CN216946887U

CN216946887U - Reducing gas preparation system for gas-based shaft furnace by using biomass gas

Info

Publication number: CN216946887U
Application number: CN202220885264.XU
Authority: CN
Inventors: 张春雷; 王忠英; 王前; 李海涛; 金守成; 王启丞; 安丰森
Original assignee: Heilongjiang Jianlong Iron and Steel Co Ltd
Current assignee: Heilongjiang Jianlong Iron and Steel Co Ltd
Priority date: 2022-04-15
Filing date: 2022-04-15
Publication date: 2022-07-12
Anticipated expiration: 2032-04-15

Abstract

A reducing gas preparation system for a gas-based shaft furnace by using biomass gas relates to the technical field of reducing gas preparation. The utility model aims to solve the problems of complex structure, waste gas generation and high operation cost in the prior tubular heating furnace for preparing reducing gas. The utility model comprises a gas-based shaft furnace, a non-catalytic partial oxidation converter, a coke oven, a biomass gas producer and oxygenThe gas outlet ends of the coke oven gas bridge pipe and the biomass gas bridge pipe are respectively communicated with the gas inlet end of the mixed gas collecting pipe, the gas outlet end of the mixed gas collecting pipe is communicated with the gas inlet end of the mixed gas pipe, the mixed gas pipe is sequentially connected with a mixed gas purification system and a mixed gas compressor from top to bottom, the gas outlet end of the mixed gas pipe is communicated with the gas pipeline of the burner of the non-catalytic partial oxidation reformer, and the CO is removed₂The gas outlet end of the furnace top purifying gas pipe is communicated with a reducing gas pipe at the outlet of the non-catalytic partial oxidation furnace. The utility model is used for preparing reducing gas.

Description

Reducing gas preparation system for gas-based shaft furnace by using biomass gas

Technical Field

The utility model relates to the technical field of reducing gas preparation, in particular to a reducing gas preparation system for a gas-based shaft furnace by using biomass gas.

Background

The gas-based shaft furnace process is a clean iron-making technology and is an important technical means for realizing the double-carbon target in the steel industry in China. However, in the prior art, the main gas source of the gas-based shaft furnace is natural gas, while the current resource situation of China is more coal and less gas, and in order to adapt to the characteristics of domestic resources, the development of a new gas source suitable for the gas-based shaft furnace and the technology thereof become more and more important. Therefore, technicians at home and abroad research the gas-based shaft furnace technology of a non-natural gas source, the research direction is a coal gas making process, coal is a non-renewable resource, and the development prospect is limited. However, the related technology of using renewable biomass gas for the gas-based shaft furnace has not been researched and reported so far, and the biomass gas as renewable energy has a better development prospect than coal gas, so that the utility model provides a reducing gas preparation system of using the biomass gas for the gas-based shaft furnace.

In addition, the existing gas-based shaft furnace process adopts a tubular heating furnace to prepare raw material gas, as proposed in patent application No. 201710676084.4 entitled system and method for preparing reducing gas of gas-based shaft furnace, "the catalyst tubes are multiple and are arranged in parallel," the heat recovery device is a heat exchanger "; in another example of this application, a,application No.: CN201910952204.8 entitled, a new reformer for producing reducing gas, which comprises a radiant chamber box, reforming tubes, burners, a transition section and a convection section; the reforming furnace tubes are vertically arranged in parallel in 2m rows in the radiation chamber box body. The preparation of reducing gas by a tubular heating furnace has the following problems: (1) the raw material gas in the tube type furnace is heated by fuel combustion, and the raw material gas in the furnace tube is heated by the fuel combustion outside the tube, so the diameter of the tube is limited, and the single furnace tube has small volume and large quantity. The number of furnace tubes in a radiation chamber of the sleeve type heating furnace is as many as hundreds, and the number of burners is dozens; the transition section and convection section equipment for discharging flue gas and utilizing the waste heat of the flue gas are huge and have complex structures. All of these cause large investment in gas-based shaft furnace gas making system; (2) the process burns fuel to discharge CO₂And other exhaust gases; (3) the catalyst for preparing the reducing gas is expensive, the using amount is large, and the catalyst needs to be replaced periodically, so that the production and operation cost is high.

SUMMERY OF THE UTILITY MODEL

The utility model aims to solve the problems of the existing tubular heating furnace for preparing the reducing gas, and further provides a system for preparing the reducing gas by using the biomass gas for the gas-based shaft furnace.

The technical scheme adopted by the utility model for solving the technical problems is as follows:

a reducing gas preparation system for a gas-based shaft furnace by using biomass gas comprises the gas-based shaft furnace, a non-catalytic partial oxidation reformer, a coke oven, a biomass gas generating furnace, an oxygen source and a steam source, wherein a gas outlet end of the coke oven is communicated with a gas inlet end of a coke oven gas riser, the gas outlet end of the coke oven gas riser is communicated with a gas inlet end of a coke oven gas bridge pipe, the gas outlet end of the biomass gas generating furnace is communicated with the gas inlet end of the biomass gas riser, the gas outlet end of the biomass gas riser is communicated with the gas inlet end of the biomass gas bridge pipe, ammonia water cooling nozzles are arranged in the coke oven gas bridge pipe and the biomass gas bridge pipe, the gas outlet ends of the coke oven gas bridge pipe and the biomass gas bridge pipe are respectively communicated with the gas inlet end of a mixed gas collecting pipe, and the gas outlet end of the mixed gas collecting pipe is communicated with the gas inlet end of the mixed gas collecting pipeThe gas outlet end of the hot gas pipe at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with a CO removal gas outlet end of a hot gas pipe at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace through a reduction gas pipe at the outlet of the non-catalytic partial oxidation furnace₂The furnace top purifies the gas pipe and does not remove CO₂The gas inlet ends of the gas pipe at the top of the gas-based shaft furnace are communicated without removing CO₂The gas outlet end of the gas pipe at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purifying gas pipe is communicated with a reducing gas pipe at the outlet of the non-catalytic partial oxidation furnace.

Further, a coke oven gas heat exchanger is arranged on the coke oven gas ascending pipe, and the CO is removed₂The gas outlet end of the furnace top purified gas pipe is communicated with the inlet of a coke oven gas heat exchanger, and the outlet pipeline of the coke oven gas heat exchanger is communicated with a reducing gas pipe at the outlet of the non-catalytic partial oxidation furnace.

Further, a coke oven gas heat exchanger is arranged on the coke oven gas ascending pipe, a biomass gas heat exchanger is arranged on the biomass gas ascending pipe, and the CO is removed₂The gas outlet end of the furnace top purified gas pipe is respectively communicated with the inlets of the coke oven gas heat exchanger and the biomass gas heat exchanger, and the outlet pipelines of the coke oven gas heat exchanger and the biomass gas heat exchanger are converged and then communicated with the outlet reduction gas pipe of the non-catalytic partial oxidation furnace.

Further, a coke oven gas heat exchanger is mounted on the coke oven gas ascending pipe, a biomass gas heat exchanger is mounted on the biomass gas ascending pipe, a biomass generator flue gas heat exchanger is mounted on a hot flue gas discharge pipe of the biomass generator, and the CO removal is performed₂The gas outlet end of the furnace top purified gas pipe is respectively communicated with the inlets of the coke oven gas heat exchanger, the biomass gas heat exchanger and the biomass generator flue gas heat exchanger, and the coke oven gas is exchangedAnd the outlet pipelines of the heat exchanger, the biomass gas heat exchanger and the biomass generator flue gas heat exchanger are converged and then communicated with a reduction gas pipe at the outlet of the non-catalytic partial oxidation furnace.

Furthermore, the mixed gas pipe is also communicated with a first gas-based shaft furnace top hot gas heat exchanger, and the first gas-based shaft furnace top hot gas heat exchanger is arranged between an outlet of the mixed gas compressor and an inlet of a gas pipeline of a burner on the non-catalytic partial oxidation reforming furnace.

Furthermore, the discharge end of the cooling section of the gas-based shaft furnace is connected with a thermal cycle gas heat exchanger, an outlet of the hot gas heat exchanger at the top of the gas-based shaft furnace is communicated with an inlet of the thermal cycle gas heat exchanger, and an outlet of the thermal cycle gas heat exchanger is communicated with a gas pipeline inlet of a burner on the non-catalytic partial oxidation reforming furnace.

Compared with the prior art, the utility model has the following beneficial effects:

1. renewable biomass gas is used as raw material gas of the gas-based shaft furnace for the first time, and a solution for distributing gas with coke oven gas is provided aiming at the problems that the biomass gas has high CO content and is not suitable for the gas-based shaft furnace. H in reducing gas prepared from mixed gas of biomass gas and coke oven gas₂The ratio of the/CO meets the gas utilization requirement of the gas-based shaft furnace; the temperature of the biomass gas producer is reduced to 650-850 ℃ by the scheme of adding the coke oven gas, so that the energy consumption of gas production is reduced;

2. the reasonable gas distribution proportion of the biomass and the coke oven gas is provided, so that the reduction gas prepared from the mixed gas of the biomass gas and the coke oven gas meets the gas demand of the gas-based shaft furnace;

3. aiming at the problems of unclean biomass gas, large independent purification investment and large environmental protection investment, the proposal is provided that the biomass gas to be purified and the coke oven gas are uniformly mixed at the same gas collecting pipe, then enter a gas treatment system and are purified together. Thereby simplifying the system and reducing the investment;

4. aiming at the problems that the content of unsaturated hydrocarbon in the biomass gas is high, carbon is easily deposited in the reforming process, and the difficulty of deep desulfurization, deep purification and the like are needed for preventing catalyst poisoning, the scheme of treating the mixed gas of the biomass gas and the coke oven gas by adopting a non-catalytic partial oxidation process is provided. The problem of easy carbon deposition is avoided, a catalyst is not needed, excessive deep purification is not needed, the process steps are simplified, and the investment and the operation cost are reduced;

5. the non-catalytic partial oxidation furnace with the refractory material lining is used for replacing a traditional tubular heating furnace consisting of hundreds of heat-resistant steel tubes, so that the investment is further reduced;

6. adjusting CO in reducing gas by proportioning coke oven gas and biomass gas and non-catalytic partial oxidation process₂The content scheme ensures that the biomass gas does not need to remove CO₂The process is directly mixed with the coke oven gas, thereby saving the CO removal of the biomass gas₂And the matching process;

7. an internal combustion type non-catalytic partial oxidation technology and a heat exchange preheating technology are used to replace a tubular external combustion heating technology, and no waste gas is discharged when a gas-based shaft furnace system heats feed gas;

8. because the furnace top purifies water and CO of the coal gas₂The content can be reduced to the design requirement by controlling, so that the effective components of the mixed reducing gas can be improved after the mixed reducing gas is mixed into the high-temperature reducing gas at the outlet of the non-catalytic partial oxidation furnace; the furnace top is preheated by the recovery mode of the waste heat of the biomass gas producer and/or the coke oven and/or the gas-based shaft furnace to purify the gas, so that the mixing amount of the purified gas on the furnace top can be increased, and the effective components of the mixed reducing gas can be further improved;

9. the mixed gas of the biomass gas and the coke oven gas is preheated by the recovery mode of the waste heat of the biomass gas producer and/or the coke oven and/or the gas-based shaft furnace, so that the amount of the gas to be combusted in the non-catalytic partial oxidation furnace can be reduced, and the water and CO generated after the combustion can be reduced₂The content of the reducing gas is increased, so that the effective components of the reducing gas at the outlet of the non-catalytic partial oxidation furnace are increased;

10. the internal combustion type non-catalytic partial oxidation technology has higher thermal efficiency and energy saving than an external combustion tubular heating furnace;

11. by the gradient utilization mode of different kinds of coal gas, CO is not removed₂The coke oven gas is replaced by the gas-based shaft furnace top gas with the same calorific value without removing CO₂Gas-based shaft furnace top gas forThe gas of other projects or as chemical raw materials, the replaced coke oven gas and the biomass gas are mixed into mixed gas, thus indirectly realizing the purpose of self-produced gas of the gas-based shaft furnace for recycling the shaft furnace in a self-circulation manner and the purpose of not discharging waste gas;

12. without CO removal₂The gas-based shaft furnace top gas is used as fuel gas of other projects or used as chemical raw materials, is not used as fuel gas of the gas-based shaft furnace any more, and can also solve the problem of N caused by the recycling of the top gas in the gas-based shaft furnace₂The problem of enrichment.

Drawings

FIG. 1 is a flow diagram of a first embodiment of a reducing gas production system for a biogas for use in a gas-based shaft furnace according to the present invention;

FIG. 2 is a flow diagram of a second embodiment of a reducing gas production system for a biogas for use in a gas-based shaft furnace according to the present invention;

FIG. 3 is a flow diagram of a third embodiment of a reducing gas production system for a gas-based shaft furnace using a biogas according to the present invention;

FIG. 4 is a flow diagram of a fourth embodiment of a reducing gas production system for a gas-based shaft furnace using a biogas according to the present invention;

FIG. 5 is a flow diagram of a fifth embodiment of a reducing gas production system for a gas-based shaft furnace utilizing a biogas according to the present invention;

FIG. 6 is a flow diagram of a sixth embodiment of a reducing gas production system for a biogas for use in a gas-based shaft furnace according to the present invention;

FIG. 7 is a flow diagram of a seventh embodiment of a reducing gas production system for a biogas for use in a gas-based shaft furnace according to the present invention.

Detailed Description

The first embodiment is as follows: the embodiment is described with reference to fig. 1 to 7, and the reducing gas preparation system for a gas-based shaft furnace using biomass gas according to the embodiment comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas generating furnace 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, and a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of the coke oven gas riser 84The coal gas inlet end of the bridge pipe 82 is communicated, the coal gas outlet end of the biomass gas producer 09 is communicated with the coal gas inlet end of the biomass gas riser pipe 94, the coal gas outlet end of the biomass gas riser pipe 94 is communicated with the coal gas inlet end of the biomass gas bridge pipe 92, ammonia water cooling spray heads 6 are arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, the coal gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with the coal gas inlet end of the mixed gas collecting pipe 81, the coal gas outlet end of the mixed gas collecting pipe 81 is communicated with the coal gas inlet end of the mixed gas pipe 5, the mixed gas pipe 5 is sequentially connected with a mixed gas purification system 51 and a mixed gas compressor 52 from top to bottom, the coal gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2, the oxygen pipeline and the steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7 The non-catalytic partial oxidation reformer 2 is communicated with the shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, and the gas outlet end of a hot gas pipe 12 at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with the CO removal₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with the gas inlet end without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

In the present embodiment, the number of the biogas risers 94 is plural, and the number of the biogas heat exchangers 93 and the number of the biogas bridge pipes 92 installed on the corresponding biogas risers 94 are also plural; the number of the coke oven gas ascending pipes 84 is multiple, and the number of the coke oven gas heat exchangers 83 and the coke oven gas bridge pipes 82 which are arranged on the corresponding coke oven gas ascending pipes 84 is also multiple.

In the present embodiment, CO is not removed₂The gas tube 122 at the top of the gas-based shaft furnace is used as a gas pipeline for other purposes instead of coke oven gas.

One of the purposes of the utility model is to provide a technical scheme and a proportion for using biomass gas in a gas-based shaft furnace.

The utility model also aims to simplify the reducing gas preparation system and reduce the investment.

The third purpose of the utility model is that the biomass gas does not need to remove CO₂The process is directly used for gas making.

The fourth purpose of the utility model is to increase the effective components of the reducing gas.

The fifth purpose of the utility model is to indirectly realize the purpose of self-producing coal gas heat energy self-circulation recycling of the gas-based shaft furnace through the gradient utilization mode of different kinds of coal gas.

Other objects of the present invention will be pointed out hereinafter or will be apparent to those skilled in the art.

The second embodiment is as follows: the present embodiment will be described with reference to fig. 1 to 7, and a coke oven gas heat exchanger 83 is attached to the coke oven gas riser 84 of the present embodiment, and the CO removal is performed₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the inlet of the coke oven gas heat exchanger 83, and the outlet pipeline of the coke oven gas heat exchanger 83 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic part oxidation furnace. The technical features not disclosed in the present embodiment are the same as those of the first embodiment.

The third concrete implementation mode: referring to fig. 1 to 7, the coke oven gas riser 84 of the present embodiment is provided with a coke oven gas heat exchanger 83, the biomass gas riser 94 is provided with a biomass gas heat exchanger 93, and the CO removal is performed₂The gas outlet end of the furnace top purified gas pipe 121 is respectively communicated with the inlets of the coke oven gas heat exchanger 83 and the biomass gas heat exchanger 93, and the outlet pipelines of the coke oven gas heat exchanger 83 and the biomass gas heat exchanger 93 are converged and then communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace. Technical features not disclosed in the present embodiment are the same as those of the first embodiment.

The fourth concrete implementation mode: referring to fig. 1 to 7, the coke oven gas riser 84 of the present embodiment is provided with a coke oven gas heat exchanger 83, a biomass gas riser 94 is provided with a biomass gas heat exchanger 93, and a hot flue gas discharge pipe 91 of the biomass generator is provided with flue gas of the biomass generatorHeat exchanger 092, said CO removal₂The outlet gas end of the furnace top purified gas pipe 121 is respectively communicated with the inlets of the coke oven gas heat exchanger 83, the biomass gas heat exchanger 93 and the biomass generator flue gas heat exchanger 092, and the outlet pipelines of the coke oven gas heat exchanger 83, the biomass gas heat exchanger 93 and the biomass generator flue gas heat exchanger 092 are communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace after being gathered. Technical features not disclosed in the present embodiment are the same as those of the first embodiment.

The fifth concrete implementation mode: referring to fig. 1 to 7, the mixed gas pipe 5 of the present embodiment is further communicated with a first gas-based shaft furnace top hot gas heat exchanger 13, and the first gas-based shaft furnace top hot gas heat exchanger 13 is disposed between an outlet of the mixed gas compressor 52 and an inlet of a gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2. Technical features not disclosed in the present embodiment are the same as those of the first embodiment.

The sixth specific implementation mode: referring to the embodiment described with reference to fig. 1 to 7, the discharge end of the cooling section of the gas-based shaft furnace 1 of the embodiment is connected with a hot circulating gas heat exchanger 01, the outlet of a hot gas heat exchanger one 13 at the top of the gas-based shaft furnace is communicated with the inlet of the hot circulating gas heat exchanger 01, and the outlet of the hot circulating gas heat exchanger 01 is communicated with the inlet of a gas pipeline of a burner 3 on a non-catalytic partial oxidation reformer 2. The technical features not disclosed in the present embodiment are the same as those in the fifth embodiment.

A preparation method of a reducing gas preparation system for a gas-based shaft furnace based on the biomass gas comprises the following steps:

firstly, communicating hot biomass gas generated by a biomass gas generator 09 and coke oven gas generated by a coke oven 08 with a mixed gas collecting pipe 81 through a biomass gas bridge pipe 92 and a coke oven gas bridge pipe 82 respectively, uniformly mixing the biomass gas and the coke oven gas in the mixed gas collecting pipe 81, and spraying ammonia water through an ammonia water cooling nozzle 6 arranged at the upper parts of the biomass gas bridge pipe 92 and the coke oven gas bridge pipe 82 for cooling;

step two, the cooled mixed gas enters the non-catalytic partial oxidation converter 2 for heating after being purified, pressurized and preheated, and the gas in the non-catalytic partial oxidation converter 2 is reformed into high-temperature reducing gas;

step three, mixing H into the high-temperature reducing gas₂And the mixed gas with the volume sum of the CO and the CO being more than 90% of the total volume of the gas becomes mixed reducing gas with the temperature of 850-1100 ℃, and the mixed reducing gas enters the gas-based shaft furnace 1.

In the first step, in the mixed gas of the biomass gas and the coke oven gas, the volume of the biomass gas is less than 60 percent of the total volume of the mixed gas.

In the second step, the amount of oxygen in the non-catalytic partial oxidation converter 2 is reduced by increasing the preheating temperature of the mixed gas, so that the H content of the gas at the outlet of the non-catalytic partial oxidation converter 2 is increased₂And the CO content.

In the third step, H₂And CO are preheated and then mixed into high-temperature reducing gas, and H is added along with the increase of the preheating temperature₂And the amount of CO gas is increased, thereby increasing the H content of the mixed reducing gas entering the gas-based shaft furnace₂And an effective amount of CO gas.

In the third step, H is mixed in₂And CO is top purified gas which is part of top hot gas of the gas-based shaft furnace, and the top purified gas is cooled, dedusted, desulfurized and stripped of CO₂The other part of the coal gas is not subjected to CO removal₂The replaced coke oven gas and/or biomass gas and newly supplemented coke oven gas and biomass gas are mixed into mixed gas which enters a gas heating furnace for heating, and the self-produced gas energy self-circulation recycling of the gas-based shaft furnace is indirectly realized through the gradient utilization mode of different kinds of gas.

Furthermore, the volume of the biomass gas accounts for 10-30% of the total volume of the mixed gas.

Further, the thermal cracking temperature of the biomass gas is 650-850 ℃.

Further, in the second step, the mixed gas of the biomass gas and the coke oven gas is preheated by a biomass gas heat exchanger 93 and a coke oven gas heat exchanger 83 and/or a biomass producer gas heat exchanger 092 and/or a gas-based shaft furnace cooling section hot circulating gas heat exchanger 01 and/or a dry quenching high-temperature nitrogen gas heat exchanger.

Further, in step three, H is mixed in₂And the CO is preheated by the biomass gas heat exchanger 93 and the coke oven gas heat exchanger 83 and/or the biomass generating furnace flue gas heat exchanger 092 and/or the gas-based shaft furnace cooling section heat exchanger 01.

Further, H is mixed in₂And CO is top purified gas which is part of top hot gas of the gas-based shaft furnace, and the top purified gas is cooled, dedusted, desulfurized and stripped of CO₂After gases, i.e. CO removal₂The furnace top of the gas pipe 121.

Further, another part is not subjected to CO removal₂The coke oven gas and/or the biomass gas are replaced by the gas-based shaft furnace top gas with the same calorific value, i.e. CO is not removed₂The replaced coke oven gas and/or biomass gas and newly supplemented coke oven gas and biomass gas are mixed into mixed gas, the mixed gas enters a gas heating furnace, namely a non-catalytic partial oxidation converter 2 to be heated, and the self-produced gas energy of the gas-based shaft furnace is indirectly recycled to the gas-based shaft furnace 1 through the gradient utilization mode of different kinds of gas.

Furthermore, the preheating temperature of the furnace top purified gas is increased, and the adding amount of the furnace top purified gas is increased, so that the effective gas amount of the mixed reducing gas entering the gas-based shaft furnace is increased.

A method for preparing reducing gas by using biomass gas in a gas-based shaft furnace comprises the following steps: introducing gas for preparing reducing gas into a gas heating furnace through a pipeline for heating, reforming at least part of the gas in the heating furnace to form reducing gas, then introducing the reducing gas into a gas-based shaft furnace 1, reacting iron oxide with the reducing gas in the gas-based shaft furnace 1 to reduce the iron oxide into direct reduced iron, discharging the direct reduced iron out of the furnace through the lower part of the gas-based shaft furnace 1, discharging raw gas generated by the reaction from the top of the gas-based shaft furnace 1, wherein the gas entering the heating furnace is mixed gas of biomass gas and coke oven gas, the ratio of the biomass gas in the mixed gas is less than 60%, the mixed gas is modified into the reducing gas through the heating furnace, and the reducing gas is mixed with part of top purified gas and then enters the gas-based shaft furnace 1.

Further: the hot biomass gas generated by the biomass gas producer 09 is communicated with a coke oven gas pipe 8 through a biomass gas pipe 9, the biomass gas and the coke oven gas are uniformly mixed in the pipe, and are sprayed with ammonia water for cooling through an ammonia water cooling nozzle 6 arranged at the upper part of the pipe, then tar, naphthalene and sulfur in the mixed gas are removed according to the treatment technology known in the industry, then the mixed gas is pressurized to 0.15-1 Mpa, and preferably, the mixed gas is pressurized after benzene and ammonia are removed.

The pressurized mixed gas enters a mixed gas pipe 5 of a burner 3 of the non-catalytic partial oxidation reformer 2 after heat exchange through a heat exchanger, and the preheated pure oxygen and steam respectively enter respective channels of the burner 3 of the non-catalytic partial oxidation reformer 2. The pure oxygen and the mixed gas are burnt in the oxygen-poor way at the outlet of the burner 3 to generate CO and H₂And H₂O is the reducing gas of the main component, and the reducing gas reaches 1100-1350 ℃ at the outlet of the non-catalytic partial oxidation converter 2.

One part of the gas-based shaft furnace top gas after heat exchange and dust removal is subjected to CO removal₂Processing to obtain furnace top purified gas; the other part is not subjected to CO removal₂The coke oven gas is replaced by the gas-based shaft furnace top gas with the same calorific value, the replaced coke oven gas and the biomass gas are mixed into mixed gas without removing CO₂The gas-based shaft furnace top gas replaces coke oven gas to serve other purposes, and the purpose of self-circulation recycling of heat energy of gas produced by the gas-based shaft furnace is achieved through a gradient utilization mode of different kinds of gas.

The furnace top purified gas is preheated and then mixed with high-temperature reducing gas at the outlet of the non-catalytic partial oxidation converter 2 to form mixed reducing gas, the temperature of the mixed reducing gas is 850-1100 ℃, and the mixed reducing gas enters the gas-based shaft furnace 1 through a shaft furnace tuyere 11.

The heat exchange and the preheating are realized in the following mode, the mixed gas of the biomass gas and the coke oven gas adopts a biomass gas heat exchanger 93 and a coke oven gas heat exchanger 83, and/or a biomass generating furnace flue gas heat exchanger 092 and/or a gas-based shaft furnace cooling section heat exchanger 01 and/or a dry quenching high-temperature nitrogen heat exchanger for heat exchange.

Example one

The present embodiment is described with reference to fig. 1:

the reducing gas preparation system for the gas-based shaft furnace using the biomass gas comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas producer 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas producer 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia cooling nozzles 6 are respectively arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with a gas inlet end of a mixed gas collecting pipe 81, a gas outlet end of the mixed gas collecting pipe 81 is communicated with a gas inlet end of a mixed gas pipe 5, the mixed gas pipe 5 is sequentially connected with a mixed gas purification system 51 and a mixed gas compressor 52 from first to last, the gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2, the oxygen pipeline and the steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reformer 2 is communicated with the shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, and the gas outlet end of a hot gas pipe 12 at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with a CO removal furnace₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet ends of the gas pipe 122 at the top of the gas-based shaft furnace are communicated without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

The coke oven gas riser 84 is provided with a coke oven gas heat exchanger 83, the biomass gas riser 94 is provided with a biomass gas heat exchanger 93, and the CO removal is carried out₂The gas outlet end of the furnace top purified gas pipe 121 is respectively communicated with the inlets of the coke oven gas heat exchanger 83 and the biomass gas heat exchanger 93, and the outlet pipelines of the coke oven gas heat exchanger 83 and the biomass gas heat exchanger 93 are converged and then communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

Further, the CO removal₂The furnace top clean gas pipe 121 includes CO removal₂The furnace top purifies the gas pipe and removes CO₂Second furnace top gas purifying pipe for removing CO₂Top purified gas pipe III and CO removal₂The top of the furnace purifies the gas pipe four, remove CO₂The first furnace top gas purifying pipe is sequentially connected with a shaft furnace top gas compressor 17 and desulfurization-CO from top to bottom₂System 18, CO removal₂The gas outlet end of the furnace top purified gas pipe I and CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated to remove CO₂The gas outlet end of the second furnace top purified gas pipe passes through the coke oven gas heat exchanger 83 and then is respectively subjected to CO removal₂Top purified gas pipe III and CO removal₂The inlet end of the furnace top purifying gas pipe IV is communicated to remove CO₂The gas outlet end of the furnace top purified gas pipe III is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace for removing CO₂The gas outlet end of the furnace top purified gas pipe IV passes through the biomass gas heat exchanger 93 and then is subjected to CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated.

The desulfurization of CO₂The system 18 includes a desulfurization unit and CO removal₂Provided is a device.

The shaft furnace top hot gas pipe 12 is sequentially connected with a shaft furnace hot gas heat exchanger group and a dust removal device 16 from top to bottom, the shaft furnace hot gas heat exchanger group comprises a first gas-based shaft furnace top hot gas heat exchanger 13, a second gas-based shaft furnace top hot gas heat exchanger 14 and a third gas-based shaft furnace top hot gas heat exchanger 15, an oxygen pipe 4 is communicated with an oxygen pipeline of a burner 3 of the non-catalytic partial oxidation reformer 2 after passing through the second gas-based shaft furnace top hot gas heat exchanger 14, a steam pipe 7 is communicated with a steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 after passing through the third gas-based shaft furnace top hot gas heat exchanger 15, and an air outlet end of a mixed gas pipe 5 is communicated with a burner pipeline of the shaft furnace top hot gas heat exchanger 13 of the non-catalytic partial oxidation reformer 2 after passing through the first gas-based shaft furnace top hot gas heat exchanger 13.

A method for producing a reducing gas by using a biomass gas for a gas-based shaft furnace is described with reference to fig. 1. The biomass gas 9 (the typical components of the biomass gas are CO: 51.76 and CH) generated at the thermal cracking temperature of about 700-800 ℃ in the biomass gas producer 09₄：14.51、H₂：8.41、CO₂：13.5、N₂: 2.37, CmHn: 6.62) is communicated with the mixed gas collecting pipe 81 through a biomass gas ascending pipe 94 and a biomass gas bridge pipe 92, the biomass gas ascending pipe 94 is provided with a biomass gas heat exchanger 93, the coke oven gas 8 generated by the coke oven 08 is communicated with the mixed gas collecting pipe 81 through a coke oven gas ascending pipe 84 and a coke oven gas bridge pipe 82, the coke oven gas ascending pipe 84 is provided with a coke oven gas heat exchanger 83, and the biomass gas 9 and the coke oven gas 8 (the typical components of the coke oven gas are CO: 8.07, CH₄：25.4、H₂：55.8、CO₂：2.83、N₂: 4.25, CmHn: 3.52) are uniformly mixed in the mixed gas collecting pipe 81 according to the ratio of 2:8 to form mixed gas (in the mixed gas pipe 5). The biomass gas 9 and the coke oven gas 8 are sprayed with ammonia water for cooling through an ammonia water cooling nozzle 6 arranged at the upper part of the biomass gas bridge pipe 92 and the coke oven gas bridge pipe 82, then tar, benzene, naphthalene, sulfur and ammonia are removed through a mixed gas purification system 51 according to the treatment technology known in the industry, and then the mixed gas is pressurized to 0.5MPa through a mixed gas compressor 52, and at the moment, the components of the mixed gas are about CO: 16.83, CH₄：23.2、H₂：46.33、CO₂：4.9、N₂: 3.9, CmHn: 4.12, the mixed gas flow is about 660M³t.Fe.

The pressurized mixed gas (in a mixed gas pipe 5) and the top hot gas (in a top hot gas pipe 12) of the gas-based shaft furnace 1 exchange heat in a first 13 of the top hot gas heat exchanger of the gas-based shaft furnace, and then enter a gas passage of a burner 3 of a non-catalytic partial oxidation reformer 2, pure oxygen (in an oxygen pipe 4) exchanges heat in a second 14 of the top hot gas heat exchanger of the gas-based shaft furnace, and then enter an oxygen passage of the burner 3 of the non-catalytic partial oxidation reformer 2, and the other one of the top hot gas (in the top hot gas pipe 12) of the gas-based shaft furnaceAnd steam generated by a third hot gas heat exchanger 15 on the top of the gas-based shaft furnace by utilizing waste heat enters a steam channel of a burner of the non-catalytic partial oxidation reformer 2. And (3) performing anoxic combustion on pure oxygen and mixed coal gas at the outlet of the burner 3, wherein the proportion of the pure oxygen in the mixed coal gas is about 23%, and the components of generated reducing gas are about CO: 28.18, CH₄：1.37、H₂：53.1、CO₂：3.0、N₂：2.53、H₂O: 11.5, the reducing gas (in the non-catalytic partial oxidation furnace outlet reducing gas pipe 21) is about 1250 deg.c at the outlet into the non-catalytic partial oxidation converter 2.

One part of the gas base shaft furnace top gas is subjected to heat exchange and dehydration through a first gas base shaft furnace top hot gas heat exchanger 13, a second gas base shaft furnace top hot gas heat exchanger 14 and a third gas base shaft furnace top hot gas heat exchanger 15, the gas base shaft furnace top gas subjected to dust removal through a dust removal device 16 is pressurized through a shaft furnace top gas compressor 17, and then is subjected to desulfurization and CO removal through a desulfurization device₂The device is used for processing the gas to become the top purified gas 121 (the flow rate is about 750M)³T. Fe), by means of a dehydration and desulfurization unit, by CO removal₂Device for controlling furnace top to purify gas (remove CO)₂Furnace top cleaning gas pipe 121) of water and CO₂The sum of the contents is less than 8 percent. Gas-based shaft furnace top gas purification (CO removal)₂In the furnace top purified gas pipe 121) and then exchanges heat with hot biomass gas and hot coke oven gas in the biomass gas heat exchanger 93 and the coke oven gas heat exchanger 83 respectively, and the furnace top purified gas (CO removal) is carried out after heat exchange₂In the furnace top purified gas pipe 121) reaches about 660 ℃, and then 1250 ℃ reducing gas (in the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation converter 2) at the outlet of the non-catalytic partial oxidation converter 2 (the flow rate is about 1000M)³T. iron) to form a mixed reducing gas, the temperature of the mixed reducing gas is about 1000 ℃, and the components of the mixed reducing gas are about CO: 28.47, CH₄：1.2、H₂：55.36、CO₂：2.89、N₂：3.2、H₂O: 8.32, the mixed reducing gas enters the gas-based shaft furnace 1 through a shaft furnace tuyere 11. In the gas-based shaft furnace 1, the iron oxide reacts with the reducing gas to be reduced into direct reduced iron, the direct reduced iron is discharged out of the furnace through the lower part of the gas-based shaft furnace 1, and the raw gas generated by the reaction is discharged from the top of the shaft furnace to become hot gas at the top of the gas-based shaft furnace (the top of the shaft furnace)Within the hot gas pipe 12).

It needs to be further explained that:

the mixed reducing gas is added with furnace top purified gas (CO removal) preheated to 660 DEG C₂In the furnace top purified gas pipe 121), the proportion of the moisture carried by the reducing gas (in the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace) generated by the non-catalytic partial oxidation converter 2 in the mixed reducing gas is reduced, and the effective components of the mixed reducing gas entering the gas-based shaft furnace 1 are improved. If the furnace top purifies the gas (removes CO)₂In the furnace top purified gas pipe 121) the preheating temperature is further raised, and the furnace top purified gas (removing CO)₂The furnace top purified gas pipe 121) can be further increased, thereby further reducing the moisture of the mixed reducing gas entering the gas-based shaft furnace 1 and improving the effective components of the mixed reducing gas entering the gas-based shaft furnace 1;

remaining undeco₂The gas-based shaft furnace top gas (in the gas-based shaft furnace top gas pipe 122 without CO2 removal) has the flow rate of about 470M³Iron (calorific value of about 2000 kcal/m)³) When the calorific value is equal to the calorific value, the coke oven gas is replaced, and the flow rate is about 235M³T-iron (coke oven gas heat value about 4000 kcal/m)³) Replaced coke oven gas 8 (flow 235M)³Iron/t) and fresh make-up coke oven gas 8 (flow rate about 295M)³T. iron) and biogas 9 (flow rate about 130M)³T. iron) mixed into a flow rate of about 660M³Mixed gas of/t.iron (in the mixed gas pipe 5).

Without CO removal₂Gas-based shaft furnace top gas (without CO removal)₂In the gas-based shaft furnace top gas pipe 122) to replace the coke oven gas 8 for other purposes, the purpose of self-producing gas heat energy self-circulation recycling of the gas-based shaft furnace is indirectly realized through the gradient utilization mode of different kinds of gas, so that the whole gas-based shaft furnace system does not need to externally combust reducing gas in the heating pipe, does not discharge waste gas generated by external combustion, does not cause enrichment of nitrogen in the gas-based shaft furnace, and does not influence the normal operation and production efficiency of production. Compared with the gas-based shaft furnace which is commercially produced at present, the raw material gas is saved by about 35 percent of heat value per ton of iron.

If a higher temperature biomass gas is used, for example, a thermal cracking temperature of about 850 to 950 ℃The biomass gas 9 generated in the biomass gas producer 09 at a certain temperature (the typical components of the biomass gas are CO: 36.03 and CH)₄：14.74、H₂：31.06、CO₂：12.75、N₂: 2. CmHn: 1.14) mixing the coke oven gas with the process according to the figure at a ratio of 5:5, purifying, pressurizing, preheating and carrying out non-catalytic partial oxidation to generate reducing gas with the components of CO: 30.9, CH₄：1.35、H₂：50.5、CO₂：5.41、N₂：2.18、H₂O：12.1。

Example two

The present embodiment is described with reference to fig. 2:

the system for preparing the reducing gas by using the biomass gas for the gas-based shaft furnace comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas producer 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas producer 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia water cooling spray heads 6 are respectively arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with a gas inlet end of a mixed gas collecting pipe 81, a gas outlet end of the mixed gas collecting pipe 81 is communicated with a gas inlet end of a mixed gas pipe 5, a mixed gas purification system 51 and a mixed gas compressor 52 are sequentially connected on the mixed gas pipe 5 from top to bottom, the gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2, the oxygen pipeline and the steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are also respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reformer 2 is communicated with the shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, the gas outlet end of a hot pipe 12 at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with the CO removal furnace₂Furnace roof cleaningGas pipe 121 and undeCO₂The gas inlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with the gas inlet end without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purifying gas pipe 121 is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

The coke oven gas ascending pipe 84 is provided with a coke oven gas heat exchanger 83, the biomass gas ascending pipe 94 is provided with a biomass gas heat exchanger 93, the hot flue gas discharge pipe 91 of the biomass generator is provided with a biomass generator flue gas heat exchanger 092, and the CO removal is carried out₂The outlet gas end of the furnace top purified gas pipe 121 is respectively communicated with the inlets of the coke oven gas heat exchanger 83, the biomass gas heat exchanger 93 and the biomass generator flue gas heat exchanger 092, and the outlet pipelines of the coke oven gas heat exchanger 83, the biomass gas heat exchanger 93 and the biomass generator flue gas heat exchanger 092 are communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace after being gathered.

Furthermore, the system for preparing the reducing gas by using the biomass gas for the gas-based shaft furnace also comprises a biomass producer medium ball heating lifting chamber 091 for removing CO₂The furnace top gas purification pipe 121 further comprises CO removal₂The furnace top purification gas pipe five is characterized in that a biomass producer medium ball heating lifting chamber 091 is arranged on one side of the biomass gas producer 09, a biomass producer flue gas pipe 91 is communicated with the biomass producer medium ball heating lifting chamber 091, a biomass producer flue gas heat exchanger 092 is connected to the biomass producer flue gas pipe 91, and CO is removed₂The gas inlet end of the furnace top purifying gas pipe five and CO removal₂The inlet end of the furnace top purifying gas pipe IV is communicated to remove CO₂The gas outlet end of the furnace top purified gas pipe five and CO removal₂The gas outlet end of the furnace top purified gas pipe IV is communicated to remove CO₂The furnace top purifying gas pipe passes through the biomass producer flue gas heat exchanger 092.

Referring to fig. 2, a method for producing reducing gas by using biomass gas in a gas-based shaft furnace is described, which is different from the embodiment of fig. 1 in that:

uniformly mixing the biomass gas 9 and the coke oven gas 8 according to the ratio of 3:7 to obtain mixed gas, pressurizing the mixed gas (in a mixed gas pipe 5) to 0.2MPa by a mixed gas compressor 52, wherein the components of the mixed gas are CO: 21.2, CH₄：22.1、H₂：41.6、CO₂：5.9、N₂：3.7、CmHn：4.4。

At the burner 3And (3) oxygen-deficient combustion of outlet pure oxygen and mixed coal gas, wherein the proportion of the pure oxygen in the mixed coal gas is about 22%, and the components of generated reducing gas are about CO: 31.38, CH₄：1.62、H₂：50.24、CO₂：3.3、N₂：2.47、H₂O: 9.5, at the outlet of the non-catalytic partial oxidation reformer 2, the reducing gas (in the non-catalytic partial oxidation furnace outlet reducing gas pipe 21) is about 1150 ℃.

Top purified gas (CO removal)₂In the furnace top purified gas pipe 121), and hot biomass gas 9, hot coke oven gas 8 and hot flue gas of the biomass generating furnace (in the flue gas pipe 91 of the biomass generating furnace) exchange heat in a biomass gas heat exchanger 93, a coke oven gas heat exchanger 83 and a flue gas heat exchanger 092 of the biomass generating furnace respectively, and after heat exchange, all branches are gathered into hot furnace top purified gas, and then the hot furnace top purified gas is mixed with reducing gas (in a reducing gas pipe 21 at the outlet of a non-catalytic partial oxidation converter 2) at 1150 ℃ to form mixed reducing gas, wherein the temperature of the mixed reducing gas is about 850-950 ℃, and the mixed reducing gas enters the gas-based shaft furnace 1 through a tuyere 11 of the shaft furnace.

The hot flue gas of the biomass generator comes from the high-temperature flue gas generated by burning the biomass residual carbon heating medium balls in the biomass generator medium ball heating lifting chamber 091.

EXAMPLE III

The present embodiment is explained with reference to fig. 3:

the reducing gas preparation system for the gas-based shaft furnace by using the biomass gas comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas generating furnace 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas generating furnace 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia water cooling nozzles 6 are arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, the gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with a gas inlet end of a mixed gas collecting pipe 81, and the mixed gas is mixed gasThe gas outlet end of the gas collecting pipe 81 is communicated with the gas inlet end of the mixed gas pipe 5, the mixed gas pipe 5 is sequentially connected with a mixed gas purification system 51 and a mixed gas compressor 52 from top to bottom, the gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2, the oxygen pipeline and the steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reformer 2 is communicated with the shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, the gas outlet end of a hot gas pipe 12 of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with the top of the CO-removing shaft furnace₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with the gas inlet end without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

Further, the CO removal₂The furnace top clean gas pipe 121 includes CO removal₂The furnace top purifies the gas pipe and removes CO₂Second furnace top gas purifying pipe for removing CO₂Top purified gas pipe III and CO removal₂The furnace top purifies the gas pipe four, remove CO₂The first furnace top gas purifying pipe is sequentially connected with a shaft furnace top gas compressor 17 and desulfurization-CO from top to bottom₂System 18, CO removal₂The gas outlet end of the furnace top purified gas pipe I and CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated to remove CO₂The gas outlet end of the second furnace top purified gas pipe is exchanged by coke oven gasAfter heating in a heater 83, CO is removed₂Top purified gas pipe III and CO removal₂The gas inlet end of the furnace top purifying gas pipe IV is communicated for removing CO₂The gas outlet end of the furnace top purified gas pipe III is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace for removing CO₂The gas outlet end of the furnace top purified gas pipe IV passes through the biomass gas heat exchanger 93 and then is subjected to CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated.

The discharge end of the cooling section of the gas-based shaft furnace 1 is connected with a thermal cycle gas heat exchanger 01, the outlet of a first hot gas heat exchanger 13 at the top of the gas-based shaft furnace is communicated with the inlet of the thermal cycle gas heat exchanger 01, and the outlet of the thermal cycle gas heat exchanger 01 is communicated with the inlet of a gas pipeline of a burner 3 on a non-catalytic partial oxidation reformer 2.

Further, the reducing gas preparation system for the gas-based shaft furnace by using the biomass gas further comprises a gas-based shaft furnace cooling section dust remover 02, a gas-based shaft furnace cooling section compressor 03, a gas-based shaft furnace cooling section thermal circulation gas pipe 82 and a supplementary coke oven gas pipe 81, and the CO removal is carried out₂The furnace top clean gas pipe 121 also includes CO removal₂The gas inlet end of a gas-based shaft furnace cooling section thermal circulation gas pipe 82 is communicated with the cooling section discharge end of the gas-based shaft furnace 1, the gas outlet end of the gas-based shaft furnace cooling section thermal circulation gas pipe 82 is communicated with the bottom of the gas-based shaft furnace 1, and the gas-based shaft furnace cooling section thermal circulation gas pipe 82 is arranged from top to bottomThe secondary connection is provided with a thermal cycle gas heat exchanger 01, a gas-based shaft furnace cooling section dust remover 02 and a gas-based shaft furnace cooling section compressor 03, the gas outlet end of a supplementary coke oven gas pipe 81 is communicated with a gas-based shaft furnace cooling section thermal cycle gas pipe 82, the connection part is arranged between the gas-based shaft furnace cooling section dust remover 02 and the gas-based shaft furnace cooling section compressor 03, and CO is removed₂The gas inlet end of the furnace top purifying gas pipe six and CO removal₂The gas outlet end of the furnace top purified gas pipe I is communicated for removing CO₂The gas outlet end of the furnace top purified gas pipe VI passes through the thermal cycle gas heat exchanger 01 and then is subjected to CO removal₂The gas outlet ends of the furnace top purified gas pipe III are communicated.

Referring to fig. 3, a method for producing reducing gas by using biomass gas in a gas-based shaft furnace is described, which is different from the embodiment of fig. 1 in that:

uniformly mixing the biomass gas 9 and the coke oven gas 8 according to the ratio of 1:9 to obtain mixed gas, pressurizing the mixed gas (in a mixed gas pipe 5) to 0.8MPa by a mixed gas compressor 52, wherein the components of the mixed gas are CO: 12.44, CH₄：24.31、H₂：51.06、CO₂：3.9、N₂：4.06、CmHn：3.83。

And (3) performing anoxic combustion on pure oxygen and mixed coal gas at the outlet of the burner 3, wherein the proportion of the pure oxygen in the mixed coal gas is about 24%, and the components of generated reducing gas are about CO: 26.03, CH₄：1.2、H₂：56.86、CO₂：2.5、N₂：2.6、H₂O: 13.1, at the outlet of the non-catalytic partial oxidation reformer 2, the reducing gas (in the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation reformer) is about 1300 ℃.

Top purified gas (CO removal)₂In the furnace top purified gas pipe 121), hot biomass gas 9, hot coke oven gas 8 and hot circulating gas (in the hot circulating gas pipe 82 of the cooling section of the gas-based shaft furnace) discharged from the cooling section of the gas-based shaft furnace exchange heat in the biomass gas heat exchanger 93, the coke oven gas heat exchanger 83 and the hot circulating gas heat exchanger 01 respectively, and after heat exchange, all branches are gathered into hot furnace top purified gas which is then mixed with 1300 ℃ reducing gas at the outlet of the non-catalytic partial oxidation reforming furnace 2 to form mixed reducing gas, wherein the temperature of the mixed reducing gas is about 1050 ℃, and the mixed reducing gas enters the gas-based shaft furnace through a tuyere 11 of the shaft furnace1。

Hot circulating gas exhausted from the cooling section of the gas-based shaft furnace passes through a hot circulating gas heat exchanger 01 and a dust remover 02 of the cooling section of the gas-based shaft furnace, is supplemented with coke oven gas (in a supplementing coke oven gas pipe 81), and then enters the bottom of the gas-based shaft furnace through a compressor 03 of the cooling section of the gas-based shaft furnace.

If a higher temperature biomass gas is used, for example, the biomass gas generated in the biomass gas producer at a thermal cracking temperature of about 850-950 ℃ (typical components of the biomass gas are CO: 36.03 and CH)₄：14.74、H₂：31.06、CO₂：12.75、N₂: 2. CmHn: 1.14) mixing the coke oven gas with the process according to the figure at a ratio of 6:4, purifying, pressurizing and partially oxidizing the non-catalytic part to generate reducing gas with the components of CO: 30.93, CH₄：1.12、H₂：47.56、CO₂：6.22、N₂：2.06、H₂O：12.1。

Example four

This embodiment is described with reference to fig. 4:

the reducing gas preparation system for the gas-based shaft furnace using the biomass gas comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas producer 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas producer 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia cooling nozzles 6 are respectively arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with a gas inlet end of a mixed gas collecting pipe 81, a gas outlet end of the mixed gas collecting pipe 81 is communicated with a gas inlet end of a mixed gas pipe 5, the mixed gas pipe 5 is sequentially connected with a mixed gas purification system 51 and a mixed gas compressor 52 from top to bottom, the gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic part oxidation converter 2, and the non-catalytic part is communicated with the gas pipelineThe oxygen pipeline and the steam pipeline of the burner 3 of the oxidation reforming furnace 2 are also respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reforming furnace 2 is communicated with a shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a non-catalytic partial oxidation furnace outlet reducing gas pipe 21, and a gas outlet end of a shaft furnace top hot gas pipe 12 communicated with the upper part of the gas-based shaft furnace is respectively communicated with a CO removal hot gas pipe 12₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet ends of the gas pipe 122 at the top of the gas-based shaft furnace are communicated without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

Further, the CO removal₂The furnace top clean gas pipe 121 includes CO removal₂The furnace top purifies the gas pipe and removes CO₂Second furnace top gas purifying pipe for removing CO₂Top purified gas pipe III and CO removal₂The top of the furnace purifies the gas pipe four, remove CO₂The first furnace top gas purifying pipe is sequentially connected with a shaft furnace top gas compressor 17 and desulfurization-CO from top to bottom₂System 18, CO removal₂The gas outlet end of the furnace top purifying gas pipe I and CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated to remove CO₂The gas outlet end of the second furnace top purified gas pipe passes through the coke oven gas heat exchanger 83 and is respectively in contact with the CO removal gas₂Top purified gas pipe III and CO removal₂The inlet end of the furnace top purifying gas pipe IV is communicated to remove CO₂The gas outlet end of the furnace top purified gas pipe III is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace for removing CO₂For cleaning gas pipe on top of furnaceThe gas outlet end passes through the biomass gas heat exchanger 93 and then is subjected to CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated.

The shaft furnace top hot gas pipe 12 is sequentially connected with a shaft furnace hot gas heat exchanger group and a dust removal device 16 from top to bottom, the shaft furnace hot gas heat exchanger group comprises a gas-based shaft furnace top hot gas heat exchanger II 14 and a gas-based shaft furnace top hot gas heat exchanger III 15, an oxygen pipe 4 is communicated with an oxygen pipeline of a burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through the gas-based shaft furnace top hot gas heat exchanger II 14, a steam pipe 7 is communicated with a steam pipeline of the burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through the gas-based shaft furnace top hot gas heat exchanger III 15, and an air outlet end of a mixed gas pipe 5 is communicated with a gas pipeline of the burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through a coke oven gas heat exchanger 83.

Referring to fig. 4, a method for producing reducing gas by using biomass gas in a gas-based shaft furnace is described, which is different from the embodiment of fig. 1 in that:

the mixed gas of the biomass gas 9 and the coke oven gas 8 is preheated by a part of coke oven gas heat exchanger 83 and then enters a gas channel of a burner 3 of the non-catalytic partial oxidation reformer 2.

EXAMPLE five

This embodiment is described with reference to fig. 5:

the reducing gas preparation system for the gas-based shaft furnace by using the biomass gas comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas generating furnace 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas generating furnace 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia water cooling nozzles 6 are respectively arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, the coal gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with the coal gas inlet end of the mixed gas collecting pipe 81, and the coal gas outlet end of the mixed gas collecting pipe 81.The mixed gas pipe 5 is sequentially connected with a mixed gas purification system 51 and a mixed gas compressor 52 from first to last, the gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2, the oxygen pipeline and the steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reformer 2 is communicated with the shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, the gas outlet end of a hot gas pipe 12 at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with a CO removal shaft furnace₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet ends of the gas pipe 122 at the top of the gas-based shaft furnace are communicated without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purifying gas pipe 121 is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

The coke oven gas riser 84 is provided with a coke oven gas heat exchanger 83, the biomass gas riser 94 is provided with a biomass gas heat exchanger 93, the hot flue gas discharge pipe 91 of the biomass generator is provided with a biomass generator flue gas heat exchanger 092, and the CO removal is carried out₂The outlet gas end of the furnace top purified gas pipe 121 is respectively communicated with the inlets of the coke oven gas heat exchanger 83, the biomass gas heat exchanger 93 and the biomass generator flue gas heat exchanger 092, and the outlet pipelines of the coke oven gas heat exchanger 83, the biomass gas heat exchanger 93 and the biomass generator flue gas heat exchanger 092 are communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace after being gathered.

Further, the CO removal₂The furnace top clean gas pipe 121 includes CO removal₂The furnace top purifies the gas pipe and removes CO₂Second furnace top gas purifying pipe for removing CO₂Top purified gas pipe III and CO removal₂The top of the furnace purifies the gas pipe four, remove CO₂The first furnace top gas purification pipe is sequentially connected with a shaft furnace top gas compressor 17 and desulfurization-CO from top to bottom₂System 18, CO removal₂The gas outlet end of the furnace top purifying gas pipe I and CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated to remove CO₂The gas outlet end of the second furnace top purified gas pipe passes through the coke oven gas heat exchanger 83 and then is respectively subjected to CO removal₂Top purified gas pipe III and CO removal₂The inlet end of the furnace top purifying gas pipe IV is communicated to remove CO₂The gas outlet end of the furnace top purified gas pipe III is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace for removing CO₂The gas outlet end of the furnace top purified gas pipe IV passes through the biomass gas heat exchanger 93 and then is subjected to CO removal₂The gas inlet end of the furnace top purifying gas pipe II is communicated.

The shaft furnace top hot gas pipe 12 is sequentially connected with a shaft furnace hot gas heat exchanger group and a dust removal device 16 from top to bottom, the shaft furnace hot gas heat exchanger group comprises a gas-based shaft furnace top hot gas heat exchanger II 14 and a gas-based shaft furnace top hot gas heat exchanger III 15, an oxygen pipe 4 is communicated with an oxygen pipeline of a burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through the gas-based shaft furnace top hot gas heat exchanger II 14, a steam pipe 7 is communicated with a steam pipeline of the burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through the gas-based shaft furnace top hot gas heat exchanger III 15, and an air outlet end of a mixed gas pipe 5 is communicated with a gas pipeline of the burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through a biomass generation furnace flue gas heat exchanger 092.

Furthermore, the system for preparing the reducing gas by using the biomass gas for the gas-based shaft furnace also comprises a biomass producer medium ball heating lifting chamber 091 for removing CO₂The furnace top gas purification pipe 121 further comprises CO removal₂The furnace top purification gas pipe five is characterized in that a biomass producer medium ball heating lifting chamber 091 is arranged on one side of the biomass gas producer 09, a biomass producer flue gas pipe 91 is communicated with the biomass producer medium ball heating lifting chamber 091, a biomass producer flue gas heat exchanger 092 is connected to the biomass producer flue gas pipe 91, and CO is removed₂The gas inlet end of the furnace top purifying gas pipe five and CO removal₂The inlet end of the furnace top purifying gas pipe IV is communicated to remove CO₂The gas outlet end of the furnace top purified gas pipe five and CO removal₂The gas outlet end of the furnace top purified gas pipe IV is communicated to remove CO₂Top purified gas pipe fivePasses through a biomass producer flue gas heat exchanger 092.

A method for producing reducing gas by using biomass gas in a gas-based shaft furnace is described with reference to fig. 5, which is different from the second embodiment of fig. 2 in that:

the mixed gas of the biomass gas 9 and the coke oven gas 8 is preheated by a biomass generator flue gas heat exchanger 092 and then enters a gas channel of a burner 3 of the non-catalytic partial oxidation reformer 2.

Example six

The present embodiment is explained with reference to fig. 6:

the reducing gas preparation system for the gas-based shaft furnace using the biomass gas comprises a gas-based shaft furnace 1, a non-catalytic partial oxidation reformer 2, a coke oven 08, a biomass gas producer 09, an oxygen source and a steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas producer 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia cooling nozzles 6 are respectively arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with a gas inlet end of a mixed gas collecting pipe 81, a gas outlet end of the mixed gas collecting pipe 81 is communicated with a gas inlet end of a mixed gas pipe 5, the mixed gas pipe 5 is sequentially connected with a mixed gas purification system 51 and a mixed gas compressor 52 from first to last, the gas outlet end of the mixed gas pipe 5 is communicated with the gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2, the oxygen pipeline and the steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reformer 2 is communicated with the shaft furnace tuyere 11 of the gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, and the gas outlet end of a hot gas pipe 12 at the top of the shaft furnace communicated with the upper part of the gas-based shaft furnace is respectively communicated with a CO removal furnace₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated withWithout CO removal₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

The coke oven gas riser 84 is provided with a coke oven gas heat exchanger 83, the biomass gas riser 94 is provided with a biomass gas heat exchanger 93, and the CO removal is carried out₂The gas outlet end of the furnace top purified gas pipe 121 is respectively communicated with the inlets of the coke oven gas heat exchanger 83 and the biomass gas heat exchanger 93, and the outlet pipelines of the coke oven gas heat exchanger 83 and the biomass gas heat exchanger 93 are communicated with the reducing gas pipe 21 at the outlet of the non-catalytic part oxidation furnace after being gathered.

The discharge end of the cooling section of the gas-based shaft furnace 1 is connected with a thermal cycle gas heat exchanger 01, the outlet of a first hot gas heat exchanger 13 at the top of the gas-based shaft furnace is communicated with the inlet of the thermal cycle gas heat exchanger 01, and the outlet of the thermal cycle gas heat exchanger 01 is communicated with the inlet of a gas pipeline of a burner 3 on a non-catalytic partial oxidation reforming furnace 2.

Further, the reducing gas preparation system for the gas-based shaft furnace by using the biomass gas further comprises a gas-based shaft furnace cooling section dust remover 02, a gas-based shaft furnace cooling section compressor 03, a gas-based shaft furnace cooling section thermal circulation gas pipe 82 and a supplementary coke oven gas pipe 81, wherein the gas inlet end of the gas-based shaft furnace cooling section thermal circulation gas pipe 82 is communicated with the cooling section discharge end of the gas-based shaft furnace 1, the gas outlet end of the gas-based shaft furnace cooling section thermal circulation gas pipe 82 is communicated with the bottom of the gas-based shaft furnace 1, the gas-based shaft furnace cooling section thermal circulation gas pipe 82 is sequentially connected with a thermal circulation gas heat exchanger 01, the gas-based shaft furnace cooling section dust remover 02 and the gas-based shaft furnace cooling section compressor 03 from first to last, the gas outlet end of the supplementary coke oven gas pipe 81 is communicated with the gas-based shaft furnace cooling section thermal circulation gas pipe 82, and the connection is arranged between the dust remover 02 of the cooling section of the gas-based shaft furnace and the compressor 03 of the cooling section of the gas-based shaft furnace;

the shaft furnace top hot gas pipe 12 is sequentially connected with a shaft furnace hot gas heat exchanger group and a dust removal device 16 from top to bottom, the shaft furnace hot gas heat exchanger group comprises a gas-based shaft furnace top hot gas heat exchanger II 14 and a gas-based shaft furnace top hot gas heat exchanger III 15, an oxygen pipe 4 is communicated with an oxygen pipeline of a burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through the gas-based shaft furnace top hot gas heat exchanger II 14, a steam pipe 7 is communicated with a steam pipeline of the burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through the gas-based shaft furnace top hot gas heat exchanger III 15, and an air outlet end of a mixed gas pipe 5 is communicated with a gas pipeline of the burner 3 of the non-catalytic partial oxidation reforming furnace 2 after passing through a gas-based shaft furnace cooling section heat exchanger 01.

The method for preparing the reducing gas by using the biomass gas for the gas-based shaft furnace is described by combining the sixth figure, and the difference from the third embodiment of the figure 3 is that:

the mixed gas of the biomass gas 9 and the coke oven gas 8 is preheated by a thermal cycle gas heat exchanger 01 and then enters a gas channel of a burner 3 of a non-catalytic partial oxidation reformer 2.

EXAMPLE seven

This embodiment is described with reference to fig. 7:

the reducing gas preparation system for the gas-based shaft furnace by using the biomass gas comprises the gas-based shaft furnace 1 and a non-catalytic partial oxidationThe reformer 2, the coke oven 08, the biomass gas producer 09, the oxygen source and the steam source, wherein a gas outlet end of the coke oven 08 is communicated with a gas inlet end of a coke oven gas riser 84, a gas outlet end of the coke oven gas riser 84 is communicated with a gas inlet end of a coke oven gas bridge pipe 82, a gas outlet end of the biomass gas producer 09 is communicated with a gas inlet end of a biomass gas riser 94, a gas outlet end of the biomass gas riser 94 is communicated with a gas inlet end of a biomass gas bridge pipe 92, ammonia water cooling nozzles 6 are respectively arranged in the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92, gas outlet ends of the coke oven gas bridge pipe 82 and the biomass gas bridge pipe 92 are respectively communicated with a gas inlet end of a mixed gas collecting pipe 81, a gas outlet end of the mixed gas collecting pipe 81 is communicated with a gas inlet end of a mixed gas pipe 5, the mixed gas purifying system 51 and the mixed gas compressor 52 are sequentially connected to the mixed gas pipe 5 from top to bottom, the coal gas outlet end of a mixed coal gas pipe 5 is communicated with a coal gas pipeline of a burner 3 of a non-catalytic partial oxidation reformer 2, an oxygen pipeline and a steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 are respectively communicated with an oxygen source and a steam source through an oxygen pipe 4 and a steam pipe 7, the non-catalytic partial oxidation reformer 2 is communicated with a shaft furnace tuyere 11 of a gas-based shaft furnace 1 through a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace, and the coal gas outlet end of a hot coal gas pipe 12 at the top of the shaft furnace, which is communicated with the upper part of the gas-based shaft furnace, is respectively communicated with a CO removal furnace₂Top of furnace clean gas pipe 121 and without CO removal₂The gas inlet ends of the gas pipe 122 at the top of the gas-based shaft furnace are communicated without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe 121 is communicated with the reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace.

The shaft furnace top hot gas pipe 12 is sequentially connected with a shaft furnace hot gas heat exchanger group and a dust removal device 16 from top to bottom, the shaft furnace hot gas heat exchanger group comprises a gas-based shaft furnace top hot gas heat exchanger I13, an oxygen pipe 4 is communicated with an oxygen pipeline of a burner 3 of the non-catalytic partial oxidation reformer 2 after passing through a biomass gas heat exchanger 93, a steam pipe 7 is communicated with a steam pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 after passing through a coke oven gas heat exchanger 83, and an air outlet end of a mixed gas pipe 5 is communicated with a gas pipeline of the burner 3 of the non-catalytic partial oxidation reformer 2 after passing through the gas-based shaft furnace top hot gas heat exchanger I13;

the reducing gas preparation system for the gas-based shaft furnace by using the biomass gas also comprises a tubular heating furnace for removing CO₂The furnace top gas purifying pipe 121 is sequentially connected with a shaft furnace top gas compressor 17 and desulfurization-CO from first to last₂System 18 and tube furnace, CO removal₂The gas outlet end of the furnace top purifying gas pipe 121 is communicated with a reducing gas pipe 21 at the outlet of the non-catalytic partial oxidation furnace without removing CO₂The gas outlet end of the gas pipe 122 at the top of the gas-based shaft furnace is discharged after passing through the tubular heating furnace.

The seventh embodiment of the utility model is combined with a seventh embodiment to describe a method for preparing reducing gas by using biomass gas in a gas-based shaft furnace, which is different from the first embodiment of the seventh embodiment of the utility model in that:

top purified gas (CO removal)₂In the furnace top purified gas pipe 121) does not enter the biomass gas heat exchanger 93 and the coke oven gas heat exchanger 83 respectively for heat exchange, but adopts a fuel indirect heating mode, such as heating by the tubular heating furnace 1. Heating fuel with undeco₂Gas-based shaft furnace top gas (without CO removal)₂In the gas-based shaft furnace top gas pipe 122), top purified gas (CO removal)₂In the top purge gas pipe 121) is heated in the tubular heating furnace 1. The biomass gas heat exchanger 93 is used to preheat pure oxygen (in the oxygen pipe 4), and the coke oven gas heat exchanger 83 is used to produce steam.

In addition to the method for preheating the mixed gas of the biomass gas 9 and the coke oven gas 8, the mixed gas of the biomass gas 9 and the coke oven gas 8 can be preheated by using dry quenching high-temperature nitrogen through a heat exchanger.

It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the present application. As used herein, the singular is intended to include the plural unless the context clearly dictates otherwise, and it should be further understood that the terms "comprises" and/or "comprising," when used in this specification, specify the presence of features, steps, operations, devices, components, and/or combinations thereof.

It should be noted that the terms "first," "second," and the like in the description and claims of this application and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It is to be understood that the data so used is interchangeable under appropriate circumstances such that the embodiments of the application described herein are capable of operation in sequences other than those illustrated or otherwise described herein. Moreover, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A system for preparing reducing gas by using biomass gas in a gas-based shaft furnace is characterized in that: the device comprises a gas-based shaft furnace (1), a non-catalytic partial oxidation converter (2), a coke oven (08), a biomass gas generating furnace (09), an oxygen source and a steam source, wherein a gas outlet end of the coke oven (08) is communicated with a gas inlet end of a coke oven gas riser (84), and a gas outlet end of the coke oven gas riser (84)The end of the mixed gas is communicated with the gas inlet end of a coke oven gas bridge pipe (82), the gas outlet end of a biomass gas producer (09) is communicated with the gas inlet end of a biomass gas ascending pipe (94), the gas outlet end of the biomass gas ascending pipe (94) is communicated with the gas inlet end of the biomass gas bridge pipe (92), ammonia water cooling spray heads (6) are respectively arranged in the coke oven gas bridge pipe (82) and the biomass gas bridge pipe (92), the gas outlet ends of the coke oven gas bridge pipe (82) and the biomass gas bridge pipe (92) are respectively communicated with the gas inlet end of a mixed gas collecting pipe (81), the gas outlet end of the mixed gas collecting pipe (81) is communicated with the gas inlet end of a mixed gas pipe (5), the mixed gas pipe (5) is sequentially connected with a mixed gas purification system (51) and a mixed gas compressor (52) from first to last, the gas outlet end of the mixed gas pipe (5) is communicated with the gas pipeline of a non-catalytic partial oxidation converter (2), the oxygen pipeline and the steam pipeline of the burner (3) of the non-catalytic partial oxidation reformer (2) are also respectively communicated with an oxygen source and a steam source through an oxygen pipe (4) and a steam pipe (7), the non-catalytic partial oxidation reformer (2) is communicated with a shaft furnace tuyere (11) of the gas-based shaft furnace (1) through a non-catalytic partial oxidation furnace outlet reducing gas pipe (21), and the gas outlet end of a shaft furnace top hot gas pipe (12) communicated with the upper part of the gas-based shaft furnace is respectively communicated with a CO removal hot gas pipe (12)₂The top of the furnace purifies the gas pipe (121) and does not remove CO₂The gas inlet ends of the gas-based shaft furnace top gas pipe (122) are communicated without removing CO₂The gas outlet end of the gas pipe (122) at the top of the gas-based shaft furnace is communicated with other user pipe networks for removing CO₂The gas outlet end of the furnace top purified gas pipe (121) is communicated with a reducing gas pipe (21) at the outlet of the non-catalytic partial oxidation furnace.

2. A reducing gas preparation system for a gas-based shaft furnace using a biomass gas according to claim 1, wherein: a coke oven gas heat exchanger (83) is arranged on the coke oven gas riser (84), and the CO is removed₂The gas outlet end of the furnace top purified gas pipe (121) is communicated with the inlet of a coke oven gas heat exchanger (83), and the outlet pipeline of the coke oven gas heat exchanger (83) is communicated with a reducing gas pipe (21) at the outlet of a non-catalytic part oxidation furnace.

3. According to the claimsThe system for preparing the reducing gas by using the biomass gas in the gas-based shaft furnace is characterized by comprising the following steps of: the coke oven gas riser (84) is provided with a coke oven gas heat exchanger (83), the biomass gas riser (94) is provided with a biomass gas heat exchanger (93), and the CO removal is carried out₂The coal gas outlet end of the furnace top purified gas pipe (121) is respectively communicated with the inlets of the coke oven gas heat exchanger (83) and the biomass gas heat exchanger (93), and the outlet pipelines of the coke oven gas heat exchanger (83) and the biomass gas heat exchanger (93) are communicated with the reducing gas pipe (21) at the outlet of the non-catalytic partial oxidation furnace after being gathered.

4. A reducing gas preparation system for a gas-based shaft furnace using a biomass gas according to claim 1, wherein: the coke oven gas ascending pipe (84) is provided with a coke oven gas heat exchanger (83), the biomass gas ascending pipe (94) is provided with a biomass gas heat exchanger (93), the hot flue gas discharge pipe (91) of the biomass generator is provided with a biomass generator flue gas heat exchanger (092), and the CO removal is carried out₂The coal gas outlet end of the furnace top purified gas pipe (121) is respectively communicated with inlets of a coke oven gas heat exchanger (83), a biomass gas heat exchanger (93) and a biomass generator flue gas heat exchanger (092), and outlet pipelines of the coke oven gas heat exchanger (83), the biomass gas heat exchanger (93) and the biomass generator flue gas heat exchanger (092) are communicated with a reducing gas pipe (21) at an outlet of a non-catalytic part oxidation furnace after being converged.

5. A reducing gas preparation system for a gas-based shaft furnace using a biomass gas according to claim 1, wherein: the mixed gas pipe (5) is also communicated with a first gas-based shaft furnace top hot gas heat exchanger (13), and the first gas-based shaft furnace top hot gas heat exchanger (13) is arranged between the outlet of the mixed gas compressor (52) and the inlet of a gas pipeline of a burner (3) on the non-catalytic partial oxidation converter (2).

6. The reducing gas production system for a gas-based shaft furnace using a biomass gas according to claim 5, wherein: the exhaust end of the cooling section of the gas-based shaft furnace (1) is connected with a thermal cycle gas heat exchanger (01), the outlet of a first hot gas heat exchanger (13) at the top of the gas-based shaft furnace is communicated with the inlet of the thermal cycle gas heat exchanger (01), and the outlet of the thermal cycle gas heat exchanger (01) is communicated with the inlet of a gas pipeline of a burner (3) on the non-catalytic partial oxidation reforming furnace (2).