Process and apparatus for the production of ethylene and / or other olefins by steam cracking

Abstract

A process (100) for the production of ethylene and / or other olefins by steam cracking is disclosed, wherein a paraffin-containing feed is charged to one or more crackers (10) and a raw gas is withdrawn from the one or more crackers (10), wherein the raw gas is at least partially subjected to a treatment (20) comprising a raw gas compression (22) and a thermal separation (23) using a C2 refrigerant and a C3 refrigerant, wherein a raw gas compressor (CGC) is used for the raw gas compression (22), wherein an ethylene refrigerant is compressed by using a C2 refrigerant compressor (ERC), and wherein a propylene refrigerant is compressed by using a C3 refrigerant compressor (PRC). The raw gas compressor (CGC) comprises two compressor trains in series, and wherein the compressor trains, the C2 refrigerant compressor (ERC) and the C3 refrigerant compressor (PRC) are each at least partially operated using an electric drive (M) having at least partially identical performance characteristics, in particular are each provided as structurally identical variable speed drives, and are each powered by a frequency converter (FU). The invention also relates to a corresponding apparatus.

Description

Technical Field

[0001] The present invention relates to a method and apparatus for producing ethylene and / or other olefins by steam cracking, according to the preamble of each independent claim. Background Technology

[0002] For example, the article "Ethylene" in the *Ulman Encyclopedia of Industrial Chemistry* (online edition, April 15, 2009, DOI 10.1002 / 14356007.a10_045.pub2) describes steam cracking methods and equipment for hydrocarbons. Steam cracking is primarily used to obtain short-chain olefins (such as ethylene and propylene), dienes (such as butadiene), or aromatics, but is not limited to obtaining these compounds.

[0003] During steam cracking, a mixture of components (also known as cracked gas or crude gas) is obtained. This mixture undergoes appropriate processing to obtain the desired individual components. Typically, in the first part of the corresponding processing flow (the front-end section), heavy compounds (if present) are removed, followed by so-called crude gas compression, acid gas removal, and drying. After the front-end processing comes fractionation, in which fractions are formed using a thermal separation process with ethylene or C2 refrigerant and propylene or C3 refrigerant, and further separation is performed if necessary. For more information, see the article "Ethylene" cited in the *Ulman Encyclopedia of Industrial Chemistry*, specifically Section 5.3.2.1 "Front-end Section" and Section 5.3.2.2 "Hydrocarbon Fractionation Section".

[0004] In one embodiment of the corresponding fractionation (also applicable to the context of this invention), fractionation first involves separating hydrocarbons with two carbon atoms and lower-boiling components (such as methane and hydrogen) from hydrocarbons with three carbon atoms and higher-boiling compounds. Such a step is also commonly referred to as deethanergating, and the corresponding fractionation configuration is called a “front-end deethanergating” or “deethanergating” method.

[0005] In the deethane removal process, the fraction of hydrocarbons with two carbon atoms and low-boiling-point components obtained in gaseous form can be fed into a further separation process, where the hydrocarbons with two carbon atoms are separated from the low-boiling-point components. This step is also called demethanization. Therefore, in the "pre-deethane" or "front-end deethane" method, demethanization occurs downstream of the deethane removal process.

[0006] In another method, the deethane and demethanization steps can also be performed in reverse order. This method is called "pre-demethanization" or "front-end demethanization." More method variations can be found in the cited technical documents.

[0007] As part of the corresponding processing flow, compressors are used in different locations. Specifically, a crude gas compressor (CGC) is used for crude gas compression, and so-called ethylene refrigerant compressors (ERC) and propylene refrigerant compressors (ERC) are used to supply ethylene or C2 refrigerant and propylene or C3 refrigerant. These terms are used below, but optionally, ethane may also be compressed in an ethylene refrigerant compressor, and propane may also be compressed in a propylene refrigerant compressor. The product fraction after thermal separation can be compressed by a separate compressor, namely a product compressor.

[0008] EP3730592A1 describes an olefin synthesis apparatus. The apparatus includes a feed pretreatment section for pretreating the feed stream; a pyrolysis section, including one or more pyrolysis reactors, for cracking hydrocarbons in the input stream in the presence of a diluent to produce a cracked gas stream. A primary fractionation and compression section is provided for providing heat recovery from the cracked gas stream and quenching the cracked gas stream, removing components from the cracked gas stream, and compressing the cracked gas stream to provide a compressed cracked gas stream. Alternatively or additionally, a product separation section may be provided for separating the product olefin stream from the compressed cracked gas stream. Compared to conventional olefin synthesis apparatuses, the construction of this olefin synthesis apparatus allows a majority and / or one or more portions of the energy and / or net energy required for the olefin synthesis apparatus to be provided by non-carbon-based and / or renewable energy sources and / or electricity.

[0009] The objective of this invention is to improve the corresponding methods and devices, and in particular, to configure them to suit the corresponding energy range of the location of the devices. Summary of the Invention

[0010] This objective is achieved by methods and apparatus for producing ethylene and / or other olefins by steam cracking, having the features of each of the independent claims. The embodiments are the subject matter of the dependent claims and the description below.

[0011] In general, the present invention proposes a method for producing ethylene and / or other olefins by steam cracking, wherein one or more crackers, i.e., cracking furnaces, are conventionally configured with convection and radiation zones, fed with a feed containing alkane, such as naphtha or ethane or a corresponding mixture or any other feed known or advantageous in the art, and crude gas is extracted from one or more crackers, wherein the crude gas undergoes at least partially processing including crude gas compression and thermal separation (23) using ethane and / or ethylene refrigerants (C2 refrigerants) and propane and / or propylene refrigerants (C3 refrigerants). In particular, the aforementioned refrigerants can be used to condense the gas mixture for boiling the tank evaporator of the separation tower or for use in the corresponding overhead condenser.

[0012] The terms "ethane and / or ethylene refrigerant," "C2 refrigerant," "propane and / or propylene refrigerant," or "C3 refrigerant" mentioned herein can refer to the respective pure substances or mixtures of the mentioned components. In each case, other components may also be present, typically in amounts less than 10%.

[0013] Within the scope of this invention, a crude gas compressor is used to compress the crude gas, a C2 refrigerant compressor is used to compress the C2 refrigerant, and a C3 refrigerant compressor is used to compress the C3 refrigerant. Further details of the corresponding methods will also be explained below by way of example, with explicit reference to the prior art cited at the beginning. As previously mentioned, the C2 refrigerant compressor and the C3 refrigerant compressor are also simply referred to as a C2 refrigerant compressor (ERC) or a C3 refrigerant compressor (PRC).

[0014] According to the present invention, the crude gas compressor comprises two compressor units in series, wherein each compressor unit, the C2 refrigerant compressor, and the C3 refrigerant compressor are operated at least partially by electric drives. To avoid misunderstanding, it should be noted that the statement that certain compressors or compressor units are "respectively" driven by electric drives should be understood to mean that one compressor unit is driven by a first electric drive, the other by a second electric drive, the C2 refrigerant compressor by a third electric drive, and the C3 refrigerant compressor by a fourth electric drive. In the present invention, one of the compressor units of the crude gas compressor, particularly the upstream compressor unit, comprises a two-stage compressor, and the other compressor unit particularly comprises a three-stage compressor. More generally, the compressor units comprise different numbers of compressor stages. As recognized according to the present invention, the operating method proposed in this invention has particular advantages compared to known drive methods in the prior art (e.g., condensing steam turbines according to API 612 or other standards). In this conventional operating mode, and the following description is not intended to limit the invention in any way, a cracker is configured, for example utilizing waste heat, to supply ultra-high pressure steam (HHP steam), i.e., steam with a pressure level of 90 to 130 bar and a temperature level of 450 to 540°C, for driving a crude gas compressor. The ultra-high pressure steam is typically expanded by the high-pressure section of the driving turbine of the crude gas compressor. Subsequently, most of the steam is extracted into high-pressure steam (HP steam), i.e., steam with a pressure of 35 to 50 bar and a temperature of 250 to 400°C, and supplied to the driving turbines of the C2 and C3 refrigerant compressors. Depending on other user requirements, medium-pressure steam (MP steam) or low-pressure steam (LP steam), i.e., steam with a pressure of 15 to 25 bar and a temperature of 200 to 250°C, or steam with a pressure of 3 to 8 bar and a temperature of 150 to 190°C, can also be produced. To improve overall energy balance, additional steam can be input from a high-pressure steam generator or an external source. In this case, a steam outlet for balancing can also be provided through the equipment boundary.

[0015] The energy balance of the conventional method described above must take into account the limitations imposed by the electricity demands of the three major consumers (i.e., the crude gas compressor, the C2 refrigerant compressor, and the C3 refrigerant compressor). This typically requires the installation of a high-pressure steam generator, consisting of a corresponding steam boiler, to decouple the ultra-high pressure and high-pressure steam demands and achieve energy balance. This increases structural complexity. Furthermore, much of the condensation heat of the steam is not utilized, and waste steam from the turbine is usually condensed via cooling water, increasing equipment costs. Using ultra-high pressure and high-pressure steam generators results in significant carbon dioxide emissions, and alternative energy sources (such as optional carbon dioxide neutral energy) are often unavailable or impossible to integrate to drive the compressors.

[0016] Using this invention allows for greater flexibility in the production of ethylene or other olefins in terms of steam and carbon dioxide balance, because the use of an electric drive significantly increases the independence of the compressor during operation. In particular, in this invention, the rigid coupling of using high-pressure steam when compressing crude gas and subsequently using high-pressure steam when compressing refrigerant no longer poses an obstacle to flexibility in the context of this invention.

[0017] According to a particularly preferred embodiment of the invention, ultra-high pressure steam is still provided using waste heat from one or more crackers. However, the ultra-high pressure steam is advantageously output at least partially from said equipment and / or used at least partially as a heat source for other process steps, rather than for driving the crude gas compressor, the C2 refrigerant compressor, and the C3 refrigerant compressor.

[0018] In a particularly preferred embodiment of the invention, or as an alternative to the measures proposed in the invention, the ultra-high pressure steam can be adapted in a adaptation unit (i.e., a so-called pressure reduction station) for pressure and / or temperature adjustment for output and / or intended use. In particular, any condensate heat generated in the adaptation unit can also be used for other purposes, such as feeding into a district heating network.

[0019] According to a particularly preferred embodiment, the method used in this invention can be carried out without the use of a high-pressure steam boiler. In other words, using this invention eliminates the need for a corresponding high-pressure steam boiler, thereby reducing the demand for fossil fuel carriers and thus improving the carbon dioxide balance. In principle, within the context of this invention, carbon dioxide-neutral energy sources can be added at any point, thus achieving considerable flexibility in terms of carbon dioxide footprint. As described above, the crude gas compressor of this invention comprises two compressor units in series, i.e., individually driven structural units, wherein each compressor unit of the crude gas compressor, the C2 refrigerant compressor, and the C3 refrigerant compressor are operated by electric actuators having at least partially identical performance characteristics. Advantageously, the electric actuators can also be substantially identical in structure. Thus, the number of shared components increases, and in the sense of standardization, the manufacture of the corresponding equipment is significantly improved.

[0020] Electric drives with at least partially identical performance characteristics are provided as structurally identical variable-speed drives, and these drives are each powered by a frequency converter. Each tandem compressor unit for crude gas compression, the C2 refrigerant compressor, and the C3 refrigerant compressor are adapted to each other in terms of torque. In this way, corresponding standardization can be achieved while simultaneously allowing for flexibility in speed. Specifically, four frequency converters can be provided, two or even all four of which are readily available to power the electric drives during equipment operation. A fifth frequency converter can be reserved for redundancy, particularly for necessary maintenance and / or repair work.

[0021] The use of this invention makes it possible to use machines with identical structures, particularly drives, thereby greatly simplifying the storage and maintenance of the (common) components required for these machines. This invention is based on the understanding that, despite the associated difficulties and corresponding concerns of experts, it is possible and advantageous to use drive devices with identical structures. Therefore, this invention particularly improves the manufacture and operation of the corresponding equipment, and the measures proposed according to this invention or its embodiments are not readily apparent in the prior art.

[0022] Because crude gas compressors, ethylene compressors, and propylene compressors differ significantly in performance, coordinating the performance of the drive is not easy. Furthermore, the performance ratio of ethylene and propylene compressors is variable, particularly dependent on feed and process management (separation of heavier hydrocarbons, especially those with five or more carbon atoms). Crude gas compressors typically consist of five stages, which appear indivisible. The pressure conditions of a crude gas compressor can only be varied within a limited range because high pressure conditions in a single stage can lead to high temperatures, thus posing a risk of scaling. Without understanding the embodiments of the invention, this hinders those skilled in the art from considering corresponding solutions.

[0023] In the context of embodiments of the invention, the crude gas compressor can be divided into two or three stages as described above, and changes in pressure conditions, particularly the use of external refrigeration, can occur within given limits, as provided in embodiments according to the invention. This, in turn, leads to the ideal loading of the propylene compressor, particularly the propylene compressor used therein, and thus also to the alignment of the propylene and ethylene compressors.

[0024] Without understanding the present invention or its corresponding embodiments, it would not be obvious to use a variable speed drive with the same structure, since not only power but also torque must be kept consistent. This means that the compressors must either rotate at similar speeds or a gear mechanism (for speed and torque conversion) must be used. Without consistent torque, even with the same power, the motors cannot be standardized. Therefore, in this example, one or more gear mechanisms are specifically used.

[0025] The advantage of this invention lies particularly in providing redundancy n+1 by using an additional frequency converter. In other embodiments of the invention, this can also be achieved using different frequency converters and / or drives, but corresponding adjustments are required in terms of efficiency, spare parts inventory, and size. Here, the additional frequency converter must correspond to the largest of the four commonly used frequency converters, which, without load coordination, will inevitably be greater than the average power of the four identical drives.

[0026] Four frequency converters can be installed in pairs with full redundancy (2 x 100%), where two of each pair can operate in parallel at partial load (2 x 50%) or at full load in switching mode (alternating) (1 x 100% in each case). In cases with two independent power supply networks, the frequency converters can be advantageously connected to both networks. This redundancy concept is particularly suitable if voltage drops / failures are anticipated in the power supply network and minimizing switching time is necessary to maximize equipment availability.

[0027] For high-power drives that exceed the performance limits of frequency converters, a 3x 50% redundancy concept can also be adopted, that is, two frequency converters operate in parallel to provide 100% of the total power.

[0028] In one embodiment of the method of the present invention, four frequency converters and a fifth frequency converter are provided as part of a frequency converter device, wherein the frequency converter device of the fifth frequency converter remains in an operational state during the execution of the method, particularly a hot standby state, i.e., at least partially powered, as will be explained below.

[0029] According to one embodiment, each inverter device includes an input transformer, particularly a VSD transformer, and inputs and outputs, wherein the inputs and outputs (inputs, particularly via the input transformer) are connected to a power supply and a corresponding drive via a switching unit. By selectively activating the switching unit at the output, the corresponding inverter can be selectively connected to that drive instead of other drives.

[0030] According to current standards, the mean time between failures (MTBF) or mean time to repair (MTTR) of a variable speed electric drive is approximately 10 years. However, due to the need for simultaneous operation of all three compressors (CGC, ERC, and PRC), availability is reduced (e.g., by reliability block diagrams), making it difficult to achieve the industry standard of 5 years of uninterrupted operation. However, the standardization of the drive allows key spare parts (sometimes necessary anyway) to be installed in a "cold standby" or "hot standby" state. Therefore, in the event of a failure, it is advantageous to switch between the corresponding units without (significant) delays. Thus, in the context of this invention, the mean time between failures (MTBF) or mean time to repair (MTTR) can be increased, for example, up to 20 years.

[0031] In the embodiments of the invention described above, the fifth frequency converter advantageously includes peripheral equipment (cooling, transformer, switching equipment), and is therefore pre-installed, ready for immediate use, and interconnected, serving as a redundant backup for each of the existing four frequency converters. For switching, temporary shutdown or stoppage (“cold standby”) can be considered. Alternatively, switching can also be performed during operation to minimize interruption of drive torque. A switching time of less than 500 milliseconds is technically feasible and desirable; in terms of control technology, the switching sequence can optionally be coupled with the compressor's pump protection control (feedforward signaling to the surge protection controller).

[0032] In embodiments of the invention, the corresponding transformers and frequency converters, especially so-called "capital spare parts," are provided during the installation of the respective equipment and remain continuously ready during operation. Therefore, they are already included in the investment cost.

[0033] If these spare parts are not placed in a warehouse as provided in the embodiments of the present invention, but are instead treated as "installed" spare parts, then these spare parts can be ready in a very short time, for example, within the aforementioned 500 milliseconds.

[0034] A particular advantage of this invention is that the crude gas compressor, the C2 refrigerant compressor, and the C3 refrigerant compressor can be installed on the ground, since the capacitor required for the base is not necessary.

[0035] Advantageously, external refrigeration can be used at least temporarily, for example, through intermediate cooling in the crude gas compressor using propane or propylene refrigeration (C3 refrigeration). In principle, this intermediate cooling can occur before each stage. Pre-cooling, particularly pre-cooling of the fourth stage, is especially advantageous because it achieves the same performance from the first to the third stages on the one hand, and the same performance from the fourth to the fifth stages on the other, while avoiding excessively high outlet temperatures. In this case, a different distribution of compressor stages and drivers than in the example above can be provided. This is particularly advantageous within the scope of the stated standardization. In the context of this invention, external refrigeration for intermediate cooling is provided using at least a portion of C2 and / or C3 refrigerants, i.e., the respective refrigerants are coupled from their respective refrigerant loops.

[0036] In embodiments of the invention, the aforementioned intercooling can be performed permanently, or (only) when the cooling water temperature and / or water injection is identified as insufficient and / or ineffective, external refrigeration can be used for intercooling. This optimizes operating costs.

[0037] In the context of this invention, in a particularly preferred embodiment, the drive power of the electric drives of the crude gas compressor, the C2 refrigerant compressor, and the C3 refrigerant compressor is regulated by the transfer of cooling capacity between the C2 refrigerant circuit and the C3 refrigerant circuit and / or by integrating C3 refrigeration as an additional intermediate cooling for the crude gas compressor, wherein C2 refrigerant is used in the C2 refrigerant circuit and C3 refrigerant is used in the C3 refrigerant circuit, thereby homogenizing the power demand as much as possible.

[0038] The present invention also relates to an apparatus for producing ethylene and / or other olefins by steam cracking, the apparatus having one or more crackers for being charged with an alkane-containing feedstock and providing crude gas, wherein the apparatus is used to subject the crude gas to at least partial treatment comprising compression and thermal separation using C2 and C3 refrigerants, wherein a crude gas compressor is used for crude gas compression, a C2 refrigerant compressor is used for C2 refrigerant compression, and a C3 refrigerant compressor is used for C3 refrigerant compression. For features of the invention, see the corresponding independent claims.

[0039] For the features and advantages of the corresponding devices and their embodiments, please refer to the explanations above regarding the methods and embodiments proposed in this invention, as these also apply to the devices and their embodiments. This is especially true for devices designed to implement the methods of the different embodiments described above.

[0040] The present invention will now be described in more detail with reference to the accompanying drawings, which illustrate embodiments of the invention. Attached Figure Description

[0041] exist Figure 1 The method of an embodiment of the present invention is illustrated in a simplified process flow diagram, and is generally indicated by 100. Although the following description refers to the method and corresponding method steps, it is equally applicable to the corresponding equipment and its components.

[0042] In method 100, one or more crackers (cracking furnaces) 10 are used, which are filled with feed A (and steam, not shown separately here), and crude gas B is taken out from said cracker.

[0043] The crude gas B undergoes at least partial processing, referred to herein as 20. This processing, in a manner known per se, includes a quenching step 21, separation of pyrolysis oil C, and compression (crude gas compression) 22, followed by thermal separation 23 using refrigerants C2 and C3. In the quenching step 21, vapor D can be provided and recycled to one or more crackers 10. In the compression process 22, for example, pyrolysis gasoline E can be separated and recycled back to the quenching step 21. In the quenching step 21, hydrocarbons F having three or more carbon atoms can be further separated and transferred to the corresponding processing step 24, where the corresponding hydrocarbon G can also be fed from the thermal separation 23. In the thermal separation 23, ethane stream H can be provided and recycled to one or more crackers 10. Ethylene stream I can be realized as a product. So-called tail gas K is discharged, specifically containing methane and hydrogen. Further product streams, referred to generally as L, are generated in other processing steps 24.

[0044] like Figure 1 As shown in the lower region, the compressor represented by CGC is used for crude gas compression 22, the refrigerant compressor represented by ERC (C2 refrigerant compressor) is used for ethylene refrigerant compression, and the refrigerant compressor represented by PRC (C3 refrigerant compressor) is used for propylene refrigerant compression. The crude gas compressor CGC, the refrigerant compressor ERC (C2 refrigerant compressor), and the refrigerant compressor PRC (C3 refrigerant compressor) are each operated at least partially using one or more electric drives M.

[0045] More specifically, in an embodiment of the invention, the crude gas compressor CGC comprises two compressor units in series (not shown separately), wherein each compressor unit, refrigerant compressor ERC (C2) and refrigerant compressor PRC (C3), is operated by an electric drive having at least partially identical performance characteristics. Here, the electric drives can be provided as structurally identical variable speed drives, each powered by a frequency converter FU. In general, five frequency converters FU are provided in this example, two (in paired full-load alternating operation) or four (in paired partial-load operation) are used to power the electric drive M at all times, with one redundantly on standby. In this example, the frequency converter FU is connected to different networks or power supplies N1, N2 as illustrated. The invention is not limited to the example shown herein.

[0046] The steam D or other steam provided in this method may particularly include ultra-high pressure steam, which is output and / or at least partially used as a heat source for other method steps, rather than for driving the crude gas compressor RGC, the C2 refrigerant compressor ERC, and the C3 refrigerant compressor PRC. The ultra-high pressure steam may be adapted in an adaptation unit, denoted herein as 50, for the pressure and / or temperature used for output and / or intended application. The condensation heat accumulated in the adaptation unit 50 may be used as described.

[0047] Regarding other embodiments of the present invention, all of these embodiments can also be used in Figure 1 In method 100 shown, please refer again to the above instructions.

[0048] Figure 2 An apparatus 200 according to an embodiment of the present invention is shown. Each element in the figure has multiple preferred identical elements, so each element is provided with only one corresponding reference numeral.

[0049] The input transformers (specifically the VSD transformers) are connected to bus 1 via switching device 2. Each input transformer is implemented by a frequency converter (represented here as 4), and specifically, as an indirect frequency converter (VSI) for DC voltage in the intermediate circuit. Each drive is again connected via switching device 5. When drive M is disconnected from the initially connected frequency converter via the corresponding switching device 5, a set of switching devices 2a and 5a shown on the left side of the figure, along with the input transformer 3a and frequency converter 4a, can be selectively connected to drive M via one of the switching devices 6. Switch 2a can remain closed throughout operation, thus keeping the input transformer 3a and frequency converter 4a in a "hot standby" state.

[0050] Figure 3 A device 300 according to another embodiment of the present invention is shown. Here, each element also has multiple preferred identical elements, so each element is provided with only one corresponding reference numeral.

[0051] and Figure 2 Compared to the device 200 shown, Figure 3 The device 300 shown illustrates a different redundancy concept, in which each driver M can be alternately connected to one of two sets of switching devices 2 and 5, input transformer 3 and frequency converter 4 (or 2a, 5a, 3a and 4a, respectively indicated only on the left driver M).

Claims

1. A method (100) for producing ethylene and / or other olefins by steam cracking, wherein, One or more crackers (10) are filled with a feed containing alkanes, and crude gas is extracted from the one or more crackers (10), wherein the crude gas undergoes at least partially a treatment (20), the treatment (20) comprising crude gas compression (22) and thermal separation (23) using C2 refrigerant and C3 refrigerant, wherein a crude gas compressor (CGC) is used for the crude gas compression (22), wherein the C2 refrigerant is compressed using a C2 refrigerant compressor (ERC), and wherein the C3 refrigerant is compressed using a C3 refrigerant compressor (PRC), characterized in that, The crude gas compressor (CGC) comprises two compressor units in series, and each of the compressor units, the C2 refrigerant compressor (ERC) and the C3 refrigerant compressor (PRC) is operated at least partially by an electric drive (M), the electric drives (M) having at least partially identical performance characteristics, being powered by a frequency converter (FU), and being provided as a variable speed drive with identical structure, wherein each of the series compressor units, the C2 refrigerant compressor (ERC) and the C3 refrigerant compressor (PRC) of the crude gas compressor (22) is identical to each other in terms of torque.

2. The method according to claim 1, wherein, Ultra-high pressure steam is obtained by using waste heat, and the ultra-high pressure steam is output and / or used at least partially as a heat source for other method steps, wherein the ultra-high pressure steam is not used to drive the crude gas compressor (CGC), the C2 refrigerant compressor (ERC), and the C3 refrigerant compressor (PRC).

3. The method according to claim 2, wherein, The ultra-high pressure steam is adapted in the adaptation unit (50) for pressure and / or temperature for output and / or intended use.

4. The method according to claim 3, wherein, The condensation heat obtained in the adaptation unit (50) is used.

5. The method according to claim 1, wherein the method is operated without using a high-pressure steam boiler.

6. The method according to claim 1, wherein, Four frequency converters (FUs) are provided, which are always available to supply power to the electric drive.

7. The method according to claim 6, wherein, Reserve the fifth frequency converter (FU) for redundancy.

8. The method according to claim 7, wherein, The four frequency converters (FU) and the fifth frequency converter (FU) are each provided as part of a frequency converter device, wherein the fifth frequency converter (FU) and its frequency converter device remain in an operational state during the execution of the method.

9. The method according to claim 8, wherein, Each of the frequency converter devices includes an input transformer and inputs and outputs, wherein the inputs and outputs are connected to a power supply and a corresponding driver via a switching unit.

10. The method according to claim 1, wherein, The crude gas compressor (CGC), the C2 refrigerant compressor (ERC), and the C3 refrigerant compressor (PRC) are located on the ground.

11. The method according to claim 1, wherein, External refrigeration is used, at least temporarily, for intermediate cooling in the crude gas compressor.

12. The method according to claim 11, wherein, The external cooling is provided using at least a portion of C2 refrigerant and / or C3 refrigerant for the intermediate cooling.

13. The method according to claim 11, wherein, When the cooling water temperature and / or water injection is identified as insufficient and / or ineffective, the external refrigeration is used for the intermediate cooling.

14. The method according to any one of the preceding claims, wherein, The drive power of the electric drives of the crude gas compressor (CGC), the C2 refrigerant compressor (ERC), and the C3 refrigerant compressor (PRC) is regulated by transferring cooling capacity between the ethylene refrigerant circuit and the propylene refrigerant circuit and / or by integrating propylene refrigeration as an additional intermediate cooling for the crude gas compressor (CGC), wherein ethylene refrigerant is used in the ethylene refrigerant circuit and propylene refrigerant is used in the propylene refrigerant circuit.

15. An apparatus for producing ethylene and / or other olefins by steam cracking, comprising one or more crackers (10) for receiving a feed containing alkane and for producing crude gas, wherein the apparatus is used to subject the crude gas to at least partially a treatment (20), the treatment (20) comprising compression (22) and thermal separation (23) using a C2 refrigerant and a C3 refrigerant, wherein a crude gas compressor (CGC) is used for crude gas compression (22), a C2 refrigerant compressor (ERC) is used for C2 refrigerant compression, and a C3 refrigerant compressor (PRC) is used for C3 refrigerant compression, characterized in that, The crude gas compressor (CGC) comprises two compressor units connected in series, and wherein, in order to provide at least a portion of the drive power for the two compressor units of the crude gas compressor (CGC), the C2 refrigerant compressor (ERC), and the C3 refrigerant compressor (PRC), electric drives (M) are provided respectively, the electric drives (M) having at least partially identical performance characteristics, being powered via frequency converters (FU), and being provided as variable speed drives with identical structures, wherein each of the series compressor units of the crude gas compressor (22), the C2 refrigerant compressor (ERC), and the C3 refrigerant compressor (PRC) is identical to each other in terms of torque.

16. The apparatus of claim 15, wherein the apparatus is used to perform the method of any one of the preceding claims.

Images