CN102285670B - Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride - Google Patents
Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride Download PDFInfo
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- CN102285670B CN102285670B CN2011101624795A CN201110162479A CN102285670B CN 102285670 B CN102285670 B CN 102285670B CN 2011101624795 A CN2011101624795 A CN 2011101624795A CN 201110162479 A CN201110162479 A CN 201110162479A CN 102285670 B CN102285670 B CN 102285670B
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Abstract
The invention provides a method and device for performing alkali concentration by utilizing the synthesis waste heat of hydrogen chloride. The method is characterized in that the method comprises the following steps: preheating a first-concentration caustic soda solution in a first preheater, and performing one-effect evaporation and two-effect evaporation to obtain a second-concentration caustic soda solution; and preheating the second-concentration caustic soda solution in a second preheater, and then performing heat exchange with the hydrogen chloride gas synthesized in a combustion reaction to obtain a third-concentration caustic soda solution and low-pressure superheated steam, wherein the heat source of the first preheater is the third-concentration caustic soda solution, the heat source of the second preheater is the hydrogen chloride gas obtained through heat exchange, and the heat sources of the one-effect evaporation and two-effect evaporation are the low-pressure superheated steam. The invention also provides a device for implementing the method. By adopting the method provided by the invention, the synthesis waste heat of hydrogen chloride can be fully complemented and utilized, the equipment number of the device can be greatly reduced and the device has a very simple structure.
Description
Technical field
The present invention relates to a kind of production method and equipment of chemical industry for making chlorine and alkali product, particularly a kind of synthetic waste heat of hydrogenchloride that utilizes carries out method and the device that alkali concentrates.
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 synthetic hydrogen chloride gas be cooled off.Hydrogen chloride gas heat-eliminating medium of the prior art is generally water, institute's output be low-pressure steam or hot water, the heat of low-pressure 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 the hydrogenchloride synthetic attached product low-pressure steam of waste heat or hot water.
The chlor-alkali production device is attached 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, be that the liquid caustic soda of 30-35wt% is the alkali concentrate apparatus of 50wt% by preheating, evaporation concentration to concentration as being provided with in the caustic soda production facilities concentration, in the process that concentrates, need to expend a large amount of energy.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 made the barreled solid caustic soda or made packed sheet solid caustic soda, pearl solid caustic soda, granular solid caustic soda by molding device again; And the membrane type method is by earlier making thermal source with steam in climbing-film evaporator the liquid caustic soda of 45-50wt% to be risen membrane concentration to 60-65wt%, 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 in falling-film evaporator and make the molten solid caustic soda, barrelling is made the barreled solid caustic soda or is made packed sheet solid caustic soda, pearl solid caustic soda, granular solid caustic soda by 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 requirements, and for example the hydrogenchloride synthesizer requires to have acid resistance, and alkali concentrates and solid potash device requires to have alkali resistance.
Because the existence of above-mentioned technical problem, its hydrogenchloride is synthetic and alkali concentrates and the thermal resource of solid caustic soda production does not obtain complementary utilization the fully, 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 invention solves and exist the synthetic thermal resource concentrated with alkali and solid caustic soda production of hydrogenchloride not obtain more, the device structure complicated technology problem of single device quantity of complementary utilization, production equipment fully in the prior art.
The invention provides a kind of synthetic waste heat of hydrogenchloride that utilizes and carry out the method that alkali concentrates, may further comprise the steps: the first concentration liquid caustic soda is carried out preheating in first preheater, carry out one then and imitate evaporation, two and imitate evaporation and obtain the second concentration liquid caustic soda; The second concentration liquid caustic soda is carried out preheating in second preheater, carry out heat exchange with the synthetic hydrogen chloride gas of combustion reactions then, obtain the 3rd concentration liquid caustic soda and low-pressure superheated steam; Wherein, the thermal source of first preheater is the 3rd concentration liquid caustic soda, and the thermal source of second preheater is the hydrogen chloride gas after the heat exchange, and thermals source of imitating evaporation, two effect evaporations are low-pressure superheated steam.
The synthetic waste heat of hydrogenchloride that utilizes provided by the invention carries out the method that alkali concentrates, and by adopting the synthetic waste heat of hydrogenchloride the second concentration liquid caustic soda is concentrated, and can obtain the 3rd concentration liquid caustic soda, simultaneously the by-product low-pressure superheated steam; And the 3rd concentration liquid caustic soda carries out preheating with self-contained surplus heat with the first concentration liquid caustic soda of opposing simultaneously, the first concentration liquid caustic soda of the heat that carries by low-pressure superheated steam after to preheating carries out one imitates evaporation, two and imitates evaporation, obtain the second concentration liquid caustic soda, thereby form the heat circulation that is concentrated into the solid caustic soda process from liquid caustic soda, the waste heat that hydrogenchloride is synthetic carries out complementary utilization the fully in the working cycle.
The present invention also provides a kind of synthetic waste heat of hydrogenchloride that utilizes to carry out the device that alkali concentrates, and described 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;
Described synthetic furnace comprise have hydrogen, the stove tube of chlorine entrance and hydrogenchloride outlet, described stove tube is provided with enclosed drum, drum is provided with the 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; Described synthetic furnace has the heat exchange element that the second concentration liquid caustic soda and hydrogen chloride gas carry out heat exchange.
The waste heat that utilizes hydrogenchloride to synthesize provided by the invention carries out the device that alkali concentrates, and described synthetic furnace both had been used for the synthetic of hydrogenchloride, also is used for the second concentration liquid caustic soda and hydrogenchloride are carried out heat exchange, and the realization liquid caustic soda concentrates and obtains the 3rd required concentration liquid caustic soda.Synthetic furnace comprises the drum on stove tube and the stove tube, and drum is provided with the outlet of the 3rd concentration liquid caustic soda and low-pressure superheated steam outlet; Wherein the 3rd concentration liquid caustic soda outlet connects with first preheater, and the surplus heat that carries by the 3rd concentration liquid caustic soda is as the thermal source of first preheater, thereby the first concentration liquid caustic soda is carried out preheating; And the low-pressure superheated steam outlet connects with 1st effective evaporator, 2nd effect evaporator, and the heat that carries by low-pressure superheated steam is as the thermal source of 1st effective evaporator, 2nd effect evaporator, thereby the first concentration liquid caustic soda is concentrated, and obtains the second concentration liquid caustic soda.The waste heat that utilizes hydrogenchloride to synthesize provided by the invention carries out the concentrated device single device quantity of alkali and is significantly reduced, and device structure is very simple.
Description of drawings
Fig. 1 is the process flow diagram that utilizes the synthetic waste heat of hydrogenchloride to carry out the concentrated method of alkali provided by the invention.
Fig. 2 is the structural representation that utilizes the synthetic waste heat of hydrogenchloride to carry out the synthetic furnace in the concentrated device of alkali provided by the invention.
Fig. 3 is the structural representation that utilizes the synthetic waste heat of hydrogenchloride to carry out the lamp holder of the synthetic furnace in the concentrated device of alkali provided by the invention.
Fig. 4 is the structural representation that utilizes the synthetic waste heat of hydrogenchloride to carry out second preheater in the concentrated device of alkali provided by the invention.
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, 4-1-lower link the 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-pre-thermal jacket, 16-traverse baffle.
Embodiment
The invention provides a kind of synthetic waste heat of hydrogenchloride that utilizes and carry out the method that alkali concentrates, may further comprise the steps: the first concentration liquid caustic soda is carried out preheating in first preheater, carry out one then and imitate evaporation, two and imitate evaporation and obtain the second concentration liquid caustic soda; The second concentration liquid caustic soda is carried out preheating in second preheater, carry out heat exchange with the synthetic hydrogen chloride gas of combustion reactions then, obtain the 3rd concentration liquid caustic soda and low-pressure superheated steam; Wherein, the thermal source of first preheater is the 3rd concentration liquid caustic soda, and the thermal source of second preheater is the hydrogen chloride gas after the heat exchange, and thermals source of imitating evaporation, two effect evaporations are low-pressure superheated steam.
Provided by the inventionly utilize technical process that the synthetic waste heat of hydrogenchloride carries out the method that alkali concentrates as shown in Figure 1, comprise two technology circuits: (1) hydrogenchloride synthetic line: the hydrogenchloride synthetic line is total source of heat in the method for the present invention, by synthesizing of chlorine, hydrogen, emit big calorimetric (following note is made synthetic heat), be used for the second circuit thereby should synthesize heat.(2) alkali concentrates circuit: the first concentration liquid caustic soda carries out preheating in first preheater, carries out one then and imitates evaporation, two and imitate evaporation and obtain the second concentration liquid caustic soda; The second concentration liquid caustic soda is carried out preheating in second preheater, concentrate by the synthetic heat that adopts hydrogenchloride then, obtain the 3rd concentration liquid caustic soda and low-pressure superheated steam; And the surplus heat of the 3rd concentration liquid caustic soda (following note is made the liquid caustic soda residual heat) carries out preheating with the first concentration liquid caustic soda of opposing, and namely the 3rd concentration liquid caustic soda is as the thermal source of first preheater; The heat that low-pressure superheated steam carries (following note is made steam heat) is used for the first concentration liquid caustic soda is concentrated, and namely low-pressure superheated steam is imitated the thermal source that evaporation is imitated in evaporation, two as one.
Among the present invention, the concentration of the described first concentration liquid caustic soda is 35-40wt%, and the concentration of the second concentration liquid caustic soda is 36-46wt%, and the concentration of the 3rd concentration liquid caustic soda is 73wt%.Among the present invention, an effect is evaporated, two effect evaporations are all concentrated for liquid caustic soda is heated, and for example an effect is evaporated the liquid caustic soda that the liquid caustic soda of 30-35wt% can be concentrated into 36-40wt%, and two effects are evaporated the liquid caustic soda that continues the liquid caustic soda of 36-40wt% is concentrated into 41-46wt%.
As those skilled in the art's common practise, the step of combustion reactions synthesising hydrogen comprises: hydrogen and chlorine in lamp holder enters synthetic furnace, are carried out combustion reactions after the igniting, can obtain described hydrogen chloride gas.Wherein, hydrogen also can carry out cooled dehydrated and demist as required and handle before entering synthetic furnace.
As a kind of preferred implementation of the present invention, comprise jacketed type and shell and tube through the second concentration liquid caustic soda after the second preheater preheating and the mode of hydrogen chloride gas heat exchange.By twice heat exchange of the second concentration liquid caustic soda and hydrogen chloride gas, the synthetic heat of hydrogenchloride can be taken full advantage of, avoid causing thermal radiation to pollute.
The method according to this invention is carried out one to the first concentration liquid caustic soda and is imitated after evaporation, two imitates evaporation, obtains the second concentration liquid caustic soda.As a further improvement on the present invention, method of the present invention also comprise one imitate evaporation finish back one imitate separate, two imitate evaporation finish after two effect separation steps.Imitate in the evaporative process because one imitates evaporation, two, the first concentration liquid caustic soda is concentrated and forms the second concentration liquid caustic soda, make one to imitate evaporation, two and imitate in the evaporative processes all byproduct steams, therefore finish one imitate evaporation, two products of imitating after the evaporation are the liquid-vapor mixture that contains liquid caustic soda and steam.Under the preferable case, imitate separation energies by an effect separation, two steam of by-product in the liquid-vapor mixture is sent into the negative-pressure vacuum system, guarantee that an effect is evaporated, two effect evaporations are carried out under negative pressure, to reduce the boiling point of liquid caustic soda, the vaporization heat of low-pressure superheated steam is fully utilized.One water of condensation of imitating after evaporation, the two effect evaporations advance hot water tank, thereby further take full advantage of heat.Among the present invention, the hot water in the hot water tank can also further send polyethylene to transform and polymerization is used.Further, the low-temperature water heating after polyethylene conversion and polymerization are used and the low-temperature water heating of negative pressure system can send the salt hydratable salt.
Among the present invention, for removing the ClO in the second concentration liquid caustic soda
3 -, under the preferable case, also comprise the second concentration liquid caustic soda mixed with liquid glucose, thereby reduce ClO
3 -Corrosive nature to equipment.The second concentration liquid caustic soda can carry out in static mixer with mixing of liquid glucose, together sent in second preheater then to react, and removed the ClO in the second concentration liquid caustic soda
3 -
The invention provides a kind of synthetic waste heat of hydrogenchloride that utilizes and carry out the device that alkali concentrates, described 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.
Among the present invention, the described first concentration liquid caustic soda basin is used for the first concentration liquid caustic soda is provided 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 among the present invention.
Described 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 by 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.Described first preheater adopts the interchanger of various high temperature resistant high density liquid caustic soda corrosion common in the prior art to get final product, and the present invention does not have particular determination.
Finish the heat exchange of liquid liquid in first preheater after, 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, device provided by the invention also comprises the 3rd concentration output terminal, and described 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, is stored after air cooling.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 after the moulding enters that wrapping machine is packed, weighing, send warehouse Ma Dui, storage then.
The first concentration liquid caustic soda of finishing in first preheater after the heat exchange of liquid liquid is preheated, and send then to carry out one in 1st effective evaporator, the 2nd effect evaporator successively and imitate evaporation and two and imitate evaporation.Described 1st effective evaporator, 2nd effect evaporator are all concentrated for liquid caustic soda is heated, 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 present invention.But among the present invention, 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.
According to device provided by the invention, after in 1st effective evaporator, 2nd effect evaporator, finishing an effect evaporation, two effect evaporations respectively, the product that obtains is the liquid-vapor mixture that contains steam and liquid caustic soda, therefore also need send into before a product of imitating evaporation send 2nd effect evaporator in the effect separating tank and carry out vapor-liquid separation; In like manner, two products of imitating evaporation send and also need send into two before second preheater and imitate in the separating tanks and carry out vapor-liquid separation.By imitating separating tank, two vapor-liquid separation of imitating in the separating tanks one, 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.Wherein, an effect separating tank, two is imitated the vapor-liquid separation tank that separating tanks can directly adopt various high temperature resistant high density liquid caustic soda corrosion common in the prior art.
The structure of described second preheater as shown in Figure 4, 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 finished after the heat exchange by 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 pre-thermal jacket 15 of cylindrical shell 14 and place the outer support saddle 13 of pre-thermal jacket 15 of described second preheater.Pass through for the hydrogen chloride gas after the heat exchange in the cylindrical shell 14, be used for the second concentration liquid caustic soda in the pre-thermal jacket 15 and pass through.As a kind of preferred implementation of the present invention, also be provided with helical baffle 12 in the pre-thermal jacket 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 described second preheater is pneumatic outlet, and described pneumatic outlet and hydrogenchloride output terminal UNICOM are delivered to the user for the hydrogenchloride after heat exchange is finished.Described hydrogen chloride gas output terminal can arrange 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 provided by the invention.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 two effect separating tanks and second preheater.
The structure of described synthetic furnace as shown in Figure 2, comprise have hydrogen, the stove tube 5 of chlorine entrance and hydrogenchloride outlet, described 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, 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.Described synthetic furnace has the heat exchange element that the second concentration liquid caustic soda and hydrogenchloride carry out heat exchange.
The bottom of described stove tube 5 is provided with the synthetic lamp holder 2 of hydrogenchloride.Therefore, described stove tube 5 one side are for the synthesis of hydrogen chloride gas, and for the synthesis of hydrogen chloride gas and the second concentration liquid caustic soda carry out heat exchange on the other hand.Particularly, the bottom of stove tube 5 is provided with drop-bottom 3, is used for the described stove tube 5 of sealing.Drop-bottom 3 belows are provided with mount holder 1, are used for supporting 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 entrance.
As a further improvement on the present invention, lamp holder 2 is for being provided with the burner of Gas Jet mixed cell and rotational flow gas mixed cell, and its structure as shown in Figure 3.Among the present invention, the gas mixed cell on the described lamp holder 2 is two groups, and namely hydrogen, chlorine carry out twice fully mixing, to reduce the content of free chlorine in the synthetic hydrogen chloride gas, guarantees the safety in production of subsequent handling (vinylchlorid is synthetic).Particularly, described 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 enter two hydrogen passages and two chlorine passages from hydrogen inlet pipe 2-7 and chlorine inlet pipe 2-1 respectively simultaneously, chlorine enters behind two chlorine passages respectively aperture uniform from the tube wall of chlorine passage pipe I 2-2 and chlorine passage pipe II 2-5 and enters two hydrogen passages with the form of jet, and this moment, chlorine carried out mixing the first time with hydrogen.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 fully mix to reduce the content of free chlorine in the synthetic hydrogen chloride gas, guarantee the safety in production of subsequent handling (vinylchlorid is synthetic).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 provided by the invention, also comprise and the sources of hydrogen, the chlorine gas source that are connected respectively at hydrogen, chlorine entrance.Among the present invention, the chlorine that the hydrogen that sources of hydrogen provides and chlorine gas source provide all obtains by salt electrolysis, and wherein chlorine then by Chlorine Buffer Vessel, is delivered to the chlorine entrance of lamp holder 2 earlier through the persulfuric acid drying at last.Under the preferable case, hydrogen also need carry out cooled dehydrated and demist and handle before sending into synthetic furnace; Wherein the hydrogen cooler that adopts of cooled dehydrated, demist are handled the hydrogen mist eliminator that adopts and all can be adopted common device of the prior art, do not have particular determination among the present invention.
As a further improvement on the present invention, among the present invention, the heat exchange element that described synthetic furnace has 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 2, described 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 hydrogen chloride gas synthetic in the stove tube 5 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 chuck 5-1 outward, is used for the second concentration liquid caustic soda and passes through.Among the present invention, 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 hydrogen chloride gas in the stove tube 5; The second concentration liquid caustic soda of finishing heat exchange for the first time enters by convection tubes 11 between the pipe of shell and tube evaporation tank 6 among the case 6-2, carries out the heat exchange second time with hydrogen chloride gas among the tubulation 6-1 that enters shell and tube evaporation tank 6.
After finishing heat exchange for the second time, hydrogen chloride gas enters 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 free cl content exceeds standard in the hydrogen chloride gas in the stove, can in stove, produce blast formation shockwave and cause local pressure sharply to increase, rupture disk 8 is blown, let out except furnace pressure, thereby nonmetal equipment and the pipeline of hydrogenchloride system played a protective role.In the device provided by the invention, also comprise the hydrogenchloride outlet 7-1 that connects with hydrogenchloride outlet on the furnace roof end socket 7.7-1 is by pipeline and the second preheater UNICOM for the outlet of described hydrogenchloride, thus the hydrogen chloride gas that will finish heat exchange send in the cylindrical shell 14 of second preheater, for the second concentration liquid caustic soda is carried out preheating.
After finishing 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 be arranged in parallel with stove tube 5.Described 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 described 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 by pre-thermal jacket 15 UNICOMs of pipeline and second preheater, thereby can enter circulation tube 4 by 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 enters the chuck 5-1 of synthetic furnace.Carry out heat exchange by case 6-2 and hydrogen chloride gas between chuck 5-1, pipe, after the second concentration liquid caustic soda is finished heat exchange, by and the pipe of shell and tube evaporation tank 6 between case 6-2 top joining in adapting pipe 4-2 enter in the circulation tube 4, and rise and enter in the drum 9.When liquid-vapor mixture rose to drum 9 surperficial, water vapor carried out surface evaporation on the surface of drum 9, and assembles in drum, and its liquid level top is the low-pressure superheated steam of by-product.The part liquid caustic soda that does not enter drum in the circulation tube 4 can be back to circulation tube 4 bottoms, and flow to again by 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.
Entering the concentrated liquid caustic soda that forms that transforms of drum 9 after heat assembles in drum 9, by the concentration control instruments on the pipeline, densometer for example, measure the liquid caustic soda concentration of the 3rd concentration liquid caustic soda outlet 9-1, after liquid caustic soda reaches finite concentration, for example during the 3rd concentration of the present invention, the 3rd concentration liquid caustic soda that obtains is delivered in first preheater by 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 by low-pressure 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 a further improvement on the present invention, 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 at skirt 1 inspection window 9-5 is set between eddy flow plate mist eliminator 9-3 and mesh mist eliminator 9-4.
Among the present invention, the described synthetic waste heat of hydrogenchloride that utilizes carries out in the device that alkali concentrates, 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.
Carry out the concentrated method and apparatus of alkali below in conjunction with the waste heat that utilizes hydrogenchloride to synthesize provided by the invention and specify principle of work of the present invention.
(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 enters one and imitates separating tank, in an effect separating tank, carry out surperficial negative pressure evaporation, obtain the liquid caustic soda of 35-40wt%; The secondary steam that evaporation simultaneously produces enters 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 to the liquid caustic soda of 35-40wt% with second 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 enters 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 enters 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.
(4) liquid glucose that will prepare is pumped into static mixer with metering, and the liquid caustic soda of the 41-46wt% that step (2) is obtained is also sent in the static mixer and mixed with liquid glucose simultaneously, together sends into then in the pre-thermal jacket 15 of second preheater.
(5) hydrogen chloride gas in the cylindrical shell by second preheater 14 carries out preheating to liquid caustic soda and the liquid glucose of the 41-46wt% in the pre-thermal jacket 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% by liquid glucose
3 -After [x1] finished, the hydrogen chloride gas of cooling sent the user through the hydrogenchloride output terminal, and the liquid caustic soda of 41-46wt% enters 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 enters the chuck 5-1 of synthetic furnace.
(6) hydrogen and the chlorine through cooled dehydrated and demist processing enters stove tube 5 through the lamp holder 2 of synthetic furnace
In, combustion reactions is carried out in igniting, and the 41-46wt% liquid caustic soda in the chuck 5-1 outside the hydrogen chloride gas that generates after the reaction in furnace and the stove tube 5 carries out the heat exchange first time; Hydrogen chloride gas enters in the tubulation 6-1 of shell and tube evaporation tank 6 then, and the 41-46wt% liquid caustic soda enters by convection tubes 11 between the pipe of shell and tube evaporation tank 6 in the case 6-2, thereby hydrogen chloride gas and 41-46wt% liquid caustic soda carry out the heat exchange second time.
(7) hydrogen chloride gas of finishing heat exchange for the second time enters the furnace roof end socket 7 of shell and tube evaporation tank 6 tops from tubulation 6-1, and by 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 41-46wt% liquid caustic soda of the finishing heat exchange for the second time second concentration liquid caustic soda import 4-3 of back by circulation tube 4 that be heated enters in the circulation tube 4, again in lower link mouth of pipe 4-1 enters the chuck 5-1 of synthetic furnace.Carry out heat exchange by case 6-2 and hydrogen chloride gas between chuck 5-1, pipe, after the second concentration liquid caustic soda is finished heat exchange, by and the pipe of shell and tube evaporation tank 6 between case 6-2 top joining in adapting pipe 4-2 enter in the circulation tube 4, and rise and enter in the drum 9.When liquid-vapor mixture rose to drum 9 surperficial, water vapor carried out surface evaporation on the surface of drum 9, and assembles in drum, 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), carrying out demist by eddy flow plate mist eliminator 9-3, the low-pressure superheated steam of mesh mist eliminator 9-4 in the drum 9 handles, be delivered to 1st effective evaporator, the 2nd effect evaporator from low-pressure superheated steam outlet 9-2 then, guarantee that heats of imitating two effect evaporations in evaporation, the step (2) are supplied with in the step (1).
(10) after the liquid caustic soda of concentration control instruments (densometer) detection the 3rd concentration liquid caustic soda outlet 9-1 that arranges on the pipeline reaches 73wt%, 9-1 delivers in first preheater by 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, is stored after air cooling; 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 after the moulding enters that wrapping machine is packed, weighing, send warehouse Ma Dui, storage.
Adopting the preheating that utilizes hydrogenchloride to synthesize provided by the invention to carry out the concentrated method and apparatus of alkali produces, 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 preferred implementation of the present invention only, should be pointed out that to those skilled in the art, and under the prerequisite that does not break away from the principle of the invention, some improvement of having done also should be considered as protection scope of the present invention.
Claims (10)
1. one kind is utilized the synthetic waste heat of hydrogenchloride to carry out the device that alkali concentrates, and it is characterized in that described 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;
Described synthetic furnace comprise have hydrogen, the stove tube of chlorine entrance and hydrogenchloride outlet, described stove tube is provided with enclosed drum, drum is provided with the 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; Described 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, described 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; Described 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 2, it is characterized in that, described synthetic furnace also comprises the liquid caustic soda circulation tube that be arranged in parallel with the stove tube, described 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 described liquid caustic soda circulation tube link.
4. device according to claim 1 is characterized in that, described stove tube bottom is provided with the synthetic lamp holder of hydrogenchloride, and described 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 described drum, the alkali mist that is used for the minimizing low-pressure superheated steam is carried secretly.
5. device according to claim 1 is characterized in that, described second preheater comprises cylindrical shell, is coated on the outer pre-thermal jacket of cylindrical shell and places the outer support saddle of pre-thermal jacket; Pass through for the chloridating gas after the heat exchange in the cylindrical shell, pre-thermal jacket is used for the second concentration liquid caustic soda to be passed through; Be provided with helical baffle in the pre-thermal jacket, 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.
7. one kind is utilized the synthetic waste heat of hydrogenchloride to carry out the method that alkali concentrates, it is characterized in that, described method adopts the described device of claim 1 to carry out, may further comprise the steps: the first concentration liquid caustic soda is carried out preheating in first preheater, carry out one then and imitate evaporation, two and imitate evaporation and obtain the second concentration liquid caustic soda; The second concentration liquid caustic soda is carried out preheating in second preheater, carry out heat exchange with the synthetic hydrogen chloride gas of combustion reactions then, obtain the 3rd concentration liquid caustic soda and low-pressure superheated steam; Wherein, the thermal source of first preheater is the 3rd concentration liquid caustic soda, and the thermal source of second preheater is the hydrogen chloride gas after the heat exchange, and thermals source of imitating evaporation, two effect evaporations are low-pressure superheated steam.
8. method according to claim 7 is characterized in that, the concentration of the described first concentration liquid caustic soda is 30-35wt%, and the concentration of the second concentration liquid caustic soda is 36-46wt%, and the concentration of the 3rd concentration liquid caustic soda is 73wt%.
9. method according to claim 7 is characterized in that, described combustion reactions comprises that earlier hydrogen being carried out cooled dehydrated and demist handles, then with chlorine at the synthesizing chlorinated hydrogen of synthetic furnace internal combustion; The mode that the second concentration liquid caustic soda after the preheating and hydrogen chloride gas carry out heat exchange comprises jacketed type and shell and tube.
10. method according to claim 7 is characterized in that, also comprise one imitate evaporation finish back one imitate vapor-liquid separation, two imitate evaporation finish after the step of two effect vapor-liquid separation.
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