CN110511773A - A device and method for coupling biomass pyrolysis and catalytic cracking reaction - Google Patents

Abstract

A reaction device for coupling biomass pyrolysis and catalytic cracking reaction, comprising a biomass pyrolysis reactor, a double riser catalytic cracking reactor and a catalyst regenerator, wherein the biomass pyrolysis reactor is placed inside the catalyst regenerator. The biomass pyrolysis reactor is placed in the catalyst regenerator, and the biochar generated by itself and the coke generated during the upgrading process are used to provide heat during the reaction process, making full use of the heat of the charred catalyst to reduce energy consumption. In the biomass pyrolysis process, no heat carrier is added, which reduces its separation from the reaction product and wear of the reactor. This method can make full use of the existing petroleum distillate catalytic cracking device, adopt double riser catalytic cracking reactor, can not only increase the scale of the device through catalytic cracking of petroleum fraction, but avoid the single biomass pyrolysis oil upgrading device scale too large Small enough to affect the operation and economics of the device.

Description

A device and method for coupling biomass pyrolysis and catalytic cracking reaction

technical field

The invention relates to a reaction device for pyrolysis of biomass, in particular to a device for coupling biomass pyrolysis and sulfidation catalytic cracking.

Background technique

Energy is an important material basis for ensuring the progress of human society and an important support for national economic development. It is closely related to human life and production, and plays an indispensable and important role in promoting social progress and economic development. With the rapid development of the economy, fossil energy is becoming increasingly exhausted, and the supply of petroleum resources is becoming more serious. At the same time, fossil fuels have brought severe environmental problems. Facing the current situation of energy crisis and environmental pollution, promoting the revolution of energy production and consumption, and promoting the transformation of economic development model to green and low-carbon are not only the internal requirements of my country's sustainable development strategy, but also the best choice to deal with global climate change. Driven by the superimposed effect of energy and environment, the development and utilization of renewable energy has attracted more and more attention. Biomass energy is a favored renewable energy source that is abundant and can be converted into conventional solid, liquid and gaseous fuels. Among them, biomass liquid fuel (bio-oil) is widely considered to have the most potential and is expected to become an important source of alternative vehicle fuel in the future.

Biomass rapid pyrolysis technology is an important way to obtain bio-oil. It adopts high heating rate (10 ² ~ 10 ⁴ K/s), short residence time (0.2 ~ 3s) and moderate cracking temperature (500 ~ 650 ℃) to pyrolyze organic polymers in biomass, and can obtain about 75% oil yield. Because a high reaction temperature is required and a large amount of heat is consumed, the energy cost of biomass pyrolysis is relatively high, which limits its industrialization process. In addition, the obtained bio-oil has a complex composition, high oxygen content (35-60wt%), high viscosity (20-200mPa·s at 40°C), high acid value (pH 2-4), low calorific value (14-19MJ/ kg) and other characteristics, there are defects in direct use as an alternative vehicle fuel, so subsequent refining is required to produce fuel oil that meets the requirements of vehicles.

How to improve the utilization of biomass fuel more effectively is the main purpose of the present invention.

Contents of the invention

One purpose of this application is to provide a device for coupling biomass pyrolysis and fluidized catalytic cracking, which can make good use of the heat of coke combustion during the regeneration process of the unborn catalyst, eliminating the need for biomass pyrolysis reaction to use additional heat source.

One purpose of this application is to provide a process for coupling biomass pyrolysis and fluidized catalytic cracking, which combines the biomass pyrolysis process with the catalytic cracking reaction process, makes full use of the scale effect of the device, and eases the supply of biomass raw materials Unstable effects, and reduce production costs. At the same time, the on-line upgrading of biomass pyrolysis oil is realized, and the deterioration of product distribution and product quality caused by the competitive adsorption of biomass pyrolysis oil and petroleum fractions is avoided.

For realizing above-mentioned purpose of the present invention, adopt following technical scheme:

A device for coupling biomass pyrolysis and fluidized catalytic cracking includes a biomass pyrolysis reaction device, a catalyst regenerator and a catalytic cracking reactor, wherein the biomass pyrolysis reactor is placed inside the catalyst regenerator.

The catalytic regenerator is a variable-diameter tank body, the diameter of the upper part of the tank body is larger than that of the lower part of the tank body, that is, the upper part of the tank body is a dilute phase section, and the lower part of the tank body is a dense phase section.

At least two sets of cyclone separators are arranged in the dilute phase section, wherein one set of cyclone separators is connected with the upper end of the biomass pyrolysis reactor.

In the present application, the catalyst may be the catalyst used in the fluidized catalytic cracking reaction in the field of petrochemical industry.

In this application, the biomass pyrolysis reactor is placed in the catalyst regenerator. During the reaction process, the biochar generated by itself and the coke generated by the catalytic cracking process are used to provide heat. energy consumption.

In the biomass pyrolysis process, no heat carrier is added, which reduces its separation from the reaction product and wear of the reactor.

Description of drawings

Fig. 1 is an embodiment of a reaction device for coupling biomass pyrolysis and fluid catalytic cracking reaction.

Detailed ways

The reaction device coupled with biomass pyrolysis and catalytic cracking of the present application will be further described in detail below. The protection scope of the present application is not limited, and the protection scope is defined by the claims. Certain disclosed specific details provide a thorough understanding of the various disclosed embodiments. However, one skilled in the relevant art will recognize that embodiments may be practiced without one or more of these specific details, and with other materials and the like.

Unless the context requires otherwise, in the specification and claims, the terms "comprising" and "comprising" should be interpreted as an open and including meaning, that is, "including, but not limited to".

The "embodiment", "an embodiment", "another embodiment" or "certain embodiments" mentioned in the specification refer to the described specifically related features and structures related to the embodiment or characteristics are included in at least one embodiment. Thus, "an embodiment," "an embodiment," "another embodiment," or "certain embodiments" are not necessarily all referring to the same embodiments. Furthermore, the particular features, structures or characteristics may be combined in any manner in one or more embodiments. Each feature disclosed in the specification can be replaced by any alternative feature that can serve the same, equivalent or similar purpose. Therefore, unless otherwise specified, the disclosed features are only general examples of equivalent or similar features.

The term "catalytic cracking riser reactor" refers to a riser for catalytic cracking reaction of petroleum distillate; Riser.

The catalytic cracking process in petroleum processing is a process in which large molecules of heavy oil are converted into small molecules such as liquefied gas, gasoline, and diesel under the action of a catalyst. While realizing the production of gasoline and diesel by lightening heavy oil, the generated coke adheres to the catalyst, and the catalyst activity can only be restored by burning. The large amount of heat generated by burning cannot be fully utilized, resulting in waste of resources. Therefore, a large amount of heat generated by the charring of the catalytic cracking unit can be used for the pyrolysis reaction of biomass, and at the same time, the biomass pyrolysis oil can be upgraded through the action of the catalytic cracking catalyst, but the biomass pyrolysis oil is high in aromatics and easy to coke. Features It is easy to compete with petroleum fractions for adsorption in the catalytic cracking process, affecting the conversion rate and product distribution of petroleum fractions. Coupling biomass pyrolysis with catalytic cracking of petroleum fractions to achieve heat self-sufficiency in the biomass pyrolysis process, and at the same time to improve the quality of biomass pyrolysis oil through catalytic upgrading, using double risers to avoid product distribution and The deterioration of product quality and the production of fuel that meets the requirements of use are the main purpose of the present invention.

Further description of this application is as follows:

On the one hand, a device for coupling biomass pyrolysis and fluidized catalytic cracking reaction, including a biomass pyrolysis reactor, a catalyst regenerator and a catalytic cracking reaction device, wherein the biomass pyrolysis reactor is placed inside the catalyst regenerator .

In this application, the biomass pyrolysis reactor is placed in the catalyst regenerator, and the pyrolysis reaction is carried out by using the heat transferred in the catalyst regenerator. After the pyrolysis reaction, the pyrolysis oil enters the catalytic cracking reaction unit and is further upgraded into the desired product. In the coupling device of the present application, the heat of the catalyst regenerator can be used, which saves the heat source required for the pyrolysis reaction in the prior art. In the prior art, the addition of the heat source increases the wear and tear on the equipment, and also plays an energy-saving effect .

The catalyst regenerator of the present application includes all structures disclosed in the prior art. For example: the catalytic regenerator is a tank with variable diameter, and the diameter of the upper part of the tank is larger than that of the lower part of the tank, that is, the upper part of the tank is a dilute phase section, and the lower part of the tank is a dense phase section.

At least two sets of cyclone separators are arranged in the dilute phase section, wherein one set of cyclone separators is connected with the upper end of the biomass pyrolysis reactor. After the pyrolysis gas and biochar generated by the pyrolysis reaction of biomass pass through the cyclone separator, the biochar enters the catalyst regenerator again to burn and release energy; the separated pyrolysis gas is separated into thermal Solve oil and non-condensable gas.

In certain embodiments, the biomass pyrolyzer is a cylindrical straight tube into which the biomass pyrolyzer extends through the bottom of the catalyst regenerator.

The ratio of the pipe diameter of the biomass pyrolyzer to the pipe diameter of the dense phase section of the catalyst regenerator is 0.1:1-0.5:1.

In the dense-phase section (dense-phase bed) of the catalytic regenerator, the pyrolysis reactor is directly buried in the catalyst, and the heat transfer efficiency will be higher than that of the dilute-phase section, which can reduce the rapid temperature rise when the biomass just enters the pyrolysis reactor. The temperature drop caused by the heat absorption of violent pyrolysis is beneficial to control the whole reaction to proceed under isothermal conditions.

In some embodiments, in the dilute phase section, the inlet port of a group of cyclone separators communicates with the dilute phase section, and the outlet port communicates with the outside.

In certain embodiments, the catalysts of the present application include, but are not limited to, catalysts used in catalytic cracking reactions in the petrochemical field. Such as molecular sieve catalysts, metal oxide catalysts.

In certain embodiments, the catalyst regenerator is connected to the catalytic cracking reactor through a catalyst regeneration inclined pipe and a catalyst standby inclined pipe.

The catalytic cracking reactor of the present application is all catalytic cracking reaction devices in the prior art. For example, a two-stage riser reactor.

In certain embodiments, the catalytic cracking reaction unit includes a two-stage riser reactor, namely a catalytic cracking riser reactor and a upgrading riser reactor.

In some embodiments, the pyrolysis oil generated by the biomass pyrolysis reaction enters the upgrading riser for further upgrading reaction.

The catalytic cracking process in petroleum processing is a process in which large molecules of heavy oil are converted into small molecules such as liquefied gas, gasoline, and diesel under the action of a catalyst. While realizing the production of gasoline and diesel by lightening heavy oil, the generated coke adheres to the catalyst, and the catalyst activity can only be restored by burning. The large amount of heat generated by burning cannot be fully utilized, resulting in waste of resources. Therefore, a large amount of heat generated by the charring of the catalytic cracking unit is used for the pyrolysis reaction of biomass, and at the same time, the biomass pyrolysis oil is upgraded through the action of the catalytic cracking catalyst. Through the coupled use of the biomass pyrolysis device and the second-stage riser reactor, the pyrolysis oil is passed into the modified riser reactor, which can better avoid the competition between the biomass pyrolysis oil and petroleum fractions in the catalytic cracking process Adsorption, further improving the conversion rate and product distribution of petroleum fractions.

In this application, the biomass includes but not limited to cellulose, lignin agricultural and forestry wastes.

This method can make full use of the existing petroleum distillate catalytic cracking device, adopt double riser catalytic cracking reactor, one riser is used for catalytic cracking and upgrading of biomass pyrolysis oil, and the other riser is used for catalytic cracking of petroleum fraction , the scale of the device can be increased through the catalytic cracking of petroleum fractions, and the operation and economic benefits of the single biomass pyrolysis oil modification device can be avoided from being too small and affecting the operation and economic benefits of the device. At the same time, the catalytic cracking reaction of the two risers can avoid the competitive adsorption of biomass pyrolysis oil and petroleum fractions, and the two reactors can determine the appropriate reaction conditions according to the reaction rules of different fractions. The reaction products of the upgrading riser and the cracking riser enter the same fractionation tower for separation, so as to alleviate the instability of the product after the biomass pyrolysis oil reaction.

In another aspect, a method for coupling biomass pyrolysis and fluidized catalytic cracking includes:

Catalytic cracking raw oil is catalyzed in the catalytic cracking reaction device. After the reaction, the oil gas and the raw catalyst are separated by the cyclone separator, and the raw catalyst enters the catalyst regenerator for combustion, and the oil gas is separated in the fractionation tower;

The biomass raw material enters the biomass pyrolysis reactor for pyrolysis reaction, and the biomass pyrolysis reactor is placed inside the catalyst regenerator;

The pyrolysis oil obtained after the biomass pyrolysis reaction enters the catalytic cracking reaction device for catalytic reaction.

The product after the biomass pyrolysis reaction is condensed to obtain pyrolysis oil and non-condensable gas, and the non-condensable gas enters the biomass pyrolysis reactor. The noncondensable gas at this time is used as the stripping gas for the biomass pyrolysis reaction.

The fractions separated from oil and gas in the fractionation tower include: cracked gas, gasoline, diesel oil, re-refined oil and oil slurry, etc. Refined oil can be returned to the catalytic cracking reactor for catalytic reaction.

In certain embodiments, the catalytic cracking raw oil is subjected to heat exchange with pyrolysis products before being sent to the catalytic cracking reactor. Recycling the heat in the process of pyrolysis reaction and catalytic cracking reaction as much as possible can achieve the effect of energy saving.

In some embodiments, the catalytic cracking reaction device includes a cracking riser reactor and a reforming riser reactor, and the catalytic cracking raw material or/and recycled oil enters the cracking riser reactor for reaction, and the biomass after pyrolysis reaction The pyrolysis oil enters the reforming riser reactor for reaction.

In some embodiments, the temperature of the regeneration reaction in the catalyst regenerator is 600-720°C.

The high-temperature regenerant and flue gas generated by the catalyst regeneration reaction provide reaction heat for biomass pyrolysis.

In some embodiments, the outlet temperature of the biomass pyrolysis reactor is 500-650° C., and the reaction pressure is 0.1-0.4 MPa.

In some embodiments, the biomass pyrolysis reaction time is 0.5-30s.

In certain embodiments, the outlet temperature of the upgrading reactor is 450-600°C, and the reaction time is 1-4s. The reaction pressure is 0.1-0.4MPa.

In certain embodiments, the outlet temperature of the cracking riser reactor is 450-550° C., the reaction time is 1-3 s, and the reaction pressure is 0.1-0.4 MPa.

In some embodiments, the pyrolysis gas separated from the biomass pyrolysis product is condensed, and the condensation process can be air-cooled, water-cooled or other condensation methods, and the final condensation temperature is 40-80° C. under normal pressure.

Through the coupling of biomass pyrolysis reaction and catalytic cracking reaction in this application, its advantages include:

(1) The heat of the biomass pyrolysis process comes from the heat in the catalyst regenerator, without heat carrier, which reduces the wear of the heat carrier on the reactor, and at the same time, reduces the separation of the reaction product and the heat carrier. In addition, the biochar generated by the biomass pyrolysis process and the coke generated by the catalytic cracking process are burned to provide heat, which makes full use of the heat of the spent agent burning and reduces energy consumption.

(2) The process provided by this application realizes the generation of high-quality biogasoline and diesel from biomass at one time, and the pyrolysis reactor and catalytic cracking reactor can flexibly change the operating conditions. The process of catalytic cracking of petroleum fractions can make full use of the scale effect of the device, alleviate the impact of unstable supply of biomass raw materials, and reduce production costs.

(3) In particular, the biomass pyrolyzer of the present application is coupled with the catalytic cracking device of the two-stage riser reactor, the cracking riser carries out the catalytic cracking reaction of fresh raw materials, and the modified riser carries out the catalysis of pyrolysis oil and recycled oil Cracking can not only avoid the impact of pyrolysis oil on the catalytic cracking of fresh raw materials, but also realize the separate control of catalytic cracking of fresh raw materials and upgrading of biomass pyrolysis oil.

The following examples only further illustrate the present invention, but do not limit the protection scope of the present invention.

Example 1

Referring to accompanying drawing 1, this embodiment is a reaction device in which a biomass pyrolyzer is coupled with a catalytic cracking reaction device of a two-stage riser generator. The catalytic cracking reaction device includes a two-stage riser reactor and a catalytic cracking reaction settler II. The two-stage riser reactors are respectively a catalytic cracking riser reactor I' and a reforming riser reactor I.

As shown in Figure 1, the biomass pyrolysis reactor III is placed in the catalyst regenerator IV through the bottom of the catalyst regenerator, the pyrolysis reactor III is a cylindrical straight pipe, and the upper end of the pyrolysis reactor III is located in the catalyst regenerator Upper part inside IV. The catalyst regenerator IV is connected with the cracking riser reactor I' and the upgrading riser reactor I respectively.

The upper end of the biomass pyrolysis reactor III is connected to the cyclone separator 14, and the pyrolysis gas and coke in the biomass pyrolysis product are separated in the cyclone separator. The top outlet of the cyclone separator is connected to the condenser VII, and the pyrolysis gas enters the condenser VII to condense. The condenser VII is connected to the oil-gas separation tank VI, and the condensed pyrolysis products are separated in the oil-gas separation tank VI, and separated into uncondensed non-condensable gas and pyrolysis oil, and the non-condensable gas enters the biomass as pre-lifting gas 3 In the pyrolysis reactor III, according to the demand, the pyrolysis oil 4 enters the upgrading riser reactor I for further catalytic upgrading reaction.

The catalytic cracking settler is connected to the catalyst regenerator IV through the catalyst standby inclined pipe 15, and the spent catalyst in the settler is sent to the regenerator for regeneration. The catalyst regenerator IV is connected with the cracking riser reactor I' and the reforming riser reactor I through the catalyst regeneration inclined pipes (16, 16'). The catalytic cracking reaction device can be the reaction device used for all petrochemical catalytic reactions in the prior art, and the pyrolysis oil can be mixed with the raw materials used for its reforming reaction or only enter the reforming riser reactor I for pyrolysis oil to carry out catalytic cracking reaction.

The catalytic cracking reaction settler II is equipped with a cyclone separator. The upper ends of the catalytic cracking riser reactor I' and the reforming riser reactor I are respectively connected with the cyclone separator, and the oil gas and the catalyst are separated through the cyclone separator, and the separated catalyst is passed through the catalyst standby inclined pipe 15 Enter the catalyst regenerator III for combustion regeneration. The top of the catalytic cracking reaction settler II is connected to the fractionation tower V, and the oil and gas obtained after the reforming reaction enters the fractionation tower V to further separate the corresponding components and recycle oil 13, and the recycle oil can be further returned to the reforming reactor I carry out modification reaction.

The process flow of the above-mentioned device coupled with biomass pyrolysis and catalytic cracking includes:

The dried and pulverized biomass raw material 1 enters the bottom of the biomass pyrolysis reactor III through the feeder, and the pyrolysis non-condensable gas 3 passed through the bottom of the pyrolysis reactor III is fluidized and lifted into the interior of the pyrolysis reactor III. Under the heating of the high-temperature catalyst and flue gas in the catalyst regenerator IV, the pyrolysis reaction is carried out to generate pyrolysis gas and biochar, wherein the outlet temperature of the biomass pyrolysis reactor is 500-650°C, and the reaction pressure is 0.1-0.4 MPa, the time of biomass pyrolysis reaction is 0.5-3s. The temperature at atmospheric pressure in the catalyst regenerator IV is 600-720°C. The catalyst and flue gas in the catalyst regenerator are used to transfer heat to the biomass pyrolysis reactor for pyrolysis reaction of biomass.

After the pyrolysis oil gas 2 and biochar flowing out from the top of pyrolysis reactor III are separated by a cyclone separator, the biochar enters the catalytic regenerator IV and burns to release heat, which is combined with the newly added fuel 6 to regenerate the standby catalyst. The pyrolysis oil gas enters the oil-gas separation tank VI after being condensed by the condenser VII, and is separated into pyrolysis oil 4 and non-condensable gas 3 . The non-condensable gas enters the bottom of the biomass pyrolysis reactor III as fluidizing gas, and the pyrolysis oil 4 enters the reforming riser reactor I. Under the action of the pre-stripping gas 7, the pyrolysis oil contacts and reacts with the regenerated catalyst And move upward, wherein, the outlet temperature of the upgrading reactor is 450-600°C, the reaction time is 1-4s, and the reaction pressure is 0.1-0.4MPa. The fresh catalytic cracking raw material 5 is heat-exchanged with the pyrolysis gas in the condenser VII, and the refractory oil 13 fraction separated from the fractionation tower enters the cracking riser reactor I', and contacts with the regenerated catalyst to carry out the catalytic cracking reaction, wherein, the cracking The outlet temperature of the riser reactor is 450-550°C, the reaction time is 1-3s, and the reaction pressure is 0.1-0.4MPa. The reaction substance entering the catalytic cracking riser I' is determined according to actual conditions, and the raw material for catalytic cracking can be one of fresh catalytic cracking raw material, back-refined oil fraction, or a combination of the two or more.

At the outlet of the catalytic cracking reaction unit, the reaction oil gas and the coked catalyst are separated by a cyclone separator, and the coked catalyst enters the stripping section of the settler II for stripping to desorb the adsorbed oil gas, reduce the coke yield, and strip The final waiting catalyst agent enters the catalyst regenerator IV through the catalyst waiting inclined pipe 15 for burning and regenerating; the reaction oil gas 9 enters the fractionating tower V and is further separated into cracked gas 10, gasoline 11 (<200°C), diesel oil 12 (200-500 ℃), back refined oil 13 (350-500 ℃) and oil slurry 14 (>500 ℃). Refined oil is returned to the cracking riser for secondary conversion.

Experimental example 1:

In this experimental example, a reaction device in which the biomass pyrolyzer in Example 1 is coupled with the catalytic cracking reaction device of the two-stage riser generator is used. Using pine sawdust as raw material, fixed fluidized bed pyrolysis reactor, fluidizing gas as nitrogen, biomass pyrolysis reaction time 20s, the obtained product distribution and properties of pyrolysis oil are shown in Table 1 and Table 2.

Table 1 Distribution of pyrolysis products

Table 2 Properties of pyrolysis oil

The pyrolysis oil (PO) obtained at the above-mentioned reaction temperature of 510°C is subjected to catalytic cracking and upgrading, the upgrading riser reactor adopts a fixed fluidized bed reactor, and the reaction temperature of the pyrolysis oil catalytic cracking is 500°C. In the catalytic cracking riser reactor, the catalytic cracking reaction is carried out with the vacuum gas oil of petroleum fraction as the raw material, and the reaction temperature is 500°C. Two commercial catalytic cracking balancers with USY and ZSM-5 as active components were used as catalysts respectively, and the weight hourly space velocity was 15h ^-1 . The properties of vacuum wax oil are shown in Table 3 and the product distribution is shown in Table 4.

Table 3 Basic properties of a vacuum wax oil

Table 4 Distribution of bio-oil upgrading and catalytic cracking products of petroleum fractions

Claims (10)

1. a kind of method that biomass pyrolytic is coupled with catalytic cracking reaction, comprising:

Catalytically cracked stock carries out catalysis reaction in catalytic cracking reaction device, and the oil gas after reaction and reclaimable catalyst pass through After cyclone separator separation, reclaimable catalyst, which enters in catalyst regenerator, to be burnt, and oil gas is separated in fractionating column；

Biomass material enters biomass pyrolysis reactor and carries out pyrolytic reaction, and biomass pyrolysis reactor is placed in catalyst regeneration Inside device；

The pyrolysis oil obtained after biomass pyrolytic reaction, which enters, carries out catalysis reaction in catalytic cracking reaction device；

Preferably, the fraction that oil gas is isolated in fractionating column includes: cracked gas, gasoline, diesel oil, recycle oil, and recycle oil is again Catalysis reaction is carried out in back to catalytic cracking reaction device.

2. the method according to claim 1, wherein the product after biomass pyrolytic reaction is after condensation process Pyrolysis oil and fixed gas are obtained, fixed gas enters in biomass pyrolysis reactor；

Preferably, condensation process uses air-cooled, water cooling or other condensing modes, 40~80 DEG C of final condensation temperature, and pressure is Normal pressure.

3. method according to claim 1 or 2, which is characterized in that catalytically cracked stock carries out catalytic cracking reaction dress Before setting, heat exchange is carried out with thermal decomposition product.

4. method according to claim 1-3, which is characterized in that catalytic cracking reaction device includes that cracking is promoted Pipe reactor and modification riser reactor, catalytically cracked material or/and recycle oil, which enter in cracking riser reactor, to carry out Reaction, the pyrolysis oil after biomass pyrolytic reaction, which enters in modification riser reactor, is reacted.

5. method according to claim 1-3, which is characterized in that the coke burning occurred in catalyst regenerator Reaction, temperature are 600-720 DEG C；

The outlet temperature of biomass pyrolysis reactor is 500~650 DEG C, and reaction pressure is 0.1~0.4MPa.

6. method according to claim 1-3, which is characterized in that it is 450- that modification, which promotes reactor outlet temperature, 600 DEG C, reaction time 1-4s.Reaction pressure is 0.1-0.4MPa；

Cracking riser reactor outlet temperature is 450-550 DEG C, reaction time 1-3s, reaction pressure 0.1-0.4MPa.

7. the reaction unit that a kind of biomass pyrolytic is coupled with petroleum distillate catalytic cracking, including biomass pyrolysis reactor, urge Change cracking reaction device and catalyst regenerator, wherein biomass pyrolysis reactor is placed in inside catalyst regenerator；

It is preferred that catalytic cracking reaction device includes cracking riser reactor and modification riser reactor.

8. reaction unit according to claim 7, which is characterized in that catalyst regenerator is the tank body of variable diameter, on tank body Partial diameter is greater than the diameter of tank body lower part point, and tank body top is divided into dilute phase section, and the lower part of tank body is divided into close phase section,

At least two groups of cyclone separators are equipped in dilute phase section, wherein first group of cyclone separator and biomass pyrolysis reactor Upper end connection.

9. reaction unit according to claim 8, which is characterized in that in dilute phase section, second group of cyclone separator enters Mouth end is connected to settling section, and outlet end communicates with the outside world.

10. reaction unit according to claim 8 or claim 9, which is characterized in that the caliber and catalyst of biomass pyrolytic device are again The caliber ratio 0.1:1-0.5:1 of the close phase section of raw device.