Apparatus and method for integrated separation of catalytic cracking and steam cracking

Abstract

The application discloses a device and method for catalytic cracking and steam cracking integration separation, which comprises a catalytic cracking system, a steam cracking system and a shared system; the catalytic cracking system comprises a catalytic cracking unit, a fractionation unit, a compression and pre-separation unit and a catalytic de-butane separation unit connected in sequence; the steam cracking system comprises a steam cracking unit, a quenching unit, a compression and front de-propane unit and a steam de-butane separation unit connected in sequence; the shared system comprises a carbon one cold separation unit, a carbon two cold separation unit and a carbon three hot separation unit connected in sequence; the carbon three outlet of the compression and pre-separation unit and the carbon three outlet of the compression and front de-propane unit are connected to the carbon one cold separation unit inlet. The technical scheme of the application reduces the number of equipment, reduces the land occupation, saves the investment, reduces the energy consumption, and can increase the carbon two recovery rate of catalytic cracking by 5-10 percent. Meanwhile, the products with large property difference are not mixed with each other, so that the economic benefits are maximized.

Description

Technical Field

[0001] This invention belongs to the field of olefin production equipment, and more specifically, relates to an apparatus and method for integrating and separating catalytic cracking and steam cracking. Background Technology

[0002] Currently, my country faces overcapacity in oil refining and oil product production, while traditional refineries are also impacted by new energy sources. Against the backdrop of "carbon peaking" and "carbon neutrality," the transformation of refineries towards chemical processing is an inevitable path for sustainable development. The integration of refining and chemical processing requires not only addressing the primary contradictions and resolving them, but also paying close attention to the specific characteristics of these contradictions to achieve optimal process configuration.

[0003] There are currently two known methods for integrating and separating catalytic cracking and steam cracking.

[0004] One type is a catalytic cracking unit that uses traditional oil absorption and separation processes such as fractionation, absorption stabilization, dual desulfurization, and gas separation to separate its various heavy products of C3 and above. The light components of C2 and below are produced as a mixture, i.e., catalytic dry gas. The specific process flow is as follows: Figure 1 As shown. Early catalytic dry gas was used as refinery fuel gas, with very low utilization value. Later, it was effectively utilized using the ethylene-to-ethylbenzene / styrene technology, but its application was limited. Subsequently, after impurity removal and C2 enrichment processes such as pressure swing adsorption and shallow-cooled oil absorption, the catalytic dry gas was sent to ethylene units (i.e., steam cracking units) for recovery to increase the production of polymerization-grade ethylene. However, in the oil absorption separation of catalytic dry gas and the C2 enrichment processes in various processes, the C2 component is generally lost by 5-15%, and the recovery rate needs to be improved. This fusion separation method, tentatively called fusion, has a very limited actual degree of fusion.

[0005] Another approach is in heavy oil catalytic thermal cracking (CPP) and naphtha catalytic cracking (such as K-COT) units, where the "reaction-regeneration + fractionation" process of catalytic cracking is separated from the "cracking unit + quench zone" of steam cracking. From the compression of rich gas / cracking gas, the separation system is fully integrated, forming an integrated "two-end-one-tail" structure. The specific process flow is as follows: Figure 2 As shown.

[0006] This fusion separation method achieves the highest level of integration, completely mixing and separating pyrolysis gasoline and its lighter components, resulting in the greatest reduction in the number of equipment units, plant space, and investment. However, it has the following drawbacks: First, catalytic cracking products contain more impurities and very little alkyne / diolefins, while steam cracking products generally contain fewer impurities and more alkyne / diolefins. Mixing them increases the amount of impurities that need to be processed and the required equipment. Second, the compositions of catalytic C4 and steam cracking C4, and catalytic gasoline and steam cracking gasoline, differ significantly. The latter contains a large amount of dienes / alkynes, and mixing them severely affects the fate of these two steam cracking products, reducing their utilization value.

[0007] Therefore, this fusion method is only suitable for situations where steam cracking is used as a supplement, the cracking feedstock is relatively light, there are few heavy products of C3 and above, and all C4 products and gasoline products are used as catalytic products. Summary of the Invention

[0008] To address the problems existing in the prior art, the purpose of this invention is to provide a novel integrated separation solution. This solution aims to maximize the integration and separation of common products, improve product recovery rate, and reduce investment; while also separating products with different properties separately so as not to interfere with each other, thereby maximizing economic benefits.

[0009] To achieve the above objectives, the first aspect of the present invention provides an apparatus for integrating and separating catalytic cracking and steam cracking, the apparatus comprising: a catalytic cracking system, a steam cracking system, and a shared system;

[0010] The catalytic cracking system includes a catalytic cracking unit, a fractionation unit, a compression and pre-fractionation unit, and a catalytic butane removal and separation unit connected in sequence.

[0011] The steam cracking system includes a steam cracking unit, a quenching unit, a compression and pre-propane removal unit, and a steam butane removal separation unit connected in sequence.

[0012] The shared system includes a C1 cold separation unit, a C2 cold separation unit, and a C3 hot separation unit connected in sequence.

[0013] The C3 outlet of the compression and pre-separation unit and the C3 outlet of the compression and pre-propane removal unit are both connected to the inlet of the C1 cold separation unit.

[0014] A second aspect of the present invention provides a method for integrating and separating catalytic cracking and steam cracking, the method comprising the following steps:

[0015] (1) Catalytic cracking feedstock oil is catalytically cracked to obtain reaction oil gas, the reaction oil gas is fractionated to obtain light hydrocarbon components, the light components are compressed, impurities are removed and pre-separated to obtain light components A of C3 and below and heavy components A of C4 and above.

[0016] (2) The C4 and above heavy component A is sent to the catalytic butane removal separation unit for separation;

[0017] (3) Steam cracking feedstock oil is steam cracked to obtain cracked gas, and the cracked gas is rapidly cooled, compressed, impurity removed and pre-ethane separation to obtain light components B of C3 and below and heavy components B of C4 and above.

[0018] (4) The C4 and above heavy component B is sent to the steam debutane separation unit for separation;

[0019] (5) The light components A and B of C3 and below are combined and sent to the C1 cold separation unit for separation to obtain C2 / C3 fraction. The obtained C2 / C3 fraction is sent to the C2 cold separation unit for separation to obtain C3 fraction. The C3 fraction is sent to the C3 hot separation unit for further separation.

[0020] The effects of this invention are:

[0021] (1) In this invention, the light components of C3 and below separated are integrated and separated in a unified manner, including a pre-cooling and C1 cold separation zone, a C2 cold separation zone, and a C3 hot separation zone. The original propylene refrigeration system and ethylene refrigeration system of the ethylene plant are shared by the two plants, as well as utilities such as waste heat, steam, and circulating cooling water. In this invention, the heavy components of C4 and above obtained by catalytic cracking and steam cracking are still separated independently, and the product quality remains unchanged.

[0022] (2) In the present invention, the catalytic cracking and steam cracking products with different properties (heavy products such as C4 and gasoline) are separated independently and do not mix with each other, so as to facilitate the direct separation and recycling of high-value-added components with concentrated concentrations in each product, thereby maximizing economic benefits.

[0023] (3) This invention optimizes and adjusts the treatment method of light hydrocarbon components in catalytic cracking, and appropriately integrates the separation process of catalytic cracking and steam cracking. Light components such as hydrogen, methane, ethylene, ethane, propylene and propane in catalytic cracking are separated together with the common components of the ethylene unit. Among them, the concentration of hydrogen + nitrogen (H2 + N2) in crude hydrogen is ≥95mol%, methane tail gas is used as fuel, ethylene purity (≥99.95mol%) reaches the polymerization grade, propylene purity (≥99.6mol%) reaches the chemical polymerization grade, and ethane / propane is returned to the steam cracking furnace for recycling cracking to increase the production of ethylene / propylene.

[0024] (4) Compared with the conventional method of oil absorption and separation and catalytic dry gas enrichment and recovery, the present invention can maximize the recovery of high value-added C2 components in catalytic cracking, and its recovery rate can be increased by at least 5-10 percentage points to more than 99.6%; at the same time, it can appropriately reduce the number of equipment, reduce the footprint, and reduce investment; and the scale of the ethylene plant integration unit is more conducive to giving full play to its scale effect.

[0025] Other features and advantages of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0026] The above and other objects, features and advantages of the present invention will become more apparent from the more detailed description of exemplary embodiments of the invention in conjunction with the accompanying drawings.

[0027] Figure 1 This is a process flow diagram of the existing conventional catalytic cracking and steam cracking fusion separation method.

[0028] Figure 2 This is a process flow diagram of the existing fusion separation method of catalytic cracking and steam cracking.

[0029] Figure 3 This is a process flow diagram of a method for integrating and separating catalytic cracking and steam cracking according to the present invention. Detailed Implementation

[0030] Preferred embodiments of the invention will now be described in more detail. While preferred embodiments of the invention are described below, it should be understood that the invention can be implemented in various forms and should not be limited to the embodiments set forth herein.

[0031] This invention provides an apparatus for integrating and separating catalytic cracking and steam cracking, the apparatus comprising: a catalytic cracking system, a steam cracking system, and a shared system;

[0032] The catalytic cracking system includes a catalytic cracking unit, a fractionation unit, a compression and pre-fractionation unit, and a catalytic butane removal and separation unit connected in sequence.

[0033] The steam cracking system includes a steam cracking unit, a quenching unit, a compression and pre-propane removal unit, and a steam butane removal separation unit connected in sequence.

[0034] The shared system includes a C1 cold separation unit, a C2 cold separation unit, and a C3 hot separation unit connected in sequence.

[0035] The C3 outlet of the compression and pre-separation unit and the C3 outlet of the compression and pre-propane removal unit are both connected to the inlet of the C1 cold separation unit.

[0036] In this invention, the catalytic cracking reaction-regeneration furnace and the steam cracking furnace, i.e., the "two heads", are still separate.

[0037] In this invention, the fluidized bed reaction products of catalytic cracking contain catalyst powder and include carbon dioxide (CO2), hydrogen sulfide (H2S), organic sulfur, and nitrogen oxides (NO). x The catalytic cracking gas contains various impurities, such as water vapor, alkynes / dienes, small amounts of carbon dioxide (CO2) and hydrogen sulfide (H2S), and very few other impurities. Therefore, the fractionation, compression, and impurity removal / pre-fractionation units of catalytic cracking are still set up separately from the quenching, compression, and pre-ethane removal and pre-hydrogenation units of steam cracking.

[0038] In this invention, pre-separation refers to the separation of catalytic cracking or steam cracking before entering the C1 cold separation unit. Pre-separation can adopt a sequential pre-propane removal process. The separation processes used for catalytic cracking and steam cracking can be the same or different. Here, catalytic cracking and steam cracking use similar separation processes, but the operating values ​​(pressure, temperature) will vary depending on the composition.

[0039] According to the present invention, the ethane outlet of the C2 cold separation unit and the propane outlet of the C3 hot separation unit are connected to the steam cracking unit.

[0040] According to the present invention, the catalytic cracking unit is selected from any one of a fluidized catalytic cracking unit, a deep catalytic cracking unit, a heavy oil high-efficiency catalytic cracking unit, and a heavy oil catalytic thermal cracking unit.

[0041] This invention also provides a method for integrating and separating catalytic cracking and steam cracking, the method comprising the following steps:

[0042] (1) Catalytic cracking feedstock oil is catalytically cracked to obtain reaction oil gas, the reaction oil gas is fractionated to obtain light hydrocarbon components, the light components are compressed, impurities are removed and pre-separated to obtain light components A of C3 and below and heavy components A of C4 and above.

[0043] (2) The C4 and above heavy component A is sent to the catalytic butane removal separation unit for separation;

[0044] (3) Steam cracking feedstock oil is steam cracked to obtain cracked gas, and the cracked gas is rapidly cooled, compressed, impurity removed and pre-ethane separation to obtain light components B of C3 and below and heavy components B of C4 and above.

[0045] (4) The C4 and above heavy component B is sent to the steam debutane separation unit for separation;

[0046] (5) The light components A and B of C3 and below are combined and sent to the C1 cold separation unit for separation to obtain C2 / C3 fraction. The obtained C2 / C3 fraction is sent to the C2 cold separation unit for separation to obtain C3 fraction. The C3 fraction is sent to the C3 hot separation unit for further separation.

[0047] According to the present invention, the catalytic debutane separation unit separates C4 fraction and catalytic cracked gasoline product; the vapor debutane separation unit separates mixed C4 and crude cracked gasoline product.

[0048] Catalytic cracking and steam cracking produce products with different properties (heavy products such as C4 and gasoline) and separate them independently without backmixing. This allows for the direct separation and recycling of high-value-added components with concentrated concentrations in each product, maximizing economic benefits.

[0049] According to the present invention, the C2 cold separation unit also separates polymer-grade ethylene and ethane.

[0050] The C3 fraction is separated into polymer-grade propylene and propane in the C3 thermal separation unit.

[0051] Preferably, the method further includes the following steps:

[0052] (6) The propane separated by the C3 thermal separation unit and the ethane separated by the C2 cold separation unit are sent back to the steam cracking unit for cyclic cracking.

[0053] The separated light components of C3 and below are integrated and separated in a unified manner, including the pre-cooling and C1 refrigeration separation zone, the C2 refrigeration separation zone, and the C3 thermal separation zone. The original propylene refrigeration system and ethylene refrigeration system of the ethylene plant are shared by the two plants, as well as waste heat, steam, circulating cooling water, and other utilities.

[0054] By optimizing and adjusting the treatment method of light hydrocarbon components in catalytic cracking and appropriately integrating the separation processes of catalytic cracking and steam cracking, light components such as hydrogen, methane, ethylene, ethane, propylene, and propane in catalytic cracking are separated from common components in the ethylene unit. Specifically, the concentration of hydrogen + nitrogen (H2 + N2) in crude hydrogen is ≥95mol%, methane tail gas is used as fuel, ethylene purity (≥99.95mol%) reaches the polymerization grade, propylene purity (≥99.6mol%) reaches the chemical polymerization grade, and ethane / propane is returned to the steam cracking furnace for recycling cracking to increase ethylene / propylene production.

[0055] According to the present invention, the pre-separation adopts a cryogenic separation process with pre-propane removal.

[0056] The pre-propane removal process employs a cryogenic separation process involving pre-propane removal followed by pre-hydrogenation.

[0057] Preferably, the catalytic cracking reaction oil and gas are further fractionated to obtain oil slurry and cracked light oil components.

[0058] After rapid cooling, the cracked gas from steam cracking yields cracked diesel and cracked fuel oil components.

[0059] Preferably, the carbon-cold separation unit also separates crude hydrogen and methane.

[0060] The present invention will be described in more detail below through embodiments.

[0061] Comparative Example

[0062] Adopting such Figure 1The process flow shown is a conventional fusion separation of catalytic cracking and steam cracking. A petrochemical DCC with a capacity of 2.4 million tons / year of heavy oil and other feedstocks produces oil and gas from catalytic cracking. After the fractionation unit removes heavy fractions such as slurry and light diesel, the rich gas and crude gasoline enter the absorption and stabilization unit to separate catalytic gasoline. The light gas / liquid fraction undergoes dual desulfurization to obtain desulfurized catalytic dry gas and liquefied petroleum gas (LPG). The LPG is sent to a gas separation unit to separate propylene products, propane, and catalytic C4, etc. The catalytic dry gas is processed by a dry gas recovery unit to obtain enriched ethylene-rich gas and methane / hydrogen tail gas. The propane and ethylene-rich gas are sent to the steam cracking unit as feedstock. Meanwhile, a certain petrochemical 600,000-ton / year ethylene unit (i.e., steam cracking unit) mainly uses naphtha and other raw materials. The cracked gas obtained from steam cracking is separated into heavy products such as cracked fuel oil (PFO), cracked diesel (PGO) and heavy cracked gasoline by a quench unit. After the cracked gas is compressed, cold separated and hot separated, products such as crude hydrogen, methane tail gas, polymer-grade ethylene, polymer-grade propylene, mixed C4 and crude cracked gasoline can be obtained.

[0063] Example

[0064] Adopting such Figure 3 The apparatus shown is for the separation of light hydrocarbons, and includes: a catalytic cracking system, a steam cracking system, and a shared system;

[0065] The catalytic cracking system includes a catalytic cracking unit, a fractionation unit, a compression and pre-fractionation unit, and a catalytic butane removal and separation unit connected in sequence.

[0066] The steam cracking system includes a steam cracking unit, a quenching unit, a compression and pre-propane removal unit, and a steam butane removal separation unit connected in sequence.

[0067] The shared system includes a C1 cold separation unit, a C2 cold separation unit, and a C3 hot separation unit connected in sequence.

[0068] The C3 outlet of the compression and pre-separation unit and the C3 outlet of the compression and pre-propane removal unit are both connected to the inlet of the C1 cold separation unit.

[0069] The process flow of the integrated light hydrocarbon separation method in this embodiment is as follows:

[0070] (1) The light hydrocarbon components obtained after catalytic cracking fractionation are compressed, impurities are removed, and pre-separated. The pre-separation adopts a cryogenic separation process route with pre-propane removal. The heavy components of C4 and above separated by the compression and pre-separation unit are sent to the butane removal tower of the catalytic cracking unit to separate catalytic C4 and catalytic cracked gasoline products.

[0071] (2) The light components of C3 and below separated from the catalytic cracking pre-separation unit are combined with the light components of C3 and below separated from the steam cracking pre-propane dehydrogenation unit and then undergo pre-cooling, demethanizing, deethanering, ethylene distillation, C3 hydrogenation and propylene distillation similar to those of an ethylene plant to obtain crude hydrogen, methane tail gas, polymer-grade ethylene and chemical-grade polymer-grade propylene.

[0072] (3) After the steam cracking cracked gas is rapidly cooled, a deep cryogenic process route of compression and pre-propane dehydrogenation is adopted. The heavy components of C4 and above separated by the compression unit and the pre-propane dehydrogenation unit are sent to the steam cracking debutane tower to separate chemical mixed C4 and crude cracked gasoline.

[0073] (4) The separated ethane and propane are sent back to the ethylene cracking furnace for circulating steam cracking to increase the yield of ethylene and propylene.

[0074] In this embodiment, the two units of catalytic cracking and fractionation, and steam cracking and quenching remain unchanged (i.e., the light diesel oil and slurry oil of catalytic cracking and the cracked diesel oil and cracked fuel oil of the ethylene unit remain unchanged).

[0075] Test Example 1

[0076] The yields of the main products from the catalytic cracking and steam cracking fusion separation processes in the examples and comparative cases were tested. The product yields were measured in tens of thousands of tons per year. The yield comparisons of the main products are shown in Table 1.

[0077] Table 1 Comparison of Production Volume of Major Products

[0078]

[0079] As shown in Table 1, using a conventional separation process, the dry gas from catalytic cracking needs to be enriched with C2 before it can be recovered in the ethylene unit. The enrichment and recovery methods include pressure swing adsorption (PSA) and oil absorption, with C2 recovery rates ranging from 85% to 95%. In any case, some ethylene and ethane will be lost to the methane / hydrogen tail gas.

[0080] Using the device integration method described in this embodiment, hydrogen produced by catalytic cracking can also be directly recovered from the crude hydrogen in the ethylene plant, increasing crude hydrogen production (from 25,200 tons / year to 34,800 tons / year), while the total hydrogen + nitrogen (H2 + N2) content remains at around 95 mol%. The C2 recovery rate can be increased to over 99.6%, almost completely recovering the ethylene, thus increasing ethylene production. This could result in at least an additional 12,000 tons of ethylene produced annually, equivalent to an economic benefit of over 100 million yuan. Furthermore, all of this can be used to produce chemical-grade polymer-grade propylene.

[0081] Test Example 2

[0082] The number of equipment units required for the fusion separation process of catalytic cracking and steam cracking in the examples and comparative examples was compared and tested. The equipment unit number comparison test data is shown in Table 2.

[0083] Table 2 Comparison Test of Equipment Quantity

[0084]

[0085] As shown in Table 2, the main changes to the integrated units after integration using the embodiment method are the absorption stabilization, dual desulfurization, C2 recovery, and gas separation of the catalytic cracking unit, and the scaling up of the cold separation, hot separation, and refrigeration systems of the ethylene unit. Compared with conventional separation, the embodiment can reduce the number of equipment by approximately 164 units, accounting for more than 20% of the total equipment in the two sets of units.

[0086] Test Example 3

[0087] The investment and land occupation of the fusion separation process of catalytic cracking and steam cracking in the examples and comparative examples were compared. The investment was in hundreds of millions of yuan and the land occupation was in hectares. The data comparing investment and land occupation are shown in Table 3.

[0088] Table 3 Comparison of Investment and Land Acquisition

[0089] Comparative Example Example Investment, 100 million yuan 40.4 38.4 Save on investment, 100 million yuan 2.0 Area, hectares 16.1 13.7 Saves land area, hectares 2.4

[0090] As can be seen from Table 3, the implementation example saves approximately 200 million yuan in investment and about 2.4 hectares of land, which are about 5% and 15% less than the traditional separation method, respectively.

[0091] Test Example 4

[0092] The energy consumption required for the fusion separation process of catalytic cracking and steam cracking in the examples and comparative examples was compared and tested.

[0093] In terms of energy consumption, due to the increased recovery rate of products such as ethylene and the increase in product output, the unit energy consumption based on ethylene products will decrease by 2.7%.

[0094] The various embodiments of the present invention have been described above. These descriptions are exemplary and not exhaustive, nor are they limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. An apparatus for catalytically cracking integrated with steam cracking separation, characterized in that, The device includes: a catalytic cracking system, a steam cracking system, and a shared system; The catalytic cracking system includes a catalytic cracking unit, a fractionation unit, a compression and pre-fractionation unit, and a catalytic butane removal and separation unit connected in sequence. The steam cracking system includes a steam cracking unit, a quenching unit, a compression and pre-propane removal unit, and a steam butane removal separation unit connected in sequence. The shared system includes a C1 cold separation unit, a C2 cold separation unit, and a C3 hot separation unit connected in sequence. The C3 outlet of the compression and pre-separation unit and the C3 outlet of the compression and pre-propane removal unit are both connected to the inlet of the C1 cold separation unit. The ethane outlet of the C2 cold separation unit and the propane outlet of the C3 hot separation unit are connected to the steam cracking unit.

2. The apparatus of claim 1, wherein, The catalytic cracking unit is selected from any one of a fluidized catalytic cracking unit, a deep catalytic cracking unit, and a heavy oil catalytic thermal cracking unit.

3. A process for the integrated separation of catalytic cracking and steam cracking using the apparatus of any one of claims 1-2, characterized in that, The method includes the following steps: (1) The catalytic cracking feedstock oil is catalytically cracked in the catalytic cracking unit to obtain reaction oil gas. The reaction oil gas is fractionated in the fractionation unit to obtain light hydrocarbon components. The light hydrocarbon components are compressed, impurities are removed and pre-separated in the compression and pre-separation unit to obtain light components A of C3 and below and heavy components A of C4 and above. (2) The C4 and above heavy component A is sent to the catalytic butane separation unit for separation; (3) The steam cracking feedstock oil is steam cracked in the steam cracking unit to obtain cracked gas. The cracked gas is then rapidly cooled, compressed, impurity removed and ethane separated in the rapid cooling unit, compression and pre-propane removal unit to obtain light components B of C3 and below and heavy components B of C4 and above. (4) The heavy component B of C4 and above is sent to the steam debutane separation unit for separation; (5) The light components A and B of C3 and below are combined and sent to the C1 cold separation unit for separation to obtain C2 / C3 fraction. The C2 / C3 fraction is sent to the C2 cold separation unit for separation to obtain C3 fraction. The C3 fraction is sent to the C3 hot separation unit for further separation. (6) The propane separated by the C3 thermal separation unit and the ethane separated by the C2 cold separation unit are sent back to the steam cracking unit for cyclic cracking.

4. The method of claim 3, wherein, The catalytic debutane separation unit separates C4 fraction and catalytic cracked gasoline product; the steam debutane separation unit separates mixed C4 and crude cracked gasoline product.

5. The method of claim 4, wherein, The C2 cold separation unit also separates polymer-grade ethylene and ethane; The C3 fraction is separated into polymer-grade propylene and propane in the C3 thermal separation unit.

6. The method according to claim 3, characterized in that, The pre-separation process employs a cryogenic separation process involving pre-propane removal. The pre-propane removal process employs a cryogenic separation process involving pre-propane removal followed by pre-hydrogenation.

7. The method according to claim 3, characterized in that, The reacted oil and gas were further fractionated to obtain oil slurry and cracked light oil components. The pyrolysis gas, after rapid cooling, yields pyrolysis diesel and pyrolysis fuel oil components.

8. The method according to claim 3, characterized in that, The carbon-1 cold separation unit also separates crude hydrogen and methane.

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