CN104058368B - A kind of hydrocarbonaceous tail gas reforming process and system - Google Patents
A kind of hydrocarbonaceous tail gas reforming process and system Download PDFInfo
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- CN104058368B CN104058368B CN201410254785.5A CN201410254785A CN104058368B CN 104058368 B CN104058368 B CN 104058368B CN 201410254785 A CN201410254785 A CN 201410254785A CN 104058368 B CN104058368 B CN 104058368B
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- 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
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- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The present invention relates to a kind of hydrocarbonaceous tail gas reforming process and system, solve existing hydrocarbonaceous tail gas reforming process exist facility investment high, running cost is high, the problem of system complex.Reclaimed out the heat energy of the hot process gases of converter by useless pot and multiple interchanger in present invention process, saturation steam is pressed for preheating material gas and oiler feed in by-product, can be good at the heat energy in recovery system, save the consumption of process furnace and burning gas, there is the advantage that technique is simple, control easy, efficient recovery system heat energy, reduce energy consumption, save facility investment.
Description
Technical field
The present invention relates to a kind of process for making hydrogen and system, specifically a kind of hydrocarbonaceous tail gas reforming process and system.
Background technology
In modern large-size chemical field, as Sweet natural gas acetylene, fixed bed crushed coal pressure gasifying, all can produce a large amount of containing CH in the flow processs such as gasification synthetic oil and coke-oven gas
4in the tail gas of hydro carbons, process and fully utilize containing CH
4tail gas Deng hydro carbons prepares hydrogen, not only achieves the process of waste gas, increases production all significant for environment protection and device.
The explained hereafter method being abroad raw material hydrogen manufacturing with hydro carbons (Sweet natural gas etc.), mainly contain Autothermal reforming method, with techniques such as the partial oxidation processs being raw material with oil, heavy oil, utilize the hydrogen-rich gases such as ammonia factory off-gas, methanation tail gas, methanol-fueled exhaust, catalytic reforming tail gas to carry out the methods such as pressure-variable adsorption, low temperature process or film permeation in addition and refine the hydrogen obtaining certain purity.In numerous process for making hydrogen routes, on industries, occupy larger advantage with the Steam Reforming Process that hydro carbons (Sweet natural gas) is raw material.
Generally in Methane Conversion, need to arrange independent process furnace and carry out preheating and overheated to by-product saturation steam to raw material tail gas, saturation steam etc., process furnace is heated by fuel gas.In patent ZL200910195146.5, methanol synthesis loop periodic off-gases needs before entering converter to carry out preheating by process furnace, process furnace have employed self-priming two sections of radiation, take first with the design of convection zone, rear radiation section, by tail gas, tail gas+steam heating to required temperature, the setting of process furnace, make device complicated, operation easier strengthens, investment raises, and too increases fuel gas consumption and running cost, reduces the comprehensive utilization ratio of energy.
Summary of the invention
The object of the invention is to solve the problems of the technologies described above, the hydrocarbonaceous tail gas reforming process that a kind of technique is simple, control easy, efficient recovery system heat energy, reduce energy consumption, save facility investment is provided.
The present invention also provides a kind of system for above-mentioned technique.
Present invention process is delivered to after being sent in feed gas heater by unstripped gas and being preheated to 110-130 DEG C after heat exchanger continues to be heated to 550 ~ 650 DEG C again and is entered converter, go out reacted 950 ~ 1100 DEG C of hot process gases of converter to send into the conversion being connected with drum and give up in pot by-product and press saturation steam, process gas cooling sends into heat exchanger and unstripped gas heat exchange successively after being down to 600 ~ 700 DEG C after, deliver to again after reforming gas water cooler and oiler feed heat exchange are cooled to 250 ~ 300 DEG C and send into shift converter, the change temperature degree going out shift converter is 220 ~ 250 DEG C, CO concentration is down to volume percent less than 0.8%, described conversion gas is after feedwater preheater and feedwater heat exchange are lowered the temperature, 160 ~ 190 DEG C are cooled to again through feed gas heater and the further heat exchange of unstripped gas, then 60 DEG C are cooled to through air cooler successively, enter 1# gas-liquid separator and carry out gas-liquid separation, the conversion gas that tank deck is drawn is cooled to 40 DEG C through water cooler and enters 2# gas-liquid separator and be separated further, the conversion pneumatic transmission that tank deck is drawn is carried hydrogen system and is done further process, obtain high-purity hydrogen, described oiler feed is sent into reforming gas water cooler again and is preheated to 200 ~ 260 DEG C and sends into drum again after feedwater preheater and conversion gas heat exchange.
Described drawn by drum in press saturation steam to be divided into three strands, first strand to send vapor superheater to carry out overheated, and send into oxygen preheat device as heating steam for second strand and be used for the pure oxygen that preheating enters converter, the 3rd strand is mixed in described pure oxygen as safe steam.
Described shift converter is two-part shift converter, and the temperature of one section outlet reaches 370 DEG C ~ 410 DEG C conversion gas, and in vapor superheater is to first strand, press saturation steam to carry out overheated, then after demineralized-water preheater is cooled to 200 ~ 220 DEG C, deliver to shift converter two sections.
Press through hot steam in pressing saturation steam to be formed after vapor superheater is overheated in first strand, be divided into two parts, a part send out-of-bounds middle pressure steam pipe network, and another part to mix with unstripped gas as process steam to be delivered to converter and participate in reacting after heat exchanger preheating.
When going into operation, the unstripped gas going out feed gas heater is first sent into after the process furnace that goes into operation is heated to 550 ~ 650 DEG C and is sent into converter.
Hydrocarbonaceous tail gas reforming hydrogen manufacturing system of the present invention, comprise converter, the outlet of described converter is successively through giving up pot, heat exchanger, reforming gas water cooler, shift converter, feedwater preheater, feed gas heater, air cooler, 1# gas-liquid separator, water cooler, 2# gas-liquid separator and carry hydrogen system and be connected with the conversion of drum, the unstripped gas entrance of described converter to export with the unstripped gas of feed gas heater through heat exchanger and is connected; The water inlet of described drum is connected with the water inlet of feedwater preheater through reforming gas water cooler.
The oxygen intake of described converter is connected with the oxygen outlet of oxygen preheat device; The vapour outlet of described drum is communicated with the steam-in of vapor superheater, the steam-in of oxygen preheat device and the oxygen intake of converter respectively.
Described shift converter is two-part shift converter, and one section outlet is connected with two sections of entrances through vapor superheater, demineralized-water preheater;
The vapour outlet of described vapor superheater shell-side is communicated with the unstripped gas entrance of heat exchanger shell-side and middle pressure steam pipe network out-of-bounds respectively.
The unstripped gas outlet of described feed gas heater is also connected with the unstripped gas entrance of converter through the process furnace that goes into operation.
Present invention process system comprises unstripped gas preheating, methane and the hydrocarbon conversion, CO conversion, recovery of heat, carries the processing step such as hydrogen, phlegma air lift, the unstripped gas being applicable to process as the tail gas produced in the flow processs such as Sweet natural gas acetylene, fixed bed crushed coal pressure gasifying, gasification synthetic oil and coke-oven gas, as containing CH
4: the gas of 10 ~ 60mol% and other hydro carbons.
Native system be with containing methane and other hydro carbons tail gas for raw material, take pure oxygen as the catalyzed conversion of oxygenant, the high purity H required for production equipment
2.This device goes out methane content in the reforming gas of battery limit (BL) and reaches below 0.6mol%, and the CO volume content after conversion gas is down to below 0.8mol%, the H after proposing hydrogen system process
2content can reach 99.5mol%, meets device to high purity H
2requirement.
The high temperature that the present invention produces after adopting methane conversion carrys out preheating material gas, the hot process gases utilizing converter to export reclaims heat through transforming useless pot and presses saturation steam in generation, process steam, preheated oxygen etc. is used as with the steam of by-product, simultaneously after gas temperature is reduced to 600 ~ 700 DEG C, be used for preheating material gas again, thus put forward high-octane comprehensive utilization ratio.Compared to using process furnace to carry out preheating gas in the past, the advantage adopt the self-produced heat energy recovery of native system to have more and save facility investment, reducing energy consumption.
Native system arranges the process furnace bypass that goes into operation, for preheating material gas under initial start-up operating mode, ensure that reaction is normally carried out, drive successfully, closedown goes into operation process furnace and relevant pipeline, is utilized transform the thermal source produced and heat the unstripped gas sending converter to by heat exchanger.
Shift converter one section outlet, in vapor superheater is drawn drum, saturation steam is pressed to carry out overheated, cooled conversion gas is delivering to shift converter two sections again after demineralized-water preheater cooling, both effectively make use of one section reaction heat centering pressure saturation steam carry out overheated, also make one section of conversion gas effective temperature-reducing out, kill two birds with one stone.
Described unstripped gas can be the tail gas as produced in the flow processs such as Sweet natural gas acetylene, fixed bed crushed coal pressure gasifying, gasification synthetic oil and coke-oven gas, as contained CH
4: the gas of 10 ~ 60mol% and other hydro carbons.
Tool of the present invention has the following advantages and beneficial effect:
1) present system does not establish process furnace, saves the investment of the aspects such as apparatus body, instrument and interlocked control;
2) present invention process system operation is more easy, is easy to control, and has wide range of applications, can be used for the methane-rich gas reforming hydrogen manufacturing processes such as synthetic ammonia, methanol-fueled CLC and coal liquifaction device;
3) converter outlet hot process gases is used for preheating material gas, byproduct steam etc., achieves the comprehensive utilization of energy, energy-saving and cost-reducing; And the steam of by-product is also partly as the reuse such as process steam, safe steam;
4) native system only arranges the process furnace that goes into operation, without the need to consume fuel gas during normal operation, although byproduct steam slightly reduces, because fuel gas cost is far above steam cost compared with band process furnace flow process, device long-time running, cost-saved, economic profit is considerable.
5) for 1,200,000 tons/year of coal liquifaction device for producing hydrogen, the technical process of employing native system can reduce process furnace and relevant device investment reaches 4000 ~ 5,000 ten thousand Renminbi, reduce fuel gas simultaneously and consume about 4700Nm3/h (2300kJ/kmol), consuming minimizing amounts to Renminbi ~ 7,000,000 every year compared with process furnace flow process.
Accompanying drawing explanation
Fig. 1 is present invention process schema and system diagram.
In figure, (1) stripping tower, (2) oxygen preheat device, (3) converter, (4) useless pot is transformed, (5) drum, (6) go into operation process furnace, (7) heat exchanger, (8) reforming gas water cooler, (9) shift converter, (9.1) one sections, (9.2) two sections, (10) vapor superheater, (11) demineralized-water preheater, (12) feedwater preheater, (13) feed gas heater, (14) air cooler, (15) 1# gas-liquid separator, (16) water cooler, (17) 2# gas-liquid separator, (18) condensate pump, (19) hydrogen system is carried, (20) phlegma preheater.
Embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail:
System embodiment:
The give up pipe side of pot 4, the pipe side of heat exchanger 7, the pipe side of reforming gas water cooler 8 of the conversion of outlet successively through being connected with drum 5 of described converter 3 is connected with one section of 9.1 entrance of shift converter 9, one section of 9.1 outlet of described shift converter 9 successively through the pipe side of vapor superheater 10, the pipe side of demineralized-water preheater 11 is connected with two section of 9.2 entrance of shift converter 9.Two section 9.2 of described shift converter 9 outlet is successively through the pipe side of the pipe side of feedwater preheater, feed gas heater, air cooler, 1# gas-liquid separator, water cooler, 2# gas-liquid separator and carry hydrogen system and be connected, and the unstripped gas entrance of described converter 3 to export with the unstripped gas of feed gas heater 13 shell-side through the shell-side of heat exchanger 7 and is connected; The oxygen intake of described converter 3 is connected with the oxygen outlet of oxygen preheat device 2 shell-side.
The vapour outlet of described drum 5 is connected with the steam-in of described vapor superheater 10 shell-side respectively, the steam-in of oxygen preheat device 2 pipe side and the oxygen intake of converter 3 are communicated with.The water inlet of described drum 5 is connected with the water inlet of feedwater preheater 12 shell-side through the shell-side of reforming gas water cooler 8.The vapour outlet of described vapor superheater 10 shell-side is communicated with the unstripped gas entrance of heat exchanger 7 shell-side and middle pressure steam pipe network out-of-bounds respectively.The unstripped gas outlet of described feed gas heater 13 shell-side is also connected with the unstripped gas entrance of converter 3 through the process furnace 6 that goes into operation.
The described conversion pot 4 that gives up can adopt fixed tube sheet type, and high temperature side is designed to pipe side, Thermal protection need be carried out in pipe side, and shell-side medium is oiler feed.
Heat exchanger 7 can select U-tube heat exchanger structure pattern, can solve the stress problem of the thermal expansion produced between the heat transfer tube of high temperature in heat exchange equipment and housing preferably, make equipment de-sign safe and reliable.
Technical process is described as follows.
The unstripped gas established technology device exhaust (SG, 5.0 ~ 5.5MPaG, 40 ~ 70 DEG C) that battery limit (BL) comes, CH
4content is 10 ~ 60mol%, other hydro carbons < 10mol%, mix with a part of superheated vapour (5.2 ~ 5.6MPaG, 340 DEG C ~ 360 DEG C) from vapor superheater 10 after feed gas heater 13 is preheated to 110 ~ 130 DEG C, the gas mixture of tail gas+steam is sent to heat exchanger 7 and is heated to 550 ~ 650 DEG C by the hot process gases from converter 3, then delivers to the unstripped gas entrance of converter 3.
From the pure oxygen (O of air separation facility
26.0 ~ 6.5MPaG, 10 DEG C ~ normal temperature) through oxygen preheat device 2 with press saturation steam heat exchange from drum 5, pure oxygen is preheating to 180 ~ 240 DEG C, then fill in the pure oxygen after preheating and press saturation steam from drum 5 as in safe steam equally on a small quantity, oxygen intake through converter 3 is sent into converter and tail gas and is reacted and produce heat of high temperature, by Autothermal reforming and under catalyst action, reaction generates H
2, the hot process gases (950 ~ 1100 DEG C) such as CO.Converter 3 pure oxygen burner can adopt circulating water.
The hot process gases going out converter is introduced into the pipe side transforming useless pot 4 and reclaims heat, utilize in drum 4 by-product and press saturation steam (5.2 ~ 5.6MPaG, 267 ~ 272 DEG C), the process gas temperature going out to transform useless pot 4 is down to 600 ~ 700 DEG C by 950 ~ 1100 DEG C, after be cooled to 295 DEG C ~ 345 DEG C through the pipe side of over-heat-exchanger 7 and the tail gas heat exchange of shell-side successively, 250 ~ 300 DEG C are cooled to heat exchange again, through the process gas (CH of recovery of heat through the pipe side of reforming gas water cooler 8 and shell-side boiler
4be down to 0.3% volume percent) send into shift converter 9 one sections, the conversion gas temperature of shift converter one section of 9.1 outlet reaches 370 DEG C ~ 410 DEG C, one section of conversion gas is overheated to pressing saturation steam to carry out in the part from drum 5 through the pipe side of vapor superheater 10, steam (MS) part after overheated mixes as the tail gas of process steam with the unstripped gas entrance sending into heat exchanger 7 shell-side, and another part delivers to middle pressure steam pipe network out-of-bounds.After demineralized-water preheater 11 further cooling, shift converter 9 two sections is delivered to again through the cooled one section of conversion gas of vapor superheater 10 heat exchange.
Shift converter 9 second stage exit conversion gas temperature 220 ~ 250 DEG C, CO concentration is down to volume percent less than 0.8%, go out the conversion gas of shift converter 9 two sections, heat is reclaimed through the pipe side of feedwater preheater 12 and the oiler feed heat exchange of shell-side, 160 ~ 190 DEG C are cooled to further again through the pipe side of feed gas heater 13 and the tail gas heat exchange of shell-side, after be cooled to 60 DEG C through air cooler 14 successively, enter 1# gas-liquid separator 15 and carry out gas-liquid separation, tank deck conversion gas is cooled to 40 DEG C through water cooler 16, enter 2# gas-liquid separator 17 gas-liquid separation further, the conversion gas of tank deck is sent and is carried hydrogen system 19 and do further process, high-purity hydrogen (the H of more than final production 99.5mol%
2).At the bottom of 1# gas-liquid separator 15 and 2# gas-liquid separator 17 tank, isolated process condensate send pump 18 to deliver to gas stripping column 1 after process condensate preheater 20 preheating by phlegma, and the process condensate (PC) after stripping process delivers to out-of-bounds water treatment device.Heat up through the shell-side of feedwater preheater 12 and the conversion gas heat exchange of pipe side successively from oiler feed (BFW) out-of-bounds, drum 5 is delivered to press saturation steam (5.2 ~ 5.6MPaG in by-product again after the shell-side of reforming gas water cooler 8 and the reforming gas heat exchange of pipe side are preheated to 200 ~ 260 DEG C, 267 ~ 272 DEG C), the middle pressure saturation steam of by-product respectively as, preheated oxygen, and the safe steam supplemented in oxygen pipeline, it is overheated that remaining steam send vapor superheater 10 to carry out, a steam part after overheated is used as production labor skill steam, residue superheated vapour delivers to battery limit (BL) outside ductwork.
The process furnace 6 that goes into operation arranged heats the gas mixture of tail gas+steam without under thermal load conditions for initial start-up stage heat exchanger 7, namely the unstripped gas entrance of converter 3 is delivered to after the gas mixture of initial start-up stage tail gas+steam is heated to 550 ~ 650 DEG C by the process furnace that goes into operation, drive successfully, closedown goes into operation process furnace 6 and relevant pipeline, is utilized transform the thermal source produced and heat the tail gas delivering to converter 3 by heat exchanger 7.
Native system goes out methane content in the reforming gas of converter and reaches below 0.6mol%, and the CO volume content after conversion gas is down to below 0.8mol%, the H after proposing hydrogen system process
2content can reach 99.5mol%, meets device to high purity H
2requirement.
Claims (10)
1. a hydrocarbonaceous tail gas reforming process, it is characterized in that, unstripped gas is sent in feed gas heater to deliver to again after heat exchanger continues to be heated to 550 ~ 650 DEG C after being preheated to 110 ~ 130 DEG C and enter converter, go out reacted 950 ~ 1100 DEG C of hot process gases of converter to send into the conversion being connected with drum and give up in pot by-product and press saturation steam, process gas cooling sends into heat exchanger and unstripped gas heat exchange successively after being down to 600 ~ 700 DEG C after, deliver to again after reforming gas water cooler and oiler feed heat exchange are cooled to 250 ~ 300 DEG C and send into shift converter, the change temperature degree going out shift converter is 220 ~ 250 DEG C, CO concentration is down to volume percent less than 0.8%, described conversion gas is after feedwater preheater and feedwater heat exchange are lowered the temperature, 160 ~ 190 DEG C are cooled to again through feed gas heater and the further heat exchange of unstripped gas, then 60 DEG C are cooled to through air cooler successively, enter 1# gas-liquid separator and carry out gas-liquid separation, the conversion gas that tank deck is drawn is cooled to 40 DEG C through water cooler and enters 2# gas-liquid separator and be separated further, the conversion pneumatic transmission that tank deck is drawn is carried hydrogen system and is for further processing, obtain high-purity hydrogen, described oiler feed is sent into reforming gas water cooler again and is preheated to 200 ~ 260 DEG C and sends into drum again after feedwater preheater and conversion gas heat exchange.
2. hydrocarbonaceous tail gas reforming process as claimed in claim 1, it is characterized in that, the middle pressure saturation steam transforming useless pot by-product is divided into three strands, first strand to send vapor superheater to carry out overheated, send into oxygen preheat device as heating steam for second strand and be used for the pure oxygen that preheating enters converter, the 3rd strand is mixed in described pure oxygen as safe steam.
3. hydrocarbonaceous tail gas reforming process as claimed in claim 2, it is characterized in that, described shift converter is two-part shift converter, the temperature of one section outlet reaches 370 DEG C ~ 410 DEG C conversion gas, and in vapor superheater is to first strand, press saturation steam to carry out overheated, then after demineralized-water preheater is cooled to 200 ~ 220 DEG C, deliver to shift converter two sections.
4. hydrocarbonaceous tail gas reforming process as claimed in claim 3, it is characterized in that, hot steam is pressed through in pressing saturation steam to be formed after vapor superheater is overheated in first strand, be divided into two parts, a part send out-of-bounds middle pressure steam pipe network, and another part to mix with unstripped gas as process steam to be delivered to converter and participate in reacting after heat exchanger preheating.
5. the hydrocarbonaceous tail gas reforming process as described in any one of claims 1-4, is characterized in that, when going into operation, the unstripped gas going out feed gas heater is first sent into after the process furnace that goes into operation is heated to 550 ~ 650 DEG C and sent into converter.
6. a hydrocarbonaceous tail gas reforming hydrogen manufacturing system, it is characterized in that, comprise converter, the outlet of described converter is successively through giving up pot, heat exchanger, reforming gas water cooler, shift converter, feedwater preheater, feed gas heater, air cooler, 1# gas-liquid separator, water cooler, 2# gas-liquid separator and carry hydrogen system and be connected with the conversion of drum, the unstripped gas entrance of described converter to export with the unstripped gas of feed gas heater through heat exchanger and is connected; The water inlet of described drum is connected with the water outlet of feedwater preheater through reforming gas water cooler.
7. hydrocarbonaceous tail gas reforming hydrogen manufacturing system as claimed in claim 6, it is characterized in that, the oxygen intake of described converter is connected with the oxygen outlet of oxygen preheat device; The vapour outlet of described drum is communicated with the steam-in of vapor superheater, the steam-in of oxygen preheat device and the oxygen intake of converter respectively.
8. hydrocarbonaceous tail gas reforming hydrogen manufacturing system as claimed in claim 7, it is characterized in that, described shift converter is two-part shift converter, and one section outlet is connected with two sections of entrances through vapor superheater, demineralized-water preheater.
9. hydrocarbonaceous tail gas reforming hydrogen manufacturing system as claimed in claim 8, is characterized in that, the vapour outlet of described vapor superheater shell-side respectively with the unstripped gas entrance of heat exchanger shell-side and out-of-bounds middle pressure steam pipe network be communicated with.
10. the hydrocarbonaceous tail gas reforming hydrogen manufacturing system as described in any one of claim 6-9, is characterized in that, the unstripped gas outlet of described feed gas heater is also connected with the unstripped gas entrance of converter through the process furnace that goes into operation.
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| CN108275653A (en) * | 2018-03-22 | 2018-07-13 | 上海华林工业气体有限公司 | A kind of steam reformer flue gas heat recycling system and method |
| CN113620241A (en) * | 2021-08-20 | 2021-11-09 | 四川恒重清洁能源成套装备制造有限公司 | Natural gas hydrogen production system and process thereof |
| CN115465836B (en) * | 2022-09-05 | 2023-07-25 | 福建永荣科技有限公司 | Hydrogen production process from methanol |
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| JP3771357B2 (en) * | 1997-06-09 | 2006-04-26 | 千代田化工建設株式会社 | Hydrogen production method |
| JP2007063066A (en) * | 2005-08-31 | 2007-03-15 | Toshiba Corp | Method and equipment for producing hydrogen |
| RU2385836C2 (en) * | 2008-04-07 | 2010-04-10 | Открытое акционерное общество "Научно-исследовательский институт вычислительной техники" (ОАО "НИИВТ") | Method of developing hydrogen energy chemical complex and device for its realisation |
| CN103781724A (en) * | 2011-09-06 | 2014-05-07 | Posco公司 | Apparatus for producing a synthetic gas including carbon monoxide and hydrogen, and method therefor |
| CN203998947U (en) * | 2014-06-10 | 2014-12-10 | 中国五环工程有限公司 | A kind of hydrocarbonaceous tail gas reforming hydrogen manufacturing system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3771357B2 (en) * | 1997-06-09 | 2006-04-26 | 千代田化工建設株式会社 | Hydrogen production method |
| JP2007063066A (en) * | 2005-08-31 | 2007-03-15 | Toshiba Corp | Method and equipment for producing hydrogen |
| RU2385836C2 (en) * | 2008-04-07 | 2010-04-10 | Открытое акционерное общество "Научно-исследовательский институт вычислительной техники" (ОАО "НИИВТ") | Method of developing hydrogen energy chemical complex and device for its realisation |
| CN103781724A (en) * | 2011-09-06 | 2014-05-07 | Posco公司 | Apparatus for producing a synthetic gas including carbon monoxide and hydrogen, and method therefor |
| CN203998947U (en) * | 2014-06-10 | 2014-12-10 | 中国五环工程有限公司 | A kind of hydrocarbonaceous tail gas reforming hydrogen manufacturing system |
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