CN103756696B - Double fluidized bed combustible solid waste pyrolysis oil-gas coproduction device and method - Google Patents

Abstract

The invention discloses a dual-fluidized bed combustible solid waste pyrolysis oil-gas cogeneration device and method, which comprises a vertically arranged pyrolysis reactor and a combustion reactor; the pyrolysis reactor is equipped with a pyrolysis The air distribution device at the bottom of the reactor and the tubular air distribution device of the pyrolysis reactor, the combustion reactor is equipped with a plate type air distribution device inside the combustion reactor, and the air outlet of the pyrolysis reactor is connected to the pyrolysis reactor for cyclone separation The exhaust port of the combustion reactor is connected to the cyclone separator of the combustion reactor. Combining the current situation of complex raw material sources and components existing in the pyrolysis technology of urban waste, the present invention solves the problems of unstable production and supply of agricultural and forestry waste and large variety changes in the actual industrial application of the pyrolysis technology of agricultural and forestry waste. The control is convenient, the operation is stable and the operation parameters can be adjusted in a wide range.

Description

Double fluidized bed combustible solid waste pyrolysis oil and gas cogeneration device and method

technical field

The invention relates to a dual-fluidized bed combustible solid waste pyrolysis oil-gas cogeneration device and method, which is used for the reuse of combustible solid waste including agricultural and forestry waste and urban domestic waste, and belongs to the heat treatment of combustible solid waste reuse technology.

Background technique

my country is a large country in agriculture and forestry. The total amount of agricultural and forestry waste produced in the annual agricultural and forestry production is quite considerable. The amount of crop straw and forestry logging and processing residues alone reaches more than one billion tons each year, equivalent to about 500 million tons of standard coal. Among them, as the most common by-product of agricultural production, straw, its national output has exceeded 800 million tons, equivalent to about 380 million tons of standard coal. As far as forestry waste is concerned, during the "Eleventh Five-Year Plan" period, the amount of forestry logging residues produced in my country reached 109 million tons every year. Therefore, the efficient utilization of such a large amount of agricultural and forestry wastes is of great significance and influence both for the alleviation of my country's energy problems and for the implementation of my country's sustainable development strategy. There are currently many energy conversion and reuse technologies involving agricultural and forestry wastes. Among the many options, pyrolysis technology is relatively easy to operate and less difficult to industrialize. It is convenient and widely concerned and applied. However, due to the seasonality and regionality of agricultural and forestry wastes, there are certain difficulties in the process of realizing stable industrial operation of agricultural and forestry waste pyrolysis technology, which is specifically manifested in the large fluctuations in the production and supply of agricultural and forestry waste produced by pyrolysis , and the frequent changes in the composition of agricultural and forestry waste make the product composition ratio also have certain instability.

On the other hand, with the rapid growth of my country's economy and the steady improvement of living standards, the output of municipal solid waste has increased rapidly, and its calorific value has also continued to increase. How to safely and cleanly deal with the rapidly increasing amount of urban waste and rationally use urban waste to convert it into effective energy has attracted more and more researchers' attention. At present, a kind of urban waste treatment technology that is widely paid attention to is pyrolysis. technology. Municipal solid waste pyrolysis can process refractory materials that are not suitable for incineration and landfill, and at the same time claim flammable gases or liquids. However, due to the complex composition of municipal waste, it is difficult to control the pyrolysis of municipal waste in practical industrial applications, and the proportion of each component of the product also changes significantly.

Contents of the invention

Purpose of the invention: Aiming at the problems of unstable production and supply of agricultural and forestry waste and large variety of types of agricultural and forestry waste pyrolysis technology in practical industrial applications, combined with the current situation of complex raw material sources and components in urban waste pyrolysis technology, The object of the present invention is to provide a dual-fluidized bed pyrolysis oil-gas cogeneration device and method that is convenient to control, stable in operation, and has a wide range of adjustment of operating parameters, and is suitable for the alternate utilization of various combustible solid wastes mainly including agricultural and forestry wastes and urban wastes .

Technical scheme: in order to achieve the above object, the technical scheme adopted in the present invention is:

A dual-fluidized bed combustible solid waste pyrolysis oil-gas cogeneration device, including a vertically arranged pyrolysis reactor and a combustion reactor;

The pyrolysis reactor is provided with a pyrolysis reactor bottom air distribution device and a pyrolysis reactor tubular air distribution device, and a pyrolysis reactor overflow port is arranged on the side wall of the pyrolysis reactor from top to bottom , pyrolysis reactor feed port, pyrolysis reactor two-way feeder return port and pyrolysis reactor one-way feeder return port, pyrolysis reactor slag discharge port is set at the bottom of the pyrolysis reactor , the top of the pyrolysis reactor is provided with a pyrolysis reactor air outlet; the position of the pyrolysis reactor tubular air distribution device is higher than that of the pyrolysis reactor bottom air distribution device, and the position of the pyrolysis reactor feed port is high In the pyrolysis reactor tubular air distribution device, the height of the position of the return port of the pyrolysis reactor's two-way feeder and the pyrolysis reactor's one-way feeder is placed at the bottom of the pyrolysis reactor. Between the tubular air distribution devices of the reactor; the raw material feeder is connected to the feed port of the pyrolysis reactor;

The combustion reactor is equipped with a combustion reactor plate-type air distribution device, and the combustion reactor overflow port, the combustion reactor feed port and the combustion reactor return port are arranged on the side wall of the combustion reactor from top to bottom. , the bottom of the combustion reactor is provided with a combustion reactor slag outlet, and the top of the combustion reactor is provided with a combustion reactor air outlet; the position of the combustion reactor return port is higher than the combustion reactor plate air distribution device; The auxiliary fuel feeder is connected with the feed port of the combustion reactor;

The air outlet of the pyrolysis reactor is connected to the cyclone separator of the pyrolysis reactor, and the lower discharge end of the cyclone separator of the pyrolysis reactor is connected to the feed pipe of the two-way feeder through the first return material drop pipe , the first inclined pipe and the second inclined pipe of the two-way feeder are respectively connected to the return port of the bidirectional return device of the pyrolysis reactor and the return port of the combustion reactor; the overflow port of the pyrolysis reactor The first inclined pipe that is inclined downward communicates with the first return material descending pipe, and a pyrolysis reactor overflow device is arranged on the first inclined pipe; the upper exhaust end of the cyclone separator of the pyrolysis reactor is connected to The first-stage condenser recovers pyrolysis products;

The exhaust port of the combustion reactor is connected to the cyclone separator of the combustion reactor, and the lower discharge end of the cyclone separator of the combustion reactor is connected to the feed end of the one-way return feeder through the second return material drop pipe, and the single The discharge end of the feeder is connected with the return port of the one-way feeder of the pyrolysis reactor; the overflow port of the combustion reactor is communicated with the second return drop pipe through the second inclined pipe inclined downward, A combustion reactor overflow device is arranged on the second inclined pipe; the upper exhaust end of the combustion reactor cyclone separator is connected to a heat pipe heat exchanger for heat energy recovery.

Preferably, the upper exhaust end of the pyrolysis reactor cyclone separator is connected to the first-stage condenser; the liquid outlet of the first-stage condenser is connected to the first pyrolysis oil collection tank, and the gas in the first-stage condenser The outlet is connected to the second-stage condenser; the liquid outlet of the second-stage condenser is connected to the second pyrolysis oil collection tank, and the gas outlet of the second-stage condenser is connected to the dehydration tower; the gas outlet of the dehydration tower is divided into two paths, one It is connected to the output channel of pyrolysis gas products, and the other is connected to the lower inlet of the heat pipe heat exchanger;

The upper exhaust end of the cyclone separator of the combustion reactor is connected to the upper inlet of the heat pipe heat exchanger; the upper outlet of the heat pipe heat exchanger is connected with the pyrolysis reactor tubular air distribution device and the pyrolysis reactor bottom air distribution device, and the heat pipe The outlet at the lower end of the heat exchanger is connected to the flue gas purification device, and the gas outlet of the flue gas purification device is connected to the bag filter.

Preferably, the pyrolysis reactor overflow device adjusts the pyrolysis reactor to work in a bubbling fluidized state, a turbulent fluidized state or a fast fluidized state; the combustion reactor overflow device adjusts the combustion reactor to work in a drum bubbly fluidization, turbulent fluidization or fast fluidization.

Preferably, the height of the pyrolysis reactor is H, from the bottom of the pyrolysis reactor: the height of the pyrolysis reactor pipe-type air distribution device is 0.2 to 0.3H, and the height of the pyrolysis reactor inlet is 0.35～0.45H, the height of the pyrolysis reactor overflow port is 0.6～0.8H, the height of the pyrolysis reactor two-way feeder return port and the pyrolysis reactor one-way feeder return port is 0.05～0.15H H, and the height of the return port of the pyrolysis reactor two-way feeder is not lower than the height of the pyrolysis reactor one-way feeder; the diameter of the pyrolysis reactor is D; the air distribution device at the bottom of the pyrolysis reactor is a small opening The bottom edge of the lower conical air distribution plate is placed at the bottom of the pyrolysis reactor, the central axis is vertical, the angle between the conical surface and the horizontal plane is 60°; the angle between the first inclined pipe and the horizontal plane is 45°.

Preferably, the height of the combustion reactor is L, L=0.8～1H, from the bottom of the combustion reactor: the height of the combustion reactor inlet is 0.3～0.4L, and the height of the combustion reactor overflow port is 0.6 ~ 0.8L, the height of the combustion reactor return port is 0.15 ~ 0.25L; the height of the combustion reactor is W, W = 0.8 ~ 1.2D; The plate-type air distribution device is set at the large end of the conical structure. The conical structure and the combustion reactor plate-type air distribution device together constitute the combustion reactor air chamber. The angle between the conical surface of the conical structure and the horizontal plane is 60°; the second The angle between the inclined pipe and the horizontal plane is 45°.

Preferably, the two-way feeder includes a cuboid cavity, and the cuboid cavity is divided into three chambers by a T-shaped partition, wherein the rear chamber is a feeding chamber, and the front two chambers are respectively The first return chamber and the second return chamber, the feed chamber is connected with the first return descending pipe, the first return chamber is connected with the first return inclined pipe, the second return chamber is connected with the second return inclined pipe connected; the air distribution plate is set in the feed chamber to isolate the air chamber of the feed chamber below; the air distribution plate is arranged in the first return chamber to isolate the first return chamber air chamber below; The second return chamber is equipped with an air distribution plate, which isolates the second return chamber air chamber below;

The width _b2 of the feeding chamber is equal to the width _b1 of the width of the first returning chamber/the width b1 of the second returning chamber, and the length _a1 of the first returning chamber is equal to the length _a2 of the second returning chamber; The diameter of the first return descending pipe is d ₁ , the diameter of the first return inclined pipe is d ₂ , the diameter of the second return inclined pipe is d ₃ , d ₂ =d ₃ =0.625d ₁ ; the first return The angle between the inclined pipe and the vertical direction is α, the angle between the second return inclined pipe and the vertical direction is β, and both α and β are less than 45°; the opening ratio of the air distribution plate is 10-15° %.

The pyrolysis reactor and combustion reactor in the above device are respectively equipped with overflow structure and gas-solid separation device, which realizes good adaptability to various working states such as bubbling fluidization state, turbulent fluidization state and rapid fluidization state , the residence time and mixing characteristics of the mixed material in the bed can be changed in a large range through the adjustment of the operating parameters, so that the device can adapt to complex types of fuels. It should be pointed out that when the pyrolysis reactor or combustion reactor is in the fast fluidized state, the valve on the corresponding overflow pipe should be closed.

The pyrolysis reactor in the above-mentioned device is equipped with a pipe-type air distribution device and a bottom air distribution device, and the degree of mixing of the materials in the pyrolysis reactor is enhanced by feeding fluidized gas in stages, and the pyrolysis gas product can be quickly carried From the pyrolysis reactor, the whole device has better reaction efficiency.

The material circulation between the two reactors of the above device is controlled by a pneumatically controlled feeder (one-way feeder and two-way feeder), and the delivery flow can be adjusted according to the actual operating conditions of the two reactors to improve reaction efficiency; The feeder can controlly distribute the solid flux sent into the pyrolysis reactor and the combustion reactor, so that the whole device can control the amount of material sent into the combustion reactor according to the temperature in the two reactors, so as to achieve accurate control of the interior of the whole device temperature purpose.

A dual-fluidized-bed combustible solid waste pyrolysis oil-gas cogeneration method, comprising the following steps:

(1) Add auxiliary fuel into the combustion reactor through the auxiliary fuel feeder, and the auxiliary fuel is fluidized and burned by the air injected by the plate-type air distribution device of the combustion reactor to increase the temperature in the combustion reactor to meet the operating requirements; high temperature inert The solid bed material enters the pyrolysis reactor through the one-way feeder, which provides the heat required for pyrolysis for the pyrolysis reactor, so that the temperature in the pyrolysis reactor gradually rises;

(2) Add combustible solid waste into the pyrolysis reactor through the raw material feeder, and supply pyrolysis gas into the pyrolysis reactor through the pyrolysis reactor tubular air distribution device and the pyrolysis reactor bottom air distribution device, The pyrolysis gas is used as fluidized mixed bed material;

(3) According to the pyrolysis characteristics of combustible solid waste and the combustion characteristics of pyrolysis solid products, through the adjustment of fluidization gas volume, the switch adjustment of the valve of the pyrolysis reactor overflow device and the switch adjustment of the valve of the combustion reactor overflow device , adjust the fluidization state in the pyrolysis reactor and the combustion reactor, so that the output of pyrolysis gas and pyrolysis oil can be optimally combined;

(4) As the reaction gradually stabilizes, the gas products of the pyrolysis reactor are separated and output by the cyclone separator, and the bio-oil is collected by cooling the first-stage condenser and the second-stage condenser to the first pyrolysis oil collection tank and pyrolysis oil In the second collection tank, the remaining gas products are dehydrated by the dehydration tower to obtain pyrolysis gas, part of the pyrolysis gas is output through the output channel of the pyrolysis gas product, and the other part of the pyrolysis gas is connected to the heat pipe heat exchanger for pyrolysis reaction The internal pyrolysis gas of the pyrolysis reactor; if the supply of the internal pyrolysis gas as the pyrolysis reactor is insufficient, it will be supplemented by feeding the external pyrolysis gas into the heat pipe heat exchanger in parallel, and the internal pyrolysis gas and the external pyrolysis gas are jointly the pyrolysis gas constituting the pyrolysis reactor;

(5) The solid product of the pyrolysis reactor is sent to the two-way feeder after being separated by the pyrolysis reactor cyclone separator, and is sent to the combustion reaction by adjusting the fluidization air volume of the two-way feeder according to the internal temperature of the two-way feeder The flow rate of pyrolysis solid products burned in the vessel;

(6) The flue gas generated by the combustion reactor is separated from the gas and solid by the cyclone separator in the combustion reactor, and the flue gas is sent to the heat pipe heat exchanger for preheating the pyrolysis gas of the pyrolysis reactor, and then the flue gas is sent into The flue gas purifier is used for purification, and is output after being dedusted by the bag filter;

(7) The inert solid bed material in the solid product of the pyrolysis reactor is separated by the pyrolysis reactor cyclone separator and sent to the two-way feeder, and then sent back to the combustion reactor by the two-way feeder to be reheated to form high-temperature inertness Solid bed material; the high-temperature inert solid bed material is sent to the one-way feeder after being separated by the cyclone separator in the combustion reactor, and is sent to the pyrolysis reactor by the one-way feeder to form a double fluidized bed reactor. energy and matter cycle.

In the above method, the operating states of the pyrolysis reactor and the combustion reactor can be adjusted respectively according to the pyrolysis characteristics of the combustible solid waste and the combustion characteristics of the pyrolysis solid product; specifically, for the relatively low yield of pyrolysis oil The fuel can reduce the amount of fluidizing gas and increase the residence time of combustible raw materials in the pyrolysis reactor, so that more pyrolysis gas can be obtained through pyrolysis reaction to achieve higher utilization efficiency of raw materials; on the other hand, for For pyrolysis solid products with a relatively low combustion reaction rate, the pyrolysis solid products have enough time to burn completely by reducing the amount of fluidizing gas in the combustion reactor.

The above method applies the layered fluidization method in the pyrolysis reactor, and strengthens the gas-solid and solid-solid mixing intensity in the pyrolysis reactor by reasonably controlling the fluidization gas volume of the air distribution device arranged in two layers, and makes the pyrolysis Gas products can more easily leave the pyrolysis reaction area, which can improve the reaction efficiency and speed up the reaction rate.

The above method requires the working temperature in the pyrolysis reactor to be 450-650°C, and the working temperature in the combustion reactor to be 1000-1100°C; care should be taken to prevent the temperature in the combustion reactor from being too high to melt the residue and cause difficulty in fluidization operation. It should be prevented that the temperature in the combustion reactor is too low and the dioxin cannot be completely decomposed.

Beneficial effects: Compared with the prior art, the dual fluidized bed combustible solid waste pyrolysis oil and gas cogeneration device and method provided by the present invention have the following advantages:

1. The pyrolysis reactor and combustion reactor of the device can adapt to the operating requirements of a wide range of adjustment parameters, so that the two reactors can be operated as either a bubbling bed reactor or a fast bed reactor, which can also be understood as the The device can meet the requirements of conventional pyrolysis and rapid pyrolysis, can effectively deal with complex types of combustible solid waste, and can maximize the reaction efficiency through the adjustment of operating parameters, so as to realize the efficient use of materials and energy;

2. It is equipped with a collection and treatment system for pyrolysis oil and pyrolysis gas, which can meet the requirements of co-production of pyrolysis oil and pyrolysis gas;

3. By adjusting the working parameters, it can adapt to the change of material composition, and can meet the alternate treatment of various types of combustible solid waste including agricultural and forestry waste and urban solid waste without stopping the work of the device;

4. The structural form of the coupling of the pyrolysis reactor and the combustion reactor is adopted, and the inert granular bed material is used as the heat carrier to circulate between the two reactors, realizing the efficient utilization of energy; at the same time, the circulation of the bed material is controlled by the pneumatic return valve amount, to achieve the purpose of accurately controlling the temperature in the pyrolysis reactor.

Description of drawings

Fig. 1 is a structural representation of the present invention;

Fig. 2 is the structural dimension figure of pyrolysis reactor;

Fig. 3 is the structural dimension drawing of combustion reactor;

Figure 4 is a structural dimension diagram of the bidirectional feeder;

Including: raw material feeder 1, pyrolysis reactor tubular air distribution device 2, pyrolysis reactor bottom air distribution device 3, pyrolysis reactor 4, pyrolysis reactor cyclone separator 5, pyrolysis reactor overflow device 6. Two-way feeding device 7, the first feeding down pipe 7-1, the first feeding inclined pipe 7-2, the second feeding inclined pipe 7-3, the feeding chamber 7-4, the first feeding chamber 7-5, the second return chamber 7-6, the first return chamber air chamber 7-7, the second return chamber air chamber 7-8, the feed chamber air chamber 7-9, pyrolysis reactor slag discharge Port 8, combustion reactor cyclone separator 9, combustion reactor overflow device 10, one-way return device 11, combustion reactor 12, combustion reactor plate air distribution device 13, combustion reactor slag outlet 14, auxiliary fuel Feeder 15, first-stage condenser 16, first-stage nozzle 16-1, second-stage nozzle 16-2, circulating spray liquid heat exchanger 17, first pyrolysis oil collection tank 18, second-stage condenser 19. Second pyrolysis oil collection tank 20, dehydration tower 21, heat pipe heat exchanger 22, flue gas purification device 23, bag filter 24.

Combustible solid waste a, pyrolysis reactor first-stage fluidization air b, pyrolysis reactor second-stage fluidization air c, auxiliary fuel d, combustion reactor fluidization air e, second-stage condenser condensing medium f , pyrolysis gas product g, external pyrolysis gas h, flue gas i, fluidization air j-1 in the feed chamber, first return air j-2, and second return air j-3.

Detailed ways

The present invention will be further described below in conjunction with the accompanying drawings.

As shown in FIG. 1 , a dual-fluidized bed combustible solid waste pyrolysis oil-gas cogeneration device includes a vertical pyrolysis reactor 4 and a combustion reactor 12 .

The pyrolysis reactor 4 is provided with a pyrolysis reactor bottom air distribution device 3 and a pyrolysis reactor tubular air distribution device 2, and a pyrolysis reaction device is arranged on the side wall of the pyrolysis reactor 4 from top to bottom. The overflow port of the pyrolysis reactor, the feed port of the pyrolysis reactor, the return port of the two-way feeder of the pyrolysis reactor and the return port of the one-way feeder of the pyrolysis reactor are provided with a pyrolysis reactor at the bottom of the pyrolysis reactor 4. Reactor slag outlet 8, pyrolysis reactor air outlet is provided on the top of pyrolysis reactor 4; The position of the pyrolysis reactor tubular air distribution device 2 is higher than the pyrolysis reactor bottom air distribution device 3, The position of the feed inlet of the pyrolysis reactor is higher than that of the tubular air distribution device 2 of the pyrolysis reactor. Between the air distribution device 3 at the bottom of the pyrolysis reactor and the tubular air distribution device 2 of the pyrolysis reactor; the raw material feeder 1 is connected to the feed port of the pyrolysis reactor, and the combustible solid waste a is sent into the pyrolysis reactor through the raw material feeder 1 Inside Reactor 4.

The combustion reactor 12 is provided with a combustion reactor plate-type air distribution device 13, and on the side wall of the combustion reactor 12, a combustion reactor overflow port, a combustion reactor feed port and a combustion reactor are arranged from top to bottom. The return port is provided with a combustion reactor slag outlet 14 at the bottom of the combustion reactor 12, and a combustion reactor air exhaust port is provided at the top of the combustion reactor 12; the position of the combustion reactor return port is higher than that of the combustion reaction The plate-type air distribution device 13; the auxiliary fuel feeder 15 is connected with the feed port of the combustion reactor, and the auxiliary fuel d is sent into the combustion reactor 12 through the auxiliary fuel feeder 15.

The air outlet of the pyrolysis reactor is connected to the pyrolysis reactor cyclone separator 5, and the lower discharge end of the pyrolysis reactor cyclone separator 5 passes through the first return material descending pipe 7-1 and the two-way return feeder The feed pipe 7-1 of 7 links to each other, and the first inclined pipe 7-2 and the second inclined pipe 7-3 of the two-way feeder 7 are respectively connected with the feed port and the combustion chamber of the two-way feeder of the pyrolysis reactor. The reactor return port is connected; the overflow port of the pyrolysis reactor is communicated with the first return drop pipe through the first inclined pipe inclined downward, and the pyrolysis reactor overflow device 6 is arranged on the first inclined pipe The upper exhaust end of the pyrolysis reactor cyclone separator 5 is connected to the first-stage condenser 16; the liquid outlet of the first-stage condenser 16 is connected to the first pyrolysis oil collection tank 18, and the first-stage condenser The gas outlet of 16 is connected to the second-stage condenser 19; the liquid outlet of the second-stage condenser 19 is connected to the second pyrolysis oil collection tank 20, and the gas outlet of the second-stage condenser 19 is connected to the dehydration tower 21; the dehydration tower 21 The gas outlet is divided into two paths, one path is connected to the pyrolysis gas product output channel, and the other path is connected to the lower end inlet of the heat pipe heat exchanger 22 .

The exhaust port of the combustion reactor is connected to the combustion reactor cyclone separator 9, and the lower discharge end of the combustion reactor cyclone separator 9 passes through the second return material downcomer and the feed end of the one-way return feeder 11 connected, the discharge end of the one-way feeder 11 is connected with the return port of the one-way feeder of the pyrolysis reactor; The pipes are connected, and a combustion reactor overflow device 10 is provided on the second inclined pipe; the upper exhaust end of the combustion reactor cyclone separator 9 is connected to the upper end inlet of the heat pipe heat exchanger 22; the upper end outlet of the heat pipe heat exchanger 22 It is connected with the pyrolysis reactor tubular air distribution device 2 and the bottom air distribution device 3 of the pyrolysis reactor, the lower end outlet of the heat pipe heat exchanger 22 is connected with the flue gas purification device 23, and the gas outlet of the flue gas purification device 23 is connected with the bag filter 24 connected.

The pyrolysis reactor overflow device 6 adjusts the pyrolysis reactor 4 to work in a bubbling fluidized state, a turbulent fluidized state or a fast fluidized state; the combustion reactor overflow device 10 regulates the combustion reactor 12 to work in Bubble fluidized state, turbulent fluidized state or fast fluidized state.

The height of the pyrolysis reactor 2 is H, from the bottom of the pyrolysis reactor 2: the height of the pyrolysis reactor tubular air distribution device 2 is 0.2～0.3H, and the height of the pyrolysis reactor inlet is 0.35～0.45H, the height of the pyrolysis reactor overflow port is 0.6～0.8H, the height of the pyrolysis reactor two-way feeder return port and the pyrolysis reactor one-way feeder return port is 0.05～0.15H H, and the height of the return port of the pyrolysis reactor two-way feeder is not lower than the height of the pyrolysis reactor one-way feeder; the diameter of the pyrolysis reactor 2 is D; the bottom air distribution device of the pyrolysis reactor 3 It is a conical air distribution plate with a small opening on the bottom, its bottom edge is placed at the bottom of the pyrolysis reactor 2, the central axis is vertical, the angle between the cone surface and the horizontal plane is 60°; the angle between the first inclined tube and the horizontal plane is 45° .

The height of the combustion reactor 12 is L, L=0.8～1H, from the bottom of the combustion reactor 12: the height of the combustion reactor inlet is 0.3～0.4L, and the height of the combustion reactor overflow port is 0.6 ～0.8L, the height of the combustion reactor return port is 0.15～0.25L; the height of the combustion reactor 12 is W, W=0.8～1.2D; the bottom of the combustion reactor 12 is a conical structure with the small end down, and the combustion reaction The plate-type air distribution device 13 is arranged at the large end of the conical structure. The conical structure and the combustion reactor plate-type air distribution device 13 together constitute the combustion reactor air chamber. The angle between the conical surface of the conical structure and the horizontal plane is 60° ; The angle between the second inclined pipe and the horizontal plane is 45°.

The two-way feeder 7 includes a cuboid cavity, and the cuboid cavity is divided into three chambers by a T-shaped partition, wherein a chamber at the rear is a feed chamber 7-4, and the two chambers at the front are respectively It is the first material return chamber 7-5 and the second material return chamber 7-6, the feed chamber 7-4 is connected with the first material return descending pipe 7-1, and the first material return chamber 7-5 is connected with the first material return chamber The inclined pipe 7-2 is connected, and the second return chamber 7-6 is connected with the second return inclined pipe 7-3; the air distribution plate is arranged in the feed chamber 7-4 to isolate the feed chamber air chamber below 7-9; the first return chamber 7-5 is provided with an air distribution plate to isolate the first return chamber air chamber 7-7 below; the second return chamber 7-6 is provided with a cloth The air plate isolates the second return chamber air chamber 7-8 below;

The width b ₂ of the feed chamber 7-4 is equal to the width b 1 of the first return chamber 7-5/the width b ₁ of the second return chamber 7-6, and the length a ₁ of the first return chamber 7-5 It is equal to the length a ₂ of the second material return chamber 7-6; the diameter of the first material return descending pipe 7-1 is d ₁ , the diameter of the first material return inclined tube 7-2 is d 2 , and the second material return inclined tube 7-2 is d ₂ . The diameter of the pipe 7-3 is d ₃ , d ₂ =d ₃ =0.625d ₁ ; the included angle between the first return inclined pipe 7-2 and the vertical direction is α, and the angle between the second return inclined pipe 7-3 and the vertical direction The included angle in the vertical direction is β, and both α and β are less than 45°; the opening ratio of the air distribution plate is 10-15%.

Pass into the feed chamber air chamber 7-9 into the feed chamber fluidization air j-1, pass into the first return chamber air chamber 7-7 into the first return air j-2, and feed the second return air The second return air j-3 is passed into the chamber air chamber 7-8; 2 and the second return air j-3) The flow and distribution ratio can control the flux of the circulating material.

The dual-fluidized-bed combustible solid waste pyrolysis oil-gas cogeneration method based on the above-mentioned device comprises the following steps:

(1) Add auxiliary fuel into the combustion reactor 12 through the auxiliary fuel feeder 15, and the auxiliary fuel is fluidized and burned by the air injected by the combustion reactor plate air distribution device 13, so as to increase the temperature in the combustion reactor 12 to reach the operating temperature. Requirements: The high-temperature inert solid bed material enters the pyrolysis reactor 4 through the one-way feeder 11, and provides the heat required for pyrolysis for the pyrolysis reactor 4, so that the temperature in the pyrolysis reactor 4 gradually rises;

(2) Add the combustible solid waste into the pyrolysis reactor 4 through the raw material feeder 1, and flow into the pyrolysis reactor 4 through the pyrolysis reactor tubular air distribution device 2 and the pyrolysis reactor bottom air distribution device 3 Supplying pyrolysis gas, said pyrolysis gas is used as fluidized mixed bed material;

(3) According to the pyrolysis characteristics of combustible solid waste and the combustion characteristics of pyrolysis solid products, through the regulation of fluidization gas volume, the switch adjustment of pyrolysis reactor overflow device 6 valves and the combustion reactor overflow device 10 valves Switch adjustment, adjust the fluidization state in the pyrolysis reactor 4 and the combustion reactor 12, so that the output of pyrolysis gas and pyrolysis oil can be optimally combined;

(4) As the reaction gradually stabilizes, the gas product of the pyrolysis reactor 4 is separated and exported by the cyclone separator 5, and the bio-oil is cooled and collected by the first-stage condenser 16 and the second-stage condenser 19 to the first pyrolysis oil collection tank 18 and the second collection tank 20 for pyrolysis oil, the remaining gas products are dehydrated by the dehydration tower 21 to obtain pyrolysis gas, part of the pyrolysis gas is output through the output channel of the pyrolysis gas product, and the other part of the pyrolysis gas is connected to the heat pipe for exchange Heater 22, as the internal pyrolysis gas of pyrolysis reactor 4; If the supply of internal pyrolysis gas as pyrolysis reactor 4 is insufficient, it will be supplemented by feeding external pyrolysis gas into heat pipe heat exchanger 22 in parallel, so The internal pyrolysis gas and the external pyrolysis gas together constitute the pyrolysis gas of the pyrolysis reactor 4;

(5) The solid product of the pyrolysis reactor 4 is sent to the two-way feeder 7 after being separated by the pyrolysis reactor cyclone separator 5, and is adjusted according to the internal temperature conditions of the two-way feeder 7 by adjusting the fluidization air volume of the two-way feeder 7 Regulate the flow rate of the pyrolysis solid product sent into the combustion reactor 12 for combustion;

(6) The flue gas that combustion reactor 12 generates is sent into heat pipe heat exchanger 22 for the pyrolysis gas of preheating pyrolysis reactor 4 after the flue gas that combustion reactor cyclone separator 9 gas-solid separation obtains, then The flue gas is sent to the flue gas purifier 23 for purification, and is output after being dedusted by the bag filter 24;

(7) The inert solid bed material in the pyrolysis reactor 4 solid products is sent into the two-way feeder 7 after being separated by the pyrolysis reactor cyclone separator 5, and is sent back to the combustion reactor 12 by the two-way feeder 7 again Heated to form a high-temperature inert solid bed material; the high-temperature inert solid bed material is sent to the one-way feeder 11 after being separated by the combustion reactor cyclone separator 9, and then sent to the pyrolysis reactor 4 by the one-way feeder 11 , to form energy and material circulation between double fluidized bed reactors.

Based on the above devices and methods, the present invention will be further described below in conjunction with the embodiments.

Example 1

The raw material is straw, and the inert solid bed material is quartz sand (mainly SiO ₂ ). Since the pyrolysis effect of straw pyrolysis is relatively good, and the pyrolysis solid product has a fast combustion reaction rate in the air atmosphere, the pyrolysis reactor 4 can be used as a fast flow by closing the valve set on the overflow device 6 of the pyrolysis reactor. The fluidized bed operates and meets the operation requirements of fast pyrolysis, and the average residence time in the pyrolysis reactor 4 is controlled to be 1 to 3 s; by closing the valve set on the overflow device 10 of the combustion reactor, the combustion reactor 12 can be used as a fast fluidized bed Operation, the average residence time in the combustion reactor 12 is controlled to be 7-9s. The distribution of fluidizing air volume in the pyrolysis reactor 4 is: 35%-45% for the tubular air distribution device 2 of the pyrolysis reactor, and 55%-65% for the air distribution device 3 at the bottom of the pyrolysis reactor.

When the device is started, coal is used as auxiliary fuel and sent into the combustion reactor 12 through the auxiliary fuel feeder 15, and air is sent into the combustion reactor 12 through the combustion reactor plate-type air distribution device 13 for fluidized bed material and providing combustion-supporting gas (O ₂ ). The mixed bed material and flue gas in the combustion reactor 12 co-fluidize and rise, and then the gas-solid separation is carried out at the cyclone separator 9 of the combustion reactor, and the high-temperature inert solid bed material enters the pyrolysis reactor 4 through the one-way feeder 11 and is This releases heat. The separated high-temperature flue gas is sent to the heat pipe heat exchanger 22 for preheating the fluidized gas of the pyrolysis reactor 4, and the flue gas after heat exchange is discharged after purification and dust removal. At the same time, the external pyrolysis gas is used as the fluidization gas of the pyrolysis reactor 4, and enters the pyrolysis reactor 4 through the air distribution device 3 at the bottom of the pyrolysis reactor and the tubular air distribution device 2 of the pyrolysis reactor respectively for fluidization. Bed material. As the combustion proceeds, the temperatures in the pyrolysis reactor 4 and the combustion reactor 12 gradually increase. The temperature inside the pyrolysis reactor 4 is controlled to be 500±50°C, and the temperature inside the combustion reactor 12 is controlled to be 1000±50°C.

When the temperature in the pyrolysis reactor 4 reaches the operating temperature requirement, the raw material feeder 1 feeds the dried and crushed straw into the pyrolysis reactor 4, where the straw is rapidly fluidized, and the violently mixed bed material undergoes pyrolysis . The mixed product generated by pyrolysis and part of the inert solid bed material are brought into the cyclone separator 5 of the pyrolysis reactor by the fluidization gas. After the gas-solid separation is carried out here, the gas product enters the first-stage condenser 16 from the upper end, and the solid product flows to the first-stage condenser 16. Enter the two-way feeder 7 down. The gas product is cooled to 40-70°C by spray cooling and indirect cooling in the first-stage condenser 16 and the second-stage condenser 17 respectively. During the cooling process, the condensable gas condenses into pyrolysis oil and enters the first pyrolysis oil collection. The tank 18 and the pyrolysis oil are collected by the second pyrolysis oil collection tank 20 . The remaining non-condensable gas is sent to the dehydration tower 21 to remove excess moisture to obtain pyrolysis gas. After the pyrolysis gas is processed by the dehydration tower, it is divided into two paths, one path is output as the pyrolysis gas product g, and the other path is sent to the heat pipe heat exchanger 22 as the fluidization gas and returned to the pyrolysis reactor after being preheated by high-temperature flue gas 4 within. The solid materials containing pyrolysis solid products and inert solid bed materials are passed through the first inclined pipe 7-2 and the second inclined pipe 7 in proportion according to the temperature conditions in the two reactors in the two-way feeder 7 -3 into the pyrolysis reactor 4 and the combustion reactor 12. The pyrolysis solid products (mainly coke) entering the combustion reactor 12 are rapidly and completely combusted in the air atmosphere, and the inert solid bed material is reheated in the combustion reactor 12, forming a cycle of matter and energy between the two reactors. After the operation of the device is stable and the reaction temperature meets the requirements, the amount of auxiliary fuel coal added is gradually reduced, and the device relies on the energy provided by the combustion of pyrolysis solid products to maintain the operation of the device.

Example 2

The raw material is forestry harvesting residue, and the inert solid bed material is quartz sand. Compared with straw, the proportion of lignin in wood is relatively large, and the process required for wood crushing to meet the particle size requirements of fast pyrolysis is relatively complicated, so it is not suitable to use forestry harvesting residues for pyrolysis oil as straw. Therefore, by opening the valve provided on the pyrolysis reactor overflow device 6, the pyrolysis reactor 4 is operated as a bubbling fluidized bed, and the average residence time in the pyrolysis reactor 4 is adjusted to be 200-300s; by closing the combustion reactor The valve provided on the overflow device 10 makes the combustion reactor 12 operate as a fast fluidized bed, and adjusts the gas residence time in the combustion reactor 12 to 7-9s. The temperature inside the pyrolysis reactor 4 is controlled to be 500±50°C, and the temperature inside the combustion reactor 12 is controlled to be 1000±50°C. The distribution of the fluidizing air volume of the pyrolysis reactor is as follows: 35% to 45% for the tubular air distribution device 2 of the pyrolysis reactor, and 55% to 65% for the air distribution device 3 at the bottom of the pyrolysis reactor.

Coal is used as an auxiliary fuel to burn in the combustion reactor 12 to provide the required energy for the initial operation of the device. When the device is running stably, feed the dried and pulverized raw materials into the pyrolysis reactor 4 through the raw material feeder 1, and the raw materials are deeply pyrolyzed in the bubbling pyrolysis reactor 4, and the obtained pyrolysis gas The product is mainly non-condensable gas with small molecules. After a small amount of tar is removed by the first-stage condenser 16 and the second-stage condenser 17, the pyrolysis gas is dehydrated by the dehydration tower 21 and divided into two paths as fluidization gas and product gas. output. The solid product obtained by pyrolysis is sent to the combustion reactor 12 and mixed with air for combustion to provide heat for the operation of the device.

Example 3

Municipal solid waste is selected as the raw material, and quartz sand is selected as the inert circulating bed material. Since the solid products of municipal solid waste pyrolysis contain certain pollutants, especially dioxins, the pyrolysis solid products need to be treated at high temperature for a long time in the combustion reactor 12 to remove pollutants. By closing the valve provided on the pyrolysis reactor overflow device 6, the pyrolysis reactor 4 is operated as a fast fluidized bed and meets the operating requirements of fast pyrolysis, and the average residence time in the control pyrolysis reactor 4 is 1 to 3 s; The combustion reactor 12 is operated as a bubbling fluidized bed by opening the valve provided on the overflow device 10 of the combustion reactor, and the average residence time in the combustion reactor 12 is controlled to be 200-300s. The temperature inside the pyrolysis reactor 4 is controlled to be 550±50°C, and the temperature inside the combustion reactor 12 is controlled to be 1150±50°C. The distribution of the fluidizing air volume of the pyrolysis reactor is as follows: 35% to 45% for the tubular air distribution device 2 of the pyrolysis reactor, and 55% to 65% for the air distribution device 3 at the bottom of the pyrolysis reactor.

Coal is used as an auxiliary fuel to burn in the combustion reactor 12 to provide the required energy for the initial operation of the device. After the device is running stably, feed the sorted, dried and pulverized raw materials into the pyrolysis reactor 4 through the raw material feeder 1, and in the pyrolysis reactor 4, the gas products obtained by rapid pyrolysis of the raw materials are separated by the pyrolysis reactor cyclone After the gas-solid separation in the device 5, the collection of pyrolysis oil is completed through the first-stage condenser 16 and the second-stage condenser 17, and a small amount of non-condensable pyrolysis gas is removed by spraying in the first-stage condenser 16 The acid gas and pyrolysis gas are dehydrated by the dehydration tower 21 and then output in two ways as fluidization gas and product gas. The solid product obtained by pyrolysis is sent to the combustion reactor 12 and mixed with air for combustion to provide heat for the operation of the device. The pyrolysis solid product is placed in the combustion reactor 12 at over 1100°C for a long time, which can completely decompose pollutants such as dioxin and furan in the raw material

The above is only a preferred embodiment of the present invention, it should be pointed out that for those of ordinary skill in the art, without departing from the principle of the present invention, some improvements and modifications can also be made, and these improvements and modifications are also possible. It should be regarded as the protection scope of the present invention.

Claims (6)

1. a double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device, is characterized in that: comprise the pyrolysis reactor (4) and combustion reactor (12) that vertically arrange;

Air-distributing device bottom pyrolysis reactor (3) and pyrolysis reactor tubular distributor (2) is provided with in described pyrolysis reactor (4), the sidewall of pyrolysis reactor (4) is from top to bottom provided with pyrolysis reactor flash mouth, pyrolysis reactor opening for feed, pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth, the bottom of pyrolysis reactor (4) is provided with pyrolysis reactor slag-drip opening (8), the top of pyrolysis reactor (4) is provided with pyrolysis reactor exhaust outlet; Described pyrolysis reactor tubular distributor (2) position is higher than air-distributing device bottom pyrolysis reactor (3), pyrolysis reactor gating location is higher than pyrolysis reactor tubular distributor (2), and pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth position height are placed between air-distributing device bottom pyrolysis reactor (3) and pyrolysis reactor tubular distributor (2); Raw materials device (1) is connected with pyrolysis reactor opening for feed;

The board-like air-distributing device of combustion reactor (13) is provided with in described combustion reactor (12), the sidewall of combustion reactor (12) is from top to bottom provided with combustion reactor flash mouth, combustion reactor opening for feed and combustion reactor returning charge mouth, the bottom of combustion reactor (12) is provided with combustion reactor slag-drip opening (14), the top of combustion reactor (12) is provided with combustion reactor exhaust outlet; Described combustion reactor returning charge mouth position is higher than the board-like air-distributing device of combustion reactor (13); Auxiliary fuel feeder (15) is connected with combustion reactor opening for feed;

Described pyrolysis reactor exhaust outlet access pyrolysis reactor cyclonic separator (5), the bottom discharge end of described pyrolysis reactor cyclonic separator (5) is connected with the feed-pipe (7-1) of two-way material returning device (7) by the first returning charge downtake (7-1), and the first returning charge inclined tube (7-2) of two-way material returning device (7) and the second returning charge inclined tube (7-3) respectively material returning device returning charge mouth two-way with pyrolysis reactor are connected with combustion reactor returning charge mouth; Described pyrolysis reactor flash mouth is communicated with the first returning charge downtake by the first downward-sloping inclined tube, and the first inclined tube is provided with pyrolysis reactor flash device (6); Upper exhaust side access first step condenser (16) of described pyrolysis reactor cyclonic separator (5) carries out pyrolysis product recovery;

Described combustion reactor exhaust outlet access combustion reactor cyclonic separator (9), the bottom discharge end of described combustion reactor cyclonic separator (9) is connected with the feed end of unidirectional material returning device (11) by the second returning charge downtake, and the discharge end of unidirectional material returning device (11) is connected with pyrolysis reactor unidirectional material returning device returning charge mouth; Described combustion reactor flash mouth is communicated with the second returning charge downtake by the second downward-sloping inclined tube, and the second inclined tube is provided with combustion reactor flash device (10); The upper exhaust side access hot tube heat exchanger of described combustion reactor cyclonic separator (9) carries out energy recovery.

2. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, is characterized in that: upper exhaust side access first step condenser (16) of described pyrolysis reactor cyclonic separator (5); The liquid exit of first step condenser (16) accesses the first pyrolysis oil holding tank (18), pneumatic outlet access second stage condenser (19) of first step condenser (16); The liquid exit of second stage condenser (19) accesses the second pyrolysis oil holding tank (20), pneumatic outlet access dehydration tower (21) of second stage condenser (19); Dehydration tower (21) pneumatic outlet is divided into two-way, a road access pyrolysis gas output of products passage, another road access hot tube heat exchanger (22) lower inlet;

The upper end entrance of upper exhaust side access hot tube heat exchanger (22) of described combustion reactor cyclonic separator (9); Hot tube heat exchanger (22) upper end outlet and pyrolysis reactor tubular distributor (2) are connected with air-distributing device (3) bottom pyrolysis reactor, the outlet of hot tube heat exchanger (22) lower end is connected with smoke eliminator (23), and smoke eliminator (23) pneumatic outlet is connected with sack cleaner (24).

3. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, is characterized in that: described pyrolysis reactor flash device (6) regulates pyrolysis reactor (4) to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state; Described combustion reactor flash device (10) regulates combustion reactor (12) to work in bubbling fluidization state, turbulent fluidised state or fast fluidization state.

4. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, is characterized in that:

The height of described pyrolysis reactor (2) is H, by the bottom of pyrolysis reactor (2): the height of pyrolysis reactor tubular distributor (2) is 0.2 ~ 0.3H, the height of pyrolysis reactor opening for feed is 0.35 ~ 0.45H, the height of pyrolysis reactor flash mouth is 0.6 ~ 0.8H, the height of pyrolysis reactor two-way material returning device returning charge mouth and pyrolysis reactor unidirectional material returning device returning charge mouth is 0.05 ~ 0.15H, and the height of pyrolysis reactor two-way material returning device returning charge mouth is higher than the height of the unidirectional material returning device of pyrolysis reactor; The diameter of pyrolysis reactor (2) is D; Bottom pyrolysis reactor air-distributing device (3) for osculum under cone shaped distributor, its, axis was vertical, and the angle of the conical surface and horizontal plane is 60 ° along being placed in pyrolysis reactor (2) bottom end; The angle of the first inclined tube and horizontal plane is 45 °;

The height of described combustion reactor (12) is L, L=0.8 ~ 1H, by the bottom of combustion reactor (12): the height of combustion reactor opening for feed is 0.3 ~ 0.4L, the height of combustion reactor flash mouth is 0.6 ~ 0.8L, and the height of combustion reactor returning charge mouth is 0.15 ~ 0.25L; The diameter of combustion reactor (12) is W, W=0.8 ~ 1.2D; Combustion reactor (12) bottom be small end under pyramidal structure, the board-like air-distributing device of combustion reactor (13) is arranged on the large end position of pyramidal structure, pyramidal structure and the board-like air-distributing device of combustion reactor (13) form combustion reactor air compartment jointly, and the conical surface of pyramidal structure and the angle of horizontal plane are 60 °; The angle of the second inclined tube and horizontal plane is 45 °.

5. double-fluidized-bed flammable solid pyrolysis of waste oil gas combination preparing device according to claim 1, it is characterized in that: described two-way material returning device (7) comprises rectangular parallelepiped cavity volume, described rectangular parallelepiped cavity volume is divided into three chambers by T-shaped dividing plate, wherein a chamber at rear is feed chamber (7-4), two chambers in front are respectively the first returning charge room (7-5) and the second returning charge room (7-6), feed chamber (7-4) is connected with the first returning charge downtake (7-1), first returning charge room (7-5) is connected with the first returning charge inclined tube (7-2), second returning charge room (7-6) is connected with the second returning charge inclined tube (7-3), in described feed chamber (7-4), air distribution plate is set, isolates the feed chamber air compartment (7-9) of below, be provided with air distribution plate in described first returning charge room (7-5), isolate the first returning charge room air compartment (7-7) of below, be provided with air distribution plate in described second returning charge room (7-6), isolate the second returning charge room air compartment (7-8) of below,

The width b of described feed chamber (7-4) ₂with the width b of the width/the second returning charge room (7-6) of the first returning charge room (7-5) ₁equal, the length a of the first returning charge room (7-5) ₁with the length a of the second returning charge room (7-6) ₂equal; The diameter of the first returning charge downtake (7-1) is d ₁, the diameter of the first returning charge inclined tube (7-2) is d ₂, the diameter of the second returning charge inclined tube (7-3) is d ₃, d ₂=d ₃=0.625d ₁; First returning charge inclined tube (7-2) is α with the angle of vertical direction, and the second returning charge inclined tube (7-3) is that β, α and β are all less than 45 ° with the angle of vertical direction; The percentage of open area of described air distribution plate is 10 ~ 15%.

6. a double-fluidized-bed flammable solid pyrolysis of waste oil gas co-production, is characterized in that: comprise the steps:

(1) in combustion reactor (12), auxiliary fuel is added by auxiliary fuel feeder (15), auxiliary fuel is by the Air Fluidized that injected by the board-like air-distributing device of combustion reactor (13) and burn, and reaches operating requirement in order to promote combustion reactor (12) interior temperature; High temperature inert Solid Bed material enters pyrolysis reactor (4) through unidirectional material returning device (11), for pyrolysis reactor (4) provides the heat needed for pyrolysis, makes pyrolysis reactor (4) interior temperature increase gradually;

(2) flammable solid waste is added in pyrolysis reactor (4) by raw materials device (1), by the supply pyrolysis gas in pyrolysis reactor (4) of air-distributing device (3) bottom pyrolysis reactor tubular distributor (2) and pyrolysis reactor, described pyrolysis gas is as fluidisation mixed bed material;

(3) according to the pyrolysis characteristics of flammable solid waste and the combustioncharacteristics of pyrolysis solid product, by the switch-mode regulation of the adjustment of fluidization gas, the switch-mode regulation of pyrolysis reactor flash device (6) valve and combustion reactor flash device (10) valve, adjust the fluidized state in pyrolysis reactor (4) and combustion reactor (12), pyrolysis gas and pyrolysis oil output are optimized and combine;

(4) along with reaction is stablized gradually, pyrolysis reactor (4) gaseous product is separated through cyclonic separator (5) and exports, cool in collecting biological oil to the first pyrolysis oil holding tank (18) and pyrolysis oil second holding tank (20) through first step condenser (16) and second stage condenser (19), residual gas product obtains pyrolysis gas after dehydration tower (21) removes moisture, part pyrolysis gas is exported by pyrolysis gas output of products passage, another part pyrolysis gas access hot tube heat exchanger (22), internal heat as pyrolysis reactor (4) is vented one's spleen, if vent one's spleen under-supply as the internal heat of pyrolysis reactor (4), then by venting one's spleen supplement to the parallel external heat that passes into of hot tube heat exchanger (22), described internal heat is vented one's spleen and external heat is vented one's spleen forms the pyrolysis gas of pyrolysis reactor (4) jointly,

(5) pyrolysis reactor (4) solid product is admitted to two-way material returning device (7) after pyrolysis reactor cyclonic separator (5) is separated, according to two-way material returning device (7) internal temperature situation, by regulating the flow of the pyrolysis solid product of two-way material returning device (7) Fluidization wind rate adjustment feeding combustion reactor (12) combustion;

(6) flue gas that the flue gas that combustion reactor (12) generates obtains after combustion reactor cyclonic separator (9) gas solid separation is admitted to the pyrolysis gas of hot tube heat exchanger (22) for preheating pyrolysis reactor (4), flue gas is admitted to flue gas cleaner (23) and purifies subsequently, and exports after sack cleaner (24) dedusting;

(7) the inert solid bed material in pyrolysis reactor (4) solid product is admitted to two-way material returning device (7) after pyrolysis reactor cyclonic separator (5) is separated, then is sent back to combustion reactor (12) by two-way material returning device (7) and again added thermosetting high temperature inert Solid Bed material; Described high temperature inert Solid Bed material is admitted to unidirectional material returning device (11) after combustion reactor cyclonic separator (9) is separated, being delivered to pyrolysis reactor (4) by unidirectional material returning device (11), form the energy between double-fluidized-bed reactor and material cycle.