide an MVR stripping ammonia removal system with low investment and easy implementation.
本发明所要解决的另一个技术问题是提供一种高效节能的该MVR汽提脱氨系统的应用方法。 Another technical problem to be solved by the present invention is to provide an application method of the MVR stripping ammonia removal system with high efficiency and energy saving.
为解决上述问题，本发明所述的一种MVR汽提脱氨系统，包括汽提脱氨塔、氨水精馏塔、冷凝器，其特征在于：所述汽提脱氨塔的一侧上部设有高氨氮污水输入管，其一侧下部设有蒸汽输入管Ⅰ，其另一侧下部通过管道Ⅰ连有再沸器，其底部设有脱氨后的废水排放口，其顶部设有含氨蒸汽排放口Ⅰ；所述高氨氮污水输入管依次连有废水进料预热器Ⅱ、废水进料预热器Ⅰ，该废水进料预热器Ⅱ、废水进料预热器Ⅰ均设有脱氨污水排放管；所述脱氨后的废水排放口通过管道Ⅱ分别连有所述废水进料预热器Ⅰ、轴流泵，该轴流泵与所述再沸器相连；所述含氨蒸汽排放口Ⅰ通过机械蒸汽压缩机与所述再沸器相连；所述再沸器的一侧设有稀氨水排放口，并通过该稀氨水排放口连有稀氨水储罐；所述稀氨水储罐依次经精馏进料泵、换热器与所述氨水精馏塔相连；所述氨水精馏塔的底部设有出料口，其顶部设有含氨蒸汽排放口Ⅱ，其一侧设有蒸汽输入管Ⅱ；所述出料口通过管道Ⅲ连有精馏塔釜出料泵，并通过精馏塔釜出料泵经所述换热器与所述废水进料预热器Ⅱ相连；所述含氨蒸汽排放口Ⅱ通过管道Ⅳ与所述冷凝器相连，该冷凝器分别设有循环水回水排放口、循环水进口、浓氨水排放口；所述浓氨水排放口通过管道Ⅴ连有浓氨水储罐，该浓氨水储罐经氨水回流泵分别与所述氨水精馏塔、浓氨水输出管相连。 In order to solve the above problems, a kind of MVR stripping deamination system according to the present invention comprises a stripping deamination tower, an ammonia water rectification tower, and a condenser, and is characterized in that: the upper part of one side of the stripping deamination tower is equipped with There is a high-ammonia-nitrogen sewage input pipe, and the lower part of one side is provided with a steam input pipe I, and the lower part of the other side is connected with a reboiler through the pipe I, and the bottom is provided with a waste water discharge port after deamination, and the top is provided with an ammonia-containing waste water discharge port. Steam discharge port I; the high-ammonia nitrogen sewage input pipe is successively connected with waste water feed preheater II and waste water feed preheater I, and the waste water feed preheater II and waste water feed preheater I are equipped with Deamination sewage discharge pipe; the deamination waste water discharge outlet is respectively connected with the waste water feed preheater I and the axial flow pump through the pipeline II, and the axial flow pump is connected with the reboiler; the containing Ammonia vapor discharge port I is connected to the reboiler through a mechanical vapor compressor; one side of the reboiler is provided with a dilute ammonia water discharge port, and a dilute ammonia water storage tank is connected through the dilute ammonia water discharge port; The ammonia water storage tank is successively connected with the ammonia water rectification tower through a rectification feed pump and a heat exchanger; the bottom of the ammonia water rectification tower is provided with a discharge port, and its top is provided with an ammonia-containing steam discharge port II, one of which is There is a steam input pipe II on the side; the outlet is connected to the rectification tower kettle discharge pump through the pipeline III, and the rectification tower kettle discharge pump passes through the heat exchanger and the waste water feed preheater II is connected; the ammonia-containing steam discharge port II is connected to the condenser through pipeline IV, and the condenser is respectively provided with a circulating water backwater discharge port, a circulating water inlet, and a concentrated ammonia water discharge port; the concentrated ammonia water discharge port passes through The pipeline V is connected with a concentrated ammonia water storage tank, and the concentrated ammonia water storage tank is respectively connected with the ammonia water rectification tower and the concentrated ammonia water output pipe through an ammonia water reflux pump.
所述机械蒸汽压缩机是指容积式压缩机或离心式压缩机，压缩机增压为20~80kPa。 The mechanical vapor compressor refers to a displacement compressor or a centrifugal compressor, and the pressurization of the compressor is 20-80kPa.
所述再沸器是指立式热虹吸式再沸器、强制循环式立式再沸器、卧式再沸器中的一种。 The reboiler refers to one of a vertical thermosiphon reboiler, a forced circulation vertical reboiler and a horizontal reboiler.
所述机械蒸汽压缩机、轴流泵、精馏进料泵、精馏塔釜出料泵、氨水回流泵上均设有流量计。 The mechanical steam compressor, the axial flow pump, the rectification feed pump, the rectification tower still discharge pump, and the ammonia water reflux pump are all provided with flow meters.
如上所述的一种MVR汽提脱氨系统的应用方法，包括以下步骤： The application method of a kind of MVR stripping ammonia removal system as described above, comprises the following steps:
⑴将经过预处理后的高氨氮污水依次经废水进料预热器Ⅰ、废水进料预热器Ⅱ进入汽提脱氨塔，同时，将蒸汽输入至所述汽提脱氨塔进行汽提脱氨，分别得到温度为95~110℃且压力为0.085~0.15MPa的含氨3~8%的蒸汽和脱氨后的废水； (1) The pretreated high-ammonia nitrogen sewage enters the stripping deamination tower through the waste water feed preheater I and waste water feed preheater II in sequence, and at the same time, steam is input into the stripping deamination tower for stripping Deamination, to obtain steam containing 3-8% ammonia at a temperature of 95-110°C and a pressure of 0.085-0.15 MPa and deaminated wastewater;
⑵所述含氨3~8%的蒸汽经含氨蒸汽排放口Ⅰ由机械蒸汽压缩机加压增温后进入再沸器；同时，所述脱氨后的废水一部分经废水进料预热器Ⅰ由脱氨污水排放管排出，其余下部分经轴流泵进入所述再沸器，所述含氨3~8%的蒸汽在所述再沸器内蒸发所述脱氨后的废水，分别得到蒸发后的蒸汽和冷凝后的质量浓度为3~8%的氨水；所述蒸发后的蒸汽作为汽提脱氨蒸汽进入所述汽提脱氨塔中； (2) The steam containing 3-8% ammonia enters the reboiler after being pressurized and heated by a mechanical steam compressor through the ammonia-containing steam discharge port I; at the same time, a part of the deammonized waste water passes through the waste water feed preheater Ⅰ is discharged from the deamination sewage discharge pipe, and the rest of the lower part enters the reboiler through an axial flow pump, and the steam containing 3-8% ammonia evaporates the deamination wastewater in the reboiler, respectively Obtaining evaporated steam and condensed mass concentration of ammonia water of 3 to 8%; the evaporated steam enters the stripping deamination tower as stripping deamination steam;
⑶所述冷凝后的质量浓度为3~8%的氨水经稀氨水排放口进入稀氨水储罐，并依次经精馏进料泵、换热器进入氨水精馏塔中；同时，将蒸汽输入至所述氨水精馏塔中进行蒸汽汽提精馏，分别得到达标后的脱氨废水和含氨15~30%的蒸汽；所述达标后的脱氨废水依次通过精馏塔釜出料泵、所述换热器经废水进料预热器Ⅱ由脱氨污水排放管排出； (3) The ammoniacal liquor with a mass concentration after the condensation of 3 to 8% enters the dilute ammonia water storage tank through the dilute ammonia water discharge port, and enters in the ammonia water rectification tower through the rectification feed pump and heat exchanger successively; at the same time, the steam is input Carry out steam stripping rectification in the ammoniacal water rectification tower, obtain the deammonization waste water after reaching the standard and the steam containing ammonia 15～30% respectively; , The heat exchanger is discharged from the deammonization sewage discharge pipe through the waste water feed preheater II;
⑷所述含氨15~30%的蒸汽经含氨蒸汽排放口Ⅱ进入冷凝器冷凝，得到质量浓度为15~30%的氨水，该质量浓度为15~30%的氨水经浓氨水排放口由氨水回流泵分为两部分，其中一部分经浓氨水输出管输出，其余部分则进入所述氨水精馏塔进行精馏。 (4) The steam containing 15-30% of ammonia enters the condenser to condense through the ammonia-containing steam discharge port II, and obtains ammoniacal liquor with a mass concentration of 15-30%. The ammonia water reflux pump is divided into two parts, one of which is output through the concentrated ammonia water output pipe, and the rest enters the ammonia water rectification tower for rectification.
所述步骤⑴中的预处理后的高氨氮污水是指氨氮含量为500~10000ppm的pH值调节到11.5~12.0的含氨废水。 The pretreated high-ammonia-nitrogen wastewater in step (1) refers to ammonia-containing wastewater with an ammonia nitrogen content of 500-10,000 ppm and a pH value adjusted to 11.5-12.0.
所述步骤⑴和所述步骤⑶中的蒸汽均是指饱和蒸汽或过热蒸汽。 The steam in the step (1) and the step (3) all refers to saturated steam or superheated steam.
本发明与现有技术相比具有以下优点： Compared with the prior art, the present invention has the following advantages:
1、本发明利用机械蒸汽再压缩技术，将汽提脱氨后的蒸汽通过机械压缩提高蒸汽的压力和温度，作为汽提脱氨塔塔底再沸器的加热热源使用，使汽提脱氨过程中仅消耗少量的压缩机启动电机功率，仅在启动过程中消耗少量的蒸汽，正常操作过程中无需额外的消耗汽提蒸汽，降低了吹脱蒸汽的耗量，有效地解决了传统遇到的高氨氮废水处理方法蒸汽耗量高、操作成本高的问题，做到了节能化、无害化、减量化、稳定化的处理。 1. The present invention utilizes mechanical steam recompression technology to mechanically compress the steam after stripping and deamination to increase the pressure and temperature of the steam, and use it as a heating heat source for the reboiler at the bottom of the stripping deamination tower to make the stripping deamination During the process, only a small amount of compressor starting motor power is consumed, and only a small amount of steam is consumed during the start-up process. During normal operation, no additional consumption of stripping steam is required, which reduces the consumption of stripping steam and effectively solves the traditional problem. The high-ammonia-nitrogen wastewater treatment method has high steam consumption and high operating costs, and has achieved energy-saving, harmless, reduction, and stabilization treatment.
2、本发明通过MVR汽提脱氨后产生的氨水浓度比较低通常在3~5%左右，需要进一步通过精馏塔进行精馏提浓，仅需要消耗少量的蒸汽，通过MVR的初步浓缩，需要精馏的稀氨水仅为原有废水量的1/20~1/100。 2. In the present invention, the concentration of ammonia water produced after deamination by MVR stripping is relatively low, usually about 3-5%, and it is necessary to further carry out rectification and enrichment through a rectification tower, and only need to consume a small amount of steam. Through the initial concentration of MVR, The dilute ammonia water that needs to be rectified is only 1/20~1/100 of the original wastewater volume.
3、以中石化某催化剂厂40m3/h高氨氮废水处理为例，由于废水中氨氮含量通常在6000mg/l左右，处理后的废水达到国家一级排放标准，经过处理后的得到的氨水浓度为25%，分别应用单塔汽提精馏技术、双效汽提脱氨技术及MVR汽提脱氨法对废水处理进行计算，计算结果见下表1 3. Taking the treatment of 40m3/h high ammonia nitrogen wastewater from a catalyst factory in Sinopec as an example, since the ammonia nitrogen content in wastewater is usually around 6000mg/l, the treated wastewater meets the national first-level discharge standard, and the ammonia concentration obtained after treatment is 25 %, using single-column stripping and rectification technology, double-effect stripping and deamination technology and MVR stripping and deamination method to calculate the wastewater treatment, the calculation results are shown in the following table 1
表1 Table 1
备注：蒸汽价格按照200元/t，工业电按照0.8元/kWh计算。 Remarks: The price of steam is calculated at 200 yuan/t, and the price of industrial electricity is calculated at 0.8 yuan/kWh.
由表1可以看出，采用MVR汽提脱氨法操作成本约为汽提精馏技术和的33%，为双效汽提技术的58%；另外，MVR汽提脱氨法的使用，由于精馏量的减少，对于循环冷却水的需要量也大大的降低，由以上分析可以得出，MVR汽提脱氨法大幅度地降低了废水处理的操作成本，对氨氮废水处理具有非常重要的现实意义。 As can be seen from Table 1, the operating cost of the MVR stripping deamination method is about 33% of the sum of the stripping rectification technology and 58% of the double-effect stripping technology; in addition, the use of the MVR stripping deamination method, due to The reduction of the rectification amount greatly reduces the demand for circulating cooling water. From the above analysis, it can be concluded that the MVR stripping and deammonization method greatly reduces the operating cost of wastewater treatment, and has a very important role in the treatment of ammonia nitrogen wastewater. Practical significance.
4、本发明投资小、易于实施，可广泛应用于石化、冶金、食品等无机氨氮废水处理行业中。 4. The invention has small investment and is easy to implement, and can be widely used in petrochemical, metallurgy, food and other inorganic ammonia nitrogen wastewater treatment industries.
附图说明 Description of drawings
下面结合附图对本发明的具体实施方式作进一步详细的说明。 The specific implementation manners of the present invention will be further described in detail below in conjunction with the accompanying drawings.
图1为发明的工艺流程图。 Fig. 1 is the process flow chart of invention.
图中：1—废水进料预热器Ⅰ 2—废水进料预热器Ⅱ 3—汽提脱氨塔4—机械蒸汽压缩机 5—再沸器 6—轴流泵 7—稀氨水储罐 8—换热器 9—氨水精馏塔 10—精馏进料泵 11—精馏塔釜出料泵 12—冷凝器 13—浓氨水储罐 14—氨水回流泵。 In the figure: 1—Wastewater Feed Preheater Ⅰ 2—Wastewater Feed Preheater Ⅱ 3—Stripping Deammonization Tower 4—Mechanical Steam Compressor 5—Reboiler 6—Axial Flow Pump 7—Dilution Ammonia Water Storage Tank 8—Heat Exchanger 9—Ammonia Distillation Tower 10—Rectification Feed Pump 11—Rectification Tower Discharge Pump 12—Condenser 13—Concentrated Ammonia Water Storage Tank 14—Ammonia Water Return Pump.
具体实施方式 Detailed ways
如图1所示，一种MVR汽提脱氨系统，包括汽提脱氨塔3、氨水精馏塔9、冷凝器12。 As shown in FIG. 1 , an MVR stripping deamination system includes a stripping deamination tower 3 , an ammonia water rectification tower 9 , and a condenser 12 .
汽提脱氨塔3的一侧上部设有高氨氮污水输入管，其一侧下部设有蒸汽输入管Ⅰ，其另一侧下部通过管道Ⅰ连有再沸器5，其底部设有脱氨后的废水排放口，其顶部设有含氨蒸汽排放口Ⅰ；高氨氮污水输入管依次连有废水进料预热器Ⅱ2、废水进料预热器Ⅰ1，该废水进料预热器Ⅱ2、废水进料预热器Ⅰ1均设有脱氨污水排放管；脱氨后的废水排放口通过管道Ⅱ分别连有废水进料预热器Ⅰ1、轴流泵6，该轴流泵6与再沸器5相连；含氨蒸汽排放口Ⅰ通过机械蒸汽压缩机4与再沸器5相连；再沸器5的一侧设有稀氨水排放口，并通过该稀氨水排放口连有稀氨水储罐7；稀氨水储罐7依次经精馏进料泵10、换热器8与氨水精馏塔9相连；氨水精馏塔9的底部设有出料口，其顶部设有含氨蒸汽排放口Ⅱ，其一侧设有蒸汽输入管Ⅱ；出料口通过管道Ⅲ连有精馏塔釜出料泵11，并通过精馏塔釜出料泵11经换热器8与废水进料预热器Ⅱ2相连；含氨蒸汽排放口Ⅱ通过管道Ⅳ与冷凝器12相连，该冷凝器12分别设有循环水回水排放口、循环水进口、浓氨水排放口；浓氨水排放口通过管道Ⅴ连有浓氨水储罐13，该浓氨水储罐13经氨水回流泵14分别与氨水精馏塔9、浓氨水输出管相连。 The upper part of one side of the stripping deamination tower 3 is provided with a high-ammonia-nitrogen sewage input pipe, the lower part of one side is provided with a steam input pipe I, and the lower part of the other side is connected with a reboiler 5 through a pipe I, and a deamination pipe is installed at the bottom. The top of the waste water discharge port is equipped with ammonia-containing steam discharge port Ⅰ; the high ammonia nitrogen sewage input pipe is connected with waste water feed preheater Ⅱ2, waste water feed preheater Ⅰ1, and the waste water feed preheater Ⅱ2, waste water feed preheater Ⅱ2, The waste water feed preheater Ⅰ1 is equipped with a deamination sewage discharge pipe; the waste water discharge port after deamination is connected with the waste water feed preheater Ⅰ1 and the axial flow pump 6 respectively through the pipe Ⅱ, and the axial flow pump 6 is connected with the reboiler 5; the ammonia-containing steam discharge port I is connected to the reboiler 5 through the mechanical steam compressor 4; one side of the reboiler 5 is provided with a dilute ammonia water discharge port, and a dilute ammonia water storage tank is connected through the dilute ammonia water discharge port 7. The dilute ammonia water storage tank 7 is connected to the ammonia water rectification tower 9 through the rectification feed pump 10 and the heat exchanger 8 successively; the bottom of the ammonia water rectification tower 9 is provided with a discharge port, and its top is provided with an ammonia-containing vapor discharge port Ⅱ, one side of which is provided with a steam input pipe Ⅱ; the outlet is connected to the rectification tower kettle discharge pump 11 through the pipeline Ⅲ, and the rectification tower kettle discharge pump 11 is preheated with the waste water feed through the heat exchanger 8 The ammonia-containing steam discharge port II is connected to the condenser 12 through the pipe IV, and the condenser 12 is respectively provided with a circulating water backwater discharge port, a circulating water inlet, and a concentrated ammonia water discharge port; the concentrated ammonia water discharge port is connected through a pipe V Concentrated ammonia water storage tank 13 is arranged, and this concentrated ammonia water storage tank 13 is respectively connected with ammonia water rectifying tower 9, concentrated ammonia water output pipe through ammonia water reflux pump 14.
其中： in:
机械蒸汽压缩机4是指容积式压缩机或离心式压缩机，压缩机增压为20~80kPa。 The mechanical vapor compressor 4 refers to a positive displacement compressor or a centrifugal compressor, and the pressurized pressure of the compressor is 20-80kPa.
再沸器5是指立式热虹吸式再沸器、强制循环式立式再沸器、卧式再沸器中的一种。 The reboiler 5 refers to one of a vertical thermosiphon reboiler, a forced circulation vertical reboiler, and a horizontal reboiler.
机械蒸汽压缩机4、轴流泵6、精馏进料泵10、精馏塔釜出料泵11、氨水回流泵14上均设有流量计。 The mechanical steam compressor 4 , the axial flow pump 6 , the rectification feed pump 10 , the rectification tower still discharge pump 11 , and the ammonia water reflux pump 14 are all equipped with flow meters.
该MVR汽提脱氨系统的应用方法，包括以下步骤： The application method of the MVR stripping ammonia removal system comprises the following steps:
⑴将经过预处理后的高氨氮污水依次经废水进料预热器Ⅰ1、废水进料预热器Ⅱ2进入汽提脱氨塔3，同时，将饱和蒸汽或过热蒸汽输入至汽提脱氨塔3进行汽提脱氨，分别得到温度为95~110℃且压力为0.085~0.15MPa的含氨3~8%的蒸汽和脱氨后的废水。 (1) The pretreated high-ammonia nitrogen sewage enters the stripping deamination tower 3 through the waste water feed preheater Ⅰ1 and waste water feed preheater Ⅱ2 in sequence, and at the same time, the saturated steam or superheated steam is input into the stripping deamination tower 3. Carry out stripping and deamination to obtain steam containing 3-8% ammonia at a temperature of 95-110°C and a pressure of 0.085-0.15 MPa and waste water after deamination.
预处理后的高氨氮污水是指氨氮含量为500~10000ppm的pH值调节到11.5~12.0的含氨废水。 The pretreated high-ammonia-nitrogen wastewater refers to ammonia-containing wastewater with an ammonia nitrogen content of 500-10,000 ppm and a pH value adjusted to 11.5-12.0.
⑵含氨3~8%的蒸汽经含氨蒸汽排放口Ⅰ由机械蒸汽压缩机4加压增温后进入再沸器5；同时，脱氨后的废水一部分经废水进料预热器Ⅰ1由脱氨污水排放管排出，其余下部分经轴流泵6进入再沸器5，含氨3~8%的蒸汽在所述再沸器（5）内蒸发脱氨后的废水，分别得到蒸发后的蒸汽和冷凝后的质量浓度为3~8%的氨水；蒸发后的蒸汽作为汽提脱氨蒸汽进入汽提脱氨塔3中。 (2) The steam containing 3~8% ammonia enters the reboiler 5 after being pressurized and heated by the mechanical steam compressor 4 through the ammonia-containing steam discharge port I; at the same time, part of the deammonized waste water passes through the waste water feed preheater I1 The deammonized sewage discharge pipe is discharged, and the rest of the lower part enters the reboiler 5 through the axial flow pump 6, and the steam containing 3-8% ammonia evaporates the deaminated waste water in the reboiler (5), and the evaporated waste water is obtained respectively. The steam and the condensed mass concentration are 3-8% ammonia water; the evaporated steam enters the stripping deamination tower 3 as the stripping deamination steam.
⑶冷凝后的质量浓度为3~8%的氨水经稀氨水排放口进入稀氨水储罐7，并依次经精馏进料泵10、换热器8进入氨水精馏塔9中；同时，将饱和蒸汽或过热蒸汽输入至氨水精馏塔9中进行蒸汽汽提精馏，分别得到达标后的脱氨废水和含氨15~30%的蒸汽；达标后的脱氨废水依次通过精馏塔釜出料泵11、换热器8经废水进料预热器Ⅱ2由脱氨污水排放管排出。 (3) the mass concentration after condensation is that the ammoniacal liquor of 3 ~ 8% enters the dilute ammonia water storage tank 7 through the dilute ammonia water discharge port, and enters in the ammonia water rectification tower 9 through the rectifying feed pump 10, the heat exchanger 8 successively; Simultaneously, Saturated steam or superheated steam is input into the ammonia water rectification tower 9 for steam stripping and rectification, and the deammonization waste water and the steam containing 15-30% ammonia after reaching the standard are obtained respectively; The discharge pump 11 and the heat exchanger 8 are discharged from the waste water discharge pipe through the waste water feed preheater II2.
⑷含氨15~30%的蒸汽经含氨蒸汽排放口Ⅱ进入冷凝器12冷凝，得到质量浓度为15~30%的氨水，该质量浓度为15~30%的氨水经浓氨水排放口由氨水回流泵14分为两部分，其中一部分经浓氨水输出管输出，其余部分则进入氨水精馏塔9进行精馏。 (4) The steam containing 15-30% ammonia enters the condenser 12 through the ammonia-containing steam discharge port II to condense to obtain ammonia water with a mass concentration of 15-30%, and the ammonia water with a mass concentration of 15-30% passes through the concentrated ammonia water discharge port The reflux pump 14 is divided into two parts, one of which is output through the concentrated ammonia water output pipe, and the rest enters the ammonia water rectification tower 9 for rectification.
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Application publication date: 20131127 |