CN106118770A - A kind of system and method catalyzing and synthesizing natural gas - Google Patents
A kind of system and method catalyzing and synthesizing natural gas Download PDFInfo
- Publication number
- CN106118770A CN106118770A CN201610515958.3A CN201610515958A CN106118770A CN 106118770 A CN106118770 A CN 106118770A CN 201610515958 A CN201610515958 A CN 201610515958A CN 106118770 A CN106118770 A CN 106118770A
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- China
- Prior art keywords
- pyrolysis
- natural gas
- unit
- temperature
- gas
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/02—Combustion or pyrolysis
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/04—Gasification
Abstract
The invention provides a kind of system and method catalyzing and synthesizing natural gas.This system includes material unit, pyrolysis unit and air processing unit；Material unit is provided with coal entrance, lime inlet and mixture outlet；Pyrolysis unit is provided with mixture inlet and pyrolysis gas outlet, and mixture inlet is connected with the mixture outlet of material unit；Pyrolysis unit is provided with the thermal source of high-temperature region and low-temperature space, high-temperature region and low-temperature space for adding heat pipe, and adding heat pipe is catalyst carrier；Air processing unit is provided with pyrolysis gas entrance and gas outlet, and pyrolysis gas entrance is connected with the pyrolysis gas outlet of pyrolysis unit.The system and method catalyzing and synthesizing natural gas that the present invention provides can synthesize the natural gas that concentration is higher.
Description
Technical field
The invention belongs to natural gas synthesis field, be specifically related to a kind of system and method catalyzing and synthesizing natural gas.
Background technology
China's petroleum resources shortage, needs in a large number from external import, and China's natural gas external dependence degree in 2014 is up to
32.2%, affect China's economic development.At present, natural gas (CH is obtained from coal4) mode predominantly: coal gasification synthesis of natural
Gas or pyrolysis gas (coke-stove gas) synthetic natural gas.The conversion per pass preparing natural gas with coal is relatively low, prepares if wanting to improve
The concentration of natural gas, it is necessary to high temperature circulation blower fan, coal gas is repeatedly circulated, increases the response time of coal gas.This preparation process
Time consumption and energy consumption, and high temperature circulation blower fan is expensive, the gas cost causing synthesis is the highest.
Summary of the invention
It is an object of the invention to provide a kind of system and method catalyzing and synthesizing natural gas.
A kind of system catalyzing and synthesizing natural gas that the present invention provides includes material unit, pyrolysis unit and gas treatment list
Unit；
Described material unit is provided with coal entrance, lime inlet and mixture outlet；
Described pyrolysis unit is provided with mixture inlet and pyrolysis gas outlet, described mixture inlet and described material unit
Mixture outlet is connected；Described pyrolysis unit is provided with high-temperature region and low-temperature space, and the thermal source of described high-temperature region and described low-temperature space is
Add heat pipe, described in add heat pipe be catalyst carrier；
Described air processing unit is provided with pyrolysis gas entrance and gas outlet, and described pyrolysis gas entrance is single with described pyrolysis
The pyrolysis gas outlet of unit is connected.
Further, described pyrolysis gas outlet is arranged on described low-temperature space.
Further, adding heat pipe described in is fin heats pipe.
A kind of method utilizing said system to catalyze and synthesize natural gas that the present invention provides, comprises the following steps:
Coal and Calx are respectively fed to described material unit mix, prepare mixture；
Catalyst is respectively coated with and adds tube surface in described high-temperature region and described low-temperature space, and described mixture is sent
Enter described pyrolysis unit to be pyrolyzed, obtain pyrolysis gas；
Carry out purifying by the described pyrolysis gas described air processing unit of feeding, dedusting and separation, obtain natural gas.
Further, it is high-temperature methanation catalyst that described high-temperature region adds the catalyst of tube surface, and described low-temperature space adds
The catalyst of tube surface is Catalyst for Low-Temperature Methanation.
Further, the temperature of described high-temperature region is 430-750 DEG C, and the temperature of described low-temperature space is 200-430 DEG C.
Further, the mass ratio of described coal and Calx is 1:0.003-0.02.
Further, the time of described pyrolysis is 1-2h.
Further, the pressure of described pyrolysis unit is 1.5-3MPa.
The system and method catalyzing and synthesizing natural gas that the present invention provides, not only technique is simple, with low cost, and can close
Become the natural gas that concentration is higher.Additionally, the service life of catalyst is long.
Accompanying drawing explanation
Fig. 1 is the structural representation of pyrolysis unit in embodiment；
Fig. 2 is the structural representation of fin heats pipe cross section in embodiment；
Fig. 3 is the top view of fin heats pipe in embodiment；
Fig. 4 is the process chart catalyzing and synthesizing natural gas in embodiment.
In figure: 1, mixture inlet；2, pyrolysis gas outlet；3, heat pipe is added；31, body；32, fin；4, drawing mechanism.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and various aspects thereof.But, specific embodiments described below and enforcement
Example is only descriptive purpose rather than limitation of the present invention.
In following embodiment, institute's taking technique condition value is exemplary, its desirable numerical range such as foregoing summary
Shown in.Detection method used by following embodiment is the detection method that the industry is conventional.
Embodiment 1
The system catalyzing and synthesizing natural gas that the present embodiment provides, including material unit, pyrolysis unit and gas treatment list
Unit.Material unit is provided with coal entrance, lime inlet and mixture outlet.As it is shown in figure 1, pyrolysis unit is provided with mixture inlet 1
With pyrolysis gas outlet 2, mixture inlet 1 is connected with the mixture outlet of material unit；Pyrolysis unit is provided with high-temperature region and low temperature
District；Adding the thermal source that heat pipe 3 is high-temperature region and low-temperature space, adding heat pipe 3 area load has catalyst.Air processing unit is provided with pyrolysis
Gas entrance and gas outlet, pyrolysis gas entrance is connected with the pyrolysis gas outlet 2 of pyrolysis unit.
Pyrolysis unit is provided with high-temperature region and low-temperature space, and the synthetic reaction of the process of pyrolysis of coal and major part natural gas is mainly sent out
Raw in high-temperature region, low-temperature space is mainly used in moisture-free coal and improves the concentration of natural gas.
In the present embodiment, pyrolysis unit is pyrolysis oven, and adding heat pipe is radial canal.
The present embodiment as the carrier of catalyst rather than additionally arranges catalyst load using adding heat pipe 3 in pyrolysis unit
Body.So on the one hand, the temperature of catalyst can be made to be rapidly achieved light-off temperature, on the other hand can reduce in pyrolysis unit and fill
The quantity put.
Pyrolysis gas outlet 2 can be arranged on any position of pyrolysis unit, and pyrolysis gas outlet 2 is arranged on low by the present embodiment
Warm area (as shown in Figure 1).In this case, the pyrolysis gas produced in high-temperature region needs to return low-temperature space and is then exhausted from, and adds sky
So time of gas synthesis, thus improve the concentration of natural gas in pyrolysis gas.
The shape adding heat pipe 3 is not required to be particularly limited to, and the present embodiment uses fin heats pipe as thermal source, fin heats
The concrete shape of pipe asks for an interview Fig. 2 and Fig. 3.The surface area of fin heats pipe is big, uses fin heats pipe as thermal source, can either increase
Add the contact area of catalyst and pyrolysis gas so that reaction carries out more abundant；The heat radiation area adding heat pipe can be increased again,
Strengthen heat transfer, be conducive to promoting the thermal efficiency.
Embodiment 2
Seeing Fig. 4, the present embodiment provides a kind of method of system catalytic synthetic natural gas utilizing embodiment 1 to provide, bag
Include following steps:
Coal and Calx are respectively fed to material unit mix, prepare mixture；
Catalyst is respectively coated with the tube surface that adds in high-temperature region and low-temperature space, and mixture is sent into pyrolysis unit enters
Row pyrolysis, obtains pyrolysis gas, pyrolysis oil and solid product；
Pyrolysis gas is sent into air processing unit carry out purifying, dedusting and separation, obtain natural gas.
Under the effect of catalyst, the hydrogen (H generated after pyrolysis of coal2), carbon monoxide (CO), carbon dioxide (CO2) reaction
Generating natural gas, reaction equation is as follows:
3H2+ CO=CH4+H2O ΔH1=-206.16KJ/mol
4H2+CO2=CH4+2H2O ΔH2=-165.08KJ/mol
Δ H in aforesaid equation is reaction heat.
Calx can consolidate sulfur, sends into pyrolysis unit and is pyrolyzed, can reduce the pyrolysis gas prepared after being mixed with coal by Calx
The content of middle sulfide, but also it is avoided that catalyst poisoning, extend the use time of catalyst.
The design parameter of the coal that the present embodiment uses asks for an interview table 1, and the design parameter of the Calx of employing asks for an interview table 2.This enforcement
In example, the particle diameter of coal and Calx is between 5-45mm.
The kind of the catalyst in said method is not required to be particularly limited to, as long as hydrogen and carbon monoxide, dioxy can be made
Change carbon reaction and generate natural gas.In the present embodiment, high-temperature region adds the catalyst of tube surface and selects high-temperature methanation catalysis
Agent, low-temperature space adds the catalyst of tube surface and selects Catalyst for Low-Temperature Methanation.Select different in pyrolysis unit zones of different
Catalyst, has more specific aim, can generate more natural gas.
It is exothermic reaction that hydrogen and carbon monoxide, carbon dioxide generate the reaction of natural gas, and pyrolysis of coal is the endothermic reaction, because of
The temperature of this high-temperature region and low-temperature space is not required to the highest needs i.e. ensureing pyrolysis of coal and natural gas synthesis.Additionally, temperature surpasses
Crossing 750 DEG C, catalyst easily inactivates.Inventor is found by substantial amounts of experiment, and the temperature of high-temperature region is 430-750 DEG C, low temperature
When the temperature in district is 200-430 DEG C, the effect of pyrolysis of coal is preferable, and the concentration of the natural gas of synthesis is higher.
In the present embodiment, the temperature of high-temperature region is 750 DEG C, and the temperature of low-temperature space is 200 DEG C.
In said method, the mass ratio of coal and Calx is 1:0.003-0.02.The mass ratio of coal and Calx is not required to spy
Not limiting, inventor is found by substantial amounts of experiment, when the mass ratio of coal and Calx is 1:0.003-0.02, neither wastes stone
Ash, and catalyst is also not easy poisoning, additionally, the content of sulfide is the lowest in the pyrolysis gas prepared.
In the present embodiment, the mass ratio of coal and Calx is 1:0.012.
In said method, the time of pyrolysis is 1-2h.The time of pyrolysis is the shortest, and pyrolysis of coal is insufficient, the natural gas of synthesis
Few；Pyrolysis time is oversize, wastes the energy.Inventor is found by substantial amounts of experiment, when the time of pyrolysis is 1-2h, and the sky of synthesis
So gas is many.
In the present embodiment, the time of pyrolysis is 1h.
In said method, the pressure of pyrolysis unit is 1.5-3MPa.Pressure is the least, hydrogen and carbon monoxide, carbon dioxide
The reaction generating natural gas is insufficient, and the natural gas of synthesis is few；Pressure is too big, and the loss of equipment is big.Inventor is by substantial amounts of
Experiment finds, when the pressure of pyrolysis unit is 1.5-3MPa, both can guarantee that the reaction of synthetic natural gas was smoothed out, and can reduce again
Infringement to equipment.
In the present embodiment, the pressure of pyrolysis unit is 1.5MPa.
In the pyrolysis gas that the present embodiment prepares, the volume content of natural gas is 80.5%.
The main character of table 1 coal
| Project | Unit | Numerical value | Remarks |
| Quan Shui | Wt% | 5.33 | As-received |
| Fixed carbon | Wt% | 55.7 | Butt |
| Volatile matter | Wt% | 37.2 | Butt |
| Ash | Wt% | 7.1 | Butt |
Table 2 Calx component analysis
From above-described embodiment, use the technical scheme that the present invention provides, the content of natural gas in prepared pyrolysis gas
The highest.
To sum up, it can be deduced that, the system and method catalyzing and synthesizing natural gas that the present invention provides, not only technique is simple, one-tenth
This is cheap, and can synthesize the natural gas that concentration is higher.
It should be noted that each embodiment above by reference to described by accompanying drawing is only in order to illustrate rather than restriction originally
The scope of invention, it will be understood by those within the art that, the most right
Amendment that the present invention is carried out or equivalent, all should contain within the scope of the present invention.Additionally, unless stated otherwise, that
All or part of of any embodiment can use in conjunction with all or part of of any other embodiments.
Claims (9)
1. catalyze and synthesize a system for natural gas, including material unit, pyrolysis unit and air processing unit；
Described material unit is provided with coal entrance, lime inlet and mixture outlet；
Described pyrolysis unit is provided with the mixing of mixture inlet and pyrolysis gas outlet, described mixture inlet and described material unit
Thing outlet is connected；Described pyrolysis unit is provided with high-temperature region and low-temperature space, and the thermal source of described high-temperature region and described low-temperature space is heating
Pipe, described in add heat pipe be catalyst carrier；
Described air processing unit is provided with pyrolysis gas entrance and gas outlet, described pyrolysis gas entrance and described pyrolysis unit
Pyrolysis gas outlet is connected.
System the most according to claim 1, it is characterised in that described pyrolysis gas outlet is arranged on described low-temperature space.
System the most according to claim 1, it is characterised in that described in add heat pipe be fin heats pipe.
4. one kind utilizes the method for arbitrary described system catalytic synthetic natural gas in claim 1-3, it is characterised in that described side
Method comprises the following steps:
Coal and Calx are respectively fed to described material unit mix, prepare mixture；
Catalyst is respectively coated with the tube surface that adds in described high-temperature region and described low-temperature space, and described mixture is sent into institute
State pyrolysis unit to be pyrolyzed, obtain pyrolysis gas；
Carry out purifying by the described pyrolysis gas described air processing unit of feeding, dedusting and separation, obtain natural gas.
The method of synthetic natural gas the most according to claim 4, it is characterised in that described high-temperature region adds urging of tube surface
Agent is high-temperature methanation catalyst, and it is Catalyst for Low-Temperature Methanation that described low-temperature space adds the catalyst of tube surface.
The method catalyzing and synthesizing natural gas the most according to claim 4, it is characterised in that the temperature of described high-temperature region is
430-750 DEG C, the temperature of described low-temperature space is 200-430 DEG C.
The method catalyzing and synthesizing natural gas the most according to claim 4, it is characterised in that described coal and the mass ratio of Calx
For 1:0.003-0.02.
The method catalyzing and synthesizing natural gas the most according to claim 4, it is characterised in that the time of described pyrolysis is 1-
2h。
The method catalyzing and synthesizing natural gas the most according to claim 4, it is characterised in that the pressure of described pyrolysis unit is
1.5-3MPa。
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| CN201610515958.3A CN106118770A (en) | 2016-07-01 | 2016-07-01 | A kind of system and method catalyzing and synthesizing natural gas |
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| CN201610515958.3A CN106118770A (en) | 2016-07-01 | 2016-07-01 | A kind of system and method catalyzing and synthesizing natural gas |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585947A (en) * | 2011-12-14 | 2012-07-18 | 新奥科技发展有限公司 | Method and device for preparing methane-containing gas by using coal |
| CN102911756A (en) * | 2012-10-26 | 2013-02-06 | 太原理工大学 | Technology for producing methane through low-rank coal |
| CN104164249A (en) * | 2014-08-14 | 2014-11-26 | 北京神雾环境能源科技集团股份有限公司 | Pyrolyzer |
| CN104350007A (en) * | 2012-06-06 | 2015-02-11 | 卡萨莱股份有限公司 | A process for gas-heated reforming of a hydrocarbon source and related equipment |
| CN105121606A (en) * | 2012-12-11 | 2015-12-02 | Sk新技术株式会社 | Gasification process and system using dryer integrated with water-gas shift catalyst |
| KR20150143080A (en) * | 2014-06-13 | 2015-12-23 | 충북대학교 산학협력단 | Reforming system for fuel cell with improved heat transfer performance |
-
2016
- 2016-07-01 CN CN201610515958.3A patent/CN106118770A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102585947A (en) * | 2011-12-14 | 2012-07-18 | 新奥科技发展有限公司 | Method and device for preparing methane-containing gas by using coal |
| CN104350007A (en) * | 2012-06-06 | 2015-02-11 | 卡萨莱股份有限公司 | A process for gas-heated reforming of a hydrocarbon source and related equipment |
| CN102911756A (en) * | 2012-10-26 | 2013-02-06 | 太原理工大学 | Technology for producing methane through low-rank coal |
| CN105121606A (en) * | 2012-12-11 | 2015-12-02 | Sk新技术株式会社 | Gasification process and system using dryer integrated with water-gas shift catalyst |
| KR20150143080A (en) * | 2014-06-13 | 2015-12-23 | 충북대학교 산학협력단 | Reforming system for fuel cell with improved heat transfer performance |
| CN104164249A (en) * | 2014-08-14 | 2014-11-26 | 北京神雾环境能源科技集团股份有限公司 | Pyrolyzer |
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Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant after: Shenwu science and technology group Limited by Share Ltd Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
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Application publication date: 20161116 |