CN202131112U - Caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis - Google Patents
Caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis Download PDFInfo
- Publication number
- CN202131112U CN202131112U CN201120203689U CN201120203689U CN202131112U CN 202131112 U CN202131112 U CN 202131112U CN 201120203689 U CN201120203689 U CN 201120203689U CN 201120203689 U CN201120203689 U CN 201120203689U CN 202131112 U CN202131112 U CN 202131112U
- Authority
- CN
- China
- Prior art keywords
- caustic soda
- liquid caustic
- tube
- concentration liquid
- hydrogen chloride
- 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.)
- Expired - Lifetime
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The utility model provides a caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis. The caustic soda concentrating device is characterized by comprising a first concentration liquid caustic soda storage tank, a first preheater, a first effect evaporator, a second effect evaporator, a second preheater and a synthetic furnace which are connected in sequence. The synthetic furnace comprises a furnace barrel provided with a hydrogen and chlorine inlet and a hydrogen chloride outlet, a closed type steam dome is arranged on the furnace barrel, a third concentration liquid caustic soda outlet and a low-pressure superheated steam outlet are arranged on the steam dome. The third concentration liquid caustic soda outlet is connected with the first preheater, and the low-pressure superheated steam outlet is connected with the first effect evaporator and the second effect evaporator. The synthetic furnace is provided with a heat exchanging element for heat exchange of second concentration liquid caustic soda and hydrogen chloride gases. The caustic soda concentrating device can completely utilize the waste heat produced by the hydrogen chloride synthesis in complementary mode and is very simple in structure, and the number of devices in the single device is greatly reduced.
Description
Technical field
The utility model relates to a kind of equipment of chemical industry for making chlorine and alkali product, and particularly a kind of hydrogenchloride synthetic waste heat that utilizes carries out the spissated device of alkali.
Background technology
In suitability for industrialized production, hydrogenchloride synthesizes in synthetic furnace and carries out, and its building-up reactions is thermopositive reaction.Therefore in the hydrogenchloride production process, must cool off the synthetic hydrogen chloride gas.Hydrogen chloride gas heat-eliminating medium of the prior art is generally water, institute's output be LP steam or hot water, the heat of LP steam or hot water fails to be fully utilized.Technological innovation is at present usually carried out around how to improve the type of furnace, and the hydrogenchloride of chlor-alkali production device is synthetic generally all to be to adopt the two-in-one steam of graphite (or hot water) synthetic furnace, and utilizes hydrogenchloride synthetic waste heat to attach the LP steam of producing or hot water.
The chlor-alkali production device attaches producing chlorine and hydrogen when producing liquid caustic soda (hereinafter to be referred as liquid caustic soda), and chlorine and hydrogen are to produce the required raw material of hydrogenchloride.The liquid caustic soda that the chlor-alkali production device is produced need heat concentrated; As being provided with in the caustic soda production facilities concentration is that the liquid caustic soda of 30-35wt% is the alkali concentrate apparatus of 50wt% through preheating, evaporation concentration to concentration, in spissated process, needs the energy of labor.Because the influence (particularly the imbalance between supply and demand of northern area caustic soda product is particularly outstanding) of transportation problem, chlor-alkali production enterprise has to produce the difficulty that solid caustic soda is alleviated production marketing.At present the method for domestic production solid caustic soda (hereinafter to be referred as solid caustic soda) has two kinds of cauldron method and membrane type methods: wherein; The cauldron method is brewed into the molten solid caustic soda with the liquid caustic soda that heavy oil or coal act as a fuel 45-50wt% in cauldron, barrelling is processed the barreled solid caustic soda or processed packed sheet solid caustic soda, pearl solid caustic soda, granular solid caustic soda through molding device again; And the membrane type method is through earlier in climbing-film evaporator, making thermal source with steam the liquid caustic soda of 45-50wt% to be risen membrane-concentrated to 60-65wt%; In falling-film evaporator, as thermal barrier the liquid caustic soda of 60-65wt% is carried out falling film evaporation with melting salt (act as a fuel heat with heavy oil or coal) again and process the molten solid caustic soda, barrelling is processed the barreled solid caustic soda or is processed packed sheet solid caustic soda, pearl solid caustic soda, granular solid caustic soda through molding device again.In the solid caustic soda production, energy consumption height and environmental pollution seriously are the big restraining factors of two in the present solid caustic soda production at home.
In existing production technology; Hydrogenchloride is synthetic, alkali concentrates and three kinds of production equipments of solid caustic soda are generally the self-contained system of mutual vicinity; Material to equipment also has different requirement, and for example the hydrogenchloride synthesizer requires to have acid resistance, and alkali concentrates with solid potash device and requires to have alkali resistance.
Because the existence of above-mentioned technical problem; Its hydrogenchloride is synthetic to be concentrated with alkali and the thermal resource of solid caustic soda production does not obtain complementary fully the utilization, and the single device quantity of production equipment is more, facility investment is big, complex structure, operator are more, floor space is big, three wastes discharge amount is big, environmental pollution is serious, need further to improve.
Summary of the invention
The utility model has solved more, the device structure complicated technology problem of single device quantity that exists the synthetic thermal resource concentrated with alkali and solid caustic soda production of hydrogenchloride not obtain complementary fully utilization, production equipment in the prior art.
The technical scheme of the utility model is:
A kind of hydrogenchloride synthetic waste heat that utilizes carries out the spissated device of alkali, it is characterized in that, said device comprises the first concentration liquid caustic soda basin, first preheater, 1st effective evaporator, 2nd effect evaporator, second preheater and the synthetic furnace that connects successively; Said synthetic furnace comprise have hydrogen, the stove tube of chlorine inlet and hydrogenchloride outlet; Said stove tube is provided with enclosed drum; Drum is provided with outlet of the 3rd concentration liquid caustic soda and low-pressure superheated steam outlet; Wherein the outlet of the 3rd concentration liquid caustic soda connects with first preheater, and the low-pressure superheated steam outlet connects with 1st effective evaporator, 2nd effect evaporator; Said synthetic furnace has the heat exchange element that the second concentration liquid caustic soda and hydrogen chloride gas carry out heat exchange.
Further improvement as the utility model: said heat exchange element comprises and is coated on the outer chuck of stove tube and is built in the synthetic furnace and is positioned at the shell and tube evaporation tank on stove tube top; Said shell and tube evaporation tank comprises case between the pipe that tubulation and tubulation form, and wherein tubulation is communicated with the stove tube, and lower box part is connected with convection tubes between pipe, and the other end of convection tubes is connected with stove tube chuck outward.
Further improvement as the utility model: described synthetic furnace also comprises the liquid caustic soda circulation tube that laterally arranges with the stove tube; Said liquid caustic soda circulation tube have that the second line of a couplet that connects with the chuck lower end is taken over and and the pipe of shell and tube evaporation tank between upper box part joining in adapting pipe, the upper end mouth of pipe and the drum of said liquid caustic soda circulation tube link.
Further improvement as the utility model: said stove tube bottom is provided with the synthetic lamp holder of hydrogenchloride, and said lamp holder is the burner that is provided with Gas Jet mixed cell and rotational flow gas mixed cell; Also be provided with eddy flow plate mist eliminator and mesh mist eliminator in the said drum, the alkali mist that is used for reducing low-pressure superheated steam is carried secretly.
Further improvement as the utility model: said second preheater comprises cylindrical shell, is coated on the outer preheating chuck of cylindrical shell and places the outer support saddle of preheating chuck; The chloridating gas that is used in the cylindrical shell after the heat exchange passes through, and the preheating chuck is used for the second concentration liquid caustic soda to be passed through; Be provided with helical baffle in the preheating chuck, be provided with traverse baffle in the cylindrical shell.
Further improvement as the utility model: also comprise sources of hydrogen, chlorine gas source, hydrogenchloride output terminal, the 3rd concentration liquid caustic soda output terminal, an effect separating tank and two effect separating tanks; Wherein the hydrogen chloride gas output terminal comprises hydrogen chloride cooler and hydrogenchloride surge tank; The 3rd concentration liquid caustic soda output terminal comprises solid caustic soda molding device and packaging facilities.
The utility model provides utilizes hydrogenchloride synthetic waste heat to carry out the spissated device single device of alkali quantity to be significantly reduced, and device structure is very simple.
Description of drawings
Fig. 1 carries out the structural representation of the synthetic furnace in the spissated device of alkali for the hydrogenchloride synthetic waste heat that utilizes that the utility model provides.
Fig. 2 carries out the structural representation of the lamp holder of the synthetic furnace in the spissated device of alkali for the hydrogenchloride synthetic waste heat that utilizes that the utility model provides.
Fig. 3 carries out the structural representation of second preheater in the spissated device of alkali for the hydrogenchloride synthetic waste heat that utilizes that the utility model provides.
Among the figure,
1-mount holder, 2-lamp holder, 2-1-chlorine inlet pipe, 2-2-chlorine passage pipe I, 2-3-hydrogen passage pipe I; 2-4-eddy flow plate mixing tank, 2-5-chlorine passage pipe II, 2-6-hydrogen passage pipe II, 2-7-hydrogen inlet pipe, 3-drop-bottom; 4-circulation tube, the 4-1-lower link mouth of pipe, the 4-2-middle connection mouth of pipe, the import of 4-3-second concentration liquid caustic soda, 5-stove tube; 5-1-chuck, 5-2-visor I, 5-3-fire hole, 6-shell and tube evaporation tank, 6-1-tubulation; Case between 6-2-pipe, 7-furnace roof end socket, 7-1-hydrogen chloride gas outlet, 8-rupture disk, 9-drum; The outlet of 9-1-the 3rd concentration liquid caustic soda, 9-2-low-pressure superheated steam outlet, 9-3-eddy flow plate mist eliminator, 9-4-mesh mist eliminator, 9-5-inspection window; 9-6-visor II, 10-liquidometer, 11-convection tubes, 12-helical baffle; 13-saddle, 14-cylindrical shell, 15-preheating chuck, 16-traverse baffle.
Embodiment
The utility model provides a kind of hydrogenchloride synthetic waste heat that utilizes to carry out the spissated device of alkali, and said device comprises the first concentration liquid caustic soda basin, first preheater, 1st effective evaporator, 2nd effect evaporator, second preheater and the synthetic furnace that connects successively.
In the utility model, the said first concentration liquid caustic soda basin is used to provide the first concentration liquid caustic soda as the first concentration liquid caustic soda source, and it adopts various liquid caustic soda storage facilities of the prior art to get final product, and does not have particular determination in the utility model.
Said first preheater is used for the first concentration liquid caustic soda is carried out preheating, and its thermal source is the liquid caustic soda residual heat, provides through the 3rd concentration liquid caustic soda that obtains in the synthetic furnace.Therefore, what realize in first preheater is the heat transfer process of the 3rd concentration liquid caustic soda and the first concentration liquid caustic soda, is liquid liquid heat transfer process.Common various high temperature resistant high density liquid caustic soda corrosive interchanger gets final product in said first preheater employing prior art, and the utility model does not have particular determination.
After in first preheater, accomplishing the heat exchange of liquid liquid, the 3rd concentration liquid caustic soda is cooled to about 100 ℃, can send the 3rd concentration liquid caustic soda output terminal to carry out subsequent disposal then, for example carries out solid caustic soda moulding and packing.Therefore, the device that the utility model provides also comprises the 3rd concentration output terminal, and said the 3rd concentration liquid caustic soda output terminal can comprise solid caustic soda molding device and packaging facilities.If pack with metal bucket, can be with the direct barrelling of the 3rd concentration liquid caustic soda that is cooled to about 100 ℃, the qualified back of weighing is sealed bucket, after air cooling, is stored.If produce sheet alkali; Then can send into and carry out moulding in the flake alkali processing machine being cooled to the 3rd concentration liquid caustic soda about 100 ℃; With recirculated water it is cooled to (zero pour of the 3rd concentration liquid caustic soda is 62.4 ℃) about 50 ℃ simultaneously; Sheet alkali entering wrapping machine after the moulding is packed, weighing, send warehouse Ma Dui, storage then.
The first concentration liquid caustic soda in first preheater after the heat exchange of completion liquid liquid is sent then and carries out an effect evaporation and two effect evaporations in 1st effective evaporator, the 2nd effect evaporator successively by preheating.Said 1st effective evaporator, 2nd effect evaporator all are used for liquid caustic soda is heated concentrated, and for example 1st effective evaporator can be concentrated into the liquid caustic soda of 30-35wt% the liquid caustic soda of 36-40wt%, and 2nd effect evaporator continues the liquid caustic soda of 36-40wt% is concentrated into the liquid caustic soda of 41-46wt%.Therefore adopt various alkali thickener of the prior art all can realize the utility model.But in the utility model, the thermal source of 1st effective evaporator, 2nd effect evaporator need not to add any thermal source all from the low-pressure superheated steam of synthetic furnace, can effectively cut down the consumption of energy.
The device that provides according to the utility model; After in 1st effective evaporator, 2nd effect evaporator, accomplishing an effect evaporation, two effect evaporations respectively; The product that obtains is the liquid-vapor mixture that contains steam and liquid caustic soda, therefore before the product of an effect evaporation send 2nd effect evaporator, also need send in the effect separating tank and carry out vapor-liquid separation; In like manner, two imitate evaporation product send and also need send into two before second preheater and imitate in the separating tanks and carry out vapor-liquid separation.Through imitating the vapor-liquid separation that separating tank, two is imitated in the separating tanks, and imitate evaporation, two with one and imitate the vapor removal in the evaporates and send into the negative-pressure vacuum system, obtain the higher liquid caustic soda of purity and send into next step operation one.Wherein, an effect separating tank, two effect separating tanks can directly adopt various high temperature resistant high density liquid caustic soda corrosive vapor-liquid separation tank common in the prior art.
The structure of said second preheater is as shown in Figure 3; Be used for that two effect separating tanks are separated the second concentration liquid caustic soda that obtains and carry out preheating; Its thermal source is the hydrogen chloride gas after the heat exchange, and the hydrogen chloride gas of having accomplished after the heat exchange through synthetic furnace provides its entrained surplus heat.Therefore, what realize in second preheater is the heat transfer process of the second concentration liquid caustic soda and hydrogen chloride gas, is the gas-liquid heat exchange process.The comprising cylindrical shell 14, be coated on the outer preheating chuck 15 of cylindrical shell 14 and place the outer support saddle 13 of preheating chuck 15 of said second preheater.The hydrogen chloride gas that is used in the cylindrical shell 14 after the heat exchange passes through, and is used for the second concentration liquid caustic soda in the preheating chuck 15 and passes through.As a kind of preferred implementation of the utility model, also be provided with helical baffle 12 in the preheating chuck 15, also be provided with traverse baffle 16 in the cylindrical shell 14, thereby can increase the turbulence of the second concentration liquid caustic soda, hydrogen chloride gas, to improve its heat exchange efficiency.
The other end of the cylindrical shell 14 of said second preheater is a pneumatic outlet, and said pneumatic outlet and hydrogenchloride output terminal UNICOM are used for the hydrogenchloride after the heat exchange completion is delivered to the user.Said hydrogen chloride gas output terminal can be provided with as required and comprise hydrogen chloride cooler and hydrogenchloride surge tank, send the user with hydrogen chloride gas then.At hydrogen chloride cooler hydrogen chloride gas is carried out can producing partial condensation hydrochloric acid in the process of cooling, condensation hydrochloric acid can send the hydrochloric acid medial launder for follow-up salt acid-utilising.
According to manufacturing technique requirent, also be provided with a plurality of alkali pumps in the device that the utility model provides.For example, be provided with first alkali pump between the first concentration liquid caustic soda basin and first preheater, be provided with second alkali pump between an effect separating tank and the 2nd effect evaporator, be provided with the 3rd alkali pump between the two effect separating tanks and second preheater.
The structure of said synthetic furnace is as shown in Figure 1; Comprise have hydrogen, the stove tube 5 of chlorine inlet and hydrogenchloride outlet; Said stove tube 5 is provided with enclosed drum 9; Drum 9 is provided with the 3rd concentration liquid caustic soda outlet 9-1 and low-pressure superheated steam outlet 9-2, and wherein the 3rd concentration liquid caustic soda outlet 9-1 connects with first preheater, and low-pressure superheated steam outlet 9-2 connects with 1st effective evaporator, 2nd effect evaporator.Said synthetic furnace has the heat exchange element that the second concentration liquid caustic soda and hydrogenchloride carry out heat exchange.
The bottom of said stove tube 5 is provided with the synthetic lamp holder 2 of hydrogenchloride.Therefore, said stove tube 5 is used for synthesizing chlorinated hydrogen on the one hand, is used for the synthetic hydrogen chloride gas on the other hand and the second concentration liquid caustic soda carries out heat exchange.Particularly, the bottom of stove tube 5 is provided with drop-bottom 3, is used to seal said stove tube 5.Drop-bottom 3 belows are provided with mount holder 1, are used to support whole synthetic furnace.Be equipped with the synthetic lamp holder 2 of hydrogenchloride on the drop-bottom 3, an end of lamp holder 2 is positioned at stove tube 5, and the other end is provided with hydrogen, chlorine inlet.
As the further improvement of the utility model, lamp holder 2 is for being provided with the burner of Gas Jet mixed cell and rotational flow gas mixed cell, and its structure is as shown in Figure 2.In the utility model, the gas mixed cell on the said lamp holder 2 is two groups, and promptly hydrogen, chlorine carry out thorough mixing twice, to reduce the content of synthetic hydrogen chloride gas Free Chlorine, guarantees the safety in production of subsequent handling (vinylchlorid is synthetic).Particularly, said lamp holder 2 is provided with two chlorine passages and two hydrogen passages, and the vertical direction of two chlorine passages is shut with shrouding.Wherein, two chlorine passages comprise: the space that (1) chlorine passage pipe I 2-2 coats, the space between (2) hydrogen passage pipe I 2-3 and the chlorine passage pipe II 2-5; Two hydrogen passages comprise: the space between (1) chlorine passage pipe I 2-2 and the hydrogen passage pipe I 2-3, the space between (2) chlorine passage pipe II 2-5 and the hydrogen passage pipe II 2-6.Hydrogen and chlorine get into two hydrogen passages and two chlorine passages from hydrogen inlet pipe 2-7 and chlorine inlet pipe 2-1 respectively simultaneously; Chlorine gets into behind two chlorine passages respectively the aperture that is uniformly distributed with from the tube wall of chlorine passage pipe I 2-2 and chlorine passage pipe II 2-5 and gets into two hydrogen passages with the effusive form, and chlorine carries out mixing the first time with hydrogen at this moment.It is more even for chlorine is mixed with hydrogen; In the exit of hydrogen passage pipe II 2-6 eddy flow plate mixing tank 2-4 is set; Make chlorine and hydrogen carry out mixing the second time; Thereby make chlorine and hydrogen be able to thorough mixing, guarantee the safety in production of subsequent handling (vinylchlorid is synthetic) to reduce the content of synthetic hydrogen chloride gas Free Chlorine.Simultaneously, owing to be provided with eddy flow plate mixing tank 2-4, the flame height when making the reaction of synthetic furnace internal combustion reduces greatly, and the temperature difference reduces in the stove, thereby making to be heated in the synthetic furnace is tending towards evenly the work-ing life that can suitably improve synthetic furnace.
In the device that the utility model provides, also comprise and the sources of hydrogen, the chlorine gas source that are connected respectively at hydrogen, chlorine inlet.In the utility model, the chlorine that hydrogen that sources of hydrogen provides and chlorine gas source provide all obtains through salt electrolysis, and wherein chlorine is dry through persulfuric acid earlier, then through Chlorine Buffer Vessel, is delivered to the chlorine inlet of lamp holder 2 at last.Under the preferable case, hydrogen also need carry out cooled dehydrated and demist and handle before sending into synthetic furnace; The hydrogen cooler that wherein cooled dehydrated adopted, demist are handled the hydrogen mist eliminator that is adopted and all can be adopted common device of the prior art, do not have particular determination in the utility model.
Further improvement as the utility model; In the utility model; The heat exchange element that said synthetic furnace had is two groups, and particularly, heat exchange element comprises the chuck 5-1 that is coated on stove tube 5 and is built in the synthetic furnace and is positioned at the shell and tube evaporation tank 6 on stove tube 5 tops.There are 7 sealings of furnace roof end socket the upper end of shell and tube evaporation tank 6.As shown in Figure 1, said shell and tube evaporation tank 6 comprises case 6-2 between tubulation 6-1 and pipe.Wherein tubulation 6-1 is communicated with stove tube 5, is used for stove tube 5 interior synthetic hydrogen chloride gas and passes through.The bottom of case 6-2 is connected with convection tubes 11 between pipe, and the other end of convection tubes 11 is connected with stove tube 5 outer chuck 5-1, is used for the second concentration liquid caustic soda and passes through.In the utility model, the quantity of convection tubes 11 does not have particular determination, for example can be 8, can be 16 yet.
Therefore, the second concentration liquid caustic soda passes through the chuck 5-1 of stove tube 5 successively, carries out the heat exchange first time with stove tube 5 interior hydrogen chloride gas; The second concentration liquid caustic soda of accomplishing heat exchange for the first time gets into through convection tubes 11 between the pipe of shell and tube evaporation tanks 6 among the case 6-2, carries out the heat exchange second time with hydrogen chloride gas among the tubulation 6-1 that gets into shell and tube evaporation tank 6.
After accomplishing heat exchange for the second time, hydrogen chloride gas gets in the furnace roof end socket 7 on shell and tube evaporation tank 6 tops, and furnace roof end socket 7 is provided with hydrogenchloride outlet 7-1 and rupture disk 8, and wherein hydrogen chloride gas is from hydrogenchloride outlet 7-1 output.When in the stove during hydrogen chloride gas Free Chlorine content overproof, can in stove, produce blast and form shockwave and cause local pressure sharply to increase, rupture disk 8 is blown, let out except that furnace pressure, thereby the nonmetal equipment and the pipeline of hydrogenchloride system played a protective role.In the device that the utility model provides, also comprise with furnace roof end socket 7 on the hydrogenchloride that connects of hydrogenchloride outlet export 7-1.7-1 is through the pipeline and the second preheater UNICOM for the outlet of said hydrogenchloride, thus the hydrogen chloride gas that will accomplish heat exchange send in the cylindrical shell 14 of second preheater, be used for the second concentration liquid caustic soda is carried out preheating.
After accomplishing heat exchange for the second time, the liquid caustic soda in the second concentration liquid caustic soda can be converted into the 3rd concentration liquid caustic soda, by-product low-pressure superheated steam.
Described synthetic furnace also comprises the liquid caustic soda circulation tube 4 that laterally arranges with stove tube 5.Said liquid caustic soda circulation tube 4 have the lower link mouth of pipe 4-1 that connects with chuck 5-1 lower end and with the pipe of shell and tube evaporation tank 6 between case 6-2 top connect mouth of pipe 4-2 in joining, the upper end mouth of pipe and the drum 9 of said liquid caustic soda circulation tube 4 link.The middle part of circulation tube 4 also is provided with the second concentration liquid caustic soda import 4-3; The second concentration liquid caustic soda import 4-3 is through preheating chuck 15 UNICOMs of the pipeline and second preheater; Thereby can get into circulation tube 4 through the second concentration liquid caustic soda import 4-3 at circulation tube 4 middle parts through the second concentration liquid caustic soda after the preheating, again in lower link mouth of pipe 4-1 gets into the chuck 5-1 of synthetic furnace.Carry out heat exchange through case 6-2 and hydrogen chloride gas between chuck 5-1, pipe, after the second concentration liquid caustic soda is accomplished heat exchange, through and the pipe of shell and tube evaporation tank 6 between case 6-2 top joining in adapting pipe 4-2 get in the circulation tube 4, and in the entering drum 9 that rises.When liquid-vapor mixture rose to drum 9 surperficial, water vapor carried out surface evaporation on the surface of drum 9, and in drum, assembles, and its liquid level top is the low-pressure superheated steam of by-product.The part liquid caustic soda that does not get into drum in the circulation tube 4 can be back to circulation tube 4 bottoms, and flow to again through lower link mouth of pipe 4-1 and to repeat above-mentioned heat exchange steps in the chuck 5-1, therefore can form the circulation passage of liquid caustic soda.
Getting into the concentrated liquid caustic soda that forms that transforms of drum 9 after heat assembles in drum 9; Through the concentration control instruments on the pipeline, for example densometer is measured the liquid caustic soda concentration that the 3rd concentration liquid caustic soda exports 9-1; After liquid caustic soda reaches finite concentration; For example during described the 3rd concentration of the utility model, the 3rd concentration liquid caustic soda that obtains is delivered in first preheater through the outlet of the 3rd concentration liquid caustic soda on the drum 9 9-1, carries out aforementioned heat exchange, solid caustic soda moulding process.And the low-pressure superheated steams in the drum 9 can export 9-2 through LP steam to deliver in 1st effective evaporator, the 2nd effect evaporator when reaching certain pressure, the first concentration liquid caustic soda is carried out alkali concentrate.As the further improvement of the utility model, carry secretly for preventing the alkali mist in the low-pressure superheated steam, also be provided with eddy flow plate mist eliminator 9-3 and mesh mist eliminator 9-4 in the drum 9.The bottom of stove tube 5 is provided with 2 visor I 5-2 and 1 fire hole 5-3.Drum 9 is provided with 2 visor II 9-6 that split and 1 inspection window 9-5 is set on skirt between eddy flow plate mist eliminator 9-3 and mesh mist eliminator 9-4.
In the utility model, the said hydrogenchloride synthetic waste heat that utilizes carries out in the spissated device of alkali, and the material of the element of installation that synthetic furnace and various and liquid caustic soda contact with hydrogen chloride gas is Langaloy.Described Langaloy be can high temperature resistant (about 200 ℃) 80wt% liquid caustic soda corrosion again can high temperature resistant (about 1200 ℃) hydrogen chloride gas and the Langaloy of cryogenic condensation hcl corrosion.
The hydrogenchloride synthetic waste heat that utilizes that provides below in conjunction with the utility model carries out the principle of work that the spissated method and apparatus of alkali specifies the utility model.
(1) from the 30-35wt% liquid caustic soda of the first concentration liquid caustic soda basin through the first preheater preheating (carrying out heat exchange) with the 73wt% liquid caustic soda that has come out from the 3rd concentration liquid caustic soda outlet 9-1 of synthetic furnace before; Send into 1st effective evaporator with first alkali pump; The low-pressure superheated steam that comes out with the low-pressure superheated steam of synthetic furnace outlet 9-2 heats; Liquid-vapor mixture after the heating gets into one and imitates separating tank, imitates in the separating tank one and carries out surperficial negative pressure evaporation, obtains the liquid caustic soda of 35-40wt%; The secondary steam that evaporation simultaneously produces gets into the negative-pressure vacuum system, and water of condensation advances hot water tank.
(2) imitate evaporation concentration through one and send into 2nd effect evaporator with second alkali pump to the liquid caustic soda of 35-40wt%; The low-pressure superheated steam that comes out with the low-pressure superheated steam of synthetic furnace outlet 9-2 heats; Liquid-vapor mixture after the heating gets into two and imitates separating tank; In two effect separating tanks, carry out surperficial negative pressure evaporation, obtain the liquid caustic soda of 41-46wt%; The secondary steam that evaporation simultaneously produces gets into the negative-pressure vacuum system, and water of condensation advances hot water tank.
(3) high-temperature-hot-water in the hot water tank send polyvinyl chloride to transform and the polymerization use, and the low-temperature water heating after polyvinyl chloride uses and the low-temperature water heating of negative-pressure vacuum system send the salt hydratable salt.
The liquid glucose that (4) will prepare is pumped into static mixer with metering, and the liquid caustic soda of the 41-46wt% that simultaneously step (2) is obtained is also sent in the static mixer and mixed with liquid glucose, together sends into then in the preheating chuck 15 of second preheater.
(5) hydrogen chloride gas in the cylindrical shell through second preheater 14 carries out preheating to liquid caustic soda and the liquid glucose of the 41-46wt% in the preheating chuck 15, and the liquid caustic soda of 41-46wt% and liquid glucose react in the warm, removes the ClO in the liquid caustic soda of 41-46wt% through liquid glucose
3 -After [x1] accomplished, the refrigerative hydrogen chloride gas sent the user through the hydrogenchloride output terminal, and the liquid caustic soda of 41-46wt% gets into circulation tube 4 from the second concentration liquid caustic soda import 4-3 at circulation tube 4 middle parts, again in lower link mouth of pipe 4-1 gets into the chuck 5-1 of synthetic furnace.
(6) hydrogen and the chlorine through cooled dehydrated and demist processing gets into stove tubes 5 through the lamp holder 2 of synthetic furnace
In, combustion reactions is carried out in igniting, and hydrogen chloride gas that generates after the reaction in furnace and the stove tube 5 outer interior 41-46wt% liquid caustic soda of chuck 5-1 carry out the heat exchange first time; Hydrogen chloride gas gets in the tubulation 6-1 of shell and tube evaporation tank 6 then, and the 41-46wt% liquid caustic soda is through in the case 6-2 between the pipe of convection tubes 11 entering shell and tube evaporation tanks 6, thereby hydrogen chloride gas and 41-46wt% liquid caustic soda carry out the heat exchange second time.
(7) hydrogen chloride gas of accomplishing heat exchange for the second time is from the furnace roof end socket 7 of tubulation 6-1 entering shell and tube evaporation tank 6 tops; And through hydrogenchloride outlet 7-1 hydrogen chloride gas is delivered in the cylindrical shell 14 of second preheater, thereby the heat that guarantees second preheater in the step (4) is supplied with.
(8) the second concentration liquid caustic soda import 4-3 through circulation tube 4 after the 41-46wt% liquid caustic soda of completion heat exchange for the second time is heated gets in the circulation tube 4, again in the chuck 5-1 of lower link mouth of pipe 4-1 entering synthetic furnace.Carry out heat exchange through case 6-2 and hydrogen chloride gas between chuck 5-1, pipe, after the second concentration liquid caustic soda is accomplished heat exchange, through and the pipe of shell and tube evaporation tank 6 between case 6-2 top joining in adapting pipe 4-2 get in the circulation tube 4, and in the entering drum 9 that rises.When liquid-vapor mixture rose to drum 9 surperficial, water vapor carried out surface evaporation on the surface of drum 9, and in drum, assembles, and its liquid level top is the low-pressure superheated steam of by-product.
(9) after the low-pressure superheated steam in the drum 9 reaches setting pressure (advancing the water seal control of hot water tank with water of condensation); Through the eddy flow plate mist eliminator 9-3 in the drum 9, mesh mist eliminator 9-4 low-pressure superheated steam being carried out demist handles; Be delivered to 1st effective evaporator, the 2nd effect evaporator heat supply of two effect evaporations in an effect evaporation, the step (2) in the assurance step (1) then from low-pressure superheated steam outlet 9-2.
(10) after the liquid caustic soda of concentration control instruments (densometer) detection the 3rd concentration liquid caustic soda outlet 9-1 that is provided with on the pipeline reaches 73wt%; 9-1 delivers in first preheater through the outlet of the 3rd concentration liquid caustic soda, thereby can guarantee that the heat in first preheater is supplied with in the step (1).The 73wt% liquid caustic soda that comes out from first preheater is cooled to 100 ℃, directly barrelling then, and the qualified back of weighing is sealed bucket, after air cooling, is stored; Perhaps send into and carry out moulding in the flake alkali processing machine, with recirculated water it is cooled to (zero pour of the 3rd concentration liquid caustic soda is 62.4 ℃) about 50 ℃ simultaneously, the sheet alkali entering wrapping machine after the moulding is packed, weighing, send warehouse Ma Dui, storage.
That adopts that the utility model provides utilizes the preheating of hydrogenchloride synthetic to carry out the spissated method and apparatus of alkali to produce; Its throughput is: hydrogenchloride output is 5000m3/h (0.06MPa; 40 ℃); 73wt% solid caustic soda (folding 100%NaOH) output is 50,000 tons/year, 8.88 ten thousand tons/year of recycle-water resources (wherein reclaim more than 90 ℃ high-temperature-hot-water 4.84 ten thousand tons/year).
Above embodiment is merely the preferred implementation of the utility model, should be pointed out that to those skilled in the art, and under the prerequisite that does not break away from the utility model principle, some improvement of having done also should be regarded as the protection domain of the utility model.
Claims (6)
1. one kind is utilized hydrogenchloride synthetic waste heat to carry out the spissated device of alkali, it is characterized in that, said device comprises the first concentration liquid caustic soda basin, first preheater, 1st effective evaporator, 2nd effect evaporator, second preheater and the synthetic furnace that connects successively; Said synthetic furnace comprise have hydrogen, the stove tube of chlorine inlet and hydrogenchloride outlet; Said stove tube is provided with enclosed drum; Drum is provided with outlet of the 3rd concentration liquid caustic soda and low-pressure superheated steam outlet; Wherein the outlet of the 3rd concentration liquid caustic soda connects with first preheater, and the low-pressure superheated steam outlet connects with 1st effective evaporator, 2nd effect evaporator; Said synthetic furnace has the heat exchange element that the second concentration liquid caustic soda and hydrogen chloride gas carry out heat exchange.
2. device according to claim 1 is characterized in that, said heat exchange element comprises and is coated on the outer chuck of stove tube and is built in the synthetic furnace and is positioned at the shell and tube evaporation tank on stove tube top; Said shell and tube evaporation tank comprises case between the pipe that tubulation and tubulation form, and wherein tubulation is communicated with the stove tube, and lower box part is connected with convection tubes between pipe, and the other end of convection tubes is connected with stove tube chuck outward.
3. device according to claim 1; It is characterized in that; Described synthetic furnace also comprises the liquid caustic soda circulation tube that laterally arranges with the stove tube; Said liquid caustic soda circulation tube have that the second line of a couplet that connects with the chuck lower end is taken over and and the pipe of shell and tube evaporation tank between upper box part joining in adapting pipe, the upper end mouth of pipe and the drum of said liquid caustic soda circulation tube link.
4. device according to claim 1 is characterized in that, said stove tube bottom is provided with the synthetic lamp holder of hydrogenchloride, and said lamp holder is the burner that is provided with Gas Jet mixed cell and rotational flow gas mixed cell; Also be provided with eddy flow plate mist eliminator and mesh mist eliminator in the said drum, the alkali mist that is used for reducing low-pressure superheated steam is carried secretly.
5. device according to claim 1 is characterized in that, said second preheater comprises cylindrical shell, is coated on the outer preheating chuck of cylindrical shell and places the outer support saddle of preheating chuck; The chloridating gas that is used in the cylindrical shell after the heat exchange passes through, and the preheating chuck is used for the second concentration liquid caustic soda to be passed through; Be provided with helical baffle in the preheating chuck, be provided with traverse baffle in the cylindrical shell.
6. device according to claim 1 is characterized in that, also comprises sources of hydrogen, chlorine gas source, hydrogenchloride output terminal, the 3rd concentration liquid caustic soda output terminal, an effect separating tank and two effect separating tanks; Wherein the hydrogen chloride gas output terminal comprises hydrogen chloride cooler and hydrogenchloride surge tank; The 3rd concentration liquid caustic soda output terminal comprises solid caustic soda molding device and packaging facilities.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120203689U CN202131112U (en) | 2011-06-16 | 2011-06-16 | Caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120203689U CN202131112U (en) | 2011-06-16 | 2011-06-16 | Caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202131112U true CN202131112U (en) | 2012-02-01 |
Family
ID=45519889
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120203689U Expired - Lifetime CN202131112U (en) | 2011-06-16 | 2011-06-16 | Caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202131112U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102285670A (en) * | 2011-06-16 | 2011-12-21 | 肖正群 | Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride |
-
2011
- 2011-06-16 CN CN201120203689U patent/CN202131112U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102285670A (en) * | 2011-06-16 | 2011-12-21 | 肖正群 | Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride |
| CN102285670B (en) * | 2011-06-16 | 2013-07-10 | 肖正群 | Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101624194A (en) | Production method for co-production of mirabilite and salt and production device thereof | |
| CN101007622A (en) | Device for tail chlorine degassing and absorption for preparing hydrochloride gas and its preparation method | |
| CN1131171C (en) | Equipment for recovering and utilizing heat energy generated by phosphor combustion and system for preparing phosphoric acid by hot method | |
| CN102583444A (en) | Alkali-manufacturing device and alkali-manufacturing method for manufacturing alkali in three-section falling film coal burning method | |
| CN202131112U (en) | Caustic soda concentrating device using waste heat produced by hydrogen chloride synthesis | |
| CN102285670B (en) | Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride | |
| CN206108917U (en) | Concentrated film -making device of potash | |
| CN102515202A (en) | Method for producing ionic membrane flake caustic by using fire coal falling film method | |
| CN104178234B (en) | Coke-stove gas prepares natural gas and residual-heat utilization method and system with producer gas | |
| CN214167372U (en) | System for preparing stannous chloride by recycling dilute hydrochloric acid tail gas | |
| CN104973572A (en) | Purification plant and purification technique of chlorinated paraffin coproduct hydrogen chloride | |
| CN212942889U (en) | Aluminum sulfate multilayer reaction device | |
| CN111099639B (en) | Ammonia supply system and method for preparing sodium carbonate | |
| CN201848198U (en) | Industrial waste gas treatment and salt regenerating unit | |
| CN205275221U (en) | Vapor -recovery unit of salt prunella coproduction | |
| CN101327939A (en) | Method for solid caustic soda production by ionic membrane method | |
| CN209771799U (en) | Comprehensive recycling system for PVC (polyvinyl chloride) waste alkali and gas burning kiln waste gas | |
| CN204768040U (en) | Sizing material is cooked and is cooled off recovery unit | |
| CN103708989B (en) | A kind of dehydrogenation unit in vinyltoluene production | |
| CN101549857A (en) | Production method and device for condensing alkali and synthesising hydrogen chloride by residual heat | |
| CN115028142B (en) | System for utilize useless hydrochloric acid to prepare hydrogen | |
| CN109205557A (en) | A kind of preparation method of water hydrogen fuel | |
| CN101830437B (en) | Production method and device for synthesizing hydrogen chloride and concentrating alkali by using waste heat | |
| CN218686371U (en) | Alkali lye concentration's enrichment facility | |
| CN214693947U (en) | Preparation facilities of coproduction benzyl chlorine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20120201 Effective date of abandoning: 20130710 |
|
| RGAV | Abandon patent right to avoid regrant |