CN211111046U - Device for producing hydrogen chloride by concentration and resolution in hydrochloric acid - Google Patents
Device for producing hydrogen chloride by concentration and resolution in hydrochloric acid Download PDFInfo
- Publication number
- CN211111046U CN211111046U CN201921034093.4U CN201921034093U CN211111046U CN 211111046 U CN211111046 U CN 211111046U CN 201921034093 U CN201921034093 U CN 201921034093U CN 211111046 U CN211111046 U CN 211111046U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- communicated
- hydrogen chloride
- effect
- tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model relates to a device for producing hydrogen chloride by concentration and analysis from hydrochloric acid, which comprises a chlorine hydride analysis system and a calcium chloride concentration and evaporation system, wherein 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 condensation acid tank, an analysis reboiler and an analysis condensation water tank; the calcium chloride concentration and evaporation system comprises a first-effect evaporator, a first-effect flash evaporation tank, a first-effect condensed water tank, a second-effect evaporator, a second-effect flash evaporation tank, a second-effect condensed water tank, a third-effect evaporator, a third-effect flash evaporation tank, a third-effect condensed water tank, a third-effect discharge preheater, an evaporation condenser, a vacuum buffer tank and a water flow injection pump vacuum unit. The utility model has the advantages that: the utility model discloses from the device of concentrated analytic production hydrogen chloride in hydrochloric acid, can improve hydrogen chloride gas content and further energy saving.
Description
Technical Field
The utility model relates to a hydrogen chloride apparatus for producing, in particular to a device for producing hydrogen chloride by concentration and resolution from hydrochloric acid.
Background
The hydrogen chloride is mainly obtained by hydrochloric acid desorption production, and the main principle is that concentrated hydrochloric acid falls from the top of a desorption tower, high-temperature hydrogen chloride and steam are introduced from the bottom of the desorption tower, and the high-temperature hydrogen chloride and the steam realize heat exchange in the tower, so that the hydrogen chloride gas in the concentrated hydrochloric acid is desorbed and removed. Before the concentrated hydrochloric acid is introduced into the desorption tower, the concentrated hydrochloric acid and the dilute hydrochloric acid need to exchange heat in a double-effect heat exchanger, generally, the concentrated hydrochloric acid enters from a bottom shell pass inlet and then flows out from a top shell pass outlet, and the dilute hydrochloric acid passes through a shell pass. As the temperature of the concentrated hydrochloric acid rises, part of hydrogen chloride is separated out from the concentrated hydrochloric acid, so that the shell pass has air resistance, and the acid feeding amount is unstable. In addition, concentrated hydrochloric acid is generally sprayed into the desorption tower at high pressure, and if part of hydrogen chloride gas is mixed, the two gas flows are opposite, and the heat exchange is not facilitated.
Through retrieval, patent CN 108840310A discloses a device for producing hydrogen chloride by deep desorption from dilute hydrochloric acid and a process thereof, comprising a preheater, a desorption tower and a reboiler, and further comprising a primary flash tower, a secondary flash tower and a water treatment system, wherein the desorption tower is provided with a middle feed inlet, the water treatment system comprises a neutralization reaction kettle, a primary filtering device, a secondary filtering device, a primary reverse osmosis device, a secondary 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 secondary flash tower through a pipeline, a discharge port is sequentially communicated with a sand filter, an ultrafilter, the primary reverse osmosis device, the secondary reverse osmosis device and an evaporator, and the use method comprises preheating, desorption, double-effect flash evaporation and water treatment to obtain dry hydrogen chloride gas; the utility model has reasonable design, improves the feeding temperature by changing the feeding mode, ensures that the hydrochloric acid is more thoroughly analyzed, does not discharge waste liquid, directly obtains dry hydrogen chloride gas by analysis, does not need secondary drying, adopts two-effect evaporation for calcium chloride solution concentration, ensures that steam heat energy is repeatedly utilized, improves the utilization rate of heat energy, reduces the heat load of a system, and saves energy consumption; however, the utility model still has certain disadvantages: 1. the hydrochloric acid and the calcium chloride solution are mixed after entering the desorption tower, and uneven mixing may exist, so that the content of the hydrogen chloride gas obtained by final desorption 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 space is still provided.
Therefore, it is necessary to develop a device for producing hydrogen chloride by concentration and desorption from hydrochloric acid, which can increase the content of hydrogen chloride gas and further save energy consumption.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a can improve the hydrogen chloride gas content and further energy saving's the concentrated analytic device of production hydrogen chloride from hydrochloric acid.
In order to solve the technical problem, the utility model adopts the technical scheme that: a device for producing hydrogen chloride by concentration and desorption from hydrochloric acid is characterized in that: comprises a chlorine hydride analysis system and a calcium chloride concentration and evaporation system,
the hydrogen chloride analysis system comprises a jet mixer, an analysis tower, a hydrogen chloride first-stage condenser, a hydrogen chloride second-stage condenser, a demister, a condensed acid tank, an analysis reboiler and an analysis condensed water tank,
a 50% calcium chloride feeding pipeline communicated with the jet mixer is arranged at the bottom end of the jet mixer, and a 31% hydrochloric acid feeding pipeline communicated with the jet mixer is arranged at one side end of the jet mixer;
a hydrogen chloride discharge pipeline A communicated with the desorption tower is arranged in the center of the top end of the desorption tower, and a hydrogen chloride/water mixed gas discharge pipeline communicated with the desorption tower is arranged in the center of the bottom end of the desorption tower; a mixed liquid feeding pipeline and a hydrogen chloride feeding pipeline which are communicated with the desorption tower are sequentially arranged at one side end of the desorption tower from top to bottom, and the other end of the mixed liquid feeding pipeline is communicated with the jet mixer; the lower part of the other side end of the analysis tower is provided with a 40% calcium chloride discharge pipeline A communicated with the analysis tower, and the 40% calcium chloride discharge pipeline A is provided with a three-effect feed pump 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 feeding pipeline A and a hydrogen chloride discharge pipeline B communicated with the hydrogen chloride primary condenser from top to bottom;
the top end of the hydrogen chloride secondary condenser is communicated with a 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 a concentrated hydrochloric acid discharge pipeline A; a circulating water return pipeline B communicated with the hydrogen chloride secondary condenser is arranged at the upper part of one side end of the hydrogen chloride secondary condenser, and a circulating water feeding pipeline B and a hydrogen chloride discharging pipeline C communicated with the hydrogen chloride secondary condenser are sequentially arranged at the other side end of 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; a hydrogen chloride discharge pipeline D communicated with the demister is arranged in the center of the top end of the demister, a concentrated hydrochloric acid discharge pipeline C communicated with the demister is arranged in the center of the bottom end of the demister, and the other end of the concentrated hydrochloric acid discharge pipeline C is communicated with the concentrated hydrochloric acid discharge pipeline A;
the top end of the condensed acid tank is communicated with a concentrated hydrochloric acid discharge pipeline A, the top end of the condensed acid tank is also provided with a hydrogen chloride discharge pipeline D communicated with the condensed acid tank, and the hydrogen chloride discharge pipeline D is communicated with a hydrogen chloride discharge pipeline C; a condensed acid discharge 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 a hydrogen chloride feeding pipeline, and the bottom end of the desorption reboiler is communicated with a hydrogen chloride/water mixed gas discharging pipeline; a saturated steam feeding pipeline A, a saturated steam discharging pipeline A and a condensed water outlet pipeline A which are communicated with the desorption reboiler are sequentially arranged at one side end of the desorption reboiler from top to bottom;
the analysis condensate tank is serially arranged on the condensate water outlet pipeline A, and the top end of the analysis condensate tank is communicated with the saturated steam discharge pipeline A;
the calcium chloride concentration and evaporation system comprises a first-effect evaporator, a first-effect flash evaporation tank, a first-effect condensed water tank, a second-effect evaporator, a second-effect flash evaporation tank, a second-effect condensed water tank, a third-effect evaporator, a third-effect flash evaporation tank, a third-effect condensed water tank, a third-effect discharge preheater, an evaporation condenser, a vacuum buffer tank and a water flow injection pump vacuum unit;
the center of the bottom end of the first-effect evaporator is communicated with a 40% calcium chloride discharge pipeline A, and the center of the top end of the first-effect evaporator is provided with a 40% calcium chloride discharge 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 primary condensed water tank is serially connected to a condensed water outlet pipeline B, and the top end of the primary condensed water tank is communicated with the saturated steam discharge pipeline B;
one side end of the primary-effect flash tank is communicated with a 40% calcium chloride discharge pipeline B, and the other side end of the primary-effect flash tank is provided with a 43.3% calcium chloride discharge pipeline A communicated with the primary-effect flash tank; a saturated steam feeding pipeline C communicated with the primary-effect flash tank is arranged in the center of the top end of the primary-effect flash tank, a 40% calcium chloride discharging pipeline C communicated with the primary-effect flash tank is arranged in the center of the bottom end of the primary-effect flash tank, and the other end of the 40% calcium chloride discharging pipeline C is communicated with the 40% calcium chloride discharging pipeline A;
the center of the bottom end of the second-effect evaporator is communicated with a 43.3% calcium chloride discharge pipeline A, and the center of the top end of the second-effect evaporator is provided with a 43.3% calcium chloride discharge pipeline B communicated with the second-effect evaporator; one side end of the second-effect evaporator is communicated with a saturated steam feeding pipeline C, and a saturated steam discharging pipeline C and a condensate water outlet pipeline C which are communicated with the second-effect evaporator are sequentially arranged at the side end of the second-effect evaporator at the lower part of the saturated steam feeding pipeline C from top to bottom;
the secondary condensed water tank is respectively communicated with a saturated steam discharge pipeline C and a condensed water outlet pipeline C, and a wastewater outlet pipeline A communicated with the secondary condensed water tank is arranged at the lower part of one side end of the secondary condensed water tank;
one side end of the two-effect flash tank is communicated with a 43.3% calcium chloride discharge pipeline B, and the other side end of the two-effect flash tank is provided with a 46.6% calcium chloride discharge pipeline A communicated with the two-effect flash tank; a saturated steam feeding pipeline D communicated with the secondary flash tank is arranged in the center of the top end of the secondary flash tank, a 43.3% calcium chloride discharging pipeline C communicated with the secondary flash tank is arranged in the center of the bottom end of the secondary flash tank, 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 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 triple-effect condensation water tank is serially arranged on the wastewater outlet pipeline B, and the top end of the triple-effect condensation water tank is communicated with the saturated steam discharge pipeline D;
one side end of the three-effect flash tank is communicated with a 46.6% calcium chloride discharge pipeline B, and the other side end of the three-effect flash tank is provided with a 50% calcium chloride discharge pipeline A communicated with the three-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 triple-effect discharge preheater is serially arranged on the condensed water outlet pipeline B and the 50% calcium chloride discharge pipeline A;
the top end of the evaporative condenser is communicated with a saturated steam feeding pipeline E, and the center of the bottom end of the evaporative condenser is provided with a wastewater outlet pipeline C communicated with the evaporative condenser; a circulating water return pipeline C, a circulating water supply pipeline C and a vacuumizing pipeline A which are communicated with the evaporative condenser are sequentially arranged at one side end of the evaporative condenser from top to bottom, and a water jet pump vacuum unit is communicated with the other end of the vacuumizing pipeline A;
the vacuum buffer tank is connected in series on a wastewater outlet pipeline C, and a vacuum condensation wastewater pump is also connected in series on the wastewater outlet pipeline C at the rear end of the vacuum buffer tank; the top end 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 the 31% hydrochloric acid feeding pipeline is also provided with a hot water feeding pipeline communicated with the 31% hydrochloric acid feeding pipeline.
Still be provided with the nitrogen gas charge-in pipeline with hydrogen chloride ejection of compact pipeline A intercommunication on the hydrogen chloride ejection of compact pipeline A, just still establish ties on the nitrogen gas charge-in pipeline that is close to hydrogen chloride ejection of compact pipeline A one end and be provided with the check valve.
The three-effect feeding pumps are arranged on the 40% calcium chloride discharging pipeline in parallel.
A concentrated hydrochloric acid discharging pipeline D communicated with the demister is further arranged at the side end of the demister, and the other end of the concentrated hydrochloric acid discharging pipeline D is communicated with a concentrated hydrochloric acid discharging pipeline C; and the concentrated hydrochloric acid discharging pipeline D is arranged at the lower end of the hydrogen chloride discharging pipeline C.
And a 50% calcium chloride discharge pipeline B is also arranged on the 46.6% calcium chloride discharge pipeline B in series, the other end of the 50% calcium chloride discharge pipeline B is communicated with a 50% calcium chloride discharge pipeline A at the front end of the triple-effect discharge preheater, and a triple-effect discharge pump is also arranged on the 50% calcium chloride discharge pipeline B in series.
The three-effect discharge pump is provided with two discharge pumps which are arranged on a 50% calcium chloride discharge pipeline B in parallel.
The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: the vacuum condensation waste water pump has two, and the parallelly connected setting is on waste water outlet pipe C.
The utility model has the advantages that:
(1) the utility model discloses from the device of concentrated analytic production hydrogen chloride in hydrochloric acid, add the jet mixer before the analysis tower, and then send to the analysis tower again and analyze after 50% calcium chloride and 31% hydrochloric acid misce bene through the jet mixer to can fully analyze out hydrogen chloride, the hydrogen chloride after the analysis separates out rare hydrochloric acid and hydrogen chloride gas through the defroster again, makes ultimate hydrogen chloride content can promote greatly; meanwhile, the calcium chloride solution is concentrated by adopting triple effect evaporation, and compared with double effect evaporation, the hydrogen chloride per ton can save steam by about 0.39t/h, so that the energy consumption can be further saved;
(2) the utility model discloses a device for producing hydrogen chloride by concentration and analysis in hydrochloric acid, wherein, a nitrogen gas feeding pipeline communicated with the hydrogen chloride discharging pipeline A is also arranged on the hydrogen chloride discharging pipeline A, and the hydrogen chloride gas is protected by nitrogen gas, thereby preventing the hydrogen chloride gas from being oxidized and ensuring the final content of the hydrogen chloride;
(3) the utility model discloses follow the device of concentrated analytic production hydrogen chloride in hydrochloric acid, wherein, triple effect charge pump and vacuum condensation waste water pump are a plurality of parallelly connected settings on the pipeline, and then can improve calcium chloride solution triple effect evaporation treatment efficiency greatly.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
Fig. 1 is a schematic structural diagram of a hydrogen chloride desorption system in the device for producing hydrogen chloride from hydrochloric acid.
Fig. 2 is a schematic structural diagram of a calcium chloride concentration and evaporation system in the device for producing hydrogen chloride by concentration and desorption from hydrochloric acid.
Detailed Description
The following examples are presented to enable those skilled in the art to more fully understand the present invention and are not intended to limit the scope of the present invention.
Examples
The device for producing the hydrogen chloride by concentrating and resolving the hydrochloric acid comprises a hydrogen chloride resolving system and a calcium chloride concentrating and evaporating system.
As shown in fig. 1, the specific configuration of the hydrogen chloride desorption system includes a jet mixer 1, a desorption tower 2, a hydrogen chloride primary condenser 3, a hydrogen chloride secondary condenser 4, a demister 5, a condensed acid tank 6, a desorption reboiler 7, and a desorption 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 the embodiment, the 31% hydrochloric acid feeding pipeline is also provided with a hot water feeding pipeline communicated with the 31% hydrochloric acid feeding pipeline.
A hydrogen chloride discharge pipeline A communicated with the desorption tower 2 is arranged in the center of the top end of the desorption tower 2, a nitrogen feeding pipeline communicated with the hydrogen chloride discharge pipeline A is further arranged on the hydrogen chloride discharge pipeline A, and a check valve 9 is further arranged on the nitrogen feeding pipeline close to one end of the hydrogen chloride discharge pipeline A in series; a hydrogen chloride/water mixed gas discharge pipeline communicated with the desorption tower 2 is arranged at the center of the bottom end of the desorption tower 2; a mixed liquid feeding pipeline and a hydrogen chloride feeding pipeline which are communicated with the desorption tower 2 are sequentially arranged at one side end of the desorption 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 discharge 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 triple-effect feed pump 10 is arranged on the 40% calcium chloride discharge pipeline A in series; in specific implementation, two triple-effect feeding pumps 10 are arranged on the 40% calcium chloride discharging pipeline A in parallel.
The top and the hydrogen chloride ejection of compact pipeline A intercommunication setting of hydrogen chloride one-level condenser 3, the bottom of hydrogen chloride one-level condenser 3 have with the concentrated hydrochloric acid ejection of compact pipeline A of 3 intercommunication settings of hydrogen chloride one-level condenser, one side of hydrogen chloride one-level condenser 3 is served the upper portion and is provided with the circulation return water pipeline A with 3 intercommunications of hydrogen chloride one-level condenser, another side top-down of hydrogen chloride one-level condenser 3 has set gradually the circulation water feeding pipeline A and the hydrogen chloride ejection of compact pipeline B with 3 intercommunications of hydrogen chloride one-level condenser.
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 feeding pipeline B and a hydrogen chloride discharging pipeline C 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; a hydrogen chloride discharge pipeline D communicated with the demister 5 is arranged in the center of the top end of the demister 5, a concentrated hydrochloric acid discharge pipeline C communicated with the demister 5 is arranged in the center of the bottom end of the demister 5, and the other end of the concentrated hydrochloric acid discharge pipeline C is communicated with the concentrated hydrochloric acid discharge 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; concentrated hydrochloric acid ejection of compact pipeline D sets up the lower extreme at hydrogen chloride ejection of compact pipeline C.
The top end of the condensed acid tank 6 is communicated with a 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 a hydrogen chloride discharge pipeline C; a condensed acid discharge pipeline communicated with the condensed acid tank 6 is arranged at the lower part of one side end of the condensed acid tank 6.
The top end of the desorption reboiler 7 is communicated with a hydrogen chloride feeding pipeline, and the bottom end of the desorption reboiler 7 is communicated with a hydrogen chloride/water mixed gas discharging pipeline; a saturated steam feeding pipeline A, a saturated steam discharging pipeline A and a condensed water outlet pipeline A which are communicated with the desorption reboiler 7 are sequentially arranged at one side end of the desorption reboiler 7 from top to bottom.
The analytic condensate tank 8 is arranged on the condensate water outlet pipeline A in series, and the top end of the analytic condensate tank 8 is communicated with the saturated steam discharge pipeline A.
The specific structure of the calcium chloride concentration and evaporation system, as shown in fig. 2, includes a first-effect evaporator 11, a first-effect flash tank 12, a first-effect condensed water tank 13, a second-effect evaporator 14, a second-effect flash tank 15, a second-effect condensed water tank 16, a third-effect evaporator 17, a third-effect flash tank 18, a third-effect condensed water tank 19, a third-effect discharge preheater 20, an evaporation condenser 21, a vacuum buffer tank 22, and a water flow injection pump vacuum unit 23.
The center of the bottom end of the first-effect evaporator 11 is communicated with a 40% calcium chloride discharge pipeline A, and the center of the top end of the first-effect evaporator 11 is provided with a 40% calcium chloride discharge pipeline B communicated with the first-effect evaporator 11; 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 are sequentially arranged at one side end of the first-effect evaporator 11 from top to bottom.
The first-effect condensed water tank 13 is arranged on the condensed water outlet pipeline B in series, and the top end of the first-effect condensed 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 one-effect flash tank 12 is equipped with the saturated steam charge-in pipeline C who communicates with one-effect flash tank 12, and the bottom center of one-effect flash tank 12 is equipped with 40% calcium chloride ejection of compact pipeline C who communicates with one-effect flash tank 12, and the other end and the 40% calcium chloride ejection of compact pipeline A intercommunication setting of 40% calcium chloride ejection of compact pipeline C.
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 second-effect evaporator 14 is communicated with a saturated steam feeding pipeline C, and a saturated steam discharging pipeline C and a condensate water outlet pipeline C which are communicated with the second-effect evaporator 14 are sequentially arranged at the side end of the second-effect evaporator 14 at the lower part of the saturated steam feeding pipeline C from top to bottom.
The two-effect condensed water tank 16 is respectively communicated with a saturated steam discharging pipeline C and a condensed water outlet pipeline C, and a wastewater outlet pipeline A communicated with the two-effect condensed water tank 16 is arranged at the lower part of one side end of the two-effect condensed water tank 16.
One side end of the secondary flash tank 15 is communicated with a 43.3% calcium chloride discharge pipeline B, and the other side end of the secondary flash tank 15 is provided with a 46.6% calcium chloride discharge pipeline A communicated with the secondary flash tank 15; the top center of the two-effect flash tank 15 is provided with a saturated steam feeding pipeline D communicated with the two-effect flash tank 15, the bottom center of the two-effect flash tank 15 is provided with a 43.3% calcium chloride discharging pipeline C communicated with the two-effect 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 center of the bottom end of the triple-effect evaporator 17 is communicated with a 46.6 percent calcium chloride discharge pipeline A, and the center of the top end of the triple-effect evaporator 17 is provided with a 46.6 percent 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 condensed water tank 19 is serially arranged on the wastewater outlet pipeline B, and the top end of the triple-effect condensed water tank 19 is communicated with the saturated steam outlet pipeline D.
One side end of the three-effect flash tank 18 is communicated with a 46.6% calcium chloride discharge pipeline B, and the other side end of the three-effect flash tank 18 is provided with a 50% calcium chloride discharge pipeline A communicated with the three-effect flash tank 18; the top center 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 further 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 triple-effect discharge preheater 20 is arranged on the condensed water outlet pipeline B and the 50% calcium chloride discharge pipeline A in series; as an example, a more specific implementation manner is that a 50% calcium chloride discharge pipeline B is further connected in series to the 46.6% calcium chloride discharge pipeline B, the other end of the 50% calcium chloride discharge pipeline B is communicated with a 50% calcium chloride discharge pipeline a at the front end of the triple-effect discharge preheater 20, a triple-effect discharge pump 24 is further connected in series to the 50% calcium chloride discharge pipeline B, and two triple-effect discharge pumps 24 are arranged in parallel to the 50% calcium chloride discharge pipeline B.
The top end of the evaporative condenser 21 is communicated with a saturated steam feeding pipeline E, and the center of the bottom end of the evaporative condenser 21 is provided with a wastewater outlet pipeline C communicated with the evaporative condenser 21; a circulating water return pipeline C, a circulating water feeding pipeline C and a vacuumizing pipeline A which are communicated with the evaporative condenser 21 are sequentially arranged at one side end of the evaporative condenser 21 from top to bottom, and a water jet pump vacuum unit 23 is arranged at the other end of the vacuumizing pipeline A in a communicated mode.
The vacuum buffer tank 22 is connected in series on the wastewater outlet pipe C, and the wastewater outlet pipe C at the rear end of the vacuum buffer tank 22 is also connected in series with a vacuum condensation wastewater pump 25; two vacuum condensation waste water pumps 25 are arranged on the waste water outlet pipeline C in parallel; the top end of the vacuum buffer tank 22 is further provided with a vacuum-pumping pipeline B communicated with the vacuum buffer tank 22, and the other end of the vacuum-pumping pipeline B is communicated with the vacuum-pumping pipeline A.
The working process of the device for producing hydrogen chloride by concentration and desorption from hydrochloric acid in the embodiment is as follows:
(1) firstly, mixing 50% of calcium chloride and 31% of hydrochloric acid in a jet mixer 1, pumping the mixture into a feed inlet at the upper part of an analytical tower, putting the mixture into an analytical tower 2, analyzing the hydrogen chloride gas obtained at the top of the tower, leading the hydrogen chloride gas out of a gas phase outlet, sequentially entering a hydrogen chloride primary condenser 3, a hydrogen chloride secondary condenser 4 and a demister 5 to obtain a finished product hydrogen chloride gas, and obtaining a calcium chloride solution with the mass fraction of 40% at the bottom of the tower;
(2) the hydrogen chloride/water mixed gas obtained by the analysis of the analysis tower 2 is evaporated and separated out through an analysis reboiler 7 at the bottom of the analysis tower 2, and is condensed through condensed water, and the condensed hydrogen chloride gas is introduced into the analysis tower 2 again for repeated cycle analysis;
(3) introducing the calcium chloride solution with the mass fraction of 40% obtained in the step (1) into a one-effect evaporator 11 and a one-effect flash tank 12 in a calcium chloride concentration evaporation system for heating and separation to obtain water vapor with the hydrogen chloride content of less than or equal to 0.1% and obtain a 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 separation to obtain water vapor with the hydrogen chloride content of less than or equal to 0.1% and obtain a 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 percent 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 separation to obtain water vapor with the hydrogen chloride content of less than or equal to 0.1 percent and obtain the calcium chloride solution with the mass fraction of 50 percent, and introducing the calcium chloride solution into an analytical tower 2 through a liquid phase outlet for recycling.
The basic principles and main features of the invention and the advantages of the invention have been shown and described above. It will be understood by those skilled in the art that the present invention is not limited to the above embodiments, and that the foregoing embodiments and descriptions are provided only to illustrate the principles of the present invention without departing from the spirit and scope of the present invention. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (8)
1. A device for producing hydrogen chloride by concentration and desorption from hydrochloric acid is characterized in that: comprises a chlorine hydride analysis system and a calcium chloride concentration and evaporation system,
the hydrogen chloride analysis system comprises a jet mixer, an analysis tower, a hydrogen chloride first-stage condenser, a hydrogen chloride second-stage condenser, a demister, a condensed acid tank, an analysis reboiler and an analysis condensed water tank,
a 50% calcium chloride feeding pipeline communicated with the jet mixer is arranged at the bottom end of the jet mixer, and a 31% hydrochloric acid feeding pipeline communicated with the jet mixer is arranged at one side end of the jet mixer;
a hydrogen chloride discharge pipeline A communicated with the desorption tower is arranged in the center of the top end of the desorption tower, and a hydrogen chloride/water mixed gas discharge pipeline communicated with the desorption tower is arranged in the center of the bottom end of the desorption tower; a mixed liquid feeding pipeline and a hydrogen chloride feeding pipeline which are communicated with the desorption tower are sequentially arranged at one side end of the desorption tower from top to bottom, and the other end of the mixed liquid feeding pipeline is communicated with the jet mixer; the lower part of the other side end of the analysis tower is provided with a 40% calcium chloride discharge pipeline A communicated with the analysis tower, and the 40% calcium chloride discharge pipeline A is provided with a three-effect feed pump 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 feeding pipeline A and a hydrogen chloride discharge pipeline B communicated with the hydrogen chloride primary condenser from top to bottom;
the top end of the hydrogen chloride secondary condenser is communicated with a 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 a concentrated hydrochloric acid discharge pipeline A; a circulating water return pipeline B communicated with the hydrogen chloride secondary condenser is arranged at the upper part of one side end of the hydrogen chloride secondary condenser, and a circulating water feeding pipeline B and a hydrogen chloride discharging pipeline C communicated with the hydrogen chloride secondary condenser are sequentially arranged at the other side end of 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; a hydrogen chloride discharge pipeline D communicated with the demister is arranged in the center of the top end of the demister, a concentrated hydrochloric acid discharge pipeline C communicated with the demister is arranged in the center of the bottom end of the demister, and the other end of the concentrated hydrochloric acid discharge pipeline C is communicated with the concentrated hydrochloric acid discharge pipeline A;
the top end of the condensed acid tank is communicated with a concentrated hydrochloric acid discharge pipeline A, the top end of the condensed acid tank is also provided with a hydrogen chloride discharge pipeline D communicated with the condensed acid tank, and the hydrogen chloride discharge pipeline D is communicated with a hydrogen chloride discharge pipeline C; a condensed acid discharge 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 a hydrogen chloride feeding pipeline, and the bottom end of the desorption reboiler is communicated with a hydrogen chloride/water mixed gas discharging pipeline; a saturated steam feeding pipeline A, a saturated steam discharging pipeline A and a condensed water outlet pipeline A which are communicated with the desorption reboiler are sequentially arranged at one side end of the desorption reboiler from top to bottom;
the analysis condensate tank is serially arranged on the condensate water outlet pipeline A, and the top end of the analysis condensate tank is communicated with the saturated steam discharge pipeline A;
the calcium chloride concentration and evaporation system comprises a first-effect evaporator, a first-effect flash evaporation tank, a first-effect condensed water tank, a second-effect evaporator, a second-effect flash evaporation tank, a second-effect condensed water tank, a third-effect evaporator, a third-effect flash evaporation tank, a third-effect condensed water tank, a third-effect discharge preheater, an evaporation condenser, a vacuum buffer tank and a water flow injection pump vacuum unit;
the center of the bottom end of the first-effect evaporator is communicated with a 40% calcium chloride discharge pipeline A, and the center of the top end of the first-effect evaporator is provided with a 40% calcium chloride discharge 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 primary condensed water tank is serially connected to a condensed water outlet pipeline B, and the top end of the primary condensed water tank is communicated with the saturated steam discharge pipeline B;
one side end of the primary-effect flash tank is communicated with a 40% calcium chloride discharge pipeline B, and the other side end of the primary-effect flash tank is provided with a 43.3% calcium chloride discharge pipeline A communicated with the primary-effect flash tank; a saturated steam feeding pipeline C communicated with the primary-effect flash tank is arranged in the center of the top end of the primary-effect flash tank, a 40% calcium chloride discharging pipeline C communicated with the primary-effect flash tank is arranged in the center of the bottom end of the primary-effect flash tank, and the other end of the 40% calcium chloride discharging pipeline C is communicated with the 40% calcium chloride discharging pipeline A;
the center of the bottom end of the second-effect evaporator is communicated with a 43.3% calcium chloride discharge pipeline A, and the center of the top end of the second-effect evaporator is provided with a 43.3% calcium chloride discharge pipeline B communicated with the second-effect evaporator; one side end of the second-effect evaporator is communicated with a saturated steam feeding pipeline C, and a saturated steam discharging pipeline C and a condensate water outlet pipeline C which are communicated with the second-effect evaporator are sequentially arranged at the side end of the second-effect evaporator at the lower part of the saturated steam feeding pipeline C from top to bottom;
the secondary condensed water tank is respectively communicated with a saturated steam discharge pipeline C and a condensed water outlet pipeline C, and a wastewater outlet pipeline A communicated with the secondary condensed water tank is arranged at the lower part of one side end of the secondary condensed water tank;
one side end of the two-effect flash tank is communicated with a 43.3% calcium chloride discharge pipeline B, and the other side end of the two-effect flash tank is provided with a 46.6% calcium chloride discharge pipeline A communicated with the two-effect flash tank; a saturated steam feeding pipeline D communicated with the secondary flash tank is arranged in the center of the top end of the secondary flash tank, a 43.3% calcium chloride discharging pipeline C communicated with the secondary flash tank is arranged in the center of the bottom end of the secondary flash tank, 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 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 triple-effect condensation water tank is serially arranged on the wastewater outlet pipeline B, and the top end of the triple-effect condensation water tank is communicated with the saturated steam discharge pipeline D;
one side end of the three-effect flash tank is communicated with a 46.6% calcium chloride discharge pipeline B, and the other side end of the three-effect flash tank is provided with a 50% calcium chloride discharge pipeline A communicated with the three-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 triple-effect discharge preheater is serially arranged on the condensed water outlet pipeline B and the 50% calcium chloride discharge pipeline A;
the top end of the evaporative condenser is communicated with a saturated steam feeding pipeline E, and the center of the bottom end of the evaporative condenser is provided with a wastewater outlet pipeline C communicated with the evaporative condenser; a circulating water return pipeline C, a circulating water supply pipeline C and a vacuumizing pipeline A which are communicated with the evaporative condenser are sequentially arranged at one side end of the evaporative condenser from top to bottom, and a water jet pump vacuum unit is communicated with the other end of the vacuumizing pipeline A;
the vacuum buffer tank is connected in series on a wastewater outlet pipeline C, and a vacuum condensation wastewater pump is also connected in series on the wastewater outlet pipeline C at the rear end of the vacuum buffer tank; the top end 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 producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: and the 31% hydrochloric acid feeding pipeline is also provided with a hot water feeding pipeline communicated with the 31% hydrochloric acid feeding pipeline.
3. The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: the hydrogen chloride discharge pipeline A is also provided with a nitrogen feeding pipeline communicated with the hydrogen chloride discharge pipeline A, and the nitrogen feeding pipeline close to one end of the hydrogen chloride discharge pipeline A is also provided with a check valve in series.
4. The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: the three-effect feeding pumps are arranged on the 40% calcium chloride discharging pipeline in parallel.
5. The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: a concentrated hydrochloric acid discharging pipeline D communicated with the demister is further arranged at the side end of the demister, and the other end of the concentrated hydrochloric acid discharging pipeline D is communicated with a concentrated hydrochloric acid discharging pipeline C; and the concentrated hydrochloric acid discharging pipeline D is arranged at the lower end of the hydrogen chloride discharging pipeline C.
6. The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: and a 50% calcium chloride discharge pipeline B is also arranged on the 46.6% calcium chloride discharge pipeline B in series, the other end of the 50% calcium chloride discharge pipeline B is communicated with a 50% calcium chloride discharge pipeline A at the front end of the triple-effect discharge preheater, and a triple-effect discharge pump is also arranged on the 50% calcium chloride discharge pipeline B in series.
7. The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 6, characterized in that: the three-effect discharge pump is provided with two discharge pumps which are arranged on a 50% calcium chloride discharge pipeline B in parallel.
8. The apparatus for producing hydrogen chloride by concentration and desorption from hydrochloric acid according to claim 1, characterized in that: the vacuum condensation waste water pump has two, and the parallelly connected setting is on waste water outlet pipe C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921034093.4U CN211111046U (en) | 2019-07-04 | 2019-07-04 | Device for producing hydrogen chloride by concentration and resolution in hydrochloric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921034093.4U CN211111046U (en) | 2019-07-04 | 2019-07-04 | Device for producing hydrogen chloride by concentration and resolution in hydrochloric acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211111046U true CN211111046U (en) | 2020-07-28 |
Family
ID=71700112
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921034093.4U Withdrawn - After Issue CN211111046U (en) | 2019-07-04 | 2019-07-04 | Device for producing hydrogen chloride by concentration and resolution in hydrochloric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211111046U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112985083A (en) * | 2021-02-06 | 2021-06-18 | 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 |
| CN116459636A (en) * | 2023-05-05 | 2023-07-21 | 南通星球石墨股份有限公司 | Deep-resolution hydrochloric acid treatment device |
-
2019
- 2019-07-04 CN CN201921034093.4U patent/CN211111046U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112985083A (en) * | 2021-02-06 | 2021-06-18 | 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 |
| CN116459636A (en) * | 2023-05-05 | 2023-07-21 | 南通星球石墨股份有限公司 | Deep-resolution hydrochloric acid treatment device |
| CN116459636B (en) * | 2023-05-05 | 2024-05-17 | 南通星球石墨股份有限公司 | Deep-resolution hydrochloric acid treatment device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110606470B (en) | Device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid | |
| CN105000612B (en) | Mechanical vapor recompression system of concentrated organic waste water and method | |
| CN108840310B (en) | Device and process for producing hydrogen chloride by deep analysis from dilute hydrochloric acid | |
| CN211111047U (en) | Calcium carbide method PVC mercury-containing waste acid treatment system | |
| CN103408086A (en) | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof | |
| CN211111046U (en) | Device for producing hydrogen chloride by concentration and resolution in hydrochloric acid | |
| CN106865860A (en) | Energy recovery type Catalytic Wet Air Oxidation for Wastewater processing unit and method of wastewater treatment | |
| CN101343208A (en) | Desorption technique for methylbenzene in tail gas from benzyl chloride preparation | |
| CN102020389A (en) | Process for recycling ammonium chloride waste water | |
| CN104843816B (en) | A kind of heat pump flash distillation stripping deamination coproduction of ammonia sulfate and the method for ammonia | |
| CN211255245U (en) | Production device for resolving hydrogen chloride from hydrochloric acid | |
| CN108671568A (en) | Energy conservation and environmental protection reforming technology is concentrated using the falling film evaporation of MVR | |
| CN104724776A (en) | Device and method for mixing secondary steam into pressurized water in pressurized evaporation | |
| CN211536562U (en) | Calcium chloride concentration and evaporation system | |
| CN104310441B (en) | Reaction heat utilization system and method in a kind of potassium nitrate combined producting ammonium chloride production | |
| CN216778404U (en) | System for capturing carbon dioxide by wet method | |
| CN211896157U (en) | Nitric acid wastewater treatment system containing aluminum nitrate | |
| CN210393786U (en) | Exhausted steam recompression low temperature evaporation waste water zero discharge system | |
| CN212403459U (en) | Deep analytical equipment of olefine acid concentration | |
| CN211752569U (en) | Multistage series horizontal tube falling film TVR steam jet evaporator | |
| CN203483883U (en) | Device for evaporating and concentrating waste liquid in caprolactam device | |
| CN104829452B (en) | Energy-saving production system of ethyl acetate and corresponding energy-saving production technology | |
| CN212450617U (en) | Waste hydrochloric acid differential pressure regeneration treatment system | |
| CN203668169U (en) | Low energy consumption hydrochloric acid wastewater recycling device | |
| CN203602362U (en) | Device for using heat energy of diammonium phosphate neutralizing tail gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20200728 Effective date of abandoning: 20230428 |
|
| AV01 | Patent right actively abandoned |
Granted publication date: 20200728 Effective date of abandoning: 20230428 |