System for prolonging operation cycle of acidic water stripping device
By introducing a parallel heat exchanger system into the acidic water stripping device, the problem of degradation of the heat exchange effect of raw water heat exchangers is solved, the stable operation of the device and the synchronization maintenance with the main production device are achieved, and energy consumption and work-off costs are reduced.
Patent Information
- Application Number
- CN202422145480.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-03
- Publication Date
- 2025-07-29
- Estimated Expiration
- 2034-09-03
AI Technical Summary
The raw water-purified water heat exchanger and raw water-desulfurized water heat exchanger of the 60t/h acidic water stripping device have decreased after 6 months of operation, resulting in an increase in energy consumption of the acidic water device, and the purification water index is unqualified, which affects the production progress and cannot be inspected and repaired simultaneously with the main production device.
Multiple parallel heat exchanger systems are adopted, including the first to fourth heat exchangers, and the valve control replaces the normal working heat exchanger when the heat exchanger fails or needs maintenance, so as to realize online cleaning and avoid unplanned shutdowns.
The operation cycle of the acidic water stripping device is extended, unplanned shutdowns are avoided, energy consumption is reduced, and the cost of shutdowns is saved.
Smart Images
Figure CN223163251U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of petrochemical equipment, and particularly relates to a system for improving the operation cycle of an acidic water stripping unit. Background Art
[0002] The acidic water stripping unit uses acidic water produced by atmospheric units, catalytic units, various hydrogenation units, reforming units, etc. in a refinery as raw materials to produce qualified purified water for reuse in external units.
[0003] The 60 t / h acidic water stripping unit adopts a domestically mature and reliable double-tower pressurized stripping ammonia recovery process technology. Hydrogen sulfide and ammonia in the acidic water are gradually removed in the hydrogen sulfide removal tower and ammonia removal tower respectively. The recovered crude ammonia is refined by a concentrated ammonia water washing process, compressed and then condensed to obtain high-purity liquid ammonia. At the same time, qualified purified water is produced. The raw water supplied to the 60 t / h acidic water stripping unit still carries some impurities into the acidic water stripping unit after being pretreated by a filter and sedimentation in an acidic water tank. After the raw water-purified water heat exchanger and the raw water-desulfurized water heat exchanger operate for 6 months, the heat exchange effect decreases, resulting in an increase in the energy consumption of the acidic water unit. Seriously, the purified water index is unqualified, causing the unplanned shutdown of the acidic water unit and failing to achieve synchronous maintenance with the main production unit, thus affecting the production progress. Content of the Utility Model
[0004] The utility model provides a system for improving the operation cycle of an acidic water stripping unit, aiming to provide a system that can extend the operation cycle of a 60 t / h acidic water unit and achieve synchronous maintenance with the main unit.
[0005] To achieve the above object, the technical solution adopted by the utility model is:
[0006] A system for improving the operation cycle of an acidic water stripping unit, at least including an acidic water stripping unit, which at least includes a raw water - purified water heat exchanger, a raw water - desulfurized water heat exchanger, a bottom reboiler of a hydrogen sulfide stripper, a bottom reboiler of an ammonia stripper, a hydrogen sulfide stripper, an ammonia stripper, a raw water input pipeline, a purified water output pipeline, a steam input pipeline and a condensate output device; the raw water - purified water heat exchanger is respectively connected to the raw water input pipeline and the purified water output pipeline, and is connected to the hydrogen sulfide stripper through the raw water - desulfurized water heat exchanger; the raw water - desulfurized water heat exchanger is connected to the ammonia stripper; the bottom reboiler of the hydrogen sulfide stripper is respectively connected to the hydrogen sulfide stripper, the steam input pipeline, the raw water - desulfurized water heat exchanger and the condensate output device; the bottom reboiler of the ammonia stripper is respectively connected to the ammonia stripper and the raw water - purified water heat exchanger; it also includes a first heat exchanger, a second heat exchanger, a third heat exchanger and a fourth heat exchanger; the first heat exchanger is in parallel with the raw water - desulfurized water heat exchanger, and the second heat exchanger is in parallel with the raw water - purified water heat exchanger; the third heat exchanger is in parallel with the bottom reboiler of the hydrogen sulfide stripper; the fourth heat exchanger is in parallel with the bottom reboiler of the ammonia stripper.
[0007] At least a first inlet of the first heat exchanger, a first outlet of the first heat exchanger, a second inlet of the first heat exchanger and a second outlet of the first heat exchanger are provided on the first heat exchanger; the first inlet of the first heat exchanger is communicated with the raw water input pipeline through the raw water - purified water heat exchanger; the first outlet of the first heat exchanger is communicated with the hydrogen sulfide stripper; the second inlet of the first heat exchanger is respectively communicated with the third heat exchanger and the bottom reboiler of the hydrogen sulfide stripper for the input of desulfurized water; the second outlet of the first heat exchanger is communicated with the ammonia stripper for inputting desulfurized water into the ammonia stripper.
[0008] A sixth valve is connected to the outer port of the first inlet of the first heat exchanger; a seventh valve is connected to the outer port of the first outlet of the first heat exchanger; an eighth valve is connected to the outer port of the second inlet of the first heat exchanger; a fifth valve is connected to the outer port of the second outlet of the first heat exchanger.
[0009] At least a first outlet of the second heat exchanger, a first inlet of the second heat exchanger, a second outlet of the second heat exchanger and a second inlet of the second heat exchanger are provided on the second heat exchanger; the first outlet of the second heat exchanger is communicated with the raw water - desulfurized water heat exchanger; the first inlet of the second heat exchanger is communicated with the raw water input pipeline; the second outlet of the second heat exchanger is communicated with the purified water output pipeline; the second inlet of the second heat exchanger is communicated with the purified water input pipeline.
[0010] A third valve is connected to the outer port of the first outlet of the second heat exchanger; a second valve is connected to the outer port of the first inlet of the second heat exchanger; a first valve is connected to the outer port of the second outlet of the second heat exchanger; a fourth valve is connected to the outer port of the second inlet of the second heat exchanger.
[0011] The third heat exchanger is provided with at least a first inlet of the third heat exchanger, a first outlet of the third heat exchanger, a second inlet of the third heat exchanger, a second outlet of the third heat exchanger, and a third outlet of the third heat exchanger; the first inlet of the third heat exchanger is communicated with the hydrogen sulfide removal tower; the first outlet of the third heat exchanger is respectively communicated with the first heat exchanger and the raw water-desulfurized water heat exchanger; the second inlet of the third heat exchanger is communicated with the steam input pipeline; the second outlet of the third heat exchanger is connected with the condensate output device; the third outlet of the third heat exchanger is communicated with the hydrogen sulfide removal tower for returning the gas phase to the hydrogen sulfide removal tower.
[0012] A nineteenth valve is connected to the second inlet of the third heat exchanger; a twentieth valve is connected to the second outlet of the third heat exchanger; a seventeenth valve is connected to the first inlet of the third heat exchanger; an eighteenth valve is connected to the first outlet of the third heat exchanger; a twenty-first valve is connected to the third outlet of the third heat exchanger.
[0013] The fourth heat exchanger is provided with at least a second inlet of the fourth heat exchanger, a second outlet of the fourth heat exchanger, a first inlet of the fourth heat exchanger, a first outlet of the fourth heat exchanger, and a third outlet of the fourth heat exchanger; the second inlet of the fourth heat exchanger is communicated with the steam input pipeline; the second outlet of the fourth heat exchanger is connected with the condensate output device; the first inlet of the fourth heat exchanger is connected with the ammonia removal tower for inputting the desulfurized water coming from the ammonia removal tower; the first outlet of the fourth heat exchanger is respectively connected with the second heat exchanger and the raw water-purified water heat exchanger; the third outlet of the fourth heat exchanger is connected with the ammonia removal tower for returning the gas phase to the ammonia removal tower for ammonia removal.
[0014] A twenty-fourth valve is connected to the second inlet of the fourth heat exchanger; a twenty-fifth valve is connected to the second outlet of the fourth heat exchanger; a twenty-third valve is connected to the first inlet of the fourth heat exchanger; a twenty-third valve is connected to the first outlet of the fourth heat exchanger; a twenty-sixth valve is connected to the third outlet of the fourth heat exchanger.
[0015] The beneficial effects produced by the present utility model are as follows:
[0016] (1) The present utility model enables the raw water heat exchanger of the 60t / h acidic water device to be cleaned online, avoiding the unplanned shutdown of the device. After three years of operation and trial use, the device has never stopped working.
[0017] (2) The present utility model reduces the energy consumption of the acidic water device.
[0018] (3) By using the present utility model, there is no shutdown during the operation period, saving the costs of starting up and shutting down the device.
[0019] The above description is only an overview of the technical solution of the present utility model. In order to understand the technical means of the present utility model more clearly and be implemented in accordance with the content of the description, the following takes the preferred embodiment of the present utility model and describes it in detail in conjunction with the drawings as follows. Description of the Drawings
[0020] In order to more clearly illustrate the technical solutions in the embodiments of the present utility model or the prior art, the following briefly introduces the drawings required to be used in the embodiments. Obviously, the drawings in the following description are only some embodiments of the present utility model. For those of ordinary skill in the art, other drawings can be obtained based on these drawings without creative efforts.
[0021] Figure 1 It is the overall composition diagram of the present utility model.
[0022] Figure 2 It is the composition diagram of the heat exchanger mechanism in the present utility model.
[0023] Figure 3 It is the composition diagram of the reboiler mechanism in the present utility model.
[0024] In the figure: 1. Raw water - purified water heat exchanger; 2. Raw water - desulfurized water heat exchanger; 3. First heat exchanger; 4. Second heat exchanger; 5. First valve; 6. Second valve; 7. Third valve; 8. Fourth valve; 9. Fifth valve; 10. Sixth valve; 11. Seventh valve; 12. Eighth valve; 13. Ninth valve; 14. Tenth valve; 15. Eleventh valve; 16. Twelfth valve; 17. Thirteenth valve; 18. Fourteenth valve; 19. Fifteenth valve; 20. Sixteenth valve; 21. First outlet of raw water - desulfurized water heat exchanger; 22. First inlet of raw water - desulfurized water heat exchanger; 23. Second outlet of raw water - desulfurized water heat exchanger; 24. Second inlet of raw water - desulfurized water heat exchanger; 25. First outlet of raw water - purified water heat exchanger; 26. First inlet of raw water - purified water heat exchanger; 27. Second outlet of raw water - purified water heat exchanger; 28. Second inlet of raw water - purified water heat exchanger; 29. First outlet of second heat exchanger; 30. First inlet of second heat exchanger; 31. Second outlet of second heat exchanger; 32. Second inlet of second heat exchanger; 33. First inlet of first heat exchanger; 34. First outlet of first heat exchanger; 35. Second inlet of first heat exchanger; 36. Second outlet of first heat exchanger; 37. Reboiler at the bottom of hydrogen sulfide removal tower; 38. Third heat exchanger; 39. Twenty - ninth valve; 40. Thirtieth valve; 41. Nineteenth valve; 42. Twentieth valve; 43. Twenty - seventh valve; 44. Seventeenth valve; 45. Twenty - eighth valve; 46. Eighteenth valve; 47. Thirty - first valve; 48. Twenty - first valve; 49. Second inlet of reboiler at the bottom of hydrogen sulfide removal tower; 50. Second outlet of reboiler at the bottom of hydrogen sulfide removal tower; 51. Second inlet of third heat exchanger; 52. Second outlet of third heat exchanger; 53. First inlet of reboiler at the bottom of hydrogen sulfide removal tower; 54. First inlet of third heat exchanger; 55. First outlet of reboiler at the bottom of hydrogen sulfide removal tower; 56. First outlet of third heat exchanger; 57. Third outlet of reboiler at the bottom of hydrogen sulfide removal tower; 58. Third outlet of third heat exchanger; 59. Reboiler at the bottom of ammonia removal tower; 60. Fourth heat exchanger; 61. Thirty - fourth valve; 62. Thirty - fifth valve; 63. Twenty - fourth valve; 64. Twenty - fifth valve; 65. Thirty - second valve; 66. Twenty - second valve; 67. Thirty - third valve; 68. Twenty - third valve; 69. Thirty - sixth valve; 70. Twenty - sixth valve; 71. Second inlet of reboiler at the bottom of ammonia removal tower; 72. Second outlet of reboiler at the bottom of ammonia removal tower; 73. Second inlet of fourth heat exchanger; 74. Second outlet of fourth heat exchanger; 75. First inlet of reboiler at the bottom of ammonia removal tower; 76. First inlet of fourth heat exchanger; 77. First outlet of reboiler at the bottom of ammonia removal tower; 78. First outlet of fourth heat exchanger; 79. Third outlet of reboiler at the bottom of ammonia removal tower; 80. Third outlet of fourth heat exchanger; 81. Hydrogen sulfide removal tower; 82. Ammonia removal tower. Detailed implementation manners
[0025] The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model. Obviously, the described embodiments are only a part of the embodiments of the present utility model, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present utility model without creative efforts shall fall within the protection scope of the present utility model.
[0026] Embodiment 1:
[0027] According to Figures 1 - 3 A system for improving the operation cycle of an acidic water stripping unit, which at least includes an acidic water stripping unit. The acidic water stripping unit at least includes a raw water-purified water heat exchanger 1, a raw water-desulfurized water heat exchanger 2, a bottom reboiler 37 of a hydrogen sulfide removal tower, a bottom reboiler 59 of an ammonia removal tower, a hydrogen sulfide removal tower 81, an ammonia removal tower 82, a raw water input pipeline, a purified water output pipeline, a steam input pipeline, and a condensate output device; the raw water-purified water heat exchanger 1 is respectively connected to the raw water input pipeline and the purified water output pipeline, and is connected to the hydrogen sulfide removal tower 81 through the raw water-desulfurized water heat exchanger 2; the raw water-desulfurized water heat exchanger 2 is connected to the ammonia removal tower 82; the bottom reboiler 37 of the hydrogen sulfide removal tower is respectively connected to the hydrogen sulfide removal tower 81, the steam input pipeline, the raw water-desulfurized water heat exchanger 2, and the condensate output device; the bottom reboiler 59 of the ammonia removal tower is respectively connected to the ammonia removal tower 82 and the raw water-purified water heat exchanger 1; it further includes a first heat exchanger 3, a second heat exchanger 4, a third heat exchanger 38, and a fourth heat exchanger 60; the first heat exchanger 3 is in parallel with the raw water-desulfurized water heat exchanger 2, and the second heat exchanger 4 is in parallel with the raw water-purified water heat exchanger 1; the third heat exchanger 38 is in parallel with the bottom reboiler 37 of the hydrogen sulfide removal tower; the fourth heat exchanger 60 is in parallel with the bottom reboiler 59 of the ammonia removal tower.
[0028] In this embodiment, the raw water - purified water heat exchanger 1 at least includes a first outlet 25 of the raw water - purified water heat exchanger, a first inlet 26 of the raw water - purified water heat exchanger, a second outlet 27 of the raw water - purified water heat exchanger, and a second inlet 28 of the raw water - purified water heat exchanger; the raw water - desulfurized water heat exchanger 2 at least includes a first outlet 21 of the raw water - desulfurized water heat exchanger, a first inlet 22 of the raw water - desulfurized water heat exchanger, a second outlet 23 of the raw water - desulfurized water heat exchanger, and a second inlet 24 of the raw water - desulfurized water heat exchanger. When the raw water - purified water heat exchanger 1 and the raw water - desulfurized water heat exchanger 2 are in a normal working state, the raw water enters the raw water - purified water heat exchanger 1 through the second inlet 28 of the raw water - purified water heat exchanger, and the raw water after heat exchange in the raw water - purified water heat exchanger 1 enters the raw water - desulfurized water heat exchanger 2 through the first outlet 25 of the raw water - purified water heat exchanger and the second inlet 24 of the raw water - desulfurized water heat exchanger. After heat exchange in the raw water - desulfurized water heat exchanger 2, it enters the raw water pipeline to the desulfurization tower through the first outlet 21 of the raw water - desulfurized water heat exchanger for desulfurization. The purified water from the purified water input pipeline enters the raw water - purified water heat exchanger 1 through the first inlet 26 of the raw water - purified water heat exchanger, and the purified water after heat exchange in the raw water - purified water heat exchanger 1 enters the purified water output pipeline through the second outlet 27 of the raw water - purified water heat exchanger and is then output. The desulfurized water enters the raw water - desulfurized water heat exchanger 2 through the first inlet 22 of the raw water - desulfurized water heat exchanger, and after heat exchange in the raw water - desulfurized water heat exchanger 2, it enters the desulfurized water pipeline to the desulfurization tower through the second outlet 23 of the raw water - desulfurized water heat exchanger for desulfurization.
[0029] In this embodiment, the hydrogen sulfide removal bottom reboiler 37 at least includes a first outlet 55 of the hydrogen sulfide removal bottom reboiler, a first inlet 53 of the hydrogen sulfide removal bottom reboiler, a second outlet 50 of the hydrogen sulfide removal bottom reboiler, a second inlet 49 of the hydrogen sulfide removal bottom reboiler, and a third outlet 57 of the hydrogen sulfide removal bottom reboiler; the ammonia removal bottom reboiler 59 at least includes a first outlet 77 of the ammonia removal bottom reboiler, a first inlet 75 of the ammonia removal bottom reboiler, a second outlet 72 of the ammonia removal bottom reboiler, a second inlet 71 of the ammonia removal bottom reboiler, and a third outlet 79 of the ammonia removal bottom reboiler. When the hydrogen sulfide removal bottom reboiler 37 and the ammonia removal bottom reboiler 59 are in normal working conditions, acidic water enters the hydrogen sulfide removal bottom reboiler 37 through the first inlet 53 of the hydrogen sulfide removal bottom reboiler, and the desulfurized water after being heated and stripped by the hydrogen sulfide removal bottom reboiler goes to the desulfurized water heat exchanger through the first outlet 55 of the hydrogen sulfide removal bottom reboiler; steam enters the hydrogen sulfide removal bottom reboiler 37 through the second inlet 49 of the hydrogen sulfide removal bottom reboiler, and the condensed water after being cooled by the hydrogen sulfide removal bottom reboiler goes to the condensed water system through the second outlet 50 of the hydrogen sulfide removal bottom reboiler; the acidic gas stripped by the hydrogen sulfide removal bottom reboiler 37 goes to the gas phase line to return to the hydrogen sulfide removal tower through the third outlet 47 of the hydrogen sulfide removal bottom reboiler; the desulfurized water enters the ammonia removal bottom reboiler 59 through the first inlet 75 of the ammonia removal bottom reboiler, and the purified water after being heated and stripped by the ammonia removal bottom reboiler goes to the purified water heat exchanger through the first outlet 77 of the ammonia removal bottom reboiler; steam enters the ammonia removal bottom reboiler 59 through the second inlet 71 of the ammonia removal bottom reboiler, and the condensed water after being cooled by the ammonia removal bottom reboiler goes to the condensed water system through the second outlet 72 of the ammonia removal bottom reboiler; the ammonia gas discharged from the ammonia removal bottom reboiler 59 goes to the gas phase line to return to the ammonia removal tower through the third outlet 79 of the ammonia removal bottom reboiler.
[0030] In normal working conditions, the raw water - purified water heat exchanger 1, the raw water - desulfurized water heat exchanger 2, the hydrogen sulfide removal bottom reboiler 37, and the ammonia removal bottom reboiler 59 are in operation, while the first heat exchanger 3, the second heat exchanger 4, the third heat exchanger 38, and the fourth heat exchanger 60 are out of service; when the raw water - purified water heat exchanger 1 or the raw water - desulfurized water heat exchanger 2, the hydrogen sulfide removal bottom reboiler 37, or the ammonia removal bottom reboiler 59 malfunctions, or when maintenance is required for the raw water - purified water heat exchanger 1 or the raw water - desulfurized water heat exchanger 2, the hydrogen sulfide removal bottom reboiler 37, or the ammonia removal bottom reboiler 59, the first heat exchanger 3 or the second heat exchanger 4, the third heat exchanger 38, and the fourth heat exchanger 60 are started to replace the raw water - purified water heat exchanger 1, the raw water - desulfurized water heat exchanger 2, the hydrogen sulfide removal bottom reboiler 37, and the ammonia removal bottom reboiler 59 in operation, thus avoiding unplanned shutdown of the acidic water unit and enabling synchronous maintenance with the main production unit.
[0031] Embodiment 2:
[0032] According to Figure 1A system for improving the operation cycle of an acidic water stripping unit, which is different from the first embodiment in that: at least a first inlet 33, a first outlet 34, a second inlet 35 and a second outlet 36 of the first heat exchanger 3 are provided; the first inlet 33 of the first heat exchanger is communicated with the raw water input pipeline through the raw water - purified water heat exchanger 1; the first outlet 34 of the first heat exchanger is communicated with the pipeline for raw water to the desulfurization tower; the second inlet 35 of the first heat exchanger is communicated with the desulfurized water input pipeline; the second outlet 36 of the first heat exchanger is communicated with the pipeline for desulfurized water to the desulfurization tower.
[0033] Furthermore, a sixth valve 10 is connected to the outer port of the first inlet 33 of the first heat exchanger; a seventh valve 11 is connected to the outer port of the first outlet 34 of the first heat exchanger; an eighth valve 12 is connected to the outer port of the second inlet 35 of the first heat exchanger; a fifth valve 9 is connected to the outer port of the second outlet 36 of the first heat exchanger.
[0034] During actual use, when the raw water - desulfurized water heat exchanger 2 is working normally, the first heat exchanger 3 is in a standby state, and the fifth valve 9, the sixth valve 10, the seventh valve 11 and the eighth valve 12 are in a closed state; when the raw water - desulfurized water heat exchanger 2 fails or needs to be overhauled, the fifth valve 9, the sixth valve 10, the seventh valve 11 and the eighth valve 12 are opened, and at the same time, the ninth valve 13, the tenth valve 14, the eleventh valve 15 and the twelfth valve 16 are closed, so that the raw water - desulfurized water heat exchanger 2 is in a shutdown state, and the first heat exchanger 3 replaces the raw water - desulfurized water heat exchanger 2 to work. At this time, the raw water enters the first heat exchanger 3 through the first inlet 33 of the first heat exchanger via the raw water input pipeline, and the raw water after heat exchange in the first heat exchanger 3 enters the pipeline for raw water to the desulfurization tower through the first outlet 34 of the first heat exchanger for desulfurization. The desulfurized water enters the first heat exchanger 3 through the second inlet 35 of the first heat exchanger via the desulfurized water input pipeline, and after heat exchange in the first heat exchanger, it enters the pipeline for desulfurized water to the desulfurization tower through the second outlet 36 of the first heat exchanger for desulfurization.
[0035] The first heat exchanger 3 replaces the raw water - desulfurized water heat exchanger 2 to work, ensuring the continuity and stability of the operation process of the entire acidic water stripping unit.
[0036] Example 3:
[0037] According to Figure 1A system for improving the operation cycle of an acidic water stripping unit is shown. The difference from Embodiment 1 is that at least a first outlet 29, a first inlet 30, a second outlet 31 and a second inlet 32 of the second heat exchanger 4 are provided; the first outlet 29 of the second heat exchanger is connected to the raw water-desulfurized water heat exchanger 2; the first inlet 30 of the second heat exchanger is connected to the raw water input pipeline; the second outlet 31 of the second heat exchanger is connected to the purified water output pipeline; the second inlet 32 of the second heat exchanger is connected to the purified water input pipeline.
[0038] Furthermore, a third valve 7 is connected to the outer port of the first outlet 29 of the second heat exchanger; a second valve 6 is connected to the outer port of the first inlet 30 of the second heat exchanger; a first valve 5 is connected to the outer port of the second outlet 31 of the second heat exchanger; a fourth valve 8 is connected to the outer port of the second inlet 32 of the second heat exchanger.
[0039] During actual use, when the raw water-purified water heat exchanger 1 is working properly, the second heat exchanger 4 is in a standby state, and the first outlet 29, the first inlet 30, the second outlet 31 and the second inlet 32 of the second heat exchanger are in a closed state; when the raw water-purified water heat exchanger 1 fails or needs to be overhauled, the first valve 5, the second valve 6, the third valve 7 and the fourth valve 8 are opened, and at the same time the thirteenth valve 17, the fourteenth valve 18, the fifteenth valve 19 and the sixteenth valve 20 are closed, so that the raw water-purified water heat exchanger 1 is in a shutdown state, and the second heat exchanger 4 replaces the raw water-purified water heat exchanger 1 to work. At this time, the raw water passes through the raw water input pipeline, enters the second heat exchanger 4 through the first inlet 30 of the second heat exchanger, and the raw water after heat exchange in the second heat exchanger 4 enters the raw water pipeline to the desulfurization tower through the first outlet 29 of the second heat exchanger for desulfurization. The purified water passes through the purified water input pipeline, enters the second heat exchanger 4 through the second inlet 32 of the second heat exchanger, and enters the purified water output pipeline through the second outlet 31 of the second heat exchanger after heat exchange in the second heat exchanger 4.
[0040] The second heat exchanger 4 replaces the raw water-purified water heat exchanger 1 to work, ensuring the continuity and stability of the operation process of the entire acidic water stripping unit.
[0041] Embodiment 4:
[0042] According to Figure 1 and Figure 3As shown in the figure, a system for improving the operation cycle of an acidic water stripping unit is different from that in the first embodiment in that: at least a first inlet 54, a first outlet 56, a second inlet 51, a second outlet 52 and a third outlet 58 of the third heat exchanger 38 are provided; the first inlet 54 of the third heat exchanger is communicated with the hydrogen sulfide removal tower 81; the first outlet 56 of the third heat exchanger is respectively communicated with the first heat exchanger 3 and the raw water - desulfurized water heat exchanger 2; the second inlet 51 of the third heat exchanger is communicated with the steam input pipeline; the second outlet 52 of the third heat exchanger is connected with the condensate output device; the third outlet 58 of the third heat exchanger is communicated with the hydrogen sulfide removal tower 81 for returning the gas phase to the hydrogen sulfide removal tower 81.
[0043] Furthermore, a nineteenth valve 41 is connected to the second inlet 51 of the third heat exchanger; a twentieth valve 42 is connected to the second outlet 52 of the third heat exchanger; a seventeenth valve 44 is connected to the first inlet 54 of the third heat exchanger; an eighteenth valve 46 is connected to the first outlet 56 of the third heat exchanger; a twenty - first valve 48 is connected to the third outlet 58 of the third heat exchanger.
[0044] During actual use, when the reboiler 37 at the bottom of the hydrogen sulfide removal tower is working normally, the third heat exchanger 38 is in a standby state, and the first outlet 56, the first inlet 54, the second outlet 52, the second inlet 51 and the third outlet 58 of the third heat exchanger are in a closed state; when the reboiler 37 at the bottom of the hydrogen sulfide removal tower fails or needs to be overhauled, the eighteenth valve 46, the seventeenth valve 44, the twentieth valve 42, the nineteenth valve 41 and the twenty - first valve 48 are opened, and at the same time, the twenty - seventh valve 43, the twenty - eighth valve 45, the twenty - ninth valve 39, the thirtieth valve 40 and the thirty - first valve 47 are closed, so that the reboiler 37 at the bottom of the hydrogen sulfide removal tower is in a shutdown state, and the third heat exchanger 38 replaces the reboiler 37 at the bottom of the hydrogen sulfide removal tower to work. At this time, the acidic water enters the third heat exchanger 38 through the acidic water input pipeline via the first inlet 54 of the third heat exchanger, and the desulfurized water heated and stripped by the third heat exchanger 38 enters the desulfurized water to heat exchanger pipeline via the first outlet 56 of the third heat exchanger. The steam enters the third heat exchanger 38 through the steam input pipeline via the second inlet 51 of the third heat exchanger, and the condensate cooled by the third heat exchanger 38 enters the condensate output pipeline through the second outlet 52 of the third heat exchanger. The acidic gas stripped by the third heat exchanger 38 goes to the gas phase line to return to the hydrogen sulfide removal tower through the third outlet 58.
[0045] The third heat exchanger 38 replaces the reboiler 37 at the bottom of the hydrogen sulfide removal tower to work, ensuring the continuity and stability of the operation process of the entire acidic water stripping unit.
[0046] Example 5:
[0047] According to Figure 1 and Figure 3 As shown, a system for improving the operation cycle of an acidic water stripping unit is different from that in Example 1 in that: at least a fourth heat exchanger second inlet 73, a fourth heat exchanger second outlet 74, a fourth heat exchanger first inlet 76, a fourth heat exchanger first outlet 78 and a fourth heat exchanger third outlet 80 are provided on the fourth heat exchanger 60; the fourth heat exchanger second inlet 73 is communicated with a steam input pipeline; the fourth heat exchanger second outlet 74 is connected to a condensate output device; the fourth heat exchanger first inlet 76 is connected to a deammoniation tower 82 for inputting desulfurized water coming from the deammoniation tower 82; the fourth heat exchanger first outlet 78 is respectively connected to the second heat exchanger 4 and the raw water-purified water heat exchanger 1; the fourth heat exchanger third outlet 80 is connected to the deammoniation tower 82 for returning the gas phase to the deammoniation tower 82 for deammoniation.
[0048] Furthermore, a twenty-fourth valve 63 is connected to the fourth heat exchanger second inlet 73; a twenty-fifth valve 64 is connected to the fourth heat exchanger second outlet 74; a twenty-third valve 66 is connected to the fourth heat exchanger first inlet 76; a twenty-third valve 68 is connected to the fourth heat exchanger first outlet 78; a twenty-sixth valve 70 is connected to the fourth heat exchanger third outlet 80.
[0049] During actual use, when the reboiler 59 at the bottom of the deammoniation tower is working properly, the fourth heat exchanger 60 is in a standby state, and the fourth heat exchanger first outlet 78, the fourth heat exchanger first inlet 76, the fourth heat exchanger second outlet 74, the fourth heat exchanger second inlet 73, and the fourth heat exchanger third outlet 80 are in a closed state; when the reboiler 59 at the bottom of the deammoniation tower fails or needs to be overhauled, the twenty-third valve 68, the twenty-second valve 66, the twenty-sixth valve 70, the twenty-fifth valve 64 and the twenty-fourth valve 63 are opened, and at the same time the thirty-second valve 65, the thirty-third valve 67, the thirty-sixth valve 69, the thirty-fourth valve 61 and the thirty-fifth valve 62 are closed, so that the reboiler 59 at the bottom of the deammoniation tower is in a shutdown state, and the fourth heat exchanger 60 replaces the reboiler 59 at the bottom of the deammoniation tower to work. At this time, the desulfurized water enters the fourth heat exchanger 60 through the desulfurized water input pipeline via the fourth heat exchanger first inlet 76, and the purified water heated and stripped by the fourth heat exchanger 60 enters the purified water to heat exchanger pipeline via the fourth heat exchanger first outlet 78. The steam enters the fourth heat exchanger 60 through the steam input pipeline via the fourth heat exchanger second inlet 73, and the condensate cooled by the fourth heat exchanger 60 enters the condensate output pipeline through the fourth heat exchanger second outlet 74. The ammonia gas stripped by the fourth heat exchanger 60 goes to the gas phase line to return to the deammoniation tower through the fourth heat exchanger third outlet 80.
[0050] The fourth heat exchanger 60 replaces the reboiler 59 at the bottom of the deammoniation tower to ensure the continuity and stability of the operation process of the entire sour water stripping unit.
[0051] Example 6:
[0052] According to Figure 1 A system for improving the operation cycle of a sour water stripping unit as shown, and its application in practice.
[0053] After four years of trial use and appraisal of the present utility model, there has been no shutdown during the operation cycle, saving the costs of startup and shutdown. Calculated based on the saved fresh water consumption and deodorant during startup and shutdown, the shutdown cost can be saved by 1.0466 million yuan; among them: fresh water cost: 500 tons × 2.62 yuan / ton × 5 times = 0.066 million yuan; the deodorant for shutdown can be saved: 16 tons × 13,000 yuan / ton × 5 times = 1 million yuan.
[0054] To sum up, the present utility model enables the raw water heat exchanger of the 60t / h sour water unit to achieve on-line cleaning, avoiding unplanned shutdowns of the unit. After three years of operation and trial use, the unit has never shut down.
[0055] The present utility model reduces the energy consumption of the sour water unit.
[0056] With the use of the present utility model, there has been no shutdown during the operation cycle, saving the costs of startup and shutdown.
[0057] In specific applications, the idle raw water - purified water heat exchanger and raw water - desulfurized water heat exchanger can also be used to replace the second heat exchanger 4 and the first heat exchanger 3, thereby saving equipment costs.
[0058] Without conflict, those skilled in the art can combine the relevant technical features in the above examples according to the actual situation to achieve the corresponding technical effects. Specific combinations are not elaborated here one by one.
[0059] It should be noted that all directional indications (such as up, down, left, right, front, back...) in the embodiments of the present utility model are only used to explain the relative position relationship and movement conditions between components in a specific posture (as shown in the drawings). If the specific posture changes, the directional indications will also change accordingly.
[0060] In addition, the descriptions involving "first", "second", etc. in the present utility model are only for descriptive purposes and cannot be understood as indicating or implying their relative importance or implicitly indicating the quantity of the indicated technical features. Thus, the features defined with "first", "second" can explicitly or implicitly include at least one such feature.
[0061] As described above, these are merely the preferred embodiments of the present utility model. The present utility model will not be limited to these embodiments shown herein, but rather will conform to the broadest scope consistent with the principles and novel features disclosed herein. Any simple modifications, equivalent changes, and embellishments made to the above embodiments based on the technical essence of the present utility model shall still fall within the scope of the technical solutions of the present utility model.
Claims
1. A system for improving the operation cycle of an acidic water stripping unit, at least comprising an acidic water stripping unit, and the acidic water stripping unit at least comprises a raw water - purified water heat exchanger (1), a raw water - desulfurized water heat exchanger (2), a bottom reboiler of the hydrogen sulfide stripping tower (37), a bottom reboiler of the ammonia stripping tower (59), a hydrogen sulfide stripping tower (81), an ammonia stripping tower (82), a raw water input pipeline, a purified water output pipeline, a steam input pipeline and a condensate output device; the raw water - purified water heat exchanger (1) is respectively connected with the raw water input pipeline and the purified water output pipeline, and is connected with the hydrogen sulfide stripping tower (81) through the raw water - desulfurized water heat exchanger (2); the raw water - desulfurized water heat exchanger (2) is connected with the ammonia stripping tower (82); the bottom reboiler of the hydrogen sulfide stripping tower (37) is respectively connected with the hydrogen sulfide stripping tower (81), the steam input pipeline, the raw water - desulfurized water heat exchanger (2) and the condensate output device; the bottom reboiler of the ammonia stripping tower (59) is respectively connected with the ammonia stripping tower (82) and the raw water - purified water heat exchanger (1); and it is characterized in that: It further includes a first heat exchanger (3), a second heat exchanger (4), a third heat exchanger (38) and a fourth heat exchanger (60); the first heat exchanger (3) is in parallel with the raw water - desulfurized water heat exchanger (2), and the second heat exchanger (4) is in parallel with the raw water - purified water heat exchanger (1); the third heat exchanger (38) is in parallel with the bottom reboiler (37) of the hydrogen sulfide removal tower; the fourth heat exchanger (60) is in parallel with the bottom reboiler (59) of the ammonia removal tower.
2. The system for improving the operation cycle of an acidic water stripping unit according to claim 1, wherein: At least a first inlet (33) of the first heat exchanger, a first outlet (34) of the first heat exchanger, a second inlet (35) of the first heat exchanger and a second outlet (36) of the first heat exchanger are provided on the first heat exchanger (3); the first inlet (33) of the first heat exchanger is communicated with the raw water input pipeline through the raw water - purified water heat exchanger (1); the first outlet (34) of the first heat exchanger is communicated with the hydrogen sulfide removal tower (81); the second inlet (35) of the first heat exchanger is respectively communicated with the third heat exchanger (38) and the bottom reboiler (37) of the hydrogen sulfide removal tower for input of desulfurized water; the second outlet (36) of the first heat exchanger is communicated with the ammonia removal tower (82) for input of desulfurized water into the ammonia removal tower (82).
3. The system for improving the operation cycle of an acidic water stripping unit according to claim 2, characterized in that: A sixth valve (10) is connected to the outer port of the first inlet (33) of the first heat exchanger; a seventh valve (11) is connected to the outer port of the first outlet (34) of the first heat exchanger; an eighth valve (12) is connected to the outer port of the second inlet (35) of the first heat exchanger; a fifth valve (9) is connected to the outer port of the second outlet (36) of the first heat exchanger.
4. The system for improving the operation cycle of an acidic water stripping unit according to claim 1, characterized in that: At least a first outlet (29) of the second heat exchanger, a first inlet (30) of the second heat exchanger, a second outlet (31) of the second heat exchanger and a second inlet (32) of the second heat exchanger are provided on the second heat exchanger (4); the first outlet (29) of the second heat exchanger is communicated with the raw water - desulfurized water heat exchanger (2); the first inlet (30) of the second heat exchanger is communicated with the raw water input pipeline; the second outlet (31) of the second heat exchanger is communicated with the purified water output pipeline; the second inlet (32) of the second heat exchanger is communicated with the purified water input pipeline.
5. The system for improving the operation cycle of an acidic water stripping unit according to claim 4, characterized in that: A third valve (7) is connected to the outer port of the first outlet (29) of the second heat exchanger; a second valve (6) is connected to the outer port of the first inlet (30) of the second heat exchanger; a first valve (5) is connected to the outer port of the second outlet (31) of the second heat exchanger; a fourth valve (8) is connected to the outer port of the second inlet (32) of the second heat exchanger.
6. The system for improving the operation cycle of an acidic water stripping unit according to claim 1, characterized in that: At least a first inlet (54) of a third heat exchanger, a first outlet (56) of the third heat exchanger, a second inlet (51) of the third heat exchanger, a second outlet (52) of the third heat exchanger, and a third outlet (58) of the third heat exchanger are provided on the third heat exchanger (38); the first inlet (54) of the third heat exchanger is communicated with a hydrogen sulfide removal tower (81); the first outlet (56) of the third heat exchanger is respectively communicated with a first heat exchanger (3) and a raw water-desulfurized water heat exchanger (2); the second inlet (51) of the third heat exchanger is communicated with a steam input pipeline; the second outlet (52) of the third heat exchanger is connected to a condensate output device; the third outlet (58) of the third heat exchanger is communicated with the hydrogen sulfide removal tower (81) for returning a gas phase to the hydrogen sulfide removal tower (81).
7. The system for improving the operation cycle of an acidic water stripping unit as described in claim 6, wherein: A nineteenth valve (41) is connected to the second inlet (51) of the third heat exchanger; a twentieth valve (42) is connected to the second outlet (52) of the third heat exchanger; a seventeenth valve (44) is connected to the first inlet (54) of the third heat exchanger; an eighteenth valve (46) is connected to the first outlet (56) of the third heat exchanger; a twenty-first valve (48) is connected to the third outlet (58) of the third heat exchanger.
8. The system for improving the operation cycle of an acidic water stripping unit as described in claim 1, characterized in that: At least a second inlet (73) of a fourth heat exchanger, a second outlet (74) of the fourth heat exchanger, a first inlet (76) of the fourth heat exchanger, a first outlet (78) of the fourth heat exchanger, and a third outlet (80) of the fourth heat exchanger are provided on the fourth heat exchanger (60); the second inlet (73) of the fourth heat exchanger is communicated with a steam input pipeline; the second outlet (74) of the fourth heat exchanger is connected to a condensate output device; the first inlet (76) of the fourth heat exchanger is connected to a deammoniation tower (82) for inputting desulfurized water coming from the deammoniation tower (82); the first outlet (78) of the fourth heat exchanger is respectively connected to a second heat exchanger (4) and a raw water-purified water heat exchanger (1); the third outlet (80) of the fourth heat exchanger is connected to the deammoniation tower (82) for returning a gas phase to the deammoniation tower (82) for deammoniation.
9. The system for improving the operation cycle of an acidic water stripping unit as described in claim 8, wherein: A twenty-fourth valve (63) is connected to the second inlet (73) of the fourth heat exchanger; a twenty-fifth valve (64) is connected to the second outlet (74) of the fourth heat exchanger; a twenty-second valve (66) is connected to the first inlet (76) of the fourth heat exchanger; a twenty-third valve (68) is connected to the first outlet (78) of the fourth heat exchanger; a twenty-sixth valve (70) is connected to the third outlet (80) of the fourth heat exchanger.