CN108439337A - A kind of method of natural gas reforming hydrogen manufacturing - Google Patents
A kind of method of natural gas reforming hydrogen manufacturing Download PDFInfo
- Publication number
- CN108439337A CN108439337A CN201810216767.6A CN201810216767A CN108439337A CN 108439337 A CN108439337 A CN 108439337A CN 201810216767 A CN201810216767 A CN 201810216767A CN 108439337 A CN108439337 A CN 108439337A
- Authority
- CN
- China
- Prior art keywords
- gas
- conversion
- steam
- reburner
- pressure
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/388—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the heat being generated by superheated steam
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The present invention relates to a kind of method of natural gas reforming hydrogen manufacturing, this method includes：Using natural gas as raw material, reburner is mixed into after pressurized desulfurization with water vapour, cracking under the effect of the catalyst is reformed, and generation contains CH4、H2、CO2, CO components conversion gas, after conversion gas recycling heat, directly purify to obtain hydrogen by PSA without CO shift conversion steps, pressure-swing absorption apparatus tail gas returns to reburner combustion chamber and provides heat for conversion reaction.The present invention saves conversion section, and the dosage of reasonable distribution unstripped gas saves conversion section equipment, do not need additional supplemental natural gas as fuel gas.
Description
Technical field
The present invention relates to natural gas steam reforming hydrogen preparation fields, and in particular to a kind of natural gas and steam are converted into hydrogen
Technique.
Background technology
Traditional natural gas hydrogen preparation technology is as shown in Figure 1, mixed with water vapour after pressurized desulfurization using natural gas as raw material
It closes and enters reburner, cracking under the effect of the catalyst is reformed, and is generated containing components such as methane, hydrogen, carbon dioxide, carbon monoxide
Conversion gas, conversion gas recycling heat after, transformed to convert carbon monoxide to hydrogen, conversion gas purifies to obtain by PSA again
Hydrogen.
There are the problem of：(1) pass through CO shift conversion steps, flow is complicated, increases conversion section equipment investment, transformation catalyst
Expense and operating cost；(2) gas water steam reformation hydrogen production need to absorb a large amount of heat, need to additionally consume natural gas as combustion
Material, hydrogen production process high energy consumption.
Invention content
Present inventor has been surprisingly found that, using natural gas as raw material, is mixed into conversion after pressurized desulfurization with water vapour
Stove, under the effect of the catalyst cracking are reformed, and the conversion gas containing components such as methane, hydrogen, carbon dioxide, carbon monoxide is generated,
After converting gas recycling heat, CO shift conversion steps are saved, directly purify to obtain hydrogen by PSA, PSA device exhausts return to conversion
Stove combustion chamber provides heat for conversion reaction, saves shift conversion step, and without additional consumption natural gas, PSA tail gas can provide combustion
Expect gas.
According to the present invention, a kind of method of natural gas reforming hydrogen manufacturing is provided, this method includes：Using natural gas as raw material, warp
It is mixed into reburner with water vapour after pressurization desulfurization, cracking under the effect of the catalyst is reformed, and generation contains CH4、H2、CO2、
The conversion gas of CO components after conversion gas recycles heat, is directly obtained by PSA (pressure-variable adsorption) purifications without CO shift conversion steps
Hydrogen, pressure-swing absorption apparatus tail gas return to reburner combustion chamber and provide heat for conversion reaction.
Further, in the conversion (cracking is reformed) process, steam/hydrocarbons ratio is 2.8~3.5, and conversion temperature degree is 680
~850 DEG C, transfer pressure 1.1-3.0MPa.
Further, in the conversion procedure, steam/hydrocarbons ratio is 3.0~3.2, and conversion temperature degree is 750~800 DEG C, is turned
Change pressure is 1.8-2.5MPa.
The middle reforming catalyst used of the application can be that commonly used in the art for the catalyst of conversion reaction, such as Ni
Base catalyst Z 108/Z108-1, Z418/Z419, C11-SL/C11-SSL etc..
The process conditions of PSA include：
Inlet temperature：30~40 DEG C
Inlet pressure：2.0±0.2MPa
Outlet pressure：2.0±0.2MPa
Adsorbent：Activated alumina, activated carbon, molecular sieve.
Pressurization desulfurization process preferably includes：After natural gas first passes around metering pressure regulation, preferably preheated by unstripped gas first
Device is warming up to 180-220 DEG C, preferably from about 200 DEG C, further through the second preheater pre-heating temperature elevation to 370-390 DEG C, and preferably from about 380
DEG C, into insulation hydrogen addition reactor, hydrogenation reaction occurs under the action of hydrogenation catalyst and generates inorganic sulfur, while alkene for organic sulfur
Hydrocarbon is saturated, and is then entered back into the chlorine in zinc oxide desulfurization reactor dechlorination section removing raw material, is finally entered zinc oxide desulfurization section,
Desulphurization reaction occurs in this.After desulfurization natural gas (370-390 DEG C of temperature, preferably from about 380 DEG C, pressure about 1.5-2.0MPa, preferably
About 1.8MPa) with steam superheated steam (about 430-470 DEG C of temperature, preferably from about 450 DEG C, the pressure about 1.5- of system production
2.0MPa, preferably 1.8MPa) it mixes, then inverted stove convection section is preheated to 550-600 DEG C, into reburner radiant section.Turning
Under the action of changing catalyst, complicated Steam Reforming reaction occurs, to produce hydrogen, methane, carbon monoxide, titanium dioxide
The equilibrium mixture of carbon and water.Conversion gas goes out about 780-810 DEG C of the temperature of reburner, further about 800 DEG C, into waste heat boiler
Tube side heat exchange after, generate high temperature and high pressure steam, after heat recovery, be cooled to 240-280 DEG C, for example, about 260 DEG C enter boiler
Feed water preheater is down to 150-170 DEG C, further about 160 DEG C.It is cooled to such as 35-50 DEG C, further about 40 DEG C of conversion gas
Using pressure-swing absorption apparatus purifying hydrogen of hydrogen, it is conversion of methane that the resolution gas of pressure-variable adsorption, which again returns to burning in reburner,
Heat is provided.
Desalted water outside device enters oxygen-eliminating device after the preheating of desalination water preheater.Steam needed for oxygen-eliminating device is by filling
Self-produced steam offer is provided.Deaerated water enters vapour after Medium pressure boiler feeding water pump boosts after feedwater preheater preheats
Packet.Boiler water by way of Natural Circulation respectively by reburner steam section, conversion gas steam generator generate high steam.
Generated steam is superheated to 430-470 DEG C in the convection section of reburner, further about 450 DEG C, and most of steam is as conversion
Reaction is used with vapour, is gone out after redundance desuperheat and is supplied original high steam pipe network outside device.
The convection section of reburner is waste heat recovery section, and radiant section flue gas enters pair after being come out from radiant section lower side
Flow section.In convection section, flue gas flows in the horizontal direction, and heat exchange coil is pre- by unstripped gas according to heating requirements and heat-transfer character
The sequences Rational Arrangements such as hot device, steam superheater, useless pot evaporator section, air preheater, so that flue gas heat obtains adequately
It recycles.Flue gas final temperature is down to 120-150 DEG C, further send chimney to be vented through air-introduced machine for about 140 DEG C.
Patent protection of the present invention is a kind of natural gas hydrogen preparation process/method, and main feature is to leave out conversion section, exceeds
Expect ground to find, advantage of this is that, the reasonable distributions dosage of unstripped gas (or making reduction material combusting), need not mend
Fuel gas is filled, (conversion section) equipment, catalyst costs and operation ten thousand yuan of about 300-400 of investment is saved, converts under hydrogen cost
About 5-10% drops.
Description of the drawings
Fig. 1 is prior art processes flow chart.
Fig. 2 is present invention process flow chart.
Specific implementation mode
The technique further illustrated the present invention below in conjunction with attached drawing.
Embodiment：
1. material gas quantity 10000Nm of embodiment3/ h, group prejudice raw material 1.After natural gas first passes around metering pressure regulation, pass through
The first preheater of unstripped gas be warming up to 200 DEG C, the second preheater pre-heating temperature elevation to about 380 DEG C, into insulation hydrogen addition reactor, hydrogen
The introduction volume of gas is 400Nm3/ h, organic sulfur occurs under the action of hydrogenation catalyst (cobalt-molybdenum series catalyst HT-211) plus hydrogen is anti-
Inorganic sulfur should be generated, while alkene is saturated, then enter back into the chlorine in zinc oxide desulfurization reactor dechlorination section removing raw material, finally
Into zinc oxide desulfurization section, desulphurization reaction occurs herein.Natural gas (about 380 DEG C of temperature, pressure about 1.8MPa) after desulfurization with
The superheated steam (about 450 DEG C of temperature, pressure about 1.8MPa) for system production of steaming mixes, then inverted stove convection section is preheated to
550-600 DEG C, into reburner radiant section.Under the action of reforming catalyst (C11-SL/C11-SSL), complicated water occurs
Steam reforming reaction, to produce hydrogen, methane, carbon monoxide, carbon dioxide and the equilibrium mixture of water.Gas is converted to go out to turn
About 800 DEG C of temperature for changing stove generates high temperature and high pressure steam, after heat recovery, is cooled into after the tube side heat exchange of waste heat boiler
About 260 DEG C are down to about 160 DEG C into feedwater preheater.It is cooled to about 40 DEG C of conversion gas, using pressure-swing absorption apparatus
Purifying hydrogen of hydrogen enters in adsorption tower the tower (while having two) for being in absorption working condition from bottom of tower, includes active oxidation wherein
Aluminium, activated carbon, molecular sieve a variety of adsorbents the absorption of selection successively under, the disposable nearly all impurity removed other than hydrogen,
The product hydrogen of purity 99.99% is obtained, it is conversion of methane that the resolution gas of pressure-variable adsorption, which again returns to burning in reburner,
Heat is provided.
Reburner condition：Steam/hydrocarbons ratio is 2.8, and conversion temperature degree is 680 DEG C, transfer pressure 1.1MPa.
| Component | CH4 (V%) | CO (V%) | CO2 (V%) | H2 (V%) | N2 (V%) |
| Convert gas 1 | 12.91 | 7.34 | 11.49 | 68.20 | 0.06 |
The present embodiment does not need converting means and carries out conversion process, and need not in addition supplement unstripped gas as fuel
Gas.
2. operating process of embodiment is the same as embodiment 1.Material gas quantity 10000Nm3/ h, group prejudice raw material 2.
Reburner condition：Steam/hydrocarbons ratio is 3.0, and conversion temperature degree is 720 DEG C, transfer pressure 2.0MPa.
| Component | CH4 (V%) | CO (V%) | CO2 (V%) | H2 (V%) | N2 (V%) |
| Convert gas 2 | 9.59 | 7.85 | 11.59 | 70.97 | 0 |
The present embodiment does not need converting means and carries out conversion process, and need not in addition supplement unstripped gas as fuel
Gas.
3. operating process of embodiment is the same as embodiment 1.Material gas quantity 10000Nm3/ h, group prejudice raw material 3.
Reburner condition：Steam/hydrocarbons ratio is 3, and conversion temperature degree is 750 DEG C, transfer pressure 2MPa.
| Component | CH4 (V%) | CO (V%) | CO2 (V%) | H2 (V%) | N2 (V%) |
| Convert gas 3 | 5.31 | 9.80 | 10.52 | 74.32 | 0.05 |
The present embodiment does not need converting means and carries out conversion process, and need not in addition supplement unstripped gas as fuel
Gas.
4. operating process of embodiment is the same as embodiment 1.Material gas quantity 10000Nm3/ h, group prejudice raw material 4.
Reburner condition：Steam/hydrocarbons ratio is 3.0, and conversion temperature degree is 800 DEG C, transfer pressure 2.5MPa.
| Component | CH4 (V%) | CO (V%) | CO2 (V%) | H2 (V%) | N2 (V%) |
| Convert gas 4 | 3.94 | 11.52 | 8.86 | 75.64 | 0.04 |
The present embodiment does not need converting means and carries out conversion process, and need not in addition supplement unstripped gas as fuel
Gas.
5. operating process of embodiment is the same as embodiment 1.Material gas quantity 10000Nm3/ h, group prejudice raw material 5.
Reburner condition：Steam/hydrocarbons ratio is 3.5, and conversion temperature degree is 850 DEG C, transfer pressure 3.0MPa.
| Component | CH4 (V%) | CO (V%) | CO2 (V%) | H2 (V%) | N2 (V%) |
| Convert gas 5 | 5.40 | 13.22 | 8.49 | 72.84 | 0.05 |
The present embodiment does not need converting means and carries out conversion process, and need not in addition supplement unstripped gas as fuel
Gas.
Comparative example 1：Material gas quantity 10000Nm3/h is formed with raw material 4.
Reburner condition：Steam/hydrocarbons ratio is 3.0, and conversion temperature degree is 800 DEG C, transfer pressure 2.5MPa.
| Component | CH4 (V%) | CO (V%) | CO2 (V%) | H2 (V%) | N2 (V%) |
| Conversion gas | 3.15 | 4.08 | 16.12 | 76.61 | 0.04 |
Comparative example 1 passes through conversion process, and requires supplementation with about 10% material gas quantity as fuel gas.
Claims (8)
1. a kind of method of natural gas reforming hydrogen manufacturing, this method include：Using natural gas as raw material, after pressurized desulfurization with water vapour
It is mixed into reburner, cracking under the effect of the catalyst is reformed, and generation contains CH4、H2、CO2, CO components conversion gas, conversion
After gas recycles heat, hydrogen is directly obtained by Pressure Swing Adsorption without CO shift conversion steps, pressure-swing absorption apparatus tail gas returns
It goes back to reburner combustion chamber and provides heat for conversion reaction.
2. according to the method described in claim 1, wherein, in the conversion procedure, steam/hydrocarbons ratio is 2.8~3.5, converts temperature
Degree is 680~850 DEG C, transfer pressure 1.1-3.0MPa.
3. according to the method described in claim 1, wherein, in the conversion procedure, steam/hydrocarbons ratio is 3.0~3.2, converts temperature
Degree is 750~800 DEG C, transfer pressure 1.8-2.5MPa.
4. according to the method described in claim 1, wherein, pressurization desulfurization process includes：After natural gas first passes around metering pressure regulation,
It is preferably from about 380 DEG C, anti-into insulation hydrogen addition by the first preheater of unstripped gas, the second preheater pre-heating temperature elevation to 370-390 DEG C
Device is answered, hydrogenation reaction occurs under the action of hydrogenation catalyst and generates inorganic sulfur for organic sulfur, while alkene is saturated, and is then entered back into
Zinc oxide desulfurization reactor dechlorination section removes the chlorine in raw material, finally enters zinc oxide desulfurization section, desulphurization reaction occurs herein.
5. according to the described method of any one of claim 1-4,370-390 DEG C of the natural gas temperature wherein after desulfurization, pressure
1.5-2.0MPa is mixed with 430-470 DEG C of the temperature for system production of steaming, pressure 1.5-2.0MPa superheated steams, then inverted stove
Convection section is preheated to 550-600 DEG C, and into reburner radiant section, under the action of reforming catalyst, complicated water vapour occurs
Conversion reaction, to produce hydrogen, methane, carbon monoxide, carbon dioxide and the equilibrium mixture of water.
6. according to the method described in claim 5, wherein, conversion gas goes out 780-810 DEG C of the temperature of reburner, into waste heat boiler
Tube side heat exchange after, generate high temperature and high pressure steam, after heat recovery, be cooled to 240-280 DEG C and enter feedwater preheater and drop
To 150-170 DEG C.35-50 DEG C of conversion gas is cooled to using pressure-swing absorption apparatus purifying hydrogen of hydrogen, the resolution gas of pressure-variable adsorption
It again returns to burning in reburner and provides heat for conversion of methane.
7. according to the method described in any one of claim 1-6, wherein the desalted water outside device is through desalination water preheater
Enter oxygen-eliminating device after preheating, the steam needed for oxygen-eliminating device is provided by device self-produced steam, and deaerated water passes through Medium pressure boiler feeding water pump
Enter drum after boosting after feedwater preheater preheats, boiler water passes through reburner respectively by way of Natural Circulation
Steam section, conversion gas steam generator generation high steam.Generated steam is superheated to 430-470 in the convection section of reburner
DEG C, most of steam is used as conversion reaction with vapour, is gone out after redundance desuperheat and is supplied original high steam pipe network outside device.
8. according to the described method of any one of claim 1-7, wherein the convection section of reburner is waste heat recovery section, radiation
Section flue gas enters convection section after being come out from radiant section lower side, and in convection section, flue gas flows in the horizontal direction, changes
Hot coil is suitable by feed gas heater, steam superheater, useless pot evaporator section, air preheater according to heating requirements and heat-transfer character
Sequence arranges, so that flue gas heat is adequately recycled, flue gas final temperature is down to 120-150 DEG C and is sent through air-introduced machine
Chimney is vented.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810216767.6A CN108439337A (en) | 2018-03-16 | 2018-03-16 | A kind of method of natural gas reforming hydrogen manufacturing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810216767.6A CN108439337A (en) | 2018-03-16 | 2018-03-16 | A kind of method of natural gas reforming hydrogen manufacturing |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108439337A true CN108439337A (en) | 2018-08-24 |
Family
ID=63194758
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810216767.6A Pending CN108439337A (en) | 2018-03-16 | 2018-03-16 | A kind of method of natural gas reforming hydrogen manufacturing |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108439337A (en) |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109225179A (en) * | 2018-10-19 | 2019-01-18 | 中南大学 | A kind of adsorption saturation organic compound containing chlorinated hydrocarbon discards regenerating active carbon and its waste gas treatment process |
| CN109467050A (en) * | 2018-12-29 | 2019-03-15 | 上海华林工业气体有限公司 | A kind of System and method for that HYCO hydrogen making by natural gas reformation is enhanced production capacities |
| CN109650335A (en) * | 2019-01-21 | 2019-04-19 | 武汉理工大学 | A kind of pressure varying adsorption of purified device for producing hydrogen and hydrogen production process |
| CN110407172A (en) * | 2019-08-20 | 2019-11-05 | 四川亚联高科技股份有限公司 | A kind of middle-size and small-size natural gas hydrogen production plant |
| CN110541690A (en) * | 2019-09-04 | 2019-12-06 | 中海石油气电集团有限责任公司 | method for improving recovery ratio by decarbonization of natural gas at gas field wellhead and CO2 reinjection |
| CN110950304A (en) * | 2019-12-16 | 2020-04-03 | 简阳绿杉新能源设备有限公司 | Method for preparing high-purity hydrogen by using natural gas |
| CN110980645A (en) * | 2019-12-27 | 2020-04-10 | 乔治洛德方法研究和开发液化空气有限公司 | Steam hydrocarbon reforming method |
| CN111288298A (en) * | 2020-03-09 | 2020-06-16 | 李明 | Method for recovering natural gas discharged by hydrogen production device through desulfurization, temperature rise and emptying |
| CN111777038A (en) * | 2020-07-02 | 2020-10-16 | 上海浩用工业炉有限公司 | Waste heat recovery system and method for hydrogen production converter |
| CN112142003A (en) * | 2019-06-27 | 2020-12-29 | 中石化南京化工研究院有限公司 | Carbon monoxide conversion process |
| CN112645283A (en) * | 2019-10-11 | 2021-04-13 | 中国石油化工股份有限公司 | System and method for producing hydrogen |
| CN112813454A (en) * | 2021-03-03 | 2021-05-18 | 中海石油气电集团有限责任公司 | Natural gas reforming and carbon dioxide combined hydrogen production power generation system and method |
| CN113213425A (en) * | 2021-06-08 | 2021-08-06 | 金川集团股份有限公司 | System and method for preparing hydrogen by using natural gas |
| WO2021223733A1 (en) * | 2020-05-07 | 2021-11-11 | 中国石油化工股份有限公司 | Natural gas steam reforming hydrogen production system and method therefor |
| CN114014270A (en) * | 2021-12-10 | 2022-02-08 | 四川天采科技有限责任公司 | Modularized natural gas reforming hydrogen production machine and hydrogen production method thereof |
| CN114436211A (en) * | 2021-12-30 | 2022-05-06 | 陕西聚能新创煤化科技有限公司 | Natural gas microwave catalytic conversion device and conversion method |
| CN114772551A (en) * | 2022-06-16 | 2022-07-22 | 浙江百能科技有限公司 | Method and system for efficiently utilizing methane-rich gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0262894A2 (en) * | 1986-10-01 | 1988-04-06 | The BOC Group, Inc. | For the co-production of carbon dioxide and hydrogen |
| CN101190781A (en) * | 2006-11-23 | 2008-06-04 | 上海标氢气体技术有限公司 | Minitype light hydrocarbon steam reforming hydrogen manufacturing technique |
| CN101391746A (en) * | 2007-09-17 | 2009-03-25 | 上海标氢气体技术有限公司 | Small-sized coal gasification hydrogen making method |
| CN102745647A (en) * | 2012-06-20 | 2012-10-24 | 青海宜化化工有限责任公司 | Process for producing hydrogen from natural gas by using calcium carbide tail gas |
-
2018
- 2018-03-16 CN CN201810216767.6A patent/CN108439337A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0262894A2 (en) * | 1986-10-01 | 1988-04-06 | The BOC Group, Inc. | For the co-production of carbon dioxide and hydrogen |
| CN101190781A (en) * | 2006-11-23 | 2008-06-04 | 上海标氢气体技术有限公司 | Minitype light hydrocarbon steam reforming hydrogen manufacturing technique |
| CN101391746A (en) * | 2007-09-17 | 2009-03-25 | 上海标氢气体技术有限公司 | Small-sized coal gasification hydrogen making method |
| CN102745647A (en) * | 2012-06-20 | 2012-10-24 | 青海宜化化工有限责任公司 | Process for producing hydrogen from natural gas by using calcium carbide tail gas |
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109225179A (en) * | 2018-10-19 | 2019-01-18 | 中南大学 | A kind of adsorption saturation organic compound containing chlorinated hydrocarbon discards regenerating active carbon and its waste gas treatment process |
| CN109225179B (en) * | 2018-10-19 | 2020-10-20 | 中南大学 | Regeneration and waste gas treatment process for adsorption saturated chlorinated hydrocarbon-containing organic compound waste activated carbon |
| CN109467050A (en) * | 2018-12-29 | 2019-03-15 | 上海华林工业气体有限公司 | A kind of System and method for that HYCO hydrogen making by natural gas reformation is enhanced production capacities |
| CN109650335A (en) * | 2019-01-21 | 2019-04-19 | 武汉理工大学 | A kind of pressure varying adsorption of purified device for producing hydrogen and hydrogen production process |
| CN112142003A (en) * | 2019-06-27 | 2020-12-29 | 中石化南京化工研究院有限公司 | Carbon monoxide conversion process |
| CN112142003B (en) * | 2019-06-27 | 2022-05-17 | 中石化南京化工研究院有限公司 | Carbon monoxide conversion process |
| CN110407172A (en) * | 2019-08-20 | 2019-11-05 | 四川亚联高科技股份有限公司 | A kind of middle-size and small-size natural gas hydrogen production plant |
| CN110407172B (en) * | 2019-08-20 | 2024-04-26 | 四川亚联氢能科技股份有限公司 | Small and medium-sized natural gas hydrogen production device |
| CN110541690A (en) * | 2019-09-04 | 2019-12-06 | 中海石油气电集团有限责任公司 | method for improving recovery ratio by decarbonization of natural gas at gas field wellhead and CO2 reinjection |
| CN112645283A (en) * | 2019-10-11 | 2021-04-13 | 中国石油化工股份有限公司 | System and method for producing hydrogen |
| CN110950304A (en) * | 2019-12-16 | 2020-04-03 | 简阳绿杉新能源设备有限公司 | Method for preparing high-purity hydrogen by using natural gas |
| CN110980645A (en) * | 2019-12-27 | 2020-04-10 | 乔治洛德方法研究和开发液化空气有限公司 | Steam hydrocarbon reforming method |
| CN111288298A (en) * | 2020-03-09 | 2020-06-16 | 李明 | Method for recovering natural gas discharged by hydrogen production device through desulfurization, temperature rise and emptying |
| WO2021223733A1 (en) * | 2020-05-07 | 2021-11-11 | 中国石油化工股份有限公司 | Natural gas steam reforming hydrogen production system and method therefor |
| CN111777038A (en) * | 2020-07-02 | 2020-10-16 | 上海浩用工业炉有限公司 | Waste heat recovery system and method for hydrogen production converter |
| CN112813454A (en) * | 2021-03-03 | 2021-05-18 | 中海石油气电集团有限责任公司 | Natural gas reforming and carbon dioxide combined hydrogen production power generation system and method |
| CN113213425A (en) * | 2021-06-08 | 2021-08-06 | 金川集团股份有限公司 | System and method for preparing hydrogen by using natural gas |
| CN114014270A (en) * | 2021-12-10 | 2022-02-08 | 四川天采科技有限责任公司 | Modularized natural gas reforming hydrogen production machine and hydrogen production method thereof |
| CN114436211A (en) * | 2021-12-30 | 2022-05-06 | 陕西聚能新创煤化科技有限公司 | Natural gas microwave catalytic conversion device and conversion method |
| CN114772551A (en) * | 2022-06-16 | 2022-07-22 | 浙江百能科技有限公司 | Method and system for efficiently utilizing methane-rich gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108439337A (en) | A kind of method of natural gas reforming hydrogen manufacturing | |
| JP5887103B2 (en) | Hydrogen production method by steam reforming oil cut with optimized steam generation | |
| CN101190781B (en) | Minitype light hydrocarbon steam reforming hydrogen manufacturing technique | |
| PL144284B1 (en) | Method of and apparatus for manufacture of ammonia | |
| US4203915A (en) | Process of producing methanol | |
| CN110407172B (en) | Small and medium-sized natural gas hydrogen production device | |
| CA3103715C (en) | Tail gas heating within psa surge tank | |
| CN112678770B (en) | Methanol and water hydrogen production device adopting PSA tail gas catalytic combustion for heat supply | |
| CN110589765A (en) | Method and system for preparing synthesis gas in different proportions by using natural gas | |
| CN109071217B (en) | Method and apparatus for producing hydrogen by catalytic steam reforming of a hydrocarbon-containing feed gas | |
| US9266805B2 (en) | System and method for producing gasoline or dimethyl ether | |
| CN107364831B (en) | Method and installation for producing synthesis gas by catalytic steam reforming of a hydrocarbon feed gas | |
| CN113896197B (en) | Method for preparing carbon monoxide by reforming hydrocarbon carbon dioxide | |
| CN208200371U (en) | A kind of methanol decomposition hydrogen manufacturing production on line | |
| CN106397121A (en) | A biogas-coke oven gas combined methanol production device | |
| KR20240012479A (en) | Ammonia cracking for hydrogen production | |
| CN104058368A (en) | Process and system for producing hydrogen by converting hydrocarbon-containing tail gas | |
| CN210419231U (en) | Medium and small natural gas hydrogen production device | |
| CN102337162A (en) | Low-water-steam-ratio saturated hot water tower CO transformation process | |
| CN214990265U (en) | Hydrogen raw material gas preparation device and hydrogen preparation system | |
| CN203998947U (en) | A kind of hydrocarbonaceous tail gas reforming hydrogen manufacturing system | |
| CN218893633U (en) | Temperature regulating system for preparing shaft furnace reducing gas from coke oven gas | |
| CN213569530U (en) | System for preparing ethanol and ethylene glycol synthesis gas through coke-oven gas carbon return conversion and by-producing hydrogen | |
| CN116924331B (en) | Natural gas hydrogen production system | |
| RU2117627C1 (en) | Method of preparing methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180824 |
|
| RJ01 | Rejection of invention patent application after publication |