CN112080322A

CN112080322A - Pulverized coal grading gasification system and method

Info

Publication number: CN112080322A
Application number: CN202010972368.XA
Authority: CN
Inventors: 马志超; 周三; 方科学; 刘明
Original assignee: ENN Science and Technology Development Co Ltd
Current assignee: ENN Science and Technology Development Co Ltd
Priority date: 2020-09-16
Filing date: 2020-09-16
Publication date: 2020-12-15

Abstract

The present disclosure relates to a pulverized coal grading gasification system and a method, wherein the system comprises a hydrogenation thermal conversion furnace, an oxygen-deficient gasification reaction furnace and a residual carbon combustion hydrogen heating furnace; the hydrogenation thermal conversion furnace is provided with a hydrogenation gasification reaction cavity, a pulverized coal inlet, a hydrogen inlet, a first oxygen inlet and a reactant outlet for discharging reactants generated in the reaction in the hydrogenation gasification reaction cavity; the lean oxygen gasification reaction furnace is provided with a lean oxygen gasification reaction cavity, a second oxygen inlet, a water vapor inlet, a feeding hole, an air outlet and a slag discharging hole; the feed inlet is communicated with the reactant outlet so that at least the solid semicoke in the reactant enters the oxygen-deficient gasification reaction cavity; the residual carbon combustion hydrogen heating furnace is provided with a residue combustion reaction cavity and a residue inlet communicated with the residue discharge port, so that residues generated in the reaction in the oxygen-deficient gasification reaction cavity sequentially enter the residue combustion reaction cavity through the residue discharge port and the residue inlet to be subjected to oxygen-enriched combustion, and the conversion rate of pulverized coal is improved.

Description

Pulverized coal grading gasification system and method

Technical Field

The disclosure relates to the technical field of coal quality-based utilization, in particular to a pulverized coal grading gasification system and a pulverized coal grading gasification method.

Background

Coal occupies a relatively important position in the energy structure of China, and the clean utilization of coal is more and more valued by people.

In the prior art, resources such as oil, gas and the like in raw coal are obtained by carrying out hydro-gasification on pulverized coal, but the reaction activity of semi-coke obtained by hydro-gasification is greatly reduced compared with that of the raw coal, so that the conversion rate of coal is low.

Therefore, how to improve the conversion rate of the pulverized coal becomes a problem to be solved urgently.

Disclosure of Invention

To address the above technical problems or at least partially solve the above technical problems, the present disclosure provides a pulverized coal staged gasification system and method.

In a first aspect, the present disclosure provides a pulverized coal staged gasification system, comprising a hydrogenation thermal conversion furnace, an oxygen-deficient gasification reaction furnace and a residual carbon combustion hydrogen heating furnace;

the hydrogenation thermal conversion furnace is provided with a hydrogenation gasification reaction cavity, a pulverized coal inlet for feeding pulverized coal into the hydrogenation gasification reaction cavity, a hydrogen inlet for feeding hydrogen into the hydrogenation gasification reaction cavity, a first oxygen inlet for feeding oxygen into the hydrogenation gasification reaction cavity and a reactant outlet for discharging reactants generated in the reaction in the hydrogenation gasification reaction cavity;

the lean oxygen gasification reaction furnace is provided with a lean oxygen gasification reaction cavity, a second oxygen inlet for oxygen to enter the lean oxygen gasification reaction cavity, a water vapor inlet for water vapor to enter the lean oxygen gasification reaction cavity, a feed inlet and a slag discharge port; the feed inlet is communicated with the reactant outlet so as to at least allow the solid semicoke in the reactants to enter the oxygen-deficient gasification reaction cavity;

the carbon residue combustion hydrogen heating furnace is provided with a residue combustion reaction cavity and a residue inlet, wherein the residue inlet is communicated with the residue discharge port, so that residues generated in the reaction in the oxygen-deficient gasification reaction cavity sequentially pass through the residue discharge port and the residue inlet enters the residue combustion reaction cavity to be subjected to oxygen-enriched combustion.

Optionally, the system further comprises a primary cyclone separator;

the primary cyclone separator has a first inlet, a first solid particle outlet, and a first gas outlet; the first inlet is communicated with the reactant outlet, and the first solid particle outlet is communicated with the feed inlet; the primary cyclone separator is used for at least separating the reactants, the separated gas is discharged from the first gas outlet, and the captured solid particles sequentially pass through the first solid particle outlet and the feed inlet and enter the oxygen-deficient gasification reaction cavity, wherein the solid particles comprise the solid semicoke.

Optionally, the device further comprises a feeding port communicated with the first inlet and used for feeding the granular materials, and the particle size and the density of the granular materials are both larger than those of the solid semicoke;

the particle materials are used for carrying the solid semicoke, so that the solid semicoke and the particle materials enter the primary cyclone separator together, are trapped by the primary cyclone separator and then enter the oxygen-deficient gasification reaction cavity through the first solid particle outlet and the feed inlet in sequence.

Optionally, the feeding port is disposed at the outlet section of the hydrogenation-heat converter and is communicated with the reactant outlet, so that the particulate material fed by the feeding port and the reactant enter the primary cyclone separator together from the first inlet.

Optionally, the outlet section of the hydrogenation heat conversion furnace is formed in a necking shape, and the outlet section is provided with a chilling gas inlet.

Optionally, the device also comprises a gas purification and separation device;

the gas purification and separation device is provided with a gas inlet and a hydrogen outlet, the gas inlet is respectively communicated with the first gas outlet and the gas outlet of the oxygen-deficient gasification reaction cavity, and the hydrogen outlet is communicated with the hydrogen inlet; the gas purification and separation device is used for purifying and separating gas entering from the gas inlet, and separated hydrogen is discharged from the hydrogen outlet and enters the hydro-gasification reaction cavity through the hydrogen inlet.

Optionally, the hydrogen outlet is communicated with the residue combustion reaction cavity, and the residue combustion reaction cavity is communicated with the hydrogen inlet, so that hydrogen discharged through the hydrogen outlet enters the residue combustion reaction cavity, is heated by heat in the residue combustion reaction cavity, and then enters the hydro-gasification reaction cavity through the hydrogen inlet.

Optionally, a secondary cyclone separator is further arranged between the primary cyclone separator and the gas purification and separation device;

the secondary cyclone has a second inlet, a second solid particle outlet, and a second gas outlet; the second inlet is respectively communicated with the first gas outlet and the gas outlet of the oxygen-deficient gasification reaction cavity, the second gas outlet is communicated with the gas inlet, and the second solid particle outlet is communicated with the oxygen-deficient gasification reaction cavity; the secondary cyclone separator is used for separating gas entering from the second inlet, the separated gas sequentially enters the gas purification and separation device through the second gas outlet and the gas inlet, and the captured solid particles enter the oxygen-deficient gasification reaction cavity through the second solid particle outlet.

Optionally, the gas purification and separation device includes a high-temperature gas filter, a hydrogen gas heat exchanger, and a gas separator;

the high temperature gas filter has the gas inlet, a third gas outlet, and a third solid particulate outlet; the third solid particle outlet is communicated with the residue combustion reaction cavity; the hydrogen heat exchanger is respectively communicated with the third gas outlet and the gas separator;

the high-temperature gas filter is used for filtering gas entering from the gas inlet, filtered solid particles enter the residue combustion reaction cavity through the third solid particle outlet, and the filtered gas enters the hydrogen heat exchanger through the third gas outlet; the hydrogen heat exchanger is used for cooling the gas discharged from the third gas outlet so as to separate an oil product, and the gas from which the oil product is separated enters the gas separator; the gas separator is used for separating the gas of the separated oil product to obtain methane and hydrogen, and the gas separator is provided with a hydrogen outlet for discharging the hydrogen.

Optionally, a hydrogen channel is arranged in the hydrogen heat exchanger;

the hydrogen outlet is communicated with the inlet of the hydrogen channel, the outlet of the hydrogen channel is communicated with the residue combustion reaction cavity, and the residue combustion reaction cavity is communicated with the hydrogen inlet, so that hydrogen discharged from the hydrogen outlet enters the residue combustion reaction cavity after being subjected to heat exchange by the hydrogen heat exchanger, and enters the hydro-gasification reaction cavity through the hydrogen inlet after being heated by heat in the residue combustion reaction cavity.

Optionally, a hydrogen compressor is further disposed between the gas separator and the hydrogen heat exchanger;

the hydrogen compressor is respectively communicated with the hydrogen outlet and the inlet of the hydrogen channel; the hydrogen compressor is used for compressing the hydrogen discharged from the hydrogen outlet and delivering the compressed hydrogen to the hydrogen channel.

In a second aspect, the present disclosure provides a method for staged gasification of pulverized coal using the staged pulverized coal gasification system as described above, the method comprising:

introducing pulverized coal, hydrogen and oxygen into a hydro-gasification reaction cavity of a hydro-thermal conversion furnace so as to enable the pulverized coal, the hydrogen and the oxygen to generate a gasification reaction in the hydro-gasification reaction cavity;

at least introducing solid semicoke in a reactant generated by the reaction in the hydrogenation gasification reaction cavity into an oxygen-deficient gasification reaction cavity of an oxygen-deficient gasification reaction furnace, and introducing oxygen and water vapor into the oxygen-deficient gasification reaction cavity so as to enable the oxygen, the water vapor and the solid semicoke to carry out an oxygen-deficient gasification reaction in the oxygen-deficient gasification reaction cavity;

and introducing the residue obtained by the reaction in the oxygen-deficient gasification reaction cavity into a residue combustion reaction cavity of a carbon residue combustion hydrogen heating furnace so as to enable the residue to be subjected to oxygen-enriched combustion in the residue combustion reaction cavity.

Optionally, the step of introducing at least the solid semicoke in the reactant generated by the reaction in the hydro-gasification reaction chamber into the oxygen-deficient gasification reaction chamber of the oxygen-deficient gasification reaction furnace includes:

introducing at least the reactant into a primary cyclone separator so that the primary cyclone separator at least separates the reactant;

and introducing solid particles captured by the primary cyclone separator into the oxygen-deficient gasification reaction cavity, wherein the solid particles comprise the solid semicoke.

Optionally, the step of introducing at least the reactant into the primary cyclone separator so that the primary cyclone separator separates the reactant includes:

and feeding a particulate material into a feeding port communicated with the first inlet of the primary cyclone separator, wherein the particle size and the density of the particulate material are both larger than those of the solid semicoke, so that the particulate material carries the solid semicoke in the reactant and enters the primary cyclone separator together with the reactant.

Compared with the prior art, the technical scheme provided by the embodiment of the disclosure has the following advantages:

the pulverized coal graded gasification system and the method provided by the disclosure are provided with a hydrogenation thermal conversion furnace, a lean oxygen gasification reaction furnace and a residual carbon combustion hydrogen heating furnace, firstly, pulverized coal, hydrogen and oxygen are respectively introduced into a reaction cavity of the hydrogenation thermal conversion furnace, so that the pulverized coal, the hydrogen and the oxygen are subjected to hydrogenation gasification reaction in the reaction cavity of the hydrogenation thermal conversion furnace, then at least solid semicoke in reactants generated by the hydrogenation gasification reaction is introduced into the reaction cavity of the lean oxygen gasification reaction furnace, and simultaneously, oxygen and water vapor are introduced into the reaction cavity of the lean oxygen gasification reaction furnace, so that the solid semicoke is subjected to the lean oxygen gasification reaction in the lean oxygen gasification reaction furnace, namely, the solid semicoke with the reaction activity lower than that of raw coal can be further reacted, and the conversion rate is improved; and then the residues generated in the lean oxygen gasification reaction are introduced into a residual carbon combustion hydrogen heating furnace, so that the residues which are difficult to rapidly react in a lean oxygen state are subjected to oxygen-enriched combustion in a reaction cavity of the residual carbon combustion hydrogen heating furnace, the residues are rapidly reacted, namely, through hydrogenation thermal conversion, lean oxygen conversion and oxygen-enriched combustion, each active component in the pulverized coal is efficiently converted, and the conversion efficiency of the pulverized coal is improved.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.

In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.

FIG. 1 is a block diagram of a pulverized coal staged gasification system according to an embodiment of the present disclosure;

FIG. 2 is a schematic structural diagram of a pulverized coal staged gasification system according to an embodiment of the disclosure;

fig. 3 is a schematic flow chart of a pulverized coal staged gasification method according to an embodiment of the present disclosure.

Wherein, 1, a hydrogenation heat converter; 11. a hydrogen inlet; 12. a pulverized coal inlet; 13. a reactant outlet; 14. a throwing port; 15. a quench gas inlet; 16. a first oxygen inlet; 10. an outlet section; 2. a lean oxygen gasification reaction furnace; 21. a second oxygen inlet; 22. a water vapor inlet; 23. a feed inlet; 24. a slag discharge port; 25. an air outlet; 3. a residual carbon combustion hydrogen heating furnace; 31. a residue inlet; 4. a primary cyclone separator; 41. a first inlet; 42. a first gas outlet; 43. a first solid particle outlet; 5. a secondary cyclone separator; 51. a second inlet; 52. a second gas outlet; 53. a second solid particle outlet; 6. a gas purification and separation device; 61. a high temperature gas filter; 611. a gas inlet; 612. a third gas outlet; 613. a third solid particle outlet; 62. a hydrogen gas heat exchanger; 621. an oil product outlet; 622. an inlet; 623. an outlet; 63. a gas separator; 631. a hydrogen outlet; 632. a methane outlet; 64. a hydrogen compressor; 71. a first slag discharge device; 72. a second slag discharge device; 8. a material returning device.

Detailed Description

In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.

In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced in other ways than those described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.

FIG. 1 is a block diagram of a pulverized coal staged gasification system according to an embodiment of the present disclosure; fig. 2 is a schematic structural diagram of a pulverized coal staged gasification system according to an embodiment of the present disclosure. Referring to fig. 1 and 2, an embodiment of the present disclosure provides a pulverized coal staged gasification system, including: a hydrogenation heat conversion furnace 1, an oxygen-deficient gasification reaction furnace 2 and a residual carbon combustion hydrogen heating furnace 3.

The hydrogenation thermal conversion furnace 1 is provided with a hydrogenation gasification reaction cavity, a pulverized coal inlet 12 for feeding pulverized coal into the hydrogenation gasification reaction cavity, a hydrogen inlet 11 for feeding hydrogen into the hydrogenation gasification reaction cavity, a first oxygen inlet 16 for feeding oxygen into the hydrogenation gasification reaction cavity, and a reactant outlet 13 for discharging reactants generated in the reaction in the hydrogenation gasification reaction cavity. It will be understood that the hydroconversion furnace 1 has an outlet section 10, the reactant outlet opening in this outlet section 10.

Wherein the input amount of the pulverized coal, the hydrogen and the oxygen can be set according to actual needs. The pulverized coal, the hydrogen and the oxygen enter the hydro-gasification reaction cavity to carry out hydro-gasification reaction, reactants generated by the reaction are discharged from a reactant outlet 13, and the generated reactants comprise oil, gas and small-particle solid carbocoal.

The oxygen-deficient gasification reaction furnace 2 is provided with an oxygen-deficient gasification reaction cavity, a second oxygen inlet 21 for oxygen gas to enter the oxygen-deficient gasification reaction cavity, a water vapor inlet 22 for water vapor to enter the oxygen-deficient gasification reaction cavity, a feed inlet 23 and a slag discharge outlet 24. Wherein, the feed inlet 23 is communicated with the reactant outlet 13, so that at least the solid semicoke in the reactant enters the oxygen-deficient gasification reaction cavity from the feed inlet 23. The water vapor, the oxygen and the solid semicoke are subjected to an oxygen-deficient gasification reaction in the oxygen-deficient gasification reaction cavity, that is, the solid semicoke with the reaction activity lower than that of the raw coal is further reacted through the oxygen-deficient gasification reaction to generate residual carbon ash (residue), and the residual carbon ash can be discharged through a residue discharge port 24.

The residual carbon combustion hydrogen heating furnace 3 is provided with a residue combustion reaction cavity and a residue inlet 31, wherein the residue inlet 31 is communicated with the slag discharging port 24, so that residues generated in the reaction in the oxygen-deficient gasification reaction cavity sequentially enter the residue combustion reaction cavity through the slag discharging port 24 and the residue inlet 31 to carry out oxygen-enriched combustion. Because the residue is difficult to react rapidly in an oxygen-deficient state, the residue is led into the residue combustion reaction cavity for oxygen-enriched combustion, so that the residue can react rapidly.

In concrete implementation, a first slag discharging device 71 can be arranged between the slag discharging port 24 of the lean oxygen gasification reaction furnace 2 and the residue inlet 31 of the residual carbon combustion hydrogen heating furnace 3, the pressure of the residue discharged from the slag discharging port 24 is reduced through the first slag discharging device 71, the residue is sent into the residue combustion reaction cavity from the residue inlet 31 to be subjected to oxygen-enriched combustion, and the heat generated by the oxygen-enriched combustion can be further utilized. Of course, in other implementations, the first slag discharge device 71 may not be provided, such as directly connecting the slag discharge port 24 with the slag inlet 31 through a pipeline.

According to the pulverized coal graded gasification system provided by the embodiment, by arranging the hydrogenation thermal conversion furnace 1, the lean oxygen gasification reaction furnace 2 and the residual carbon combustion hydrogen heating furnace 3, firstly, pulverized coal, hydrogen and oxygen are respectively introduced into the reaction cavity of the hydrogenation thermal conversion furnace 1, so that the pulverized coal, the hydrogen and the oxygen are subjected to hydrogenation gasification reaction in the hydrogenation thermal conversion furnace 1, then at least solid semicoke in reactants generated by the hydrogenation gasification reaction is introduced into the reaction cavity of the lean oxygen gasification reaction furnace 2, and simultaneously, oxygen and water vapor are introduced into the reaction cavity of the lean oxygen gasification reaction furnace 2, so that the solid semicoke is subjected to the lean oxygen gasification reaction in the lean oxygen gasification reaction furnace 2, namely, the solid semicoke with the reaction activity lower than that of raw coal can further react, and the conversion rate is improved; and then the residue produced in the lean oxygen gasification reaction is introduced into the residual carbon combustion hydrogen heating furnace 3, so that the residue which is difficult to rapidly react in a lean oxygen state is subjected to oxygen-enriched combustion in a reaction cavity of the residual carbon combustion hydrogen heating furnace 3, the residue is rapidly reacted, namely, each active component in the pulverized coal is efficiently converted through hydrogenation thermal conversion, lean oxygen conversion and oxygen-enriched combustion, and the conversion efficiency of the pulverized coal is improved.

In a specific implementation, the hydrogenation thermal reformer 1 may be a fluidized bed reactor. In the present embodiment, the outlet section 10 of the hydrogenation heat reformer 1 is formed in a neck shape, and it is understood that the inner diameter at the outlet section 10 is smaller than that of the other part of the reaction chamber. That is, by reducing the exit section internal diameter, the exit velocity of the reactants is increased.

Wherein, a chilling gas inlet 15 for chilling gas to enter can be arranged at the outlet section 10, chilling gas is introduced into the outlet section 10 through the chilling gas inlet 15, so that the temperature at the outlet of the hydrogenation thermal conversion furnace 1 can be controlled, and the hydrogenation gasification reaction can be stopped.

In some embodiments, the pulverized coal staged gasification system further comprises: a primary cyclone 4, the primary cyclone 4 having a first inlet 41, a first solid particles outlet 43 and a first gas outlet 42. The first inlet 41 is in communication with the reactant outlet 13 and the first solid particle outlet 43 is in communication with the feed inlet 23. The primary cyclone separator 4 is used for separating at least reactants, the separated gas is discharged from the first gas outlet 42, and the captured solid particles sequentially pass through the first solid particle outlet 43 and the feed inlet 23 and enter the oxygen-deficient gasification reaction cavity, wherein the solid particles comprise solid semicoke.

Because the particle size of the solid semicoke in the reactant generated by the hydro-gasification reaction is smaller, in order to enable the primary cyclone separator 4 to capture the solid semicoke more effectively, in some embodiments, the primary cyclone separator further comprises a feeding port 14 which is communicated with the first inlet 41 and is used for feeding the particulate material, and the particle size and the density of the particulate material are both larger than those of the solid semicoke. For example, the particulate material may be high density particles such as limestone, quartz sand, and the like. Illustratively, the particle size of the granular material is 0.1mm to 5mm, and the particle size of the solid semicoke is less than 100 μm.

The large-particle-size particle materials are used for carrying the solid semicoke, enter the primary cyclone separator 4 together with the solid semicoke, are collected by the primary cyclone separator 4, and then enter the oxygen-deficient gasification reaction cavity through the first solid particle outlet 43 and the feeding hole 23 in sequence. That is to say, the particle materials are used for reducing the separation difficulty of the solid semicoke and the gas, and the characteristic that large particle materials are easy to collect is fully utilized through a 'belt type' particle separation method of 'small belt size', so that the solid semicoke can be effectively collected by the primary cyclone separator 4, and then enters the oxygen-deficient gasification reaction cavity for further reaction and conversion as much as possible. That is to say, by virtue of the characteristics of large particles, such as large particle size and high density, the solid carbocoal with small particles can be carried into the cyclone dipleg of the primary cyclone separator 4, and the separation efficiency is improved.

When large granule material and the solid semicoke of tiny particle pass through one-level cyclone 4, the small granule solid semicoke is taken secretly to the large granule material and is caught, gets into the dipleg of one-level cyclone 4 to the large granule can be in the dipleg propose effective sealed, has overcome the solid semicoke of tiny particle and can't establish the sealed difficult problem of effective dipleg because of density is little, has guaranteed the required material of dipleg normal returning charge and has sealed.

During specific implementation, the lean oxygen gasification reaction furnace 2 can be selected from a circulating fluidized bed, the circulating fluidized bed gasifies solid semicoke entering the circulating fluidized bed, the reacted residues are mainly ash, and the volume of discharged materials is reduced by improving the density of the residues, so that the size of equipment and the discharge difficulty are reduced. The large-particle materials play a role in blocking the small-particle solid semicoke from being brought out along with the gas in the circulating fluidized bed, so that the fluidized state in the circulating fluidized bed is optimized, the retention time of the small-particle solid semicoke in the circulating fluidized bed is prolonged, and the conversion rate of the solid semicoke lean-oxygen gasification is improved.

In this embodiment, it is preferable that the input port 14 is disposed at the outlet section 10 of the hydrogenation-heat conversion furnace 1 and is communicated with the reactant outlet 13, so that the particulate material input from the input port 14 and the reactant enter the primary cyclone 4 together from the first inlet 41. Through putting into mouthful 14 setting in the export section 10 of hydrogenation heat converter 1 for the particulate material who is put into by putting into mouthful 14 can not only play the effect of carrying on smuggleing secretly to the solid semicoke in the reactant, can also play the effect to export section 10 cooling, thereby reducible sharp cold gas's use has saved the cost to a certain extent.

Of course, in other implementations, the dosing port 14 may also be provided at the first inlet 41 of the primary cyclone 4.

Further, in some embodiments, the pulverized coal staged gasification system further comprises a gas clean-up separation device 6. Wherein, the gas purification and separation device 6 is provided with a gas inlet 611 and a hydrogen outlet 631, the gas inlet 611 is respectively communicated with the first gas outlet 42 and the gas outlet 25 of the oxygen-deficient gasification reaction cavity, and the hydrogen outlet 631 is communicated with the hydrogen inlet 11. The gas purification and separation device 6 is used for purifying and separating the gas entering from the gas inlet 611, and the separated hydrogen is discharged from the hydrogen outlet and enters the hydro-gasification reaction chamber through the hydrogen inlet 11.

That is, by providing the gas purification and separation device 6, the gas discharged from the first gas outlet 42 of the primary cyclone 4 and the gas discharged from the gas outlet 25 of the oxygen-deficient gasification reaction chamber are purified and separated, so that the separated hydrogen gas enters the hydro-gasification reaction chamber of the hydrogenation-thermal conversion furnace 1 through the hydrogen gas inlet 11, thereby providing the reaction gas source for the hydrogenation-thermal conversion furnace 1. Therefore, the hydrogen separated by the gas purification and separation device 6 is directly used for providing hydrogen for the hydrogen gasification reaction cavity without additionally arranging a hydrogen supply source, so that the hydrogen can be effectively utilized.

Specifically, the hydrogen outlet 631 may be communicated with the residue combustion reaction chamber, and the residue combustion reaction chamber may be communicated with the hydrogen inlet 11, so that the hydrogen discharged through the hydrogen outlet 631 enters the residue combustion reaction chamber, is heated by the heat in the residue combustion reaction chamber, and then enters the hydro-gasification reaction chamber through the hydrogen inlet 11. It can be understood that the residue burns in residue combustion reaction intracavity and produces the heat, hydrogen that discharges from hydrogen export 631 enters into residue combustion reaction intracavity, and the heat in residue combustion reaction intracavity carries out the heat exchange with hydrogen, promptly, heats hydrogen, and the hydrogen after the heating is discharged from residue combustion reaction intracavity, enters into to the hydro-gasification reaction intracavity from hydrogen entry 11 to make the hydrogen that enters into to the hydro-gasification reaction intracavity have certain heat, has further guaranteed the effective reaction in the hydro-gasification reaction intracavity.

In the present embodiment, a secondary cyclone 5 is further provided between the primary cyclone 4 and the gas purification and separation apparatus 6. Wherein the secondary cyclone 5 has a second inlet 51, a second solid particle outlet 53 and a second gas outlet 52. The second inlet 51 is respectively communicated with the first gas outlet 42 and the gas outlet 25 of the oxygen-deficient gasification reaction cavity, the second gas outlet 52 is communicated with the gas inlet 611, and the second solid particle outlet 53 is communicated with the oxygen-deficient gasification reaction cavity. The secondary cyclone separator 5 is used for separating the gas entering from the second inlet 51, the separated gas enters the gas purification and separation device 6 through the second gas outlet 52 and the gas inlet 611 in sequence, and the trapped solid particles enter the oxygen-deficient gasification reaction cavity through the second solid particle outlet 53.

That is, the gas separated by the primary cyclone 4 and the gas discharged from the gas outlet 25 of the oxygen-deficient gasification reaction furnace 2 firstly enter the secondary cyclone 5 through the second inlet 51, the secondary cyclone 5 separates the gas entering the secondary cyclone, that is, the unreacted small-particle solid semi-coke and part of the entrained large-particle materials enter the secondary cyclone 5 for secondary trapping, and the trapped solid particles are sent to the oxygen-deficient gasification reaction chamber again. Specifically, a material returning device 8 can be arranged between the second solid particle outlet 53 and the oxygen-deficient gasification reaction cavity, and the collected particles are sent into the oxygen-deficient gasification reaction cavity again through the material returning device 8, so that the gasification efficiency is improved. The fine particles which are not collected by the secondary cyclone 5 enter the gas cleaning and separating device 6 through the second gas outlet 52.

Wherein, the gas purification and separation device 6 may specifically include: a high-temperature gas filter 61, a hydrogen gas heat exchanger 62, and a gas separator 63.

The high temperature gas filter 61 has a gas inlet 611, a third gas outlet 612, and a third solid particle outlet 613. It is understood that the gas inlet 611 of the high-temperature gas filter 61 is formed as the gas inlet 611 of the gas purification and separation apparatus 6. The third solid particle outlet 613 is in communication with the residue combustion reaction chamber. It will be appreciated that the gas inlet 611 of the high temperature gas filter 61 communicates with the first gas outlet 42 of the primary cyclone 4 and the gas outlet 25 of the oxygen-depleted gasification reaction chamber, respectively. Referring to fig. 2, in the present embodiment, the gas inlet 611 of the high temperature gas filter 61 is in particular in communication with the second gas outlet 52 of the secondary cyclone 5. It can be understood that, since the second inlet 51 of the secondary cyclone 5 is respectively communicated with the first gas outlet 42 of the primary cyclone 4 and the gas outlet 25 of the oxygen-deficient gasification reaction chamber, and the gas inlet 611 of the high-temperature gas filter 61 is communicated with the second gas outlet 52 of the secondary cyclone 5, that is, the gas inlet 611 of the high-temperature gas filter 61 is indirectly communicated with the first gas outlet 42 of the primary cyclone 4 and the gas outlet 25 of the oxygen-deficient gasification reaction chamber.

The high temperature gas filter 61 is used for filtering the gas entering from the gas inlet 611, the filtered solid particles enter the residue combustion reaction chamber through the third solid particle outlet 613, and the filtered gas enters the hydrogen heat exchanger 62 through the third gas outlet 612. It is understood that the high temperature gas filter 61 can perform fine dust removal on the entering gas, and the solid particles trapped by the high temperature gas filter 61 have too low reactivity to be suitable as an oxygen-deficient gasification raw material, and are sent to the carbon residue combustion hydrogen heating furnace 3 together with carbon residue ash.

Specifically, the second slag discharge device 72 may be provided between the third solid particle outlet 613 and the residual carbon combustion hydrogen heating furnace 3, and the second slag discharge device 72 may reduce the pressure of the residue discharged from the third solid particle outlet 613, and further send the residue from the residue inlet 31 into the residue combustion reaction chamber to perform oxygen-enriched combustion, thereby further reacting the residue and further improving the conversion rate. The heat generated by the oxygen-enriched combustion can be further utilized, for example, the hydrogen outlet is communicated with the residue combustion reaction cavity, the residue combustion reaction cavity is communicated with the hydrogen inlet 11, and the heat generated by the oxygen-enriched combustion can heat the hydrogen entering the residue combustion reaction cavity, so that the hydrogen enters the hydrogenation-heating converter 1 after the heat exchange of the residue combustion reaction cavity, and the reaction speed in the hydrogenation-heating converter 1 is improved. Of course, the slag discharging device may not be provided, for example, the third solid particle outlet 613 is directly connected to the residue inlet 31 through a pipe.

That is, the gas discharged through the first gas outlet 42 of the primary cyclone 4 and the gas outlet 25 of the oxygen-deficient gasification reaction chamber is separated by the secondary cyclone 5, and then the gas separated by the secondary cyclone 5 is filtered by the high temperature gas filter 61. Through multi-stage separation, each active component is further converted, and the gasification efficiency is improved.

Wherein the hydrogen heat exchanger 62 is in communication with the third gas outlet 612 and the gas separator 63, respectively. The hydrogen heat exchanger 62 is used for cooling the gas discharged from the third gas outlet 612 to separate oil products, and the gas from which the oil products are separated enters the gas separator 63. Specifically, the inlet of the hydrogen heat exchanger 62 communicates with the third gas outlet 612 of the high-temperature gas filter 61, the outlet of the hydrogen heat exchanger 62 communicates with the gas separator 63, and the hydrogen heat exchanger 62 has an oil outlet 621. The gas filtered by the high-temperature gas filter 61 enters the hydrogen heat exchanger 62, the gas is cooled, the oil is separated at the moment, the oil can be specifically aromatic oil, and the aromatic oil can be discharged from the oil outlet 621 and further collected. The gas from which the oil is separated flows to the outlet of the hydrogen heat exchanger 62, and enters the gas separator 63 from the outlet of the hydrogen heat exchanger 62.

The gas separator 63 is used for separating the gas from which the oil is separated to obtain methane and hydrogen. The gas separator 63 has a hydrogen outlet 631 and a methane outlet 632. The separated methane may be discharged from the methane outlet 632 and the separated hydrogen may be discharged from the hydrogen outlet 631.

In a feasible implementation manner, a hydrogen channel is arranged in the hydrogen heat exchanger 62, the hydrogen outlet 631 is communicated with the inlet 622 of the hydrogen channel, the outlet 623 of the hydrogen channel is communicated with the residue combustion reaction chamber, and the residue combustion reaction chamber is communicated with the hydrogen inlet 11, so that hydrogen discharged from the hydrogen outlet enters the residue combustion reaction chamber after being subjected to heat exchange by the hydrogen heat exchanger 62, is heated by heat in the residue combustion reaction chamber, and then enters the hydro-gasification reaction chamber through the hydrogen inlet 11. That is, the hydrogen separated by the gas separator 63 enters the hydrogen channel, because the gas separated by the high temperature gas filter 61 flows into the hydrogen heat exchanger 62, the gas separated by the high temperature gas filter 61 has a certain amount of heat, the heat exchanges heat with the hydrogen entering the hydrogen channel in the hydrogen heat exchanger 62, that is, the hydrogen entering the hydrogen channel is heated, the heated hydrogen enters the carbon residue combustion hydrogen heating furnace 3, the heat generated by the oxygen-enriched combustion in the residue combustion reaction chamber can further heat the hydrogen entering the hydrogen heat exchanger, the further heated hydrogen finally enters the hydrogenation heat conversion furnace 1 from the hydrogen inlet 11 to participate in the hydro-gasification reaction as a hydrogen source, so that the hydrogen can be effectively utilized, and no special hydrogen source is required to be additionally arranged to provide a hydrogen source for the hydrogenation heat conversion furnace 1, further saving resources.

In a specific implementation, a hydrogen compressor 64 may be disposed between the gas separator 63 and the hydrogen heat exchanger 62. The hydrogen compressor 64 communicates with the hydrogen outlet and the inlet of the hydrogen passage, respectively. The hydrogen compressor 64 is for compressing hydrogen discharged from the hydrogen outlet and delivering the compressed hydrogen to the hydrogen passage.

In another realizable manner, the hydrogen outlet may be directly communicated with the hydrogen inlet 11, so that the hydrogen discharged from the hydrogen outlet is directly fed into the hydro-thermal converter 1 as hydrogen required for the reaction.

The pulverized coal staged gasification system provided by the embodiments of the present disclosure is further described below by specific examples:

the normal temperature raw material pulverized coal (the average grain diameter is 30-60 μm), the high temperature hydrogen and oxygen are respectively added into the hydrogenation heat conversion furnace 1 through the pulverized coal inlet 12, the hydrogen inlet 11 and the first oxygen inlet 16, the hydrogenation reaction is carried out in the hydrogenation heat conversion furnace 1, the reaction temperature is 700-900 ℃, the reaction pressure is 5-7MPa, and the gaseous oil, gas and the small-grain solid carbocoal are generated. A chilling means is designed at the outlet section of the hydrogenation thermal conversion furnace 1, particle materials with large particle diameters (such as limestone, quartz sand and other high-density particles) are added from a feeding opening 14, large particle materials are used for carrying small particle solid semi-coke on one hand, and can play a role in chilling and cooling on the other hand, and the flexibility of temperature control of the outlet section 10 is improved by introducing chilling air. The outlet section 10 of the hydrogenation heat conversion furnace 1 is set to be in a necking shape, and the inner diameter of the section is reduced, so that the flow speed is increased, and large-particle materials can be guaranteed to be entrained with small-particle solid carbocoal to enter a rear system together.

The gas carrying solid particles firstly enters a primary cyclone separator 4, the solid particles are captured and sent to an oxygen-deficient gasification reaction furnace 2, the oxygen-deficient gasification reaction furnace 2 can adopt a high-rate circulating fluidized bed, large particle materials stay in the fluidized bed to ensure the stability of the reaction temperature of the bed layer and ensure the gasification efficiency, the operation of the fluidized bed selects the fluidizing gas velocity according to the fluidizing state of the added large particle materials, the small particle solid semicoke and the added oxygen and water vapor generate oxygen-deficient gasification in the process of passing through the bed layer, and the gasification temperature is 900-. Unreacted small-particle solid semi-coke and part of large-particle materials carried by the unreacted small-particle solid semi-coke enter the secondary cyclone separator 5 for secondary capture, and the captured particles are sent into the oxygen-deficient gasification reaction furnace 2 again through the material returning device 8 so as to improve the gasification efficiency. The fine particles which are not collected by the secondary cyclone separator 5 enter the high-temperature gas filter 61 to finish fine dust removal, the reactivity of the particles collected by the high-temperature gas filter 61 is too low to be suitable for being used as an oxygen-deficient gasification raw material, and the particles and the carbon residue ash are sent to the carbon residue combustion hydrogen heating furnace 3 together. The carbon residue ash after gasification in the oxygen-deficient gasification reaction furnace 2 is decompressed to low pressure by the first slag discharging device 71, and is sent to the carbon residue combustion hydrogen heating furnace 3, and the carbon residue is converted into heat energy for hydrogen for hydrogenation thermal conversion reaction through the oxygen-enriched combustion process.

The high-temperature gas dedusted by the high-temperature gas filter 61 enters a hydrogen heat exchanger 62, and on one hand, the hydrogen heat exchanger 62 reduces the temperature of the high-temperature gas to below 40 ℃, and the aromatic oil product is obtained by separation. The gas from which the oil is separated enters a gas separator 63 to obtain a methane product and hydrogen. Meanwhile, the separated hydrogen is pressurized by a hydrogen compressor 64 and then enters a hydrogen heat exchanger 62, and the other side of the hydrogen heat exchanger 62 heats the entering hydrogen to 200 ℃.

The reaction in the hydrogenation-heat converting furnace 1 generally requires hydrogen gas with a higher temperature (for example, about 1100 ℃) to participate in the reaction, and in this embodiment, the high-temperature hydrogen gas can be obtained by three steps, wherein the first step is realized by the hydrogen gas heat exchanger 62, the hydrogen gas heat exchanger 62 exchanges heat with the hydrogen gas separated by the gas separator 63, for example, the temperature of the hydrogen gas is increased to 200 ℃, the second step is completed by the carbon residue combustion hydrogen gas heating furnace 3, the heat exchange is performed with the hydrogen gas entering the carbon residue combustion hydrogen gas heating furnace 3 from the hydrogen gas heat exchanger 62, for example, the hydrogen gas is heated to 450-.

Referring to fig. 3, an embodiment of the present disclosure also provides a pulverized coal staged gasification method, which may be performed by part or all of the pulverized coal staged gasification system of the above embodiment, to improve the conversion rate of the pulverized coal.

With reference to fig. 1 to 3, the pulverized coal staged gasification method is described below by using a specific embodiment, and the method specifically includes:

s101, introducing pulverized coal, hydrogen and oxygen into a hydro-gasification reaction cavity of the hydro-thermal conversion furnace 1 so that the pulverized coal, the hydrogen and the oxygen are subjected to gasification reaction in the hydro-gasification reaction cavity.

S102, at least introducing solid semicoke in a reactant generated by reaction in the hydrogenation gasification reaction cavity into an oxygen-deficient gasification reaction cavity of an oxygen-deficient gasification reaction furnace, and introducing oxygen and water vapor into the oxygen-deficient gasification reaction cavity to enable the oxygen, the water vapor and the solid semicoke to carry out oxygen-deficient gasification reaction in the oxygen-deficient gasification reaction cavity;

s103, introducing the residue obtained by reaction in the oxygen-deficient gasification reaction cavity into a residue combustion reaction cavity of a carbon residue combustion hydrogen heating furnace so as to enable the residue to be subjected to oxygen-enriched combustion in the residue combustion reaction cavity.

The method for the graded gasification of the pulverized coal comprises the steps of firstly respectively introducing the pulverized coal, hydrogen and oxygen into a hydrogenation thermal conversion furnace 1 to enable the pulverized coal, the hydrogen and the oxygen to generate hydrogenation gasification reaction in the hydrogenation thermal conversion furnace 1, then at least introducing solid semicoke in reactants generated by the hydrogenation gasification reaction into a reaction cavity of an oxygen-deficient gasification reaction furnace 2, and simultaneously introducing oxygen and water vapor into the reaction cavity of the oxygen-deficient gasification reaction furnace 2 to enable the solid semicoke to generate the oxygen-deficient gasification reaction in the oxygen-deficient gasification reaction furnace 2, namely enabling the solid semicoke with reaction activity lower than that of raw coal to further react; and then the residue produced in the lean oxygen gasification reaction is introduced into the residual carbon combustion hydrogen heating furnace 3, so that the residue which is difficult to rapidly react in a lean oxygen state is subjected to oxygen-enriched combustion in a reaction cavity of the residual carbon combustion hydrogen heating furnace 3, the residue is rapidly reacted, namely, each active component in the pulverized coal is efficiently converted through hydrogenation thermal conversion, lean oxygen conversion and oxygen-enriched combustion, and the conversion efficiency of the pulverized coal is improved.

Further, the step S102 specifically includes:

at least the reactants are first passed into the primary cyclone 4 so that the primary cyclone 4 separates at least the reactants.

In this step, specifically, the particulate material may be put into the putting-in port 14 communicated with the first inlet 41 of the primary cyclone 4, so that the particulate material entrains the solid carbocoal in the reactant and enters the primary cyclone 4 together with the reactant, the primary cyclone 4 separates the gas entering the primary cyclone, and the separated gas is discharged through the first gas outlet 42 of the primary cyclone 4. Because the particle size and the density of the particle materials are both larger than those of the solid semicoke, the separation difficulty of the fixed semicoke and the gas is reduced.

And then introducing the solid particles collected by the primary cyclone separator 4 into an oxygen-deficient gasification reaction cavity, wherein the solid particles entering the oxygen-deficient gasification reaction cavity comprise solid semicoke and granular materials.

The specific technical features are the same as those of the above embodiments, and can bring about the same or similar technical effects, which are not described in detail herein. Reference may be made in particular to the description of the embodiments above.

It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.

The foregoing are merely exemplary embodiments of the present disclosure, which enable those skilled in the art to understand or practice the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A pulverized coal grading gasification system is characterized by comprising a hydrogenation thermal conversion furnace (1), an oxygen-deficient gasification reaction furnace (2) and a residual carbon combustion hydrogen heating furnace (3);

the hydrogenation thermal conversion furnace (1) is provided with a hydrogenation gasification reaction cavity, a pulverized coal inlet (12) for feeding pulverized coal into the hydrogenation gasification reaction cavity, a hydrogen inlet (11) for feeding hydrogen into the hydrogenation gasification reaction cavity, a first oxygen inlet (16) for feeding oxygen into the hydrogenation gasification reaction cavity and a reactant outlet (13) for discharging reactants generated in the reaction in the hydrogenation gasification reaction cavity;

the lean oxygen gasification reaction furnace (2) is provided with a lean oxygen gasification reaction cavity, a second oxygen inlet (21) for oxygen supply gas to enter the lean oxygen gasification reaction cavity, a water vapor inlet (22) for water vapor to enter the lean oxygen gasification reaction cavity, a feed inlet (23) and a slag discharge port (24); the feed inlet (23) is communicated with the reactant outlet (13) so as to at least allow the solid semicoke in the reactants to enter the oxygen-deficient gasification reaction cavity;

carbon residue burning hydrogen heating furnace (3) have residue burning reaction chamber and residue entry (31), residue entry (31) with row cinder notch (24) intercommunication, so that the residue that produces in the oxygen deficiency gasification reaction intracavity reaction passes through in proper order row cinder notch (24) with residue entry (31) enter into extremely carry out the oxygen boosting burning in the residue burning reaction chamber.

2. Pulverized coal staged gasification system according to claim 1, further comprising a primary cyclone (4);

the primary cyclone (4) has a first inlet (41), a first solid particle outlet (43) and a first gas outlet (42); the first inlet (41) is communicated with the reactant outlet (13), and the first solid particle outlet (43) is communicated with the feed inlet (23); the primary cyclone separator (4) is used for separating at least the reactants, the separated gas is discharged from the first gas outlet (42), and the captured solid particles sequentially pass through the first solid particle outlet (43) and the feed inlet (23) and enter the oxygen-deficient gasification reaction cavity, wherein the solid particles comprise the solid semicoke.

3. The pulverized coal staged gasification system according to claim 2, further comprising a charging opening (14) communicated with the first inlet (41) for charging a particulate material, wherein the particle size and the density of the particulate material are both larger than those of the solid semicoke;

the particle materials are used for carrying the solid semicoke, enter the primary cyclone separator (4) together with the solid semicoke, are collected by the primary cyclone separator (4), and then sequentially enter the oxygen-deficient gasification reaction cavity through the first solid particle outlet (43) and the feed inlet (23).

4. Pulverized coal staged gasification system according to claim 3, wherein the input opening (14) is arranged in the outlet section (10) of the hydroconversion furnace (1) and communicates with the reactant outlet (13) so that the particulate material input by the input opening (14) enters the primary cyclone (4) together with the reactant from the first inlet (41).

5. The pulverized coal staged gasification system according to any of claims 1 to 4, wherein the outlet section (10) of the hydro-thermal reformer (1) is formed in a neck shape, the outlet section (10) being provided with a quench gas inlet (15).

6. Pulverized coal staged gasification system according to any of the claims 2 to 4, further comprising a gas cleaning and separation device (6);

the gas purification and separation device (6) is provided with a gas inlet (611) and a hydrogen outlet (631), the gas inlet (611) is respectively communicated with the first gas outlet (42) and the gas outlet (25) of the oxygen-deficient gasification reaction cavity, and the hydrogen outlet (631) is communicated with the hydrogen inlet (11); the gas purification and separation device (6) is used for purifying and separating the gas entering from the gas inlet (611), and the separated hydrogen is discharged from the hydrogen outlet (631) and enters the hydro-gasification reaction cavity through the hydrogen inlet (11).

7. The pulverized coal staged gasification system as claimed in claim 6, wherein the hydrogen outlet (631) is in communication with the residue combustion reaction chamber, and the residue combustion reaction chamber is in communication with the hydrogen inlet (11), so that the hydrogen discharged through the hydrogen outlet (631) enters the residue combustion reaction chamber, is heated by the heat in the residue combustion reaction chamber, and then enters the hydro-gasification reaction chamber through the hydrogen inlet (11).

8. The pulverized coal staged gasification system as claimed in claim 6, wherein a secondary cyclone separator (5) is further provided between the primary cyclone separator (4) and the gas purification and separation device (6);

the secondary cyclone (5) having a second inlet (51), a second solid particle outlet (53) and a second gas outlet (52); the second inlet (51) is communicated with the first gas outlet (42) and the gas outlet (25) of the oxygen-deficient gasification reaction cavity respectively, the second gas outlet (52) is communicated with the gas inlet (611), and the second solid particle outlet (53) is communicated with the oxygen-deficient gasification reaction cavity; the secondary cyclone separator (5) is used for separating the gas entering from the second inlet (51), the separated gas sequentially enters the gas purification and separation device (6) through the second gas outlet (52) and the gas inlet (611), and the captured solid particles enter the oxygen-deficient gasification reaction cavity through the second solid particle outlet (53).

9. Pulverized coal staged gasification system according to claim 6, characterized in that the gas cleaning separation device (6) comprises a high temperature gas filter (61), a hydrogen gas heat exchanger (62) and a gas separator (63);

the high temperature gas filter (61) has the gas inlet (611), a third gas outlet (612) and a third solid particle outlet (613); the third solid particle outlet (613) is in communication with the residue combustion reaction chamber; the hydrogen heat exchanger (62) is in communication with the third gas outlet (612) and the gas separator (63), respectively;

the high-temperature gas filter (61) is used for filtering gas entering from the gas inlet (611), filtered solid particles enter the residue combustion reaction cavity through the third solid particle outlet (613), and the filtered gas enters the hydrogen heat exchanger (62) through the third gas outlet (612); the hydrogen heat exchanger (62) is used for cooling the gas discharged from the third gas outlet (612) to separate oil products, and the gas from which the oil products are separated enters the gas separator (63); the gas separator (63) is used for separating the gas of the separated oil product to obtain methane and hydrogen, and the gas separator (63) is provided with the hydrogen outlet (631) for discharging the hydrogen.

10. The pulverized coal staged gasification system as claimed in claim 9, wherein the hydrogen heat exchanger (62) has a hydrogen channel therein;

the hydrogen outlet (631) is communicated with the inlet (622) of the hydrogen channel, the outlet (623) of the hydrogen channel is communicated with the residue combustion reaction cavity, and the residue combustion reaction cavity is communicated with the hydrogen inlet (11), so that hydrogen discharged from the hydrogen outlet (631) enters the residue combustion reaction cavity after being subjected to heat exchange by the hydrogen heat exchanger (62), and is heated by heat in the residue combustion reaction cavity and enters the hydro-gasification reaction cavity through the hydrogen inlet (11).

11. The pulverized coal staged gasification system according to claim 10, wherein a hydrogen compressor (64) is further provided between the gas separator (63) and the hydrogen heat exchanger (62);

the hydrogen compressor (64) is communicated with the hydrogen outlet (631) and the inlet (622) of the hydrogen passage, respectively; the hydrogen compressor (64) is used for compressing the hydrogen discharged from the hydrogen outlet (631) and delivering the compressed hydrogen to the hydrogen channel.

12. A method for staged gasification of pulverized coal using the staged pulverized coal gasification system as claimed in any one of claims 1 to 11, the method comprising:

13. The method of claim 12, wherein the step of passing at least the solid char of the reactants produced by the reaction in the hydro-gasification reaction chamber into an oxygen-depleted gasification reaction chamber of an oxygen-depleted gasification reaction furnace comprises:

14. The method of claim 13, wherein the step of passing at least the reactant to a primary cyclone such that the primary cyclone separates the reactant comprises: