WO2018126651A1 - 一种蒸发结晶干燥一体化装置及蒸发结晶干燥方法 - Google Patents

一种蒸发结晶干燥一体化装置及蒸发结晶干燥方法 Download PDF

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WO2018126651A1
WO2018126651A1 PCT/CN2017/094487 CN2017094487W WO2018126651A1 WO 2018126651 A1 WO2018126651 A1 WO 2018126651A1 CN 2017094487 W CN2017094487 W CN 2017094487W WO 2018126651 A1 WO2018126651 A1 WO 2018126651A1
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outlet
inlet
dryer
drying
evaporation
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PCT/CN2017/094487
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English (en)
French (fr)
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姜广义
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广州市心德实业有限公司
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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
    • 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
    • C02F1/08—Thin film evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions

Definitions

  • the invention belongs to the field of industrial wastewater treatment, and in particular relates to an evaporation crystal drying integrated device and an evaporation crystal drying method.
  • Organic salty wastewater generally refers to wastewater with organic matter concentration greater than 2000mg/L, mainly from dyes, electroplating, petrochemical, pharmaceutical, food, landfills, etc., a large amount of organic wastewater is discharged into water bodies, due to biodegradation, high concentration of organic Salt-containing wastewater will cause oxygenation and even anaerobic in the receiving water body. Most of the water organisms will die, which will not only cause eutrophication of the water body, but also cause black odor in the water body. The difficulty and cost of water treatment will increase, and the water body will lose its use value, even to the population and The organism produces toxic effects.
  • the wastewater When treating the organic salty wastewater, the wastewater is first subjected to organic matter removal treatment, and then the wastewater is concentrated and crystallized.
  • Oxidation is conventionally carried out by preliminary coagulation, adsorption and sedimentation, followed by Fenton reagent catalytic oxidation and flocculant flocculation, and then sedimentation filtration to achieve the purpose of removing organic matter, but the efficiency of de-organization by this method is low.
  • the effluent organic matter is still high.
  • the biochemical method routinely performs air flotation and degreasing, then enters the anaerobic tank for preliminary degradation, then enters the anoxic tank for denitrification reaction, further degrades, and finally enters the aerobic tank, where the final degradation of the organic matter is eliminated.
  • the wastewater passes through the aerobic tank, is settled and filtered, and then discharged.
  • this method has great limitations on organic matter. Above 5000mg/L of organic wastewater, the strain is difficult to grow; there are many kinds of biodegradable substances in organic matter, which are difficult to remove all; the salt concentration of wastewater is high, and the strain cannot survive. , easy to be killed.
  • the prior art In the desalination process, the prior art often uses a multi-effect evaporation system for the concentration and crystallization of wastewater, which has problems of large demand for raw steam, high energy consumption, low thermal efficiency, large space occupied by equipment, and the like, and the pretreatment cannot be completely completed.
  • the organic matter is removed and the organic matter is enriched.
  • the mother liquor separated by the solid-liquid separation device needs to be discharged, so as to ensure the normal operation of the system, and the system cannot meet the requirements of zero discharge.
  • the object of the present invention is to provide an evaporation crystal drying integrated device and an evaporation crystal drying method, which can reduce energy consumption to a large extent by treating organic salty wastewater or other raw materials by the present invention. It can achieve zero discharge of wastewater.
  • an evaporation crystal drying integrated device which mainly comprises an evaporative vapor compressor, a dry steam compressor and a dryer; the outlet of the dryer secondary steam and dry steam The inlets of the compressor are connected by a line; the outlet of the dry steam compressor is connected to the inlet of the evaporative vapor compressor; the outlet of the evaporative vapor compressor is connected to the steam inlet of the dryer.
  • an evaporation device is disposed in front of the inlet of the evaporative vapor compressor, and a secondary steam outlet of the evaporation device is connected to an inlet of the evaporative vapor compressor together with an outlet of the dry steam compressor;
  • the outlet of the steam compressor is also connected to the steam inlet of the evaporation device;
  • the evaporation device is provided with a feed inlet for the feed of raw materials;
  • the material outlet of the evaporation device is connected to the material inlet of the dryer by a pipe.
  • the evaporation device is one or a combination of a rising film evaporator, a falling film evaporator, and a forced circulation evaporator.
  • the pipeline between the material outlet of the evaporation device and the material inlet of the dryer is provided with a solid-liquid separation device; the inlet of the solid-liquid separation device is connected with the material outlet of the evaporation device; The outlet of the solid-liquid separation device is connected to the material inlet of the dryer by a pipeline.
  • a screw feeder is arranged on the pipeline between the material outlet of the evaporation device and the material inlet of the dryer; the inlet of the screw feeder is connected with the outlet of the material of the evaporation device; The outlet of the screw feeder is connected to the inlet of the material of the dryer.
  • a screw feeder is arranged on the pipeline connection between the outlet of the solid-liquid separation device and the material inlet of the dryer; the inlet of the screw feeder and the solid-liquid separation device An outlet connection; the outlet of the screw feeder is connected to the material inlet of the dryer.
  • a dust separator is arranged on the pipeline between the secondary steam outlet of the dryer and the inlet of the dry steam compressor, and the inlet and the outlet of the dust collector are respectively connected to the secondary steam outlet of the dryer And an inlet of the dry steam compressor; a material outlet of the dryer is provided with a vacuum barrier to connect the inlet of the vacuum barrier; the outlet of the vacuum barrier produces a dried solid.
  • the invention also discloses an evaporation crystallization drying method using the above device, which adopts the technical scheme that: the raw material is evaporated by an evaporation device, and the evaporated and concentrated material is separated after being separated by the solid-liquid separation device, and the screw feeder is used.
  • the dryer for low-temperature drying Entering the dryer for low-temperature drying; the secondary steam generated by the drying is dedusted by the dust collector, and then enters the dry steam compressor for compression; the secondary steam compressed by the drying steam compressor is mixed with the secondary steam generated by the evaporation device to enter To the evaporative vapor compressor, it is compressed again, and a part of the secondary steam that has been compressed again enters the evaporation device, and the other portion enters the dryer.
  • the secondary steam after compression by the dry steam compressor has the same temperature as the secondary steam generated by the evaporation device, and the pressure is the same; the secondary steam after the evaporation steam compressor is compressed again according to the heat exchange
  • the area and heat transfer system automatically distributes the flow into the evaporator and dryer.
  • the secondary steam generated by the dryer is subjected to two-stage compression and then re-entered into the dryer to exchange heat with the material to achieve a heat transfer temperature difference of 40-50 ° C.
  • the secondary steam generated by the drying process is compressed and heated, and the heat is recovered and reused.
  • the entire evaporative drying system is heat-balanced, no external steam is required, and the drying process is saved.
  • the secondary steam condensing device greatly reduces the energy consumption, optimizes the utilization of thermal energy, improves the drying heat transfer temperature difference, and solves the problem that the prior art dryer has insufficient temperature difference and requires a large amount of steam generation.
  • Figure 1 is a schematic illustration of an embodiment of the invention.
  • connection relationships mentioned in the text are not directly connected to the components, but are connected by the technical means in the technical field, or may be combined or added according to the actual situation to form a better connection structure.
  • An evaporation crystal drying integrated device as shown in FIG. 1 includes an evaporation device, a solid-liquid separation device, a screw feeder, a dryer, a vacuum barrier, a dust remover, an evaporative vapor compressor, and a dry steam compressor.
  • the secondary steam outlet of the evaporation device is connected to the inlet of the evaporation steam compressor, and the outlet of the evaporation steam compressor is connected to the steam inlet of the evaporation device and the dryer.
  • the evaporation device is provided with a raw material inlet, a material outlet of the evaporation device and a solid-liquid separation device.
  • the outlet of the solid-liquid separation device is connected to the inlet of the screw feeder, the outlet of the screw feeder is connected to the inlet of the dryer, and the secondary steam outlet of the dryer Connected to the inlet of the precipitator, the outlet of the precipitator is connected to the inlet of the dry steam compressor, the outlet of the dry steam compressor is connected to the inlet of the evaporative vapor compressor, the solid outlet of the dryer is connected to the inlet of the vacuum compartment, and the vacuum compartment is dry.
  • the evaporation device is one or a combination of a falling film evaporator, a rising film evaporator, a plate evaporator, and a forced circulation evaporator. Both the evaporative vapor compressor and the dry steam compressor are Roots compressors or centrifugal blowers or high speed centrifugal compressors.
  • the evaporative crystallization drying method of the apparatus is as follows. The following method selects the preferred method and is only used to illustrate the apparatus of the present invention without limitation.
  • the organic salty wastewater is preheated by the preheater to recover the heat of the condensed water, then enters the falling film evaporator, and after preconcentration, enters the forced circulation evaporator, and the wastewater is continuously circulated and concentrated in the forced circulation evaporator.
  • the salt is saturated and crystallized, and then discharged to a solid-liquid separation device (preferably a centrifuge) for solid-liquid separation to obtain a crystal slurry. Since the organic matter content in the wastewater is continuously enriched during the concentration process, the concentrated liquid becomes thick and difficult to centrifuge, and if it is not treated, it will affect the normal crystallization separation.
  • the prior art reoxidizes the front end of the return system, which causes the concentrated liquid to carry away part of the heat, the system energy is unbalanced, and the salt content in the concentrated liquid is large, and oxidation is difficult. Therefore, the thick concentrated liquid is dried and dehydrated by a drying process to separate the organic matter from the water.
  • the dryer uses a hollow blade dryer for low-temperature evaporation and drying, and the thick concentrate passes through a screw feeder in a hot state, enters the dryer to flash, and then uses the steam and thickened from the evaporation steam compressor.
  • the concentrated liquid is subjected to heat exchange, and the thick concentrated liquid is gradually dehydrated to gradually solidify, thereby achieving the purpose of drying.
  • the secondary steam exiting the thick concentrate is subjected to a first-stage compression by a dry steam compressor, and then reaches the same temperature and pressure of the vaporized vapor compressor inlet, and then enters the evaporative vapor compressor.
  • the secondary compression is carried out to further increase the temperature of the secondary steam, and the heat exchange temperature difference between the steam after the secondary compression and the thick concentrate in the hollow blade dryer can reach 40-50 °C.
  • Drying utilizes a dry steam compressor and an evaporative vapor compressor to recompress the steam, recovering the secondary evaporation caused by the drying, so that the heat of the system is not taken away, ensuring the heat balance between evaporation and drying of the system.
  • the secondary steam generated by the hollow blade dryer has more tiny particles and droplets, so it first enters the dust collector and then enters the dry steam compressor. Since the hollow blade dryer is low-temperature drying and the inside is negative pressure, the vacuum barrier is used to periodically cut the hollow blade dryer to discharge the material of the vacuum barrier.
  • the evaporative vapor compressor is used in combination with a dry steam compressor to reduce the temperature rise requirement of the dry steam compressor, so that evaporation crystallization and drying are integrated.
  • the condensed water produced by the falling film evaporator, the forced circulation evaporator and the hollow blade dryer is used as a heat medium to heat-recover the heat of the organic salty wastewater through the preheater, and then the low temperature water is obtained.

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)

Abstract

公开了一种蒸发结晶干燥一体化装置，主要包括蒸发蒸汽压缩机、干燥蒸汽压缩机和干燥机；干燥机二次蒸汽的出口与干燥蒸汽压缩机的入口之间以管路连接；干燥蒸汽压缩机的出口与蒸发蒸汽压缩机的入口连接；蒸发蒸汽压缩机的出口与干燥机的蒸汽入口连接。还公开了使用该一体化装置的蒸发结晶干燥方法，可以节能、高效地实现有机含盐废水的脱盐脱有机物处理，实现蒸发及干燥一体化。

Description

一种蒸发结晶干燥一体化装置及蒸发结晶干燥方法 技术领域
本发明属于工业废水处理领域，具体涉及一种蒸发结晶干燥一体化装置及蒸发结晶干燥方法。
背景技术
有机含盐废水一般是指有机物浓度大于2000mg/L的废水，主要来源于染料、电镀、石化、制药、食品、垃圾填埋场等，大量有机物废水排入水体，由于生物降解作用，高浓度有机含盐废水会使受纳水体缺氧甚至厌氧，多数水体生物死亡，不仅引起水体富营养化、造成水体黑臭，给水处理的难度和成本加大，使水体失去使用价值，甚至对人群及生物产生毒害作用。
处理有机含盐废水时，首先对废水进行有机物去除处理，后对废水进行浓缩结晶处理。
在现有技术中，主要利用氧化法和生化法去除高浓度有机物。氧化法常规为先进行初步混凝、吸附沉降，然后用芬顿试剂催化氧化和絮凝剂进行絮凝，然后进行沉降过滤，从而达到脱除有机物的目的，但是采用该方法脱有机物的效率较低，出水有机物仍偏高。生化法常规为先进行气浮除油，然后进入厌氧池进行初步降解，再进入到缺氧池进行反硝化反应，进一步降解，最后进入到好氧池，在此完成有机物的最终降解各消除反应，废水经过好氧池后沉降过滤然后排放。但是采用该方法对有机物有很大的限制，高于5000mg/L的有机物废水，菌种难以生长；有机物中的生物难降解物种类多，难全部去除；废水含盐浓度高，菌种不能生存，容易被杀死。
在除盐工艺中，现有技术对废水进行浓缩结晶处理时常采用多效蒸发系统，存在生蒸汽需求量大、能耗要求高、热效率低、设备占用空间大等问题，且由于前处理不能完全去除有机物，有机物富集，固液分离装置分离后的母液需要外排，才能保证系统正常运行，使系统不能达到零排放的要求。
在现有技术中，干燥机大部分需要采用生蒸汽作为热源进行干燥，干燥机的二次蒸汽出口需要设置抽真空装置，使干燥机内达到较低的蒸发温度，干燥机产生的二次蒸汽不能回收利用，需要用冷凝设备对二次蒸汽进行冷凝，且干燥过程需要不断补充生蒸汽，造成生蒸汽需求量大、能耗要求高、热效率低、设备投资成本高等问题。
发明内容
鉴于现有技术的不足，本发明的目的在于提供一种蒸发结晶干燥一体化装置及蒸发结晶干燥方法，通过本发明处理有机含盐废水或其他原料，能在很大程度上降低能耗，同时能实现废水的零排放。
为实现上述目的，本发明所采用的技术方案是：一种蒸发结晶干燥一体化装置，主要包括蒸发蒸汽压缩机、干燥蒸汽压缩机和干燥机；所述干燥机二次蒸汽的出口与干燥蒸汽压缩机的入口之间以管路连接；所述干燥蒸汽压缩机的出口与蒸发蒸汽压缩机的入口连接；所述蒸发蒸汽压缩机的出口与干燥机的蒸汽入口连接。
作为上述技术方案的进一步改进，所述蒸发蒸汽压缩机的入口前设有蒸发装置，该蒸发装置的二次蒸汽出口与干燥蒸汽压缩机的出口一并连接蒸发蒸汽压缩机的入口；所述蒸发蒸汽压缩机的出口还连接蒸发装置的蒸汽入口；所述蒸发装置设有原料入口，用于原料的进料；所述蒸发装置的物料出口与干燥机的物料入口之间以管路连接。
作为上述技术方案的进一步改进，所述蒸发装置为升膜蒸发器、降膜蒸发器、强制循环蒸发器的一种或多种组合。
作为上述技术方案的进一步改进，所述蒸发装置的物料出口与干燥机的物料入口之间的管路设有固液分离装置；所述固液分离装置的入口与蒸发装置的物料出口连接；所述固液分离装置的出口与干燥机的物料入口之间以管路连接。
作为上述技术方案的进一步改进，所述蒸发装置的物料出口与干燥机的物料入口之间的管路上设有螺旋给料机；所述螺旋给料机的入口与蒸发装置的物料的出口连接；所述螺旋给料机的出口与干燥机的物料的入口连接。
作为上述技术方案的进一步改进，所述固液分离装置的出口与干燥机的物料入口之间的管路连接上设有螺旋给料机；所述螺旋给料机的入口与固液分离装置的出口连接；所述螺旋给料机的出口与干燥机的物料入口连接。
作为上述技术方案的进一步改进，所述干燥机的二次蒸汽出口与干燥蒸汽压缩机的入口之间的管路上设有除尘器，该除尘器的入口和出口分别连接干燥机的二次蒸汽出口和干燥蒸汽压缩机的入口；所述干燥机的物料出口设有真空隔料仓，连接该真空隔料仓的入口；所述真空隔料仓的出口产出干燥后的固体。
本发明还公开了一种使用上述装置的蒸发结晶干燥方法，其采用的技术方案是：原料通过蒸发装置蒸发，经过固液分离装置分离后产生的被蒸发浓缩后的物料，利用螺旋给料机进入干燥机进行低温干燥；干燥产生的二次蒸汽经过除尘器除尘后，进入干燥蒸汽压缩机进行压缩；经过干燥蒸汽压缩机压缩后的二次蒸汽，与蒸发装置产生的二次蒸汽混合，进入到蒸发蒸汽压缩机，进行再次压缩，经过再次压缩后的二次蒸汽一部分进入蒸发装置，另一部分进入干燥机。
作为上述技术方案的进一步改进，所述干燥蒸汽压缩机压缩后的二次蒸汽与蒸发装置产生的二次蒸汽温度相同，压力相同；所述蒸发蒸汽压缩机再次压缩后的二次蒸汽根据换热面积及传热系统自动分配流量进入蒸发装置和干燥机。
作为上述技术方案的进一步改进，所述干燥机产生的二次蒸汽经过两级压缩后重新进入干燥机与物料换热，达到40-50℃的传热温差。
本发明的有益效果如下。
1、通过干燥蒸汽压缩机与蒸发蒸汽压缩机的耦合，把干燥过程产生的二次蒸汽压缩升温，回收热量再利用，整个蒸发干燥系统热量平衡，不需要外加生蒸汽，还节省了干燥过程产生的二次蒸汽的冷凝设备，大幅度降低了能耗，优化了热能的利用，提高了干燥的传热温差，解决了现有技术的干燥机温差不足、需要大量生蒸汽的问题。
2、利用蒸发与干燥相结合，先蒸发结晶，后对物料进行低温干燥，不仅能使原液浓缩结晶干燥，把结晶盐分离出来，而且能使得原液全部得到固液分离，达到废水零排放，还能实现水资源的回收利用，尤其解决了有机废水的有机物富集，固液分离装置分离后的母液需要外排的问题。
附图说明
图1为本发明实施例的示意图。
具体实施方式
为了使本技术领域的技术人员更好地理解本技术方案，下面结合附图和实施例对本发明作进一步说明。文中所提到的所有连接关系，并非单指组件直接相连，而是采用该技术领域内的技术手段相连，或可根据实际情况，通过添加或减少连接附件，来组成更优的连接结构。
如图1所示的一种蒸发结晶干燥一体化装置，包括蒸发装置、固液分离装置、螺旋给料机、干燥机、真空隔料仓、除尘器、蒸发蒸汽压缩机和干燥蒸汽压缩机，其中蒸发装置的二次蒸汽出口接入蒸发蒸汽压缩机入口，蒸发蒸汽压缩机出口接入蒸发装置和干燥机的蒸汽入口，蒸发装置设有原料入口，蒸发装置的物料出口与固液分离装置的入口连接，固液分离装置的出口与螺旋给料机入口连接，螺旋给料机出口接入干燥机入口，干燥机二次蒸汽出口 与除尘器入口连接，除尘器出口接入到干燥蒸汽压缩机入口，干燥蒸汽压缩机出口接入蒸发蒸汽压缩机入口，干燥机的固体出口连接真空隔料仓入口，真空隔料仓设有干燥后的固体出口。其中蒸发装置为降膜蒸发器、升膜蒸发器、板式蒸发器、强制循环蒸发器的一种或多种组合。蒸发蒸汽压缩机和干燥蒸汽压缩机均为罗茨压缩机或离心鼓风机或高速离心压缩机。
该装置的蒸发结晶干燥方法如下，以下方法选用了较优方法，仅用于说明本发明的装置而非限制。
有机含盐废水经过初步过滤后，经预热器预热使冷凝水回收热量后，进入降膜蒸发器，经预浓缩后进入强制循环蒸发器，废水在强制循环蒸发器中不断循环蒸发浓缩，盐饱和结晶析出，随后排至固液分离装置(优选为离心机)进行固液分离，得到晶浆。由于废水中有机物含量在浓缩的过程中不断被富集，浓缩液变稠状物，离心困难，若不做处理会影响到正常的结晶分离。现有技术为返回系统前端再氧化，这样会导致浓缩液带走部分热量，系统能量不平衡，且浓缩液中盐分含量大，氧化困难。因此选用干燥工艺对稠状浓缩液进行干燥脱水，使有机物与水份分离。其中，干燥机使用空心浆叶干燥器作低温蒸发干燥，稠状浓缩液在较热状态下经过螺旋给料机，进入干燥机闪蒸，然后再利用从蒸发蒸汽压缩机分配过来的蒸汽与稠状浓缩液进行换热，使稠状浓缩液失水逐渐固化，从而达到干燥的目的。而在空心浆叶干燥器中脱离稠状浓缩液的二次蒸汽，经过干燥蒸汽压缩机作一级压缩后，使其达到蒸发蒸汽压缩机进口相同的温度与压力后，进入到蒸发蒸汽压缩机进行二级压缩，进一步提升二次蒸汽的温度，经过二级压缩后的蒸汽与空心浆叶干燥器内的稠状浓缩液的换热温差可达到40-50℃。干燥利用了干燥蒸汽压缩机与蒸发蒸汽压缩机对蒸汽再压缩，回收了干燥产生的二次蒸发，使系统的热量不被带走，保证了系统蒸发与干燥的热平衡。
空心浆叶干燥器产生的二次蒸汽带有较多的微小颗粒及飞沫，所以先进入到除尘器过滤，再进入到干燥蒸汽压缩机。空心浆叶干燥器由于是低温干燥，内部为负压，故使用真空隔料仓，定期切断空心浆叶干燥器，把真空隔料仓的物料放出来。
通过蒸发器与干燥机的耦合，优化了热能的利用，在不改变蒸发系统的处理能力前提的情况下，增加进入蒸发蒸汽压缩机的蒸汽量，从而利用干燥产生的低温蒸汽，大大降低了能耗。蒸发蒸汽压缩机与干燥蒸汽压缩机配合使用，降低了干燥蒸汽压缩机的温升要求，使得蒸发结晶与干燥一体化。
降膜蒸发器、强制循环蒸发器和空心浆叶干燥器产生的冷凝水作为热介质经预热器对有机含盐废水进行换热回收热量后，得到低温回用水。
通过本装置处理有机含盐废水或其他原料，能实现废水零排放，同时还能实现水资源的回收利用。

Claims (10)

  1. 一种蒸发结晶干燥一体化装置，其特征在于：主要包括蒸发蒸汽压缩机、干燥蒸汽压缩机和干燥机；所述干燥机二次蒸汽的出口与干燥蒸汽压缩机的入口之间以管路连接；所述干燥蒸汽压缩机的出口与蒸发蒸汽压缩机的入口连接；所述蒸发蒸汽压缩机的出口与干燥机的蒸汽入口连接。
  2. 根据权利要求1所述的一种蒸发结晶干燥一体化装置，其特征在于：所述蒸发蒸汽压缩机的入口前设有蒸发装置，该蒸发装置的二次蒸汽出口与干燥蒸汽压缩机的出口一并连接蒸发蒸汽压缩机的入口；所述蒸发蒸汽压缩机的出口还连接蒸发装置的蒸汽入口；所述蒸发装置设有原料入口，用于原料的进料；所述蒸发装置的物料出口与干燥机的物料入口之间以管路连接。
  3. 根据权利要求2所述的一种蒸发结晶干燥一体化装置，其特征在于：所述蒸发装置为升膜蒸发器、降膜蒸发器、强制循环蒸发器的一种或多种组合。
  4. 所述蒸发装置的物料出口与干燥机的物料入口之间的管路设有固液分离装置；所述固液分离装置的入口与蒸发装置的物料出口连接；所述固液分离装置的出口与干燥机的物料入口之间以管路连接。
  5. 所述蒸发装置的物料出口与干燥机的物料入口之间的管路上设有螺旋给料机；所述螺旋给料机的入口与蒸发装置的物料的出口连接；所述螺旋给料机的出口与干燥机的物料的入口连接。
  6. 根据权利要求4所述的一种蒸发结晶干燥一体化装置，其特征在于：所述固液分离装置的出口与干燥机的物料入口之间的管路连接上设有螺旋给料机；所述螺旋给料机的入口与固液分离装置的出口连接；所述螺旋给料机的出口与干燥机的物料入口连接。
  7. 根据权利要求5或6所述的一种蒸发结晶干燥一体化装置，其特征在于：所述干燥机的二次蒸汽出口与干燥蒸汽压缩机的入口之间的管路上设有除尘器，该除尘器的入口和出口分别连接干燥机的二次蒸汽出口和干燥蒸汽压缩机的入口；所述干燥机的物料出口设有真空隔料仓，连接该真空隔料仓的入口；所述真空隔料仓的出口产出干燥后的固体。
  8. 一种使用权利要求1至7中任一权利要求所述的蒸发结晶干燥一体化装置的蒸发结晶干燥方法，其特征在于：原料通过蒸发装置蒸发，经过固液分离装置分离后产生的被蒸发浓缩后的物料，利用螺旋给料机进入干燥机进行低温干燥；干燥产生的二次蒸汽经过除尘器除尘后，进入干燥蒸汽压缩机进行压缩；经过干燥蒸汽压缩机压缩后的二次蒸汽，与蒸发装置产生的二次蒸汽混合，进入到蒸发蒸汽压缩机，进行再次压缩，经过再次压缩后的二次蒸汽一部分进入蒸发装置，另一部分进入干燥机。
  9. 根据权利要求8所述的蒸发结晶干燥方法，其特征在于：所述干燥蒸汽压缩机压缩后的二次蒸汽与蒸发装置产生的二次蒸汽温度相同，压力相同；所述蒸发蒸汽压缩机再次压缩后的二次蒸汽根据换热面积及传热系统自动分配流量进入蒸发装置和干燥机。
  10. 根据权利要求9所述的蒸发结晶干燥方法，其特征在于：所述干燥机产生的二次蒸汽经过两级压缩后重新进入干燥机与物料换热，达到40-50℃的传热温差。
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