CN204247177U - A kind of thermal insulation-isothermal methanation reactor - Google Patents
A kind of thermal insulation-isothermal methanation reactor Download PDFInfo
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- CN204247177U CN204247177U CN201420707199.7U CN201420707199U CN204247177U CN 204247177 U CN204247177 U CN 204247177U CN 201420707199 U CN201420707199 U CN 201420707199U CN 204247177 U CN204247177 U CN 204247177U
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Abstract
The utility model discloses a kind of thermal insulation-isothermal methanation reactor, object is to solve existing methanator, there is unstripped gas moves hot limited in one's ability, gaseous heat transfer coefficient is low, cannot reach and move heat request, and distribution of gas is uneven between inside and outside layer housing, may and cause the problem of localized hyperthermia.This reactor comprises housing, upper cover, low head etc.Meanwhile, the utility model arranges heat insulation layer catalyst layer on tubulation, can improve reacting gas temperature fast.The utility model adopts the design of transfer of heat and the design of gas distributor, efficiently solves the problem of moving heat and distribution of gas.Adopt the utility model when carrying out methanation reaction, distribution of gas be even, conversion ratio is high, selective good, can and time shift heat, effectively avoid reaction temperature too high, extend the methane synthesizing catalyst life-span.Meanwhile, the utility model equipment cost is low, and effectively improves the utilization rate of the energy.
Description
Technical field
The utility model relates to chemical field, especially natural gas field, is specially a kind of thermal insulation-isothermal methanation reactor, and it can be used in oven gas or coal preparing natural gas.
Background technology
In recent years, along with China's natural gas consumption figure constantly increases, and China's natural gas reserve is limited, and production capacity can not satisfy the demands, and causes natural gas insufficiency of supply-demand to expand year by year.Coal preparing natural gas is as the effective means of supplementing out economy to China's natural gas resource, and it can solve the problem of natural gas supply deficiency to a certain extent.The flow process of coal preparing natural gas is: the raw gas that coal gasification apparatus is produced is successively after carbon monodixe conversion, acid gas removal, and be purified gas, purified gas, again after methanation reaction and drying, is met relevant national standard natural gas.Methanation technology is the technique core of coal preparing natural gas, is then nucleus equipment wherein accordingly for the methanator of methanation technology.
In the method, the main component of purified gas is carbon monoxide and hydrogen, and it is after desulfurization process, enters thermal insulation-isothermal methanation reactor, and under catalyst action, reaction generates methane and water, and methanation reaction is strong exothermal reaction.This makes reactor shell to bear elevated pressures, bears the sharply temperature rise that methanation reaction brings again.Therefore, the traditional requirement of cold wall adiabatic reactor to material is higher, and quench gas will be used to lower the temperature, and this makes catalyst efficiency lower, also makes reactor be divided into multistage, and bulky.Catalyst is under the high temperature action of reaction generation simultaneously, also easy inactivation.
Heat problem is moved in order to solve, Chinese patent CN103752227A proposes a kind of methanator, this reactor has double Shell, internal layer shell is equipped with methanation catalyst, unstripped gas enters from passage between outer casing and internal layer shell, removable methanation reaction releases heat, and unstripped gas is heated simultaneously, enters internal layer shell and carry out methanation reaction after heat exchange.Adopt this structure, the outer casing of this reactor only bears high pressure, and internal layer shell only bears high temperature.But methanator is strong exothermal reaction, still there is unstripped gas and move hot limited in one's ability in this reactor, gaseous heat transfer coefficient is low, cannot reach and move heat request, meanwhile, between inside and outside layer housing, distribution of gas is uneven, may and cause localized hyperthermia, be still further improved.
Utility model content
Applicant is found by research, and existing thermal insulation-isothermal methanation reactor interior reaction temperature is high, mainly contains two reasons: one is that Reactor inlet distribution of gas is uneven, and two is that heat is not removed in time.Although aforementioned methanator improves, appoint and have certain limitation.
Goal of the invention of the present utility model is: for existing methanator, there is unstripped gas moves hot limited in one's ability, gaseous heat transfer coefficient is low, cannot reach and move heat request, and distribution of gas is uneven between inside and outside layer housing, may and cause the problem of localized hyperthermia, a kind of thermal insulation-isothermal methanation reactor is provided.The utility model has carried out brand-new structural design to reactor, adopts the design of transfer of heat and the design of gas distributor, efficiently solves the problem of moving heat and distribution of gas.Adopt the utility model when carrying out methanation reaction, distribution of gas be even, conversion ratio is high, selective good, can and time shift heat, effectively avoid reaction temperature too high, extend the methane synthesizing catalyst life-span.Meanwhile, the utility model can reduce the material requirement to reactor, reduces equipment cost, and effectively improves the utilization rate of the energy.
To achieve these goals, the utility model adopts following technical scheme:
A kind of thermal insulation-isothermal methanation reactor, comprise housing, the upper cover of housing upper end is set, the low head of housing lower end is set, described upper cover, housing, low head is connected successively, described upper cover is provided with the charging mouth of pipe, described low head is provided with the discharging mouth of pipe, the tubulation for loading catalyst is provided with in described housing, the two ends up and down of described tubulation are respectively arranged with upper perforated plate, lower perforated plate, the two ends of described tubulation respectively with upper cover, low head is communicated with, described tubulation and housing, upper perforated plate, the heat transfer space being used for being connected with cooling medium is formed between lower perforated plate,
Also be provided with gas distributor between described upper cover and upper perforated plate, between described low head and lower perforated plate, be provided with heat insulating filling material.
Also be provided with adiabatic catalytic oxidant layer, fixing silk screen for fixing adiabatic catalytic oxidant layer in described upper cover, described adiabatic catalytic oxidant layer is between fixing silk screen and upper perforated plate.
The height of described adiabatic catalytic oxidant layer is 1 ~ 400mm.
Described heat insulating filling material is heat-insulating porcelain ball.
Described gas distributor is the back taper cylinder of hollow, and the sidewall of described back taper cylinder is provided with distribution hole.
The diameter of described distribution hole is 20 ~ 25mm.
Described distribution hole be axially perpendicular to distribution hole place plane.
The height of described back taper cylinder is 0.3 ~ 0.5 times of upper cover height, the diameter of described back taper cylinder upper surface is vertically 2 ~ 2.5 times of charging nozzle diameter, and the diameter of described back taper cylinder lower surface is vertically 1 ~ 1.5 times of charging nozzle diameter.
Also comprise the catch arranged in back taper cylinder.
Described catch is rounded, and the diameter of described catch is 1 ~ 1.2 times of charging nozzle diameter, and described catch is 0.5 ~ 0.6 times of back taper height of column to the distance of upper surface.
Described catch is connected with gas distributor by support bar.
Described upper cover, low head are respectively hemispherical.
Tubulation external diameter is 38 ~ 50mm, and internal diameter is 32 ~ 44mm.
The cooling medium of described heat transfer space is saturation water.
Described tubulation is that equilateral triangle is arranged, the tube pitch of tubulation is 50 ~ 65mm.
For the problem existing for existing patent, the utility model provides a kind of thermal insulation-isothermal methanation reactor.Applicant, to after existing thermal insulation-isothermal methanation reactor analytic, think that the too high reason of existing temperature of reactor is inlet gas skewness, and heat is not removed in time.For the reactor of Chinese patent CN103752227, it adopts double Shell, and by unstripped gas heat exchange, solve foregoing problems, outer casing only bears high pressure, and internal layer shell only bears high temperature.And the heat transfer coefficient of unstripped gas is low, cannot reaches and move heat request, and still there is the problem of distribution of gas inequality, there is larger limitation.For this reason, applicant has carried out brand-new design to the structure of reactor.This thermal insulation-isothermal methanation reactor comprises housing, upper cover, low head, and upper cover, low head are separately positioned on the two ends up and down of housing, and upper cover, housing, low head are connected successively, form shell of the present utility model.Wherein, upper cover is provided with the charging mouth of pipe, low head is provided with the discharging mouth of pipe, purified gas enters in reactor by the charging mouth of pipe, carries out the gas after methanation reaction and is discharged by the discharging mouth of pipe.The tubulation for loading catalyst is provided with in housing, the two ends up and down of tubulation are respectively arranged with upper perforated plate, lower perforated plate, the two ends of tubulation are communicated with upper cover, low head respectively, tubulation and the heat transfer space formed between housing, upper perforated plate, lower perforated plate for being connected with cooling medium.In the utility model, by cooperatively interacting between tubulation and housing, upper perforated plate, lower perforated plate, form the heat transfer space being used for being connected with cooling medium, heat exchange can be carried out to tubulation by the cooling medium in heat transfer space, thus under enabling tubulation be in reaction temperature, effectively avoid the sharply temperature rise because methanation reaction causes.Because the utility model adopts this structure, thus greatly can reduce reaction temperature, in the service life of effective extending catalyst, be conducive to the carrying out of positive reaction simultaneously, effectively improve the conversion ratio of ending.Due in the gas product of gained, methane content is high, thus without the need to circulation, reduce further compression power consumption, simultaneously can also by-product middle pressure steam, the effectively utilization rate of the raising energy.
Meanwhile, the utility model is also provided with gas distributor between upper cover and upper perforated plate, is provided with heat insulating filling material between low head and lower perforated plate, and wherein, heat insulating filling material can be heat-insulating porcelain ball.This gas distributor is the back taper cylinder of hollow, and the sidewall of back taper cylinder is provided with distribution hole.Adopt this structure, gas uniform can be made to distribute, after effectively avoiding gas to enter upper cover by the charging mouth of pipe, at localized clusters, cause reaction temperature too high.By aforementioned improved, effectively avoid distribution of gas uneven, in reactor, gas temperature is too high, easily causes the problem of catalysqt deactivation.Relative to pre-existing reactors, the utility model can service life of very big extending catalyst, and improve reaction efficiency, in the gas product of gained, methane content significantly improves.As previously mentioned, because in gas product, methane content is higher, it effectively can reduce energy resource consumption.Further, distribution hole be axially perpendicular to distribution hole place plane, it makes gas to shell wall face directional spreding, gas can be avoided to concentrate to middle part, avoid the localized hyperthermia caused due to skewness further.
As preferably, the height of back taper cylinder is 0.3 ~ 0.5 times of upper cover height, the diameter of back taper cylinder upper surface is vertically 2 ~ 2.5 times of charging nozzle diameter, and the diameter of back taper cylinder lower surface is vertically 1 ~ 1.5 times of charging nozzle diameter.Also comprise the catch arranging in back taper cylinder, be connected with gas distributor by support bar, catch is rounded, and the diameter of catch is 1 ~ 1.2 times of charging nozzle diameter, and catch is 0.5 ~ 0.6 times of back taper height of column to the distance of upper surface.Adopt this structure can the uniformity of lift gas distribution, meanwhile, circular baffle plate can prevent gas from directly leading to middle part, thus is more evenly distributed.
Also be provided with adiabatic catalytic oxidant layer, fixing silk screen for fixing adiabatic catalytic oxidant layer in upper cover, adiabatic catalytic oxidant layer is between fixing silk screen and upper perforated plate, and the height of adiabatic catalytic oxidant layer is 1 ~ 400mm.The utility model arranges one section of heat insulation layer catalyst on tubulation, and it can improve reacting gas temperature fast.Meanwhile, adiabatic catalytic oxidant layer can reduce the temperature requirement of reactor inlet, enhancing reactor adaptability for working condition.Further, the cooling medium of heat transfer space is saturation water.Unstripped gas reacts and generates methane in tubulation, and releases heat, and pressure saturation water during heat transfer space is logical, saturation water is evaporated to middle pressure steam and absorbs a large amount of reaction heat, and heat transfer coefficient is high, moves thermally-stabilised.Adopt saturation water as cooling medium, while methanation reaction carries out, middle pressure steam can be produced as accessory substance, realize effective utilization of the energy.
In the utility model, in tubulation, loading catalyst is main reaction region, and the heat transfer space outside tubulation leads to saturation water to carry out moving heat, produces accessory substance middle pressure steam simultaneously, and maintains tubulation interior reaction temperature close to constant temperature.Tubulation of the present utility model and case temperature all close to saturation water temperature, and can reduce housing and tubulation bear pressure, require greatly to reduce to material, thus effectively reduce equipment cost, extend service life of the present utility model.The utility model adopts saturated water shifting heat, temperature stabilization, substantially temperature runaway phenomenon can not occur, and can maintain higher conversion.
Further, upper cover, low head are respectively hemispherical, and tubulation external diameter is 38 ~ 50mm, and internal diameter is 32 ~ 44mm, and tubulation is that equilateral triangle is arranged, the tube pitch of tubulation is 50 ~ 65mm.
When adopting the utility model to carry out methanation reaction, isothermal reaction greatly reduces reaction temperature, and housing only needs to bear saturation water pressure, and reduce further the requirement to material.The utility model adopts the design of tubulation external-cooling type, and move thermal velocity soon, reaction temperature is stablized, and effectively extends catalyst life.Methanation reaction is strong exothermal reaction, and reaction temperature of the present utility model is low, is conducive to the carrying out of positive reaction, end of a period conversion ratio is high simultaneously, and in products obtained therefrom gas, methane content is high, thus without the need to circulation, reduce compression power consumption, and energy by-product middle pressure steam, effectively achieve the efficiency utilization of the energy.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Fig. 2 is the close-up schematic view of upper cover and gas distributor.
Mark in figure: 1 is housing, and 2 is upper cover, and 3 is low head, 4 is the charging mouth of pipe, and 5 is the discharging mouth of pipe, and 6 is tubulation, 7 is upper perforated plate, and 8 is lower perforated plate, and 9 is gas distributor, 10 is heat insulating filling material, 11 is adiabatic catalytic oxidant layer, and 12 is fixing silk screen, and 13 is distribution hole, 14 is catch, and 15 is support bar.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is described in detail.
In order to make the purpose of this utility model, technical scheme and advantage clearly understand, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein only in order to explain the utility model, and be not used in restriction the utility model.
Embodiment 1
As shown in the figure, thermal insulation-isothermal methanation the reactor of the present embodiment comprises housing 1, upper cover 2, low head 3, upper cover 2, low head 3 are separately positioned on the two ends up and down of housing 1, and upper cover 2, housing 1, low head 3 are connected successively, form shell of the present utility model.In the present embodiment, upper cover 2, low head 3 adopt hemispherical respectively, wherein, upper cover 2 are provided with the charging mouth of pipe 4, low head 3 are provided with the discharging mouth of pipe 5.The tubulation 6 for loading catalyst is provided with in housing 1, the two ends up and down of tubulation 6 are respectively arranged with upper perforated plate 7, lower perforated plate 8, the two ends of tubulation 6 are communicated with upper cover 2, low head 3 respectively, tubulation 6 and the heat transfer space formed between housing 1, upper perforated plate 7, lower perforated plate 8 for being connected with cooling medium.In the present embodiment, the cooling medium of heat transfer space adopts saturation water, and tubulation 6 is arranged in equilateral triangle, and the tube pitch of tubulation 6 is 50 ~ 65mm.
Also be provided with gas distributor 9 between upper cover 2 and upper perforated plate 7, be provided with heat insulating filling material 10 between low head 3 and lower perforated plate 8, heat insulating filling material 10 is heat-insulating porcelain ball.Also be provided with the thick adiabatic catalytic oxidant layer 11 of 1 ~ 400mm, fixing silk screen 12 for fixing adiabatic catalytic oxidant layer 11 in upper cover 2, adiabatic catalytic oxidant layer 11 is between fixing silk screen 12 and upper perforated plate 7.
Gas distributor 9 is the back taper cylinder of hollow, the sidewall of back taper cylinder is provided with distribution hole 13, distribution hole 13 be axially perpendicular to distribution hole 13 place plane, the diameter of distribution hole 13 is 20 ~ 25mm.The height of back taper cylinder is 0.3 ~ 0.5 times of upper cover 2 height, the diameter of back taper cylinder upper surface is vertically 2 ~ 2.5 times of the charging mouth of pipe 4 diameter, and the diameter of back taper cylinder lower surface is vertically 1 ~ 1.5 times of the charging mouth of pipe 4 diameter.Rounded tabs 14, support bar 15 is also provided with in gas distributor 9, catch 14 is connected with gas distributor 9 by support bar 15, the diameter of catch 14 is 1 ~ 1.2 times of the charging mouth of pipe 4 diameter, and catch 14 is 0.5 ~ 0.6 times of back taper height of column to the distance of upper surface.
During utility model works, purified gas enters in reactor by the charging mouth of pipe 4, under the effect of gas distributor 9, reach and be uniformly distributed, effectively avoid hot-spot, the purified gas after gas distributor 9 can promote temperature rapidly by adiabatic catalytic oxidant layer 11, reaches ideal response temperature.Enter in tubulation 6 again and carry out methanation reaction, release amount of heat simultaneously, remove heat by the saturation water outside tubulation 6, ensure stable reaction temperature, the saturation water in heat transfer space is then vaporizated into middle pressure steam.Unstripped gas, after tubulation 6 reacts, is substantially converted into methane, is sent after collecting by the discharging mouth of pipe 5.In the present embodiment, adiabatic catalytic oxidant layer 11 can improve rapidly the temperature of reacting gas, promotes the adaptability to inlet gas, and the outer logical saturation water of tubulation 6 removes heat rapidly, stablizes reaction temperature, and byproduct steam.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all do within spirit of the present utility model and principle any amendment, equivalent to replace and improvement etc., all should be included within protection domain of the present utility model.
Claims (10)
1. thermal insulation-isothermal methanation reactor, it is characterized in that, comprise housing (1), the upper cover (2) of housing (1) upper end is set, the low head (3) of housing (1) lower end is set, described upper cover (2), housing (1), low head (3) is connected successively, described upper cover (2) is provided with the charging mouth of pipe (4), described low head (3) is provided with the discharging mouth of pipe (5), the tubulation (6) for loading catalyst is provided with in described housing (1), the two ends up and down of described tubulation (6) are respectively arranged with upper perforated plate (7), lower perforated plate (8), the two ends of described tubulation (6) respectively with upper cover (2), low head (3) is communicated with, described tubulation (6) and housing (1), upper perforated plate (7), the heat transfer space being used for being connected with cooling medium is formed between lower perforated plate (8),
Also be provided with gas distributor (9) between described upper cover (2) and upper perforated plate (7), between described low head (3) and lower perforated plate (8), be provided with heat insulating filling material (10).
2. thermal insulation according to claim 1-isothermal methanation reactor, it is characterized in that, also be provided with adiabatic catalytic oxidant layer (11), fixing silk screen (12) for fixing adiabatic catalytic oxidant layer (11) in described upper cover (2), described adiabatic catalytic oxidant layer (11) is positioned between fixing silk screen (12) and upper perforated plate (7).
3. thermal insulation according to claim 2-isothermal methanation reactor, is characterized in that, the height of described adiabatic catalytic oxidant layer (11) is 1 ~ 400mm.
4. thermal insulation according to claim 1-isothermal methanation reactor, is characterized in that, described heat insulating filling material (10) is heat-insulating porcelain ball.
5. thermal insulation according to any one of claim 1-4-isothermal methanation reactor, is characterized in that, the back taper cylinder that described gas distributor (9) is hollow, the sidewall of described back taper cylinder is provided with distribution hole (13).
6. thermal insulation according to claim 5-isothermal methanation reactor, is characterized in that, described distribution hole (13) be axially perpendicular to distribution hole (13) place plane.
7. thermal insulation according to claim 5-isothermal methanation reactor, it is characterized in that, the height of described back taper cylinder is 0.3 ~ 0.5 times of upper cover (2) height, the diameter of described back taper cylinder upper surface is vertically 2 ~ 2.5 times of the charging mouth of pipe (4) diameter, and the diameter of described back taper cylinder lower surface is vertically 1 ~ 1.5 times of the charging mouth of pipe (4) diameter.
8. thermal insulation according to claim 5-isothermal methanation reactor, is characterized in that, also comprises the catch (14) arranged in back taper cylinder.
9. thermal insulation according to claim 8-isothermal methanation reactor, it is characterized in that, described catch (14) is rounded, and the diameter of described catch (14) is 1 ~ 1.2 times of the charging mouth of pipe (4) diameter, and described catch (14) is 0.5 ~ 0.6 times of back taper height of column to the distance of upper surface.
10. thermal insulation according to claim 1-isothermal methanation reactor, is characterized in that, the cooling medium of described heat transfer space is saturation water.
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105349193A (en) * | 2015-12-10 | 2016-02-24 | 西南化工研究设计院有限公司 | Method for making methane-enriched gas in low-temperature and heat exchange mode |
| CN105413592A (en) * | 2015-12-17 | 2016-03-23 | 北京烨晶科技有限公司 | Combined type fixed bed reactor and device formed thereby |
| CN105542889A (en) * | 2015-12-15 | 2016-05-04 | 山西高碳能源低碳化利用研究设计院有限公司 | Quenching type methanation process with heat removing internally |
| 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 |
| CN105820847A (en) * | 2016-05-04 | 2016-08-03 | 四川天科技股份有限公司 | Methanation methane preparing technology with water supplementing circulation |
| CN107987907A (en) * | 2016-10-26 | 2018-05-04 | 中国石油天然气股份有限公司 | It is a kind of that the method rich in methane gas is prepared by synthesis gas |
| 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 |
| CN109482129A (en) * | 2019-01-18 | 2019-03-19 | 山东诺为制药流体系统有限公司 | A kind of multi-thread sequentially reaction system |
| CN109482128A (en) * | 2019-01-18 | 2019-03-19 | 山东诺为制药流体系统有限公司 | A kind of multi-thread reactor |
| CN109593581A (en) * | 2018-12-21 | 2019-04-09 | 惠生工程（中国）有限公司 | It is a kind of once to pass through methanation process |
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2014
- 2014-11-24 CN CN201420707199.7U patent/CN204247177U/en active Active
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105349193A (en) * | 2015-12-10 | 2016-02-24 | 西南化工研究设计院有限公司 | Method for making methane-enriched gas in low-temperature and heat exchange mode |
| CN105542889A (en) * | 2015-12-15 | 2016-05-04 | 山西高碳能源低碳化利用研究设计院有限公司 | Quenching type methanation process with heat removing internally |
| CN105413592A (en) * | 2015-12-17 | 2016-03-23 | 北京烨晶科技有限公司 | Combined type fixed bed reactor and device formed thereby |
| 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 |
| CN105820847A (en) * | 2016-05-04 | 2016-08-03 | 四川天科技股份有限公司 | Methanation methane preparing technology with water supplementing circulation |
| CN107987907B (en) * | 2016-10-26 | 2020-07-10 | 中国石油天然气股份有限公司 | Method for preparing methane-rich gas from synthesis gas |
| CN107987907A (en) * | 2016-10-26 | 2018-05-04 | 中国石油天然气股份有限公司 | It is a kind of that the method rich in methane gas is prepared by synthesis gas |
| 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 |
| CN108212025B (en) * | 2016-12-14 | 2020-07-03 | 中国石化工程建设有限公司 | Composite tower type methanation reactor |
| CN109593581A (en) * | 2018-12-21 | 2019-04-09 | 惠生工程（中国）有限公司 | It is a kind of once to pass through methanation process |
| CN109482128A (en) * | 2019-01-18 | 2019-03-19 | 山东诺为制药流体系统有限公司 | A kind of multi-thread reactor |
| CN109482129A (en) * | 2019-01-18 | 2019-03-19 | 山东诺为制药流体系统有限公司 | A kind of multi-thread sequentially reaction system |
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