CN113149176A

CN113149176A - Catalytic wet oxidation reactor

Info

Publication number: CN113149176A
Application number: CN202110426829.8A
Authority: CN
Inventors: 张玉新; 傅重喜; 万彬; 邱地恒
Original assignee: Shaoguan Beitextile Technology Co ltd; Shanghai Yuke Environmental Engineering Co ltd
Current assignee: Shanghai Yuke Environmental Engineering Co ltd
Priority date: 2021-04-20
Filing date: 2021-04-20
Publication date: 2021-07-23

Abstract

The invention discloses a catalytic wet oxidation reactor, which relates to the technical field of wastewater treatment equipment and comprises an air compressor, a gas-liquid separator, a main pipeline, a liquid inlet pump, a circulating pump, a heat exchanger and a reaction kettle, wherein the liquid inlet pump, the circulating pump, the heat exchanger and the reaction kettle are sequentially arranged on the main pipeline; the air compressor is connected with the main pipeline, and the gas-liquid separator is connected with the heat exchanger. Through the optimization of whole set of system equipment configuration in this application for the lower of cost of capital equipment is more, and the waste water treatment trade in each field of application that can be extensive, and the treatment effeciency is high, the running cost is lower, and the cost is low, and the energy consumption still less, can also energy recuperation.

Description

Catalytic wet oxidation reactor

Technical Field

The invention relates to the technical field of wastewater treatment equipment, in particular to a catalytic wet oxidation reactor.

Background

Currently, most chemical enterprises in China generally adopt a mode of simply pretreating wastewater and then entering a biochemical tank for biochemical treatment in the aspect of wastewater treatment. Although the biochemical method is an industrial method with a mature technology and has low treatment cost, the industrial high-concentration organic wastewater has high toxicity, contains a plurality of organic matters which are difficult to biodegrade, has high COD concentration, contains a plurality of biological toxic substances and has complex components, so the wastewater treated by the method is difficult to obtain ideal effects. The traditional physical and chemical methods have a lot of defects in the aspects of removing the toxicity of the wastewater, improving the biodegradability of the wastewater and the like, and some physical pretreatment technologies can not completely degrade toxic components and can cause a series of problems of pollution transfer, secondary pollution and the like. Therefore, the traditional sewage biochemical treatment method cannot meet the requirements, and the high-efficiency treatment of the refractory high-concentration organic wastewater becomes one of the problems to be solved urgently in the domestic sewage treatment industry.

The wet oxidation technology can completely degrade or convert pollutants which are high in toxicity and difficult to biodegrade into easily degradable substances under the conditions of high temperature (120-320 ℃) and high pressure (0.5-20MPa), remove COD (chemical oxygen demand) in high-concentration organic wastewater, completely degrade toxic components in water, and perform biochemical treatment to achieve an ideal treatment effect, so that the problems are well solved, and the wet oxidation technology is widely applied to treatment of high-concentration small-flow industrial wastewater such as petrochemical waste alkali liquor, olefin production washing liquid, pesticide wastewater, medical wastewater and the like.

However, the traditional wet oxidation equipment has high equipment cost, high operation cost and poor oxidation effect.

Disclosure of Invention

The present invention aims to provide a catalytic wet oxidation reactor for solving the above technical problems.

The technical scheme adopted by the invention is as follows:

a catalytic wet oxidation reactor comprises an air compressor, a gas-liquid separator, a main pipeline, a liquid inlet pump, a circulating pump, a heat exchanger and a reaction kettle, wherein the liquid inlet pump, the circulating pump, the heat exchanger and the reaction kettle are sequentially arranged on the main pipeline; the air compressor is connected with the main pipeline, and the gas-liquid separator is connected with the heat exchanger.

Preferably, the gas-liquid separator is provided with a tail gas discharge port, a water outlet and a gas inlet, wherein the gas inlet is connected with the heat exchanger through a third branch pipeline.

Preferably, the reaction kettle comprises a kettle body and a catalyst mechanism arranged in the kettle body, the liquid inlet is arranged on one side of the kettle body, and the catalyst mechanism is positioned on the lower side of the liquid inlet.

As a further optimization, the reactor also comprises a heat conduction oil liquid inlet pipe and an electric heater, wherein the heat conduction oil liquid inlet pipe is arranged at the lower end of the kettle body, and the electric heater is arranged on the heat conduction oil liquid inlet pipe.

As a further optimization, the kettle further comprises a sewage draining outlet, and the sewage draining outlet is further arranged at the lower end of the kettle body.

As a further optimization, the reactor also comprises a heat conduction oil outlet pipe, and the other side of the kettle body is provided with the heat conduction oil outlet pipe.

Preferably, the upper end of the kettle body is provided with a pressure sensor interface and a temperature sensor interface.

Preferably, the kettle further comprises an exhaust pipe and a safety valve interface, wherein the exhaust pipe and the safety valve interface are arranged at the upper end of the kettle body.

Further preferably, the exhaust pipe is located around the pressure sensor port and the temperature sensor port.

As a further preference, the safety valve interface is located around the pressure sensor interface and the temperature sensor interface.

The technical scheme has the following advantages or beneficial effects:

according to the invention, through optimization of the configuration of the whole set of system equipment, the cost of main equipment is lower, the system can be widely applied to wastewater treatment industries in various fields, and the system has the advantages of high treatment efficiency, lower operation cost, low cost, less energy consumption and capability of recovering energy.

Drawings

FIG. 1 is a schematic diagram of the catalytic wet oxidation reactor of the present invention;

FIG. 2 is a schematic view of the structure of the reaction vessel in the present invention.

In the figure: 1. an air compressor; 2. a gas-liquid separator; 201. a tail gas discharge port; 202. a water outlet; 3. a main pipeline; 4. a liquid inlet pump; 5. a circulation pump; 6. a heat exchanger; 7. a reaction kettle; 701. a kettle body; 702. a liquid inlet; 703. a liquid outlet; 704. a circulating liquid port; 705. a catalyst mechanism; 706. a heat-conducting oil inlet pipe; 707. an electric heater; 708. a sewage draining outlet; 709. a heat conducting oil outlet pipe; 710. a pressure sensor interface; 711. a temperature sensor interface; 712. an exhaust pipe; 8. a liquid outlet pipeline; 9. a circulation line; 10. a third branch pipeline; 11. and a fourth branch pipeline.

Detailed Description

The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

In the description of the present invention, it should be noted that, as the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. appear, their indicated orientations or positional relationships are based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" as appearing herein are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should be noted that, unless otherwise explicitly stated or limited, the terms "mounted," "connected," and "connected" should be interpreted broadly, e.g., as being fixed or detachable or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

FIG. 1 is a schematic diagram of the catalytic wet oxidation reactor of the present invention; fig. 2 is a schematic structural diagram of a reaction kettle in the present invention, please refer to fig. 1 to 2, which illustrate a preferred embodiment, showing a catalytic wet oxidation reactor, including an air compressor 1, a gas-liquid separator 2, a main pipeline 3, and a liquid inlet pump 4, a circulating pump 5, a heat exchanger 6 and a reaction kettle 7 sequentially disposed on the main pipeline 3, wherein one side of the reaction kettle 7 is sequentially provided with a liquid inlet 702, a liquid outlet 703 and a circulating liquid port 704 from top to bottom, one end of the main pipeline 3 is connected with the liquid inlet 702, the liquid outlet 703 is connected with the heat exchanger 6 through a liquid outlet pipeline 8, the circulating liquid port 704 is connected with the main pipeline 3 through a circulating pipeline 9, and one end of the circulating pipeline 9 is located between the liquid inlet pump 4 and the circulating pump 5; the air compressor 1 is connected with the main pipeline 3, and the gas-liquid separator 2 is connected with the heat exchanger 6. In this embodiment, as shown in fig. 1, the other end of main pipeline 3 is located to feed liquor pump 4, a raw water is pumped into to main pipeline 3, the raw water enters heat exchanger 6 after through circulating pump 5 in, air compressor machine 1 is connected with main pipeline 3 through fourth pipeline 11 simultaneously, and fourth pipeline 11 is located between circulating pump 5 and the heat exchanger 6, when the raw water is pumped into to the pump, simultaneously through air compressor machine 1 to 3 interior pump-in air of main pipeline, the air heats up in entering heat exchanger 6 after mixing with the raw water, and simultaneously, the raw water in the reation kettle gets into main pipeline 3 through circulating line 9, and realize oxygen and raw water intensive mixing in the air under circulating pump 5 and air compressor machine 1's effect. After reaching the preset decomposition reaction initial temperature, the mixture is sent into a reaction kettle 7 for reaction. Part of the steam-water mixture generated in the reaction process enters the heat exchanger 6 through the liquid outlet pipe 8 for cooling, then is subjected to gas-liquid separation through the gas-liquid separator 2, carbon dioxide and nitrogen generated after separation are discharged into the air, and raw water can be discharged after being purified to reach the standard. In this embodiment, the air compressor machine 1 compressed air supplies gas to mix with the circulation liquid, can make the more abundant that oxidant oxygen in liquid and the air mixes, can further strengthen the reaction effect. Further, as a preferred embodiment, the gas-liquid separator 2 is provided with a tail gas discharge port 201, a water outlet 202 and an air inlet, wherein the air inlet is connected with the heat exchanger 6 through a third branch pipeline 10. In this embodiment, carbon dioxide and nitrogen in the gas-liquid separator 2 are discharged from the tail gas discharge port 201, and separated water is discharged from the water outlet 202.

Further, as a preferred embodiment, the reaction kettle 7 includes a kettle body 701 and a catalyst mechanism 705 disposed in the kettle body 701, the liquid inlet 702 is disposed on one side of the kettle body 701, and the catalyst mechanism 705 is disposed on the lower side of the liquid inlet 702. Catalyst mechanism 705 in this embodiment includes catalyst holding box and fills the catalyst in catalyst holding box, is equipped with a plurality of separating tanks in the catalyst holding box, and the catalyst separately sets up in catalyst holding box, and catalyst holding box provides a reaction liquid circulation channel for catalyst and reaction liquid contact are more abundant, and the reaction goes on more abundant. Wherein, catalyst holds the box and is connected with one side inner wall detachably of cauldron body 701, has the opening design in the upper end of catalyst holds the box to and the downside is provided with the filter screen interception, is convenient for raw water to get into and flows out after the catalyst reaction. The catalyst containing box is arranged right below the liquid inlet 702, so that raw water can directly enter the catalyst containing box, and catalytic reaction is facilitated.

Further, as a preferred embodiment, the reaction kettle 7 further comprises a heat conduction oil inlet pipe 706 and an electric heater 707, the heat conduction oil inlet pipe 706 is arranged at the lower end of the kettle body 701, and the electric heater 707 is arranged on the heat conduction oil inlet pipe 706. In this embodiment, an oil conduit is disposed inside the kettle 701, and the oil conduit is located in a middle gap of the catalyst accommodating box, and bends at a suitable position to penetrate out from the middle gap of the catalyst accommodating box to be connected with the kettle 701. In other preferred embodiments, the oil conduit may be coiled around the inner wall of the vessel 701 or wrapped around the outside of the catalyst containment vessel. In this embodiment, one end of the oil conduit is connected to the heat transfer oil inlet pipe 706, and the other end is connected to the heat transfer oil outlet pipe 709, and the hot oil heated by the electric heater 707 enters the oil conduit in the kettle body 701 to exchange heat with the raw water in the kettle body 701 to heat the raw water, so that the reaction effect is better. In this embodiment, the water-gas mixture generated after the raw water reaction is circulated under the action of the circulation pump 5, and the flow of the fluid causes the heat given by the electric heater 707 and the heat given by the heat exchanger 6 to be fully mixed by the fluid, so that the reaction liquid is heated more uniformly, and the reaction effect is better. And the fluid is circulated, the energy of the heat exchanger 6 is reused, the energy is recycled, the energy consumption of the system is reduced, and the operation cost is lower. In this embodiment, through oil pipe's design for heating fluid (hot oil) with by the separation of heating fluid (raw water), make the reactor no longer suffer from the puzzlement of revealing the problem, still economic environmental protection more.

Further, as a preferred embodiment, the reaction kettle 7 further comprises a drain 708, and the lower end of the kettle body 701 is further provided with the drain 708. In this embodiment, the precipitate generated in the reaction process of the raw water is discharged through the drain 708, and the solenoid valve is provided on the drain 708 for automatically controlling the opening and closing of the drain 708.

Further, as a preferred embodiment, the reaction kettle 7 further includes a heat conduction oil outlet pipe 709, and the other side of the kettle body 701 is provided with the heat conduction oil outlet pipe 709.

Further, as a preferred embodiment, the upper end of the kettle 701 is provided with a pressure sensor interface 710 and a temperature sensor interface 711. In this example, the design pressure and design temperature of the reactor were both reduced, so that the cost of the reactor was only 1/4, which is the equivalent cost of the equipment available on the market.

Further, as a preferred embodiment, the reaction kettle 7 further comprises an exhaust pipe 712 and a safety valve interface, and the upper end of the kettle body 701 is provided with the exhaust pipe 712 and the safety valve interface. The relief valve interface is located on one side of the exhaust pipe 712. In this embodiment, the exhaust pipe 712 may be periodically opened or closed to control the pressure inside the kettle 701.

Further, as a preferred embodiment, exhaust 712 is located around pressure sensor port 710 and temperature sensor port 711. As shown in fig. 1, the exhaust pipe 712 is specifically disposed between the pressure sensor port 710 and the temperature sensor port 711.

As a further preference, the safety valve interface is located around the pressure sensor interface and the temperature sensor interface. As shown in fig. 1, the relief valve interface is specifically disposed between the pressure sensor interface 710 and the temperature sensor interface 711.

In this application, through the optimization to the reactor configuration and the change of reation kettle 7 structure for oxidant (oxygen in the air) and reaction liquid, catalyst contact more abundant, select suitable temperature, pressure and catalyst, can get rid of the organic matter more than 95%, great improvement the efficiency of handling.

In this application, through mutually supporting between circulating pump 5, electric heater 707 and the heat exchanger 6, realized convection heat transfer, improved heat transfer efficiency for reaction liquid is heated more evenly, has further improved the reaction effect. Meanwhile, the energy of the treated liquid is recycled, so that the operation cost is further saved.

In this application, through the design to 7 inside circulation passageways of reation kettle for catalyst and reaction liquid contact more abundant, the reaction effect is better.

In the present application, the reactor has a lower operating temperature and operating pressure than conventional wet oxidation, and the pressure rating of the reactor is reduced, thereby reducing the cost to 1/4.

While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the invention.

Claims

1. A catalytic wet oxidation reactor is characterized by comprising an air compressor, a gas-liquid separator, a main pipeline, a liquid inlet pump, a circulating pump, a heat exchanger and a reaction kettle, wherein the liquid inlet pump, the circulating pump, the heat exchanger and the reaction kettle are sequentially arranged on the main pipeline; the air compressor is connected with the main pipeline, and the gas-liquid separator is connected with the heat exchanger.

2. The catalytic wet oxidation reactor according to claim 1, wherein the gas-liquid separator is provided with a tail gas discharge port, a water outlet and a gas inlet, wherein the gas inlet is connected with the heat exchanger through a third branch pipe.

3. The catalytic wet oxidation reactor according to claim 1, wherein the reaction vessel comprises a vessel body and a catalyst mechanism disposed in the vessel body, the liquid inlet is disposed at one side of the vessel body, and the catalyst mechanism is disposed at a lower side of the liquid inlet.

4. The catalytic wet oxidation reactor according to claim 3, further comprising a heat transfer oil inlet pipe and an electric heater, wherein the heat transfer oil inlet pipe is provided at a lower end of the vessel body, and the electric heater is provided on the heat transfer oil inlet pipe.

5. The catalytic wet oxidation reactor as set forth in claim 3, further comprising a drain outlet, wherein the drain outlet is further provided at a lower end of the vessel body.

6. The catalytic wet oxidation reactor according to claim 3, further comprising a heat transfer oil outlet pipe, wherein the heat transfer oil outlet pipe is provided at the other side of the vessel body.

7. The catalytic wet oxidation reactor according to claim 3, wherein the upper end of the vessel body is provided with a pressure sensor port and a temperature sensor port.

8. The catalytic wet oxidation reactor of claim 7, further comprising an exhaust pipe and a safety valve interface, wherein the exhaust pipe and the safety valve interface are disposed at an upper end of the vessel body.

9. The catalytic wet oxidation reactor of claim 8, wherein the exhaust pipe is positioned around the pressure sensor interface and the temperature sensor interface.

10. The catalytic wet oxidation reactor of claim 8, wherein said relief valve interface is located around said pressure sensor interface and said temperature sensor interface.