CN105112111A - Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas - Google Patents
Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas Download PDFInfo
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- CN105112111A CN105112111A CN201510617499.5A CN201510617499A CN105112111A CN 105112111 A CN105112111 A CN 105112111A CN 201510617499 A CN201510617499 A CN 201510617499A CN 105112111 A CN105112111 A CN 105112111A
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Abstract
The invention provides an integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas. The integration process includes a methanation portion and an acidic gas removing portion with two stages mutually independent, the methanation portion comprises a high-temperature methanation reactor and at least one low-temperature methanation reactor which are arranged sequentially, the acidic gas removing portion comprises a first-stage sulfur-containing component removing portion and a second-stage CO2 removing portion, the first-stage sulfur-containing component removing portion is arranged in front of the methanation portion, the second-stage CO2 removing portion is arranged in or in rear of the methanation portion, and a circulating compressor is omitted in the whole process. Compared with conventional technical methods, the integration process and equipment has the advantages of higher economic benefit, lower comprehensive energy consumption and smaller equipment size.
Description
Technical field
The present invention relates to methanation field, furtherly, relate to integrated technique and the equipment of coal based synthetic gas preparing natural gas by methanation.
Background technology
Methanation reaction is strong exothermal reaction, at present, the methanation technology of existing industrialized unit is in order to remove reaction heat fast and ensure that reaction temperature rising is unlikely to excessive, the object controlling temperature of reaction is all reached by cyclic part gas product, namely fresh feed gas all or major part enter the first methanator, the high methane gas be cooled by a certain reactor outlet that circulates controls the temperature rise of the first methanator.Some problems will be there are like this, such as: technique can be produced coagulate water thus cause power loss in circulation gas working cycle, reduce energy recovery rate; The setting of recycle compressor adds the energy consumption of device, occupation of land and running cost; Add invalid gas volume in unstripped gas, reduce the First Pass Yield of raw material, add reactor, valve, line size, thus add investment; Complicated and the multiple stage reactor of temperature control regulation measure operates under being in the extreme operating condition such as high temperature, high pressure, and equipment material requires harsh, invests huge.
Therefore, on the basis of existing research, exploitation reduces running cost and plant energy consumption, and the methanation process of simplification of flowsheet extremely needs.
Summary of the invention
In order to solve the aforementioned problems in the prior, the invention provides a kind of coal based synthetic gas without the integrated technique of circulation preparing natural gas by methanation and equipment.This technique reduces running cost and plant energy consumption, simplifies the configuration of technical process and external system, finally realizes better economic benefit.
The invention provides the integrated technique of a kind of coal based synthetic gas without circulation preparing natural gas by methanation, this technique comprises methanation part and the mutual independently sour gas of two-stage removes part; Wherein, described methanation part comprises the high-temperature methanation reactor and at least one low temperature methanator that set gradually; Described two-stage mutually independently sour gas remove part and comprise one-level and remove sulfur component part and secondary removes CO
2part; Described one-level removes before sulfur component part is arranged at methanation part, and described secondary removes CO
2part is arranged among methanation part or afterwards, whole technological process cancels recycle compressor.
The present invention also provides a kind of coal based synthetic gas without the integrated equipment of circulation preparing natural gas by methanation, and this equipment comprises methanation part and the mutual independently sour gas of two-stage removes part; Wherein, described methanation part comprises the high-temperature methanation reactor and at least one low temperature methanator that set gradually; Described two-stage mutually independently sour gas remove part and comprise one-level and remove sulfur component device and secondary removes CO
2device; Described one-level removes before sulfur component device is arranged at methanation part, and described secondary removes CO
2device is arranged among methanation part or afterwards, whole technological process cancels recycle compressor.
The present invention is by utilizing sulfur component and CO in synthetic gas
2the feature of component stage treatment in sour gas subtractive process, by methanation and sour gas being removed Appropriate application, the effective integration of device, in whole process, recycle gas compressor not being set, significantly reducing plant energy consumption and running cost, technique does not have complex control, simpler than prior art flow process.
Another advantage is, by removing the effective integration of device with sour gas, removing in sulfur component device only remove sulfur component in one-level, residue CO
2reduce the content of high-temperature methanation reactor inlet CO as dilution inert component to control to react temperature out, thus reduce the middle pressure steam amount of allocating into.
Above-mentioned all advantages make present invention process and device compared with traditional technology method, have higher economic benefit, lower comprehensive energy consumption, less equipment size.
Accompanying drawing explanation
In conjunction with the drawings present invention process flow process is described more intuitively.
Fig. 1 shows the schema of coal based synthetic gas of the present invention without the integrated technique of circulation preparing natural gas by methanation.
Embodiment
The invention provides the integrated technique of a kind of coal based synthetic gas without circulation preparing natural gas by methanation, this technique comprises methanation part and the mutual independently sour gas of two-stage removes part; Wherein, described methanation part comprises the high-temperature methanation reactor and at least one low temperature methanator that set gradually; Described two-stage mutually independently sour gas remove part and comprise one-level and remove sulfur component part and secondary removes CO
2part; Described one-level removes before sulfur component part is arranged at methanation part, and described secondary removes CO
2part is arranged among methanation part or afterwards, whole technological process cancels recycle compressor.
Preferably, in the present invention, integrated technique comprises: unstripped gas removes sulfur component partial removal sulfur component through one-level, then, press through hot steam in allocating into react in high-temperature methanation reactor, after reaction, gas enters low temperature methanator I after residual neat recovering system I, after reaction, gas is by entering low temperature methanator II after residual neat recovering system II and condensation skimmer I, and after low temperature methanation reaction, gas enters secondary and removes CO
2partial removal CO
2the coal system of reaching substitutes Sweet natural gas (being called for short SNG) gas product requirement, or removes CO
2after through low temperature methanator III, reach the requirement of SNG gas product after reaction.
Preferably, described one-level removes the sulphur content of working off one's feeling vent one's spleen of sulfur component part is below 0.1ppm.
Preferably, the described middle pressure steam amount of allocating into is the 1%-10% of material gas quantity.
Preferably, secondary removes CO
2the CO of part
2decreasing ratio is 90%-99%.
Preferably, the temperature in of described high-temperature methanation reactor is 260-320 DEG C.
Preferably, described low temperature methanator is 2-3 platform, and the temperature in of low temperature methanator is 240-260 DEG C.
Preferably, point liquid temp of described condensation skimmer I is between 60 DEG C-130 DEG C.
The present invention also provides a kind of coal based synthetic gas without the integrated equipment of circulation preparing natural gas by methanation, and this equipment comprises methanation part and the mutual independently sour gas of two-stage removes part; Wherein, described methanation part comprises the high-temperature methanation reactor and at least one low temperature methanator that set gradually; Described two-stage mutually independently sour gas remove part and comprise one-level and remove sulfur component device and secondary removes CO
2device; Described one-level removes before sulfur component device is arranged at methanation part, and described secondary removes CO
2device is arranged among methanation part or afterwards, whole technological process cancels recycle compressor.
Preferably, described methanation device comprises 1 the high-temperature methanation reactor and 2-3 platform low temperature methanator that set gradually, and described secondary removes CO
2after device next-door neighbour is arranged at second low temperature methanator.
Preferably, residual neat recovering system I and residual neat recovering system II is respectively arranged with between described high-temperature methanation reactor and First low temperature methanator and between First low temperature methanator and second low temperature methanator.
Preferably, condensation skimmer I is provided with between a described residual neat recovering system II and second low temperature methanator.
Figure 1 shows that a kind of preferred implementation of the present invention, unstripped gas removes sulfur component device through one-level and only removes sulfur component, then, press through hot steam in allocating into react in high-temperature methanation reactor, after reaction, gas enters low temperature methanator I after residual neat recovering system I, and after reaction, gas reacts by entering low temperature methanator II after residual neat recovering system II and condensation skimmer I.Low temperature methanator II works off one's feeling vent one's spleen and enters secondary and remove CO
2device, removes CO
2after through low temperature methanator III, reach the requirement of SNG gas product after reaction.
Embodiment
The integrated technique of coal based synthetic gas without circulation preparing natural gas by methanation is carried out in equipment as shown in Figure 1.
Mark square gauge mould for annual output methanation gas product 1,300,000,000, unstripped gas is broken coal gasification synthesis gas is example after changing device, and its feature consists of: H
2: 45.2mol%, CO:14.3mol%, CO
2: 32.6mol%, CH
4: 7.4mol%.As shown in Figure 1, first material synthesis gas removes sulfur component device by one-level, only removes the sulfur component in unstripped gas, and sulphur content is down to below 0.1ppm (in mol), retains CO
2component enters methanation part as rare gas element together with synthetic gas.In methanation part, unstripped gas allocate into a certain amount of in press through hot steam and react in a high-temperature methanation reactor I, the described middle pressure steam amount of allocating into is 30000kg/h, and temperature of reaction controls at 650 DEG C.After reaction, gas reclaims after high-temperature residual heat through residual neat recovering system I, enter low temperature methanator I, temperature of reaction 450 DEG C, after reaction, gas enters low temperature methanator II, temperature of reaction 300 DEG C after there are high pressure steam and 120 DEG C of condensation skimmer I separatory by residual neat recovering system II.Low temperature methanator II works off one's feeling vent one's spleen and enters sour gas and remove part secondary, removes CO
2reach the requirement of SNG gas product, or remove CO
2after through low temperature methanator III, reach the requirement of gas product gas after reaction.
Wherein, fresh feed temperature degree 40 DEG C, molar flow 30937Kmol/h, high-temperature methanation reactor inlet temperature 280 DEG C, three low temperature methanator temperature ins are 260 DEG C.The superheated vapour 367t/h of 3.5MPag420 DEG C can be there is.Secondary removes CO
2the CO of device
2decreasing ratio 98%, obtains the methanation gas product of 7254.46Kmol/h after low temperature methanator III.
Prior art reaches by arranging recycle compressor circulation large-tonnage product gas the object controlling temperature of reaction, different from the technology of the present invention.
Prior art also has the situation of adding middle pressure steam, but is do not remove efficient coupling with sour gas with difference of the present invention, and prior art is disposable removes whole sulphur components and CO
2carry out methanation reaction after component, could not CO be utilized
2steam consumption is reduced as indifferent gas.The middle pressure steam amount of allocating into of the present invention is significantly smaller than prior art, is only the 30-50% of prior art.
Claims (10)
1. coal based synthetic gas is without an integrated technique for circulation preparing natural gas by methanation, it is characterized in that, this technique comprises methanation part and the mutual independently sour gas of two-stage removes part; Wherein, described methanation part comprises the high-temperature methanation reactor and at least one low temperature methanator that set gradually; Described two-stage mutually independently sour gas remove part and comprise one-level and remove sulfur component part and secondary removes CO
2part; Described one-level removes before sulfur component part is arranged at methanation part, and described secondary removes CO
2part is arranged among methanation part or afterwards, whole technological process cancels recycle compressor.
2. coal based synthetic gas according to claim 1 is without the integrated technique of circulation preparing natural gas by methanation, wherein, unstripped gas removes sulfur component partial removal sulfur component through one-level, then, press through hot steam in allocating into react in high-temperature methanation reactor, after reaction, gas enters low temperature methanator I after residual neat recovering system I, after reaction, gas is by entering low temperature methanator II after residual neat recovering system II and condensation skimmer I, and after low temperature methanation reaction, gas enters secondary and removes CO
2partial removal CO
2after reach gas product requirement.
3. coal based synthetic gas according to claim 1 is without the integrated technique of circulation preparing natural gas by methanation, and wherein, the sulphur content of working off one's feeling vent one's spleen that one-level removes sulfur component part is below 0.1ppm.
4. coal based synthetic gas according to claim 2 is without the integrated technique of circulation preparing natural gas by methanation, and wherein, the described middle pressure steam amount of allocating into is the 1%-10% of material gas quantity.
5. coal based synthetic gas according to claim 1 is without the integrated technique of circulation preparing natural gas by methanation, and wherein, secondary removes CO
2the CO of part
2decreasing ratio is 90%-99%.
6. according to the integrated technique of the coal based synthetic gas in claim 1-5 described in any one without circulation preparing natural gas by methanation, wherein, the temperature in of described high-temperature methanation reactor is 260-320 DEG C.
7. according to the integrated technique of the coal based synthetic gas in claim 1-5 described in any one without circulation preparing natural gas by methanation, wherein, described low temperature methanator is 2-3 platform, and the temperature in of low temperature methanator is 240-260 DEG C.
8. according to the integrated technique of the coal based synthetic gas in claim 1-5 described in any one without circulation preparing natural gas by methanation, wherein, point liquid temp of described condensation skimmer I is between 60 DEG C-130 DEG C.
9. coal based synthetic gas is without an integrated equipment for circulation preparing natural gas by methanation, it is characterized in that, this equipment comprises methanation part and the mutual independently sour gas of two-stage removes part; Wherein, described methanation part comprises the high-temperature methanation reactor and at least one low temperature methanator that set gradually; Described two-stage mutually independently sour gas remove part and comprise one-level and remove sulfur component device and secondary removes CO
2device; Described one-level removes before sulfur component device is arranged at methanation part, and described secondary removes CO
2device is arranged among methanation part or afterwards, whole technological process cancels recycle compressor.
10. equipment according to claim 9, wherein, described methanation device comprises 1 the high-temperature methanation reactor and 2-3 platform low temperature methanator that set gradually, and described secondary removes CO
2after device next-door neighbour is arranged at second low temperature methanator; Residual neat recovering system I and residual neat recovering system II is respectively arranged with between described high-temperature methanation reactor and First low temperature methanator and between First low temperature methanator and second low temperature methanator; Condensation skimmer I is provided with between a described residual neat recovering system II and second low temperature methanator.
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| CN201510617499.5A CN105112111A (en) | 2015-09-24 | 2015-09-24 | Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas |
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| CN201510617499.5A CN105112111A (en) | 2015-09-24 | 2015-09-24 | Integration process and equipment for loop-free methanation of coal-based syngas to prepare natural gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106190382A (en) * | 2016-07-16 | 2016-12-07 | 中国科学院山西煤炭化学研究所 | The technique that producing synthesis gas from coal carries out methanation synthesis substitute natural gas |
| CN109593580A (en) * | 2018-12-21 | 2019-04-09 | 惠生工程（中国）有限公司 | A kind of semi-coke furnace tail gas fine de-sulfur and adiabatic methanation process |
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| US20130046031A1 (en) * | 2008-04-16 | 2013-02-21 | Methanol Cassale SA | Process and Plant for Substitute Natural Gas |
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| CN103897758A (en) * | 2012-12-26 | 2014-07-02 | 浦项产业科学研究院 | Equipment and method for producing synthesized gas with low H2/CO ratio |
| CN104357117A (en) * | 2014-10-31 | 2015-02-18 | 西南化工研究设计院有限公司 | Non-circulating methanation process of coal-based synthetic natural gas and liquefied natural gas |
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Patent Citations (8)
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| DE2234654A1 (en) * | 1972-07-14 | 1974-02-07 | Metallgesellschaft Ag | PROCESS FOR PRODUCING A METHANE-RICH GAS EXCHANGEABLE WITH NATURAL GAS |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106190382A (en) * | 2016-07-16 | 2016-12-07 | 中国科学院山西煤炭化学研究所 | The technique that producing synthesis gas from coal carries out methanation synthesis substitute natural gas |
| CN106190382B (en) * | 2016-07-16 | 2019-08-06 | 中国科学院山西煤炭化学研究所 | Producing synthesis gas from coal carries out the technique that methane is combined to substitute natural gas |
| CN109593580A (en) * | 2018-12-21 | 2019-04-09 | 惠生工程（中国）有限公司 | A kind of semi-coke furnace tail gas fine de-sulfur and adiabatic methanation process |
| CN109593580B (en) * | 2018-12-21 | 2021-02-05 | 惠生工程（中国）有限公司 | Semi-coke furnace tail gas fine desulfurization and adiabatic methanation process |
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Application publication date: 20151202 |