CN101830554B - Method for improving oxygen utilization rate of supercritical water oxidation system - Google Patents
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- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 82
- 239000001301 oxygen Substances 0.000 title claims abstract description 81
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 78
- 238000009284 supercritical water oxidation Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 67
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 238000006243 chemical reaction Methods 0.000 claims abstract description 35
- 238000001704 evaporation Methods 0.000 claims abstract description 28
- 150000003839 salts Chemical class 0.000 claims abstract description 16
- 239000012530 fluid Substances 0.000 claims abstract description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 24
- 230000008020 evaporation Effects 0.000 claims description 16
- 239000007789 gas Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 6
- 235000011089 carbon dioxide Nutrition 0.000 claims 4
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 claims 1
- 238000001816 cooling Methods 0.000 claims 1
- 239000010808 liquid waste Substances 0.000 claims 1
- 239000010815 organic waste Substances 0.000 abstract description 11
- 238000004064 recycling Methods 0.000 abstract description 3
- 230000006837 decompression Effects 0.000 abstract 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 10
- 239000001569 carbon dioxide Substances 0.000 description 8
- 239000005416 organic matter Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 5
- 230000008021 deposition Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 230000008018 melting Effects 0.000 description 3
- 238000002844 melting Methods 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- -1 oxygen peroxide Chemical class 0.000 description 3
- 239000012266 salt solution Substances 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 150000007522 mineralic acids Chemical class 0.000 description 1
- 239000012454 non-polar solvent Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000009279 wet oxidation reaction Methods 0.000 description 1
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Abstract
本发明涉及一种提高超临界水氧化系统氧气利用率的方法。过量的氧气和经预热的有机废液从蒸发壁反应器上部注入混合并进行超临界水氧化反应，蒸发水从蒸发壁反应器侧面注入，从而在反应器内形成上部为超临界温度反应区而下部为亚临界温度溶盐区。反应剩余的氧气从超临界温度区向下流动到亚临界温度溶盐区的过程中，一部分氧气析出并循环到反应器上部的超临界温度区而形成氧气内循环利用；反应后的流体经过冷凝和减压进入高压气液分离器，被亚临界水溶解并携带流出反应器的氧气，通过高压气液分离器分离后重新注入反应器而形成外循环利用。本发明通过提高氧气的利用率而显著降低过氧量系数，提高超临界水氧化系统运行的经济性。
The invention relates to a method for improving the oxygen utilization rate of a supercritical water oxidation system. Excess oxygen and preheated organic waste liquid are injected from the upper part of the evaporating wall reactor to mix and carry out supercritical water oxidation reaction, and the evaporating water is injected from the side of the evaporating wall reactor to form a supercritical temperature reaction zone in the upper part of the reactor The lower part is the subcritical temperature salt-dissolving zone. During the process of the remaining oxygen in the reaction flowing downward from the supercritical temperature zone to the subcritical temperature molten salt zone, a part of oxygen is precipitated and circulated to the supercritical temperature zone on the upper part of the reactor to form an internal circulation of oxygen; the reacted fluid is condensed And the decompression enters the high-pressure gas-liquid separator, is dissolved by subcritical water and carries the oxygen flowing out of the reactor, is separated by the high-pressure gas-liquid separator and reinjected into the reactor to form an external recycling. The invention significantly reduces the coefficient of peroxygen by increasing the utilization rate of oxygen, and improves the economical efficiency of the operation of the supercritical water oxidation system.
Description
一、技术领域 1. Technical field
本发明属于有机废物处理领域，特别涉及一种提高超临界水氧化系统氧气利用率的方法。The invention belongs to the field of organic waste treatment, in particular to a method for improving the oxygen utilization rate of a supercritical water oxidation system.
二、背景技术 2. Background technology
超临界水氧化(Supercritical Water Oxidation)技术是一种新型的处理有机废物及回收能量和纯CO2的技术。该技术是在超过水的临界点(T＝374℃，P＝22.1MPa)的高温高压条件下，以氧气或其他氧化剂，将有机物进行“燃烧”氧化的方法。超临界水具有类似液体的密度、溶解能力和良好的流动性，是一种非极性溶剂，同时又具有类似气体的扩散系数和低黏度。在超临界水中，气液两相的界面消失，有机物和O2在超临界水中完全互溶，形成均一相体系，反应速度大大加快。在小于1分钟甚至几秒的反应停留时间内，99.99％以上的有机物迅速燃烧氧化成CO2、H2O和无机盐等无毒无害的终端产物，同时氧化反应过程中会释放出大量的热能。Supercritical Water Oxidation technology is a new technology for treating organic waste and recovering energy and pure CO 2 . This technology is a method of "burning" and oxidizing organic matter with oxygen or other oxidants under high temperature and high pressure conditions exceeding the critical point of water (T=374°C, P=22.1MPa). Supercritical water has a liquid-like density, solubility and good fluidity. It is a non-polar solvent, and it also has a gas-like diffusion coefficient and low viscosity. In supercritical water, the gas-liquid two-phase interface disappears, organic matter and O2 are completely soluble in supercritical water, forming a homogeneous phase system, and the reaction speed is greatly accelerated. In the reaction residence time of less than 1 minute or even a few seconds, more than 99.99% of the organic matter is rapidly burned and oxidized into non-toxic and harmless terminal products such as CO 2 , H 2 O and inorganic salts, and a large amount of carbon dioxide will be released during the oxidation reaction. thermal energy.
超临界水氧化技术的高温、高压、高氧浓度等特殊反应条件及无机盐在超临界水中几乎不溶的特性，使得反应器的腐蚀及堵塞问题阻碍了该技术发展及推广应用。采用蒸发壁反应器能有效缓解反应器内的腐蚀和盐沉积问题。蒸发壁反应器一般由承压外壳和多孔内壳组成，蒸发水从反应器侧面注入，通过多孔内壳渗入到反应器内并在多孔内壁形成一层亚临界水膜，水膜能阻止无机酸与壁面的接触并能溶解在超临界温度反应区析出的无机盐，从而解决了反应器内的腐蚀和盐沉积问题。The special reaction conditions such as high temperature, high pressure, and high oxygen concentration of supercritical water oxidation technology and the almost insoluble characteristics of inorganic salts in supercritical water make the corrosion and blockage of the reactor hinder the development and application of this technology. The use of evaporating wall reactors can effectively alleviate the problems of corrosion and salt deposition in the reactor. The evaporating wall reactor is generally composed of a pressure-bearing outer shell and a porous inner shell. Evaporating water is injected from the side of the reactor, penetrates into the reactor through the porous inner shell, and forms a subcritical water film on the porous inner wall. The water film can prevent inorganic acids from The contact with the wall surface can dissolve the inorganic salt precipitated in the supercritical temperature reaction zone, thereby solving the problems of corrosion and salt deposition in the reactor.
应用于超临界水氧化反应的氧化剂一般有空气、氧气、双氧水、臭氧等，其中以氧气作为氧化剂的经济性最好。在利用蒸发壁反应器的超临界水氧化系统中，氧气消耗所需费用占总耗资的70％以上，且随着过氧量系数的增加，系统运行成本也显著的增加。但是为了保证有机物的完全降解，过氧量系数一般在1.5-3之间，反应后的流体含有大量未利用的氧气。The oxidizing agents used in the supercritical water oxidation reaction generally include air, oxygen, hydrogen peroxide, ozone, etc., among which oxygen is the most economical as the oxidizing agent. In a supercritical water oxidation system using an evaporating wall reactor, the cost of oxygen consumption accounts for more than 70% of the total cost, and with the increase of the oxygen peroxide coefficient, the operating cost of the system also increases significantly. However, in order to ensure the complete degradation of organic matter, the oxygen peroxide coefficient is generally between 1.5-3, and the fluid after the reaction contains a large amount of unused oxygen.
因此，过高的过氧量系数是造成超临界水氧化系统运行成本较高的原因。Therefore, the high peroxygen coefficient is the reason for the high operating cost of the supercritical water oxidation system.
在目前国内外的超临界水氧化系统中，提高氧气利用率的方法还未见报道。如US4822497“湿式氧化工艺中固体分离的方法”，其在釜式反应器中建立上部超临界温度反应区和下部亚临界温度溶盐区，在上部超临界温度反应区析出的无机盐沉淀在下部亚临界温度区被溶解排出，反应后的超临界流体逆流返回到反应器上部排出，但该专利没有提出如何在反应器内实现氧气的循环利用。涉及蒸发壁反应器的专利中只侧重解决反应器内的腐蚀和盐沉积问题，但都未提出如何在蒸发壁反应器内外实现氧气的循环利用，如US5387398“带有壁面边界层流动控制导管的超临界水氧化反应器”和US5571423“超临界水氧化的装置和工艺”等。此外，由于超临界水氧化系统都在过氧量系数下运行，反应后的流体必然携带高浓度的氧气，因此，回收反应后的剩余氧气是提高系统运行的经济性必然选择。In the current supercritical water oxidation system at home and abroad, the method of improving the utilization rate of oxygen has not been reported yet. For example, US4822497 "Method for solid separation in wet oxidation process", which establishes an upper supercritical temperature reaction zone and a lower subcritical temperature salt melting zone in a tank reactor, and the inorganic salt precipitated in the upper supercritical temperature reaction zone is precipitated in the lower part The subcritical temperature zone is dissolved and discharged, and the supercritical fluid after the reaction is returned to the upper part of the reactor and discharged, but this patent does not propose how to realize the recycling of oxygen in the reactor. Patents related to evaporating wall reactors only focus on solving the problems of corrosion and salt deposition in the reactor, but do not propose how to realize the recycling of oxygen inside and outside the evaporating wall reactor, such as US5387398 "with wall boundary layer flow control conduit Supercritical Water Oxidation Reactor" and US5571423 "Supercritical Water Oxidation Device and Process", etc. In addition, because the supercritical water oxidation system operates under the oxygen peroxide coefficient, the fluid after the reaction must carry a high concentration of oxygen. Therefore, the recovery of the remaining oxygen after the reaction is an inevitable choice to improve the economy of the system operation.
三、发明内容 3. Contents of the invention
一种提高超临界水氧化系统氧气利用率的方法，本发明针对超临界水氧化系统运行中氧气成本高而利用率低的问题，提出通过在蒸发壁反应器内外实现氧气的双循环利用，来提高超临界水氧化系统氧气利用率，进而提高系统运行的经济性。本发明通过以下方式实现：A method for improving the utilization rate of oxygen in a supercritical water oxidation system. The invention aims at the problem of high cost and low utilization rate of oxygen in the operation of a supercritical water oxidation system, and proposes to achieve double cycle utilization of oxygen inside and outside the evaporation wall reactor. Improve the oxygen utilization rate of the supercritical water oxidation system, thereby improving the economy of system operation. The present invention is realized in the following ways:
一种提高超临界水氧化系统氧气利用率的方法，该系统包括氧气罐、废水储罐、纯水储罐、氧气增压泵、废液增压泵、蒸发水增压泵、废水加热器、上支路蒸发水加热器、氧气混合器、蒸发壁反应器、氧气循环泵、换热器、减压阀、高压气液分离器、背压阀和常压气液分离器，该方法的步骤如下：A method for improving the oxygen utilization rate of a supercritical water oxidation system, the system comprising an oxygen tank, a waste water storage tank, a pure water storage tank, an oxygen booster pump, a waste liquid booster pump, an evaporated water booster pump, a waste water heater, Upper branch evaporation water heater, oxygen mixer, evaporation wall reactor, oxygen circulation pump, heat exchanger, pressure reducing valve, high pressure gas-liquid separator, back pressure valve and normal pressure gas-liquid separator, the steps of the method as follows:
(1)有机废液升压至23-30MPa，并预热到350-450℃，与相同压力条件下的氧气从蒸发壁反应器上部注入混合，进行超临界水氧化反应，超临界水氧化反应温度为400-650℃，停留时间为5-60s。(1) The organic waste liquid is boosted to 23-30MPa, preheated to 350-450°C, and mixed with oxygen under the same pressure from the upper part of the evaporation wall reactor to carry out supercritical water oxidation reaction, supercritical water oxidation reaction The temperature is 400-650°C, and the residence time is 5-60s.
(2)蒸发水加压至23-30MPa，分两支路从反应器侧面注入，上支路蒸发水温度为250-370℃，下支路蒸发水保持常温，在反应器内形成上部为超临界温度反应区和下部为亚临界温度溶盐区，反应剩余的氧气从超临界温度反应区向下流动到亚临界温度溶盐区的过程中，一部分氧气析出并循环到反应器上部而而被重新利用。(2) Evaporated water is pressurized to 23-30MPa, and injected from the side of the reactor in two branches. The temperature of the evaporated water in the upper branch is 250-370°C, and the evaporated water in the lower branch is kept at room temperature. The critical temperature reaction zone and the lower part are the subcritical temperature salt melting zone. During the process of the remaining oxygen flowing down from the supercritical temperature reaction zone to the subcritical temperature salt melting zone, a part of oxygen is precipitated and circulated to the upper part of the reactor to be absorbed. reuse.
(3)反应后的流体经换热器降温和减压阀降压后进入高压气液分离器，氧气从高压气液分离器上部排出并通过氧气循环泵升压后重新注入反应器而而被重新利用，水和二氧化碳的混合物则从高压气液分离器下部流出。(3) The reacted fluid enters the high-pressure gas-liquid separator after being cooled by the heat exchanger and depressurized by the pressure-reducing valve. For reuse, the mixture of water and carbon dioxide flows out from the lower part of the high-pressure gas-liquid separator.
(4)水和二氧化碳的混合物进入常压气液分离器，二氧化碳和水分别从常压气液分离器的上部出口和下部出口流出，并回收高浓度的二氧化碳。(4) The mixture of water and carbon dioxide enters the atmospheric pressure gas-liquid separator, and the carbon dioxide and water flow out from the upper outlet and the lower outlet of the atmospheric pressure gas-liquid separator respectively, and high-concentration carbon dioxide is recovered.
上述的一种提高超临界水氧化系统氧气利用率的方法，有机废液的浓度在3-20wt％；氧气的质量流量为有机废液中有机物完全氧化理论需氧量的1-3倍；蒸发水的质量流量为有机废液和氧气质量流量总和的1-4倍；上支路蒸发水和下支路蒸发水的质量流量比为0.3-1.5。In the method for improving the oxygen utilization rate of the supercritical water oxidation system, the concentration of the organic waste liquid is 3-20wt%; the mass flow rate of oxygen is 1-3 times of the theoretical oxygen demand for the complete oxidation of organic matter in the organic waste liquid; The mass flow of water is 1-4 times of the sum of the mass flow of organic waste liquid and oxygen; the mass flow ratio of evaporated water in the upper branch and evaporated water in the lower branch is 0.3-1.5.
上述的一种提高超临界水氧化系统氧气利用率的方法，高压气液分离器内的压力为2-20MPa，温度在20-150℃。In the above method for improving the oxygen utilization rate of the supercritical water oxidation system, the pressure in the high-pressure gas-liquid separator is 2-20MPa, and the temperature is 20-150°C.
上述的一种提高超临界水氧化系统氧气利用率的方法，氧气和经过预热的有机废水从蒸发壁反应器上部注入混合并进行超临界水氧化反应，反应释放出大量的热能，从而在反应器上部形成超临界温度反应区。与此同时，从蒸发壁反应器侧面注入亚临界温度的蒸发水。蒸发水通过多孔壁渗入到反应器内，并在多孔内壁形成一层保护性的水膜，水膜能避免反应器的腐蚀和盐沉积问题。蒸发水对反应器中心的超临界温度流体进行冷却，因此反应器下部形成亚临界温度溶盐区。A method for improving the oxygen utilization rate of the supercritical water oxidation system mentioned above, oxygen and preheated organic waste water are injected and mixed from the upper part of the evaporation wall reactor to carry out the supercritical water oxidation reaction, and the reaction releases a large amount of heat energy, thus in the reaction The upper part of the device forms a supercritical temperature reaction zone. At the same time, evaporated water at subcritical temperature is injected from the side of the evaporation wall reactor. Evaporated water penetrates into the reactor through the porous wall and forms a protective water film on the porous inner wall, which can avoid the corrosion and salt deposition problems of the reactor. The evaporated water cools the supercritical temperature fluid in the center of the reactor, so the lower part of the reactor forms a subcritical temperature molten salt zone.
同时，上支路蒸发水和下支路常温蒸发水存在200-350℃的温差，因此反应器上部的超临界温度反应区会迅速过渡到亚临界温度溶盐区。在反应器内的超临界温度反应区的流体与亚临界温度溶盐区的流体存在较大的密度差；同时在反应器内的亚临界温度溶盐区，水和氧气也存在较大密度差。因此，反应剩余的氧气从超临界温度反应区向下流动到亚临界温度溶盐区的过程中，一部分氧气析出并循环到反应器上部的超临界温度反应区而形成氧气内循环利用，另一部分氧气则溶解在亚临界水中而流出反应器。而反应生成的CO2与亚临界水密度差相差较小，且在亚临界水中的溶解度比O2高近10倍，因此CO2被亚临界水溶解而携带流出反应器。At the same time, there is a temperature difference of 200-350°C between the evaporated water in the upper branch and the normal temperature evaporated water in the lower branch, so the supercritical temperature reaction zone in the upper part of the reactor will quickly transition to the subcritical temperature salt solution zone. There is a large density difference between the fluid in the supercritical temperature reaction zone in the reactor and the fluid in the subcritical temperature salt solution zone; at the same time, there is a large density difference between water and oxygen in the subcritical temperature salt solution zone in the reactor . Therefore, when the remaining oxygen in the reaction flows downward from the supercritical temperature reaction zone to the subcritical temperature molten salt zone, part of the oxygen is precipitated and circulated to the supercritical temperature reaction zone on the upper part of the reactor to form an internal oxygen cycle, and the other part Oxygen is dissolved in subcritical water and flows out of the reactor. The density difference between the CO 2 produced by the reaction and the subcritical water is small, and the solubility in the subcritical water is nearly 10 times higher than that of O 2 , so the CO 2 is dissolved by the subcritical water and carried out of the reactor.
从反应器流出的流体主要成分为H2O、CO2和O2。由于CO2在高压气液分离器内的高压液态水中的溶解度比O2高近10倍，因此在高压气液分离器中，氧气富集在气相中而CO2则溶解在高压液态水中。The main components of the fluid flowing out of the reactor are H 2 O, CO 2 and O 2 . Since the solubility of CO2 in the high-pressure liquid water in the high-pressure gas-liquid separator is nearly 10 times higher than that of O2 , in the high-pressure gas-liquid separator, oxygen is enriched in the gas phase while CO2 is dissolved in the high-pressure liquid water.
本发明提出通过在蒸发壁反应器内外实现氧气的双循环利用，来提高超临界水氧化系统氧气利用率的方法，其能有效降低超临界水氧化系统中的过氧量系数，提高系统运行的经济性，因此具有广阔的应用前景。The present invention proposes a method for improving the oxygen utilization rate of the supercritical water oxidation system by realizing the double cycle utilization of oxygen inside and outside the evaporating wall reactor, which can effectively reduce the peroxygen coefficient in the supercritical water oxidation system and improve the operating efficiency of the system. Economical, so it has broad application prospects.
四、附图说明 4. Description of drawings
图1、本发明流程示意图。Fig. 1, schematic flow chart of the present invention.
图2、蒸发壁反应器结构图。Figure 2. Structural diagram of the evaporation wall reactor.
图1中：1为氧气罐、2为废水储罐、3为纯水储罐、4为氧气增压泵、5为废液增压泵、6为蒸发水增压泵、7为废水加热器、8为上支路蒸发水加热器、9为氧气混合器、10为蒸发壁反应器、11为氧气循环泵、12为换热器、13为减压阀、14为高压气液分离器、15为背压阀、16为常压气液分离器。In Figure 1: 1 is an oxygen tank, 2 is a waste water storage tank, 3 is a pure water storage tank, 4 is an oxygen booster pump, 5 is a waste liquid booster pump, 6 is an evaporated water booster pump, and 7 is a waste water heater , 8 is the upper branch evaporation water heater, 9 is the oxygen mixer, 10 is the evaporation wall reactor, 11 is the oxygen circulation pump, 12 is the heat exchanger, 13 is the pressure reducing valve, 14 is the high-pressure gas-liquid separator, 15 is a back pressure valve, and 16 is a normal pressure gas-liquid separator.
图2中：17为氧气入口、18为废液入口、19为上支路蒸发水入口、20为下支路蒸发水入口、21为多孔管、22为挡水环、23为承压外壳、24为反应器出口。In Fig. 2: 17 is an oxygen inlet, 18 is a waste liquid inlet, 19 is an upper branch evaporated water inlet, 20 is a lower branch evaporated water inlet, 21 is a porous tube, 22 is a water retaining ring, 23 is a pressure-bearing shell, 24 is the outlet of the reactor.
五、具体实施方式 5. Specific implementation
下面结合附图和发明人给出的一个具体实施例对本发明作进一步的说明。The present invention will be further described below in conjunction with the accompanying drawings and a specific embodiment given by the inventor.
废液储罐2中浓度为8wt％的有机废液经废液增压泵5升压至25MPa，并经过废液加热器7加热到400℃，从蒸发壁反应器10上部的废液入口18注入。氧气罐1中氧气经氧气增压泵4增压至25MPa，以2倍于有机物完全氧化的需氧量不经预热直接从蒸发壁反应器10上部的氧气入口17注入。在蒸发壁反应器10上部，氧气和有机物混合并进行超临界水氧化反应。纯水储罐3中的蒸发水以有机废液和氧气质量流量总和的3倍的流量经蒸发水增加泵6升压至25.1MPa后，分两支路从蒸发壁反应器10侧面注入。其中，上支路蒸发水经上支路蒸发水加热器8预热至350℃从上支路蒸发水入口19注入，而下支路蒸发水不经预热直接从下支路蒸发水入口20注入，上下两路蒸发水的质量流量比为1∶2。The organic waste liquid with a concentration of 8wt% in the waste
蒸发水通过承压外壳23和多孔管21之间的环隙内的挡水环22进行分区，分区的蒸发水经多孔管21渗入到反应器内并在多孔管21内壁形成一层亚临界的水膜，对多孔管21起到保护作用。蒸发壁反应器10内形成上部为超临界温度反应区和下部为亚临界温度溶盐区，反应剩余的氧气从超临界温度反应区向下流动到亚临界温度溶盐区的过程中，一部分氧气析出并循环到蒸发壁反应器10上部的超临界温度反应区而被重新利用，另一部分氧气则溶解在亚临界水中而流出反应器。The evaporated water is partitioned through the
反应后的流体经反应器出口24排出反应器，流体经换热器12降温至50℃，经减压阀13降压至12MPa进入高压气液分离器14。氧气从高压气液分离器14上部出口排出，经氧气循环泵11升压至25MPa后，与原氧气回路在氧气混合器9中混合并重新注入蒸发壁反应器10。高压水和二氧化碳的混合物从高压气液分离器14下部排出，经背压阀15降至常压后进入常压气液分离器16。二氧化碳和水分别从常压气液分离器16的上部出口和下部出口流出，并回收高浓度的二氧化碳气体。本发明的超临界水氧化系统稳定运行后，可逐渐降低氧气流量，直至氧气流量接近有机废液中有机物完全氧化的需氧量。The reacted fluid is discharged from the reactor through the
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| CN102787830B (en) * | 2012-08-17 | 2015-01-21 | 山东大学 | Method and device for exploiting deep sea combustible ice |
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