Three-way Intake Combined Centrifugal Compression and Conveying Method for Double Pyrolysis Section Vertical Coal Pyrolysis Furnace

Abstract

The invention discloses a three-way air intake combined centrifugal compression and transportation method for a double-pyrolysis-stage coal vertical pyrolysis furnace. In a double-pyrolysis-stage coal vertical pyrolysis furnace system with internal heat gas-solid countercurrent heat transfer, a first combustion-aiding gas and a first fuel gas are pressurized by a combined centrifugal compressor and then passed through a first mixer to form a first mixed gas that enters the main fire channel of the stripping section for combustion and / or enters the furnace of the coal pyrolysis furnace for combustion to release heat to form an upward gas heat carrier to heat and pyrolyze the descending coal material; the combustion of the first mixed gas is oxygen-deficient combustion, and the remaining gas is used as temperature-control gas; the temperature-adjusting gas is pressurized by a combined centrifugal compressor and then passes through the temperature-adjusting gas channel of the low-temperature pyrolysis section to enter the furnace to reduce the temperature of the ascending gas; the combined centrifugal compressor uses a prime mover to drive three centrifugal compressors to start and stop at the same time, and reliably controls the flow ratio of the three gases to prevent the main fire channel from causing the risk of deflagration and detonation due to excessive oxygen in the intake air and insufficient temperature-controlling gas, and to prevent the temperature-adjusting gas from being cut off and causing overheating of the low-temperature distillation section.

Description

Technical Field

[0001] The invention relates to a three-way air intake combined centrifugal compression and transportation method for a double-pyrolysis-section coal vertical pyrolysis furnace. In a double-pyrolysis-section coal vertical pyrolysis furnace system with internal heat gas-solid countercurrent heat transfer, a first combustion-supporting gas and a first fuel gas are pressurized by a combined centrifugal compressor and then formed into a first mixed gas by a first mixer. The first mixed gas enters a main fire channel of a stripping section for combustion and / or enters a furnace of a coal pyrolysis furnace for combustion to release heat to form an upward gas heat carrier, thereby heating and pyrolyzing the descending coal material. The combustion of the first mixed gas belongs to oxygen-deficient combustion, and the remaining gas is used as temperature-control gas. The temperature-adjusting gas is pressurized by a combined centrifugal compressor and then enters the furnace through a temperature-adjusting gas channel of a low-temperature pyrolysis section to reduce the temperature of the ascending gas. The combined centrifugal compressor uses a prime mover to drive three centrifugal compressors to start and stop at the same time, thereby reliably controlling the flow ratio of the three gases, reliably preventing the risk of deflagration and detonation caused by excessive oxygen in the intake air and insufficient temperature-controlling gas in the main fire channel, and preventing the temperature-adjusting gas from being cut off and causing overheating of the low-temperature dry distillation section. The invention is a basic safety guarantee measure for a coal pyrolysis device using oxygen-enriched oxygen or pure oxygen as the combustion-supporting gas. Background Art

[0002] The present invention relates to an internally heated moving bed vertical coal pyrolysis furnace, which refers to a moving bed vertical coal pyrolysis furnace which uses at least the flue gas of the main fire channel combustion gas of the pyrolysis furnace as a gas heat carrier to pyrolyze coal.

[0003] The coal pyrolysis furnace of the present invention can be simultaneously provided with a system for providing external heat to the pyrolysis section (preheating section and / or pyrolysis section and / or stripping section); in the external heat supply system, the high-temperature gas flowing through the heat source material channel of the external heat supply system does not enter the furnace of the pyrolysis furnace, and the heat source material channel of the external heat supply system indirectly transfers heat to the furnace of the coal dry distillation zone of the pyrolysis furnace through the heat transfer wall.

[0004] The present invention relates to an internal heating type moving bed coal vertical pyrolysis furnace, which may or may not be provided with a semi-coke cooling section and a coke quenching section as required.

[0005] The present invention relates to the compression and transportation process of the component gases of the combustion gas used in the main fire channel of an internally heated moving bed coal vertical pyrolysis furnace, namely, the combustion-supporting gas and the combustion gas, and also to the compression and transportation of the temperature-regulating gas in the low-temperature pyrolysis section; the main fire channel refers to the fire channel from which most of the internal heating heat supply of the internally heated moving bed coal vertical pyrolysis furnace comes.

[0006] In the coal pyrolysis section of the present invention, the first mixed fuel gas burns in the main fire channel and / or enters the furnace of the coal pyrolysis furnace to burn and release heat to form flue gas which goes upward as a gas heat carrier to heat and pyrolyze the descending coal.

[0007] National Standard GB / T 25212-2010 Classification of Varieties and Grades of Semi-coke Products stipulates the standard values of each grade for each performance index of semi-coke. It can be seen that sometimes the index values differ very little, but the grades are completely different. For example, for the fixed carbon index FCd of semi-coke, within the range of 74.01% to 92.00%, each increase of 2% raises the grade by one level; for example, for the volatile matter index Vdaf of semi-coke, within the range of 15.00% to 4.00%, each decrease of 5% raises the grade by one level. The increase in grade means a significant improvement in service performance and applicable scope, and there is a huge difference in product price. For example, for the volatile matter index Vdaf of semi-coke, when it decreases from 7.0% (belonging to the range of 5.01% to 10.00% and classified as V-2 grade) to 4.5% (belonging to the range of ≤5.00% and classified as V-1 grade), the grade is raised by one level, and the product price difference reaches 100 - 150 yuan / ton or even higher. Since pyrolytic semi-coke has the highest yield among pyrolysis products, the output value increases significantly. For example, for a semi-coke production plant with an annual output of 1 million tons, the sales difference is 100 - 150 million yuan / year or even higher.

[0008] In fact, if the normal progress of the low-temperature pyrolysis process can be ensured and the volatile matter of semi-coke is further reduced reasonably, the following beneficial effects will be produced:

[0009] ① Improve the yields of high-value products (coal gas and tar) and increase the output value;

[0010] ② Reduce the volatile matter content of semi-coke, increase the strength of semi-coke, raise the price of semi-coke, and increase the output value.

[0011] Under the conditions of a single pyrolysis section pyrolysis furnace or a pyrolysis furnace that is substantially a single pyrolysis section pyrolysis furnace, taking low-rank coal as an example, when the final pyrolysis temperature is 600 - 900 °C, the increase in the coal gas yield is particularly significant; the pyrolysis time directly affects the pyrolysis degree and product distribution of low-rank coal. The extension of the pyrolysis time will increase the degree of secondary cracking of tar, resulting in a decrease in the tar yield and an increase in the coal gas yield.

[0012] Under the condition of the same coal material, reducing the volatile matter of semi-coke requires a higher final pyrolysis temperature. However, the conventional method of increasing the final pyrolysis temperature (such as forming medium-temperature pyrolysis) will inevitably lead to the change from low-temperature pyrolysis to medium-temperature pyrolysis. More heavy volatile matters in coal are thermally condensed into coke (i.e., burned out), resulting in a decrease in the tar yield. The higher the final pyrolysis temperature, the easier the secondary cracking of tar. When the final pyrolysis temperature is higher than a certain specific optimal value (varying with coal types), the secondary cracking reaction of tar increases sharply, leading to a decrease in the actual tar yield and an increase in the gas yield at the same time. The increase in the thermal cracking rate and thermal condensation rate of this coal tar vapor (i.e., losing hydrogen and becoming heavier) will also deteriorate the tar quality, increase the difficulty of hydro-upgrading, and reduce the use value. Generally speaking, for low-rank coal with high volatile matter, compared with low-temperature pyrolysis (high tar yield, light oil quality, low gas yield, and relatively high volatile matter of semi-coke), medium-temperature pyrolysis (low tar yield, heavy oil quality, higher gas yield, and low volatile matter of semi-coke) is less economical, which has led to the prevalence of low-temperature pyrolysis technology and the rare application of medium-temperature pyrolysis technology (only used in the occasion of producing more gas).

[0013] Therefore, there is a need for a double-pyrolysis-section coal dry distillation process. On the premise of ensuring the operation effect of low-temperature pyrolysis, a stripping section for reducing the volatile matter content of semi-coke is added. The main burner at the bottom of the stripping section provides hot flue gas, and a temperature-regulating gas is sprayed into the bottom of the low-temperature pyrolysis section to control and reduce the temperature of the rising gas.

[0014] The first common problem in the current internal-heat low-temperature pyrolysis device for low-rank coal is that the volatile matter of semi-coke is relatively high and the strength of semi-coke is relatively low. In the existing technical solutions, to reduce the volatile matter of semi-coke, the final pyrolysis temperature must be increased, which will inevitably result in tar burnout. This is mainly caused by the control method of the pyrolysis temperature field. In the current pyrolysis temperature field of the semi-coke furnace, along the descending direction of the coal material, the temperature gradually increases, and there is no internal-heat moving-bed vertical pyrolysis furnace or pyrolysis operation mode with a sudden drop in the temperature of the rising gas in the double-pyrolysis section. In fact, there is no low-temperature pyrolysis section and medium-temperature pyrolysis section with independent and flexible control of each pyrolysis temperature. The medium-temperature pyrolysis section is used to ensure the reduction of the volatile matter of semi-coke, and at the same time, the low-temperature pyrolysis section with independent temperature control is used to increase the tar yield and quality.

[0015] The second common problem in current low-rank coal internal heating medium and low temperature pyrolysis devices is that the nitrogen content in the coal gas is about 50%, the contents of hydrogen and methane are low, the calorific value is low, and it is rich in light hydrocarbons, oxygen, hydrogen sulfide, organic sulfur, ammonia, water vapor, etc. The costs of hydrogen recovery and methane recovery are high, and the utilization value is low, which restricts to a certain extent the comprehensive processing and utilization of the effective gases (hydrogen and methane) in the coal gas, limits the use value of the effective gases in the coal gas, and reduces the efficiency of the device. The main reason is that it is difficult to control the combustion of high-purity combustible gas coal gas and oxygen-enriched or pure oxygen. If not handled properly, it will cause sintering and caking of coal at the outlet of the air distribution bricks in the flue, uneven flue gas outlet, resulting in uneven furnace temperature in the pyrolysis furnace, and the quality of semi-coke cannot be guaranteed, leading to inability to produce. Moreover, once excessive oxygen-enriched or pure oxygen is introduced into the furnace of the pyrolysis furnace, deflagration or even detonation will occur, forming a vicious accident of furnace explosion. One of the reasons is the lack of process equipment and control methods for controlling the excessive introduction of oxygen into the furnace of the pyrolysis furnace.

[0016] In an internal heating moving bed coal vertical pyrolysis furnace, when using air as the combustion-supporting gas, the volume concentration of the effective gas in its coal gas is very low. Table 1 shows the coal gas compositions corresponding to different combustion-supporting gases of coal pyrolysis furnaces, which are a set of typical production data of a certain coal low-temperature pyrolysis device. Compared with the pure combustion reaction of combustible components and oxygen, the non-combustible gas (mainly nitrogen) from air becomes the cooling component in the combustion process, and its volume flow rate is 3.77 times that of the oxygen volume flow rate. The non-combustible gas (H 2 O, CO 2 、N 2 、) in the recycled fuel coal gas is also the cooling component in the combustion process. Coupled with the artificially arranged recycled coal gas exceeding the combustion ratio, which is also the cooling component in the combustion process, the normal value of the combustion flue gas temperature in the flue is about 650-900°C. If combustion is carried out according to the chemical equivalent, the calculation results are shown in Table 2 for the flue gas temperature and volume expansion ratio during the chemical equivalent combustion process of coal gas under different working conditions. The flue gas temperature is about 1694°C, and the short-term high temperature can be tolerated by high-aluminum bricks or silica bricks. The volume expansion ratio of the combustion raw gas to the combustion flue gas is 5.70, and a deflagration with a lower intensity can be formed.

[0017] In an internal heating moving bed coal vertical pyrolysis furnace, assuming that oxygen-enriched gas with an oxygen volume concentration of 34.71% and a carbon dioxide volume concentration of 65.29% is used as the combustion-supporting gas, the estimated value of the volume concentration of the effective gas in its coal gas is shown in Table 1. Under accident conditions (excessive addition of combustion-supporting gas), when combustion is carried out according to the chemical equivalent, the calculation results are shown in Table 2, and the flue gas temperature can reach 2633°C. The volume expansion ratio of the combustion raw gas to the combustion flue gas is 8.09, and deflagration will be formed, which indicates that the danger has increased significantly under accident conditions.

[0018] For an internally heated moving - bed vertical coal pyrolysis furnace, assuming pure oxygen is used as the combustion - assisting gas, the estimated values of the effective gas volume concentration in the coal gas are shown in Table 1. In the accident state (excessive addition of the combustion - assisting gas), burning according to the chemical equivalence, the calculated results of the flue gas temperature and volume expansion ratio during the chemical - equivalent combustion of coal gas and pure oxygen are shown in Table 3. The flue gas temperature is expected to reach about 4316 °C, and the volume expansion ratio of the combustion raw gas to the combustion flue gas is 11.47. Since the flame propagation speed in the high - hydrogen - concentration gas is very high, deflagration or detonation is extremely likely to occur, which may cause furnace wall rupture accidents or catastrophic furnace explosion accidents.

[0019] Table 1 Gas composition of coal gas corresponding to different combustion - assisting gases in coal pyrolysis furnaces

[0020]

[0021] Table 2 Flue gas temperature and volume expansion ratio during the chemical - equivalent combustion of coal gas under different working conditions

[0022]

[0023]

[0024] Table 3 Flue gas temperature and volume expansion ratio during the chemical - equivalent combustion of coal gas and pure oxygen

[0025]

[0026] There are theoretical prediction deviations in the gas composition in the above - mentioned calculations, and there will also be slight deviations in the flue gas composition and temperature. However, it does not affect the basic correctness of the analysis conclusion.

[0027] Therefore, for an internally heated moving - bed vertical coal pyrolysis furnace using oxygen - enriched gas or pure oxygen as the combustion - assisting gas, it is necessary to eliminate the hidden dangers of deflagration and detonation, and it is also necessary to reliably control the appropriate temperature in each dry - distillation section. Since the mixer feed (the first combustion - assisting gas and the first fuel gas) in the main flue (also known as the main gas chamber) of the current internally heated moving - bed vertical coal pyrolysis furnace is compressed and transported by independent combustion - assisting gas centrifugal compressors and coal - gas centrifugal compressors respectively, it is impossible to ensure simultaneous start - up and shutdown. Therefore, under the condition that the coal gas supply is reduced or stopped in the combustion flue while the combustion - assisting gas continues to be fed in the combustion flue, that is, the out - of - control of the combustion - assisting gas in the combustion flue is formed, and a vicious accident of deflagration or detonation will occur in the combustion flue of the pyrolysis furnace and the nearby furnace chamber area. And the present invention is proposed to avoid such accidents or accident hidden dangers. Its basic concept is that the combustion - assisting gas in the combustion flue must enter together with the gas in the expected proportion, and the temperature - regulating gas must also enter the bottom of the low - temperature pyrolysis section of the furnace chamber synchronously to accurately control the temperature of the low - temperature dry - distillation section (preventing the temperature from being too high), thus becoming the basic safety guarantee measure for the coal pyrolysis device using oxygen - enriched gas or pure oxygen as the combustion - assisting gas.

[0028] The concept of the present invention is: a three-way air intake combined centrifugal compression and transportation method for a double-pyrolysis-stage coal vertical pyrolysis furnace, in which a double-pyrolysis-stage coal vertical pyrolysis furnace system with internal heat gas-solid countercurrent heat transfer exists, a first combustion-supporting gas and a first fuel gas are pressurized by a combined centrifugal compressor and then passed through a first mixer to form a first mixed gas that enters the main fire channel of the stripping section for combustion and / or enters the furnace of the coal pyrolysis furnace for combustion to release heat to form an upward gas heat carrier to heat and pyrolyze the descending coal material; the combustion of the first mixed gas belongs to oxygen-deficient combustion, and the remaining gas is used as temperature-control gas; the temperature-adjusting gas is pressurized by a combined centrifugal compressor and then passes through the temperature-adjusting gas channel of the low-temperature pyrolysis section to enter the furnace to reduce the temperature of the rising gas; the combined centrifugal compressor uses a prime mover to drive three centrifugal compressors to start and stop at the same time, reliably controls the flow ratio of the three gases, reliably prevents the main fire channel from causing the risk of deflagration and detonation due to excessive oxygen in the intake air and too little temperature-controlling gas, and prevents the temperature-adjusting gas from being cut off and causing overheating of the low-temperature distillation section, which is a basic safety guarantee measure for coal pyrolysis devices using oxygen-enriched oxygen or pure oxygen as combustion-supporting gas.

[0029] Several patent documents on combined centrifugal compressors involving multiple centrifugal compressors are described below. Their mechanical structures and functions can be used for reference by the present invention if they are suitable and available.

[0030] Chinese Patent ZL201210361133.2 A single-shaft plus multi-shaft carbon dioxide centrifugal compressor includes a double-shaft drive device, the left shaft of the double-shaft drive device is directly connected to the single-shaft low-pressure cylinder by a diaphragm coupling, and the right shaft of the double-shaft drive device is connected to the multi-shaft high-pressure cylinder by a diaphragm coupling; CO 2 The gas enters from the first-stage impeller of the single-shaft low-pressure cylinder, undergoes four-stage compression, flows out from the fourth-stage outlet pipe of the low-pressure cylinder and enters the first-stage impeller of the multi-shaft high-pressure cylinder, and then is discharged from the 3rd and 4th-stage impeller outlet of the multi-shaft high-pressure cylinder after four-stage compression and enters the subsequent process system; the present invention saves more than 10% energy compared with the traditional single-shaft + single-shaft model, and has higher safety and stability than foreign multi-shaft carbon dioxide compressors. The multi-stage centrifugal compressor of the invention is used for a gas, namely CO 2 The gas is compressed in multiple stages in series.

[0031] Chinese Patent ZL201410351897.2 Multistage Centrifugal Compressor, which provides a multistage centrifugal compressor with reduced thrust load generated on the output shaft, high efficiency and high mechanical reliability. The multistage centrifugal compressor includes: an input shaft (4) driven by an engine; a main gear (20) provided on the input shaft (4); a pinion (21) meshing with the main gear (20); an output shaft (5) provided with the pinion (21); a first-stage centrifugal impeller (11) provided at one end of the output shaft (5); and a second-stage centrifugal impeller (12) provided at the other end of the output shaft (5) and located on the downstream side of the fluid flow relative to the first-stage centrifugal impeller (11). Moreover, the outer diameter (D1) of the first-stage centrifugal impeller (11) is set larger than the outer diameter (D2) of the second-stage centrifugal impeller (12). The multistage centrifugal compressor of this invention is used for multistage series compression of a gas.

[0032] Chinese Patent ZL201480030156.2 Centrifugal Compressor, which includes: a drive shaft (2) for rotational drive; a drive gear (11) connected to the drive shaft (2); driven gears (12, 13) for obtaining the rotation transmitted by the drive gear (11); a driven shaft (3) extending toward both ends in the central axis direction of the driven gears (12, 13); a first compression part (41) provided on the first end side in the central axis direction of the driven shaft (3); a second compression part (42) provided on the second end side in the central axis direction of the driven shaft (3); and a pressure adjustment part (7) for uniformly adjusting the pressure in the fluid ejection side space of the first compression part (41) and the pressure in the fluid ejection side space of the second compression part (42). The multistage centrifugal compressor of this invention is used for multistage series compression of a gas.

[0033] The method of this invention has not been reported.

[0034] The object of the invention is to propose a three-way intake combined centrifugal compression and transportation method for a double pyrolysis section vertical coal pyrolysis furnace. Summary of the Invention

[0035] The three-way intake combined centrifugal compression and transportation method for the double pyrolysis section vertical coal pyrolysis furnace of this invention is characterized in that:

[0036] ⑴ Double pyrolysis section vertical coal pyrolysis furnace

[0037] The coal pyrolysis furnace is an upflow gas temperature sudden drop type double pyrolysis section internal heat type moving bed vertical coal pyrolysis furnace. When the coal material enters the pyrolysis furnace and moves downward, it passes through at least a preheating section, a low-temperature pyrolysis section, and a stripping section, and gradually becomes preheated coal material, low-temperature pyrolysis semi-coke, and stripping semi-coke;

[0038] In the pyrolysis chamber of the pyrolysis furnace, the stripping section is located below the low-temperature pyrolysis section, and the stripping section space is communicated with the low-temperature pyrolysis section space;

[0039] In the low-temperature pyrolysis section, the heat source for the low-temperature pyrolysis section is provided by the initial gas heat carrier of the low-temperature pyrolysis section rising within the low-temperature pyrolysis section; a temperature-regulating gas distribution airway is arranged at the bottom of the low-temperature pyrolysis section, and the temperature-regulating gas distribution airway discharges the temperature-regulating gas into the furnace cavity; the temperature-regulating gas entering the furnace cavity is mixed with the upward output gas of the stripping section from the stripping section to become the initial gas heat carrier of the low-temperature pyrolysis section, and the temperature of the initial gas heat carrier of the low-temperature pyrolysis section is at least 100 °C lower than the temperature of the output gas of the stripping section;

[0040] In the low-temperature pyrolysis section, the temperature-regulating gas distribution airway is located within the lower coke layer and / or on the side of the lower coke layer of the low-temperature pyrolysis section;

[0041] In the low-temperature pyrolysis section, the gas heat carrier of the low-temperature pyrolysis section rises, countercurrently contacts and cools with the downward preheated coal material from the preheating section, and mixes with the low-temperature pyrolysis net-produced coal gas to become the output gas of the low-temperature pyrolysis section; the output gas of the low-temperature pyrolysis section enters the preheating section; the downward preheated coal material is gradually heated for low-temperature pyrolysis, reducing the volatile matter to become low-temperature semi-coke; the low-temperature semi-coke descends and is discharged from the low-temperature pyrolysis section into the stripping section;

[0042] In the stripping section, most to all of the heat source for the stripping section is provided by the gas heat carrier rising within the stripping section; a main flue is arranged at the bottom of the stripping section; the stripping heat supply gas discharged from the main flue rises, countercurrently contacts and cools with the downward low-temperature pyrolysis semi-coke from the low-temperature pyrolysis section, and mixes with the stripping net-produced coal gas to become the output gas of the stripping section; the output gas of the stripping section enters the low-temperature pyrolysis section; the downward low-temperature pyrolysis semi-coke is gradually heated for deep pyrolysis, reducing the volatile matter to become stripping semi-coke; the stripping semi-coke is discharged from the stripping section;

[0043] The main flue of the stripping section is located within the lower coke layer and / or on the side of the lower coke layer of the stripping section;

[0044] The internally heated lump coal moving bed vertical pyrolysis furnace is composed of one or multiple carbonization chambers; on at least one side of each carbonization chamber, a temperature-regulating gas distribution airway and a main flue are provided;

[0045] Outlet openings are arranged on the temperature-regulating gas distribution airway, and outlet openings are arranged on the main flue;

[0046] A coal distribution plate is provided at the upper part of the pyrolysis chamber, and a riser is provided at the top of the pyrolysis chamber; the riser discharges the primary coal gas from the pyrolysis furnace;

[0047] ⑵ Three-way intake combined centrifugal compression and transportation

[0048] In the combined centrifugal compressor, a single prime mover drives the first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature-regulating gas centrifugal compressor. The first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature-regulating gas centrifugal compressor operate in a mode of starting simultaneously, running simultaneously, and stopping simultaneously;

[0049] The prime mover of the combined centrifugal compressor transmits power to the first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature-regulating gas centrifugal compressor through a power transmission mechanism;

[0050] The first combustion-supporting gas is boosted by the first combustion-supporting gas centrifugal compressor of the combined centrifugal compressor to become the boosted first combustion-supporting gas; the first fuel gas is boosted by the first fuel gas centrifugal compressor of the combined centrifugal compressor to become the boosted first fuel gas;

[0051] The boosted first combustion-supporting gas and the boosted first fuel gas enter the first mixer to become the first mixed fuel gas; the first mixed fuel gas enters the main flue to burn and / or enters the furnace of the coal pyrolysis furnace to burn and release heat, forming an upward gas heat carrier to heat the downward coal material; the ratio of the volume of the first fuel gas entering the first mixer to the volume of the first fuel gas with a chemical combustion equivalent entering the first mixer is defined as the first fuel gas supply combustion ratio K1, and K1≥1.15;

[0052] The temperature-regulating gas is boosted by the temperature-regulating gas centrifugal compressor of the combined centrifugal compressor to become the boosted temperature-regulating gas;

[0053] The boosted temperature-regulating gas enters the temperature-regulating gas air distribution channel, passes through the air distribution port of the air distribution channel connecting the furnace to enter the furnace, and contacts the upward hot gas and the downward carbon material to reduce the temperature of the upward gas;

[0054] The temperature-regulating gas is the purified coal gas obtained from the primary coal gas of the pyrolysis furnace through a purification process including at least steps of cooling, deoiling, and dehydration;

[0055] The first fuel gas is the purified coal gas obtained from the primary coal gas of the pyrolysis furnace through a purification process including at least steps of cooling, deoiling, and dehydration.

[0056] For the method of the present invention, the first structural scheme of the combined centrifugal compressor is as follows:

[0057] The combined centrifugal compressor adopts a prime mover with a double output shaft;

[0058] The first output shaft of the double output shaft prime mover is connected to the input shaft of the first transmission mechanism for driving;

[0059] The main gear of the first transmission mechanism is arranged on the input shaft of the first transmission mechanism;

[0060] The first pinion gear meshes with the main gear of the above-mentioned first transmission mechanism;

[0061] The output shaft of the first pinion gear is used to arrange the above-mentioned first pinion gear and form one side and the other side of the output shaft of the first pinion gear;

[0062] On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor is arranged, and on the other side of the output shaft of the first sprocket wheel, a temperature regulating gas centrifugal compressor is arranged;

[0063] The second output shaft of the double-output shaft prime mover is connected to the impeller rotating shaft of the first combustion-supporting gas centrifugal compressor.

[0064] The second structural scheme of the combined centrifugal compressor in the method of the present invention is as follows:

[0065] The combined centrifugal compressor adopts a double-output shaft prime mover;

[0066] The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission to drive;

[0067] The main gear of the first transmission is arranged on the input shaft of the first transmission;

[0068] The first sprocket wheel meshes with the main gear of the above-mentioned first transmission;

[0069] The output shaft of the first sprocket wheel is used to arrange the above-mentioned first sprocket wheel and form one side and the other side of the output shaft of the first sprocket wheel;

[0070] On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor is arranged, and on the other side of the output shaft of the first sprocket wheel, a temperature regulating gas centrifugal compressor is arranged;

[0071] The second output shaft of the double-output shaft prime mover is connected to the input shaft of the second transmission to drive;

[0072] The main gear of the second transmission is arranged on the input shaft of the second transmission;

[0073] The second sprocket wheel meshes with the main gear of the above-mentioned second transmission;

[0074] The output shaft of the second sprocket wheel is used to arrange the above-mentioned second sprocket wheel and form one side and the other side of the output shaft of the second sprocket wheel;

[0075] On one side of the output shaft of the second sprocket wheel, a first combustion-supporting gas centrifugal compressor A is arranged, and on the other side of the output shaft of the second sprocket wheel, a first combustion-supporting gas centrifugal compressor B is arranged;

[0076] The first combustion-supporting gas is divided into two paths with the same flow rate and enters the first combustion-supporting gas centrifugal compressor A and the first combustion-supporting gas centrifugal compressor B respectively.

[0077] The third structural scheme of the combined centrifugal compressor in the method of the present invention is as follows:

[0078] The combined centrifugal compressor adopts a double-output shaft prime mover;

[0079] The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission for driving;

[0080] The main gear of the first transmission is arranged on the input shaft of the first transmission;

[0081] The first pinion gear meshes with the main gear of the above-mentioned first transmission;

[0082] The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0083] The first fuel gas centrifugal compressor A is arranged on one side of the first pinion gear output shaft, and the first fuel gas centrifugal compressor B is arranged on the other side of the first pinion gear output shaft;

[0084] The first fuel gas is divided into two paths with the same flow rate and enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B respectively;

[0085] The second output shaft of the double-output shaft prime mover is connected to the input shaft of the second transmission for driving;

[0086] The main gear of the second transmission is arranged on the input shaft of the second transmission;

[0087] The second pinion gear meshes with the main gear of the above-mentioned second transmission;

[0088] The second pinion gear output shaft is used to arrange the above-mentioned second pinion gear and form one side and the other side of the second pinion gear output shaft;

[0089] The first combustion-supporting gas centrifugal compressor is arranged on one side of the second pinion gear output shaft, and the temperature-regulating gas centrifugal compressor is arranged on the other side of the second pinion gear output shaft.

[0090] The fourth structural scheme of the combined centrifugal compressor in the method of the present invention is:

[0091] The combined centrifugal compressor uses a single-output shaft prime mover to drive the first transmission;

[0092] The input shaft of the first transmission is connected to the prime mover output shaft;

[0093] The main gear is arranged on the input shaft of the above-mentioned first transmission;

[0094] The first pinion gear meshes with the above-mentioned main gear;

[0095] The second pinion gear meshes with the above-mentioned main gear;

[0096] The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0097] The second eccentric wheel output shaft is used to set the above-mentioned second eccentric wheel;

[0098] On one side of the first eccentric wheel output shaft, a first fuel gas centrifugal compressor is arranged, and on the other side of the first eccentric wheel output shaft, a temperature regulating gas centrifugal compressor is arranged;

[0099] On one side of the second eccentric wheel output shaft, a first combustion-supporting gas centrifugal compressor is arranged.

[0100] The fifth structural scheme of the combined centrifugal compressor in the method of the present invention is:

[0101] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission;

[0102] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0103] The main gear is arranged on the input shaft of the above-mentioned first transmission;

[0104] The first eccentric wheel meshes with the above-mentioned main gear;

[0105] The second eccentric wheel meshes with the above-mentioned main gear;

[0106] The first eccentric wheel output shaft is used to set the above-mentioned first eccentric wheel and form one side and the other side of the first eccentric wheel output shaft;

[0107] The second eccentric wheel output shaft is used to set the above-mentioned second eccentric wheel and form one side and the other side of the second eccentric wheel output shaft;

[0108] On one side of the first eccentric wheel output shaft, a first fuel gas centrifugal compressor is arranged, and on the other side of the first eccentric wheel output shaft, a temperature regulating gas centrifugal compressor is arranged;

[0109] On one side of the second eccentric wheel output shaft, a first combustion-supporting gas centrifugal compressor A is arranged, and on the other side of the second eccentric wheel output shaft, a first combustion-supporting gas centrifugal compressor B is arranged;

[0110] The first combustion-supporting gas is divided into two paths with the same flow rate and enters the first combustion-supporting gas centrifugal compressor A and the first combustion-supporting gas centrifugal compressor B respectively.

[0111] The sixth structural scheme of the combined centrifugal compressor in the method of the present invention is:

[0112] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission;

[0113] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0114] The main gear is arranged on the input shaft of the above-mentioned first transmission;

[0115] The first pinion gear meshes with the above-mentioned main gear;

[0116] The second pinion gear meshes with the above-mentioned main gear;

[0117] The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0118] The second pinion gear output shaft is used to arrange the above-mentioned second pinion gear and form one side and the other side of the second pinion gear output shaft;

[0119] On one side of the first pinion gear output shaft, a first fuel gas centrifugal compressor A is arranged, and on the other side of the first pinion gear output shaft, a first fuel gas centrifugal compressor B is arranged;

[0120] The first fuel gas is divided into two paths with the same flow rate and enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B respectively;

[0121] On one side of the second pinion gear output shaft, a first combustion-supporting gas centrifugal compressor is arranged, and on the other side of the second pinion gear output shaft, a temperature-regulating gas centrifugal compressor is arranged.

[0122] The seventh structural scheme of the combined centrifugal compressor in the method of the present invention is as follows:

[0123] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission;

[0124] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0125] The main gear is arranged on the input shaft of the above-mentioned first transmission;

[0126] The first pinion gear meshes with the above-mentioned main gear;

[0127] The second pinion gear meshes with the above-mentioned main gear;

[0128] The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0129] The second pinion gear output shaft is used to arrange the above-mentioned second pinion gear and form one side and the other side of the second pinion gear output shaft;

[0130] On one side of the first pinion gear output shaft, a temperature-regulating gas centrifugal compressor A is arranged, and on the other side of the first pinion gear output shaft, a temperature-regulating gas centrifugal compressor B is arranged;

[0131] The temperature-regulating gas is divided into two paths with the same flow rate and enters the temperature-regulating gas centrifugal compressor A and the temperature-regulating gas centrifugal compressor B respectively;

[0132] On one side of the output shaft of the second sprocket wheel, a first secondary combustion air centrifugal compressor is arranged, and on the other side of the output shaft of the second sprocket wheel, a first fuel gas centrifugal compressor is arranged.

[0133] In the method of the present invention, generally, the first secondary combustion air entering the combined centrifugal compressor comes from the first secondary combustion air buffer tank;

[0134] The operating pressure of the first secondary combustion air buffer tank is lower than the pressure at the outlet of the first mixer connected to the main flue.

[0135] In the method of the present invention, generally, on the pipeline of the boosted first secondary combustion air discharged from the combined centrifugal compressor, a first secondary combustion air emergency interlock cut-off valve is provided. Once the combined centrifugal compressor loses power, the first secondary combustion air emergency interlock cut-off valve is interlocked and closed;

[0136] Generally, on the pipeline of the boosted first fuel gas discharged from the combined centrifugal compressor, a first fuel gas emergency interlock cut-off valve is provided. Once the combined centrifugal compressor loses power, the first fuel gas emergency interlock cut-off valve is interlocked and closed;

[0137] Generally, on the pipeline of the boosted temperature-regulating gas discharged from the combined centrifugal compressor, a temperature-regulating gas emergency interlock cut-off valve is provided. Once the combined centrifugal compressor loses power, the temperature-regulating gas emergency interlock cut-off valve is interlocked and closed.

[0138] In the method of the present invention, generally, the first secondary combustion air entering the combined centrifugal compressor comes from the first secondary combustion air buffer tank;

[0139] The operating pressure of the first secondary combustion air buffer tank is lower than the pressure at the outlet of the first mixer connected to the main flue;

[0140] On the pipeline of the first secondary combustion air discharged from the first secondary combustion air buffer tank to the combined centrifugal compressor, a first secondary combustion air buffer tank overpressure interlock cut-off valve is provided. Once the pressure of the first secondary combustion air buffer tank is higher than the pressure at the outlet of the first mixer, the first secondary combustion air buffer tank overpressure interlock cut-off valve is interlocked and closed.

[0141] In the method of the present invention, generally, the first secondary combustion air is oxygen-rich air with an oxygen volume concentration higher than 35% and a carbon dioxide volume concentration higher than 60%.

[0142] In the method of the present invention, generally, in the coal pyrolysis furnace, a cold air distribution chamber of the semicoke cooling section is arranged at a certain height interval below the main flue;

[0143] The cooling gas enters the cold air distribution chamber of the semicoke cooling section, enters the cavity of the semicoke cooling section through the air distribution openings of the air distribution channels, and rises upward to contact the descending semicoke countercurrently to cool the semicoke.

[0144] In the method of the present invention, for the temperature-adjusting gas centrifugal compressor, its intake air may include temperature-adjusting gas and cold air for the semi-coke cooling section;

[0145] The pressurized gas discharged from the temperature-adjusting gas centrifugal compressor is at least divided into two paths, one path is used as temperature-adjusting gas, and one path is used as cold air for the semi-coke cooling section.

[0146] In the method of the present invention, generally, the gas flow temperature at 300 mm above the air outlet of the temperature-adjusting gas distribution duct in the low-temperature pyrolysis section is taken as the qualitative temperature of the initial gas heat carrier in the low-temperature pyrolysis section;

[0147] In the stripping section, the gas flow temperature at 300 mm below the air outlet of the temperature-adjusting gas distribution duct in the low-temperature pyrolysis section is taken as the qualitative temperature of the output gas in the stripping section;

[0148] The temperature of the low-temperature pyrolysis semi-coke at 300 mm above the air outlet of the temperature-adjusting gas distribution duct in the low-temperature pyrolysis section is taken as the qualitative temperature of the low-temperature pyrolysis section;

[0149] The temperature of the stripping semi-coke at 300 mm above the air outlet of the main flue in the stripping section is taken as the qualitative temperature of the stripping section;

[0150] The coal fed into the pyrolysis furnace is low-rank coal;

[0151] In the preheating section, the temperature of the preheated coal material discharged is 180 - 370 °C;

[0152] The qualitative temperature of the low-temperature pyrolysis section is 430 - 680 °C; the qualitative temperature of the initial gas heat carrier in the low-temperature pyrolysis section is at least 200 °C lower than the qualitative temperature of the output gas in the stripping section;

[0153] The qualitative temperature of the stripping section is 700 - 1000 °C, and is 100 - 450 °C higher than the qualitative temperature of the low-temperature pyrolysis section;

[0154] Each coking chamber is wider at the top and narrower at the bottom, and the middle cross-section is a variable cross-section. The temperature-adjusting gas distribution duct and the main flue are both arranged in the narrow cavity section below the transition section where the middle cross-section of the coking chamber becomes narrower;

[0155] The volatile content of the stripping semi-coke is at least 2.0 wt% lower than that of the low-temperature pyrolysis semi-coke;

[0156] The volatile content of the stripping semi-coke is lower than 4.95 wt%.

[0157] In the method of the present invention, generally, for the coal pyrolysis furnace, a semi-coke cooling section and / or a coke quenching section is provided below the pyrolysis section.

[0158] In the method of the present invention, generally, for the coal pyrolysis furnace, an external heat supply system is simultaneously provided. The high-temperature gas flowing through the heat transfer channel of the external heat supply system does not enter the furnace chamber of the pyrolysis furnace, and the external heat supply system indirectly transfers heat to the furnace chamber of the coal dry distillation area of the pyrolysis furnace through the heat transfer wall surface.

[0159] In the method of the present invention, generally, the first fuel gas supply ratio K1 is 1.5 to 5.0.

[0160] In the method of the present invention, generally, each centrifugal compressor is a single-stage centrifugal compressor.

[0161] In the method of the present invention, the impeller of the first combustion-supporting gas centrifugal compressor can adopt an impeller provided with an additional extended impeller area, and by increasing the area and gas pressure on the back of the impeller disc of the first combustion-supporting gas centrifugal compressor, the overall fluid load on the integrated output shaft is reduced.

[0162] In the method of the present invention, generally, the prime mover is an electric motor or a turbine.

[0163] In the method of the present invention, generally, the connection mode between the output shaft of the prime mover and the rotation shaft of the centrifugal compressor impeller or the input shaft of the transmission is direct connection or connection through a coupling.

[0164] In the method of the present invention, generally, the main gear and the pinion are helical gears;

[0165] The helix direction of the above-mentioned helical gears is set in such a way that the gear load acting axially on the pinion and the fluid load acting along the same axis on the corresponding output shaft are in opposite directions. Brief Description of the Drawings

[0166] Figure 1 It is a schematic diagram of the structure and function of the first combustion-supporting gas centrifugal compressor of the present invention provided with an additional extended impeller area.

[0167] Figure 2 is Figure 1 a partial enlarged view of the flow channel of the additional extended impeller area in

[0168] Figure 3 It is a schematic diagram of the power transmission mechanism (speed governor) of a combined centrifugal compressor of the present invention and the configuration mode of the centrifugal compressor.

[0169] Figure 4 It is a schematic diagram of the structure of a double pyrolysis section pyrolysis furnace.

[0170] For the convenience of explaining the problem, the drawings sometimes deform or locally enlarge the dimensions and shapes of some components.

[0171] Figure 1 、 Figure 2 The marking descriptions in

[0172] Rotating shaft 703, first combustion-supporting gas centrifugal compressor 720, first impeller 721, back panel 722, hub portion 723, through-hole 723a, main blade 724, first centrifugal compressor housing 726, side surface 726a, space portion 727, suction port 727a, main discharge port 727b, flow path 727c, insertion port 728, electric motor rotor 730, bearing 740L, motor housing 745, rotor space portion 745b, heat sink 746, bearing housing 750, protruding step portion 751, face portion 752, bolt 753, additional extended impeller region flow path 220, outer extension ring body 7221, outer edge blade 221, auxiliary exhaust port 225.

[0173] Figure 3 Marking descriptions in

[0174] Speed increaser section 100, first fuel gas centrifugal compressor C1, temperature-adjusting gas centrifugal compressor C2, first combustion-supporting gas centrifugal compressors C3A and C3B, input shaft 4, main gear 20, ratchet wheels 21, 22, output shaft 5, thrust rings 66, 67, output shaft 6, thrust rings 68, 69, housing 101, composite bearings 60, 61, gaps 70, 71, 72, centrifugal impeller 1001 of first fuel gas centrifugal compressor C1, centrifugal impeller 2001 of temperature-adjusting gas centrifugal compressor C2, centrifugal impellers 3001A, 3001B of first combustion-supporting gas centrifugal compressors C3A and C3B, gear load Fp1, gear load Fp2, resultant load F, fluid loads Fi1, Fi2, Fi3A, Fi3B.

[0175] Figure 4 Marking descriptions in

[0176] Figure 4 For the pyrolysis furnace part shown, a preheating section, a low-temperature pyrolysis section, a rectifying section, a direct air-cooling section, and a coke quenching section are provided, and the five-section cavity spaces of the preheating section, the low-temperature pyrolysis section, the rectifying section, the direct air-cooling section, and the coke quenching section are directly vertically connected.

[0177] Figure 4 The pyrolysis furnace shown is composed of a porous carbonization chamber 1000, and each carbonization chamber 1000 is wider at the top and narrower at the bottom, and the middle cross-section is a variable cross-section.

[0178] Figure 4 The component numbers of the pyrolysis furnace are described as follows:

[0179] Ascending pipe 9005, top charging plate 9006, low-temperature pyrolysis section 9008, channel 9009, gas transmission pipe 9009M, gas distribution brick 9010, main flue 9012, combustion gas mixer 9012M, gas distribution brick 9013, channel 9015, heat absorption gas transmission pipe 9015M, gas distribution brick 9016, quenching water main pipe and distribution pipe 9019, refractory brick 9050, thermocouple 9060, furnace protection ironware 9080; Interface FJM between the preheating section and the low-temperature pyrolysis section.

[0180] Figure 4 The description of the internal material numbers in the medium pyrolysis furnace is as follows:

[0181] LM represents the cold coal material in the upper part of the preheating section of the pyrolysis furnace;

[0182] RM represents the hot coal material in the lower part of the preheating section of the pyrolysis furnace;

[0183] DWBJ represents the low-temperature pyrolysis semi-coke discharged from the lower part of the low-temperature pyrolysis section;

[0184] TLBJ represents the stripping semi-coke discharged from the lower part of the stripping section;

[0185] QLBJ represents the gas-cooled semi-coke discharged from the lower part of the direct gas-cooling section;

[0186] XHBJ represents the quenched semi-coke discharged from the lower part of the quenching section.

[0187] The low-temperature pyrolysis section 9008 includes a wide horizontal cross-section section, namely the upper part of the low-temperature pyrolysis section 9081, a variable cross-section transition section, namely the middle part of the low-temperature pyrolysis section 9082, and a narrow horizontal cross-section section, namely the lower part of the low-temperature pyrolysis section 9083.

[0188] In the low-temperature pyrolysis section 9008, the temperature-regulating cooling gas distribution part is composed of the channel 9009, the gas transmission pipe 9009M arranged in the channel, the gas distribution brick 9010, etc.

[0189] In the stripping section, the stripping hot flue gas distribution part is composed of the main flue 9012, the combustion gas mixer 9012M arranged in the channel, the gas distribution brick 9013, etc.

[0190] In the direct gas-cooling section, the direct gas-cooling section heat absorption gas distribution part is composed of the channel 9015, the heat absorption gas transmission pipe 9015M arranged in the channel, the gas distribution brick 9016, etc.

[0191] The quenching section is provided with a quenching water main pipe and distribution pipe 9019. Specific implementation mode

[0192] The following describes the vertical coal pyrolysis furnace

[0193] The carbonization of coal is a process in which coal is thermally decomposed in the absence of air to produce coal tar, semicoke, pyrolysis gas, water, etc. According to the final heating temperature, coal carbonization can be roughly divided into three types: low-temperature carbonization (500 - 600 °C), medium-temperature carbonization (600 - 900 °C), and high-temperature carbonization (900 - 1100 °C). According to the heating method, coal carbonization furnaces can be divided into externally heated type, internally heated type, and dual external and internal heating type. Currently, internally heated furnaces are widely used and are divided into gas heat carrier and solid heat carrier carbonization furnaces. Gas heat carrier carbonization furnaces mainly include Lurgi three-stage furnaces, pyrolysis furnaces developed by Anshan Research Institute of Thermo-Energy Co., Ltd., China National Steel Corporation, and Shenmu Sanjiang Coal Chemical Industry Co., Ltd.

[0194] The processing of medium- and low-temperature coal pyrolysis has mild processing conditions, low investment, and low production costs. When processing high-volatile low-rank coal, the medium- and low-temperature pyrolysis process enriches the hydrogen in coal into tar and gas with a large output, and at the same time obtains carbon-rich semicoke, thus producing higher-value products. Usually, a coal pyrolysis device includes sections such as coal preparation, pyrolysis, crude gas purification, gas recycling, and pretreatment of phenol-containing wastewater.

[0195] Although specific optimal targeted operating conditions need to be determined according to different coal types and product properties and these operating conditions have a wide range, the main changes that occur during the heating process of low-rank coal in the entire medium- and low-temperature coal pyrolysis have the following general regularities, and the temperature stage division is fuzzy:

[0196] ① The drying and degassing stage, corresponding to the preheating stage of the present invention. Usually, the stage from room temperature to about 300 °C is the preheating, drying, and degassing stage; during this stage, there is no obvious change in the appearance of coal. Low-rank coals such as lignite undergo decarboxylation reactions above about 200 °C and start pyrolysis reactions at about 300 °C, while bituminous coal and anthracite generally have no changes in this stage; dehydration mainly occurs before 120 °C, and degassing (mainly removing carbon dioxide, methane, and nitrogen adsorbed and enclosed in the pores of coal) is generally completed around about 200 °C; the solid product of this stage is preheated coal or dried coal;

[0197] ② The active pyrolysis stage (about 300 - about 600 °C), corresponding to the low-temperature pyrolysis stage of the present invention. This stage is mainly dominated by depolymerization and decomposition reactions. The coal agglomerates into semicoke and undergoes a series of changes. The coal begins to soften at about 300 °C, and gas and tar are released. The tar yield is the largest around about 450 °C, and the gas evolution is the largest between about 450 - about 600 °C; in addition to pyrolysis product water, carbon monoxide, and carbon dioxide, the components of the gas are mainly gaseous hydrocarbons, so the calorific value is relatively high; the solid product of this stage is low-temperature pyrolysis semicoke; one of the main purposes of the present invention is to controllably achieve an optimized low-temperature pyrolysis operation stage and prevent high-temperature gas in the stripping section from entering the low-temperature pyrolysis section and burning off the formed tar;

[0198] ③ Pyrolysis and polycondensation stage (about 700 to about 1000 °C): This is the stage where low-temperature pyrolysis semicoke turns into distillation semicoke or even coke, corresponding to the distillation stage of the present invention, mainly involving pyrolysis and polycondensation reactions. The amount of tar precipitated is extremely small, and the volatile matter is mainly gas. After 700 °C, the main component of the gas is hydrogen. In this stage, the aromatic nucleus significantly increases, becomes more regular in arrangement, the structure becomes denser, and the colloid undergoes polycondensation and solidification reactions to form semicoke. From low-temperature pyrolysis semicoke to distillation semicoke, on the one hand, a large amount of gas is precipitated and the volatile matter content decreases; on the other hand, the volume of the semicoke itself shrinks, the true density increases, and the strength increases. A main objective of the present invention is to controllably achieve an optimized distillation pyrolysis operation stage, with less tar production (as it is mostly coal tar) and more gas production (of high value) during the process of increasing the strength of the semicoke and reducing the volatile matter of the semicoke.

[0199] The field of the present invention belongs to the coal pyrolysis process, generally to the medium and low-temperature coal pyrolysis process, and particularly to the medium and low-temperature coal pyrolysis process of high-volatile low-rank coal. The difference from other coal pyrolysis processes is that it has a low-temperature pyrolysis section and a distillation pyrolysis section with less tar production and more gas production.

[0200] The pyrolysis furnace and its system of the present invention are generally suitable for processing low-rank coals such as long-flame coal, non-caking coal, weakly caking coal, or lignite, and are particularly suitable for processing high-volatile low-rank coal, with good economy. It can optimize the operation of the low-temperature pyrolysis section, increase the tar yield, optimize the operation of the distillation section, reduce the volatile matter of the semicoke, increase the strength of the semicoke, and can also adapt to the combustion-supporting gas conditions of oxygen-enriched or pure oxygen to produce gas with a low nitrogen concentration, featuring a simple system, flexible operation, and high thermal efficiency.

[0201] The objective of the present invention is that "the first combustion-supporting gas in the main flue must enter synchronously with the first fuel gas in the expected volume ratio, and at the same time, the temperature-regulating gas in the expected volume ratio enters the furnace chamber of the low-temperature pyrolysis section". The specific solution is: a combined centrifugal compressor is set up, with a prime mover to drive the centrifugal compressor for 3 paths of gas to start, operate, and stop simultaneously.

[0202] For the combined centrifugal compressor of the present invention, the prime mover can be any suitable prime mover, which can be an electric motor or a steam turbine.

[0203] For the combined centrifugal compressor of the present invention, when using a transmission, the connection method between the output shaft and the input shaft can be any suitable method, such as direct connection or connection with a coupling.

[0204] The prime mover of the combined centrifugal compressor of the present invention can adopt a double-output shaft type or a single-output shaft type.

[0205] When the combined centrifugal compressor of the present invention adopts a double-output shaft type prime mover, the power transmission mechanism can be any effective power transmission mechanism, and at least the following several schemes are available for selection:

[0206] ① Use a prime mover with a double output shaft. The first output shaft of the prime mover is connected to the input shaft of the first transmission. One side of the output shaft of the first transmission drives the first fuel gas centrifugal compressor, and the other side of the output shaft of the first transmission drives the temperature regulating gas centrifugal compressor. The second output shaft of the prime mover is connected to the impeller rotor shaft of the first auxiliary combustion gas centrifugal compressor. For this type, reference can be made to Chinese Patent ZL201480069099.9 multi-stage electric centrifugal compressor (the prime mover is a double output shaft motor), and Chinese Patent ZL201210361133.2 (the prime mover can be a double output shaft steam turbine).

[0207] For this configuration method of the first transmission, generally, since the conveying media of the first fuel gas centrifugal compressor and the temperature regulating gas centrifugal compressor are both the same circulating coal gas (with the same molecular weight, temperature, and pressure), and the pressure differences of the first fuel gas centrifugal compressor and the temperature regulating gas centrifugal compressor are almost equal (and both are very small), the axial fluid thrust acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers is in opposite directions and almost equal in magnitude, that is, most of the axial forces cancel each other out, so the dynamic balance performance of the first transmission is good.

[0208] ② Use a prime mover with a double output shaft. The first output shaft of the prime mover is connected to the input shaft of the first transmission. One side of the output shaft of the first transmission drives the first fuel gas centrifugal compressor, and the other side of the output shaft of the transmission drives the temperature regulating gas centrifugal compressor.

[0209] The second output shaft of the prime mover is connected to the input shaft of the second transmission. One side of the output shaft of the second transmission drives the first auxiliary combustion gas centrifugal compressor A, and the other side of the output shaft of the second transmission drives the first auxiliary combustion gas centrifugal compressor B. For this type, reference can be made to Chinese Patent ZL201480030156.2.

[0210] The first auxiliary combustion gas is divided into two paths with the same flow rate and enters the first auxiliary combustion gas centrifugal compressor A and the first auxiliary combustion gas centrifugal compressor B respectively.

[0211] For this configuration method of the second transmission, the operating parameters of the first auxiliary combustion gas centrifugal compressor A and the first auxiliary combustion gas centrifugal compressor B are exactly the same. Therefore, the axial fluid thrust acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers is in opposite directions and equal in magnitude, that is, the axial forces completely cancel each other out, so the dynamic balance performance of the second transmission is good.

[0212] ③ Use a prime mover with a double output shaft. The first output shaft of the prime mover is connected to the input shaft of the first transmission. One side of the output shaft of the first transmission drives the first fuel gas centrifugal compressor A, and the other side of the output shaft of the transmission drives the first fuel gas centrifugal compressor B.

[0213] The second output shaft of the prime mover is connected to the input shaft of the second transmission. One side of the output shaft of the second transmission drives the first auxiliary gas centrifugal compressor, and the other side of the output shaft of the second transmission drives the temperature-regulating gas centrifugal compressor; for this type, reference can be made to Chinese Patent ZL201480030156.2;

[0214] In this configuration of the first transmission, the operating parameters of the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B are exactly the same. Therefore, the axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are opposite in direction and equal in magnitude, that is, the axial forces cancel each other out. In this way, the dynamic balance performance of the first transmission is good;

[0215] In this configuration of the second transmission, for the first auxiliary gas centrifugal compressor and the temperature-regulating gas centrifugal compressor, since the gas molecular weights differ greatly (the ratio of the molecular weight of the first auxiliary gas to the molecular weight of the first fuel gas is about 1.25 - 1.70), when the pressure differences are similar or the pressure difference of the auxiliary gas centrifugal compressor is smaller, the impeller diameter of the first auxiliary gas centrifugal compressor is smaller and the impeller area is smaller. The axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are opposite in direction and not equal in magnitude. That is, after the axial forces cancel each other out, the direction of the remaining axial force is the same as the direction of the fluid load received by the impeller of the temperature-regulating gas centrifugal compressor. In this way, it is required that the direction of the axial gear load received by the output shaft of the second transmission is opposite to the direction of the fluid load received by the impeller of the temperature-regulating gas centrifugal compressor to cancel part of the axial load and reduce the total axial load value, thereby improving the dynamic balance performance of the second transmission;

[0216] In order to reduce the unbalanced fluid load on the above-mentioned output shaft (reduce the total fluid load) and improve the overall efficiency of the combined centrifugal compressor, the present invention proposes a scheme of setting an additional extended impeller area on the impeller of the first auxiliary gas centrifugal compressor, and by increasing the area and gas pressure on the back of the impeller disc of the first auxiliary gas centrifugal compressor, the total fluid load on the integrated output shaft is reduced to zero as much as possible.

[0217] When the combined centrifugal compressor of the present invention adopts a prime mover with a single output shaft, the power transmission mechanism of the combined centrifugal compressor of the present invention can be any effective power transmission mechanism. Reference can be made to the multi-stage centrifugal compressor of Chinese Patent ZL201410351897.2. There are at least the following several schemes for selection:

[0218] ① The prime mover is provided with a single output shaft to drive the first transmission;

[0219] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0220] The main gear is provided on the input shaft of the above-mentioned first transmission;

[0221] The first pinion gear, which meshes with the above-mentioned main gear;

[0222] The second pinion gear, which meshes with the above-mentioned main gear;

[0223] The first pinion gear output shaft, which is used to arrange the above-mentioned first pinion gear and form the left side and the right side of the first pinion gear output shaft;

[0224] The second pinion gear output shaft, which is used to arrange the above-mentioned second pinion gear;

[0225] On one side of the first pinion gear output shaft, a single-stage first fuel gas centrifugal compressor is arranged, and on the other side of the first pinion gear output shaft, a single-stage temperature-regulating gas centrifugal compressor is arranged;

[0226] On one side of the second pinion gear output shaft, a single-stage first combustion-supporting gas centrifugal compressor is arranged.

[0227] For this configuration of the first pinion gear output shaft, generally, since the conveying media of the first fuel gas centrifugal compressor and the temperature-regulating gas centrifugal compressor are both the same circulating coal gas (with the same molecular weight, the same temperature, and the same pressure), and the pressure differences of the first fuel gas centrifugal compressor and the temperature-regulating gas centrifugal compressor are almost equal (and both are very small), therefore, the axial fluid thrust acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers is in the opposite direction and almost equal in magnitude, that is, most of the axial forces cancel each other out, so the dynamic balance performance of the first prime mover is good;

[0228] ② The prime mover is provided with a single output shaft to drive the first prime mover;

[0229] The input shaft of the first prime mover is connected to the output shaft of the prime mover;

[0230] The main gear is arranged on the input shaft of the above-mentioned first prime mover;

[0231] The first pinion gear, which meshes with the above-mentioned main gear;

[0232] The second pinion gear, which meshes with the above-mentioned main gear;

[0233] The first pinion gear output shaft, which is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0234] The second pinion gear output shaft, which is used to arrange the above-mentioned second pinion gear and form one side and the other side of the second pinion gear output shaft;

[0235] On one side of the first pinion gear output shaft, a single-stage first fuel gas centrifugal compressor is arranged, and on the other side of the first pinion gear output shaft, a single-stage temperature-regulating gas centrifugal compressor is arranged;

[0236] On one side of the output shaft of the second sprocket wheel, a single-stage first combustion-supporting gas centrifugal compressor A is arranged, and on the other side of the output shaft of the second sprocket wheel, a single-stage first combustion-supporting gas centrifugal compressor B is arranged;

[0237] The first combustion-supporting gas is divided into two paths with the same flow rate and enters the first combustion-supporting gas centrifugal compressor A and the first combustion-supporting gas centrifugal compressor B respectively.

[0238] With this configuration of the output shaft of the second sprocket wheel, the operating parameters of the first combustion-supporting gas centrifugal compressor A and the first combustion-supporting gas centrifugal compressor B are exactly the same. Therefore, the axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are opposite in direction and equal in magnitude, that is, the axial forces cancel each other out, and in this way, the dynamic balance performance of the second transmission is good;

[0239] ③ The prime mover is provided with a single output shaft to drive the first transmission;

[0240] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0241] The main gear is arranged on the input shaft of the above-mentioned first transmission;

[0242] The first sprocket wheel meshes with the above-mentioned main gear;

[0243] The second sprocket wheel meshes with the above-mentioned main gear;

[0244] The output shaft of the first sprocket wheel is used to arrange the above-mentioned first sprocket wheel and form one side and the other side of the output shaft of the first sprocket wheel;

[0245] The output shaft of the second sprocket wheel is used to arrange the above-mentioned second sprocket wheel and form one side and the other side of the output shaft of the second sprocket wheel;

[0246] On one side of the output shaft of the first sprocket wheel, a single-stage first fuel gas centrifugal compressor A is arranged, and on the other side of the output shaft of the first sprocket wheel, a single-stage first fuel gas centrifugal compressor B is arranged;

[0247] The first fuel gas is divided into two paths with the same flow rate and enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B respectively;

[0248] On one side of the output shaft of the second sprocket wheel, a single-stage first combustion-supporting gas centrifugal compressor is arranged, and on the other side of the output shaft of the second sprocket wheel, a single-stage temperature-regulating gas centrifugal compressor is arranged.

[0249] With this configuration of the output of the first sprocket wheel, the operating parameters of the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B are exactly the same. Therefore, the axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are opposite in direction and equal in magnitude, that is, the axial forces cancel each other out, and in this way, the dynamic balance performance of the first transmission is good;

[0250] In this configuration of the output shaft of the second sprocket wheel, for the first auxiliary gas centrifugal compressor and the temperature regulating gas centrifugal compressor, since there is a large difference in the molecular weights of the gases (the ratio of the molecular weight of the first auxiliary gas to the molecular weight of the temperature regulating gas is about 1.25 - 1.70), when the pressure differences are similar or the pressure difference of the auxiliary gas centrifugal compressor is smaller, the impeller diameter of the first auxiliary gas centrifugal compressor is smaller and the impeller area is smaller. The axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are in opposite directions and not equal in magnitude, that is, the direction of the remaining axial force after the axial forces cancel each other out is the same as the direction of the fluid load on the impeller of the temperature regulating gas centrifugal compressor. This requires that the direction of the axial gear load received by the output shaft of the second transmission is opposite to the direction of the fluid load on the impeller of the temperature regulating gas centrifugal compressor, so as to offset part of the axial load, reduce the total axial load value, and improve the dynamic balance performance of the second transmission;

[0251] In order to reduce the unbalanced fluid load (total fluid load) on the output shaft of the second sprocket wheel described above and improve the overall efficiency of the combined centrifugal compressor, the present invention proposes a scheme of setting an additional extended impeller area on the impeller of the first auxiliary gas centrifugal compressor, and by increasing the area and gas pressure on the back of the impeller disc of the first auxiliary gas centrifugal compressor, the total fluid load on the integrated output shaft is reduced to zero as much as possible.

[0252] ④ The prime mover is provided with a single output shaft to drive the first transmission;

[0253] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0254] The main gear is provided on the input shaft of the first transmission described above;

[0255] The first sprocket wheel meshes with the main gear described above;

[0256] The second sprocket wheel meshes with the main gear described above;

[0257] The output shaft of the first sprocket wheel is used to set the first sprocket wheel and form one side and the other side of the output shaft of the first sprocket wheel;

[0258] The output shaft of the second sprocket wheel is used to set the second sprocket wheel and form one side and the other side of the output shaft of the second sprocket wheel;

[0259] A single-stage temperature regulating gas centrifugal compressor A is arranged on one side of the output shaft of the first sprocket wheel, and a single-stage temperature regulating gas centrifugal compressor B is arranged on the other side of the output shaft of the first sprocket wheel;

[0260] The temperature regulating gas is divided into two paths with the same flow rate and enters the temperature regulating gas centrifugal compressor A and the temperature regulating gas centrifugal compressor B respectively;

[0261] On one side of the output shaft of the second sprocket wheel, a single-stage first auxiliary gas centrifugal compressor is arranged, and on the other side of the output shaft of the second sprocket wheel, a single-stage first fuel gas centrifugal compressor is arranged.

[0262] In this configuration of the output of the first sprocket wheel, the operating parameters of the temperature regulating gas centrifugal compressor A and the temperature regulating gas centrifugal compressor B are exactly the same. Therefore, the axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are opposite in direction and equal in magnitude, that is, the axial forces cancel each other out. In this way, the dynamic balance performance of the first prime mover is good.

[0263] In this configuration of the output shaft of the second sprocket wheel, for the first auxiliary gas centrifugal compressor and the first fuel gas centrifugal compressor, since the gas molecular weights differ greatly (the ratio of the molecular weight of the first auxiliary gas to the molecular weight of the first fuel gas is about 1.25 - 1.70), in the case of similar pressure differences or a smaller pressure difference for the auxiliary gas centrifugal compressor, the impeller diameter of the first auxiliary gas centrifugal compressor is smaller and the impeller area is smaller. The axial fluid thrusts acting on the impeller shaft generated by the pressure differences before and after the two centrifuge impellers are opposite in direction and not equal in magnitude. That is, the remaining axial force after the axial forces cancel each other out has the same direction as the fluid load on the impeller of the temperature regulating gas centrifugal compressor. In this way, it is required that the direction of the axial gear load received by the output shaft of the second prime mover is opposite to the direction of the fluid load on the impeller of the temperature regulating gas centrifugal compressor to offset part of the axial load and reduce the total value of the axial load, thereby improving the dynamic balance performance of the second prime mover.

[0264] In order to reduce the unbalanced fluid load (total fluid load) on the output shaft of the above-mentioned second sprocket wheel and improve the overall efficiency of the combined centrifugal compressor, the present invention proposes a scheme of setting an additional extended impeller area for the impeller of the first auxiliary gas centrifugal compressor, and by increasing the area and gas pressure on the back of the impeller disc of the first auxiliary gas centrifugal compressor, the total fluid load on the integrated output shaft is reduced to zero as much as possible.

[0265] Figure 1 A sectional view showing the local structure of the first auxiliary gas centrifugal compressor and the motor of a two-stage electric centrifugal compressor is used to illustrate the structure and function of setting an additional extended impeller area for the first auxiliary gas centrifugal compressor. The structures and functions of other parts can be replaced in various ways. Or rather, Figure 1 The structure and function of setting an additional extended impeller area for the first auxiliary gas centrifugal compressor shown can be applied to the first auxiliary gas centrifugal compressor of any suitable combined centrifugal compressor of the present invention.

[0266] As Figure 1 shown, the two-stage electric centrifugal compressor has a rotating shaft 703 that is rotatably supported. A single-stage impeller first auxiliary gas centrifugal compressor 720 is installed on the left end side of the rotating shaft 703, and a first fuel gas centrifugal compressor is provided on the right side ( Figure 1(not shown in the figure).

[0267] As Figure 1 shown, the first combustion-supporting gas centrifugal compressor 720 has a first impeller 721 installed on the left side of the rotating shaft 703 and a first centrifugal compressor housing 726 surrounding the first impeller 721. The first centrifugal compressor housing 726 has a space portion 727 that rotatably accommodates the first impeller 721 therein. An inlet port 727a for sucking in intake air opens at the other end side of the space portion 727, and a flow path 727c that communicates with the inlet port 727a and bends in the circumferential direction of the first combustion-supporting gas centrifugal compressor 720 is formed in the radial direction of the space portion 727. An outlet port 727b communicating with the flow path 727c opens at one end portion in the width direction of the first centrifugal compressor housing 726, that is, Figure 1 the end portion on the paper surface side. The intake air flowing in from the inlet port 727a is compressed and heated by the first impeller 721, flows through the flow path 727c, and is discharged from the outlet port 727b.

[0268] As Figure 1 shown, an insertion port 728 that can insert the first impeller 721 and is circular when viewed from the side opens at one end side of the first centrifugal compressor housing 726. The insertion port 728 opens larger than the first impeller 721 to expose a part of the flow path 727c. A side surface 726a on the insertion port 728 side of the first centrifugal compressor housing 726 is formed in a planar shape and is formed in an annular shape when viewed from the side.

[0269] As Figure 1 shown, the first impeller 721 has a disk-shaped back panel 722, a frustum-shaped hub portion 723 that protrudes in a direction orthogonal to one side surface of the back panel 722 and is integrally provided with the back panel 722, and a plurality of blades 724 that are integrally provided from the outer peripheral surface of the hub portion 723 to the back panel 722. A through hole 723a is provided at the central portion of the hub portion 723; one end of the through hole 723a is inserted into the rotating shaft 703, and thus, the first impeller 721 rotates integrally with the rotating shaft 703.

[0270] Generally, simply from the process requirements, the intake air pressures and the main exhaust pressures of the first centrifugal compressor and the second centrifugal compressor are the same, but the molecular weight of the first combustion-supporting gas is greater than the molecular weight of the first fuel gas. Therefore, the diameter of the first impeller 721 is smaller than the diameter of the impeller of the first fuel gas centrifugal compressor.

[0271] On the left side of the rotating shaft 703 extending on both sides of the electric motor rotor, bearings 740L are provided, and the 740L can be a rolling bearing of the lubricating grease type. The bearing 740L is provided in a bearing housing 750.

[0272] The bearing housing 750 is annular, and an insertion hole 750a capable of inserting the rotating shaft 703 is provided at its central part. A bearing mounting hole 750b (not shown) larger in inner diameter than the insertion hole 750a is provided on the second centrifugal compressor side of the insertion hole 750a. A bearing 740L (not shown) is mounted in the bearing mounting hole 750b, and the rotating shaft 703 is inserted into the bearing 740L, and the rotating shaft 703 is rotatably supported via the bearing 740L.

[0273] At the end of the bearing housing 750 on the first combustion-supporting gas centrifugal compressor 720 side, there is a protruding step portion 751 that fits into the insertion port 728 of the first centrifugal compressor housing 726 and is annular when viewed from the side. And on the radially outer side of the protruding step portion 751, there is an annular surface portion 752 that faces and contacts the side surface 726a of the first centrifugal compressor housing 726. The bearing housing 750 is integrally fixed to the first centrifugal compressor housing 726 via bolts 753 inserted into the first centrifugal compressor housing 726.

[0274] On the right end side of the motor housing 745, there is a rotor space portion 745b (partially shown) that rotatably surrounds the electric motor rotor. On the outer periphery of the motor housing 745, there are a plurality of heat dissipation fins 746 extending radially outward, which can release the heat generated from the electric motor rotor 730 or the bearing 740L, etc. to the outside.

[0275] The electric motor rotor 730 is the rotor of the electric motor, and is driven by a motor coil (not shown) to make the rotating shaft 703 rotate at high speed.

[0276] As Figure 1 、 Figure 2 shown, the protruding step portion 751 and the first centrifugal compressor housing 726 form an additional extended impeller region flow passage 220, which houses the outer ring body 7221 of the circular plate-shaped back panel 722 of the first impeller 721 and a plurality of outer edge blades 221 arranged on the outer ring body 7221; on the back of the circular plate-shaped back panel 722 and the outer ring body 7221, there is a gas chamber on the back of the impeller, which generates an axial fluid load pointing to the suction port 727a on the circular plate-shaped back panel 722 and the outer ring body 7221.

[0277] As Figure 2 shown, the protruding step portion 751 and the first centrifugal compressor housing 726 form an additional extended impeller region flow passage 220, which houses the outer ring body 7221 of the circular plate-shaped back panel 722 of the first impeller 721 and a plurality of outer edge blades 221 arranged on the outer ring body 7221; the auxiliary exhaust port 225 is the exhaust port of the additional extended impeller region flow passage 220.

[0278] As Figure 2As shown, the gap between the circular plate-shaped back panel 722, the back surface of the extended circular ring body 7221 and the protruding step portion 751 is the impeller back air chamber, which generates an axial fluid load on the circular plate-shaped back panel 722 and the extended circular ring body 7221 pointing to the suction port 727a; due to the energy applied by the rotation of the outer edge blades 221, the gas pressure at the secondary exhaust port 225 is higher than that at the main exhaust port. In this way, compared with not using the extended circular ring body 7221 and the outer edge blades 221, the axial fluid load generated by the circular plate-shaped back panel 722 and the extended circular ring body 7221 pointing to the suction port 727a is greatly increased. In order to save energy, the width of the outer edge blades 221 is reduced as much as possible, that is, the exhaust volume of the secondary exhaust port 225 is reduced.

[0279] Since the initial pressure of the oxygen-rich first combustion-supporting gas is usually higher than that of the first fuel gas, thus, the control value of the pressure difference of the first combustion-supporting gas is usually lower than that of the first fuel gas to save power consumption. At this time, the diameter of the impeller of the first combustion-supporting gas centrifugal compressor will be much smaller than that of the impeller of the first fuel gas centrifugal compressor and is not suitable for use. Figure 1 The technical solution to reduce the axial fluid load is that the first fuel gas centrifugal compressor adopts two-stage or multi-stage compression, so that the diameter of the last-stage impeller of the first fuel gas centrifugal compressor is basically the same as that of the impeller of the first combustion-supporting gas centrifugal compressor.

[0280] Figure 3 It is a schematic diagram of the power transmission mechanism (governor) of a combined centrifugal compressor and the configuration mode of the centrifugal compressor of the present invention.

[0281] As Figure 3 shown in the combined centrifugal compressor unit, a single-output shaft prime mover is used, a transmission (governor) is used and two output shafts are provided, and one first fuel gas centrifugal compressor, one temperature-regulating gas centrifugal compressor, and two first combustion-supporting gas centrifugal compressors are installed. It is also a schematic structural diagram of the horizontal section of the power transmission mechanism. At the same time, Figure 3 It is used to illustrate the axial fluid load received by the output shaft and the gear load acting in the thrust direction due to the meshing of the main gear and the pinion.

[0282] Figure 3 The combined centrifugal compressor shown has: an engine (not shown); a transmission, that is, a speed increasing machine part 100, which transmits the rotational driving force of the engine; a first fuel gas centrifugal compressor C1, a temperature-regulating gas centrifugal compressor C2, and first combustion-supporting gas centrifugal compressors C3A and C3B.

[0283] As Figure 3As shown, on the rotating shaft (not shown) of the engine, the input shaft 4 of the speed governor section 100, which is usually a speed increaser, is connected via a coupling (not shown). A main gear 20, which is a large gear, is mounted on the input shaft 4. Two pinions 21 and 22 are meshed with the main gear 20. From the viewpoint of reducing vibration and noise, it is recommended that helical gears with a higher contact ratio than spur gears be used for the main gear 20 and the pinions 21 and 22.

[0284] As Figure 3 shown, the pinion 21 is integrally formed with the output shaft 5, and the input shaft 4 and the output shaft 5 are arranged in parallel. Alternatively, the pinion 21 can be made separate from the output shaft 5 and fixed to the output shaft 5. On the output shaft 5, substantially cylindrical thrust rings 66 and 67 are fixed by shrink fitting.

[0285] As Figure 3 shown, the pinion 22 is integrally formed with the output shaft 6, and the input shaft 4 and the output shaft 6 are arranged in parallel. Alternatively, the pinion 22 can be made separate from the output shaft 6 and fixed to the output shaft 6. On the output shaft 6, substantially cylindrical thrust rings 68 and 69 are fixed by shrink fitting.

[0286] As Figure 3 shown, the input shaft 4, the output shafts 5 and 6, the main gear 20, the pinions 21 and 22, and the thrust rings 66 to 69 are components of the speed governor section 100 and are housed in the housing 101. The housing 101 has a horizontal plane dividing structure and is divided into an upper housing and a lower housing by a plane substantially equal to the horizontal plane including the central axes of the input shaft 4 and the output shafts 5 and 6. The upper housing and the lower housing are joined together by bolts (not shown).

[0287] As Figure 3 shown, the input shaft 4 and the main gear 20 are rotatably supported by composite bearings 60 and 61 held by the housing 101. The composite bearings 60 and 61 are bearings that support radial (radial direction) loads (radial loads) and thrust direction (axial) loads (thrust loads).

[0288] As Figure 3 shown, the output shaft 5 provided with the pinion 21 is rotatably supported by radial bearings 62 and 63 (not shown) held by the housing 101; the output shaft 6 provided with the pinion 22 is rotatably supported by radial bearings 64 and 65 (not shown) held by the housing 101; the thrust loads acting on the output shaft 5 are borne and supported by the thrust rings 66 and 67, which are clamped with the main gear 20 with a gap 71 therebetween; the thrust loads acting on the output shaft 6 are borne and supported by the thrust rings 68 and 69, which are clamped with the main gear 20 with a gap 72 therebetween.

[0289] As Figure 3 shown, in order to lubricate the radial bearings (not shown) of the composite bearings 60, 61, output shafts 5, 6, thrust rings 66 - 69, main gear 20, and ratchets 21, 22, etc., lubricating oil is supplied from a lubricating oil system (not shown) and returned to a fuel tank (not shown) provided at the lower part of the engine.

[0290] As Figure 3 shown, the clearance 70 between the input shaft 4 and the main gear 20 and the sliding surfaces in the thrust direction of the composite bearings 60, 61 is reasonably set as required, for example, about 0.2 mm. During the stable operation of the combined centrifugal compressor, either the composite bearing 60 or the composite bearing 61 in contact with the sliding surface of the main gear 20, and the sliding surface of the other composite bearing maintains a clearance from the main gear 20. However, during the start-up and shutdown of the combined centrifugal compressor, when the combined centrifugal compressor operates beyond the operating limit range of the small flow rate region called surge, the composite bearing in contact and sliding with the main gear 20 varies according to the operating state at that time.

[0291] As Figure 3 shown, the output shaft 5 and the ratchet 21 are radially supported by radial bearings 62, 63 (not shown). On the other hand, the support in the thrust direction of the output shaft 5 and the ratchet 21 is provided by thrust rings 66, 67.

[0292] As Figure 3 shown, the output shaft 6 and the ratchet 22 are radially supported by radial bearings 64, 65 (not shown). On the other hand, the support in the thrust direction of the output shaft 6 and the ratchet 22 is provided by thrust rings 68, 69.

[0293] As Figure 3 shown, the thrust rings 66 and 67 have the following structure, that is, they are shrink-fitted on the output shaft 5 in such a way as to sandwich the main gear 20 with a clearance 71 therebetween, and contact the main gear 20 at the sliding surfaces located on the inner side in the axial direction. The surface-to-surface distance between the sliding surface of the thrust ring 66 and the sliding surface of the thrust ring 67 is larger than the surface-to-surface distance between the two sliding surfaces of the main gear 20 by about 0.2 mm. That is, the clearance 71 between the main gear 20 and the sliding surfaces in the thrust direction of the thrust rings 66, 67 is about 0.2 mm, for example. During the stable operation of the combined centrifugal compressor, either the thrust ring 66 or the thrust ring 67 contacts the sliding surface of the main gear 20, and the sliding surface of the other thrust ring maintains a clearance from the sliding surface of the main gear 20. In addition, the thrust rings 66, 67 maintain a clearance of about 2 - 3 mm from the housing 101 and do not come into contact.

[0294] As Figure 3As shown, thrust rings 68 and 69 are configured such that they are shrink-fitted onto output shaft 6 while sandwiching main gear 20 with a gap 72 therebetween, and their sliding surfaces located on the inner side in the axial direction come into contact with main gear 20. The surface-to-surface distance between the sliding surface of thrust ring 68 and the sliding surface of thrust ring 69 is larger than the surface-to-surface distance between the two sliding surfaces of main gear 20 by about 0.2 mm, for example. That is, the gap 72 between the sliding surfaces of main gear 20 and thrust rings 68 and 69 in the thrust direction is about 0.2 mm, for example. During the stable operation of the combined centrifugal compressor, either thrust ring 68 or thrust ring 69 comes into contact with the sliding surface of main gear 20, and the sliding surface of the other thrust ring maintains a gap with the sliding surface of main gear 20. In addition, thrust rings 68 and 69 maintain a gap of about 2 - 3 mm with housing 101 and do not come into contact.

[0295] As Figure 3 shown, the combined centrifugal compressor shown has: an input shaft 4 driven by an engine; a main gear 20 provided on input shaft 4; pinions 21 and 22 meshing with main gear 20; and an output shaft 5 on which pinion 21 is provided and an output shaft 6 on which pinion 22 is provided. At one end of output shaft 5, a centrifugal impeller 1001 of the first fuel gas centrifugal compressor C1 (the back surface 16 of this impeller and the impeller diameter D1) is provided, and at the other end of output shaft 5, a centrifugal impeller 2001 of the temperature control gas centrifugal compressor C2 (the back surface 17 of this impeller and the impeller diameter D2) is provided.

[0296] As Figure 3 shown, the impeller is subject to fluid thrust, the output shaft is subject to fluid thrust and gear load, and main gear 20 is subject to gear load and combined load.

[0297] As Figure 3 shown, at one end of output shaft 5, a centrifugal impeller 1001 of the first fuel gas centrifugal compressor C1 is arranged, and a protective housing 111 (not shown) covers the outside of centrifugal impeller 1001, and a housing 101 (not shown) covers the back surface 16 of centrifugal impeller 1001. In addition, between housing 101 and output shaft 5, a shaft seal device 15 (not shown) for preventing compressed fluid from leaking outside the first fuel gas centrifugal compressor C1 is provided. The temperature control gas centrifugal compressor C2 and the first auxiliary fuel gas centrifugal compressors C3A and C3B have a similar structure.

[0298] As Figure 3 shown, since the first fuel gas centrifugal compressor C1 and the temperature control gas centrifugal compressor C2 are centrifugal compressors with almost the same parameters such as gas molecular weight, inlet temperature, inlet pressure, and pressure difference, and their impeller diameters are basically the same, the axial net fluid loads Fi1 and Fi2 acting on output shaft 5 by these two impellers 1001 and 2001 are almost equal in magnitude and opposite in direction, so the axial net fluid load on output shaft 6 is very small or almost zero.

[0299] As Figure 3 shown, at one end of the output shaft 6, there is a centrifugal impeller 3001A of the first auxiliary combustion air centrifugal compressor C3A. Since the pressure difference of the first auxiliary combustion air centrifugal compressor C3A is very small, the diameter D3A of the centrifugal impeller 3001A is very small, and the back area of the impeller is very small. Therefore, the axial net fluid load Fi3A acting on the output shaft 6 by the centrifugal impeller 3001A is very small.

[0300] As Figure 3 shown, at the other end of the output shaft 6, there is a centrifugal impeller 3001B of the first auxiliary combustion air centrifugal compressor C3B with a diameter of D3B. Since the sizes and operating conditions of the centrifugal impeller 3001A and the centrifugal impeller 3001B are exactly the same, the axial net fluid loads Fi3A and Fi3B acting on the output shaft 6 by these two impellers 3001A and 3001B are equal in magnitude and opposite in direction. Therefore, the axial net fluid load on the output shaft 6 is almost zero.

[0301] As Figure 3 shown, when observing from above, the main gear 20 provided on the input shaft 4 and the ratchet wheel 21 provided on the output shaft 5 rotate meshingly. As shown by the arrow in the figure, the main gear 20 rotates clockwise when observed from the side opposite to the engine. The main gear 20 is a left-handed helical gear with teeth inclined to the upper left when the axis serving as the rotation center faces the up-down direction and is observed from the side, and the ratchet wheel 21 is a right-handed helical gear with teeth inclined to the upper right when the axis serving as the rotation center faces the up-down direction and is observed from the side.

[0302] As Figure 3 shown, the ratchet wheel 21 receives a gear load Fp1 in the thrust direction from the main gear 20 to the right. As a reaction, the main gear 20 receives a gear load (with a value equal to Fp1) in the thrust direction from the ratchet wheel 21 to the left.

[0303] As Figure 3 shown, the ratchet wheel 22 receives a gear load Fp2 in the thrust direction from the main gear 20 to the right. As a reaction, the main gear 20 receives a gear load (with a value equal to Fp2) in the thrust direction from the ratchet wheel 22 to the left.

[0304] As Figure 3 shown, the gear loads Fp1 and Fp2 form a combined load F of the main gear 20.

[0305] Usually, since the initial pressure of the oxygen-rich first auxiliary combustion air is higher than the pressure of the first fuel gas, thus, the control value of the pressure difference of the first auxiliary combustion air centrifugal compressor is usually lower than that of the first fuel gas compressor to save power consumption. At this time, the diameters D3A and D3B of the impellers of the first auxiliary combustion air centrifugal compressor will be much smaller than the diameter D1 of the impeller of the first fuel gas centrifugal compressor. At this time, useFigure 3 The described technical solution can form a combined centrifugal compressor with good mechanical properties.

[0306] Figure 3 In it, the tooth spiral direction of the helical gear of the main gear 20 (not the rotation direction of the output shaft) can be left-handed or right-handed. Correspondingly, the tooth spiral direction of the helical gears of the pinwheels 21 and 22 (not the rotation direction of the output shaft) can be right-handed or left-handed.

[0307] Figure 3 The structure and assembly relationship shown in it can be adjusted according to specific circumstances.

[0308] The following description Figure 4 The structure of the pyrolysis furnace shown.

[0309] Such as Figure 4 For the pyrolysis furnace system shown, only the structure of the part illustrating the features of the present invention is shown. The coal addition tank arranged in the upper part of the preheating section, the upper feed valve and the lower discharge valve of the coal addition tank, the coal addition hopper arranged on the upper part of the coal addition tank, the coke discharging tank arranged in the lower part of the coke quenching section and the upper feed valve and the lower discharge valve of the coke discharging tank, and the process medium pipeline connected to the pyrolysis furnace are not shown in the figure.

[0310] In Figure 4 The internal heating vertical furnace shown is composed of a porous carbonization chamber 1000. Gas distribution bricks 9010, 9013, and 9016 are arranged at different positions in the carbonization chamber 1000. The vertical furnace is built with refractory bricks 9050. A combustion gas mixer 9012M, a gas transmission pipe 9009M, and a heat absorption gas transmission pipe 9015M are arranged on the side of the furnace body. Thermocouples 9060 are arranged in an appropriate coal material layer or semi-coke material layer. Furnace protection iron parts 9080 are arranged around the furnace body.

[0311] The circulating cold coal gas is the purified coal gas after the cooling, separation, dehydration, deoiling, and other possible required treatment steps of the raw coal gas discharged from the pyrolysis furnace. Usually, it is pressurized by a fan to maintain the circulating flow of the coal gas.

[0312] The coke quenching water is fresh water or the deeply purified water of the sewage obtained from the cooling, separation, and dehydration processes of the raw coal gas, and its water quality meets the requirements of national standard specifications.

[0313] The following combines Figure 4 , and describes in detail Figure 4 The working process of the pyrolysis furnace system shown, and a brief description of the relevant external systems is given.

[0314] The following describes in detail Figure 4 The process and process objectives of each functional section of the pyrolysis furnace shown.

[0315] Figure 4The pyrolysis furnace shown adopts the operation mode of mixing fuel gas with combustion-supporting gas and then entering the mixing chamber, and then spraying it into the furnace chamber through a gas distribution brick. That is, the pyrolysis furnace is used as a flue gas generator, which saves the investment in a dedicated flue gas generator and reduces the heat dissipation loss of the furnace body. It is a basic measure to simplify the pyrolysis system.

[0316] Figure 4 In the pyrolysis furnace shown, the preheating section is at the top of the furnace chamber of the pyrolysis furnace. It preheats and dries the coal material at a moderate temperature rise rate, and at the same time recovers the heat energy of the upward hot coal gas discharged from the low-temperature pyrolysis section (usually at a temperature of 300-450°C) to reduce the energy consumption during the coal preheating process, reduce the temperature and volume flow rate of the coal gas discharged from the pyrolysis furnace, filter the dust in the coal gas, and adsorb the asphalt droplets in the coal gas; if the upward hot coal gas discharged from the low-temperature pyrolysis section is directly discharged from the pyrolysis furnace along with the raw coal gas, during the process of coal gas cooling, separation, and oil recovery, due to the excessive tar and asphalt in the coal gas, it cannot be effectively recovered, and it will increase the energy consumption during the cooling process, and will also exacerbate the thermal condensation of tar, and the large-volume coal gas will carry more dust and asphalt, resulting in channel blockage; 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 will quickly turn into steam and expand and burst the coal particles, generating a large amount of pulverized coal; therefore, the preheating section is a necessary and important heating process with an appropriate temperature rise rate, especially for coal materials with medium moisture content (such as coal with a water content of 10-28% by weight), of course, coal materials with too high moisture content (such as coal with a water content greater than 35% by weight) are more suitable for an independent drying process, and then the dried coal is introduced into the pyrolysis furnace of the present invention. The operating temperature of the preheating section also needs to be strictly and flexibly controlled. Therefore, it is necessary to arrange thermocouples at the bottom and top coal seams of the expected preheating section to monitor the temperature, and even multiple thermocouple measuring points need to be set at different height positions at the bottom of the expected preheating section; the flow rate and temperature of the temperature-regulating cooling gas in the low-temperature pyrolysis section can be adjusted in a timely manner according to the monitored temperature of the preheating section, and even the flow rate and temperature of the input gas in the stripping section can be adjusted, and even the flow rate of the input gas in the direct air-cooling section can be adjusted; of course, the volume of the preheating section must be large enough or the residence time of the coal material during the preheating process must be long enough to meet the operating time requirements of the preheating or drying process, and there should be a certain margin to adapt to the fluctuations of the operating conditions. The overall operating goal is to fully recover the heat energy of the upward hot coal gas discharged from the low-temperature pyrolysis section, heat the coal material, and reduce the water content of the coal material to below the expected value.

[0317] The operating temperature of the preheating section and the volume of the preheating section (coal preheating residence time) are determined by the production target, i.e., the moisture content by weight of the preheated coal discharged from the preheating section and the temperature of the coal after preheating. They are affected by the flow, moisture and temperature of the coal entering the furnace, as well as by multiple factors such as the temperature of the gas heat carrier and the flow of the gas heat carrier. The ideal moisture content by weight of the preheated coal discharged from the preheating section is usually less than 6.0%, generally less than 5.0%, and preferably less than 4.0%. The temperature of the coal after preheating is usually 180-370°C, generally 200-350°C, and preferably 200-320°C.

[0318] Figure 4 The pyrolysis furnace shown in the figure has a low-temperature pyrolysis section arranged below the preheating section, which is used to perform low-temperature pyrolysis on the preheated coal to reduce its volatile matter and maximize the tar yield. At the same time, it is necessary to prevent the high-temperature gas from the distillation section from invading the low-temperature pyrolysis section, causing actual medium-temperature pyrolysis and causing tar burnout. This requires strict and flexible control of the temperature of the low-temperature pyrolysis process. Therefore, the temperature-regulating cooling gas distribution element arranged at the bottom of the low-temperature pyrolysis section is required to have a certain flexible adjustment range. It is necessary to strictly monitor the upper and lower operating temperatures of the mixing area, and adjust the flow rate and temperature of the temperature-regulating cooling gas in time 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 operating time requirements of the heat transfer and pyrolysis process of the low-temperature pyrolysis section, and there should be a certain margin to adapt to fluctuations in operating conditions. The overall operating goal is to fully extract tar and ensure that the low-temperature semi-coke is burned through without being undercooked.

[0319] The operating temperature of the low-temperature pyrolysis section and the volume of the low-temperature pyrolysis section (residence time of the coal after preheating) are determined by the production target, i.e., the volatile matter weight content of the low-temperature pyrolysis semi-coke discharged from the low-temperature pyrolysis section, and are affected by the flow rate, moisture, volatile matter, temperature of the preheated coal, and the temperature of the gas heat carrier, the flow rate of the gas heat carrier, and other factors; the ideal volatile matter weight content of the low-temperature pyrolysis semi-coke is 8.50% to 12.50% or 6.50% to 8.50%. The temperature of the low-temperature semi-coke discharged from the low-temperature pyrolysis section is usually 430 to 680°C, generally 460 to 650°C, and preferably 500 to 650°C.

[0320] Figure 4The pyrolysis furnace shown has a rectifying section arranged below the low-temperature pyrolysis section, which is used to deeply pyrolyze the low-temperature semicoke to reduce its volatile content. At the same time, in order to prevent excessive tar and pitch from being generated in the rectifying section and to produce more gas, that is, it is necessary for the low-temperature semicoke to rapidly heat up in the upper bed layer of the rectifying section and enter a pyrolysis process at a higher temperature. Therefore, the gas temperature in the upper bed layer of the rectifying section is still very high, usually at least 150 °C higher than the temperature of the mixed gas at the bottom of the low-temperature pyrolysis section. In this way, it is necessary to strictly monitor the gas temperature in the upper bed layer of the rectifying section and timely adjust the flow rate and temperature of the rectifying hot flue gas according to the monitored temperature. Of course, the volume of the rectifying section (the residence time of the low-temperature pyrolyzed semicoke) must be large enough, or the residence time of the low-temperature semicoke must be long enough to meet the operating time requirements of the heat transfer and pyrolysis process in the rectifying section, and there should be a certain margin to adapt to the fluctuations of the operating conditions and ensure that the rectified semicoke is completely burned without being undercooked.

[0321] The operating temperature of the rectifying section and the volume of the rectifying section (the residence time of the low-temperature pyrolyzed semicoke) are determined by the production target, that is, the weight content of the volatile matter of the rectified semicoke discharged from the rectifying section, and are affected by the flow rate, volatile content, and temperature of the low-temperature pyrolyzed semicoke. At the same time, they are affected by various factors such as the temperature and flow rate of the gas heat carrier. The ideal weight content of the volatile matter of the rectified semicoke is 3.00% - 4.95% or lower than 3.00%. The temperature of the rectified semicoke discharged from the rectifying section is usually 700 - 1000 °C, generally 750 - 950 °C, and preferably 800 - 950 °C.

[0322] Figure 4 The pyrolysis furnace shown has a direct air-cooling section arranged below the rectifying section, which is used to recover the heat energy of the hot rectified semicoke discharged from the rectifying section. In this way, the operating value of the highest final temperature of the rectifying section can be flexibly increased as needed to ensure that the volatile content of the rectified semicoke is lower than the expected upper limit value. This operating mode can prevent a large amount of gas consumption caused by increasing the highest final temperature of the rectifying section. For the case where the gas comes from the separated gas of the raw gas of the pyrolysis furnace, this scheme can increase the yield of the exported effective gas. Of course, the volume of the direct air-cooling section must be large enough, or the residence time of the rectified semicoke must be long enough to meet the operating time requirements of the heat transfer during the cooling process of the rectified semicoke, and there should be a certain margin to adapt to the fluctuations of the operating conditions and ensure that the rectified semicoke is completely cooled.

[0323] The operating temperature of the direct air-cooling section and the volume of the direct air-cooling section are determined by the production target, that is, the temperature of the rectified semicoke discharged from the direct air-cooling section, and are affected by the flow rate and temperature of the rectified semicoke. At the same time, they are affected by various factors such as the temperature and flow rate of the gas heat carrier. The ideal temperature of the rectified semicoke discharged from the direct air-cooling section is usually 150 - 400 °C, generally 180 - 350 °C, and preferably 200 - 300 °C. Under economic conditions, the temperature of the coke discharged from the direct air-cooling section should be reduced as much as possible to reduce the water consumption in the coke quenching section.

[0324] Since the ideal temperature of the semi-coke after coke quenching is 70-90°C, at such a low temperature, if it is achieved by the method of circulating gas cooling, the volume of the coke quenching section will be too large, the height and weight of the pyrolysis furnace will increase excessively, the gas circulation pressure difference will increase greatly, the bottom pressure of the pyrolysis furnace will increase greatly, resulting in a decrease in safety, and overall leading to a large increase in investment and energy consumption, which is uneconomical. On the other hand, below the direct gas cooling section, an inert gas interlayer is required to prevent atmospheric air from entering the direct gas cooling section and to prevent the gas in the direct gas cooling section from leaking into the atmospheric air.

[0325] Figure 4 In the shown pyrolysis furnace, a coke quenching section using water is arranged below the direct gas cooling section to achieve complete coke quenching. Since the heat absorption process of water coke quenching mainly utilizes the latent heat of vaporization of water, the amount of water required is very small. Such a coke quenching section has a very small volume, which can reduce investment, lower the height of the coke quenching section, and reduce the weight of the coke quenching section. The steam generated by coke quenching enters the direct gas cooling section as a gas heat carrier; of course, the volume of the coke quenching section must be large enough or the coke quenching time must be long enough to meet the operation requirements of heat transfer and pyrolysis in the coke quenching section, and there should be a certain margin to adapt to the fluctuations of the operation conditions and ensure that the semi-coke is cooled through without being undercooked (i.e., cooling the core of the semi-coke to a certain limit temperature).

[0326] In particular, the present invention is suitable for the working conditions where the combustion-supporting gas is oxygen-rich gas or pure oxygen.

[0327] The total residence time of the coal material from entering the furnace chamber of the pyrolysis furnace to leaving the furnace chamber of the pyrolysis furnace to become the retorted semi-coke and the residence time of each stage vary according to the specific properties of the coal material, the requirements for the volatile matter content of the retorted semi-coke, and the expected yield of low-temperature dry distillation tar. Usually, the total residence time of the coal material passing through the furnace chamber of the pyrolysis furnace is 4-15 hours, generally 5-12 hours.

[0328] Usually, the retorted semi-coke discharged from the coke discharging box of the pyrolysis furnace is collected and transported to the semi-coke storage bin.

[0329] As required, in the preheating section of the pyrolysis furnace, hot flue gas drying of the coal entering the furnace of the pyrolysis furnace can be carried out. The working method is as follows, but this working method is not preferred:

[0330] Between the preheating section and the low-temperature pyrolysis section of the pyrolysis furnace, a vertical coal feeding pipe in the preheating section is arranged. The coal feeding pipe in the preheating section forms a pressure difference for the gas in the low-temperature pyrolysis section to prevent the gas in the low-temperature pyrolysis section from rising, 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;

[0331] In the preheating section of the pyrolysis furnace, a hot flue gas distribution pipe is arranged at the bottom. The hot flue gas rises and contacts the descending coal material in the preheating section of the pyrolysis furnace to transfer heat, causing the moisture in the coal material to evaporate and enter the ascending drying gas. The drying gas is discharged from the upper part of the preheating section of the pyrolysis furnace; the dried coal material enters the low-temperature pyrolysis section of the pyrolysis furnace through the coal discharging pipe in the preheating section;

[0332] 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;

[0333] The hot flue gas entering the bottom of the preheating section of the pyrolysis furnace can be the hot flue gas provided by an independent flue gas generator or the hot flue gas generated in the indirect cooling section of the stripping semi-coke of the pyrolysis furnace.

[0334] The following describes the characteristic part of the present invention.

[0335] The three-way intake air combined centrifugal compression and conveying method of the double pyrolysis section vertical coal pyrolysis furnace of the present invention is characterized in that:

[0336] ⑴ Double pyrolysis section vertical coal pyrolysis furnace

[0337] The coal pyrolysis furnace is an internal-heated moving bed vertical coal pyrolysis furnace with a sudden drop in the temperature of the rising gas in the double pyrolysis section. When the coal material enters the pyrolysis furnace and descends, it passes through at least the preheating section, the low-temperature pyrolysis section, and the stripping section, and gradually becomes preheated coal material, low-temperature pyrolysis semi-coke, and stripping semi-coke;

[0338] In the pyrolysis chamber of the pyrolysis furnace, the stripping section is located below the low-temperature pyrolysis section, and the space of the stripping section is connected to the space of the low-temperature pyrolysis section;

[0339] In the low-temperature pyrolysis section, the heat source of the low-temperature pyrolysis section is provided by the initial gas heat carrier rising in the low-temperature pyrolysis section; a temperature regulating gas distribution channel is arranged at the bottom of the low-temperature pyrolysis section, and the temperature regulating gas discharged from the temperature regulating gas distribution channel enters the furnace cavity; the temperature regulating gas entering the furnace cavity is mixed with the ascending stripping section output gas from the stripping section to become the initial gas heat carrier of the low-temperature pyrolysis section. The temperature of the initial gas heat carrier of the low-temperature pyrolysis section is at least 100 °C lower than the temperature of the stripping section output gas;

[0340] In the low-temperature pyrolysis section, the temperature regulating gas distribution channel is located in and / or on the side of the lower coke layer of the low-temperature pyrolysis section;

[0341] In the low-temperature pyrolysis section, the gas heat carrier of the low-temperature pyrolysis section rises, countercurrently contacts the descending preheated coal material from the preheating section, cools down, and mixes with the low-temperature pyrolysis net produced gas to become the output gas of the low-temperature pyrolysis section; the output gas of the low-temperature pyrolysis section enters the preheating section; the descending preheated coal material is gradually heated for low-temperature pyrolysis, reducing the volatile matter to become low-temperature semi-coke; the low-temperature semi-coke descends and is discharged from the low-temperature pyrolysis section into the stripping section;

[0342] In the stripping section, most to all of the heat source in the stripping section is provided by the hot gas carrier rising within the stripping section; a main flue is arranged at the bottom of the stripping section; the stripping heat supply gas discharged from the main flue ascends, countercurrently contacts and cools with the downward-flowing low-temperature pyrolysis semi-coke from the low-temperature pyrolysis section and mixes with the net produced gas from stripping to become the output gas of the stripping section; the output gas of the stripping section enters the low-temperature pyrolysis section; the downward-flowing low-temperature pyrolysis semi-coke is gradually heated for deep pyrolysis to reduce the volatile matter and become the stripping semi-coke; the stripping semi-coke is discharged from the stripping section.

[0343] The main flue of the stripping section is located within the lower coke layer and / or on the side of the lower coke layer of the stripping section.

[0344] The internally heated lump coal moving bed vertical pyrolysis furnace for coal consists of one or multiple carbonization chambers; on at least one side of each carbonization chamber, a temperature-regulating gas distribution airway and a main flue are provided.

[0345] Outlet openings are arranged on the temperature-regulating gas distribution airway, and outlet openings are arranged on the main flue.

[0346] A coal distribution plate is provided at the upper part of the pyrolysis chamber, and a riser is provided at the top of the pyrolysis chamber; the raw gas from the pyrolysis furnace is discharged through the riser.

[0347] ⑵ Three-way intake combined centrifugal compression and transportation

[0348] In the combined centrifugal compressor, a prime mover drives the first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature-regulating gas centrifugal compressor. The first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature-regulating gas centrifugal compressor are started, operated, and stopped simultaneously.

[0349] The prime mover of the combined centrifugal compressor transmits power to the first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature-regulating gas centrifugal compressor through a power transmission mechanism.

[0350] The first combustion-supporting gas is boosted by the first combustion-supporting gas centrifugal compressor of the combined centrifugal compressor to become the boosted first combustion-supporting gas; the first fuel gas is boosted by the first fuel gas centrifugal compressor of the combined centrifugal compressor to become the boosted first fuel gas.

[0351] The boosted first combustion-supporting gas and the boosted first fuel gas become the first mixed gas through the first mixer; the first mixed gas enters the main flue for combustion and / or enters the furnace of the coal pyrolysis furnace for combustion to release heat and form a hot gas carrier ascending to heat the downward-flowing coal material; the ratio of the volume of the first fuel gas entering the first mixer to the volume of the first fuel gas with a chemical combustion equivalent entering the first mixer is defined as the first fuel gas combustion supply ratio K1, and K1 ≥ 1.15.

[0352] The temperature-regulating gas is boosted by the temperature-regulating gas centrifugal compressor of the combined centrifugal compressor to become the boosted temperature-regulating gas.

[0353] After the temperature is raised, the temperature-adjusting gas enters the temperature-adjusting gas distribution airway, passes through the temperature-adjusting gas distribution airway and enters the furnace through the gas distribution port connecting the furnace, contacts the upward hot gas and the downward carbon material, and reduces the temperature of the upward gas;

[0354] The temperature-adjusting gas is the purified gas obtained from the raw gas of the pyrolysis furnace through a purification process including at least steps of cooling, deoiling, and dehydration;

[0355] The first fuel gas is the purified gas obtained from the raw gas of the pyrolysis furnace through a purification process including at least steps of cooling, deoiling, and dehydration.

[0356] For the method of the present invention, the first structural scheme of the combined centrifugal compressor is as follows:

[0357] The combined centrifugal compressor adopts a double-output shaft prime mover;

[0358] The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission for driving;

[0359] The main gear of the first transmission is arranged on the input shaft of the first transmission;

[0360] The first pinion gear meshes with the main gear of the above-mentioned first transmission;

[0361] The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0362] The first fuel gas centrifugal compressor is arranged on one side of the first pinion gear output shaft, and the temperature-adjusting gas centrifugal compressor is arranged on the other side of the first pinion gear output shaft;

[0363] The second output shaft of the double-output shaft prime mover is connected to the impeller rotating shaft of the first auxiliary combustion gas centrifugal compressor.

[0364] For the method of the present invention, the second structural scheme of the combined centrifugal compressor is as follows:

[0365] The combined centrifugal compressor adopts a double-output shaft prime mover;

[0366] The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission for driving;

[0367] The main gear of the first transmission is arranged on the input shaft of the first transmission;

[0368] The first pinion gear meshes with the main gear of the above-mentioned first transmission;

[0369] The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and form one side and the other side of the first pinion gear output shaft;

[0370] On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor is arranged, and on the other side of the output shaft of the first sprocket wheel, a temperature regulating gas centrifugal compressor is arranged;

[0371] The second output shaft of the double-output shaft prime mover is connected to the input shaft of the second transmission for driving;

[0372] The main gear of the second transmission is arranged on the input shaft of the second transmission;

[0373] The second sprocket wheel meshes with the main gear of the second transmission mentioned above;

[0374] The output shaft of the second sprocket wheel is used to arrange the second sprocket wheel mentioned above, and form one side and the other side of the output shaft of the second sprocket wheel;

[0375] On one side of the output shaft of the second sprocket wheel, a first auxiliary combustion gas centrifugal compressor A is arranged, and on the other side of the output shaft of the second sprocket wheel, a first auxiliary combustion gas centrifugal compressor B is arranged;

[0376] The first auxiliary combustion gas is divided into two paths with the same flow rate and enters the first auxiliary combustion gas centrifugal compressor A and the first auxiliary combustion gas centrifugal compressor B respectively.

[0377] The third structural scheme of the combined centrifugal compressor in the present invention is:

[0378] The combined centrifugal compressor adopts a double-output shaft prime mover;

[0379] The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission for driving;

[0380] The main gear of the first transmission is arranged on the input shaft of the first transmission;

[0381] The first sprocket wheel meshes with the main gear of the first transmission mentioned above;

[0382] The output shaft of the first sprocket wheel is used to arrange the first sprocket wheel mentioned above, and form one side and the other side of the output shaft of the first sprocket wheel;

[0383] On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor A is arranged, and on the other side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor B is arranged;

[0384] The first fuel gas is divided into two paths with the same flow rate and enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B respectively;

[0385] The second output shaft of the double-output shaft prime mover is connected to the input shaft of the second transmission for driving;

[0386] The main gear of the second transmission is arranged on the input shaft of the second transmission;

[0387] The second ratchet wheel meshes with the main gear of the above-mentioned second transmission mechanism;

[0388] The output shaft of the second ratchet wheel is used to install the above-mentioned second ratchet wheel, and form one side and the other side of the output shaft of the second ratchet wheel;

[0389] One side of the output shaft of the second ratchet wheel is provided with a first combustion-supporting gas centrifugal compressor, and the other side of the output shaft of the second ratchet wheel is provided with a temperature-regulating gas centrifugal compressor.

[0390] The fourth structural scheme of the combined centrifugal compressor in the method of the present invention is as follows:

[0391] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission mechanism;

[0392] The input shaft of the first transmission mechanism is connected to the output shaft of the prime mover;

[0393] The main gear is arranged on the input shaft of the above-mentioned first transmission mechanism;

[0394] The first ratchet wheel meshes with the above-mentioned main gear;

[0395] The second ratchet wheel meshes with the above-mentioned main gear;

[0396] The output shaft of the first ratchet wheel is used to install the above-mentioned first ratchet wheel, and form one side and the other side of the output shaft of the first ratchet wheel;

[0397] The output shaft of the second ratchet wheel is used to install the above-mentioned second ratchet wheel;

[0398] One side of the output shaft of the first ratchet wheel is provided with a first fuel gas centrifugal compressor, and the other side of the output shaft of the first ratchet wheel is provided with a temperature-regulating gas centrifugal compressor;

[0399] One side of the output shaft of the second ratchet wheel is provided with a first combustion-supporting gas centrifugal compressor.

[0400] The fifth structural scheme of the combined centrifugal compressor in the method of the present invention is as follows:

[0401] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission mechanism;

[0402] The input shaft of the first transmission mechanism is connected to the output shaft of the prime mover;

[0403] The main gear is arranged on the input shaft of the above-mentioned first transmission mechanism;

[0404] The first ratchet wheel meshes with the above-mentioned main gear;

[0405] The second ratchet wheel meshes with the above-mentioned main gear;

[0406] The first sprocket output shaft is used to set the above-mentioned first sprocket and form one side and the other side of the first sprocket output shaft;

[0407] The second sprocket output shaft is used to set the above-mentioned second sprocket and form one side and the other side of the second sprocket output shaft;

[0408] On one side of the first sprocket output shaft, a first fuel gas centrifugal compressor is arranged, and on the other side of the first sprocket output shaft, a temperature regulating gas centrifugal compressor is arranged;

[0409] On one side of the second sprocket output shaft, a first combustion-supporting gas centrifugal compressor A is arranged, and on the other side of the second sprocket output shaft, a first combustion-supporting gas centrifugal compressor B is arranged;

[0410] The first combustion-supporting gas is divided into two paths with the same flow rate and enters the first combustion-supporting gas centrifugal compressor A and the first combustion-supporting gas centrifugal compressor B respectively.

[0411] The sixth structural scheme of the combined centrifugal compressor in the method of the present invention is:

[0412] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission;

[0413] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0414] The main gear is arranged on the input shaft of the above-mentioned first transmission;

[0415] The first sprocket is engaged with the above-mentioned main gear;

[0416] The second sprocket is engaged with the above-mentioned main gear;

[0417] The first sprocket output shaft is used to set the above-mentioned first sprocket and form one side and the other side of the first sprocket output shaft;

[0418] The second sprocket output shaft is used to set the above-mentioned second sprocket and form one side and the other side of the second sprocket output shaft;

[0419] On one side of the first sprocket output shaft, a first fuel gas centrifugal compressor A is arranged, and on the other side of the first sprocket output shaft, a first fuel gas centrifugal compressor B is arranged;

[0420] The first fuel gas is divided into two paths with the same flow rate and enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B respectively;

[0421] On one side of the second sprocket output shaft, a first combustion-supporting gas centrifugal compressor is arranged, and on the other side of the second sprocket output shaft, a temperature regulating gas centrifugal compressor is arranged.

[0422] The seventh structural scheme of the combined centrifugal compressor in the method of the present invention is as follows:

[0423] The combined centrifugal compressor adopts a single-output shaft prime mover to drive the first transmission;

[0424] The input shaft of the first transmission is connected to the output shaft of the prime mover;

[0425] The main gear is arranged on the input shaft of the first transmission;

[0426] The first pinion is meshed with the main gear;

[0427] The second pinion is meshed with the main gear;

[0428] The output shaft of the first pinion is used to arrange the first pinion and form one side and the other side of the output shaft of the first pinion;

[0429] The output shaft of the second pinion is used to arrange the second pinion and form one side and the other side of the output shaft of the second pinion;

[0430] On one side of the output shaft of the first pinion, the temperature-regulating gas centrifugal compressor A is arranged, and on the other side of the output shaft of the first pinion, the temperature-regulating gas centrifugal compressor B is arranged;

[0431] The temperature-regulating gas is divided into two paths with the same flow rate and enters the temperature-regulating gas centrifugal compressor A and the temperature-regulating gas centrifugal compressor B respectively;

[0432] On one side of the output shaft of the second pinion, the first combustion-supporting gas centrifugal compressor is arranged, and on the other side of the output shaft of the second pinion, the first fuel gas centrifugal compressor is arranged.

[0433] In the method of the present invention, generally, the first combustion-supporting gas entering the combined centrifugal compressor comes from the first combustion-supporting gas buffer tank;

[0434] The operating pressure of the first combustion-supporting gas buffer tank is lower than the pressure at the outlet of the first mixer connected to the main flue.

[0435] In the method of the present invention, generally, on the pipeline of the boosted first combustion-supporting gas discharged by the combined centrifugal compressor, a first combustion-supporting gas emergency interlock cut-off valve is set. Once the combined centrifugal compressor loses power, the first combustion-supporting gas emergency interlock cut-off valve is interlocked and closed;

[0436] Generally, on the pipeline of the boosted first fuel gas discharged by the combined centrifugal compressor, a first fuel gas emergency interlock cut-off valve is set. Once the combined centrifugal compressor loses power, the first fuel gas emergency interlock cut-off valve is interlocked and closed;

[0437] Generally, an emergency interlock cut-off valve for temperature-regulating gas is installed on the pipeline of the temperature-regulating gas with increased pressure discharged from the combined centrifugal compressor. Once the combined centrifugal compressor loses power, the emergency interlock cut-off valve for temperature-regulating gas will be interlocked and closed.

[0438] In the method of the present invention, generally, the first combustion-supporting gas entering the combined centrifugal compressor comes from the first combustion-supporting gas buffer tank;

[0439] The operating pressure of the first combustion-supporting gas buffer tank is lower than the pressure at the outlet of the first mixer connected to the main flue;

[0440] On the pipeline where the first combustion-supporting gas discharged from the first combustion-supporting gas buffer tank goes to the combined centrifugal compressor, a first combustion-supporting gas buffer tank overpressure interlock cut-off valve is installed. Once the pressure of the first combustion-supporting gas buffer tank is higher than the pressure at the outlet of the first mixer, the first combustion-supporting gas buffer tank overpressure interlock cut-off valve will be interlocked and closed.

[0441] In the method of the present invention, generally, the first combustion-supporting gas is oxygen-rich gas with an oxygen volume concentration higher than 35% and a carbon dioxide volume concentration higher than 60%.

[0442] In the method of the present invention, generally, in the coal pyrolysis furnace, a cold gas distribution chamber for the semi-coke cooling section is arranged at a certain height interval below the main flue;

[0443] The cooling gas enters the cold gas distribution chamber of the semi-coke cooling section, enters the cavity of the semi-coke cooling section through the gas distribution openings of the gas distribution channels, and moves upward to contact the downward-flowing semi-coke in a countercurrent manner to cool the semi-coke.

[0444] In the method of the present invention, for the temperature-regulating gas centrifugal compressor, its intake air can include temperature-regulating gas and cold gas for the semi-coke cooling section;

[0445] The pressurized gas discharged from the temperature-regulating gas centrifugal compressor is at least divided into two paths, one path is used as temperature-regulating gas, and the other path is used as cold gas for the semi-coke cooling section.

[0446] In the method of the present invention, generally, the gas flow temperature at 300 mm above the gas outlet of the temperature-regulating gas distribution channel in the low-temperature pyrolysis section is used as the qualitative temperature of the initial gas heat carrier in the low-temperature pyrolysis section;

[0447] In the stripping section, the gas flow temperature at 300 mm below the gas outlet of the temperature-regulating gas distribution channel in the low-temperature pyrolysis section is used as the qualitative temperature of the output gas in the stripping section;

[0448] The temperature of the low-temperature pyrolysis semi-coke at 300 mm above the gas outlet of the temperature-regulating gas distribution channel in the low-temperature pyrolysis section is used as the qualitative temperature of the low-temperature pyrolysis section;

[0449] The temperature of the stripping semi-coke at 300 mm above the gas outlet of the main flue in the stripping section is used as the qualitative temperature of the stripping section;

[0450] The coal fed into the pyrolysis furnace is low-rank coal;

[0451] In the preheating section, the temperature of the preheated coal material discharged is 180 - 370 °C;

[0452] The qualitative temperature of the low-temperature pyrolysis section is 430 - 680 °C; the qualitative temperature of the initial gas heat carrier in the low-temperature pyrolysis section is at least 200 °C lower than the qualitative temperature of the gas output from the stripping section;

[0453] The qualitative temperature of the stripping section is 700 - 1000 °C, and it is 100 - 450 °C higher than the qualitative temperature of the low-temperature pyrolysis section;

[0454] Each coking chamber is wider at the top and narrower at the bottom, with a variable cross-section in the middle transverse section. The temperature-regulating gas distribution airway and the main flue are both arranged in the narrow cavity section below the transition section where the middle transverse section of the coking chamber becomes narrower;

[0455] The volatile content of the stripped semicoke is at least 2.0 wt% lower than that of the low-temperature pyrolysis semicoke;

[0456] The volatile content of the stripped semicoke is lower than 4.95 wt%.

[0457] In the method of the present invention, generally, in the coal pyrolysis furnace, a cooling section and / or a coke quenching section for semicoke is provided below the pyrolysis section.

[0458] In the method of the present invention, generally, an external heating system is provided in the coal pyrolysis furnace. The high-temperature gas flowing through the heat transfer channel of the external heating system does not enter the furnace chamber of the pyrolysis furnace, and the heat transfer channel of the external heating system indirectly transfers heat to the furnace chamber of the coal dry distillation area of the pyrolysis furnace through the heat transfer wall surface.

[0459] In the method of the present invention, generally, the first fuel gas supply combustion ratio K1 is 1.5 - 5.0.

[0460] In the method of the present invention, generally, each centrifugal compressor is a single-stage centrifugal compressor.

[0461] In the method of the present invention, the impeller of the first auxiliary air centrifugal compressor can adopt an impeller with an additional extended impeller area, and by increasing the area and gas pressure on the back of the impeller disc of the first auxiliary air centrifugal compressor, the overall fluid load on the integrated output shaft is reduced.

[0462] In the method of the present invention, generally, the prime mover is an electric motor or a turbine.

[0463] In the method of the present invention, generally, the connection mode between the output shaft of the prime mover and the rotating shaft of the centrifugal compressor impeller or the input shaft of the transmission is direct connection or connection through a coupling.

[0464] In the method of the present invention, generally, the main gear and the pinion are helical gears;

[0465] Set the helix direction of the helical gear such that the gear load acting axially on the pinion and the fluid load acting axially on the corresponding output shaft act in opposite directions.

Claims

1. Three-way intake combined centrifugal compression and transportation method for a double pyrolysis section vertical coal pyrolysis furnace Characterized in that: ⑴ Double pyrolysis section vertical coal pyrolysis furnace The coal pyrolysis furnace is an internal heat type moving bed vertical coal pyrolysis furnace with a sudden drop in the temperature of the rising gas in a double pyrolysis section. During the downward movement of the coal material entering the pyrolysis furnace, it passes through at least a preheating section, a low-temperature pyrolysis section, and a stripping section, gradually becoming preheated coal material, low-temperature pyrolysis semi-coke, and stripping semi-coke; In the pyrolysis chamber of the pyrolysis furnace, the stripping section is located below the low-temperature pyrolysis section, and the space of the stripping section is connected to the space of the low-temperature pyrolysis section; In the low-temperature pyrolysis section, the heat source of the low-temperature pyrolysis section is provided by the initial gas heat carrier of the low-temperature pyrolysis section rising in the low-temperature pyrolysis section; a temperature regulating gas distribution channel is arranged at the bottom of the low-temperature pyrolysis section, and the temperature regulating gas discharged from the temperature regulating gas distribution channel enters the furnace cavity; the temperature regulating gas entering the furnace cavity is mixed with the upward output gas of the stripping section from the stripping section to become the initial gas heat carrier of the low-temperature pyrolysis section, and the temperature of the initial gas heat carrier of the low-temperature pyrolysis section is at least 100°C lower than the temperature of the output gas of the stripping section; In the low-temperature pyrolysis section, the temperature regulating gas distribution channel is located in and / or on the side of the lower coke layer of the low-temperature pyrolysis section; In the low-temperature pyrolysis section, the gas heat carrier of the low-temperature pyrolysis section rises, countercurrently contacts the downward preheated coal material from the preheating section, cools down, and mixes with the low-temperature pyrolysis net produced gas to become the output gas of the low-temperature pyrolysis section; the output gas of the low-temperature pyrolysis section enters the preheating section; the downward preheated coal material is gradually heated for low-temperature pyrolysis, reducing the volatile matter to become low-temperature semi-coke; The low-temperature semi-coke discharges downward from the low-temperature pyrolysis section and enters the 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 main flue is arranged at the bottom of the stripping section; the stripping heating gas discharged from the main flue rises, countercurrently contacts the downward low-temperature pyrolysis semi-coke from the low-temperature pyrolysis section, cools down, and mixes with the stripping net produced gas to become the output gas of the stripping section; the output gas of the stripping section enters the low-temperature pyrolysis section; the downward low-temperature pyrolysis semi-coke is gradually heated for deep pyrolysis, reducing the volatile matter to become stripping semi-coke; the stripping semi-coke is discharged from the stripping section; The main flue of the stripping section is located in and / or on the side of the lower coke layer of the stripping section; The internal heat type lump coal moving bed vertical pyrolysis furnace is composed of one or multiple carbonization chambers; on at least one side of each carbonization chamber, a temperature regulating gas distribution channel and a main flue are provided; An air outlet is arranged on the temperature regulating gas distribution channel, and an air outlet is arranged on the main flue; A coal distribution plate is arranged at the upper part of the pyrolysis chamber, and a riser is arranged at the top of the pyrolysis chamber; the riser discharges the primary gas of the pyrolysis furnace; ⑵ Three-way intake combined centrifugal compression and transportation In the combined centrifugal compressor, a prime mover drives the first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature regulating gas centrifugal compressor. The first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature regulating gas centrifugal compressor start, operate, and stop simultaneously; The prime mover of the combined centrifugal compressor realizes power transmission to the first combustion-supporting gas centrifugal compressor, the first fuel gas centrifugal compressor, and the temperature regulating gas centrifugal compressor through a power transmission mechanism; The first auxiliary combustion gas is boosted in pressure by the first auxiliary combustion gas centrifugal compressor of the combined centrifugal compressor to become the first auxiliary combustion gas after pressure boost; the first fuel gas is boosted in pressure by the first fuel gas centrifugal compressor of the combined centrifugal compressor to become the first fuel gas after pressure boost; The first auxiliary combustion gas after pressure boost and the first fuel gas after pressure boost pass through the first mixer to become the first mixed combustion gas; the first mixed combustion gas enters the main flue for combustion and / or enters the furnace of the coal pyrolysis furnace for combustion to release heat, forming an upward gas heat carrier to heat the downward coal material for pyrolysis; the ratio of the volume of the first fuel gas entering the first mixer to the volume of the first fuel gas with a chemical combustion equivalent entering the first mixer is defined as the first fuel gas supply combustion ratio K1, and K1≥1.15; The temperature regulating gas is boosted in pressure by the temperature regulating gas centrifugal compressor of the combined centrifugal compressor to become the temperature regulating gas after pressure boost; The temperature regulating gas after pressure boost enters the temperature regulating gas air distribution duct, and enters the furnace through the air distribution port of the air distribution duct connecting the furnace, and contacts the upward hot gas and the downward carbon material to reduce the temperature of the upward gas; The temperature regulating gas is the purified coal gas obtained from the primary coal gas of the pyrolysis furnace through a purification process including at least steps of cooling, deoiling, and dehydration; The first fuel gas is the purified coal gas obtained from the primary coal gas of the pyrolysis furnace through a purification process including at least steps of cooling, deoiling, and dehydration.

2. The method according to claim 1, characterized in that: The combined centrifugal compressor adopts a double-output shaft prime mover; The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission for driving; The main gear of the first transmission is arranged on the input shaft of the first transmission; The first pinion gear meshes with the main gear of the above-mentioned first transmission; The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and forms one side of the first pinion gear output shaft and the other side of the first pinion gear output shaft; The first fuel gas centrifugal compressor is arranged on one side of the first pinion gear output shaft, and the temperature regulating gas centrifugal compressor is arranged on the other side of the first pinion gear output shaft; The second output shaft of the double-output shaft prime mover is connected to the impeller rotating shaft of the first auxiliary combustion gas centrifugal compressor.

3. The method according to claim 1, characterized in that: The combined centrifugal compressor adopts a double-output shaft prime mover; The first output shaft of the double-output shaft prime mover is connected to the input shaft of the first transmission for driving; The main gear of the first transmission is arranged on the input shaft of the first transmission; The first pinion gear meshes with the main gear of the above-mentioned first transmission; The first pinion gear output shaft is used to arrange the above-mentioned first pinion gear and forms one side of the first pinion gear output shaft and the other side of the first pinion gear output shaft; The first fuel gas centrifugal compressor is arranged on one side of the first pinion gear output shaft, and the temperature regulating gas centrifugal compressor is arranged on the other side of the first pinion gear output shaft; The second output shaft of the double-output shaft prime mover is connected to the input shaft of the second transmission for driving; The main gear of the second transmission is arranged on the input shaft of the second transmission; The second pinion gear meshes with the main gear of the above-mentioned second transmission; The second pinion gear output shaft is used to arrange the above-mentioned second pinion gear and forms one side of the second pinion gear output shaft and the other side of the second pinion gear output shaft; On one side of the output shaft of the second sprocket wheel, a first combustion-supporting gas centrifugal compressor A is arranged, and on the other side of the output shaft of the second sprocket wheel, a first combustion-supporting gas centrifugal compressor B is arranged; The first combustion-supporting gas is divided into two paths with the same flow rate and respectively enters the first combustion-supporting gas centrifugal compressor A and the first combustion-supporting gas centrifugal compressor B.

4. The method according to claim 1, characterized in that: The combined centrifugal compressor adopts a double-output-shaft prime mover; The first output shaft of the double-output-shaft prime mover is connected to the input shaft of the first transmission for driving; The main gear of the first transmission is arranged on the input shaft of the first transmission; The first sprocket wheel is meshed with the main gear of the above-mentioned first transmission; The output shaft of the first sprocket wheel is used to arrange the above-mentioned first sprocket wheel and form one side and the other side of the output shaft of the first sprocket wheel; On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor A is arranged, and on the other side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor B is arranged; The first fuel gas is divided into two paths with the same flow rate and respectively enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B; The second output shaft of the double-output-shaft prime mover is connected to the input shaft of the second transmission for driving; The main gear of the second transmission is arranged on the input shaft of the second transmission; The second sprocket wheel is meshed with the main gear of the above-mentioned second transmission; The output shaft of the second sprocket wheel is used to arrange the above-mentioned second sprocket wheel and form one side and the other side of the output shaft of the second sprocket wheel; On one side of the output shaft of the second sprocket wheel, a first combustion-supporting gas centrifugal compressor is arranged, and on the other side of the output shaft of the second sprocket wheel, a temperature-regulating gas centrifugal compressor is arranged.

5. The method according to claim 1, characterized in that: The combined centrifugal compressor adopts a single-output-shaft prime mover to drive the first transmission; The input shaft of the first transmission is connected to the output shaft of the prime mover; The main gear is arranged on the input shaft of the above-mentioned first transmission; The first sprocket wheel is meshed with the above-mentioned main gear; The second sprocket wheel is meshed with the above-mentioned main gear; The output shaft of the first sprocket wheel is used to arrange the above-mentioned first sprocket wheel and form one side and the other side of the output shaft of the first sprocket wheel; The output shaft of the second sprocket wheel is used to arrange the above-mentioned second sprocket wheel; On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor is arranged, and on the other side of the output shaft of the first sprocket wheel, a temperature-regulating gas centrifugal compressor is arranged; On one side of the output shaft of the second sprocket wheel, a first combustion-supporting gas centrifugal compressor is arranged.

6. The method according to claim 1, characterized in that: The combined centrifugal compressor adopts a single-output-shaft prime mover to drive the first transmission; The input shaft of the first transmission is connected to the output shaft of the prime mover; The main gear is arranged on the input shaft of the above-mentioned first transmission; The first sprocket wheel is meshed with the above-mentioned main gear; The second sprocket wheel is meshed with the above-mentioned main gear; The output shaft of the first sprocket wheel is used to arrange the above-mentioned first sprocket wheel and form one side and the other side of the output shaft of the first sprocket wheel; The output shaft of the second sprocket wheel is used to arrange the above-mentioned second sprocket wheel and form one side and the other side of the output shaft of the second sprocket wheel; On one side of the output shaft of the first sprocket wheel, a first fuel gas centrifugal compressor is arranged, and on the other side of the output shaft of the first sprocket wheel, a temperature-regulating gas centrifugal compressor is arranged; On one side of the output shaft of the second sprocket, the first auxiliary combustion air centrifugal compressor A is arranged, and on the other side of the output shaft of the second sprocket, the first auxiliary combustion air centrifugal compressor B is arranged; The first auxiliary combustion air is divided into two paths with the same flow rate and enters the first auxiliary combustion air centrifugal compressor A and the first auxiliary combustion air centrifugal compressor B respectively.

7. According to the method described in claim 1, it is characterized in that: The combined centrifugal compressor uses a single-output shaft prime mover to drive the first transmission; The input shaft of the first transmission is connected to the output shaft of the prime mover; The main gear is arranged on the input shaft of the above-mentioned first transmission; The first sprocket is meshed with the above-mentioned main gear; The second sprocket is meshed with the above-mentioned main gear; The output shaft of the first sprocket is used to arrange the above-mentioned first sprocket and form one side and the other side of the output shaft of the first sprocket; The output shaft of the second sprocket is used to arrange the above-mentioned second sprocket and form one side and the other side of the output shaft of the second sprocket; On one side of the output shaft of the first sprocket, the first fuel gas centrifugal compressor A is arranged, and on the other side of the output shaft of the first sprocket, the first fuel gas centrifugal compressor B is arranged; The first fuel gas is divided into two paths with the same flow rate and enters the first fuel gas centrifugal compressor A and the first fuel gas centrifugal compressor B respectively; On one side of the output shaft of the second sprocket, the first auxiliary combustion air centrifugal compressor is arranged, and on the other side of the output shaft of the second sprocket, the temperature regulating gas centrifugal compressor is arranged.

8. According to the method described in claim 1, it is characterized in that: The combined centrifugal compressor uses a single-output shaft prime mover to drive the first transmission; The input shaft of the first transmission is connected to the output shaft of the prime mover; The main gear is arranged on the input shaft of the above-mentioned first transmission; The first sprocket is meshed with the above-mentioned main gear; The second sprocket is meshed with the above-mentioned main gear; The output shaft of the first sprocket is used to arrange the above-mentioned first sprocket and form one side and the other side of the output shaft of the first sprocket; The output shaft of the second sprocket is used to arrange the above-mentioned second sprocket and form one side and the other side of the output shaft of the second sprocket; On one side of the output shaft of the first sprocket, the temperature regulating gas centrifugal compressor A is arranged, and on the other side of the output shaft of the first sprocket, the temperature regulating gas centrifugal compressor B is arranged; The temperature regulating gas is divided into two paths with the same flow rate and enters the temperature regulating gas centrifugal compressor A and the temperature regulating gas centrifugal compressor B respectively; On one side of the output shaft of the second sprocket, the first auxiliary combustion air centrifugal compressor is arranged, and on the other side of the output shaft of the second sprocket, the first fuel gas centrifugal compressor is arranged.

9. According to the method described in claim 1, it is characterized in that: The first auxiliary combustion air entering the combined centrifugal compressor comes from the first auxiliary combustion air buffer tank; The operating pressure of the first auxiliary combustion air buffer tank is lower than the pressure at the outlet of the first mixer connected to the main flue.

10. According to the method described in claim 9, it is characterized in that: On the pipeline of the first auxiliary combustion air with increased pressure discharged by the combined centrifugal compressor, a first auxiliary combustion air emergency interlock cut-off valve is set. Once the combined centrifugal compressor loses power, the first auxiliary combustion air emergency interlock cut-off valve is interlocked and closed; On the pipeline of the first fuel gas after pressure boosting discharged from the combined centrifugal compressor, a first fuel gas emergency interlock cut-off valve is set. Once the combined centrifugal compressor loses power, the first fuel gas emergency interlock cut-off valve is interlocked and closed. On the pipeline of the temperature-regulating gas after pressure boosting discharged from the combined centrifugal compressor, a temperature-regulating gas emergency interlock cut-off valve is set. Once the combined centrifugal compressor loses power, the temperature-regulating gas emergency interlock cut-off valve is interlocked and closed.

11. According to the method described in claim 1, it is characterized in that: The first combustion-supporting gas entering the combined centrifugal compressor comes from the first combustion-supporting gas buffer tank; The operating pressure of the first combustion-supporting gas buffer tank is lower than the pressure at the outlet of the first mixer connected to the main flue; On the pipeline where the first combustion-supporting gas discharged from the first combustion-supporting gas buffer tank goes to the combined centrifugal compressor, a first combustion-supporting gas buffer tank overpressure interlock cut-off valve is set. Once the pressure of the first combustion-supporting gas buffer tank is higher than the pressure at the outlet of the first mixer, the first combustion-supporting gas buffer tank overpressure interlock cut-off valve is interlocked and closed.

12. According to the method described in claim 1, it is characterized in that: The first combustion-supporting gas is oxygen-rich gas with an oxygen volume concentration higher than 35% and a carbon dioxide volume concentration higher than 60%.

13. According to the method described in claim 1, it is characterized in that: In the coal pyrolysis furnace, below the main flue, a cold gas distribution chamber of the semicoke cooling section is set at an interval of a certain height; The cooling coal gas enters the cold gas distribution chamber of the semicoke cooling section, passes through the gas distribution openings of the gas distribution channels, enters the cavity of the semicoke cooling section and rises, and contacts the descending semicoke countercurrently to cool the semicoke.

14. According to the method described in claim 13, it is characterized in that: The temperature-regulating gas centrifugal compressor has an intake including temperature-regulating gas and cold gas for the semicoke cooling section; The gas after pressure boosting discharged from the temperature-regulating gas centrifugal compressor is at least divided into two paths, one path is used as temperature-regulating gas, and one path is used as cold gas for the semicoke cooling section.

15. According to the method described in claim 1, it is characterized in that: Taking the gas flow temperature at 300 mm above the gas outlet of the temperature-regulating gas distribution channel in the low-temperature pyrolysis section as the qualitative temperature of the initial gas heat carrier in the low-temperature pyrolysis section; In the stripping section, taking the gas flow temperature at 300 mm below the gas outlet of the temperature-regulating gas distribution channel in the low-temperature pyrolysis section as the qualitative temperature of the output gas in the stripping section; Taking the temperature of the low-temperature pyrolysis semicoke at 300 mm above the gas outlet of the temperature-regulating gas distribution channel in the low-temperature pyrolysis section as the qualitative temperature of the low-temperature pyrolysis section; Taking the temperature of the stripping semicoke at 300 mm above the gas outlet of the main flue in the stripping section as the qualitative temperature of the stripping section; The coal fed into the pyrolysis furnace is low-rank coal; In the preheating section, the temperature of the preheated coal material discharged is 180 - 370 °C; The qualitative temperature of the low-temperature pyrolysis section is 430 - 680 °C; the qualitative temperature of the initial gas heat carrier in the low-temperature pyrolysis section is at least 200 °C lower than the qualitative temperature of the output gas in the stripping section; The qualitative temperature of the stripping section is 700 - 1000 °C, and is 100 - 450 °C higher than the qualitative temperature of the low-temperature pyrolysis section; Each coking chamber is wider at the top and narrower at the bottom, and the middle cross-section is a variable cross-section. The temperature-regulating gas distribution channels and the main flues are both arranged in the narrow cavity section below the transition section where the middle cross-section of the coking chamber becomes narrower; The volatile content of the stripping semicoke is at least 2.0 wt% lower than that of the low-temperature pyrolysis semicoke; The volatile matter of the rectified semicoke is less than 4.95% by weight.

16. According to the method described in claim 1 or 15, wherein: In the coal pyrolysis furnace, a cooling section and / or a coke quenching section for semicoke are provided below the pyrolysis section.

17. According to the method described in claim 1, wherein: In the coal pyrolysis furnace, an external heating type heat supply system is provided at the same time. The high-temperature gas flowing through the heat transfer channel of the external heating type heat supply system does not enter the furnace chamber of the pyrolysis furnace, and the heat transfer channel of the external heating type heat supply system indirectly transfers heat to the furnace chamber of the coal dry distillation area of the pyrolysis furnace through the heat transfer wall surface.

18. According to the method described in claim 1, wherein: The first fuel gas supply combustion ratio K1, and K1 is 1.5 to 5.

0.

19. According to the method described in claim 1, wherein: Each centrifugal compressor is a single-stage centrifugal compressor.

20. According to the method described in claim 4 or 7, wherein: The impeller of the first auxiliary air centrifugal compressor adopts an impeller provided with an additional extended impeller area, and by increasing the area and gas pressure on the back of the impeller disc of the first auxiliary air centrifugal compressor, the overall fluid load on the integrated output shaft is reduced.

21. According to the method described in claim 1, wherein: The prime mover is an electric motor or a turbine.

22. According to the method described in claim 1, wherein: The connection mode between the output shaft of the prime mover and the rotation shaft of the centrifugal compressor impeller or the input shaft of the transmission is direct connection or connection through a coupling.

23. According to the method described in claim 2 or 3 or 4 or 5 or 6 or 7 or 8, wherein: The main gear and the pinion are helical gears; The helix direction of the above-mentioned helical gears is set in such a way that the gear load acting axially on the pinion and the fluid load acting along the same axis on the corresponding output shaft are in opposite directions.

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