CN113278437A

CN113278437A - Rising temperature sudden-falling type double-pyrolysis-section internal heating type moving bed coal vertical pyrolysis furnace

Info

Publication number: CN113278437A
Application number: CN202110621789.2A
Authority: CN
Inventors: 何巨堂; 何艺帆
Original assignee: Luoyang Ruihua New Energy Technology Development Co ltd
Current assignee: Luoyang Ruihua New Energy Technology Development Co ltd
Priority date: 2021-05-30
Filing date: 2021-05-30
Publication date: 2021-08-20

Abstract

An ascending temperature sudden-falling type double-pyrolysis-section internal heating moving bed coal vertical pyrolysis furnace, wherein hot flue gas formed by a mixing chamber of fuel gas and combustion-supporting gas arranged at the bottom of a stripping section is used as stripping heating gas to heat up low-temperature pyrolysis semicoke; at the bottom of the low-temperature pyrolysis section, low-temperature coal gas is generally used as temperature-adjusting cooling gas to cool stripping section output gas from the stripping section, a gas heat carrier for the low-temperature pyrolysis section with suddenly reduced temperature is formed, and the gas heat carrier ascends to contact with the preheated carbon material to carry out low-temperature pyrolysis on the gas heat carrier; the pyrolysis furnace carries out segmented pyrolysis at the optimal temperature; the coal material entering the furnace descends and passes through a preheating section, a low-temperature pyrolysis section and a stripping section, and can continue to pass through a cooling section and a coke quenching section; the low-temperature pyrolysis section avoids a large amount of tar from being burned out, the stripping section reduces the volatile component of the semicoke product, improves the fixed carbon content of the semicoke, improves the strength of the semicoke, generates stripping clean gas and improves the gas yield; the combustion-supporting gas is air or oxygen-rich gas or pure oxygen; the pyrolysis furnace can be provided with a direct gas cooling section for stripping the semicoke and recover the sensible heat of the semicoke by using cold circulating gas.

Description

Rising temperature sudden-falling type double-pyrolysis-section internal heating type moving bed coal vertical pyrolysis furnace

Technical Field

The invention relates to an internal heating type moving bed coal vertical pyrolysis furnace, in particular to an ascending temperature sudden-falling type double-pyrolysis-section internal heating type moving bed coal vertical pyrolysis furnace.A hot flue gas formed by a mixing chamber of fuel gas and combustion-supporting gas arranged at the bottom of a stripping section is used as stripping heating gas to heat up low-temperature pyrolysis semicoke; at the bottom of the low-temperature pyrolysis section, low-temperature coal gas is generally used as temperature-adjusting cooling gas to cool stripping section output gas from the stripping section, a gas heat carrier for the low-temperature pyrolysis section with suddenly reduced temperature is formed, and the gas heat carrier ascends to contact with the preheated carbon material for low-temperature pyrolysis; the pyrolysis furnace carries out segmented pyrolysis at the optimal temperature; the coal material entering the furnace descends and passes through a preheating section, a low-temperature pyrolysis section and a stripping section, and can continue to pass through a cooling section and a coke quenching section; the low-temperature pyrolysis section avoids a large amount of tar from being burned out, the stripping section reduces the volatile component of the semicoke product, improves the fixed carbon content of the semicoke, improves the strength of the semicoke, generates stripping clean gas and improves the gas yield; the combustion-supporting gas is air or oxygen-rich gas or pure oxygen; the pyrolysis furnace can be provided with a direct gas cooling section for stripping the semicoke and recover the sensible heat of the semicoke by using cold circulating gas. The gas consumption is reduced, and a coke quenching section using liquid water or vapor can be arranged; when the combustion-supporting gas is rich oxygen gas or pure oxygen gas, the produced gas belongs to low-nitrogen carbon dioxide-rich gas, and is beneficial to separation and recovery of hydrogen and methane; the carbon dioxide gas replacement in the coal feeding bin can reduce the contents of oxygen and nitrogen in the coal gas product; the overall operation of the invention, which can be formed into a variety of configurations and for a variety of uses, tends to optimize pyrolysis furnaces.

Background

The coal material can produce coal tar with higher yield and coal gas with higher yield through low-temperature pyrolysis or low-temperature dry distillation, and simultaneously produce low-temperature pyrolysis semicoke with certain quality. The hydrogen, carbon monoxide and methane contained in the coal gas can be used for extracting the hydrogen and the methane. The coal tar can be used for extracting phenols and producing clean oil products by hydrogenation. The pyrolytic semicoke can be used as a reducing agent for ferroalloy coke and calcium carbide coke. At present, the semicoke (or semi coke) capacity of a domestic low-temperature coal pyrolysis device is about 1 hundred million tons, an industry is formed, an internal heating type vertical pyrolysis furnace with a gas heat carrier is mainly adopted, and coal materials are directly heated for pyrolysis by hot waste gas (smoke and a circulating gas heat carrier) generated by gas oxygen-deficient combustion (combustion-supporting gas is air).

The national standard GB/T25212-2010 Lanzhong product is divided into varieties and grades, standard values of all grades of all performance indexes of the Lanzhong are specified, and it can be seen that sometimes the index values have small difference, but the grades are completely different; for example, the fixed carbon index FCd of the semi-coke is 74.01-92.00%, and the fixed carbon index is increased by one grade every time the fixed carbon index is increased by 2%; for example, the semi-coke volatile index Vdaf is between 15.00% and 4.00%, and the grade is increased when the volatile index is reduced by 5%; the grade rise means that the service performance and the application range are remarkably improved, the price difference of products is huge, for example, the semi-coke volatile component index Vdaf is reduced from 7.0 percent (which belongs to the range of 5.01-10.00 percent and belongs to the V-2 grade) to 4.5 percent (which belongs to the range of less than or equal to 5.00 percent and belongs to the V-1 grade), namely, the grade is increased, the price difference of the products reaches 100-150 yuan/ton or even higher, because the pyrolysis semi-coke is a pyrolysis product with the highest yield, the yield is greatly increased, for example, for a semi-coke production plant with 100 million tons/year, the sales difference is 1.0-1.5 million yuan/year or even higher.

In fact, if the normal operation of the low-temperature pyrolysis process can be ensured, the volatilization and combination theory of the semi coke is further reduced, and the following beneficial effects can be produced:

the yield of high-value products (coal gas and tar) is improved, and the yield value is increased;

secondly, the content of volatile components of the semi-coke is reduced, the strength of the semi-coke is increased, the price of the semi-coke is improved, and the output value is increased.

Under the condition of a single pyrolysis section pyrolysis furnace or a single pyrolysis section pyrolysis furnace, when the pyrolysis final temperature is 600-900 ℃, the coal gas yield is particularly obviously increased by taking low-rank coal as an example; the pyrolysis time directly influences the pyrolysis degree and the product distribution of the low-rank coal, and the extension of the pyrolysis time can increase the secondary cracking degree of tar, so that the tar yield is reduced, and the coal gas yield is increased.

Under the condition of the same coal material, a higher pyrolysis end temperature is required for reducing semi-coke volatile components, but the conventional method for increasing the pyrolysis end temperature (such as formation of intermediate-temperature pyrolysis) inevitably changes low-temperature pyrolysis into intermediate-temperature pyrolysis, more heavy volatile components in coal are thermally condensed into coke (i.e. loss of ignition) to reduce the yield of coal tar, the higher the pyrolysis end temperature is, the more easy the secondary cracking of the tar is, and when the pyrolysis end temperature is higher than a certain optimal value (changed due to different coal types), the sharp increase of the secondary cracking reaction of the tar causes the actual yield of the tar to be reduced, and simultaneously the yield of coal gas is increased; the coal tar steam thermal cracking rate and the thermal condensation rate are increased (namely, the coal tar steam thermal cracking rate and the thermal condensation rate are increased), the quality of the coal tar is also deteriorated, the hydro-upgrading difficulty is increased, and the use value is reduced.

The first problem of present internally heated low temperature pyrolysis device of low order coal ubiquitous is that blue charcoal volatile matter is on the high side, blue charcoal intensity is on the low side, among the prior art scheme, it must improve the pyrolysis final temperature to reduce blue charcoal volatile matter, must form the tar loss of burning, this is mainly because the control mode of pyrolysis temperature field causes, and present blue charcoal stove pyrolysis zone temperature field, along the decline direction of coal charge, the temperature progressively changes, does not have the temperature of rising to fall the upright pyrolysis oven of two pyrolysis section internally heated moving bed coal of formula or pyrolysis mode of operation suddenly. Actually, a low-temperature pyrolysis section and a medium-temperature pyrolysis section which are independently and flexibly controlled in pyrolysis temperature are not formed, the medium-temperature pyrolysis section is used for ensuring that the volatile components of the semi coke are reduced, and meanwhile, the low-temperature pyrolysis section is independently controlled in temperature, so that the yield and the quality of the tar are improved.

The second problem commonly existing in the existing low-rank coal internally heated medium-low temperature pyrolysis device is that the content of nitrogen in coal gas is about 50%, the content of hydrogen and methane is low, the calorific value is low, the low-rank coal internally heated medium-low temperature pyrolysis device is rich in light hydrocarbon, oxygen, hydrogen sulfide, organic sulfur, ammonia, water vapor and the like, the cost of hydrogen recovery and methane recovery is high, the utilization value is low, the comprehensive utilization of processing of effective gas (hydrogen and methane) in coal gas is restricted to a certain extent, the use value of the effective gas in coal gas is restricted, and the benefit of the device is reduced. The main reasons are that the combustion control difficulty of high-purity combustible gas coal gas and oxygen enrichment or pure oxygen is high, the treatment is not good, coal sintering and caking at the outlet of a flame path air distribution brick are caused, the discharged flue gas is not uniform, the temperature of a hearth of a pyrolysis furnace is not uniform, the quality of semi coke cannot be guaranteed, and the production cannot be realized.

The idea of the invention is: an ascending temperature sudden-falling type double-pyrolysis-section internal heating moving bed coal vertical pyrolysis furnace, wherein hot flue gas formed by a mixing chamber of fuel gas and combustion-supporting gas arranged at the bottom of a stripping section is used as stripping heating gas to heat up low-temperature pyrolysis semicoke; at the bottom of the low-temperature pyrolysis section, low-temperature coal gas is generally used as temperature-adjusting cooling gas to cool stripping section output gas from the stripping section, a gas heat carrier for the low-temperature pyrolysis section with suddenly reduced temperature is formed, and the gas heat carrier ascends to contact with the preheated carbon material for low-temperature pyrolysis; the pyrolysis furnace carries out segmented pyrolysis at the optimal temperature; the coal material entering the furnace descends and passes through a preheating section, a low-temperature pyrolysis section and a stripping section, and can continue to pass through a cooling section and a coke quenching section; the low-temperature pyrolysis section avoids a large amount of tar from being burned out, the stripping section reduces the volatile component of the semicoke product, improves the fixed carbon content of the semicoke, improves the strength of the semicoke, generates stripping clean gas and improves the gas yield; the combustion-supporting gas is air or oxygen-rich gas or pure oxygen; the pyrolysis furnace can be provided with a direct gas cooling section for stripping the semicoke and recover the sensible heat of the semicoke by using cold circulating gas. The gas consumption is reduced, and a coke quenching section using liquid water or vapor can be arranged; when the combustion-supporting gas is rich oxygen gas or pure oxygen gas, the produced gas belongs to low-nitrogen carbon dioxide-rich gas, and is beneficial to separation and recovery of hydrogen and methane; the carbon dioxide gas replacement in the coal feeding bin can reduce the contents of oxygen and nitrogen in the coal gas product; the overall operation of the invention, which can be formed into a variety of configurations and for a variety of uses, tends to optimize pyrolysis furnaces.

The following are several known close technical solutions in comparison with the present invention.

Chinese patent ZL200610076463.1 is a hierarchical clean utilization method of fine coal with pyrolysis as the first order, including fluidized bed drying pyrolysis process, multicycle fluidized bed gasification process, circulating fluidized bed boiler combustion process, the raw coal gets into the drying pyrolysis device with the fine coal of certain granularity and carries out the drying pyrolysis reaction after the raw coal processing device processing screening, and the high carbon semicoke powder after the pyrolysis gets into multicycle fluidized bed gasification device and carries out multicycle gasification reaction, the synthetic gas that produces gets into chemical production, then send the lower grey coke of solid phase carbon content into circulating fluidized bed boiler, make it fully burn in circulating fluidized bed boiler. In the chinese patent ZL200610076463.1, the powdered coal is dried in a fluidized bed, pyrolyzed at low temperature in the fluidized bed, and pyrolyzed at medium temperature in the fluidized bed, and the semi-coke powder discharged from the medium temperature pyrolysis bed enters a dense phase fluidized bubbling gasification bed to react with steam while gasifying and moving downward.

Chinese patent ZL200610076463.1, first, it is not a downward moving bed of particles, and it cannot realize a nearly pure countercurrent one-way temperature-rising carbonization mode of gradually rising carbon material temperature in a single carbonization zone, and along the rising path of gas in carbonization zone, the temperature is gradually lowered, but because the coal bed layer belongs to a fluidized bed rather than a downward moving bed, it is impossible to form an operation mode of gradually rising carbonization zone temperature; secondly, only one path of pyrolysis gas heat carrier is a natural operation result of entering the bottom of the intermediate temperature pyrolysis section by the hot combustion flue gas of the fuel gas and the air from the independent combustion chamber, and the temperature of the gas entering the low temperature pyrolysis section and leaving the intermediate temperature pyrolysis section is not provided with an independent temperature regulating facility for the gas at the inlet of the low temperature pyrolysis section, so that the aim of the invention cannot be achieved, and the invention has no comparability with the technical scheme of the invention. In fact, chinese patent ZL200610076463.1 cannot be applied to lump coal downward moving bed dry distillation, for example, because lump coal cannot be transported in flow fields between the drying bed and the low-temperature dry distillation bed and between the low-temperature dry distillation bed and the medium-temperature dry distillation bed by using pipes, while the lump coal downward moving bed dry distillation retort is arranged in a continuous cavity between the drying bed and the low-temperature dry distillation bed and between the low-temperature dry distillation bed and the medium-temperature dry distillation bed.

Chinese patent ZL200720012049.4 is an internal heating vertical furnace for dry distillation of lignite, including dry distillation messenger, nozzle, gas vent etc., this vertical furnace is made up of porous dry distillation room, the dry distillation room cross section of each hole is the variable cross section, dry distillation room upper portion is equipped with the bed of cloth board, the dry distillation room top is equipped with the gas vent, be equipped with the heating gas room in vertical furnace, be equipped with regulating plate and gas distribution brick in the heating gas room, vertical furnace is cut into multilayer firebrick annular structure by opposite sex's firebrick, the furnace body side is equipped with the coal gas nozzle, be equipped with the protection stove ironware all around.

In the chinese patent ZL200720012049.4, the facility for controlling the operation temperature of the carbonization section is a heating gas chamber, in which an adjusting plate and a gas distribution brick are arranged, and the temperature field of the carbonization zone of the semi-coke furnace, therefore, the object of the present invention cannot be achieved, and there is no comparability with the technical scheme of the present invention.

The Chinese patent ZL200920222643.5 external combustion internal heating type coal carbonization furnace sequentially comprises from top to bottom: a drying section for drying the raw material coal; a dry distillation section for performing dry distillation treatment on the dried raw material coal, wherein the raw material coal forms a dry distillation product after the dry distillation treatment; a cooling section for cooling the dry distillation product produced in the dry distillation section by introducing a cooling carrier; and a cooling device for introducing a cooling carrier into the cooling section. The utility model discloses an external combustion internal heating type coal gas retort utilizes cooling device to cool off the quenching to the dry distillation product, and is efficient, output is big.

In the Chinese patent ZL200920222643.5, an independent drying section and an independent dry distillation section are included, and a preheating section can be arranged on the drying section; the facility for controlling the operation temperature of the dry distillation section is added with a path of gas heat carrier, so the aim of the invention can not be realized, and the invention has no comparability with the technical scheme of the invention.

The Chinese patent ZL201220003775.0 vertical low-temperature dry distillation furnace is composed of a feeding section, a drying section, a material sealing section, a dry distillation section, a cooling section and a discharging section. The method is characterized in that: the drying section and the dry distillation section are used for drying and dry distillation of the materials outside the tube by heating the hot flue gas in the low-temperature fire tube 2 and the high-temperature fire tube 10. The dry exhaust steam is collected and cooled by a low-temperature cloth heat conduction fin 7 and then sent to a biological deodorization device, the smoke is discharged outside by a low-temperature fire tube 2, a smoke outlet 3, an exhaust fan 4, a regulating valve 5 and a low-temperature flue 6, and the self-produced gas generated by dry distillation is collected by a high-temperature cloth heat conduction fin 12 and a self-produced gas collecting hood 9 and then sent to a combustion furnace 14 as a heat source. The dry distillation product is cooled by cooling circulating water in the spiral plate type heat exchanger 18, so that the dried products of the lignite and the sewage treatment plant can become a new energy source which is odorless, hydrophobic, sterile, nontoxic, capable of being transported in a long distance, safe and sanitary.

In the chinese patent ZL201220003775.0, an independent external heating type drying section and an independent external heating type dry distillation section are included, so that the object of the present invention cannot be achieved, and there is no comparability with the technical scheme of the present invention.

Chinese patent ZL201310386172.2 is a method and device for low-temperature dry distillation and pyrolysis of low-rank coal and oil shale, wherein coal gas is preheated to 700-800 ℃ by a coal gas preheating device, and then enters an internal heating type vertical furnace suitable for hot coal gas carbonization through a pipeline to be carbonized into long flame coal, non-sticky coal and weakly sticky coal, and the coal gas preheating device is composed of a heat supply system and a preheating system. The invention has the advantages that: the cold coal gas is preheated by the coal gas preheating device and used as heat-carrying gas (flue gas is indirectly heated instead of air and coal gas combustion flue gas, nitrogen carried in the flue gas is avoided), and through the improvement of the vertical furnace heating mode and the furnace body structure, the content of hydrogen and methane in the coal gas composition is improved, the content of nitrogen is reduced, and the heat value of the coal gas is improved while high-quality ferroalloy coke and calcium carbide coke are produced. The high-quality raw material is provided for the comprehensive utilization of hydrogen production, methanol preparation, LNG liquefied natural gas and the like of the coal gas; the coal tar and coal gas which are byproducts can be further processed deeply, thereby improving the use value. However, the coal gas preheating device consists of a heat supply system and a preheating system: the combustion system is a regenerative combustion furnace using low-heat value gas as fuel, and generates high-temperature flue gas at 1000-1300 ℃; the regenerative combustion furnace is provided with double regenerative burners, and radiant tube preheaters are uniformly distributed in the regenerative combustion furnace; the preheating system is a radiant tube preheater arranged in the regenerative combustion furnace, the radiant tube preheater mainly comprises radiant tubes, and cold coal gas and high-temperature flue gas exchange heat through the radiant tube preheater. The internal heating vertical furnace consists of porous carbonization chambers, wherein both sides of each hole of the carbonization chamber are provided with a hot gas furnace inlet channel and an auxiliary combustion chamber, the upper part of each hole of the carbonization chamber is wide and the lower part of the carbonization chamber is narrow, the middle cross section is a variable cross section, the upper part of the carbonization chamber is provided with a distributing plate, the top of the carbonization chamber is provided with an ascending pipe, and the bottom of the carbonization chamber is filled with cooling gas; the carbonization chamber is internally provided with gas distribution bricks, the vertical furnace is built by refractory bricks, the side surface of the furnace body is provided with auxiliary burners, and furnace protection iron pieces are arranged around the furnace body.

The Chinese patent ZL201320534076.3 is an internal heating type vertical furnace using heated high-temperature coal gas as a heat source, and is matched with the Chinese patent ZL 201310386172.2.

In chinese patent ZL201310386172.2 and chinese patent ZL201320534076.3, in order to realize that the heat carrier gas does not contain nitrogen, a regenerative combustion furnace system using low-heat value gas as fuel is adopted, and the low-heat value gas must be provided by another low-heat value gas generating device, so that the system needs a retort furnace system, a regenerative furnace system and a low-heat value gas generating furnace system, the whole process is too complex, the investment increment is huge, and the thermal efficiency or the thermal efficiency is very low (at least the heat loss is greatly increased); in addition, both sides of each hole carbonization chamber are provided with a hot gas furnace inlet channel (without using combustion-supporting gas) and an auxiliary combustion chamber (for supplementing insufficient heat energy of hot gas in the carbonization process and facilitating adjustment operation), the auxiliary combustion chamber is positioned above the hot gas furnace inlet channel, coal material descends in the carbonization furnace, enters a lower cavity after the coal material passes through the corresponding material level of the auxiliary combustion chamber and is heated, the coal material continues to descend, the carbonization is completed through the corresponding material level of the hot gas furnace inlet channel, and then enters a blue carbon cooling section, so that cooling gas is introduced into the furnace bottom to exchange heat with blue carbon, the cooling gas ascends after being mixed with high-temperature hot gas introduced into the bottom of the carbonization section and is heated, the coal material ascends and is in countercurrent contact with the lower section of the carbonization section and then is mixed with hot flue gas discharged from the auxiliary combustion chamber in the middle of the carbonization section, the carbon material ascends and is in countercurrent contact with the upper section of the carbonization section after the reheating, which is not the operation mode of the invention, therefore, the aim of the invention cannot be achieved, and the technical scheme of the invention has no comparability.

The coal medium-low temperature carbonization furnace and the carbonization device based on the same are disclosed in the Chinese patent ZL201320199037.2, wherein the carbonization furnace sequentially comprises a first cavity, a second cavity and a cooling cavity from top to bottom, and the first cavity, the second cavity and the cooling cavity are sequentially communicated through a feeding channel; the first cavity and the second cavity are identical in structure, a plurality of heat exchange tube bundles are arranged inside the first cavity and the second cavity, a plurality of material guides are arranged between adjacent heat exchange tube bundles, and the placing direction of the heat exchange tube bundles is perpendicular to the moving direction of raw coal in the cavity; a plurality of heat storage pipes are arranged on the side walls of the first cavity and the second cavity; the first cavity is divided into a drying section and a first dry distillation section according to different temperatures.

In the Chinese patent ZL201320199037.2, an independent external heating type drying section and an independent external heating type dry distillation section are included; the facility for controlling the operation temperature of the carbonization section is an external heating type heater, and the temperature field of the carbonization area of the semi-coke furnace is a means for gradually increasing the temperature along the descending path of the coal material without adjusting the temperature in the middle of the carbonization area, so the aim of the invention cannot be achieved, and the invention has no comparability with the technical scheme of the invention.

Chinese patent ZL201420317700.9 is a small-particle shale retort, which comprises a retort body, an inner cavity of which is sequentially divided into a preheating section, a heating dry distillation section, an intensified dry distillation section and a cooling section from top to bottom; the middle parts of the preheating section, the temperature-raising dry distillation section and the strengthening dry distillation section are provided with a gas collection chamber and an internal guide gas chamber; an outer guide gas chamber is arranged on the outer side of the middle upper part of the temperature-rising dry distillation section; an external guide air chamber is arranged outside the intensified destructive distillation section; the outer guide air chamber of the intensified dry distillation section is communicated with the inner guide air chamber of the intensified dry distillation section through the louver boards, the intensified dry distillation section and the louver boards, the inner guide air chamber of the intensified dry distillation section is communicated with the outer guide air chamber of the temperature rise dry distillation section through the louver boards, the temperature rise dry distillation section and the louver boards, and the upper part of the outer guide air chamber of the temperature rise dry distillation section is communicated with the inner air collection chamber of the temperature rise dry distillation section through the louver boards, the temperature rise dry distillation section and the louver boards. Because the temperature-rising dry distillation section and the strengthening dry distillation section are provided with the internal and external guide gas chambers, dry distillation gas flows through and returns back along a snake-shaped path to dry distill the small-particle shale, and the dry distillation efficiency is high. The oil yield is more than 96% through pilot test inspection.

In the chinese patent ZL201420317700.9, the destructive distillation gas heat carrier passes through the intensified destructive distillation section and the temperature-rising destructive distillation section in series (the gas main body passes through the shale material layer in cross flow, the gas main body flow direction is upward), a fluidized bed of shale particles is formed in the destructive distillation cavity, the destructive distillation zone comprises the temperature-rising destructive distillation section and the intensified destructive distillation section, the facility for controlling the operation temperature of the destructive distillation section is an external gas heat carrier, and the temperature field of the destructive distillation zone does not have a means for adjusting the temperature in the middle of the destructive distillation zone along the descending path of the shale particles, so the object of the present invention cannot be achieved, and the present invention has no comparability with the technical.

The novel coal carbonization furnace disclosed in the Chinese patent ZL201420632063.4 is sequentially provided with a drying section, a carbonization section and a cooling section; firstly, dehydrating and drying raw coal in the drying chamber; then, in the dry distillation section, firstly, performing low-temperature dry distillation on the dried raw material coal by adopting high-temperature flue gas at a lower temperature of 600-650 ℃, then performing high-temperature dry distillation at a higher temperature of 900-950 ℃, and separating the finally obtained dry distillation product to obtain semicoke, coal tar and coal gas; finally, cooling the semicoke in the cooling chamber by using cold flue gas; coal gas retort through from top to bottom setting up low temperature dry distillation section earlier and setting up the high temperature dry distillation section again, does benefit to in the low temperature dry distillation section and produces a large amount of tar, and the material continues to do benefit to after the high temperature dry distillation and produces a large amount of coal gas down, through the mode that sets up low temperature dry distillation and high temperature dry distillation and combine together in the dry distillation section, can realize obtaining high-quality tar and coal gas simultaneously to through the control to the temperature, can effectively improve the value of utilization of coal gas.

In the Chinese patent ZL201420632063.4, a dry distillation section is divided into an upper dry distillation section and a lower dry distillation section; high-temperature flue gas obtained by burning coal gas and air from the combustion chamber passes through a first heating gas distribution device which is arranged in the middle of the dry distillation section and is provided with a through hole, enters an upper dry distillation area (low-temperature dry distillation section) and moves upwards to be in countercurrent contact with coal; the first heating gas distribution device is positioned at the middle and upper parts of the dry distillation section, and the coal particles moving downwards flow through the surfaces of the upper parts and the side surfaces of the upper parts of the first heating gas distribution device;

the second heating gas distribution device is arranged at the lower part of the dry distillation section and is positioned below the first heating gas distribution device; the coke bed layer between the first heating gas distribution device and the second heating gas distribution device belongs to the lower dry distillation section (high temperature dry distillation section)

High-temperature flue gas obtained by burning coal gas and air from the combustion chamber passes through a first heating gas distribution device which is arranged in the middle of the dry distillation section and is provided with a through hole, enters an upper dry distillation area and moves upwards to be in countercurrent contact with the coal material;

the destructive distillation gas heat carrier passes through a reinforced destructive distillation section and a heating destructive distillation section in series (the gas main body passes through a shale material layer in a cross flow mode, the flow direction of the gas main body is upward), a fluidized bed of shale particles is formed in a destructive distillation cavity, a destructive distillation area comprises the heating destructive distillation section and the reinforced destructive distillation section, the facility for controlling the operation temperature of the destructive distillation section is an external gas heat carrier, and the temperature field of the destructive distillation area does not have a means for adjusting the temperature in the middle of the destructive distillation area along the descending path of the shale particles, so that the aim of the invention cannot be achieved, and the technical scheme of the invention has no comparability.

The invention has the following disadvantages:

the technical scheme of claim 1 needs to be set as a combustion chamber for providing high-temperature flue gas by a first heating gas distribution device, and combustion-supporting air of the combustion-supporting chamber is limited to air (not oxygen-enriched or pure oxygen), so that the system is complex in investment and the reduction of nitrogen content of the dry distillation coal gas cannot be realized;

secondly, in the first embodiment, in order to realize the high-temperature carbonization of the high-temperature carbonization section, the heat carrier generated by the second heating and gas distribution device is necessary to belong to high-temperature gas, and because the carbonization load (consumed heat) of the high-temperature carbonization section is small, the upward hot gas leaving the high-temperature carbonization section belongs to high-temperature gas, if the temperature is not reduced, the operation mode of the low-temperature carbonization section is changed into an undesirable high-temperature carbonization mode or medium-temperature carbonization mode, therefore, the first embodiment provides the scheme that the first gas collecting device is arranged, the gas collecting main pipe is divided into two layers, the first layer is positioned at the upper part of the low-temperature carbonization section and is used for collecting gas leaving the low-temperature high-sulfur section, the second layer is positioned below the low-temperature carbonization section and at the middle-upper part of the high-temperature carbonization section and is used for collecting gas leaving the high-temperature carbonization section, and the temperature impact of the top hot gas of the high-temperature carbonization section on the low-temperature carbonization section is relieved to a certain extent, however, at least a part of high-temperature dry distillation coal gas in a high-temperature state is directly led out of the dry distillation furnace, and the coal gas 11 contains easily deposited and coked components such as easily deposited coal pitch, coal dust and the like, so that the heat is difficult to recycle, and meanwhile, the investment and energy consumption in the cooling process are increased, and heat energy waste is formed; meanwhile, as the heat energy of the coal gas of the partial temperature dry distillation section cannot be recycled by the dry distillation process, the heat energy carried by the hot flue gas which is introduced from the low temperature dry distillation section and is released at a proper temperature in the combustion chamber must be more;

in the second aspect, in the first embodiment, the cold flue gas is used for indirectly exchanging heat to cool the high-temperature carbonization semi-coke, the gas heat capacity is very small, the heat conductivity coefficient is very low, a large amount of heat transfer area is needed, the investment is huge, and the method is not economical; the coal material in the drying section is dehydrated and dried by hot flue gas (the temperature is usually 250-350 ℃) generated by a cooling section of the retort furnace, the temperature at the bottom of the drying section is usually 200-250, the discharged flue gas inevitably carries part of hydrocarbons, the flue gas is directly discharged to pollute the environment, and if secondary treatment (such as combustion treatment) is carried out, the investment of a secondary treatment process (such as incineration) system for drying the discharged flue gas is high, and the energy consumption is high;

in fact, due to the combustion process, excessive air or excessive fuel gas, hot flue gas enters the drying section, and dry coal is inevitably adsorbed to carry oxygen into the low-temperature drying section or dry flue gas carries combustible components;

in the third aspect, because of the reason of the second aspect, hot flue gas is used for drying, and hot coal gas from a low-temperature carbonization section is not used, huge heat energy contained in the hot coal gas of the low-temperature carbonization section is directly carried into the coal gas 11 leaving the carbonization furnace, and the coal gas 11 contains easily deposited and coked components such as easily-coal asphalt, coal powder and the like, so that the heat is difficult to recycle, and meanwhile, the investment and energy consumption in the cooling process are increased, and heat energy waste is formed;

the heat energy carried by the coal gas 11 leaving the retort and incapable of being directly recycled is finally from the fuel and air consumed by the combustion chamber and the second heating gas distribution device, the consumption of the fuel and the air is greatly increased, the actual output product yield of the effective gas in the retort coal gas is greatly reduced, and the theoretical fuel consumption is increased by about 0.9-1.2 times;

in addition, compared with the conventional scheme that gas of an internal heating type gas retort rises in series to pass through a drying section, high-temperature hot gas entering a pipeline of the first gas collecting device is high-temperature hot gas carrying a large amount of asphaltene steam and coal dust dirty gas, and the gas collecting device is easy to block, so that the gas collecting device cannot operate for a long time; in the conventional scheme that gas of the internally heated dry distillation furnace rises in series and passes through the drying section, dirty gas leaving the dry distillation section is purified in the process that the gas rises and passes through the drying section:

firstly, the temperature is reduced, so that coal tar pitch is condensed and deposited on the coal material;

secondly, the porous coal material has certain adsorption capacity to the coal pitch, and plays a role of an adsorption filter bed;

thirdly, the coal powder in the coal gas is filtered and intercepted by a fresh coal material (with low crushing degree) layer at the top of the retort furnace, so as to realize the primary dust removal of the coal gas.

In the first embodiment, the second heating gas distribution device is arranged at the bottom of the dry distillation section 2, in this embodiment, the second heating gas distribution device is a gas distribution wall 9, and the gas and air in the gas distribution wall 9 are combusted to generate high-temperature flue gas with the temperature of 900 plus 950 ℃ which directly exchanges heat with the coal and pyrolyzes the coal;

in the second embodiment, the second heating gas distribution device is arranged at the bottom of the dry distillation section 2 and is a combustion gas distribution device, through holes are formed in the combustion gas distribution device, and mixed gas of air and coal gas is conveyed into the dry distillation section, namely, the combustion gas distribution device adopts an internal combustion and internal heating type heating mode, and after being input into the dry distillation section, the mixed gas of air and coal gas is combusted together with coal raw materials to generate high-temperature flue gas at 900-950 ℃ to directly exchange heat with coal and pyrolyze the coal;

the technical solution of the second embodiment also has the technical disadvantages of the technical solution of the first embodiment.

The whole patent document does not mention the measure of recovering the heat energy of the high-temperature blue-carbon by using cold circulating gas.

Chinese patent ZL201420858413.9 is a flue gas mixing type dry distillation furnace, which is characterized in that a drying bin is arranged at the top of a dry distillation furnace body, a storage bin is fixedly connected on the drying bin, a flue gas inlet and a flue gas outlet are arranged on the drying bin, an array umbrella with a central air guide pipe and arranged at the upper part in the dry distillation furnace body is communicated with an oil gas outlet of the dry distillation furnace, a low-temperature dry distillation section A is arranged at the lower end of the central air guide pipe of the array umbrella, a thermal circulation gas inlet is arranged below the low-temperature dry distillation section A, the thermal circulation gas inlet is communicated with a mixing chamber of the low-temperature dry distillation section, a middle-temperature dry distillation section B communicated with the mixing chamber of the low-temperature dry distillation section is arranged below the mixing chamber of the low-temperature dry distillation section, an arch lift is arranged on an upper arch of the middle-temperature dry distillation section B, a middle-temperature dry distillation section central air distributor is arranged on a lower arch of the middle-temperature dry distillation section B, the middle-temperature dry distillation section mixing chamber arranged below the middle-temperature dry distillation section is communicated with the hot flue gas inlet arranged on the dry distillation furnace body, the bottom of the dry distillation furnace body is provided with a basin, and an ash discharger is arranged in the basin.

In the chinese patent ZL201420858413.9, the gasification reaction in the gasification stage 9 is completed by adjusting the amount of main air, the saturation of main air and the amount of treatment, and accounts for about 70-80% of the total heat required for dry distillation. The other 20-30% of heat comes from the circulating gas of the regenerator heating furnace, and when the heating furnace adopts a double-combustion double-delivery heating mode, the medium temperature of the circulating gas is generally required to be 680-700 ℃. The temperature difference is generally between 50 and 70 ℃.

The Chinese patent ZL201420858413.9 has the defects similar to or the same as the technical defects of a part of the novel coal carbonization furnace in the Chinese patent ZL 201420632063.4:

firstly, flue gas with the temperature of 200-250 ℃ after heat exchange is introduced as drying gas, so that a large amount of steam and dust are taken away, the sensible heat of the coal gas at the low-temperature carbonization section cannot be directly utilized, and the energy consumption in the process of generating the drying flue gas is increased; meanwhile, the temperature at the bottom of the drying section is usually 200-250, the discharged smoke inevitably carries partial hydrocarbons, the smoke is directly discharged to pollute the environment, and if secondary treatment (such as combustion treatment) is carried out, the secondary treatment process (such as incineration) of the dried discharged smoke has high system investment and energy consumption because of containing a large amount of water vapor;

secondly, the low-temperature dry distillation coal gas with higher temperature contains more asphaltene and dust, and the heat energy cannot be directly recovered; the crude dry distillation gas is not cooled, adsorbed and filtered by a fresh shale particle layer, and the shale oil condensed by the crude dry distillation gas contains more dust and asphaltene and has poor oil quality;

the heat energy of the high-temperature gas discharged from the medium-temperature dry distillation section is not fully utilized, the flow rate of the thermal cycle gas of the low-temperature dry distillation section A is increased, and a transition region with a higher operating temperature between the temperature of the medium-temperature dry distillation region and the temperature of the low-temperature dry distillation region is formed at the lowest part in the low-temperature dry distillation section;

the whole invention document does not mention the measure of recovering the heat energy of the high-temperature shale ash by using the cold circulating coal gas, only a water ash quenching mode is arranged, the use amount of the ash quenching water is increased, the heat energy is wasted, the ash quenching water is converted into steam crude dry distillation gas to be discharged out of a dry distillation furnace, the cooling load of the crude dry distillation gas cooling separation process is increased, and the investment and the energy consumption of a subsequent sewage treatment system are increased.

The internally heated gas retort of Chinese patent ZL201420862574.5, an oil shale internally heated gas retort with strong handling capacity, high oil yield and less supplementary saturated steam, comprises a furnace body, an arch center is arranged in the middle of the interior of the furnace body, an annular upper mixing chamber and an annular lower mixing chamber are arranged on the inner wall of the furnace body corresponding to the arch center, a gas generating inlet communicated with a gasification section is arranged on the lower mixing chamber, gas spray holes communicated with the dry distillation section are arranged around the upper mixing chamber, a thermal circulation gas inlet is arranged on the upper mixing chamber, and an annular arrangement hole is arranged on the arch center to communicate the dry distillation section with the lower gasification section; a group of umbrellas with downward open ends are arranged at the upper part of the dry distillation section in the furnace body; arrange grey equipment and constitute by ash ejector, wind head, basin, transmission and spade, the basin seat sets up on the stove bottom stove dish, sets up the water seal below the basin, and transmission sets up outside the furnace body and is connected with the basin, arrange grey ware setting on the basin, the spade becomes 45 with the stove bottom and installs on the furnace body, and the lower extreme of spade is located the basin upper surface and corresponds the ash ejector fin outside.

In the Chinese patent ZL201420862574.5, the heat energy of the hot gas product of the gasification section is not enough to meet the total heat energy consumption of the dry distillation process, so a supplementary heat carrier is required to provide heat energy; the supplementary heat carrier is heat circulating gas from heat accumulating chamber heating furnace, and the material, the dry distillation section, the temperature controlling mode and the system structure are different from those of the present invention.

The Chinese patent ZL201520177695.0 is a full-circulation retort furnace for the dry distillation of low-rank bituminous coal, and the retort furnace body is sequentially divided into from top to bottom: the top end of the retort furnace body is provided with an auxiliary coal bunker communicated with the preheating section, and the upper end of the auxiliary coal bunker is connected with a raw coal storage bunker through an electro-hydraulic gate valve; the cooling section is connected with a plurality of coke discharge boxes, the lower ends of the coke discharge boxes are connected with star-shaped discharge valves, heat exchange gas pipelines are inserted into the cooling section and the coke discharge boxes, cooling gas enters from the heat exchange gas pipelines at the lower parts of the coke discharge boxes and reversely contacts with the red-hot semi coke to absorb sensible heat, and the cooling gas is led out of the furnace through pipelines after heat exchange is finished; the bottom of the dry distillation section is provided with a thermal cycle gas input pipe, and the dry distillation section is also provided with a thermal cycle gas distribution arch road for uniformly dispersing semi coke after dry distillation to each coke discharging box. The utility model adopts the direct contact of raw coal and hot circulating coal gas to complete the dry distillation, has high thermal efficiency and fast heat transfer, and solves the defect of low heat value of the coal gas produced by the dry distillation of low-metamorphic bituminous coal in the current industry. .

In the Chinese patent ZL201520177695.0, the dry distillation section belongs to a single dry distillation temperature control mode, and the bottom of the dry distillation section is provided with a hot circulating coal gas input pipe, so the raw materials processed by the method, the heat supply mode and the temperature control mode of the dry distillation section and the system constitution are all different from the method.

The Chinese patent ZL201620467684.0 is a low-temperature carbonization furnace for preparing semi coke, which is characterized by comprising a raw coal inlet, wherein the lower part of the raw coal inlet is connected with the carbonization furnace; the retort furnace comprises a retort section and a cooling section which are arranged in the furnace from top to bottom; an air collecting umbrella a (11) and an air guide umbrella device (2) facilitating air circulation are arranged in the dry distillation section from top to bottom, and an air distribution umbrella device (3) introducing air and coal gas mixed gas is arranged below the air guide umbrella device (2); and a spray pipe device (4) which is filled with cooling water is arranged in the cooling furnace section from top to bottom, and a coke pusher device (8) which can uniformly discharge the semi-coke is arranged below the spray pipe device (4). The utility model discloses can improve the utilization ratio of air, coal gas, more even distribution raw coal, area utilization in the increase retort can purify the raw coke oven gas that the dry distillation produced simultaneously, and the environmental protection is pollution-free, has reduced moisture in the blue charcoal of finished product.

In the Chinese patent ZL201620467684.0, the dry distillation section belongs to a single dry distillation temperature control mode, and the bottom of the dry distillation section is provided with a gas distribution umbrella device (3) for introducing mixed gas of air and coal gas, so that the raw materials processed by the method, the heat supply mode and the temperature control mode of the dry distillation section and the system composition are all different from those of the invention. ,

chinese patent ZL201621314632.6 is a semi-gas-fired oil shale low-temperature retort, which is additionally provided with a gas-fired section on the basis of a smoothing retort, namely, two gas distribution tracery walls are additionally arranged in the middle of the generation section, spray holes are arranged on two sides of the tracery walls, and air and gas-fuel gas mixtures are arranged in the holes of the spray holes. The function of adding the gas combustion section has three points, and one of the three points makes up the deficiency of the heat of dry distillation in the furnace; secondly, the consumption of saturated air is reduced, and the phenomenon of oil burning due to excessive oxygen is avoided; the arrangement of the three and two gas distribution pattern walls enables shale semicoke to be uniformly distributed in the diameter direction of the hearth in the blanking process, the problem that original smooth fire slag is not uniform is solved, and air and gas mixture is sprayed into the furnace through the spray holes on the two sides of the gas distribution pattern walls, so that heat distribution is more uniform.

In chinese patent 201621314632.6, as described in example one, the heat required for dry distillation of oil shale consists of three parts: (1) saturated air at the temperature of 75-85 ℃ enters the generation section 8 through a saturated air inlet 10 at the bottom of the retort, flows from bottom to top, and reacts with fixed carbon in shale semicoke to generate generation gas after being preheated by shale ash; (2) the mixture of air and gas in a certain proportion is uniformly sprayed into the furnace through spray holes 7 on two sides of a gas distribution tracery wall 6, and high-temperature flue gas generated by burning the mixed gas on the surface of the shale semicoke is mixed with generated gas and then flows upwards to enter a dry distillation section; (3) the hot circulating dry distillation gas with the temperature of 680 ℃ enters the furnace from the hot circulating gas inlet 5 and is in uniform contact with the oil shale in the dry distillation section 4 to generate dry distillation. The heat carrier supplies heat required by the dry distillation of the oil shale, the temperature of the oil shale in the furnace is stabilized at about 550 ℃, finally the oil shale and the dry distillation gas are led out of the furnace from an upper umbrella array 2 of the dry distillation furnace, and the temperature of the gas at the furnace outlet is about 90-110 ℃. The support body 12 is used for supporting the gas distribution wall 6 and preventing the gas distribution wall 6 from collapsing.

In chinese patent 201621314632.6, the heat energy of the hot gas product in the gasification stage is not enough to satisfy the total heat energy consumption in the dry distillation process, so a supplementary heat carrier must be used to provide heat energy, and two ways of supplementary heat energy gas are used, namely: hot circulating dry distillation gas with the temperature of 680 ℃ enters the furnace from a hot circulating gas inlet 5 and is uniformly contacted with the oil shale in the dry distillation section 4; the mixture of air and gas in a certain proportion is uniformly sprayed into the furnace through the spray holes 7 at the two sides of the gas distribution tracery wall 6, the high-temperature flue gas generated by burning the mixed gas on the surface of the shale semicoke is mixed with the generated gas and then flows upwards to enter the dry distillation section, the temperature and the oxygen concentration of the rising gas are improved, a second dry distillation section (also a carbon deposition initial combustion section) is formed, and it needs to be explained again that the purpose of the two gas circuits is to supplement heat energy, rather than recovering the excess heat energy, in the ascending process from bottom to top of the generation section 8, the gas combustion section 11, the dry distillation section 4 and the preheating section 3 of the dry distillation furnace, after the gas temperature is reduced by the heat absorption of the shale or the shale ash, the hot flue gas is mixed and heated for heating after being combusted by the gas externally input into the second dry distillation section for the first time, and the hot circulating dry distillation gas with the temperature of 680 ℃ externally input into the first dry distillation section for the second time is mixed and heated for heating.

In the chinese patent 201621314632.6, the temperature field of the controlled retort area is an operation mode in which the temperature gradually increases along the descending path of the shale or the shale ash, and the temperature of the heating gas does not suddenly and greatly cool down in the ascending process of the heating gas, so that the object of the present invention cannot be achieved, and there is no comparability with the technical scheme of the present invention.

Chinese patent ZL202020972110.5 a low temperature gas retort, a serial communication port, it is from last to including the feeding section down in proper order, the dry distillation section, cooling zone and row material section, the dry distillation section includes the furnace body, the inside longitudinal section of furnace body is the shape that from the top down narrows down gradually, the furnace body both sides evenly are provided with first heating element mounting hole along the direction of height, heating member has been placed in the first heating element mounting hole, the inside of furnace body is provided with the gas collection spare, the gas collection spare includes main gas collection umbrella, a plurality ofly and the perpendicular supplementary gas collection umbrella of being connected of main gas collection umbrella, the top in the middle of main gas collection umbrella links to each other with the coal gas collecting pipe, the below of gas collection spare is provided with middle heating member, be provided with second heating element mounting hole on the middle heating member, the downthehole heating member of having placed of second heating element mounting. The utility model discloses utilize furnace body and middle heating member as the heat-carrying medium, carry out the direct heating to the material through the mode of radiation heat transfer, can make burning and temperature distribution more even, the regulation and control of being more convenient for.

In chinese patent ZL 202020972110.5: the heat supply of the dry distillation section belongs to an external heating type, the fuel gas is used for heating the furnace body and the intermediate heating member by burning in the heating member, the furnace body and the intermediate heating member are used as a heat carrier, the material is directly heated by a radiation heat exchange mode, and the combustion and the temperature distribution are more uniform and the regulation and the control are more convenient because a plurality of heating elements are arranged in the furnace body along the height direction. Therefore, the method is completely different from the method that the internal heating type heating mode is adopted in the dry distillation section of the dry distillation furnace, the gas heating process in the dry distillation section of the dry distillation furnace does not have an operation mode that the temperature is suddenly and greatly cooled, the' process of descending along coal materials cannot be formed, the semi coke at the bottom of the upper dry distillation area enters the upper part of the lower dry distillation area, the semi coke is rapidly heated by the high-temperature gas at the upper part of the lower dry distillation area and enters an intermediate-temperature dry distillation state, and a facility for adding quick cooling gas is not arranged at the middle upper part of a bed layer of the dry distillation section, so that the aim of the invention cannot be achieved, and the method is not comparable to the technical scheme of the invention.

The low-temperature oil shale gas retort of the Chinese patent ZL201320237967.2 comprises a furnace top bin, a furnace body and a bottom ash discharge device, and is characterized in that: the furnace body top is fixed with the furnace roof feed bin, and there is the stove export furnace body top side, and the furnace body inner chamber comprises the dry distillation section on upper portion and the emergence section of lower part, and it has the cold circulation gas entry and the hot circulation gas entry that extend to the furnace body outside to open respectively on the lateral wall of the furnace body middle part position between dry distillation section and the emergence section, and the cold circulation gas entry is located hot circulation gas entry below, and the emergence section below of furnace body is blast head and bottom ash discharging equipment. The device can properly reduce the temperature of the gasified gas, prevent the lower part of the dry distillation section from being overhigh in temperature and generating coking phenomenon, and simultaneously can consume the residual oxygen in the gasified gas, thereby avoiding the phenomenon that the oxygen enters the dry distillation section to generate oil burning phenomenon and influence the oil yield.

In the Chinese patent ZL201320237967.2, a cold circulating gas inlet in the middle of a furnace body is positioned below a hot circulating gas inlet; the cold circulating gas that lets in the dry distillation section bottom mixes the direct cooling with the gasification gas that the section produced and forms the gas heat carrier that the temperature is suitable, prevents that dry distillation section lower part temperature is too high, produces the coking phenomenon, can also react the surplus oxygen in consuming the gasification gas fast simultaneously, avoids oxygen to get into the dry distillation section, produces the phenomenon of burning oil, influences oil yield. Because the heat energy provided by the gasification section is not enough to meet the requirement of dry distillation heat absorption, the hot circulating gas is used for supplementing the dry distillation heat energy.

Therefore, the chinese patent ZL201320237967.2 is different from the arrangement and operation schemes of the low-temperature carbonization temperature-adjusting gas distribution chamber above the combustion gas inlet of the temperature-raising carbonization mixing chamber in the carbonization section of the present invention, and the heating method is completely different, and the gas-raising process in the carbonization section of the carbonization furnace has no operation mode of suddenly and greatly cooling the temperature of the gas-raising, and the middle and upper part of the bed layer of the carbonization section has no facility for adding the quick-cooling gas, so the present invention can not be realized, and the present invention has no comparability with the technical scheme of the present invention.

Chinese patent ZL201320237968.7 is a novel interior hot oil shale retort, and it includes vertical square furnace body (4) that is piled up by red brick, characterized by: the retort furnace chamber (2) in the furnace body (4) is sequentially provided with a retort furnace inlet, a retort section, a generation section and a retort furnace outlet from top to bottom, wherein the retort section and the generation section are divided into six channels through five groups of channel grids (3), the side wall of the furnace body (4) in the middle of each channel is provided with a thermal circulation air hole (7) extending out of the furnace body (4), the part above the thermal circulation air hole (7) of each channel is a retort section channel (6), and the part below the thermal circulation air hole is a generation section channel (12). The gas retort has the advantages of uniform material distribution, gas exhaust and slag discharge, full dry distillation and greatly improved daily processing capacity.

In Chinese patent ZL201320237968.7, a hot circulating gas inlet is arranged in the middle of a furnace body, the part above a hot circulating gas hole (7) is a carbonization section channel (6), and the part below the hot circulating gas hole is a generation section channel (12); the dry distillation section is not provided with other temperature adjusting facilities; in the generation section, the downward shale slag is in countercurrent contact with the upward generation gas containing water vapor, carbon dioxide gas and oxygen to gasify the coke and combust the coke. Because the heat energy provided by the gasification section is not enough to meet the requirement of dry distillation heat absorption, the hot circulating gas is used for supplementing the dry distillation heat energy.

Therefore, the chinese patent ZL201320237968.7 is different from the arrangement and operation schemes of the low-temperature carbonization temperature-adjusting gas distribution chamber above the combustion gas inlet of the temperature-raising carbonization mixing chamber in the carbonization section of the present invention, and the heating method is completely different, and the gas-raising process in the carbonization section of the carbonization furnace has no operation mode of suddenly and greatly cooling the temperature of the gas-raising, and the middle and upper part of the bed layer of the carbonization section has no facility for adding the quick-cooling gas, so the present invention can not be realized, and the present invention has no comparability with the technical scheme of the present invention.

Chinese patent ZL201510140748.6 is a full-circulation low-temperature dry distillation device and process for producing semi coke, wherein, a dry distillation system composed of a raw coal storage bin, a full-circulation dry distillation furnace and a coke discharging device pyrolyzes raw coal into semi coke and coal gas containing tar; a coal gas purification system consisting of a gas collecting tank, an intercooler, an electric tar precipitator, a desulfurizing tower and a blower is used for washing, purifying and cooling coal gas containing coal tar; the tar-ammonia water separation system separates the condensate generated in the gas purification system into tar residues, coal tar and ammonia water; the coal gas heating system uses the tar residue generated by the tar-ammonia water separation system and the coal gas after heat exchange as fuels to heat the circulating hot coal gas to the carbonization temperature required by the raw material coal.

In the Chinese patent ZLL201510140748.6, the circulating hot coal gas discharged by an independent circulating coal gas heating system enters the middle part of a retort furnace body, raw material coal is heated to the required carbonization temperature in a carbonization chamber, a carbonization section is not provided with a second temperature adjusting facility, and the arrangement scheme and the operation scheme of a low-temperature carbonization temperature adjusting gas distribution chamber adopted by the carbonization section are different from those of a combustion gas inlet of a temperature raising carbonization mixing chamber, so that the aim of the invention cannot be realized.

The Chinese patent application 201110058345.9 discloses a coal carbonization process using CO2 as a combustion process temperature control component, wherein the purpose of changing a raw coke oven gas component system into a nitrogen-poor system can be realized by partially or completely replacing nitrogen of the combustion process temperature control component of the conventional coal carbonization process with CO 2. The method is particularly suitable for the semi-coke manufacturing process, can produce semi-coke, tar, hydrogen, natural gas, CO2 gas, sulfur and methanol preparation feed gas by taking coal, water and oxygen as raw materials on the premise of basically not changing the structure and the operating conditions of the existing carbonization equipment, can greatly improve the resource recovery rate and purity, greatly improve the flexibility of regulating the product quality, obviously enhance the stability of controlling the product quality and obviously reduce the energy consumption.

In the chinese patent application 201110058345.9, a method of partially or completely replacing the temperature control component nitrogen in the combustion process of the conventional coal carbonization process with CO2 is proposed to achieve the purpose of changing the crude gas component system into a nitrogen-poor system, but the carbonization furnace belongs to a single carbonization zone operation mode, and the temperature field in the carbonization zone of the semi-coke furnace is gradually increased along the descending path of the coal, so that no means for adjusting the temperature in the middle of the carbonization zone exists, and the purpose of the invention cannot be achieved, and the invention has no comparability with the technical scheme of the invention.

The method of the invention is not reported.

The invention aims to provide an ascending air temperature abrupt-falling type double-pyrolysis-section internal heating type moving bed coal vertical pyrolysis furnace and a use method thereof.

Disclosure of Invention

The invention relates to an ascending temperature sudden-falling type double-pyrolysis-section internal heating type moving bed coal vertical pyrolysis furnace, which is characterized in that:

an ascending temperature sudden-descending type double-pyrolysis-section internal heating type moving bed coal vertical pyrolysis furnace, wherein coal materials entering the pyrolysis furnace gradually become preheated coal materials, low-temperature pyrolysis semicoke and stripping semicoke through at least a preheating section, a low-temperature pyrolysis section and a stripping section in a descending process;

in a pyrolysis chamber of the pyrolysis furnace, a stripping section is positioned below a low-temperature pyrolysis section, and the space of the stripping section is communicated with the space of the low-temperature pyrolysis section;

in the low-temperature pyrolysis section, a heat source of the low-temperature pyrolysis section is provided by a low-temperature pyrolysis section initial gas heat carrier rising in the low-temperature pyrolysis section; the bottom of the low-temperature pyrolysis section is provided with a temperature-regulating cooling gas distribution element which discharges temperature-regulating cooling gas entering a furnace chamber; the temperature-adjusting cooling gas entering the furnace chamber is mixed with the stripping section output gas from the upward stripping section to form a low-temperature pyrolysis section initial gas heat carrier, and the temperature of the low-temperature pyrolysis section initial gas heat carrier is at least 100 ℃ lower than that of the stripping section output gas;

in the low-temperature pyrolysis section, a temperature-regulating cooling gas distribution element is positioned in the lower coke layer, or on the side edge of the lower coke layer or on the periphery of the lower coke layer;

in the low-temperature pyrolysis section, the gas heat carrier in the low-temperature pyrolysis section moves upwards, and is in countercurrent contact with the downwards preheated coal material from the preheating section to cool and mix the gas produced in the low-temperature pyrolysis section to form output gas of the low-temperature pyrolysis section; the output gas of the low-temperature pyrolysis section enters a preheating section; the downward preheated coal material is gradually heated up for low-temperature pyrolysis, and volatile components are reduced to become low-temperature semicoke; the low-temperature semicoke is discharged downwards from the low-temperature pyrolysis section and enters a stripping section;

in the stripping section, most to all of the heat source of the stripping section is provided by the gas heat carrier rising in the stripping section; a stripping heat supply gas distribution element is arranged at the bottom of the stripping section; the stripping heat supply gas is discharged by the stripping heat supply gas distribution element and flows upwards, and is in countercurrent contact with descending low-temperature pyrolysis semicoke from the low-temperature pyrolysis section to reduce the temperature and mix the stripping clean produced gas to form stripping section output gas; the output gas of the stripping section enters a low-temperature pyrolysis section; gradually heating and deeply pyrolyzing the descending low-temperature pyrolysis semicoke, and reducing volatile components to obtain stripping semicoke; the stripping semicoke is discharged from the stripping section;

in the stripping section, stripping heat gas distribution elements are positioned in the lower coke layer and/or on the side edge of the lower coke layer or on the periphery of the lower coke layer;

the low-rank coal internally heated lump coal moving bed vertical pyrolysis furnace consists of a 1-hole or 2-hole or porous carbonization chamber; temperature-regulating cooling gas distribution elements and stripping heat-supply gas distribution elements are arranged on two sides of each hole of the carbonization chamber;

the temperature-regulating cooling gas distribution element is provided with a gas outlet, and the stripping heating gas distribution element is provided with a gas outlet;

a coal distributing plate is arranged at the upper part of the pyrolysis chamber, and an ascending pipe is arranged at the top of the pyrolysis chamber; the uptake discharges the pyrolysis furnace gas.

The operating conditions of the present invention are typically:

taking the airflow temperature 300mm above the air outlet of the low-temperature pyrolysis section temperature-adjusting cooling air distribution element as the initial gas heat carrier qualitative temperature of the low-temperature pyrolysis section;

in the stripping section, the gas flow temperature at the position 300mm below the gas outlet of the temperature-regulating cooling gas distribution element of the low-temperature pyrolysis section is taken as the output gas qualitative temperature of the stripping section;

the temperature of the low-temperature pyrolysis semicoke at the 300mm position above the air outlet of the temperature-adjusting cooling air distribution element of the low-temperature pyrolysis section is taken as the qualitative temperature of the low-temperature pyrolysis section;

the temperature of the stripping semicoke at the 300mm position of the upper part of the gas outlet of the stripping section stripping heat supply gas distribution element is taken as the qualitative temperature of the stripping section;

the coal as fired of the pyrolysis furnace is low-rank coal;

in the preheating section, the temperature of the discharged preheated coal material is 180-370 ℃;

the qualitative temperature of the low-temperature pyrolysis section is 430-680 ℃; the qualitative temperature of the initial gas heat carrier of the low-temperature pyrolysis section is at least 200 ℃ lower than the qualitative temperature of the gas output by the stripping section;

the qualitative temperature of the stripping section is 700-1000 ℃, and is 100-450 ℃ higher than that of the low-temperature pyrolysis section;

each hole of the carbonization chamber is wide at the top and narrow at the bottom, the middle cross section is a variable cross section, and the temperature-adjusting cooling gas distribution element and the stripping heat-supply gas distribution element are both arranged on the narrow cavity section below the narrowing transition section of the middle cross section of the carbonization chamber.

The volatile component of the stripping semicoke is at least 2.0 weight percent lower than that of the low-temperature pyrolysis semicoke;

the volatile content of the stripping semicoke is less than 4.98 weight percent.

The operating conditions of the invention are generally:

the coal as fired of the pyrolysis furnace is low-rank coal, the anhydrous and ashless volatile components of the coal as fired are more than 28 wt%, and the total moisture of the coal as fired is less than 25%;

in the preheating section, the temperature of the discharged preheated coal material is 200-320 ℃;

the qualitative temperature of the low-temperature pyrolysis section is 500-650 ℃;

the qualitative temperature of the stripping section is 800-950 ℃, and is 250-400 ℃ higher than that of the low-temperature pyrolysis section;

the volatile component of the stripping semicoke is at least 4.0 weight percent lower than that of the low-temperature pyrolysis semicoke;

the volatile content of the stripping semicoke is less than 3.5 weight percent.

In the stripping section, the residence time of the semicoke can be selected from one of the following:

1-2 hours;

② 2-3 hours;

③ more than 3 hours.

The stripping hot gas source can be selected from one of the following:

arranging an independent combustion furnace for fuel gas and combustion-supporting gas, wherein flue gas discharged by the independent combustion furnace is used as stripping heat supply gas of a pyrolysis furnace, and the oxygen concentration of a medium in a stripping heat supply gas distribution element is lower than 1% in volume; the stripping heat supply gas enters a bottom cavity of the stripping section through gas outlets on stripping heat supply gas distribution elements arranged at the periphery of a semicoke material layer at the bottom of the stripping section and/or in the semicoke material layer of the stripping section, and goes upward to contact with semicoke to heat the semicoke;

the stripping heat supply gas distribution element comprises a stripping combustion gas mixing chamber formed by refractory bricks, a stripping combustion gas mixer inserted into the stripping combustion gas mixing chamber and a gas distribution brick, wherein the fuel gas and the combustion-supporting gas are respectively introduced into the stripping combustion gas mixer to be mixed, then enter the stripping combustion gas mixing chamber, enter a bottom cavity of the stripping section through a nozzle of the gas distribution brick and go upward to be in contact with the semicoke, and generate combustion exothermic reaction of oxygen and the fuel gas to heat the semicoke;

and the stripping heat supply gas distribution element comprises a stripping combustion gas combustion chamber formed by refractory bricks, a stripping combustion gas burner inserted into the stripping combustion gas combustion chamber, and a gas distribution brick, wherein after the gas and the combustion-supporting gas are respectively introduced into the stripping combustion gas burner to be mixed, the gas and the combustion-supporting gas are sprayed out to enter the stripping combustion gas combustion chamber for combustion, and the combustion flue gas enters a bottom cavity of the stripping section through a nozzle of the gas distribution brick and ascends to contact with the semicoke to heat the semicoke.

According to the invention, the hot stripping semicoke discharged from the stripping section can directly enter a semicoke gasification process or a semicoke combustion process.

According to the vertical pyrolysis furnace, an indirect cooling section for stripping semicoke can be arranged below the stripping section of the carbonization chamber, and an indirect cooler for stripping semicoke is used;

the heat exchange channel of the indirect cooler for stripping the semicoke is arranged at the periphery of a semicoke material layer and/or in the material layer of the indirect cooling section;

the inner side of the indirect cooler of the stripping semicoke flows through an indirect cooling channel as an indirect cooling medium, the outer side of the indirect cooler of the stripping semicoke is an indirect cooling chamber in which a stripping semicoke material layer moves downwards, and the stripping semicoke carries out contact heat transfer and radiation heat transfer on a heat exchange element of the indirect cooler of the stripping semicoke;

in the indirect cooler of the indirect cooling section, the main body flow direction of the indirect cooling medium is horizontal flow or upward flow in an inclined mode, the indirect cooling medium is in cross flow with the downward stripping semicoke or contacts with the downward stripping semicoke in a counter-flow mode to absorb heat and then becomes a hot indirect cooling medium to leave the indirect cooler, and the cold stripping semicoke leaves the indirect cooling section of the stripping semicoke after temperature reduction.

In the indirect cooler of the indirect cooling section, the used indirect cooling medium is usually desalted water and generates steam or hot water;

in the indirect cooling section, the temperature of the hot stripping semi-coke is 700-1000 ℃, and the temperature of the cold intermediate temperature semi-coke is 80-350 ℃.

In the invention, a coke quenching section using liquid water as coke quenching fluid can be arranged below the indirect cooling section, and a coke quenching fluid input pipe and/or a dispersion pipeline are arranged;

a coke quenching water input pipe and/or a dispersion pipeline of the coke quenching section, which is positioned in the lower coke layer of the coke quenching section and/or at the periphery of the lower coke layer of the coke quenching section;

in the coke quenching section, the coke quenching water absorbs heat and evaporates to become coke quenching steam which ascends, and the coke quenching steam is contacted with descending cooling semicoke from the indirect cooling section in a countercurrent way to absorb heat to become hot coke quenching steam which ascends to enter the indirect cooling section, and the stripped semicoke leaves the coke quenching section after the coke quenching;

generally, in a coke quenching section, the temperature of quenching water is 20-50 ℃, and the temperature of hot quenching steam is 150-350 ℃;

generally, in a coke quenching section, the temperature of the extracted semicoke after indirect cooling is 150-350 ℃, and the temperature of the extracted semicoke after coke quenching is 50-100 ℃;

typically, carbon dioxide gas is blown or not blown at the bottom of the quench section to reduce the moisture of the water quench.

In the invention, a cold coke quenching section which uses liquid water as a cold coke quenching fluid can be arranged below a stripping section of a carbonization chamber, and an input pipe and/or a dispersion pipeline of the cold coke quenching water are arranged;

the coke cooling water inlet pipe and/or the dispersion pipeline are positioned in the coke layer at the lower part of the coke cooling section and/or on the side edge of the coke layer at the lower part of the coke cooling section and/or on the periphery of the coke layer at the lower part of the coke cooling section;

in the cold coke quenching section, the cold coke quenching water absorbs heat and evaporates to become cold coke quenching vapor which ascends and contacts with descending thermal-state stripping semi-coke from the stripping section in a countercurrent manner to absorb heat to become thermal-state cold coke quenching vapor which ascends to enter the stripping section, and the stripping semi-coke leaves the cold coke quenching section after the cold coke is quenched;

generally, in a cold coke quenching section, the temperature of cold coke quenching water is 20-50 ℃, and the temperature of hot cold coke quenching water vapor is 450-800 ℃;

generally, in a cold coke quenching section, the temperature of hot stripping semi-coke is 700-1000 ℃, and the temperature of the stripped semi-coke after quenching is 50-100 ℃.

In the invention, a direct gas cooling section for extracting semicoke can be arranged below the stripping section of the carbonization chamber, and cold gas is used as direct cooling gas;

the lower part of the direct air cooling section is provided with an input pipe and/or a dispersing pipeline of direct cooling air;

in the direct air cooling section, a direct cooling air input pipe and/or a dispersion pipeline are positioned in the lower coke layer and/or at the periphery of the lower coke layer;

in the direct gas cooling section, the direct cooling gas goes upward, and after being in countercurrent contact with descending stripping semicoke to absorb heat, the direct cooling gas becomes outward-conveyed ascending gas of the direct gas cooling section and goes upward to enter the stripping section, and after being cooled, the stripping semicoke leaves the stripping semicoke direct gas cooling section;

the cooling gas is externally supplied gas or circulating purified gas from raw gas of a pyrolysis furnace;

generally, in the direct gas cooling section, the temperature of cold direct cooling gas is 20-80 ℃, and the temperature of outgoing ascending gas of the direct gas cooling section is 500-800 ℃;

generally, in the direct gas cooling section, the temperature of hot stripping semicoke is 700-1000 ℃, and the temperature of the stripping semicoke after temperature reduction is 80-350 ℃.

In the invention, a coke quenching section using liquid water as coke quenching fluid can be arranged below a direct air cooling section of a carbonization chamber, and a coke quenching fluid input pipe and/or a dispersion pipeline are arranged;

a coke quenching water input pipe and/or a dispersion pipeline of the coke quenching section are positioned in the coke layer at the lower part of the coke quenching section and/or on the periphery of the coke layer at the lower part of the coke quenching section;

in the coke quenching section, the coke quenching water absorbs heat and evaporates to become coke quenching steam which ascends, and the coke quenching steam is contacted with descending cooling semicoke from the direct gas cooling section in a counter-current manner to absorb heat and then becomes hot coke quenching steam which ascends to enter the direct gas cooling section, and the stripping semicoke leaves the coke quenching section after coke quenching;

generally, in a coke quenching section, the temperature of the stripping semicoke is 150-350 ℃ after cooling in a direct air cooling section, and the temperature of the stripping semicoke is 50-100 ℃ after quenching;

at the bottom of the quenching section, carbon dioxide gas is blown or not blown to reduce the moisture of water quenching.

According to the invention, in general, the semicoke is stripped in a hot state, or is stripped in a cooling mode, or is stripped after coke quenching, enters the coke discharging box through a feeding valve at the upper part of the coke discharging box, and is discharged out of the coke discharging box through a discharging valve at the lower part of the coke discharging box after buffering.

According to the invention, the volatile matter content of the stripping semicoke is usually 3.00-4.95% by weight, preferably less than 3.00%.

In the invention, the vertical pyrolysis furnace is generally used for feeding coal by using a coal feeding box;

the coal material enters the coal feeding box through a feeding valve at the upper part of the coal feeding box, is discharged out of the coal feeding box through a discharging valve at the lower part of the coal feeding box after being buffered, and flows downwards into a preheating section chamber of the pyrolysis furnace;

generally, a coal feeding box is replaced by carbon dioxide gas, and air and water adsorbed by coal material blocks are desorbed and discharged, so that the flow of oxygen and nitrogen carried by the pyrolysis coal materials fed into a hearth of a pyrolysis furnace by the coal feeding box is reduced;

generally, the working procedure of the coal feeding box is that the coal discharging valve at the lower part of the coal feeding box is in a closed state, and after the coal feeding box is filled with a desired amount of coal, the coal feeding valve at the upper part is closed; then opening a valve on a carbon dioxide gas input pipeline to pressurize to 0.2-1.0 MPA under the closing state of an exhaust valve on a replacement gas exhaust pipeline; then closing a valve on the carbon dioxide gas input pipeline, then opening an exhaust valve on the replacement gas exhaust pipeline to exhaust, reducing the pressure to normal pressure, and then closing the exhaust valve on the replacement gas exhaust pipeline;

the above-described routine is executed 1 time or 2 times or more according to the exhaust need.

In the stripping section, in a stripping heat supply gas distribution element, fuel gas and combustion-supporting gas are respectively introduced into a stripping combustion gas mixer to complete mixing or combustion, and the obtained hot gas enters a bottom cavity of the stripping section and ascends to contact with semicoke to heat the semicoke;

in the direct gas cooling section, the direct cooling gas entering the direct gas cooling section cavity can be an oxygen-containing direct gas cooling section obtained by mixing combustible gas and combustion-supporting gas through a mixer, internal combustion heat is formed at the upper part of the direct gas cooling section, the direct gas cooling section is used for reducing the oxygen flow in the stripping heat supply gas distribution element of the stripping section, and the direct gas cooling section has the functions of: the volume ratio of the oxygen of the stripping section combustion gas to other components is reduced, the mixing difficulty of the oxygen of the stripping section combustion gas and other components is reduced, and the volume of a high-temperature combustion area is reduced.

Generally, the flow rate of combustion-supporting oxygen contained in the direct cooling gas of the direct gas cooling section is 0.05-0.20 times of the flow rate of oxygen in the stripping gas supply and distribution element of the stripping section.

In the invention, a mixer can be arranged in the low-temperature pyrolysis section temperature-adjusting cooling gas distribution element to mix the coal gas and the combustion-supporting gas, oxygen flowing through the low-temperature pyrolysis section temperature-adjusting cooling gas distribution element is theoretically lower than the temperature of the output gas of the stripping section by at least 250 ℃ after the temperature-adjusting gas oxygen is completely burnt;

generally, the flow rate of oxygen contained in the temperature-adjusting cooling gas of the low-temperature pyrolysis section is 0.05-0.10 times of the flow rate of oxygen in the stripping section stripping heat-supply gas distribution element.

In the invention, the temperature of the pyrolysis furnace gas discharged from the ascending pipe is 80-150 ℃ generally.

In the invention, the combustion-supporting gas can be air.

In the invention, the combustion-supporting gas can be oxygen-enriched gas or pure oxygen;

the coal gas used by the temperature-adjusting gas of the low-temperature pyrolysis section is purified coal gas of crude coal gas produced by the vertical pyrolysis furnace;

the gas used by the combustion gas in the stripping section is purified gas from crude gas produced by the vertical pyrolysis furnace;

the gas produced by the pyrolysis furnace belongs to low-nitrogen gas, and is convenient for separating and recycling hydrogen and methane.

the combustion-supporting gas is oxygen-enriched gas consisting of oxygen and carbon dioxide;

the coal gas used by the combustion gas in the medium-temperature pyrolysis section is purified coal gas of crude coal gas produced by the vertical pyrolysis furnace;

when the circulating coal gas cooling section exists, the cold circulating coal gas comes from purified coal gas of crude coal gas produced by the vertical pyrolysis furnace;

the coal gas produced by the pyrolysis furnace belongs to low-nitrogen carbon dioxide-rich coal gas, and is convenient for separating and recycling hydrogen and methane.

In the invention, the combustion-supporting gas used by the pyrolysis furnace is oxygen-enriched gas consisting of oxygen and carbon dioxide, and is introduced into the mixing position of the pyrolysis furnace after being mixed in a special mixing tank outside the pyrolysis furnace, and is mixed with the combustible gas, so that the volume ratio of the combustion-supporting oxygen to the combustible gas is reduced, the mixing difficulty of the combustion-supporting oxygen to the combustible gas is reduced, and a high-temperature combustion area is reduced.

According to the invention, the coal material entering the preheating section of the pyrolysis furnace can be selected from one or more of the following materials in the particle size:

①3mm～100mm；

②5mm～20mm；

③20mm～60mm；

④30mm～80mm。

according to the invention, when the coal material entering the preheating section of the pyrolysis furnace is divided into 2 or more size grades, coal feeding and uniform distribution are respectively and independently carried out in the preheating section of the pyrolysis furnace.

According to the invention, the coal material entering the preheating section of the pyrolysis furnace can be dried coal material discharged in the drying process of the coal material outside the pyrolysis furnace.

The temperature-regulating cooling gas distribution element used in the invention can comprise a mixer of coal gas and combustion-supporting gas; the gas supply pipeline and the combustion-supporting gas supply pipeline are both provided with flow regulating valves;

the used stripping heat supply gas distribution element can comprise a mixer of coal gas and combustion-supporting gas; the gas supply pipeline and the combustion-supporting gas supply pipeline are both provided with flow regulating valves.

The input pipe system for directly cooling gas used in the invention can comprise a mixer of coal gas and combustion-supporting gas; the gas supply pipeline and the combustion-supporting gas supply pipeline are both provided with flow regulating valves.

In the invention, in general, thermocouples are arranged in a coal bed and a semicoke bed of a pyrolysis furnace.

In the invention, generally, the horizontal section of a pyrolysis section furnace chamber of the pyrolysis furnace is square, and the furnace body belongs to a square box furnace;

or the horizontal section of the furnace chamber of the pyrolysis section is circular, and the pyrolysis section of the furnace body belongs to a cylindrical furnace.

In the invention, generally, in the low-temperature pyrolysis section, the upper part of the temperature-adjusting gas distribution pipe arranged in the horizontal section of the material layer is in an inverted V shape, and the temperature-adjusting gas distribution pipe is provided with an opening in the downward or lateral direction.

In the invention, generally, in the direct air cooling section, the upper part of a direct cooling air distribution pipe arranged in the horizontal section of a material layer is in an inverted V shape, and the temperature adjusting air distribution pipe is provided with an opening in the downward or lateral direction.

Drawings

FIG. 1 is a schematic view of a pyrolysis furnace according to an exemplary embodiment of the present invention.

The pyrolysis furnace part shown in figure 1 is provided with a preheating section, a low-temperature pyrolysis section, a stripping section, a direct gas cooling section and a coke quenching section, wherein cavity spaces of the preheating section, the low-temperature pyrolysis section, the stripping section, the direct gas cooling section and the coke quenching section are directly and vertically communicated.

The pyrolysis furnace shown in fig. 1 is composed of a plurality of carbonization chambers 1000, each carbonization chamber 1000 has a wide upper part and a narrow lower part, and the middle cross section is a variable cross section.

The numbers of the pyrolysis furnace components in the figures are described as follows:

the device comprises an ascending pipe 5, a furnace top distributing plate 6, a low-temperature pyrolysis section 8, a channel 9, a gas conveying pipe 9M, a gas distribution brick 10, a channel 12, a combustion gas mixer 12M, a gas distribution brick 13, a channel 15, a heat absorption gas conveying pipe 15M, a gas distribution brick 16, a coke quenching water main pipe and distribution pipe 19, refractory bricks 50, a thermocouple 60 and a furnace protection iron piece 80; interface FJM of the preheating section and the low-temperature pyrolysis section.

The numbers of the materials in the pyrolysis furnace in FIG. 1 are described as follows:

LM represents the cold coal charge at the upper part of the preheating section of the pyrolysis furnace;

RM represents hot coal charge at the lower part of the preheating section of the pyrolysis furnace;

DWBJ represents low-temperature pyrolysis semicoke discharged from the lower part of the low-temperature pyrolysis section;

TLBJ represents the stripping semicoke discharged from the lower part of the stripping section;

QLBJ denotes the cooled char exiting the lower portion of the direct air-cooled section;

XHBJ denotes quenched semicoke discharged from the lower part of the quenching section.

The low-temperature pyrolysis section 8 includes a wide horizontal section, i.e., a low-temperature pyrolysis section upper section 81, a variable cross-section transition section, i.e., a low-temperature pyrolysis section middle section 82, and a narrow horizontal section, i.e., a low-temperature pyrolysis section lower section 83.

In the low-temperature pyrolysis section 8, the temperature-adjusting cooling gas distribution part comprises a channel 9, a gas conveying pipe 9M with a main body arranged in the channel, a gas distribution brick 10 and the like.

In the stripping section, the stripping hot flue gas distribution part is composed of a channel 12, a combustion gas mixer 12M with a main body arranged in the channel, a gas distribution brick 13 and the like.

In the direct air cooling section, the heat absorption and air distribution part of the direct air cooling section is composed of a channel 15, a heat absorption air conveying pipe 15M with a main body arranged in the channel, an air distribution brick 16 and the like.

The quenching section is provided with a quenching water main pipe and a distribution pipe 19.

Detailed Description

The dry distillation of coal is the process of generating coal tar, semicoke, dry distillation gas and water by the thermal decomposition of coal under the condition of air isolation. Coal carbonization is roughly classified into 3 types according to the difference in heating final temperature: low temperature carbonization (500-600 ℃), medium temperature carbonization (600-900 ℃), and warm carbonization (900-1100 ℃). According to different heat supply modes, the coal gas retort can be divided into an external heating type, an internal heating type and a simultaneous internal and external double heat supply type. The current internal heating furnaces are widely applied and are divided into gas heat carrier furnaces and solid heat carrier retorts. The gas heat carrier retort furnace mainly comprises a Lurgi three-section furnace, a pyrolysis furnace developed by Anshan thermal energy research institute Co., Ltd, Sanjiang coal chemical industry Co., Ltd, Shenmu county and the like.

The medium-low temperature coal is processed in the pyrolysis process, the processing condition is mild, the investment is less, and the production cost is low; when high-volatile low-rank coal is processed, hydrogen in the coal is enriched into tar and coal gas in the medium-low temperature pyrolysis process, the yield is high, and meanwhile, carbon-rich semicoke is obtained, so that a product with higher value is produced. The common coal pyrolysis device comprises working sections of coal preparation, pyrolysis, raw gas purification, gas return, pretreatment of phenol-containing wastewater and the like.

Although specific optimal targeted operating conditions need to be determined for different coal types and different product properties and the operating conditions are wide in range, the main changes of the low-rank coal in the whole heating process of medium-low temperature coal pyrolysis have the following regularity in a general sense, wherein the temperature stage division is fuzzy:

drying and degassing, which corresponds to the preheating stage of the invention, and is generally a preheating, drying and degassing stage from room temperature to about 300 ℃; at this stage, the appearance of the coal is not significantly changed, low-rank coals such as lignite undergo decarboxylation reaction at about 200 ℃ or more and start pyrolysis reaction at about 300 ℃, while bituminous and anthracite coals generally have no change at this stage; dehydration occurs mainly before 120 ℃ while degassing (mainly to remove carbon dioxide, methane and nitrogen trapped in the pores and adsorbed by the coal) is generally completed around 200 ℃; the solid product at this stage is preheated coal or dry coal;

an active thermal decomposition stage (about 300 to about 600 ℃) corresponds to the low-temperature pyrolysis stage of the invention, the active thermal decomposition stage mainly takes depolymerization and decomposition reactions, coal is bonded into semi-coke and generates a series of changes, the coal begins to soften at about 300 ℃ and has separated out coal gas and tar, the tar amount is the largest before and after about 450 ℃, and the gas separation amount is the largest at about 450 to about 600 ℃; the components of the coal gas are mainly gaseous hydrocarbon except pyrolysis water, carbon monoxide and carbon dioxide, so the heat value is higher; the solid product of this stage is low temperature pyrolysis semicoke; one main purpose of the invention is to controllably realize an optimized low-temperature pyrolysis operation stage, and prevent high-temperature gas in a stripping section from entering a low-temperature pyrolysis section to burn off tar;

③ the thermal polycondensation stage (about 700 to about 1000 ℃) which is the stage of changing the low-temperature pyrolysis semicoke into stripping semicoke or even coke, and corresponds to the stripping stage of the invention, and takes the thermal polycondensation reaction as the main part. The amount of the separated tar is very small, the volatile component is mainly coal gas, and the coal gas component after 700 ℃ is mainly hydrogen. At this stage, the aromatic nucleus is obviously enlarged, the arrangement is regular, the structure is compact, and the colloid is subjected to condensation polymerization and solidification reaction to form semicoke. From low-temperature pyrolysis of semicoke to stripping semicoke, on one hand, the semicoke is separated out a large amount of coal gas and the content of volatile components is reduced, on the other hand, the volume of the semicoke per se is shrunk, the true density is increased and the strength is increased.

The invention belongs to the field of coal pyrolysis processes, generally belongs to medium and low temperature coal pyrolysis processes, and particularly belongs to the medium and low temperature coal pyrolysis processes of low-rank coal with high volatile content.

The pyrolysis furnace and the system thereof are generally suitable for processing low-rank coal such as long flame coal, non-caking coal, weakly caking coal or lignite, are particularly suitable for processing high-volatile low-rank coal, have good economical efficiency, can optimize the operation of a low-temperature pyrolysis section, improve the yield of tar, optimize the operation of a stripping section, reduce the volatile content of semicoke, improve the strength of semicoke, can also adapt to the working condition of oxygen-enriched or pure oxygen combustion-supporting gas to produce coal gas with low nitrogen concentration, and have the characteristics of simple system, flexible operation and high thermal efficiency.

The structure of the pyrolysis furnace shown in fig. 1 is described below.

The pyrolysis furnace system shown in fig. 1 shows only the structure of the characteristic parts for illustrating the present invention, the upper feed valve and the lower discharge valve of the coal charging box and the coal charging box arranged at the upper part of the preheating section, the coal charging hopper arranged at the upper part of the coal charging box, the upper feed valve and the lower discharge valve of the coke discharging box and the coke discharging box arranged at the lower part of the quenching section, and the process medium piping connected to the pyrolysis furnace, which are not shown in the figure.

The internally heated vertical furnace shown in fig. 1 is composed of a porous carbonization chamber 1000,

gas distribution bricks

10, 13 and 16 are arranged at different positions of the carbonization chamber 1000, the vertical furnace is built by refractory bricks 50, an auxiliary burner 12M, a gas pipe 9M and a gas pipe 15M are arranged on the side surface of a furnace body, a thermocouple 60 is arranged on a proper coal material layer or a proper semicoke material layer, and furnace protection iron pieces 80 are arranged on the periphery of the furnace body.

The circulating cold gas, the purified gas from the cooling, separation, dehydration, deoiling and other processing steps of the raw gas discharged from the pyrolysis furnace, is usually pressurized by a fan to maintain the circulating flow of the gas.

The coke quenching water is fresh water or deep purified water of sewage obtained in the processes of cooling, separating and dehydrating the crude gas, and the water quality of the coke quenching water meets the requirements of national standard specifications.

The operation of the pyrolysis furnace system shown in fig. 1 will be described in detail below with reference to fig. 1, and the relevant external systems will be briefly described.

The process and process objectives of the various functional sections of the pyrolysis furnace shown in fig. 1 are described in detail below.

The pyrolysis furnace shown in figure 1 adopts an operation mode that fuel gas is mixed with combustion-supporting gas and then enters a mixing chamber, and then the fuel gas is sprayed into a hearth through a gas distribution brick, namely the pyrolysis furnace is used as a flue gas generating furnace, so that the investment of the special flue gas generating furnace is saved, the heat dissipation loss of a furnace body is reduced, and the method is a basic measure for simplifying a pyrolysis system.

In the pyrolysis furnace shown in fig. 1, a preheating section is arranged at the top of a furnace chamber of the pyrolysis furnace, and is used for preheating coal materials and drying the coal materials at a moderate temperature rise speed, and simultaneously recovering heat energy of upward hot coal gas (generally at a temperature of 300-450 ℃) discharged from a low-temperature pyrolysis section so as to reduce energy consumption in a coal preheating process, reduce the temperature and volume flow of the discharged pyrolysis furnace gas, filter dust in the coal gas and adsorb asphalt fog drops in the coal gas; if the upward hot coal gas discharged from the low-temperature pyrolysis section is directly discharged out of the pyrolysis furnace along with the crude coal gas, in the processes of cooling, separating and recovering the coal gas, the coal gas contains too much tar pitch, so that the energy consumption in the cooling process is increased, the thermal condensation of the tar is also aggravated, and the coal gas with large volume can carry more dust and pitch, so that the channel is blocked; on the other hand, if the coal material entering the furnace directly contacts the upward hot coal gas discharged from the low-temperature pyrolysis section for dehydration and drying, a large amount of water can be quickly converted into steam to expand and burst coal particles to generate a large amount of pulverized coal; therefore, the preheating section is a necessary and important heating process with a proper temperature rise speed, and is particularly more important for coal materials with medium moisture (such as coal with 10-28 wt% of water), and of course, coal materials with too high moisture (such as coal with more than 35 wt% of water) are more suitable for being subjected to a separate drying process, and then the dried coal is introduced into the pyrolysis furnace. The operation temperature of the preheating section also needs to be strictly and flexibly controlled, so that thermocouples are arranged at the bottom and the top coal seams of the expected preheating section to monitor the temperature, and even a plurality of thermocouple measuring points are arranged at different height positions at the bottom of the expected preheating section; the flow and the temperature of the temperature-adjusting cooling gas of the low-temperature pyrolysis section can be adjusted in time according to the monitored temperature of the preheating section, even the flow and the temperature of the input gas of the stripping section are adjusted, even the flow of the input gas of the direct gas cooling section is adjusted; of course, the volume of the preheating section must be large enough or the residence time of the coal preheating process must be long enough to meet the operating time requirements of the preheating or drying process, with a certain margin to accommodate fluctuations in operating conditions, with the overall operating objectives being: fully recovering the heat of the upward hot coal gas discharged from the low-temperature pyrolysis section, heating the coal material, and reducing the water content of the coal material to be below an expected value.

The operation temperature and the volume (coal preheating residence time) of the preheating section are determined according to the moisture weight content of preheated coal discharged from the preheating section and the temperature of the preheated coal which are production targets, and are influenced by the flow, moisture and temperature of the coal entering the furnace, the temperature of a gas heat carrier, the flow of the gas heat carrier and other factors; the moisture content of the preheated coal exiting the preheating stage is desirably less than about 6.0% by weight, typically less than about 5.0% by weight, and most preferably less than about 4.0% by weight; the temperature of the preheated coal is usually 180 to 370 ℃, usually 200 to 350 ℃, and preferably 200 to 320 ℃.

In the pyrolysis furnace shown in fig. 1, a low-temperature pyrolysis section is arranged below a preheating section and is used for performing low-temperature pyrolysis on preheated coal to reduce volatile components of the preheated coal, so that the yield of tar is improved as much as possible, and meanwhile, the temperature of a low-temperature pyrolysis process needs to be strictly and flexibly controlled to prevent the fact that tar is burned out due to the fact that high-temperature gas in a stripping section enters the low-temperature pyrolysis section, so that a temperature-adjusting cooling gas distribution element arranged at the bottom of the low-temperature pyrolysis section needs to have a certain flexible adjustment range, the operating temperatures of the upper part and the lower part of a mixing area need to be strictly monitored, and the flow and the temperature of the temperature-adjusting cooling gas are timely adjusted according to the monitored temperature; of course, the volume of the low-temperature pyrolysis section must be large enough or the residence time of the preheated coal must be long enough to meet the operation time requirements of the heat transfer pyrolysis process of the low-temperature pyrolysis section, and a certain margin should be provided to accommodate fluctuations in the operation conditions, and the overall operation target is: the tar is fully extracted, and the low-temperature semicoke is ensured to be burnt thoroughly without undercooking.

The operation temperature and the volume of the low-temperature pyrolysis section (the retention time of the preheated coal) are determined according to the production target, namely the weight content of volatile matters of the low-temperature pyrolysis semicoke discharged from the low-temperature pyrolysis section, and are influenced by the flow, moisture, volatile matters and temperature of the preheated coal, and meanwhile, the temperature of a gas heat carrier, the flow of the gas heat carrier and other factors; the ideal low-temperature pyrolysis semicoke has 8.50-12.50% of volatile component weight content or 6.50-8.50% of volatile component weight content. The temperature of the low-temperature semicoke discharged from the low-temperature pyrolysis section is usually 430 to 680 ℃, usually 460 to 650 ℃, and preferably 500 to 650 ℃.

In the pyrolysis furnace shown in fig. 1, a stripping section is arranged below a low-temperature pyrolysis section, and is used for deeply pyrolyzing low-temperature semicoke to reduce volatile components thereof, and simultaneously preventing the stripping section from generating excessive tar pitch to hopefully produce more coal gas, that is, the upper bed layer of the low-temperature semicoke in the stripping section needs to be rapidly heated to enter a pyrolysis process with higher temperature, so that the gas temperature of the upper bed layer in the stripping section is still very high and is usually at least 150 ℃ higher than the gas temperature after mixing at the bottom of the low-temperature pyrolysis section, and thus the gas temperature of the upper bed layer in the stripping section needs to be strictly monitored, and the flow and the temperature of stripping hot flue gas are timely adjusted according to the monitored temperature; of course, the volume of the stripping section (the residence time of the low-temperature pyrolysis semicoke) must be large enough or the residence time of the low-temperature semicoke must be long enough to meet the operation time requirement of the heat transfer pyrolysis process of the stripping section, and a certain margin is provided so as to adapt to the fluctuation of the operation condition and ensure that the stripping semicoke is burnt thoroughly without being half-burned.

The operation temperature of the stripping section and the volume of the stripping section (the retention time of the low-temperature pyrolysis semicoke) are determined according to the weight content of volatile matters of the stripping semicoke discharged from the production target, namely the stripping section, and are influenced by the flow, the volatile matters and the temperature of the low-temperature pyrolysis semicoke and the temperature of a gas heat carrier, the flow of the gas heat carrier and other factors; the ideal weight content of volatile components of the stripping semicoke is 3.00-4.95% or less than 3.00%. The temperature of the stripping semicoke discharged from the stripping section is usually 700 to 1000 ℃, usually 750 to 950 ℃, and preferably 800 to 950 ℃.

In the pyrolysis furnace shown in fig. 1, a direct gas cooling section is arranged below a stripping section and is used for recovering heat energy of hot stripped semicoke discharged from the stripping section, so that the operation value of the highest final temperature of the stripping section can be flexibly increased as required to ensure that the content of volatile components in the stripped semicoke is lower than an expected upper limit value, and the operation mode can prevent a large amount of fuel gas from being consumed due to the increase of the highest final temperature of the stripping section, and can improve the yield of externally output effective gas in the case that the fuel gas comes from separated gas of crude gas of the pyrolysis furnace; of course, the volume of the direct gas cooling section must be large enough or the residence time of the stripping semicoke must be long enough to meet the operation time requirement of heat transfer in the cooling process of the stripping semicoke, and a certain margin is provided so as to adapt to the fluctuation of the operation condition and ensure the thorough cooling of the stripping semicoke.

The operation temperature of the direct gas cooling section and the volume of the direct gas cooling section are determined according to the production target, namely the temperature of the stripping semicoke discharged from the direct gas cooling section, and are influenced by the flow and the temperature of the stripping semicoke and the temperature of a gas heat carrier, the flow of the gas heat carrier and other factors; the temperature of the extracted semicoke discharged from the ideal direct air cooling section is usually 150-400 ℃, generally 180-350 ℃, preferably 200-300 ℃; under economic conditions, the coke discharging temperature of the direct air cooling section is reduced as much as possible so as to reduce the water consumption of the coke quenching section.

Because the ideal temperature of the semi-coke after coke quenching is 70-90 ℃, if the temperature is low, the coke quenching section is too large in volume, the height and weight of the pyrolysis furnace are increased too much, the circulating pressure difference of the coal gas is increased greatly, the bottom pressure of the pyrolysis furnace is increased greatly, the safety is reduced, the investment is greatly increased, the energy consumption is greatly increased, and the method is uneconomical. On the other hand, an inert gas interlayer is needed below the direct gas cooling section, so that atmospheric air is prevented from entering the direct gas cooling section, and gas in the direct gas cooling section is prevented from leaking into the atmospheric air.

In the pyrolysis furnace shown in fig. 1, a quenching section using water is arranged below a direct gas cooling section for complete quenching, the required amount of water is small because the heat absorption process of water quenching mainly utilizes the latent heat of evaporation of water, the capacity of the quenching section is small, the investment can be reduced, the height of the quenching section is reduced, the weight of the quenching section is reduced, and steam generated by quenching enters the direct gas cooling section as a gas heat carrier; of course, the volume of the quenching section must be large enough or the quenching time must be long enough to meet the operating requirements of the heat transfer pyrolysis of the quenching section, and a certain margin should be provided to accommodate fluctuations in operating conditions to ensure that the char is cooled to a certain limit temperature without being entrained (i.e., to cool the char core).

In particular, the invention is suitable for the working condition that the combustion-supporting gas is rich oxygen or pure oxygen.

The total retention time and the retention time of each stage of the coal material from the coal material entering the hearth of the pyrolysis furnace to the coal material leaving the hearth of the pyrolysis furnace to become the stripping semicoke are changed according to the specific coal material property, the requirement of the volatile content of the stripping semicoke and the expected yield of the low-temperature dry distillation tar, and the total retention time of the coal material passing through the hearth of the pyrolysis furnace is usually 10-20 hours, and is usually 13-17 hours.

Generally, the extracted semicoke discharged from a coke discharge box of the pyrolysis furnace is collected and conveyed to a semicoke storage bin.

According to the requirement, in the preheating section of the pyrolysis furnace, the hot flue gas drying of the coal fed into the pyrolysis furnace can be carried out, and the operation mode is as follows, but the operation mode is not preferable:

an upright coal feeding pipe of the preheating section is arranged between the preheating section and the low-temperature pyrolysis section of the pyrolysis furnace, the coal feeding pipe of the preheating section forms pressure difference on gas of the low-temperature pyrolysis section to prevent the gas of the low-temperature pyrolysis section from ascending, and the operating pressure of the preheating section of the pyrolysis furnace is slightly greater than the operating pressure of the low-temperature pyrolysis section;

a hot flue gas distributing pipe is arranged at the bottom of the preheating section of the pyrolysis furnace, hot flue gas ascends to contact with the coal material descending at the preheating section of the pyrolysis furnace for heat transfer, so that water in the coal material is evaporated and then enters ascending dry gas, and the dry gas is discharged from the upper part of the preheating section of the pyrolysis furnace; feeding the dried coal material into a low-temperature pyrolysis section of the pyrolysis furnace through a coal material feeding pipe of the preheating section;

a small amount of hot flue gas enters the top of the low-temperature pyrolysis section of the pyrolysis furnace from the preheating section of the pyrolysis furnace;

the hot flue gas entering the bottom of the preheating section of the pyrolysis furnace can be hot flue gas provided by an independent flue gas generating furnace or hot flue gas generated by an indirect cooling section of the stripping semicoke of the pyrolysis furnace.

The invention is characterized in that:

The operating conditions of the present invention are typically:

the coal as fired of the pyrolysis furnace is low-rank coal;

The operating conditions of the invention are generally:

the volatile content of the stripping semicoke is less than 3.5 weight percent.

1-2 hours;

② 2-3 hours;

③ more than 3 hours.

The stripping hot gas source can be selected from one of the following:

In the invention, the combustion-supporting gas can be air.

①3mm～100mm；

②5mm～20mm；

③20mm～60mm；

④30mm～80mm。

Claims

1. Rising temperature suddenly drop type double-pyrolysis-section internal heating moving bed coal vertical pyrolysis furnace is characterized in that:

2. The pyrolysis furnace of claim 1, wherein:

the coal as fired of the pyrolysis furnace is low-rank coal;

each hole of the carbonization chamber is wide at the top and narrow at the bottom, the middle cross section is a variable cross section, and the temperature-adjusting cooling gas distribution element and the stripping heat-supply gas distribution element are both arranged on the narrow cavity section below the narrowing transition section of the middle cross section of the carbonization chamber;

3. The pyrolysis furnace of claim 2, wherein:

the volatile content of the stripping semicoke is less than 3.5 weight percent.

4. The pyrolysis furnace of claim 1, wherein:

in the stripping section, the residence time of the semicoke is selected from one of the following:

1-2 hours;

② 2-3 hours;

③ more than 3 hours.

5. The pyrolysis furnace of claim 1, wherein:

a stripping heat supply gas source selected from one of the following:

6. A pyrolysis furnace according to claim 1 or 2 or 3 or 4 or 5, wherein:

and (4) the hot stripping semicoke discharged from the stripping section enters a semicoke gasification process or a semicoke combustion process.

7. The pyrolysis furnace of claim 1, wherein:

the vertical pyrolysis furnace is provided with an indirect cooling section for stripping semicoke below the stripping section of the carbonization chamber, and an indirect cooler for stripping semicoke is used;

8. The pyrolysis furnace of claim 7, wherein:

in the indirect cooler of the indirect cooling section, the used indirect cooling medium is desalted water, and water vapor or hot water is generated;

9. The pyrolysis furnace of claim 7, wherein:

a coke quenching section using liquid water as coke quenching fluid is arranged below the indirect cooling section, and a coke quenching fluid input pipe and/or a dispersion pipeline are arranged:

in the coke quenching section, the coke quenching water absorbs heat and evaporates to become coke quenching steam which ascends, and the coke quenching steam is contacted with descending cooling semicoke from the indirect cooling section in a countercurrent way to absorb heat to become hot coke quenching steam which ascends to enter the indirect cooling section, and the stripped semicoke leaves the coke quenching section after the coke is quenched.

10. The pyrolysis furnace of claim 9, wherein:

in a coke quenching section, the temperature of coke quenching water is 20-50 ℃, and the temperature of hot coke quenching steam is 150-350 ℃;

in a coke quenching section, indirectly cooling and then extracting the semicoke at the temperature of 150-350 ℃, wherein the extracted semicoke after quenching is at the temperature of 50-100 ℃;

11. The pyrolysis furnace of claim 1, wherein:

a cold coke quenching section which uses liquid water as a cold coke quenching fluid is arranged below a stripping section of the carbonization chamber, and an input pipe and/or a dispersion pipeline of the cold coke quenching water are arranged;

in the cold coke quenching section, the cold coke quenching water absorbs heat and evaporates to become cold coke quenching vapor which ascends, and the cold coke quenching vapor is contacted with descending hot stripping semi-coke from the stripping section in a countercurrent way to absorb heat to become hot cold coke quenching water vapor which ascends to enter the stripping section, and the stripping semi-coke leaves the cold coke quenching section after the cold coke is quenched.

12. The pyrolysis furnace of claim 11, wherein:

in a cold coke quenching section, the temperature of cold coke quenching water is 20-50 ℃, and the temperature of hot cold coke quenching water vapor is 450-800 ℃;

in a cold coke quenching section, the temperature of hot stripping semi-coke is 700-1000 ℃, and the temperature of the stripped semi-coke after quenching is 50-100 ℃.

13. The pyrolysis furnace of claim 1, wherein:

a direct gas cooling section for extracting semicoke is arranged below the stripping section of the carbonization chamber, and cold gas is used as direct cooling gas;

the cooling gas is external supply gas or circulating purified gas from raw gas of a pyrolysis furnace.

14. The pyrolysis furnace of claim 13, wherein:

in the direct air cooling section, the temperature of cold direct cooling air is 20-80 ℃, and the temperature of outgoing ascending air of the direct air cooling section is 500-800 ℃;

in the direct air cooling section, the temperature of the hot stripping semicoke is 700-1000 ℃, and the temperature of the stripping semicoke is 80-350 ℃ after temperature reduction.

15. The pyrolysis furnace of claim 13, wherein:

a coke quenching section using liquid water as coke quenching fluid is arranged below a direct air cooling section of a carbonization chamber, and a coke quenching fluid input pipe and/or a dispersion pipeline is arranged;

in the coke quenching section, the coke quenching water absorbs heat and evaporates to become coke quenching vapor which ascends, and the coke quenching vapor is contacted with descending cooling semicoke from the direct gas cooling section in a counter-current manner to absorb heat and then becomes hot coke quenching vapor which ascends to enter the direct gas cooling section, and the stripping semicoke leaves the coke quenching section after coke quenching.

16. The pyrolysis furnace of claim 15, wherein:

in a coke quenching section, after cooling in a direct air cooling section, the temperature of the stripping semicoke is 150-350 ℃, and the temperature of the stripping semicoke after quenching is 50-100 ℃;

17. The pyrolysis furnace of claim 1, wherein:

and (3) thermally stripping the semicoke or cooling and stripping the semicoke or stripping the semicoke after quenching, feeding the semicoke into a coke discharging box through a feeding valve at the upper part of the coke discharging box, buffering, and discharging the semicoke out of the coke discharging box through a discharging valve at the lower part of the coke discharging box.

18. The pyrolysis furnace of claim 1, wherein:

the volatile component weight content of the stripping semicoke is 3.00-4.95% or less than 3.00%.

19. The pyrolysis furnace of claim 1, wherein:

the vertical pyrolysis furnace uses a coal feeding box for feeding coal;

the coal material enters the coal feeding box through a feeding valve at the upper part of the coal feeding box, is discharged out of the coal feeding box through a discharging valve at the lower part of the coal feeding box after being buffered, and flows downwards into a preheating section chamber of the pyrolysis furnace.

20. The pyrolysis furnace of claim 19, wherein:

the coal feeding box is replaced by carbon dioxide gas, and air and water adsorbed by the coal material blocks are desorbed and discharged, so that the quantity of oxygen and nitrogen carried by the pyrolysis coal materials fed into the hearth of the pyrolysis furnace by the coal feeding box is reduced.

21. The pyrolysis furnace of claim 20, wherein:

the working procedure of the coal feeding box is that the coal discharging valve at the lower part of the coal feeding box is in a closed state, and the coal feeding valve at the upper part is closed after the coal feeding box is filled with the expected amount of coal; then opening a valve on a carbon dioxide gas input pipeline to pressurize to 0.2-1.0 MPA under the closing state of an exhaust valve on a replacement gas exhaust pipeline; then closing a valve on the carbon dioxide gas input pipeline, then opening an exhaust valve on the replacement gas exhaust pipeline to exhaust, reducing the pressure to normal pressure, and then closing the exhaust valve on the replacement gas exhaust pipeline;

22. The pyrolysis furnace of claim 13, wherein:

in the stripping section, gas and combustion-supporting gas are respectively introduced into a stripping combustion gas mixer to complete mixing or combustion in a stripping gas supply gas distribution element, and the obtained hot gas enters a bottom cavity of the stripping section and ascends to contact with the semicoke to heat the semicoke;

in the direct gas cooling section, the direct cooling gas entering the direct gas cooling section cavity is an oxygen-containing gas direct gas cooling section obtained by mixing the combustible gas and the combustion-supporting gas through a mixer, internal combustion internal heat is formed at the upper part of the direct gas cooling section, and the direct cooling gas is used for reducing the oxygen flow in the stripping heat supply gas distribution element of the stripping section.

23. The pyrolysis furnace of claim 22, wherein:

the flow rate of combustion-supporting oxygen contained in the direct cooling gas of the direct gas cooling section is 0.05-0.20 times of the flow rate of oxygen in the stripping gas supply and distribution element of the stripping section.

24. The pyrolysis furnace of claim 1, wherein:

in the low-temperature pyrolysis section temperature-regulating cooling gas distribution element, a mixer is arranged to mix coal gas and combustion-supporting gas, oxygen flowing through the low-temperature pyrolysis section temperature-regulating cooling gas distribution element is cooled, and the temperature of oxygen-deficient combustion flue gas after the temperature-regulating gas oxygen is completely burned is at least 250 ℃ lower than the temperature of output gas of the stripping section.

25. The pyrolysis furnace of claim 24, wherein:

the flow rate of oxygen contained in the temperature-adjusting cooling gas of the low-temperature pyrolysis section is 0.05-0.10 times of the flow rate of oxygen in the stripping section stripping gas supply and distribution element.

26. The pyrolysis furnace of claim 1, wherein:

the temperature of the pyrolysis furnace gas discharged from the ascending pipe is 80-150 ℃.

27. The pyrolysis furnace of claim 1, wherein:

the combustion-supporting gas is air.

28. The pyrolysis furnace of claim 1, wherein:

the combustion-supporting gas is rich oxygen or pure oxygen;

29. The pyrolysis furnace of claim 1, wherein:

30. The pyrolysis furnace of claim 29, wherein:

the combustion-supporting gas used by the pyrolysis furnace is oxygen-enriched gas consisting of oxygen and carbon dioxide, and is introduced into the mixing position of the pyrolysis furnace after being mixed in a special mixing tank outside the pyrolysis furnace to be mixed with combustible gas,

the volume ratio of the combustion-supporting oxygen to the combustible gas is reduced, the mixing difficulty of the combustion-supporting oxygen and the combustible gas is reduced, and a high-temperature combustion area is reduced.

31. The pyrolysis furnace of claim 1, wherein:

the coal material entering the preheating section of the pyrolysis furnace has the material block particle size selected from one or more of the following materials:

①3mm～100mm；

②5mm～20mm；

③20mm～60mm；

④30mm～80mm。

32. the pyrolysis furnace of claim 1, wherein:

the coal material entering the preheating section of the pyrolysis furnace is divided into 2 or more size grades of coal materials, and the coal feeding and the uniform distribution are respectively and independently carried out in the preheating section of the pyrolysis furnace.

33. The pyrolysis furnace of claim 1, wherein:

the coal material entering the preheating section of the pyrolysis furnace is dried coal material discharged in the drying process of the coal material outside the pyrolysis furnace.

34. The pyrolysis furnace of claim 1, wherein:

the temperature-adjusting cooling gas distribution element comprises a mixer of coal gas and combustion-supporting gas; the gas supply pipeline and the combustion-supporting gas supply pipeline are both provided with flow regulating valves;

a stripping heat supply gas distribution element comprising a mixer of coal gas and combustion-supporting gas; the gas supply pipeline and the combustion-supporting gas supply pipeline are both provided with flow regulating valves.

35. The pyrolysis furnace of claim 22, wherein:

the input pipe system for directly cooling the gas comprises a mixer of coal gas and combustion-supporting gas; the gas supply pipeline and the combustion-supporting gas supply pipeline are both provided with flow regulating valves.

36. The pyrolysis furnace of claim 1, wherein:

thermocouples are arranged in a coal bed and a semicoke bed of the pyrolysis furnace.

37. The pyrolysis furnace of claim 1, wherein:

the horizontal section of a furnace chamber of the pyrolysis section of the pyrolysis furnace is square, and the furnace body belongs to a square box furnace;

38. The pyrolysis furnace of claim 1, wherein:

in the low-temperature pyrolysis section, the upper part of the temperature-adjusting gas distribution pipe arranged in the horizontal section of the material layer is in an inverted V shape, and the temperature-adjusting gas distribution pipe is provided with an opening in the downward or lateral direction.

39. The pyrolysis furnace of claim 13, wherein:

in the direct air cooling section, the upper part of a direct cooling air distribution pipe arranged in the horizontal section of the material layer is in an inverted V shape, and the temperature regulating air distribution pipe is provided with an opening in the downward or lateral direction.