CN109879342B - Sour water stripper distillate heat utilization device and method - Google Patents
Sour water stripper distillate heat utilization device and method Download PDFInfo
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- CN109879342B CN109879342B CN201910326648.0A CN201910326648A CN109879342B CN 109879342 B CN109879342 B CN 109879342B CN 201910326648 A CN201910326648 A CN 201910326648A CN 109879342 B CN109879342 B CN 109879342B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 238000000034 method Methods 0.000 title claims abstract description 25
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 175
- 239000007788 liquid Substances 0.000 claims abstract description 124
- 238000000926 separation method Methods 0.000 claims abstract description 121
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 86
- 239000000463 material Substances 0.000 claims abstract description 50
- 238000010992 reflux Methods 0.000 claims abstract description 31
- 238000011084 recovery Methods 0.000 claims abstract description 24
- 238000010168 coupling process Methods 0.000 claims abstract description 20
- 230000008878 coupling Effects 0.000 claims abstract description 19
- 238000005859 coupling reaction Methods 0.000 claims abstract description 19
- 239000007791 liquid phase Substances 0.000 claims abstract description 16
- 230000002378 acidificating effect Effects 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 89
- 239000008213 purified water Substances 0.000 claims description 48
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 42
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 40
- 239000002994 raw material Substances 0.000 claims description 31
- 239000002253 acid Substances 0.000 claims description 26
- 230000008569 process Effects 0.000 claims description 17
- 239000012071 phase Substances 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 9
- 238000001802 infusion Methods 0.000 claims description 7
- 230000001105 regulatory effect Effects 0.000 claims 1
- 229910052717 sulfur Inorganic materials 0.000 description 23
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 18
- 239000002904 solvent Substances 0.000 description 18
- 239000011593 sulfur Substances 0.000 description 18
- 230000008929 regeneration Effects 0.000 description 8
- 238000011069 regeneration method Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- 238000007664 blowing Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004321 preservation Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000003303 reheating Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000011982 device technology Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a device and a method for heat utilization of an acidic water stripper distillate, comprising a heat recovery unit for performing heat energy coupling utilization on an ammonia-containing material output from the top of a stripper, wherein the heat recovery unit comprises at least two gas-liquid separation tanks, wherein a first gas pipeline connected with an inlet of the first gas-liquid separation tank can control higher pressure according to requirements by arranging a pressure control valve, so that a pipeline in front of the pressure control valve and a heat utilization unit of an adjacent section perform heat energy efficient coupling utilization, a subsequent gas-liquid separation part can also adopt lower operating pressure, the ammonia concentration of water in the first gas-liquid separation tank is reduced, and a liquid-phase material in the subsequent gas-liquid separation tank is a pipeline in front of the first gas-liquid separation tank, so that an ammonia concentration circulation unit independent of the stripper is formed between the first gas-liquid separation tank and the subsequent gas-liquid separation tank, the reflux of the high ammonia concentration material at the top of the stripper is avoided, and the operation efficiency of the heat utilization of the stripper is improved.
Description
Technical Field
The invention relates to a device and a method for utilizing heat of a distillate of an acid water stripping tower.
Background
The acid water stripping device is used for treating mixed acid water discharged from various devices in the whole plant, the products are acid gas (hydrogen sulfide), ammonia and purified water, the purified water is sent to an upstream device for recycling, the acid gas is sent to a sulfur recovery part, and the ammonia is taken as a product sending device. Existing acid water stripping generally has three processes:
(1) A single-tower low-pressure full blowing process: and (3) under the lower operation pressure of the stripping tower, H 2 S and NH 3 in the acidic water are stripped completely, the top ammonia-containing acidic gas is sent to an ammonia burning nozzle of a sulfur recovery device, and the purified water at the bottom of the tower can be recycled.
(2) Single tower pressurized stripping process: the method is characterized in that hydrogen sulfide is stripped from the top of a stripping tower by utilizing the characteristic that the relative volatility of the hydrogen sulfide is higher than that of ammonia, acid gas at the top of the stripping tower can be sent to a sulfur recovery device for recovering sulfur, ammonia in a liquid phase and residual hydrogen sulfide are driven out to a gas phase at the lower part of the stripping tower under the action of stripping steam, so that purified water quality meets the requirement, high ammonia-rich gas is formed at the middle part of the stripping tower, the ammonia-rich gas is extracted, and the ammonia-rich gas is cooled, depressurized and condensed to obtain liquid ammonia.
(3) A double-tower pressurized stripping process: under the condition of arranging a hydrogen sulfide stripping tower and an ammonia stripping tower, the acid water is advanced into the hydrogen sulfide stripping tower and then is fed into the ammonia stripping tower for stripping respectively. The acid gas at the top of the hydrogen sulfide stripping tower can be sent to a sulfur recovery device for recovering sulfur, and the gas ammonia at the top of the ammonia stripping tower is refined and compressed to prepare liquid ammonia which can be recycled or used as chemical raw materials.
In the process of acid water stripping technology, the existing acid water stripping device always has a strand of tower top material or middle extracted material which is cooled by heat exchange of an air or water cooler, the heat energy is transferred into the atmosphere and is wasted, the heat energy is large in quantity (a large amount of water vapor exists in distilled medium and a large amount of latent heat energy exists), the maximum optimal utilization is not obtained, and the energy waste is caused; on the other hand, the top reflux mode of the existing sour water stripping device is to concentrate the liquid phases in each liquid separating tank together and directly reflux the liquid phases to the top of the tower, and the pressure control of the stripping tower is generally realized through a pressure control valve arranged on a gas phase output pipeline of the gas separating tank at the top of the tower, for example, the pressure lifting operation is directly carried out, when the reflux components at the top of the tower return into the tower, the reflux components at the top of the tower inevitably increase the ammonia components in the gas at the top of the tower correspondingly, the partial pressure of the water vapor in the stripping tower is reduced, the heat utilization efficiency of the gas at the top of the tower is greatly reduced, the load of the stripping tower is greatly increased, and the production cost of sour water treatment is improved.
Disclosure of Invention
The first technical problem to be solved by the invention is to provide an acid water stripper distillate heat utilization device capable of efficiently utilizing heat energy of an acid water stripper distillate.
The invention solves the first technical problem by adopting the technical scheme that: the utility model provides a sour water stripper distillate heat utilization device, includes at least one stripper and carries out the heat recovery unit that heat energy coupling utilized with the ammonia-containing material of the top output of corresponding stripper, this heat recovery unit includes the first gas-liquid separation jar that is used for carrying out the gas-liquid separation to the ammonia-containing material of the top output from the stripper, the top of stripper passes through first gas line and connects the import of first gas-liquid separation jar, the bottom of first gas-liquid separation jar passes through first backflow pipeline and connects the top of stripper, be equipped with on the first gas line in proper order and be used for carrying out the heat exchanger that exchanges heat with the heat unit of adjacent workshop section and be used for carrying out the pressure control valve of regulation to the top pressure of stripper; the device comprises a first gas-liquid separation tank, and is characterized by further comprising a first gas-liquid separation tank, wherein the top of the first gas-liquid separation tank is connected to the inlet of the first gas-liquid separation tank through a first gas pipeline, a first heat exchanger for exchanging heat with an acid water raw material pipeline is arranged on the first gas pipeline, the bottom of the first gas-liquid separation tank is connected to the first gas pipeline through a first backflow pipeline, the position of a connecting point of the first backflow pipeline and the first gas pipeline is positioned at the lower stream of the pressure control valve, and the top of the first gas-liquid separation tank is connected with a second gas pipeline for conveying gas-phase materials.
In order to fully mix the liquid phase separated by the second gas-liquid separation tank with the materials in the first gas pipeline, so as to improve the liquid separation effect of the first gas-liquid separation tank, the first gas pipeline is also provided with a pipeline mixer, the pipeline mixer is positioned at the downstream of the pressure control valve, and the position of the connecting point of the second reflux pipeline and the first gas pipeline is positioned between the pressure control valve and the pipeline mixer.
In order to efficiently utilize the heat energy of the purified water output from the bottom of the stripping tower, the bottom of the stripping tower is also provided with a purified water output pipeline, a third heat exchanger for exchanging heat with an acidic water raw material pipeline and a first cooler for further cooling the purified water are arranged on the purified water output pipeline, and the first cooler is positioned at the downstream of the third heat exchanger; the purified water output pipeline is also provided with the first tributary pipeline, and the connection point position of the first tributary pipeline and the purified water output pipeline is positioned between the first cooler and the third heat exchanger. The first branch pipeline can lead out high-temperature purified water to reduce circulating water for cooling of the first cooler and reduce heat input required by reheating the purified water to the utilization part.
In order to improve the gas-liquid separation effect of the second gas-liquid separation tank, a second cooler is further arranged on the second gas transmission pipeline and is positioned at the downstream of the second heat exchanger.
In order to regulate the temperature and flow of the top reflux material of the stripping tower, a third cooler and a first pump are sequentially arranged on the first reflux line, and a second pump is arranged on the second reflux line.
In order to further improve the concentration of ammonia components in the distillate, a third gas-liquid separation tank is further arranged at the downstream of the second gas-liquid separation tank, the third gas pipeline is connected with an inlet of the third gas-liquid separation tank through a fourth cooler, the bottom of the third gas-liquid separation tank is connected to the second return pipeline through a third return pipeline, and the top of the third gas-liquid separation tank is connected with a fourth gas pipeline for conveying gas-phase materials.
As another preferred embodiment, the number of the stripping towers is two, namely a hydrogen sulfide stripping tower and an ammonia stripping tower which are sequentially connected in series, the heat recovery unit is connected with the top of the ammonia stripping tower, the bottom of the ammonia stripping tower is connected with a purified water output pipeline, an acidic water raw material pipeline is connected with the hydrogen sulfide stripping tower, the bottom of the hydrogen sulfide stripping tower is connected with the ammonia stripping tower through a first infusion pipeline, and the top of the hydrogen sulfide stripping tower is connected with a fifth gas pipeline for conveying hydrogen sulfide.
As an improvement, the first infusion pipeline is provided with a third pump and a fourth heat exchanger for exchanging heat with the acid water raw material pipeline.
The second technical problem to be solved by the invention is to provide a method for utilizing heat of the sour water stripper distillate, which can effectively utilize the heat energy of the sour water stripper distillate.
The invention solves the second technical problem by adopting the technical proposal that: the operation pressure of the corresponding stripping tower is increased to 0.25-0.6MPa, and ammonia-containing materials output from the top of the stripping tower are conveyed to a heat recovery unit; the ammonia-containing material firstly exchanges heat with a heat utilization unit of an adjacent working section through a first heat exchanger, then is decompressed through a pressure control valve and enters a first gas-liquid separation tank for gas-liquid separation, wherein a liquid phase separated by the first gas-liquid separation tank is further cooled through a third cooler, is pressurized through a first pump and is then conveyed to the top of the stripping tower through a first backflow pipeline; the gas phase separated from the first gas-liquid separation tank is output through the second gas pipeline, enters the second gas-liquid separation tank for gas-liquid separation after heat exchange with the acid water raw material pipeline through the second heat exchanger, wherein the liquid phase separated by the second gas-liquid separation tank is pressurized through a second pump and returns to the first gas pipeline through the second return pipeline, is mixed with the material decompressed by the pressure control valve in the first gas pipeline, is further blended through a pipeline mixer and is then conveyed to the first gas-liquid separation tank, and thus an ammonia concentration circulation unit is formed; the gas phase separated from the second gas-liquid separation tank is sent downstream through the third gas line.
As another preferred embodiment, the two stripping towers are respectively a hydrogen sulfide stripping tower and an ammonia stripping tower which are sequentially connected in series, wherein after the ammonia stripping tower is subjected to pressure increasing operation, ammonia-containing materials are output from the top of the ammonia stripping tower and enter the heat recovery unit; the purified water output from the bottom of the ammonia stripping tower is divided into two streams, wherein one stream of purified water exchanges heat with the raw material of the acid water for the first time through a third heat exchanger, then is further cooled by a first cooler and is sent to the downstream, and the other stream of purified water exchanges heat with the raw material of the acid water through the third heat exchanger and is directly used as high-temperature purified water for the downstream; the sour water raw material firstly exchanges heat with a gas phase separated from a first gas-liquid separation tank for the first time through a second heat exchanger, and then exchanges heat with purified water output from the bottom of an ammonia stripping tower through a third heat exchanger for the second time, and enters the hydrogen sulfide stripping tower; the ammonia-rich material output from the bottom of the hydrogen sulfide stripping tower exchanges heat with the sour water raw material through a fourth heat exchanger, is pressurized by a third pump and is conveyed into the ammonia stripping tower; the hydrogen sulfide gas output from the top of the hydrogen sulfide stripping tower is sent to the downstream through a fifth gas pipeline.
Compared with the prior art, the invention has the advantages that: the sour water stripper distillate heat utilization device is characterized in that at least two gas-liquid separation tanks are arranged on the top of the stripping tower on the basis of carrying out pressure-increasing operation on the corresponding stripping tower, wherein a first gas pipeline connected with the inlet of the first gas-liquid separation tank ensures stable control of the operation pressure of the stripping tower through arranging a pressure-controlled valve, and can control higher pressure according to requirements, so that the pipeline in front of the pressure-controlled valve and a heat utilization unit (such as a reboiler or a feed heat exchanger with the bottom material temperature of a sulfur plant solvent regeneration tower needing to utilize heat energy below 150 ℃) of an adjacent section carry out efficient coupling utilization of heat energy, and secondly, the arrangement of the pressure-controlled valve can enable a subsequent gas-liquid separation part to adopt lower operation pressure as much as possible, so that the ammonia concentration in the first gas-liquid separation tank is reduced, the ammonia carrying quantity is reduced in a way of directly returning to the top of the stripping tower as reflux after the original process is cooled simply, the partial pressure of vapor at the top of the stripping tower is further improved, and the heat utilization operation efficiency of the stripping tower is improved; on the other hand, the heat utilization device is characterized in that liquid phase materials in the subsequent gas-liquid separation tanks (the second gas-liquid separation tank and the third gas-liquid separation tank) with relatively low temperature and high ammonia concentration are pumped back into a pipeline behind a pressure control valve of the stripping tower, and are further mixed, gasified and separated with medium materials behind the pressure control valve, so that an ammonia concentration circulation unit independent of the stripping tower is formed between the first gas-liquid separation tank and the subsequent gas-liquid separation tank, and compared with the mode of taking all liquid separation tanks together as tower top reflux in the prior art, the reflux of high ammonia concentration materials at the tower top is avoided, and the partial pressure of water vapor at the top of the stripping tower and the heat utilization operation efficiency of the stripping tower are further improved; in addition, the sour water stripper distillate heat utilization device provides a new way for utilizing the waste heat of the sour water stripper and a new method for controlling the pressure of the stripper, can be conveniently applied to the existing single-tower low-pressure full-blowing process, single-tower pressurized stripping process and double-tower pressurized stripping process, and can flexibly adjust working conditions such as surplus or insufficient heat energy on the basis of keeping the original flow of the adjacent sections when the heat utilization device is used for carrying out heat energy coupling with a heat utilization unit of the adjacent sections.
Drawings
FIG. 1 is a schematic diagram of the sour water stripper distillate heat utilization apparatus of example 1 of the present invention;
FIG. 2 is a schematic diagram of the sour water stripper distillate heat utilization apparatus of example 2 of the present invention;
FIG. 3 is a schematic diagram of a sour water stripper distillate heat utilization unit thermally coupled to a sulfur plant solvent regenerator, wherein the first heat exchanger is utilized thermally coupled as a feed heat exchanger to the solvent regenerator;
Fig. 4 is a schematic diagram of a structure of a sour water stripper distillate heat utilization device and a sulfur plant solvent regeneration tower for heat coupling utilization, wherein the first heat exchanger is used as a reboiler of the solvent regeneration tower for heat coupling utilization.
Detailed Description
The technical scheme of the invention is further specifically described below by means of examples and with reference to the accompanying drawings.
Example 1
Referring to fig. 1, an embodiment of applying the sour water stripper distillate heat utilization device to a single-tower full-blowing process is shown, wherein the ammonia-containing material distilled from the top of the stripper is a mixture of H 2 S and NH 3, purified water output from the bottom of the stripper can be recycled, specifically, in the single-tower full-blowing process, the stripper can strip out all H 2 S and NH 3 in the sour water, and then send the ammonia-containing sour gas to an ammonia burning nozzle of a sulfur recovery device after gas-liquid separation, which is common knowledge of the existing sour water stripper device technology and is not repeated herein.
In this embodiment, the heat recovery unit a is mainly configured to perform heat energy coupling utilization on an ammonia-containing material distilled from the top of the stripping tower 10, and specifically, the heat recovery unit a includes a first gas-liquid separation tank 20, a second gas-liquid separation tank 40, a first heat exchanger 30, a second heat exchanger 32, and a pressure control valve 31, where the first gas-liquid separation tank 20 is used for performing gas-liquid separation on the ammonia-containing material output from the top of the stripping tower, specifically, the top of the stripping tower is connected to an inlet of the first gas-liquid separation tank 20 through a first gas pipeline 21, a bottom of the first gas-liquid separation tank 20 is connected to the top of the stripping tower through a first reflux pipeline 22, and a third cooler 36 and a first pump 37 are sequentially disposed on the first reflux pipeline 22. The first heat exchanger 30 is arranged on the first gas pipeline 21 and is used for exchanging heat with a heat using unit of an adjacent working section, wherein the heat using unit of the adjacent working section can be a feeding heat exchanger or a tower bottom reboiler of a solvent regeneration tower of a sulfur plant which needs to utilize heat energy, the pressure control valve 31 is also arranged on the first gas pipeline 21 and is positioned at the downstream of the first heat exchanger 30 so as to perform stable control and adjustment on the tower top pressure of the stripping tower, namely, the pressure control valve 31 is arranged on a pipeline part of the first gas pipeline 21 which is cooled by the first heat exchanger 30 and is not subjected to vapor-liquid separation, the front pipeline is controlled to be high in pressure, and a vapor-liquid separation tank behind the pressure control valve 31 is controlled to be low in pressure as much as possible, so that the concentration of liquid phase ammonia in each vapor-liquid separation tank is reduced, and thus the circulation of ammonia components through reflux, the top of the stripping tower and the first heat exchanger 30 (namely, the reboiler or the heat exchanger of the heat using unit of the adjacent working section) is reduced, and the vapor partial pressure is increased. The second gas-liquid separation tank 40 is disposed downstream of the first gas-liquid separation tank 20, the top of the first gas-liquid separation tank 20 is connected to the inlet of the second gas-liquid separation tank 40 through a second gas line 23, and the second gas line 23 is provided with a second heat exchanger 32 for exchanging heat with the sour water raw material line 12, of course, in order to improve the gas-liquid separation effect of the second gas-liquid separation tank 40, the second gas line 23 may be further provided with a second cooler 11, specifically, in this embodiment, the second cooler 11 may be an air cooler or a water cooler, and still specifically, the second cooler 11 is located downstream of the second heat exchanger 32. The bottom of the second gas-liquid separation tank 40 is connected to the first gas pipeline 21 through a second backflow pipeline 41, wherein a second pump 38 is arranged on the second backflow pipeline 41, the position of a connection point on the second backflow pipeline 41 and the first gas pipeline 21 is located downstream of the pressure control valve 31, and a third gas pipeline 42 for conveying gas-phase materials is connected to the top of the second gas-liquid separation tank 40. In order to fully mix the liquid phase separated by the second gas-liquid separation tank 40 with the material in the first gas pipeline 21, so as to improve the liquid separation effect of the first gas-liquid separation tank 20, the first gas pipeline 21 is further provided with a pipeline mixer 33, the pipeline mixer 33 is located downstream of the pressure-controlled valve 31, and correspondingly, a connection point between the second reflux pipeline 41 and the first gas pipeline 21 is located between the pressure-controlled valve 31 and the pipeline mixer 33.
In this embodiment, the pressure control valve 31 is provided to ensure stable control of the operation pressure of the stripping tower, and control the higher pressure according to the requirement, so that the heat provided by the pipeline in front of the pressure control valve 31 can meet the requirement of coupling and utilizing the heat unit (such as a bottom material temperature reboiler or a feeding heat exchanger of a sulfur plant solvent regeneration tower which needs to utilize heat energy in the prior art, the temperature required by the reboiler is generally 130-150 ℃, see fig. 3 and fig. 4 in detail), and secondly, the pressure control valve 31 is provided to enable the subsequent gas-liquid separation part to adopt lower operation pressure as much as possible, thereby reducing the ammonia concentration of water in the first gas-liquid separation tank 20, reducing the ammonia carrying amount in a way of directly returning to the top of the tower as reflux after simple cooling and liquid separation in comparison with the prior art, further improving the steam-water partial pressure at the top of the stripping tower and improving the heat utilization operation efficiency of the stripping tower; on the other hand, the heat utilization device is characterized in that liquid phase materials in the second gas-liquid separation tank 40 with relatively low temperature and high ammonia concentration are pumped back to a pipeline behind the pressure control valve 31 of the stripping tower, and are further mixed, gasified and separated with medium materials behind the pressure control valve 31, so that an ammonia concentration circulating unit B independent of the stripping tower is formed between the first gas-liquid separation tank 20 and the subsequent gas-liquid separation tank, and compared with the mode of centralizing the gas-liquid separation tanks together as tower top reflux in the prior art, the reflux of high ammonia concentration materials at the tower top is avoided, the load of the stripping tower is reduced, and the partial pressure of water vapor at the top of the stripping tower and the heat utilization operation efficiency of the stripping tower are further improved.
With continued reference to fig. 1, in order to make efficient use of the heat energy of the purified water output from the bottom of the stripper, the bottom of the respective stripper is further provided with a purified water output line 111, the purified water output line 111 being provided with a third heat exchanger 34 for exchanging heat with the sour water feed line 12 and a first cooler 35 for further cooling the purified water, the first cooler 35 being located downstream of the third heat exchanger 34; the purified water output line 111 is further provided with a first branch line 112, and a connection point between the first branch line 112 and the purified water output line 111 is located between the third heat exchanger 34 and the first cooler 35, wherein the first branch line 112 can lead out high-temperature purified water to reduce the consumption of circulating water for cooling the first cooler 35 and reduce the heat input required for reheating the purified water from the reuse part.
In this example, the process flow using the sour water stripper distillate heat utilization apparatus is: the temperature range of the overhead gas ammonia-containing material of the existing sour water stripper is generally 115-120 degrees, which cannot be directly utilized by the heat utilization units of the adjacent sections, so that the heat utilization units of the adjacent sections (especially a reboiler or a feed heat exchanger which needs to utilize heat energy and has the bottom material temperature of the solvent regeneration tower of a sulfur plant below 150 ℃) and the overhead gas material distilled from the overhead of the stripper in the embodiment can be utilized in a high-efficiency heat energy coupling way, the operation pressure of the stripper needs to be increased and the operation pressure of the stripper needs to be stably controlled at 0.25-0.6MPa through a pressure control valve, and particularly, the operation pressure of the stripper is preferably 0.3-0.45MPa.
Delivering a mixed material of H 2 S and NH 3 which are output from the top of the stripping tower to a heat recovery unit A, wherein the mixed material exchanges heat with a heat utilization unit of an adjacent section through a first heat exchanger 30 (namely a reboiler or a heat exchanger of the heat utilization unit of the adjacent section), then the mixed material is decompressed through a pressure control valve 31 and enters a first gas-liquid separation tank 20 for gas-liquid separation, wherein a liquid phase separated by the first gas-liquid separation tank 20 is further cooled through a third cooler 36, pressurized through a first pump 37 and then delivered to the top of the stripping tower 10 through a first reflux pipeline 22; the gas phase separated from the first gas-liquid separation tank 20 is output through a second gas pipeline 23, exchanges heat with the acid water raw material pipeline 12 through a second heat exchanger 32, is further cooled by a second cooler 11 to about 45 ℃ and enters a second gas-liquid separation tank 40 for gas-liquid separation again, wherein the liquid phase separated by the second gas-liquid separation tank 40 is pressurized by a second pump 38 and returns to the first gas pipeline 21 through a second reflux pipeline 41, is mixed with the material decompressed by the pressure control valve 31 in the first gas pipeline 21, is further blended by a pipeline mixer 33 and is then conveyed to the first gas-liquid separation tank 20, and thus an ammonia concentrating and circulating unit B is formed; the mixture of H 2 S and NH 3 separated from the second gas-liquid separation tank 40 is transported downstream via the third gas line 42.
The purified water output from the bottom of the ammonia stripping tower 10 is divided into two streams, wherein one stream of purified water exchanges heat with the sour water raw material for the first time through the third heat exchanger 34, is further cooled by the first cooler 35 and then sent to the downstream, and the other stream of purified water exchanges heat with the sour water raw material through the third heat exchanger 34, has the temperature of about 100 ℃, and can be directly used as low-temperature heat of other devices. In the traditional acid water stripping tower process, the purified water at the bottom of the stripping tower is directly discharged out of the device to a sewage treatment plant through cooling, and the embodiment provides a new scheme for using the high-temperature purified water, so that the circulating water for cooling a cooler can be reduced, and the heat input required by heating the purified water to the utilization part is reduced, thereby maximally utilizing the heat energy. In addition, when being worth noting, the traditional acid water stripping tower top pipeline is originally cooled, so that heat preservation treatment is not carried out, and the heat coupling is changed into heat coupling utilization, so that heat preservation design is needed, and meanwhile, when high-temperature purified water needs to be utilized, heat preservation treatment is needed to be carried out on the pipeline.
The application of the sour water stripper distillate heat utilization apparatus of this example will be further described with reference to a desulfurization solvent regeneration apparatus that has the most thermal coupling advantage to the sour water stripper.
Referring to fig. 3, a schematic diagram of a structure of a sour water stripper distillate heat utilization device and a sulfur plant solvent regenerator for performing heat coupling utilization is shown, wherein a first heat exchanger 30 of the sour water stripper distillate heat utilization device in this embodiment can be used as a feed heat exchanger of the solvent regenerator for performing heat coupling utilization (see a thickened portion of a diagram in fig. 3 for details), the process is applicable to the situation that the sour water stripper is far away from a device needing to utilize heat energy, the feed heat exchanger is arranged close to the sour water stripper, the elevation is as high as possible, the horizontal bending heat compensation of a pipeline is performed along, the solvent pipeline returned to the solvent regenerator after heat exchange is slightly enlarged, the pressure at the desulfurizing solvent end of the feed heat exchanger is reduced as much as possible, and the solvent is partially vaporized, so that heat energy is recovered.
Referring to fig. 4, a schematic diagram of the thermal coupling utilization of sour water stripper distillate heat utilization and sulfur plant solvent regenerator is shown, wherein the first heat exchanger 30 is utilized as a reboiler of the solvent regenerator. The process is suitable for the condition that the distance between the sour water stripping device and the device needing heat energy utilization is relatively short, in the thermal coupling process, the solvent regeneration tower of the sulfur device can keep one side of steam heating for adjusting and controlling the temperature of the tower bottom, the reformed reboiler (the first heat exchanger 30) can keep the original steam heating pipeline, the first gas liquid tank of the sour water stripping device is arranged close to the reboiler, the elevation is slightly lower than the reboiler, and the pipeline water attack is prevented.
Example 2
Referring to fig. 2, an embodiment of applying the sour water stripper distillate heat utilization device to a double-tower pressurized steam stripping process is shown, namely, in the case of setting a hydrogen sulfide steam stripping tower 101 and an ammonia steam stripping tower 102, sour water is advanced into the hydrogen sulfide steam stripping tower 101 and then is fed into the ammonia steam stripping tower 102 to be respectively stripped, wherein the sour gas at the top of the hydrogen sulfide steam stripping tower 101 can be sent to a sulfur recovery device to recover sulfur, and the gaseous ammonia at the top of the ammonia steam stripping tower 102 is refined and compressed to prepare liquid ammonia which can be recycled or used as chemical raw materials, which is common knowledge of the prior art of the sour water steam stripping tower device and is not repeated herein.
The heat recovery unit a flow arrangement in this embodiment and the manner of performing heat energy coupling utilization with the heat unit for the adjacent section are the same as those in embodiment 1, and the difference between this embodiment and embodiment 1 is that: in the embodiment, two stripping towers are respectively a hydrogen sulfide stripping tower 101 and an ammonia stripping tower 102 which are sequentially connected in series, a heat recovery unit A is connected with the top of the ammonia stripping tower 102 to carry out the transformation of heat energy coupling utilization on the material of the top of the tower, the bottom of the ammonia stripping tower 102 is connected with a purified water output pipeline 111, an acid water raw material pipeline 12 is connected with the hydrogen sulfide stripping tower 101, the bottom of the hydrogen sulfide stripping tower 101 is connected with the ammonia stripping tower 102 through a first infusion pipeline 13, the top of the hydrogen sulfide stripping tower 101 is connected with a fifth air pipeline 14 for conveying hydrogen sulfide, a third pump 16 and a fourth heat exchanger 15 for carrying out heat exchange with the acid water raw material pipeline 12 are arranged on the first infusion pipeline 13, the sour water raw material pipeline 12 is divided into a first raw material pipeline 121 and a second raw material pipeline 122, wherein the first raw material pipeline 121 directly drives a part of the sour water raw material into the hydrogen sulfide stripping tower 101, the second raw material pipeline 122 sequentially passes through the second heat exchanger 32, the third heat exchanger 34 and the fourth heat exchanger 15, and sequentially exchanges heat with the gas phase material in the second gas pipeline 23, the high-temperature purified water in the purified water output pipeline and the ammonia-rich material in the first infusion pipeline 13, and then enters the hydrogen sulfide stripping tower 101, so that the maximum utilization of heat energy is realized.
The ammonia-rich material output from the bottom of the hydrogen sulfide stripping tower 101 exchanges heat with the sour water raw material through the fourth heat exchanger 15, is pressurized by the third pump 16 and then is conveyed to the ammonia stripping tower 102, and the hydrogen sulfide gas output from the top of the hydrogen sulfide stripping tower 101 is conveyed to the downstream through the fifth gas pipeline 14.
In addition, in the heat recovery unit a of the present embodiment, in order to further increase the concentration of the ammonia component in the distillate, a third gas-liquid separation tank 60 is further disposed downstream of the second gas-liquid separation tank 40, the third gas line 42 is connected to the inlet of the third gas-liquid separation tank 60 through a fourth cooler 39, the bottom of the third gas-liquid separation tank 60 is connected to the second reflux line 41 through a third reflux line 61, that is, the high-concentration ammonia-containing liquid phase separated by the second gas-liquid separation tank 40 and the third gas-liquid separation tank 60 is pumped by the second pump 38 and then pumped back to the gas-liquid pipeline after the pressure-controlled valve 31 at the inlet of the first gas-liquid separation tank 20, and is mixed into the first gas-liquid separation tank 20 through the pipeline mixer 33 for gas-liquid separation, and the top of the third gas-liquid separation tank 60 is connected to a fourth gas line 62 for conveying NH 3 material. Of course, the third gas-liquid separation tank 60 may be omitted when the gas phase outputted from the outlet of the first gas-liquid separation tank 20 is directly cooled to 45 ℃ by heat exchange of the sour water feed and cooling by the second cooler 11.
Claims (9)
1. A sour water stripper distillate heat utilization apparatus, characterized by: the device comprises at least one stripping tower and a heat recovery unit (A) for carrying out heat energy coupling utilization on ammonia-containing materials output from the top of the corresponding stripping tower, wherein the heat recovery unit (A) comprises a first gas-liquid separation tank (20) for carrying out gas-liquid separation on the ammonia-containing materials output from the top of the stripping tower, the top of the stripping tower is connected with an inlet of the first gas-liquid separation tank (20) through a first gas pipeline (21), the bottom of the first gas-liquid separation tank (20) is connected with the top of the stripping tower through a first reflux pipeline (22), and a first heat exchanger (30) for carrying out heat exchange with a heat utilization unit of an adjacent section and a pressure control valve (31) for regulating the pressure of the top of the stripping tower are sequentially arranged on the first gas pipeline (21);
The system further comprises a second gas-liquid separation tank (40), wherein the top of the first gas-liquid separation tank (20) is connected to an inlet of the second gas-liquid separation tank (40) through a second gas pipeline (23), a second heat exchanger (32) for exchanging heat with an acid water raw material pipeline (12) is arranged on the second gas pipeline (23), the bottom of the second gas-liquid separation tank (40) is connected to the first gas pipeline (21) through a second reflux pipeline (41), the position of a connecting point of the second reflux pipeline (41) and the first gas pipeline (21) is located at the downstream of the pressure control valve (31), and a third gas pipeline (42) for conveying gas phase materials is connected to the top of the second gas-liquid separation tank (40);
The first gas pipeline (21) is further provided with a pipeline mixer (33), the pipeline mixer (33) is located at the downstream of the pressure control valve (31), and the position of the connecting point of the second reflux pipeline (41) and the first gas pipeline (21) is located between the pressure control valve (31) and the pipeline mixer (33).
2. The sour water stripper distillate heat utilization apparatus of claim 1, wherein: the bottom of the stripping tower is also provided with a purified water output pipeline (111), a third heat exchanger (34) for exchanging heat with the sour water raw material pipeline (12) and a first cooler (35) for further cooling purified water are arranged on the purified water output pipeline (111), and the first cooler (35) is positioned at the downstream of the third heat exchanger (34);
the purified water output pipeline (111) is also provided with a first branch pipeline (112), and the connection point position of the first branch pipeline (112) and the purified water output pipeline (111) is positioned between the first cooler (35) and the third heat exchanger (34).
3. The sour water stripper distillate heat utilization apparatus of claim 1, wherein: the second gas pipeline (23) is also provided with a second cooler (11), and the second cooler (11) is positioned downstream of the second heat exchanger (32).
4. The sour water stripper distillate heat utilization apparatus of claim 1, wherein: the first return line (22) is provided with a third cooler (36) and a first pump (37) in sequence, and the second return line (41) is provided with a second pump (38).
5. The sour water stripper distillate heat utilization apparatus of claim 1, wherein: the downstream of the second gas-liquid separation tank (40) is further provided with a third gas-liquid separation tank (60), the third gas pipeline (42) is connected with an inlet of the third gas-liquid separation tank (60) through a fourth cooler (39), the bottom of the third gas-liquid separation tank (60) is connected to the second reflux pipeline (41) through a third reflux pipeline (61), and the top of the third gas-liquid separation tank (60) is connected with a fourth gas pipeline (62) for conveying gas-phase materials.
6. The sour water stripper distillate heat utilization apparatus of any one of claims 1-5, wherein: the stripping towers are two hydrogen sulfide stripping towers (101) and an ammonia stripping tower (102) which are sequentially connected in series, the heat recovery unit (A) is connected with the top of the ammonia stripping tower (102), the bottom of the ammonia stripping tower (102) is connected with a purified water output pipeline (111), an acidic water raw material pipeline (12) is connected with the hydrogen sulfide stripping tower (101), the bottom of the hydrogen sulfide stripping tower (101) is connected with the ammonia stripping tower (102) through a first infusion pipeline (13), and the top of the hydrogen sulfide stripping tower (101) is connected with a fifth gas pipeline (14) for conveying hydrogen sulfide.
7. The sour water stripper distillate heat utilization apparatus of claim 6, wherein: the first infusion pipeline (13) is provided with a third pump (16) and a fourth heat exchanger (15) for exchanging heat with the acid water raw material pipeline (12).
8. A heat utilization process employing a sour water stripper distillate heat utilization apparatus of any one of claims 1-5, characterized by: the operating pressure of the corresponding stripping tower is increased to 0.25-0.6MPa, and the ammonia-containing material output from the top of the stripping tower is conveyed to the heat recovery unit (A);
The ammonia-containing material firstly exchanges heat with a heat utilization unit of an adjacent working section through a first heat exchanger (30), then is decompressed through a pressure control valve (31) and enters a first gas-liquid separation tank (20) for gas-liquid separation, wherein a liquid phase separated by the first gas-liquid separation tank (20) is further cooled through a third cooler (36), is pressurized through a first pump (37) and is then conveyed to the top of the stripping tower through a first reflux pipeline (22);
The gas phase separated from the first gas-liquid separation tank (20) is output through the second gas pipeline (23), exchanges heat with the acid water raw material pipeline (12) through the second heat exchanger (32), enters the second gas-liquid separation tank (40) for gas-liquid separation again, wherein the liquid phase separated by the second gas-liquid separation tank (40) is pressurized through the second pump (38) and then returns to the first gas pipeline (21) through the second reflux pipeline (41), is mixed with the material decompressed by the pressure control valve (31) in the first gas pipeline (21), is further blended through the pipeline mixer (33) and then is conveyed into the first gas-liquid separation tank (20), so that an ammonia concentrating and circulating unit (B) is formed;
the gas phase separated from the second gas-liquid separation tank (40) is sent downstream through the third gas line (42).
9. The heat utilization method according to claim 8, characterized in that: the two stripping towers are respectively a hydrogen sulfide stripping tower (101) and an ammonia stripping tower (102) which are sequentially connected in series, wherein after the ammonia stripping tower (102) is subjected to pressure-increasing operation, ammonia-containing materials are output from the top of the ammonia stripping tower (102) and enter the heat recovery unit (A);
The purified water output from the bottom of the ammonia stripping tower (102) is divided into two streams, wherein one stream of purified water exchanges heat with the raw sour water for the first time through a third heat exchanger (34), then is further cooled by a first cooler (35) and is sent to the downstream, and the other stream of purified water exchanges heat with the raw sour water through the third heat exchanger (34) and is directly used as high-temperature purified water for the downstream;
The sour water raw material firstly exchanges heat with a gas phase separated from a first gas-liquid separation tank (20) through a second heat exchanger (32), then exchanges heat with purified water output from the bottom of an ammonia stripping tower (102) through a third heat exchanger (34) for the second time, and enters the hydrogen sulfide stripping tower (101);
the ammonia-rich material output from the bottom of the hydrogen sulfide stripping tower (101) exchanges heat with the sour water raw material through a fourth heat exchanger (15), is pressurized by a third pump (16) and is conveyed into the ammonia stripping tower (102);
The hydrogen sulfide gas outputted from the top of the hydrogen sulfide stripping column (101) is sent downstream via a fifth gas line (14).
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