CN102198931A - Method and device for co-producing hydrogen and synthesis gas by using dry gas - Google Patents
Method and device for co-producing hydrogen and synthesis gas by using dry gas Download PDFInfo
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- CN102198931A CN102198931A CN2011100952792A CN201110095279A CN102198931A CN 102198931 A CN102198931 A CN 102198931A CN 2011100952792 A CN2011100952792 A CN 2011100952792A CN 201110095279 A CN201110095279 A CN 201110095279A CN 102198931 A CN102198931 A CN 102198931A
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/32—Hydrogen storage
Abstract
The invention provides a method and a device for co-producing hydrogen and synthesis gas by using dry gas. The method comprises the following steps of: introducing raw material gas into a converter and performing conversion reaction of hydrocarbons and water vapor to obtain first converted gas, wherein the raw material gas comprises the dry gas and the water vapor, and the first converted gas comprises CO, CO2 and H2; introducing the first converted gas in a preset ratio into a conversion reactor and performing CO conversion reaction to obtain second converted gas; mixing the second converted gas and the first converted gas which is not subjected to the CO conversion reaction, and removing the CO2 by using a CO2 removing device to obtain third converted gas; and making the third converted gas pass through a pressure swing adsorption device to obtain the H2 and the synthesis gas respectively. By the method and the device, the H2 and the synthesis gas in an adjustable ratio can be prepared from the dry gas with unsteady components or quantity, the optimal utilization of the dry gas is realized, energy consumption is reduced, and economic benefits are improved.
Description
Technical field
The present invention relates to chemical technology field, relate in particular to the method and the device of a kind of dry gas combination producing hydrogen and synthetic gas.
Background technology
Industrial hydrogen more than 75% is to be raw material with hydro carbons (oil, Sweet natural gas and gas containing hydrocarbon for example coke(oven)gas etc.) in the world, adopts the hydrocarbon vapours catforming to produce synthetic gas, gets access to hydrogen again from synthetic gas.Sweet natural gas is the preferred raw materials of hydrogen manufacturing, but often is subjected to region restriction and uses less.Though foreign matter content is few in the light oil, the cost of light oil is high, becomes the restraining factors that are used for hydrogen manufacturing.Be rich in lighter hydrocarbons in the rich oil refinery dry gas that produces of refinery, and have the high characteristics of hydrogen-carbon ratio.Generally speaking, coking dry gas and catalytic cracked dry gas account for more than 80% of oil refinery dry gas, and wherein catalytic cracked dry gas then accounts for more than 60%, if with it as hydrogen feedstock, source of the gas will be very competent.
Yet in the prior art, because the composition or the tolerance of oil refinery dry gas is in unstable state, so untappedly always go out reliable, energy-conservation technology and effectively utilize oil refinery dry gas.Thus, need provide new technology, to realize the optimal utilization of oil refinery dry gas.
Summary of the invention
The invention provides the method and the device of a kind of dry gas combination producing hydrogen and synthetic gas, with the optimization utilization that realizes dry gas, cut down the consumption of energy, increase economic efficiency.
The invention provides the method for a kind of dry gas combination producing hydrogen and synthetic gas, comprising:
Unstripped gas is fed the conversion reaction that converter carries out hydro carbons and water vapor, obtain first reforming gas; Described unstripped gas comprises dry gas and water vapor, and described first reforming gas comprises CO, CO
2And H
2
Described first reforming gas feeding shift-converter of preset proportion is carried out the CO transformationreation, obtain second reforming gas;
Pass through CO after described second reforming gas and described first reforming gas that do not carry out the CO transformationreation mixed
2Remove device and remove CO
2, obtain the 3rd reforming gas;
Described the 3rd reforming gas is obtained H respectively by pressure-swing absorption apparatus
2And synthetic gas.
Wherein, dry gas for example can be coking dry gas or catalytic cracked dry gas; Synthetic gas is H
2Gas mixture with CO.
Further, described converter comprises one-stage converter and secondary reformer, and described one-stage converter is a heat-exchanged reformer; Described unstripped gas is fed the conversion reaction that converter carries out hydro carbons and water vapor, the process that obtains first reforming gas comprises: described unstripped gas is fed the conversion reaction that described one-stage converter carries out hydro carbons and water vapor, obtain the 4th reforming gas; With described the 4th reforming gas and O
2, water vapor feeds the conversion reaction that described secondary reformer carries out hydro carbons and water vapor, obtains the 5th reforming gas; Described the 5th reforming gas is fed the heat transfer tube of described one-stage converter, carry out obtaining described first reforming gas after the heat exchange with gas in the described one-stage converter.
Further, this method can also comprise: with the portion C O that removes
2Return described secondary reformer, with supplementary carbon source.
Further, this method can also comprise: the tail gas that described the 3rd reforming gas is obtained by described pressure-swing absorption apparatus returns described secondary reformer, with supplementary carbon source.
Further, the pressure that enters the unstripped gas of described one-stage converter is 1.0-6.0MPa, and temperature is 400-650 ℃, and total sulfur content is less than 0.1ppm.
Further, the temperature out of described the 4th reforming gas of discharging from described one-stage converter is 650-750 ℃, CH
4Volume content be 12-18%; The temperature out of carrying out described first reforming gas that obtains after the heat exchange with gas in the described one-stage converter is 550-750 ℃.
Further, the temperature out of described the 5th reforming gas of discharging from described secondary reformer is 800-1050 ℃, CH
4Volume content be less than or equal to 0.8%.
The present invention also provides the device of a kind of dry gas combination producing hydrogen and synthetic gas, and this device comprises: converter, shift-converter, CO
2Remove device and pressure-swing absorption apparatus;
The outlet of described converter links to each other with the inlet of described shift-converter and the inlet of described pressure-swing absorption apparatus respectively;
The outlet of described shift-converter links to each other with the inlet of described pressure-swing absorption apparatus;
Be connected described CO between the outlet of described shift-converter and the inlet of described pressure-swing absorption apparatus
2Remove device, be connected described CO between the outlet of described converter and the inlet of described pressure-swing absorption apparatus
2Remove device.
Further, described converter comprises: one-stage converter and secondary reformer, described one-stage converter are heat-exchanged reformer; The outlet of described one-stage converter links to each other with the inlet of described secondary reformer, and the outlet of described secondary reformer links to each other with the inlet of the heat transfer tube of described one-stage converter, and the outlet of the heat transfer tube of described one-stage converter is the outlet of described converter.
Further, described CO
2Remove the CO of device
2Outlet links to each other with the inlet of described secondary reformer, and the tail gas outlet of described pressure-swing absorption apparatus links to each other with the inlet of described secondary reformer.
The method and the device of dry gas combination producing hydrogen of the present invention and synthetic gas have the following advantages:
1, the present invention is applicable to coking dry gas or catalytic cracked dry gas, because the present invention carries out the CO transformationreation with first reforming gas of preset proportion, and another part first reforming gas does not carry out the CO transformationreation, making can be according to technology and product requirement, adjust the tolerance of first reforming gas that carries out the CO transformationreation flexibly, and then CO and H in the feasible synthetic gas that finally obtains
2Adjustable ratio.The present invention especially goes for forming or tolerance is astable dry gas thus, is suitable for plurality of raw materials gas operating mode.
2, the hydrocarbon steam among the present invention transforms (the forwarding reaction that is hydro carbons and water vapor) and adopts the heat exchange type conversion, utilize the pyrolytic conversion gas of secondary reformer outlet that the reactant gases in the one-stage converter is heated, reduce the load of converter, and can reduce fuel hydrocarbon consumption and smoke discharge amount significantly.
3, decarbonization device of the present invention (promptly removes CO
2Device) flashed vapour can return process furnace and do the fuel use, and perhaps, this flashed vapour can return the carbon content of replenishing in the secondary reformer in the unstripped gas, thereby can cut down the consumption of energy, increase economic efficiency.
4, the tail gas of pressure-swing absorption apparatus can return secondary reformer and replenish carbon content in the unstripped gas among the present invention, thereby can cut down the consumption of energy, increase economic efficiency.
Description of drawings
Fig. 1 is the schema of the method embodiment one of dry gas combination producing hydrogen of the present invention and synthetic gas;
Fig. 2 is the process flow sheet of the method embodiment two of dry gas combination producing hydrogen of the present invention and synthetic gas.
Embodiment
For making the purpose, technical solutions and advantages of the present invention clearer, below in conjunction with accompanying drawing, technical scheme of the present invention is clearly and completely described, obviously, described embodiment is the present invention's part embodiment, rather than whole embodiment.Based on the embodiment among the present invention, those of ordinary skills belong to the scope of protection of the invention not making the every other embodiment that is obtained under the creative work prerequisite.
Fig. 1 is the schema of the method embodiment one of dry gas combination producing hydrogen of the present invention and synthetic gas, and as shown in Figure 1, this method comprises:
The dry gas and the water vapor of certain flow, temperature and pressure are mixed back feeding converter, under the catalysis of hydro carbons catalyzer, carry out the conversion reaction of hydro carbons and water vapor.Wherein, the conversion reaction of hydro carbons and water vapor is an existing processes.Be rich in for example CH of lower carbon number hydrocarbons in the dry gas
4, mainly comprise CO, CO in first reforming gas that dry gas and water vapor carry out obtaining after the conversion reaction
2And H
2
Wherein, in a concrete embodiment, this converter can be the multistage converter, comprise one-stage converter and follow-up multistage converter in the multistage converter, in follow-up multistage converter, can replenish the unstripped gas except dry gas, and can return the leading portion converter, carry out heat exchange with reactant gases in the leading portion converter from the pyrolytic conversion gas of follow-up multistage converter middle outlet.Being two sections with this converter below is that example describes:
Converter comprises one-stage converter and secondary reformer, and wherein this one-stage converter is a heat-exchanged reformer; Step 101 is specifically as follows: unstripped gas (dry gas and water vapor) is fed one-stage converter carry out the conversion reaction of hydro carbons and water vapor, obtain the 4th reforming gas, then with the 4th reforming gas and O
2, water vapor feeds secondary reformer and carries out the conversion reaction of hydro carbons and water vapor, obtains the 5th reforming gas; Afterwards the 5th reforming gas is fed the heat transfer tube of one-stage converter, carry out obtaining first reforming gas after the heat exchange with gas in the one-stage converter.
Wherein, the pressure that enters the unstripped gas of one-stage converter can be 1.0-6.0MPa, and temperature can be 400-650 ℃, and total sulfur content is less than 0.1ppm.
Further, the temperature out of the 4th reforming gas of discharging from one-stage converter can be 650-750 ℃, CH
4Volume content can be 12-18%; The temperature out of carrying out first reforming gas that obtains after the heat exchange with gas in the one-stage converter can be 550-750 ℃.
Further, the temperature out of the 5th reforming gas of discharging from secondary reformer can be 800-1050 ℃, CH
4Volume content be less than or equal to 0.8%.
Need to prove that the conversion reaction of hydro carbons described in the present invention and water vapor is the hydrocarbon steam conversion reaction, the process of this conversion reaction can for: under the katalysis of nickel-base catalyst, be vaporized chemical, the hydrocarbon conversion become H with the water vapor
2, CO and CO
2This is a strong endothermic reaction process.
The present invention can adopt the alkanes in the heat-exchanged reformer pre-inversion dry gas, enters the technology that oxygen carries out degree of depth conversion in the secondary reformer then; This technology can reduce one section and transform required heat, a part of hydrocarbon steam conversion load transfer is gone to finish in the secondary reformer of heat-insulating, and utilize the waste heat of the high-temperature gas of secondary reformer outlet, for one section conversion provides required heat, realization system thermal equilibrium, thus the fuel that accounts for total burn-off about 30% can be got off with the hydrocarbon saving.
After obtaining first reforming gas, can a part of first reforming gas is carried out the CO transformationreation, and another part first reforming gas not carry out the CO transformationreation according to the requirement of technology or product by converter.Carry out the ratio of first reforming gas of CO transformationreation by adjustment, promptly CO is transformed to CO by the CO transformationreation
2And H
2Thereby, can regulate CO and H in the final product
2Ratio.
First reforming gas that will carry out second reforming gas that obtains after the CO transformationreation and not carry out the CO transformationreation mixes, and passes through CO then
2Remove device (being decarbonization device) and remove CO wherein
2, obtain the 3rd reforming gas.
Further, can be with the portion C O that removes
2Return secondary reformer, with supplementary carbon source; According to the requirement of technology or product, can the CO that obtain will be removed
2A part return in the secondary reformer CO
2After turning back to secondary reformer, CO
2Can and H
2Reaction obtains CO, thereby has reached the effect that increases carbon content in the finished product.
Because CO
2Discharging be the emphasis of energy-saving and emission-reduction, the present invention is with CO
2Turn back in the secondary reformer, both can supplementary carbon source, also can solve CO
2Emission problem.
Further, decarbonization device removes the CO that obtains
2Can also make technical grade or food grade dry ice through existing corollary apparatus, reach the purpose of GHG (Greenhouse Gases) emissions mitigation carbonic acid gas.
The 3rd reforming gas is passed through the multitower pressure-swing absorption apparatus, and can control each material absorption and desorption ability, obtain H respectively according to the requirement of technology or product
2And synthetic gas.
Further, the 3rd reforming gas can be returned secondary reformer by the tail gas that pressure-swing absorption apparatus obtains, with supplementary carbon source; May comprise unreacted alkane in this tail gas and not be removed CO completely
2, this tail gas is returned secondary reformer, can increase the carbon content in the finished product.Wherein, when tail gas returns secondary reformer, can pressurize tail gas through pressurizing device earlier, and then return secondary reformer.
Dry gas among the present invention can be oil refinery dry gas such as coking dry gas or catalytic cracked dry gas; Oil refinery dry gas of the prior art also can pollute atmosphere simultaneously generally as fuel or put into torch and waste; And scheme provided by the invention can realize oil refinery dry gas the optimization utilization, cut down the consumption of energy, increase economic efficiency.
It is low to the invention provides a kind of power consumption, the simple technology of flow process, can improve the effective rate of utilization of the energy, reach the purpose of energy-saving and emission-reduction, and resource distribution between each device of optimization refinery, make between each device, the product and form the chain type industrial system, and can in time adjust coordination optimization between product production capacity and device, improve competitiveness of product according to the market requirement.
Describe the method for dry gas combination producing hydrogen, carbon monoxide and synthetic gas that the inventive method embodiment one provides in detail below by Fig. 2, Fig. 2 is the process flow sheet of the method embodiment two of dry gas combination producing hydrogen of the present invention and synthetic gas, as shown in Figure 2, this method comprises:
The dry gas of 40 ℃ of flow 317.5kmol/h, pressure 1.8MPa, temperature after smart desulfurization and being heated to 360 ℃ of sulphur content＜0.1ppm, flow 317.5kmol/h, pressure 1.69MPa, temperature, is mixed the unstripped gas 1 that obtains flow 938.3kmol/h, pressure 1.66MPa, 505 ℃ of temperature, total carbon content 16.3% with the water vapor of flow 620.8kmol/h; Unstripped gas 1 is fed in heat-exchanged reformer (the being one-stage converter) pipe, by managing the heat that two sections reforming gas of outer high temperature provide, under the katalysis of pipe inner catalyst, carry out the conversion reaction of hydro carbons and water vapor, the pressure that goes out one section reforming gas 2 (being equivalent to the 4th above-mentioned reforming gas) of heat-exchanged reformer can be 655 ℃, remaining CH for 1.46MPa, temperature
4Volume content is 13.3%;
Oxygen 3 (wherein oxygenous amount is 98%) from 40 ℃ of flow 98.5kmol/h, pressure 3.6MPa, the temperature of air separation facility (not shown), after a small amount of water vapor 4 of 450 ℃ of flow 27.8kmol/h, pressure 4.8MPa, temperature is mixed, enter after the process furnace (not shown) is heated to 500 ℃, enter secondary reformer with above-mentioned one section reforming gas 2, hydro carbons (CH for example takes place under the effect of catalyzer
4) and the degree of depth conversion reaction of water vapor;
The pressure that goes out two sections reforming gas 5 (being equivalent to the 5th above-mentioned reforming gas) of secondary reformer can be 931 ℃, remaining CH for 1.4MPa, temperature
4Volume content≤0.5%; Two sections reforming gas 5 are fed the pipe external space of heat-exchanged reformer, its high level heat is passed to air-flow in the heat-exchanged reformer pipe, two sections reforming gas 5 carry out discharging reforming gas 6 (being equivalent to the first above-mentioned reforming gas) after the heat exchange in heat-exchanged reformer, and the temperature out of reforming gas 6 can be 588 ℃;
Reforming gas 6 can be that 367 ℃, pressure are that (volume content of CO wherein is 9.7%, CO for the reforming gas 6 of 1.32MPa through comprising that multistage waste heat recovery unit such as waste heat boiler (not shown) reclaims heat to temperature
2Volume content be 5.9%);
The reforming gas 6 that goes out the gas 7 of middle temperature transformation reactor and do not feed the middle temperature transformation reactor is mixed into reforming gas 8, and reforming gas 8 can be again continues to reclaim heat, separate vapour phlegma and be that 893.2kmol/h, pressure are 40 ℃ of 1.2MPa, temperature with being water-cooled to flow through multistage waste heat recovery unit (not shown);
Reforming gas 8 after waste heat recovery can (be CO through decarbonization device
2Remove device) remove CO
2After obtain the gas 10 (being equivalent to the 3rd above-mentioned reforming gas) of 40 ℃ of flow 789.25kmol/h, pressure 1.2MPa, temperature, the CO that removes
2The flow of gas 9 can be 104.5kmol/h, CO
2Volume content be 99%;
The gas 10 that goes out decarbonization device enters multitower pressure-swing absorption apparatus (PSA), control each material absorption and desorption ability, can make the hydrogen 11 of flow 540.4kmol/h, pressure 6.65MPa, 85.6 ℃ of temperature, content 99.99%, and, flow 212.8kmol/h, pressure 1.9MPa, 132 ℃ of temperature, contain 52% (volume) CO and 48% (volume) H
2Synthetic gas 13;
The flashed vapour 14 of decarbonization device can partly return the process furnace device and (be used for the device to the unstripped gas heating, not shown) make fuel, perhaps, flashed vapour 14 can part be sent to secondary reformer to replenish the carbon content in the unstripped gas after the air supply compressor pressurization;
The tail gas 15 of pressure-swing absorption apparatus (flow can can be 40 ℃ for 0.1MPa, temperature for 32kmol/h, pressure) is sent to secondary reformer to replenish the carbon content in the unstripped gas after the pressurizing device pressurization.
Wherein, can discharge gas 12 from tail gas 15, gas 12 is parts of tail gas 15, and gas 12 is for N in the anti-locking system
2, CH
4Deng the accumulation of gas and the general gas of discharging, its flow can be by the N of system
2, CH
4The balance decision.
The flow of each road gas, pressure and temperature are by preparation H in the present embodiment
2Decide with the required proportioning raw materials of synthetic gas,, can make the H of different ratios by regulating the flow of each road gas
2And synthetic gas.
H in the present embodiment
2Can in the scope of a broad, regulate with the output of synthetic gas, and H in the synthetic gas
2Also can regulate with the ratio of CO by the preparation method; For example by regulating the ratio that reforming gas 6 carries out the CO transformationreation, the hydrogen-carbon ratio that can regulate the finished product.
Method provided by the invention, can adopt composition or tolerance is that astable dry gas is the H that raw material is produced adjustable ratio
2And synthetic gas, the present invention integrates hydrocarbon steam conversion, conversion, decarburization, pressure-swing absorption apparatus, recycle simultaneously fully tail gas, reached the effect of the comprehensive utilization energy, belong to power-saving technology.
The present invention also provides the device of dry gas combination producing hydrogen and synthetic gas, and this device is used to realize the method for dry gas combination producing hydrogen provided by the invention and synthetic gas.Referring to Fig. 2, the device embodiment of dry gas combination producing hydrogen of the present invention and synthetic gas can comprise: converter, shift-converter (being the CO shift-converter), CO
2Remove device and pressure-swing absorption apparatus.
The outlet of converter links to each other with the inlet of shift-converter and the inlet of pressure-swing absorption apparatus respectively;
The outlet of shift-converter links to each other with the inlet of pressure-swing absorption apparatus;
Be connected CO between the outlet of shift-converter and the inlet of pressure-swing absorption apparatus
2Remove device, be connected CO between the outlet of converter and the inlet of pressure-swing absorption apparatus
2Remove device.
Further, converter comprises: one-stage converter and secondary reformer; Wherein one-stage converter is a heat-exchanged reformer.
The outlet of one-stage converter links to each other with the inlet of secondary reformer, and the outlet of secondary reformer links to each other with the inlet of the heat transfer tube of one-stage converter, and the outlet of the heat transfer tube of one-stage converter is the outlet of converter.
Further, CO
2Remove the CO of device
2Outlet links to each other with the inlet of secondary reformer; The tail gas outlet of pressure-swing absorption apparatus links to each other with the inlet of secondary reformer.
Use device in the present embodiment to realize that the method for dry gas combination producing hydrogen provided by the invention and synthetic gas and idiographic flow referring to the description among above-mentioned each the method embodiment of the present invention, do not repeat them here.
The device that uses present embodiment to provide, can adopt composition or tolerance is that astable dry gas is the H that raw material is produced adjustable ratio
2And synthetic gas, the present invention integrates hydrocarbon steam conversion, conversion, decarburization, pressure-swing absorption apparatus, recycle simultaneously fully tail gas, reached the effect of the comprehensive utilization energy, belong to power-saving technology.
It should be noted that at last: above embodiment only in order to technical scheme of the present invention to be described, is not intended to limit; Although with reference to previous embodiment the present invention is had been described in detail, those of ordinary skill in the art is to be understood that: it still can be made amendment to the technical scheme that aforementioned each embodiment put down in writing, and perhaps part technical characterictic wherein is equal to replacement; And these modifications or replacement do not make the essence of appropriate technical solution break away from the spirit and scope of various embodiments of the present invention technical scheme.
Claims (10)
1. the method for dry gas combination producing hydrogen and synthetic gas is characterized in that, comprising:
Unstripped gas is fed the conversion reaction that converter carries out hydro carbons and water vapor, obtain first reforming gas; Described unstripped gas comprises dry gas and water vapor, and described first reforming gas comprises CO, CO
2And H
2
Described first reforming gas feeding shift-converter of preset proportion is carried out the CO transformationreation, obtain second reforming gas;
Pass through CO after described second reforming gas and described first reforming gas that do not carry out the CO transformationreation mixed
2Remove device and remove CO
2, obtain the 3rd reforming gas;
Described the 3rd reforming gas is obtained H respectively by pressure-swing absorption apparatus
2And synthetic gas.
2. method according to claim 1 is characterized in that described converter comprises one-stage converter and secondary reformer, and described one-stage converter is a heat-exchanged reformer; Described unstripped gas is fed the conversion reaction that converter carries out hydro carbons and water vapor, the process that obtains first reforming gas comprises:
Described unstripped gas is fed the conversion reaction that described one-stage converter carries out hydro carbons and water vapor, obtain the 4th reforming gas;
With described the 4th reforming gas and O
2, water vapor feeds the conversion reaction that described secondary reformer carries out hydro carbons and water vapor, obtains the 5th reforming gas;
Described the 5th reforming gas is fed the heat transfer tube of described one-stage converter, carry out obtaining described first reforming gas after the heat exchange with gas in the described one-stage converter.
3. method according to claim 2 is characterized in that, also comprises:
With the portion C O that removes
2Return described secondary reformer, with supplementary carbon source.
4. method according to claim 2 is characterized in that, also comprises:
The tail gas that described the 3rd reforming gas is obtained by described pressure-swing absorption apparatus returns described secondary reformer, with supplementary carbon source.
5. method according to claim 2 is characterized in that:
The pressure that enters the unstripped gas of described one-stage converter is 1.0-6.0MPa, and temperature is 400-650 ℃, and total sulfur content is less than 0.1ppm.
6. method according to claim 2 is characterized in that:
The temperature out of described the 4th reforming gas of discharging from described one-stage converter is 650-750 ℃, CH
4Volume content be 12-18%;
The temperature out of carrying out described first reforming gas that obtains after the heat exchange with gas in the described one-stage converter is 550-750 ℃.
7. method according to claim 2 is characterized in that: the temperature out of described the 5th reforming gas of discharging from described secondary reformer is 800-1050 ℃, CH
4Volume content be less than or equal to 0.8%.
8. the device of dry gas combination producing hydrogen and synthetic gas is characterized in that, comprising: converter, shift-converter, CO
2Remove device and pressure-swing absorption apparatus;
The outlet of described converter links to each other with the inlet of described shift-converter and the inlet of described pressure-swing absorption apparatus respectively;
The outlet of described shift-converter links to each other with the inlet of described pressure-swing absorption apparatus;
Be connected described CO between the outlet of described shift-converter and the inlet of described pressure-swing absorption apparatus
2Remove device, be connected described CO between the outlet of described converter and the inlet of described pressure-swing absorption apparatus
2Remove device.
9. device according to claim 8 is characterized in that, described converter comprises: one-stage converter and secondary reformer, described one-stage converter are heat-exchanged reformer;
The outlet of described one-stage converter links to each other with the inlet of described secondary reformer, and the outlet of described secondary reformer links to each other with the inlet of the heat transfer tube of described one-stage converter, and the outlet of the heat transfer tube of described one-stage converter is the outlet of described converter.
10. device according to claim 9 is characterized in that:
Described CO
2Remove the CO of device
2Outlet links to each other with the inlet of described secondary reformer, and the tail gas outlet of described pressure-swing absorption apparatus links to each other with the inlet of described secondary reformer.
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|---|---|---|---|
| CN2011100952792A CN102198931A (en) | 2011-04-15 | 2011-04-15 | Method and device for co-producing hydrogen and synthesis gas by using dry gas |
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|---|---|---|---|
| CN2011100952792A CN102198931A (en) | 2011-04-15 | 2011-04-15 | Method and device for co-producing hydrogen and synthesis gas by using dry gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104150442A (en) * | 2014-07-04 | 2014-11-19 | 宁夏宝塔石化科技实业发展有限公司 | Method for recycling heat in deep processing and utilization of olefin-rich oil refining tail gas |
| CN104150441A (en) * | 2014-07-29 | 2014-11-19 | 山西潞安环保能源开发股份有限公司 | Method for converting Fischer-Tropsch synthesis tail gas into Fischer-Tropsch synthesis feed gas |
| CN104150441B (en) * | 2014-07-29 | 2016-04-13 | 山西潞安环保能源开发股份有限公司 | A kind of Fischer-Tropsch process exhaust is converted into the method for F-T synthesis unstripped gas |
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Application publication date: 20110928 |