CN204298356U - The system of raw gas direct methanation - Google Patents
The system of raw gas direct methanation Download PDFInfo
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- CN204298356U CN204298356U CN201420670033.2U CN201420670033U CN204298356U CN 204298356 U CN204298356 U CN 204298356U CN 201420670033 U CN201420670033 U CN 201420670033U CN 204298356 U CN204298356 U CN 204298356U
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Abstract
The utility model discloses the system of raw gas direct methanation, comprise: a kind of system of raw gas direct methanation, it is characterized in that, comprise: raw gas preheater, pre-methanator, hydrogen carbon adjuster, methanator and desulfurization and decarburization device, pre-methanator is connected with raw gas preheater and the raw gas be suitable for through the pre-heat treatment carries out pre-methanation reaction, to obtain pre-methanation mist; Hydrogen carbon adjuster is connected with pre-methanator and is suitable for pre-methanation mist and carries out transformationreation, to obtain transformationreation mist; Methane reactor is connected with hydrogen carbon adjuster and is suitable for transformationreation mist and carries out multistage methanation reaction, to obtain rough methane and steam; Desulfurization and decarburization device is connected to obtain refine methane with methanator.Simple according to the system architecture of the raw gas direct methanation of the utility model embodiment, significantly can save Equipments Setting, shorten preparation flow, save energy consumption, significantly reduce costs.
Description
Technical field
The utility model relates to methanation field, particularly relates to the system of raw gas direct methanation.
Background technology
Traditional raw gas SNG technological process, by the raw gas after dedusting after conversion, reduces temperature to normal temperature, raised temperature again after process for purifying process, then carries out methanation reaction, and then deliver to lower procedure after lowering the temperature; Because process for purifying is between conversion and methanation, cause conversion gas must lower the temperature and purified gas must heat up, need more than the ten platform high-tension apparatuses such as supporting heat exchanger, separator and corresponding pipeline, instrument control etc. thus, cause flow process complexity, investment is higher and energy consumption is larger.
Therefore still there is the demand improved further in the above-mentioned technique for the preparation of methane.
Utility model content
The utility model is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, an object of the present utility model is that proposition is a kind of more rationally, the system of Low investment, low consumed raw gas direct methanation.
For this reason, according to an aspect of the present utility model, the utility model proposes a kind of system of raw gas direct methanation, comprising:
Raw gas preheater, described raw gas preheater is suitable for the pre-heat treatment of described raw gas;
Pre-methanator, described pre-methanator is connected with described raw gas preheater and the raw gas be suitable for through described the pre-heat treatment carries out pre-methanation reaction, to obtain pre-methanation mist;
Hydrogen carbon adjuster, described hydrogen carbon adjuster is connected with described pre-methanator and is suitable for described pre-methanation mist and carries out transformationreation, to obtain transformationreation mist;
Methanator, described methane reactor is connected with described hydrogen carbon adjuster and is suitable for described transformationreation mist and carries out multistage methanation reaction, to obtain described rough methane and steam;
Desulfurization and decarburization device, described desulfurization and decarburization device is connected with described methanator and is suitable for described rough methane and carries out desulfurization and carbonization treatment, to obtain refine methane.
Thus, the system architecture of the raw gas direct methanation of the utility model above-described embodiment is simple, and flow process is short, small investment.And adopt the system of above-mentioned raw gas direct methanation effectively can prepare methane, significantly reduce cost simultaneously.
In the utility model, the system of above-mentioned raw gas direct methanation comprises further:
First useless pot, the described first useless pot is connected with described hydrogen carbon adjuster and is suitable for carrying out cooling to described transformationreation mist and processes, to obtain the first saturated vapor;
Second useless pot, the described second useless pot is connected with described methanator and is suitable for carrying out the first cooling process to rough methane, to obtain the second saturated vapor;
Three wastes pot, described three wastes pot and the described second useless pot are connected and are suitable for carrying out the second cooling process, to obtain low-pressure steam to through the described first rough methane processed of lowering the temperature.Transformationreation and the extra output saturated vapor of methanation reaction liberated heat and low-pressure steam can be made full use of thus, improve the heat utilization rate of system, balance sysmte energy consumption.
In the utility model, the system of above-mentioned raw gas direct methanation comprises further:
Steam superheater, described steam superheater is connected with the described first useless pot with the described second useless pot and is suitable for changing described first saturated vapor and the second saturated vapor into superheated steam.
In the utility model, the system of above-mentioned raw gas direct methanation comprises further:
First cooler, described first cooler is connected with described three wastes pot and is suitable for carrying out cooling processing to through the described second rough methane processed of lowering the temperature;
First gas-liquid separator, described first gas-liquid separator and described first condenser are connected with desulfurization and decarburization device and are suitable for carrying out gas-liquid separation to the rough methane through described cooling processing, to obtain dry rough methane.
In the utility model, the system of above-mentioned raw gas direct methanation comprises further:
Final stage preheater, described final stage preheater is connected with described desulfurization and decarburization device and is suitable for carrying out preheating to the rough methane through desulfurization and decarburization process;
Final stage methane reactor, described final stage methane reactor is connected with described final stage preheater and the rough methane be suitable for through described desulfurization and decarburization process carries out final stage methanation reaction, to obtain refine methane.Methane production can be improved further thus.
In the utility model, the system of above-mentioned raw gas direct methanation comprises further:
Second cooler, described second cooler is connected with described final stage methane reactor and is suitable for carrying out the second cooling processing to refine methane;
Second gas-liquid separator, described second gas-liquid separator is connected with described second condenser and is suitable for carrying out gas-liquid separation to the refine methane through described second cooling processing, to obtain dry refine methane.
Accompanying drawing explanation
Fig. 1 is the structural representation of the system of raw gas direct methanation according to the utility model embodiment.
Fig. 2 is the flow chart of the system direct methanation method of the raw gas direct methanation adopting the utility model embodiment.
Detailed description of the invention
Be described below in detail embodiment of the present utility model, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the utility model, and can not be interpreted as restriction of the present utility model.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In description of the present utility model, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the utility model, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements.For the ordinary skill in the art, the concrete meaning of above-mentioned term in the utility model can be understood as the case may be.
According to an aspect of the present utility model, the utility model proposes a kind of system of raw gas direct methanation.The system of the raw gas direct methanation of the utility model above-described embodiment is described below with reference to Fig. 1.
System according to the raw gas direct methanation of the utility model embodiment comprises: raw gas preheater 01, pre-methanator 02, hydrogen carbon adjuster 03, methanator 04 and desulfurization and decarburization device 05.
Wherein, raw gas preheater 01 is suitable for the pre-heat treatment of raw gas; Pre-methanator 02 is connected with raw gas preheater 01 and the raw gas be suitable for through the pre-heat treatment carries out pre-methanation reaction, to obtain pre-methanation mist; Hydrogen carbon adjuster 03 is connected with pre-methanator 02 and is suitable for pre-methanation mist and carries out transformationreation, to obtain transformationreation mist; Methane reactor 04 is connected with hydrogen carbon adjuster 03 and is suitable for transformationreation mist and carries out multistage methanation reaction, to obtain rough methane and steam; Desulfurization and decarburization device 05 is connected with methanator 04 and is suitable for rough methane and carries out desulfurization and carbonization treatment, to obtain refine methane.
Thus, the system architecture of the raw gas direct methanation of the utility model above-described embodiment is simple, and flow process is short, small investment.And adopt the system of above-mentioned raw gas direct methanation effectively can prepare methane, significantly reduce cost simultaneously.Adopt the system of the raw gas direct methanation of the utility model above-described embodiment raw gas can be carried out pre-methanation reaction, transformationreation and methanation reaction successively, can methane be prepared.Inventor of the present utility model has used pre-methanation reaction to provide steam for transformationreation dexterously, and transformationreation provides suitable C/Hratio for methanation reaction, and then improves productive rate and the purity of preparing methane.The system of the raw gas direct methanation of the utility model above-described embodiment is utilized to prepare methane without the need to repeatedly being carried out lowering the temperature and hyperthermic treatment by raw gas in conventional method, and then significantly can save energy consumption, this system architecture is simple simultaneously, flow process is short, and then significantly can save equipment investment, fundamentally reduce the cost preparing methane.
According to specific embodiment of the utility model, the system of above-mentioned raw gas direct methanation comprises further: the first useless pot 07 of useless pot 06, second and three wastes pot 08.Wherein, the first useless pot 06 is connected with hydrogen carbon adjuster 03 and is suitable for carrying out cooling to transformationreation mist and processes, to obtain the first superheated vapor; Second useless pot 07 is connected with methanator 04 and is suitable for carrying out the first cooling process to rough methane, to obtain the second superheated vapor; Three wastes pot 08 and the second useless pot 07 are connected and are suitable for carrying out the second cooling process, to obtain low-pressure steam to through the first rough methane processed of lowering the temperature.
The above-mentioned first useless pot 07 of useless pot 06, second and three wastes pot 08 can make full use of transformationreation and the extra output saturated vapor of methanation reaction liberated heat and low-pressure steam thus, improve the heat utilization rate of system, balance sysmte energy consumption.According to specific embodiment of the utility model, the saturated vapor of above-mentioned output and low-pressure steam may be used for other technique, also may be used for the transformationreation in hydrogen carbon adjuster simultaneously, and then improve the efficiency of transformationreation, simultaneously for the methanation reaction in methanator provides sound assurance.In addition, the transformationreation saturated vapor of above-mentioned output and low-pressure steam are used in hydrogen carbon adjuster effectively can also reduce the pressure of pre-methanation reaction in pre-methanator.
According to another specific embodiment of the present utility model, the system of above-mentioned raw gas direct methanation can further include: the first cooler 09 and the first gas-liquid separator 10.Wherein, the first cooler 09 is connected with three wastes pot 08 and is suitable for carrying out cooling processing to through the second rough methane processed of lowering the temperature; First gas-liquid separator 10 and the first condenser 09 are connected with desulfurization and decarburization device 05 and are suitable for carrying out gas-liquid separation to the rough methane through cooling processing, to obtain dry rough methane.Be convenient to the desulfurization and decarburization process of rough methane thus, and then improve the purity of rough methane.
According to another specific embodiment of the present utility model, the system of above-mentioned raw gas direct methanation can further include: final stage preheater 11 and final stage methane reactor 12.Wherein, final stage preheater 11 is connected with desulfurization and decarburization device 05 and is suitable for carrying out preheating to the rough methane through desulfurization and decarburization process; Final stage methane reactor 12 is connected with final stage preheater 11 and the rough methane be suitable for through described desulfurization and decarburization process carries out final stage methanation reaction, to obtain refine methane.The purity of methane production and methane can be improved thus further.
According to another specific embodiment of the present utility model, the system of above-mentioned raw gas direct methanation can further include: the second cooler 13 and the second gas-liquid separator 14.Wherein, the second cooler 13 is connected with final stage methane reactor 12 and is suitable for carrying out the second cooling processing to refine methane; Second gas-liquid separator 14 is connected with the second condenser 13 and is suitable for carrying out gas-liquid separation to the refine methane through the second cooling processing, to obtain dry refine methane.Thus, effectively can be removed the water vapour of final stage methanation reaction generation by the second cooler 13 and the second gas-liquid separator 14, and then improve the purity of refine methane.
According to another specific embodiment of the present utility model, the system of above-mentioned raw gas direct methanation can further include: steam superheater 15, steam superheater 15 is connected with the first useless pot 06 and the second useless pot 07, the first saturated vapor of output in the pot 07 that gives up from the first useless pot 06 and second and the second saturated vapor can be changed into the superheated steam of more high-quality thus by steam superheater 15.And then the thermal energy that transformationreation and methanation reaction are released the most at last is the superheated steam that can recycle, the cost of investment of the system of balance raw gas direct methanation.
The transformationreation in hydrogen carbon adjuster that the pre-methanation reaction in pre-methanator is next step is utilized to provide steam needed for reaction dexterously according to the system of the raw gas direct methanation of above-described embodiment of the present utility model, and further, utilize the transformationreation in hydrogen carbon adjuster be next step ground methanator in methanation reaction suitable C/Hratio is provided, and then significantly improve methanation reaction efficiency, improve the productive rate preparing methane.This system is more traditional without the need to more than the ten platform high-tension apparatuses such as supporting heat exchanger, separator and the corresponding equipment such as pipeline, instrument control, and then save considerably equipment investment, reduces raw methanogenic cost.
The system of the raw gas direct methanation adopting the utility model embodiment is described to the method for raw gas direct methanation below with reference to Fig. 2.The method comprises: raw gas is carried out the pre-heat treatment; Hocket the raw gas through the pre-heat treatment methanation reaction and transformationreation, to obtain rough methane; And rough methane is carried out desulfurization and carbonization treatment, to obtain refine methane.
Thus, adopt the method for the raw gas direct methanation of the utility model above-described embodiment, raw gas without the need to entering methanation operation again after conversion, cooling, desulfurization, decarburization, but directly carries out methanation reaction and transformationreation, prepares methane.Technological process more traditional thus significantly can save Equipments Setting, shortens preparation flow, saves energy consumption, significantly reduces costs.
S100: the pre-heat treatment
According to specific embodiment of the utility model, first raw gas is carried out the pre-heat treatment, the efficiency of pre-methanation reaction can be improved thus further.
According to specific embodiment of the utility model, raw gas is the industrial gasses through dust removal process produced in gasification furnace, comprises carbon monoxide, hydrogen, carbon dioxide, methane and water vapour in described raw gas.The method of raw gas direct methanation of the present utility model is to unstripped gas raw gas not special requirement.Therefore, the method for the raw gas direct methanation of the utility model above-described embodiment has wider applicability.
More of the present utility model be in embodiment, the temperature of described raw gas is 20 ~ 280 degrees Celsius.May be used for the temperature of the unstripped gas raw gas of the method for raw gas direct methanation of the present utility model and be not particularly limited, significantly can save energy consumption thus.
In method according to the raw gas direct methanation of the utility model specific embodiment, hocket methanation reaction and transformationreation are specifically carried out according to the following step: pre-methanation reaction, transformationreation and methanation reaction.
S200: pre-methanation reaction
First, raw gas is carried out pre-methanation reaction, to obtain pre-methanation mist.According to specific embodiment of the utility model, methanation main technique principle is: carbon monoxide or carbon dioxide and hydrogen issue biochemical reaction in the effect of certain temperature, pressure and catalyst, and chemical equation is:
Thus, first inventor makes raw gas that pre-methanation reaction occurs, and produces portion of methane and produces steam.The object of this step is to produce steam, and then provides reaction raw materials for next step transformationreation, and transformationreation is then for further methanation reaction is prepared.
According to specific embodiment of the utility model, pre-methanation reaction is exothermic reaction.Thus, the method of the raw gas direct methanation reaction of above-described embodiment comprises the pre-methanation mist that obtained by pre-methanation reaction further and raw gas carries out heat exchange process, and then utilize pre-methanation reaction liberated heat to carry out preheating for raw gas, improve the reaction efficiency of pre-methanation reaction, improve so that final the efficiency preparing methane.
S300: transformationreation
Pre-methanation mist is carried out transformationreation, to obtain transformationreation mist.According to specific embodiment of the utility model, conversion main technique principle is: carbon monoxide and water vapour issue biochemical reaction at certain temperature, pressure and catalyst action, and chemical equation is:
Thus, inventor applies pre-methanation reaction is dexterously that transformationreation provides reaction raw materials steam.And transformationreation can provide suitable C/Hratio for methanation reaction further.And then the productive rate of methanation reaction can be significantly improved.According to specific embodiment of the utility model, transformationreation is exothermic reaction equally.Thus, the method of the raw gas direct methanation reaction of above-described embodiment comprises the conversion mist that conversionization is obtained by reacting further and supplementing water carries out heat exchange process, and then output saturated vapor while making full use of transformationreation liberated heat, reduce production cost thus.
S400: methanation reaction
Transformationreation mist is carried out methanation reaction, to obtain rough methane and steam.According to specific embodiment of the utility model, the principle of methanation reaction is with above-mentioned pre-methanation reaction.The raw material of methanation reaction is the product of above-mentioned reacting condition, and the C/Hratio obtained by transformationreation is applicable to the demand of methanation reaction more, can improve the productive rate of methanation reaction thus further.Inventor of the present utility model regulates C/Hratio in raw gas by transformationreation dexterously thus, and direct methanation reaction has prepared methane.In addition, above-mentioned methanation reaction is similarly exothermic reaction.Thus, the method of the raw gas direct methanation reaction of above-described embodiment can further include the rough methane that obtained by methanation reaction and supplementing water carries out heat exchange process, and then output saturated vapor while making full use of methanation reaction liberated heat, reduce production cost thus.
According to specific embodiment of the utility model, above-mentioned methanation reaction is multipolarity methanation reaction.The efficiency of methanation reaction and the purity of productive rate and methane can be improved thus further.
Thus, adopt the system of the raw gas direct methanation of the utility model above-described embodiment simple to the method technique of raw gas direct methanation, flow process is short, and then significantly can save energy consumption.And the method for what the method was more traditional prepare methane eliminates cooling repeatedly, temperature-rise period, and then not only save technological equipment investment cost and significantly reduce energy consumption simultaneously.
According to specific embodiment of the utility model, the above-mentioned saturated vapor of the heat output of transformationreation and methanation reaction product that utilizes also can return for above-mentioned transformationreation, significantly can reduce the pressure of pre-methanation reaction thus.Improve the productive rate of transformationreation simultaneously further, and then obtain the reacting condition mist that C/Hratio is suitable for methanation reaction more.Thus, finally the efficiency and productive rate and purity of preparing methane is improved.
According to specific embodiment of the utility model, the reaction conditions such as above-mentioned pre-methanation reaction, transformationreation and the temperature required for methanation reaction, pressure and catalyst are all not particularly limited, and carry out as long as can ensure and maintain conventional reaction.
S500: desulfurization and carbonization treatment
The rough methane that above-mentioned hocket methanation reaction and transformationreation finally obtain is carried out desulfurization and carbonization treatment, to obtain refine methane.The purity of methane can be improved thus further.
In the description of this description, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present utility model or example.In this manual, to the schematic representation of above-mentioned term not must for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this description or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and described embodiment of the present utility model above, be understandable that, above-described embodiment is exemplary, can not be interpreted as restriction of the present utility model, those of ordinary skill in the art can change above-described embodiment, revises, replace and modification in scope of the present utility model.
Claims (5)
1. a system for raw gas direct methanation, is characterized in that, comprising:
Raw gas preheater, described raw gas preheater is suitable for the pre-heat treatment of described raw gas;
Pre-methanator, described pre-methanator is connected with described raw gas preheater and the raw gas be suitable for through described the pre-heat treatment carries out pre-methanation reaction, to obtain pre-methanation mist;
Hydrogen carbon adjuster, described hydrogen carbon adjuster is connected with described pre-methanator and is suitable for described pre-methanation mist and carries out transformationreation, to obtain transformationreation mist;
Methanator, described methane reactor is connected with described hydrogen carbon adjuster and is suitable for described transformationreation mist and carries out multistage methanation reaction, to obtain described rough methane and steam;
Desulfurization and decarburization device, described desulfurization and decarburization device is connected with described methanator and is suitable for described rough methane and carries out desulfurization and carbonization treatment, to obtain refine methane.
2. the system of raw gas direct methanation according to claim 1, is characterized in that, comprise further:
First useless pot, the described first useless pot is connected with described hydrogen carbon adjuster and is suitable for carrying out cooling to described transformationreation mist and processes, to obtain the first saturated vapor;
Second useless pot, the described second useless pot is connected with described methanator and is suitable for carrying out the first cooling process to rough methane, to obtain the second saturated vapor;
Three wastes pot, described three wastes pot and the described second useless pot are connected and are suitable for carrying out the second cooling process, to obtain low-pressure steam to through the described first rough methane processed of lowering the temperature;
Steam superheater, described steam superheater is connected with the described first useless pot with the described second useless pot and is suitable for changing described first saturated vapor and the second saturated vapor into superheated steam.
3. the system of raw gas direct methanation according to claim 2, is characterized in that, comprise further:
First cooler, described first cooler is connected with described three wastes pot and is suitable for carrying out cooling processing to through the described second rough methane processed of lowering the temperature;
First gas-liquid separator, described first gas-liquid separator and described first condenser are connected with desulfurization and decarburization device and are suitable for carrying out gas-liquid separation to the rough methane through described cooling processing, to obtain dry rough methane.
4. the system of raw gas direct methanation according to claim 1, is characterized in that, comprise further:
Final stage preheater, described final stage preheater is connected with described desulfurization and decarburization device and is suitable for carrying out preheating to the rough methane through desulfurization and decarburization process;
Final stage methane reactor, described final stage methane reactor is connected with described final stage preheater and the rough methane be suitable for through described desulfurization and decarburization process carries out final stage methanation reaction, to obtain refine methane.
5. the system of raw gas direct methanation according to claim 4, is characterized in that, comprise further:
Second cooler, described second cooler is connected with described final stage methane reactor and is suitable for carrying out the second cooling processing to refine methane;
Second gas-liquid separator, described second gas-liquid separator is connected with described second condenser and is suitable for carrying out gas-liquid separation to the refine methane through described second cooling processing, to obtain dry refine methane.
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Effective date of registration: 20150603 Address after: 200131 Shanghai Free Trade Zone, Shanghai, No. 29, Tai 2 Road, West 404-A12 Patentee after: Shanghai Yao Xing management of investment company limited Address before: 201112 room 1, building 60, No. 719, Lane three, 127 Lu Lu, Shanghai, Minhang District Patentee before: Shanghai Xinxing Chemical Technology Co., Ltd. |