CN110066083B - Sludge pyrolysis recycling system and pyrolysis method - Google Patents

Abstract

The embodiment of the invention provides a sludge pyrolysis recycling system, which adopts solid porcelain balls or quartz sand as a heat carrier to rapidly transfer heat to sludge according to the material and pyrolysis characteristics of the sludge, and comprises a spiral pyrolysis reactor which is specially designed and can realize forced mixing and rapid heat transfer of the sludge. The invention adopts the solid heat carrier and sludge to mix and heat directly, and has high heat efficiency and uniform heating compared with an indirect heating mode; the spiral blades and the stirring blades are reasonably arranged in the pyrolysis reactor, so that the full mixing and the rapid heat transfer of the sludge and the heat carrier can be realized, the pyrolysis reaction rate is high, the system processing capacity is high, the coking problem caused by uneven sludge stirring is effectively solved, and the long-term stable operation of the system is realized; the waste heat flue gas pre-drying sludge is recycled, so that the energy grading utilization is realized, the energy consumption can be effectively reduced, and the energy utilization efficiency of the system is improved. The embodiment of the invention also provides a method for pyrolyzing the sludge by adopting the sludge pyrolysis recycling system.

Description

Sludge pyrolysis resource utilization system and pyrolysis method

Technical field

The invention belongs to the technical field of harmlessness and resource utilization of sewage treatment by-product sludge, and particularly relates to a sludge pyrolysis resource utilization system. The present invention also provides a sludge pyrolysis method using the above-mentioned sludge pyrolysis resource utilization system.

Background technique

Sludge is a by-product of sewage treatment production. Its composition is extremely complex. In addition to containing a large amount of water, it also contains nitrogen, phosphorus and other nutrients, heavy metals and organic matter. If the sludge is directly discharged into the environment, it will cause harm to the environment. Harmful, and the organic matter contained in the sludge is not utilized, which is a serious waste. Current sludge treatment technologies mainly include landfill, composting, drying and incineration, and pyrolysis. Among them, sludge pyrolysis is an important means for sludge resource utilization. Sludge pyrolysis is the integration of drying and thermal decomposition of sludge under certain temperature and anoxic conditions. Under heating conditions, the sludge is converted into gas and solid phases, and the gas is then converted into gas and liquid through condensation. Two-phase, the sludge is finally converted into three phase substances: gas, liquid and solid. The gas obtained by sludge conversion is rich in gaseous hydrocarbons, hydrogen, carbon monoxide and other combustible gases. Oil resources can be obtained from the liquid after oil-water separation. Therefore, sludge pyrolysis technology can effectively achieve the reduction, harmlessness and resource utilization of sludge, and is increasingly widely used.

At present, sludge pyrolysis technology is mainly divided into continuous type and intermittent type. Among them: intermittent pyrolysis technology has small processing scale, short running time and limited application scope; continuous pyrolysis technology mainly adopts the rotating kiln or rotary kiln type with outer wall heating. The spiral stirring pyrolysis process has strong processing capacity and is suitable for industrial applications. However, during the continuous pyrolysis process of sludge, the sludge materials tend to adhere to lumps, making it difficult to break up the materials and transfer heat, leading to uneven heating and reactions. Problems such as insufficient or long response time lead to reduced system efficiency. In view of the above-mentioned shortcomings of the existing technology, it is urgent to develop a pyrolysis process that is conducive to sludge mixing and heat transfer to achieve efficient and continuous pyrolysis treatment of sludge and meet the needs of industrial applications.

Contents of the invention

The present invention aims to solve the problems existing in the existing sludge pyrolysis technology such as uneven heating, low thermal efficiency, and insufficient system processing capacity. It provides a new sludge pyrolysis reaction system and pyrolysis method, which adopts internal heating technology. Using solid heat carrier as reaction heat transfer carrier and based on optimized pyrolysis reactor design, it has the characteristics of uniform heating, high efficiency and low price, and easy industrialization.

In order to solve the aforementioned technical problems, embodiments of the present invention provide a sludge pyrolysis resource utilization system, which includes a pre-drying device, a feed carrier hopper, a discharge carrier hopper, a pyrolysis reactor, a hot smoke furnace, and a heating riser. Condenser, oil-water separator, cyclone separator and slag discharger, including:

The pyrolysis reactor includes a reactor barrel with a hollow truncated cone structure with a large top and a small bottom. A rotating shaft is installed at the central axis of the reactor barrel; spiral blades are coiled and fixed on the rotating shaft, and the spiral The leaves stir with the rotation of the rotating shaft; the pre-drying device pre-dries the sludge raw materials, and the pre-dried sludge is sent to the pyrolysis reactor; the feed carrier hopper is located in the pyrolysis reactor. Above the reactor, the solid matter outlet in the feed carrier hopper is connected to the pyrolysis reactor, and solid heat carriers are fed into the pyrolysis reactor; sludge and solid heat carriers are stored in the pyrolysis reactor The pyrolysis reaction occurs during mixing; the pyrolysis gas in the pyrolysis reactor is sent to the condenser, and the liquid produced by condensation in the condenser is sent to the oil-water separator, and in the oil-water separator Water and oil are separated from the medium; the discharge carrier hopper is located below the pyrolysis reactor, and the solid matter in the pyrolysis reactor is sent into the heating riser through the discharge carrier hopper; the heating The lower part of the riser tube is connected to the hot smoke furnace, and the flue gas generated by the combustion of gas in the hot smoke furnace is sent into the heating riser tube for heating and lifting of solid objects; the outlet of the upper part of the heating riser tube is connected to the The inlet of the feed carrier hopper sends solid matter and flue gas into the feed carrier hopper; the gas outlet of the feed carrier hopper is connected to the cyclone separator, and dust-containing flue gas is sent into the cyclone separation in the device; the solid matter separated in the cyclone separator is sent to the slag discharger, and the residue is discharged from the slag discharger.

Preferably, the pyrolysis reactor has a plurality of stirring blades fixed on the spiral blades along the blade extension direction, and the stirring blades are square or circular raised ribs.

As a preferred option of the pyrolysis reactor, the heat carrier inlet and the sludge inlet are provided on one side of the upper end of the reactor barrel, and the pyrolysis gas outlet is provided on the opposite side. The heat carrier inlet is located at the Higher than the sludge inlet, a solid matter outlet is also provided at the lower end side of the reactor barrel; the sludge outlet of the pre-drying device is connected to the sludge inlet and is fed into the pyrolysis reactor sludge; the solid outlet of the feed carrier hopper is connected to the heat carrier inlet, and the solid heat carrier is fed into the pyrolysis reactor; the pyrolysis gas outlet is connected to the inlet of the condenser, and the pyrolysis gas outlet is connected to the inlet of the condenser. The pyrolysis gas after the reaction is sent into the condenser; the solid matter outlet is connected to the discharge carrier hopper, and the solid mixture after the pyrolysis reaction is discharged into the discharge carrier hopper. Further preferably, the pyrolysis gas outlet of the pyrolysis reactor is connected to several side exhaust ports, and the side exhaust ports extend into the reactor barrel for collecting the internal pyrolysis gas and collecting the pyrolysis gas. The collected pyrolysis gases are collected and directed to the pyrolysis gas outlet for discharge.

As the preferred heating riser, the heating riser consists of a feed section, an expansion section and a lifting section from bottom to top. The feed section includes a solid feed port, a hot flue gas pipe, an outer casing, and an inner casing. Pipes, feed chute and solid distributor, including:

The solid feed port is provided on the upper side of the outer casing; the inner casing is placed inside the outer casing, and the material slide is arranged between the lower end of the inner casing and the bottom of the outer casing. port, the solid material in the outer casing can enter the inner casing through the material slip port; the hot flue gas pipe is inserted from the bottom of the outer casing and extends into the inner casing from below , there is a gap between the hot flue gas pipe and the inner casing; the solid distributor is located at the feed opening and surrounds the outer wall of the hot flue gas pipe, and the solid distributor is provided with A high-pressure gas inlet and a plurality of distributed gas nozzles evenly arranged along the circumferential direction. The distributed gas flows from the high-pressure gas inlet into the solid distributor and is sprayed upward through the distributed gas nozzles.

Preferably, the gas outlet of the cyclone separator is connected to the gas inlet of the pre-drying device, and the flue gas in the cyclone separator is sent to the pre-drying device as a heat source for drying sludge; The heat-exchanged flue gas in the pre-drying device is sent to the exhaust gas induced draft fan through the flue gas outlet, and then discharged from the exhaust gas induced draft fan.

Preferably, the gas outlet of the condenser is connected to the hot smoke furnace, and the non-condensable gas in the condenser is sent to the hot smoke furnace as fuel.

Embodiments of the present invention also provide a sludge pyrolysis method, using the sludge pyrolysis resource utilization system provided by the above technical solution to perform pyrolysis treatment on sludge, including the following steps:

1. Send the water-containing sludge into the pre-drying device for pre-drying;

2. Send the pre-dried sludge into the pyrolysis reactor and mix it with the solid heat carrier. After the pyrolysis reaction, high-temperature pyrolysis gas and solid matter containing the solid heat carrier are obtained;

3. Send the high-temperature pyrolysis gas in the pyrolysis reactor to the condenser, and obtain liquid and non-condensable gas after condensation;

4. Separate the water and oil from the liquid condensed in the condenser in the oil-water separator;

5. Send the solid matter in the pyrolysis reactor into the heating riser, where the solid matter is heated by the flue gas from the hot smoke furnace and lifted into the feed carrier hopper;

6. Send the solid heat carrier in the feed carrier hopper into the pyrolysis reactor to mix with the pre-dried sludge;

7. Send the dusty flue gas in the feed carrier hopper to the cyclone separator to separate the solid and flue gas, and discharge the solid as residue.

Preferably, the non-condensable gas obtained after condensation in the condenser in step 3 is sent to the hot smoke furnace for use as fuel.

Preferably, the flue gas separated from the dust-containing flue gas in step 7 is sent to the pre-drying device as a heat source for drying sludge.

The beneficial effects of the above technical solutions of the embodiments of the present invention are:

1. Based on the material and pyrolysis characteristics of the sludge, a solid heat carrier is used to conduct heat to the sludge. Compared with the existing indirect heating method, it has the advantages of high thermal efficiency and uniform heating;

2. Properly setting spiral blades and stirring blades in the pyrolysis reactor can achieve full mixing of sludge and heat carrier and rapid heat transfer. The pyrolysis reaction rate is fast, the system processing capacity is strong, and at the same time, it can effectively solve the problem of uneven sludge mixing. It reduces the coking problem and achieves long-term stable operation of the system;

3. Through the rapid heating of sludge and the rapid export of oil and gas, the secondary cracking of pyrolysis products is reduced, a high yield of pyrolysis oil is achieved, and the utilization of sludge resources is maximized;

4. Use a sludge pre-drying device to initially remove moisture from the sludge using waste heat flue gas to reduce the energy consumption of the pyrolysis device, achieve graded utilization of energy, and improve the energy utilization efficiency of the system.

Description of drawings

Figure 1 is a system diagram of a sludge pyrolysis resource utilization system provided by an embodiment of the present invention;

Figure 2 is a schematic structural diagram of the pyrolysis reactor in the sludge pyrolysis resource utilization system provided by the embodiment of the present invention;

Figure 3 is a schematic structural diagram of the heating riser in the sludge pyrolysis resource utilization system provided by the embodiment of the present invention;

Figure 4 is a schematic flow chart of the steps of the sludge pyrolysis method provided by the embodiment of the present invention.

[Explanation of main component symbols]

1-Pre-drying device; 11-Tail gas induced draft fan; 12-Dust collector;

2-pyrolysis reactor; 21-reactor barrel; 22-rotating shaft; 23-spiral blade; 231-stirring blade; 24-heat carrier inlet; 25-sludge inlet; 26-solid matter outlet; 27-heat Degassing outlet; 271-side exhaust port;

31-feed carrier hopper; 32-discharge carrier hopper;

41-Outgoing carrier helix; 42-Incoming carrier helix;

5-Hot smoke stove; 51-Air distribution fan;

6-heating riser; 61-feed section; 611-solid feed port; 612-hot flue gas pipe; 613-outer casing; 614-inner casing; 615-feed opening; 616-solid distributor; 616a -High-pressure gas inlet; 616b-distributed gas nozzle; 6L-solid material line; 62-expansion section; 63-lifting section;

71-Condenser; 72-Oil-water separator;

8-Cyclone separator;

9-Slag discharger.

Detailed ways

In order to make the technical problems, technical solutions and advantages to be solved by the present invention clearer, a detailed description will be given below with reference to the accompanying drawings and specific embodiments.

Aiming at the problems of uneven heating, low thermal efficiency, and insufficient system processing capacity existing in the existing sludge pyrolysis technology, the present invention provides a new sludge pyrolysis reaction system and pyrolysis method, which has the characteristics of uniform heating, high efficiency, low price, and ease of use. industrialization and other characteristics.

In order to realize the above technical solution, embodiments of the present invention provide a sludge pyrolysis resource utilization system, the basic structure of which is shown in Figure 1, including a pre-drying device 1, a feed carrier hopper 31, and a discharge carrier hopper 32 , Pyrolysis reactor 2, hot smoke furnace 5, heating riser 6, condenser 71, oil-water separator 72, cyclone separator 8 and slag discharger 9, among which:

The sludge raw materials to be processed are sent into the system from the pre-drying device 1. The sludge raw materials are first pre-dried in the pre-drying device 1, and the pre-dried sludge is sent to the pyrolysis reactor 2.

The feed carrier hopper 31 is located above the pyrolysis reactor 2. The solid matter outlet in the feed carrier hopper 31 is connected to the pyrolysis reactor 2, and high-temperature solid heat carriers are sent into the pyrolysis reactor 2 as a better implementation. In this way, the feed carrier hopper 31 transports the solid heat carrier into the pyrolysis reactor 2 through the feed carrier screw 42. The solid heat carrier can be porcelain balls or quartz sand, or other materials can be selected as needed; sludge and solids After the heat carrier is mixed in the pyrolysis reactor 2, heat is transferred from the solid heat carrier to the sludge, and a pyrolysis reaction occurs; the discharge carrier hopper 32 is located below the pyrolysis reactor 2, and the solid matter in the pyrolysis reactor 2 passes through The discharge carrier hopper 32 is sent into the heating riser 6. As a better embodiment, a carrier spiral 41 is connected between the discharge carrier hopper 32 and the heating riser 6. The solid heat carrier containing the solid heat carrier is discharged by the discharge carrier spiral 41. The materials are transported into the heating riser 6; the lower part of the heating riser 6 is connected to the hot smoke furnace 5. The hot smoke furnace 5 can be connected to the air distribution fan 51 to inject air to support combustion, and the flue gas generated by the gas combustion in the hot smoke furnace 5 is sent into the heating riser. 6 is used to heat and lift solid matter; the outlet of the upper part of the heating riser 6 is connected to the inlet of the feed carrier hopper 31, and the solid matter and flue gas are sent into the feed carrier hopper 31 together; the solid heat carrier is in the feed carrier hopper 31. The pyrolysis reactor 2, the discharge carrier hopper 32 and the heating riser 6 form a cycle.

The high-temperature pyrolysis gas generated in the pyrolysis reactor 2 is sent to the condenser 71, and the liquid produced by condensation in the condenser 71 is sent to the oil-water separator 72. Water and oil are separated in the oil-water separator 72, and the water and oil can be separated. Oil is sent out; the non-condensable gas remaining after the pyrolysis gas is condensed in the condenser 71 can be sent out as fuel. As a better implementation, the gas outlet of the condenser 71 can be connected to the hot smoke furnace 5, and the discharged non-condensable gas can be sent out. The gas is sent into the hot smoke furnace 5 for use as gas.

The gas outlet of the feed carrier hopper 31 is connected to the cyclone separator 8, and the dust-containing flue gas is sent to the cyclone separator 8; the solid matter separated in the cyclone separator 8 is sent to the slag discharger 9, and then the slag discharger 9 It is discharged as system residue; the flue gas separated in the cyclone separator 8 can be directly discharged after necessary treatment. As a better implementation, as shown in Figure 1, the gas outlet of the cyclone separator 8 can also be connected to a pre-drying device. 1. Introduce the flue gas into the pre-drying device 1 as a heat source for drying sludge. The tail gas induced draft fan 11 is connected to the flue gas outlet of the pre-drying device 1, and the flue gas after exchanging heat with the water-containing sludge is sent to the dust collector 12 for processing. then discharged.

Figure 2 shows an example of a pyrolysis reactor 2. The pyrolysis reactor 2 includes a reactor barrel 21 and a heat carrier inlet 24, a sludge inlet 25 and a pyrolysis gas outlet 27 provided on the reactor barrel 21. , the reactor barrel 21 is a hollow truncated cone structure with a large top and a small bottom. A rotating shaft 22 is installed at the central axis of the reactor barrel 21; a spiral blade 23 is coiled and fixed on the rotating shaft 22, and the spiral blade 23 rotates with the rotating shaft 22. And stir; the upper end of the reactor barrel 21 is provided with a heat carrier inlet 24 and a sludge inlet 25, and the opposite side is provided with a pyrolysis gas outlet 27. The heat carrier inlet 24 is positioned higher than the sludge inlet 25; the reactor barrel 21 The lower end side is also provided with a solid matter outlet 26 for discharging solid heat carriers and pyrolysis solid products.

The pyrolysis reactor 2 can adopt the following settings as a better implementation:

The angle α between the side elevation and the lower bottom surface of the reactor barrel 21 is greater than 90°, preferably no more than 135°; the side of the reactor barrel 21 can be provided with several side openings connected to the pyrolysis gas outlet 27 The number of exhaust ports 271 and side exhaust ports 271 is preferably three to five. The side exhaust ports 271 extend into the reactor barrel 21 and are used to collect the internal pyrolysis gas and guide it to the pyrolysis gas outlet 27 Discharge; the side exhaust port 271 can be set to be circular or square, extending horizontally by 4~95mm from the inner wall of the reactor barrel 21;

The rotating shaft 22 is installed at the central axis of the reactor barrel 21 and runs vertically through the reactor barrel 21 from top to bottom; spiral blades 23 are coiled and fixed on the rotating shaft 22, and the spiral blades 23 can be welded to the rotating shaft 22. Fixed, when the rotating shaft 22 rotates, the spiral blades 23 stir with the rotating shaft 22 as the axis, stirring and pushing the biomass in the reactor barrel 21; the distance between adjacent blades of the spiral blade 23 can be set to 300~500mm. , the distance between the edge of the spiral blade 23 and the inner wall of the reactor barrel 21 is 5~100mm; in order to further improve the mixing effect, a plurality of ribs can be welded and fixed on the spiral blade 23 in sequence along the blade extension direction as the mixing blade 231, the ribs are For square or circular protrusions, the height of the protrusion can be set to 50~100mm, and the spacing between adjacent ribs can be set to 200~300mm.

In the sludge pyrolysis resource utilization system, in response to the heating and lifting requirements of the solid heat carrier, the heating riser adopts the example shown in Figure 3, and its specific structure and settings are:

The heating riser 6 is composed of a feed section 61, an expansion section 62 and a lift section 63 from bottom to top. The feed section 61 includes a solid feed port 611, a hot flue gas pipe 612, an outer casing 613, an inner casing 614, and a slide material. Port 615 and solid distributor 616. The solid feed port 611 is provided on the upper side of the outer casing 613; the inner casing 614 is set inside the outer casing 613, and a feed opening 615 is provided between the lower end of the inner casing 614 and the lower bottom of the outer casing 613. The solid material can enter the inner casing 614 through the feed opening 615; the hot flue gas pipe 612 is inserted from the bottom of the outer casing 613 and extends into the inner casing 614 from below. There is a gap; the solid distributor 616 is located at the feed opening 615 and surrounds the outer wall of the hot flue gas pipe 612. The solid distributor 616 is provided with a high-pressure gas inlet 616a and a plurality of distributed gas nozzles 616b evenly arranged along the circumferential direction. The distributed gas flows into the solid distributor 616 from the high-pressure gas inlet 616a, and is sprayed upward through the distributed gas nozzle 616b.

As a better implementation, the distance between the position of the solid feed port 611 and the bottom of the outer casing 613 should be set to 500~1000mm, and the fed solid material accumulates to form an inclined solid material line 6L; the diameter of the inner casing 614 is 200~800mm. The inner casing 614 supplies heating flue gas, and the speed of the hot flue gas flowing in the inner casing 614 is limited to 30~75m/s; the diameter of the hot flue gas pipe 612 is 20~50mm smaller than the diameter of the inner casing 614, forming hot flue gas. The gap between the pipe 612 and the inner casing 614, the length H of the hot flue gas pipe 612 pipe mouth extending into the inner casing 614 is 10~50mm; the height of the feed opening 615 is set to 50~150mm, and the feed speed passes through the solid The distribution gas speed of the distributor 616 is adjusted; the distribution gas of the solid distributor is compressed air or nitrogen, the gas pressure range at the high-pressure gas inlet 616a is 0.1~0.6Mpa, and the number of the distribution gas nozzles 616b is eight to sixteen The nozzle can adopt a dome hood type to control the air outlet speed at 30~50m/s.

Embodiments of the present invention also provide a biomass pyrolysis reaction method that uses the aforementioned biomass vertical pyrolysis reaction system to process biomass raw materials, including the following steps:

S1. Send the water-containing sludge into the pre-drying device for pre-drying;

S2. Send the pre-dried sludge into the pyrolysis reactor to mix with the solid heat carrier, and obtain high-temperature pyrolysis gas and solid matter containing the solid heat carrier through the pyrolysis reaction;

S3. Send the high-temperature pyrolysis gas in the pyrolysis reactor to the condenser, and obtain liquid and non-condensable gas after condensation;

S4. Separate the water and oil from the liquid condensed in the condenser in the oil-water separator;

S5. Send the solid matter in the pyrolysis reactor into the heating riser, where the solid matter is heated by the flue gas from the hot smoke furnace and lifted into the feed carrier hopper;

S6. Send the solid heat carrier in the feed carrier hopper into the pyrolysis reactor to mix with the pre-dried sludge;

S7. Send the dusty flue gas in the feed carrier hopper to the cyclone separator to separate the solid and flue gas, and discharge the solid as residue.

A better implementation of the above steps is as follows:

In step S1, the drying temperature when the high water content sludge is sent to the pre-drying device for pre-drying is set to 100~200°C; in order to improve energy utilization and make full use of the waste heat of high-temperature flue gas, the cyclone separation in step 7 can be The flue gas separated from the dusty flue gas is sent to the pre-drying device as a heat source for drying sludge. The temperature of the flue gas is controlled at 200~400°C.

In step S2, the pre-dried sludge is sent to the pyrolysis reactor for mixing with the solid heat carrier. The temperature of the solid heat carrier is controlled at 600~800°C. According to the properties of different types of sludge, the pyrolysis reactor is adjusted The rotation speed of the middle spiral blade can control the residence time of the sludge in the pyrolysis reactor to 1~10 minutes, so that the sludge can be pyrolyzed to produce high-temperature pyrolysis gas.

In step S3, when the high-temperature pyrolysis gas is sent to the condensation device for oil-water condensation, the condensation temperature is 20~50°C. The non-condensable gas obtained after condensation can be sent out as a product, or directly sent to the hot smoke furnace for use as gas. Non-condensable gas burns in a hot smoke furnace to produce high-temperature flue gas.

In step S5, the temperature of the solid matter containing the solid heat carrier discharged from the pyrolysis reactor is 400~500°C. The solid matter is heated by the combustion flue gas of 800~1200°C in the heating riser and lifted into the feed carrier hopper. .

The following are specific examples of pyrolysis of sludge using the above pyrolysis reaction system and pyrolysis method:

Taking a certain sludge as an example, the main properties of the sludge are as follows:

project unit numerical value Remark water content % 79.30 received base Mud content % 20.70 received base

The high water content sludge is sent to the pre-drying device for pre-drying. The drying temperature is 180°C. The high-temperature flue gas temperature entering the pre-drying device is 350°C. When leaving the pre-drying device, the moisture content of the sludge drops to 21%. . After predrying, the sludge is sent to the pyrolysis reactor for mixing with the solid heat carrier, where the temperature of the heat carrier is 700°C. The angle α of the pyrolysis reactor used is 125°, the distance between the spiral blades is 250mm, the spiral blades have square stirring blades with a welding height of 50mm, the spacing between the stirring blades is 150mm, and there are three heat pumps on the side of the pyrolysis reactor. The side exhaust port is connected to the degassing outlet. The distance between the spiral blade and the inner wall of the reactor barrel is 30 mm. The side exhaust port extends horizontally into the reactor barrel by 20 mm. By adjusting the spiral speed of the pyrolysis reactor so that the sludge residence time is 6 minutes, the high-temperature pyrolysis gas generated by pyrolysis is sent to the condensation device for oil-water condensation, and the condensation temperature is 40°C. The temperature of the solids discharged from the pyrolysis reactor is 500°C. The solid heat carrier sent into the heating riser is heated by the combustion flue gas with a temperature of 1000°C and lifted to the feed carrier hopper, where it is input into the pyrolysis reactor and mixed with the sludge.

Based on the products of the above pyrolysis system, the yield of pyrolysis oil is 25.3%, the yield of pyrolysis gas is 40.2%, the yield of slag is 11.2%, and the yield of pyrolysis water is 23.3%. The gas components are CH ₄ and H ₂ , CO mainly, with a calorific value as high as 3750kcal/Nm ³ .

Regarding the above-mentioned embodiments of the present invention, common knowledge such as the well-known specific structures and characteristics of the solutions are not described too much; each embodiment is described in a progressive manner, and the technical features involved in each embodiment are different from each other. They can be combined with each other if there is a conflict, and the same and similar parts between the various embodiments can be referred to each other.

In the description of the present invention, the orientation or positional relationship indicated by the terms "upper", "lower", "horizontal", "inner", "outer", etc. are based on the orientation or positional relationship shown in the drawings, and are only for convenience. The invention is described and the description is simplified without indicating or implying that the device or element referred to must have a particular orientation, be constructed and operate in a particular orientation and should not be construed as a limitation of the invention. Unless otherwise clearly stated and limited, the terms "connected" and "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be directly connected or through an intermediate connection. The medium is indirectly connected, which can be the internal connection between two components.

The above embodiments are only used to illustrate the technical solutions of the present invention but not to limit them. Although the present invention has been described in detail with reference to the above embodiments, those of ordinary skill in the art can still make modifications or equivalent substitutions to the specific embodiments of the present invention. , any modifications or equivalent substitutions that do not depart from the spirit and scope of the invention are within the scope of the claims of the pending invention.

Claims (9)

1. The utility model provides a mud pyrolysis resourceful system, includes predrying unit (1), feed carrier fill (31), ejection of compact carrier fill (32), pyrolysis reactor (2), hot smoke stove (5), heating riser (6), condenser (71), oil-water separator (72), cyclone (8) and scum ware (9), its characterized in that:

the pyrolysis reactor (2) comprises a reactor cylinder body (21) with a hollow round platform structure, the upper part of which is large and the lower part of which is small, and a rotary shaft (22) is arranged at the center axis position of the reactor cylinder body (21); a spiral blade (23) is coiled and fixed on the rotating shaft (22), and the spiral blade (23) rotates along with the rotating shaft (22) to stir;

the pre-drying device (1) pre-dries the sludge raw material, and the pre-dried sludge is sent into the pyrolysis reactor (2); the feeding carrier hopper (31) is positioned above the pyrolysis reactor (2), a solid outlet in the feeding carrier hopper (31) is connected with the pyrolysis reactor (2), and a solid heat carrier is fed into the pyrolysis reactor (2); the sludge and the solid heat carrier are mixed in the pyrolysis reactor (2) to carry out pyrolysis reaction;

the pyrolysis gas in the pyrolysis reactor (2) is sent into the condenser (71), liquid generated by condensation in the condenser (71) is sent into the oil-water separator (72), and water and oil are separated in the oil-water separator (72); the discharging carrier hopper (32) is positioned below the pyrolysis reactor (2), and solid matters in the pyrolysis reactor (2) are sent into the heating riser (6) through the discharging carrier hopper (32); the lower part of the heating riser tube (6) is connected with the hot smoke furnace (5), and flue gas generated by gas combustion in the hot smoke furnace (5) is sent into the heating riser tube (6) for heating and lifting solid matters; an outlet at the upper part of the heating riser (6) is connected with an inlet of the feeding carrier bucket (31) to send solid matters and flue gas into the feeding carrier bucket (31); the gas outlet of the feeding carrier hopper (31) is connected with the cyclone separator (8) and sends dust-containing flue gas into the cyclone separator (8); the solid matters separated in the cyclone separator (8) are sent to the slag extractor (9), and residues are discharged by the slag extractor (9);

the heating riser (6) is from bottom to top in proper order feed section (61), expansion section (62) and hoisting section (63), feed section (61) are including solid feed inlet (611), hot flue gas pipeline (612), outer tube (613), interior sleeve pipe (614), swift current material mouth (615) and solid distributor (616), wherein:

the solid feed inlet (611) is arranged at the upper side part of the outer sleeve (613); the inner sleeve (614) is arranged in the outer sleeve (613), the material sliding opening (615) is arranged between the lower end of the inner sleeve (614) and the lower bottom of the outer sleeve (613), and solid materials in the outer sleeve (613) can enter the inner sleeve (614) through the material sliding opening (615); the hot flue gas pipeline (612) is inserted from the bottom of the outer sleeve (613) and extends into the inner sleeve (614) from below, a gap is reserved between the hot flue gas pipeline (612) and the inner sleeve (614), and the inner sleeve (614) supplies heat and circulates flue gas; the solid distributor (616) is positioned at the position of the material sliding opening (615) and surrounds the outer wall of the hot flue gas pipeline (612), the solid distributor (616) is provided with a high-pressure air inlet (616 a) and a plurality of distribution air nozzles (616 b) which are uniformly distributed along the circumferential direction, and the distribution air is introduced into the solid distributor (616) from the high-pressure air inlet (616 a) and is sprayed upwards through the distribution air nozzles (616 b).

2. The sludge pyrolysis recycling system according to claim 1, wherein a plurality of stirring blades (231) are sequentially fixed on the spiral blades (23) of the pyrolysis reactor (2) along the extending direction of the blades, and the stirring blades (231) are square or round raised ribs.

3. The sludge pyrolysis recycling system according to claim 1, characterized in that the upper end side of the reactor cylinder (21) is provided with the heat carrier inlet (24) and the sludge inlet (25), the opposite side is provided with the pyrolysis gas outlet (27), the heat carrier inlet (24) is positioned higher than the sludge inlet (25), the lower end side of the reactor cylinder (21) is further provided with a solid outlet (26), wherein:

the sludge outlet of the pre-drying device (1) is connected with the sludge inlet (25), and sludge is fed into the pyrolysis reactor (2); the solid outlet of the feeding carrier hopper (31) is connected with the heat carrier inlet (24) and is used for feeding solid heat carriers into the pyrolysis reactor (2); the pyrolysis gas outlet (27) is connected with the inlet of the condenser (71), and pyrolysis gas after pyrolysis reaction is sent into the condenser (71); the solid outlet (26) is connected with the discharging carrier bucket (32) and discharges the solid mixture after the pyrolysis reaction into the discharging carrier bucket (32).

4. A sludge pyrolysis recycling system according to claim 3, characterized in that the pyrolysis gas outlet (27) of the pyrolysis reactor (2) is in communication with a number of side exhaust openings (271), which side exhaust openings (271) extend into the reactor cylinder (21) for collecting the pyrolysis gas inside and leading the collected pyrolysis gas to the pyrolysis gas outlet (27) for discharge.

5. Sludge pyrolysis recycling system according to claim 1, characterized in that the gas outlet of the cyclone separator (8) is connected with the gas inlet of the pre-drying device (1), and the flue gas in the cyclone separator (8) is sent into the pre-drying device (1) as a heat source for drying sludge; and the flue gas after heat exchange in the pre-drying device (1) is sent into a tail gas induced draft fan (11) through a flue gas outlet, and is discharged from the tail gas induced draft fan (11).

6. Sludge pyrolysis reclamation system according to any of claims 1 to 5, characterized in that the gas outlet of the condenser (71) is connected to the hot fume furnace (5) and non-condensable gas in the condenser (71) is fed into the hot fume furnace (5) as fuel.

7. A method for pyrolysis of sludge, characterized in that the sludge is subjected to pyrolysis treatment using the sludge pyrolysis recycling system according to any one of claims 1 to 6, comprising the steps of:

step 1: the sludge containing water is sent into a pre-drying device for pre-drying;

step 2: the sludge after pre-drying is sent into a pyrolysis reactor to be mixed with a solid heat carrier, and pyrolysis reaction is carried out to obtain pyrolysis gas and solid matters containing the solid heat carrier;

step 3: sending the high-temperature pyrolysis gas in the pyrolysis reactor into a condenser, and condensing to obtain liquid and non-condensable gas;

step 4: separating water and oil from the liquid obtained by condensation in the condenser in an oil-water separator;

step 5: feeding the solids in the pyrolysis reactor into a heating riser where the solids are heated by flue gas from a hot flue gas furnace and lifted into a feed carrier hopper;

step 6: feeding the solid heat carrier in the feeding carrier hopper into a pyrolysis reactor to be mixed with the pre-dried sludge;

step 7: and sending the dust-containing flue gas in the feeding carrier hopper into a cyclone separator to separate solids and flue gas, and discharging the solids as residues.

8. The sludge pyrolysis method as claimed in claim 7, wherein the non-condensable gas obtained by condensing in the condenser in the step 3 is fed into the hot smoke furnace to be used as fuel.

9. The sludge pyrolysis method as claimed in claim 7, wherein the flue gas separated from the dust-containing flue gas in step 7 is fed into the pre-drying device as a heat source for drying the sludge.