CN102358849B - Heat recovering type fuel gas preparation system and fuel gas preparation method thereof - Google Patents
Heat recovering type fuel gas preparation system and fuel gas preparation method thereof Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The present invention discloses a heat recovering type fuel gas preparation system. The system comprises: an entrained-flow gasifier, a waste heat boiler connected with the top of the entrained-flow gasifier, and a lock hopper connected with the bottom of the entrained-flow gasifier. The entrained-flow gasifier is provided with at least two secondary oxygen supplying nozzle chambers, wherein the secondary oxygen supplying nozzle chambers are respectively provided with a secondary oxygen supplying nozzle, respectively positioned below a process nozzle chamber provided with a process nozzle, and are symmetrically arranged on the circumference of the main body of the entrained-flow gasifier. The invention further discloses a fuel gas preparation method by adopting the fuel gas preparation system. The method comprises that: an oxidizing agent is introduced to the secondary oxygen supplying nozzle chambers during the gasification reaction process to promote the further gasification reaction; the resulting fuel gas generated from the reaction enters the waste heat boiler to carry out heat recovering; the generated liquid residue is discharged downward by the lock hopper. The system and the method of the present invention have characteristics of strong adaptability of the raw materials, good indicator, flexible operation, sanitation and environmental protection.
Description
Technical field
The present invention relates to a kind of combustion gas preparation system, particularly relate to a kind of heat reclamation type combustion gas preparation system and gas preparation method thereof, it is based on entrained flow gasification and useless pot heat recuperation technology.
Background technology
The annual industrial combustion gas that need to be a large amount of of the industries such as building, building materials, traffic, pottery, glass, metallurgy, machinofacture and light textile that China is widely distributed, for heating various kilns, stove or direct heating product or work in-process.Wherein, as the Sweet natural gas of industrial combustion gas important sources, because the growth of its deliverability and demand is not mated, and domestic natural gas source is limited, causes domestic natural gas supply anxiety, and particularly each relevant enterprise use gas is difficult to guarantee stable supply.Therefore, adopt the combustion gas technology of preparing to prepare the manufactured gas, manufactured fuel gas, become another important channel that meets domestic growing industrial combustion gas demand.
At present, the manufactured gas, manufactured fuel gas that China produces mainly adopts traditional normal pressure to fix (movement) bed gasification furnace technology.In existing manufactured gas, manufactured fuel gas produces, normal pressure is fixed (movement) bed gasification technology and is existed at large the problems such as the kinds of coals for gasification requirement is high, coal particle size large (lump coal), gasification efficiency is low, gasification intensity is low, energy consumption is large, caloric power of gas is low, environmental pollution is large, the disposal of three wastes is poor.Although carried out multinomial improvement for this type of gasification furnace structure for a long time, automatic control level also improves a lot, and certain achievement has also been made in the disposal of three wastes, yet gasification technology does not have the breakthrough of essence, and the problems referred to above fail to be solved.
As from the foregoing, China's industrial combustion gas applied range, total demand is huge, and existing manufactured gas, manufactured fuel gas's technology of preparing falls behind, and kinds of coals for gasification and granularity requirements are high, and environmental pollution is serious.Therefore the combustion gas technology of preparing in the urgent need to a kind of low cost, clean and effective substitutes prior art.
Summary of the invention
The technical problem to be solved in the present invention is to fall behind in order to overcome manufactured gas, manufactured fuel gas's technology of preparing in prior art, kinds of coals for gasification and granularity requirements are high, the defect that environmental pollution is serious, provide a kind of heat reclamation type combustion gas preparation system and gas preparation method thereof, and its cost is low, efficiency is high and free from environmental pollution.
The present invention solves above-mentioned technical problem by following technical proposals: a kind of heat reclamation type combustion gas preparation system, its characteristics are, it comprises: an airflow bed gasification furnace, a waste heat boiler be connected with the top of described airflow bed gasification furnace, and a lock hopper be connected with the bottom of described airflow bed gasification furnace;
Described airflow bed gasification furnace is provided with at least two the secondary oxygen supply nozzle box that establishes a secondary oxygen supply nozzle, described secondary oxygen supply nozzle box lays respectively in one the below of the technique nozzle box that establishes a technique nozzle, and is symmetrically arranged in the surrounding of the main body of described airflow bed gasification furnace.
Arranging of secondary oxygen supply nozzle and secondary oxygen supply nozzle box can be adjusted the oxygen distribution that enters vapourizing furnace, thereby reduces the oxidant content of technique nozzle, and the temperature that suitably provides secondary oxidation dosage to improve the slag-drip opening slag, guarantees the smooth outflow of molten slag.In addition, adopt secondary oxygen supply nozzle can also reduce the consumption of oxygenant and the consumption of raw material.
Wherein, the high-temperature fuel gas after gasification enters waste heat boiler and reclaims sensible heat, can further reduce the temperature of combustion gas, improves the formation efficiency of cold combustion gas.
Preferably, described waste heat boiler arranges a superheat section water wall and an evaporator section water wall from top to bottom, on the surface of described superheat section water wall and the surface of described evaporator section water wall, one dust stratification clearing device all is set.
Preferably, described dust stratification clearing device adopts gas purging or mechanical vibrator.
Like this, the part flying dust in waste heat boiler in combustion gas can be deposited on the water wall surface, thereby further reduces the dustiness of combustion gas.The dust stratification clearing device can be removed the flying dust on water wall surface in time, effectively prevents the decline of heat transfer efficiency.
Preferably, the axis of described technique nozzle box and described vapourizing furnace main body angle α radially are 0 °～45 °; The axis of described technique nozzle box and the angle β of described vapourizing furnace main body axis are 60 °～120 °.
Preferably, the angle r of axis on horizontal plane of the axis of described technique nozzle and described technique nozzle box is 0 °～20 °, and the angle δ on vertical surface is 0 °～20 °.
Preferably, the axis of described secondary oxygen supply nozzle box and described vapourizing furnace main body angle ε radially are 0 °～45 °; The angle ζ of the axis of described secondary oxygen supply nozzle box and the axis of described vapourizing furnace main body is 60 °～120 °.
Preferably, the angle η of axis on horizontal plane of the axis of described secondary oxygen supply nozzle and described secondary oxygen supply nozzle box is 0 °～20 °, and the angle theta on vertical surface is 0 °～20 °.
Setting and coupling by technique nozzle and technique nozzle box, secondary oxygen supply nozzle and secondary oxygen supply nozzle box angle, can in stove, form percussion flow and carry out enhancing mixed (caloic transmission) process, and form the Swirling Flow of varying strength in stove, thereby reach good technique and engineering effort, the available gas composition is high, efficiency of carbon conversion is high.
The present invention also provides a kind of gas preparation method that adopts above-mentioned heat reclamation type combustion gas preparation system, and it comprises: carbonaceous material, oxygenant and steam are passed in described airflow bed gasification furnace and carried out gasification reaction by described technique nozzle box;
Its characteristics are, described method also comprises: in described gasification reaction process, described secondary oxygen supply nozzle box is passed into to oxygenant, promote further gasification reaction; The combustion gas that reaction generates up enters described waste heat boiler through the top of described airflow bed gasification furnace and carries out recovery of heat; The liquid slag generated is discharged by described lock hopper downwards.
Preferably, the gasification operation pressure in described gasification reaction process is 0-8.0MPa.
Preferably, the gas that described oxygenant is oxygen level 21%～100%.
Oxygenant can adopt the oxygen gas mixture that contains of air, pure oxygen or other oxygen level 21%～100%.Here mainly utilized the combustion-supporting property of oxygenant, oxygen and carbonaceous material are burnt, to obtain available gas CO and H
2.
Preferably, the oxygenant that passes into described technique nozzle box accounts for 80%～100% of operating oxidizer, and the oxygenant that passes into secondary oxygen supply nozzle box accounts for 0%～20% of operating oxidizer.
Originally the 100% oxygenant classification that passes into the technique nozzle is passed into to vapourizing furnace, can reduce like this temperature of synthetic gas, improve cold gas efficiency.And pass into the temperature that suitable oxygenant can improve slag in secondary oxygen supply nozzle, and guaranteed that slag discharges with liquid form, avoided stifled slag phenomenon.
Preferably, described carbonaceous material comprises slurry state carbonaceous material and powdery carbonaceous material.
Wherein, when carbonaceous material is the powdery carbonaceous material, oxygenant need to add water vapour synthetic gas agent.Improve the efficiency of combustion of powdery carbonaceous material by vaporized chemical, be convenient to adjust load, reduce disposal of pollutants.
Preferably, described carbonaceous material comprises coal, refinery coke, residual oil, pitch, biomass or mud.
In the present invention, but above-mentioned optimum condition arbitrary combination on the basis that meets this area general knowledge obtains each preferred embodiment of the present invention.
Positive progressive effect of the present invention is: the present invention has adopted the airflow bed gasification furnace of a kind of gas slag shunting and classification oxygen supply, makes the interior temperature distribution of vapourizing furnace more reasonable, has reduced the syngas outlet temperature.Secondary oxygen supply nozzle can significantly reduce the oxidant content of technique nozzle, suitably pass into the secondary oxidation agent and improve vapourizing furnace cinder notch slag temperature, guaranteeing that gasifier slag oral fluid state slag flows, and when avoiding cinder notch to stop up, has significantly reduced the consumption of oxygenant and raw material.Combustion gas after gasification is carried out recovery of heat by a waste heat boiler, has reduced further the fly ash content in the combustion gas, has improved the productive rate of low temperature combustion gas, more clean environment firendly.
The accompanying drawing explanation
The structural representation that Fig. 1 is heat reclamation type combustion gas preparation system of the present invention.
The structural representation that Fig. 2 is airflow bed gasification furnace in the present invention.
The partial enlarged drawing that Fig. 3 is A part in Fig. 2.
The partial enlarged drawing that Fig. 4 is B part in Fig. 2.
The structural representation of the technique nozzle that Fig. 5 is airflow bed gasification furnace in the present invention.
The structural representation of the secondary oxygen supply nozzle that Fig. 6 is airflow bed gasification furnace in the present invention.
Embodiment
Provide preferred embodiment of the present invention below in conjunction with accompanying drawing, to describe technical scheme of the present invention in detail.
As shown in Figure 1, heat reclamation type combustion gas preparation system of the present invention comprises an airflow bed gasification furnace 1, a waste heat boiler 2 and a lock hopper 3.Wherein, waste heat boiler 2 is connected with the top of airflow bed gasification furnace 1, and lock hopper 3 is connected with the bottom of airflow bed gasification furnace 1, thereby forms the system of a preparation combustion gas.
As shown in Figure 2, airflow bed gasification furnace 2 adopts entrained-flow bed gasifier with staged oxygen feeding, and it comprises at least two technique nozzle boxs 11 and two secondary oxygen supply nozzle boxs 13.Interior in each technique nozzle box 11 a technique nozzle 12 is set.Technique nozzle box 11 is arranged at the bottom of the main body of airflow bed gasification furnace 1, and be symmetrically arranged in equably the surrounding of the main body of airflow bed gasification furnace 1, for inputting carbonaceous material and partial oxygen agent (be vaporized chemical for pulverulent material, i.e. oxygenant and water vapor).Accordingly, establish a secondary oxygen supply nozzle 14 in each secondary oxygen supply nozzle box 13.Secondary oxygen supply nozzle box 13 is positioned at respectively the below of technique nozzle box 11 accordingly, and is symmetrically arranged in the surrounding of the main body of airflow bed gasification furnace 1.
Arranging of secondary oxygen supply nozzle 14 and secondary oxygen supply nozzle box 13 can be adjusted the oxygen distribution that enters vapourizing furnace, thereby reduce the oxidant content of technique nozzle, and the temperature that suitably provides secondary oxidation dosage to improve the slag-drip opening slag, guarantee the smooth outflow of molten slag.In addition, adopt secondary oxygen supply nozzle 14 can also reduce the consumption of oxygenant and the consumption of raw material.
As shown in Fig. 3-Fig. 6, preferably, the main body of the axis of technique nozzle box 11 and airflow bed gasification furnace 1 angle α radially is 0 °～45 °; The angle β of the main body axis of the axis of technique nozzle box 11 and airflow bed gasification furnace 1 is 60 °～120 °.The angle r of the axis of the axis of technique nozzle 12 and technique nozzle box 11 on horizontal plane is 0 °～20 °, and the angle δ on vertical surface is 0 °～20 °.The axis of secondary oxygen supply nozzle box 13 and the main body of airflow bed gasification furnace 1 angle ε radially are 0 °～45 °; The angle ζ of the axis of the axis of secondary oxygen supply nozzle box 13 and the main body of airflow bed gasification furnace 1 is 60 °～120 °.The angle η of the axis of the axis of secondary oxygen supply nozzle 14 and secondary oxygen supply nozzle box 13 on horizontal plane is 0 °～20 °, and the angle theta on vertical surface is 0 °～20 °.
Setting and coupling by technique nozzle 12 and technique nozzle box 11, secondary oxygen supply nozzle 14 and secondary oxygen supply nozzle box 13 angles, can in stove, form percussion flow and carry out enhancing mixed (caloic transmission) process, and form the Swirling Flow of varying strength in stove, thereby reach good technique and engineering effort, the available gas composition is high, efficiency of carbon conversion is high.
After 1 gasification of said flow bed gasification furnace, high-temperature fuel gas enters waste heat boiler 2 (as shown in Figure 1) by the top of airflow bed gasification furnace 1.Then, high-temperature fuel gas is successively by a superheat section water wall 21 and an evaporator section water wall 22 in waste heat boiler 2.Like this, the part flying dust in high-temperature fuel gas can be deposited on the water wall surface, can further reduce the combustion gas dustiness.Further, on the surface of superheat section water wall 21 and the surface of evaporator section water wall 22, a dust stratification clearing device all is set.Preferably, described dust stratification clearing device adopts the mode of gas purging or mechanical vibrator, has effectively prevented that the water wall heat transfer efficiency that the flying dust deposition causes from descending.
In addition, the lime-ash major part after gasification is discharged through lock hopper 3 with liquid form by the bottom of airflow bed gasification furnace 1.Wherein, lock hopper 3 is controlled by valve member, can realize that like this discharge the intermittence of lime-ash, convenient operation personnel's control and management.And, after heat recuperation, the flying dust of removing on the dust stratification clearing device is discharged by the bottom outlet 23 of waste heat boiler 2, and the sensible heat of the high-temperature fuel gas that waste heat boiler 2 is reclaimed is for byproduct steam.The steam generated can have the rear system needed to use for airflow bed gasification furnace 1 or other.Wherein, bottom outlet 23 can adopt ash bucket, for collecting by the flying dust of removing on the dust stratification clearing device, and regularly discharges.Whole system both can generate clean combustion gas, had recycled again heat, had realized the effect of environmental protection and energy saving.
The present invention also provides the gas preparation method that adopts above-mentioned heat reclamation type combustion gas preparation system, and it comprises following process:
The entrained-flow bed gasifier with staged oxygen feeding of 4 nozzles of take is example, carbonaceous material pressurizes through surge pump, by 4 technique nozzles that are arranged symmetrically in vapourizing furnace main body top same level, with the oxygenant (as the oxygen gas mixture that contains of air, pure oxygen or other oxygen level 21%～100%) of oxygen level 21%～100%, together by the technique nozzle, pass into vapourizing furnace.
The gasification of carbonaceous material in vapourizing furnace mainly is divided into primary first-order equation and secondary reaction:
Primary first-order equation betides combustion zone.When carbonaceous material blending oxidizing agent/vaporized chemical enters the vapourizing furnace burning by the technique nozzle, carbonaceous material is atomized.While is owing to being subject to the radiant heat such as flame, stove inwall, high-temperature gas, solids, and the heat effects of reflow stream thigh and baffling stream thigh, and carbonaceous material evaporates rapidly, thermo-cracking occurs and also discharge volatile matter.Large calorimetric is emitted in split product, volatile matter and the perfect combustion under high temperature, hyperoxia concentration of other inflammable components simultaneously.
In this process, the present invention has only dropped into the partial oxygen agent, accounts for 80%～100% of operating oxidizer, guarantee that gasification reaction carries out smoothly, and the temperature of synthetic gas is without more than reaching coal ash fusion temperature (FT).Due to the effect of vapourizing furnace inner high voltage, synthetic gas is up walked, and by the syngas outlet at vapourizing furnace main body top, is discharged.Synthetic gas is lowered the temperature in the upper process of walking, and makes the gas temperature of syngas outlet lower.
In said process, pass into remaining oxygenant by secondary oxygen supply nozzle in vapourizing furnace, account for 0%～20% of operating oxidizer.The oxygenant here further promotes gasification reaction, and more than Operational Temperature for Entrained Flow Gasifiers rises to coal ash fusion temperature (FT), the temperature of slag is brought up to more than 1300 ℃, thereby realizes the high-temperature liquid state deslagging.The lime-ash that gasification produces is discharged through lock hopper with liquid form by the entrained flow gasification furnace bottom.
Then, the mixture after burning enters secondary reaction.Wherein, the coal tar in component, CH
4deng with water, CO
2the generating gasification reaction.This gasification reaction generates available gas composition CO and H
2.
Because secondary reaction be take heat absorption as main, can reduce to a certain extent the temperature of conversion zone, relatively play the effect of protection refractory liner.
Then, the combustion gas of generation is passed into to waste heat boiler by the top of airflow bed gasification furnace.Now, the fuel gas temperature of entrained flow gasification outlet of still is 700～1200 ℃.Superheat section water wall and evaporator section water wall are passed through in this combustion gas successively, carry out the recovery of high temperature sensible heat.
Then, carry out byproduct steam with the heat reclaimed.The steam generated can be for airflow bed gasification furnace or rear system.The process of whole heat recuperation makes the fly ash content of combustion gas further reduce, and the temperature of the clean fuel gas of generation is reduced to 150～500 ℃.
Finally, the molten slag that gasification reaction generates is discharged by the lock hopper of entrained flow gasification furnace bottom, has avoided the generation of stifled slag phenomenon.And the flying dust that is deposited on the water wall surface is collected in regularly discharge of ，You bottom, waste heat boiler bottom outlet after purging removing by the dust stratification clearing device.
Further, the gasification operation pressure in described gasification reaction process is 0-8.0MPa.Because the capacity in vapourizing furnace is larger, also corresponding increasing of required gasification operation pressure.Therefore, this gasification operation force value need to be determined according to actual gasification and customer requirements.
In addition, above-mentioned carbonaceous material can be for slurry state carbonaceous material and powdery carbonaceous material, as coal, refinery coke, residual oil, pitch, biomass or mud.Wherein, when carbonaceous material is the powdery carbonaceous material, oxygenant need to add water vapour synthetic gas agent.By vaporized chemical, the efficiency of combustion of powdery carbonaceous material is improved, be convenient to adjust load, reduce disposal of pollutants.
For the present invention is described better, below provides a typical case to implement example and further illustrate:
Example: the scale of processing 75 tons, coal with day prepares combustion gas, adopts the fine coal charging, and coal analysis as shown in Table 1.
Table one, coal analysis table
Process conditions and combustion gas index are as follows:
Gasification system pressure 0.5MPa (G), adopt air as oxygenant, 270 ℃ of air preheating temperatures, 800 ℃ of top of gasification furnace outlet fuel gas temperatures, 500 ℃ of waste heat boiler outlet fuel gas temperatures, gas flow 14637Nm
3/ h, CO+H in combustion gas
2+ CH
4content 39.62%, waste heat boiler by-product 4.0MPa (G), 390 ℃ of superheated vapour～2.3t/h.
As can be seen here, combustion gas preparation system of the present invention can further reduce the temperature of combustion gas, effectively improves cleanliness factor and the production efficiency of combustion gas.And, carry out byproduct steam by recycling heat, both saved the energy, solved again problem of environmental pollution.The advantages such as therefore, whole gas preparation method has that adaptability to raw material is strong, index is good, flexible operation and clean environment firendly.
Although more than described the specific embodiment of the present invention, it will be understood by those of skill in the art that these only illustrate, protection scope of the present invention is limited by appended claims.Those skilled in the art, under the prerequisite that does not deviate from principle of the present invention and essence, can make various changes or modifications to these embodiments, but these changes and modification all fall into protection scope of the present invention.
Claims (8)
1. a heat reclamation type combustion gas preparation system, is characterized in that, it comprises: an airflow bed gasification furnace, a waste heat boiler be connected with the top of described airflow bed gasification furnace, and a lock hopper be connected with the bottom of described airflow bed gasification furnace;
Described airflow bed gasification furnace is provided with at least two the secondary oxygen supply nozzle box that establishes a secondary oxygen supply nozzle, described secondary oxygen supply nozzle box lays respectively in one the below of the technique nozzle box that establishes a technique nozzle, and is symmetrically arranged in the surrounding of the main body of described airflow bed gasification furnace;
Described waste heat boiler arranges a superheat section water wall and an evaporator section water wall from top to bottom, on the surface of described superheat section water wall and the surface of described evaporator section water wall, one dust stratification clearing device all is set;
The axis of described technique nozzle box and described vapourizing furnace main body angle α radially are 0 °～45 °; The axis of described technique nozzle box and the angle β of described vapourizing furnace main body axis are 60 °～120 °; The angle r of the axis of the axis of described technique nozzle and described technique nozzle box on horizontal plane is 0 °～20 °, and the angle δ on vertical surface is 0 °～20 °; The axis of described secondary oxygen supply nozzle box and described vapourizing furnace main body angle ε radially are 0 °～45 °; The angle ζ of the axis of described secondary oxygen supply nozzle box and the axis of described vapourizing furnace main body is 60 °～120 °; The angle η of axis on horizontal plane of the axis of described secondary oxygen supply nozzle and described secondary oxygen supply nozzle box is 0 °～20 °, and the angle theta on vertical surface is 0 °～20 °.
2. combustion gas preparation system as claimed in claim 1, is characterized in that, described dust stratification clearing device adopts gas purging or mechanical vibrator.
3. a gas preparation method that adopts heat reclamation type combustion gas preparation system as claimed in claim 1, it comprises: carbonaceous material, oxygenant and steam are passed in described airflow bed gasification furnace and carried out gasification reaction by described technique nozzle box;
It is characterized in that, described method also comprises: in described gasification reaction process, described secondary oxygen supply nozzle box is passed into to oxygenant, promote further gasification reaction; The combustion gas that reaction generates up enters described waste heat boiler through the top of described airflow bed gasification furnace and carries out recovery of heat; The liquid slag generated is discharged by described lock hopper downwards.
4. combustion gas preparation technology as claimed in claim 3, is characterized in that, the gasification operation pressure in described gasification reaction process is 0-8.0MPa.
5. combustion gas preparation technology as claimed in claim 3, is characterized in that, the gas that described oxygenant is oxygen level 21%～100%.
6. combustion gas preparation technology as claimed in claim 3, is characterized in that, the oxygenant that passes into described technique nozzle box accounts for 80%～100% of operating oxidizer, and the oxygenant that passes into secondary oxygen supply nozzle box accounts for 0%～20% of operating oxidizer.
7. combustion gas preparation technology as claimed in claim 3, is characterized in that, described carbonaceous material comprises slurry state carbonaceous material and powdery carbonaceous material.
8. combustion gas preparation technology as claimed in claim 3, is characterized in that, described carbonaceous material comprises coal, refinery coke, residual oil, pitch, biomass or mud.
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| CN103374418B (en) * | 2012-04-27 | 2017-05-17 | 任相坤 | Entrained-flow bed gasification method of sludge and pulverized coal |
| DK2931840T3 (en) * | 2012-12-12 | 2017-05-01 | Ammann Schweiz Ag | Process and plant for making a binder foam for the asphalt manufacture |
| CN104976760B (en) * | 2015-06-18 | 2018-08-28 | 关要领 | Half gasfication atmospheric hot-water boiler |
| CN108410508A (en) * | 2018-05-14 | 2018-08-17 | 北京金泰瑞和工程科技有限公司 | High gas yield dry coal powder pressure gasifying reactor |
| CN108517227B (en) * | 2018-06-27 | 2023-09-15 | 华东理工大学 | Industrial gas preparation system and industrial gas preparation method |
| CN112961707B (en) * | 2021-02-19 | 2022-06-24 | 新奥科技发展有限公司 | Fly ash furnace returning device, coal catalytic gasification system and fly ash furnace returning method |
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