CN110606470B - Device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid - Google Patents
Device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid Download PDFInfo
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- CN110606470B CN110606470B CN201910598887.1A CN201910598887A CN110606470B CN 110606470 B CN110606470 B CN 110606470B CN 201910598887 A CN201910598887 A CN 201910598887A CN 110606470 B CN110606470 B CN 110606470B
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- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
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Abstract
The invention relates to a device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid, which comprises a hydrogen chloride resolving system and a calcium chloride concentrating and evaporating system, wherein the hydrogen chloride resolving system comprises a jet mixer, a resolving tower, a hydrogen chloride primary condenser, a hydrogen chloride secondary condenser, a demister, a condensed acid tank, a resolving reboiler and a resolving condensed water tank; the calcium chloride concentration evaporation system comprises a first-effect evaporator, a first-effect flash tank, a first-effect condensation water tank, a second-effect evaporator, a second-effect flash tank, a second-effect condensation water tank, a third-effect evaporator, a third-effect flash tank, a third-effect condensation water tank, a third-effect discharge preheater, an evaporation condenser, a vacuum buffer tank and a water flow jet pump vacuum unit. The invention has the advantages that: the device for producing the hydrogen chloride by concentrating and analyzing the hydrochloric acid can improve the gas content of the hydrogen chloride and further save energy consumption.
Description
Technical Field
The invention relates to a hydrogen chloride production device, in particular to a device for producing hydrogen chloride by concentrating and analyzing hydrochloric acid.
Background
The main principle of the present hydrogen chloride is that concentrated hydrochloric acid falls down from the top of a resolving tower, high-temperature hydrogen chloride and water vapor are introduced from the bottom of the resolving tower, and heat exchange is realized in the tower, so that the hydrogen chloride gas in the concentrated hydrochloric acid is resolved and separated. Before the concentrated hydrochloric acid is introduced into the resolving tower, heat exchange is carried out on the concentrated hydrochloric acid and the diluted hydrochloric acid in the double-effect heat exchanger, and in general, the concentrated hydrochloric acid enters from the inlet of the bottom shell pass and then flows out from the outlet of the top shell pass, and the diluted hydrochloric acid passes through the shell pass. As the temperature of the concentrated hydrochloric acid is increased, part of hydrogen chloride is separated out from the concentrated hydrochloric acid, so that air resistance exists in the shell side, and the acid loading amount is unstable. In addition, concentrated hydrochloric acid is sprayed into the desorption tower at high pressure, and if part of hydrogen chloride gas is mixed, two air flows are opposite, so that heat exchange is not facilitated.
Through retrieval, patent CN 108840310A discloses a device for producing hydrogen chloride by deep analysis from dilute hydrochloric acid and a process thereof, the device comprises a preheater, an analysis tower, a reboiler, a first-stage flash tower, a second-stage flash tower and a water treatment system, wherein the analysis tower is provided with a middle feed inlet, the water treatment system comprises a neutralization reaction kettle, a first-stage filtering device, a second-stage filtering device, a first-stage reverse osmosis device, a second-stage reverse osmosis device and an evaporation crystallization device, the feed inlet of the neutralization reaction kettle is communicated with a gas phase outlet of the second-stage flash tower through a pipeline, and a discharge port is sequentially communicated with a sand filter, an ultrafilter, the first-stage reverse osmosis device, the second-stage reverse osmosis device and an evaporator; the method has reasonable design, improves the feeding temperature by changing the feeding mode, enables the hydrochloric acid to be resolved more thoroughly, does not discharge waste liquid, directly obtains dry hydrogen chloride gas by resolving, does not need to carry out secondary drying, adopts double-effect evaporation for calcium chloride solution concentration, enables steam heat energy to be utilized for multiple times, improves the heat energy utilization rate, reduces the heat load of a system and saves energy consumption; however, the design of the invention still has certain disadvantages: 1. hydrochloric acid and calcium chloride solution are mixed after entering the analysis tower, and uneven mixing possibly exists, so that the content of hydrogen chloride gas obtained by final analysis is low; 2. the concentration of the calcium chloride solution adopts double-effect evaporation, so that the energy consumption can be saved, but the improvement still has room.
Therefore, it is necessary to develop a device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid, which can increase the gas content of hydrogen chloride and further save energy.
Disclosure of Invention
The invention aims to provide a device for producing hydrogen chloride by concentrating and resolving hydrochloric acid, which can improve the content of hydrogen chloride gas and further save energy consumption.
In order to solve the technical problems, the technical scheme of the invention is as follows: the utility model provides a concentrate device of analytical production hydrogen chloride in follow hydrochloric acid which characterized in that: comprises a hydrogen chloride analysis system and a calcium chloride concentration evaporation system,
the hydrogen chloride analysis system comprises a jet mixer, an analysis tower, a hydrogen chloride primary condenser, a hydrogen chloride secondary condenser, a demister, a condensed acid tank, an analysis reboiler and an analysis condensed water tank,
the bottom end of the jet mixer is provided with a 50% calcium chloride feeding pipeline communicated with the jet mixer, and one side end of the jet mixer is provided with a 31% hydrochloric acid feeding pipeline communicated with the jet mixer;
the center of the top end of the analytic tower is provided with a hydrogen chloride discharging pipeline A communicated with the analytic tower, and the center of the bottom end of the analytic tower is provided with a hydrogen chloride/water mixed gas discharging pipeline communicated with the analytic tower; a mixed liquid feeding pipeline and a hydrogen chloride feeding pipeline which are communicated with the resolving tower are sequentially arranged at one side end of the resolving tower from top to bottom, and the other end of the mixed liquid feeding pipeline is communicated with the jet mixer; a 40% calcium chloride discharging pipeline A communicated with the resolving tower is arranged at the lower part of the other side end of the resolving tower, and a three-effect feeding pump is arranged on the 40% calcium chloride discharging pipeline A in series;
the top end of the hydrogen chloride primary condenser is communicated with a hydrogen chloride discharge pipeline A, the bottom end of the hydrogen chloride primary condenser is provided with a concentrated hydrochloric acid discharge pipeline A communicated with the hydrogen chloride primary condenser, the upper part of one side end of the hydrogen chloride primary condenser is provided with a circulating water return pipeline A communicated with the hydrogen chloride primary condenser, and the other side end of the hydrogen chloride primary condenser is sequentially provided with a circulating water supply pipeline A and a hydrogen chloride discharge pipeline B which are communicated with the hydrogen chloride primary condenser from top to bottom;
the top end of the hydrogen chloride secondary condenser is communicated with the hydrogen chloride discharge pipeline B, the bottom end of the hydrogen chloride secondary condenser is provided with a concentrated hydrochloric acid discharge pipeline B communicated with the hydrogen chloride secondary condenser, and the other end of the concentrated hydrochloric acid discharge pipeline B is communicated with the concentrated hydrochloric acid discharge pipeline A; the upper part of one side end of the hydrogen chloride secondary condenser is provided with a circulating water return pipeline B communicated with the hydrogen chloride secondary condenser, and the other side end of the hydrogen chloride secondary condenser is sequentially provided with a circulating water supply pipeline B and a hydrogen chloride discharge pipeline C which are communicated with the hydrogen chloride secondary condenser from top to bottom;
one side end of the demister is communicated with the hydrogen chloride discharging pipeline C, and the other side end of the demister is provided with an industrial water feeding pipeline communicated with the demister; the center of the top end of the demister is provided with a hydrogen chloride discharging pipeline D communicated with the demister, the center of the bottom end of the demister is provided with a concentrated hydrochloric acid discharging pipeline C communicated with the demister, and the other end of the concentrated hydrochloric acid discharging pipeline C is communicated with a concentrated hydrochloric acid discharging pipeline A;
the top end of the condensed acid tank is communicated with the concentrated hydrochloric acid discharging pipeline A, the top end of the condensed acid tank is also provided with a hydrogen chloride discharging pipeline D communicated with the condensed acid tank, and the hydrogen chloride discharging pipeline D is communicated with the hydrogen chloride discharging pipeline C; a condensed acid discharging pipeline communicated with the condensed acid tank is arranged at the lower part of one side end of the condensed acid tank;
the top end of the desorption reboiler is communicated with the hydrogen chloride feeding pipeline, and the bottom end of the desorption reboiler is communicated with the hydrogen chloride/water mixed gas discharging pipeline; a saturated steam feeding pipeline A, a saturated steam discharging pipeline A and a condensed water discharging pipeline A which are communicated with the analysis reboiler are sequentially arranged at one side end of the analysis reboiler from top to bottom;
the analysis condensate water tank is arranged on the condensate water outlet pipeline A in series, and the top end of the analysis condensate water tank is communicated with the saturated steam discharge pipeline A;
the calcium chloride concentration evaporation system comprises a first-effect evaporator, a first-effect flash tank, a first-effect condensation water tank, a second-effect evaporator, a second-effect flash tank, a second-effect condensation water tank, a third-effect evaporator, a third-effect flash tank, a third-effect condensation water tank, a third-effect discharge preheater, an evaporation condenser, a vacuum buffer tank and a water flow jet pump vacuum unit;
the center of the bottom end of the first-effect evaporator is communicated with a 40% calcium chloride discharging pipeline A, and the center of the top end of the first-effect evaporator is provided with a 40% calcium chloride discharging pipeline B communicated with the first-effect evaporator; a saturated steam feeding pipeline B, a saturated steam discharging pipeline B and a condensed water discharging pipeline B which are communicated with the first-effect evaporator are sequentially arranged at one side end of the first-effect evaporator from top to bottom;
the first-effect condensate water tank is arranged on the condensate water outlet pipeline B in series, and the top end of the first-effect condensate water tank is communicated with the saturated steam outlet pipeline B;
one side end of the first-effect flash tank is communicated with a 40% calcium chloride discharging pipeline B, and the other side end of the first-effect flash tank is provided with a 43.3% calcium chloride discharging pipeline A communicated with the first-effect flash tank; the center of the top end of the first-effect flash tank is provided with a saturated steam feeding pipeline C communicated with the first-effect flash tank, the center of the bottom end of the first-effect flash tank is provided with a 40% calcium chloride discharging pipeline C communicated with the first-effect flash tank, and the other end of the 40% calcium chloride discharging pipeline C is communicated with a 40% calcium chloride discharging pipeline A;
the center of the bottom end of the two-effect evaporator is communicated with a 43.3% calcium chloride discharge pipeline A, and the center of the top end of the two-effect evaporator is provided with a 43.3% calcium chloride discharge pipeline B communicated with the two-effect evaporator; one side end of the two-effect evaporator is communicated with a saturated steam feeding pipeline C, and a saturated steam discharging pipeline C and a condensed water discharging pipeline C which are communicated with the two-effect evaporator are sequentially arranged at the side end of the two-effect evaporator at the lower part of the saturated steam feeding pipeline C from top to bottom;
the secondary condensate water tank is respectively communicated with the saturated steam discharging pipeline C and the condensate water discharging pipeline C, and a wastewater discharging pipeline A communicated with the secondary condensate water tank is arranged at the lower part of one side end of the secondary condensate water tank;
one side end of the secondary flash tank is communicated with a 43.3% calcium chloride discharge pipeline B, and the other side end of the secondary flash tank is provided with a 46.6% calcium chloride discharge pipeline A communicated with the secondary flash tank; the center of the top end of the secondary flash tank is provided with a saturated steam feeding pipeline D communicated with the secondary flash tank, the center of the bottom end of the secondary flash tank is provided with a 43.3% calcium chloride discharging pipeline C communicated with the secondary flash tank, and the other end of the 43.3% calcium chloride discharging pipeline C is communicated with a 43.3% calcium chloride discharging pipeline A;
the center of the bottom end of the triple effect evaporator is communicated with a 46.6% calcium chloride discharge pipeline A, and the center of the top end of the triple effect evaporator is provided with a 46.6% calcium chloride discharge pipeline B communicated with the triple effect evaporator; one side end of the triple-effect evaporator is communicated with a saturated steam feeding pipeline D, and a saturated steam discharging pipeline D and a wastewater discharging pipeline B which are communicated with the triple-effect evaporator are sequentially arranged at the side end of the triple-effect evaporator at the lower part of the saturated steam feeding pipeline D from top to bottom;
the three-effect condensation water tank is arranged on the wastewater outlet pipeline B in series, and the top end of the three-effect condensation water tank is communicated with the saturated steam outlet pipeline D;
one side end of the triple-effect flash tank is communicated with a 46.6% calcium chloride discharge pipeline B, and the other side end of the triple-effect flash tank is provided with a 50% calcium chloride discharge pipeline A communicated with the triple-effect flash tank; a saturated steam feeding pipeline E communicated with the triple-effect flash tank is arranged in the center of the top end of the triple-effect flash tank, a saturated steam feeding pipeline F is further communicated with the saturated steam feeding pipeline E, and the other end of the saturated steam feeding pipeline F is communicated with a saturated steam discharging pipeline D;
the three-effect discharge preheater is arranged on the condensed water outlet pipeline B and the 50% calcium chloride outlet pipeline A in series;
the top end of the evaporation condenser is communicated with a saturated steam feeding pipeline E, and a wastewater outlet pipeline C communicated with the evaporation condenser is arranged in the center of the bottom end of the evaporation condenser; one side end of the evaporation condenser is sequentially provided with a circulating water return pipeline C, a circulating water supply pipeline C and a vacuumizing pipeline A which are communicated with the evaporation condenser from top to bottom, and the other end of the vacuumizing pipeline A is communicated with a water flow jet pump vacuum unit;
the vacuum buffer tank is arranged on the wastewater outlet pipeline C in series, and a vacuum condensation wastewater pump is also arranged on the wastewater outlet pipeline C at the rear end of the vacuum buffer tank in series; the top of the vacuum buffer tank is also provided with a vacuumizing pipeline B communicated with the vacuum buffer tank, and the other end of the vacuumizing pipeline B is communicated with the vacuumizing pipeline A.
And a hot water feeding pipeline communicated with the 31% hydrochloric acid feeding pipeline is further arranged on the 31% hydrochloric acid feeding pipeline.
The hydrogen chloride discharging pipeline A is further provided with a nitrogen gas feeding pipeline communicated with the hydrogen chloride discharging pipeline A, and the nitrogen gas feeding pipeline close to one end of the hydrogen chloride discharging pipeline A is further provided with a check valve in series.
Two triple-effect feed pumps are arranged in parallel on a 40% calcium chloride discharge pipeline.
The side end of the demister is also provided with a concentrated hydrochloric acid discharging pipeline D communicated with the demister, and the other end of the concentrated hydrochloric acid discharging pipeline D is communicated with a concentrated hydrochloric acid discharging pipeline C; the concentrated hydrochloric acid discharging pipeline D is arranged at the lower end of the hydrogen chloride discharging pipeline C.
The 46.6% calcium chloride discharging pipeline B is also provided with a 50% calcium chloride discharging pipeline B in series, the other end of the 50% calcium chloride discharging pipeline B is communicated with a 50% calcium chloride discharging pipeline A at the front end of the three-effect discharging preheater, and the 50% calcium chloride discharging pipeline B is also provided with a three-effect discharging pump in series.
Two triple-effect discharging pumps are arranged in parallel on a 50% calcium chloride discharging pipeline B.
The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: the two vacuum condensation wastewater pumps are arranged on the wastewater outlet pipeline C in parallel.
The invention has the advantages that:
(1) According to the device for concentrating and analyzing the hydrogen chloride from the hydrochloric acid, the jet mixer is additionally arranged in front of the analyzing tower, and then 50% calcium chloride and 31% hydrochloric acid are uniformly mixed through the jet mixer and then sent to the analyzing tower for analysis, so that the hydrogen chloride can be fully analyzed, and the analyzed hydrogen chloride is separated into dilute hydrochloric acid and hydrogen chloride gas through the demister, so that the final hydrogen chloride content can be greatly improved; meanwhile, three-effect evaporation is adopted for calcium chloride solution concentration, and compared with two-effect evaporation, each ton of hydrogen chloride can save about 0.39t/h of steam, so that the energy consumption can be further saved;
(2) The device for producing the hydrogen chloride by concentration and analysis from the hydrochloric acid is characterized in that a nitrogen gas feeding pipeline communicated with the hydrogen chloride discharging pipeline A is further arranged on the hydrogen chloride discharging pipeline A, and the hydrogen chloride gas is protected by nitrogen gas, so that the hydrogen chloride gas is prevented from being oxidized, and the content of final hydrogen chloride is ensured;
(3) The device for producing the hydrogen chloride by concentrating and analyzing the hydrochloric acid, disclosed by the invention, has the advantages that the three-effect feeding pump, the three-effect discharging pump and the vacuum condensation wastewater pump are all arranged on the pipeline in parallel, so that the three-effect evaporation treatment efficiency of a calcium chloride solution can be greatly improved.
Drawings
The invention will be described in further detail with reference to the drawings and the detailed description.
FIG. 1 is a schematic diagram showing the structure of a hydrogen chloride analysis system in an apparatus for concentrating and analyzing hydrogen chloride from hydrochloric acid according to the present invention.
Fig. 2 is a schematic structural diagram of a calcium chloride concentration and evaporation system in the device for concentrating and resolving hydrogen chloride from hydrochloric acid.
Detailed Description
The following examples will provide those skilled in the art with a more complete understanding of the present invention and are not intended to limit the invention to the embodiments described.
Examples
The device for concentrating and analyzing to produce hydrogen chloride from hydrochloric acid in the embodiment comprises a hydrogen chloride analyzing system and a calcium chloride concentrating and evaporating system.
The specific structure of the hydrogen chloride analysis system is shown in fig. 1, and comprises a jet mixer 1, an analysis tower 2, a hydrogen chloride primary condenser 3, a hydrogen chloride secondary condenser 4, a demister 5, a condensed acid tank 6, an analysis reboiler 7 and an analysis condensed water tank 8.
The bottom end of the jet mixer 1 is provided with a 50% calcium chloride feeding pipeline communicated with the jet mixer 1, one side end of the jet mixer 1 is provided with a 31% hydrochloric acid feeding pipeline communicated with the jet mixer 1, and in an embodiment, the 31% hydrochloric acid feeding pipeline is further provided with a hot water feeding pipeline communicated with the 31% hydrochloric acid feeding pipeline.
The center of the top end of the analysis tower 2 is provided with a hydrogen chloride discharge pipeline A communicated with the analysis tower 2, the hydrogen chloride discharge pipeline A is also provided with a nitrogen gas feed pipeline communicated with the hydrogen chloride discharge pipeline A, and a check valve 9 is also arranged on the nitrogen gas feed pipeline near one end of the hydrogen chloride discharge pipeline A in series; the center of the bottom end of the analytic tower 2 is provided with a hydrogen chloride/water mixed gas discharging pipeline communicated with the analytic tower 2; a mixed liquid feeding pipeline and a hydrogen chloride feeding pipeline which are communicated with the analysis tower 2 are sequentially arranged at one side end of the analysis tower 2 from top to bottom, and the other end of the mixed liquid feeding pipeline is communicated with the jet mixer 1; a 40% calcium chloride discharging pipeline A communicated with the analysis tower 2 is arranged at the lower part of the other side end of the analysis tower 2, and a three-effect feeding pump 10 is arranged on the 40% calcium chloride discharging pipeline A in series; in specific implementation, two triple-effect feed pumps 10 are arranged in parallel on a 40% calcium chloride discharge pipeline A.
The top of the hydrogen chloride primary condenser 3 is communicated with the hydrogen chloride discharging pipeline A, the bottom of the hydrogen chloride primary condenser 3 is provided with a concentrated hydrochloric acid discharging pipeline A communicated with the hydrogen chloride primary condenser 3, the upper part of one side end of the hydrogen chloride primary condenser 3 is provided with a circulating water return pipeline A communicated with the hydrogen chloride primary condenser 3, and the other side end of the hydrogen chloride primary condenser 3 is sequentially provided with a circulating water supply pipeline A and a hydrogen chloride discharging pipeline B communicated with the hydrogen chloride primary condenser 3 from top to bottom.
The top end of the hydrogen chloride secondary condenser 4 is communicated with a hydrogen chloride discharge pipeline B, the bottom end of the hydrogen chloride secondary condenser 4 is provided with a concentrated hydrochloric acid discharge pipeline B communicated with the hydrogen chloride secondary condenser 4, and the other end of the concentrated hydrochloric acid discharge pipeline B is communicated with a concentrated hydrochloric acid discharge pipeline A; the upper part of one side end of the hydrogen chloride secondary condenser 4 is provided with a circulating water return pipeline B communicated with the hydrogen chloride secondary condenser 4, and the other side end of the hydrogen chloride secondary condenser 4 is sequentially provided with a circulating water supply pipeline B and a hydrogen chloride discharging pipeline C which are communicated with the hydrogen chloride secondary condenser 4 from top to bottom.
One side end of the demister 5 is communicated with the hydrogen chloride discharging pipeline C, and the other side end of the demister 5 is provided with an industrial water feeding pipeline communicated with the demister 5; the center of the top end of the demister 5 is provided with a hydrogen chloride discharging pipeline D communicated with the demister 5, the center of the bottom end of the demister 5 is provided with a concentrated hydrochloric acid discharging pipeline C communicated with the demister 5, and the other end of the concentrated hydrochloric acid discharging pipeline C is communicated with the concentrated hydrochloric acid discharging pipeline A; a concentrated hydrochloric acid discharging pipeline D communicated with the demister 5 is further arranged at the side end of the demister 5, and the other end of the concentrated hydrochloric acid discharging pipeline D is communicated with a concentrated hydrochloric acid discharging pipeline C; the concentrated hydrochloric acid discharging pipeline D is arranged at the lower end of the hydrogen chloride discharging pipeline C.
The top end of the condensed acid tank 6 is communicated with the concentrated hydrochloric acid discharge pipeline A, the top end of the condensed acid tank 6 is also provided with a hydrogen chloride discharge pipeline D communicated with the condensed acid tank 6, and the hydrogen chloride discharge pipeline D is communicated with the hydrogen chloride discharge pipeline C; the lower part of one side end of the condensed acid tank 6 is provided with a condensed acid discharging pipeline communicated with the condensed acid tank 6.
The top end of the analysis reboiler 7 is communicated with a hydrogen chloride feeding pipeline, and the bottom end of the analysis reboiler 7 is communicated with a hydrogen chloride/water mixed gas discharging pipeline; and a saturated steam feeding pipeline A, a saturated steam discharging pipeline A and a condensed water discharging pipeline A which are communicated with the analysis reboiler 7 are sequentially arranged at one side end of the analysis reboiler 7 from top to bottom.
The analysis condensate water tank 8 is arranged on the condensate water outlet pipeline A in series, and the top end of the analysis condensate water tank 8 is communicated with the saturated steam outlet pipeline A.
The specific structure of the calcium chloride concentration and evaporation system, as shown in fig. 2, comprises a first-effect evaporator 11, a first-effect flash tank 12, a first-effect condensation water tank 13, a second-effect evaporator 14, a second-effect flash tank 15, a second-effect condensation water tank 16, a third-effect evaporator 17, a third-effect flash tank 18, a third-effect condensation water tank 19, a third-effect discharge preheater 20, an evaporation condenser 21, a vacuum buffer tank 22 and a water flow jet pump vacuum unit 23.
The bottom center of the first-effect evaporator 11 is communicated with a 40% calcium chloride discharge pipeline A, and the top center of the first-effect evaporator 11 is provided with a 40% calcium chloride discharge pipeline B communicated with the first-effect evaporator 11; one side end of the first-effect evaporator 11 is sequentially provided with a saturated steam feeding pipeline B, a saturated steam discharging pipeline B and a condensed water discharging pipeline B which are communicated with the first-effect evaporator 11 from top to bottom.
The first-effect condensate water tank 13 is arranged on the condensate water outlet pipeline B in series, and the top end of the first-effect condensate water tank 13 is communicated with the saturated steam outlet pipeline B.
One side end of the first-effect flash tank 12 is communicated with a 40% calcium chloride discharge pipeline B, and the other side end of the first-effect flash tank 12 is provided with a 43.3% calcium chloride discharge pipeline A communicated with the first-effect flash tank 12; the top center of the first-effect flash tank 12 is provided with a saturated steam feeding pipeline C communicated with the first-effect flash tank 12, the bottom center of the first-effect flash tank 12 is provided with a 40% calcium chloride discharging pipeline C communicated with the first-effect flash tank 12, and the other end of the 40% calcium chloride discharging pipeline C is communicated with a 40% calcium chloride discharging pipeline A.
The center of the bottom end of the second-effect evaporator 14 is communicated with a 43.3% calcium chloride discharge pipeline A, and the center of the top end of the second-effect evaporator 14 is provided with a 43.3% calcium chloride discharge pipeline B communicated with the second-effect evaporator 14; one side end of the two-effect evaporator 14 is communicated with a saturated steam feeding pipeline C, and a saturated steam discharging pipeline C and a condensed water discharging pipeline C which are communicated with the two-effect evaporator 14 are sequentially arranged at the side end of the two-effect evaporator 14 at the lower part of the saturated steam feeding pipeline C from top to bottom.
The two-effect condensation water tank 16 is respectively communicated with the saturated steam discharging pipeline C and the condensation water discharging pipeline C, and a wastewater discharging pipeline A communicated with the two-effect condensation water tank 16 is arranged at the lower part of one side end of the two-effect condensation water tank 16.
One side end of the two-effect flash tank 15 is communicated with a 43.3% calcium chloride discharge pipeline B, and the other side end of the two-effect flash tank 15 is provided with a 46.6% calcium chloride discharge pipeline A communicated with the two-effect flash tank 15; the center of the top end of the secondary flash tank 15 is provided with a saturated steam feeding pipeline D communicated with the secondary flash tank 15, the center of the bottom end of the secondary flash tank 15 is provided with a 43.3% calcium chloride discharging pipeline C communicated with the secondary flash tank 15, and the other end of the 43.3% calcium chloride discharging pipeline C is communicated with the 43.3% calcium chloride discharging pipeline A.
The bottom center of the triple effect evaporator 17 is communicated with a 46.6% calcium chloride discharge pipeline A, and the top center of the triple effect evaporator 17 is provided with a 46.6% calcium chloride discharge pipeline B communicated with the triple effect evaporator 17; one side end of the triple-effect evaporator 17 is communicated with a saturated steam feeding pipeline D, and a saturated steam discharging pipeline D and a wastewater discharging pipeline B which are communicated with the triple-effect evaporator 17 are sequentially arranged at the side end of the triple-effect evaporator 17 at the lower part of the saturated steam feeding pipeline D from top to bottom.
The triple-effect condensation water tank 19 is arranged on the wastewater outlet pipeline B in series, and the top end of the triple-effect condensation water tank 19 is communicated with the saturated steam outlet pipeline D.
One side end of the triple-effect flash tank 18 is communicated with a 46.6% calcium chloride discharge pipeline B, and the other side end of the triple-effect flash tank 18 is provided with a 50% calcium chloride discharge pipeline A communicated with the triple-effect flash tank 18; the center of the top end of the triple-effect flash tank 18 is provided with a saturated steam feeding pipeline E communicated with the triple-effect flash tank 18, the saturated steam feeding pipeline E is also communicated with a saturated steam feeding pipeline F, and the other end of the saturated steam feeding pipeline F is communicated with a saturated steam discharging pipeline D.
The three-effect discharge preheater 20 is arranged on the condensed water outlet pipeline B and the 50% calcium chloride outlet pipeline A in series; as an example, a more specific embodiment is that a 50% calcium chloride discharging pipeline B is further arranged on a 46.6% calcium chloride discharging pipeline B in series, the other end of the 50% calcium chloride discharging pipeline B is communicated with a 50% calcium chloride discharging pipeline a at the front end of the triple effect discharging preheater 20, a triple effect discharging pump 24 is further arranged on the 50% calcium chloride discharging pipeline B in series, two triple effect discharging pumps 24 are arranged on the 50% calcium chloride discharging pipeline B in parallel.
The top end of the evaporative condenser 21 is communicated with a saturated steam feeding pipeline E, and a wastewater outlet pipeline C communicated with the evaporative condenser 21 is arranged in the center of the bottom end of the evaporative condenser 21; one side end of the evaporative condenser 21 is sequentially provided with a circulating water return pipeline C, a circulating water supply pipeline C and a vacuumizing pipeline A which are communicated with the evaporative condenser 21 from top to bottom, and the other end of the vacuumizing pipeline A is communicated with a water flow jet pump vacuum unit 23.
The vacuum buffer tank 22 is arranged on the wastewater outlet pipeline C in series, and the wastewater outlet pipeline C at the rear end of the vacuum buffer tank 22 is also provided with a vacuum condensation wastewater pump 25 in series; two vacuum condensation wastewater pumps 25 are arranged in parallel on the wastewater outlet pipeline C; the top end of the vacuum buffer tank 22 is also provided with a vacuumizing pipeline B communicated with the vacuum buffer tank 22, and the other end of the vacuumizing pipeline B is communicated with the vacuumizing pipeline A.
The working procedure of the device for concentrating and analyzing hydrogen chloride from hydrochloric acid in this embodiment is as follows:
(1) Firstly, 50% calcium chloride and 31% hydrochloric acid are mixed in a jet mixer 1, then pumped into a feed inlet at the upper part of an analysis tower to be put into the analysis tower 2, hydrogen chloride gas obtained by analysis at the tower top is led out from a gas phase outlet and sequentially enters a first-stage hydrogen chloride condenser 3, a second-stage hydrogen chloride condenser 4 and a demister 5 to obtain finished product hydrogen chloride gas, and a calcium chloride solution with the mass fraction of 40% is obtained at the tower bottom;
(2) The hydrogen chloride/water mixed gas analyzed by the analysis tower 2 is evaporated and separated out by an analysis reboiler 7 at the bottom of the analysis tower 2, condensed by condensed water, and the condensed hydrogen chloride gas is introduced into the analysis tower 2 again for repeated cyclic analysis;
(3) Introducing the 40% calcium chloride solution obtained in the step (1) into a first-effect evaporator 11 and a first-effect flash tank 12 in a calcium chloride concentration evaporation system for heating and separating to obtain water vapor with the hydrogen chloride content less than or equal to 0.1% and calcium chloride solution with the mass fraction of 43.3%;
(4) Introducing the calcium chloride solution with the mass fraction of 43.3% obtained in the step (3) into a double-effect evaporator 14 and a double-effect flash tank 15 in a calcium chloride concentration evaporation system for heating and separating to obtain water vapor with the hydrogen chloride content of less than or equal to 0.1% and calcium chloride solution with the mass fraction of 46.6%;
(5) And (3) introducing the calcium chloride solution with the mass fraction of 46.6% obtained in the step (4) into a triple-effect evaporator 17 and a triple-effect flash tank 18 in a calcium chloride concentration evaporation system for heating and separating to obtain water vapor with the hydrogen chloride content of less than or equal to 0.1% and obtain the calcium chloride solution with the mass fraction of 50%, and introducing the calcium chloride solution into an analytical tower 2 through a liquid phase outlet for recycling.
The foregoing has shown and described the basic principles and main features of the present invention and the advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (8)
1. The utility model provides a concentrate device of analytical production hydrogen chloride in follow hydrochloric acid which characterized in that: comprises a hydrogen chloride analysis system and a calcium chloride concentration evaporation system,
the hydrogen chloride analysis system comprises a jet mixer, an analysis tower, a hydrogen chloride primary condenser, a hydrogen chloride secondary condenser, a demister, a condensed acid tank, an analysis reboiler and an analysis condensed water tank,
the bottom end of the jet mixer is provided with a 50% calcium chloride feeding pipeline communicated with the jet mixer, and one side end of the jet mixer is provided with a 31% hydrochloric acid feeding pipeline communicated with the jet mixer;
the center of the top end of the analytic tower is provided with a hydrogen chloride discharging pipeline A communicated with the analytic tower, and the center of the bottom end of the analytic tower is provided with a hydrogen chloride/water mixed gas discharging pipeline communicated with the analytic tower; a mixed liquid feeding pipeline and a hydrogen chloride feeding pipeline which are communicated with the resolving tower are sequentially arranged at one side end of the resolving tower from top to bottom, and the other end of the mixed liquid feeding pipeline is communicated with the jet mixer; a 40% calcium chloride discharging pipeline A communicated with the resolving tower is arranged at the lower part of the other side end of the resolving tower, and a three-effect feeding pump is arranged on the 40% calcium chloride discharging pipeline A in series;
the top end of the hydrogen chloride primary condenser is communicated with a hydrogen chloride discharge pipeline A, the bottom end of the hydrogen chloride primary condenser is provided with a concentrated hydrochloric acid discharge pipeline A communicated with the hydrogen chloride primary condenser, the upper part of one side end of the hydrogen chloride primary condenser is provided with a circulating water return pipeline A communicated with the hydrogen chloride primary condenser, and the other side end of the hydrogen chloride primary condenser is sequentially provided with a circulating water supply pipeline A and a hydrogen chloride discharge pipeline B which are communicated with the hydrogen chloride primary condenser from top to bottom;
the top end of the hydrogen chloride secondary condenser is communicated with the hydrogen chloride discharge pipeline B, the bottom end of the hydrogen chloride secondary condenser is provided with a concentrated hydrochloric acid discharge pipeline B communicated with the hydrogen chloride secondary condenser, and the other end of the concentrated hydrochloric acid discharge pipeline B is communicated with the concentrated hydrochloric acid discharge pipeline A; the upper part of one side end of the hydrogen chloride secondary condenser is provided with a circulating water return pipeline B communicated with the hydrogen chloride secondary condenser, and the other side end of the hydrogen chloride secondary condenser is sequentially provided with a circulating water supply pipeline B and a hydrogen chloride discharge pipeline C which are communicated with the hydrogen chloride secondary condenser from top to bottom;
one side end of the demister is communicated with the hydrogen chloride discharging pipeline C, and the other side end of the demister is provided with an industrial water feeding pipeline communicated with the demister; the center of the top end of the demister is provided with a hydrogen chloride discharging pipeline D communicated with the demister, the center of the bottom end of the demister is provided with a concentrated hydrochloric acid discharging pipeline C communicated with the demister, and the other end of the concentrated hydrochloric acid discharging pipeline C is communicated with a concentrated hydrochloric acid discharging pipeline A;
the top end of the condensed acid tank is communicated with the concentrated hydrochloric acid discharging pipeline A, the top end of the condensed acid tank is also provided with a hydrogen chloride discharging pipeline D communicated with the condensed acid tank, and the hydrogen chloride discharging pipeline D is communicated with the hydrogen chloride discharging pipeline C; a condensed acid discharging pipeline communicated with the condensed acid tank is arranged at the lower part of one side end of the condensed acid tank;
the top end of the desorption reboiler is communicated with the hydrogen chloride feeding pipeline, and the bottom end of the desorption reboiler is communicated with the hydrogen chloride/water mixed gas discharging pipeline; a saturated steam feeding pipeline A, a saturated steam discharging pipeline A and a condensed water discharging pipeline A which are communicated with the analysis reboiler are sequentially arranged at one side end of the analysis reboiler from top to bottom;
the analysis condensate water tank is arranged on the condensate water outlet pipeline A in series, and the top end of the analysis condensate water tank is communicated with the saturated steam discharge pipeline A;
the calcium chloride concentration evaporation system comprises a first-effect evaporator, a first-effect flash tank, a first-effect condensation water tank, a second-effect evaporator, a second-effect flash tank, a second-effect condensation water tank, a third-effect evaporator, a third-effect flash tank, a third-effect condensation water tank, a third-effect discharge preheater, an evaporation condenser, a vacuum buffer tank and a water flow jet pump vacuum unit;
the center of the bottom end of the first-effect evaporator is communicated with a 40% calcium chloride discharging pipeline A, and the center of the top end of the first-effect evaporator is provided with a 40% calcium chloride discharging pipeline B communicated with the first-effect evaporator; a saturated steam feeding pipeline B, a saturated steam discharging pipeline B and a condensed water discharging pipeline B which are communicated with the first-effect evaporator are sequentially arranged at one side end of the first-effect evaporator from top to bottom;
the first-effect condensate water tank is arranged on the condensate water outlet pipeline B in series, and the top end of the first-effect condensate water tank is communicated with the saturated steam outlet pipeline B;
one side end of the first-effect flash tank is communicated with a 40% calcium chloride discharging pipeline B, and the other side end of the first-effect flash tank is provided with a 43.3% calcium chloride discharging pipeline A communicated with the first-effect flash tank; the center of the top end of the first-effect flash tank is provided with a saturated steam feeding pipeline C communicated with the first-effect flash tank, the center of the bottom end of the first-effect flash tank is provided with a 40% calcium chloride discharging pipeline C communicated with the first-effect flash tank, and the other end of the 40% calcium chloride discharging pipeline C is communicated with a 40% calcium chloride discharging pipeline A;
the center of the bottom end of the two-effect evaporator is communicated with a 43.3% calcium chloride discharge pipeline A, and the center of the top end of the two-effect evaporator is provided with a 43.3% calcium chloride discharge pipeline B communicated with the two-effect evaporator; one side end of the two-effect evaporator is communicated with a saturated steam feeding pipeline C, and a saturated steam discharging pipeline C and a condensed water discharging pipeline C which are communicated with the two-effect evaporator are sequentially arranged at the side end of the two-effect evaporator at the lower part of the saturated steam feeding pipeline C from top to bottom;
the secondary condensate water tank is respectively communicated with the saturated steam discharging pipeline C and the condensate water discharging pipeline C, and a wastewater discharging pipeline A communicated with the secondary condensate water tank is arranged at the lower part of one side end of the secondary condensate water tank;
one side end of the secondary flash tank is communicated with a 43.3% calcium chloride discharge pipeline B, and the other side end of the secondary flash tank is provided with a 46.6% calcium chloride discharge pipeline A communicated with the secondary flash tank; the center of the top end of the secondary flash tank is provided with a saturated steam feeding pipeline D communicated with the secondary flash tank, the center of the bottom end of the secondary flash tank is provided with a 43.3% calcium chloride discharging pipeline C communicated with the secondary flash tank, and the other end of the 43.3% calcium chloride discharging pipeline C is communicated with a 43.3% calcium chloride discharging pipeline A;
the center of the bottom end of the triple effect evaporator is communicated with a 46.6% calcium chloride discharge pipeline A, and the center of the top end of the triple effect evaporator is provided with a 46.6% calcium chloride discharge pipeline B communicated with the triple effect evaporator; one side end of the triple-effect evaporator is communicated with a saturated steam feeding pipeline D, and a saturated steam discharging pipeline D and a wastewater discharging pipeline B which are communicated with the triple-effect evaporator are sequentially arranged at the side end of the triple-effect evaporator at the lower part of the saturated steam feeding pipeline D from top to bottom;
the three-effect condensation water tank is arranged on the wastewater outlet pipeline B in series, and the top end of the three-effect condensation water tank is communicated with the saturated steam outlet pipeline D;
one side end of the triple-effect flash tank is communicated with a 46.6% calcium chloride discharge pipeline B, and the other side end of the triple-effect flash tank is provided with a 50% calcium chloride discharge pipeline A communicated with the triple-effect flash tank; a saturated steam feeding pipeline E communicated with the triple-effect flash tank is arranged in the center of the top end of the triple-effect flash tank, a saturated steam feeding pipeline F is further communicated with the saturated steam feeding pipeline E, and the other end of the saturated steam feeding pipeline F is communicated with a saturated steam discharging pipeline D;
the three-effect discharge preheater is arranged on the condensed water outlet pipeline B and the 50% calcium chloride outlet pipeline A in series;
the top end of the evaporation condenser is communicated with a saturated steam feeding pipeline E, and a wastewater outlet pipeline C communicated with the evaporation condenser is arranged in the center of the bottom end of the evaporation condenser; one side end of the evaporation condenser is sequentially provided with a circulating water return pipeline C, a circulating water supply pipeline C and a vacuumizing pipeline A which are communicated with the evaporation condenser from top to bottom, and the other end of the vacuumizing pipeline A is communicated with a water flow jet pump vacuum unit;
the vacuum buffer tank is arranged on the wastewater outlet pipeline C in series, and a vacuum condensation wastewater pump is also arranged on the wastewater outlet pipeline C at the rear end of the vacuum buffer tank in series; the top of the vacuum buffer tank is also provided with a vacuumizing pipeline B communicated with the vacuum buffer tank, and the other end of the vacuumizing pipeline B is communicated with the vacuumizing pipeline A.
2. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: and a hot water feeding pipeline communicated with the 31% hydrochloric acid feeding pipeline is further arranged on the 31% hydrochloric acid feeding pipeline.
3. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: the hydrogen chloride discharging pipeline A is further provided with a nitrogen gas feeding pipeline communicated with the hydrogen chloride discharging pipeline A, and the nitrogen gas feeding pipeline close to one end of the hydrogen chloride discharging pipeline A is further provided with a check valve in series.
4. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: two triple-effect feed pumps are arranged in parallel on a 40% calcium chloride discharge pipeline.
5. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: the side end of the demister is also provided with a concentrated hydrochloric acid discharging pipeline D communicated with the demister, and the other end of the concentrated hydrochloric acid discharging pipeline D is communicated with a concentrated hydrochloric acid discharging pipeline C; the concentrated hydrochloric acid discharging pipeline D is arranged at the lower end of the hydrogen chloride discharging pipeline C.
6. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: the 46.6% calcium chloride discharging pipeline B is also provided with a 50% calcium chloride discharging pipeline B in series, the other end of the 50% calcium chloride discharging pipeline B is communicated with a 50% calcium chloride discharging pipeline A at the front end of the three-effect discharging preheater, and the 50% calcium chloride discharging pipeline B is also provided with a three-effect discharging pump in series.
7. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 6, wherein: two triple-effect discharging pumps are arranged in parallel on a 50% calcium chloride discharging pipeline B.
8. The apparatus for concentrating and resolving hydrogen chloride from hydrochloric acid according to claim 1, wherein: the two vacuum condensation wastewater pumps are arranged on the wastewater outlet pipeline C in parallel.
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| CN111943141A (en) * | 2020-09-02 | 2020-11-17 | 南通山剑防腐科技有限公司 | Hydrochloric acid analysis device with negative pressure dehydration function and analysis process |
| CN112985083B (en) * | 2021-02-06 | 2022-12-23 | 四川省金路树脂有限公司 | Device and method for synthesizing hydrogen chloride and coproducing medium-low pressure steam in three-stage manner |
| CN115180594B (en) * | 2022-07-11 | 2023-12-26 | 新疆西部合盛硅业有限公司 | Recovery process of wastewater from organosilicon slurry residue treatment |
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| IL36399A0 (en) * | 1971-03-11 | 1971-05-26 | Israel Mining Ind Inst For Res | Production of concentrated hydrogen chloride from aqueous solutions thereof |
| CN101525121A (en) * | 2009-04-16 | 2009-09-09 | 张孟存 | Method for analyzing chlorine hydride in hydrochloric acid |
| CN102285641A (en) * | 2010-06-21 | 2011-12-21 | 南通星球石墨设备有限公司 | Recycling process of waste hydrochloric acid |
| CN108840310A (en) * | 2018-09-27 | 2018-11-20 | 淄博晟钛复合材料科技有限公司 | A kind of device and its technique of producing hydrogen chloride by resolving deep from dilute hydrochloric acid |
| CN109207747A (en) * | 2018-10-30 | 2019-01-15 | 云南驰宏国际锗业有限公司 | A method of recycling hydrochloric acid from germanium concentrate slops |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP6738268B2 (en) * | 2016-12-14 | 2020-08-12 | 株式会社クボタ | Water treatment method and water treatment system |
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| IL36399A0 (en) * | 1971-03-11 | 1971-05-26 | Israel Mining Ind Inst For Res | Production of concentrated hydrogen chloride from aqueous solutions thereof |
| CN101525121A (en) * | 2009-04-16 | 2009-09-09 | 张孟存 | Method for analyzing chlorine hydride in hydrochloric acid |
| CN102285641A (en) * | 2010-06-21 | 2011-12-21 | 南通星球石墨设备有限公司 | Recycling process of waste hydrochloric acid |
| CN108840310A (en) * | 2018-09-27 | 2018-11-20 | 淄博晟钛复合材料科技有限公司 | A kind of device and its technique of producing hydrogen chloride by resolving deep from dilute hydrochloric acid |
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