CN201040750Y - Coke oven gas converter - Google Patents
Coke oven gas converter Download PDFInfo
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- CN201040750Y CN201040750Y CNU2007200795678U CN200720079567U CN201040750Y CN 201040750 Y CN201040750 Y CN 201040750Y CN U2007200795678 U CNU2007200795678 U CN U2007200795678U CN 200720079567 U CN200720079567 U CN 200720079567U CN 201040750 Y CN201040750 Y CN 201040750Y
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- coke
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Abstract
The utility model discloses a coke oven gas reformer, the structure of which includes an oxygen inlet, a coke oven gas inlet, a burner on top of the oven, an oven body, a distribution arch at the bottom of the oven, and a reformed gas outlet. The oven body casing includes a casing and a refractory layer from outside to inside. The oven cavity is divided into a recirculation zone, a frame combustion zone, a jet flow zone and a pipe flow zone. The proportion of the height (h) of the jet flow zone and the oven body inner diameter (phi) is 1.8-2.4/1; the proportion of the oven body inner diameter (phi) and the height (h1) of the jet flow zone is 0.9-1.5/1; the proportion of the oven cavity height (H) and the oven body inner diameter (phi) is 2.7-3.9/1. Compared to the existing technology, the utility model can both meet the oxidation process operation requirements of the non-catalytic site and the catalytic site of the coke oven gas. And the utility model is simple in structure, stable in operation, low in cost, and can improve the synthesis methanol conversion and reduce energy consumption.
Description
Technical field
The utility model relates to chemical process equipment, particularly relates to a kind of coke(oven)gas non-catalytic partial oxidation technology operating requirement that both can satisfy, and can satisfy the coke(oven)gas converter of coke(oven)gas catalytic oxidation process operating requirement again.
Background technology
The coke(oven)gas converter is that coke(oven)gas is one of key equipment in the chemical plant installationss such as raw material production synthetic ammonia or production synthesizing methanol.At present, utilize the method for coke(oven)gas portion oxidation synthesis gas to be divided into catalyzing part oxidation method and non-catalytic partial oxidation method, therefore the coke(oven)gas converter that adopts at present mostly designs according to coke(oven)gas catalytic oxidation process operating requirement or coke(oven)gas non-catalytic partial oxidation technology operating requirement.
According to coke(oven)gas catalytic oxidation process operating requirement, the coke(oven)gas converter of design specialized, owing to will load nickel series conversion catalyzer in the coke(oven)gas converter in the technological process, needing filling copper in the synthetic tower of synthesizing methanol in the back operation is catalst for synthesis of methanol, and the sulfide in the coke(oven)gas etc. are the main poisonous substances of catalyzer, all toxic to catalytic converting catalyst and methanol synthesis catalyst, can cause used poisoning of catalyst inactivation, directly influence total system and normally move.So require to raw coke oven gas carry out strict desulfurization (require usually contained organic sulfide and inorganic sulphide in the coke(oven)gas total amount should≤0.1ppm).But, contain a lot of difficult organosulfurs that remove in the coke(oven)gas, it is more particularly to contain thiophene phenol, contains more CO, CO in the coke(oven)gas in addition
2, alkene and hydrogen, can not adopt common cobalt-molybdenum hydrogenation catalyst with the inorganic sulfur H of the thorough hydrocracking of organosulfurs such as thiophene phenol for easily removing
2S (because the strong exothermal reaction of CO, CO2, hydrogenation of olefins can take place).Cause when adopting the coke(oven)gas catalytic oxidation process, adopted very complicated sulfur removal technology, but sweetening effectiveness is still unsatisfactory.In addition, on the top of coke(oven)gas catalyzing part oxidation converter inner catalyst layer is the space of carrying out the partial oxidation combustion reactions for coke(oven)gas, the design of furnace roof burner and processing and manufacturing, the fluctuation of system loading intensity in service, the operating fluctuation of automatic control system, the height of Operational Control Level etc., the capital influences the variation of the furnace roof burner length of flame and the uniform distribution of furnace roof room temps and hot-fluid, as long as flame front or superheated air-flow touch the conversion catalyst in the stove, very short time (as long as generally the several minutes time) will make the conversion catalyst fusion, agglomerate, system can't normally be moved, can be directed at the generation major accident when serious.Similar accident all took place in the coke(oven)gas catalyzing part oxidation converter of the factory of the employing coke(oven)gas catalytic oxidation process that has put into operation.
The technical process of non-catalytic partial oxidation method is short (during high temperature, gas actual stop in stove can be finished reaction in about 0.6 second), the converter volume is less and simple in structure, (can adopt unstripped gas adaptability is good from Sweet natural gas, refinery gas, coke(oven)gas, light oil, heavy oil, residual oil is to pitch, coal water slurry etc.), requirement to impurity and poisonous substance in the feed stock for blast furnace coke(oven)gas is looser, and can in about 30 minutes, not need cooling reactor just can change to be another kind of unstripped gas, help improving reaction pressure and reach energy-saving effect, and the organic sulfides such as thiophene phenol that contain in the coke(oven)gas in the reaction of on-catalytic high-temp combustion all change the inorganic sulfur H that is easy to remove into
2S (after the reforming gas cooling of coming out of the stove, promptly can guarantee to reach the strict demand of total sulfur≤0.1ppm level with conventional sulfur method); Because do not adorn catalyzer in the stove, do not worry that the variation of the furnace roof length of flame, heat flux distribution and temperature distribution variation cause the impaired accident of catalyzer yet.Obviously coke(oven)gas non-catalytic partial oxidation technology has series of advantages, but adopts elevated pressures to carry out coke(oven)gas high temperature non-catalytic partial oxidation preparing synthetic gas, and device structure, material and operation control aspect have been increased difficulty.The present domestic example that does not still adopt coke(oven)gas non-catalytic partial oxidation Technology system synthesizing methanol synthetic gas actual motion.
The utility model content
The purpose of this utility model is exactly at the deficiencies in the prior art, a kind of coke(oven)gas non-catalytic partial oxidation technology operating requirement that both can satisfy is provided, can satisfy coke(oven)gas catalytic oxidation process operating requirement again, and simple in structure, stable, cost is lower, can improve the synthesizing methanol transformation efficiency, save the coke(oven)gas converter of energy consumption.
For achieving the above object, the technical solution of the utility model is as follows:
The coke(oven)gas converter that the utility model proposes, its structure comprise oxygen intake, coke(oven)gas inlet, be positioned at burner, the body of heater of furnace roof, be positioned at the distribution arch of furnace bottom, and the reforming gas outlet.Described body of heater shell comprises housing and flame retardant coating from outside to inside, and described housing adopts metal material, and described flame retardant coating has thermal insulation, fireproof function.Furnace chamber is divided into recirculating zone, flame district, fluerics and Guan Liuqu from top to bottom; There is obvious effect described recirculating zone to keeping flame stabilization; In described fluerics, distribute all inhomogeneous along the air flow line of furnace chamber radial section and the composition of velocity distribution, temperature distribution, heat flux distribution and gas; In described Guan Liuqu, along the more even rules such as composition of the air flow line of furnace chamber radial section and distribution, heat flux distribution, temperature distribution, gas.Ratio between fluerics height h and the body of heater internal diameter φ is 1.8～2.4/1, wherein preferred 2.0～2.2/1; Body of heater internal diameter φ and Guan Liuqu height h
1Between ratio be 0.9～1.5/1, wherein preferred 1.0～1.3/1; Ratio between furnace chamber overall height H and the body of heater internal diameter φ is 2.7～3.9/1, wherein preferred 3.0～3.3/1.
Can or not load partial oxidation catalyst in described Guan Liuqu filling.When Guan Liuqu does not load the coke(oven)gas partial oxidation catalyst, can satisfy the requirement of coke(oven)gas non-catalytic partial oxidation technology operation; In the time of necessary, can so just can change into by coke(oven)gas catalytic oxidation process technical qualification and move at the Guan Liuqu of described coke(oven)gas converter filling coke(oven)gas partial oxidation catalyst.Described coke(oven)gas converter can adapt to " on-catalytic " and " catalysis " two condition runnings, has eliminated the risk when adopting uncatalysed processes.When pressing the catalytic oxidation process operation, partial oxidation catalyst be seated in temperature lower and evenly, air-flow distribution uniform, heat flux distribution Guan Liuqu uniformly, the temperature range of Guan Liuqu is 1000 ℃～1250 ℃, can avoid taking place the converter of the existing coke(oven)gas catalytic oxidation process of having built and the accident that conversion catalyst is often burnt out.Described coke(oven)gas converter goes for pure oxygen or the operation of oxygen-rich air condition, promptly is applicable to the requirement of the synthetic gas of system synthesizing methanol synthetic gas or system synthetic ammonia.
The described burner that is positioned at furnace roof can adopt multilayer sleeve formula structure, or the center tube structure of employing band shape tangential admission etc.Described reforming gas exit can be provided with the donkey boiler of heat exchange cooling, or adopts water spray Quench reforming gas etc.
Compared with prior art, the beneficial effects of the utility model are: both can move by non-catalytic partial oxidation technology, promote to realize coke(oven)gas non-catalytic partial oxidation technology, can move by catalytic oxidation process again, eliminated the risk that adopts non-catalytic partial oxidation technology; And the utility model is simple in structure, stable, reduce investment outlay about 8%～10%, the ratio of hydrogen and CO, CO2 will be when adopting Catalytic processes in the composition of synthetic gas about 2.67 reduces to about 2.1 (optimum ratio should be 2～2.05 in theory) of adopting uncatalysed processes, not only can improve the synthesizing methanol transformation efficiency, save energy consumption, and can consume, reduce discharge amount of exhaust gas by the conservation coke(oven)gas.
Description of drawings
Fig. 1 is coke(oven)gas structure of reborner figure.
Fig. 2 is the partial oxidation catalyst filling mode synoptic diagram in the coke(oven)gas converter.
Fig. 3 is the flow area synoptic diagram in the coke(oven)gas converter.
Number in the figure is as follows:
1 burner, 2 flame retardant coatings
3 housings 4 distribute and encircle
5 oxygen intakes, 6 coke(oven)gas inlet
7 reforming gas export 8 recirculating zones
10 fluericses, 9 flame districts
11 Guan Liu districts, 12 refractory layers
13 heat resistant catalysts, 14 conversion catalysts
Embodiment
Below in conjunction with accompanying drawing, preferred embodiment of the present utility model is further described.
Embodiment one
As Fig. 1, Fig. 2, shown in Figure 3.Make the coke(oven)gas converter, this coke(oven)gas structure of reborner comprises oxygen intake 5, coke(oven)gas inlet 6, be positioned at burner 1, the body of heater of furnace roof, be positioned at the distribution arch 4 of furnace bottom, and reforming gas outlet 7.Described burner 1 adopts multilayer sleeve formula structure, and described reforming gas exports the donkey boiler that 7 places are provided with the heat exchange cooling.The body of heater shell comprises metal shell 3 and flame retardant coating 2 from outside to inside.Described furnace chamber is divided into recirculating zone 8, flame district 9, fluerics 10 and Guan Liuqu 11 from top to bottom.Ratio between fluerics height h and the body of heater internal diameter φ is 2.4/1, body of heater internal diameter φ and Guan Liuqu height h
1Between ratio be 1.5/1, the ratio between furnace chamber overall height H and the body of heater internal diameter φ is 3.9/1.The temperature of the Guan Liuqu 11 of described coke(oven)gas converter is 1000 ℃, wherein is filled with partial oxidation catalyst, and partial oxidation catalyst comprises heat resistant catalyst 13 and conversion catalyst 14, and they are arranged in the below of Guan Liuqu 11 refractory layers 12 of furnace chamber.
Embodiment two
As Fig. 1, shown in Figure 3.Make the coke(oven)gas converter, this coke(oven)gas structure of reborner comprises oxygen intake 5, coke(oven)gas inlet 6, be positioned at burner 1, the body of heater of furnace roof, be positioned at the distribution arch 4 of furnace bottom, and reforming gas outlet 7.Described burner 1 adopts the center tube structure of band shape tangential admission, and described reforming gas exports 7 places and adopts water spray Quench reforming gas.The body of heater shell comprises metal shell 3 and flame retardant coating 2 from outside to inside.Described furnace chamber is divided into recirculating zone 8, flame district 9, fluerics 10 and Guan Liuqu 11 from top to bottom.Ratio between fluerics height h and the body of heater internal diameter φ is 1.8/1, body of heater internal diameter φ and Guan Liuqu height h
1Between ratio be 0.9/1, the ratio between furnace chamber overall height H and the body of heater internal diameter φ is 2.7/1.Do not load partial oxidation catalyst among the Guan Liuqu 11 of described coke(oven)gas converter.
Embodiment three
As Fig. 1, Fig. 2, shown in Figure 3.The place identical with embodiment one be repeated description no longer, and difference is: the ratio between fluerics height h and the body of heater internal diameter φ is 2.2/1, body of heater internal diameter φ and Guan Liuqu height h
1Between ratio be 1.3/1, the ratio between furnace chamber overall height H and the body of heater internal diameter φ is 3.3/1.The temperature of the Guan Liuqu 11 of described coke(oven)gas converter is 1250 ℃.
Embodiment four
As Fig. 1, shown in Figure 3.The place identical with embodiment two be repeated description no longer, and difference is: the ratio between fluerics height h and the body of heater internal diameter φ is 2.0/1, body of heater internal diameter φ and Guan Liuqu height h
1Between ratio be 1.0/1, the ratio between furnace chamber overall height H and the body of heater internal diameter φ is 3.0/1.
Claims (9)
1. coke(oven)gas converter, this coke(oven)gas structure of reborner comprise oxygen intake (5), coke(oven)gas inlet (6), the burner (1) that is positioned at furnace roof, body of heater, are positioned at the distribution arch (4) of furnace bottom, and reforming gas outlet (7); The body of heater shell comprises housing (3) and flame retardant coating (2) from outside to inside; Furnace chamber is divided into recirculating zone (8), flame district (9), fluerics (10) and Guan Liuqu (11), it is characterized in that: the ratio between fluerics height (h) and the body of heater internal diameter (φ) is 1.8～2.4/1, body of heater internal diameter (φ) and Guan Liuqu height (h
1) between ratio be 0.9～1.5/1, the ratio between furnace chamber total height (H) and the body of heater internal diameter (φ) is 2.7～3.9/1.
2. coke(oven)gas converter according to claim 1 is characterized in that: the ratio between fluerics height (h) and the body of heater internal diameter (φ) is 2.0～2.2/1, body of heater internal diameter (φ) and Guan Liuqu height (h
1) between ratio be 1.0～1.3/1, the ratio between furnace chamber total height (H) and the body of heater internal diameter (φ) is 3.0～3.3/1.
3. coke(oven)gas converter according to claim 1 and 2 is characterized in that: Guan Liuqu (11) loads or does not load partial oxidation catalyst.
4. coke(oven)gas converter according to claim 3 is characterized in that: when Guan Liuqu (11) filling partial oxidation catalyst, it is 1000 ℃～1250 ℃ Guan Liuqu (11) that partial oxidation catalyst is seated in temperature range.
5. according to claim 1 or 2 or 4 described coke(oven)gas converters, it is characterized in that: burner (1) adopts multilayer sleeve formula structure, or adopts the center tube structure of band shape tangential admission.
6. coke(oven)gas converter according to claim 3 is characterized in that: burner (1) adopts multilayer sleeve formula structure, or adopts the center tube structure of band shape tangential admission.
7. according to claim 1 or 2 or 4 or 6 described coke(oven)gas converters, it is characterized in that: reforming gas outlet (7) locates to be provided with the donkey boiler of heat exchange cooling, or adopts water spray Quench reforming gas.
8. coke(oven)gas converter according to claim 3 is characterized in that: reforming gas outlet (7) locates to be provided with the donkey boiler of heat exchange cooling, or adopts water spray Quench reforming gas.
9. coke(oven)gas converter according to claim 5 is characterized in that: reforming gas outlet (7) locates to be provided with the donkey boiler of heat exchange cooling, or adopts water spray Quench reforming gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200795678U CN201040750Y (en) | 2007-05-18 | 2007-05-18 | Coke oven gas converter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200795678U CN201040750Y (en) | 2007-05-18 | 2007-05-18 | Coke oven gas converter |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201040750Y true CN201040750Y (en) | 2008-03-26 |
Family
ID=39252457
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007200795678U Expired - Fee Related CN201040750Y (en) | 2007-05-18 | 2007-05-18 | Coke oven gas converter |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201040750Y (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101891150A (en) * | 2010-07-09 | 2010-11-24 | 太原重工股份有限公司 | Reborner for reforming coke-oven gas |
| CN102020244A (en) * | 2009-09-10 | 2011-04-20 | 巴布考克日立株式会社 | Conversion furnace |
| CN102923658A (en) * | 2012-11-16 | 2013-02-13 | 华东理工大学 | Converter for oxidation of non-catalytic part of gaseous hydrocarbon and application thereof |
-
2007
- 2007-05-18 CN CNU2007200795678U patent/CN201040750Y/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102020244A (en) * | 2009-09-10 | 2011-04-20 | 巴布考克日立株式会社 | Conversion furnace |
| CN102020244B (en) * | 2009-09-10 | 2013-02-27 | 巴布考克日立株式会社 | Conversion furnace |
| CN101891150A (en) * | 2010-07-09 | 2010-11-24 | 太原重工股份有限公司 | Reborner for reforming coke-oven gas |
| CN101891150B (en) * | 2010-07-09 | 2011-12-07 | 太原重工股份有限公司 | Reborner for reforming coke-oven gas |
| CN102923658A (en) * | 2012-11-16 | 2013-02-13 | 华东理工大学 | Converter for oxidation of non-catalytic part of gaseous hydrocarbon and application thereof |
| CN102923658B (en) * | 2012-11-16 | 2015-04-08 | 华东理工大学 | Converter for oxidation of non-catalytic part of gaseous hydrocarbon and application thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080326 Termination date: 20130518 |