CN203971914U - Isothermal reactor - Google Patents
Isothermal reactor Download PDFInfo
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- CN203971914U CN203971914U CN201420403510.9U CN201420403510U CN203971914U CN 203971914 U CN203971914 U CN 203971914U CN 201420403510 U CN201420403510 U CN 201420403510U CN 203971914 U CN203971914 U CN 203971914U
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Abstract
The utility model relates to a kind of isothermal reactor, has solved that the control of existing isothermal reactor system temperature is unstable, the problem of the easy inactivation of catalyst.Technical scheme comprises housing, epimere in described housing and hypomere are respectively equipped with chamber water-locator and lower chamber water-locator, the many heat exchanger tubes through being evenly arranged between described upper chamber water-locator and lower chamber cloth device are connected, described upper chamber water-locator is communicated with the steam outlet of case top, lower chamber water-locator is connected with the boiler feed pipe of housing bottom, described case top is provided with raw material gas inlet, bottom is provided with reaction gas outlet, the stage casing of described housing is filled with beds, and reative cell central tube is positioned at housing stage casing position of center line and is communicated with reaction gas outlet.The utility model is simple in structure, control is reliable, equipment investment is low, operating cost is low, catalyst long service life, energy-saving and cost-reducing, can by-product high-grade steam.
Description
Technical field
The utility model relates to a kind of methanator, specifically a kind of isothermal reactor.
Background technology
Adopt methanation reaction produce gas product as SNG, LNG, CNG etc. be an important approach in gas chemical industry.Taking SNG as example, the unstripped gas of SNG need of production is carbon monoxide and hydrogen, and methanation reaction is the effect of unstripped gas by means of catalyst, at a certain temperature, makes carbon monoxide and hydrogen reaction in methanator, generates the technical process of methane.Methanation reaction belongs to strong exothermal reaction, and be the process of a thermodynamics control, industrial methanation device adopts insulation fix bed reactor more, many insulation fix bed reactors of this reaction process one general configuration and Duo Tai heat transmission equipment, process route is long, and SR is large, construction investment is large, the high and low grade heat energy of operation energy consumption is many but can not effectively utilize, and system energy consumption is high, the problems such as the easy temperature runaway of reactor, the easy high temperature deactivation of catalyst.
Summary of the invention
The utility model object is in order to solve the problems of the technologies described above, provide a kind of simple in structure, be easy to control, the long service life of low, the catalyst of operating cost, energy-saving and cost-reducing, the isothermal reactor that obtains high-grade steam.
Technical scheme comprises housing, epimere in described housing and hypomere are respectively equipped with chamber water-locator and lower chamber water-locator, the many heat exchanger tubes through being evenly arranged between described upper chamber water-locator and lower chamber cloth device are connected, described upper chamber water-locator is communicated with the steam outlet of case top, lower chamber water-locator is connected with the boiler feed pipe of housing bottom, described case top is provided with raw material gas inlet, bottom is provided with reaction gas outlet, the stage casing of described housing is filled with beds, and reative cell central tube is positioned at housing stage casing position of center line and is communicated with reaction gas outlet.
Described reative cell central tube hypomere evenly has multiple apertures, and small aperture is 0.1mm～20mm.
The ratio of height to diameter of described isothermal reactor is 2.0:1～3.5:1.
Described upper chamber water-locator is positioned at chamber gripper shoe, and described upper chamber gripper shoe has annular space apart from shell wall side, and described unstripped gas is through the downward inflow catalyst bed of annular space.
Described lower chamber water-locator is positioned at lower chamber gripper shoe.
Steam outlet on described housing has been evenly arranged four, and described boiler feed pipe has also been evenly arranged four.
Inventor has changed methanation process in the past and has adopted multistage insulation reactor and many flow processs that heat exchanger is connected, use the isothermal reactor of a constant temperature instead, simultaneously for improving the conversion ratio of unstripped gas, the Cryo Heat Insulation reactor of only having connected, and the structure of isothermal reactor is also improved, main manifestations is in the following areas.
Inventor improves isothermal reactor, by pass into boiler feedwater in heat exchanger tube, can, to the beds high efficient heat exchanging in isothermal reactor, remove methanation reaction heat, ensure temperature constant in isothermal reactor, avoid catalyst high temperature deactivation, by-product high-grade steam, changes traditional adiabatic multistage methanation reaction flow process simultaneously, optimization technological process, reduce methanator and heat exchanger quantity, economy system investment, convenient operation management; By lower chamber water-locator is set, boiler feedwater can be entered in every heat exchanger tube uniformly, ensure that reaction bed temperature is even, the catalysqt deactivation of avoiding bed temperature inequality to cause, the service life of improving catalyst.
Further, reative cell central tube is arranged on the center line in housing stage casing, ensures that unstripped gas fully reacts with catalyst through beds with long as far as possible stroke, and then enter reative cell central tube; On the hypomere tube wall of reative cell central tube, evenly have multiple apertures, when so just can making unstripped gas concentrated to beds center, also having increased descending route could be drawn by reative cell central tube, improves the uniformity of catalytic reaction and the stability of system.Small aperture is 0.1mm～20mm, and conference causes unstripped gas fully not carry out catalytic reaction and just leaves system by macropore excessively, thereby reduces unstripped gas conversion ratio, also causes the waste of raw material; The too small SR that can strengthen falls, and makes the gas occurring after methanation reaction can not shift out in time system.The ratio of height to diameter of described isothermal reactor is 2.0:1～3.5:1, has maximum methanation reaction efficiency in this proportion.
Described upper chamber water-locator and lower chamber water-locator can be arranged in corresponding Ji Xia chamber, upper chamber gripper shoe, described upper chamber gripper shoe has certain annular space apart from shell wall side, play as unstripped gas guide effect, make unstripped gas descending along shell wall side through annular space, advance to middle part from the perimembranous of beds.
The utility model is simple and reliable for structure, easy operating, facility compact, equipment investment and operating cost are low, methanation efficiency is high, the long service life of catalyst, by-product high-grade steam simultaneously, there is wide market application foreground, be applicable to the flow process of carrying out abundant methanation as unstripped gas taking the carbon monoxide in purified gas and hydrogen in chemical plant.
Brief description of the drawings
Fig. 1 is methanation reaction process flow chart;
Fig. 2 is the structural representation of the utility model isothermal reactor;
Fig. 3 is the elevation of hot replace tubes and water-locator in isothermal reactor.
Wherein: A-knockout drum, B-desulfurizer, C-feeding gas heater, D-isothermal reactor, E-adiabatic reactor, F-drum.
Chamber lower supporting plate, 13-heat exchanger tube, 14-aperture, 15-beds, 16-housing under chamber water-locator, 9-reative cell central tube, 10-annular space, the upper chamber of 11-gripper shoe, 12-under 1-raw material gas inlet, 2-reaction gas outlet, 3-boiler feedwater inlet tube, 4-steam outlet, 5-catalyst inlet, 6-catalyst outlet, the upper chamber of 7-water-locator, 8-.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is further explained to explanation:
The structure of isothermal reactor D is for comprising housing 16, epimere in described housing 16 and hypomere are respectively equipped with the upper chamber water-locator 7 of installing in chamber gripper shoe 11 and are arranged on the interior lower chamber of lower chamber gripper shoe 12 water-locator 8, described upper chamber gripper shoe 11 has annular space 10 apart from housing 16 walls, many heat exchanger tubes 13 through being evenly arranged between described upper chamber water-locator 7 and lower chamber cloth device 8 are communicated with, described upper chamber water-locator 7 is communicated with four, the housing 16 top steam outlet 4 being evenly arranged, lower chamber water-locator 8 is communicated with four of 16 bottoms of the housing boiler feed pipe being evenly arranged 3, described housing 16 tops are also provided with raw material gas inlet 1, bottom is provided with reaction gas outlet 2, the stage casing of described housing 16 is filled with beds 15, being positioned at housing 16 stage casing position of center line and being communicated with reaction gas outlet 2 of reative cell central tube 9, described reative cell central tube 9 hypomeres evenly have multiple apertures 14, small aperture is 0.1mm～20mm, the ratio of height to diameter of described isothermal reactor is 2.0:1～3.5:1.On described housing, be also provided with the catalyst inlet 5 and the catalyst outlet 5 that are communicated with beds 15.
Technical process:
Referring to Fig. 1, unstripped gas is (using carbon monoxide and hydrogen as unstripped gas, temperature 180-280 DEG C, pressure 3.0-6.5MPaG) after knockout drum A gas-liquid separation, send into desulfurizer B desulfurization, unstripped gas (it is following that sulfur content is down to 20ppb) after desulfurization is then sent in feeding gas heater C and is warming up to 550-580 DEG C with the reaction gas heat exchange that goes out isothermal reactor D, unstripped gas after intensification is sent into isothermal reactor D and is reacted, the transformation efficiency of methane in unstripped gas is reached more than 90%, reacted reaction gas is sent into and after described feeding gas heater C is cooled to 330-380 DEG C with unstripped gas heat exchange, is sent into Cryo Heat Insulation reactor E again and further fully react and obtain methane gas (methane conversion efficiency reaches more than 99.5%).The boiler feedwater inlet tube 3 of isothermal reactor D bottom is sent in boiler feedwater by the boiler feedwater pipeline through drum F, the water vapour (saturated vapor of 550-580 DEG C) of described isothermal reactor D Base top contact is sent and sent outside through the jet chimney of drum F again after steam outlet 4 is drawn.
Referring to Fig. 2, in described isothermal reactor D, described unstripped gas enters housing 16 epimeres by raw material gas inlet 1 and leads through upper chamber gripper shoe 11, annular space 10 through between upper chamber gripper shoe 11 and housing 15 is descending along the wall of housing 16, when the beds 15 and catalyst react, reacted gas enters in reaction gas outlet 2 through the aperture 14 of reative cell central tube 9 hypomeres, is finally discharged by reaction gas outlet 2; Described boiler feedwater enters lower chamber water-locator 8 by boiler feedwater inlet tube 3, enters beds 15 indirect heat exchanges outside heat exchanger tube 13 and pipe by lower chamber water-locator 8, and the water vapour after heat exchange is drawn by steam outlet 4 through upper chamber water-locator 7.Owing to continuing passing into of boiler feedwater in isothermal reactor D, can constantly remove the heat that catalytic reaction produces, make the temperature constant in isothermal reactor D, unstripped gas can fully be reacted in reactor, there will not be the problems such as the easy temperature runaway of reactor, the easy high temperature deactivation of catalyst.Same because the temperature control of isothermal reactor is constant, therefore, for adiabatic reactor, the material cost of isothermal reactor D equipment and manufacture difficulty are also corresponding falls mutually, and equipment investment is lower.
Described adiabatic reactor E is the existing conventional reactor of methanation process, and concrete structure is not described further at this.Described water-locator can be coil pipe.The catalyst of filling in described beds can be high temperature resistant methanation catalyst conventional in market.
To produce 2200000000 Nm per year
3the methanation process of natural gas is example, if adopt our bright technique, temperature of reactor control steadily, catalyst can efficiently utilize non-inactivation, reaction hop count only to need two sections of isothermal reactor and adiabatic reactors, can effectively improve unstripped gas transformation efficiency (reaching more than 99.5%), byproduct steam is sent outside simultaneously, and energy-saving and cost-reducing synergistic effect is obvious.Because flow process is simple, number of devices is few, do not need frequent maintenance and repair apparatus few, can greatly reduce the maintenance cost of equipment, directly reduce approximately 2,500 ten thousand yuan of equipment investments, save approximately 1,600 ten thousand yuan of operating costs, send steam outside and produce approximately 4,000,000 yuan of added benefit, total can produce the economic benefit of 4,500 ten thousand yuan.
Claims (6)
1. an isothermal reactor, comprise housing, epimere in described housing and hypomere are respectively equipped with chamber water-locator and lower chamber water-locator, the many heat exchanger tubes through being evenly arranged between described upper chamber water-locator and lower chamber cloth device are connected, described upper chamber water-locator is communicated with the steam outlet of case top, lower chamber water-locator is connected with the boiler feed pipe of housing bottom, described case top is provided with raw material gas inlet, bottom is provided with reaction gas outlet, the stage casing of described housing is filled with beds, reative cell central tube is positioned at housing stage casing position of center line and is communicated with reaction gas outlet.
2. isothermal reactor as claimed in claim 1, is characterized in that, described reative cell central tube hypomere evenly has multiple apertures, and small aperture is 0.1mm～20mm.
3. isothermal reactor as claimed in claim 1, is characterized in that, the ratio of height to diameter of described isothermal reactor is 2.0:1～3.5:1.
4. the isothermal reactor as described in claim 1-3 any one, is characterized in that, described upper chamber water-locator is positioned at chamber gripper shoe, and described upper chamber gripper shoe has annular space apart from shell wall side, and described unstripped gas is through the downward inflow catalyst bed of annular space.
5. isothermal reactor as claimed in claim 4, is characterized in that, described lower chamber water-locator is positioned at lower chamber gripper shoe.
6. the isothermal reactor as described in claim 1-3 any one, is characterized in that, the steam outlet on described housing has been evenly arranged four, and described boiler feed pipe has also been evenly arranged four.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420403510.9U CN203971914U (en) | 2014-07-21 | 2014-07-21 | Isothermal reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420403510.9U CN203971914U (en) | 2014-07-21 | 2014-07-21 | Isothermal reactor |
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| CN203971914U true CN203971914U (en) | 2014-12-03 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105749818A (en) * | 2016-04-27 | 2016-07-13 | 中国华能集团清洁能源技术研究院有限公司 | Low temperature methanation reactor and working process |
| CN108212025A (en) * | 2016-12-14 | 2018-06-29 | 中国石化工程建设有限公司 | A kind of compound tower-type methanator |
| CN111115576A (en) * | 2020-01-17 | 2020-05-08 | 中国华能集团清洁能源技术研究院有限公司 | External heat transfer isothermal converter of antitoxic furnace |
-
2014
- 2014-07-21 CN CN201420403510.9U patent/CN203971914U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105749818A (en) * | 2016-04-27 | 2016-07-13 | 中国华能集团清洁能源技术研究院有限公司 | Low temperature methanation reactor and working process |
| CN105749818B (en) * | 2016-04-27 | 2018-08-28 | 中国华能集团清洁能源技术研究院有限公司 | A kind of low temperature methanator and the course of work |
| CN108212025A (en) * | 2016-12-14 | 2018-06-29 | 中国石化工程建设有限公司 | A kind of compound tower-type methanator |
| CN111115576A (en) * | 2020-01-17 | 2020-05-08 | 中国华能集团清洁能源技术研究院有限公司 | External heat transfer isothermal converter of antitoxic furnace |
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