CN203096014U - Device for producing natural gas from factory waste gas - Google Patents
Device for producing natural gas from factory waste gas Download PDFInfo
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- CN203096014U CN203096014U CN 201320022697 CN201320022697U CN203096014U CN 203096014 U CN203096014 U CN 203096014U CN 201320022697 CN201320022697 CN 201320022697 CN 201320022697 U CN201320022697 U CN 201320022697U CN 203096014 U CN203096014 U CN 203096014U
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- gas
- methanation
- water
- natural gas
- methane
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Abstract
The utility model discloses a device for producing artificial natural gas from factory waste gas. According to the device, a methanation synthesis reactor, a tower-ahead the heat exchanger, an operation heater, a water cooler, a water separator, a methane concentration device, a compressor and a steam turbine are sequentially connected, the methanation synthesis reactor is externally connected with a steam dome, a water pump and the operation heater, and the steam dome is further connected with the steam turbine. The device disclosed by the utility model has the advantages that methane is synthesized from industrial waste gas instead of coal produced gas, so that national resources are saved, the emission of CO2 is reduced, and the environment is protected; meanwhile, low-temperature methanation is carried out by using water-cooling heat exchange, so that the methanation reaction conditions are optimized, the methane synthesis ratio is increased, the process flow is simplified, equipment is reduced, a circulator is cancelled, and the power consumption is reduced; and high-pressure steam, namely a heat byproduct of methane synthesis reaction, is used for supplying power required for driving the steam turbine and the water pump to compress the natural gas, so that the device has the advantages of energy saving and consumption reducing.
Description
Technical field
The utility model relates to technical field of chemical engineering, relates in particular to a kind of device that utilizes plant gas system synthetic natural gas.
Background technology
Sweet natural gas is a kind of clean energy, China's natural gas at the domestic energy proportion far below the international average level, National Development and Reform Committee " 12 " natural gas development planning clearly takes and year increases amount of natural gas 50,000,000,000 sides, the coal preparing natural gas can be with direct hydrogasification of coal or the methanation of steam catalyzed conversion single stage method, but the gasification that extensively adopts at present makes the H that synthetic gas again will be wherein
2, CO, CO
2Carry out methanation reaction, produce synthetic natural gas, and though more than be single stage method methanation or gasification again methanation all to consume a large amount of coal resources, and China has multiple plant gas or industrial tail gas to contain the H of above-mentioned synthesizing methane
2, CO, CO
2, for example ammonia factory off-gas has H about in the of 70%
2With about 10%CH
4The decarburization stripping gas has CO more than 90%
2, the Methanol Plant off-gas has high-load H
2, CO, CO
2, coke-oven plant's coke(oven)gas has CH4 and H about in the of 20%
2, CO, CO
2, steel mill's blast furnace gas and converter gas have 10% above CO
2And 20-55%CO, furnace of calcium carbide and yellow phosphorus stove have 75-90%CO, and above-mentioned industrial gaseous waste all can utilize the raw material as synthetic artificial Sweet natural gas.
The characteristics of the methane of the at present domestic and international artificial Sweet natural gas of synthetic gas system, the one, synthetic technology substantially all adopts many adiabatic methanation reactors, for example use the high-temperature methanation (see figure 1) of rope company of Denmark Top, take three methanator series connection, before and after two intersegmental the heat exchange water cooler arranged, reduce temperature and advance the hypomere methanation again, first methanator part gas of giving vent to anger in addition loops back import and reacts, this class methanation method exists easy cross of methanation catalyst to occur knot carbon in heat inactivation and the methanation and influence ordinary production, and heat recovery efficiency is low, energy consumption is big.The 2nd, the used synthetic gas of synthesizing methane is mainly the CO hydrogenation reaction, and for example Top's rope company is H
2/ CO=3 (SNG) promptly presses CO+3H
2=CH
4+ H
2The O reaction, Dai Wei company is then with containing CO=19.2% and H
2Reaction, CO in the synthetic gas
2=0.8%.
CO
2Add H
2Methanation reaction is a strong exothermal reaction:
CO
2+4H
2＝CH
4+2H
2O
Along with reaction heat discharges, the reaction gas temperature raises in above-mentioned adiabatic reactor, and the equilibrium constant that generates methane declines to a great extent, and influences CO
2The synthesizing methane transformation efficiency.CO
2Add H
2Synthetic CH
4The equilibrium constant
During by 280 ℃ 1.486 * 10
6Drop to 600 ℃ 0.76,0.51 * 10 when having only 280 ℃
-6Doubly.
The utility model content
At the problems referred to above, the purpose of this utility model provides a kind of device that utilizes the artificial Sweet natural gas of plant gas system of energy-conserving and environment-protective.
For achieving the above object, the utility model is taked following technical scheme:
A kind of device that utilizes the artificial Sweet natural gas of plant gas system, comprise drum, boiler water pump, interchanger, the well heater that goes into operation, water cooler, water separator, methane concentration unit, compressor and steam turbines before methanation synthesis reactor, the tower, interchanger, the well heater that goes into operation, water cooler, water separator, methane concentration unit, compressor are connected successively with steam turbines before described methanation synthesis reactor, the tower, described methanator also is circumscribed with drum and water pump, and described drum is connected with steam turbines.
The described well heater that goes into operation is steam injector or electric heater (being installed in when selecting electric heater for use between preceding interchanger of tower and the methanation synthesis reactor).
Described methanation synthesis reactor is that water-cooled heat exchange type fixed-bed reactor or water-cooled are around tubular reactor.
Interchanger and the synthetic gas heat exchange that goes out the methanation synthesis reactor before the advanced tower of industrial gaseous waste after the purification, advance the methanation synthesis reactor again and carry out methanation reaction, the synthetic gas that goes out the methanation synthesis reactor is isolated water of condensation through water cooler, water separator after the interchanger cooling more successively before tower, send to methane concentration unit and compressor and propose dense, compression and obtain artificial Sweet natural gas.The drum that is connected with the methanation synthesis reactor produces high pressure steam, sends to steam turbines with being used as power or going generator for electricity generation.
The utility model device is mainly used in the artificial Sweet natural gas technology of the plant gas system of utilization, and this technology is with a kind of CO that contains
2And/or CO and H
2Plant gas, or the multiple CO that contains separately
2And/or CO and/or H
2Plant gas, remove objectionable impurities through purification to catalyzer, pass through CO
2Add H
2And/or CO adds H
2Artificial gas product is produced in the reaction that generates methane.
, when described plant gas is multiple, the wherein at least a H that contains
2
As a kind of preferred, the methane of generation is carried dense from product gas with transformation absorption or membrane separation process or Deep Cooling Method.
As a kind of preferred, when described plant gas is a kind of, adopt the coke(oven)gas of synthesizing methanol factory's off-gas or coking plant.
As a kind of preferred, when described plant gas is multiple, adopt synthesis ammonia plant to contain H
2Off-gas, synthesis ammonia plant decarburization contain CO
2Stripping gas, synthesizing methanol factory off-gas, coking plant coke(oven)gas, blast furnace gas, converter gas, calcium carbide stove exhaust, yellow phosphoric tail gas or silicon carbide gas in several.
Described ammonia factory off-gas also can purify removes behind the ammonia separation of nitrogen again, uses H
2With CO
2Hydrogenation reaction system CH
4
Adorn in being reflected at of described generation methane in the water-cooled heat exchange type fixed-bed reactor of Ni-based methanation catalyst and carry out.
The water-cooled that is reflected at of described generation methane is carried out in tubular reactor.
Present technique and existing be that raw material makes synthetic gas H with Lurgi furnace gasization or coal water slurry gasification with coal
2, CO, CO
2, adopt Lurgi or DAVY or
Etc. the artificial Sweet natural gas of external adiabatic high-temperature methanation system significant advantage is arranged relatively:
1. present technique is without the gas maked coal synthesizing methane, and utilizes industrial gaseous waste, saved national resources;
2. utilize industrial gaseous waste, particularly utilize CO
2Synthetic natural gas reduces CO
2Discharging, the protection environment;
3. with the methanation of water-cooled heat exchange low temperature, optimize the methanation reaction condition, improved the methane synthetic ratio, available separate unit methanator replaces the high-temperature heat insulation methanation needs 3-4 platform methanator and intermediate heat, simplifies flow process, minimizing equipment, the cancellation circulator reduces power consumption;
4. utilize methane synthesising reacting heat by-product high-pressure steam, be used for steam turbines and water pump power that the drive compression Sweet natural gas need be used, energy-saving and cost-reducing.
Description of drawings
Fig. 1 is the high-temperature methanation process flow sheet of rope company of Denmark Top.
Fig. 2 is the process flow diagram of the utility model device when using a kind of industrial gaseous waste as raw material, for example Methanol Plant off-gas.
Fig. 3 is the process flow diagram of the utility model device device when using multiple industrial gaseous waste as raw material, for example ammonia factory decarburization stripping gas CO
2Contain H with ammonia synthesis
2Off-gas.
Fig. 4 is the utility model schematic representation of apparatus.
Fig. 5 is the synoptic diagram of the water-cooled of the methanator employing in the utility model device around tubular reactor.
Embodiment
Be described in detail of the present utility model below in conjunction with drawings and Examples.
Embodiment 1
Adopt technical process as shown in Figure 3, (synthesis ammonia plant contains H by plant gas 1
2, N
2Off-gas) purify to remove ammonia, be equipped with the plant gas 2 (decarburization stripping gas) after the purification, total tolerance 1000Kmol/h is being equipped with the vertical around the pipe water-cooled reactor, at air speed 3000h of the Ni-based TiO of having carrier methanation catalyst under the pressure 2MPa
-1Under carry out CO
2The hydrogenation methanation reaction must contain CH behind cooling de-watering
4About 50%, N
240% product gas 4959Kmol/h gets CH through the transformation fractionation by adsorption
488% product gas recompresses 25MPa, gets the 2580Kmol/h compressed natural gas used as vehicle fuel.
Embodiment 2
The utility model device as shown in Figure 4, comprise drum 101, water pump 102, methanation synthesis reactor 103, interchanger 104 before the tower, well heater 105 goes into operation, water cooler 106, water separator 107, methane concentration unit 108, compressor 1010 and steam turbines 109, described methanation synthesis reactor 103, interchanger 104 before the tower, water cooler 106, water separator 107, methane concentration unit 108, compressor 1010 is connected successively with steam turbines 109, described methanator 103 also is circumscribed with drum 101, the water pump 102 and the well heater 105 that goes into operation, described drum 101 also is connected with steam turbines 109.
The described well heater 105 that goes into operation can be selected steam injector for use, or selects the electric heater on the inlet line that is installed between preceding interchanger 104 of tower and the methanation synthesis reactor 103 for use.
Interchanger 104 and the synthetic gas heat exchange that goes out methanation synthesis reactor 103 before the advanced tower of industrial gaseous waste after the purification, advance methanation synthesis reactor 103 again and carry out methanation reaction, the synthetic gas that goes out methanation synthesis reactor 103 is isolated water of condensation through water cooler 106, water separator 107 after interchanger 104 coolings more successively before tower, send to methane concentration unit 108 and compressor 1010 and propose dense, compression and obtain artificial Sweet natural gas.The drum that is connected with methanation synthesis reactor 103 101 produces high pressure steam, sends to steam turbines 109 usefulness and is used as power or goes generator for electricity generation, also can be used for process steam.
Fig. 5 adopts water-cooled (Fig. 5 is other equipment in the display unit not as the methanation synthesis reactor around tubular reactor, all the other equipment are formed and are connected with embodiment 2) synoptic diagram, utility model patent (the application number 201210033806.1 that this water-cooled has been applied for for the applicant around tubular reactor, February 14 2012 applying date) a kind of reactor in, comprise housing 1 and heat exchanging piece, described housing 1 top is provided with inlet mouth 3 and manhole 4, inlet mouth 3 is furnished with gas distribution grid 81, and lower housing portion is provided with the header of a pair of band tube sheet: inlet header 9a and outlet header 9b.Internal and external cycle or connects by inverted U-shaped elbow with the top of adjacent two heat transfer tubes 2 in circle footpath, the up heat transfer tube of logical heat transferring medium and descending heat transfer tube layout in constituting, promptly up heat transfer tube is connected with inlet header 9a, descending heat transfer tube is connected with outlet header 9b.
Each layer heat transfer tube is by longitudinal register plate 19 location.Housing 1 inside center also is provided with around tubular axis core 7, up heat transfer tube that same return bend connects and descending heat transfer tube are along arranging by counter clockwise direction or clockwise direction helically separately respectively around tubular axis core 7, at the bottom of tubular axis core 7 bottoms are bearing in by supporting member 23 tin, around the top of tubular axis core 7 retractable.The up heat transfer tube that same return bend connects is opposite with the winding direction of descending heat transfer tube.Housing bottom is provided with air outlet 5 and catalyzer unloads outlet 6, and air outlet 5 is furnished with porous gas collection plate 82.Heat transferring medium adopts water.
When above-mentioned heat transfer reactor used, catalyst loading was between pipe, and outlet header 9b is by vapour outlet pipe coupling drum, and drum connects recycle pump by rising pipe, and recycle pump also connects additional water pipe, and inlet header 9a connects recycle pump by the heat transferring medium circulation tube.Reaction gas enters from inlet mouth 3, heat transferring medium enters into each heat transfer tube 2 from inlet header 9a, up along up heat transfer tube with volution, change descending heat transfer tube over to through return bend again, descending with the volution direction opposite with up direction, with the reaction gas heat exchange of axially passing catalyst layer, the part water vapor is a steam in the pipe during this time, removes drum with variable valve through outlet header 9b.
Above-mentioned water-cooled is walked coolant water in tubular type methanation reaction organ pipe, for example can adopt the tubule of 12mm diameter directly to manage, and significantly improves heat interchanging area, up to every 1M
3Catalyzer 200M
2Up and down, around pipe synthetic tower gas with around pipe cross-flow heat exchange, than inside and outside the straight tube pipe and to flow the heat exchange heat transfer coefficient much higher, significantly improve heat exchange efficiency, effectively realize low temperature and samming methanation.
Embodiment 4
Produce 1000000 tons of Methanol Plant off-gas per year after methyl alcohol is removed in the washing recovery, off-gas 2000Kmol is under pressure 3MPa, and the water-cooled that nickel type methanation catalyst is housed is around the tubular type methanator, at air speed 5000h
-1Under carry out methanation reaction, behind refrigerated separation water 625.7Kmol contain CH
473.46% product gas, with pressure swing adsorption process separate CH
490% product gas recompresses 25MPa, gets the compressed natural gas used as vehicle fuel CNG of 5200Kmol/h.
Claims (3)
1. device that is used to utilize the artificial Sweet natural gas of plant gas system, comprise drum, boiler water pump, the methanation synthesis reactor, interchanger before the tower, well heater goes into operation, water cooler, water separator, the methane concentration unit, compressor and steam turbines, it is characterized in that: described methanation synthesis reactor, interchanger before the tower, well heater goes into operation, water cooler, water separator, the methane concentration unit, compressor is connected successively with steam turbines, described methanator also is circumscribed with drum, the water pump and the well heater that goes into operation, described drum also is connected with steam turbines.
2. the device that is used to utilize the artificial Sweet natural gas of plant gas system as claimed in claim 1 is characterized in that: described methanation synthesis reactor is that horizontal water-cooled heat exchange type fixed-bed reactor or water-cooled are around tubular reactor.
3. the device that is used to utilize the artificial Sweet natural gas of plant gas system as claimed in claim 1 is characterized in that: the described well heater that goes into operation is steam injector or electric heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320022697 CN203096014U (en) | 2013-01-06 | 2013-01-06 | Device for producing natural gas from factory waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320022697 CN203096014U (en) | 2013-01-06 | 2013-01-06 | Device for producing natural gas from factory waste gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203096014U true CN203096014U (en) | 2013-07-31 |
Family
ID=48847432
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201320022697 Expired - Lifetime CN203096014U (en) | 2013-01-06 | 2013-01-06 | Device for producing natural gas from factory waste gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203096014U (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103911196A (en) * | 2013-01-06 | 2014-07-09 | 杭州林达化工技术工程有限公司 | Method and apparatus for utilizing plant waste gas to prepare natural gas |
| CN104557390A (en) * | 2015-02-12 | 2015-04-29 | 鹤壁宝发能源科技股份有限公司 | Method for coproducing and synthesizing liquid methane from methanol purge gas |
| CN106015064A (en) * | 2016-06-06 | 2016-10-12 | 贵州赤天化股份有限公司 | Structure and operation method for driving compressor with motors instead of steam |
| EP3199231A4 (en) * | 2014-09-24 | 2018-08-01 | Ren Lou | Large reactor and device and process thereof |
| CN113499596A (en) * | 2021-08-16 | 2021-10-15 | 华峰集团上海工程有限公司 | Esterification device and method for AA and BDO in PBAT production process |
| CN113522198A (en) * | 2021-08-16 | 2021-10-22 | 华峰集团上海工程有限公司 | Esterification device and method for PTA and BDO in PBAT production process |
| CN113877225A (en) * | 2021-08-16 | 2022-01-04 | 华峰集团上海工程有限公司 | Full-mixing esterification device and method in PBAT production process |
| CN114031761A (en) * | 2021-10-14 | 2022-02-11 | 华峰集团上海工程有限公司 | PPC synthesis system and synthesis process thereof |
-
2013
- 2013-01-06 CN CN 201320022697 patent/CN203096014U/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103911196A (en) * | 2013-01-06 | 2014-07-09 | 杭州林达化工技术工程有限公司 | Method and apparatus for utilizing plant waste gas to prepare natural gas |
| EP3199231A4 (en) * | 2014-09-24 | 2018-08-01 | Ren Lou | Large reactor and device and process thereof |
| CN104557390A (en) * | 2015-02-12 | 2015-04-29 | 鹤壁宝发能源科技股份有限公司 | Method for coproducing and synthesizing liquid methane from methanol purge gas |
| CN106015064A (en) * | 2016-06-06 | 2016-10-12 | 贵州赤天化股份有限公司 | Structure and operation method for driving compressor with motors instead of steam |
| CN106015064B (en) * | 2016-06-06 | 2019-04-26 | 贵州赤天化股份有限公司 | The operating method of motor-driven compressor substitution steam driven compressor |
| CN113499596A (en) * | 2021-08-16 | 2021-10-15 | 华峰集团上海工程有限公司 | Esterification device and method for AA and BDO in PBAT production process |
| CN113522198A (en) * | 2021-08-16 | 2021-10-22 | 华峰集团上海工程有限公司 | Esterification device and method for PTA and BDO in PBAT production process |
| CN113877225A (en) * | 2021-08-16 | 2022-01-04 | 华峰集团上海工程有限公司 | Full-mixing esterification device and method in PBAT production process |
| CN114031761A (en) * | 2021-10-14 | 2022-02-11 | 华峰集团上海工程有限公司 | PPC synthesis system and synthesis process thereof |
| CN114031761B (en) * | 2021-10-14 | 2023-09-08 | 华峰集团上海工程有限公司 | PPC synthesis system and synthesis process thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130731 |