Equipment and method for preparing needle coke from direct coal liquefaction oil residues

Abstract

The invention relates to a device and method for preparing needle coke from direct coal liquefaction oil residue, the device comprises a raw material buffer tank, a coking fractionating tower and a coke tower group, the raw material buffer tank is communicated with one end of a pipeline I, and the other end of the pipeline I is used for being communicated with the raw material tank; the bottom of the raw material buffer tank is communicated with the lower part of the coking fractionating tower through a pipeline II; a coking feeding pump is fixedly mounted on the pipeline II; the top of the coke tower group is communicated with the lower part of the coking fractionating tower through a pipeline III, the bottom of the coke tower group is communicated with the bottom of the coking fractionating tower through a pipeline IV, and a heating furnace feeding pump and a coking heating furnace are fixedly mounted on the pipeline IV. The equipment and the method for producing the high-quality needle coke and sponge coke by using the coal direct liquefaction pitch as the raw material are suitable for the coal direct liquefaction oil residue pitch, and the oil product yield of the existing oil product prepared by coal direct liquefaction is improved.

Description

Technical Field

[0001] The present invention relates to the technical field of chemical equipment, and particularly relates to an apparatus and method for preparing needle coke from directly liquefied coal oil residue. Background Art

[0003] Currently, a technology for extracting and preparing asphalt from liquefied coal oil residue has been developed. The device can annually process 350,000 tons of liquefied coal oil residue, consuming 7,300 tons of extraction solvent and 10,500 tons of anthracene oil. It produces 59,000 tons of primary asphalt, 74,000 tons of intermediate asphalt, 74,000 tons of high-grade asphalt, and 159,000 tons of by-product gasification raw materials. The added value of the produced asphalt products is relatively low, and the application fields and regional coverage are limited.

[0004] "Exploration and Research on the Preparation of High-Value-Added Products from Direct Coal Liquefaction Residue" mentions that many domestic and foreign institutions have conducted extensive research on the pyrolysis properties and conversion and utilization of coal liquefaction residues, but mainly focus on combustion, gasification, extraction, and hydroconversion. Through the analysis of the composition, structure, and properties of direct coal liquefaction residues, it is proposed to use direct coal liquefaction residues to prepare products such as asphalt modifiers, mesophase pitch, and needle coke. This method will extremely effectively increase the added value of coal liquefaction residues, and thus provide a new research direction for improving the economic benefits of enterprises, realizing the protective utilization of resources, and achieving the goals of low-carbon environmental protection. The article only mentions the results of the small-scale preparation of needle coke, without citing the preparation method and relevant literature.

[0005] Literatures such as "Preliminary Evaluation of the Modification Effect of Direct Coal Liquefaction Residue on Road Asphalt" and "Research on Modified Asphalt Prepared from Direct Coal Liquefaction Residue" mainly focus on the research on preparing road asphalt from direct coal liquefaction residues.

[0006] The article "Research on the Preparation of Mesophase Pitch from Direct Coal Liquefaction Residue" obtains mesophase pitch through a thermal polycondensation process, proving the possibility of preparing mesophase pitch from direct coal liquefaction residues. Summary of the Invention

[0007] The present invention provides an apparatus and method for preparing needle coke from directly liquefied coal oil residue, aiming to solve the problems in the prior art.

[0008] The technical solution of the present invention for solving the above technical problems is as follows:

[0009] An apparatus for preparing needle coke from directly liquefied coal oil residue includes a raw material buffer tank, a coking fractionating tower, and a group of coke drums. The raw material buffer tank is connected to one end of pipeline 1, and the other end of pipeline 1 is used to connect to a raw material tank. The bottom of the raw material buffer tank is connected to the lower part of the coking fractionating tower through pipeline 2, and a coking feed pump is fixedly installed on pipeline 2. The top of the group of coke drums is connected to the lower part of the coking fractionating tower through pipeline 3, and its bottom is connected to the bottom of the coking fractionating tower through pipeline 4. A heating furnace feed pump and a coking heating furnace are fixedly installed on pipeline 4.

[0010] The beneficial effects of the present invention are as follows: During the preparation process, the raw materials enter the raw material buffer tank for buffering and are sent to the coking fractionating tower by the coking feed pump. The raw materials entering the coking fractionating tower come into contact and exchange heat with the hot oil gas sent by the group of coke drums. The obtained heavy fraction is sent into the group of coke drums after being heated by the coking heating furnace, and cracking and condensation chemical reactions occur to obtain oil gas and needle coke green coke, which is convenient for preparation.

[0011] The present invention provides an apparatus and method for producing high-quality needle coke using directly liquefied coal pitch as a raw material, which is applicable to directly liquefied coal oil residue pitch and improves the oil yield of existing directly liquefied coal to produce oil products.

[0012] On the basis of the above technical solution, the present invention can be further improved as follows.

[0013] Further, the group of coke drums includes a plurality of coke drums, and the plurality of coke drums are distributed in parallel. Their tops are respectively connected to pipeline 3 through a plurality of top branch pipelines, and the bottoms of the plurality of coke drums are respectively connected to pipeline 4 through bottom branch pipelines.

[0014] The beneficial effect of adopting the above further solution is that the structure is simple, and the number of the plurality of coke drums can be designed according to production requirements, further improving the processing efficiency.

[0015] Further, the bottoms of the plurality of coke drums are also respectively connected to one end of a product main pipeline through product branch pipelines, and the other end of the product main pipeline is used to connect to a product collector.

[0016] The beneficial effect of adopting the above further solution is that the structure is simple. The plurality of product branch pipelines converge into one product main pipeline, saving pipelines and occupying less space.

[0017] Further, heat exchange mechanisms are respectively fixedly installed on pipeline 1 and / or pipeline 2.

[0018] The beneficial effect of adopting the above further solution is that the structure is simple and the design is reasonable. The materials are heated through the heat exchange mechanism to ensure the normal operation of the preparation process.

[0019] Further, it further includes a fractionation top reflux drum. The top of the coking fractionation tower is communicated with the top of the fractionation top reflux drum through pipeline five. The bottom of the fractionation top reflux drum is communicated with the top of the coking fractionation tower through pipeline six. A fractionation top pump is fixedly installed on pipeline six.

[0020] The beneficial effect of adopting the above further scheme is that the structure is simple and the design is reasonable. The substances discharged from the top of the coking fractionation tower are processed by the fractionation top reflux drum, and the corresponding refluxed substances are sent back into the coking fractionation tower for reuse, with low cost.

[0021] Further, the part of pipeline six corresponding to the position between the coking fractionation tower and the fractionation top pump is communicated with one end of a light oil pipeline, and the other end of the light oil pipeline is used to communicate with a light oil collector; the lower part of the coking fractionation tower is communicated with one end of a heavy oil pipeline, and the other end of the heavy oil pipeline is used to communicate with a heavy oil collector.

[0022] The beneficial effect of adopting the above further scheme is that the structure is simple and the pipeline distribution is reasonable, which can realize the reflux and recovery of different products and is convenient for preparation.

[0023] Further, the top of the fractionation top reflux drum is also communicated with one end of a coking rich gas pipeline.

[0024] The beneficial effect of adopting the above further scheme is that the structure is simple and the design is reasonable. The coking rich gas can be collected by using the coking rich gas pipeline.

[0025] The present invention also relates to a method for preparing needle coke from coal direct liquefaction oil residue, which is realized by using the equipment for preparing needle coke from coal direct liquefaction oil residue as described above, and includes the following specific steps:

[0026] The raw materials enter the raw material buffer tank for buffering, and are sent to the coking fractionation tower by the coking feed pump. The raw materials entering the coking fractionation tower are in contact with and exchange heat with the hot oil gas sent by the coke drum group. The obtained heavy fraction is sent into the coke drum group after being heated and treated by the coking heating furnace, and undergoes cracking and condensation chemical reactions to obtain oil gas and needle coke green coke.

[0027] The beneficial effect of adopting the above further scheme is that the present invention provides a method for producing high-quality needle coke using coal direct liquefaction pitch as a raw material, which is applicable to coal direct liquefaction oil residue pitch and improves the oil yield of the existing coal direct liquefaction for producing oil products.

[0028] Further, the temperature of the material at the inlet of the coking heating furnace is 300 - 350 °C.

[0029] The beneficial effect of adopting the above further scheme is that the temperature setting is reasonable, which is convenient for the coking heating furnace to heat up the material.

[0030] Furthermore, the temperature of the material at the outlet of the coking heating furnace is 490 - 510 °C.

[0031] The beneficial effect of adopting the above further solution is that the coking heating furnace heats up the material to a suitable temperature for subsequent preparation operations. Description of the Drawings

[0032] Figure 1 It is a schematic structural diagram of the present invention.

[0033] In the drawings, the list of components represented by each reference numeral is as follows:

[0034] 1. Heat exchange mechanism; 2. Raw material buffer tank; 3. Coking feed pump; 4. Coking rich gas pipeline; 5. Coking fractionating tower; 6. Heating furnace feed pump; 7. Coking heating furnace; 8. Coke drum; 9. Fractionating tower top reflux drum; 10. Fractionating tower top pump; 11. Light oil pipeline; 12. Heavy oil pipeline. Detailed Embodiments

[0035] It should be noted that, without conflict, the embodiments in the present invention and the features in the embodiments can be combined with each other.

[0036] In the description of the present invention, it should be understood that the orientation or positional relationship indicated by the terms "center", "longitudinal", "transverse", "up", "down", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus cannot be construed as a limitation to the present invention. In addition, the terms "first", "second", etc. are only used for descriptive purposes and cannot be understood as indicating or implying relative importance or implicitly indicating the quantity of the indicated technical features. Thus, the features defined with "first", "second", etc. may explicitly or implicitly include one or more of such features. In the description of the present invention, unless otherwise stated, the meaning of "a plurality" is two or more.

[0037] In the description of the present invention, it should be noted that, unless otherwise clearly defined and limited, the terms "installed", "connected", "connected" should be understood in a broad sense. For example, it may be a fixed connection, a detachable connection, or an integral connection; it may be a mechanical connection or an electrical connection; it may be directly connected or indirectly connected through an intermediate medium, and it may be the internal communication of two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood through specific situations.

[0038] The present invention will be described in detail below with reference to the accompanying drawings and in conjunction with embodiments.

[0039] Embodiment 1

[0040] As Figure 1 shown, this embodiment provides a device for preparing needle coke from coal direct liquefaction oil residue, including a raw material buffer tank 2, a coking fractionation tower 5 and a coke tower group. One end of a pipeline 1 is connected to the raw material buffer tank 2, and the other end of the pipeline 1 is used to connect to a raw material tank; the bottom of the raw material buffer tank 2 is connected to the lower part of the coking fractionation tower 5 through a pipeline 2, and a coking feed pump 3 is fixedly installed on the pipeline 2; the top of the coke tower group is connected to the lower part of the coking fractionation tower 5 through a pipeline 3, and its bottom is connected to the bottom of the coking fractionation tower 5 through a pipeline 4, and a heating furnace feed pump 6 and a coking heating furnace 7 are fixedly installed on the pipeline 4.

[0041] During the preparation process, the raw materials enter the raw material buffer tank for buffering and are sent to the coking fractionation tower by the coking feed pump. The raw materials entering the coking fractionation tower contact and exchange heat with the hot oil gas sent by the coke tower group. The obtained heavy fraction is heated by the coking heating furnace and then sent into the coke tower group, where cracking and condensation chemical reactions occur to obtain oil gas and needle coke green coke, which is convenient for preparation.

[0042] Based on the above scheme, the above raw material buffer tank 2, coking fractionation tower 5 and coking heating furnace 7 respectively adopt existing equipment, and their specific structures and principles will not be elaborated here.

[0043] This embodiment provides a device and method for producing high-quality needle coke using coal direct liquefaction pitch as a raw material, which is applicable to coal direct liquefaction oil residue pitch and improves the oil yield of existing coal direct liquefaction for producing oil products.

[0044] Embodiment 2

[0045] On the basis of Embodiment 1, in this embodiment, the coke tower group includes a plurality of coke towers 8, and the plurality of coke towers 8 are distributed in parallel. Their tops are respectively connected to the pipeline 3 through a plurality of top branch pipelines, and the bottoms of the plurality of coke towers 8 are respectively connected to the pipeline 4 through bottom branch pipelines.

[0046] This scheme has a simple structure, and the number of the plurality of coke towers 8 can be designed according to production requirements, further improving the processing efficiency.

[0047] Preferably, in this embodiment, the above coke tower 8 is preferably two.

[0048] Alternatively, the tops of the above plurality of coke towers 8 are respectively connected to the lower part of the coking fractionation tower 5 through pipelines, but this scheme has unreasonable pipeline distribution and occupies a large space.

[0049] Embodiment 3

[0050] On the basis of Embodiment 2, in this embodiment, the bottoms of the plurality of coking towers 8 are respectively communicated with one end of a product main pipeline through product branch pipelines, and the other end of the product main pipeline is used to communicate with a product collector.

[0051] This solution has a simple structure. A plurality of product branch pipelines converge into one product main pipeline, saving pipelines and occupying little space.

[0052] Alternatively, the bottoms of the above-mentioned plurality of coking towers 8 are respectively communicated with the product collector through pipelines, but this solution has an unreasonable pipeline distribution and occupies a large space.

[0053] Embodiment 4

[0054] On the basis of the above embodiments, in this embodiment, a heat exchange mechanism 1 is fixedly installed on the pipeline 1 and / or the pipeline 2 respectively.

[0055] This solution has a simple structure and reasonable design. The material is heated by the heat exchange mechanism 1 to ensure the normal operation of the preparation process.

[0056] Each of the above heat exchange mechanisms 1 is provided with an interface 1 and an interface 2 that communicate with each other and an interface 3 and an interface 4 that communicate with each other. The interface 1 and the interface 2 are respectively communicated with both ends of the break on the pipeline 1 or the pipeline 2, and the interface 3 and the interface 4 are respectively communicated with a heat exchange medium supply device.

[0057] It should be noted that the above heat exchange mechanism 1 is preferably a heat exchanger in the prior art, and its specific structure and principle will not be elaborated here.

[0058] Embodiment 5

[0059] On the basis of the above embodiments, this embodiment further includes a fractionation top reflux drum 9. The top of the coking fractionation tower 5 is communicated with the top of the fractionation top reflux drum 9 through a pipeline 5, and the bottom of the fractionation top reflux drum 9 is communicated with the top of the coking fractionation tower 5 through a pipeline 6. A fractionation top pump 10 is fixedly installed on the pipeline 6.

[0060] This solution has a simple structure and reasonable design. The fractionation top reflux drum 9 is used to process the substances discharged from the top of the coking fractionation tower 5, and the corresponding substances for reflux are sent back into the coking fractionation tower 5 for reuse, with low cost.

[0061] It should be noted that the above fractionation top reflux drum 9 adopts the prior art, and its specific structure and principle will not be elaborated here.

[0062] Embodiment 6

[0063] On the basis of Embodiment 5, in this embodiment, the part of Pipeline VI corresponding to the position between the coking fractionating tower 5 and the fractionation top pump 10 is communicated with one end of the light oil pipeline 11, and the other end of the light oil pipeline 11 is used to communicate with a light oil collector; the lower part of the coking fractionating tower 5 is communicated with one end of the heavy oil pipeline 12, and the other end of the heavy oil pipeline 12 is used to communicate with a heavy oil collector.

[0064] This solution has a simple structure and reasonable pipeline distribution, can realize the reflux and recovery of different products, and is convenient to prepare.

[0065] Embodiment 7

[0066] On the basis of any one of Embodiments 5 to 6, in this embodiment, the top of the fractionation top reflux drum 9 is also communicated with one end of the coking rich gas pipeline 4.

[0067] This solution has a simple structure and reasonable design, and the coking rich gas can be collected by using the coking rich gas pipeline 4.

[0068] Embodiment 8

[0069] On the basis of the above embodiments, this embodiment further provides a method for preparing sponge coke from coal direct liquefaction oil residue, which is realized by using the equipment for preparing needle coke from coal direct liquefaction oil residue as described above, and includes the following specific steps:

[0070] The raw materials enter the raw material buffer tank 2 for buffering, and are sent to the coking fractionating tower 5 by the coking feed pump 3. The raw materials entering the coking fractionating tower 5 are in contact with the hot oil gas sent by the coke drum group for heat exchange. The obtained heavy fraction is sent into the coke drum group after being heated by the coking heating furnace 7, and cracking and condensation chemical reactions are carried out to obtain oil gas and needle coke green coke.

[0071] This embodiment provides a method for producing high-quality needle coke using coal direct liquefaction pitch as a raw material, which is applicable to coal direct liquefaction oil residue pitch and improves the oil yield of existing coal direct liquefaction for producing oil products.

[0072] Embodiment 9

[0073] On the basis of Embodiment 8, in this embodiment, the temperature of the material at the inlet of the coking heating furnace 7 is 300 - 350 °C.

[0074] In this solution, the temperature is set reasonably, which is convenient for the coking heating furnace to heat up the material.

[0075] Embodiment 10

[0076] On the basis of any one of Embodiments 8 to 9, in this embodiment, the temperature of the material at the outlet of the coking heating furnace 7 is 490 - 510 °C.

[0077] The coking heater 7 heats the material to a suitable temperature for subsequent preparation operations.

[0078] Preferably, in this embodiment, the temperature of the material at the outlet of the coking heater 7 is preferably 500 °C.

[0079] The preparation process of the present invention is as follows:

[0080] (1) The coal direct liquefaction pitch and anthracene oil are mixed in a ratio of 1:2 to 4 to adjust its softening point to be between 30 and 60 °C.

[0081] (2) Use steam to heat the entire coking system to 380 °C and maintain the system pressure at 0.3 to 0.6 Mpa.

[0082] (3) Use anthracene oil as the circulating oil and enter the coking system at a ratio of 1:1 with the adjusted raw material. The feeding time is 24 hours. Among them, in the first 18 hours, the outlet temperature of the heating furnace is controlled at 480 to 490 °C, and in the last 6 hours, the outlet temperature of the heating furnace is controlled at 490 to 510 °C.

[0083] (4) After the feeding is completed, steam blowing is carried out for not less than 6 hours, and the blowing temperature is not less than 380 °C.

[0084] (5) After the blowing is completed, it is naturally cooled to a system temperature not higher than 90 °C.

[0085] (6) Control the heating rate. During the entire experimental heating process, in the early stage (within 480 °C), the heating is controlled at about 2 °C / min; in the later stage (490 - 510 °C), it is controlled at 5 °C / min.

[0086] Using the equipment provided by the present invention, sponge coke can also be prepared. The specific process is as follows:

[0087] (1) The coal direct liquefaction pitch and anthracene oil are mixed in a volume ratio of 1:(2 - 4) to adjust its softening point to be between 30 and 60 °C.

[0088] (2) Use steam to heat the entire coking system to 380 °C and maintain the system pressure at 0.3 to 0.6 Mpa.

[0089] (3) Use anthracene oil as the circulating oil and enter the coking system at a ratio of 1:1 with the adjusted raw material. The feeding time is 24 hours, and the outlet temperature of the heating furnace is controlled at 480 to 490 °C.

[0090] (4) After the feeding is completed, steam blowing is carried out for not less than 6 hours, and the blowing temperature is not less than 380 °C.

[0091] (5) After the blowing is completed, it is naturally cooled to a system temperature not higher than 90 °C.

[0092] (6) Control of the heating rate. During the entire heating-up process of the experiment, in the early stage (within 480 °C), the heating is controlled at about 2 °C / min; in the later stage (480 - 490 °C), a constant temperature is controlled.

[0093] It should be noted that all the electronic components involved in the present invention adopt the existing technologies, and the above-mentioned components are electrically connected to the controller. The control circuits between the controller and each component are existing technologies.

[0094] For those skilled in the art, it is obvious that the present invention is not limited to the details of the above-mentioned exemplary embodiments, and without departing from the spirit or basic characteristics of the present invention, the present invention can be implemented in other specific forms. Therefore, from any point of view, the embodiments should be regarded as exemplary and non-limiting. The scope of the present invention is defined by the appended claims rather than the above description. Therefore, all changes falling within the meaning and scope of the equivalent elements of the claims are intended to be included in the present invention. Any reference signs in the claims should not be regarded as limiting the claims involved.

[0095] In addition, it should be understood that although this specification is described according to embodiments, not every embodiment only contains an independent technical solution. This narrative way of the specification is only for clarity. Those skilled in the art should regard the specification as a whole, and the technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

[0096] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. An apparatus for preparing needle coke from coal direct liquefaction oil residue, characterized in that: It includes a raw material buffer tank (2), a coking fractionating tower (5) and a coke drum group. One end of the first pipeline is communicated with the raw material buffer tank (2), and the other end of the first pipeline is used for communicating with a raw material tank; the bottom of the raw material buffer tank (2) is communicated with the lower part of the coking fractionating tower (5) through a second pipeline, and a coking feed pump (3) is fixedly installed on the second pipeline; the top of the coke drum group is communicated with the lower part of the coking fractionating tower (5) through a third pipeline, and its bottom is communicated with the bottom of the coking fractionating tower (5) through a fourth pipeline, and a heating furnace feed pump (6) and a coking heating furnace (7) are fixedly installed on the fourth pipeline.

2. The equipment for preparing needle coke from directly liquefied coal oil residue according to claim 1, characterized in that: The coke drum group includes a plurality of coke drums (8), and the plurality of coke drums (8) are distributed in parallel. Their tops are respectively communicated with the third pipeline through a plurality of top branch pipelines, and the bottoms of the plurality of coke drums (8) are respectively communicated with the fourth pipeline through bottom branch pipelines.

3. The equipment for preparing needle coke from directly liquefied coal residue according to claim 2, characterized in that: The bottoms of the plurality of coke drums (8) are also respectively communicated with one end of a product main pipeline through product branch pipelines, and the other end of the product main pipeline is used for communicating with a product collector.

4. The equipment for preparing needle coke from directly liquefied coal oil residue according to any one of claims 1-3, characterized in that: A heat exchange mechanism (1) is fixedly installed on the first pipeline and / or the second pipeline respectively.

5. The equipment for preparing needle coke from directly liquefied coal oil residue according to any one of claims 1-3, characterized in that: It further includes a fractionating tower top reflux tank (9). The top of the coking fractionating tower (5) is communicated with the top of the fractionating tower top reflux tank (9) through a fifth pipeline, and the bottom of the fractionating tower top reflux tank (9) is communicated with the top of the coking fractionating tower (5) through a sixth pipeline, and a fractionating tower top pump (10) is fixedly installed on the sixth pipeline.

6. The equipment for preparing needle coke from directly liquefied coal oil residue according to claim 5, wherein: The part of the sixth pipeline corresponding to the position between the coking fractionating tower (5) and the fractionating tower top pump (10) is communicated with one end of a light oil pipeline (11), and the other end of the light oil pipeline (11) is used for communicating with a light oil collector; the lower part of the coking fractionating tower (5) is communicated with one end of a heavy oil pipeline (12), and the other end of the heavy oil pipeline (12) is used for communicating with a heavy oil collector.

7. The equipment for preparing needle coke from directly liquefied coal oil residue according to claim 5, characterized in that: The top of the fractionating tower top reflux tank (9) is also communicated with one end of a coking rich gas pipeline (4).

8. A method for preparing needle coke from coal direct liquefaction oil residue, characterized in that: It is realized by using the equipment for preparing needle coke from directly liquefied oil residue of coal as described in any one of claims 1-7, and includes the following specific steps: The raw material enters the raw material buffer tank (2) for buffering, and is sent to the coking fractionating tower (5) by the coking feed pump (3). The raw material entering the coking fractionating tower (5) contacts and exchanges heat with the hot oil gas sent by the coke drum group. The obtained heavy fraction is sent into the coke drum group after being heated by the coking heating furnace (7), and cracking and condensation chemical reactions are carried out to obtain oil gas and needle coke green coke.

9. The method for preparing needle coke from directly liquefied coal residue according to claim 8, characterized in that: The temperature of the material at the inlet of the coking heating furnace (7) is 300-350 °C.

10. The method for preparing needle coke from coal direct liquefaction oil residue according to claim 8, characterized in that: The temperature of the material at the outlet of the coking heating furnace (7) is 490-510 °C.

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