CN102234213A - Complete methanation reaction device for synthesis gas - Google Patents
Complete methanation reaction device for synthesis gas Download PDFInfo
- Publication number
- CN102234213A CN102234213A CN2010101549268A CN201010154926A CN102234213A CN 102234213 A CN102234213 A CN 102234213A CN 2010101549268 A CN2010101549268 A CN 2010101549268A CN 201010154926 A CN201010154926 A CN 201010154926A CN 102234213 A CN102234213 A CN 102234213A
- Authority
- CN
- China
- Prior art keywords
- gas
- tubulation
- methanation
- reaction
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 64
- 230000015572 biosynthetic process Effects 0.000 title abstract 4
- 238000003786 synthesis reaction Methods 0.000 title abstract 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 13
- 239000000047 product Substances 0.000 claims abstract description 10
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 230000001105 regulatory effect Effects 0.000 claims abstract description 5
- 238000009826 distribution Methods 0.000 claims description 20
- 239000012071 phase Substances 0.000 claims description 13
- 238000006555 catalytic reaction Methods 0.000 claims description 11
- 239000007791 liquid phase Substances 0.000 claims description 9
- 239000006227 byproduct Substances 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000005266 casting Methods 0.000 claims description 3
- 239000012263 liquid product Substances 0.000 abstract description 3
- 239000007795 chemical reaction product Substances 0.000 abstract description 2
- 230000001276 controlling effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 59
- 238000000034 method Methods 0.000 description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 238000010926 purge Methods 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 239000008358 core component Substances 0.000 description 1
- 208000002925 dental caries Diseases 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a complete methanation reaction device for synthesis gas. The device consists of a tube-shell reactor, a heat exchanger, a steam pocket, a make-up water pump, a condenser and a gas-liquid separator, wherein a catalyst is filled in a tube of the reactor; the shell pass is superheated water for removing heat; heat released in methanation reaction is absorbed through the phase change of high-pressure superheated water in the shell pass of the reactor and taken out of the device; the generated steam enters the steam pocket, is subjected to gas-liquid balance and can directly form superheated steam to be supplied to the outside; the temperature of a catalyst bed in the tube of the reactor is regulated and controlled by controlling the balance pressure of the superheated steam; reaction product exit gas exchanges heat with raw material gas and is continuously condensed; and a gaseous product and a liquid product are separated by the gas-liquid separator. The device can realize the continuous and stable operation of the complete methanation reaction of the synthesis gas, can effectively improve heat transfer efficiency and control the temperature of the reaction bed in a phase change heat transfer mode at a high temperature and under high pressure, expands the operation range of the complete methanation reaction of the synthesis gas, and can effectively recycle the heat released in the reaction.
Description
Technical field
The invention belongs to synthetic gas methanation field, particularly a kind of synthetic gas full methanation reaction unit.
Background technology
The synthetic gas methanation reaction can improve fuel gas calorie density, reduces consumption of combustion gas transportation power and warehousing and transportation facilities investment, has better economy.Methanation reaction is a strong exothermal reaction, for productive efficiency and the continuity of operation that guarantees methanation, avoid the bed temperature runaway to cause the sintering of catalyst inactivation and cause can't ordinary production, the technological design that reaction heat shifts out mode becomes the core content of methanation process technology.
Disclose the multistage insulation fix bed reaction process of the common exploitation of German Lurgi company and South Africa SASOL company among the CN91106812.0, adopted and improve water to steam ratio control exothermic heat of reaction amount; US3967936 discloses the fixed bed methanation process of plural serial stage, cooperates a plurality of quench region to use jointly between each reactor, in order to regulate the reactor product temperature degree that each reactor discharges.One way reactor product purity is lower in the above process, and reactor needs repeatedly circulation, causes the technological operation complexity, and heat utilization efficiency is low, and the stable operation narrow range.
A kind of hydro-thermal transformationreation and the integrated technical process of methanation reaction that the CN1071190A of Hunan Chemical Industry Design Inst.'s application and CN1195020A successively disclose and optimize, its methanator adopts the external cooling calandria type fixed bed reactor, the reaction heat that cooling is shifted out with thermal oil is used to produce the water vapour of steam reacting condition, this technology is mainly used in water-gas through methanation reaction production city coal gas, and its shortcoming is that sulphur content needs less than satisfying the reaction requirement more than the 1ppm in the unstripped gas.In order to improve the sulfur tolerance of reaction, patent CN1718692A discloses a kind of methanation producing and manufacturing technique of low pressure sulfur resistant, the core component methanation reaction equipment of this technology has still adopted the calandria type fixed bed reaction process of external cooling, and the reaction liberated heat is shifted out by thermal oil gasification in the shell side.As a whole, built-in heat exchanger formula fixed bed reaction Technology has improved speed and device capbility that the reactor heat pipettes to a certain extent, and multistage relatively adiabatic reaction technology has certain technical superiority.But the heat transfer process of above-mentioned patented technology has all adopted thermal oil gasification heat-obtaining, and its reaction heat is recycled efficient and is restricted.
Summary of the invention
The object of the invention be in the methanation fixed-bed process since reaction conduct heat and recycle problem such as the less and complex process of the production capacity that causes, and provide a kind of synthetic gas full methanation reaction unit and integrated reaction method, this device and method is applicable to that the shell and tube-type reactor of methanation fixed-bed process moves the integrated technology of heat and while by-product superheated vapour, utilize high pressure superheater water as moving thermal medium, move heat by the superheated water phase transformation, and by-product higher-grade superheated vapour; This method can improve heat transfer efficiency, simplifies technological process, increases device capbility.
In order to realize the foregoing invention purpose, technical scheme of the present invention is as follows:
Synthetic gas full methanation reaction unit provided by the invention, it comprises: a shell and tube-type reactor, an interchanger 2, a drum 8, a make-up pump 6, a condenser 10 and a gas-liquid separator 11;
Described shell and tube-type reactor by reactor cavity, be individually fixed in following horizontal gas distribution grid that described reactor cavity is divided into upper chamber 3, middle part chamber and bottom chamber 31 3 parts 32 ' and last horizontal gas distribution grid 32 on reactor cavity intracoelomic cavity top and the bottom chamber wall, and form by the tubulation array that tubulation constitutes; Have one group of corresponding up and down through hole on described down horizontal gas distribution grid 32 ' and the last horizontal gas distribution grid 32, the tubulation 33 in the tubulation array is loaded on respectively on the described through hole of described horizontal gas distribution grid 32 ' down and last horizontal gas distribution grid 32; Be filled with methanation catalyst 4 in the described tubulation 33 and constitute methanation catalyzed reaction bed; Leave the space between described tubulation 33 and the reactor cavity and between the described tubulation 33, described space is made up of middle part vapour phase part and middle part liquid phase part, temperature is housed is 100 to 550 ℃ superheated water heat transferring medium in the liquid phase part of described middle part, be full of water vapor in the described top vapour phase part;
Described interchanger 2 inlets are connected with raw material of synthetic gas gas source of the gas, and unstripped gas is exported by pipeline by interchanger 2 and enters bottom chamber and be connected with all tubulations 33 the described tubulation array bottom reactor cavity through the heat exchange back of heating up;
Described drum 8 bottoms are connected with the middle part liquid phase part in described space by pipeline; Drum 8 tops partly are connected with the middle part gas phase in space by pipeline;
Described make-up pump 6 is connected with described drum 8 by pipeline, and on the pipeline that is connected a water regulating valve 7 is installed;
Described condenser 10 bottoms are connected with described gas-liquid separator 11 tops; Described condenser 10 bottoms are connected with described make-up pump 6; Described condenser 10 tops are connected with described interchanger 2;
The superheated vapour delivery port pipe 14 of band pressure regulator valve 9 is equipped with on described drum 8 tops;
The condensing water inlet pipe is equipped with on described condenser 10 tops;
The product outlet pipe 12 after the synthetic gas methanation is equipped with on described gas-liquid separator 11 tops; Byproduct outlet pipe 13 is equipped with in described gas-liquid separator 11 bottoms.
Triangular in shape or the rectangular arranged in axle center of adjacent tubulation 33 in the described tubulation array.
Described trilateral is an equilateral triangle, and described rectangle is a square.
Described tubulation 33 shape of cross sections are circular, square or Polygons.
Described tubulation diameter is 10-100mm, and tube pitch is 15-150mm.
Described tubulation is for casting tubulation or being the tubulation that adds fin on the outer wall.
Synthetic gas full methanation reaction unit of the present invention, adopt shell and tube-type reactor to realize that methanation reaction and heat of reaction pipette, wherein filling methanation catalyst 4 constitutes methanation catalyzed reaction bed in the tubulation 33 of shell and tube-type reactor inside, in the reactor shell side (being between tubulation 33 and the reactor cavity and the space of leaving between the tubulation 33) the superheated water heat transferring medium is housed; The unstripped gas of synthetic gas methanation reaction with the mixed gas that contains carbon monoxide and hydrogen as raw material, after at first being warmed up to certain temperature by heat exchange, enter by the shell and tube-type reactor bottom, through gas distribution grid after up by the methanation catalyzed reaction bed of inside reactor tubulation, under methanation catalyst 4 effects, the building-up reactions gas that contains carbon monoxide and hydrogen is finished methanation reaction, the reaction liberated heat is that the decalescence of 100 to 550 ℃ superheated water heat transferring medium is taken reactor out of by temperature in the shell and tube-type reactor, and the by-product superheated vapour; Methanation reaction outlet product gas enters Water in Condenser after the unstripped gas heat exchange cold, enters gas-liquid separator then and realize that gas-phase product separates with liquid product; The superheated vapour that whole technological process produces can be used for outer for generating electricity or supplying with the hydrogen-carbon ratio that is used for the conditioned reaction unstripped gas in this reaction process in the water gas shift reation; Make-up pump 6 injects drum 8 with the hot water of exporting in the condenser, and is constant with liquid level in the maintenance drum 8.
Shell and tube-type reactor of the present invention is the heat resisting and pressure resisting container of material, the synthetic gas methanation reaction carries out under normal pressure or high pressure, adopt superheated water as moving thermal medium,, take away the heat that methanation reaction produces by the decalescence in the superheated water part vaporescence.
The present invention perhaps by modifying tubulation outer wall proterties etc., increases heat interchanging area by adjusting the tubulation diameter and the number of shell and tube-type reactor, improves the production capacity and the efficient of reaction unit.
The present invention can also move the temperature and pressure of thermal medium by adjustment, realizes reacting under the different production efficiencys shifting out of strong heat release.
The thermal medium that moves of the present invention shows high-temperature characteristic, the bigger temperature stress of having avoided tubulation and horizontal gas distribution grid junction to exist; Move thermal medium and also show the high pressure feature, make superheated water slowly to vaporize, reduced the vibratory stress of eddy current in the rapid vaporescence.
Technique effect of the present invention is very remarkable:
Synthetic gas full methanation reaction unit of the present invention by the decalescence of superheated water heat transferring medium, has effectively improved the efficient that rate of heat transfer and heat of reaction are recycled, and has simplified technological process, has increased the operating restraint of reactor; In addition, the envelope type reactor thermal-transferring method of this synthetic gas full methanation reaction unit has improved the force-bearing situation of reactor in the methanation fixed-bed process greatly, has improved equipment serviceability and stability.
Description of drawings
Fig. 1 is the structural representation of synthetic gas full methanation reaction unit of the present invention;
Fig. 2 is the synoptic diagram that tubulation distributes among the embodiment.
Embodiment
Further describe the present invention below in conjunction with drawings and Examples.
Fig. 1 is the structural representation of the synthetic gas full methanation reaction unit of present embodiment, as shown in Figure 1, synthetic gas full methanation reaction unit provided by the invention, it comprises: a shell and tube-type reactor, an interchanger 2, a drum 8, a make-up pump 6, a condenser 10 and a gas-liquid separator 11;
Described shell and tube-type reactor by reactor cavity, be individually fixed in following horizontal gas distribution grid that described reactor cavity is divided into upper chamber 3, middle part chamber and bottom chamber 31 3 parts 32 ' and last horizontal gas distribution grid 32 on reactor cavity intracoelomic cavity top and the bottom chamber wall, and form by the tubulation array that tubulation constitutes; Have one group of corresponding up and down through hole on described down horizontal gas distribution grid 32 ' and the last horizontal gas distribution grid 32, the tubulation 33 in the tubulation array is loaded on respectively on the described through hole of described horizontal gas distribution grid 32 ' down and last horizontal gas distribution grid 32; Be filled with methanation catalyst 4 in the described tubulation 33 and constitute methanation catalyzed reaction bed; Leave the space between described tubulation 33 and the reactor cavity and between the described tubulation 33, described space is made up of middle part vapour phase part and middle part liquid phase part, temperature is housed is 100 to 550 ℃ superheated water heat transferring medium in the liquid phase part of described middle part, be full of water vapor in the described top vapour phase part;
Described interchanger 2 inlets are connected with raw material of synthetic gas gas source of the gas, and unstripped gas is exported by pipeline by interchanger 2 and enters bottom chamber and be connected with all tubulations 33 the described tubulation array bottom reactor cavity through the heat exchange back of heating up;
Described drum 8 bottoms are connected with the middle part liquid phase part in described space by pipeline; Drum 8 tops partly are connected with the middle part gas phase in space by pipeline;
Described make-up pump 6 is connected with described drum 8 by pipeline, and on the pipeline that is connected a water regulating valve 7 is installed;
Described condenser 10 bottoms are connected with described gas-liquid separator 11 tops; Described condenser 10 bottoms are connected with described make-up pump 6; Described condenser 10 tops are connected with described interchanger 2;
The superheated vapour delivery port pipe 14 of band pressure regulator valve 9 is equipped with on described drum 8 tops;
The condensing water inlet pipe is equipped with on described condenser 10 tops;
The product outlet pipe 12 after the synthetic gas methanation is equipped with on described gas-liquid separator 11 tops; Byproduct outlet pipe 13 is equipped with in described gas-liquid separator 11 bottoms.
Triangular in shape or the rectangular arranged in axle center of adjacent tubulation 33 in the described tubulation array.
Described trilateral is an equilateral triangle, and described rectangle is a square.
Described tubulation 33 shape of cross sections are circular, square or Polygons.
Described tubulation diameter is 10-100mm, and tube pitch is 15-150mm.
Described tubulation is for casting tubulation or being the tubulation that adds fin on the outer wall.
The axle center of adjacent tubulation 33 is equilateral triangle arrangement, its best results in the tubulation array of present embodiment.
The synthetic gas of present embodiment is the mixed gas that contains carbon monoxide and hydrogen;
The used methanation catalyst 4 of present embodiment is that the nickel of 40-52wt% is a methanation catalyst for Ni content.
The tubulation diameter of present embodiment is 20mm, and tube pitch is 30mm (can as required the tubulation diameter be controlled at 10-100mm, tube pitch is controlled between the 15-150mm).
The step of using synthetic gas full methanation reaction unit of the present invention to carry out synthetic gas full methanation integrated reaction is as follows:
Inject superheated water heat transferring medium 5 in the reactor cavity of the present invention; The filling nickel is the methanation catalyzed reaction bed that methanation catalyst 4 (Ni content is 40-52%) constitutes in the tubulation; At first feed nitrogen purging apparatus of the present invention, and will purge with nitrogen and be heated to 500 ℃ gradually, stop to purge after making methanation catalyzed reaction bed temperature in the tubulation be warmed up to 420 ℃, and guarantee that no oxygen exists in the reaction unit of the present invention;
The nitrogen purging gas circuit is switched to again and be blown into hydrogen, keeping hydrogen to be blown into mouthful preheating temperature is 400-450 ℃, and tubulation inner catalyst 4 is activated 4-6h; After catalyst activation finishes, adopt make-up pump 6 will move hot water via in the drum 8 injecting reactor cavitys, during this time need be before drum 8 inlet the employing auxiliary oven move hot water and be preheating to 300-350 ℃ described, can it be 260-300 ℃ by the temperature of pressure regulator valve 9 control water, corresponding pressure is 4.7-8.6MPa, after treating that simultaneously catalyzer 4 (methanation catalyzed reaction bed) temperature-stable in the tubulation 33 is 260-280 ℃, the synthetic gas that will contain carbon monoxide and hydrogen is entered in the reactor tubulation bottom shell and tube-type reactor through the interchanger 2 heat exchange back of heating up by raw material gas inlet 1; Synthetic raw gas consists of: hydrogen 61.8%, and carbon monoxide 20.2%, nitrogen 18.0%, the reaction temperature in of unstripped gas is 160-240 ℃ behind interchanger 2 pre-heating temperature elevations, pressure is 1.5-3.0MPa, reaction velocity 6000-8000h
-1After the reaction beginning, catalyzer 4 in the tubulation 33 (methanation catalyzed reaction bed) is rapidly heated, regulating pondage variable valve 7 and pressure regulator valve 9, make catalyzer 4 (the methanation catalyzed reaction bed) temperature in the tubulation 33 be controlled at 320-420 ℃, the temperature of high pressure superheater water 5 is controlled at 220-260 ℃, and corresponding superheated vapour pressure is 2.3-4.7MPa; After reactive system is stable, the temperature of reaction at catalyzer 4 (the methanation catalyzed reaction bed) center in the control tubulation 33 is 380-390 ℃, this moment, the per pass conversion of carbon monoxide was greater than 99%, and methane selectively is 78-86%, and by-product superheated vapour pressure is 2.4-2.8MPa; After gained reaction product and the unstripped gas heat exchange, continue to enter gas-liquid separator 11 after the cooling through condenser 10, separate the aqueous solution that obtains being rich in the gas-phase product of methane and containing micro-content organism and enter follow-up purification process through gas-phase product delivery port 12 and liquid product delivery port 13 respectively.Condenser 10 used condensation-water drain temperature are 40-70 ℃, are used for the supply water of reactor heat exchange; The superheated vapour of by-product is by superheated vapour delivery port 15 outer confessions in its reaction process.
Claims (6)
1. synthetic gas full methanation reaction unit, it comprises: a shell and tube-type reactor, an interchanger (2), a drum (8), a make-up pump (6), a condenser (10) and a gas-liquid separator (11);
Described shell and tube-type reactor by reactor cavity, be individually fixed in last horizontal gas distribution grid (32) that described reactor cavity is divided into upper chamber (3), middle part chamber and bottom chamber (31) three parts and following horizontal gas distribution grid (32 ') on reactor cavity intracoelomic cavity top and the bottom chamber wall, and form by the tubulation array that tubulation constitutes; Have one group of corresponding up and down through hole on described horizontal gas distribution grid (32 ') down and the last horizontal gas distribution grid (32), the tubulation in the tubulation array (33) is loaded on respectively on the described through hole of described horizontal gas distribution grid (32 ') down and last horizontal gas distribution grid (32); Be filled with methanation catalyst (4) in the described tubulation (33) and constitute methanation catalyzed reaction bed; Leave the space between described tubulation (33) and the reactor cavity and between the described tubulation (33), described space is made up of middle part vapour phase part and middle part liquid phase part, temperature is housed is 100 to 550 ℃ superheated water heat transferring medium in the liquid phase part of described middle part, be full of water vapor in the described top vapour phase part;
Described interchanger (2) inlet is connected with raw material of synthetic gas gas source of the gas, and unstripped gas is exported by pipeline by interchanger (2) and enters bottom chamber and be connected with all tubulations (33) the described tubulation array bottom reactor cavity through the heat exchange back of heating up;
Described drum (8) bottom is connected with the middle part liquid phase part in described space by pipeline; Drum (8) top partly is connected with the middle part gas phase in space by pipeline;
Described make-up pump (6) is connected with described drum (8) by pipeline, and on the pipeline that is connected a water regulating valve (7) is installed;
Described condenser (10) bottom is connected with described gas-liquid separator (11) top; Described condenser (10) bottom is connected with described make-up pump (6); Described condenser (10) top is connected with described interchanger (2);
The superheated vapour delivery port pipe (14) of band pressure regulator valve (9) is equipped with on described drum (8) top;
The condensing water inlet pipe is equipped with on described condenser (10) top;
The product outlet pipe (12) after the synthetic gas methanation is equipped with on described gas-liquid separator (11) top; Byproduct outlet pipe (13) is equipped with in described gas-liquid separator (11) bottom.
2. by the described synthetic gas full methanation of claim 1 reaction unit, it is characterized in that the triangular in shape or rectangular arranged in axle center of adjacent tubulation (33) in the described tubulation array.
3. by the described synthetic gas full methanation of claim 2 reaction unit, it is characterized in that described trilateral is an equilateral triangle, described rectangle is a square.
4. by the described synthetic gas full methanation of claim 1 reaction unit, it is characterized in that described tubulation (33) shape of cross section is circular, square or Polygons.
5. by the described synthetic gas full methanation of claim 1 reaction unit, it is characterized in that described tubulation (33) diameter is 10-100mm, tube pitch is 15-150mm.
6. by the described synthetic gas full methanation of claim 1 reaction unit, it is characterized in that described tubulation (33) is for casting tubulation or being the tubulation that adds fin on the outer wall.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101549268A CN102234213B (en) | 2010-04-20 | 2010-04-20 | Complete methanation reaction device for synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101549268A CN102234213B (en) | 2010-04-20 | 2010-04-20 | Complete methanation reaction device for synthesis gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102234213A true CN102234213A (en) | 2011-11-09 |
| CN102234213B CN102234213B (en) | 2013-05-01 |
Family
ID=44885391
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010101549268A Expired - Fee Related CN102234213B (en) | 2010-04-20 | 2010-04-20 | Complete methanation reaction device for synthesis gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102234213B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103373887A (en) * | 2012-04-24 | 2013-10-30 | 上海汉兴能源科技有限公司 | Method and isothermal methanator for preparing methane by using synthesis gas |
| CN104437266A (en) * | 2014-11-18 | 2015-03-25 | 安徽新月化工设备有限公司 | Phase change heat absorption temperature control reactor |
| 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 |
| CN106943957A (en) * | 2017-03-21 | 2017-07-14 | 淄博赢信达知识产权咨询服务有限公司 | A kind of coal bed gas deoxidation reaction unit |
| CN106943958A (en) * | 2017-03-25 | 2017-07-14 | 淄博赢信达知识产权咨询服务有限公司 | Low-pressure medium circulation moves the reactor assembly of thermal control temperature |
| CN106955647A (en) * | 2017-03-21 | 2017-07-18 | 淄博赢信达知识产权咨询服务有限公司 | A kind of low-pressure medium circulation moves the reactor assembly of thermal control temperature |
| CN106994319A (en) * | 2017-03-25 | 2017-08-01 | 淄博赢信达知识产权咨询服务有限公司 | The deoxygenation device of coalbed methane containing oxygen |
| CN108636300A (en) * | 2018-05-28 | 2018-10-12 | 中国五环工程有限公司 | Horizontal shell and tube reactor |
| CN109404873A (en) * | 2018-09-19 | 2019-03-01 | 上海兖矿能源科技研发有限公司 | A method of utilizing the hot by-product superheated steam of high-temperature Fischer-Tropsch synthesis reaction |
| CN112604640A (en) * | 2020-12-28 | 2021-04-06 | 苏州欣影生物医药技术有限公司 | Nano material preparation device and method |
| CN112675790A (en) * | 2020-12-04 | 2021-04-20 | 厦门大学 | Reactor and method for self-heat storage co-production of carbon nanotubes |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4177202A (en) * | 1977-03-07 | 1979-12-04 | Mobil Oil Corporation | Methanation of synthesis gas |
| CN87102871A (en) * | 1986-04-16 | 1987-11-18 | 于利奇核子研究设备公司 | The method for catalytic production of methane and the methanator that contain the synthetic gas of carbon monoxide, carbonic acid gas and hydrogen |
-
2010
- 2010-04-20 CN CN2010101549268A patent/CN102234213B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4177202A (en) * | 1977-03-07 | 1979-12-04 | Mobil Oil Corporation | Methanation of synthesis gas |
| CN87102871A (en) * | 1986-04-16 | 1987-11-18 | 于利奇核子研究设备公司 | The method for catalytic production of methane and the methanator that contain the synthetic gas of carbon monoxide, carbonic acid gas and hydrogen |
Non-Patent Citations (1)
| Title |
|---|
| 刘少文等: "流化床与固定床中甲烷裂解制氢过程的比较", 《化工学报》 * |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103373887A (en) * | 2012-04-24 | 2013-10-30 | 上海汉兴能源科技有限公司 | Method and isothermal methanator for preparing methane by using synthesis gas |
| CN103373887B (en) * | 2012-04-24 | 2014-12-10 | 上海汉兴能源科技有限公司 | Method and isothermal methanator for preparing methane by using synthesis gas |
| CN104437266A (en) * | 2014-11-18 | 2015-03-25 | 安徽新月化工设备有限公司 | Phase change heat absorption temperature control reactor |
| 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 |
| CN106955647A (en) * | 2017-03-21 | 2017-07-18 | 淄博赢信达知识产权咨询服务有限公司 | A kind of low-pressure medium circulation moves the reactor assembly of thermal control temperature |
| CN106943957A (en) * | 2017-03-21 | 2017-07-14 | 淄博赢信达知识产权咨询服务有限公司 | A kind of coal bed gas deoxidation reaction unit |
| CN106943958A (en) * | 2017-03-25 | 2017-07-14 | 淄博赢信达知识产权咨询服务有限公司 | Low-pressure medium circulation moves the reactor assembly of thermal control temperature |
| CN106994319A (en) * | 2017-03-25 | 2017-08-01 | 淄博赢信达知识产权咨询服务有限公司 | The deoxygenation device of coalbed methane containing oxygen |
| CN108636300A (en) * | 2018-05-28 | 2018-10-12 | 中国五环工程有限公司 | Horizontal shell and tube reactor |
| CN109404873A (en) * | 2018-09-19 | 2019-03-01 | 上海兖矿能源科技研发有限公司 | A method of utilizing the hot by-product superheated steam of high-temperature Fischer-Tropsch synthesis reaction |
| CN112675790A (en) * | 2020-12-04 | 2021-04-20 | 厦门大学 | Reactor and method for self-heat storage co-production of carbon nanotubes |
| CN112604640A (en) * | 2020-12-28 | 2021-04-06 | 苏州欣影生物医药技术有限公司 | Nano material preparation device and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102234213B (en) | 2013-05-01 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102234213B (en) | Complete methanation reaction device for synthesis gas | |
| CN103908929B (en) | A kind of methanol-to-olefins fixed bed production equipment combining heat exchange type muitishell and production method thereof | |
| US4865624A (en) | Method for steam reforming methanol and a system therefor | |
| CN101704513B (en) | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof | |
| CN101773808B (en) | Combined reaction device | |
| CN101817716B (en) | Method and device for catalyzing methanation of synthesis gas | |
| CN101480592B (en) | Fixed bed composite reaction equipment | |
| CN201168595Y (en) | Composite reaction equipment | |
| JP4073960B2 (en) | Hydrocarbon steam reforming method | |
| CN110550602B (en) | Controllable semi-isothermal conversion process for high-concentration carbon monoxide for oxo synthesis | |
| CN101723775A (en) | Method and equipment for preparing hydrocarbon by methyl alcohol or/ and dimethyl ether | |
| JP5188895B2 (en) | Methanol synthesis reactor and methanol synthesis method | |
| CN101519336B (en) | Method and equipment for producing hydrocarbon with synthetic gas | |
| CN201211474Y (en) | Fixed bed composite reaction equipment | |
| CN101580748A (en) | Method and device for producing natural gas from synthetic gas through methanation reaction | |
| CN102337160B (en) | High-water-steam-ratio saturated hot water tower split CO transformation process | |
| KR102193200B1 (en) | Thermochemical upgrading system of bio-gas | |
| CN101659879B (en) | Chemical-electric poly-generation method and equipment | |
| WO2021083234A1 (en) | Equalized-temperature processing system and method for synthesizing natural gas by means of methanation of carbon dioxide | |
| CN203170305U (en) | Combined-heat-exchange multi-shell-side fixed bed production equipment for preparing olefin from methanol | |
| CN203568842U (en) | Combined conversion device for synthesized gas CO | |
| CN101928206B (en) | Method for producing dimethyl ether by synthesis gas and equipment thereof | |
| CN203750514U (en) | Reactor for producing gasoline by using synthesis gas | |
| CN201439492U (en) | Shunting isothermal sulphur-resisting conversion device | |
| CN204619936U (en) | A kind of split type methanator utilizing heat pipe heat-obtaining |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130501 |