CN101892334A - Method for recycling blast furnace gas - Google Patents
Method for recycling blast furnace gas Download PDFInfo
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- CN101892334A CN101892334A CN2010102422940A CN201010242294A CN101892334A CN 101892334 A CN101892334 A CN 101892334A CN 2010102422940 A CN2010102422940 A CN 2010102422940A CN 201010242294 A CN201010242294 A CN 201010242294A CN 101892334 A CN101892334 A CN 101892334A
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Abstract
The invention relates to a method for recycling blast furnace gas, and solves the problems of low additional value and poor using effect of the blast furnace gas because the advantages of the composition and chemical properties of the blast furnace gas cannot be brought into full play in the conventional method for recycling the blast furnace gas. The method comprises the following steps of: firstly, compressing the blast furnace gas and then allowing the compressed blast furnace gas to enter a temperature swing adsorption system for treatment to obtain purified blast furnace gas; secondly, pressurizing the purified blast furnace gas and then conveying the pressurized blast furnace gas to a pressure swing adsorption carbon extraction system for adsorption and purification to obtain carbon mixed gas; thirdly, pressurizing the rest blast furnace gas and then conveying the pressurized blast furnace gas to a pressure swing adsorption nitrogen extraction system to separate and recycle nitrogen; and finally, returning the rest blast furnace gas to a gas fuel system. The volume purity of the CO and CO2 mixed gas is over 95 percent and the mixed gas provides a synthesis air source for methanol and an organic synthesis and processing system; the volume purity of the nitrogen is over 99.5 percent, so that the problem that steel enterprises need the nitrogen with the volume purity of over 99 percent is solved; and the blast furnace gas has high additional value.
Description
Technical field
The present invention relates to a kind of recoverying and utilizing method of blast furnace gas.
Background technology
In iron and steel enterprise, blast furnace gas is the byproduct that produces in the iron manufacturing process, and main component is: CO, CO
2, N
2, H
2Deng, wherein combustiblecomponents CO content accounts for about 27%, H
2Content account for about 2.7% CO
2, N
2Content account for 15%, 55% respectively, CH
4Account for about 0.3%, calorific value is lower.The production technique that generally adopts big volume, high wind-warm syndrome, high smelting intensity, high Coal powder spray amount is produced in modern ironmaking, adopt these advanced production technique to improve labour productivity and cut down the consumption of energy, but the blast furnace gas calorific value that is produced is lower, has increased to utilize difficulty.CO in the blast furnace gas
2, N
2Neither participate in burning and produce heat, can not be combustion-supporting, on the contrary, also absorb the heat that produces in a large amount of combustion processeses, cause the theoretical combustion temperature of blast furnace gas on the low side.As if the point of ignition of blast furnace gas is not high, does not have the obstacle that catches fire, but in the Actual combustion process, is subjected to the influence of various factors, and the temperature of mixed gas must just can be guaranteed incendiary stability much larger than point of ignition.The theoretical combustion temperature of blast furnace gas is low, and the amount that participates in the incendiary blast furnace gas is very big, causes the heat-up rate of mixed gas very slow, and temperature is not high, and combustion stability is bad.And at present in the iron and steel enterprise, the utilization of blast furnace gas mainly contained light discharging, fuel refreshment heat energy or combustion power generation, more than utilize mode all not give full play to the composition of blast furnace gas and the advantage of chemical property, low, the weak effect of its added value.Promptly cause the waste of resource, caused the decline of enterprise's comprehensive competitive power again.
Iron and steel enterprise can only compress separation with air in order to access the nitrogen that needs in the production simultaneously, produces nitrogen, considers from carbon reduction and economic benefit aspect, all remains to be inquired into.
Summary of the invention
The objective of the invention is to give full play to the composition of blast furnace gas and the advantage of chemical property for the recoverying and utilizing method that solves existing blast furnace gas, make the added value of blast furnace gas low, utilize the problem of weak effect, the invention provides a kind of method of recycling blast furnace gas.
A kind of method of recycling blast furnace gas of the present invention, realize by following steps: one, blast furnace gas is fed gas holder, blast furnace gas in the gas holder being compressed to pressure then is 0.01～0.1MPa, then blast furnace gas being fed temperature swing adsorption system (TSA) handles, the inlet temperature of control alternating temperature absorption is 300～400 ℃, temperature out is 170～200 ℃, is purified blast furnace gas; Two, after the purification blast furnace gas that step 1 is obtained is pressurized to 0.2～5MPa, being transported to transformation absorption puies forward carbon system (PSA-C) and adsorbs purification carbon one gas mixture, transformation fractionation by adsorption purification condition is: behind absorption 1min～12min, stop to carry the purification blast furnace gas, in gauge pressure be then-condition of 0.1MPa～0.15MPa under desorption 1min～10min, obtain bulk purity and reach CO and CO more than 95%
2Carbon one gas mixture; Three, will carry the remaining blast furnace gas of discharging carbon system air outlet and be forced into 0.5～3MPa by transformation absorption in the step 2 after, be delivered to transformation absorption again and carry nitrogen system (PSA-N), nitrogen separation is reclaimed, wherein transformation fractionation by adsorption recovering condition is: behind absorption 1～10min, stop to carry, in gauge pressure be then-condition of 0.1MPa～0.5MPa under desorption 1min～10min, obtain bulk purity and reach nitrogen more than 99.5%; Four, will carry the residue blast furnace gas of discharging the nitrogen system air outlet by the transformation absorption of step 3 and be recycled to the coal gas fuel system, promptly finish the recycling of blast furnace gas.
Have 5～8 adsorption towers in the step 1 of the present invention in the temperature swing adsorption system; Transformation absorption in the step 2 is carried has 5～8 adsorption towers in the carbon system; Transformation absorption in the step 3 is carried has 5～8 adsorption towers in the nitrogen system.Transformation absorption in carbon system and the step 3 is proposed in the absorption of temperature swing adsorption system in the step 1 of the present invention, the transformation in the step 2, and to carry nitrogen system be conventional equipment, provided by Sichuan Tianyi Science ﹠ Technology Co., Ltd.
The method of recycling blast furnace gas of the present invention is separated into blast furnace gas the unstripped gas that can be recycled, handle through step 1, remove dirt in the blast furnace gas and a small amount of organic impurity etc., thereby accomplish not influence the normal steady running of next step blast furnace gas separation system; Step 2 utilizes transformation absorption to carry isolated CO of carbon system (PSA-C) and CO
2The bulk purity of carbon one gas mixture reach more than 95%, be to be used for replenishing methyl alcohol or the valuable carbon one synthetic source of the gas of other organic synthesis; The bulk purity of the nitrogen that step 3 reclaims reaches more than 99.5%, and this highly purified nitrogen just can be applied to the equipment protection gas of Steel Complex and the inertia substitution gas of production equipment.Contain a spot of H in the remaining blast furnace gas of after step 3 is handled, discharging
2, CH
4, a spot of CO and CO
2, and a spot of nitrogen, it is isolated system, be recycled to the coal gas fuel system and get final product.
The method of recycling blast furnace gas of the present invention has solved iron and steel enterprise, and to need bulk purity be nitrogen problem more than 99.5%, provide valuable carbon one synthetic source of the gas for methyl alcohol and organic synthesis system of processing again, the composition of blast furnace gas and the advantage of chemical property have been given full play to, make the added value of blast furnace gas uprise, utilize effect to improve, thereby the economic benefit of low value-added blast furnace gas is significantly promoted.Simultaneously, the energy utilization rate height alleviates environmental pollution, and it is obvious to improve business economic benefit effect.
Description of drawings
Fig. 1 is the simple process figure of method of the recycling blast furnace gas of embodiment one.
Embodiment
Technical solution of the present invention is not limited to following cited embodiment, also comprises the arbitrary combination between each embodiment.
Embodiment one: present embodiment is recycled the method for blast furnace gas, realize by following steps: one, blast furnace gas is fed gas holder, blast furnace gas in the gas holder being compressed to pressure then is 0.01～0.1MPa, then blast furnace gas being fed temperature swing adsorption system (TSA) handles, the inlet temperature of control alternating temperature absorption is 300～400 ℃, temperature out is 170～200 ℃, is purified blast furnace gas; Two, after the purification blast furnace gas that step 1 is obtained is pressurized to 0.2～5MPa, being transported to transformation absorption puies forward carbon system (PSA-C) and adsorbs purification carbon one gas mixture, transformation fractionation by adsorption purification condition is: behind absorption 1min～12min, stop to carry the purification blast furnace gas, in gauge pressure be then-condition of 0.1MPa～0.15MPa under desorption 1min～10min, obtain bulk purity and reach CO and CO more than 95%
2Carbon one gas mixture; Three, will carry the remaining blast furnace gas of discharging carbon system air outlet and be forced into 0.5～3MPa by transformation absorption in the step 2 after, be delivered to transformation absorption again and carry nitrogen system (PSA-N), nitrogen separation is reclaimed, wherein transformation fractionation by adsorption recovering condition is: behind absorption 1～10min, stop to carry, in gauge pressure be then-condition of 0.1MPa～0.5MPa under desorption 1min～10min, obtain bulk purity and reach nitrogen more than 99.5%; Four, will carry the residue blast furnace gas of discharging the nitrogen system air outlet by the transformation absorption of step 3 and be recycled to the coal gas fuel system, promptly finish the recycling of blast furnace gas.
The simple process figure of present embodiment as shown in Figure 1.The recycling technology of present embodiment is simple, and is all linked with one another between each treatment process, complements each other, and reaches the effect of effective recycling blast furnace gas.
The method of the recycling blast furnace gas of present embodiment has solved iron and steel enterprise, and to need bulk purity be nitrogen problem more than 99.5%, provide valuable carbon one synthetic source of the gas for methyl alcohol and organic synthesis system of processing again, the composition of blast furnace gas and the advantage of chemical property have been given full play to, make the added value of blast furnace gas uprise, utilize effect to improve, thereby the economic benefit of low value-added blast furnace gas is significantly promoted.Simultaneously, the energy utilization rate height alleviates environmental pollution, and it is obvious to improve business economic benefit effect.
Transformation absorption in carbon system and the step 3 is proposed in the absorption of temperature swing adsorption system in the present embodiment step 1, the transformation in the step 2, and to carry nitrogen system be conventional equipment, provided by Sichuan Tianyi Science ﹠ Technology Co., Ltd.
Embodiment two: present embodiment and embodiment one are different is that the blast furnace gas in the gas holder to be compressed to pressure then in the step 1 be 0.03～0.08MPa.Other step and parameter are identical with embodiment one.
Embodiment three: present embodiment and embodiment one are different is that the blast furnace gas in the gas holder to be compressed to pressure then in the step 1 be 0.06MPa.Other step and parameter are identical with embodiment one.
Embodiment four: present embodiment and embodiment one, two or three are different is that the inlet temperature of control alternating temperature absorption in the step 1 is 320～380 ℃, and temperature out is 175～195 ℃.Other step and parameter are identical with embodiment one, two or three.
Embodiment five: present embodiment and embodiment one, two or three are different is that the inlet temperature of control alternating temperature absorption in the step 1 is 350～360 ℃, and temperature out is 180～190 ℃.Other step and parameter are identical with embodiment one, two or three.
Embodiment six: what present embodiment was different with one of embodiment one to five is that the gas booster compressor that in the step 1 compression of the blast furnace gas in the gas holder is adopted is a compressor.Other step and parameter are identical with one of embodiment one to five.
Embodiment seven: what present embodiment was different with one of embodiment one to six is to have 5～8 adsorption towers in the step 1 in the temperature swing adsorption system.Other step and parameter are identical with one of embodiment one to six.
Embodiment eight: what present embodiment was different with one of embodiment one to six is to have 6 adsorption towers in the step 1 in the temperature swing adsorption system.Other step and parameter are identical with one of embodiment one to six.
Embodiment nine: what present embodiment was different with one of embodiment one to eight is that the purification blast furnace gas that in the step 2 step 1 is obtained is pressurized to 0.3～4MPa.Other step and parameter are identical with one of embodiment one to eight.
Embodiment ten: what present embodiment was different with one of embodiment one to eight is that the purification blast furnace gas that in the step 2 step 1 is obtained is pressurized to 0.5～3MPa.Other step and parameter are identical with one of embodiment one to eight.
Embodiment 11: present embodiment is different with one of embodiment one to ten is that the pressure exerting device that the purification blast furnace gas pressurization that in the step 2 step 1 obtained is adopted is a compressor.Other step and parameter are identical with one of embodiment one to ten.
Embodiment 12: what present embodiment was different with one of embodiment one to 11 is that transformation fractionation by adsorption purification condition is in the step 2: behind absorption 1min～8min, stopping carry to purify blast furnace gas, is desorption 1min～6min under the condition of 0MPa～0.1MPa in gauge pressure then.Other step and parameter are identical with one of embodiment one to 11.
Embodiment 13: what present embodiment was different with one of embodiment one to 11 is that transformation fractionation by adsorption purification condition is in the step 2: behind absorption 1min～6min, stopping carry to purify blast furnace gas, is desorption 1min～6min under the condition of 0.05MPa in gauge pressure then.Other step and parameter are identical with one of embodiment one to 11.
Embodiment 14: present embodiment is different with one of embodiment one to 13 is that transformation absorption in the step 2 is carried and had 5～8 adsorption towers in the carbon system.Other step and parameter are identical with one of embodiment one to 13.
Embodiment 15: present embodiment is different with one of embodiment one to 13 is that transformation absorption in the step 2 is carried and had 6 adsorption towers in the carbon system.Other step and parameter are identical with one of embodiment one to 13.
Embodiment 16: what present embodiment was different with one of embodiment one to 15 is will carry the remaining blast furnace gas of discharging carbon system air outlet by transformation absorption in the step 2 in the step 3 to be forced into 1～2.5MPa.Other step and parameter are identical with one of embodiment one to 15.
Embodiment 17: what present embodiment was different with one of embodiment one to 15 is will carry the remaining blast furnace gas of discharging carbon system air outlet by transformation absorption in the step 2 in the step 3 to be forced into 2MPa.Other step and parameter are identical with one of embodiment one to 15.
Embodiment 18: present embodiment is different with one of embodiment one to 17 is that will to carry the pressure exerting device that the remaining blast furnace gas pressurization of discharging carbon system air outlet adopts by transformation absorption in the step 2 in the step 3 be compressor.Other step and parameter are identical with one of embodiment one to 17.
Embodiment 19: what present embodiment was different with one of embodiment one to 18 is that transformation fractionation by adsorption recovering condition is in the step 3: behind absorption 1～8min, stopping to carry, is desorption 1min～8min under the condition of 0MPa～0.3MPa in gauge pressure then.Other step and parameter are identical with one of embodiment one to 18.
Embodiment 20: what present embodiment was different with one of embodiment one to 18 is that transformation fractionation by adsorption recovering condition is in the step 3: behind absorption 1～6min, stopping to carry, is desorption 1～6min under the condition of 0.1MPa in gauge pressure then.Other step and parameter are identical with one of embodiment one to 18.
Embodiment 21: present embodiment is different with one of embodiment one to 20 is that transformation absorption in the step 3 is carried and had 5～8 adsorption towers in the nitrogen system.Other step and parameter are identical with one of embodiment one to 20.
Embodiment 22: present embodiment is different with one of embodiment one to 20 is that transformation absorption in the step 3 is carried and had 6 adsorption towers in the nitrogen system.Other step and parameter are identical with one of embodiment one to 20.
Embodiment 23: present embodiment is different with one of embodiment one to 22 is that temperature swing adsorption system, the absorption of the transformation in the step 2 in the step 1 is proposed transformation absorption in carbon system and the step 3 to carry nitrogen system is conventional equipment, is provided by Sichuan Tianyi Science ﹠ Technology Co., Ltd.Other step and parameter are identical with one of embodiment one to 22.
Embodiment 24: present embodiment is recycled the method for blast furnace gas, realize by following steps: one, blast furnace gas is fed gas holder, blast furnace gas in the gas holder being compressed to pressure then is 0.01MPa, then blast furnace gas being fed temperature swing adsorption system (TSA) handles, the inlet temperature of control alternating temperature absorption is 350～360 ℃, temperature out is 180～190 ℃, is purified blast furnace gas; Two, after the purification blast furnace gas that step 1 is obtained is pressurized to 5MPa, being transported to transformation absorption puies forward carbon system (PSA-C) and adsorbs purification carbon one gas mixture, transformation fractionation by adsorption purification condition is: behind the absorption 12min, stop to carry the purification blast furnace gas, in gauge pressure be then-condition of 0.1MPa under desorption 10min, obtain bulk purity and reach CO and CO more than 95%
2Carbon one gas mixture; Three, will carry the remaining blast furnace gas of discharging carbon system air outlet and be forced into 3MPa by transformation absorption in the step 2 after, be delivered to transformation absorption again and carry nitrogen system (PSA-N), nitrogen separation is reclaimed, wherein transformation fractionation by adsorption recovering condition is: behind absorption 1～10min, stop to carry, in gauge pressure be then-condition of 0.1MPa under desorption 1～10min, obtain bulk purity and reach nitrogen more than 99.5%; Four, will carry the residue blast furnace gas of discharging the nitrogen system air outlet by the transformation absorption of step 3 and be recycled to the coal gas fuel system, promptly finish the recycling of blast furnace gas.
The employed equipment of pressurization in the compression of present embodiment step 1, step 2 and the step 3 is compressor.Have 6 adsorption towers in the present embodiment step 1 in the temperature swing adsorption system; Transformation absorption in the step 2 is carried has 6 adsorption towers in the carbon system; Transformation absorption in the step 3 is carried has 6 adsorption towers in the nitrogen system.Transformation absorption in carbon system and the step 3 is proposed in the absorption of temperature swing adsorption system in the present embodiment step 1, the transformation in the step 2, and to carry nitrogen system be conventional equipment, provided by Sichuan Tianyi Science ﹠ Technology Co., Ltd.
The method that present embodiment is recycled blast furnace gas is separated into blast furnace gas the unstripped gas that can be recycled.Handle through step 1, remove dirt in the blast furnace gas and a small amount of organic impurity etc., thereby accomplish not influence the normal steady running of next step blast furnace gas separation system; Step 2 utilizes transformation absorption to carry isolated CO of carbon system (PSA-C) and CO
2The bulk purity of carbon one gas mixture reach more than 95%, be to be used for replenishing methyl alcohol or the valuable carbon one synthetic source of the gas of other organic synthesis; The bulk purity of the nitrogen that step 3 reclaims reaches more than 99.5%, and this highly purified nitrogen just can be applied to the equipment protection gas of Steel Complex and the inertia substitution gas of production equipment.Contain a spot of H in the remaining blast furnace gas of after step 3 is handled, discharging
2, CH
4, a spot of CO and CO
2, and a spot of nitrogen, it is isolated system, be recycled to the coal gas fuel system and get final product.
Present embodiment reuses the valuable gases efficient recovery that can be recycled in the blast furnace gas, when reducing environmental pollution, can also reduce the loss of enterprise, improves the business economic benefit.
Embodiment 25: present embodiment is recycled the method for blast furnace gas, realize by following steps: one, blast furnace gas is fed gas holder, blast furnace gas in the gas holder being compressed to pressure then is 0.1MPa, then blast furnace gas being fed temperature swing adsorption system (TSA) handles, the inlet temperature of control alternating temperature absorption is 350～360 ℃, temperature out is 180～190 ℃, is purified blast furnace gas; Two, after the purification blast furnace gas that step 1 is obtained is pressurized to 0.2MPa, being transported to transformation absorption puies forward carbon system (PSA-C) and adsorbs purification carbon one gas mixture, transformation fractionation by adsorption purification condition is: behind the absorption 3min, stop to carry the purification blast furnace gas, be desorption 3min under the condition of 0.15MPa in gauge pressure then, obtain bulk purity and reach CO and CO more than 95%
2Carbon one gas mixture; Three, will carry the remaining blast furnace gas of discharging carbon system air outlet and be forced into 3MPa by transformation absorption in the step 2 after, be delivered to transformation absorption again and carry nitrogen system (PSA-N), nitrogen separation is reclaimed, wherein transformation fractionation by adsorption recovering condition is: behind absorption 1～6min, stop to carry, in gauge pressure be then-condition of 0.1MPa under desorption 1～6min, obtain bulk purity and reach nitrogen more than 99.5%; Four, will carry the residue blast furnace gas of discharging the nitrogen system air outlet by the transformation absorption of step 3 and be recycled to the coal gas fuel system, promptly finish the recycling of blast furnace gas.
The employed equipment of pressurization in the compression of present embodiment step 1, step 2 and the step 3 is compressor.Have 6 adsorption towers in the present embodiment step 1 in the temperature swing adsorption system; Transformation absorption in the step 2 is carried has 6 adsorption towers in the carbon system; Transformation absorption in the step 3 is carried has 6 adsorption towers in the nitrogen system.Transformation absorption in carbon system and the step 3 is proposed in the absorption of temperature swing adsorption system in the present embodiment step 1, the transformation in the step 2, and to carry nitrogen system be conventional equipment, provided by Sichuan Tianyi Science ﹠ Technology Co., Ltd.
Present embodiment reuses the valuable gases efficient recovery that can be recycled in the blast furnace gas, when reducing environmental pollution, can also reduce the loss of enterprise, improves the business economic benefit.
Embodiment 26: present embodiment is recycled the method for blast furnace gas, realize by following steps: one, blast furnace gas is fed gas holder, blast furnace gas in the gas holder being compressed to pressure then is 0.06MPa, then blast furnace gas being fed temperature swing adsorption system (TSA) handles, the inlet temperature of control alternating temperature absorption is 350～360 ℃, temperature out is 180～190 ℃, is purified blast furnace gas; Two, after the purification blast furnace gas that step 1 is obtained is pressurized to 3MPa, being transported to transformation absorption puies forward carbon system (PSA-C) and adsorbs purification carbon one gas mixture, transformation fractionation by adsorption purification condition is: behind the absorption 2min, stop to carry the purification blast furnace gas, be desorption 2min under the condition of 0.05MPa in gauge pressure then, obtain bulk purity and reach CO and CO more than 95%
2Carbon one gas mixture; Three, will carry the remaining blast furnace gas of discharging carbon system air outlet and be forced into 3MPa by transformation absorption in the step 2 after, be delivered to transformation absorption again and carry nitrogen system (PSA-N), nitrogen separation is reclaimed, wherein transformation fractionation by adsorption recovering condition is: behind absorption 1～2min, stop to carry, be desorption 1～2min under the condition of 0.1MPa in gauge pressure then, obtain bulk purity and reach nitrogen more than 99.5%; Four, will carry the residue blast furnace gas of discharging the nitrogen system air outlet by the transformation absorption of step 3 and be recycled to the coal gas fuel system, promptly finish the recycling of blast furnace gas.
The employed equipment of pressurization in the compression of present embodiment step 1, step 2 and the step 3 is compressor.Have 6 adsorption towers in the present embodiment step 1 in the temperature swing adsorption system; Transformation absorption in the step 2 is carried has 6 adsorption towers in the carbon system; Transformation absorption in the step 3 is carried has 6 adsorption towers in the nitrogen system.Transformation absorption in carbon system and the step 3 is proposed in the absorption of temperature swing adsorption system in the present embodiment step 1, the transformation in the step 2, and to carry nitrogen system be conventional equipment, provided by Sichuan Tianyi Science ﹠ Technology Co., Ltd.
Present embodiment reuses the valuable gases efficient recovery that can be recycled in the blast furnace gas, when reducing environmental pollution, can also reduce the loss of enterprise, improves the business economic benefit.
Claims (10)
1. method of recycling blast furnace gas, it is characterized in that the method for recycling blast furnace gas realizes by following steps: one, blast furnace gas is fed gas holder, blast furnace gas in the gas holder being compressed to pressure then is 0.01～0.1MPa, then blast furnace gas being fed temperature swing adsorption system handles, the inlet temperature of control alternating temperature absorption is 300～400 ℃, temperature out is 170～200 ℃, is purified blast furnace gas; Two, after the purification blast furnace gas that step 1 is obtained is pressurized to 0.2～5MPa, being transported to transformation absorption puies forward the carbon system and adsorbs purification carbon one gas mixture, transformation fractionation by adsorption purification condition is: behind absorption 1min～12min, stop to carry the purification blast furnace gas, in gauge pressure be then-condition of 0.1MPa～0.15MPa under desorption 1min～10min, obtain bulk purity and reach CO and CO more than 95%
2Carbon one gas mixture; Three, will carry the remaining blast furnace gas of discharging carbon system air outlet and be forced into 0.5～3MPa by transformation absorption in the step 2 after, be delivered to transformation absorption again and carry nitrogen system, nitrogen separation is reclaimed, wherein transformation fractionation by adsorption recovering condition is: behind absorption 1～10min, stop to carry, in gauge pressure be then-condition of 0.1MPa～0.5MPa under desorption 1min～10min, obtain bulk purity and reach nitrogen more than 99.5%; Four, will carry the residue blast furnace gas of discharging the nitrogen system air outlet by the transformation absorption of step 3 and be recycled to the coal gas fuel system, promptly finish the recycling of blast furnace gas.
2. a kind of method of recycling blast furnace gas according to claim 1 is characterized in that in the step 1 blast furnace gas in the gas holder being compressed to pressure is 0.03～0.08MPa.
3. a kind of method of recycling blast furnace gas according to claim 1 and 2 is characterized in that the inlet temperature of control alternating temperature absorption in the step 1 is 320～380 ℃, and temperature out is 175～195 ℃.
4. a kind of method of recycling blast furnace gas according to claim 3 is characterized in that having 5～8 adsorption towers in the step 1 in the temperature swing adsorption system.
5. according to claim 1,2 or 4 described a kind of methods of recycling blast furnace gas, it is characterized in that the purification blast furnace gas that in the step 2 step 1 is obtained is pressurized to 0.3～4MPa.
6. a kind of method of recycling blast furnace gas according to claim 5, it is characterized in that transformation fractionation by adsorption purification condition is in the step 2: behind absorption 1min～8min, stopping carry to purify blast furnace gas, is desorption 1min～6min under the condition of 0MPa～0.1MPa in gauge pressure then.
7. according to claim 1,2,4 or 6 described a kind of methods of recycling blast furnace gas, it is characterized in that transformation absorption in the step 2 carries and have 5～8 adsorption towers in the carbon system.
8. a kind of method of recycling blast furnace gas according to claim 7 is characterized in that will carry the remaining blast furnace gas of discharging carbon system air outlet by transformation absorption in the step 2 in the step 3 is forced into 1～2.5MPa.
9. according to claim 1,2,4,6 or 8 described a kind of methods of recycling blast furnace gas, it is characterized in that transformation fractionation by adsorption recovering condition is in the step 3: behind absorption 1min～8min, stopping to carry, is desorption 1min～8min under the condition of 0MPa～0.3MPa in gauge pressure then.
10. a kind of method of recycling blast furnace gas according to claim 9 is characterized in that transformation absorption in the step 3 carries and have 5～8 adsorption towers in the nitrogen system.
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| CN102643681A (en) * | 2011-02-21 | 2012-08-22 | 北京北大先锋科技有限公司 | A technology of blast furnace gas condensation |
| CN102876824A (en) * | 2012-09-12 | 2013-01-16 | 首钢总公司 | Method for guaranteeing high blast temperature by using blast furnace gas |
| CN104190207A (en) * | 2014-08-20 | 2014-12-10 | 衡阳华菱钢管有限公司 | Coal gas purification system and coal gas purification method |
| CN104225951A (en) * | 2014-09-25 | 2014-12-24 | 南京都乐制冷设备有限公司 | Benzene organic vapor recycling device and benzene organic vapor recycling method |
| CN104930865A (en) * | 2015-06-05 | 2015-09-23 | 浙江大学 | Energy-saving blast furnace system utilizing waste heat and excessive pressure to supply oxygen-enriched air itself |
| CN105570095A (en) * | 2015-12-21 | 2016-05-11 | 七台河宝泰隆煤化工股份有限公司 | Coal gas compressing method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102643681A (en) * | 2011-02-21 | 2012-08-22 | 北京北大先锋科技有限公司 | A technology of blast furnace gas condensation |
| CN102876824A (en) * | 2012-09-12 | 2013-01-16 | 首钢总公司 | Method for guaranteeing high blast temperature by using blast furnace gas |
| CN102876824B (en) * | 2012-09-12 | 2014-07-23 | 首钢总公司 | Method for guaranteeing high blast temperature by using blast furnace gas |
| CN104190207A (en) * | 2014-08-20 | 2014-12-10 | 衡阳华菱钢管有限公司 | Coal gas purification system and coal gas purification method |
| CN104190207B (en) * | 2014-08-20 | 2016-03-02 | 衡阳华菱钢管有限公司 | Coal gas purification system and coal gas method of purification |
| CN104225951A (en) * | 2014-09-25 | 2014-12-24 | 南京都乐制冷设备有限公司 | Benzene organic vapor recycling device and benzene organic vapor recycling method |
| CN104225951B (en) * | 2014-09-25 | 2016-02-03 | 南京都乐制冷设备有限公司 | A kind of benzene class organic vapor recovery device and recovery method thereof |
| CN104930865A (en) * | 2015-06-05 | 2015-09-23 | 浙江大学 | Energy-saving blast furnace system utilizing waste heat and excessive pressure to supply oxygen-enriched air itself |
| CN105570095A (en) * | 2015-12-21 | 2016-05-11 | 七台河宝泰隆煤化工股份有限公司 | Coal gas compressing method |
| CN106995864A (en) * | 2017-03-23 | 2017-08-01 | 江苏省冶金设计院有限公司 | Coal gas of converter utilizes system and the method for utilizing coal gas of converter |
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Application publication date: 20101124 |