CN105561889A - Radial flow by-product steam isothermal shift converter - Google Patents
Radial flow by-product steam isothermal shift converter Download PDFInfo
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- CN105561889A CN105561889A CN201410572326.1A CN201410572326A CN105561889A CN 105561889 A CN105561889 A CN 105561889A CN 201410572326 A CN201410572326 A CN 201410572326A CN 105561889 A CN105561889 A CN 105561889A
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Abstract
The invention relates to the technical field of chemical engineering, in particular to a radial flow by-product steam isothermal shift converter. The radial by-product steam isothermal shift converter disclosed by the invention comprises a pressured furnace body, a catalyst bed, a gas distribution cylinder and a gas collector, and is characterized in that a raw material gas inlet and a water outlet are formed in the upper part of the pressured furnace body; a gas distributor is arranged in the pressured furnace body at the raw material gas inlet; a shift gas outlet and a water inlet are formed in the lower part of the pressured furnace body; the gas distribution cylinder is arranged between the inner wall of the pressured furnace body and the catalyst bed; the gas collector is arranged at the central axis of the pressured furnace body; a vertical heat extraction device is arranged in the catalyst bed, and comprises two ring-shaped tube boxes which are respectively arranged at the upper and lower positions of the catalyst red; a plurality of vertical column tubes are connected between the two ring-shaped tube boxes, and penetrate through the catalyst bed; the upper ring-shaped tube box is communicated with the water outlet; the lower ring-shaped tube box is communicated with the water inlet.
Description
Technical field
The present invention relates to chemical technology field, particularly relate to a kind of Radial Flow byproduct steam formula isothermal change furnace.
Background technology
With coal be in recent years raw material produce artificial oil, synthetic ammonia, methyl alcohol coal chemical technology greatly developed, wherein to prepare the application of the typical process of conversion gas particularly general for CO sulphur-resistant conversion.In coal gasification corollary apparatus, carbon monoxide conversion device regulates the hydrogen/carbon content of gasification installation output raw gas by transformationreation, meet the needs of downstream product, the selection of its technology, in conjunction with the feature of the raw gas of different gasifying process output, also should to consider the requirement of follow up device and downstream product.The composition difference of the raw gas of various gasifying process output is comparatively large, even if for downstream identical product, the conversion process technology supporting from different gasifying process is also not quite similar.The selection of conversion process, except should adapting to raw gas composition and meeting except product requirement, also should consider the problems such as safe and energy-conservation.Secure context, emphasis should avoid the overtemperature of change furnace; Energy-conservation aspect, emphasis should reduce steam consumption and effectively utilize waste heat.According to the configuring condition of conversion process in whole process for purifying of current big-and-middle-sized factory, catalyst and the heat recovery mode of conversion use are very crucial, which determine the flow process configuration of conversion process and the advance of technique.Conversion process is operation important in Coal Chemical Industry technique, and effect is by H
2o and excessive CO changes H into
2and CO
2.The degree of depth of carbon monodixe conversion needed for downstream product can be different.Require when hydrogen manufacturing, synthetic ammonia that the CO in raw gas is all transformed to H2 as far as possible, adopts and converts completely; Only require that the H2/CO in conversion gas reaches certain proportion when methyl alcohol processed, artificial oil, carbonyl product, adopt Partial Transformation can meet the requirement of synthesis gas.
The Axial response type of furnace of what current most conversion process adopted is heat-insulating.Water-gas enters in change furnace from top, carry out reaction through beds to generate hydrogen and carbon dioxide gas and discharge amount of heat simultaneously, hydrogen and carbon dioxide gas and unreacted water-gas etc. enter waste heat boiler (or claiming heat exchanger) from lower part outlet and carry out heat exchange, enter the second change furnace after the heat absorption of high-temperature gas being lowered the temperature and again carry out transformationreation, carry out three grades or fourth-order reaction successively.
The chemical reaction that reaction bed mainly carries out:
CO+H
2O→H
2+CO
2+Q
The shortcoming that heat-insulating change furnace exists:
1. change furnace interior reaction temperature is wayward, and the heat of reaction discharged in course of reaction can not be withdrawn from time, therefore can cause catalyst burn-off phenomenon, the low conversion rate of one section of change furnace;
2. catalyst bed layer height is higher, and synthetic reaction resistance drop is large, and the more resistance drops of number of units of series connection are larger, and energy consumption is larger, and three train overall presure drops are up to 0.5 ~ 0.8MPa;
3. due to the architectural feature of adiabatic reaction, cause the metal temperature of equipment compression shell higher, compression shell thickness is thick, high to the requirement of material, and equipment manufacturing cost is expensive.
Chinese invention patent " CO overall diameter is to isothermal change furnace " (CN201210378026.0) discloses a kind of CO overall diameter to isothermal change furnace, it comprises body of heater, the heat-exchanging tube bundle be arranged in described body of heater, gas distributor, gas collector and upper and lower tube sheet, it is characterized in that described body of heater comprise be detachably connected epimere, stage casing and hypomere, the top of described body of heater is also provided with conversion gas outlet; The lower end of described gas collector connects described lower perforated plate, and described upper perforated plate is provided with connecting hole, and the upper end of described gas collector to removably connect escape pipe through this connecting hole; The other end of this escape pipe exports through described conversion gas and exposes to described body of heater; The upper seal of described upper perforated plate connects annular upper cover, and described lower perforated plate is tightly connected described body of heater between described stage casing and described hypomere.Its shortcoming is: the unstripped gas of device is enterprising, and reacted conversion gas goes out on being also, gas flow is U-shaped, and resistance is large; Bottom adopts large flange clamping integral tubesheet, and material consumption is very big; The expansion joint of gas-collecting pipe is arranged at device interior and requires expansion joint high, and this expansion joint needs the external pressure bearing more than 4MPa, can only adopt import expansion joint; Equipment barrel is arranged 2 pairs of large flange, there is the defect such as sealing and expense height; When unloading catalyst, need whole internals to hang out, take time and effort.
Summary of the invention
Object of the present invention solves above-mentioned prior art produced problem exactly, provides a kind of Radial Flow byproduct steam formula isothermal change furnace.
For this reason, the invention discloses a kind of Radial Flow byproduct steam formula isothermal change furnace, it comprises pressurized body of heater, beds, gas distributing cylinder, gas collector, it is characterized in that described pressurized upper of furnace body is provided with unstripped gas entrance and water out, in unstripped gas entrance body of heater, be provided with gas distributor; Pressurized lower portion of furnace body is provided with conversion gas outlet and water inlet; Gas distributing cylinder is provided with between described pressurized inboard wall of furnace body and beds; Pressurized body of heater axle centre is provided with gas collector; Longitudinal heat-obtaining device is set in described beds, described longitudinal heat-obtaining device is that the upper and lower parts of beds respectively arrange an annular bobbin carriage, connect with many longitudinal tubulations between two annular bobbin carriages, tubulation is through beds, upper, annular bobbin carriage connects water out, and lower annular bobbin carriage connects water inlet.
In certain embodiments, outside described water outlet, expansion joint is set, will the axial displacement comprising the internals such as longitudinal tubulation, annular bobbin carriage and produce because of thermal expansion be absorbed.
In certain embodiments, described pressurized lower portion of furnace body is provided with catalyst discharge port, so that the replacing of catalyst.
In certain embodiments, described pressurized upper of furnace body is provided with inspection manhole, so that the regular maintenance of equipment.
In certain embodiments, described water out and water inlet are 4, to reduce flow resistance, to improve heat-obtaining efficiency.
In certain embodiments, described gas distributing cylinder is evenly provided with pore, and the aperture of pore is less than or equal to 6mm.
In certain embodiments, described gas distributing cylinder top apart from not perforate in the 500mm of gas distributing cylinder top, preferred described gas distributing cylinder apart from not perforate in 100mm bottom it, gas backflow and short circuit in case catalyst sedimentation induces reaction.
In certain embodiments, described gas collector is divided into upper, middle and lower three sections, the each section of multiple pore of distribution, and each section of stomatal number difference, described gas collector is apart from not perforate in the 500mm of its top, described gas collector is apart from not perforate in its end 800mm, in case catalyst sedimentation induces reaction, gas refluxes and short circuit.
Described gas collector, described gas distributing cylinder and described annular bobbin carriage are provided with multiple locating piece, and accordingly, the inwall of described pressurized body of heater is provided with multiple location-plate, and body of heater and built-in system are located mutually by locating piece, so that installation and removal.
The invention has the advantages that: catalyst reaction bed temperature is controlled; Reaction bed there will not be overheating problem; Reaction bed uniformity of temperature profile; One way reaction conversion ratio is high, and after heat-insulating change furnace one-stage transfor-mation, carbon monoxide content is up to more than 10%, and after one-stage transfor-mation of the present invention, carbon monoxide content is less than or equal to 3%; Less demanding to the temperature applicable range of catalyst; The distance that conversion gas passes radially through beds is short, and pressure drop is little; By-product middle pressure steam; Compression shell metal temperature is lower, and equipment manufacturing cost is lower.
Accompanying drawing explanation
The structural representation of Fig. 1 one embodiment of the present invention.
Detailed description of the invention
Below in conjunction with specific embodiment, set forth the present invention further.These embodiments are only not used in for illustration of the present invention and limit the scope of the invention.The experimental technique of unreceipted actual conditions in the following example, the usually conveniently conditioned disjunction condition of advising according to manufacturer.Unless otherwise indicated, otherwise all percentage and number all by weight.
Unless otherwise defined, all specialties used in literary composition and scientific words and one skilled in the art the meaning be familiar with identical.In addition, any method similar or impartial to described content and material all can be applicable in the inventive method.The use that better implementation method described in literary composition and material only present a demonstration.
As shown in Figure 1, a kind of Radial Flow byproduct steam formula isothermal change furnace, it comprises pressurized body of heater 13, beds 7, gas distributing cylinder 6, gas collector, and described pressurized upper of furnace body is provided with water-gas entrance 1 and water out 3, is provided with gas distributor 4 in water-gas entrance 1 body of heater; Pressurized lower portion of furnace body is provided with conversion gas outlet 12 and water inlet 11; Gas distributing cylinder 6 is provided with between described pressurized body of heater 13 inwall and beds 7; Pressurized body of heater axle centre is provided with gas collector 9; In described beds 7, longitudinal heat-obtaining device is set, described longitudinal heat-obtaining device is that the upper and lower parts of beds 7 respectively arrange an annular bobbin carriage 5,10, connect with many longitudinal tubulations 8 between two annular bobbin carriages, tubulation 8 is through beds 7, upper, annular bobbin carriage 5 connects water out 3, and lower annular bobbin carriage 10 connects water inlet 11.
Outside described delivery port 3 place, expansion joint 2 is set, will the axial displacement comprising the internals such as longitudinal tubulation 8, annular bobbin carriage 5,10 and produce because of thermal expansion be absorbed.
Described pressurized lower portion of furnace body is provided with catalyst discharge port 14, and described pressurized upper of furnace body is provided with inspection manhole.Described water out and water inlet are 4; Described gas distributing cylinder is evenly provided with pore, and the aperture of pore is less than or equal to 6mm; Described gas distributing cylinder top is apart from not perforate in the 500mm of gas distributing cylinder top, and not perforate in 100mm at the bottom of the distance gas distributing cylinder of described gas distributing cylinder bottom, in case catalyst sedimentation induces reaction, gas refluxes and short circuit.
Described gas collector is divided into upper, middle and lower three sections, the each section of multiple pore of distribution, and each section of stomatal number difference, described part is apart from not perforate in the 500mm of gas collector top, not perforate in 800mm at the bottom of described part distance gas collector, gas backflow and short circuit in case catalyst sedimentation induces reaction.
Water-gas from change furnace upper water gas entry 1 after gas distributor 4 and gas distributing cylinder 6 distribute radial through beds 7, after reaction, conversion gas is after center gas surge drum 9 is collected, and flows out from change furnace bottom conversion gas outlet 12.Longitudinal tubulation 8 is provided with in beds, boiler water enters from bottom water inlet 11, by entering longitudinal row pipe 8 after lower annular bobbin carriage 10, flow out from upper, annular bobbin carriage 5 through water out 3 after this absorption reaction heat, water out 3 place is provided with expansion joint 2, absorbs the axial displacement that whole internals produce because of thermal expansion.
Through practical application, one way reaction conversion ratio of the present invention is high, and after one-stage transfor-mation, carbon monoxide content is less than or equal to 3%; And after heat-insulating change furnace one-stage transfor-mation carbon monoxide content up to more than 10%.
Unstripped gas upper entering and lower leaving of the present invention, resistance is little; Adopt be arranged at the annular tubesheet of device interior and the consumption of ring pipe box material few; Expansion joint of the present invention is arranged at device external, low to the requirement of expansion joint, adopts domestic expansion joint; The present invention is without equipment large flange, and without sealing problem, equipment manufacturing cost is low; Catalyst of the present invention unloads outlet and is arranged on bottom bulkhead, unloads catalyst very convenient.
Scope of the present invention is not by the restriction of described specific embodiments, and described embodiment, only as the single example of illustrating various aspects of the present invention, also comprises method and the component of functional equivalent in the scope of the invention.In fact, except content as herein described, those skilled in the art can easily grasp multiple improvement of the present invention with reference to description above and accompanying drawing.Described improvement also falls within the scope of appended claims.Every section of bibliography mentioned above is listed in herein as a reference all in full.
Claims (10)
1. a Radial Flow byproduct steam formula isothermal change furnace, it comprises pressurized body of heater (13), beds (7), gas distributing cylinder (6), gas collector (9), it is characterized in that described pressurized body of heater (13) top is provided with water-gas entrance (1) and water out (3), in water-gas entrance (1) body of heater, be provided with gas distributor (4); Pressurized body of heater (13) bottom is provided with conversion gas outlet (12) and water inlet (11); Gas distributing cylinder (6) is provided with between described pressurized body of heater (13) inwall and beds (7); Pressurized body of heater axle centre is provided with gas collector (9); In described beds (7), longitudinal heat-obtaining device is set, described longitudinal heat-obtaining device is that the upper and lower parts of beds (7) respectively arrange an annular bobbin carriage (5,10), connect with many longitudinal tubulations (8) between two annular bobbin carriages, tubulation (8) is through beds (7), upper, annular bobbin carriage (5) connects water out (3), and lower annular bobbin carriage (10) connects water inlet (11).
2. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, becomes and it is characterized in that arranging expansion joint (2) outside described delivery port (3) place.
3. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described pressurized lower portion of furnace body is provided with catalyst discharge port (14).
4. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described pressurized upper of furnace body is provided with inspection manhole.
5. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described water out and water inlet are 4.
6. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, it is characterized in that described gas distributing cylinder is evenly provided with pore, the aperture of pore is less than or equal to 6mm.
7. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described gas distributing cylinder is apart from not perforate in the 500mm of its top.
8. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described gas distributing cylinder is apart from not perforate in 100mm bottom it.
9. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described gas collector is divided into upper, middle and lower three sections, each section of distributed pores, and each section of stomatal number difference.
10. Radial Flow byproduct steam formula isothermal change furnace according to claim 1, is characterized in that described gas collector is apart from not perforate in the 500mm of its top, and described gas collector is apart from not perforate in 800mm bottom it.
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| CN201410572326.1A CN105561889A (en) | 2014-10-23 | 2014-10-23 | Radial flow by-product steam isothermal shift converter |
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| CN201410572326.1A CN105561889A (en) | 2014-10-23 | 2014-10-23 | Radial flow by-product steam isothermal shift converter |
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Citations (7)
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| JP2003081610A (en) * | 2001-09-10 | 2003-03-19 | Nippon Soken Inc | Reforming apparatus |
| CN1429764A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | CO isothermal sulfur resistant conversion process |
| US20060062706A1 (en) * | 1999-09-29 | 2006-03-23 | Johnson Matthey Plc | Catalytic reactor |
| CN102580626A (en) * | 2012-03-20 | 2012-07-18 | 南京国昌化工科技有限公司 | Double-shaft radial flow reactor |
| CN102886231A (en) * | 2012-10-08 | 2013-01-23 | 中国石油化工集团公司 | Fully-radial isothermal CO (carbon monoxide) conversion furnace |
| CN203227477U (en) * | 2013-04-09 | 2013-10-09 | 上海国际化建工程咨询公司 | Constant-temperature fixed-bed reactor for filling catalysts among heat exchange tubes |
| CN204182370U (en) * | 2014-10-23 | 2015-03-04 | 新煤化工设计院（上海）有限公司 | A kind of Radial Flow byproduct steam formula isothermal change furnace |
-
2014
- 2014-10-23 CN CN201410572326.1A patent/CN105561889A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060062706A1 (en) * | 1999-09-29 | 2006-03-23 | Johnson Matthey Plc | Catalytic reactor |
| JP2003081610A (en) * | 2001-09-10 | 2003-03-19 | Nippon Soken Inc | Reforming apparatus |
| CN1429764A (en) * | 2001-12-30 | 2003-07-16 | 中国石化集团齐鲁石油化工公司 | CO isothermal sulfur resistant conversion process |
| CN102580626A (en) * | 2012-03-20 | 2012-07-18 | 南京国昌化工科技有限公司 | Double-shaft radial flow reactor |
| CN102886231A (en) * | 2012-10-08 | 2013-01-23 | 中国石油化工集团公司 | Fully-radial isothermal CO (carbon monoxide) conversion furnace |
| CN203227477U (en) * | 2013-04-09 | 2013-10-09 | 上海国际化建工程咨询公司 | Constant-temperature fixed-bed reactor for filling catalysts among heat exchange tubes |
| CN204182370U (en) * | 2014-10-23 | 2015-03-04 | 新煤化工设计院（上海）有限公司 | A kind of Radial Flow byproduct steam formula isothermal change furnace |
Non-Patent Citations (1)
| Title |
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| 尹先清 等主编: "《化学化工专业实习》", 28 February 2009 * |
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Application publication date: 20160511 |