A device for capturing carbon dioxide in industrial flue gases

Abstract

The application provides a carbon dioxide capturing device in industrial flue gas, comprising a carbon dioxide supercritical Rankine cycle system, an organic Rankine cycle system, a carbon dioxide liquefaction process and an LNG regasification process, which utilizes LNG cold energy coupling multi-tube heat exchangers, combines with low-energy-consumption LNG cold energy carbon capturing technology research, breaks through the technical bottleneck of existing LNG cold energy utilization technology such as cold energy air separation and cold energy power generation, researches the realization of low-temperature, low-pressure and low-energy-consumption liquefaction of carbon dioxide by using LNG cold energy, realizes intermediate energy conversion power generation, reduces investment cost and improves production capacity.

Description

Technical Field

[0001] This invention relates to a carbon dioxide capture device in industrial flue gas, belonging to the fields of LNG cold energy utilization and carbon capture in flue gas technology. Background Technology

[0002] Existing LNG receiving terminals contain combustion emission equipment such as multi-pass heat exchangers, gas-fired boilers, and flares. The combustion of natural gas produces carbon dioxide emissions. LNG receiving terminals also possess a significant amount of LNG cold energy. Current cold energy utilization technologies are limited to cold energy air separation and cold energy power generation, failing to achieve cascaded utilization of this cold energy. Therefore, research into carbon capture technology for LNG receiving terminals is necessary. Based on an analysis of the current status of carbon capture technologies both domestically and internationally, and simultaneously overcoming the bottlenecks in existing LNG cold energy utilization technologies such as cold energy air separation and cold energy power generation, the development of low-energy carbon dioxide capture technology for LNG receiving terminals is urgently needed to contribute to energy conservation and emission reduction. Summary of the Invention

[0003] To address the aforementioned technical problems, this invention provides a carbon dioxide capture device for industrial flue gas. This device utilizes an LNG cold energy coupled multi-pass heat exchanger and combines it with research on low-energy LNG cold energy carbon capture technology. It breaks through the bottlenecks of existing LNG cold energy utilization technologies such as cold energy air separation and cold energy power generation. The research explores the use of LNG cold energy to achieve low-temperature, low-pressure, and low-energy liquefaction of carbon dioxide, realizes intermediate energy conversion for power generation, reduces investment costs, and improves production capacity.

[0004] To achieve the above objectives, the present invention adopts the following technical solution:

[0005] A carbon dioxide capture device for industrial flue gas includes:

[0006] The device of this invention consists of two circulation systems and two phase change processes: a supercritical carbon dioxide Rankine cycle system, an organic Rankine cycle system, a carbon dioxide liquefaction process, and an LNG regasification process. Each circulation system and phase change process has a different function and can independently achieve its corresponding function, but they are interconnected through heat exchange equipment. In the carbon dioxide liquefaction process, after the flue gas enters the device, it is treated to liquefy the carbon dioxide in the flue gas and separate the liquid carbon dioxide from the remaining waste gas.

[0007] In the carbon dioxide liquefaction process, industrial flue gas enters a primary evaporator and a secondary evaporator, where it is heated by the supercritical Rankine cycle and organic Rankine cycle of carbon dioxide. After being cooled to a gas-liquid mixture by a condenser, it enters a primary separator to separate the liquid water. The flue gas with the separated liquid water then enters a primary heat exchanger for heat exchange and passes through a secondary separator for further gas-liquid separation. The carbon dioxide with the separated water enters a multi-pass heat exchanger and is cooled to a liquid state by LNG. Subsequently, the liquid carbon dioxide mixed with the exhaust gas undergoes a cyclone separator to achieve gas-liquid separation. The liquid carbon dioxide is recovered and reused from the bottom outlet, while the exhaust gas is discharged from the top outlet, thus completing the carbon dioxide liquefaction and separation process in the flue gas.

[0008] The LNG regasification process utilizes an LNG cold energy cascade utilization system to achieve a step-by-step cooling process for LNG, and after completing the cold energy exchange, it is gasified into natural gas.

[0009] The LNG regasification process involves the LNG being pressurized by a primary pressurization pump and then entering a multi-pass heat exchanger where carbon dioxide from the secondary separator is condensed into a low-temperature, low-pressure liquid. The LNG then enters the primary heat exchanger to exchange heat with carbon dioxide hydrate and organic working fluid, gradually vaporizing into natural gas. This process completes the LNG regasification.

[0010] The multi-pass heat exchanger includes a closed shell and staggered carbon dioxide cooling pipes, flue gas cooling pipes, and LNG pipes arranged inside the shell. The carbon dioxide cooling pipes and flue gas cooling pipes form the heat exchange tube bundle within the multi-pass heat exchanger. The LNG pipe inlet is connected to the first-stage pressurization pump, and the outlet is connected to the first-stage heat exchanger. The flue gas cooling pipe inlet is connected to the flue gas from the outlet of the second-stage separator, and the outlet of the flue gas cooling pipe is connected to the inlet of the cyclone separator. The carbon dioxide cooling pipe inlet is connected to gaseous carbon dioxide from the first-stage regenerator, which is condensed into liquid carbon dioxide by LNG and transported from the outlet of the carbon dioxide cooling pipe to the second-stage pressurization pump.

[0011] Furthermore, the carbon dioxide cooling pipes and the flue gas cooling pipes are arranged in a cross shape in space.

[0012] The supercritical Rankine cycle system for carbon dioxide utilizes the phase change process of carbon dioxide for heat exchange and expansion work to achieve supercritical Rankine cycle power generation.

[0013] The supercritical Rankine cycle system for carbon dioxide involves condensing carbon dioxide into a low-temperature, low-pressure saturated liquid by LNG in a multi-pass heat exchanger. The liquid is then pressurized by a secondary pressurization pump and heated by another secondary pressurization pump before being fed into a primary evaporator where it is reheated to a high-temperature, high-pressure gas. After passing through a primary expander, the gas performs work, driving a generator to produce electricity. The gas, after being cooled and depressurized, first enters a primary regenerator for precooling before returning to the multi-pass heat exchanger to exchange heat with LNG, thus forming a closed supercritical Rankine cycle system for carbon dioxide.

[0014] In the organic Rankine cycle system, the organic working fluid exchanges heat with flue gas and LNG to achieve energy storage and release, enabling the expander to generate electricity.

[0015] In the organic Rankine cycle system, the organic working fluid is pressurized by a three-stage pressurization pump, preheated by a two-stage regenerator, and then enters a two-stage evaporator where it is heated into a high-temperature, high-pressure gas. After that, it enters a two-stage expander to do work, driving a generator to generate electricity. The low-pressure gas after doing work first returns to the two-stage regenerator for precooling, and then passes through a first-stage heat exchanger to exchange heat with low-temperature natural gas. Finally, it returns to the three-stage pressurization pump to complete the entire organic Rankine cycle process.

[0016] The organic working fluid can be a series of organic working fluids with high latent heat of vaporization and specific heat ratio, such as R245fa.

[0017] All pipelines and equipment in the supercritical Rankine cycle system, organic Rankine cycle system, carbon dioxide liquefaction process, and LNG regasification process are insulated or cooled.

[0018] At least one visualization window is provided on the shell of the multi-pass heat exchanger, the carbon dioxide cooling pipe, the flue gas cooling pipe, or the cyclone separator.

[0019] The present invention has the following advantages due to the adoption of the above technical solutions:

[0020] (1) The technical solution of the present invention designs a multi-pass heat exchanger with an internal tube bundle forming a pipe network, which provides a possibility for breaking through the technical bottleneck of LNG cold energy utilization in existing cold energy air separation and cold energy power generation, realizing the concept of LNG cold energy cascade utilization and full utilization of LNG cold energy.

[0021] (2) The technical solution of the present invention couples the supercritical Rankine cycle system and the organic Rankine cycle system into the process route of capturing carbon dioxide from flue gas using LNG cold energy. The two cycle systems are independent and the pipelines are closed to form their own cycles. They are coupled with the equipment in their respective cycles to form a compact whole with the entire process, so as to fully and efficiently achieve the purpose of cascade utilization of LNG cold energy. Compared with the existing carbon capture devices in flue gas, it can reduce production costs and increase production capacity.

[0022] (3) The device includes a visualization window to facilitate observation of the carbon dioxide liquefaction phase change process. The process flow is complete, the system structure is compact, and the carbon dioxide liquefaction, purification and separation effects are good and efficient. Attached Figure Description

[0023] Figure 1 A process flow diagram of the carbon dioxide capture device provided by the present invention;

[0024] Figure 2 This is a schematic diagram of the multi-pass heat exchanger structure in the process flow of this invention;

[0025] The markings in the diagram are as follows:

[0026] 1-LNG inlet, 2-First-stage pressurization pump, 3-Second-stage pressurization pump, 4-First-stage regenerator, 5-First-stage evaporator, 6-First-stage expander, 7-Multi-pass heat exchanger, 8-Flue gas inlet, 9-Second-stage evaporator, 10-Condenser, 11-First-stage separator, 12-First-stage heat exchanger, 13-Second-stage separator, 14-Swirl separator, 15-Top gas outlet, 16-Bottom liquid outlet, 17-Third-stage pressurization pump, 18-Second-stage regenerator, 19-Second-stage expander, 20-Natural gas outlet, 21-First-stage water outlet, 22-Second-stage water outlet, 23-Carbon dioxide cooling pipeline, 24-Flue gas cooling pipeline, 25-LNG pipeline. Detailed Implementation

[0027] To make the objectives, technical solutions, and advantages of this invention clearer, the technical solutions of this invention are described clearly and completely below. Obviously, the described embodiments are only some, not all, of the embodiments of this invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0028] Unless otherwise defined, the technical or scientific terms used in this invention shall have the ordinary meaning understood by one of ordinary skill in the art to which this invention pertains. The terms "first," "second," "third," "fourth," and similar terms used in this invention do not indicate any order, quantity, or importance, but are merely used to distinguish different components. Terms such as "comprising" or "including" mean that the element or object preceding the word encompasses the elements or objects listed following the word and their equivalents, without excluding other elements or objects. Terms such as "connected" or "linked" are not limited to physical or mechanical connections, but can include electrical connections, whether direct or indirect.

[0029] This invention addresses the problem that existing LNG receiving terminals have a large amount of LNG cold energy, and that current cold energy utilization technologies are limited to cold energy air separation and cold energy power generation, failing to achieve cascade utilization of cold energy. It proposes a carbon capture device for industrial flue gas. This device reverses the use of existing submerged combustion gasification structures, coupling LNG cold energy utilization and carbon dioxide capture from flue gas into one integrated system. This achieves both objectives simultaneously and efficiently, reducing production costs and increasing production capacity compared to existing carbon capture devices for flue gas.

[0030] The technical solution of the present invention will be described in detail below with reference to specific examples.

[0031] like Figure 1 The diagram shown is a process flow chart of the carbon dioxide capture device provided by this invention. The carbon dioxide capture device in industrial flue gas of this invention consists of two circulation systems and two phase change processes, namely a supercritical Rankine cycle system for carbon dioxide, an organic Rankine cycle system, a carbon dioxide liquefaction process, and an LNG regasification process. In actual operation, each circulation system and phase change process is independent yet interconnected. The LNG regasification process includes an LNG inlet 1, which is sequentially connected to a primary pressurization pump 2, a multi-pass heat exchanger 7, and a primary heat exchanger 12. After heat exchange, the resulting natural gas is discharged from the natural gas outlet 20. The LNG regasification process utilizes an LNG cold energy cascade utilization system to achieve a step-by-step cooling process for LNG. After completing the cold energy exchange, the LNG is vaporized into natural gas. The LNG is first pressurized by the primary pressurization pump 2 and then enters the multi-pass heat exchanger 7 to condense the carbon dioxide from the secondary separator 13 into a low-temperature, low-pressure liquid. Then, it enters the primary heat exchanger 12 to exchange heat with carbon dioxide hydrate and organic working fluid, gradually vaporizing into natural gas. This process completes the LNG regasification.

[0032] The carbon dioxide liquefaction process includes an industrial flue gas inlet 8, which is sequentially connected to a primary evaporator 5, a secondary evaporator 9, a condenser 10, a primary separator 11, a primary heat exchanger 12, a secondary separator 13, a multi-pass heat exchanger 7, and a cyclone separator 14. The industrial flue gas enters the primary evaporator 5 and the secondary evaporator 9, where it provides heat for the supercritical Rankine cycle and organic Rankine cycle of carbon dioxide. After being cooled to a gas-liquid mixture by the condenser 10, it enters the primary separator 11 to separate the liquid water. The flue gas containing the separated liquid water then enters the primary... After heat exchange in heat exchanger 12, the gas-liquid mixture undergoes another gas-liquid separation in secondary separator 13. The carbon dioxide separated from the water enters multi-pass heat exchanger 7 and is cooled into liquid by LNG. At the same time, operating parameters are controlled (such as compressing the flue gas to a pressure of 12 bar and controlling the flue gas temperature to below -50°C). Then, the liquid carbon dioxide mixed with the exhaust gas undergoes gas-liquid separation in cyclone separator 14. The liquid carbon dioxide is recovered and reused from bottom outlet 16, and the exhaust gas is discharged from top outlet 15, thus completing the liquefaction and separation process of carbon dioxide in the flue gas.

[0033] The supercritical carbon dioxide Rankine cycle system and the organic Rankine cycle system are cold energy utilization systems coupled throughout the entire process to achieve gradient utilization of LNG cold energy in conjunction with the LNG regasification and carbon dioxide liquefaction processes. The supercritical carbon dioxide Rankine cycle system is sequentially connected to a multi-pass heat exchanger 7, a secondary pressurization pump 3, a primary regenerator 4, a primary evaporator 5, a primary expander 6, and a primary regenerator 4, before returning to the multi-pass heat exchanger 7, forming a complete supercritical carbon dioxide Rankine cycle system. It utilizes the phase change process of carbon dioxide for heat exchange and expansion work to achieve supercritical carbon dioxide Rankine cycle power generation. After carbon dioxide is condensed into a low-temperature, low-pressure saturated liquid by LNG in the multi-pass heat exchanger 7, it is pressurized by the secondary pressurization pump 3 and heated by the secondary pressurization pump 3. It is then fed into the primary evaporator 5 and heated again to a high-temperature, high-pressure gas. After that, it enters the primary expander 6 to do work and drive the generator to generate electricity. The gas, after being cooled and depressurized, first enters the primary regenerator 4 for precooling and then returns to the multi-pass heat exchanger 7 to exchange heat with LNG, forming a closed supercritical Rankine cycle system for carbon dioxide.

[0034] The organic Rankine cycle system is sequentially connected to a three-stage pressurization pump 17, a two-stage regenerator 18, a two-stage evaporator 9, a two-stage expander 19, a two-stage regenerator 18, and a one-stage heat exchanger 12, before returning to the three-stage pressurization pump 17, forming a complete organic Rankine cycle system. In the organic Rankine cycle system, the organic working fluid R245fa exchanges heat with flue gas and LNG, achieving energy storage and release, enabling the expander to generate electricity. The organic working fluid, pressurized by the three-stage pressurization pump 17 and preheated by the two-stage regenerator 18, enters the two-stage evaporator 9 and is heated into a high-temperature, high-pressure gas. It then enters the two-stage expander 19 to perform work, driving the generator to produce electricity. The low-pressure gas after performing work first returns to the two-stage regenerator 18 for precooling, then passes through the one-stage heat exchanger 12 to exchange heat with the low-temperature natural gas, before returning to the three-stage pressurization pump 17, completing the entire organic Rankine cycle process.

[0035] like Figure 2The diagram shows the internal structure of a multi-pass heat exchanger 7, which includes a carbon dioxide cooling pipe 23, a flue gas cooling pipe 24, and an LNG pipe 25. The LNG pipe 25 can be directly formed from the internal space of the multi-pass heat exchanger 7 shell, with its inlet connected to the first-stage pressurization pump 2 and its outlet connected to the first-stage heat exchanger 12. The flue gas cooling pipe 24 is a multi-tube bundle structure with its inlet and outlet connected to the outside of the multi-pass heat exchanger 7 shell via independent confluence spaces. The inlet of the flue gas cooling pipe 24 located outside the multi-pass heat exchanger 7 shell (not shown in the diagram) connects to the second-stage heat exchanger 12. The flue gas from the outlet of separator 13, the flue gas cooling pipe 24 located outside the shell of the multi-pass heat exchanger 7, is connected to the inlet of the cyclone separator 14; the carbon dioxide cooling pipe 23 is also set as a multi-tube parallel tube bundle structure, and its inlet and outlet are connected to the outside of the shell of the multi-pass heat exchanger 7 through independent space converging. The difference is that the tube bundle structure of the flue gas cooling pipe 24 and the tube bundle structure of the carbon dioxide cooling pipe 23 are evenly spaced and perpendicular to each other, forming a pipe network structure to turbulent the LNG fluid, so that it flows evenly through the multi-pass heat exchanger 7, thereby improving the cold energy exchange efficiency.

[0036] The inlet (not shown in the figure) of the carbon dioxide cooling pipe 23, located outside the shell of the multi-pass heat exchanger 7, connects to gaseous carbon dioxide from the first-stage regenerator 4. After being condensed by LNG, the gaseous carbon dioxide becomes liquid carbon dioxide and is transported from the outlet of the carbon dioxide cooling pipe 23 outside the shell of the multi-pass heat exchanger 7 to the second-stage pressurization pump 3, realizing the common cooling of multiple components in the multi-pass heat exchanger. The tube bundle structure of the flue gas cooling pipe 24 is evenly spaced and perpendicular to the tube bundle structure of the carbon dioxide cooling pipe 23, that is, the carbon dioxide cooling pipe 23 and the flue gas cooling pipe 24 are arranged in a cross shape in space. Preferably, each single tube of the tube bundle structure of the carbon dioxide cooling pipe 23 and the flue gas cooling pipe 24 adopts a spiral tube, finned tube or other type of pipe to increase the efficiency of flue gas absorbing LNG cold energy inside the multi-pass heat exchanger 7 and reduce the temperature to below the liquefaction temperature of carbon dioxide within the flow time.

[0037] All pipelines and equipment in the supercritical Rankine cycle system, organic Rankine cycle system, carbon dioxide liquefaction process, and LNG regasification process are insulated or cooled.

[0038] Multiple visualization windows can be set in the shell of the multi-pass heat exchanger 7, a certain area or section of the carbon dioxide cooling pipe 23 and the flue gas cooling pipe 24, and in the cyclone separator 14 using materials such as low-temperature resistant glass, to facilitate observation of the phase change process of cryogenic liquefied carbon dioxide.

[0039] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of the present invention.

Claims

1. A carbon dioxide capture device for industrial flue gas, characterized in that, It includes a supercritical carbon dioxide Rankine cycle system, an organic Rankine cycle system, a carbon dioxide liquefaction process, and an LNG regasification process. The LNG regasification process releases cold energy, and the supercritical carbon dioxide Rankine cycle system, the organic Rankine cycle system, and the carbon dioxide liquefaction process together achieve gradient utilization of cold energy. It also includes a multi-pass heat exchanger, with an LNG inlet pipeline connected to the multi-pass heat exchanger. After releasing cold energy inside the multi-pass heat exchanger, the LNG is connected to the first-stage heat exchanger via a pipeline. After further releasing cold energy inside the first-stage heat exchanger, the gaseous natural gas is transported out. This line constitutes the LNG regasification process. The industrial flue gas inlet pipeline is sequentially connected to a primary evaporator, a secondary evaporator, a condenser, a primary separator, a primary heat exchanger, a secondary separator, a multi-pass heat exchanger, and a cyclone separator. The flue gas releases heat in the primary and secondary evaporators, and then the condenser cools it to remove moisture. The primary separator separates the moisture from the flue gas. The moisture-free flue gas enters the primary heat exchanger and exchanges heat with natural gas in a counter-current flow to further cool and remove moisture. The secondary separator separates the water and gas, and the gaseous flue gas then enters the multi-pass heat exchanger. In the multi-pass heat exchanger, it absorbs the cold energy released by LNG, cooling the carbon dioxide in the flue gas to a liquid state. The liquid carbon dioxide then mixes with the waste gas in the cyclone separator to achieve gas-liquid separation. The liquid carbon dioxide is recovered and reused from the bottom outlet, while the waste gas is discharged from the top outlet. This circuit constitutes a carbon dioxide liquefaction process. Both the supercritical Rankine cycle system for carbon dioxide and the organic Rankine cycle system are coupled to the above-mentioned carbon dioxide liquefaction process and LNG regasification process through independent working fluid circulation. The multi-pass heat exchanger includes a closed shell and carbon dioxide cooling pipes and flue gas cooling pipes disposed inside the shell. An LNG inlet and an LNG outlet are disposed on the shell and communicate with its internal space, which forms an LNG pipeline. The flue gas cooling pipes are multi-tube bundle structures, with the inlet and outlet of the bundle structure connected to the outside of the multi-pass heat exchanger shell via independent spaces. The inlet of the flue gas cooling pipe located outside the multi-pass heat exchanger shell connects to the flue gas from the outlet of the secondary separator, and the outlet of the flue gas cooling pipe located outside the multi-pass heat exchanger shell connects to the inlet of the cyclone separator. The carbon dioxide cooling pipes are also configured as multi-tube bundle structures, with the inlet and outlet of the bundle structure also connected to the outside of the multi-pass heat exchanger shell via independent spaces. The inlet of the carbon dioxide cooling pipe located outside the multi-pass heat exchanger shell connects to the primary regenerator, and the outlet of the carbon dioxide cooling pipe located outside the multi-pass heat exchanger shell connects to the secondary booster pump. The tube bundle structures of the carbon dioxide cooling pipes and the flue gas cooling pipes are arranged in a cross shape in space.

2. The carbon dioxide capture device according to claim 1, characterized in that, The supercritical Rankine cycle system for carbon dioxide includes a multi-pass heat exchanger, a secondary pressurizing pump, a primary regenerator, a primary evaporator, a primary expander, and a primary regenerator connected in sequence to form a loop. The working fluid in this loop is carbon dioxide. Gaseous carbon dioxide absorbs the cold energy released by LNG in the multi-pass heat exchanger and is cooled to a liquid state. The liquid carbon dioxide is pressurized by the secondary pressurizing pump and transported to the primary regenerator to release cold energy. Then it enters the primary evaporator and is heated to a high temperature and high pressure by the flue gas from the carbon dioxide liquefaction process. The high temperature and high pressure gas enters the primary expander to do work and drive the generator to generate electricity. After being cooled and depressurized, the gaseous carbon dioxide first enters the primary regenerator for precooling and then returns to the multi-pass heat exchanger to form a loop.

3. The carbon dioxide capture device according to claim 1 or 2, characterized in that, The organic Rankine cycle system includes a three-stage pressurization pump, a two-stage regenerator, a two-stage evaporator, a two-stage expander, a two-stage regenerator, and a one-stage heat exchanger connected in sequence to form a circulation loop. The working fluid in this circulation loop is a refrigerant. After being pressurized by the three-stage pressurization pump and preheated by the two-stage regenerator, the working fluid enters the two-stage evaporator and is heated into a high-temperature, high-pressure gas. Then, it enters the two-stage expander to do work, driving a generator to generate electricity. The low-pressure gas after doing work first returns to the two-stage regenerator for precooling, and then passes through the one-stage heat exchanger to exchange heat with low-temperature natural gas. Finally, it returns to the three-stage pressurization pump to form a cycle.

4. The carbon dioxide capture device according to claim 1, characterized in that, It also includes a primary booster pump, which is installed between the LNG inlet pipeline and the multi-pass heat exchanger.

5. The carbon dioxide capture device according to claim 1, characterized in that, During the carbon dioxide liquefaction process, the operating parameters are controlled so that the flue gas pressure after entering the multi-pass heat exchanger from the secondary separator is 12 bar and the temperature is reduced to below -50°C.

6. The carbon dioxide capture device according to claim 3, characterized in that, The working fluid of the organic Rankine cycle system is the organic working fluid R245fa.

7. The carbon dioxide capture device according to claim 1, characterized in that, The tube bundle structure of both the carbon dioxide cooling pipe and the flue gas cooling pipe adopts spiral tube or finned tube.

8. The carbon dioxide capture device according to claim 1, characterized in that, At least one visualization window is provided on the shell of the multi-pass heat exchanger, the carbon dioxide cooling pipe, the flue gas cooling pipe, or the cyclone separator.

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