CN214880202U - System for utilize liquid metal schizolysis natural gas hydrogen manufacturing - Google Patents
System for utilize liquid metal schizolysis natural gas hydrogen manufacturing Download PDFInfo
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- CN214880202U CN214880202U CN202120835329.5U CN202120835329U CN214880202U CN 214880202 U CN214880202 U CN 214880202U CN 202120835329 U CN202120835329 U CN 202120835329U CN 214880202 U CN214880202 U CN 214880202U
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Abstract
The utility model discloses a system for producing hydrogen by cracking natural gas with liquid metal, which comprises a liquid metal melting tank, a liquid metal cracking reactor and a separator; the liquid metal cracking reactor is internally provided with a uniformly distributed structure for bearing liquid metal, and is provided with a natural gas inlet and a cracking gas outlet, the cracking gas outlet is connected with a separator, and the separator is provided with a carbon black outlet; and an overflow port connected with the liquid metal cracking reactor is arranged on the liquid metal melting tank. The utility model discloses the system that utilizes liquid metal schizolysis natural gas hydrogen manufacturing can not only make hydrogen, can also make high-quality carbon black, reduction in production cost, and greenhouse gas such as no carbon dioxide or harmful product discharge.
Description
Technical Field
The utility model relates to a hydrogen preparation technical field, concretely relates to utilize system of liquid metal schizolysis natural gas hydrogen manufacturing.
Background
With the aggravation of global warming, the increase of carbon emission year by year will affect the living environment of human beings, and in order to the long-term living environment of human beings, the carbon emission must be controlled, so hydrogen energy is considered as the most ideal new energy, and the hydrogen energy has the characteristics of good combustion performance, no toxicity, high utilization rate, convenient transportation and the like, and is a clean energy with development prospect for replacing the traditional energy. At present, the domestic main energy structure mainly comprises coal, petroleum and natural gas, 96 percent of hydrogen is also prepared from stone resources such as coal, petroleum, natural gas and the like, and the hydrogen preparation by adopting the natural gas is most reasonable and economical.
In the natural gas hydrogen production technology, thermal plasma thermal cracking, solar thermal cracking and natural gas catalytic cracking are mainly adopted, but the prior art is relatively immature, and the yield and safety are low. The thermal plasma thermal cracking hydrogen production technology adopted in industry mainly adopts a non-transfer plasma torch, uses natural gas as working medium gas, and has the main defects of short arc service life and incapability of working for a long time; the solar energy pyrolysis hydrogen production mainly utilizes solar energy to decompose water at high temperature to produce hydrogen, the reaction operation temperature is about 2000 ℃, and the decomposed high-temperature gas product has the danger of contact explosion; the natural gas catalytic cracking technology comprises a partial oxidation method and a steam conversion method, wherein the partial oxidation method needs to use pure oxygen as an oxidant, the cost is extremely high, the partial oxidation method is rarely used at present, the steam conversion method comprises ammonia synthesis, the emission of carbon dioxide is large, the synthesis gas obtained after conversion also contains CO impurities, the CO impurities can poison the ammonia synthesis catalyst, the CO impurities need to be removed before the synthesis gas enters a synthesis reactor, the production cost is increased, the ammonia synthesis is reversible, the single-pass conversion rate is low, and the hydrogen yield is not high and can only reach about 80%.
Therefore, the hydrogen production by natural gas can not be distinguished in a plurality of hydrogen production processes, and if a natural gas hydrogen production system with high hydrogen yield, economy and environmental protection can be developed, the use requirement of people on new energy can be greatly met, the market competitiveness of a hydrogen source is provided, and the popularization and the development are further realized.
SUMMERY OF THE UTILITY MODEL
The utility model discloses the main technical problem who solves provides an utilize system of liquid metal schizolysis natural gas hydrogen manufacturing, not only can obtain the hydrogen of high productivity, can also obtain high-quality carbon black.
In order to solve the technical problem, the utility model discloses a technical scheme be:
the system for producing hydrogen by cracking natural gas with liquid metal comprises a liquid metal melting tank, a liquid metal cracking reactor and a separator;
a support frame is arranged in the liquid metal cracking reactor, a uniform distribution structure for bearing liquid metal is arranged on the support frame, a natural gas inlet and a cracking gas outlet are arranged on the liquid metal cracking reactor, the cracking gas outlet is connected with a separator, and a carbon black outlet is arranged on the separator;
and the liquid metal melting tank is also provided with an overflow port connected with the liquid metal cracking reactor.
In the specific embodiment of the utility model, be connected with the electromagnetic pump between liquid metal melting tank and the liquid metal cracking reactor.
In a particular embodiment of the invention, the liquid metal melting tank is externally provided with an electromagnetic heater.
Furthermore, the heating mode of the electromagnetic heater comprises medium-frequency electromagnetic heating and high-frequency electromagnetic heating;
further, the frequency of the medium-frequency electromagnetic heating is 400HZ～10KHZ；
The frequency of the high-frequency electromagnetic heating is 10 KHz-40 KHZ。
In the specific embodiment of the present invention, the temperature of the liquid metal cracking reactor is 700-1400 ℃.
In a particular embodiment of the present invention, the uniform distribution structure has a square grid and/or a circular hole.
The size of the square is 20-100 mm multiplied by 20-100 mm; the diameter of the round hole is 10-120 mm;
the uniform distribution structure is made of high-temperature ceramics.
In a particular embodiment of the invention, the separator comprises a plurality of cyclone coolers arranged in parallel;
a water-cooling jacket is arranged on the separator; a plurality of flow disturbing columns are uniformly distributed in the water-cooling jacket;
the temperature in the separator is 150-400 ℃.
In the specific embodiment of the utility model, the outlet of the separator is also connected with a bag-type dust remover and a condenser in sequence, and the bag-type dust remover and the condenser are both provided with carbon black discharge ports,
the exhaust end of the condenser is also provided with a pressure swing absorber,
a recycling pipeline is also connected between the liquid metal cracking reactor and the pressure swing absorber.
Further, the temperature of the bag-type dust collector is 180-230 ℃;
the temperature of the condenser is less than or equal to 50 ℃.
In a particular embodiment of the present invention, the liquid metal cracking reactor is further provided with a carbon black discharge port.
The utility model has the advantages that:
(1) the utility model discloses the system is simple, and equipment cost is low, has improved hydrogen manufacturing efficiency.
(2) Through the utility model discloses the hydrogen productivity that the system preparation obtained is more than 90%, and the carbon black yield is high, and does not have carbon dioxide and harmful gas and produce, and the hydrogen manufacturing cost is less than 20 yuan/kg, economic environmental protection.
Drawings
Fig. 1 is a schematic diagram of a system for producing hydrogen by cracking natural gas with liquid metal.
Wherein, 1: electromagnetic heater, 2: liquid metal melting tank, 3: electromagnetic pump, 4: liquid metal cracking reactor, 5: separator, 6: bag-type dust collector, 7: condenser, 8: pressure swing adsorbers.
Detailed Description
The technical solution of the present invention will be described clearly and completely with reference to the accompanying drawings, and obviously, the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the directions or positional relationships indicated by "upper", "lower", "inner", "outer", etc. are the directions or positional relationships indicated on the basis of the drawings, and are only for convenience of description and simplification of description, and do not indicate or imply that the device or element indicated must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention.
In the description of the present invention, it should be noted that, unless otherwise explicitly stated or limited, the terms "connected" and "connected" are to be interpreted broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example 1
The system for producing hydrogen by cracking natural gas by using liquid metal provided by the utility model is shown in figure 1,
the system for preparing hydrogen by cracking natural gas with liquid metal comprises a liquid metal melting tank 2, a liquid metal cracking reactor 4 and a separator 5; a support frame is arranged in the liquid metal cracking reactor 4, an evenly distributed structure for bearing liquid metal is arranged on the support frame, the support frame is of a frame structure, the heat dissipation effect of the evenly distributed structure is not influenced, the support frame is made of high-temperature-resistant (above 1400 ℃), and the evenly distributed structure is made of square grids and/or round holes; the size of the square grids in the uniform distribution structure is 20-100 mm multiplied by 20-100 mm; the diameter of the round hole is 10-120 mm; the material of equipartition structure is high temperature ceramics. The liquid metal cracking reactor 4 is provided with a natural gas inlet and a cracked gas outlet, and natural gas uniformly enters the liquid metal cracking reactor 4 from the bottom of the liquid metal cracking reactor 4; further, a pyrolysis gas outlet is connected with the separator 5, and a carbon black outlet is formed in the separator 5; the liquid metal melting tank 2 is also provided with an overflow port connected with the liquid metal cracking reactor 4, and the liquid metal enters the liquid metal melting tank 2 through the overflow port to be heated, so that the temperature required by hydrogen production through natural gas cracking is maintained at 800-1100 ℃.
In some embodiments, an electromagnetic pump 3 is connected between the liquid metal melting tank 2 and the liquid metal cracking reactor 4, and the liquid metal in the liquid metal melting tank 2 is pumped into the liquid metal cracking reactor 4 under the action of the electromagnetic pump 3.
In some embodiments, the separator 5 comprises a plurality of cyclones; the cyclone coolers are arranged in parallel; the pyrolysis gas enters the separator 5 tangentially and uniformly, and most of carbon black is separated out under the action of centrifugal force generated by the gas flow.
Further, the cyclone cooler is provided with a water cooling jacket; the water cooling jacket is provided with a water flow channel, and cooling water cools the cracked gas through the water cooling jacket outside the cyclone cooler; a plurality of turbulence columns are uniformly distributed in the water-cooling jacket, and water and pyrolysis gas perform dividing wall heat exchange to enhance the heat exchange effect.
In some embodiments, an electromagnetic heater 1 is arranged outside the liquid metal melting tank, and the heating mode of the electromagnetic heater 1 comprises medium-frequency electromagnetic heating and high-frequency electromagnetic heating; the frequency of the medium-frequency electromagnetic heating is 400HZ～10KHZ(ii) a The frequency of the high-frequency electromagnetic heating is 10 KHz-40 KHZThe metal in the liquid metal melting tank 2 is melted into liquid metal by the electromagnetic heater 1.
In some embodiments, the cyclone cooler is provided with a pyrolysis gas outlet, pyrolysis gas enters the cyclone cooler with a heat exchange structure, and after the pyrolysis gas and cooling water undergo partition wall heat exchange, carbon black is separated under the action of self gas rotating centrifugal force; a pyrolysis gas outlet of the cyclone cooler is connected with the bag-type dust collector 6, pyrolysis gas cooled to 200-250 ℃ by the cyclone cooler enters the bag-type dust collector 6 for gas-solid separation, and the separation temperature is 180-230 ℃; the bag-type dust collector 6 is provided with a cracking gas outlet, and the cracking gas passes through a cyclone cooler and the bag-type dust collector and then more than 95% of carbon black is collected; a cracking gas outlet of the bag-type dust collector is connected with a condenser 7, and the temperature of the condenser 7 is less than or equal to 50 ℃; the condenser 7 is provided with a cracked gas outlet and a cooling water inlet; the pyrolysis gas outlet of the condenser 7 is connected with the pressure swing absorber 8, and the pyrolysis gas cooled by the condenser 7 enters the pressure swing absorber 8 to be separated into hydrogen.
In some embodiments, the liquid metal cracking reactor 4 is further provided with a carbon black discharge port for discharging carbon black out of the cracking reactor according to the increase of the liquid metal level, thereby facilitating the collection of carbon black.
In some embodiments, a recovery pipeline is connected between the liquid metal cracking reactor 4 and the pressure swing adsorber 8, so that the gas without cracking can enter the cracking reactor 4 again for cracking.
In some embodiments, the separator 5 and the condenser 7 are provided with a water vapor recovery device, and the cooling water and the cracked gas generate hot water or steam after heat exchange to be transported for utilization, so that the hot water or steam can be used as hot water or steam for production and living.
Example 2 preparation of hydrogen
(1) The metal Sn50kg in the liquid metal melting tank 2 is heated and liquefied by the electromagnetic induction heating method using the external electromagnetic heater 1, and the liquid metal Sn is formed.
(2) Liquid metal Sn in the liquid metal melting tank 2 is pumped into the liquid metal melting tank 2 through an overflow port under the action of an electromagnetic pump 3, natural gas uniformly enters from the bottom of a liquid metal cracking reactor 4, and the natural gas and the liquid metal Sn are subjected to heat and mass transfer reaction under the action of 25% of Ni to 75% of Bi13.5kg of a catalyst to crack the natural gas into hydrogen and cracked gas containing carbon black, wherein the cracking temperature is 1100 ℃, and the cracked gas containing the carbon black is collected according to the liquid level of the liquid metal Sn.
(3) The pyrolysis gas containing a small amount of carbon black is input into a cyclone sub-cooler with a heat exchange structure, after the pyrolysis gas containing the carbon black and cooling water are subjected to partition wall heat exchange, the carbon black is separated under the action of self gas rotating centrifugal force, and hot water or steam generated after the cooling water and the pyrolysis gas are subjected to heat exchange can be output for utilization and can be used as hot water or steam for production and living.
(4) And cooling the pyrolysis gas from which the carbon black is separated to 230 ℃, then feeding the pyrolysis gas into a bag-type dust collector 6 for gas-solid separation, collecting more than 95% of the carbon black after the pyrolysis gas passes through a cyclone cooler and the bag-type dust collector 6, and reducing the temperature of the pyrolysis gas to 200-250 ℃.
(5) The cracked gas after temperature reduction and dust removal enters a condenser 7 to be continuously cooled, the temperature is reduced to below 50 ℃, and a small amount of carbon black is enriched in the condenser 7; the cracked gas cooled by the condenser 7 enters a Pressure Swing Adsorption (PSA) device 8 to separate hydrogen and hydrocarbon substances. The yield of hydrogen obtained was 96.2%; the yield of the carbon black is 70 percent, and the cost of hydrogen production is 22.3 yuan/kg. In order to further increase the cracking rate, the separated hydrocarbon substances can be returned to the liquid metal cracking reactor 4 for cracking again, so that the cracking rate of the natural gas is increased.
Example 3 preparation of hydrogen
(1) The metal Sn50Kg in the liquid metal melting tank 2 is heated and liquefied by an electromagnetic induction heating method using an external electromagnetic heater 1, and the liquid metal Sn is formed.
(2) Liquid metal Sn in the liquid metal melting tank 2 is pumped into the liquid metal melting tank 2 through an overflow port under the action of an electromagnetic pump 3, natural gas uniformly enters from the bottom of a liquid metal cracking reactor 4, and is subjected to heat and mass transfer reaction with the liquid metal Sn under the action of a catalyst Fe10kg to crack the natural gas into hydrogen and cracked gas containing carbon black, wherein the cracking temperature is 800 ℃, and the cracked gas containing the carbon black is collected according to the liquid level of the liquid metal Sn.
(3) The pyrolysis gas containing a small amount of carbon black is input into a cyclone sub-cooler with a heat exchange structure, after the pyrolysis gas containing the carbon black and cooling water are subjected to partition wall heat exchange, the carbon black is separated under the action of self gas rotating centrifugal force, and hot water or steam generated after the cooling water and the pyrolysis gas are subjected to heat exchange can be output for utilization and can be used as hot water or steam for production and living.
(4) And cooling the pyrolysis gas from which the carbon black is separated to 230 ℃, then feeding the pyrolysis gas into a bag-type dust collector 6 for gas-solid separation, collecting more than 95% of the carbon black after the pyrolysis gas passes through a cyclone cooler and the bag-type dust collector 6, and reducing the temperature of the pyrolysis gas to 200-250 ℃.
(5) The cracked gas after temperature reduction and dust removal enters a condenser 7 to be continuously cooled, the temperature is reduced to below 50 ℃, and a small amount of carbon black is enriched in the condenser 7; the cracked gas cooled by the condenser 7 enters a Pressure Swing Adsorption (PSA) device 8 to separate hydrogen and hydrocarbon substances, and the yield of the hydrogen is 90%; the yield of the carbon black is 67 percent, and the hydrogen production cost is 20 yuan/kg. In order to further increase the cracking rate, the separated hydrocarbon substances can be returned to the liquid metal cracking reactor 4 for cracking again, so that the cracking rate of the natural gas is increased.
The hydrogen production cost of the invention compared with the prior art is as follows:
| hydrogen production technology | Efficiency of hydrogen production | Yield of carbon black | CO2Discharging | Cost of hydrogen production (Yuan/kg) |
| Natural gas steam reforming | 83％ | Is free of | Is provided with | 6.74～13.49 |
| Hydrogen production by electrolyzing water | 45％～55％ | Is free of | Is free of | 33.7～50 |
| Hydrogen production by natural gas pyrolysis of liquid metal | 90％～99％ | 70％～90％ | Is free of | 19～25 |
Although the existing hydrogen production technology by reforming natural gas steam has low hydrogen production cost, the produced CO is low2The emission is large, and the cost for treating carbon emission is far higher than the hydrogen production cost of the application, so that the hydrogen production efficiency and the hydrogen production cost of the application are better than those of the prior art relatively.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. A system for producing hydrogen by cracking natural gas with liquid metal is characterized by comprising a liquid metal melting tank, a liquid metal cracking reactor and a separator;
a support frame is arranged in the liquid metal cracking reactor, a uniform distribution structure for bearing liquid metal is arranged on the support frame, a natural gas inlet and a cracking gas outlet are arranged on the liquid metal cracking reactor, the cracking gas outlet is connected with a separator, and a carbon black outlet is arranged on the separator;
and the liquid metal melting tank is also provided with an overflow port connected with the liquid metal cracking reactor.
2. The system of claim 1, wherein an electromagnetic pump is connected between the liquid metal melting tank and the liquid metal cracking reactor.
3. The system of claim 1, wherein an electromagnetic heater is provided external to the liquid metal melting tank.
4. The system of claim 3, wherein the electromagnetic heater is heated by a heating mode comprising medium-frequency electromagnetic heating and high-frequency electromagnetic heating;
further, the frequency of the medium-frequency electromagnetic heating is 400HZ～10KHZ；
The frequency of the high-frequency electromagnetic heating is 10 KHz-40 KHZ。
5. The system of claim 1, wherein the liquid metal cracking reactor has a temperature of 700-1400 ℃.
6. The system according to claim 1, characterized in that the equipartition structure is provided with square grids and/or round holes;
the size of the square is 20-100 mm multiplied by 20-100 mm; the diameter of the round hole is 10-120 mm;
the uniform distribution structure is made of high-temperature ceramics.
7. The system of claim 1, wherein the separator comprises a plurality of cyclone coolers arranged in parallel;
a water-cooling jacket is arranged on the separator; a plurality of flow disturbing columns are uniformly distributed in the water-cooling jacket;
the temperature in the separator is 150-400 ℃.
8. The system of claim 1, wherein the outlet of the separator is further connected with a bag-type dust remover and a condenser in sequence, and the bag-type dust remover and the condenser are both provided with carbon black discharge ports,
the exhaust end of the condenser is also provided with a pressure swing absorber,
a recycling pipeline is also connected between the liquid metal cracking reactor and the pressure swing absorber.
9. The system of claim 8, wherein the temperature of the bag-type dust collector is 180-230 ℃;
the temperature of the condenser is less than or equal to 50 ℃.
10. The system of claim 1, wherein the liquid metal cracking reactor is further provided with a soot discharge.
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| CN202120835329.5U CN214880202U (en) | 2021-04-22 | 2021-04-22 | System for utilize liquid metal schizolysis natural gas hydrogen manufacturing |
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| CN202120835329.5U CN214880202U (en) | 2021-04-22 | 2021-04-22 | System for utilize liquid metal schizolysis natural gas hydrogen manufacturing |
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