CN114657305A - Energy gradient utilization system and method for coupling production of gas-based shaft furnace and coke oven - Google Patents
Energy gradient utilization system and method for coupling production of gas-based shaft furnace and coke oven Download PDFInfo
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- CN114657305A CN114657305A CN202210413926.8A CN202210413926A CN114657305A CN 114657305 A CN114657305 A CN 114657305A CN 202210413926 A CN202210413926 A CN 202210413926A CN 114657305 A CN114657305 A CN 114657305A
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- 239000000571 coke Substances 0.000 title claims abstract description 208
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 34
- 230000008878 coupling Effects 0.000 title claims description 19
- 238000010168 coupling process Methods 0.000 title claims description 19
- 238000005859 coupling reaction Methods 0.000 title claims description 19
- 239000007789 gas Substances 0.000 claims abstract description 624
- 230000003647 oxidation Effects 0.000 claims abstract description 75
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 75
- 230000003197 catalytic effect Effects 0.000 claims abstract description 61
- 238000010438 heat treatment Methods 0.000 claims abstract description 19
- 238000007599 discharging Methods 0.000 claims abstract description 5
- 230000001174 ascending effect Effects 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 15
- 238000002485 combustion reaction Methods 0.000 claims description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 6
- 239000003546 flue gas Substances 0.000 claims description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 38
- 239000011261 inert gas Substances 0.000 abstract description 9
- 239000002912 waste gas Substances 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 4
- 238000010791 quenching Methods 0.000 abstract description 3
- 230000000171 quenching effect Effects 0.000 abstract description 3
- 239000002028 Biomass Substances 0.000 description 18
- 229910052742 iron Inorganic materials 0.000 description 14
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 12
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 10
- 239000000428 dust Substances 0.000 description 10
- 239000002918 waste heat Substances 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 8
- 230000018044 dehydration Effects 0.000 description 8
- 238000006297 dehydration reaction Methods 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 229910052717 sulfur Inorganic materials 0.000 description 6
- 239000011593 sulfur Substances 0.000 description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 description 4
- 239000003034 coal gas Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000008021 deposition Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000004227 thermal cracking Methods 0.000 description 3
- 239000013064 chemical raw material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
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- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
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- Industrial Gases (AREA)
Abstract
The invention relates to an energy gradient utilization system and an energy gradient utilization method for coupled production of a gas-based shaft furnace and a coke oven, in particular to a system and a method for utilizing heat energy of the gas-based shaft furnace and the coke oven, which are used for heating by using a tubular heating furnace and discharging CO in the prior art2And other waste gases, the direct reduced iron is produced by using a dry quenching coupled shaft furnace, and the heat exchange efficiency is low; increase the manufacturing investment and operating cost of inert gas; the top gas of the shaft furnace is completely used as reducing gas for recycling, so that the production efficiency and the normal production operation of production are influenced. The coke oven gas pipe is communicated with the non-catalytic partial oxidation converter, the coke oven gas pipe is arranged on the coke oven, the reducing gas pipe at the outlet of the oxidation converter is arranged on the non-catalytic partial oxidation converter, and the first branch pipe of the gas pipe at the top of the gas-based shaft furnace is desulfurized and subjected to CO removal2The system is connected with a coke oven gas riser pipe and an oxidation furnace outlet reduction gas pipe of the non-catalytic partial oxidation converter in parallel and is communicated with a shaft furnace tuyere of the gas-based shaft furnace, and a second branch pipe of a gas pipe at the top of the gas-based shaft furnace is communicated with an external gas pipeline. The invention belongs to the field of direct reduction.
Description
Technical Field
The invention belongs to the field of direct reduction, and relates to a system and a method for utilizing heat energy of a gas-based shaft furnace and a coke oven, in particular to a method for utilizing the heat energy gradient in coupling production of the gas-based shaft furnace and the coke oven.
Background
Currently, the existing gas-based shaft furnace process includes two basic methods, i.e., MIDREX and HYL, and other PREDE processes, HYL-ZERO processes, ENERGIRON processes, and the like, are developed on the basis of the two basic methods. The basic feature of these processes is that about 1/3 gas-based shaft furnace top gas is used as fuel to burn the raw material gas in the heating tube furnace. The disadvantages of this process are: a, CO2 and other waste gases are discharged by a mode of heating raw material gas by burning fuel; the investment of the b-tube type heating furnace is large. In response to the above problems, some solutions have been proposed in the prior art, such as application No. CN201280023094.3, entitled system and method for reducing iron oxide to metallic iron using coke oven gas and oxygen steelmaking furnace gas, proposing "minimizing equipment by eliminating external catalytic reformers and thus minimizing plant costs". However, the technology of the patent still partially uses a tubular heating furnace for heating, so that the problems of CO2 emission and other waste gases and high equipment investment still exist. For another example, application No. CN202010762774.3, entitled, a method for distributed utilization of heat in a process of producing direct reduced iron by dry quenching coupled shaft furnace, proposes to utilize high-temperature inert gas generated by a dry quenching furnace to exchange heat with cold reducing gas in a heat exchanger, and this patent uses the inert gas as a heat energy conversion medium of sensible heat of red coke and cold reducing gas to replace fuel part in raw material gas in the prior art to supply heat for a system, which is a way to solve the problem of discharging CO2 and other waste gases, but still has the following problems: a, heat exchange between the red coke and the cold reducing gas is realized by taking inert gas as a heat energy conversion medium, the inert gas loses energy in the two heat energy conversion processes, and the heat exchange efficiency is low; b, increasing the manufacturing investment and the operating cost of the inert gas; c, adding a power system and a dust removal system for inert gas circulation; d, adding a safety-guaranteed air distribution system; e, properly improving the content of CO in the reducing gas by adjusting the carbon-hydrogen ratio in the reducing gas to reduce the consumption of the reducing gas, which is a known technology; f, the top gas (furnace top gas) of the shaft furnace is completely used as reducing gas for cycle use, which can cause the enrichment of inert gas in the top gas and influence the production efficiency and the positive production operation of production. The present invention proposes a solution to the above problems.
Disclosure of Invention
In order to solve the technical problems, an energy gradient system and a gradient utilization method for coupled production of a gas-based shaft furnace and a coke oven are further provided.
The technical scheme adopted by the invention for solving the technical problems is as follows:
the method comprises the following steps: a part of top hot gas of the gas-based shaft furnace is cooled, dedusted, desulfurized and CO2Then the gas becomes the purified gas at the top of the gas-based shaft furnace;
step two: replacing coke oven gas with the same calorific value of the other part of the top hot gas of the gas-based shaft furnace, replacing the coke oven gas with the other part of the top hot gas for other purposes, preheating coke oven total gas formed by the replaced coke oven gas and newly supplemented coke oven gas, entering a non-catalytic partial oxidation converter for combustion and heating, and discharging the generated high-temperature reducing gas from an outlet of the non-catalytic partial oxidation converter;
step three: and (3) exchanging heat between the purified gas at the top of the gas-based shaft furnace in the first step and hot gas in a coke oven gas riser pipe, adding the purified gas into the high-temperature reducing gas at the outlet of the non-catalytic partial oxidation converter in the second step to form mixed reducing gas at 850-1100 ℃, and feeding the mixed reducing gas into the gas-based shaft furnace.
The device comprises a gas-based shaft furnace, a coke oven, a non-catalytic partial oxidation converter, an oxidation oven outlet reducing gas pipe, a coke oven gas pipe and a gas-based shaft furnace top gas pipe; the coke oven gas pipe is communicated with the non-catalytic partial oxidation converter, the coke oven gas pipe is arranged on the coke oven, the reducing gas pipe at the outlet of the oxidation converter is arranged on the non-catalytic partial oxidation converter, and the first branch pipe of the gas pipe at the top of the gas-based shaft furnace is subjected to CO removal2System and coke oven gas ascending pipe heat exchangerAnd then the reduction gas pipe at the outlet of the oxidation furnace of the non-catalytic partial oxidation converter is connected in parallel and then communicated with the blast hole of the gas-based shaft furnace, and the second branch pipe of the gas pipe at the top of the gas-based shaft furnace is communicated with an external gas pipeline.
Compared with the prior art, the invention has the following beneficial effects:
1. waste heat generated by the coke oven is used for heating the top of the gas-based shaft furnace to purify gas, and waste heat generated by the gas-based shaft furnace is used for heating coke oven gas, so that the unified management of the waste heat of the coke oven and the gas-based shaft furnace is realized, and the coupling utilization is more reasonable according to the temperature gradient; the low-temperature waste heat of the coke oven and the gas-based shaft furnace is selected to heat the coke oven gas, so that the problem of carbon deposition of the coke oven gas is avoided, and the high-temperature waste heat of the coke oven and the gas-based shaft furnace is selected to heat the purified gas at the top of the gas-based shaft furnace, so that the requirement of high temperature required by the purified gas at the top of the gas-based shaft furnace is met; the method of twice preheating is adopted, and the problem that the single heat source cannot reach the ideal heating temperature is solved. The scheme realizes the coupling gradient utilization of different waste heat sources of the coke oven and the gas-based shaft furnace.
2. The reasonable gradient utilization of different kinds of gas is realized by the mode of replacing the coke oven gas by the top gas of the gas-based shaft furnace and other calorific values. Namely: in one aspect, CO is not removed2The gas-based shaft furnace top gas replaces coke oven gas to serve other purposes, is not used as fuel gas of the gas-based shaft furnace any more, not only avoids the problem of smoke gas emission of combustion heating of the gas-based shaft furnace, but also solves the problem of N caused by recycling of the top gas in the gas-based shaft furnace2Enrichment problem; on the other hand, the replaced coke oven gas is used for the non-catalytic partial oxidation furnace, and the requirement that the non-catalytic partial oxidation furnace needs to take the hydrocarbon-rich gas as the raw material is met. In addition, the gas-based shaft furnace can be recycled by self-produced gas energy self-circulation through a mode of replacing coke oven gas with the equal heat value of the top gas of the gas-based shaft furnace.
3. By adopting different heating modes for coal gases with different properties, at least 3 purposes are realized: a, the problem of carbon deposition caused by heating of coke oven gas is avoided; b, realizing no waste gas emission in the whole reducing gas preparation process; c, removing CO by improving the preheating temperature of the coke oven gas and the top gas of the gas-based shaft furnace2The temperature of the purified gas is reduced, thereby reducing the water and CO in the reducing gas entering the gas-based shaft furnace2The content of the effective components of the reducing gas is improved: on the one hand, on the premise of no carbon deposition of the coke oven gas, the higher the preheating temperature of the coke oven gas is, the less the coke oven gas is burnt in the non-catalytic partial oxidation furnace, and water and CO in the generated reducing gas2The lower the proportion, the higher the effective content of the reducing gas, on the other hand, the water and CO due to the top of the furnace purifying the gas2The content can be reduced to the target requirement by controlling, so that after the high-temperature reducing gas at the outlet of the non-catalytic partial oxidation furnace is mixed, the effective components of the mixed reducing gas can be improved, and the mixing amount of the top purified gas can be increased by preheating the top purified gas, so that the effective components of the mixed reducing gas can be further improved.
4. The method is used for heating the purified gas after CO2 is removed from the top of the gas-based shaft furnace by adopting a heat exchange mode with hot gas in a rising pipe of the coke oven for the first time. Solves the problem of 'using inert gas as the heat exchange mode of the energy conversion medium between the red coke and the reducing gas'.
5. The coke oven gas is preheated by hot circulating gas discharged from the cooling section of the gas-based shaft furnace and hot gas at the top of the gas-based shaft furnace for the first time. The preheating mode is adopted twice for the first time, and the temperature of the preheated gas is improved.
Drawings
FIG. 1 is a flow chart of a heat gradient utilization system for coupled production of a gas-based shaft furnace and a coke oven according to a first aspect of the present invention;
FIG. 2 is a flow chart of a heat gradient utilization system for coupled production of a second gas-based shaft furnace and a coke oven according to the present invention;
FIG. 3 is a flow chart of a heat gradient utilization system for coupled production of a third gas-based shaft furnace and a coke oven according to the present invention;
Detailed Description
The first embodiment is as follows: the embodiment is described by combining the figures 1-3, and the energy gradient utilization method for coupled production of the gas-based shaft furnace and the coke oven is realized according to the following steps:
the method comprises the following steps: a part of top hot gas of the gas-based shaft furnace 1 is cooled, dedusted, desulfurized and CO2Then the gas becomes the purified gas at the top of the gas-based shaft furnace;
step two: replacing coke oven gas by the other part of the top hot gas of the gas-based shaft furnace 1 with the same calorific value, replacing the coke oven gas by the other part of the top hot gas for other purposes, preheating the coke oven total gas formed by the replaced coke oven gas and newly supplemented coke oven gas, entering the non-catalytic partial oxidation converter 2 for combustion and heating, and discharging the generated high-temperature reducing gas from the outlet of the non-catalytic partial oxidation converter 2;
step three: and (3) after heat exchange is carried out between the purified gas at the top of the gas-based shaft furnace in the first step and hot gas in a coke oven gas riser pipe, adding the purified gas into the high-temperature reducing gas at the outlet of the non-catalytic partial oxidation conversion furnace 2 in the second step to obtain mixed reducing gas at the temperature of 850-1100 ℃, and feeding the mixed reducing gas into the gas-based shaft furnace.
The second embodiment is as follows: the embodiment is described with reference to fig. 1 to fig. 3, and in the energy gradient utilization method for coupled production of the gas-based shaft furnace and the coke oven according to the embodiment, in the second step, the total coke oven gas is preheated by heat exchange with hot gas at the top of the gas-based shaft furnace 1. The other modes are the same as the first embodiment.
The third concrete implementation mode: in the energy gradient utilization method for coupled production of the gas-based shaft furnace and the coke oven according to the present embodiment, after the total coke oven gas preheated by the hot gas at the top of the gas-based shaft furnace is preheated, the total coke oven gas is further preheated by the hot circulating gas exhausted from the cooling section of the gas-based shaft furnace 1. The other modes are the same as the second embodiment.
The fourth concrete implementation mode is as follows: the embodiment is described with reference to fig. 2 to 3, and the energy gradient utilization method for coupling production of the gas-based shaft furnace and the coke oven in the embodiment exchanges heat with hot flue gas of a coke oven flue before exchanging heat between purified gas at the top of the gas-based shaft furnace and hot gas in a coke oven gas riser. The other modes are the same as the first embodiment.
The fifth concrete implementation mode: the embodiment is described with reference to fig. 2 to 3, and the energy gradient utilization method for coupling production of the gas-based shaft furnace and the coke oven according to the embodiment includes the third step of dividing the coke oven gas ascending pipes into two groups, and performing first heat exchange on purified gas at the top of the gas-based shaft furnace through the first group of coke oven gas ascending pipes and then performing second heat exchange and temperature rise through the second group of coke oven gas ascending pipes. The other modes are the same as the first embodiment.
The sixth specific implementation mode: the embodiment is described with reference to fig. 1 to fig. 3, and the energy gradient utilization system for coupling production of the gas-based shaft furnace and the coke oven in the embodiment comprises a gas-based shaft furnace 1, a coke oven, a non-catalytic partial oxidation converter 2, an oxidation oven outlet reducing gas pipe 21, a coke oven gas pipe and a gas-based shaft furnace top gas pipe; the coke oven gas pipe is communicated with the non-catalytic partial oxidation converter 2, the coke oven gas pipe is arranged on a coke oven, the reducing gas pipe 21 at the outlet of the oxidation furnace is arranged on the non-catalytic partial oxidation converter 2, and the first branch pipe of the gas base shaft furnace top gas pipe is sequentially subjected to desulfurization and CO removal2The system 18 is connected with a reducing gas pipe 21 at the outlet of an oxidation furnace of a non-catalytic partial oxidation conversion furnace 2 in parallel after being connected with a heat exchanger of a coke oven gas ascending pipe, and then is communicated with a shaft furnace tuyere 11 of a gas-based shaft furnace 1, and a second branch pipe of a gas pipe at the top of the gas-based shaft furnace is communicated with an external gas pipeline. Desulfurization and CO removal2The system 18 includes a sulfur removal unit and a CO removal unit2Provided is a device.
The seventh embodiment: the embodiment is described with reference to fig. 1 to fig. 3, and the energy gradient utilization system produced by coupling the gas-based shaft furnace and the coke oven according to the embodiment is characterized in that the coke oven is communicated with a hot gas heat exchanger at the top of the gas-based shaft furnace 1 through a coke oven gas pipe and then is communicated with a non-catalytic partial oxidation converter 2. The other components are the same as those in the sixth embodiment.
The specific implementation mode is eight: the embodiment is described with reference to fig. 2, and the coke oven is communicated with a hot gas heat exchanger at the top of the gas-based shaft furnace 1 and a hot circulating gas heat exchanger discharged from a cooling section of the gas-based shaft furnace through coke oven gas pipes and then communicated with a non-catalytic partial oxidation converter 2. The other components are the same as those in the sixth embodiment.
The specific implementation method nine: the present embodiment will be described with reference to fig. 2, and the present embodiment describes an energy gradient utilization system for coupled production of a gas-based shaft furnace and a coke oven, i.e., a gas-based shaft furnace 1The first branch pipe of the top gas pipe is sequentially desulfurized and CO is removed2The system 18, the coke oven flue hot flue gas heat exchanger and the coke oven gas riser heat exchanger are connected in parallel with the reducing gas pipe 21 at the outlet of the oxidation furnace of the non-catalytic partial oxidation conversion furnace 2. The other components are the same as those in the sixth embodiment.
The detailed implementation mode is ten: referring to FIG. 3, the present embodiment is described, and in the present embodiment, a first branch pipe of a top gas pipe of a gas-based shaft furnace 1 is sequentially subjected to desulfurization and CO removal2The system 18, a first coke oven gas riser heat exchanger 83 and a second coke oven gas riser heat exchanger 83 are arranged in parallel with the reducing gas pipe 21 at the outlet of the oxidation furnace of the non-catalytic partial oxidation conversion furnace 2. The other components are the same as those in the sixth embodiment.
The concrete implementation mode eleven: the embodiment will be described with reference to fig. 3, and the energy gradient utilization system for the coupled production of the gas-based shaft furnace and the coke oven of the embodiment is used for removing sulfur and CO2The gas-based shaft furnace top gas pipeline behind the system 18 is divided into n branch pipelines, each branch pipeline is communicated with the inlets of n coke oven gas ascending pipe heat exchangers 83 of a first coke oven, the outlets of the n coke oven gas ascending pipe heat exchangers 83 are converged into a first main pipe, the first main pipe is divided into n branch pipelines, each branch pipeline is communicated with the inlets of the n coke oven gas ascending pipe heat exchangers 83 of a second coke oven, the outlets of the n coke oven gas ascending pipe heat exchangers 83 are converged into a second main pipe, and the second main pipe is connected with the outlet pipeline of the non-catalytic partial oxidation furnace 2 in parallel.
The first embodiment is as follows: as described with reference to fig. 1;
biomass gas (typical components of biomass gas are CO: 51.76, CH)4：14.51、H2：8.41、CO2：13.5、N2: 2.37, CmHn: 6.62) is communicated with a gas collecting pipe 81 through a biomass gas bridge pipe 9, coke oven gas is communicated with the gas collecting pipe 81 through a coke oven gas pipe 8, a coke oven gas ascending pipe and a coke oven gas bridge pipe 82, the coke oven gas ascending pipe is provided with a coke oven gas ascending pipe heat exchanger 83, and biomass gas and coke oven gas (typical components of coke oven gas are CO: 8.07, CH4：25.4、H2：55.8、CO2：2.83、N2: 4.25, CmHn: 3.52) are evenly mixed in the gas collecting pipe 81 according to the proportion of 3:7 to form mixed gas 5, the coke oven gas and the biomass gas are sprayed with ammonia water for cooling through a cooling nozzle 6 arranged at the upper part of a bridge pipe, then tar, naphthalene and sulfur are removed through a gas purification system 51 according to the treatment technology known in the industry, then the mixed gas is pressurized to 0.2MPa through a gas compressor 52, and the components of the mixed gas are about CO: 21.2, CH4：22.1、H2：41.6、CO2：5.9、N2：3.7、CmHn：4.4。
The pressurized mixed gas and the top hot gas 12 of the gas-based shaft furnace exchange heat in a first shaft furnace hot gas heat exchanger 13 and then enter a gas passage of a burner 3 of a non-catalytic partial oxidation reformer 2, pure oxygen exchanges heat in a second shaft furnace hot gas heat exchanger 14 and then enters an oxygen passage of the burner 3 of the non-catalytic partial oxidation reformer 2, and the other waste heat of the top hot gas of the gas-based shaft furnace utilizes steam generated by a third shaft furnace hot gas heat exchanger 15 and then enters a steam passage of a burner of the non-catalytic partial oxidation reformer. And (3) performing anoxic combustion on pure oxygen and the mixed gas at the outlet of the burner nozzle 3, wherein the pure oxygen accounts for about 22% of the mixed gas, and the generated reducing gas has the components of 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 furnace, the reducing gas 21 is about 1150 ℃.
One part of the gas base shaft furnace top gas is subjected to heat exchange and dehydration through a first shaft furnace hot gas heat exchanger 13, a second shaft furnace hot gas heat exchanger 14 and a third shaft furnace hot gas heat exchanger 15, is subjected to dust removal through a dust remover 16, is pressurized through a shaft furnace top gas compressor 17, and is subjected to desulfurization and CO removal2The system 18 processes to become top cleaned gas 121. By dehydration and CO removal2Controlling water and CO of top-cleaned gas 1212The sum of the contents is less than 10 percent, the top purified gas 121 exchanges heat with hot coke oven gas in a plurality of coke oven gas riser heat exchangers 83, the top purified gas 121 is mixed with reducing gas 21 at 1150 ℃ at the outlet of a non-catalytic partial oxidation conversion furnace 2 after heat exchange to form mixed reducing gas, the temperature of the mixed reducing gas is about 850-950 ℃, and the mixed reducing gas passes through a vertical shaftThe furnace tuyere 11 enters the gas-based shaft furnace 1. In the gas-based shaft furnace 1, the iron oxide reacts with the reducing gas and is 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 raw gas generated by the reaction is discharged from the top of the shaft furnace to form gas-based shaft furnace top gas 12.
The other part is not subjected to CO removal2The gas-based shaft furnace top gas 122 is output as a chemical raw material for preparing the methanol, and the whole gas-based shaft furnace system has no gas discharge.
The second embodiment: as described with reference to fig. 1;
biomass gas (typical components of the biomass gas are CO: 51.76 and CH) generated in the biomass gas producer at the thermal cracking temperature of about 700-800 DEG C4：14.51、H2：8.41、CO2：13.5、N2: 2.37, CmHn: 6.62) is communicated with a coke oven gas collecting pipe 81 through a biomass gas bridge pipe 9, the coke oven gas is communicated with the coke oven gas collecting pipe 81 through a coke oven gas pipe 8, a coke oven gas ascending pipe and a coke oven gas bridge pipe 82, the coke oven gas ascending pipe is provided with a coke oven gas ascending pipe heat exchanger 83, and the biomass gas and the coke oven gas (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 coke oven gas collecting pipe 81 according to the proportion of 2:8 to form mixed gas, the coke oven gas and the biomass gas are sprayed with ammonia water for cooling through a cooling nozzle 6 arranged at the upper part of a bridge pipe, then tar, benzene, naphthalene, sulfur and ammonia are removed through a gas purification system 51 according to the treatment technology known in the industry, then the mixed gas is pressurized to 0.4MPa through a 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 and the top hot gas 12 of the gas-based shaft furnace exchange heat in a first shaft furnace hot gas heat exchanger 13 and then enter a gas channel of a burner 3 of the non-catalytic partial oxidation reformer 2, and the pure oxygen exchanges heat in a second shaft furnace hot gas heat exchanger 14 and then enters an oxygen channel of the burner 3 of the non-catalytic partial oxidation reformer 2And the other waste heat of the hot gas at the top of the gas-based shaft furnace utilizes a third shaft furnace hot gas heat exchanger 15 to generate steam in a steam pipe 7 and enters a steam channel of a burner 3 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, at the outlet of the non-catalytic partial oxidation furnace 2, the reducing gas 21 is about 1250 ℃.
One part of the gas base shaft furnace top gas is subjected to heat exchange and dehydration through a first shaft furnace hot gas heat exchanger 13, a second shaft furnace hot gas heat exchanger 14 and a third shaft furnace hot gas heat exchanger 15, is subjected to dust removal through a dust remover 16, is pressurized through a shaft furnace top gas compressor 17, and is subjected to desulfurization and CO removal2The system 18 processes the gas to become top purified gas 121 (flow rate is about 750M)3T. iron) by dehydration and CO removal2Controlling water and CO of top-cleaned gas 1212The sum of the contents is less than 9 percent. The gas-based shaft furnace top purified gas 121 exchanges heat with hot coke oven gas in a coke oven gas riser heat exchanger 83, the temperature of the top purified gas 121 reaches about 660 ℃ after heat exchange, and then the top purified gas and the 1250 ℃ reducing gas 21 (the flow is about 1000M) at the outlet of the non-catalytic partial oxidation furnace 23T. 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 the blast hole 11 of the shaft furnace, and the top purified gas 121 is added into the mixed reducing gas, so that the proportion of water brought by the reducing gas 21 generated by the non-catalytic part oxidation furnace in the mixed reducing gas is reduced, and the effective components of the mixed reducing gas entering the gas-based shaft furnace are improved. With the increase of the preheating temperature of the top purified gas 121, the mixing amount of the top purified gas 121 is increased, the moisture of the mixed reducing gas entering the gas-based shaft furnace is further reduced, and the effective components of the mixed reducing gas entering the gas-based shaft furnace are increased. In the gas-based shaft furnace 1, the iron oxide reacts with reducing gas to be reduced into direct reduced iron, and the direct reduced iron passes through the gas-based shaft furnace 1And the crude gas generated by the reaction is discharged from the top of the shaft furnace to become gas-based shaft furnace top gas 12.
Remaining undeco2At a flow rate of about 470M, of the top gas 122 of the gas-based shaft furnace3T-iron (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 (flow 235M)3Iron/t) and fresh make-up coke oven gas 8 (flow rate about 295M)3Iron/t) and biogas (flow rate about 130M)3T. iron) to a flow rate of about 660M3Mixed gas of/t.Fe without CO removal2The top gas 122 of the gas-based shaft furnace 1 replaces coke oven gas to serve other purposes, and the purpose of self-producing gas heat energy self-circulation recycling of the gas-based shaft furnace is indirectly achieved through a gradient utilization mode of different kinds of gas, so that the whole gas-based shaft furnace system does not need to externally burn reducing gas in a heating tube, does not discharge waste gas generated by external combustion, and does not cause enrichment of nitrogen in the gas-based shaft furnace to influence normal production operation and production efficiency.
Example three: as described with reference to fig. 1;
the biomass gas producer adopts a thermal cracking technology, and biomass gas (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 producer4：14.51、H2：8.41、CO2：13.5、N2: 2.37, CmHn: 6.62) is communicated with a gas collecting pipe 81 through a biomass gas bridge pipe 9, coke oven gas is communicated with the coke oven gas collecting pipe 81 through a coke oven gas pipe 8, a coke oven gas ascending pipe and a coke oven gas bridge pipe 82, the coke oven gas ascending pipe is provided with a coke oven gas ascending pipe heat exchanger 83, biomass gas and coke oven gas (typical components of coke oven gas are CO: 8.07, CH4：25.4、H2：55.8、CO2：2.83、N2: 4.25, CmHn: 3.52) are evenly mixed in the gas collecting pipe 81 according to the proportion of 1:9 to form mixed gas, the coke oven gas and the biomass gas are sprayed with ammonia water for cooling through a cooling nozzle 6 arranged at the upper part of the bridge pipe, and then tar, benzene, naphthalene, sulfur and ammonia are removed through a purification system 51 according to the treatment technology known in the industryAnd then the mixed gas is pressurized to 0.6MPa by a compressor 52, and the components of the mixed gas are about CO: 12.44, CH4：24.31、H2：51.06、CO2：3.9、N2：4.06、CmHn：3.83。
The pressurized mixed gas and the top hot gas 12 of the gas-based shaft furnace exchange heat in a first shaft furnace hot gas heat exchanger 13 and then enter a gas channel of a burner 3 of a non-catalytic partial oxidation reformer 2, pure oxygen exchanges heat in a second shaft furnace hot gas heat exchanger 14 and then enters an oxygen channel of the burner 3 of the non-catalytic partial oxidation reformer 2, and the other waste heat of the top hot gas of the gas-based shaft furnace utilizes a third shaft furnace hot gas heat exchanger 15 to generate steam in a steam pipe 7 and then enters a steam channel of the burner 3 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 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 furnace, the reducing gas 21 is about 1300 ℃.
One part of the gas base shaft furnace top gas is subjected to heat exchange and dehydration through a first shaft furnace hot gas heat exchanger 13, a second shaft furnace hot gas heat exchanger 14 and a third shaft furnace hot gas heat exchanger 15, is subjected to dust removal through a dust remover 16, is pressurized through a shaft furnace top gas compressor 17, and is subjected to desulfurization and CO removal2The system 18 processes to become top cleaned gas 121. By dehydration and CO removal2Controlling water and CO of top-cleaned gas 1212The sum of the contents is less than 8 percent, the top purified gas 121 exchanges heat with hot coke oven gas in a heat exchanger 83 of a coke oven gas riser, the top purified gas 121 is mixed with 1300 ℃ reducing gas 21 at the outlet of a non-catalytic partial oxidation furnace 2 after heat exchange to form mixed reducing gas, the temperature of the mixed reducing gas is about 1050 ℃, and the mixed reducing gas enters the gas-based shaft furnace 1 through a tuyere 11 of the shaft furnace. In the gas-based shaft furnace 1, the iron oxide reacts with the reducing gas and is 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 form gas-based shaft furnace top gas 12.
The other part is not subjected to CO removal2The gas-based shaft furnace top gas 122 is output as a chemical raw material for preparing urea, the whole gas-based shaft furnace system has no gas emission, and nitrogen is not enriched in the gas-based shaft furnace, so that the normal operation and the production efficiency of production are not influenced.
Example four: as described with reference to fig. 2;
the coke oven gas is communicated with the coke oven gas collecting pipe 81 through a coke oven gas pipe 8, a coke oven gas ascending pipe and a coke oven gas bridge pipe 82, the coke oven gas ascending pipe is provided with a coke oven gas ascending pipe heat exchanger 83, and 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, spraying ammonia water for cooling by a cooling nozzle 6 arranged at the upper part of the bridge pipe, then removing tar, benzene, naphthalene, sulfur and ammonia by a purification system 51 according to the well-known treatment technology in the industry, and pressurizing the coke oven gas to 0.8MPa by a compressor 52.
The pressurized coke oven gas exchanges heat with top hot gas 12 of the gas-based shaft furnace in a first shaft furnace hot gas heat exchanger 13, then exchanges heat with hot circulating gas exhausted from a cooling section of the gas-based shaft furnace in a heat exchanger 100, and enters a gas channel of a burner 3 of a non-catalytic partial oxidation reformer 2, pure oxygen exchanges heat in a second shaft furnace hot gas heat exchanger 14 and enters an oxygen channel of the burner 3 of the non-catalytic partial oxidation reformer 2, and the other waste heat of the top hot gas of the gas-based shaft furnace utilizes a third shaft furnace hot gas heat exchanger 15 to generate steam in a steam pipe 7 and enters a steam channel of the burner 3 of the non-catalytic partial oxidation reformer 2. And (3) performing oxygen-deficient combustion on the pure oxygen and the coke oven gas at the outlet of the burner 3, wherein the proportion of the pure oxygen in the coke oven gas is about 25%, and the generated reducing gas has the components of CO: 22.8, CH4：1.26、H2：59.1、CO2：2.1、N2：3.53、H2O: 11.2, at the outlet of the non-catalytic partial oxidation furnace 2, the reducing gas 21 is at about 1270 ℃. The hot circulating gas exhausted from the cooling section of the gas-based shaft furnace passes through the heat exchanger 100 and the dust remover 200, supplements coke oven gas, and then enters the bottom of the gas-based shaft furnace through the compressor 300.
One part of the gas passes through a first shaft furnace hot gas heat exchanger 13, a second shaft furnace hot gas heat exchanger 14 and a second shaft furnace hot gas heat exchangerHeat exchange and dehydration are carried out by a third heat exchanger 15, the gas-based shaft furnace top gas after dust removal by a dust remover 16 is pressurized by a shaft furnace top gas compressor 17, and desulfurization and CO removal are carried out2The system 18 processes the gas to become top purified gas 121 (with a flow rate of about 500M)3T. iron) by dehydration and CO removal2Controlling water and CO of top-cleaned gas 1212The sum of the contents is less than 7 percent. The gas-based shaft furnace top purified gas 121 exchanges heat with coke oven hot flue gas in a hot flue gas heat exchanger 84, then exchanges heat with hot coke oven gas in a coke oven gas ascending tube heat exchanger 83, the temperature of the top purified gas 121 reaches about 550 ℃ after heat exchange, and then the top purified gas 21 (the flow is about 1300M) at 1270 ℃ at the outlet of a non-catalytic partial oxidation furnace 2 is added3t.Fe) to form mixed reducing gas, the temperature of the mixed reducing gas is about 1070 ℃, the mixed reducing gas enters the gas-based shaft furnace 1 through the tuyere 11, and the top purified gas 121 is added into the mixed reducing gas, so that the proportion of moisture brought by the reducing gas 21 generated by the non-catalytic partial oxidation furnace in the mixed reducing gas is reduced, and the effective components of the mixed reducing gas entering the gas-based shaft furnace are improved. In the gas-based shaft furnace 1, the iron oxide reacts with the reducing gas and is 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 raw gas generated by the reaction is discharged from the top of the shaft furnace to form gas-based shaft furnace top gas 12.
Remaining undeco2At a flow rate of about 780M, of the top gas 122 of the gas-based shaft furnace3T-iron (calorific value of about 2000 kcal/m)3) Equal calorific value to replace coke oven gas, the flow rate is about 390M3T-iron (coke oven gas heat value about 4000 kcal/m)3) Coke oven gas (flow rate 390M)3Iron/t) and fresh make-up coke oven gas (flow about 470M)3T. iron) forming a flow of about 860M3Total coke oven gas (coke oven gas passing through coke oven gas pipe 8) of/t.Fe without CO removal2The top gas 122 of the gas-based shaft furnace 1 replaces the coke oven gas 8 to be used 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, the whole gas-based shaft furnace system does not need to externally burn reducing gas in a heating tube, no waste gas generated by external combustion is discharged, and no nitrogen is enriched in the gas-based shaft furnace,affecting the normal operation and production efficiency of production. Compared with the gas-based shaft furnace which is commercially produced at present, the method saves about 20 percent of coke oven gas per ton of iron.
Example five: as described with reference to fig. 3;
fig. 3 differs from fig. 2: the gas-based shaft furnace top purified gas 121 exchanges heat with hot coke oven gas 8 of a first coke oven in each ascending tube heat exchanger 83 of the coke oven gas, the gas-based shaft furnace top purified gas and the hot coke oven gas 8 of a second coke oven in each ascending tube heat exchanger 83 of the coke oven gas are gathered in a first main tube after heat exchange, the gas-based shaft furnace top purified gas and the hot coke oven gas 8 of the first coke oven are gathered in a second main tube after heat exchange, and the second main tube is communicated with a tuyere of the gas-based shaft furnace 1 after being connected in parallel with an outlet pipeline of a non-catalytic part oxidation oven (2).
Claims (10)
1. An energy gradient utilization method for coupling production of a gas-based shaft furnace and a coke oven is characterized in that: the method is realized according to the following steps:
the method comprises the following steps: a part of top hot gas of the gas-based shaft furnace (1) is cooled, dedusted, desulfurized and CO2Then the gas becomes the purified gas at the top of the gas-based shaft furnace;
step two: replacing coke oven gas with the other part of top hot gas of the gas-based shaft furnace (1) with the same calorific value, replacing the coke oven gas with the other part of top hot gas for other purposes, preheating coke oven total gas formed by the replaced coke oven gas and newly supplemented coke oven gas, entering a non-catalytic partial oxidation converter (2) for combustion and heating, and discharging the generated high-temperature reducing gas from an outlet of the non-catalytic partial oxidation converter (2);
step three: and (3) after heat exchange is carried out between the purified gas at the top of the gas-based shaft furnace in the first step and hot gas in a coke oven gas riser pipe, adding the purified gas into the high-temperature reducing gas at the outlet of the non-catalytic partial oxidation converter (2) in the second step to obtain mixed reducing gas at the temperature of 850-1100 ℃, and feeding the mixed reducing gas into the gas-based shaft furnace.
2. The method for utilizing the energy gradient generated by the coupling of the gas-based shaft furnace and the coke oven according to claim 1, is characterized in that: and in the second step, the total coke oven gas is preheated in a heat exchange mode with hot gas at the top of the gas-based shaft furnace (1).
3. The method for utilizing the energy gradient generated by coupling the gas-based shaft furnace and the coke oven according to claim 2, wherein the method comprises the following steps: after being preheated by coke oven gas of the total coke oven gas of the gas-based shaft furnace top hot coke oven, the coke oven gas is further preheated by hot circulating gas exhausted from the cooling section of the gas-based shaft furnace (1).
4. The method for utilizing the energy gradient generated by the coupling of the gas-based shaft furnace and the coke oven according to claim 1, is characterized in that: in the third step, the purified gas at the top of the gas-based shaft furnace exchanges heat with the hot gas in the coke oven gas ascending pipe, and the heat is exchanged with the hot flue gas in the coke oven flue before exchanging heat with the hot gas in the coke oven gas ascending pipe.
5. The method for utilizing the energy gradient generated by the coupling of the gas-based shaft furnace and the coke oven according to claim 1, is characterized in that: in the third step, the coke oven gas riser pipes are divided into two groups, and the purified gas at the top of the gas-based shaft furnace firstly exchanges heat for the first time through the first group of coke oven gas riser pipes and then exchanges heat for the second time through the second group of coke oven gas riser pipes to increase the temperature.
6. An energy gradient utilization system for coupling production of a gas-based shaft furnace and a coke oven comprises the gas-based shaft furnace (1), the coke oven, a non-catalytic partial oxidation converter (2), an oxidation oven outlet reducing gas pipe (21), a coke oven gas pipe and a gas-based shaft furnace top gas pipe; the coke oven gas pipe is communicated with the non-catalytic partial oxidation converter (2), the coke oven gas pipe is arranged on the coke oven, the reducing gas pipe (21) at the outlet of the oxidation furnace is arranged on the non-catalytic partial oxidation converter (2), and the first branch pipe of the gas pipe at the top of the gas-based shaft furnace is sequentially desulfurized and subjected to CO removal2The system (18) is connected with a reducing gas pipe (21) at the outlet of an oxidation furnace of a non-catalytic partial oxidation conversion furnace (2) in parallel after being connected with a heat exchanger of a coke oven gas riser, and then is communicated with a shaft furnace tuyere (11) of a gas-based shaft furnace (1), and a second branch pipe of a gas pipe at the top of the gas-based shaft furnace is communicated with an external gas pipeline.
7. The energy gradient system for coupling production of the gas-based shaft furnace and the coke oven according to claim 6, wherein: the coke oven is communicated with a hot gas heat exchanger at the top of the gas-based shaft furnace (1) through a coke oven gas pipe and then is communicated with the non-catalytic partial oxidation converter (2).
8. The energy gradient system for coupling production of the gas-based shaft furnace and the coke oven according to claim 6, wherein: the coke oven is communicated with a hot gas heat exchanger at the top of the gas-based shaft furnace (1) and a hot circulating gas heat exchanger exhausted from a cooling section of the gas-based shaft furnace through a coke oven gas pipe and then is communicated with the non-catalytic partial oxidation converter (2).
9. The system for the gradient utilization of the energy produced by the coupling of the gas-based shaft furnace and the coke oven according to claim 6, wherein: the first branch pipe of the gas-based shaft furnace top gas pipe of the gas-based shaft furnace (1) is desulfurized and CO removed in sequence2The system (18), the coke oven flue hot flue gas heat exchanger and the coke oven gas riser heat exchanger are connected in parallel with a reducing gas pipe (21) at the outlet of the oxidation furnace of the non-catalytic partial oxidation conversion furnace (2).
10. The system for the gradient utilization of the energy produced by the coupling of the gas-based shaft furnace and the coke oven according to claim 6, wherein: the first branch pipe of the gas-based shaft furnace top gas pipe of the gas-based shaft furnace (1) is sequentially desulfurized and removed with CO2The system (18), the first coke oven gas riser heat exchanger (83) and the second coke oven gas riser heat exchanger (83) are arranged in parallel with the reducing gas pipe (21) at the outlet of the oxidation furnace of the non-catalytic partial oxidation conversion furnace (2).
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