CN-122006649-A - Reaction device and reaction method for pyrolysis of gas-solid double-circulation pulverized coal

CN122006649ACN 122006649 ACN122006649 ACN 122006649ACN-122006649-A

Abstract

The invention relates to a reaction device and a reaction method for gas-solid double-circulation pulverized coal pyrolysis, wherein the reaction device comprises an uplink reactor, a settler, a continuous oxidation self-heating type uplink pipe reactor, an oxidant preheater, a heat carrier heater, a feeding unit, a gas-solid separation unit, an oil-gas separation unit and a circulating gas pipeline, wherein the inlet end of the uplink reactor is connected with the bottom heat carrier outlet of the heat carrier heater, the pulverized coal outlet of the feeding unit and the outlet of the circulating gas pipeline, the outlet end of the uplink reactor is positioned in the settler, the bottom pulverized coal outlet of the settler and the outlet of the oxidant preheater are connected with the continuous oxidation self-heating type uplink pipe reactor, the outlet end of the continuous oxidation self-heating type uplink pipe reactor is connected with the top inlet of the heat carrier heater, and the bottom pulverized coal outlet of the settler is connected with the bottom inlet of the heat carrier heater through a circulating inclined pipe. The reaction device provided by the invention can realize equipment miniaturization, temperature control precision and operation stabilization, and improves the charcoal burning efficiency.

Inventors

CHEN SHUQUN
REN PENG
ZHANG MIAO
WANG QINGYUAN
FENG JIANHUA
CHEN PENG
LI HAO
YU QINGJIANG

Assignees

胜帮科技股份有限公司

Dates

Publication Date: 20260512
Application Date: 20260401

Claims (10)

1. The reaction device for pyrolyzing the pulverized coal in a gas-solid double-circulation mode is characterized by comprising an uplink reactor, a settler, a continuous oxidation self-heating type uplink pipe reactor, an oxidant preheater, a heat carrier heater, a feeding unit, a gas-solid separation unit, an oil-gas separation unit and a circulating gas pipeline; The inlet end of the uplink reactor is respectively connected with the bottom heat carrier outlet of the heat carrier heater, the pulverized coal outlet of the feeding unit and the outlet of the circulating gas pipeline; The outlet end of the uplink reactor is positioned in the settler; The outlet of the bottom coke breeze of the settler and the outlet of the oxidant preheater are respectively connected with the inlet end of the continuous oxidation self-heating type up-tube reactor, and the outlet end of the continuous oxidation self-heating type up-tube reactor is connected with the top inlet of the heat carrier heater; The bottom coke breeze outlet of the settler is connected with the bottom inlet of the heat carrier heater through a circulating inclined pipe; and a gas phase outlet at the top of the settler is sequentially connected with the gas-solid separation unit and the oil-gas separation unit.
2. The reactor apparatus according to claim 1, wherein the upgoing reactor includes a first straight pipe portion, a bent portion, and a second straight pipe portion in a gas flow direction, the bent portion having a bent angle of 90 °.
3. The reactor according to claim 1 or 2, wherein the continuous oxidation autothermal up-tube reactor comprises a first horizontal section, a first curved section, a vertical section, a second curved section and a second horizontal section in the gas flow direction, the first curved section and the second curved section each having a curved angle of 90 °; Preferably, the vertical section has an aspect ratio of (20-50): 1; preferably, the continuous oxidation self-heating type up-tube reactor is of a hollow tube structure.
4. A reaction apparatus according to any one of claims 1 to 3 wherein the oxidant preheater is provided with a first oxidant inlet; preferably, the bottom of the settler is provided with a coke breeze product outlet; preferably, the heat carrier heater is provided with a second oxidant inlet.
5. The reaction apparatus of any one of claims 1 to 4, wherein a heat carrier heating temperature controller is provided outside the heat carrier heater; Preferably, the heat source inlet of the heat carrier heating temperature controller is connected with the bottom heat carrier outlet of the heat carrier heater; Preferably, a heat source outlet of the heat carrier heating temperature controller is connected with a bottom inlet of the heat carrier heater through a heat carrier circulating pipeline; Preferably, the heat carrier circulation line is further provided with an air inlet to make the transport gas of the heat carrier circulation line air.
6. The reaction device of any one of claims 1-5, further comprising a waste heat recovery unit; preferably, a top gas phase outlet of the oil-gas separation unit is communicated with a circulating gas pipeline through a cold source side of the waste heat recovery unit; preferably, the top flue gas outlet of the heat carrier heater communicates with the heat source side of the waste heat recovery unit.
7. The reaction apparatus according to any one of claims 1 to 6, wherein the gas phase outlet of the gas-solid separation unit is connected to the oil-gas separation unit; preferably, the top gas phase outlet of the oil-gas separation unit is connected with the gas product outlet; Preferably, the oil-gas separation unit is provided with a coal tar product outlet.
8. A reaction method for gas-solid double-circulation pulverized coal pyrolysis, which is characterized by adopting the reaction device for gas-solid double-circulation pulverized coal pyrolysis according to any one of claims 1-7, and comprising the following steps: Conveying pulverized coal and a high-temperature heat carrier through circulating coal gas, and carrying out pyrolysis reaction in an uplink reactor to obtain a mixed reaction product containing coal gas, coal tar and pulverized coke; Carrying out first gas-solid separation on the mixed reaction product in a settler, settling part of powdered coke at the bottom of the settler, carrying out second gas-solid separation on the mixed reaction product of the residual gas phase in a gas-solid separation unit, and carrying out oil-gas separation on the gas phase obtained by the second gas-solid separation in the oil-gas separation unit to obtain circulating gas, gas products and coal tar products; Part of coke breeze at the bottom of the settler and preheated oxidant from an oxidant preheater are subjected to a first combustion reaction in a continuous oxidation self-heating type up-tube reactor to obtain high-temperature coke breeze, and the high-temperature coke breeze enters a heat carrier heater; part of the coke breeze at the bottom of the settler, the high-temperature coke breeze from the continuous oxidation self-heating type up-pipe reactor and the oxidant are subjected to a second combustion reaction in a heat carrier heater to obtain a high-temperature heat carrier for pyrolysis reaction; And the coke breeze output at the bottom of the settler is a coke breeze product.
9. The reaction process of claim 8, wherein the temperature of the pyrolysis reaction is 450-650 ℃; Preferably, the pyrolysis reaction time is 1 to 10s; preferably, the mass ratio of the high-temperature heat carrier to the pulverized coal in the pyrolysis reaction is (3-10): 1; Preferably, the temperature of the first combustion reaction is 600-950 ℃; Preferably, the temperature of the second combustion reaction is 600-950 ℃; preferably, the residence time of the coke breeze in the continuous oxidation autothermal up-pipe reactor is 1-10s; preferably, the oxidant comprises air or oxygen-rich gas; Preferably, the temperature of the preheated oxidant is in the range of 200-600 ℃.
10. The reaction method according to claim 8 or 9, wherein the flue gas generated by the second combustion reaction is used as a heat source to preheat the circulating gas in the waste heat recovery unit, and the preheated circulating gas is obtained and used for conveying materials; preferably, the temperature of the preheated circulating gas is 200-400 ℃; Preferably, part of the high-temperature heat carrier in the heat carrier heater enters a heat source side of the heat carrier heating temperature controller to heat the heat taking medium to generate medium-pressure steam, and then the medium-pressure steam is conveyed back into the heat carrier heater through air to regulate and control the temperature of the high-temperature heat carrier; preferably, the heat extraction medium comprises deoxygenated water; preferably, the load adjustment range of the heat taking medium is 0-100%.

Description

Reaction device and reaction method for pyrolysis of gas-solid double-circulation pulverized coal Technical Field The invention relates to the technical field of coal chemical industry, in particular to a reaction device and a reaction method for gas-solid double-circulation pulverized coal pyrolysis. Background Along with the increase of energy demand and the improvement of environmental protection requirements, the efficient clean conversion of low-order pulverized coal is the research focus in the field of coal chemical industry at present. The pulverized coal pyrolysis process is an effective low-rank coal conversion technology, has realized the operation of a megaton device, and has good application prospect. However, two major technical bottlenecks still exist in the field of pulverized coal pyrolysis at present. Firstly, the charcoal-fired heating system needs to be optimized. Because the operation pressure of pulverized coal pyrolysis is low, and the heat carrier heater needs to simultaneously meet core functions such as pulverized coal feeding distribution, oxidant distribution and mixed combustion, heat carrier mixed heating, gas-solid two-phase separation, combustion tail gas emission and the like. In order to meet the cooperative realization of the functions, a larger redundant space needs to be reserved for the heat carrier heater, wherein the redundant space comprises a powder coke and oxidant mixing space, a gas-solid separation buffer space, a heat carrier uniform temperature and storage space, an operation and maintenance space and the like, so that mutual noninterference among all functional areas is ensured, the heat carrier heater is further caused to adopt a large-volume and thick-pipe-diameter design, the occupied area and the whole size of equipment are greatly increased, and the investment cost is increased. Secondly, the operation flexibility of the heat carrier heater is small. The heat carrier heater is usually in a turbulent bed form, when the load changes, the flow of the oxidant also changes correspondingly, and when the flow changes, if the flow speed decreases, uneven temperature distribution can be caused, and a local overtemperature phenomenon occurs. Thus, the lack of operational flexibility limits the adaptability of the heat carrier heater to different operating conditions. Therefore, based on the technical bottleneck, how to realize miniaturization, temperature control precision and operation stabilization of equipment is a technical problem to be solved at present. Disclosure of Invention The invention aims to provide a reaction device and a reaction method for pyrolysis of gas-solid double-circulation pulverized coal. In order to achieve the aim of the invention, the invention adopts the following technical scheme: In a first aspect, the invention provides a reaction device for pyrolyzing pulverized coal in a gas-solid dual-cycle manner, which comprises an uplink reactor, a settler, a continuous oxidation self-heating type uplink pipe reactor, an oxidant preheater, a heat carrier heater, a feeding unit, a gas-solid separation unit, an oil-gas separation unit and a circulating gas pipeline; The inlet end of the uplink reactor is respectively connected with the bottom heat carrier outlet of the heat carrier heater, the pulverized coal outlet of the feeding unit and the outlet of the circulating gas pipeline; The outlet end of the uplink reactor is positioned in the settler; The outlet of the bottom coke breeze of the settler and the outlet of the oxidant preheater are respectively connected with the inlet end of the continuous oxidation self-heating type up-tube reactor, and the outlet end of the continuous oxidation self-heating type up-tube reactor is connected with the top inlet of the heat carrier heater; The bottom coke breeze outlet of the settler is connected with the bottom inlet of the heat carrier heater through a circulating inclined pipe; and a gas phase outlet at the top of the settler is sequentially connected with the gas-solid separation unit and the oil-gas separation unit. The reaction device provided by the invention adopts a closed loop system comprising a settler, a heat carrier heater, an uplink reactor and a continuous oxidation self-heating uplink pipe reactor, wherein the settler is generally positioned at the upper part of the heat carrier heater, and the coke breeze at the bottom of the settler is conveyed into the heat carrier heater through a circulating inclined pipe. The continuous oxidation self-heating type up-tube reactor is specially designed and arranged between the bottom of the settler and the top of the heat carrier heater, so that the coke breeze pre-burning, the intensified fluidization and the directional transportation can be integrated, and the high efficiency of the coke breeze is improved. The continuous oxidation self-heating type up-tube reactor and the heat carrier heater provided by the invention cooperate to form a core